CN104971599A - Acid gas reactor and processing technology - Google Patents
Acid gas reactor and processing technology Download PDFInfo
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- CN104971599A CN104971599A CN201410141493.0A CN201410141493A CN104971599A CN 104971599 A CN104971599 A CN 104971599A CN 201410141493 A CN201410141493 A CN 201410141493A CN 104971599 A CN104971599 A CN 104971599A
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Abstract
The invention discloses an acid gas reactor comprising a reaction pipeline and a liquid storage tank. One end of the reaction pipeline is a gas phase inlet and the other end of the reaction pipeline is a gas phase outlet. The reaction pipeline includes more than two reaction sections. The liquid storage tank includes a plurality of liquid storage zones of which the number is equal to that of the reaction sections. Each reaction section is communicated with a corresponding liquid storage zone and is provided with an absorption liquid inlet. A separating plate is arranged on the reaction pipeline between each two adjacent downcomers. An overflow plate is arranged on the liquid storage tank between each two adjacent downcomers. A reaction liquid outlet is arranged at a lower part of each liquid storage zone. The reaction liquid outlets are connected to the absorption liquid inlets through pipelines. The last liquid storage zone is provided with an alkali gas inlet. In the acid gas processing method, a NaOH solution is employed as an absorption liquid to treat the acid gas and produce sodium hydrosulfide. Compared with a reactor in the prior art, the acid gas reactor achieves both acid gas purification and pollutant recycling.
Description
Technical field
The present invention relates to a kind of sour gas reactor and treatment process, be applicable to sour gas field of gas purification, be particularly useful for containing the purification of sour gas such as sulfohydrate and the processing method of pollutant resources and device.
Background technology
Sour gas mainly comes from the devices such as sewage stripping, desulphurization of recycle hydrogen, dry gas desulfurization, main containing H in sour gas
2s, CO
2.The sour gas of the small-sized refinery of current major part adopts the processing method of post combustion emission substantially.This method causes the waste of resource on the one hand, brings huge pressure on the other hand, affect the development space of enterprise to environmental protection.For protection of the environment and guarantee making full use of of resource, recycling is carried out to the sour gas of small-sized refinery imperative.
The process of big-and-middle-sized sour gas, mainly utilizes sour gas to prepare sulphur, and that relatively commonly uses at present has two kinds of technologies, and one is secondary Claus+ tail gas hydrogenation reduction+solvent absorption process technology; Another kind is the LO-CAT technology of gas technology Products Co., Ltd of Merichem company of U.S. exploitation.
Secondary Claus+ tail gas hydrogenation reduction+solvent absorption technical matters maturation, stable operation, product sulphur steady quality, but due to long flow path, investment large, Claus technique can only process the sour gas of high concentration, usually as the H in unstripped gas
2when S volume fraction is less than 20%, device just not easily operates.Therefore, Claus technique is suitable for the device producing more than sulphur 5000t per year.
LO-CAT technique adopts the iron catalyst of multicomponent chelate to make H
2s is converted into elementary sulfur, H
2the removal efficiency of S is more than 99.9%.LO-CAT technique can be applicable to acid tolerance and fluctuate comparatively greatly and H
2s content 0 ~ 100% various operating modes, raw material condition of compatibility is wide in range, adapt to sour gas fluctuation change actual conditions.And LO-CAT liquid redox treatment scheme does not use any poisonous chemicals, and can not produce any harmful exhaust gas by-products, environmentally safe catalyst constantly can regenerate in processing procedure.But due to LO-CAT have that operating cost is high, sulfur purity and color and luster be slightly worse than claus process; and the sulphur particle produced in process of production meeting blockage phenomenon; therefore, LO-CAT technique economy poor (relative to secondary Claus+ tail gas hydrogenation reduction+solvent absorption technology) in the following scale of annual output sulphur 5000t.
For small-sized refinery, because acid tolerance is relatively little, adopt secondary Claus+ tail gas hydrogenation reduction+solvent absorption technical matters to there is long flow path, complicated operation, investment greatly, scale and benefit are poor.And adopt LO-CAT technology also to exist once to invest comparatively large, catalyst and the problem such as patent royalties are higher.
Sulfuric acid, as one of basic industrial chemicals, is widely used in all trades and professions.With the hydrogen sulfide contained in sour gas as raw material, many processing steps can be saved, namely save investment, again reduce cost, effectively can also recycle Sulphur ressource.Because small-sized sour gas tolerance is less, the industrial sulphuric acid of low concentration can only be produced, can not the higher oleum of productive value, economic benefit is not high, simultaneously, due to sulfuric acid transport, store all acquire a certain degree of difficulty, therefore, the market demand stable near oil plant be limit its development key factor.
