JPRS ID: 8334 TRANSLATIONS ON USSR RESOURCES

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• Document Creation Date: November 1, 2016
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• Content Type: REPORTS

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JPFtS L/8334
13 March 1979
~
TRANSLATIONS ON USSR RESOURCES ~
CFOUO 6/79)
U. S. JOINT PUBLICATIONS RESEARCH SERVICE
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- Unfamiliar names rendered phonetically or transliterated arA
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BIOLIOGRAF'HIC OATA Heport No. 2� 1. Recipient's AecesRion No.
SNEE7 JPR$ L/ 8334
n c+n, tiu i it e S. eport ote
T[tANSLAT'ION5 ON U5SR RESOURCES, (FC?UO 6/79) 13 March 1979
6.
7. Autho~(s) 8. Perlamin6 Oraani:~cion ReEr�
No.
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Joint Publicationa Reaearch Service ~
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Covered
As above
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iS. 5upplement~cy Note~
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This serial repart contains information on energy, fuels an,d related equipment;
fishing industry and marine resources; water resources, minerals, timber, and
electric power.
- 17. Key w'ords ~nd Document Analysis. 17a De~criptors
~ ussx
Natural Resources
Electric Power
Energy
_ Energy Conservation
Fi.sheries -
Fuels ~
- Minerals
Timber
Water Supply
176. Identi(iers/Open-Ended Terms
11c. (:OSATI Firld/Group SC~ IO~ ZID~ ZC~ HG~ ZF ,
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JPR~ L/8334 -
1.3 March 7.979 _
TRANSLATIONS ON USSR RESOURCES ~
(FOUO 6/29)
CoNT~N'fs PAGE
FUEL5 AND REJ.ATED EQUIPMENT
EquipmenC for Removing Water and Salt From Oil ~
(PROMYSLOVAI'A PODGOTOVKA NEFTI, 1977) 1 -
Tyumentransgaz Association During lOth FYP
(T.G. Zhuzhgova; GAZOVAYA PROMYSHLENNOST' SERIYA:
EKONOMIKA GA7.OVOY PROMYSHLENNOSTI, Jan 79) 45
Economic Eff iciency of Newly Introduced Natural Gas Deposits -
(S.V. Dubrova; GAZOVAYA PROMY~HLENNOST'.SERIYA:
EKONOMIKA GAZOVOY PROMYSHLENNOSTI, Jan 79) S1
Prime Cost of Gas ~eposits
(N.M. Soshnin; GAZOVAYA PROMYSHLENNOST'. SERIYA:
EKONOMIKA GAZOVOY PROMYSHLENNOSTI, Jan 79) 57
- a - [III - USSR - 37 FOUO]
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FULL5 ANU RELAZ'~U EQUIPMCNT
r
EQUIPMENT FOR REMOVING WATER AND SALT FRUM OIL .
Moscow PROMYSLOVAYA PODGOTOVKA NEFTI in Russisn 1977 pp 72-109 .
[Chapter ITI from the book "Promyslovaya Fodgotovka Nefti, Nedra]
[TextJ Hydrodynamic Coaleacers (Drop Formera) _
The hydrodynamic drop formers are designed to rupture the armoring shells
o r s t r a t a 1 water globules , the enlargement of Che globules and the
~tratification of thQ atream into oil and water before standing of the
_ emulsi.on. The coneolidation of the drops takes place directly in the oil
flow, on Che walls of the drop formers or on the built-in hydrophilic
elementg undez the effect of turbulent pulsations.
The volumetric and tubular drop formere are distinguished (see Figure 29).
The volumetric drop formera are hollow or have rigid hydrophilic elements.
In the hollow volumetric drop formers, the collision and coalesence of the
globules are achieved by introduction of the emi,lsion into the volume of _
the equipment th=ough nozzlQa directed at diffe� ~D! angles to each other
or turbulization of the flow inaide the equipraer '+y mechanical or other
meana. For inteneification of the processes of lescence of the globules~
the additional coaleac.~ent elements have been int iuced into the emulsion
flow, for example, in the form of dropa of draina~,e water which are easily
- removed from the flow with subsequent standing~ and the problems of their
regeneration are not created (in contrast to shavings, glass, and eo on).
The v~r~ion of intenee coalescence of the drops by turbulization of the
emulsion in the volume of the drainage water (the hydraphilic medium)
_ by mechanical meane is possible. The application of volumetric drop furmers
with developed hydrophilic coalescing surface nade up of corrugated, platy
or tubular elements operating, in contrast to the other materials (balls~ ~
ahavingb) in the self-cleaning mode is prospective.
The tubular drop formers are structurally made of bundles of tubes of cal-
culated length and diameter. Tne linear and sectional tubular drop formers
are distinguiehed. The linear drop formers are made of tubes of idFntical
- diameter. In the aectional drop formers the tube diameter increases from
section to aection [94, 111, 163, 191]. This permits succ~ssive enlargement
of the dropa to the given sizes. Just as in the volumetric and in the
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_
i
Hok a~~ici~ Us~: oc2Y ;
i
aectional drop formere, the application of a moving hydrophilic coalescin~ i
medium is pos~ible in the form of drops of dralnage wnter, centrifugal '
ewirlere of the flow which Chrow Che globules against the walls of the drop '
_ formere and bui1C-in rigid plare or Cubular coalescing elements ~perating i
in the self-purifl.caCion mode. -
The advantages of the vnlumetric hydrodynamic drop formere are the following:
high qpecific output capucity, small size, low metal conaumption, the pos-
sibility of their use as autonomous elemen.Cs or elementa built into a
aettling tank and also the possibility of Che applicaCion in pro~ects with
small process eites and under eapeciallv crowded conditions. The advanCages
oE the linear and eectional tubular drop formers are the following: the
possibility of. their uae simultaneously both as coalescing units and as
communication lines between the heat exchange and aettling equipmenC, the
- seCtling tanke of the firat and aucceaeive atages, the seCtling Canks and
the commercial tank parks, and so on. The advantages of Che hydrodynamic
drop formera over the electrical coalescers are the fo~lowing: the posaibility
of. calculating the enlargement of the drops to a give:l diameter, the pos-
sibility of control (regulationj~ of the coalescence process by connection
and diaconner.tion of the required number of sections, the ].ow cost and metal ~
consumption~ the law coneumption of electric power, the simplicity and safety
of servicing, and operating reliability.
areakdown of the Emulaion in the Drop Formers
The linear drop formers, their peculiarities and natura of 6reakdown of _
the emulsiona in them have been investigated in the literature j85, 107,
147, 168]. The first experimental model of the sectional drop former was
investigated on the Bablinskaya tnermochemical units and sufise~uently on
the Biryuchevskaya thermochemical units of the Tatneft' Asaocia~ion. T~e
drop former had three sections made of thermally inaulated tufies lo~:ated on
the lower supports and the horizontal plane. Tfieir diameter increases from '
section to section in the direction of movement of the treated emulsion.
The firet section i8 designed, just as the ordinary iinear drop former~ -
for breakdown of the armoring shells of the glohules of stratal ~ater and _
their consolidation with high parameters of the turtiulenC flo~r both in the
volume of the treated emulaion and on the walls of the tubes; the second
section is for coalescence of drops to larger dimensions with lower values j
of the Reynolds parameters; ehe third (last) section was designed for
investigation of the theoretical possi3ility of stratification of the flow ~
into oil and water in the pipeline for values of t:~e Reynol.ds parameter ~
- above critical aiid holding time of the oil in the equipment less than 10
minutes.
2
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~ 2 ~ fl 1--1 h Z Z
5+. i I
3
~ ~
b z~ ~2 ~ Z Z .
000 1
1 S o o�o�o�
i ~ o
o�o� 3
~ ~
5 ~ e . ~y
e Z ~ 1 ~ t ~
1 1 _~_5 ~ .
_ Z
= IO -
. 1 5 J Z -
4 s
/
_ L ,
2 4 k Z 3 4 5 6
Y _
1
3 5 ' 7
~
~ . .
- 6 3 y 5
g _ 8 4 .
t2 67
~ ~ ~
g
.
~?6
Figure 29. Schematic Diagrama of Hydrodynamic Drop Formers and Tubular
Settling Tanks;
Volumetric Drop Formere (a, b, c, d, e, f, g):
1--Emulsion input; 2--Housing of the drop forr,~ers; 3--Nozzles;
4--Housing of the settling tanks; S--Terminal distributing
liquid input and output; 6--Water discharge; 7--Drainage water ~
input; 8--Diatributing baffle; 9--Settling tank; 10--Mixer;
11--Sheet coalescing elements; 12--Tubular coalescing elements.
Tubular Drop Formers (h, i, j):
1--Tubular drop former with settling Cank; 2--Settling tank; _
3--Emulsion input.
Tubular Settling Tank Module (k):
' 1--Emulsion input; 2--Vertical distributor; 3--Horizontal e-
distributor; 4--Sectiona of the drop former; S--Horizontal
header; 6--Vertical header; 7--Emulsion output.
3
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~
Tt~e studies of the nature of the breakdown of the emulsion in the drop
- former oE the Biryuchevskaya thermochemicttl device demonstrated (see Figure 30)
thaC aCanding of the oil taken at a disCattce of 20 meters from the beginning
of the Firat eection of the drop fo~mer (the tube diameter 250 mm, -
R~ 53~000, q~ 35 g/ton, t ~ 40� C~ W a 10--15 percent, movement time 20
seconde) ends on after 1.5 houre. The increaee in etanding time does not
- in practice lead to further aeparation of the water. The reaidual water
content in the oil is on the average 3.58 percent. This indicates that in ~
the initial aection of the drop former the finely dispersed par.t of the
- stratal water globules remains undisturbed, and the emulsion is characterized
by a finely dieperse structure. Incrc~;;ing Che emulsion processing time in
rhe drop former to 2.5 minutea (sampling point at a distance of 200 meters, -
section diameter 250 mm) led to significant reduction of the water content
in ttie oii while standing (the residual water content in the oil in this
case was on Che average 1.17 percent). A further increase in Che emulsion `
processing time in the drop former to 3.5 minutes (sampling at a distance
of 500 meters, section diameter 250 mm) led to a still greater increase in
- depth of destruction of the emulsion. After the.oil sample at thia point -
stands for an hour, the residual water content in it is 0.53 percent which
is 6 times less than the water content in the oil taken from the initial ~
- section of the drop former (Figure 30, a) with a standing of 1.5 hours.
Attentio~ ie attracted to the uniformity of the emulsion structure ~it:~ _
respect to the croas-section of the first section of the drop former. The
water content in the oil and the depth of dehydration during standing oi
the emulsion s~mples taken in different cross-sectiona are in practice
identical. Still more efficient consolidation of the drops of water free ~
of the shelle in the first section was achieved in the second section of '
_ the drop former. As a resulr. of sharp consolidation of the water drops ~
during movemen[ of the emulsion through this section -for 1.5 minutes, the _
time required �or the oil to stand was reduced to 30 minutes. Simultaneously,
the residual w:3ter content in the oil was cut in half (after 30 minutes of
_ standing it waaa 0.3 percent, which characterizes the oil as deeply dehydrated). ~
Thus, inclusion ~f the second aection of the drop former with processing of
the emulsion in it for 1.5 minutes makes it possible to cut the standing
time in half with aimultaneous improvement of the quality of the oil. It
should be added that a tendency of the emulsion towards stratification has
- been detected in the second section. This is manifested in increased
water content in the lower sample, faster and deeper suppression of the -
water from the oil during standing.
4
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Q N !1 1
e
~ /
I! `
5 ID 13 %
b 111 Il I -
- ~ _
~ ~ s ,o ~sy -
d I
~
~ \
- 5 15% !p ZO JO 40 50 60 70 80 90 ~00%
~ dl 11 1 ~
1~ Il 1
S 10 15 �
S 10 IS %
Figure 30. ~Variation in Degree of Dehydration of the Water Samples Taken
_ along the Length of the Drop Former Characterized by Different
Flow Parameters. _
a--Re = 53,000, t= 20 seconds, D= 250 mm, v= 2.6 m/sec;
b--Re ~ 53,000, t~ 2.5 minutes, D= 250 mm~ v= 2.6 m/sec;
c--Re = 53,OOt~, t= 3.5 minutea, D= 25U mm, v= 2.6 m/sec;
d--Re = 36,000, t= 5 minutes, D a 350 mm, v= 1.3 m/sec;
' e--Re m�;~`0, t= 5 minutes 50 aeconds, D= 1400 mm, v= 0.08 -
m/sec; f--na = 36,000, t= 6 minutes, D= 350 mm, v= 1.3 m/sec.
a, b, c, d, e, f--Sample taking points; t--Time �or the emulsion
- to move from the beginning of the drop former; D--Diameter of
the drop former; I--Water content in the emulsions, 2--Amount
of water released, 3--Reaidual water content, X. -
5 -
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- , r .
~
~ -
^ d�ZS~MM -(1~�JSOrrM � dW,'Ye
E
~00
BO - E 4,0
6C 3, 0 -
- 40 2, 0
ZO . d ~v I,0
0
~ 20 J00 S00 ^ $ L,ro
_ Figure 31. Variation of Degree of Del.~�1Y�ation (E) and Reaidual Water _
_ Content in the Oil Samples (d W) with Reap~ct to Length oF -
~ the Sectional Drop Former L'with an Emulsion Consumption of
460 m3/hr.
Tn order to eatimate ri?e poseibility of stratification of the emulaion flow
into oil and water ir.~ the settling tanke with minimum folding time of the =
oil, a 7 cubic meter tank ~aas installed as the third aection of Che drop _
former, the deaign o� which made it poesible to discharge the separated water -
from the lower aection oi 1~. The flow turbulence was characterized by
~ a Reynolda number of 8800. The oil samples taken in this section with
re3pect to the flow croas~section demonstrated that its stratification -
. duxing atanding in lESa thsn 2 minutes in the equipment is impossible for
th~: given degree of turbulence. The first aigns of atratification were~ -
detected for valuea of Re ~ 5,000 and confinement time of the oil in the
apparatus of 2 minutes.
It is obvious that these two parameters are mutually compensated within
de.Eined limits, and incressing the time the oil is in the apparatus to _
10 to 15 minutes permits discharge of the stratal water for large values of
the Reynolds numbera. ~ ,
The dependence of the depth of dehydration of the oil on the length and
diameter of the tubes of the sectional drop former is illustrated in Figure
31. From the grapha it is obvioua that with an increase in length of the
_ drop former with simultaneoua stepped increase in tube diameter from section
to aection in the direction of motion of the emulsion, the efficiency of
treating it increases, which, in the final analysis, makea it possible to
obtain in pract~.ce water-free oil from the settling tanks.
From Figure 31 it fbllowa Chat if the length of the first sect~on of the
experimental drop former turned out to be twice as high as necessary it can
be decreased. Connection of the drop former to a 200 cubic meter settling
tank produced oil with a residual water content of 0.1-0.2 percent for an _
output capacity of 460 m3/hour.
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a N
-
~ D~ ~M - _
O 2050 40 30 D~2p 1D ~
_ ~ A ~
o ~g 'B '
.
~ ~
r+ 16 5 dynes/cm
. -
- a 14 I II G~ 1p
l2 ~ 2~I
- f0
30
8 , -
- 6 -
4 ~
_ Q~
_ 2 . _
; SO ~ ~uP C d~P
u , D I _
~.40 4 ~ 7 -
g ~ ~
30 ~
1 ~
- 20 3
_ Z
10 9 5
6
~10 Z~ ,3 T; ~ 40 0 0 10 m~, 100 /000 . 1~000
T, C p(mu micXons
Figure 32. Nomogram for Calculating ti-,e Diameter of the Mass Exchange
Section of a Drop Former, the Drop Size and Other Parameters:
Q--Ou tput capacity; D--Diameter of the drop former; dmu is the _
maximum stable diameter of the globules (intermediat~e value);
_ d~u is the maximum stable diameter of the globules; u is the
viecoaity of the dispersion medium (oil). Oil: 1--Romashka
(coal-bearing); 2--Bavlinskaya (coal-bearing); 3--Romashka
" (devonakaya); 4--Zapadnosurgutskaya; S--Ust'-Balikskaya; _
6--Samotlorskaya; 7--Mangyshlakskaya; 8--Arlanskaya; 9--
Krasnoyarskaya
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Ca].culating Hydradynamic Drop Form~rs
For proper aelection of the equipment ensuring effective deatruction of the
emulsion by the thermocMemical method under the most favorable hydrodynamic
;.onditions, it is very importanC to have clefinite methods o.t calculating
it. In connection with the rapid increase in extraction of dehydrated
oil and the neceaeity for building a large number of new oil preparation
units, it ie neceseary to learn how to calculate the parame:.ers of such _
units as the secCional drop formers. The applicaCion will permit the
output capacity of the aettling tanks t.o be increased in the stages of _
" removing water and salt f rom the oil, rhe number of settling tanks on site -
and their metnl consumption to be decreased, the size of the process areas
' and number of monitoring and aervice points ro be decreased, and the
- srabilit}� of Che oil preparation proceases to be improved. In this case
_ the processea of. removing the water and salt from the oil can take place at
low temperature, with low consumption of the emulsifiers and fresh wash
water. The construction time for the units and the cos~ of preparing the
- oil are reduced. The productivity of labor Is improved.
