CN1062854A - Hydrogen sulfide and ammonia process for recovering mixing gas - Google Patents
Hydrogen sulfide and ammonia process for recovering mixing gas Download PDFInfo
- Publication number
- CN1062854A CN1062854A CN 90106490 CN90106490A CN1062854A CN 1062854 A CN1062854 A CN 1062854A CN 90106490 CN90106490 CN 90106490 CN 90106490 A CN90106490 A CN 90106490A CN 1062854 A CN1062854 A CN 1062854A
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- ammonia
- hydrogen sulfide
- tourie
- alkali lye
- absorption tower
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Abstract
The invention belongs to the treatment of waste gas technical field, is a kind of recovery technology about hydrogen sulfide and ammonia gas mixture.This technology is that said gas mixture is fed in the absorption tower, contact with the alkali lye in the tower, make hydrogen sulfide and alkaline reaction generate sulfuration alkali lye, remaining ammonia comes out to enter in the ammonia absorption liquid of tourie after the water cooler cooling pneumatic tube from the absorption tower, be in water or the acidic solution, generate ammoniacal liquor or ammonium salt, Sodium Sulphide and ammoniacal liquor or ammonium salt all are useful materials, therefore turn waste into wealth, reduce environmental pollution.Technology of the present invention is simple, and waste gas rate of recovery height is applicable in the industrial production that hydrogen sulfide and ammonia gas mixture are discharged and recycled.
Description
The invention belongs to the treatment of waste gas technical field, is a kind of recovery technology about hydrogen sulfide and ammonia gas mixture.
In Industrial processes, usually can discharge and contain hydrogen sulfide (H
2S) and ammonia (NH
3) mixed gas, this mix waste gas enters in the atmosphere and pollutes the environment, and is harmful to the healthy and infringement animals and plants of human body.How handling this waste gas, is the problem that must solve in the industrial production.March 11 1980 U.S. Pat 4192054(day for announcing), introduced a kind of from containing hydrogen sulfide, ammonia and also having the mixed gas of a kind of acidity or alkaline gas, earlier with mixed gas through washing tower, wash mixed gas with copper-bath, make two kinds of gases of hydrogen sulfide and ammonia generate (NH
4)
2SO
4With the throw out of S, and then with (NH
4)
2SO
4Separate with S.Adopt this method to handle mix waste gas, though waste gas is converted into useful (NH
4)
2SO
4With the S material, but this complex treatment process, investment are big, the processing of the gas mixture of being made up of hydrogen sulfide and ammonia that is unsuitable for discharging in present China industrial production.
The purpose of this invention is to provide that a kind of technology is simple, investment is little, hydrogen sulfide and ammonia gas mixture can be converted into useful matter, reclaim two kinds of waste gas of hydrogen sulfide and ammonia simultaneously, the production technique that turns waste into wealth.
The objective of the invention is to realize with following technical scheme.By hydrogen sulfide of discharging in the industrial production and ammonia mix waste gas, feed in the absorption tower through pneumatic tube, contact with the alkali lye in the tower, make hydrogen sulfide and alkaline reaction generate Sodium Sulphide liquid, remaining ammonia comes out to enter after the water cooler cooling pneumatic tube in the ammonia absorption liquid of tourie from the absorption tower to be in water or the acidic solution, to generate ammoniacal liquor or ammonium salt, so just with the mix waste gas recovery of hydrogen sulfide and ammonia, be separately converted to useful Sodium Sulphide and ammoniacal liquor or ammonium salt, turn waste into wealth.The present invention is described in further detail below in conjunction with an embodiment.
