CN101264901A - Ammonia recovery method for gas mixture in hydrogen cyanide production - Google Patents
Ammonia recovery method for gas mixture in hydrogen cyanide production Download PDFInfo
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- CN101264901A CN101264901A CNA2008100548966A CN200810054896A CN101264901A CN 101264901 A CN101264901 A CN 101264901A CN A2008100548966 A CNA2008100548966 A CN A2008100548966A CN 200810054896 A CN200810054896 A CN 200810054896A CN 101264901 A CN101264901 A CN 101264901A
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- ammonium phosphate
- ammonia
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- decyanation
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 163
- LELOWRISYMNNSU-UHFFFAOYSA-N hydrogen cyanide Chemical compound N#C LELOWRISYMNNSU-UHFFFAOYSA-N 0.000 title claims abstract description 104
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 80
- 238000000034 method Methods 0.000 title claims abstract description 57
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 24
- 238000011084 recovery Methods 0.000 title claims abstract description 17
- 239000000203 mixture Substances 0.000 title claims description 33
- 239000007789 gas Substances 0.000 title abstract description 43
- MNNHAPBLZZVQHP-UHFFFAOYSA-N diammonium hydrogen phosphate Chemical compound [NH4+].[NH4+].OP([O-])([O-])=O MNNHAPBLZZVQHP-UHFFFAOYSA-N 0.000 claims abstract description 80
- 239000004254 Ammonium phosphate Substances 0.000 claims abstract description 75
- 229910000148 ammonium phosphate Inorganic materials 0.000 claims abstract description 75
- 235000019289 ammonium phosphates Nutrition 0.000 claims abstract description 75
- 238000010521 absorption reaction Methods 0.000 claims abstract description 47
- 238000003795 desorption Methods 0.000 claims abstract description 34
- 238000007255 decyanation reaction Methods 0.000 claims abstract description 27
- 239000000243 solution Substances 0.000 claims description 88
- 238000001816 cooling Methods 0.000 claims description 24
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 22
- 241000282326 Felis catus Species 0.000 claims description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 15
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 12
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 11
- 239000011259 mixed solution Substances 0.000 claims description 9
- 238000009833 condensation Methods 0.000 claims description 6
- 230000005494 condensation Effects 0.000 claims description 6
- 238000010792 warming Methods 0.000 claims description 6
- 239000005696 Diammonium phosphate Substances 0.000 claims description 5
- 229910000388 diammonium phosphate Inorganic materials 0.000 claims description 5
- 235000019838 diammonium phosphate Nutrition 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 2
- 230000009615 deamination Effects 0.000 claims description 2
- 238000006481 deamination reaction Methods 0.000 claims description 2
- 238000000354 decomposition reaction Methods 0.000 claims description 2
- 238000010025 steaming Methods 0.000 claims 1
- 239000002253 acid Substances 0.000 abstract description 3
- 230000002093 peripheral effect Effects 0.000 abstract 1
- 238000006386 neutralization reaction Methods 0.000 description 7
- LFVGISIMTYGQHF-UHFFFAOYSA-N ammonium dihydrogen phosphate Chemical compound [NH4+].OP(O)([O-])=O LFVGISIMTYGQHF-UHFFFAOYSA-N 0.000 description 5
- 229910000387 ammonium dihydrogen phosphate Inorganic materials 0.000 description 5
- 235000019837 monoammonium phosphate Nutrition 0.000 description 5
- 239000006012 monoammonium phosphate Substances 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 238000011109 contamination Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- JMANVNJQNLATNU-UHFFFAOYSA-N oxalonitrile Chemical compound N#CC#N JMANVNJQNLATNU-UHFFFAOYSA-N 0.000 description 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- 239000006096 absorbing agent Substances 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000007600 charging Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000002939 deleterious effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 229910052703 rhodium Inorganic materials 0.000 description 1
- 239000010948 rhodium Substances 0.000 description 1
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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Abstract
The invention discloses an ammonia recovery method from the mixing gas produced in the process of hydrogen cyanide production, comprising ammonia absorption process, decyanation process, desorption process and rectifying process for solving the technical problem. The invention is characterized in that decyanation process is set separately to recovery hydrogen cyanide gas, avoiding the loss of hydrogen cyanide caused by a large amount of acid gas like hydrocyanic acid contained in the ammonium phosphate solution directly steamed in Versum method, reducing production cost of hydrogen cyanide, reducing the emission of the harmful acid gas like hydrogen cyanide, and avoiding the serious pollution of peripheral enviroment. Besides, the ammonium phosphate solution contains a much smaller amout of hydrocyanic acid after hydrogen cyanide is recovered, which can not influence production process and make the production process more safety.
