CN101069806A - Process for removing hydrogen sulphide from carbon bisulfide waste gas and apparatus therefor - Google Patents
Process for removing hydrogen sulphide from carbon bisulfide waste gas and apparatus therefor Download PDFInfo
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- CN101069806A CN101069806A CN 200710010718 CN200710010718A CN101069806A CN 101069806 A CN101069806 A CN 101069806A CN 200710010718 CN200710010718 CN 200710010718 CN 200710010718 A CN200710010718 A CN 200710010718A CN 101069806 A CN101069806 A CN 101069806A
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- absorption liquid
- gas
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- type absorber
- hydrogen sulphide
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Abstract
The present invention relates to a carbon disulfide waste gas dehydrosulfurization process and its dehydrosulfurization equipment. It is mainly characterized by that said dehydrosulfurization adopts tubular absorber with spray head in stead of general spray-type absorption tower, so that the H2S removing rate can be up to 99.5%-100%.
Description
Technical field
The present invention relates to a kind of industrial gasses processing method, relate to the processing method of hydrogen sulfide specifically.
Background technology
Usually contain hydrogen sulfide in industrial gasses, the waste gas carbon disulfide during for example coal gas, viscose rayon are produced all pollutes environment when using gases or combustion gas, and especially the discharge amount of exhaust gas of viscose rayon production is big, and main component is to contain CS
2And H
2The gas of S, wherein CS
2Account for 80%, H
2S is 20%, and the annual viscose rayon of producing of China has reached about 1,000,000 tons, need use CS
2About about 300,000 tons, wherein remove the CS that reclaims with condensation method at present
2About 30%～40%, more than 20 ten thousand tons CS still has an appointment
2And H
2S is by high altitude discharge or uncontrollable discharge.To this, many strong-willed persons did research, existing multiple improvement method, and conclusion gets up to have following several:
Alkali absorb method, alkali absorb method are the most formal methods of a specified duration of history.Adopted tall and big absorption tower or eluting column, this method capital construction investment is big in the past, the big and H of alkali consumption
2S removes not thoroughly.
Firing method mainly is to utilize CS
2And H
2All contain S in the S molecule, can form SO after the burning
2, can be recycled into H
2SO
4Or be reacted into Na through NaOH
2SO
3Deng being reclaimed.Firing method needs waste gas that finite concentration and stability are arranged, otherwise combustion instability, this difficult at home accomplishing.Corrosion such as instrumentation simultaneously is bigger, and the value of the product of recovery is lower, to the recovery of can't burning of the waste gas of low concentration.
Biological harnessing method is that to utilize microorganism be the nutrients decomposition of eating to the decomposition of polluter or with it, reaches the purification purpose.Bioanalysis is newer in the world method, and US and European all has research and development the nineties in eighties of last century.Mainly be that one deck microorganism covering is arranged, work as CS
2And H
2S by the time, just decomposed by Institute of Micro-biology, become the mud of sulfide, be embedded in underground or be used as a kind of sulphur resource.This method control is tighter, and operating cost all will drop into no byproduct income every year.
Catalysis method adopts catalyst to take off H
2S is based on claus reaction substantially, the employing organic solvent that has, carry out liquid phase reactor, reclaim sulphur, this method complicated operation, expense height, perhaps under gas phase condition, carry out, the sulphur that this method produces sticks to catalyst surface, reduces catalyst activity, thereby the regeneration of catalyst, catalyst directly influence the processing cost recovery service life.
Have not yet to see the method report of small investment, removal hydrogen sulfide treatment that operating cost is low.
Summary of the invention
The present invention proposes a kind of invest little, that operating cost is low depriving hydrogen sulphide process and treating apparatus according to the defective that existing hydrogen sulfide treatment method exists.
Finish the foregoing invention purpose, the concrete technical measures of being taked are: the simplest with alkali absorb method in existing depriving hydrogen sulphide method, to implement easily, and alkali absorb method mainly is to absorb H with alkali
2S, its reaction equation is as follows:
NaOH+H
2S → NaHS+H
2O or 2NaOH+H
2S → Na
2S+2H
2O
Carbon disulfide exhuast gas desulfurization hydrogen process of the present invention and depriving hydrogen sulphide device are:
1 absorption liquid preparation: be made into the absorption liquid that contains NaOH mass concentration 50～200g/L
2 depriving hydrogen sulphides: absorption liquid atomizes it through fog-spray nozzle under the pressure of 0.2MPa～0.5MPa in the tubular type absorber, and drop＜200 μ m is handled gas and then sent into the tubular type absorber with 25～100m/s
3 absorption liquids reclaim: the gaseous mixture after the desulfurization is through keeping off the separator gas-liquid separation again, and absorption liquid enters the mixing flow container, and devulcanization hydrogen is delivered to basin through keeping off the separator gas outlet again
Absorption liquid is viscose rayon production stoste workshop hydraulic fluid or maceration extract or NaOH
Flow of process air speed is to select to determine according to treating capacity and fog-spray nozzle quantity.
