CN1230158A - Process for recovery of sulfur from SO2 containing gases - Google Patents

Process for recovery of sulfur from SO2 containing gases Download PDF

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Publication number
CN1230158A
CN1230158A CN97197730A CN97197730A CN1230158A CN 1230158 A CN1230158 A CN 1230158A CN 97197730 A CN97197730 A CN 97197730A CN 97197730 A CN97197730 A CN 97197730A CN 1230158 A CN1230158 A CN 1230158A
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liquid sulfur
sulfur
gas
sulphur
reaction
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J·A·拉加斯
J·波尔斯波姆
P·D·克拉克
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Stork Engineers and Contractors BV
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8603—Removing sulfur compounds
    • B01D53/8612—Hydrogen sulfide
    • B01D53/8615—Mixtures of hydrogen sulfide and sulfur oxides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/02—Preparation of sulfur; Purification
    • C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
    • C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
    • C01B17/0426—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process characterised by the catalytic conversion
    • C01B17/0439—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process characterised by the catalytic conversion at least one catalyst bed operating below the dew-point of sulfur
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/02—Preparation of sulfur; Purification
    • C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
    • C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
    • C01B17/0456—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process the hydrogen sulfide-containing gas being a Claus process tail gas

Abstract

The invention relates to a process for recovering sulfur from an SO2 containing gas stream through catalytic conversion thereof to elemental sulfur, comprising converting SO2 and H2S in the presence of liquid sulfur and a catalyst system based on a heterogeneous catalyst which catalyzes the Claus reaction, while as promoter for the Claus reaction a basic nitrogen compound is present in the liquid sulfur.

Description

From containing SO 2Air-flow in reclaim the method for sulphur
In many technological processs, for example in the refining of oil, the purifying of Sweet natural gas and produce the process of synthetic gas from coal or oil residue all discharges sulfur-bearing and particularly contains H 2The gas of S.Before above-mentioned gas is used, this H 2S gas must be removed.Remove H 2The most important reason of S is to prevent to pass through H 2The burning of S produces SO 2Smog.As everyone knows, H 2S also is very malicious gas, and frowziness.
At the industrial H that from gas, removes 2The prevailing method of S is to absorb by liquid-absorbant, makes H 2S concentrates, and makes regenerated H then 2The S gas reforming becomes harmless elementary sulfur.
In many cases, also first step can be omitted, promptly H can be omitted 2The spissated step of S can be H 2S directly changes into elementary sulfur.
H 2One of well-known and widely used method that S changes into elementary sulfur is so-called Kraus process.Kraus process is undertaken by different modes, and this depends on the H in the unstripped gas 2S content.According to the most traditional scheme, a part of H 2The S burning generates SO 2, then further with remaining H 2S reaction generting element sulphur.
The detailed description of Kraus process can find in following document, and these documents are: R.N.Maddox " Gas and Liquid Sweetening "; Campbell Petroleum Series (1977) pp.239-243 and in H.G.Paskall " Capabilities of theModified Claus Process ", publ.Western Research﹠Development.Calgary alberta, Canada (1997).
Kraus process is based on following reaction:
(1)
(2)
Reaction (1) and (2) forms total reaction
(3)
Be suitable for handling H 2The traditional Cross unit of S content between 50 and 100% is by hot arc (burner, combustion chamber, tail gas container and sulfur condenser) and many reactor regions subsequently (gas heating, loading catalyst reactor and sulfur condenser), is generally two or three reactor regions and forms.In hot arc, react (1) and (2) in reactor region, only is called as the reaction (2) of claus reaction.But, in the claus reaction process, H 2S not exclusively changes into elementary sulfur, mainly is because incomplete result is carried out in Crouse's balanced reaction (2).
So H 2S and SO 2Keep certain content.By strict environmental requirement viewpoint, this residual gas that burns never allows.The further desulfurization of this so-called tail gas.Treatment process those skilled in the art of tail gas are known and open, for example, and B.G.Goar, the exhaust purifying method of in the 33rd gas processing annual meeting, delivering, Norman, Oklahoma, 7-9 day March nineteen eighty-three.