In the modern oil preparation procese in the desalination and dehydration
stages, broad use is made of mass exchange and coalescence sec2ions, each
- of which is apecially designed. _
Determination of the Parameters of the Drop Formers in the Dehydration Stage
The supply of the reagent to the globules of the stratal water and the ~
destruction of the protective ~hells on their surface in the mixing units _
of existing etructures (valves, gates, nozzles, and so) are not efficient -
for the following reaona:
Insufficient mixing time (fractions of seconds, seconds);
_ Extraordinary fractionation of the drops (to 1-2 microns); -
- Impossibility of mor,itoring the process.
The mass exchange proce~;ses, as a rule, are realized outside these units in ~
the lines be~ween units, and they take place spontaneously. Their efficiency
is determined by the random parameters of motion of the emulsion. Under
these conditione a aignificant number of drops with unruptured protective
_ shells reach the settling tank, lowering its operating efficiency. The
mass exchange section of the drop former is designed for effective mass
_ exchange between the globules of etratal water and the drops of water
containing the emulsifier reagent (with probability of 0.999 and more) under
_ conditions ensuring the p~~~sibility of existen,:e of drops of ~ given size
_ in the flow.
In contraet to the usual type mixers, in the mass exchange section of the
drop farmer, the delivery nf the reagent to the globules of stratal water ~
� 3
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and the degtruction of the protective shello nr~ realized under ehe con-
ditione of interfering proceeeee of frnctionation and coaleecence nf the
- drope~ the given eize oE which ie controtled by the flow regime chnrac-
~ terie~ic~. Thi.e permit~ excluoion o~ the poesibility of r.edi~pe~sion of
th~ drope and ensurPS repid coneolidation of them it~ the coaleecence aection. ~
Only the resulte ~f the cnll.ieione of the drops within the oil are Caken
inC~~ account in th~a. calculatione. The maso exch~nge proce8aes which take
place on the walls of the ~ections, whic~ play the role of inverCing screen~~
are not taken into account. Thia makeg it poseible to obtain a reliability -
r_oefficient f~r Che calculated data on the order of 1.7 (153j. In order to
~ enaure completenese of the mnse exchange proce~e in a technologically
acceptaLle time~ an effort ia made t~ fractionate the drope in Che flow to
defined dimensione ~elected as a function of the water cont~nt of the oil
tc be treated. Beginning with the condiCions of equnlity of the distances
between dropa in the emuleione with different ~~ater content it ie rectn~n;ended
that the following calculated values of the diametera of the water drops in
= the oil treated in the mass exchange section be used: _
- W+ x���~~~�~��........1 5 10 1S 20 30 -
d, micron~............5 10 22 27 36 68
- These values are taken into account when detenuining the diameter and the
length of the mass exchange section.
The diameter of the ma88-exchange sectiun D is determined by the given or
known parameters Q. uH~ pH~ dmean� Q, using the nomogrsm in Figure 32 or
from the expresalon: ~
'i~,~ to
4:1.3rt~.sr~--~.~ ( rt
U - L ~ ~ ~ ~62~
- ~c~u2.:,'~~~�~('n
* *mean
~ where v ie the aurface tension at the oil-water interi. dynes/cm; uB
and UH are the dynamic viecoaity of th~ water and oil respectively~ poise;
dmean is the ~verage diameter of the drops~ cm; u is t~e mean volumetric
flow ra[e~ cm /aec; pH is the density of the oil, g/cm .
The value of o is determined experimentally the known procedure on a atalag-
mometer after dehydration of the oil at the process temperature for the -
adopted flow rate of the reagent under actual conditions. The determination
of the diameter of the mass-exchange section using the nomogrcun in Figure 32
is made ae followa. The intersection point of tl~e horizontal and perpendicular
drawn from the corresponding given values in the C quadrant is found by the
known valuea of ug in the D quadrant. From t:~e point V obtained, moving
parallel to the directing curves, the intermediate axis d.mUp is reached~ and
a perpendicular ie drawn from it to the intersection with one of the curves
_ correaponding to the value of Q in the V quadrant (point II). Drawing a
horizontal line from the point II to the left into the quadrant A to the
9
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~oK ~rNtctaL usr: ONtY
irltereecCion with the curve corresponding to the given value of the output �
cr~pr~city Q~ the point I ie obteined. The perpendicular from Chie point to
the D nxig givee the deeired value of the maes exchnnge eection diameter.
~ In th~: case nf noncoincidence of the value of the diameter with the standard
_ value, the next l~igheat value of Che standard tube gize ig aesumEd the
curves in quadrant B correspond to the val~ea of the eurface tension c:oef-
ficient of 5~ 10, 20 and 30 dynea/cm. Curves 1-9 nf quadrant D exprees -
the viecoeity-temperature funcrion for the oils of different oil-extracting _
parts of the country. For example, for Q1 = 3 millions/year, uH = 30
centipoiec, dmean ` 35 microna and Q-~jynes/cm the diameter of the mass
exc}~ange aection turns uut Co be equal to 22 cm (the reckonin~ scheme as -
noted by the nrrows on the nomogram). -
d~e~n,s microne
w, �i.
A 6
16 ~
ct~ (Re)
/,0 8
12
/ ~ 0,8
0,6
s%1 J 4 s 6 0,4
- 4 0,1
r Z
~ 0 t0 20 ~ 34 i~ 30 60 70 RO 90 0 1 1 J ~ S
- * t~, M Rr f0'`
*L1 int � intermediate value of line length. -
Figure 33. ;lomagram for Determining the Length of the Mass :xchange of the
Drop Former or t61e Process Line:
W-- Water content; dmeari 'Average size of the glahules;
L1 int ia the intermediate value of the line length,
_ al is the correction factor for the motion regimen. The -
point of introduction of the demulaifer into the flow:
1--On group units; 2--On the head sections of the collecting
lines; 3~-In the terminal stages of aeparation; 4--For
reception of raw material pumps; S--Befnre the p~ps;
- 6--At the entrance to the mass exchange aection
The calculated length ef the masa exchange section can be detex~ined by
the nemogra~ in Figure 33 or by the formula [151j
~C - IS~op ) I C _ �o
~ it ~t a ~ ZOU, (63)
K~ ( -*!Ic o.zs
~cp t~, \ ~;~1 ~
wnere W ia the flooding of the oil (in relative units); Wp0 is the amount ~
of introduced reagent solution (in relative units); W is the amount of
- water in the oil enriched by che reagent ae a result of the mass-exchange
10
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proceseee during movement in the section (usually given ae 0.999); K1 ie
the collieion efficiency conatant; d ie the mean drop diameter, cm;
D ia the diameter of the maea exchange~aecCion, cm; v ia Che kinematic 3
viecoeity of the oil~ etokes; Q is the flow raCe of the treated oi1, cm / sec.
The mean drop eize is selected ae g function of the water content of the
treated oil: with an increase in water content the drop diameter ie aseumed
to be large, which subeequently facilitatea the operation of the coalaecing
- section. The length of the section is determined with rhe help of the
- nomogram ~see Figure 33) in the following way. The given value of W is
found on the flooding auis, and a curve is c:rawn from it parallel to the
_ lines with equal flooding to the intersection with the perpendicular dropped
from the selected value dmegn (point I). Drawing a horizontal line from
- the point obtained to the right to the intereection with the selected
collisio7 effectiveness curve~ point II ia obtained. Dropping a perpendicular
. from it to the L1 axis, Che inte~mediaze value of the length of the mass
exchange I.1 int ia reckoned. The total length of the aection is determined
conaidering the coefficient of the motion regimen al and the section for
eatabliahment of the flow AL e 20 D. The value of al is determined uaing
the auxiliary graph in Figure 33 by the known value of the Reynolds number
which ia calculated by Che formula -
- ~,~1
Ro ~n,; ,
_ where ve is the kinematic viacoaity of the ~muleion, stokes.
L~ � aif i�p + 20D. ~
. Depending on the reagent feed point in the process system for preparation
_ of the oil various curves are uaed for the collision effectiveness conatants.
- In particular, ~ahen feeding the reagent on the group devices curve 1 is
used; on the head aectiona of the collecting lines~ curve 2, in the terminal
3eparation stagea, curve 3; for the crude oil materialpump intake cutve 4;
before the pumping elementa curve 5; directly before the mass exchange -
aection curve 6. For example, for dmean a 10 microns, W~ 1.5 percent,
22 cm (the reagent is sznt to the crude oil material pump input),and Q=2
million tone/yenr by the nomogram in Figure 33 in the intezmediate value of
the length of the masa exchange aec~ion L1 int turns out to be 28 meters.
For the calculated value of Re = 2G,000~ a1= 0.84 meters, a1L1 int = 33.8
metere. For D a 22 cm the v~lue of ~L1 s 4.4 meters. The total length of
the mass exchange aection is defined as
~ I= x~ f lnp L~l 1 a Za3,J 1.4 = 27,~ \I,
Deterwination of the Parametere of the Coalescing Section
The output capecity of the settling equipment increasea proportionally to
the aquare of the diameter of the stratal water globules. Therefore before
arrival of the emuleion in the settling units it is nece~sary to see that
11
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the globulea free of the protective shella coalesc:e Co Che largeat dimensions
poesible. The baeic parameter~ limieing the possibility of unlimiCed increa~e
_ in dimenaiona of the water globules are Q, D~ uK, o~154, 207, 217, 222].
T1~e cnlcul~tion of tt~e conleocing section ie realized considering the hydro- -
dyncunic p~rc~metera of the flnw Ensuring Che poseibility of obtaining the
largest eize drops with the exception of the poesibility of premature
. stratification ~f the emulsion as a result of gravitationnl setCling. Thie
enaures the possibility of prolonged interaction of all the drops in it,
constriction of the epectrum of the drop diameters and mriximum possible
approach of them to the optimul v~lue. In order to prevent stratification
of the emuleion in the coalescing secrS.on, the turburent regime is maintained
oci Che level where Che verticul component of the velocity pulsations will
exceed the rate of gravitational sedimentation of the water dropa. This
condition ie aleo aseumed ae the initial condition limiting the conaolidation
proceae.
The maximum aize of the wnter drops not sub~ect to fractionaeion in the
turbulent flow of oil and the aize of the drope Which have been suspended
in this flow are defined for various valuea of Q, uH using the nomogram in
Figure 25 conatructed for fixed values of o a 10 dynes/cm in the coordinate
d= f(D). For the given value of Q and uH with respect to the intersection _
of the cur~?es of maximum drop size (1-7) with the curvea of the drop diametere
~ (1'-7') which can be auspended under the given conditions, the position of
= point I on the graph is defined. Dropping the perpendicular to the axis of
the tube diameter, its value of Dlim is defined. The effect of the values
oi the surface teneion differing from 10 dynes/cm is taken into account
using the correction factor KQ which is defined by the formula
-
KQ~~( ~ii)II'
where o io the actual magnitude of the surface tenaion, dynes/cm.
The final diameter of the coalescing section is written as D= DID~KQ, and
t1~e least aize with respect to the standard is assumed. The graphs of the
nomogram in Figure 25a-e correspond to the oil viecosity of S0, 30, 20, 10
and 5 centipoiae. Curves 1-7 and 1'-7' were constructed for the productive
section of 0.5, 1, 2, 4~ 6, 8 and 10 million tons/year. For example, for
Q= 2 million tone/year and uH = 10 centipoise, on the corresponding graph _
_ of the nomogram in Figure 25 we find the interaectton point of curves 3 and
3' and decermined the diameter ~f the coalescing section D= 38 cm. The least
standard aize is ~seumed; in the given case D= 35 cm. The maximum drop size
not sub~ected to fractionation by the turbulent oil flvw and in the suapended
stat~ is 900 microna. The length of the coalescing section is defined by
the formula
2 ,s ,
1= O,OZr~~ih,lt'U ~ n,Dv ~~0~.
(64)
12
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where dQ nnd d are tt� initial ~nd final eizee of the dropa respectively.
The mugniCude of th~ collieion effectiveneae con~Cant K2 was aesumed equ~l
tn 0,0001 [154J. F~r gcceleration of the calculaCion of the length of the
~ co~lescing eection, the nomagram in Figure 34 wae conatructed. The required
~ ittitial daCa were as follows: D, Q, d and v. From the known values of
d and D~ a line of equal diameters and the perpendicular to Che mutual
inter.section axe drawn respectively (point I). The horizontal line to the
right to intersection wiCh the curve of given output capacity gives the
point II. Dropping a perpendicular to the L2 int ~ig+ the intermediate
values of the length L2 int are reckoned. Then the value of the coefficient -
a2 ie found on Che auxiliary nomogram graph by the known value of the
viacosiCy. Then the length of the coaleacing aection is determined from
the following expresaion considering the section of establiahment of the
flow:
L2 ~ a2L2 int + 20D.
The curves 1-5 of the nomogram in Figure 34 correspond to the output capa~ity
of the section at 0.5, 1, 2, 5 and 10 million tona/year. Thus, for D= 30
rm, Q= 2 million tonsi~year, d= 370 microns, L2 int � 49 metera. For
v~ 20 centistokes a~ 1.07; hence L2 = 49~10.7 + 20�0.3 = 56 meters. _
Determination of the Parametera of the Drop Formers in the Desalination Stage
The determination of the diameter of the section of the deaalination stage
is made in the eame way as the coalescing section in the dehydration stage.
The boundary conditione also include the possibility of the suspension of
- all of the drope of water in the flow for given Q, v and other parameters.
Beginning with this, the diameter of the section D is determined by the
nomogram in Figure 25. The maximum drop size is found by it. The length
of the line on which the given degree of encompassing of the globules of
stratal water by freehwater drops ie achieved with a probability of the
procesa of 0.999 is determined using the nanogram in Figure 35 or the formula
W - tiS~nmi - ti~~nn,k
f7 _ L~ ~-~~no~~ ~ i?'~n ~ 20D, *stratal (65)
xp ~it~ / lo.zs
, ~ **mean
where W is the water content of the oil after introduction of fresh flushing
water into it; Wstratal p is the stratal water content in the oil after the
dehydration stage; Wstratal is stratal water content in the oil after the
desalination atage, having made contact with the freah flushing water K3
is the collision effectivenesa constant; dmean is the mean drop size cm;
D is the diameter of the des;+lination section, cm; v is the kinematic
viscosity of thP oil, atokes; Q is the flow rate of desalinated oil, cm3/sec.
13
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_ In order to deCerm.ine the length of the desalinatinn section using Che
nomogram in Figtir~, 35~ the given value of Che volume of the flu~hing wnter
- i~ found nn the Wlim ~is. and on the d~ean ~is, Che mean drop size which ~
cnn exiet in the fldw in the euepended sCate fnr Che given regime of morion. -
Hrom ehe point of intersectian of Che curve fnr Che freehwaCer flow rate _
with the perpendicular dropped from ~lmean ~poinC I), a horizonenl is drawn
ro the right Co ehe inCersection with the curve of the collision effective-
- ness constanCe of Cl~e dr.ope (point II). Dropping the perpendicular from thie `T
- point to the L3 axis, L3 in is reckoned. The tatal length of Che desalina-
- rion section ia found conai~ering the coefficient of the motion regim~n
a3 (Che auxiliary graph of the nomogr:~m) and the section of establishment
of the flow ~L @ 20D:
- L3 a a3L3 int 20D.
- D, cm
d, mi- 50 4D JD 20 0
_ crons A B
600 ~ 5
50(I ~ \ 4
J
400 ~ Z p(y~ C.
300
Z00 f,10 -
100
- ~ 0 50 ~Z int ~00 15~~'~~0 f0 20 JO 40 50 60
LZ, M y, � aentistokes
_ Figure 34. Nomogram for Determining the Length of the Coalescence Section
of the Drop Formet or the Procese Line:
L--Section diau:eter; dL--Drop size to which it is required
to consolidate the globules; L2 int is the intermediate length
of the section, a2 is the correction factor for the viscoaity
v 1, 2, 3, 4~5 is the flow rate of 0.5, 1, 2, 5, 10 million
tone/year.
