CN1092696A - Device with membrane separation technique recover hydrogen from catalysis drying gas - Google Patents
Device with membrane separation technique recover hydrogen from catalysis drying gas Download PDFInfo
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- CN1092696A CN1092696A CN 93103019 CN93103019A CN1092696A CN 1092696 A CN1092696 A CN 1092696A CN 93103019 CN93103019 CN 93103019 CN 93103019 A CN93103019 A CN 93103019A CN 1092696 A CN1092696 A CN 1092696A
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- gas
- hydrogen
- pressure
- membrane separator
- water cooler
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- Separation Using Semi-Permeable Membranes (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The invention provides a kind of device with membrane separation technique recover hydrogen from catalysis drying gas.This device adopts and boosts, after the cooling, separatory demist, heating, carrying out gas-gas with film separates, the hydrogen-rich gas that comes out from one-level membrane separator infiltrating gas side again through supercooling, cushion, boost, cooling, separatory demist, heating, carry out gas-gas with film again and isolate high concentration hydrogen, and by deoxidation, divide water just can obtain concentration to reach 97% (V), yield reaches 92% hydrogen product, this technological process is simple, easy to operate, be suitable for the hydrogeneous hydrogen product that in the catalysis drying gas of 30～70% (V), reclaims high concentration.
Description
The invention belongs to the petroleum refining process process, refer more particularly to the catalysis drying gas after catalytic unit and corollary apparatus thereof are handled, utilize the process unit of membrane separation technique recover hydrogen.
Well-known continuous development along with the thin film fabrication technology, the field of reclaiming light component or hydrogen with membrane separating method from refinery's gas constantly enlarges in the world, for example United States Patent (USP) (US4892564) discloses a kind of " being used to reclaim the membrane process of liquid hydrocarbon " and sees accompanying drawing 2, its goal of the invention is in order to reclaim liquid hydrocarbon, and the after-treatment system-cryogenic separation part of replacement oleflex technology, its unstripped gas is the gas after the catalytic dehydrogenation (oleflex), the employing unstripped gas boosts, cooling, isolate a part of liquid hydrocarbon after the heat exchange, carry out gas-gas with film again and separate, with light component (H
2, CH
4) permeate away after, fixed gas enters membrane separator and penetrates light component (H
2, CH
4), tail gas cools off separatory again and obtains liquid hydrocarbon, and this process is constantly carried out, and is the purpose product until reaching the recovery liquid hydrocarbon, and this patent is a Computer simulation results, does not carry out industrial lab scale and amplification.
French Patent (FRP) FR2636249 separates film, and transformation absorption and cryogenic separation triplicity are got up, and in order to the technical process of recover hydrogen, liquid hydrocarbon and fuel gas, this patent complex technical process relates to three kinds of separation processes of gas.European patent EP 0445041A1 is that a kind of film separates the patent that combines with cryogenic separation, is used for reclaiming the technology of liquid hydrocarbon, hydrogen and fuel gas, and this patent complex technical process also needs refrigeration plant.
It is simple to the purpose of this invention is to provide a kind of technological process, and operating condition is convenient, is suitable for reclaiming high yield, the process unit of high concentration hydrogen from the catalysis drying gas after existing catalytic unit of oil plant and the corollary apparatus processing thereof.