Be used for the well-known of tail gas desulfurization and so far effective means is the SCOT method of Maddox in " gas and liquid desulfurization " (1977) description.The sulfur recovery rate of SCOT method is 99.8-99.9%.The shortcoming of SCOT method is high investment cost and high energy consumption.
The another kind of method that improves Kraus process efficient is SUPERCLAUS Method.In this method, the efficient of Kraus process is brought up to more than 99% from 94-97%.
At the 38th the chemical engineering conference of Canada (on October 25th, 1988, Edmonton, the Alberta, " SUPERCLAUS that delivers on Canada) , the restriction that solves Cross unit " in SUPERCLAUS has been described Method.
Compare SUPERCLAUS with other known exhaust gas treating method The method expense is lower.At SUPERCLAUS In the method, reaction (2) is at excessive H in hot arc and claus reaction device section 2Carry out under the S, so in the gas from last claus reaction device section, H 2S and SO 2Content be respectively about 1% (V) and 0.02% (V).In the downstream reactor section that is connected with it, H 2S on the special oxide catalyst of selecting, by following reaction preference be oxidized to elementary sulfur.
(4)
These catalyzer are disclosed in EPO242920 number and EPO409353 number.
Therefore, from SUPERCLAUS The tail gas of reactor region still contains the H of 0.02% (V) 2The SO of S and about 0.2% (V) 2And the O of 0.2-0.5% (V) 2
Describe another kind of Kraus process in No. 4280990, the United States Patent (USP) of Jagodzinski etc., in the method, in the presence of the claus catalyst of standard, under high pressure, claus reaction (2) takes place in liquid sulfur, and the condensation of water does not take place.
In this method, hot arc is operation under the 5-50 crust at pressure, and after this expellant gas enters the reactor that catalyzer is housed under uniform pressure.So H 2S and SO 2Between the pressure that is reflected at 5-50 crust take place down, be condensate on the catalyzer by reacting thiourea.Liquid sulfur circulates in catalyst bed, and reaction heat is disperseed.The H that contains about 7.9% (V) from the gas of hot arc 2The SO of S and 3.95% (V) 2, so H 2S: SO 2=2: 1.The temperature of the reactor in first makes temperature out be 275 ℃ and sets like this.In second, temperature out is set in 195 ℃.From the embodiment of this method as can be seen, H 2S and SO 2The conversion pressurize of this high percent more favourable.For realizing the Claus tail gases desulfurization, selective same procedure has been proposed also.In this method, Claus tail gases is pressurized to very big pressure.
The shortcoming of Kraus process operating air and the two sulfur method of Claus tail gases is respectively H 2S gas (Crouse's unstripped gas) and the high cost of air compressor and the high cost of tail-gas compressor; The high energy consumption of these compressors, spillage risk and these compressor movement reliability problems of deleterious H2S gas in these compressors of desulfurizer and in the miscellaneous equipment.
Here it is why these methods do not find the reason of any industrial application so far.In No. 4280990 described methods of United States Patent (USP), use the claus catalyst of standard.When above-mentioned patent was awarded, people used surface-area to be about 300m 2/ gr and mean pore size for about 50A ° activated alumina as claus catalyst.In No. 4280990, United States Patent (USP), also put down in writing this catalyzer.
In recent years, this method has developed, and normally the aluminium oxide catalyst of standard is arranged in the claus reaction device.So, think other type of catalyzer do not studied, or think that they are non-availability, or think that as if they also be not developed rationally.To depending on H 2S and SO 2The operating pressure of concentration is not studied yet.Many experiments described in No. 4280990, United States Patent (USP) are the H at 2.5% (V) 2The SO of S and 1.2% (V) 2Condition under carry out.
United States Patent (USP) discloses another kind of method No. 3447903, and this method also is based on Kraus process and uses in liquid sulfur.According to the method, a small amount of basic nitrogen compound catalysis of being existed of reaction.Know that from several embodiment the consumption of this compound is about 1-50ppm.This method is also determined not in industrial application.