Less for the total tolerance of small-sized sour gas, the new desulfurization process that investment is less can be adopted, by H
2s reclaims and prepares sulphite, first sour gas is carried out burning and generates SO
2, then send into absorption tower and carry out chemical absorbing generation sulfite solution, then solution and alkaline absorbent are reacted, prepare sulphite fluid product, or generate sulphite crystal, be prepared into sulphite solid product through operations such as separation, dryings.This device flow process is shorter, reaction is simple, operating flexibility is large, the impact of small-sized sour gas fluctuation on production process can be adapted to, solid or fluid product is produced by selecting different operations, select different absorbents can produce dissimilar sulphite, and realize tail gas qualified discharge by three sections of absorptions, realize the object of cleaning of off-gas.But it is serious to there is equipment corrosion in actual production process, the determination that maintenance cost is higher.
CN101143714A discloses a kind of method utilizing the acid gas to prepare sulfuric acid of high hydrocarbon-containing, acid hydrogen sulfide gas enters respectively in proportion in first, second sulfureted hydrogen burning stove and burns, from the first combustion furnace high-temperature furnace gas out, pass through burner-gas cooler, by Air flow to uniform temperature, then enter the second combustion furnace to continue to burn together with surplus air in furnace gas with the sulfide hydrogen sour gas supplemented, second combustion furnace high-temperature furnace gas out enters waste heat boiler heat accumulation, then enter purification section, conversion section, dry absorption section carry out conventional relieving haperacidity.This process can only produce 98% industrial sulphuric acid, can not the higher oleum of productive value, meanwhile, due to sulfuric acid transport, store and all acquire a certain degree of difficulty, therefore, the market demand stable near oil plant is the key factor limiting its development.
CN1836767A discloses a kind of processing method of oil-extraction plant acidic gas, utilizes sour gas as the fuel of cement plant shaft kiln, sour gas when kiln combustion, H wherein
2s composition and cement material generation chemical reaction and generate CaSO
4, other harmful components are also sintered and transform, and fundamentally solve a difficult problem for Acidic Gas Treating, simultaneously; sour gas, as a kind of gaseous fuel, makes cement plant energy-saving fuel, realizes the dual purpose of environmental protection and solution fuel; but this method has certain limitation, be not easy to promote.
CN101337661A mono-kind prepares in the method for NaHS, and the sour gas first adopting caustic soda and milk of lime to absorb containing hydrogen sulfide and carbon dioxide respectively generates intermediate liquid, then mixes in proportion, obtains the NaHS product of low-carbon (LC) acid group.The method does not require that sour gas is purer hydrogen sulfide gas, but flow process is longer, and automaticity is low.
Document " producing vulcanized sodium industrial technology with sodium hydroxide solution absorbing hydrogen sulphide " [give birth by Shangfang, " inorganic chemicals industry ", 44th volume the 2nd phase, in February, 2012] hydrogen sulfide sodium hydroxide solution absorbs and produces the production technology of vulcanized sodium by this technique, with 380 ~ 420g/L sodium hydroxide solution absorbing hydrogen sulphide in packed tower, control of reaction end point vulcanized sodium mass concentration is 330 ~ 350g/L, and hydrogen sulfide absorption rate reaches 95% ~ 98%.This technique not only can available protecting environment, and can be enterprise and create benefit.But this process products vulcanized sodium is apt to deteriorate, and not easily stores.
At present, for small-sized sour gas, need a kind of the Acidic Gas Treating method and the sour gas reactor that consider the factors such as safety, environmental protection, economy.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of sour gas reactor and treatment process, compared with prior art, inventive pipeline formula structure of reactor is simple, and equipment scale is little, and energy consumption is low, operating cost is few, high financial profit, can realize the double goal of sour gas purification and pollutant resources, be applicable to the process of sour gas.