Accompanying drawing and being described as follows:
Accompanying drawing 1 is apparatus of the present invention process flow diagrams
Explanation in the accompanying drawing 1:
1a-unstripped gas surge tank A unstripped gas
2a-feed gas compressor B product hydrogen
3a-unstripped gas water cooler
4a-unstripped gas separatory demist jar
5a-unstripped gas heater
6a-one-level membrane separator
7a-hydrogen-rich gas (one-level infiltration gas) water cooler
8a-hydrogen-rich gas surge tank
9a-hydrogen-rich gas compressor
10a-hydrogen-rich gas water cooler
11a-hydrogen-rich gas separatory demist jar
12a-hydrogen-rich gas heater
13a-secondary membrane separator
The 14a-degasifier
The 15a-water cooler
Explanation in the accompanying drawing 2:
One section compressor of 1-
One section compressor outlet air cooler of 3-
One section compressor outlet water cooler of 5-
One section compressor outlet of 7-divides flow container
Two sections compressors of 9-go out
Two sections compressor outlet air coolers of 11-
Two sections compressor outlet water coolers of 13-
Two sections compressor outlets of 15-divide flow container
The 17-heat exchanger
The 19-cooler
21-divides flow container
The 23-membrane separator
The 25-water cooler
27-divides flow container
The 29-heat exchanger
The 31-cooler
33-divides flow container
The 35-membrane separator
The 37-water cooler
The 39-heat exchanger
The 41-cooler
43-divides flow container
The 45-heater
The 47-membrane separator
The 49-water cooler
The 51-cooler
53-divides flow container
55-divides flow container
The 57-fractionating column
Process unit of the present invention is seen accompanying drawing 1, be suitable for through absorbing stable, after the desulfurization, hydrogeneous at 30～70%(V) catalysis drying gas, its pressure is 0.5～1.8MPa(a) to enter surge tank (1a) as unstripped gas (A), in surge tank, remove the liquid that carries in the unstripped gas, and unstripped gas (A) played cushioning effect, through buffering, catalysis drying gas behind the separatory is boosted by feed gas compressor (2a), rise to outlet pressure 2.0～7.0MPa(a) by inlet pressure 0.5～1.8MPa(a), enter again water cooler (3a), water cooler (3a) operating pressure 2.0～7.0MPa(a), temperature is 30～50 ℃, enter separatory demist tank (4a) and remove droplet in the liquids and gases that condensation gets off, prevent that liquid from sticking on the film surface, unstripped gas is heated to 45～100 ℃ and enters one-level membrane separator (6a) in heater (5a), (6a) formed by a plurality of membrane separators, the osmotic pressure of enrichment hydrogen is 0.4～1.5MPa(a) hydrogen-rich gas, earlier be cooled to below 40 ℃ and behind a minute flow container (8a) separatory through water cooler (7a), enter into rich hydrogen compressor (9a), its inlet pressure is 0.4～1.5MPa(a), outlet pressure is 2.3～7.3MPa(a), enter water cooler (10a), operating pressure is 2.3～7.3MPa(a), and temperature is 30～50 ℃. To separatory demist tank (11a) separatory, be heated to 45～100 ℃ by heater (12a) again, enter the secondary membrane separator (13a) that is formed by a plurality of membrane separators, its inlet pressure is 2.3～7.3MPa(a), 45～100 ℃ of inlet temperatures, the pressure that obtains from the infiltrating gas side of secondary membrane separator is 0.1～1.5MPa(a) infiltration gas, pass through earlier degasifier (14a), after passing through again water cooler (15a) branch water, be concentrate hydrogen product (B), its concentration reaches 97%(V), yield reaches 92%(V), can directly deliver to hydrogenation plant and use.
Higher from the tail gas hydrogen concentration that secondary membrane separator (13a) is discharged, in order to improve the rate of recovery of device hydrogen, this tail gas is turned back to the front of raw material pretreatment portion water cooler (3a), the gas of discharging with feed gas compressor (2a) mixes; The tail gas that primary separator (6a) is discharged, pressure is 2.0～7.0MPa(a), and the concentration of hydrogen is very low, and the gas that acts as a fuel goes out device, also can be with and press absorption or deep cooling to obtain products such as liquefied gas, ethene.
Good effect of the present invention is to use simple process flow, can reclaim the hydrogen of high concentration, high yield under operating condition easily from catalysis drying gas.