The purpose of this invention is to provide a kind of improving one's methods of sulphur of from tail gas, reclaiming, by this method SO that removes as much as possible 2And H 2S.More particularly, the purpose of this invention is to provide a kind of method, by this method, improved traditional sulfur recovery method, realized that in commercial quantity sulphur recovery efficiency is more than 99.5%.
The invention provides a kind of passing through the SO in the air-flow 2Be catalytically converted into elementary sulfur, from containing SO 2Air-flow in reclaim the method for sulphur.Described method is included in liquid sulfur and exists down based on the catalyst system of the heterogeneous catalyst of catalysis claus reaction, simultaneously, exists in liquid sulfur under the condition as the basic nitrogen compound of claus reaction promotor, transforms H 2S and SO 2
Be astoundingly, have been found that, utilize the special promotor of heterogeneous catalyst, realized improving significantly the efficient that changes into elementary sulfur according to method of the present invention.For example, all use liquid sulfur to make reaction medium for a long time.But, only according to method of the present invention, can under low pressure carry out, promptly under atmospheric pressure or under a little higher than normal atmosphere carry out.
This method can be carried out in many ways.Basic mode is that catalyzer directly contacts with the liquid sulfur of being supplied with by external source.Preferred this liquid sulfur has contained the H of amount to be transformed 2S.Because transformation efficiency improves significantly, therefore just can from gas phase, supply with H 2S and SO 2But this produces lower efficient.
In the method for the invention, in the presence of the liquid sulfur that contains suitable catalyzer, reaction pressure is preferably 1-5 crust and temperature of reaction and is preferably under the condition between 120-250 ℃, H 2S and SO 2Between reaction press H 2S: SO 2Carry out at=2: 1, generates sulphur and water.
In the method for the invention, Shi Yi catalyzer has big macroporous structure.These catalyzer comprise the activated alumina that a small amount of microvoid structure and a large amount of medium and macroporous structure are arranged.The hole of the medium pore structure of these activated aluminas, macroporous structure and oversized hole structure accounts for more than 65% of total pore volume.Also can use the catalyzer of these character to make solid support material, this solid support material active substance such as metal oxide impregnated.These catalyzer are commonly referred to " promotion catalyzer ".
In general, can think that these catalyzer are useful in the catalysis claus reaction.Except the activated alumina of having discussed, known other catalyzer of this reaction also is suitable for.Titanium dioxide and be loaded in metal oxide on the carrier for example.
We find, when water vapour is when the pressure that are lower than 5 crust add pending gas, or when having water vapour in pending gas, also promote H 2S and SO 2Between generation sulphur and the reaction of water, same, by suitably selecting the residence time, efficient also can improve significantly.
At the pressure that is lower than 5 crust, when sulphur exists with the polysulfide form, SO 2With H 2S reacts in an identical manner and generates sulphur and water.Have been found that when pending gas contains oxygen, this oxygen hardly with H 2The reaction of Salmon-Saxl of S or existence generates SO 2
The major advantage of the inventive method is under low pressure to react, so whole shortcomings of No. 4280990 described methods of United States Patent (USP) have all been got rid of.
In the method for the invention, by H 2S gas joins and contains SO 2Gas in, or dissolve H in advance 2S also can handle and contains SO in liquid sulfur 2Gas.
In the method for the invention, work as H 2When S was dissolved in liquid sulfur in advance, this can produce higher SO 2Transformation efficiency, and provide desired H 2S changes into SO 2The advantage that can quite simplify of control because H 2S is dissolving earlier, untapped H 2The S residuum is deposited on sulphur, so sulphur can be once more by H 2The S load.
Be astoundingly, have been found that in the method for the invention, when in sulphur, having a spot of basic nitrogen compound, H 2S and SO 2The transformation efficiency that changes into sulphur and water improves significantly, even is issued to virtually completely equilibrated point in service temperature.
Suitable basic nitrogen compound is an amine, (for example alkyl amine), alkanolamine (for example MEA, DGA, DEA, DIPA, MDEA, TEA), ammonia, ammonium salt class, aromatics nitrogen compound, (for example quinoline, morpholine).