14 -
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- ~m~an~ ~crons - -
rooo eoo coo aoo zno 0
. ~ ~s
w A $ �
~
'
' cr~ (Re)
II !,0
' 0,8
~ ~ ~ S 0,6 � C
.J - 4 0,4
i 2 ~ 0,2
� 0 SO 1511 200 250 J~D JSO 0 1 2 J 4 S
LQ,r+ Ile�l0~~ _
Figure 35. Nomogram for DeCermining the Length of the Coa2eacing 5ection
of the Drop Forcner L3 :in the Desalinatin Stage:
Wli~ ie the amount of wash water used, X; ap is the correction
factor Caking into account the motion regime; 1, 2, 3, 4, 5
are the varioua degreea of breakdown of the emulsion and ratio
_ of drop eizes of the introduced flushing and atratal water.
From the nomogram it is obvious that the same degree of trapping of the
drops of atratal water from the oil can be achieved for different flow rates
of the f reah watPr. With a decrease in the freahwater flow rate, the
length of the section increasee. Conaidering the expenditures on acquiring _
freah water and subeequent purification of it exceed the depreciation reckaned
from the cost of the desalination section, for the calculations it is neces-
sary to select the leaet acceptable level of freshwater flow rate, for
example~ 2-3 percent. Thia should correspond to the degree of dehydration
of the oil in the preceding stage characterized by the residual water content
in the oi.l of 0.1 to 0.2 percent. The section of the curve for the collision
effectiveness constante dependa on the method of introducing the wash water
into the oil, the nature of the mixing and the ratio of the stratal and
freshwater drop aizes. Depending on the exiating conditiona, it is recommended
that the calculatione be made ueing the following curves: S--for an unsatis-
factory dehydration procese characterized by the coz~tent of a large number
of globules with undiaturbed shielding ahelle in the flow; 4--with mixing
of the oil wi[h fresh water on the mixing valves and the presaure gradienta
of 0.5-1.5 kg-force/cm2; 3, 2, 1--on introduction of the previously diepersed
freah water into the flow of crude (drop size d8tratal ` dlim~ dstratal � alim~
dstratal ~ dlim� reapectively).
In order to obtain drops of fresh water of the required size, autonomous =
tubular mase exchange aectiona are used, the parameters of which~are selected
with the help of the nomograme in Figures 32-33 or forcing with the calculated -
nozzle parametera.
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,ae~me ~2~ -
d ~
- 8 Hedme ~2) / ~ ~ -
_
/y ~
� ~ ~ ~ ~
3nyn?cu,~ x tr--
= 1~--'`~ 1
- - _ ~ ~ I
_ +
/1CEHQM'NQR - ~M~in~u~r
~ 3~ eoaa = -
.~0 ~oJa Nca . .
b Hemme ~ 3 ~ -
Y --y Ne~m~
~ } } ~ ~ ~ ~
- - - - - - ~ 2)
_~;r = - =_-_=f
3nynicua
~~~a~e~Q~3~ ~1~ ,IDCNQM'MQI?C3)
Jnynecu~~ 1~ Qoda -
f
~ He~cme ~ 2~ ~ 2~ Nr~n~
~ -
- f t f f t I 1 } I I
- . - - -
- - _ _ _ -
~ ~�a"~"~3
APQoda a" ~ 3 ~
Jnynecus El~
,jryneeuA 1 �
Figure 36. Schematic Diagrams of the Settling Tank Installations of
Varioua Typea:
a--With perforated grating; b--With lower distribution input
of the emulsion under the drainage water level and upper
distributed removal of ehe oil; c--With sectional drop former,
low distriduted input of the emulsion and upper dietributed
removal of the oil; d--Vertical with sectional drop former and
low distributed input of the emulaion under the layer of -
drain~ge water; e--With end diatribution units for introduting
the emulsion and removing the oil; f--With overflow baffle and
fluahing of the oil in the drainage water Igyer.
Key: (1) Emulsion -
- (2) Oil
(3) Drainage water
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_
~Olt OF~ICIAL U5E ONLY
SetCling ~;quipment ~
Volumetric UniCe
The problem of creating highly ef�icient settling equipment has in recent -
yeara become one of the moet urgent problems. The high rates of increaee in
the volumee of oil extraction and preparaCion, its concenCration in enormoua
amounte at the central collection points have required the creation of
high-ouCput aeCtling equipment. The applicatton of the settling equipment
- with previous Cechnological procesa characteristics ui~avoidably leads to the `
- creation of expenaive and meCal-consuming industrial complexes, the inv~lve-
ment ~f large p1oCe of ground in the procesa aiCea, the use of a significant
~ amount of conCrol and regulating equipmenC and fittinge, complication of _
servicing~ and so on.
Until recently the improvement of the etructural design of the aettling
- installationa h~s developed along two basic lines:
Improvement of the hydrodynamica inaida the unite for more compleCe utiliza-
tion of Cheir useful volume (diatribution units, baffles, and so on) (see
' Figure 36) ;
- Intenaification of the procese of coalescence of the globulea of etratal
_ water and separation of it from the oil (baffles which change Che direction
� of flow~ the introduction of emulsion under a layer of water, the applica-
- Cion of an electric field~ the application of vibrationa to the boundary
layer~ and so on) (see Figure 36). However, here the achieved level of
output capacity turned ouC to be low, and the problera remained as before
in pracCice unreeolved. Thus, the loading of the beat Eettling installations
with Yeapect to fluid to a voZume of 200 m3 amounts to 1.2-1.3 mil]ion tons/
tons/year. The problem conaiata in creating equipment with an output
capacity exceeding this level by aeveral times. The theoretical prerequiaites
explaining the poesibility of achieving this level reduced to the following
(130] . -
' The output capacity of the horizontal units of cylindrical shape can be
calculated by the formula auitable for drops less rhan 0.1 mm in size (the
_ sedimentation regime in laminar): _
c~~~i~1. S,~Ir1-~-2 I~r �~-ti~n ~z~r-n11(n-~+1}
P:, = a~cir~�r~~ . ~66~ -
where QR ie the output capacity; g ie the gravitational acceleration; d is the
diameter of the stratal water globules; Qp is the difference in water and
oil denaities; L ie the length of the unit; R is the radius of the unit; h -
is the height of the water cushion; v is the kinematic viscosity of thp oil;
pK ie the density of the oil.
17
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For h~ 0 the fnrmula asaumes the form:
~ n.~a:llrlld~A~~/, (67) -
n- '
~'(~u
From fonnula (67) iC is obvioue that the output capacity of the se.ttling
tank depends on the dimeneione of the sCratal wster globulea to the aecond
power. Thus~ the increase in drop eiz~ by only 3.3 times leads to an
inc:ease in ouCpuC capacity o.~ the setCling tanks By 10 times. The other ~
pnrametere influence the ,rrutpuC capac:i~y of the aettling Canks linearly. _
Hence it follows thgt in ~~rder to increase the output capacity of the aettling
tank unit Che latter muet be equipped with devicea napable of consolidating
the drope ~efore Che emuleion enCera the etagnation zone. This must be
preceded by completion of the maes exchange processes with reapect to
bringing the reagent to each globule of atratal water and destruction of the _
protective ehelle in them. With an increase in the drop size to 0.1 mm or
more the aedimentation rate increae~s, the sedimentation regime becomea
turbulent and the output capacity of the settling tank is determined by
the formula
Q 2,7~il.lt j~Rdep C68, _
*e .
v P~,
The analysis of formulas (67) and (68) and alao Cheir comparison indicatea =
that QT is two orders more than QR. Consequently, theoretically the output
- capacity of the settling tanks can be increased by 100 times under the
condition of preliminary conaolidation of the drops. If we consider a number
of factors limiting the poasibility of increasing the output capacity of
the settling tanka to this level under practical conditiona, the poseible
loading of the units turne out to be 10 times higher than that achieved on
the average with respect to the b:anch.
Therefore it is necessary:
To realize preliminary coneolidation of the emulsion drops before their
introduction into the stagnation zone or stratifi.cation of the e.mulsion; ~
Enaure the end uniform input of the liquid witfi respect to the cross-section !
of the unit and also the uniform sampling of the liquid;
Maintenance of a low level of the water cuahion or in practice excluaion of
it;
Exclusion of the operation of "fluahing" the emulsion through the drair.sge
water layer from the aettling zone.
18 -
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The devicea which permie the drop eize to be 3ncreased hefore the emulaion
_ re achea Che settling zone can be the hydrodynamic type Cubular and volumeCric
drop formere. The Cubular drop formere have already become wideapread in F
the deposits; the volumetric ones are in the development atage. Their
applicatiott hae in individual cases made 3C poaeible to increase the output _
capacity of Che settltng tank unit with a volume of 200 m3 to 4~05 millton
tona/year (Che Btryuchevskaya Thermochemical Units of the Tatneft' Aasocia-
tion) . -
While keeping the output capacity invariant, the use of the drop formera
permits improvement of the quality of the oil tiy 5 to 10 times. The flushing
of the emuleion Chrough the water layer during proceaeing of the undiaturbed
emuleion unconditionally hae played a posiCive role, for it has promoted a
reduction in etrength of the protective shells on the dropa of etraCal water
- and traneition of a significant number of Chem to tk?e drainage waeer tank.
~uring the proceseea of breaking down the emulsion and coalescence of the
drops in the drop formers th~ necessiCy for flushing is removed, and its -
exlusion permita the ouCput capacity of the settling tanks to be increased,
for in this it becomea poseihle to remove part of the drop~ 6y the ascending
oil flow.
The output capacity of the settling tanks with rectangular crosa-section
under the condition of motion of the liquid perpendicular to the direction
of the gravitational force (the tern~inal input) is determined by the equality:
Q, ,
F~a~,
- where w'eed ia the sedimentation rate.
The maximum output capacity of the settling tank wtth the tap at the top is
- de termined by the equality of the velocitiea of tE~: aecending flow and the
- settling of the drope in the vicinity of the oil-water phase interface,
the aize of which ie taken into account wben cal~ulating
.
Q" = Fo~o:,
where w~sed ` W~sed ' w1iquid is the resultant sedimentation rate; Wliquid
is the speed of the ascending flow of liquid.
_ However,
_ ~ .
Wliquid F ' -
- from which
a _ 4.
W~sed ~~sed F'
conaequently:
.
Q" = F Cu~oc - ) = !'cno~ - Q";
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H~oK or~icr~ usc oM,Y
or
r ~'~~~oc ~
. 'l
r The ratio Q'/Q" gi.ves Che expreaeion
Fwor _ 2
,
/''woc
'l
from which it followa that the output capacity of the settling tanks with
end distributed input under acCual conditions can be twice the output capaciCy
- of Che settling tank with 1ow input distribuCion operating wiCh a water -
cuehion inasmuch as w'8ed ~ wi~sed� The semi-industrial teaCs demonatrated
that the output capacity o� the settling unit with a drop former and terminal
- ' inp~at can be brought to 9 million m3/year (see Figure 37).
d W, % 1
8
6
- 4 - 2
2 -
D Z00 4~0 6~0 800 1~OOQ,M%~x
~ Figure 37. Oil Quality as a Function of the Output Capacity of the
Settling Tank Installationa:
1--Settling tank with low distrihuted input and fluehing
- of the emulsion in a layer of water; 2--Settling tank with
sectional drop former and end distributed input; 6W--residual
water content in the oil
The maximum output cap~city of the aettling tank achieved under practical
conditions in the dehydration atage is 4 mfllion tons/hour. In the desalina-
~ tion sCage for Devonian oil (Romashka) settling tanks have been tested ~ith
an output capacity of 2.1 to 3.6 million tons/year. If we conaider that
the average load of the aettling tank installations on such units as the
Karabashkaya UKPN Refinery is 0.167 million tons/year then it becomes impor-
tant how many reservea industry has its disposal. For oil with increased
viscoaity, a somewhat different picture has been put together (the Bondyuzh-
_ skaya oil). Here the maximum output capacity was 2.7 million tons/year,
which, however, is not the limit.
Selection of the Volumetric Settling Tank Installations.
The output capacity of the settling tank installation of field and plant
~lnita for treating oil ia determined by th~ degree of disperseness of the
drops of wat~r, the viecoeity of the oil and other parameters influencing the
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_ sCratification xate of the oil and water emulsiona. Tl:e technological -
procedures directed at the degree of consolidaCion of the stratal water
drope b.efore rhe emulsion stands have a decisive effect on the increase in
output capac:~ty of the settling tank inatallationa under equal conditions. _
When e large number of drops settle, the rate of conatxicted fall m is de-
termined not only by the parameters entering into the expression for the
SCokea Law, but also the ratio of the emulsion phase volumes. In ieference
' [25], on the basis of the experimental studtes of the constricted aedimenr~a-
tion, an empirical relation ia preaented whicfi takes this factor inCo ac-
count and which, after some traneformations, can be represented as follows:
_ w_ ~p~,,~z ( yy~a, ~ s
~ t /'~~r~ ni~ ' (69)
_ ~ , ~ -
;iu ~ / ; r~~~
where uH is the actual viacosity of the oil, poise; ~p is the difference ~
in denaity of the water and oil, g/cm3; g is the graviCational acceleration;
d is the drop diameter~ cm; W is the relative water content of the oil;
vi.~ is the kinematic viecoeity of the oil, stokes; pH is the oil density,
8/cm3.
The first cofactor in formula (69) ia the sedimentation rate of a single
' particle in a;cordance with Stokes Law, and the second cofactor is a cor-
rection for the condittons of constricted sedimentation. It has been
eatabliahr-d that for calculating ~he stratification in the settling tank
unit of ~rater and oil emulsions, expression (69) can be simplified. _
The following values are preaented in Table 2
~_'1IC1+3u i' ~~9 pH ~l-W)a,~s~~ -
N
calculated for the characteriatic conditions: pg = 0.8 g/cm3; pB = 1.1 g/cm~;
vH m 0.1 stokea. '
The data obtained make it posaible to arrive at the conclusion that for water
and oil emulaions it is poasible to neglect the value of s, and during the
ae3imentation calculations, to use the f ormula
- w - ~
8~id' (1- 6~)a?6 . ~ 70~ -
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I
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Tab1e 2 -
Vn1ue af p Cor wuter
- dropa aize, microns
w
~ ~o I~oo I zoo I~~no I ~oo ~
0,05 0,4108 U,U~35 U,93fi O,OG3 0,948
U,1 O,flOfl O,fl~JG 0,4~88 O,fl67 0,055
0,2 9,000 O,fl~J7 0,99f O,U75 O,OG5
_ 0,3 1,OOU O,fl~JB O,~J~3 O,~J81 0,;175 ~
0,4 f,000 O,nOJ O,9~Jl; 0,9H7 O,fl82
U,5 1,000 9,000 O,U9~ 0,0`J2 U,fl88
U,G 9,OOU 1,U00 1,000 O,UO(l 0,993
The error for the range of variation of the water drap size from 50 tc, ~uu
microne does not exceed 4-5 percent. The nomogram constructed considering
the above-inveaCigated factors will permit rapid determination of the type
= and required numher af settling tanks. In this case the calculation of the
aettling tank units reduces to determination of the number and type of
settling tanks required for dehydration and deaalination of the oil for the
_ given technol.ogical procesa parameters and thR selected sectiona of the
drop formera. The required initial data are as follows: d, ug (or T, �C), -
- V--volume of the settling tank installation, m3, and W--relaCive volumetric
content of water in the oil.
The procedure for calculating the numher of units for a degree of dehydra-
tion is a,s follows: being given the drop aize at the output from the drop
former dnd the viacoaity of the oil, the nomogram in Figure 38 was used to -
determine the intersection point of the perperdicular reproduced from the
value of uH with the curve for the given drop diameter (point I). Drawing
a horizontal line to the right from the point obtained to the curve cor-
responding to the eelected volume of the seCtling tank installation, we
obtain the point II. The perpendicular from this point to the Q axis gives
an output capacity of the settling tank of the selected volume Qli~. The
correction for the rest~�tcted conditions of sedimentation Kres taking into
account the water conten!,: of the crude oil going into the settling tanks
is selected on the auxiliary graph D of the nomogram in Figure 38. Finally,
- the output capacity is defined as
Q ~ Q1im~Kst'
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_
I~'0!~ 0~'F'ICIAL US~ ON1.Y
microne A ~
i i1
f00~ - - - -
800 ~ - ~ 2 3 4 S 6
6~0
400
zoo ~
~
_ o
T c ~ r ?u roo rooo ,~~o; ~o
e ~ . . .
~4D - ~ QtM~~..