In industrial production Sodium Thiocyanate 99 process, the reaction process below adopting:
Resultant of reaction is NH
4SCN and NH
4The mixture of HS is in order to obtain NH
4SCN needs heating, makes NH
4HS is decomposed into gas and discharges, promptly
Like this, the resultant of reaction gained only stays NH
4SCN, just can further finish following reaction:
This reaction has just obtained required Sodium Thiocyanate 99 (NaSCN), and the high-content Sodium Thiocyanate 99 technology that adopts this method to produce is described in another patent application.The H of Pai Chuing in process of production
2S and NH
3Mix waste gas must recycle, and pollutes the environment otherwise enter in the atmosphere.For reclaiming hydrogen sulfide and ammonia gas mixture,, adopt double loop shown in Figure 1 to absorb H synchronously according to the technical solution of the present invention
2S and NH
3The tail gas process schema.
Among the figure: 1,3,21,23,28,30,32, the 34-pneumatic tube, 2,22, the 31-surge tank, the 4-squirt pump, 5,6,8,10,12,14,15,17, the 27-tubing, 7-alkali liquid tank, 9, the 13-recycle pump, the 11-absorption tower, the 16-concentration kettle, 18-delivery pipe, 19-vapour pipe, 20-Sodium Sulphide basin, the 24-water cooler, 25-sprinkler head, 26-level ammonia tourie, the 29-liquid-inlet pipe, the 41-transferpump, 33-tail gas extraction pump, 35-refrigerating fulid pipe, 36-secondary amine tourie, 8,37,38,39, the 40-valve, I-hydrogen sulphide absorption process, II-ammonia absorption technique.
The hydrogen sulfide that in the Sodium Thiocyanate 99 production process, produces and the mixed tail gas of ammonia, enter surge tank (2), air-flow is steadily exported by pneumatic tube (1), behind squirt pump (4), enter absorption tower (11) by pneumatic tube (3), recycle pump (9) is input to squirt pump (4), alkali lye with the alkali lye of bottom, absorption tower (11) and is ejected in by squirt pump (4) and produces negative pressure in the squirt pump (4), the gas mixture suction is flowed in the absorption tower (11) with alkali lye, and and alkaline reaction, generate Sodium Sulphide.Recycle pump (13) with the alkali lye of bottom, absorption tower (11) through tubing (12), with the top that is pumped into absorption tower (11), alkali lye descends from the cat head spray, with upstream hydrogen sulfide contact reacts generation Sodium Sulphide in the tower and at the bottom of falling into tower, recycle pump (13) with the Sodium Sulphide of bottom, absorption tower (11) through tubing (15), concentrate with being pumped into concentration kettle (16), by recycle pump (13) spissated Sodium Sulphide is pumped into Sodium Sulphide basin (20) through tubing (17) and tubing (14) again.The Sodium Sulphide that enters in the concentration kettle (16) is discharged by delivery pipe (18) by the aqueous vapor that heating concentrates, produces to Sodium Sulphide in the chuck of vapour pipe (19) feeding concentration kettle (16) with steam.Also can in the cooking stove of autocracy, use fiery direct heating, the boiling of rare sulfuration alkali lye is concentrated.(11) internal reaction generates Sodium Sulphide on the absorption tower for hydrogen sulfide and alkali lye, the tower interior reaction temperature is controlled at 50-125 ℃, reaction is finished, the PH of alkali lye 〉=8, alkali content should excessive 5-15% be best with respect to the hydrogen sulfide amount in the absorption liquid, and the main ingredient of alkali lye is for containing sodium ion mineral alkali or basic salt such as NaOH or Na
2CO
3Or NaHCO
3Deng.The ammonia that comes out from absorption tower (11) is behind pneumatic tube (21) and surge tank (22), enter in the primary amine tourie (26), entering primary amine tourie (26) before, pneumatic tube (23) is introduced in the water cooler (24), going up spray water by sprinkler head (25) to water cooler (24) cools off, the ammonia temperature that enters like this in the primary amine tourie (26) is below 50 ℃, refrigerating fulid pipe (35) is arranged in the primary amine tourie (26), feed refrigerated water or chilled brine in the refrigerating fulid pipe (35), absorption liquid reaction in ammonia and the primary amine tourie (26), the ammonia that unreacted finishes are discharged to enter the secondary amine tourie (36) from the top and are