CN1197763A - Carbon dioxide eliminating technology used in ammonia synthesis and hydrogen production processes - Google Patents
Carbon dioxide eliminating technology used in ammonia synthesis and hydrogen production processes Download PDFInfo
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- CN1197763A CN1197763A CN98101270A CN98101270A CN1197763A CN 1197763 A CN1197763 A CN 1197763A CN 98101270 A CN98101270 A CN 98101270A CN 98101270 A CN98101270 A CN 98101270A CN 1197763 A CN1197763 A CN 1197763A
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- gas
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Abstract
On the basis of physical absorption tower, physical-chemical absorption tower and regeneration tower are arranged. Row material gas is divided into two pathes entering the bottom of two absorption towers for gas-liquid contacting to remove CO2, the CO2 removed gas from physical absorption tower is fed to the middle part of the physical-chemical absorption tower to remove residual CO2 together with gas in tower, and the purified gas is fed out from the top of tower. The absorbant liquid from the physical-chemical absorption tower is regenerated in regeration tower and the removed CO2 gas is fed out from the top of tower. The said process can reach the purification degree of chemical absorption process and has low power consumption.
Description
The present invention relates to the CO in a kind of synthetic ammonia or the hydrogen production process
2Removing process.
In the chemical fertilizers production process, CO
2Removal methods has physical absorption method, chemical absorption method and physics-chemical absorption method three major types.The physical absorption method is to utilize different CO
2Divide and depress CO
2The difference of solubleness in solution adopts pressurizing absorption, decompression or gas to put forward modes such as desorption and regeneration, with CO
2From unstripped gas, remove.This law regeneration need not heated, thereby energy consumption is the end of than, but CO
2Filter effect the end of than, increased the difficulty of follow-up workshop section.Chemical absorption method is to utilize CO
2With the main component generation chemical reaction in the absorption liquid, form comparatively firm compound and remove CO
2Be characterized in that receptivity is strong, the gas purification degree height, but regeneration not only needs decompression or gas to carry, and also need to rely on heating, thereby heat exhaustion is bigger, and running cost improves.Physics-chemical absorption method in solution existing physical dissolution, again chemical reaction is arranged, existing decompression desorb has thermal degradation again during regeneration, so this method can have higher CO
2Filter effect, but the reactivation heat that consumes is also more relatively.
The chemical fertilizers production producer that China is present is in synthetic ammonia or hydrogen production process, for CO
2Remove the physical absorption methods that adopt more, promptly have a physical absorption tower, process gas enters from the bottom of tower, carries out pressurizing absorption with the lean solution that enters from tower top, and gas is carried desorption and regeneration etc., and then removes CO
2Because CO
2Filter effect low, therefore manyly fit into one-step removal CO with back workshop section's additive method such as the ammonia method of washing
2Because the continuous employing of novel procesies such as synthetic ammonia, throughput significantly improves, but a factor that is restricted is exactly the CO in synthetic ammonia or the hydrogen feedstock gas
2The ability that removes does not obviously match.For increasing processing power, new tower is extended on the old absorption tower of can dismantling again, but it is huge to do not only financial need amount like this, and the construction period is long, and CO
2Removal effect can not be significantly improved yet.
Purpose of the present invention just provides a kind of CO that can address the above problem effectively
2Remove novel process, maximally utilising existing installation, and match, also will improve CO simultaneously with growing chemical fertilizers production ability
2Filter effect, to reduce the difficulty of follow-up workshop section.
The present invention is achieved in that and keeps existing physical absorption tower, and string and a cover physics-chemical absorption tower and a regenerator column.Need remove CO
2Process gas, a part enters the physical absorption tower, another part enters the bottom of physics-chemical absorption tower.Process gas after the physics method absorbs decarburization is introduced to the middle part of physics-chemical absorption tower from the top of physical absorption tower, converge with process gas after absorbing decarburization through physics-chemical method, again with lean solution reaction decarburization from top, absorption tower.Purified gas is sent from the top on absorption tower.Be sent to the top of regenerator column through decompression by physics-rich solution that draw chemical absorption tower bottom, after last tower gas gas is carried, send from regenerator column middle part and become two-way, the one tunnel is sent to the middle part of physics-chemical absorption tower as semi lean solution, participates in the decarburizing reaction of tower under this absorption tower; Another road is sent the middle part of regenerator column back to again after the interchanger heat exchange, after down tower gas gas is carried, partially absorb liquid and drawn tower and deliver to reboiler outward, is heated into high-temperature gas through reboiler, sends the bottom of regenerator column back to.The absorption liquid of regenerator column bottom becomes lean solution after this high-temperature gas gas is carried, draw at the bottom of tower, is sent to the top of physics-chemical absorption tower through interchanger and water cooler.Through the isolated CO of regenerator column
2Gas is sent this process system by the top of regenerator column.