Embodiment 1
Disposal ability is 10000Nm
3The catalysis drying gas recover hydrogen device of/hr, the access to plant raw gas pressure is 0.88MPa(a), 40 ℃ of temperature, its dry gas is composed as follows:
Gas title H
2N
2O
2CH
4C
2H
6C
2H
4C
3H
8
Content %(V) 59.58 11.17 0.91 7.64 6.37 9.24 0.18
Gas title C
3H
6C
4H
10C
4H
8C
+ 5CO
2CO H
2S adds up to
Content %(V) 0.70 1.62 2.12 0.47---100%
Above-mentioned catalysis drying gas adopts the present invention to see the technological process of accompanying drawing 1, and its main operating condition is as follows:
Feed gas compressor (2a) inlet pressure 0.88MPa(a), outlet pressure 6.2MPa(a), the outlet pressure 6.1MPa(a of water cooler (3a)), 40 ℃ of outlet temperatures, one-level membrane separator (6a) amounts to 14 Dg200(area 5600m
2) silicon rubber-polysulfones asymmetric compound hollow-fibre membrane, its inlet pressure 6.0MPa(a), 60 ℃ of inlet temperatures, infiltration gas (hydrogen-rich gas) pressure 0.8MPa(a), rich hydrogen compressor (9a) inlet pressure 0.75MPa(a), outlet pressure 6.5MPa(a), water cooler (10a) outlet pressure 6.4MPa(a), 40 ℃ of outlet temperatures, secondary membrane separator (13a) amounts to 4 Dg200(area 1600m
2) silicon rubber-polysulfones asymmetric compound hollow-fibre membrane, inlet pressure 6.3MPa(a), 60 ℃ of inlet temperatures, infiltration gas (hydrogen) pressure 1.3MPa(a), degasifier (14a) inlet pressure 1.3MPa(a), 50 ℃ of inlet temperatures, it is composed as follows to handle the resulting hydrogen in back through this device:
Gas title H
2N
2O
2CH
4C
2H
6
Content % (V) 97.0000 0.0345 0.1ppm 2.9396 0.0096
Gas title C
2H
4C
3H
8C
3H
6C
4H
10C
4H
8C
+ 5
Content % (V) 0.0095 0.0002 0.0009 0.0034 0.0041 0.0021
Add up to 100.0000
Hydrogen recovery rate is 92%, and the product density of hydrogen is 97%.
Claims (2)
1, a kind of device with membrane separation technique recover hydrogen from catalysis drying gas, it is characterized in that through absorbing stable, catalysis drying gas after the gas sweetening is as unstripped gas (A) process surge tank (1a), entering feed gas compressor (2a) boosts, after water cooler (3a) cooling, enter separatory demist jar (4a) again, after heater (5a) heating, enter one-level membrane separator (6a) and carry out gas-gas separation, the hydrogen-rich gas that comes out from one-level membrane separator (6a) infiltrating gas side enters surge tank (8a) after water cooler (7a) cooling, extremely rich hydrogen compressor (9a) boosts again, water cooler (10a) cooling, after separatory demist jar (11a) and heater (12a) heating, enter into secondary membrane separator (13a) and carry out gas-gas separation, from the high concentration hydrogen elder generation process degasifier (14a) that secondary membrane separator (13a) infiltrating gas side comes out, after passing through water cooler (15a) branch water again, just can obtain concentration and reach 97% (V), yield reaches 92% hydrogen (B) and goes out device as product.