reacted with the ammonia absorption liquid.When treating that ammoniacal liquor in the primary amine tourie (26) or ammonium salt reach needed concentration, this absorption liquid can be sent through transferpump (41), and with the resultant in the secondary amine tourie (36) put into primary amine tourie (26) again with ammonia gas react, the concentration of resultant is improved, in secondary amine tourie (36), add fresh absorption liquid (water or acid) simultaneously, more qualified resultant is exported through transferpump (41) by primary amine tourie (26) bottom.The temperature of the refrigerated water in the refrigerating fulid pipe (35) is 0 ℃-10 ℃ (advance jar place), if chilled brine then temperature be 0-20 ℃ (entering a jar place), the temperature of reaction of the interior liquid of tourie (26) is maintained-10-50 ℃ between, reaction pressure is≤0.2MPa; Temperature of reaction in the secondary amine tourie (36) is 0-50 ℃, and pressure is normal pressure, and the ammonia absorption liquid is water or acidic solution example hydrochloric acid or sulfuric acid etc.The ammonia absorption liquid is added by liquid-inlet pipe (29).Unabsorbable gas is transported to chimney by tail gas extraction pump (33) and is entered in the atmosphere behind pneumatic tube (30), surge tank (31) and pneumatic tube (32) in secondary amine tourie (36).
The gas mixture of hydrogen sulfide and ammonia enters surge tank (2) in the technical process of the present invention, opens valve (8), alkali lye and flows into the bottom, absorption tower by alkali liquid tank (7), shuts valve (8) after putting into the alkali lye of specified amount.Open valve (37), start recycle pump (9 simultaneously, 10), open valve (40), gas mixture enters absorption tower (11), wait to enter behind the gas mixture of regulation value valve-off (37) again, hydrogen sulfide and alkali lye react, behind the valve of closing (37), recycle pump (9) cuts out, after treating that hydrogen sulfide and alkaline reaction finish, valve-off (40), open valve (39) simultaneously, the Sodium Sulphide resultant is sent into concentration kettle (16) internal heating and is concentrated, concentrate reach specified requirement after, open valve (38), it is to be packaged that while valve-off (39), finished product Sodium Sulphide are sent into the interior storage of Sodium Sulphide basin (20).In hydrogen sulfide and alkaline reaction, ammonia reacts with added ammonia absorption liquid in primary amine tourie (26) and secondary amine tourie (36) after pneumatic tube (21) is by water cooler (24) cooling, generate ammoniacal liquor or ammonium salt, resultant is to be packaged by transferpump (41) output.In having finished production process, repeat last operating process again.
Technology of the present invention is simple, and waste gas rate of recovery height, its resultant Sodium Sulphide are the important source material of papermaking, dyestuff, sodium thiosulfate and other Chemical Manufacture, and ammoniacal liquor or ammonium salt are good chemical fertilizer, also can be used as industrial raw material, therefore turns waste into wealth.The present invention is applicable in the industrial production that hydrogen sulfide and ammonia gas mixture discharge and recycle.
Claims (8)
1, the recovery technology of a kind of hydrogen sulfide and ammonia gas mixture, it is characterized in that said gas mixture is fed in the absorption tower (11) by pneumatic tube (3), contact with the alkali lye in the tower, make hydrogen sulfide and alkaline reaction generate sulfuration alkali lye, remaining ammonia is from absorption tower (11) come out to enter ammonia absorption liquid in the tourie after water cooler (24) cooling pneumatic tube (23), be in water or the acidic solution, generate ammoniacal liquor or ammonium salt.
2, the recovery technology of hydrogen sulfide according to claim 1 and ammonia gas mixture, it is characterized in that said gas mixture enters the absorption tower by pneumatic tube (3) behind squirt pump (4), recycle pump (9) with the alkali lye of bottom, absorption tower (11) be input to squirt pump (4), alkali lye is sprayed by squirt pump (4), producing negative pressure in squirt pump flows into the gas mixture suction in the absorption tower with alkali lye, and and alkaline reaction, generate Sodium Sulphide.
