RU2528689C1 - Gas separation - Google Patents

Gas separation Download PDF

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RU2528689C1
RU2528689C1 RU2013120874/05A RU2013120874A RU2528689C1 RU 2528689 C1 RU2528689 C1 RU 2528689C1 RU 2013120874/05 A RU2013120874/05 A RU 2013120874/05A RU 2013120874 A RU2013120874 A RU 2013120874A RU 2528689 C1 RU2528689 C1 RU 2528689C1
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Russia
Prior art keywords
absorber
bottom
top
fed
absorbent
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RU2013120874/05A
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Russian (ru)
Inventor
Александр Ильич Быстров
Вячеслав Николаевич Деменков
Ильдар Рашидович Хайрудинов
Урал Булатович Имашев
Original Assignee
Государственное унитарное предприятие "Институт нефтехимпереработки Республики Башкортостан" (ГУП ИНХП РБ)
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Priority to RU2013120874/05A priority Critical patent/RU2528689C1/en
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Abstract

FIELD: oil-and-gas industry.
SUBSTANCE: proposed process includes gas feed to absorber. Cooled absorbent is fed to absorber top, dry gas being diverted therefrom and saturated absorbent being discharged from absorber bottom to rectifier tower. Propane-butane fraction is diverted the rectifier top and used as reflux. Gas gasoline is diverted is off-stream via evaporation section while absorbent is discharged from rectifier bottom. After cooling, said absorbent is fed to absorber top and, then, heat is fed to its bottom, rectifier bottom and heat evaporation section bottom. Fluid at absorber lower trays is heated by rectifier column residue preheated in boiler and fed to absorber bottom.
EFFECT: power savings.
2 dwg, 2 tbl

Description

The invention relates to methods of gas separation and can be used in the oil refining and gas processing industries.

A known method of gas separation in two distillation columns (I. A. Alexandrov. "Distillation and distillation in oil refining." M: Chemistry, 1981, p. 283, Fig. V-10a).

The disadvantage of this method is the use of artificial cold as a refrigerant.

The closest to the proposed invention in terms of technical essence and the achieved effect is a gas separation method, comprising introducing gas into the absorber, to the top of which a cooled absorbent is fed, taking dry absorber from the top of the absorber and withdrawing the saturated absorbent from the bottom of the absorber to the distillation column, from the top of which the propane-butane fraction, which is also used as a reflux, is taken, gasoline is removed through a stripping section through the stripping section, and absorbent is removed from the bottom of the column, which after cooling return to the top of the absorber, with the bottom of the absorber, distillation column and stripping section of heat (A.M. Churakaev. "Processing of petroleum gases." M .: Nedra, 1983, p. 116, Fig. 33).

The disadvantage of this method is the high energy consumption in connection with a significant supply of heat to the bottom of the absorber.

The objective of the present invention is to reduce energy consumption.

This problem is solved by the fact that in the method of gas separation, which includes introducing gas into the absorber, to the top of which a cooled absorbent is fed, taking dry absorber from the top of the absorber and transferring the saturated absorbent from the bottom of the absorber to a distillation column, from the top of which a propane-butane fraction is taken , which is also used as a phlegm, gasoline is removed through a stripping section through a stripping section and an absorbent is removed from the bottom of the column, which, after cooling, is returned to the top of the absorber, with rectifier fed to the bottom of the absorber of the column and the stripping section of heat, according to the invention, the liquid from the lower plates of the absorber is heated by the remainder of the distillation column, previously heated in a boiler, and fed to the bottom of the absorber.

By heating the liquid from the lower plates of the absorber with the remainder of the distillation column and supplying the bottom of the absorber, it is possible to reduce the amount of heat supplied to the bottom of the absorber, and this solution allows to reduce energy consumption.

Figure 1 presents a diagram of an implementation of the proposed method according to option 1.