The H that takes off of the present invention
2The S process is to adopt the tubular type absorber to replace common spray column, its structure of tubular type absorber is: on tubular type absorber body the absorption liquid feed pipe is housed, on the absorption liquid feed pipe in pipe fog-spray nozzle is housed, on body, is shaped on the outlet of exhaust gas inlet and sweet gas.
Tubular type absorber installation quantity and tubular type absorber length, diameter, fog-spray nozzle quantity are selected according to the exhaust-gas treatment amount.
Beneficial effect of the present invention: carbon disulfide exhuast gas desulfurization hydrogen process of the present invention and depriving hydrogen sulphide device, owing in depriving hydrogen sulphide technology, adopt the tubular type absorber to replace common spray absorber, H
2S can remove 99.5%～100%, and has reduced capital construction investment, and operating cost is low.Particularly handle the carbon disulfide waste gas of viscose rayon, depriving hydrogen sulphide uses hydraulic fluid or spent lye not only to reduce processing cost but also helps hemicellulose in the balance immersion liquid, saves the construction cost and the operating cost of hydraulic fluid dialysis, takes off H
2Absorption liquid behind the S all is better than the conventional inorganic agent that uses and reduces operating cost as refining desulfuration agent and its effect of zinc-containing water inorganic agent of viscose rayon.CS behind absorption, desorption
2But the return system has reduced CS
2Consumption, improve viscose rayon production economic benefit.
Description of drawings
Fig. 1 is a depriving hydrogen sulphide process flow diagram of the present invention
Fig. 2 is a tubular type absorber structure schematic diagram of the present invention
101 blower fan 102-1 1# tubular type absorber 102-2 2# tubular type absorber 103-1 103-2 keep off separator 104-1 104-2 mixing flow container 105 circulating pumps 106 absorption liquid blend tanks again among the figure
The outlet of 1 body, 2 absorption liquid feed pipes, 3 fog-spray nozzles, 4 exhaust gas inlet, 5 sweet gas
The specific embodiment
The tail gas that the tail gas that embodiment 1 spinning-drawing machine to the exhaust and the plasticizing-bath condensation of boundling reclaimed and the acid bath degassing are reclaimed is sent into long 10m with 25m/s speed by 1# tubular type absorber 102-1 exhaust gas inlet 4 through blower fan 101, the 1# tubular type absorber 102-1 of diameter 50mm, structure is seen accompanying drawing 2,6 groups of absorption liquid feed pipes 2 are housed in body 1,1 fog-spray nozzle 3 (fog-spray nozzle is the commercial goods) is housed on every group of absorption liquid feed pipe 2, the absorption liquid feed pipe connects absorption liquid circulating pump 105, circulating pump 105 imports connect and mix flow container 104-2 discharging opening, 1# tubular type absorber 102-1 sweet gas outlet 5 connections keep off separator 103-1 import again, keep off the exhaust gas inlet 4 of separator 103-1 waste gas outlet connection 2# tubular type absorber 102-2 again, with stoste workshop hydraulic fluid, be made into the liquid of newly joining after absorption liquid is delivered to 2# tubular type absorber 102-2 earlier that contains NaOH 50g/L at absorption liquid blend tank 106 and enter mixing flow container 104-2 through keeping off separator 103-2 again.This absorption liquid is delivered to 1# tubular type absorber 102-1 through circulating pump 105 with 0.2MPa, and absorption liquid is through fog-spray nozzle 3 atomizing, droplet below 200 μ m, the H in the waste gas
2S and alkali effect also enter multiple retaining separator 103-1 gas-liquid separation with absorption liquid and enter and mix flow container 104-1, as contained NaHS and Na
2S reaches 2～7g/L and delivers to refining and sewage-farm use, takes off H
2The waste gas of S enters 2# tubular type absorber 102-2, and 2# tubular type absorber is identical with 1# tubular type absorber, sends into 1# tubular type absorber 102-1 by the absorption liquid that 2# tubular type absorber 102-2 discharges, and has realized recycling.Through bi-level treatment, (see figure 1) can make H
2S removes 99.5%～100%, has also washed acid mist etc. simultaneously.
Below according to a conventional method will be by the H that takes off that keeps off separator 103-2 outlet discharge again
2S waste gas makes the relative humidity of waste gas be lower than 60% through dehumidifier and heater oven dry, delivers to absorbent charcoal adsorption tank again, to CS
2Adsorb.Gas after absorption contains CS
2Be lower than 50mg/kg (on average about 20mg/kg), H
2S content is lower than 1mg/kg, directly high altitude discharge.Desorption then, desorption process is first inflated with nitrogen, back steam stripping.
