CN1088131A - Remove high-concentration hydrogen sulfide and dithiocarbonic anhydride waste gas and reclaim the method and system of sulphur - Google Patents
Remove high-concentration hydrogen sulfide and dithiocarbonic anhydride waste gas and reclaim the method and system of sulphur Download PDFInfo
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- CN1088131A CN1088131A CN 93117722 CN93117722A CN1088131A CN 1088131 A CN1088131 A CN 1088131A CN 93117722 CN93117722 CN 93117722 CN 93117722 A CN93117722 A CN 93117722A CN 1088131 A CN1088131 A CN 1088131A
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- waste gas
- absorption tower
- reactive tank
- sulphur
- high density
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Abstract
A kind of high density H that removes
2S and CS
2Waste gas also reclaims the method and system of deflated voluntarily of sulphur, mainly is made up of secondary or the spray absorption tower more than the secondary, reactive tank, jet regeneration tank etc.Desulfuration solution is inwardly sprayed from the spray absorption tower top, with high density H
2S and CS
2Waste gas sucks, H
2S and CS
2Be absorbed, all the other waste gas are brought into its reactive tank; This waste gas is sucked by back one-level spray absorption tower again, repeats said process; The rest may be inferred, last emptying.The present invention replaces vacuum fan with spray liquid flow, and the danger of blast greatly descends, and operational management is convenient; To H
2S, CS
2Concentration height and the big situation of tolerance fluctuation also adapt to.
Description
The invention belongs to and remove H in the waste gas
2S, CS
2, and the method and system of recovery sulphur.
Always produce dithiocarbonic anhydride with electric furnace process, the sulfur method of its tail gas is: absorb H with sodium hydroxide solution in the absorption tower
2S makes sodium sulphite, reclaims CS at the adsorption tower internal adsorption
2; Or in stirring the absorption still, absorb H with milk of lime
2S, adding calcium hydroxide reaction system thiocarbamide reclaims CS at the adsorption tower internal adsorption
2; Or absorb H with common liquid phase oxidation
2S, recovery sulphur reclaims CS at the adsorption tower internal adsorption
2, its flow process is, waste gas in the absorption tower with desulfuration solution convection current, H
2S is absorbed and brings reactive tank into, and reacted desulfuration solution is admitted to injector and flows to regeneration tank, and both are collectively referred to as jet regeneration tank, makes the oxidized regeneration of its catalyzer, separates with the sulphur foam, send the absorption tower to use again.The exhaust power that aforesaid method adopted is mechanical driver unit, and necessary exactissima diligentia is explosion-proof; Can not adapt to tail gas H
2S, CS
2High and the big situation of exhausted air quantity fluctuation range of concentration, the operational management inconvenience.
The purpose of this invention is to provide a kind of high density H that removes
2S, CS
2Gas also reclaims the method and system of deflated voluntarily of sulphur.
The objective of the invention is to realize by following method: desulfuration solution is sent into secondary or the spray absorption tower more than the secondary by liquor pump, is sprayed downwards by its top, produces negative pressure around the desulfuration solution injection stream, with high density H in the waste pipe
2S and CS
2Waste gas sucks first step spray absorption tower, H
2S and CS
2The desulfuration solution that is ejected absorbs, and unabsorbed waste gas therewith is brought into the reactive tank of first step spray absorption tower; Waste gas in first reactive tank is inhaled into second stage spray absorption tower again, unabsorbed H
2S and CS
2The desulfuration solution that is ejected again absorbs once more, and remaining waste gas therewith is brought into the reactive tank of second stage spray absorption tower again; The rest may be inferred, the waste gas in last reactive tank, directly discharging or through adsorption tower absorption CS
2The back discharging.This waste gas is difficult for blasting for discharging voluntarily.Enter the reacted desulfuration solution of reactive tank, send into injector, enter the regeneration tank oxidation regeneration through liquor pump; The catalyzer of desulfuration solution is oxidized regeneration in jet regeneration tank, after breaking away from the sulphur foam, sends spray absorption tower back to by liquor pump again and use.High density H
2S and CS
2Waste gas can make it by being lower than subzero 14 ℃ condenser, condensation portion CS earlier before being inhaled into first step spray absorption tower
2
Custom-designed for implementing aforesaid method, remove high density H
2S and CS
2The system of waste gas and recovery sulphur, be provided with the above spray absorption tower of secondary or secondary, every grade of spray absorption tower top all has inlet pipe, the reactive tank that a correspondence is all arranged below it, each reactive tank top all has a vapor pipe, the order that connects the inlet pipe of back one-level spray absorption tower according to the vapor pipe of the reactive tank in front is connected, the inlet pipe of first step spray absorption tower connects waste pipe, the vapor pipe of last reactive tank is received outdoor or adsorption tower, and the vapor pipe of adsorption tower is received outdoor.Have pipe to lead to jet regeneration tank through liquor pump below the reactive tank, regeneration tank has pipe to lead to spray absorption tower through another liquor pump.Before the inlet pipe and waste pipe of first step spray absorption tower, can be provided with one and be lower than and have CS below subzero 14 ℃ its
2The condenser of liquid storing tank.The following of each reactive tank can connect each other.