The heated feed gas is fed through line 1 to the absorber 2. Dry gas is removed from the top of the absorber 2 via line 3. To the top of the absorber 2, line 4 serves the absorbent cooled in the refrigerator 5. Liquid is drawn off from the absorber 2 through line 6, heated in the heat exchanger 7 with a hot absorbent supplied through line 8, and through line 9 is introduced into the cube of the absorber 2. The remainder of the absorber 2 through line 10 is fed into the boiler 11. Vapors from the top of the boiler 11 through line 12 return to the bottom of the absorber 2. The liquid from the bottom of the boiler 11 via line 13 is fed to the distillation column 14. Vapors from the top of the distillation column 14 are condensed in the condenser 15 and fed through the line 16 to the reflux tank 17. Liquid is taken from the bottom of the reflux tank 17 and 18 return for irrigation re casing column 14. The balance excess of the fraction C 3 -C 4 along line 19 is removed from the installation. A side stream is taken from the distillation column 14 along line 20 and fed to the top of the stripping section 21. Vapors from the top of stripping section 21 are returned to line 14 through line 22. The liquid from the bottom of stripping section 21 is fed into boiler 24 through line 23. Vapors from the top the boiler 24 via line 25 is returned to the bottom of the stripping section 21. The liquid from the bottom of the boiler 24 via line 26 is withdrawn as gas gasoline. The liquid from the bottom of the distillation column 14 via line 27 is fed into the boiler 28. The vapor from the top of the boiler 28 via line 29 is returned to the bottom of the distillation column 14. The liquid from the bottom of the boiler 28 via line 8 is fed to the heat exchanger 7, and then fed to the refrigerator through line 30 5. There, fresh absorbent is supplied via line 31.

Option 2 of the circuit of the proposed method, presented in figure 2, differs from option 1 by supplying liquid from the bottom of the boiler 28 via line 8 to the heat exchanger plates of the absorber 2, outputting it via line 9 and feeding it to the heat exchanger 7 to heat the feed gas supplied to a heat exchanger 7 along line 1 and introduced after heating through line 6 into column 2.

Comparative performance indicators of gas separation schemes for the prototype and the proposed method are shown in the attached tables.

As can be seen from table 1, the proposed method in comparison with the prototype allows to reduce the total heat input from the outside from 6.60 to 4.26-4.30 Gcal / h, that is, 1.54 times, the total heat removal from the outside from 6.719 to 3.961 -4.369 Gcal / h, i.e. 1.54-1.70 times.

Thus, the present invention allows to reduce energy consumption.

Table 1 Key performance indicators of the columns Indicators Option 0 (prototype) Option 1 (the proposed method) Option 2 proposed method) one 2 3 four Consumption, t / h - feed gas 7.60 7.60 7.60 - absorbent 35.00 35.00 35.00 - dry gas 3.46 3.46 3.46 - fr. C 3 -C 4 2.73 2.73 2.73 - gas gasoline 1.41 1.41 1.38 - the remainder of K-2 from T-4 35.00 35.00 35.03 - vapor from the top K-1 3.46 3.46 3.46 - irrigation K-1 35.00 35.00 35.00 - liquids from the bottom K-1 56.64 54.76 42.30 - bottom fluid T-1 39.14 42.41 47.53 - vapors from T-1 17.50 12.35 3.21 - liquids from the bottom of T-2 - 39.14 39.14 - vapors from T-2 - 3.27 3.16 - bottom fluid T-3 - - 42.30 - vapors from T-3 - - 5.24 - vapor to the bottom K-1 17.50 15.62 3.16 - power K-2 39.14 39.14 39.14 - vapor from the top K-2 31.18 31.18 31.17 - acute irrigation K-2 28.45 28.45 28.44 - side shoulder strap in K-3 3.62 3.62 3.62 - vapor from the top K-3 2.21 2.21 2.24 - liquids from the bottom K-3 to T-5 4.44 4.44 4.42 - vapor to the bottom K-3 3.03 3.03 3.04 - liquids from the bottom K-2 to T-4 89.53 89.53 89.54 - vapor to the bottom K-2 54.53 54.53 54.51 Temperature ° C - input of raw gas 40 40 one hundred - input absorbent thirty thirty thirty - input irrigation K-1 thirty thirty thirty - top K-1 34 34 34 - bottom K-1 118 107 164 - in T-1 186 164 126 - in T-2 - 187 186 - in T-3 - - 164 - input irrigation in K-2 40 40 40 - top K-2 51 51 51