From the gas that charcoal canister blows out, contain water vapour and CS
2Gas, it is sent to the condensation of multi-stage condensing device, and steam condensation is before this got off, and is gas cooled again, is CS at last
2Gas is condensed into liquid.The liquid of condensation separates through knockout drum, liquid CS
2Deliver to CS
2Basin, and the remaining CS that is not condensed
2Gas is sent gas recovery system again back to and is reclaimed.
The tail gas that the tail gas that embodiment 2 spinning-drawing machines to the exhaust and the plasticizing-bath condensation of boundling reclaimed and the acid bath degassing are reclaimed is sent into long 20m with 100m/s speed by 1# tubular type absorber 102-1 exhaust gas inlet 4 through blower fan 101, the 1# tubular type absorber 102-1 of diameter 300mm, structure is seen accompanying drawing 2,10 groups of absorption liquid feed pipes 2 are housed in body 1,6 fog-spray nozzles 3 (fog-spray nozzle is the commercial goods) are housed on every group of absorption liquid feed pipe 2, absorption liquid feed pipe 2 connects absorption liquid circulating pump 105, circulating pump 105 imports connect and mix flow container 104-2 discharging opening, 1# tubular type absorber 102-1 sweet gas outlet 5 connections keep off separator 103-1 import again, keep off the exhaust gas inlet 4 of separator 103-1 waste gas outlet connection 2# tubular type absorber 102-2 again, with stoste workshop maceration extract, be made at absorption liquid blend tank 106 and contain hydrogen-oxygen and enter and mix flow container 104-2 through keeping off separator 103-2 again than the liquid of newly joining after absorption liquid is delivered to 2# tubular type absorber 102-2 earlier of sodium 150g/L.This absorption liquid is delivered to 1# tubular type absorber 102-1 through circulating pump 105 with 0.5MPa, and absorption liquid is through fog-spray nozzle 3 atomizing, droplet below 200 μ m, the H in the waste gas
2S and alkali effect also enter multiple retaining separator 103-1 gas-liquid separation with absorption liquid and enter and mix flow container 104-1, as contained NaHS and Na
2S reaches 2～7g/L and delivers to refining and sewage-farm use, takes off H
2The waste gas of S enters 2# tubular type absorber 102-2, and 2# tubular type absorber is identical with 1# tubular type absorber, sends into 1# tubular type absorber 102-1 by the absorption liquid that 2# tubular type absorber 102-2 discharges, and has realized recycling.Through bi-level treatment, (see figure 1) can make H
2S removes 99.5%～100%, has also washed acid mist etc. simultaneously.
The tail gas that the tail gas that embodiment 3 spinning-drawing machines to the exhaust and the plasticizing-bath condensation of boundling reclaimed and the acid bath degassing are reclaimed is sent into long 40m with 50m/s speed by the exhaust gas inlet 4 of 2# tubular type absorber 102-2 through blower fan 101, the 2# tubular type absorber 102-2 of diameter 700mm is (with reference to Fig. 1, save 1# tubular type absorber and corollary equipment), 26 groups of absorption liquid feed pipes 2 are housed in body 1, every group of absorption liquid feed pipe 2 is equipped with 10 fog-spray nozzles 3, absorption liquid feed pipe 2 connects absorption liquid blend tank 106, be made into the absorption liquid that contains NaOH 200g/L at absorption liquid blend tank 106 with NaOH and deliver to tubular type absorber 102-2 with 0.3MPa, absorption liquid is through fog-spray nozzle 3 atomizings, droplet below 200 μ m, the H in the waste gas
2S and alkali effect, the gaseous mixture after the desulfurization is through keeping off separator 103-2 gas-liquid separation again, and absorption liquid enters and mixes flow container 104-2, and waste gas is delivered to CS through keeping off separator 103-2 gas vent again
2Basin.Through handling, can make H
2S removes 99.5%～100%.
Claims (3)
1 one kinds of carbon disulfide exhuast gas desulfurization hydrogen processes and depriving hydrogen sulphide device, its depriving hydrogen sulphide process is characterized in that:
1 absorption liquid preparation: be made into the absorption liquid that contains NaOH mass concentration 5～20g/L
2 depriving hydrogen sulphides: absorption liquid atomizes it through fog-spray nozzle under the pressure of 0.2MPa～0.5MPa in the tubular type absorber, and drop＜200 μ m is handled gas and then sent into the tubular type absorber with 25～100m/s
3 absorption liquids reclaim: the gaseous mixture after the desulfurization is through keeping off the separator gas-liquid separation again, and absorption liquid enters the mixing flow container, and devulcanization hydrogen is delivered to basin through keeping off the separator gas outlet again
2 by claim 1 carbon disulfide exhuast gas desulfurization hydrogen process and depriving hydrogen sulphide device, said absorption liquid preparation, and it is characterized in that: absorption liquid is viscose rayon production stoste workshop hydraulic fluid or maceration extract or NaOH.