~ y QUFV ~l . ....1 !0 !00
30 - ~ o, 4 p Q'
~ m~~lione of
20 ~.-2 o~Z ~ m ~Year _
8 / 'S 3 ~ 6
- ~~5~ 40 ~9 20 10 U ~ 1 IO 20 J~
~ ~uN, ~ntipoiee K~k ~
Figure 38. Nomogram for Calculating the Output Capacity of the 5ettling
Tank Inetallations:
Quadrant A: drop size curves; Quadrant B: 1-6--Settling t3nks _
, with a volume of 28~ 50~ 100 and 200 m^ and tanka with a
volume of 2~000 and 5,000 m3; Quedrant C: 1-9--Viscogity ae
- a function of the temperature respectively for the oil of the
Romaehka coal bearing, Bavlinakaya coal bearing, Romashka
Devoni~n, Zapadnosurgutskaya~ Ust'-Balykskaya; Samotlorskaya;
Mangyehlak; Arlanskaya; the red Yar deposits.
The required type of settling tank inetallatidnis selected beginning vith
the output capacity of the unit, the sizes of the area for installation of
_ them and other factore. The number of aettling eanks is determined by
- the fot~ula
n = Q/V.
- Curves 1-6 of the nomogram in Figure 38 correapond to the volume of the
settling tanks of 28, S0, 100, 200 m3 and the tanks 2,000 and 5,000 m3.
Curvea 1-9, which are the oil viacosity of different oil extracting regions
as a function of temperature~ are analogous to the curves on the nomogram
in Figure 32. For example, on conaolidation of the drops in the coalescing
section to a value of d~ 700 mi,:rons, the viscoaity of the oil uH = 20
centipoise and the aater content W s 20 percent~ the settling [ank with a
volume of 200 m3 hae the output rapacity (m3/hr):
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~~?o
Q .3 - 30U.
~
- With an o�tput capacity of the dehyd~aeion unit of 2 million tone/year it
te necessary to u~e one eettling rank wittr a volume of 200 m3, The procedure
for calculating the settling tank ingt~ll~tinns for the des~]' ation stage
- is the ~ame ~s for ehe dehydration stage. Here the drop ~izeg cnn be taken
into ~ccount which can ~.xist in ehe flow ~t ehe exit frum thp eeCtion of
the desglination etage. ~or both st~ges it i~ propoged th~t we uge a re-
serve settling tat~k, the fittings for which make it po~~ible to connect
it when necegeary both tn the dehydration etage and td the dedalingeion
stage.
The Operation of the Settling Tanke in the Optimal Monitoring Mode
Orte of [he condi.tions eneuring opeteting reliability of the procee~ equipment -
and stability of the regimen parameters of the devi~eg for ff~ld treatment
of the oil ie preciee regulation of the oil-phase water interface in the
settling tank inetallatione. 'This to a great e~ctent determines the quality
of the oil trea[ed ott the unit attd the diecharged waste water. Therefore
each settling tank inetellaCion or electrodehydrator is equipped with
level reguiatora. 51nce on the atandard oil treatment units up to 30
settling tank inetallationa are used (the Karabash~kaya UKPN with a capacity
of 6 million tone/year), the servicing, preventive maintenance, repair and
level re~~lation are greatly complicated. Accordingly~ the flow charta
for hooking up the settling tank unite permitting a aignificant decrease
in the requirement for level regulatorg and a reduction in the degree of
cheir influence on r.he operation of the unite and quality of the oil prepared
in them are of aignificant intereet. With a decrenee in the number of
level regulators in the aettling tenk unit, not only does the number of
service points diminish, but Uetter quality preventive maintenance and
~ reliabie monitoring of the operation of the latter become posaible. With
- respect to the optimal monitoring scheme the follo~ring are provided for:
The inatallation of a level regulator in one or tWO units with realization
of hydrodynamic connection between these operating aectling tanks;
Returt~ of all of the drainage water to the process cycle for preparation
o; the oil.
With respect to the flow chart for the dehydrating unit operating in the
optimal monitoring mode, the quality control i8 realized on the stratal water
in che etage of preliminary diacharge along with control of the quality of
thc vil at ihe exit from the set[ling tank 10 operating in the flow strati-
fier caode (see Figure 39). In accordance With this scheme, the well production
treated with reagent in the field lines reaches the aeparator 3. The emulsion
which >>as been degased and broken down in advance is sent through a hydro-
dynamic drop former 4 into the preliminary water discharge settling tank.
The introduction of hot drainage water into the emulsion flow ahrad of the
separator 3 or the drop former 4 ensures purification of it to the degree
~
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petmitting it tn be pumped into the hed~ ie promotes cnngnlid~tion nf the -
gl~~bul~~ nf ~trntal water and fast geparation of the phgees in the ~ettling
tank 5~ Ar the exit from the 1~tter~ the quality of the die~harge drainage
water ie monitored by ueing the analyz~r 19. -
With ~ cnntent nf pnllutante in the wgter a6~ve the admi~~ible normg, it i~
puri:ied in the ~ettling tnnk 16 using thc liquid hydYOphobiC filCer~. The
oil leaving it wieh a waCer content of 5 to 7 percent ie heated in the heat
exchanger 7 to g temperature of 40�'C and is fed ~ay the pump 6 thrnugh the
drop fnrmer 8 to three out of fo~r of the gvgil~ble settling tgnkB 9 gnd
then to the water eepgrator aettling tankl0, the fittinge of which permit
inClueion of it in eeri~s and in parallel with the seteling tank~ 9. The
setting tgnk 10 i~ hydrodynamically connected with the settling tanka 9.
It can be in the ~ame unit with it, and it is regulated by the quality of
the oil coming out of it. The rQgulator of the interface level ig inetalled
in thie aetCling tank or in another one of them. The ~cCive drainage water
is fed to the intake of the eeparetor 3 after the unie~ 9-10.
. . 9
12 ~~2
~ 7 J y S 6 7 8 j r~ y
~ - -
I ~ 19 ~ ~ ~ ~J
L---L...~
- ( f6
I ~n
_ ~~f9 ~ 17 t~
~20 r 1~
_ ~ � - - u-
Figure 39. Flow Chart of the F':ttings of Settling Tanks for the Oil Treatment
Unit Operating in che Optimal Monitoring Mode:
1--Demulsifier batcher; 2--Line used for breaking down the
emulsion; 3--Separator; 4--Cold atage drop former; S--Preliminary
water discharge tank; 6--Pump; 7--Heater; B--Hot etage drop for~er;
9--Set[ling tank; 10--Tank for water discharge; 11--Gas drier;
- 12--Gas line; 13--Drainage water meter; 14--Meter and quality
analyzer of the prepared oil; 15--Purified water line to the Q�
' pump; 16--Settling tank with hydronhobic liquid filter; 17--
Buffer tank; 18--Pump; 19--Meter and quality analyzez for the
_ drainage water; 20--Hydrodynamfc tubular coaleacer.
The layout by this �low chart excludes the necessity for quality control of
the drainage Water diecharged from the aettling tank, for the latter is
purified in the oil preparation process cycle where the drops of oil removed
with [he water are returned to the com~on flow of incoming production of
the wells. The invPStigated process permita significant improvement of the
8ystem, moni[oring af the quality of the water and oil and a simultaneous
decrease in the [otal number of required level regulators.
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Tuhular 5ettling Tank~ _
_ i'r~?m the nb~vc+ inveatiqnted materinl~ it follnwn thnt tm m~ny ca~ee thc
vc~lumr.trlc: earcllt~K canke c~n b~e replncnJ by tubulnr onc~. It i~ eaey tn
demon~trnte Chnt the output capacity of the s~ttling tnnk with rudiug !t i~
equal tu the sum of the output capacities of the group of settling tanks
with rr~dii rl, rz, ...,rn under thc condition th~t
~ r� ,i
_ ~
Ir r,~ and /,?r = (ri~ r~, . . r�),
Indeed, if we aet:
~ 11 /t; Q~ ~1r1~
~ s=-- it r,:; (1� - A r,,,
where A is the co~efficient equal to the numerical value of the remaining ~
paramecers in the formula for the output capacity of the settling tnnk
and we take the sum from Q1 to Qn, we obtain
n
v' Q( ' ~l'1 r1 . . . rn~.
i��t
- For R~ rl + r2 + r3 + rn, we obtain
~
Q~ = AR ~
,
lience, it followe that
A
Q fr..' `~f 1 �
~^t
In other words, one unit of radius R can be replaced hy banks of tubes with
small diameter of the same length under the condition thae the aum of the
radii of [heae tuhes will be equal to thP ra.~t�A ~f r~,P large settling
~tlnk. This opene up the way to the creation, for example, of small, portable
and nonmetal consuming aettling tank installations. It is natural that the
increaye in output capacity of the settling tank installations is connected
with the neceasity for varying the hydrodynamic flow regime and increasing
_ che speed of the liquid in them to values characterizing the turbulent flow~.
The factor limiting the output capacity of the settling tank units with
properly eelected hydrodynamic characteristics is the transverse pulsation
componente of the velocity operating 2gainst the gravitational forces.
In Figur~ 27 (curves 1-4) a graph is presented for the turbulent flow pul-
y:3tLons as a function of the diameter of the unit with a Reynolds number of
l0,OQ0 from which it followa tha: the diameter of the settling tank under .
other equal conditiona~ for example~ average flow velocity~ is one of the
_ de:ining parametere influencing the possibility of stratification of the
emulaion with moderate turbulent regime characterized by the Reynolds numbers
of order 5~000 to 20,000.
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rnk c~a~rtt.tnt, ust: nNt,v
In accordence with [211J, khe length of the ~?eCCling tank unie on ~rhich rhe
procesg nf etratification of the emul~ion r.an be aompleeed in the laminar
regime nf moCion~ ie defined by the following expression:
4 t~ninf l~
L�' ~ s u~:T, ' (71)
I
where um~ ie the speed of the lrneinar flow alang the a~cig of the gettling
tank; uC~ i~ Ch~ gravitaCiottal ~edimentation rate of the dropa; D is the
dinmeter of Che unit.
For eettling of the drops on the bottom of the tubular ~~eCling tank ~rom a
flow moving in the turhulent regime, the required ~ength of the unit is
determined by the expree~ion:
~
~mn~ K r�
I,, = ~~A D, ~~2~ -
where vmax is the maximum flow velocity; x is the CurSulence cone[ant; u~
is the dynamic settling rate.
~igure 28 shows the length of the units of different diam~ter ae a function
of the waCer drop eize required for stratificaCion of the turbulent flow of
the emulaion characterized by the Reynolds number of 10,000 for an oil
viacosity of 0.044 poise.
As was pointed out earlier, there ia a limiting eize of the dropa which can
settle in a unit of given diameter. This fact is reflected on the curvea
by a sharp increase in length of the unit when the drop diameter approaches
the maximum. With an increase in drop diameter, the length of the settling
tank required for stratification of the flow ia eignificantly reduced.
The analysie of the curvea in Figure 28 makes it poesible to draw the con-
clusion of the poasibility of rapid stratification of the emulsion in the
- horizontal tubular units, the diameter of which is appreciably lese than
3 meters. The preliminary cor.solidation of the finely dispersed part of
the emulsion will permit realization of this process during its movement -
in the turbulent regime with high output capacity. Thus, for example, the
stratification of the emulaion with drop sizes of 600 microns turns out to
be identically attainable both in the settling tank with a diameter of
50 cm, the length of which is small--near 3 meters--and in the standard
settling tank with a diameter of more than 3 meters. In the latter case the
required length of the aettling tank is 2 meters. On consolidation of the
drops to 8 microns the aettling of the water from the oil becomea possible
in the settling tanks with a diameter of 20 and 10 cm respectively. Hence,
it followa that the realization of the principle of preliminary consolidation
of the drops before eending the emulsion to the settling tank opens up the
possibilities for the creation and use of small high output wa[er separating
equipment made of tubes.
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F~Ott c~~~t~tCt~1L U5~ oNLY
Ttie theoreticul po~~ibiliry of ~trnti�icntion intn oil gnd water of the
em~leion with drops con~olidnted in advance in Che tubular elemente under
turhulent ronditions wgd checked out under induetrial conditidns gt Ch~ r
~LOU-1 NGbU (011 and Ga~ ~xtr~ction AdminigtrationJ BavlynefC' (Tntneft'
Aesociution) which proc~seee nil from the coal-hearing horizona.
The hreakdown of the emuleion and the hydrodynamic consolidaCion of the -
dropg before the weter settles out of the oil were realiz~d uging the
gection~l drop former, and the stratific~tion o~ Che flow intn oi1 and wnter,
in the experimental tuhular settling tanlc. The eeCtinn~l drop fnrmer con-
sisted of the geriee connected heat irs+~lated tu6ular elemente 150 ~nd 250
mn in diameter lnid on a foundation. The }ient in~ulaCed Cubular settling
tank was made of tuGes 350 mm in diameter. At the end of the settling tank
there were two tapg for diecharge of the sep~rated water nnd tnpping the
desalinated oil. 'The unseparaCed mixture of water ~nd oil from the inter--
mediate turbulence zone wne removed through the ceneral tube 150 mm in -
diameter. It ue~ally quickly etrntifies witti sub~gequent finigh of the
settling. The flow ratp of the prepnred oil and drainage water tapped off
was controlled hy the Voltman meters. The time for movement of the oil
through the firet section of the drop former was 5 minutea (with Re ~ 21,000);
in the second secCion, 11 minutes (with Re = 14,000) and in the Curbulent
settling tank~ 12 minutea (with Re ~ 8,000).
a b 8 -
J y 5
~ 8 7
12 4 7 !2
~ y 6 9
2
4 8
~ 7 g r Z~ 4 ,5 6 7
- 9 9
~
~ g d f 2 4 8 2 1
7 "
r Z a 4 2~
} -
_ 9
2 4 7`~8 4 2 2 y 7 B
r t i
~
9 9
F'igure 40. Tubulur and Combined Settling Tanks:
- u--Hcriaontal, single row; b--Vertical, multirow; c--Horizontal
- two-way, multirow; d--Multilayer, horizontal, tWO-Way, mul.tirow;
1--Output emulsion; 2--Horizontal distributor; 3--Vertical dis-
tributor; 4--Tubular settling elements; S--Vertical collector;
6--~lorizontal collector; 7--Tank; B--Oil outpnt; 9--Water dis-
charge.
28
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The oil wa~ treated by the following flow ch~re. Th~ di1 from the ~onl bearing
horixon (~~~00-4~q00 tone/dey) with g aaCer cont~nt of 30 eo 40 percent rogched
the tgnk for preliminary di~ch~rge of the dgter and hence, with n r~eidugl
water Content to 12 percent end the reagent introduced into it (from Cglculg-
tiong nf 50 g/ton) it went to the heae exchgnger~ w6~r~ it vae hegted to
GO� C~nd th~n, pasging ehrougti the sectiong o� tfie dr~p former, it w~ttt tn
th~ tubulnr seetling tank.
Obgervntions have demdnetre.ted that for deep deetruction of the protective
ghell~ gnd preliminary enlgrgement of the gloGalee of the emulginn in the
drnp former sectidn~~ the etratifiaatinn of Che flnw into oil ~nd water in -
the settling tank 35 cm in diameter is rpalixed for valueg of the iteynoldg
numberg on the order of ~,000. Hence tt follows thgt up to theap valuee of ~
the parameter Re the output capacity can aleo be increaged fnr the gCand~rd
~ettling tenk inetallation~ It wae noeed Chgt ~ layer of p~re drainage
water moved in the lawer pgrt of Che tubular getrling tattk. Ite cetttr~l
- section~ including the contact zone with thp water wae repreaented by oil
dehydr~ted to 1.6-2 percent, and the upper section, dehydrgted oil. The
intermediate zone iteelf contained no more than 2-4 percent waCer. Here it
turned out that the stratification of the mixture of water and oil picked
up from thie zone tnkes plnce in 15 minutes with a temperature of 45� C.
" Analogous results were gchieved when using g tubular complex also in the
- desalination stage. In this case the freeh water, calcul~ting 8 percent of
- the treated oil, wae supplied ai the beginning of the drop former aection
150 r~m in diameter.
~ It was establighed that during the proce~s of the joint movement of the coal-
bearing oil and fresh Water through the eectional drop former, effective
- desalinution of the oil takea place and, on reduction of the turbulence level ~
to a value of Ke = 14~000 (at the end of the section of the drop former
250 mm in diameter), che baeic amount of Wash water is isolated in the lower
part of the drop former. The process of stratificati~~n of the emulaion
- with Re = 8,000 ia completed in the tubular settling tank in the section '
10 metera long. The total amount of desalinated oil to 50-120 mg/liter
picked up directly from the tu6ular settling tank reached 25 percent of the
output capacity of the unit. 5imultaneou8ly, 85 to 90 percent of the drain-
age water was diecharged out of its total content in the oil j78~ 179, 191].
The unstable mixture of water and oil from the intermediate zone, for the
etratitication of which no more than 15 minutes are needed, was picked up
through a eeparate line.