Description
Technical field
The present invention relates to a kind of ammonia recovery method, a kind of specifically method that the ammonia of gas mixture reclaims from prussic acid is produced.
Background technology
The production method of prussic acid industrial many be raw material with methane, ammonia and air, under 800 ℃ of-1000 ℃ of conditions, react production with platinum or aluminium, rhodium mesh catalyst.In the prussic acid production process from the mixed gas that reactor comes out because the generation of side reaction, make the composition more complicated in the gas mixture, wherein contain the product water that a large amount of unreacted ammonias and reaction generate, no matter event is made hydrogen cyanide product or is participated in next step reaction, all must remove ammonia and water in the gas mixture.Existingly industrially contain the method that the cyanogen mixture removes ammonia and adopt the Fu Samufa that purifies coal gas in the coking industry more.Simply introduce Fu Samu ratio juris and flow process below: gas mixture enters with the absorption tower and contacts with monoammonium phosphate solution to absorb the ammonia in the gas mixture, and the monoammonium phosphate solution that has absorbed ammonia is generated as diammonium phosphate solution, is called rich solution.Owing to be dissolved with a small amount of sour gas in the rich solution, in vaporizer, use open steam that sour gas is directly steamed earlier before delivering to desorb.The rich solution preheating that removes sour gas is directly advanced desorption tower afterwards, makes the diammonium phosphate in the rich solution be decomposed into monoammonium phosphate solution and ammonia with the open steam heating in desorption tower, and ammonia and portion water steam are from the cat head extraction.Decompose the monoammonium phosphate solution that generates after finishing, be called lean solution, lean solution turns back to the absorption tower once more and recycles as absorption liquid.Then get to rectifying tower from the ammoniacal liquor of cat head extraction and carry out rectifying, thereby obtain anhydrous ammonia by pump.
In this technical process, mainly containing following aspect reason is the ammonia recovering process that Fu Samufa can not directly apply to the gas mixture that produces in the prussic acid production: 1, the content owing to prussic acid gas in the coal gas has only 0.6g/m
3-0.7g/m
3, and hydrogen cyanide content reaches 85.48g/m in the gas mixture that produces in the prussic acid production
3, hydrogen cyanide content difference in the phosphoric acid rich solution, the recovering effect of ammonia is poor.2, in decyanation part, Fu Samufa adopts the method that directly steams the sour gas such as a large amount of prussic acid that ammonium phosphate solution contains, thereby causes the production cost of prussic acid to raise, and also can cause severe contamination to surrounding enviroment.The prussic acid of the high density in ammonium phosphate solution also can generate the prussic acid polymkeric substance, can cause column plate to stop up even blast, has potential safety hazard.3, vapour content is more in the gas mixture that produces during prussic acid is produced, and can condensation go out a large amount of water in absorbing the ammonia process, thereby cause the expansion of water in the system.
Summary of the invention
Technical problem to be solved by this invention is to provide a kind of ammonia recovery method that is used for prussic acid production gas mixture, to improve the recovering effect of ammonia in the prussic acid production, the production cost of reduction prussic acid, minimizing pollution.
For solving the problems of the technologies described above, the ammonia recovery method of gas mixture is in the prussic acid production of the present invention: (1), ammonia absorption process: the gas mixture that produces in the prussic acid production enters the absorption tower, contact with the ammonium phosphate lean solution, to absorb the ammonia that exists in the gas mixture, generate the ammonium phosphate rich solution that is rich in ammonium ion than described ammonium phosphate lean solution;
(2), decyanation process: described ammonium phosphate rich solution enters the decyanation tower after interchanger heats up, to remove the sour gas that includes prussic acid that contains in the ammonium phosphate rich solution, the sour gas that removes returns the absorption tower;
(3), desorption process: enter desorption tower from the effusive ammonium phosphate rich solution of decyanation tower,, get back to the absorption tower after the ammonium phosphate lean solution cooling that obtains after the decomposition and recycle so that the diammonium phosphate that contains in the ammonium phosphate rich solution is decomposed into ammonium phosphate lean solution and ammonia;
(4), rectifying: the ammonia and the water that decomposite from desorption tower enter rectifying tower, and rectifying obtains anhydrous ammonia.