3 by claim 1 carbon disulfide exhuast gas desulfurization hydrogen process and depriving hydrogen sulphide device, said depriving hydrogen sulphide device is characterized in that: on tubular type absorber body the absorption liquid feed pipe is housed, on the absorption liquid feed pipe in pipe fog-spray nozzle is housed, on body, is shaped on the outlet of exhaust gas inlet and sweet gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2007100107189A CN100450586C (en) | 2007-03-26 | 2007-03-26 | Process for removing hydrogen sulphide from carbon bisulfide waste gas and apparatus therefor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2007100107189A CN100450586C (en) | 2007-03-26 | 2007-03-26 | Process for removing hydrogen sulphide from carbon bisulfide waste gas and apparatus therefor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101069806A true CN101069806A (en) | 2007-11-14 |
| CN100450586C CN100450586C (en) | 2009-01-14 |
Family
ID=38897319
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2007100107189A Expired - Fee Related CN100450586C (en) | 2007-03-26 | 2007-03-26 | Process for removing hydrogen sulphide from carbon bisulfide waste gas and apparatus therefor |
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|---|---|
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101274203B (en) * | 2007-12-27 | 2011-06-15 | 唐山三友集团兴达化纤有限公司 | Method for removing carbon disulfide gas in production process of viscose fiber |
| CN102743969A (en) * | 2012-07-16 | 2012-10-24 | 北京绿创环保设备股份有限公司 | Treatment method for mixed waste gas containing H2S and CS2 |
| CN104096467A (en) * | 2014-06-05 | 2014-10-15 | 浙江南化防腐设备有限公司 | Liquid strong oxidant atomization desulphurization system and method |
| CN106390673A (en) * | 2016-11-30 | 2017-02-15 | 成都丽雅纤维股份有限公司 | System for recovering waste gas in production of viscose |
| CN107715620A (en) * | 2017-11-18 | 2018-02-23 | 江苏长虹智能装备集团有限公司 | A kind of active carbon absorption technology |
| CN108166105A (en) * | 2018-02-12 | 2018-06-15 | 赛得利（福建）纤维有限公司 | A kind of viscose rayon post processing production system and its processing method |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2173356Y (en) * | 1993-06-03 | 1994-08-03 | 苏文贤 | Dust-removing desulfurate dehydrogenate device for funnel exhanting gas |
| CN2188701Y (en) * | 1993-12-27 | 1995-02-01 | 西安交通大学 | Desulfurizing and denitrating dust collector |
| CN2278519Y (en) * | 1996-09-28 | 1998-04-15 | 于云杰 | Smoke purifier |
| US5795523A (en) * | 1996-10-30 | 1998-08-18 | Alfacel S.A. | Method for treatment of CS2 and H2 S emissions during viscose regeneration |
| CN2338623Y (en) * | 1998-09-30 | 1999-09-15 | 许屹磊 | Device for removing sulphur for coal biler |
-
2007
- 2007-03-26 CN CNB2007100107189A patent/CN100450586C/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101274203B (en) * | 2007-12-27 | 2011-06-15 | 唐山三友集团兴达化纤有限公司 | Method for removing carbon disulfide gas in production process of viscose fiber |
| CN102743969A (en) * | 2012-07-16 | 2012-10-24 | 北京绿创环保设备股份有限公司 | Treatment method for mixed waste gas containing H2S and CS2 |
| CN104096467A (en) * | 2014-06-05 | 2014-10-15 | 浙江南化防腐设备有限公司 | Liquid strong oxidant atomization desulphurization system and method |
| CN104096467B (en) * | 2014-06-05 | 2016-06-29 | 浙江南化防腐设备有限公司 | A kind of liquid strong oxidizing agent atomization desulphurization system and method |
| CN106390673A (en) * | 2016-11-30 | 2017-02-15 | 成都丽雅纤维股份有限公司 | System for recovering waste gas in production of viscose |
| CN107715620A (en) * | 2017-11-18 | 2018-02-23 | 江苏长虹智能装备集团有限公司 | A kind of active carbon absorption technology |
| CN108166105A (en) * | 2018-02-12 | 2018-06-15 | 赛得利（福建）纤维有限公司 | A kind of viscose rayon post processing production system and its processing method |
| CN108166105B (en) * | 2018-02-12 | 2023-05-09 | 赛得利（福建）纤维有限公司 | Viscose fiber post-treatment production system and treatment method thereof |
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| Publication number | Publication date |
|---|---|
| CN100450586C (en) | 2009-01-14 |
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Granted publication date: 20090114 Termination date: 20110326 |