The method and system that the injection that the present invention adopts absorbs, the negative pressure that produces with the desulfuration solution that sprays replaces vacuum fan, not only bleeds but also absorb, and has improved production security, and the danger of blast greatly reduces, and operational management is convenient; Before waste gas is inhaled into first step spray absorption tower, reclaim CS owing to set up the one-level condensation
2Device, condensable about 40% CS
2, basic non-wastewater discharge can not produce new source of pollution; To H
2S, CS
2The situation that concentration height and exhausted air quantity fluctuation range are big also is suitable for; Technical economic benefit is good, because the sulphur products C S that reclaims
2With sulphur be respectively its product and raw material.
The invention will be further described below in conjunction with accompanying drawing.
Fig. 1 is the synoptic diagram of a kind of two-stage injection absorption system of the present invention.
With reference to Fig. 1, what present embodiment adopted is that two-stage injection is absorbed as example.Be built-in with the desulfuration solution of HP=8.7, wherein Na at reactive tank D and jet regeneration tank E+F
2CO
3=0.5g/l, NaHCO
3=2.4g/l, desulfurization catalyst THS=0.075g/l.Handle electric furnace process and produce the tail gas of dithiocarbonic anhydride, tolerance is from 7～20m
3/ h, concentration is: H
2S10～1000g/Nm
3; CS
250～1000g/Nm
3Offgas duct is connected with subzero 15 ℃ condenser A, meet liquid storing tank C below the condenser A, condenser A vapor pipe connects the inlet pipe of first step spray absorption tower B, connect its reactive tank D below the first step spray absorption tower B, vapor pipe connects the inlet pipe of second stage spray absorption tower B above the reactive tank D, connect each other below its reactive tank of the connection D below the spray absorption tower B of the second stage, two reactive tank D, and by liquor pump P
1Connect with injector F.Be regeneration tank E below the injector F, its lower end also places regeneration tank E, and the side of injector F mouth spray end is provided with air inlet port, and injector F and regeneration tank E are called jet regeneration tank E+F together.Regeneration tank E is connected with sulphur separator G near top side, and regeneration tank E side is by liquor pump P
2Connect with spray absorption tower B top.Vapor pipe above second reactive tank D inserts gac and absorbs attached tower H, and the escape pipe of activated carbon adsorber H is received outdoor.
Working process: connect power supply, liquor pump P
1, P
2Start working, desulfuration solution is by liquor pump P
2Deliver to the top of spray absorption tower B, in it, spray, at this moment around the jetting fluid outflow, produce negative pressure, the waste gas in the offgas duct is sucked condenser A condensation, make portion C S
2Become liquid, flow to storage tanks C.The waste gas that is not condensed is sucked into first step spray absorption tower B, along with jetting fluid enters reactive tank D, H
2S, CS
2Be desulfurized solution absorption simultaneously, and react.The waste gas that enters reactive tank D is inhaled into second stage spray absorption tower B again, along with spray liquid flow enters its corresponding reactive tank D, is not absorbed most H in the first step
2S, CS
2Be absorbed once more and react.After this two-stage spray absorption tower B absorbed, its purification efficiency reached: H
2S99.97%, CS
296.01%.Because waste gas constantly is brought into second reactive tank D, so waste gas will enter activated carbon adsorber H by its vapor pipe voluntarily, again to CS
2Adsorb, the waste gas after the absorption leads to outdoor emptying by its vapor pipe.Also can directly lead to outdoor emptying to the vapor pipe of second reactive tank D.Absorbed H
2The desulfuration solution of S is by solution pump P
1Deliver to injector F and spray in regeneration tank E and go, the negative pressure that sprayed solution produces is brought air into regeneration tank E, makes the oxidized regeneration of catalyzer THS of desulfuration solution simultaneously, with the sulphur foam separation, again by solution pump P
2Deliver to spray absorption tower B top and spray absorption.The sulphur foam that is separated enters sulphur separator G, tells sulphur cream and removes molten sulphur.