3, hydrogen sulfide according to claim 1 and 2 and ammonia process for recovering mixing gas, (13) deliver to top, absorption tower (11) with the lye pump of bottom, absorption tower (11) to it is characterized in that recycle pump is arranged, alkali lye descends from the cat head spray, generates Sodium Sulphide with upstream hydrogen sulfide contact reacts in the tower.
4, hydrogen sulfide according to claim 3 and ammonia process for recovering mixing gas, it is characterized in that recycle pump (13) is pumped into concentration kettle (16) with rare Sodium Sulphide of bottom, absorption tower (11) through tubing (15) and concentrates, by recycle pump (13) spissated Sodium Sulphide is pumped into Sodium Sulphide basin (20) through tubing (17) and tubing (14) again.
5, hydrogen sulfide according to claim 4 and ammonia process for recovering mixing gas, it is characterized in that feeding in the concentration kettle (16) concentrated by vapour pipe (19) to rare sulfuration alkali lye heating with steam, or in the cooking stove of autocracy, use fiery direct heating, the boiling of rare sulfuration alkali lye is concentrated.
6, hydrogen sulfide according to claim 3 and ammonia process for recovering mixing gas, it is characterized in that the temperature of reaction in the absorption tower (11) is 50-125 ℃, hydrogen sulfide and alkali reaction are finished, PH 〉=8 that should keep alkali lye, the main ingredient of base excess 5-15% alkali lye is for containing sodium ion mineral alkali or basic salt in the absorption liquid.
7, hydrogen sulfide according to claim 1 and ammonia process for recovering mixing gas, it is characterized in that being introduced into the primary amine tourie (26) and react with the ammonia absorption liquid from the ammonia that come out absorption tower (11), the ammonia that unreacted finishes is discharged to enter the secondary amine tourie (36) from the top and is reacted with the ammonia absorption liquid, when treating that ammoniacal liquor in the primary amine tourie (26) or ammonium salt reach needed concentration, this absorption liquid can be sent into packing through transferpump (41), and with the resultant in the secondary amine tourie (36) put into primary amine tourie (26) again with ammonia gas react, the concentration of resultant is improved, in secondary amine tourie (36), add fresh absorbent such as water or acid simultaneously, again qualified resultant is exported by primary amine tourie bottom, carried out and so forth.
8, hydrogen sulfide according to claim 7 and ammonia process for recovering mixing gas is characterized in that the temperature of reaction in the primary amine tourie is 50--10 ℃, and pressure is≤0.2MPa, and the temperature of reaction in the secondary amine tourie (36) is 0-50 ℃, and pressure is normal pressure.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 90106490 CN1062854A (en) | 1990-12-29 | 1990-12-29 | Hydrogen sulfide and ammonia process for recovering mixing gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 90106490 CN1062854A (en) | 1990-12-29 | 1990-12-29 | Hydrogen sulfide and ammonia process for recovering mixing gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1062854A true CN1062854A (en) | 1992-07-22 |
Family
ID=4880129
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 90106490 Pending CN1062854A (en) | 1990-12-29 | 1990-12-29 | Hydrogen sulfide and ammonia process for recovering mixing gas |
Country Status (1)
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|---|---|