The calculationa demonatrated that the modular tuhular complex including
the two-sec[ion drop former and the settling tank vith an expanded with an
outpuc capaci[y 1 million tons/year weighs 25 tone. The series aettling
tank units operating under analogous conditions vith the same total output
capacity weight 144 tona~ that ie, S times more. The savings from introducing
- one tubular settling tank with a drop former (with an output capacity of -
1 million tona/year) amount to 53.000 rublee/year.
29
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i~Olt [1I~I~IC1~1L U5F. ONI.Y
'The it~cr~aae in output capacity o� the exi~ting ~eteling tank equipment can -
be achieved gl~o tay using the advantgg~g chgra~eeri~tic of hoth Che volumetric
and tubu~ar aettling tgnk~ (eee ~igut~e 40)~ It i~ neceg~nxy to congider the
pogeibility of u~ing the volumetric units simultaneou~ly as n distributing
d~evir.e and n drop former and aiso a gtratifying t~nk guitgUle for picking
up oil and waCer in l~rge amounts ~mong their ~dvant~geg. The quality of
eh~ w~t~r itt thig ~~se i~ eu~h th~t it Can oft~n b~ pump~d intn the 6ed
without additiotsal purificat3on. The adv~nt~ges of the tu6ulgr unitg Come
from their low metal congumption, gimr~c instnllation and cottv~nienCe. The
creation of Che combined units provide~ for combined inet~llgtion of the
tubular nnd volumetric element~ itt n_c.;~bination which correapondg to the
~tated proceee goalg. ~or example~ several tubular ~ettling kanka with drop
formers can be blocked with nne lgrge vnlume gettling Cank, gnd included in
it ng in a eepgraring tank.
The uae of the ahove tnvesti~ated principle~ and the crention of the highly
productive settling equipment on the bagis of it equipped with tu6ular drop
formers hae made it posaible to bring the problem af the complete geal di the
- collection and transportation of the well production in the "well-oil
treatment complex" interval to a practical level. ~or the solution ~f the
problem (91~ it was proposed that part or a11 of the seCtlittg tank equipment
in the firet eCage of the desalineting unitg equipped with drop formers
be used as the preliminary water diacharge unitg. ~n the latter case, qufte
deep dehydration of the oil mueC be achieved pezmiCCing desalination of it
in the aubeequent stagee. Here the transportation of the emulgion from the
field is realized by the ~cheme providing for pumping of it directly into the
unit~ bypasaing the preliminary discharge tanks. The existing aettling tank
equipment and drainage eystem for the units in this case muat be suit~ble
for di~charge of the en[ire volume of water reaching the complex with the
oil. The preliminary water discharge unit in this case is excluded from the
set of field equipment.
On the whole~ the prospecta for increasing the output capacity of the settling
tank installationa, the creation of modular small-eized equipment on the
besis of thie for treating oil and Water with t~igh output capacity and low
- metal consumption $nd also obcaining pure drainage water directly from the
proceas units for treating the ail are connected with the observation of
the following procees principleg: -
Consolidation of cbe dropa of atratal water to desalination of the flow into
oil and water in the proceas of movement ~f the emulsion from Che vells to -
the settling tunk installation and the use of the field collection systems
- and built-in drop formera for these purpoaea;
A reduction in che flow turbulence with respect to direction of motion of the
emulsion toward the settling tank units;
Realization of terminal distributed input and pickup of the oil in the
settling tank units;
30
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t~OIt c)l~'i~'ICIAL U5F: (1Ni.Y
The hook up of the s~ttling tenk ingCnllneinn ~o ehgt ehe drginnge water is -
returned to the heAd nf th~ prdce~s for prin~ry purificgeion gnd demulei~ica~
tion of the oil and ita aperaCion in the optim~l monitoring regime.
Modular Demulaifier~
The indu~tri~lizetion of Che structurce far field trentment of oi1 by u~ing
fgcCory-built moduler automated equipment wi11 theoreCiCally make ie pnsgible
to find efficient ~oluGione to many of ehe pro6lems Connected with field
equipment~ in particulgr, a reduction in cgpital invegtments, meCal con-
guroption, a reduction in congtruction Cime, decrene~ in siz~ of the procesa
sites, and go on [64]. However, the~e prn6leme C~n be eolved only if the
dutput units have high c~pncity and enaure that high quglity oil ie ob-
tained. Industry has built a large number of demulsifiers in different
vergione, many of which h~ve operated for a long time. Depending on Che
methodg u~ed to break down the emulsion, the demulaifiere can be clgggified
in two groupg~ corrpeponding to the eecond and third levels of Creating the
oil. As has already been noted, the second level corresponde to the process
and the equipment (in addition to the aettling operation) providin~t fnr the
application of eome menne of inteneifying the breakddwn of Che protective
shells on the glob~lee of stratal water (hegting, Creatment with demulsifier~
use of drninage water). The third level corresponds to the units and the
process in which~ along with the n~~ed onea, varioue methodg of coalescence
of the dropa are uaed (the coaleecing filtere, electric field, hydrodynamic
coalescere and drop formere).
Considering Chat the modern proceea of preparing the oil ia reckoned at
six levels, it ie e~sy to see thnt the demulaifiers produced by the industry -
vf different countries have become obaolete and are in need of modernization.
The characteristica of cerCain types of demulsifiera developed by the American
BSB Company are presented in Table 3. From the data in the table it is
, obvious that the output capacity of the unita permits their use in small -
formationx. but in medium and large ones~ too large a number of them would
be required to dehydrate the oil. In additian, the units are designed for
obtnining oil with a residual water content of about 2 percent, which at
the presen[ time cannot be conaidered satisfactory.
Anai:,,;~us equipment used in the Soviet fields also fails to provide high
output capacfty with high quality of the treated oil.
The analysie of the flow charts for the oil treatment unitsl which include
_ the type SP units, has demonstrated that out of 97 SP-1000 (SP-2000) de-
mulsifiers, less than 25 percent have operated in the mode of dehydration of
the oil with a degree of treatment noted at the output from the unit to
1-2 percent. The remaining SP-1000 (SP-2000) emulsifiers in the oil treat-
ment unita were used as heaters before the preliminary water diacharge
tanks (tiGDU Shaimneft', Nizhnevartovt~kneft') or ahead of the settling tanks
and the tanka for preliminary dischar~e of the water.
1. Performed at the VNIISPTneft' Institute.
31
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~~nti ~~c~~F~ir, int, tis?, ONLY '
Tnbl~ 3
G
(1) ~2~ ~3~ ~4~ ~S~ it~~nu:ni~~:tnte ii~m~cri~
6 (7) (8)
,)Wy:ii,rnn Ilco~lYnt~rnrri~i ~~na~tepi,i, >i -
: u~r >irnn- nn nc~~~rn, ~~n P:i.~V,
Q ~ i:~~~ru, .r ti.ir.
M~IC)'T 1l~iC)'t
r, L
.
610~ ,
(9) il~~p- ep ~icnn~nWti Ttin S 1,20 X ~t,0 1,5-3 JO-ZI7U IJ~J-UOC~70-31iU
Atn JI6110 q
(11) CTOtVxntt ' epaoxmur~ectnnl Tnn 1,2 X ri,'~ f,5--3 U7--217015,5-GOU~iU---3ii~?
~ ('opuaoliTeJf~nb?ii, Tep. ?--4 370--3000 f02-IG2U 20--'_'UO
?toxu~t~tecKtiii
Key: (1) ~mulsion (7) With reapecC to oil, m3/day
, (2) nemulsifier (8) W~th reapect to gas, thousands of
(3) Dimensions~ meters m /day
(4) Preesure, kg-force/cm2 (9) Normal
(5) OuCput capacity (10) Vertical type 5 -
(6) With reapect to the liquid~ (11) Stable
m3/day (12) Thermochemical type N
(13) Horizontal, thermochemical
Wirh the exception of the ail preparation units of Glavtyumenneftega2 and _
NGDU Tadzhikneft' Administratton in which the output capacity of the units
reached 1,300 to 2,000 m3/day, the actual load of the uniC turned out eo be
2 to 3 times leas than th^ pro~ected load. However, even under such con-
ditions the SP-1000 (SP-; ~0) separators turned out to be ineffective both
as demulsifiers and ae he~ters (Table 4).
In contrast to the type SP units, the UDO type demulsifiers were designed
for a large output capacity (to 3000 m3/day). Some of the results of their
operation are presenCed in Table 5. _
It is inexpedient to use the UDO-2M and UDO-3 uniCs in the heater mode, for -
the thermal efficiency of these units and their other technical-economic
characteristica are much lower than for the NN-2,5 and NN-6,3 modular heaterts
(see Table 6). The thermochemical demulsifiers which do not have effective ~
coalescing devicea and both in the Soviet oil refineries and abroad are
being forced out by the improved electrical dehydrators of various types
(horizontal, vertical, ball) quite completely investigated in references
[8, 198~ 64j.
32
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roFi c~~�rtr.rnt, 115~ ONLY
0
Table 4
lrnMYni,~u~r~~~~ 5~ Ilnunrp~nnTau~
3
~la ~(2~ (4) )
- ~ d ronep~i~nui~o noni~ 64eNnepnTyPn~ �C
unLCn~~uci~us, tIC,~~� ~ n ue~,r~~, %
n
0
m~
n r r~~ r7
~ ~ � iik'akone un ~h~~i~6nc ~n( ~xottc un ~8~otte
. ,
(9) FI1'l~~ ~'~u~Ypr~ir~j~rt, 750 17,8 ,I~o 2 5-14 30
(10) UG~.eiameuiie Cnxnnuu~ic~]~rr~ -
11I'J~J' I3ocTU~cuc~~T?~ 700 20 ~jn 2 4-f0 30
11r~~Y exnGan~fiTr, 230 f0 J~o 3 !2 30
(13} (~fii,ell~inciuiu~ Bi~n~pycnc~rTt~,
III J~Y ro~~in~nncvi~rt~ . 800 5-20 ~(0 3 17 32
- (14) UG~,~~n~~u~iine~'afiottuc~~rt~,rirj~v
AuJU~~tinnuc~jrr~~ 450 f2-5U 2-8 23 40-45
(15) f)fi~~c~umctniu 'l'nTUe~~~Tt,, HC~~Y
Cyn~~nn~~~~~~r?~ . . . . 2i0 - - $ 35
(16) b i,r~umeuiu~ Iiopr+na~ Tn
- (17 HI'1lY c~cuucttue~rr~~ , ; G8U _ _ 1R 30� -
(1$ 1111(Y 1~~'nrypue~~ti, . 90U 18 35
(19) H J(Y '1'nJt>r,uKnc~hTt, . . . . 35U - - 22 48
Key: (1) NGDU Association 3 (12) NGDU Ekhabaneft'
(2) Output capacity, m/day (13) Belarusneft Ass~ciation, -
(3) Demulaifier NGDU RechiCsaneft'
(4) Water content in the oil, ~6 (14) Uzbekneft',Association, -
(5) Heater NGDU Andizhanneft'
~ (6) Temperature, �C ~.(15) Tatneft' Association, NGDU
(7) At the input Suleyevneft'
(8) At the output (16) Permneft' Association
(9) ~iGDU Udmurtneft' (17) NGDU Osinskneft' _
(10) Sakhalinneft' Association (18) NGDU Kungurneft' _
(11) NGDU Vostokneft' (19) NGDU Tadzhikneft'
33
FOR OFFICIAL USE ONLY
,
~
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APPR~VED FOR RELEASE: 2007/02/08: CIA-RDP82-00850R000100030037-7
1~Olt O1~'l~ IC I:AI, IJ5l: ONI.Y '
_ . _ .
O ~ M
N rl Orl
v N NN '
v w
~1 ~ p n ~ N
r
~ t~ b
~~Q~ A Rr 1~{; A A A ~
vJ.~ C v O A~ O~ . ~
L n c a~ o~' M
w ~ t~` ~ rC r v
d
a M i~ cSS i~� ~
~ "
ii p
�J K N d O ~
F vm ro c~ pe3 ~ .a~ A ~ " O
y~ c Z q u o ~
~ ~ o o cv
. n ' , o " N c~d u
K c~ oo in ~n ~n ~ q N
~ ~ ^ I I o ~ o d d~ ~ cA,7 u o 6 v'o
~ o M M z tA ~C D+ W O yt!~ ~ -
~ 0� ir U~ U~ N O O) .1G 6 1.~ ~
o a ~ K ~ o 0 0 o p u o~~ N a G q y W a.~
N W N 4-1 H tA aL q~ Gl W
~K I I ~ ~ ~ .Q~' N Cl N G! � Cl .C N rl 1~ q d
~ ~ ~ ~1 l.i ,1] N .C 'U W aG C
F ~ p `.C ~C W O rl N~ Gl O.~G Gl _
O O N� .~L N'J O ri .C C+' ~ c0 �rl
~ H c`~ ~i O ~ ~ i.~ .C R1 D O c1 G: tA r-1 W
~ ~ ~ $ $ w oo w ~n ~ ~ ~ o .c
..~n` I o I I~ I I~., ~ co n~ a owc~ a~~~~ ~n N~
~Y' : i,. Q ~r ~ O~ ~ O.~� G g q q 1.1 c0 ~ M Gl ~-1 N '
~ G d^ c~ u; ~ .C aC H N,.7 ~C 00 I ~ I
C r ~ ~ ~ tp cU ~ N i-~ A A N A~ A G'+ O cC Q O
oc0ac~ia ~vizzzzviz ~Paxa~
r. r
c'r1 ~ c~ c~ r> N ~ ~ ~ r. i. r. r. ~ rr r. ~
v J, r-1 N ~"1 ~7' u'1 ~O 1~ GO Q~ O r-I N
~ r{ rl e-~ r-I r-1 N N N
v v ~v..~v u vv~~~
~ x ii
~ M N C!h I N N N CV
F ~
v v~ ~ v~ v~ v~ ~0
~
~
~ a ~ . . . ~ � . tA 1 O ~
. ~ . ~ . . . . . O Ti)IOq![NC T109H J(CDMy7ibCi1T0~1
\ /
n~~1:A8~TCJ1{I
~2~5 I ~ -8~3 jJDQ �2M I jJ~Q '3 -
~4~ IIpONB(IOJ~HTOn6IlOCTb IIO -
- ciapua i~pn uarpeao na 40~ C
II OGDOJ~YIPffHOCTtI SO~o ~ T~CyT 3000 8000 ~600 3000 -
~rj~ TPIIAOfIPON880J(itTCJ16ROCTb~ t
~anu. RitAJt~7 2,5 6,3 9,5 3,5 -
(6) Maccu, T . . . . . . . . . 27,2 5y,0 54,9 58,1
(7) 3oeoucims~ cro?+~u~cr~~, Tirc.
pyG. . . . . . . . . . . 27,7 35,2 48,3 4G,A
Key: (1) Indexes
- (2) Modular furnaces
(3) Demulsifier
~ (4) Output capacity with respPCt to crude oil when heating to 40� C
and with water conten~ :,i .i~ percent, tons/day
(5) Thermal output, millions of kcal/hour
(6) Masa, tona
_ (7) Factory coat, thousands of rubles
35
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, F'0~ OrI~'ICIAL USL' ONLY
4,` ,5 5 4
<
~ -
- - _ - -6
2~ _ 7
f , " _.~6 _.._8
. 9
_ f0
_ Figure 41. Nikodimesku Electrodehydr::::or Hquipped at the Tank Base:
1--Oil input; 2--Tank; 3--Oil output; 4--Transf.ormer; S--Insulatar; _
6--Additional electrodes and solid baffle; 7--Electrodes;
8, 9--Input and o~atpuC coils of the steam heaCer; 10--Water dis-
charge.
The electrodehydrators in the United StaCes were initially uaed only for
desalination of the oil at the planta. The output capacity of one unit varied
from several hundreds to 250q m3/day. The residual salt content in a number
of casea reached 1 mg/liter. Then the devices began to be used for dehydra-
tion in the fields. Their outpuC capacity was from 167 to 16,700 m3/day
with a res~dual water content to 0.5 percent.
Depending on the output ct~pacity, the units have dimensions from ]..8 meters
in diameter and 3.6 metert~ in length to 3.6 meters in diameter, a*.d 24.4
_ meters in length. The electric power consumption during dehydration depends
on the conductivity of tl.~e emulsion. Uaually for processing o~ the least _
conducting emulsions, 3.0 kilowatts are required for each 1,000 m3/day of
output capacity of the unit. On the average the cost of treating the oil
on the Petreko electrodehydratora is about 1.12 cents/m3 of dehydrated oil.