The invention provides a kind of sour gas pipeline reactor, described pipeline reactor comprises reacting pipe and reservoir, reacting pipe one end is gas phase entrance, the reacting pipe other end is gaseous phase outlet, reacting pipe comprises the conversion zone of more than two-stage, reservoir arranges the liquid storage district with conversion zone equal number, every order reaction section is communicated with corresponding liquid storage district by downspout, every order reaction section all arranges absorbing liquid entrance, dividing plate is provided with in reacting pipe between adjacent downspout, overflow plate is provided with in reservoir between adjacent downspout, bottom, Mei Ji liquid storage district is equipped with reactant liquor outlet, reactant liquor outlet is connected with absorbing liquid entrance through pipeline, district is provided with alkali liquor inlet to afterbody liquid storage, the reactant liquor outlet in most previous stage liquid storage district and absorbing liquid entrance connecting line are provided with product discharge by-pass line.
In reactor of the present invention, described reacting pipe arranges 2 ~ 6 order reaction sections, preferably arranges 3 ~ 4 order reaction sections.
In reactor of the present invention, described reservoir arranges 2 ~ 6 grades of liquid storage districts, preferably arranges 3 ~ 4 grades of liquid storage districts.
In reactor of the present invention, described absorbing liquid entrance is connected with liquid phase spray equipment, and described liquid phase spray equipment comprises feed tube and nozzle, and the spray direction of nozzle is perpendicular to direction, gas access, contact with gas flow direction is reverse, nozzle is preferably arranged on reacting pipe axial centre.
In reactor of the present invention, described divider height is 1/4 ~ 3/4 of reacting pipe diameter, is preferably 1/3 ~ 1/2.
In reactor of the present invention, described downspout is straight tube structure, preferably has the straight tube of necking down structure, arranges oblique otch bottom downspout, and otch angle is 15 ~ 90 °, preferably 30 ~ 60 °.Downspout extend in reservoir below liquid level, be positioned at bottom downspout overflow plate radial height 1/4 ~ 2/3 place, be positioned at 1/3 ~ 1/2 place of overflow plate radial height bottom preferred downspout.
In reactor of the present invention, described overflow plate height is 1/2 ~ 4/5 of reservoir diameter, is preferably 2/3 ~ 3/4.
In reactor of the present invention, described overflow plate adopts height form arrangement straggly, and wherein, the low 10mm ~ 100mm of previous stage overflow plate aspect ratio rear stage overflow plate height, is preferably 20mm ~ 50mm.
In reactor of the present invention, district is provided with alkali liquor inlet to afterbody liquid storage, and NaOH solution directly enters fluid reservoir, realizes continuous feed.
In reactor of the present invention, most previous stage liquid storage district arranges Liquid level, and when in most previous stage liquid storage district, liquid level is 1/2 ~ 3/4 of overflow plate height, when to be preferably liquid level be 2/3 of overflow plate height, product is through pumping out device.
In reactor of the present invention, afterbody liquid storage district arranges Liquid level, by detecting liquid level in afterbody liquid storage district, regulates NaOH solution liquid inlet volume.
The invention provides a kind of Acidic Gas Treating method, adopting the pipeline reactor that the present invention is above-mentioned, take NaOH solution as absorbing liquid, and process sour gas produces NaHS, and NaOH solution fills into from the circulation of afterbody liquid storage district.
In Acidic Gas Treating method of the present invention, sour gas is hydrogen sulfide containing waste gas, can be various source containing H
2s sour gas.NaOH solution mass concentration is 20% ~ 60%, is preferably 32% ~ 38%.
In Acidic Gas Treating method of the present invention, reaction temperature is 70 ~ 100 DEG C, is preferably 80 ~ 95 DEG C.
In Acidic Gas Treating method of the present invention, Mei Ji liquid storage district enters corresponding conversion zone reaction solution through reactant liquor outlet is long-pending than being 1/3 ~ 9/10 with the overall reaction produce liquid in Mei Ji liquid storage district, is preferably 5/6 ~ 8/9.
In Acidic Gas Treating method of the present invention, in every order reaction section, the liquid-gas ratio of absorbing liquid and sour gas is 3 ~ 20L/m
3, preferably 5 ~ 10 L/m
3.
In Acidic Gas Treating method of the present invention, the reaction solution of discharging through product discharge nozzle line is 1/3 ~ 3/4 with the reaction solution volume ratio being circulated to conversion zone through pipeline, is preferably 1/2 ~ 2/3.