Ammonia absorption process in the prussic acid production of the present invention in the ammonia recovery method of gas mixture can select for use following step to carry out: a, gas mixture enter the bottom of absorption tower hypomere tower, directly contact with tower still round-robin ammonium phosphate solution, when inhaling ammonia, mixed gas is once lowered the temperature; Ammonium phosphate solution behind the suction ammonia is discharged from the tower still, wherein the ammonium phosphate solution behind the suction ammonia of volume 85%-95% is after cooling, the hypomere top of tower that enters the absorption tower is used for the cooling of mixed gas and the absorption of ammonia once more, goes the decyanation tower to descend the step to handle after the ammonium phosphate lean solution heat exchange that ammonium phosphate solution process and the desorption tower of all the other volume 5%-15% comes out;
B, at the bottom of the absorption tower cooling after, mixed gas enters the epimere tower on absorption tower from the hypomere tower on absorption tower; The ammonium phosphate lean solution that the ammonium phosphate solution of epimere tower and desorption tower come out is formed the ammonium phosphate mixed solution, enters absorption tower epimere column overhead after the mixed solution cooling; Mixed solution after the cooling absorbs ammonia and carries out the cooling second time mixed gas at the epimere tower; The volume 75%-80% of the mixed solution behind the suction ammonia is used to return the cat head circulation by the discharge of epimere tower bottom and inhales ammonia, cooling, and rest part then directly overflows to down head tower by the epimere tower bottom and replenishes hypomere tower round-robin ammonium phosphate solution amount;
C, through the mixed gas after twice deamination, the cooling, enter the subsequent processing production technique after overflowing by cat head;
D, absorption tower in the course of the work, the adding phosphoric acid that continues from cat head, the loss of the phosphoric acid that in recycling process, causes with make-up ammonium phosphate solution.
The decyanation process is set separately in the inventive method, prussic acid gas is reclaimed, avoid the loss that directly steams the prussic acid that sour gas causes such as a large amount of prussic acid that still contain in the ammonium phosphate solution adopted among the Fu Samufa, reduced the production cost of prussic acid.Prussic acid gas is reclaimed the discharging that has also reduced sour gas such as deleterious prussic acid, avoided surrounding enviroment are caused severe contamination.Very low to the prussic acid content in the ammonium phosphate solution after the prussic acid recovery, can not exert an influence to production process, production process is safer.
Description of drawings
Fig. 1 is a production unit synoptic diagram of the present invention.
Embodiment
Ammonia recovery system of the present invention comprises ammonia absorption process, decyanation process, desorption process and rectifying.Its concrete equipment comprises: phosphoric acid storage tank 1, absorption tower 2, last tower cooler device 6, following tower cooler device 4, surge tank 3,5, decyanation tower 8, poor rich liquid heat exchanger 7, desorption tower 9, desorption tower feed preheater 11, desorb overhead condenser 12, weak ammonia storage tank 10, rectifying tower 14, rectifying tower feed preheater 13, rectifying tower top condenser 16, liquefied ammonia storage tank 15, steam system and circulating water system.
Technical process of the present invention:
(1), ammonia absorption process: the about 220 ℃ of prussic acid gas mixtures that come out by the prussic acid synthesis reactor at first enter the bottom of ammonia absorber 2, with tower still round-robin ammonium phosphate solution (degree of neutralization: 1.7) directly contact, thereby the water vapor condensation in the mixed gas is got off, make the mixed gas temperature reduce to 50 ℃-60 ℃, the most of ammonia in the prussic acid gas mixture is absorbed by tower still round-robin ammonium phosphate solution simultaneously; 70 ℃ of ammonium phosphate solution (rich solutions from the discharge of tower still, main content is diammonium phosphate, degree of neutralization: 1.7) enter surge tank 3, wherein volume 85%-95%, be preferably 90% ammonium phosphate solution, after passing through following tower cooler device 4 secondary circulation water for cooling, advance the hypomere top of tower and be used for the cooling of mixed gas and the absorption of part ammonia, ammonium phosphate solution (the lean solution that the ammonium phosphate rich solution of all the other volumes comes out through rich or poor interchanger 7 and desorption tower 14, main content is monoammonium phosphate, degree of neutralization: 1.2-1.3) go 8 times steps of decyanation tower to handle after the heat exchange.