The preferred tertiary alkanol amine that uses because they do not generate sulfamate, has high boiling point, and because these amines are convenient.
Now, with reference to the accompanying drawings, the present invention will be clearer.In Fig. 1, contain H 2S and SO 2Gas be transported to the reactor 2 that catalyzer 3 is housed through managing 1.
Liquid sulfur passes through catalyzer through managing 4 supplies with the gas that enters.On catalytic bed from H 2S and SO 2Between reaction produce liquid sulfur.At H 2S and SO 2After the reaction, discharge gas through managing 5 dischargings.
Liquid sulfur leads to water cooler 7 through managing 6 from reactor, disperses reaction heat at water cooler 7.By pump 8, sulphur is recycled to reactor 2 through managing 4.The sulphur that generates is through managing 9 dischargings.
In Fig. 2, contain H 2The H that S90% (V) is above 2S gas is transported to the Cross unit of being made up of hot arc and two catalyst reaction section subsequently 10 through managing 1.
The needed air of claus reaction is supplied with through managing 11.Sulphur in hot arc and reactor region generation discharges through managing 12.Still contain H from the second catalyticreactor section 2S and SO 2Tail gas, through managing 13 reactors 2 that are transported to apparatus with catalyst inside 3.On catalyst bed, through managing 4 feeding liquid sulphur.At H 2S and SO 2After the catalyzer bed reaction generated sulphur, tail gas left reactor through managing 5.Liquid sulfur through manage 6 and water cooler 7 leave reactor and be recycled to reactor 2.The sulphur that generates is through managing 9 dischargings.In addition, basic nitrogen compound can add through managing 14.
In Fig. 3, the preferred version of the inventive method has been described, in this scheme, contain H 2The gas of S is transported to the Cross unit of being made up of hot arc and two catalytic section subsequently 10 through managing 1.
The needed air of claus reaction is supplied with through managing 11.Discharge through managing 12 at the sulphur that hot arc and reactor region generated.That comes from the second catalyticreactor section still contains H 2S and SO 2Tail gas be transported to SUPERCLAUS device 15 through managing 13.
Supply with the air that selective oxidation is used through managing 16.And through managing 17 discharge liquid sulphur.Tail gas is through managing 13 reactors 2 that are transported to apparatus with catalyst inside 3.On catalyst bed, through managing 4 feeding liquid sulphur.
With contain H 2The contacted liquid sulfur from tower 18 of the gas of S is transported to Cross unit through managing 1.In tower 18, liquid sulfur with from the H of gas 2S merges.At H 2After S is dissolved in the liquid sulfur, on catalyst bed with SO 2Reaction generates sulphur, and tail gas leaves reactor through managing 5.Liquid sulfur leaves reactor 2 and is recycled to tower 18 by pump 8 through managing 19 through managing 6.The sulphur that generates is through managing 9 dischargings.In tower, sulphur absorbs H once more 2S, and through manage 20, pump 21, water cooler 22 and manage 4 and be transported to reactor 2 once more.If desired, basic nitrogen compound can flow to liquid sulfur through managing 14.
The present invention further specifies by following embodiment.
Embodiment 1
Use the described device of Fig. 2, in the Cross unit that two catalytic section are arranged, carry out claus reaction.Contain 90.0% (V) H to the hot arc supply 2S (36.OKmol/h), 3.5% (V) CO 2, 2.0% (V) hydro carbons, 4.5% (V) H 2O and 19.5Kmol/h O 2Crouse's gas as atmospheric oxygen.H in the tail gas after second catalytic section 2The percent by volume of S is 0.58% (V), and SO wherein 2Content is that 0.29% (V) and water-content wherein are 33.2% (V).The sulfur recovery rate of Cross unit is 94%.