| CN (1) | CN1062854A (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100404105C (en) * | 2005-10-27 | 2008-07-23 | 陈明功 | Technique for removing CO2 from flue-gas |
| CN102641657A (en) * | 2011-02-18 | 2012-08-22 | 上海离岛电子新材料有限公司 | Method for strictly controlling discharge of ammonia-containing tail gas in the ammonium salt production and improving ammonium salt output using the tail gas |
| CN102895864A (en) * | 2012-10-30 | 2013-01-30 | 黄立维 | Method and device for absorbing and purifying harmful gas through electrochemical oxidation |
| CN103041679A (en) * | 2013-01-15 | 2013-04-17 | 美景（北京）环保科技有限公司 | Waste gas treatment system of acid gas containing ammonia |
| CN103638775A (en) * | 2013-12-09 | 2014-03-19 | 深圳市芭田生态工程股份有限公司 | Treatment method of water vapor containing fluoride ammonia |
| CN107519755A (en) * | 2017-10-19 | 2017-12-29 | 张家港市艾尔环保工程有限公司 | Multi-functional washing absorption plant |
| CN107684814A (en) * | 2017-10-23 | 2018-02-13 | 张家港市艾尔环保工程有限公司 | The method for removing inorganic gas in removing exhaust gas |
| CN107754602A (en) * | 2017-11-21 | 2018-03-06 | 湖南内特环保科技有限公司 | Containing ammonia and ammonium sulfide waste gas processing method and system |
| CN111252839A (en) * | 2020-01-18 | 2020-06-09 | 河北荣特化工股份有限公司 | Novel process for treating hydrogenation type waste water and waste gas |
| CN112984373A (en) * | 2019-12-17 | 2021-06-18 | 大庆金星燃气股份有限公司 | Liquefied petroleum gas residual liquid recovery system and method |
| CN115212706A (en) * | 2022-07-11 | 2022-10-21 | 江苏楷鼎环保装备有限公司 | Tail gas treatment method for sulfur black dye production system |
-
1990
- 1990-12-29 CN CN 90106490 patent/CN1062854A/en active Pending
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100404105C (en) * | 2005-10-27 | 2008-07-23 | 陈明功 | Technique for removing CO2 from flue-gas |
| CN102641657A (en) * | 2011-02-18 | 2012-08-22 | 上海离岛电子新材料有限公司 | Method for strictly controlling discharge of ammonia-containing tail gas in the ammonium salt production and improving ammonium salt output using the tail gas |
| CN102895864A (en) * | 2012-10-30 | 2013-01-30 | 黄立维 | Method and device for absorbing and purifying harmful gas through electrochemical oxidation |
| CN103041679A (en) * | 2013-01-15 | 2013-04-17 | 美景（北京）环保科技有限公司 | Waste gas treatment system of acid gas containing ammonia |
| CN103041679B (en) * | 2013-01-15 | 2015-02-04 | 美景（北京）环保科技有限公司 | Waste gas treatment system of acid gas containing ammonia |
| CN103638775A (en) * | 2013-12-09 | 2014-03-19 | 深圳市芭田生态工程股份有限公司 | Treatment method of water vapor containing fluoride ammonia |
| CN107519755A (en) * | 2017-10-19 | 2017-12-29 | 张家港市艾尔环保工程有限公司 | Multi-functional washing absorption plant |
| CN107684814A (en) * | 2017-10-23 | 2018-02-13 | 张家港市艾尔环保工程有限公司 | The method for removing inorganic gas in removing exhaust gas |
| CN107754602A (en) * | 2017-11-21 | 2018-03-06 | 湖南内特环保科技有限公司 | Containing ammonia and ammonium sulfide waste gas processing method and system |
| CN112984373A (en) * | 2019-12-17 | 2021-06-18 | 大庆金星燃气股份有限公司 | Liquefied petroleum gas residual liquid recovery system and method |
| CN111252839A (en) * | 2020-01-18 | 2020-06-09 | 河北荣特化工股份有限公司 | Novel process for treating hydrogenation type waste water and waste gas |
| CN115212706A (en) * | 2022-07-11 | 2022-10-21 | 江苏楷鼎环保装备有限公司 | Tail gas treatment method for sulfur black dye production system |
| CN115212706B (en) * | 2022-07-11 | 2023-08-18 | 江苏楷鼎环保装备有限公司 | Tail gas treatment method for sulfur black dye production system |
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