The oil is present in the ~nit for 20 minutes. The cost of the electro-
dehydrators ie from 6 to 24 dollars/m3 of daily output capacity, and it
depends on the parametera of the oil. The large units are more economical _
when treating heavy oil. Thus, the Petreko unit on Lake Marac~iho in
- Venezuela removes water from the oil treated with demulsifier at the natur~l
- flow temperature (47� C) For dimensions of the unit of 3 meters x 6.2
meters, a volume of 43 m~ and an output capacity of 2~000 m3/day (730,000
m3/year), the water content in the oil drops from 5~ to 0.3 percent. The _
electrodehydrators 3.7 x 12 meters in size, depending on the density of the
oil, ensure an output capacity from 830 to 1240 m3/day. The units in a
variable electric field develop an output capacity of 15,200 m3/day (p = 0.87)
and 11,450 m3/day (p = 0.9). With a length of tfie unit of 10 meters and
about 40 percent water content in the oil, the designed output capacity
is 3.3 million m3/yQar with a heating temperature of 37� C, The demulsifiers
~ of different type are developed By many companies. The electrodehydrators
developed by the BSB company (for stable emulsions) have the following
characteristica.
36
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;
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'Cype I Type II Type I Type II
Type of de- Horizontal Output cgpgcity: ~
mulsifier
Dimeneione, m: with respect to
Dinm eter 1.8 3.0 liquid~ m3/day 167 5,300
Length 3.6 15.0 with resp~ect to
Pressure, kg- oil, m/day 67 3,300
force/cm2 3.25 1.5 with respect Co
gag, Chou~ands
of m3/day 100 20,000
- The petrolight Company aleo manufactures chemical electrodehydrators, the
coat of which~ depending on their output capacity, can be determined by the
_ data presented below:
Output capac:ity,
thousande of m3/year 150 300 600 900 1200 1500 1800 2100
Cost of equipment~
tho~sande of dollara 10 15 20 24 30 35 36 36
- The electroatatic horizontnl demulsifiera built by the NATCO Company calculated
for dehydration of oil are beginning to be widely used. The primary ad-
vantage of these units ie that the dehydration proceas can be realized nt
a lower temperature than when using the ordinary type dehydrators, as a
result of which the fuel gas is aaved, the oil ccxnposition is improved, the
corrosicn of the equipment and scale formation are reduced. At high oil
temp~rature in the wells, the need for heaticig is in practice eliminated.
The fire i~azard of the ~bjects is reduced, and the environmental protection
is improved. The data on the dimensions and designed output capacity of
the electrostatic demu:c~ifiera built by the NATCO Company are presented in
Table 7. The lower limit of their output capacity corresponds to treatment
of high-deneity emulaione (0.966) not containing free water; the upper iimit _
corresponds to the treatment of unstable emulsions of light oil (0.815) in
the units with a high amount of free wa[er. The purity of the releas~d
water is not guaranteed. The compan;~ produces electroetatic demulsifiers,
the designed (advertised) onCput capacity of which reaches 12 million m3/~ear
(Figure 42). However, models confirming the operation of the demulsifiers
with such high output capacity are in practice atill unknown.
37
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Table 7 -
N
~1~ ~ ~ ~a~ o ~g ~4~ ttpon,m,n~~rc.,~,m,cr~, 8~~',~oa
F ~
P.iaftCV ~mpi~yCe p~ L ~ p r �r, � a
(UxL), N x
~ h
r+1 a~~~~ IIC~b1M, TMC. BOAA~ t~~IC~ RI~
~ucv.o ~'~a.f. M~lPOIl M~/POA ~bIC. ~~o
~~h� 7~O~Cv ~S~ C~~ 7,M ~~~T ~Oo
w x~
1,2 x 3,f b3 1-30,5 8,7-~26,3 1f,(i-28,R (1~�17 2
1,R X 4,[i f30 1-45,7 20,3--f40 28,8--SA 14--28 ;'i
1,8 x 6,1 2;,2 f--45,7 14--28 5
2~4 X 4~G 189 1-t31~0 70-2,ri4 74,fi-104 4`C--S7 5
2,4 x 4,6 '.ti7 2--45,7 42-57 5
2,4 x fi,t 378 f~-Gf,O 4G-f39 42-57 5
~,4 Y, G,f G30 2-45,7 f40-324 42-57 5
2,4 x 7,G 378 f-G1,0 42-57 5
2,4 x i,6 5fi7 2-45,i f75-350 42-57 5
3,1 X fi, t 504 2-45,7 57-Sfi 5
5,1 x 11,f f~3~ 2--G1,0 193--394 5G-17~i 57-85 5
3,1 X G,1 7~i(i 3-45,7 57-SS 5
3, t x 7,f ~d14 2--5'n, i 57-85 1 S
~,f x;,~ G3u 2-ff,o 24r,--,~5 SG-f~4 57-85 15
3,! X 7,(; 751~ 3_45,7 57--S.i 15
3~1 X 0,1 :d)~i 2-~~i~7 57-85 1Ci
'4,1 x t),t C~30 2-(i1,0 :230-800 SG-174 57-8:i 15
3,f x 0,1 7:~t; 3-45,7 57-85 15
3,f X IU,7 7,58 2-~1,0 280-800 87-2f~0 57-85 15
3,1 f0,7 D45 3-45,7 57-85 15
3,f x 12,2 ~J45 Z-G1,0 115-~SA 85-f43 2S
3,f x f3,7 1260 2-6f,0 490-9~0 i45-43~ 85-l4~ 25
3,1 x 15,2~ f512 2-G1,0 174-520 85-f42 25
Key: (1) Size of housing (DxL~~ meters
(2) Capacity of the heating tuhes, 1000 kcal/hour
(3) Number of hall tu6es witti nutside diameter. cm
(4) Output capacity -
(5) Oil~ thousands of m3/year
(6) Water~ thousands of m3/year
(1) Cas, thoueands of m3/year
(8) Rated transformer power~ kilovolt-amperes
The electroatatic demulsfiers operate on 16,OQo volt DC current with a strength
of 0.2 a~ps. The ou[put cnpacity of such demulsifiers is 15 to 20 percent
. higher than the capacity of the AC electrodehydrators, and they cost 2 to
3 percent leae than the latter. The main part of the electrostatic coalescer
--the basic Element of the electrostatic demulsifier--is the transformer
6 with eaturea core. The unit fias the property of transforming power from
the feed line in accordance with the required load depending on the con-
duc[ivity of the oil [reated in each instance. If the load becomes too
great, the transformer reduces it to the admissible level. The operation of
che equipment in the self-adjustment mode excludes the problem of
38
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~Oit OF~'ICTAL USE ONLY
ehorC-circuiting and the disconnection of the feed s~ysCem hy protection
which can be Cbfi[i10t1 to it and the transformer.
Figure 43 show~ the ueual schemntic ~or cregting ~n elertrir field in an
- electrodehydrntor nnd in nn electroetaCic demulsifier. The em.~leion to be -
trcated ie fed to ehe AC field (see ~igure 43) created between the electrodes
- 1-2. Inasmuch ns the water in the lower part of the unit had a pdtential
equal Co ground potential, it also acta like an electrode 3. The emulsion
~lowing off the oil-water phase inCerface is first sub~ected Co the effect
of the variable field with low volCage gr~dient and Che basic amount vf the
water settlea ouc. After passage rhrougfi the electrode to the emulsion
goeB into a higher voltage zone in whi~h ehe basic amount of water rero~ining
in the oil coalESCes. In a large number of cagea the oil undergoing treat-
ment in thi~ zone containe no morp than 0.1 percent water.
~'igure 43~ b ahowa the circuit diagram for Che new electrosCatic demulsifier.
The same transformer ie used here, but there are two lines at the output
leading through the rectifiere Ca the poeitive electrode 10 and the negative -
electrode 9 respectively. This crentee an extraordinarily high DC valtage
between the electrodes 9-10. In this equipment the oil-water phase inter-
face hae the same potential ae ground~ and it is a third electrode 3. The
interaction with the electrodee 9-10 in this zone createa a variable field
with low volta~e gradient.
a ~
6 -
Z~~ 14 d3 ~4
, III~
�1! 14 !s i4 ~
~ o 0
_ - - = T V
b 8 6 .
9 =
~ ~0= 9= !0 III~
~
!i * '
J . - --y~ �7
Figure 43. Schematic of the Arrangement of the Electrodes and the Directions
of the Lines of Force in the Electrodehydrators of Different
Structural Designs:
a--In the usual type equipment; b--In the electroatatic dehydra-
tor; 1, 2, 3--Upper, middle, and lower electrodes; 4--Direction
of motlon of the emulsion; S--Direction of motion Qf the enlarged
drops of water; 6--Transformers; 7--Rounding; 8--Rec[ifiers;
9--Negative electrodes; 10--Positive electrodes; 11--Direction _
_ of the lines of force of the field.
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roK o~~ icinr. Us~ orn.Y
I?~ th~ operatit~g procesg~ only ttie poaitive part of the Cyc1e comeg to
the electrode 10, I~ the oil between th~ elecCrnde~ cont~ins c~ gmull tunount
_ of wnter, leaka of the charges ftrom the elentrodeg ld dr 9 will noC occur,
ac~d tt~e voltage gradient wi11 be quiCe high. If the wnter content in Che
otl. tncre~ses~ p~rt nf the charges will be lose~ and the voltage grudient
wilt drop autom~tic~lly. Although the voltage gradient decreases and is
reatored 60 Cimes s sernttd, the direction rem~ins constanC, which creates
~ DC voltuge field. Witl~ th~s design, we have CFie possibility df using a
variable field in the zone of increa~ed waCer content between the electrodes
and ttie aurface of Che water and ~ DC voltage field with high parameters itt
~ the zone of reduced water content~ wh:~c~h permiCs coalescence o� the smallegt
drops. 'This c.ombin~tion nf the electric fieldg improves the operation of
rhe dehydration units which are highly superior wiCh reapecC to efficiency
to r_he traditional uni.ts. On Che ma,jority of unite wiCh moderate output
cnpncity only "traces" of wster remain in the oil.
Q ~ millione S,5 ~ Z ~
of m3/Year 45 f ~
4,0 ~ ~
J,S ~ -
~o ~ ,
2,0 ~
~
~s
O,' f03 097 091 OBS 0,79: ~~3
T, �C ~
95
~
6S
60
SS
30 ~
45 ~
~ JS -
~
l2J
F'i~ure 44. Output Capacity and Heating Temperature as Functions of the
Oil Density:
- 1--Electroatatic'dehydrators; 2--Usual type electrodehydrator;
3--Thermochemical settling tank.
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r, �c -
u
65
1
35
45 2
~50,2 O,J 0,3 1,0 2,0 J,OdW
Figure 45. Reaidual Water Content in the Oil AW as a FuncCion of the Heating
Temperature for Oil with a beneity of 0.8498:
1--Thermochemical settling tank; 2--Electroetatic dehydrator.
The study (202J points to the possibility of a significant increase in
equipment productivity with the use of electrostaCic dehydrators in com-
parison with thermochemical settling tanks or ordinary electrode-
hydratora.
In Figure 44 it is obvious that when treating oil with a denaity of 0.87 the
theoretical load on the thermochemical unit 180 m3 in volume exceeds 3 million
m3/year, the ordinary type electrodehydrator, 4.8 million m3/year and the _
electroetatic dehydrator, 5.5 million m3/year.
According to the data of R. V. Koggins [51], the degree of dehydration of _
the oil on the unite utilizing an electrostatic field also increases by
comparison with the ordinary thern~ochemical settling tank (see Figure 45).
For equal heating temperature the degree of dehydration of the oil using
the electroatatic dehydrator increases by 6-8 times.
�
If we compare the graphs in Figures G4 and 45 and try to find the relation
between the output capacity of the units of different types and the degree
of dehydration of the oil at equal temperatures, it turns out that for oil
with a denaity of 0.849, the following relations will be valid.
- For a heating temperature~of 48� C, the residual water content in the oil
during treatment in the thermochemical settling tank with an autput capacity
of 3.7 million m3/year will be 3.0 percent. Wfien treating the oil in the
electrostatic demulaifier at the same temperature the residual water content
will he 0.5 percent, and the output capacity will exceed 5 million m3/year.
_ Hence, it follows that for the given parameters of the oil treatment in
the thermochemir.al settling tank, it is not ensured that conditioned de-
hydrated oil be obtained~ or in the electrostatic dehydrator, desalinated.
_ Obviously this turns out to be poasible only wfien working with equipment
with an output capacity appreciably less than the maximum valuea which are
presen[ed in the graph in Figure 4b.
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Table 8
11Pnuan~~dnTC.ii~nncr~, y~tn- ~
ItnbHll~ !n. Ilpil nCti~tn411uM
rCMIIPrOT\'pq C~IIICp~ltdllllll Bu7L1 n IIC~tII
nnrdeda, �C
0,1!: I 0.2!:
3U IUI) I i ~i
~iU I;IU 210
5U � ' fiU 245
GU 21O 280
i 0 l4 S
Key: (1) Heating Cemperature, �C
(2) Output capacity of the unit, X, for a residual water content in
- the oil of
Note. The output capacity of the unit at T= 30� C and a residual water
content in the oil of 0.1 percent is taken as 100 percent.
- Table 9 -
lfnmr~~rruo ronap-
uut? ue~n~. Mac. : ~
= upif mMn~pnrypc
ii:i~rru~kTi. unrpcu~, �C
nc~pn~
J~ I A2
0,8U9 ~J4 9t
1),873 :~7 Uli
0,913 fl8 98
Key: (1) Oil density
(2) Amount of commercial oil, mass percent, at a heating temperature
of, �C _
The output capacity of the units easentially depends on the heating tempera-
ture and the area of the electrodes. Table 8 gives the data on the increase -
in output capacity of the electrostatic dehydrators as a function of the
heating temperature. -
In the electrostatic demulsifiers the oil can be treated at a temperature ~
of 8 to 15� C, which will permit a significant increase in the output of
commercial oil. Table 9 shows the values calculated according to the data
of reference [202J for the variation in the amount of commercial oil as a =
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functiot~ of ite den~ity gnd heating temper~ture; hence, ie i~ c~bvinug th~t
with gn in~regge in e~mpernture its losse~ cpn he ~ignifiCent, egpeclnlly
fdr light nil.
Thr. ~per~~Cing expendit~res ~n electric power dcpend on the,eize di thc unit
(the ~rex of the e1~CCrodeg) and the electric~l conductivity of the oil.
With gn inerease in electrical cottductivity of th~ oil, th~ expenditurea on
the electric power increase. With an electric pow~r coet of nne cent per
kilowatt, the expenditures on electric power when treating 1,m3 of oil gre
_ on the average (for the average oil of the Gulf of Mexico), 1.2 cente.
On the whole~ the advantages connected wiCh Che dperati~n of the electro-
stgCic dehydraeora uaually include the following:
High output capacity of th~ unite;
A de~rease in aize of the process aites;
The possibility of carrying the process out nt low temperature and with low
consumption of freal~ wash wgcer;
Fuel savinga;
_ A reduction in lossea and an increase in volume of the commercial oil. -
Without discussing the atructural problems with the third lev~l demulsifiers,
_ let us indicate a number of decisive deficienciea characteristic of the
equipment of thia type as a result of ~rhich basic atructural reworking of
the equipment is necessary from the pi~int of view of the modern concepts of
the optimal conditions of breaking do~wn emulsions: -
Absence of mass exchange and stratify:t.~~g section intensifying the demulsifica-
tion procesa (and for the second level equipment~ also the coalescing medium);
Failure to ~bserve the principle of the optimal sequence of operations
(heating, treatment with reagent, destruction of the protective ahells,
- coalescence of the drops and stratification of the flow) and realization of
them simultaneously with the same hydrodynamic unfavorable conditions of
movement of the flow (more frequently, laminar);
; Technologically inefficient combination of operations connected with heating
the emulsion and its standing in one unit;
Realization of low distributed input of the emulsion through the layer of
drainage water~ in connection with which the output capacity of the unit
is limited to the aettling rate of the drops of stratal water suspended in
tt~e body of the oil directed opposite to the flow.