Claims (8)
1, a kind of high density H that removes
2S and CS
2Waste gas also reclaims the method for sulphur, comprising:
1) reacted desulfuration solution in reactive tank is sent into injector through liquor pump, enters regeneration tank regeneration;
2) catalyzer of desulfuration solution after the oxidized regeneration, breaks away from the sulphur foam in jet regeneration tank, is used to the absorption tower by liquid pumping again;
3) it is characterized in that: desulfuration solution is delivered to secondary or the spray absorption tower more than the secondary respectively by liquor pump, is sprayed downwards by its top, with high density H
2S and CS
2Waste gas sucks first step spray absorption tower, wherein H
2S and CS
2The desulfuration solution that is ejected absorbs, and unabsorbed waste gas therewith is brought into its reactive tank; Waste gas in reactive tank is inhaled into second stage spray absorption tower again, unabsorbed H
2S and CS
2The desulfuration solution that is ejected again absorbs once more, and remaining waste gas therewith is brought into second reactive tank again; The rest may be inferred, and the waste gas in last reactive tank directly discharges.
2, the high density H that removes according to claim 1
2S and CS
2Waste gas also reclaims the method for sulphur, it is characterized in that: high density H
2S and CS
2Waste gas can make it by being lower than subzero 14 ℃ condenser, condensation portion CS earlier before being inhaled into first step spray absorption tower
2
3, the high density H that removes according to claim 1 and 2
2S and CS
2Waste gas also reclaims the method for sulphur, it is characterized in that: the waste gas in described last reactive tank can be again through adsorption tower absorption residue CS
2Back emptying.
4, for implementing the custom-designed high density H that removes of the described method of claim 1
2S and CS
2Waste gas also reclaims the system of sulphur, comprises absorption tower, reactive tank [D], jet regeneration tank [E+F], liquor pump [P
1, P
2], it is characterized in that: described absorption tower is to be made of secondary or the spray absorption tower more than the secondary [B], every grade of spray absorption tower [B] top all has inlet pipe, the described reactive tank [D] that a correspondence is all arranged below it, each reactive tank [D] top all has vapor pipe, the order that connects the inlet pipe of back one-level spray absorption tower [B] according to the vapor pipe of the reactive tank in front [D] is connected, the inlet pipe of first step spray absorption tower [B] connects waste pipe, and the vapor pipe of last reactive tank [D] is received outdoor.
5, the high density H that removes according to claim 4
2S and CS
2Waste gas also reclaims the system of sulphur, it is characterized in that: between the inlet pipe and waste pipe of described first step spray absorption tower [B], can be provided with one and be lower than subzeroly 14 ℃, have the condenser [A] of liquid storing tank [C] below it.
6, according to claim 4 or the 5 described high density H that remove
2S and CS
2Waste gas also reclaims the system of sulphur, and it is characterized in that: the following of described reactive tank [D] can connect each other.
7, according to claim 4 or the 5 described high density H that remove
2S and CS
2Waste gas also reclaims the system of sulphur, and it is characterized in that: the vapor pipe of described last reactive tank [D] can insert an adsorption tower [H], and the vapor pipe of adsorption tower [H] is received outdoor.