Key point of the present invention is, goes here and there on the basis of existing physical absorption method and suitable also supporting with it physics-chemical absorption (as the N methyldiethanol amine method) device of a cover scale, and one side is with the CO of original physical absorption process remnants
2Utilize chemical absorptive power to absorb fully, reach higher filter effect; On the other hand, utilization has absorbed a small amount of CO
2The physical absorptivity of physics-chemical absorption solution, absorb the most of CO in the process gas with the shunting in parallel of physical absorption gas
2Thereby, reach and can improve CO
2Filter effect can improve the purpose of total system throughput again.Owing to the internal circulating load of physics-chemical absorption solvent in this part is wanted much less than independent chemistry or the physics-chemical absorption method of adopting, so just can reach under the situation that increases small investment and energy consumption simultaneously, thoroughly solve original physical absorption process CO
2The problem that filter effect is low, and the corresponding carbonization treatment ability that increased.
Below in conjunction with accompanying drawing the present invention is further described.
Fig. 1 is a process flow sheet of the present invention.Wherein 1 is the physical absorption tower, and 2 is physics-chemical absorption tower, and 3,10 is separator, and 4,5,9 is water cooler, and 6 is regenerator column, and 7 is interchanger, and 8 is reboiler.
Need remove CO
2Process gas (as the unstripped gas of synthetic ammonia or hydrogen manufacturing) be divided into A1 and A2 two portions, wherein A1 is the tolerance that the physical absorption tower is handled, A2 is the tolerance that tower is handled under physics-chemical absorption tower.The ratio of shunting gas can be determined according to production requirement.Two portions gas enters the bottom of physical absorption tower 1 and physics-chemical absorption tower 2 respectively, this two portions gas carries out gas-to-liquid contact with the lean solution B1 of physical absorption method and the semi lean solution C2 of physics-chemical absorption method respectively in two towers, sponge the most of CO among gas A1 and the A2
2Remove most of CO
2Gas A1 be introduced to the middle part of physics-chemical absorption tower 2 from the top of physical absorption tower 1, and sponge most of CO by semi lean solution
2Gas A2 converge, continue to rise, contact with lean solution C1 and remove remaining CO in all gas through regenerated physics-chemical absorption liquid
2, purify qualified gas E and 2 top send from the absorption tower.For further reducing the difficulty of back workshop section, Purge gas E cools off through water cooler 4 earlier, behind the moisture content of separator 3 separating and condensings, sends to back workshop section again.Separator 3 isolated water of condensation are sent back to the top on absorption tower 2.
In this technology, the lean solution B1 that inserts on the physical absorption tower 1 is a physical absorption liquid, and the solution B 2 that draw 1 bottom from the absorption tower is to adopt old process to go regeneration.Absorption liquid in physics-chemical absorption tower 2 then is to realize regenerated by regenerator column 6.Specifically be the rich solution D that draws from 2 bottoms, absorption tower is sent to regenerator column 6 after decompression top, after the gas gas that rises on by the bottom in last tower is carried, send from the middle part of regenerator column 6 and be divided into two-way two portions, a part is sent the middle part of physics-chemical absorption tower 2 as semi lean solution C1; Another part C3 in interchanger 7 with lean solution heat exchange (heat absorption) after, send the middle part of regenerator column 6 back to, after the gas gas that rises on by the bottom in following tower is carried, partially absorb liquid C4 to draw outside the tower, send reboiler 8.Be heated into the bottom that high-temperature gas is sent regenerator column 6 back to through reboiler 8.The absorption liquid of regenerator column 6 bottoms becomes lean solution C1 after this high-temperature gas gas is carried, draw at the bottom of tower, reclaims heat is delivered to physics-chemical absorption tower 2 again after water cooler 5 coolings top through interchanger 7.