This results in low output capaci[y of the units, increased fire hazard, the
neceasity for ahu[ting down the entire unit in case of a failure in any
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F'Oit nl~'~'ICIAL USG QNI.Y -
gection, incre~eed dero~nd for mdnitnrin~ ~nd autom~tintt equ~.pment and ul~o
regul~ting nnd valv~ fi.ttingg, nnd th~ neceggity for u~ing g high number nf
units et th~ high-output installatione
COPY~IGHT: Izdgtel'gtvo "Nedra", 1977
10845
C50:8344/0812
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F'U~L5 ANb ItEI,ATED ~QUIPM~NT
TYUM~NTItAN5GAZ A550CIATION UURING lOTH ~'Y1'
~~oscow GAZOVAYA PR0~4YSHLFNNO~T' ~ERIYA: EKONOr4IKA ~A.ZOvOY
= PROMYSHLF.NNOSTI in Russian Nn 1, Jan 79, pp 1-5
(Article by T. Zhuzhgova, Tyumantransgaz Production
Association]
(Text]In accordance with the targets set in the "~~ain llirections
for the Development of the National Economy o.f the USSF During
1976-1980", in 1980 it is nlanned to extract 435 b~llion m3 of _
gas and increase gas extraction by 145.7 billion m. Of this
total~ growth in Tyumenskaya Oblast will amount to 120 billion m3,
in 1980 the entire annual increase planned for the nation will
be attained from gas deposits in Tyumenskaya Oblast. Iluring the
current five~year plan the volume of gas transported by the -
_ association will increase 2.6 fold, i.e. from 87.2 billion m3
in the Ninth Five-Year P1~ it will increase to 344.6 billion m3,
a growth af 257.4 billion m
While in 1975 consumers in the ilrals and the center of the nation
obtained 31.5 billion m3 of Tyumen gas, in 1980 they will
- receive 82.6 hillion m3 through the association's gas ~ipelines,
annual deliveries of gas will am~unt to 225.8 milliQn m,(in
_ 1975 the figure was 86 million m).
In order to transport this quantity of gas 2,964.2 kilometers
of gas lines and 21 compressor facilities will be built ( of this
figure, 717 kilometers of lines and 6 facilities were intro-
duced in 1976). Capital investments will total 1,916 million
rubles and fixed capital valued at 1,072 million rubles (see
T~ble) will be introduced. By the end of the five-year plan _
the value of fixed productive capital will amount to 3,404
million rubles~ i.e. an increase of 2.7 fold in compa.~ison
with the corresponding data in 1975..
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T~ble: Technicnl-~conomic Indicators of Tyumentransgaz huring
the Tenth Five Yeax Platt ~
1975 1976 1977 1978 1 78 as
Report Report Report Plan percent of
1977
CommerCia~ gas 31,47 41.74 59.18 78.39 132.5
billion m
Value of fixed -
capital, million
rubles 1,247.9 1,634.7 1,670.8 2,486.7
Capital invest-
ments, million
ruhles 463.7 319,5 310.I 202.5 65.2
Prime co~t per
_ 10,000 m o� gas, ,
rubles 25.08 24.56 23.68 23.66 100.00
Profits, million
rubles 16.27 33.~0 26.42 32.32 122.00
Profitability,
percent 1.3 2.03 1.3 1.29 99.2
Output/capital
ratio, rubles 0.23 0.24 0.26 0,26 100,00 _
Ratio of rlaterial
Incentives Fund to ~
Wages Fund, percent 11 10.1 8.76 9.50 108.5
The output/capital ratio of fixed productiv~pital will be
reduced somewhat by the end of the five-year plan (from 0.23
to 0.21). -
The output/capital ratio, characterizing the efficiency of
fixed capital utilization, has especially great significance
in pipeline transportation, since practical experience has
_ shown that the introduction of compressor stations lags behind
the introduction of gas lines and the time required to attain
the planned productivity of gas lines is increased. In other
words, the growth rate of fixed capital exceeds the growth rate
of the amount of gas transported. -
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The development of the production association similar to the
transportation subsector, is being increasingly inFluenced by
negative factors, The main ones are the 3ncreased average dis-
tance of gas transportation, and natural-c~imatic conditions.
These �actors are, to a considerable extent, causing deterior-
ation of such indicators as prime cost and profitability,
By the end of the five-year plan prime cost for the association -
w311 increase by 24 percent, and the output/capital ratio will
_ drop by 9 percent, The number of workers per 100 kilometer5 of
gas, computed on n single line basis, continues to grow, ~
althoagh it is felt that it should decline. Insignificant -
increases in gas line distance have been accompanied by sizable
growth in the number of GPA and th~ number of workers in gas
transport is increasing primaril~ in the compressor service
area: gas compressor station, KI and A(Control and measure-
ment equipment and automation), and EVC (C~mputers). For -
example, in 1976 717 kilometers of line were installed. The -
number of workers in gas transportation during this same period
increased by 421; of which 144 were at the gas compressor
stations, 59 at the KIP and A, sections, and 64 at the EVS
section, There are 44 people directly engaged in servicing
the line sections of the system, 10 percent of. the total increase
in personnel.
By the end of the five-year plan th~ number of workers will _
increase 2.9 fold and amount to 9,724 (in 1975 it was 3,327).
Pipeline distance will increase by 66.7 percent -7,407 kila -
meters. By 1980 economic incentive funds will have practically
doubled. In 1975 the FMP material incentives fund was
869,000 rubles, in 1980 it will be 1,683,100 rubles.The FMP
is usually planned as a percentage of the FZP Wages fund and
if examined from this perspective, everything is normal, i.e.
the FF1P is 10 percent of the FZP, However, if one looks at
FMP payments per worker, then this indicator has; deteriorated
in 1975 it was 296 rubles, in 1976 - 281, and 1980 - 173.
In order to solve the problems facing the nation in the Tenth
Five-Year Plan it is necessary to carry out a complex of -
measures directed at revealing reserves, and improving the
efficiency of fixed capital utilization and equipment oper-
ation reliability.
Specialists at the association have developed a five-year plan
for improving the management system with these goals in mind.
The economic effect from implementing measures in this plan
amounts to 202.7 million rubles. Implementing the measures
will cost 159.5 million rubles.
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The basic mensures in the plan for improving the man agement
system aret
1, ]:mprovements in organizational structure - an economic effect
of 8 million rubles.
2. Reductions in nonproductive expenditures and losses - an
economic effect of 1.2 million rubles. _
3. Increases in the reliability uf equipment operation - an
economic effect of 1.2 million rt~bles.
4, Measures for the acceleration of scienti�ic~technical
_ progress - an economic effect of 192.0 million rubles,
S. The mechanization and automation of management work. This
section contains measures to provide workers in the management
apparatus with management equi~ment, which includes computer
hardware, equipment for preparing and copying documents, all
types of communications. In 1975 the amount of equipment avail-
able for management work was worth 3,C92 rubles per worker,
and by the end of the five-year plan it wi11 reach 7,~00 rubles, _
_ i,e, a growth of 1.9 fo~ld. This same section includes the intro- _
duction of automated management systems. The economic effect
of ineasures for the mechanization and automation of management
work is expected to reach 2.6 million rubles,
6. Reduction of the relative share of workers in the management
apparatus by 22.3 percent in comparison to the norm and
reductions in apvarat�s maintenance expenses through the intro-
duction of a set of ineasures reflected in the management impro-
vement plan. It is expected that the economic effect from this
will amount to 1.9 million rubles.
ln 1975 the numher of workers in the management apparatus
amounted 18.7 percent of the total, and in 1976 the figure was
17.9 percent, a reduction of. 4.3 percent.
- In the Tenth Five-Year Plan of efficiency and quality, the
intensification of the conservatio,l, rational and thrifty use
of raw materials, other materials, and fuel and energy
resources is very important.
Collectives at many enterprises in the sector have outlined and
are implementing specific measures to reduce the material inten-
sity of output, and conserve the use of materials, energy and _
other resources. In 1976 the Board of the Ministry of the Gas
ordered an All-tlnion review of the efficiency of the use of
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materials, and fuel and energy resources at enterprises and
oxganizations ~In the ministry.
The Tyumentransgaz Association, including all LPiTMG, par~icipated
in the review. In 1976, during the course of the inspection,
531 suggestions were made~ 0~ this number 491 were implemented
and the economic e�fect from their introduction amounted to
171,500 rubles. Ninety-nine tons of turbine oil, 19,500 kilowatt
ho~~rs of elect rical energy and 6.6 million m3 of gas were
sav,~d. The following measur~s were implemented:
- Nadymskoye LPiTMG Line production administration for main gas
pipelines - additional feeding of hot air into the compressor
s~~p through redesigning oil coolers. This ensures the
reliability of the compressor station machinery hall heating
system5 and increases the temperature in the facility by
S-6 degrees.
- Krasnotur'inskoye LPiJMG - sold excess materials and equipment -
amounting to 26,000 rubles.
- Kazymskoye LPi1MG - heated production facilities at the field
- site through utilizing heat of reserve boilers. This reduced -
_ gas consumption for its own needs.
In order to develop the scientific and technical creativity af _
y ouung people and to more extensively enlist young workers,
specialists, engineers and technicians, a scientific-technical
review of youth creativity was announced for 1977-1980.
A review commission of nine individuals chaired by the
association's chief engineer has heen created.
An integrated program for engaQing young workers and specialists
in scientific creativity has been develope.l.
In order to improve the standards ~f technical creativity of
young collectives competition has been organized among youn
_ creative brigades to attain the best indicators for efficiency
promotion. In 1977 the results showed that during the first stage
of the review the better indicators were attained by t~e
brigade of young innovators at the Long-Yuganskoye LPUMG, in
which T. I. Zakharov, V. G. Nimchenko, and A.S. Vorob'yev.
The better works of young innovators are included in the collect-
ion "Rationalization Suggestions" published by the Tycmentrans- x
gaz printing office and recommended for introduction at other
LPUMG.
49
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Thirty-nine young specialists underwent training at courses
- and institutes for improving qualifications in TToscow, Kiev,
and Kaliningrad,
Innovators participated in the seminar: "Experience in the
_ Utilization of Automated Management Systems at Enterprises in
the Sector" conducted at the VDNKH Exhibit of the Achievements
of the National Economy ; at a conference of. young specialists
in Tyumengazprom A11 Union ProdLiction Associa~ion, held under
tlie slogan "Enthusiasm and Creativity of Youth in the Tenth
Five -Year Plan", and in the Fourth Creative seminar in Urgencli.
COPYRIGHT: VNII~gazprom, 1979
11,574
CSO: 1822
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~Oit O~~ICIAL U5~ dNLY ~
_
, ~'U~LS ANU It~LAT~U EQUIpM~NT '
~CUNOMIC EF~ICI~NCY 0~ NEWI.Y INTRODUCED NATURAI. GAS bEPOSITS
Moscow GAZOVAYA PROMYSHLENNOST'. SFRIYA: EKONOMIKA GAZOVOY
PRUMYSFILENN~STI in Russian No 1, Jan 79 pp 20-21
(Article by S, V~ nubrova, Komi Branch VNIPI All iinion
_ Scientific Research and Planning Institute for the Gas Industryj
(Text 1 In compiling designs of OPE and developing gas deposits,
the comparative efficiency of. their operatinn is de*~rmir~ed
by com~aring costs for the exploration, extraction, ~nd trans-
portation of gas with the closing costs at the site of its
_ use (1 iJsing such comparisons, even very capital-intensive
deposits are more efficient tha~i coal extraction.
However, if one calculates the absolute efficiency of the gas
extracting enterprise and the time required to recover capital
investments in gas extraction, not every gas field's profits
justify expenses for project development within the norm period.
Thus, with respect to cost levels, the majority of small and
rnedium deposits in the Timano-Pechora province of the Komi
ASSR are lower than closing costs, but have low profitability
or even losses. The time required to recover investments amounts
to 8-27 years, with an average cost of 6 rubles per 1,000 m3
of gas (see Table I)
in connection with work on the new system of economic incentives
now being conducted, the profitahility level indicator has
great significance in evaluating the economic activity of gas
enterprises. It is computed as the ratio of total profit to
productive capital and shows the prafit society obtains per
rub:e of produetive resources expended. However, in the practical
~vork of planning deposit development, this indicator is still not
widely used. It permits relatin~ the efficiency of capital
investments in deposit development with the syster~ of _
~nterprise profit and loss indicators and gives consideration
to real investment r~co,very periods for deposit development (1).
51
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'Table I, Indic~tors nf the ~fficiency of the Development
_ of PromisinQ Denosits in the Komi A55R
Mer,ropo~utep?~ ao 2 i? aee ~ H e a r a ~
peAaiow npo~~tu:e H8 !?e I'~P e aa spaH- or~cnoCb o- rabenb- oo g4uasr~a~~os~~
~od~y rpoecnopr cnopr ar ~roro EBNNX I'83B no HOCTb~ Oy'CKx~H Il@fla
) ) ~ip yzru Yxre+ 1to Cp9PHUHMD C qn~ n n nRren
~ 3 (~1) yegrpe ~eKUaeuuiu+ c yver~ or~uc-
crQaNU ( 5 ~ Toa~Ba+ ' a ( R~ ae~o0 xa i'P~~
P96�/i00b w pya./I000 M
i n ) Na .a~-a~B~cN�~ ~
10 . l~~o~Y~ 5,8 4.3 ' 4.5 ~ i4.6 d.4 I3 9.3
(1 f1 , 2 Be~enBrcc~oe 6.4 4.3 4.5 I5.2 '7~8, II ~ ~.9
(1 3~aoe~aoecroe 7.5 4.3 4.5 16.3 6.7 8 9.0
~ n. a#~y~~Hexoe ~.I 4.3 4.5 I7.Q ~.I . 5 I0,6 `
~ l 1) 6e a~e-I~eaopo~rl ' ' , -
~ l l. l. ~occoxddctcoe y.2 6.I 4.5 I9.8 � 3~2 ' 4 I4.7
(11 . 2 prAHCxoe 9.3 6.I 4,5 I9.9 ~~I 4 ~ I0.8
(1 1. 3~YPLAacxoe I4.7 6.I 4~5 25.3 -2.3 - I6.2
1 2 ) Cp~aHe-uevopcK~q
_ ~ 12 . j)Ievopo~o~ceqHC~oe I3.9 3.8 4,5 22.2 0~8 3 I5,4
2. 2~x~poropat- 22.5 3.8 4.5 30~8 -7.8 - ~ 24.0 -
(1 2 . 3'~aaeRao-Con- , ~
~.~cxoe 4I.5 ~ 3.8 4.5 49.~ -26.8 - 43.0
Kcy: 1. Deposit by 10. Nar'yan-Marskiy
kegion of 10.1. Layavozhskoye
Province 10.2 Vaneyvisskoye
2. f'alculated Costs, 10,3. Vasilkovskoye
ruhles per 1,000 m3 10.4. Kumzhinskoye
3, For extraction 11. Verkhne-Pechnrskiy
11.1. Rassokhinskoye -
4, For geological explor- 11.2. Pachginskoye
atory work and trans- 11.3, Kur'inskoye
portation to Ukhta 12. Sredne-Pechorskiy
S. For trans*~ortation from 12.1. Pechorokizhvinskoye
tikhta t~ Center 12.2. Pechorogorodskoye
6. Total 12.3. Zapadno-Soplyaskoye
7. Effect f rom the use of
- gas in comparison with
- closing cost fue~,
rubles per 1,000
8. Profitability
9. Plinimal necessary transfer
price for enterprise,
includin~ deductions for
geological exploratory
work. rubles ~er 1,000 m3
52
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The pro~it~bilitiy 1eve1 involves m~ny interacting factors which
depend on initial reserves, well productivity, development
~ conditions, gas extraction technology and processes, production
organiz~tion~ and others, ?t is related to the coe�ficient of
the economic efficiency of deposit development, E, which is
the relationship of profit to capital investment. If, as a
result of the measurc..; suggested, the coefficient o� efficiency -
is lower than the norm (En) the expenditures are not justified
w3thin the sector pay off period. For example, if in industry
- En ~ 0,12, the production profitability level should not be
_ less than 12 percent, i.e. the margins for the econ~mically
rational development of a deposit are determined by the
conditions E is greater than or equal to 0.12, or T is less
than or equal to 8.3 years.
As practical experience h~s indicated, at large, high production
rate deposits the coefficient c~� effici~ency is quite high, while
: at medium and sma11 production rate deposits it is low. Small
and capital intensive deposits will have coefficients of effic-
_ iency less than 0,12 (see Table I).
At the Timano-Pechora province several groups of promising dep- -
osits are distinguished by the level of prime costs:
Low cost hydrocarbon resources (2-3 rubles per 1,000 m3) -
- Layavoznskoye, Vasilkovskoye, Vaneyvisskoye; _
Medium cost (4-5 rubles per 1,000 m3) - Kur'inskoye,
Rassokhinskoye, Pechginskoye;
High cost (6-7 rubles per 1,000 m3) - Kur'inskoye, Pechorokozh-
vinskoye';
Very high cost (9-15 rubles per 1,000 m3) - Pechorogorodskoye,
Zapadno-Soplyanskoye
The efficiency of devel~ping the majority o.f. these deposits
is beyond the limits of the cut off. �or capital investment
recover~y. However, the enterprise price for gas (6 rubles per -
1,000 m) does not give an objective evaluation of the absolute
efficiency. Since part of the gas field profits are used by
the enterprise to transport gas, some authors (1,2) recommend
calculating the coefficient of capital investment efficiency
not within the framework of a single deposit, but from the
perspective of the gas sector (Eo). Table I shows the coeffic-
ients of. efficiency for the developing of deposits with con-
sideration given to costs and profits for transportation enter-
prises in the sales of gas to consumers in the Komi ASSR and :
the Center of the natio~. The total efficiency of capital invest-
ments calculated in this way is higher than for a gas field,
however, Eo is greater than or equal to En only for three
deposits in the province. 53
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Tn connection with the n~tion's growing sc~rcity of gas, espec-
ially in the ~urdpe~n sect~ons, one should attempti to find con-
ditions unde~� which develoning the.low production rate deposits
would be economically ~ustifiable, A recovery period within the
norm can be att,~ined t rough increasing well �low and reducing
the c~st of well installation and f.ield development. Nowever,
_ tliis is not now al?vays done.~
' Changes in existing enterprise transfer pric;es for gas could
also help improve profitability. The minimal transfer price, p
for obtaining the n~cessary profir and compensating for enter-
prise expense~ is found hy the recovery formul.a.