Be cooled to 35 ℃-45 ℃ through the mixed gas of preliminary cooling once more from the epimere tower that enters the absorption tower after the hypomere tower on absorption tower 2 is overflowed, be preferably 40 ℃, with the vapour content in the control exhaust gas body, continue to absorb ammonia remaining in the mixed gas simultaneously, the content of the ammonia in the mixed gas that guarantees to export reaches processing requirement.45 ℃ of-50 ℃ of ammonium phosphate solutions that come out from the epimere tower (degree of neutralization: the 1.3-1.35) phosphoric acid solution (lean solution of coming out with desorption tower 9, degree of neutralization: 1.2-1.3) mix after through entering the cat head of absorption tower epimere tower behind the last tower cooler device 6 secondary circulation water for cooling to 35 ℃, with the abundant heat exchange of mixed gas and absorb ammonia.(degree of neutralization: 75%-80% 1.3-1.35) (volume) is used to return absorption tower cat head circulation after entering surge tank 5 by the epimere tower bottom to the ammonium phosphate mixed solution, is recycled and reused for and inhales the ammonia cooling after inhaling ammonia.Rest part then directly overflows to the hypomere tower by absorption tower epimere tower bottom, is used for replenishing hypomere tower round-robin solution amount.
After being overflowed by cat head, the mixed gas that absorbs through twice cooling go subsequent processing to use.
In the working process of absorption tower, the fresh phosphoric acid of 80%-90% is got to the absorption tower cat head from phosphoric acid storage tank 1 by volume pump and is recycled loss the process to replenish phosphoric acid.
(2), decyanation process: the ammonium phosphate rich solution that is come out by 2 bottoms, absorption tower is warming up to 100 ℃-110 ℃ through rich or poor interchanger 7, is preferably 104 ℃, enters decyanation tower 8 then, to remove prussic acid and other sour gas that contains in the ammonium phosphate rich solution.The acid gas that contains of being come out by decyanation tower 8 tops turns back in the absorption tower 2 again.Phosphoric acid rich solution (the degree of neutralization: 1.7) go desorption tower 9 to carry out the desorb of ammonia that comes out by the decyanation tower bottom.
(3), desorption process: the ammonium phosphate rich solution of sloughing sour gas through decyanation tower 8 is forced into 1.2MPa-1.4MPa by pump, be preferably 1.3MPa, and the ammonia and the water vapour heat transfer of mixture gas of coming out with the desorption tower cat head in desorption tower feed preheater 11 are warming up to 170 ℃-190 ℃, enter desorption tower after being preferably 180 ℃, the ammonium phosphate rich solution is heated to 190 ℃-200 ℃ gradually in desorption tower 9, and the ammonium phosphate rich solution is thermal decomposited and is ammonium phosphate lean solution and ammonia.
From the ammonium phosphate rich solution, decompose the ammonia that comes out and steam, behind feed preheater 11 and overhead condenser 12, together condense to 130 ℃, obtain certain density weak ammonia and enter weak ammonia storage tank 10 with portion water steam from the desorption tower cat head.
The ammonium phosphate lean solution that decompose to generate in desorption tower 9 is discharged at the bottom of then by tower, and pyritous ammonium phosphate lean solution enters the ammonia that the absorption tower is used for absorbing mixed gas, thereby finishes recycling of ammonium phosphate solution after rich or poor interchanger 7 heating decyanation tower chargings.
(4), rectifying: the weak ammonia storage tank 10 interior weak ammonias that got off by the desorption tower overhead condensation pass through 13 preheatings again of rectifying tower feed preheaters, be warming up to and enter rectifying tower 14 after 180 ℃ and carry out rectifying and reach 99.98% liquefied ammonia to produce purity, liquefied ammonia enters liquefied ammonia storage tank 15 after 16 condensations of rectifying tower top condenser.Ammonia content is less than 0.01% in the waste water that comes out at the bottom of the tower.