2, according to claim 1 with membrane separation technique recover hydrogen device from catalysis drying gas, the process condition that it is characterized in that this device is: the inlet pressure of feed gas compressor (2a) is 0.5～1.8MPa(a), and outlet pressure is 2.0～7.0MPa(a); The inlet pressure of one-level membrane separator (6a) is 2.0～7.0MPa(a), and inlet temperature is 45～100 ℃, and the infiltration atmospheric pressure is 0.4～1.5MPa(a); The inlet pressure of rich hydrogen compressor (9a) is 0.4～1.5MPa(a), and outlet pressure is 2.3～7.3MPa(a); The inlet pressure of secondary membrane separator (13a) is 2.3～7.3MPa(a), and inlet temperature is 45～100 ℃, and the infiltration atmospheric pressure is 0.1～1.5MPa(a); Tail gas pressure is 2.0～7.0MPa(a).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 93103019 CN1030821C (en) | 1993-03-24 | 1993-03-24 | Apparatus for recovering hydrogen from catalytic dry gas by membrane separation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 93103019 CN1030821C (en) | 1993-03-24 | 1993-03-24 | Apparatus for recovering hydrogen from catalytic dry gas by membrane separation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1092696A true CN1092696A (en) | 1994-09-28 |
| CN1030821C CN1030821C (en) | 1996-01-31 |
Family
ID=4984434
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 93103019 Expired - Lifetime CN1030821C (en) | 1993-03-24 | 1993-03-24 | Apparatus for recovering hydrogen from catalytic dry gas by membrane separation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1030821C (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1095440C (en) * | 1998-02-12 | 2002-12-04 | 中国科学院大连化学物理研究所 | Hydrogen-making process of dry-gas selective catalyst oxidation for oil refinery |
| CN101757830A (en) * | 2010-01-18 | 2010-06-30 | 党延斋 | Method for recovering C2 and C3 components and hydrogen from refinery dry gas |
| CN102718185A (en) * | 2012-07-20 | 2012-10-10 | 河南科技大学 | Separation device and separation method of hydrogen gas in hydrogen production through fermentation |
| CN104031684A (en) * | 2014-05-23 | 2014-09-10 | 四川天采科技有限责任公司 | Method for recovering ethylene and hydrogen from refinery dry gases by combining cold oil absorption and membrane separation |
| CN104071749A (en) * | 2014-07-16 | 2014-10-01 | 北京燕华工程建设有限公司 | Method for using dry gas to separate hydrogen as well as system |
| CN111467913A (en) * | 2020-03-27 | 2020-07-31 | 大连海奥膜技术有限公司 | Comprehensive recycling process and equipment for refinery tail gas |
-
1993
- 1993-03-24 CN CN 93103019 patent/CN1030821C/en not_active Expired - Lifetime
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1095440C (en) * | 1998-02-12 | 2002-12-04 | 中国科学院大连化学物理研究所 | Hydrogen-making process of dry-gas selective catalyst oxidation for oil refinery |
| CN101757830A (en) * | 2010-01-18 | 2010-06-30 | 党延斋 | Method for recovering C2 and C3 components and hydrogen from refinery dry gas |
| CN101757830B (en) * | 2010-01-18 | 2014-11-05 | 党延斋 | Method for recovering C2 and C3 components and hydrogen from refinery dry gas |
| CN102718185A (en) * | 2012-07-20 | 2012-10-10 | 河南科技大学 | Separation device and separation method of hydrogen gas in hydrogen production through fermentation |
| CN102718185B (en) * | 2012-07-20 | 2014-03-26 | 河南科技大学 | Separation device and separation method of hydrogen gas in hydrogen production through fermentation |
| CN104031684A (en) * | 2014-05-23 | 2014-09-10 | 四川天采科技有限责任公司 | Method for recovering ethylene and hydrogen from refinery dry gases by combining cold oil absorption and membrane separation |
| CN104031684B (en) * | 2014-05-23 | 2016-10-05 | 四川天采科技有限责任公司 | Oil refinery dry gas cold oil absorbs, ethylene and the method for hydrogen are reclaimed in membrance separation combination |
| CN104071749A (en) * | 2014-07-16 | 2014-10-01 | 北京燕华工程建设有限公司 | Method for using dry gas to separate hydrogen as well as system |
| CN104071749B (en) * | 2014-07-16 | 2016-03-16 | 北京燕华工程建设有限公司 | A kind of dry gas separating hydrogen gas method and system |
| CN111467913A (en) * | 2020-03-27 | 2020-07-31 | 大连海奥膜技术有限公司 | Comprehensive recycling process and equipment for refinery tail gas |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1030821C (en) | 1996-01-31 |
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| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
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| C14 | Grant of patent or utility model | ||
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| CX01 | Expiry of patent term |
Expiration termination date: 20130324 Granted publication date: 19960131 |