CN1235862A - Variable-pressure adsorption separating method for simultaneously purifying easy-to-adsorb phase and difficult-to-adsorb phase - Google Patents
Variable-pressure adsorption separating method for simultaneously purifying easy-to-adsorb phase and difficult-to-adsorb phase Download PDFInfo
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- CN1235862A CN1235862A CN 99116508 CN99116508A CN1235862A CN 1235862 A CN1235862 A CN 1235862A CN 99116508 CN99116508 CN 99116508 CN 99116508 A CN99116508 A CN 99116508A CN 1235862 A CN1235862 A CN 1235862A
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Abstract
The whole equipment is usually divided into two sections and the gas mixture is first treated in the front section or/and then in the rear section before further treatment. The front section with serial process relieves pressure forwards only and purifies easy-to-adsorb phase of gas, whereas the rear section relives pressure backwards only and purifies difficult-to-adsorb phase of gas. Thus, both the easy-to-adsorb phase of gas and the difficult-to-adsorb phase of gas are purified simultaneously with least power consumption.
Description
The present invention relates to utilize transformation to adsorb the method that admixture of gas is separated, relate in particular to and obtain difficult absorption phase of high-purity and the easy method of product gas mutually of adsorbing simultaneously.
The phase of purification absorption simultaneously is mutually attached with difficulty or ease from gaseous mixture, and in these two kinds of products, easily absorption is adsorbed mutually impurity each other with difficulty.Easily absorption is relative with difficult absorption mutually mutually.From conversion gas, obtaining high-purity CO simultaneously
2In hydrogen and nitrogen gas technology, CO
2Be easily to adsorb phase, hydrogen and nitrogen gas is difficult absorption phase; From air, producing N simultaneously
2And O
2Technology in, N
2Be easy absorbed component, O
2It is difficult absorbed component; And in produce CO and hydrogen and nitrogen gas technology simultaneously from water-gas, CO easily adsorbs phase, and hydrogen and nitrogen gas is difficult absorption phase, or the like.
Transformation adsorption seperation of gas, more common method are to remove as impurity easily adsorbing in the gaseous mixture with one section adsorbent equipment, get difficult absorption phase product; Perhaps will easily adsorb purify mutually product, difficult absorption is removed as impurity.Phase of purify easy absorption simultaneously and difficulty were adsorbed pressure swing absorption process mutually in the past, and a kind of is that two essentially identical two sections adsorption tower devices are gone here and there simply mutually, with impurity (USP4790858) in the difficult absorbed component product of the further purification gas; Another kind is with one section adsorption tower device, pre-absorption FA is set, adsorbs the LA process again, in the hope of reaching phase of purify easy absorption simultaneously and difficult absorption purpose (CN1195572) mutually.But in above-mentioned two kinds of methods, first method is oversize because of the adsorption tower unsaturation district of first section apparatus, and easy absorption phase replacement amount is strengthened, and energy consumption is higher, and yield is low, and investment is big; Second method then because of existing the adsorption tower outlet easily to be adsorbed the phase pollution problems in the process, carry not high by difficult absorption phase product purity, and energy consumption is also high, can not satisfy and produce and the economic scale requirement.
The purpose of this invention is to provide a kind of purity and yield that can improve easy absorbed component and difficult absorbed component product simultaneously, invest relative with energy consumption lessly, adsorption tower outlet is difficult for the variable-pressure adsorption separating method of contaminated band cascade process.
The present invention is achieved in that a kind of while purify easy absorption phase and difficult absorption variable-pressure adsorption separating method mutually, the method is adsorbed the PSA devices with two sections transformations, the last period, device had cascade process, each adsorption tower comprise successively pre-absorption FA, absorption A, again adsorb LA, drop pressure ED, along put PP, easily adsorb phase product gas displacement P, vacuumize VC, boost pressure ER, difficult absorption phase product gas lift is pressed the FR step; Each adsorption tower of back one section apparatus comprises absorption A, drop pressure ED successively, contrary puts BD, vacuumizes VC, the final pressure FR step of boost pressure ER, difficult absorption phase product gas.Difficult absorption phase product gas lift is pressed both outlets of available the last period of gas of FR, and available again back one section outlet also can be introduced highly purified difficult absorption phase product gas in addition; Between drop pressure ED or the boost pressure ER step waiting step I is arranged; All pressing number of times is 2-6 time; The adsorption tower number is the 6-32 platform.