After regenerator column was regenerated physics-chemical absorption liquid, isolated CO
2Gas F is sent by cat head.According to as a same reason, the CO that is sent
2Gas is to cool off through water cooler 9 earlier, behind the moisture content of separator 10 separating and condensings, sends this process system again.Separator 10 isolated water of condensation are sent back to the top of regenerator column 6.
The invention has the advantages that, when need are expanded production capacity, can continue to use the original physical absorption to establish In the situation of standby and absorbent, connection in series-parallel one cover physics-chemical absorbing device all can reach all gas To the degree of purification requirement of chemical absorption method, kept again the advantage of original physical absorption process low energy consumption simultaneously. This Invention with all adopt physics-chemical methods relatively, (ammonia per ton can to save the steam consumption of regenerating section Save 400 kg of vapor), to producing 40000 tons of synthesis ammonia plants per year, can save 800,000 yuan every year. The present invention with Physical is compared, and can reduce the solution circulation amount, has exempted the double purification with Ammonia Process, has saved the ammonia consumption And post processing expense. In addition, also can save one-time investment or improvement expenses about 40%.
Claims (3)
1, the CO of a kind of synthetic ammonia or hydrogen production process
2Removing process is characterized in that:
A. need remove CO
2Process gas A1 enter physical absorption tower (1), process gas A
2Enter the bottom of physics-chemical absorption tower (2), process gas A1 after the physics method absorbs decarburization is introduced to the middle part of physics-chemical absorption tower (2) from the top of physical absorption tower (1), converge with the process gas after absorbing decarburization through physics-chemical method, again with lean solution C from top, absorption tower (2)
1The reaction decarburization, purified gas E the top of (2) sends from the absorption tower,
B. be sent to the top of regenerator column (6) by the rich solution D that physics-draws chemical absorption tower (2) bottom through decompression, after last tower gas gas is carried, send from regenerator column (6) middle part and be divided into two-way, the one tunnel as semi lean solution C
2Be sent to the middle part of physics-chemical absorption tower (2), another road C
3After interchanger (7) heat exchange, send the middle part of regenerator column (6) again back to, after tower gas gas is carried down, absorption liquid C
4Draw tower and deliver to reboiler (8) outward, be heated into the bottom that high-temperature gas is sent regenerator column (6) back to through reboiler (8), the absorption liquid of regenerator column (6) bottom becomes lean solution C after high-temperature gas gas is carried
1, at the bottom of tower, draw, be sent to the top of physics-chemical absorption tower (2) through interchanger (7) and water cooler (5), through the isolated CO of regenerator column (6)
2Gas is sent by the top of regenerator column (6).
2, technology according to claim 1 is characterized in that the Purge gas E that physics-chemical absorption tower (2) top is sent cools off through water cooler (4) earlier, sends to back workshop section again after separator (3) separates moisture content.