Compared with prior art, sour gas reactor of the present invention and treatment process tool have the following advantages:
1, reactor of the present invention, structure composition is simple, small scale.Reacting pipe and reservoir subregion is adopted to arrange, adopt dividing plate and overflow plate to realize intermediate liquid classification to use, the overflow plate that difference of height falls, form the transmitting procedure to side overflow, liquid phase transfer line, pipe valve and pump can be omitted, can effectively prevent liquid phase from dispelling the heat, and avoid crystallization to produce blocking pipe pump.Reacting pipe arranges dividing plate, prevents absorbing liquid mixing in conversion zone, improves liquid-phase product definition; Downspout gos deep into certain depth in reservoir, prevents sour gas short circuit, realizes purified gas up to standard; Every order reaction sets up self-loopa absorption process, improves reaction depth, realizes that liquid-phase product is up-to-standard, purified gas is up to standard.
2, sour gas reactor of the present invention, segmentation realizes gas-liquid mass transfer and reaction, eliminates the gas phase transmission inner members such as gas phase connecting line and riser, avoids radiating and cooling on the one hand; Avoid the generation of topical hypothermia's point on the other hand.Thus effectively prevent entrained liquid liquid foam and the blocking that decrease temperature crystalline causes.
3, process Acidic Gas Treating method of the present invention, not only ensures the quality of product NaHS, and realizes Hydrogen Sulfide Tail Gas decontamination index, reaches the resultant effect of waste gas purification and the qualify chemical product of production, simultaneously assurance device long period, continuous, steady running.By answering Matter Transfer, while taking-up reaction heat, material fully being contacted with sour gas, ensureing product quality, Na in product NaHS
2the content of S is less than 4%.Ensure purified gas qualified discharge, H in purified gas
2s content is less than 30mg/Nm
3.
4, Acidic Gas Treating method of the present invention compared with prior art, equipment scale is little, energy consumption is low, operating cost is few, generate the NaHS product that may be used for the industries such as printing and dyeing, papermaking, be convenient to transport, and have certain market, be applicable to the process of sour gas, realize the double goal of sour gas purification and pollutant resources.
Accompanying drawing explanation
Fig. 1 is sour gas reactor of the present invention and treatment process schematic diagram.
Detailed description of the invention
As shown in Figure 1, the invention provides a kind of sour gas pipeline reactor, described pipeline reactor comprises reacting pipe 1 and reservoir 2, reacting pipe one end is gas phase entrance 3, the reacting pipe other end is gaseous phase outlet 4, reacting pipe comprises the conversion zone of more than two-stage, reservoir arranges the liquid storage district with conversion zone equal number, every order reaction section is communicated with corresponding liquid storage district by downspout 5, every order reaction section all arranges absorbing liquid entrance 10, absorbing liquid entrance is connected with liquid phase spray equipment, described liquid phase spray equipment comprises feed tube 11 and nozzle 12, nozzle is preferably arranged on reacting pipe axial centre, the spray direction of nozzle is perpendicular to gas phase Way in, contact with sour gas flow direction is reverse, reacting pipe between adjacent downspout is provided with dividing plate 6, reservoir between adjacent downspout is provided with overflow plate 7, bottom, Mei Ji liquid storage district is equipped with reactant liquor outlet 8, district is provided with alkali liquor inlet 9 to afterbody liquid storage, reactant liquor outlet is connected with absorbing liquid entrance through pipeline, and the reactant liquor in most previous stage liquid storage district exports and absorbing liquid entrance connecting line is provided with product discharge pipeline 13.
Below in conjunction with embodiment, reaction effect of the present invention is described, but does not therefore limit the scope of the invention.
Embodiment 1
In the present embodiment, described pipeline reactor arranges 3 order reaction sections, and reservoir arranges 3 grades of liquid storage districts.
As shown in Figure 1, the present invention is Acidic Gas Treating process schematic diagram, with sour gas and NaOH solution for raw material, carries out reacting the Acidic Gas Treating process generating product NaHS.