While purify easy absorption phase provided by the invention and difficult absorption variable-pressure adsorption separating method mutually, mist adsorbs easily absorption phase component in first section apparatus, in the difficult absorption of the control adsorption tower outlet phase gas easily absorption phase component reach promptly to switch behind the finite concentration and advance another adsorption tower, shortened the unsaturation section length in the adsorption tower, reached the easy absorption of few usefulness and replace tolerance mutually, increase the purpose of handling tolerance, energy efficient; Simultaneously, first section apparatus finishes in absorption, forward finish drop pressure recovery gas after, only adopt forward emptying that gas in the tower is put to normal pressure, can make the easy adsorbed gas of high concentration of tower bottom desorb replace unsaturation district, top in advance, also reach few with displacement tolerance, the purpose of energy efficient.
The difficulty absorption phase gas of readily accessible, a both economical purity of first section apparatus outlet enters second section apparatus and further adsorbs, to remove the easy absorption phase impurity in the difficult absorption phase gas, obtain highly purified difficult absorption phase product, finish in adsorption process, finishing forward, drop pressure reclaims after the available gas, adopt the reverse pressure of putting that adsorption tower is put to normal pressure, high concentration is easily adsorbed phase impurity to the pollution of each mouthful of adsorption tower outlet absorption product at the bottom of having avoided tower like this, thereby make the difficult absorption of adsorption tower outlet phase product obtain high-purity easily, and energy efficient.
The invention will be further described below in conjunction with drawings and Examples.
Fig. 1 is a kind of flow chart of the present invention.
Fig. 2 is a kind of sequential chart of the present invention.
A-F, a-f are adsorption tower among the figure, and G1-G9, g1-g5 are pipeline, 1A-8A, 1B-8B, 1C-8C, 1D-8D, 1E-8E, 1F-8F, 1a-5a, 1b-5b, 1c-1c, 1d-5d, 1f-5f valve, and KV22, KV21, KV42, KV41 are valve.
When working, the present invention adopts two-stage pressure swing adsorption apparatus. The last period, device was with cascade process, and bleed off pressure only exist suitable To, obtaining economically the easy Adsorption Phase of high-purity to be used for satisfying, each adsorption tower in the device experiences following steps successively:
(1) adsorb in advance FA: the easy Adsorption Phase component that flows out from previous tower is higher than the first paragraph export requirement but is lower than The gas of content enters in the adsorption tower of just finishing the process of boosting and adsorbs in advance in the unstripped gas;
(2) absorption A: under adsorptive pressure, unstripped gas is passed into adsorption tower, from unstripped gas, select the easy absorption group of absorption Divide;
(3) adsorb LA: easily the Adsorption Phase composition impurity is soon super in the difficult Adsorption Phase gas product in the exit of adsorption tower again Cross when requiring, unstripped gas continues to pass into this tower and adsorbs, and this tower exit gas switches to another adsorption tower import, in addition One tower adsorbs in advance.
(4) drop pressure ED: the gas in the adsorption tower is entered respectively in addition several adsorption towers through drop pressure several times The middle recovery closed path at every turn to two pressure tower equilibriums;
(5) along putting PP: gas is emitted along the absorption direction in the adsorption tower, and last portion gas is recycled in the unstripped gas, and a part of gas emptying in back is to normal pressure;
(6) displacement P: forward replace adsorption tower with high-purity easy absorption phase product gas, replace the emptying of giving vent to anger;
(7) vacuumize VC: drive vavuum pump, highly purified easy absorption in the adsorption tower is extracted out mutually as product send;
(8) boost pressure ER: reclaim the gas branch of emitting from other several adsorption towers and enter this adsorption tower boost pressure several times respectively, to two pressure tower equilibriums, close path at every turn;
(9) FR that finally boosts: the absorption direction with the difficult absorption phase product circulation of vital energy in the wrong direction and be pressurized to adsorptive pressure to adsorption tower.
Back one section apparatus is put pressure and is only existed reversely, is used for obtaining economically highly purified difficult absorption phase product, and each adsorption tower in the device experiences following steps successively:
(1) absorption A: the product gas that the last period, device came enters the further easy absorption of absorption phase of adsorption tower, obtains highly purified difficult absorption phase product and sends;
(2) drop pressure ED;
(3) reverse putting pressed BD: emit overbottom pressure in the tower against the absorption direction, put pressure for the first time and be recycled in the unstripped gas, put for the second time and press sky;
(4) vacuumize VC: drive vavuum pump, the gas emptying or the recovery of absorption in the reverse extraction tower;
(5) boost pressure ER;
(6) FR that finally boosts: adsorption tower is risen to adsorptive pressure with the difficult absorption of high-purity phase product gas.