- output side shoulder strap in K-3 99 99 one hundred - bottom K-2 241 241 241 - in T-4 246 246 246 - top K-3 105 105 106 - bottom K-3 147 147 147 - in T-5 157 157 156 - absorbent from T-1 210 135 150 - absorbent from T-3 - - 190 Pressure, ata - top K-1 14.00 14.00 14.00 - bottom K-1 14.46 14.46 14.46 - in T-1 14.56 14.56 14.43 - in T-2 - 14.66 14.66 - in T-3 - - 14.45 - in E-2 10.80 10.80 10.80 - top K-2 11.00 11.00 11.00 - bottom K-2 11.60 11.60 11.60 - in T-4 11.90 11.90 11.90 - top K-3 11.38 11.38 11.38 - bottom K-3 11.57 11.57 11.57 - in T-5 11.88 11.88 11.88 Heat, Gcal / h - introduced with raw gas - administered with absorbent 0.699 0.699 1.005 - allocated to X-1 0.493 0.493 0.493 - brought in T-1 4,336 1,986 1,578 - brought in T-2 3,300 2,530 0.886 - brought in T-3 - 0,800 0.760 - allocated to X-2 - - 1,348 - brought in T-4 2,383 2,383 2,383 - brought in T-5 3,300 3,300 3,300 - the total supply of heat from the outside to T-1 (prototype), T-2, T-4, T-5 (options 1 and 2) 0,200 0,200 0,200 - total heat removal from the outside in X-1 and X-2 6,600 4,300 4,260 6,719 4,369 3,961 The number of theoretical plates (double-drain valve) - in 1 section K-1 - in 2 (distant) section K-1 fourteen fourteen fourteen - in 1 section K-2 7 7 7 - in 2 sections K-2 7 7 7 - in 3 (distant) section K-2 9 9 9 - in K-3 9 9 9

fourteen fourteen fourteen Diameter m - K-1 1,2 1,2 1,0 - K-2 2.0 2.0 2.0 - K-3 0.6 0.6 0.6 The distance between the plates, mm - in K-1 400 400 400 - in K-2 400 400 400 - in K-3 300 300 300 Linear / maximum permissible steam speed, m / s - in K-1 - in K-2 0.10-0.18 / 0.26-0.41 0.10-0.18 / 0.26-0.41 0.14-0.24 / 0.24-0.41 - in K-3 0.12-0.19 / 0.21-0.26 0.12-0.19 / 0.21-0.26 0.12-0.19 / 0.21-0.26 0.12-0.15 / 0.15-0.17 0.12-0.15 / 0.15-0.17 0.12-0.15 / 0.15-0.17 Drain head height, mm - in K-1 28-41 28-41 31-44 - in K-2 17-43 17-43 19-43 - in K-3 12-13 12-13 12-13 Content,% mass. - C 3 in dry gas 0.12 0.10 0.20 - absorbent in dry gas 3.31 3.31 3.30 - C 2 in French C 3 -C 4 0.29 0.29 0.29 - C 5 in French C 3 -C 4 0.09 0.09 0.11 - C 4 in gasoline 0.09 0.09 0.06 - fr. > 110 ° C in gasoline 2.92 2.92 2.64 - fr. up to 100 ° C in residue K-2 2.02 2.02 2.08

