CN85108560A - The liquefied ammonia dilution method is separated the ammonia in the synthetic cyclic gas - Google Patents
The liquefied ammonia dilution method is separated the ammonia in the synthetic cyclic gas Download PDFInfo
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- CN85108560A CN85108560A CN85108560.1A CN85108560A CN85108560A CN 85108560 A CN85108560 A CN 85108560A CN 85108560 A CN85108560 A CN 85108560A CN 85108560 A CN85108560 A CN 85108560A
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- ammonia
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- synthetic cyclic
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- cyclic gas
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Abstract
The present invention relates to ammonia isolation technique in the synthetic cyclic gas, a kind of new branch ammonia method has been proposed, this method adopts organic solvent as thinner, the double as absorption agent, the ammonia in dilution and the absorption circulation gas carries out reversible regeneration, can improve separating effect, also can reduce the power consumption of synthesis ammonia plant, applicable to dissimilar synthesis ammonia plants, low pressure synthesis system especially.
Description
The present invention relates to the isolation technique of ammonia in the synthetic cyclic gas.In existing technology, cold method is adopted in the separation of ammonia usually in the synthetic cyclic gas, and as at present domestic big, medium and small synthesis ammonia plant all adopts this method.Cold method is divided ammonia, need to consume a large amount of freezing merits, and when pressure process reduced, power consumption improves thereupon, is difficult to adapt to synthesis pressure and reduces and requirements of saving energy.Non-refrigeration method divides ammonia, and more sophisticated have a WATER-WASHING METHOD.As the HumphereysGlasgen company of Britain (ampo, 78, papers) and Dutch SNAM company (Hydrocarbon processing, 7, P 106,1972).Domestic Gongxian is gone back to Guo fertilizer plant and is adopted the washing of inhaling the ammonia comb to divide ammonia, but washing divides the ammonia method to need huge drying installation, and the regeneration energy consumption is big, is difficult for promoting.
The objective of the invention is to overcome the shortcoming of above-mentioned all methods, propose the method for ammonia in a kind of new separation synthetic cyclic gas, i.e. the liquefied ammonia dilution method.
Main points of the present invention are, select a kind of ideal organic solvent as the liquefied ammonia thinner, simultaneously the double as absorption agent.Synthetic cyclic gas at first contacts with absorption agent under the overhead streams in the absorption tower, and cooling continuously.Absorption agent can adopt with ammonia and infinitely dissolve each other, and the organic solvent that vapour pressure is very low, play dual parts dilution and absorption during the course, thereby the content that makes the absorption tower be sent to ammonia in the synthetic gas of subsequent handling can significantly be lower than conventional cold method, and the content of organic solvent can be lower than 1PPM usually in the gas.The rich solution that tower bottom flow goes out by the decompression and (or) heating method, in revivifier, the ammonia in the rich solution is discharged.Regenerative process adopts the renovation process of the reversible adverse current of heating continuously.The ammonia that discharges under different regeneration pressures can be gas ammonia or liquefied ammonia, and respectively as product, lean solution then recycles by the pumped back absorption tower.
Fig. 1 is the 150kg/cm of this method
2The large-scale ammonia plant process flow sheet.
Fig. 2 is the 300kg/cm of this method
2Medium-sized synthesis ammonia plant process flow sheet.
Fig. 3 is the 200kg/cm of this method
2Small-sized synthesis ammonia plant process flow sheet.
In the flow process of Fig. 1, synthetic cyclic gas is sent into absorption tower (2) and is contacted with absorption agent after replenishing virgin gas, finishes branch ammonia purpose.Synthetic gas behind minute ammonia leaves cat head, by charcoal filter (1), enters synthetic tower behind the removing absorption agent.And rich solution is drawn from cat head, can be decompressed to 16kg/cm through turbine (3) recovered energy
2, behind preheater (5), enter regenerator column (6), heating continuously in tower, lean solution is sent the absorption tower back to by pump (4) pressurization and is recycled after heat recuperation and cooling.The gas ammonia that discharges obtains liquefied ammonia by reflux tower (7) through cooling, sends into liquefied ammonia groove (8).
In the flow process of Fig. 2, its absorption is identical substantially with large-scale ammonia plant with regeneration flow process partly, and difference is that medium-sized synthesis ammonia plant is provided with copper washing section, returns 350 kilograms of/ton NH usually approximately
3Gas ammonia, need liquefaction, the method for its liquefaction system absorbs the gas ammonia of washing from copper by absorption agent in absorption tower (11), the rich solution after the absorption is admitted in the regenerator column (10), the working pressure in the regenerator column (10) is 16kg/cm
2, with 130 ℃～150 ℃ hot water heating, this part hot water also can continue on for regenerator column (6) and make the regeneration thermal source.The gas ammonia that regenerator column (10) comes out is through return channel (9), and the liquefied ammonia groove is sent in the liquefaction of cooling back.Absorption agent send regenerator column (10) through pump (12) and interchanger (5 '), recycles.