Between drop pressure ED or boost pressure ER, the waiting step I is arranged.
All pressing number of times is 2-6 time.
The adsorption tower number is the 6-32 platform.
Used adsorbent among the present invention is in activated alumina, active carbon, silica gel, the zeolite molecular sieve etc. one or more.
Embodiment:
Fig. 1 has shown a kind of embodiment of the present invention, is raw material with conversion gas, produces hydrogen and nitrogen gas and pure CO
2Gas.
Conversion gas is composed as follows
H
2 48-52％(V)
N
2 18-22％(V)
CO ≤1％
CH
4 1-2％(V)
CO
2 25-28％(V)
Temperature≤40 ℃
Pressure 0.6-0.8MPa
Load activated alumina, active carbon, three kinds of adsorbents of silica gel in the adsorption tower, form the combine adsorption bed successively from the bottom up.
Be example with the A tower the last period of device, and method of the present invention is described.
(1) adsorbs the FA:A tower in advance and finish difficult absorption phase product H
2, N
2Gas lift is pressed step F R, opens sequencing valve 3F, 8A, 2A.F tower exit gas enters the A tower through valve 3F, pipeline G3, G9, G8, valve 8A, and the A tower adsorbs in advance, difficult adsorption production gas H
2, N
2Gas flows out from valve 2A and enters house steward.Close 8A during end.
(2) absorption A: open 1A, conversion gas enters the A tower through pipeline G1, valve 1A, and absorption is absorption phase CO easily
2, qualified H
2, N
2Product gas flows out from valve 2A.As outlet CO
2When reaching finite concentration, stop absorption, close 2A.
(3) adsorb LA again: conversion gas continues to enter the A tower, and the A tower adsorbs again, opens 3A, 8B, 2B, and the A tower is worked off one's feeling vent one's spleen and entered the absorption of B tower, qualified H
2, N
2Purified gas flows out from 2B, closes 1A when absorption finishes again.
(4) one equal step-down E
1D: open 3C, allow the interior gas of A tower enter the C tower and reclaim, when reaching isostasy, close 3A through valve 3A, pipeline G3, valve 3C.
(5) two equal step-down E
2D: open valve 4A, 4D, A tower gas is got back to the D tower, close 4D after making two pressure tower equilibriums.
(6) three equal step-down E
3D: open 4E, A tower gas further is recovered to the E tower, close 4E after the two pressure tower equilibriums.
(7) one along putting PP
1: open KV21, A tower gas is recovered in the unstripped gas through valve 4A, pipeline G4, valve KV21, closes KV21 after pressure touches the mark.
(8) two along putting PP
2: open KV22, the emptying of A tower gas to normal pressure, is closed 4A, KV22.
(9) displacement P: open 6A, 5A, use pure CO
2Gas displacement A tower is closed 6A, 5A after the end.
(10) vacuumize VC: open 7A, extract A tower height purity out with vavuum pump and easily adsorb phase CO
2Gas is sent as product, closes 7A after the end.
(11) three E that all boost
3R: open 4A, 4C, receive the C tower and boost, close 4A after the isostasy.
(12) for the first time wait for all valve closings of I:A tower, remain static, wait for that other tower all presses end.
(13) two E that all boost
2R: open 4A, 4D, receive D tower gas and further boost, close 4A after the isostasy.
(14) etc. secondary is waited for I: with 12.
(15) one E that all boost
1R: open 3A, 3E, receive E tower gas and boost once more, 3E is closed in balanced back.
(16) FR that finally boosts: open KV1, with difficult absorption phase product H
2, N
2Gas rises to adsorptive pressure with the A tower, closes 3A after the end.
So far, the A tower has been finished a circulation, enters next circulation again; The circulation step of other tower is the same with the A tower, and just the time staggers mutually.
When carried out above-mentioned circulation the last period of device, back one section of device was carried out following circulation step (is example with the A tower) simultaneously:
1, absorption A:
Open 1A, 2A, the gas of the last period adsorbs in the A tower, obtains high-purity H
2, N
2The product pneumatic transmission is closed 1A, 2A to back workshop section after being adsorbed onto to a certain degree.
2, an equal step-down E
1D:
Open 3A, 3C, A, C two towers are all pressed, and close 3C during end.
3, two equal step-down E
2D:
Open 3D, A, D two towers are all pressed, and close 3A during end.