T = K
CQr(p - s)
P= K + S� kyd. S d
Qr . T
Where: K- Total capital investments for the development
of the deposit
kUd - Relative capital investments
T- Norm pay off period (8,3 years)
Qg - Annual gas extraction
- S- Prime cost for the extraction of 1,000 m3 of gas.
That is, product transfer price should, at a minimum be equal
to calculated costs and differentiated for enterprises with
- regard to their size. In ~ddition, it is necessary to increase it
by 1.5 rubles per 1,000 m in order to compensate for costs for
geological exploratory work (GRR). Thi~ means that if gas prices
w~re increased to 8 rubles per 1,000 m, the development of the
Layavozhskoye and Vaneyvisskoye depos~ts would hecome feasible,
if increased to 11 rubles per 1,000 m, then the development of
the Kumzhinskoye, Rassokhinskoye, Pachginskoye deposits, etc.
would become feasible (see Table I). �
To the extent that the marginal value of prices are closing
costs, reflectin~ the level of socially necessary costs to
satisfy requi.rements in cases of lack of output (I), the problem
of the possibility of increasing enter~rise gas transfer prices
should be solved on the basis of the difference between costs
54
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fnr closing output in regions of its consumpt3on and calculated
costs �or the exploration, extraCtion, ~nd transportation. of
g~s to consumers,
Calculated costs for geological exploration work and transport-
ation of gas ~rom the city of Ukhta and then on to the eenter
of the nation are c~lculated for four arbitrary r~gions of
_ the Komi ASSR. The difference between closing cost and these
costs determines the maximum allowable calculated costs for
gas extraction in the region of the deposits (Table 2), or
tlie 1imi.ting maximum price for gas sales. _
Table 2. Calculated Costs for Cas Extracting Regions of
the Timano-Pechorskaya Province
Costs Nar- yan Verkhne- Credne- North
PTarskoy Pechorskiy Pechorskiy east
Calculated Costs
For geological
exploratory
work 3.4 5.7 3.8 6.5
For transportation
to 1lkhta 0, 9 0. 4 - 0. 5
For mainline trans-
portation from Ukhta -
to the Center 4,5 4.5 4.5 4.5 .
Maximum allowable ca~.-
culated costs for gas
extraction 14,2 12,4 14.7 11.5
Closing costs 23.0 23.0 23.0 23.0
In comparing the calculated minimal necessary price for the
enterprise (see Tab1e 1) with the marQinal cut off for cal-
culated extraction costs by region (Table 2) we come to the
conclusion that these prices cannot be set for all deposits
in the province. For the last four (see Table 1) the necessary
pr.ices exceed the maximum allowable costs (or prices) for gas
extraction. Consequently, one can see that their development
_ is not now advisable.
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In solving the prohlem of deposit development efficiency, it
is not suffictent to estim~te the national economic e�f.iciency
only through determining comparative efficier.cy. Tt is necessary
to simultaneously determine the ~bsolute ef.ficiency of capital -
investments in development, comparing the coefficient of
effiriency (or profitability)with the normed efficiency coef�ic-
ient of the sector.
I~or deposits where ~ is less than or equal to En one should
look at conditions under ~vhich their development will be
stifficiently profitable. This in~-ludes the possibility of
changing transfer prices for field output. If this requires
setting a transfer price hi~her than the allowable cost
for gas extraction (clo,sing in the region of consumption minus
costs for geological exploratory work and transport~tion, it
is not economically advisable to develop the deposit.
BIBLIOGRAPHY
1, (Irison, G. S. ~ Tyshlar, I. S. , Khosh, r+. "E;conomika
razrahotka azov kh mestorozhdeni "(Economics o t e
evelopment o Gas Deposits ~+oscow, Nedra, 1973, p 297,
2. Brents, A. D., Garidkin, V. Ya., Urison, S. 11Ekonomika
azodab va ushche rom shlennosti"') (Economics o -
t e as xtraction n ustry oscow Nedra, 1975, p 248
3. Gandkin, V, Ya., Shamis, L. V., 5hpakov, V. A., "Economics
of the Efficiency of Deposit Development and Introduction"
EKONOMIKA GAZOVOY PROMYSHLENNOSTI, Moscow, VNIIEgazprom,
1976, No 5, pp 3-6.
- COPYRIGHT: VNIIEgazprom, 1979
11,574
CSO: 1822
SG
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~'U~LS ANb RELATED ~QUIpM~NT
UDC 622.279,5.003,14
PRIM~ CO5T OF GA5 U~PO5ITS
Moscow GAZOVAYA PROMYSHLENNOST', SERIYA: EKONOMIKA GAZOVOY
PR.OMYSHLENNO5TT in Russian No 1, Jan 79, pp 25-29
(Article by N. M. 5oshnin (5evka.vniigaz, G.S~Urison,(VNTIgaz)]
[mext~ In accordance with the presentily existing organizational
structure, the majority of aas field administrations (GPit) for
gas extraction, or administrations for gas extraction and trans-
portation (UDTG) include several gas deposits. For exam le. in
1976 the Kuban'gazprom [Kuban gas industry Association]~had
developed 25 gas and gas condensate deposits, including the
Krasnodarskoye UDTG - 10, the Kanevskoye GPtT - 12, and the
Maykopskoye DGT - 3. In existing report procedures expenditures
are considered for the GPIi as a whole without distribution to
individual deposits, The f;PU~s individual deposits differ sig-
- nificantly with regard to their geological and technical charac-
teristics, and correspondingly their economic characteristics.
In order to analyze economic activity, determine deposit develop-
ment efficiency, and ascertain basic directions for the improve-
ment of economic indicators it is necessary to define costs for
each deposit under examination. Such studies are heing made by
workers at scientific research organizations or gas extracting
enterprises. However, the methodology for allocating costs has
not yet been developed and studies use different methods for
allocating overall costs between individual deposits. A s~impli- -
fied method for determining costs for individual deposits is
suggested.
In accordance with existing instructions, the planning, account-
ing and calculation of gas and condensate extraction pr~me costs
is carried out by the following computational class of
expenditure:
Auxiliary materials (reagents)
Basic, sup~lementary wages and deductions for social -
of productive workers;
57
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~ou o~~rr.rnr. us~ orr~Y
~xpendi.tures tor production prep~ratzon and development;
Well umortization;
~xpenditures for the maintenance and operata.on of field equipment;
~xpenditures for preparing (compressing) gas;
~xpenditures ~'or the intr field ~ransport~tion of condensate;
Shop expenditures;
General field expenditures; -
Other field expenditures; _
Non-production expenditures.
5ome of these c~~sses - wages, amortization of wells, costs of
as preparatinn - can be c~lculated directly for each deposit.
~xpenditures for aux.iliary materials can also be determined hy
calculation: by mu?tiplying the quantity of gas extracted at
deposits ttnd the relative expenditur~ of ~uxiliary materials.
~xpenditures for intrafield transportation of conde;~sate are also
calculated dire~tly if they are spent ior one field. If, however,
condensate transportation is for a group of deposits, costs
- for individual deposits are determined proportionally to the
amount of condensate trans~orte~. In calculating gas extraction
prime cost, well amortization has its own section. The amort-
ization of other fixed capital is included under the expend-
itures for maintenance and operation of field equipment, and
under shop and general field expenditures. However, in the
"Estimate of production costs", the total sum of amortization
is calculated. By suLtracting well amortization from it one can
determine the amortizaxion of other fixed capital for GPi1.
The resulting figure is broken down into individual deposits
proportionally to the value of fixed capital (without wells) of
each deposit.
Expenditures for all other classes of costs - shop, general
field, for the maintenance a~nd operation of field equipment (minus =
um~rtization) are ~11 comprehensive. They should be distributed
among individual deposits. The magnitude of these costs depenc~s
upon a number of factors, however, the most important are the
number of. operating wells and the volume of gas produced. To
determine these expenditures for individual deposits the following
formula can be used: pi Qi
+
Ko a P 9
2
Where:
Ko - Is a coefficient reflecting thesshare of wells and
gas extraction of individual deposits in the
total amount of wells and gas extraction in the
_ administration, in shares of units
p~ and P - Operating wells by deposit and administration
qi and q - Gas and econdensate extraction by deposit and GPU
58
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~ox or~icr~v~ us~ ornY
Table 1 presents the calCUlntion o~ gas extraction prime costs
for the Kuban'gazprom AssoCi~tion and indivi.dual gas �ield
administrat3ons~ Table 2 gives the structure of operating expend-
itures calculated according to the suggested classification~
Table 1. Cal~ulation of the prime Cost of Gas and Condensate
by Administration of the Kuban'g~zprom Association
for 1976
Cr~rba aarper ~ OO~e1tr- ~ ~ w Hc :
H@HB8 `~CHO- K8N@BQROA 1I0IIXOQCl~Oe
~ 1) ( 2) Ay~r 3 5~JCrr
(6) &mowores N?e waTepNenr
(peareNr~~ 440 148 I69 I29
OCIIOBHBR M A01101Wp4@1IbH8R ' ~ ~
~ ~ ~ 86Q8b~fN6A t1A8T8. ~Q~H3B4114T- '
DA9flFL( p8609NJf~ B1f11nH8H Ot- ,
VMQd@Naft H8 COt1118116H0A ^.TQA-
xoeaNae 1I65 266 683 2I6
Pecxo~ He n atroroeKy N oo-
(8 ) Hoeaae npo~aeato:ea 23 ' 8 8 7 _
( 9) AMOptaaaw~a c~ee~KN IIAI3 5684 '~OCi ~ 2826
P8CX4QY HB COAOQiEHNA / '
' ~ 1 ~ ~KCQJ[y3Telj[D OQOMW.7t~BOfO ~ ~
oaopyAoeanan Y1408 3558 ' 62I0 I6~0 ~
( ~o~zc~a Na aHyrprnpoKaczo- �
`11' `8k1p Tp6qC00pT KOli,Q9HC8T8 j:2 - !~J ' 47 `
12 ~Obwenpow~~~~e peczqtW , 40~16 I59I I654 - d0I
~Z ~~Qpoaae npcwtiQaaeue peoxqtr? 29 d 7 4
TO t A 1 ~9046 I I26a 22II9 566~
Note: Pri e cost calculated without compensating for ~RR
Key: cos~s.
1. Class of cost 11. Expenditures~for
2. Association intrafield transport-
3. Krasnodarskoye ation of condensate
4. Kanevskoye GPti -
5. Maykopskoye 12, General field expend-
itures
6. Auxiliary materials 13. Other f.ield expend- -
_ (reagents) itures
7. $asic and supplementary
wages of production workers
including deductions for
social insurance
8. Expenditures for production -
- preparation and development
9. Well amortization -
10. Expenditures for the maintenance
and operation of field equipment -
59
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'Cab1~ 2. ~reakdown of ~perxting Expenditures for Gas ~xtract-
ion Followa,ng Recommended Methodology (Percent of
Tot~~.1)
A ministration
~lass of rasno ar- ~nevs oye May ops oye
~xpenditi~re skoye UDTG (;pU tiDTG
~
Auxili~ry -
materials
(reagents) 1,3 1.4 2.2
Basic and supplem-
entary wages o� pro-
duction workers,
including dedu~tions
for social insu rance 2.4 5.6 3,g
Well amortization 50.5 2~.3 4g,g
Amortization of
ather fixed capital 16,9 2g,g 21.2
Other expenditures 28.9 35.9 22.g
Total 100.0 100.0 100.0 ~
_ As can be seen from tables 1 and 2 the prime cost structure
is dominated by expenditures for well amortization, maintenance
and operation of field equipment (the latter section includes
expenditures for installing low temperature separation equipment
and gas collection networks), Outlays for these two classes
amount to about 80 percent of operating expenses.
Using this methodology, calculations ?vere made of gas extract-
ion prime costs in the largest deposits in the Kuban'gazprom
Association (Table 3)
It is obvious from Table 3 that gas extraction prime costs for
individual deposits differ significantly from the average for
the GPIJ. Thus, gas Pxtraction prime cost at the Starominskoye
deposit, was 3.3 fold and for the Len~ngradskoye 4.6 fold higher
than the average.prime cost.for the Kanevskoye GPU, while at
the Kanevskoye and Kushchevskoye deposits the figures were -
1.8 - 1.9 fold lower.
Thus, the sugRested method for allocating onerating expenditures
permits calculating costs for the development of individual
deposits and determining the economic economic efficiency, as
well as setting the most important directions for the improve-
ment of gas field administration management activity.
60
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Table 3~ C.alculation of the Prime Cost of Gtts f,xtraction
for the Kuhan'gazpromi Association in 1976, -
Thousands of Rubles,
ke.ro~or.aenNa no ynpan- 1'anoguo a oay, e ~ Ccoecra
aeue~w ~kcanyaTe- Nu~:rb
BCt10N0I'8~ 8Ape00iH8A EMOp?038- aNOpraaa7 ~pOVY@ ~
LINOHlfd_B'.~ ~~y~
~ (1~~O~W; ~ T@1tbNNe f1118TA pNll CR86- ua~ npo ~aTpaiw caaa
~ ~ ~C@CO 2 ~ Ye'j0f,1NeJW ~ ~ ~ ~ ~~1 qltY OCN00- ~ ~ ~ py~~f ooaa
( 4 G~ N Wt t~0lt40B
~ 1 O~;~p8B0/tOQ 17Dr ~ anero I2II9 I69 663 :~UO ~625 4; 39 5.27
e ro~ aacne ao Meero-
~ 11) po~teu~uw: ,
( 1 2~ naaeaoaoe 2548 66 I38 646 a30.0 I26~ I.80
13 neeKarpettoroe I328 4 I25 ',,'S 443.0 2xI I.i.U6
1 4 qea0ncc?coe .~~3 y P9 345 239 i9i 4.60
15 "�rep~~toroe I428 6 97 680 422 223 I0.79
(16 ) Kywe~c~oe ~ I4I9 ~~7 H2 ~u3 328 668 I?75 -
7~ HpY1(OBClf08 IQ99 35 I12 622 GW7 353 2~5�
~ 1 g~E(pa:noaapcrtoe Y,~TC,noero II263 I48 266 5684 I�00 3~6b I0.02
~19~ 8 T~N qH01IB no wecro- ,
poa~tae~w: -
- ( 2 p~"cepeaoHOxoe a2d4 46 9I I475 57I I06I ~.36 ~
21 Cepa.acoeoxoe 80I II ' . 20 , a79 I0~7 304 �.47
Hexpeconckoe 263I � d8 ~7 I250 434 eI2 7.I7~
Z aqKOncKOe YATI'~ Bcero 5664 I~ , 2I6 1826 II97 230~ I3.I0
~ 2 4~ 8 TOY a4cne ao t'agROn-
cROMy wecropoxuenna 434I II3 I84 2065 y25 II~4 I0,9I
T 0 t a 1Hroro 29046 430 1I~i II8I3 o:,,i0 d738 ~.37 _
.
x) Inclucles expenditures for gas and condensate
extraction
Key:
1. Deposit (by 12. Kanevskoye
administration) 13. Leningradskoye
2. Annual operat~ng 14. Chelbasskoye
expendituresx 15. Starominskoye
total 16. Kushchevskoye
3. Including 17. Krylovskoye -
4. Auxiliary materials 18. Krasnodarskoye UDTG, total
5. Wages 19. IncludinA the following
6. tiVell amor*.,ization deposits
7. Amortization of o ther 20. Berezanskoye
fixed capital 21. Serdyukovskoye
8. Other costs 22. N~krasovskoye -
9. Prime cost of gas 23. Maykopskoye UDTG, total -
. extraction, rubles 24. Including the Maykopskoye
per 1,000 m3 deposit
10. Kanevskoye GPU total -
11. Including the following
deposits
COPYRIGHT: VNIIEgazprom, 1979
11574 ~
CSO: 1822 END
61
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