Claims (7)
1, the ammonia recovery method of gas mixture during a kind of prussic acid is produced is characterized in that the processing step of this method is:
(1), ammonia absorption process: the gas mixture that produces in the prussic acid production enters the absorption tower, contacts with the ammonium phosphate lean solution, to absorb the ammonia that exists in the gas mixture, generates the ammonium phosphate rich solution that is rich in ammonium ion than described ammonium phosphate lean solution;
(2), decyanation process: described ammonium phosphate rich solution enters the decyanation tower after interchanger heats up, to remove the sour gas that includes prussic acid that contains in the ammonium phosphate rich solution, the sour gas that removes returns the absorption tower;
(3), desorption process: enter desorption tower from the effusive ammonium phosphate rich solution of decyanation tower,, get back to the absorption tower after the ammonium phosphate lean solution cooling that obtains after the decomposition and recycle so that the diammonium phosphate that contains in the ammonium phosphate rich solution is decomposed into ammonium phosphate lean solution and ammonia;
(4), rectifying: the ammonia and the water that decomposite from desorption tower enter rectifying tower, and rectifying obtains anhydrous ammonia.
2, the ammonia recovery method of gas mixture during prussic acid according to claim 1 is produced is characterized in that described ammonia absorption process undertaken by following steps:
A, gas mixture enter the bottom of absorption tower hypomere tower, directly contact with tower still round-robin ammonium phosphate solution, when inhaling ammonia mixed gas are once lowered the temperature; Ammonium phosphate solution behind the suction ammonia is discharged from the tower still, wherein the ammonium phosphate solution behind the suction ammonia of volume 85%-95% is after cooling, the hypomere top of tower that enters the absorption tower is used for the cooling of mixed gas and the absorption of ammonia once more, goes the decyanation tower to descend the step to handle after the ammonium phosphate lean solution heat exchange that ammonium phosphate solution process and the desorption tower of all the other volume 5%-15% comes out;
B, at the bottom of the absorption tower cooling after, mixed gas enters the epimere tower on absorption tower from the hypomere tower on absorption tower; The ammonium phosphate lean solution that the ammonium phosphate solution of epimere tower and desorption tower come out is formed the ammonium phosphate mixed solution, enters absorption tower epimere column overhead after the mixed solution cooling; Mixed solution after the cooling absorbs ammonia and carries out the cooling second time mixed gas at the epimere tower; The volume 75%-80% of the mixed solution behind the suction ammonia is used to return the cat head circulation by the discharge of epimere tower bottom and inhales ammonia, cooling, and rest part then directly overflows to down head tower by the epimere tower bottom and replenishes hypomere tower round-robin ammonium phosphate solution amount;
C, through the mixed gas after twice deamination, the cooling, enter down the operation production technique after overflowing by cat head;
D, absorption tower in the course of the work, the adding phosphoric acid that continues from cat head, the loss of the phosphoric acid that in recycling process, causes with make-up ammonium phosphate solution.
3, the ammonia recovery method of gas mixture is characterized in that gas mixture is cooled to 50 ℃-60 ℃ for the first time in the absorption tower during prussic acid according to claim 2 was produced, and was cooled to 35 ℃-45 ℃ for the second time.
4, produce according to claim 1,2 or 3 described prussic acid in the ammonia recovery method of gas mixture, it is characterized in that in the described decyanation process ammonium phosphate lean solution heat exchange that the ammonium phosphate rich solution that comes out from the bottom, absorption tower and desorption tower come out, the ammonium phosphate rich solution is warming up to 100 ℃-110 ℃ and enters the decyanation tower.
5, the ammonia recovery method of gas mixture during prussic acid according to claim 4 is produced is characterized in that the ammonium phosphate rich solution is warming up to 104 ℃ in the described decyanation process to enter the decyanation tower.
6, produce according to claim 1,2 or 3 described prussic acid in the ammonia recovery method of gas mixture, it is characterized in that described desorption process comprises: the ammonium phosphate rich solution that the decyanation tower is discharged is forced into 1.2MPa-1.4MPa and ejects next ammonia and the heat exchange of water vapour mixed gas with desorption tower, the ammonium phosphate rich solution is warming up to 170 ℃-190 ℃, enters desorption tower; In desorption tower the ammonium phosphate rich solution being heated to 190 ℃-200 ℃ decomposes the ammonium phosphate rich solution; The ammonium phosphate lean solution that obtains after the ammonium phosphate rich solution decomposes is discharged at the bottom of tower, enters the absorption tower after the ammonium phosphate lean solution of discharge and the ammonium phosphate rich solution heat exchange that will enter the decyanation tower; From the ammonium phosphate rich solution, decompose the ammonia and the portion water steam that come out and steam, become weak ammonia after the condensation from the desorption tower cat head.