4, a contrary BD of putting
1:
Open 4A, KV41, put back in the unstripped gas A tower gas is reverse, close KV41 during end.
5, the two contrary BD of putting
2:
Open KV42, A tower gas is vented to normal pressure, closes 4A after the end.
6, vacuumize VC:
Open 5A, vacuumize with vavuum pump and make A tower adsorbent reactivation, close 5A during end.
7, two E that all boost
2R:
Open 3A, 3C, A, C two towers are all pressed, and close 3A during end.
8, wait for:
All valve closings of A tower are static.
9, the E that all boosts
1R:
Open 3A, 3D, A, D two towers are all pressed, and close 3D after the end.
10, the FR that finally boosts:
Open KV3, use H
2, N
2Product gas rises to adsorptive pressure with the A tower, closes 3A after the end.
The A tower finishes a circulation like this, enters next circulation again, and other tower carries out the circulation the same with the A tower, just staggers mutually on the time.
The present embodiment result is products C O
2Purity 98.8%, yield 85%; H
2, N
2CO in the gas
20.15%, H
2Yield 99%, N
2Yield 95%; Vacuumizing energy consumption is 33.92KWh/KNm
3Unstripped gas.
Claims (5)
1, a kind of while purify easy absorption phase and difficult absorption variable-pressure adsorption separating method mutually, it is characterized in that the method is with two sections transformations absorption PSA devices, the last period, device had cascade process, each adsorption tower comprise successively pre-absorption FA, absorption A, again adsorb LA, drop pressure ED, along put PP, easily adsorb phase product gas displacement P, vacuumize VC, boost pressure ER, difficult absorption phase product gas lift is pressed the FR step; Each adsorption tower of back one section apparatus comprises absorption A, drop pressure ED successively, contrary puts BD, vacuumizes VC, the final pressure FR step of boost pressure ER, difficult absorption phase product gas.
2, while purify easy absorption phase according to claim 1 and difficult absorption variable-pressure adsorption separating method mutually, it is characterized in that both outlets of available the last period of gas of difficult absorption phase product gas lift pressure FR, available again back one section outlet also can be introduced highly purified difficult absorption phase product gas in addition.
3, while purify easy absorption phase according to claim 1 and 2 and difficult absorption variable-pressure adsorption separating method mutually is characterized in that between drop pressure ED or the boost pressure ER step waiting step I being arranged.
4, while purify easy absorption phase according to claim 1 and difficult absorption variable-pressure adsorption separating method mutually, it is characterized in that all pressing number of times is 2-6 time.
5, while purify easy absorption phase according to claim 1 and difficult absorption variable-pressure adsorption separating method mutually is characterized in that the adsorption tower number is the 6-32 platform.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99116508A CN1126585C (en) | 1999-06-05 | 1999-06-05 | Variable-pressure adsorption separating method for simultaneously purifying easy-to-adsorb phase and difficult-to-adsorb phase |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99116508A CN1126585C (en) | 1999-06-05 | 1999-06-05 | Variable-pressure adsorption separating method for simultaneously purifying easy-to-adsorb phase and difficult-to-adsorb phase |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1235862A true CN1235862A (en) | 1999-11-24 |
| CN1126585C CN1126585C (en) | 2003-11-05 |
Family
ID=5279313
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN99116508A Expired - Fee Related CN1126585C (en) | 1999-06-05 | 1999-06-05 | Variable-pressure adsorption separating method for simultaneously purifying easy-to-adsorb phase and difficult-to-adsorb phase |
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| Country | Link |
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| CN (1) | CN1126585C (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100340323C (en) * | 2004-06-11 | 2007-10-03 | 成都天立化工科技有限公司 | Improved one stage pressure-varying adsorption gas separation method |
| CN100340324C (en) * | 2004-06-11 | 2007-10-03 | 成都天立化工科技有限公司 | Two-section totally recovering pressure swing adsorption gas separating method |