3, technology according to claim 1 is characterized in that the CO that regenerator column (6) top is sent
2Gas is to cool off through water cooler (9) earlier, sends this process system again after separator (10) separates moisture content.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98101270A CN1197763A (en) | 1998-04-10 | 1998-04-10 | Carbon dioxide eliminating technology used in ammonia synthesis and hydrogen production processes |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98101270A CN1197763A (en) | 1998-04-10 | 1998-04-10 | Carbon dioxide eliminating technology used in ammonia synthesis and hydrogen production processes |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1197763A true CN1197763A (en) | 1998-11-04 |
Family
ID=5216576
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN98101270A Pending CN1197763A (en) | 1998-04-10 | 1998-04-10 | Carbon dioxide eliminating technology used in ammonia synthesis and hydrogen production processes |
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| Country | Link |
|---|---|
| CN (1) | CN1197763A (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101935056A (en) * | 2010-09-19 | 2011-01-05 | 昆明理工大学 | Ammonia separating process for ammonia synthesis |
| CN101612512B (en) * | 2008-06-25 | 2011-05-25 | 苏庆泉 | Carbon dioxide separating system and separating method |
| CN102247740A (en) * | 2011-07-15 | 2011-11-23 | 攀钢集团有限公司 | Multi-stage desorption process for desulfurization solution |
| CN102350175A (en) * | 2011-07-15 | 2012-02-15 | 攀钢集团有限公司 | Multistage desorption system for desulphurization solution |
| CN101837221B (en) * | 2009-12-29 | 2012-08-22 | 中国恩菲工程技术有限公司 | Regeneration tower |
| CN102784546A (en) * | 2012-08-03 | 2012-11-21 | 中国华能集团清洁能源技术研究院有限公司 | Efficient CO2 capture system |
| CN102824815A (en) * | 2012-09-17 | 2012-12-19 | 江苏润丰环境工程有限公司 | Absorption extraction process for carbon dioxide in normal-pressure gas |
| CN103991845A (en) * | 2013-02-19 | 2014-08-20 | 中石化洛阳工程有限公司 | Method for removal of CO2 from shift gas during hydrogen production |
| CN104815529A (en) * | 2015-04-21 | 2015-08-05 | 中国华能集团清洁能源技术研究院有限公司 | Carbon dioxide capture regeneration system |
| CN113230832A (en) * | 2021-05-27 | 2021-08-10 | 浙江浙能技术研究院有限公司 | CO with low volatile organic pollutant emission2Trapping system and method |
-
1998
- 1998-04-10 CN CN98101270A patent/CN1197763A/en active Pending
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101612512B (en) * | 2008-06-25 | 2011-05-25 | 苏庆泉 | Carbon dioxide separating system and separating method |
| CN101837221B (en) * | 2009-12-29 | 2012-08-22 | 中国恩菲工程技术有限公司 | Regeneration tower |
| CN101935056A (en) * | 2010-09-19 | 2011-01-05 | 昆明理工大学 | Ammonia separating process for ammonia synthesis |
| CN102247740B (en) * | 2011-07-15 | 2014-07-09 | 攀钢集团有限公司 | Multi-stage desorption process for desulfurization solution |
| CN102350175A (en) * | 2011-07-15 | 2012-02-15 | 攀钢集团有限公司 | Multistage desorption system for desulphurization solution |
| CN102350175B (en) * | 2011-07-15 | 2013-12-25 | 攀钢集团有限公司 | Multistage desorption system for desulphurization solution |
| CN102247740A (en) * | 2011-07-15 | 2011-11-23 | 攀钢集团有限公司 | Multi-stage desorption process for desulfurization solution |
| CN102784546A (en) * | 2012-08-03 | 2012-11-21 | 中国华能集团清洁能源技术研究院有限公司 | Efficient CO2 capture system |
| CN102824815A (en) * | 2012-09-17 | 2012-12-19 | 江苏润丰环境工程有限公司 | Absorption extraction process for carbon dioxide in normal-pressure gas |
| CN102824815B (en) * | 2012-09-17 | 2013-12-25 | 江苏润丰环境工程有限公司 | Absorption extraction process for carbon dioxide in normal-pressure gas |
| CN103991845A (en) * | 2013-02-19 | 2014-08-20 | 中石化洛阳工程有限公司 | Method for removal of CO2 from shift gas during hydrogen production |
| CN103991845B (en) * | 2013-02-19 | 2016-01-13 | 中石化洛阳工程有限公司 | A kind of method of hydrogen production process conversion gas carbon dioxide removal |
| CN104815529A (en) * | 2015-04-21 | 2015-08-05 | 中国华能集团清洁能源技术研究院有限公司 | Carbon dioxide capture regeneration system |
| CN113230832A (en) * | 2021-05-27 | 2021-08-10 | 浙江浙能技术研究院有限公司 | CO with low volatile organic pollutant emission2Trapping system and method |
| CN113230832B (en) * | 2021-05-27 | 2022-06-28 | 浙江浙能技术研究院有限公司 | CO2 capturing system and method for low-volatile organic pollutant emission |
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| C01 | Deemed withdrawal of patent application (patent law 1993) | ||
| WD01 | Invention patent application deemed withdrawn after publication |