It is that 1.13 tail gas that cling to are transported to catalyst bed shown in Figure 2 with 120Kmol/h with pressure that temperature is 150 ℃.Catalyzer 3 is activated aluminas of high medium pore structure and macroporous structure, on catalyst bed, liquid sulfur at 150 ℃ with 50m 3The amount circulation of/h.The temperature of circulation sulphur is by disperseing the reaction heat that technological process is emitted in the water cooler to keep constant.In order not make the sulphur content rising De Taigao in the reactor, from system, discharge some sulphur at any time.H in the gas behind catalyst bed 2The percentage ratio of S is 0.188% (V), and SO wherein 2Percentage ratio be 0.088% (V), therefore, to change into the transformation efficiency of sulphur be 68% to H2S in reactor, SO 2The transformation efficiency that changes into sulphur is 70%.
Therefore, in the Cross unit of following this reactor region, H in liquid sulfur 2S and SO 2Between the total sulfur recovery that reacts be more than 97.7%.
Embodiment 2
With the described same apparatus of Fig. 2 in, arylamine (quinoline) adds in the logistics of round-robin sulphur through managing 14.The amount of the quinoline that adds is that to make the concentration for quinoline in the sulphur logistics of reactor be 500ppm (weight).
Identical among the Crouse's gas that is added to hot arc and the embodiment 1, still, the oxygen of supplying with as atmospheric oxygen is 19.85Kmol/h now, so that after second catalytic section, the SO in the tail gas 2Picture H 2S as many.H in tail gas 2S and SO 2Percent by volume all be 0.46%, and water-content is 33.0% (V).Behind catalyst bed, the H in the tail gas 2The percent by volume of S is 0.046%, and SO 2Percent by volume be 0.018%.H in reactor 2The transformation efficiency that S changes into sulphur is 90%, and SO 2Transformation efficiency be 96%.
Therefore, in the Cross unit of following this reactor region, H in liquid sulfur 2S and SO 2Between the total sulfur recovery that reacts more than 99.0%.
Embodiment 3
In the device that Fig. 3 describes, after second catalytic section of Cross unit, the SUPERCLAUS reactor region is set, make from the H in the gas of second catalytic section 2The S selective oxidation becomes sulphur.Tail gas from the SUPERCLAUS section is transported to catalyst bed shown in Figure 3.Crouse's gas is by before the hot arc, in contacting container at first with sulphur logistics counter current contact.The Crouse's unstripped gas that flows into this contacting container is identical with embodiment's 1.In contacting container, H 2S is dissolved in sulphur with the speed of 0.193Kmol/h, therefore and from the Crouse's unstripped gas by hot arc discharges.Supply with oxygen with the speed of 18.87Kmol/h to hot arc as air oxygen.In addition supply with oxygen to SUPERCLAUS as atmospheric oxygen with the speed of 1.40Kmol/h.H in the tail gas after the SUPERCLAUS section 2S content is 0.032% (V), and SO 2Content be that the content of 0.189% (V) and oxygen is 0.50% (V).From the tail gas of the SUPERCLAUS section amount with 122Kmol/h, temperature is 130 ℃, and pressure is that 1.13 crust (definitely) are transported to catalyst bed shown in Figure 3.From the liquid sulfur of contacting container on the catalyst bed by and in liquid sulfur, add tertiary alkanolamine (TEA).
After this, sulphur turns back to contacting container.Set the amount of recycle stream, make with respect to SO 2Enough H are arranged 2S is transported to catalyst bed, so that H 2S: SO 2Minimum is 1: 1.
H in the vent gas behind catalyst bed 2The concentration of S is 0.015% (V), SO 2Content be 0.011% (V).Like this, H in reactor 2The transformation efficiency that S changes into sulphur is 92%, SO 2Transformation efficiency be 94%.
Therefore, behind the SUPERCLAUS reactor region, follow in the Cross unit of this reactor region H in liquid sulfur 2S and SO 2Between the reaction total sulfur recovery more than 99.5%.

Claims (14)

1. one kind is passed through SO 2Be catalytically converted into elementary sulfur from containing SO 2Air-flow in reclaim the method for sulphur, described method is included in liquid sulfur and there is catalyzed conversion SO down in catalyst system 2And H 2S, described catalyst system are the heterogeneous catalyst systems of catalysis claus reaction, have the promotor basic nitrogen compound of claus reaction simultaneously in described liquid sulfur.