Third-order reaction section is set for pipeline reactor and illustrates Acidic Gas Treating method course of reaction of the present invention: when adopting inventive pipeline formula reactor for treatment sour gas, sour gas enters first order reaction section in reacting pipe through gas phase entrance, (reaction solution that the district's overflow of secondary liquid storage comes comprises Na with the reaction solution from one-level liquid storage district
2s and NaHS) be absorbing liquid, in reacting pipe, form the liquid film on axis direction through nozzle, when sour gas passes through liquid film, there is neutralization reaction, under the effect of gravitational field, liquid film is ejected on reacting pipe tube wall, enters liquid storage district corresponding in reservoir along wall through downspout.By arranging dividing plate, after preventing liquid film to be ejected into tube wall, liquid crossfire enters in adjacent reaction section.At H
2when S is excessive, Na
2s liquid phase and H
2s reacts, and generates NaHS.NaHS in one-level liquid storage district dispenses out device through pumping section, is partly recycled to first order reaction section and circulates, and realizes the absorbing liquid degree of depth and absorbs.The reacted sour gas of first order reaction section enters second order reaction section, wherein H
2s and CO
2concentration reduces greatly, but still does not reach emission request.(reaction solution that three grades of liquid storage district overflows come comprises most of Na with the reaction solution from secondary liquid storage district
2s and a small amount of NaOH mixed solution) be absorbing liquid, in pipeline, form the liquid film of axis direction through nozzle, when sour gas passes through liquid film, there is neutralization reaction, under the effect of gravitational field, liquid film is ejected on reacting pipe tube wall, enters liquid storage district corresponding in reservoir along wall through downspout.At H
2when S is little over amount, Na
2s and NaOH mixed liquor and H
2s reacts, and generates Na
2s and NaHS mixed liquor.Reaction solution is circulated to second order reaction section through pump, circulates, and realizes the absorbing liquid degree of depth and absorbs.H in the reacted sour gas of second order reaction section
2s concentration is extremely low, substantially reaches emission request.In third-order reaction section, take NaOH solution as absorbing liquid, when NaOH solution is little over amount, NaOH solution and H
2s reacts, and generates Na
2s, realizes purified gas qualified discharge.Reaction solution is circulated to third-order reaction section through pump, circulates, and realizes the absorbing liquid degree of depth and absorbs.Third-order reaction generates liquid and NaOH solution overflow enters secondary liquid storage district, and when secondary liquid storage district liquid level is higher than overflow plate, second order reaction generates liquid and enters in one-level liquid storage district.
In the present embodiment, CO in sour gas
2volume fraction is 7%, H
2s volume fraction is 92%, and hydro carbons volume fraction is 1%.NaOH solution mass concentration is 35%.Acid little over amount in first order reactor, H in the reactor of the second level
2s is little over amount, and in third level reaction, NaOH solution is little over amount.In Acidic Gas Treating method of the present invention, every order reaction sets up cyclic absorption process.In first order reaction section, second order reaction section and third-order reaction section, circulation ratio is 2:3.In every order reaction section, liquid-gas ratio is 5L/m
3.Concrete operations condition is in table 1, and reaction result is in table 1.
Table 1 embodiment 1 reaction condition and reaction result
| Embodiment 1 | |
| Reaction temperature (DEG C) | 85 |
| NaHS product design | 40% |
| Na 2S content | <3% |
| H in purified gas 2S content (mg/Nm 3） | 25 |
Claims (20)
1. a sour gas reactor, described reactor comprises reacting pipe and reservoir, reacting pipe one end is gas phase entrance, the reacting pipe other end is gaseous phase outlet, reacting pipe comprises the conversion zone of more than two-stage, reservoir arranges the liquid storage district with conversion zone equal number, every order reaction section is communicated with corresponding liquid storage district by downspout, every order reaction section all arranges absorbing liquid entrance, dividing plate is provided with in reacting pipe between adjacent downspout, overflow plate is provided with in reservoir between adjacent downspout, bottom, Mei Ji liquid storage district is equipped with reactant liquor outlet, reactant liquor outlet is connected with absorbing liquid entrance through pipeline, district is provided with alkali liquor inlet to afterbody liquid storage, the reactant liquor outlet in most previous stage liquid storage district and absorbing liquid entrance connecting line are provided with product discharge by-pass line.
2. according to reactor according to claim 1, it is characterized in that: described reacting pipe arranges 2 ~ 6 order reaction sections, 3 ~ 4 order reaction sections are preferably set.
3. according to reactor according to claim 1, it is characterized in that: described reservoir arranges 2 ~ 6 grades of liquid storage districts, 3 ~ 4 grades of liquid storage districts are preferably set.
4. according to reactor according to claim 1, it is characterized in that: described absorbing liquid entrance is connected with liquid phase spray equipment, described liquid phase spray equipment comprises feed tube and nozzle.
5. according to reactor according to claim 4, it is characterized in that: the spray direction of nozzle, perpendicular to direction, gas access, contacts with gas flow direction is reverse.
6. according to reactor according to claim 4, it is characterized in that: nozzle is arranged on reacting pipe axial centre.