table 2 The composition of the raw materials and separation products of the columns,% of the mass. Components and fractions, ° C Feed gas Absorbent Dry gas (option 0) Fr. C 3 -C 4 options 0 and 1) Gas gasoline (options 0 and 1) Residue K-2 (options 0 and 1) Dry gas (option 1) Dry gas (option 2) Fr. C 3 -C 4 (option 2) Gas gasoline (option 2) The remainder of K-2 (option 2) C 1 27.42 - 60.21 - - - 60.27 60.17 - - - C 2 16.63 - 36.36 0.29 - - 36.32 36.32 0.29 - - C 3 21.73 - 0.12 60.22 - - 0.10 0.20 60.22 - - iC 4 4.14 - - 11.47 - - - - 11.47 - - nC 4 10.04 - - 27.93 0.09 - - - 27.91 0.06 - iC 5 2.21 - - 0.08 11.76 - - - 0.10 12.05 - nC 5 2.67 - - 0.01 14.38 - - - 0.01 14.71 - 40-50 1.00 - - - 5.25 - - - - 5.37 - 50-60 1.77 0.01 - - 9.58 0.01 - - - 9.80 0.01 60-70 2.00 0.04 0.01 - 11.11 0.02 0.01 0.01 - 11.35 0.02 70-80 2.00 0.14 0,03 - 12,20 0.08 0,03 0,03 - 12.40 0.08 80-90 2.00 0.48 0,07 - 14.02 0.34 0,07 0,07 - 13.97 0.36 90-100 3.28 1.41 0.16 - 13,20 1,57 0.16 0.16 - 12.60 1,61 100-110 1.00 4.04 0.32 - 5.49 4.00 0.32 0.32 - 5.05 4.02 110-120 1.00 10.88 0.62 - 2.18 10.95 0.62 0.62 - 1.97 10.95 120-130 1,08 24.04 0.93 - 0.65 24.16 0.93 0.93 - 0.59 24.14 130-140 0.01 26.56 0.69 - 0.08 26.52 0.69 0.69 - 0,07 26.49 140-150 0.01 20.97 0.36 - 0.01 20.93 0.36 0.36 - 0.01 20.91 150-160 0.01 8.99 0.10 - - 8.98 0.10 0.10 - - 8.97 160-170 - 1.99 0.02 - - 1.99 0.02 0.02 - - 1.99 170-180 - 0.38 - - - 0.38 - - - - 0.38 180-190 - 0.06 - - - 0.06 - - - - 0.06 190-200 - 0.01 - - - 0.01 - - - - 0.01 Z 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00

Claims (1)

  1. A method of gas separation, which includes introducing gas into the absorber, on top of which a cooled absorbent is fed, taking dry gas from the top of the absorber and withdrawing the saturated absorbent from the bottom of the absorber to a distillation column, from the top of which a propane-butane fraction is taken, which is also used as a reflux gas gas is withdrawn through a stripping section through a stripping section and an absorbent is removed from the bottom of the column, which, after cooling, is returned to the top of the absorber, with the absorber, distillation column and stripping section being fed to the bottom la, characterized in that the liquid from the lower plates of the absorber is heated by the remainder of the distillation column, previously heated in a boiler, and fed to the bottom of the absorber.
RU2013120874/05A 2013-05-06 2013-05-06 Gas separation RU2528689C1 (en)

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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SU939896A1 (en) * 1980-07-01 1982-06-30 Всесоюзный Научно-Исследовательский И Проектный Институт По Переработке Газа Method of separating hydrocarbon gaseous mixtures
WO2003100334A1 (en) * 2002-05-20 2003-12-04 Fluor Corporation Twin reflux process and configurations for improved natural gas liquids recovery
EA006872B1 (en) * 2002-05-08 2006-04-28 Флуор Корпорейшн Installation and method for isolating natural gasoline using absorption reflux process supercooled
RU2479620C1 (en) * 2012-04-10 2013-04-20 Общество с ограниченной ответственностью "Инжиниринговый центр" Method of gas separation during catalytic cracking of petroleum direction

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SU939896A1 (en) * 1980-07-01 1982-06-30 Всесоюзный Научно-Исследовательский И Проектный Институт По Переработке Газа Method of separating hydrocarbon gaseous mixtures
EA006872B1 (en) * 2002-05-08 2006-04-28 Флуор Корпорейшн Installation and method for isolating natural gasoline using absorption reflux process supercooled
WO2003100334A1 (en) * 2002-05-20 2003-12-04 Fluor Corporation Twin reflux process and configurations for improved natural gas liquids recovery
RU2479620C1 (en) * 2012-04-10 2013-04-20 Общество с ограниченной ответственностью "Инжиниринговый центр" Method of gas separation during catalytic cracking of petroleum direction

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
ЧУРАКАЕВ А.М., Переработка нефтяных газов, Москва, Недра, 1983, с.116-118. *

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Effective date: 20180507