7, produce according to claim 1,2 or 3 described prussic acid in the ammonia recovery method of gas mixture, it is characterized in that steaming from the desorption tower cat head in the described rectifying, enter rectifying tower behind the weak ammonia pre-heating temperature elevation to 180 of condensation ℃ and carry out rectifying.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2008100548966A CN101264901B (en) | 2008-04-29 | 2008-04-29 | Ammonia recovery method for gas mixture in hydrogen cyanide production |
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|---|---|---|---|
| CN2008100548966A CN101264901B (en) | 2008-04-29 | 2008-04-29 | Ammonia recovery method for gas mixture in hydrogen cyanide production |
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| CN101264901A true CN101264901A (en) | 2008-09-17 |
| CN101264901B CN101264901B (en) | 2010-07-14 |
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| CN102502707A (en) * | 2011-10-26 | 2012-06-20 | 重庆紫光化工股份有限公司 | Method for purifying hydrocyanic acid from mixed gas containing hydrocyanic acid |
| CN102730720A (en) * | 2011-04-14 | 2012-10-17 | 重庆紫光化工股份有限公司 | Method and system for recovering ammonia from gas containing hydrocyanic acid |
| CN103936033A (en) * | 2012-12-18 | 2014-07-23 | 英威达科技公司 | Process for heat recovery from ammonia stripper in ADRUSSOW process |
| CN104724725A (en) * | 2014-11-21 | 2015-06-24 | 重庆紫光化工股份有限公司 | Hydrocyanic acid gas separation and purification system and method |
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| CN102730720A (en) * | 2011-04-14 | 2012-10-17 | 重庆紫光化工股份有限公司 | Method and system for recovering ammonia from gas containing hydrocyanic acid |
| CN102730720B (en) * | 2011-04-14 | 2014-04-23 | 重庆紫光天化蛋氨酸有限责任公司 | Method and system for recovering ammonia from gas containing hydrocyanic acid |
| CN102502707A (en) * | 2011-10-26 | 2012-06-20 | 重庆紫光化工股份有限公司 | Method for purifying hydrocyanic acid from mixed gas containing hydrocyanic acid |
| CN102502707B (en) * | 2011-10-26 | 2014-04-23 | 重庆紫光化工股份有限公司 | Method for purifying hydrocyanic acid from mixed gas containing hydrocyanic acid |
| CN103936033B (en) * | 2012-12-18 | 2017-08-11 | 英威达科技公司 | The method that heat is reclaimed from the ammonia desorber of Andrussow techniques |
| CN103936033A (en) * | 2012-12-18 | 2014-07-23 | 英威达科技公司 | Process for heat recovery from ammonia stripper in ADRUSSOW process |
| CN108455529A (en) * | 2012-12-18 | 2018-08-28 | 英威达纺织（英国）有限公司 | Device and method for hydrogen retrieval in andrussow process |
| CN108455529B (en) * | 2012-12-18 | 2022-02-25 | 英威达纺织（英国）有限公司 | Device and method for hydrogen recovery in andrussow process |
| CN104724725A (en) * | 2014-11-21 | 2015-06-24 | 重庆紫光化工股份有限公司 | Hydrocyanic acid gas separation and purification system and method |
| CN107628976A (en) * | 2017-09-27 | 2018-01-26 | 山东新和成氨基酸有限公司 | A kind of method of the methylmercapto butyric acid of 2 hydroxyl of continuous preparation 4 of cleaning |
| CN107628976B (en) * | 2017-09-27 | 2019-06-04 | 山东新和成氨基酸有限公司 | A kind of method of clean continuous preparation 2-Hydroxy-4-methylthiobutyric acid |
| CN108926962A (en) * | 2018-08-10 | 2018-12-04 | 重庆天原化工有限公司 | Ammonia-containing exhaust recovery and treatment method |
| CN112479227A (en) * | 2020-12-11 | 2021-03-12 | 李同军 | Equipment and process for purifying crude ammonia water |
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| CN101264901B (en) | 2010-07-14 |
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