The flow process of Fig. 3 and Fig. 1, Fig. 2 is identical substantially, difference is to be provided with 2 regenerator columns (6), (10), in absorption tower (2), absorbed the rich solution regeneration in regenerator column (6) earlier of ammonia, obtain liquefied ammonia, then in further regeneration of regenerator column (10), obtain gas ammonia, liquefied ammonia is sent to copper washing section, and gas ammonia is sent to carbonization workshop section, replaces turbine with throttling valve (3) simultaneously, and corresponding increase heat-exchange equipment (5 '), (5 ") and reflux (9), because regenerator column (6) adopts phreatic water, the regeneration pressure of regenerator column (10) is low; then distinguish available hot water below 85 ℃ as thermal source, has opened up approach for carbonization flow process small fertilizer plant makes full use of low-grade heat source.
Key problem in technology of the present invention is to select function admirable, has diluting effect for ammonia, and organic solvent such as ethylene glycol, glycerine, PVOH and the derivative thereof of absorption arranged again.
Of the present invention minute ammonia technology, advantage are significantly, owing to left out refrigerator, make the power consumption decrease, and the low-grade heat source of putting aside as useless is fully utilized. Table 1, table 2, table 3 have been made technical and economic evaluation to various types of ammonia factory respectively, and the data in the table have illustrated this point fully.
The energy of table 1 Large Scale Synthetic Ammonia Plants and economic evaluation
The liquefied ammonia product, summer temperature
(benchmark: ton NH
3)
Purify and require: NH
3=2.1%
*The energy converting standard:
1Kwh＝3000kcal;
1 ton of recirculated water=1000kcal;
Low-grade heat source is pressed 7kg/cm
2The thermo-efficiency of steam is benchmark, converts to standard thermal with thermal efficiency ratio.
The energy of the medium-sized ammonia of table 2 factory and economic evaluation liquefied ammonia product, summer temperature
(benchmark: ton NH
3)
Purify and require: NH
3=1.5%
*The energy conversion is accurate referring to table 1
The table 3 small ammonia (200kg/cm of factory
2) energy and economic evaluation
The gas ammonia product, summer temperature
(benchmark: ton NH
3)
Purify and require: NH
3=1.5%
*The energy converting standard is referring to table 1
Claims (2)
1, ammonia isolation technique in the synthetic cyclic gas the invention is characterized in that synthetic cyclic gas contacts with organic solvent earlier, cooling continuously in the absorption tower, dilution also absorbs ammonia in the circulation gas, and rich solution then is sent to regenerator column, decompression continuously and (or) under the condition of heating, can send regeneration, ammonia is discharged.Lean solution is then recycled by the pumped back absorption tower.The ammonia that discharges can be liquefied ammonia after cooling.
2, method according to claim 1 is characterized in that can adopting ethylene glycol as the organic solvent of thinner and absorption agent, glycerol, polyoxyethylene glycol and derivative thereof.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN85108560.1A CN1003582B (en) | 1985-10-31 | 1985-10-31 | Separation of ammonia from synthetic recycle gas by liquid ammonia dilution method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN85108560.1A CN1003582B (en) | 1985-10-31 | 1985-10-31 | Separation of ammonia from synthetic recycle gas by liquid ammonia dilution method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN85108560A true CN85108560A (en) | 1987-05-06 |
| CN1003582B CN1003582B (en) | 1989-03-15 |
Family
ID=4796074
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN85108560.1A Expired CN1003582B (en) | 1985-10-31 | 1985-10-31 | Separation of ammonia from synthetic recycle gas by liquid ammonia dilution method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1003582B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102923732A (en) * | 2012-11-27 | 2013-02-13 | 天津衡创工大现代塔器技术有限公司 | Method for separating ammonia |
| CN102923733A (en) * | 2012-11-27 | 2013-02-13 | 天津衡创工大现代塔器技术有限公司 | Ammonia separation device and method |
-
1985
- 1985-10-31 CN CN85108560.1A patent/CN1003582B/en not_active Expired
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102923732A (en) * | 2012-11-27 | 2013-02-13 | 天津衡创工大现代塔器技术有限公司 | Method for separating ammonia |
| CN102923733A (en) * | 2012-11-27 | 2013-02-13 | 天津衡创工大现代塔器技术有限公司 | Ammonia separation device and method |
| CN102923732B (en) * | 2012-11-27 | 2014-08-20 | 天津衡创工大现代塔器技术有限公司 | Method for separating ammonia |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1003582B (en) | 1989-03-15 |
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