| CN100372758C (en) * | 2004-06-11 | 2008-03-05 | 成都天立化工科技有限公司 | Method for oxygen enriching by improved two-stage pressure swing adsorption |
| CN100372757C (en) * | 2004-06-11 | 2008-03-05 | 成都天立化工科技有限公司 | Method for oxygen enriching by improved two stage pressure swing adsorption |
| CN100423812C (en) * | 2004-06-11 | 2008-10-08 | 成都天立化工科技有限公司 | Improved one-section variable pressure obsorbing gas separation method |
| CN101549240B (en) * | 2009-04-23 | 2011-05-04 | 天津大学 | Method for absorbing methane in condensed coal bed gas through pressure varying mode including carbon dioxide replacement |
| CN102431967A (en) * | 2011-07-18 | 2012-05-02 | 何巨堂 | Method for preparing hydrogen and nitrogen gas with specific composition from multi-ingredient gas containing H2 and N2 |
| CN102626580A (en) * | 2011-02-02 | 2012-08-08 | 何巨堂 | Two-step pressure swing adsorption separation method of multicomponent gas containing hydrogen and hydrogen sulfide |
| CN105347304A (en) * | 2015-12-18 | 2016-02-24 | 四川天采科技有限责任公司 | Double-high PSA (pressure swing adsorption) hydrogen purification method adopting pressure desorption |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4790858A (en) * | 1988-01-29 | 1988-12-13 | Air Products And Chemicals, Inc. | Fractionation of multicomponent gas mixtures by pressure swing adsorption |
| CN1040292C (en) * | 1992-12-03 | 1998-10-21 | 黄家鹄 | Gas separation method by pressure swing adsorption for simultaneously preparing two gas products with high-purity and high-yield |
| KR970008347B1 (en) * | 1994-04-12 | 1997-05-23 | 한국에너지기술연구소 | Method and apparatus for separating argon and hydrogen from purge gas of nh3 synthesis |
| CN1195572A (en) * | 1998-01-24 | 1998-10-14 | 伍仁兴 | Pressure swing adsorption gas separation method for simultaneously purifying easy-adsorption phase and difficult-adsorption phase from mixed gas |
-
1999
- 1999-06-05 CN CN99116508A patent/CN1126585C/en not_active Expired - Fee Related
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100340323C (en) * | 2004-06-11 | 2007-10-03 | 成都天立化工科技有限公司 | Improved one stage pressure-varying adsorption gas separation method |
| CN100340324C (en) * | 2004-06-11 | 2007-10-03 | 成都天立化工科技有限公司 | Two-section totally recovering pressure swing adsorption gas separating method |
| CN100372758C (en) * | 2004-06-11 | 2008-03-05 | 成都天立化工科技有限公司 | Method for oxygen enriching by improved two-stage pressure swing adsorption |
| CN100372757C (en) * | 2004-06-11 | 2008-03-05 | 成都天立化工科技有限公司 | Method for oxygen enriching by improved two stage pressure swing adsorption |
| CN100423812C (en) * | 2004-06-11 | 2008-10-08 | 成都天立化工科技有限公司 | Improved one-section variable pressure obsorbing gas separation method |
| CN101549240B (en) * | 2009-04-23 | 2011-05-04 | 天津大学 | Method for absorbing methane in condensed coal bed gas through pressure varying mode including carbon dioxide replacement |
| CN102626580A (en) * | 2011-02-02 | 2012-08-08 | 何巨堂 | Two-step pressure swing adsorption separation method of multicomponent gas containing hydrogen and hydrogen sulfide |
| CN102431967A (en) * | 2011-07-18 | 2012-05-02 | 何巨堂 | Method for preparing hydrogen and nitrogen gas with specific composition from multi-ingredient gas containing H2 and N2 |
| CN105347304A (en) * | 2015-12-18 | 2016-02-24 | 四川天采科技有限责任公司 | Double-high PSA (pressure swing adsorption) hydrogen purification method adopting pressure desorption |
| CN105347304B (en) * | 2015-12-18 | 2017-07-14 | 四川天采科技有限责任公司 | A kind of double high desorption PSA with pressure carry hydrogen methods |
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| CN1126585C (en) | 2003-11-05 |
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Assignee: Hubei Chuxing Chemical Co., Ltd. Assignor: Yihua Group Co., Ltd., Hubei Prov. Contract fulfillment period: 2009.3.17 to 2019.3.16 contract change Contract record no.: 2009420000015 Denomination of invention: Variable-pressure adsorption separating method for simultaneously purifying easy-to-adsorb phase and difficult-to-adsorb phase Granted publication date: 20031105 License type: Exclusive license Record date: 2009.5.6 |
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Free format text: EXCLUSIVE LICENSE; TIME LIMIT OF IMPLEMENTING CONTACT: 2009.3.17 TO 2019.3.16; CHANGE OF CONTRACT Name of requester: HUBEI CHUXING CHEMICAL CO., LTD. Effective date: 20090506 |
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Granted publication date: 20031105 Termination date: 20120605 |