7. according to reactor according to claim 1, it is characterized in that: described divider height is 1/4 ~ 3/4 of reacting pipe diameter, be preferably 1/3 ~ 1/2.
8. according to reactor according to claim 1, it is characterized in that: described downspout is straight tube structure, arrange oblique otch bottom downspout, otch angle is 15 ~ 90 °, preferably 30 ~ 60 °.
9. according to reactor according to claim 1, it is characterized in that: described downspout to extend in reservoir below liquid level, be positioned at bottom downspout overflow plate radial height 1/4 ~ 2/3 place, be positioned at 1/3 ~ 1/2 place of overflow plate radial height bottom preferred downspout.
10. according to reactor according to claim 8, it is characterized in that: described downspout is the straight tube structure having necking down structure.
11., according to reactor according to claim 1, is characterized in that: described overflow plate adopts height form arrangement straggly, and the low 10mm ~ 100mm of previous stage overflow plate aspect ratio rear stage overflow plate height, is preferably 20mm ~ 50mm; Described overflow plate height is 1/2 ~ 4/5 of reservoir diameter, is preferably 2/3 ~ 3/4.
12. according to reactor according to claim 1, it is characterized in that: most previous stage liquid storage district arranges Liquid level, when in most previous stage liquid storage district, liquid level is 1/2 ~ 3/4 of overflow plate height, when being preferably that in most previous stage liquid storage district, liquid level is 2/3 of overflow plate height, product is through pumping out device.
13., according to reactor according to claim 1, is characterized in that: afterbody liquid storage district arranges Liquid level, by detecting liquid level in afterbody liquid storage district, regulate liquid inlet volume.
14. 1 kinds of Acidic Gas Treating techniques take NaOH solution as absorbing liquid, and process sour gas produces NaHS, and NaOH solution fills into from the circulation of afterbody liquid storage district, it is characterized in that: adopt the reactor described in arbitrary claim in claim 1 ~ 13.
15., according to technique according to claim 14, is characterized in that: sour gas is hydrogen sulfide containing waste gas, can be various source containing H
2s sour gas.
16., according to technique according to claim 14, is characterized in that: NaOH solution mass concentration is 20% ~ 60%, are preferably 32% ~ 38%.
17., according to technique according to claim 14, is characterized in that: reaction temperature is 70 DEG C ~ 100 DEG C, are preferably 80 DEG C ~ 95 DEG C.
18., according to technique according to claim 14, is characterized in that: the volume ratio that the reaction solution that Mei Ji liquid storage district enters corresponding conversion zone through reactant liquor outlet and the district's overall reaction of Mei Ji liquid storage generate liquid is 1/3 ~ 9/10, preferably 5/6 ~ 8/9.
19., according to technique according to claim 14, is characterized in that: in every order reaction section, the liquid-gas ratio of absorbing liquid and sour gas is 3 ~ 20L/m
3, preferably 5 ~ 10 L/m
3.
20., according to technique according to claim 14, is characterized in that: the reaction solution of discharging through product discharge nozzle line is 1/3 ~ 3/4 with the volume ratio being circulated to the reaction solution in conversion zone through pipeline, is preferably 1/2 ~ 2/3.
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|---|---|---|---|
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116251539A (en) * | 2023-05-15 | 2023-06-13 | 黑龙江莱睿普思环境科技发展有限公司 | Absorption reactor for preparing sodium hydrosulfide from acid gas |
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| CN101186280A (en) * | 2007-11-29 | 2008-05-28 | 青岛奥海科工贸有限公司 | Method for preparing sodium sulfhydrate from hydrogen sulfide tail gas |
| CN103203170A (en) * | 2013-04-11 | 2013-07-17 | 周勇定 | Flue-gas cleaner |
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| US4102982A (en) * | 1972-03-24 | 1978-07-25 | Weir Jr Alexander | Process for treating stack gases |
| US5518696A (en) * | 1991-10-28 | 1996-05-21 | Jain; Roop C. | Emergency scrubbing system |
| US20070237695A1 (en) * | 2006-04-07 | 2007-10-11 | Liang Hu | Phase transitional absorption method |
| CN101186280A (en) * | 2007-11-29 | 2008-05-28 | 青岛奥海科工贸有限公司 | Method for preparing sodium sulfhydrate from hydrogen sulfide tail gas |
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| CN116251539A (en) * | 2023-05-15 | 2023-06-13 | 黑龙江莱睿普思环境科技发展有限公司 | Absorption reactor for preparing sodium hydrosulfide from acid gas |
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