8, the high density H that removes according to claim 6
2S and CS
2Waste gas also reclaims the system of sulphur, and it is characterized in that: the vapor pipe of described last reactive tank [D] can insert an adsorption tower [H], and the vapor pipe of adsorption tower [H] is received outdoor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 93117722 CN1088131A (en) | 1993-09-12 | 1993-09-12 | Remove high-concentration hydrogen sulfide and dithiocarbonic anhydride waste gas and reclaim the method and system of sulphur |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 93117722 CN1088131A (en) | 1993-09-12 | 1993-09-12 | Remove high-concentration hydrogen sulfide and dithiocarbonic anhydride waste gas and reclaim the method and system of sulphur |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1088131A true CN1088131A (en) | 1994-06-22 |
Family
ID=4992150
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 93117722 Pending CN1088131A (en) | 1993-09-12 | 1993-09-12 | Remove high-concentration hydrogen sulfide and dithiocarbonic anhydride waste gas and reclaim the method and system of sulphur |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1088131A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101791517A (en) * | 2010-04-08 | 2010-08-04 | 北京至清时光环保工程技术有限公司 | Method for recycling sulfur from acid gases containing hydrogen sulfide |
| CN101890295A (en) * | 2010-08-04 | 2010-11-24 | 姜辉 | Method and device for regenerating desulphurization mother solution |
| CN102153053A (en) * | 2010-11-20 | 2011-08-17 | 辽宁瑞兴化工集团有限公司 | Methods for purifying and comprehensively utilizing hydrogen sulfide byproduct during production of carbon disulfide by methane method |
| CN101687141B (en) * | 2007-04-12 | 2012-09-05 | Cefco有限责任公司 | Process and apparatus for carbon capture and elimination of multi-pollutants in flue gas from hydrocarbon fuel sources and recovery of multiple by-products |
| CN103285722A (en) * | 2013-06-06 | 2013-09-11 | 浙江晋巨化工有限公司 | Highly sulfur-containing pressurized shifted gas wet-process desulphurization technique |
| CN104258662A (en) * | 2014-09-27 | 2015-01-07 | 安徽金禾实业股份有限公司 | Sulfur melting waste gas recycling method |
| CN109967129A (en) * | 2017-12-28 | 2019-07-05 | 柏美迪康环境科技（上海）股份有限公司 | A kind of composite catalyst and its preparation method and application removing stench and resourcebility recycling sulfur-containing compound |
-
1993
- 1993-09-12 CN CN 93117722 patent/CN1088131A/en active Pending
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101687141B (en) * | 2007-04-12 | 2012-09-05 | Cefco有限责任公司 | Process and apparatus for carbon capture and elimination of multi-pollutants in flue gas from hydrocarbon fuel sources and recovery of multiple by-products |
| CN101791517A (en) * | 2010-04-08 | 2010-08-04 | 北京至清时光环保工程技术有限公司 | Method for recycling sulfur from acid gases containing hydrogen sulfide |
| CN101791517B (en) * | 2010-04-08 | 2012-05-23 | 北京至清时光环保工程技术有限公司 | Method for recycling sulfur from acid gases containing hydrogen sulfide |
| CN101890295A (en) * | 2010-08-04 | 2010-11-24 | 姜辉 | Method and device for regenerating desulphurization mother solution |
| CN102153053A (en) * | 2010-11-20 | 2011-08-17 | 辽宁瑞兴化工集团有限公司 | Methods for purifying and comprehensively utilizing hydrogen sulfide byproduct during production of carbon disulfide by methane method |
| CN102153053B (en) * | 2010-11-20 | 2013-04-10 | 辽宁瑞兴化工集团有限公司 | Methods for purifying and comprehensively utilizing hydrogen sulfide byproduct during production of carbon disulfide by methane method |
| CN103285722A (en) * | 2013-06-06 | 2013-09-11 | 浙江晋巨化工有限公司 | Highly sulfur-containing pressurized shifted gas wet-process desulphurization technique |
| CN104258662A (en) * | 2014-09-27 | 2015-01-07 | 安徽金禾实业股份有限公司 | Sulfur melting waste gas recycling method |
| CN109967129A (en) * | 2017-12-28 | 2019-07-05 | 柏美迪康环境科技（上海）股份有限公司 | A kind of composite catalyst and its preparation method and application removing stench and resourcebility recycling sulfur-containing compound |
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| C01 | Deemed withdrawal of patent application (patent law 1993) | ||
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