2. by the process of claim 1 wherein that promotor is selected from amine, alkyl amine, alkanolamine, ammonia, ammonium salt and fragrant nitrogen compound.
3. by the method for claim 2, wherein promotor is selected from Monoethanolamine MEA BASF, diethanolamine, DGA, DIPA, MDEA and trolamine.
4. by the method for claim 2 or 3, wherein use tertiary amine.
5. by the method for claim 1-4, the porous alumina that wherein uses porous alumina or be loaded with metal oxide on porous alumina is made the active heterogeneous catalyst of Crouse.
6. by the method for claim 5, wherein the surface-area of aluminum oxide is at least 150m 2/ g.
7. by the method for claim 6, wherein the aperture is that the pore volume in 5nm or littler hole is less than 35% (V) in the pore volume of measuring with nitrogen.
8. by the method for claim 1-7, this method is to carry out under the pressure of 1-5 crust.
9. by the method for claim 1-8, this method is to carry out under 120-250 ℃ temperature.
10. press the method for claim 1-9, wherein H 2S is dissolved in the liquid sulfur, after this with SO 2Contact.
11. by the method for claim 10, wherein H 2The gas that S content is at least 0.5% (V) contacts with liquid sulfur, thus section H 2S is dissolved in liquid sulfur, after this, and containing H 2The gas delivery of S is to Cross unit, a part of thus H 2S is heated and changes into SO 2, after this, in one or several conversion zone, in the catalysis Cross unit, generate sulphur, after separate sulfur, the gaseous mixture that obtains is containing dissolved H 2The existence of the liquid sulfur of S directly transforms down, or if desired, is optionally transforming behind the oxidation step.
12. by the method for claim 1-10, wherein H 2The tail gas that S content is at least the Cross unit catalytic section of 0.25% (V) contacts with liquid sulfur, thus at least a portion H 2S is dissolved in liquid sulfur, after this, in the presence of the heterogeneous catalyst system of catalysis claus reaction and in liquid sulfur in the presence of the basic nitrogen compound as claus reaction promotor, the above-mentioned H that contains 2The liquid sulfur of S with contain SO 2The gas contact.
13. by the method for claim 1-12, wherein in the weight of liquid sulfur, the amount of promotor is 1-1000ppm, is preferably 1-50ppm.
14. by the method for claim 1-13, wherein reaction is in bed of catalyst particles or is loaded with thereon and carries out on other material of catalyzer and wherein these particles or carrier substance soaked into liquid sulfur.
CN97197730A 1996-07-08 1997-07-07 Process for recovery of sulfur from SO2 containing gases Pending CN1230158A (en)

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CN109529578B (en) * 2017-09-21 2021-07-09 中国石油化工股份有限公司 Process device and process method for liquid-phase reaction desulfurization of hydrogen sulfide and sulfur dioxide
CN109529567B (en) * 2017-09-21 2021-07-09 中国石油化工股份有限公司 Process for desulfurizing hydrogen sulfide and sulfur dioxide through reaction
CN109529573A (en) * 2017-09-21 2019-03-29 中国石油化工股份有限公司 The process unit and process of hydrogen sulfide and sulfur dioxide liquid desulfuration
CN109529573B (en) * 2017-09-21 2021-07-09 中国石油化工股份有限公司 Process device and process method for liquid-phase desulfurization of hydrogen sulfide and sulfur dioxide
CN109529580B (en) * 2017-09-21 2021-07-09 中国石油化工股份有限公司 Process device and process method for desulfurizing sulfur dioxide and hydrogen sulfide through liquid-phase reaction
CN109772134A (en) * 2019-01-10 2019-05-21 昆明理工大学 A kind of circularly removing H2S and SO2And the method for recycling sulphur
CN109772134B (en) * 2019-01-10 2021-12-28 昆明理工大学 Circulation desorption H2S and SO2And process for recovering sulfur

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