CN115121092B

CN115121092B - Application of campylobacter xanthus in desulfurization

Info

Publication number: CN115121092B
Application number: CN202210647185.XA
Authority: CN
Inventors: 魏雄辉; 袁本雄; 叶青保; 冯家俊; 周稳华; 王跃发; 李世嵩; 户春; 蒋俊华; 张洪; 汉春利; 郑立华; 占善亮; 魏建国; 刘家旭; 袁冬秀; 聂金鹏; 魏子卿; 万明金; 李祥斌
Original assignee: Beijing Hengtai Yuansheng High Tech Co ltd; Beijing Honglong Environmental Protection Co ltd; Beijing Boyuan Hengsheng High Technology Co Ltd; Jiangxi Yongfeng Boyuan Industrial Co Ltd; Tongling Pacific Special Material Ltd
Current assignee: Beijing Hengtai Yuansheng High Tech Co ltd; Beijing Honglong Environmental Protection Co ltd; Beijing Boyuan Hengsheng High Technology Co Ltd; Jiangxi Yongfeng Boyuan Industrial Co Ltd; Tongling Pacific Special Material Ltd
Priority date: 2022-06-09
Filing date: 2022-06-09
Publication date: 2023-04-04
Anticipated expiration: 2042-06-09
Also published as: CN115121092A

Abstract

The invention provides application of Campylobacter flavus in desulfurization of gas containing hydrogen sulfide and/or organic sulfur. The sulfur is hydrogen sulfide and/or organic sulfur in the sulfur-containing gas. The campylobacter flavus with the saliferous membrane has wide industrial application in the field of sulfur-containing gas desulfurization, can be used for desulfurization of natural gas, coke oven gas, oil field gas, blast furnace gas, city gas, gas, water gas, synthetic ammonia semi-water gas and conversion gas, synthetic waste gas of dye factories, waste gas of chemical fiber factories, biogas and other industrial raw material gases or waste gases containing hydrogen sulfide and organic sulfur, and the total sulfur content of the sulfur-containing gas is less than 99.9 percent. Not only can remove hydrogen sulfide in the organic sulfur, but also has certain removal capacity for organic sulfur. And the traditional wet desulphurization method can not keep high desulphurization efficiency economically for a long time, but the desulphurization method can keep high desulphurization efficiency economically for a long time because the halophilic membrane campylobacter flavus can be regenerated and used.

Description

Application of campylobacter xanthus in desulfurization

Technical Field

The invention relates to application of campylobacter xanthus in salt-inhabiting membrane in desulfurization.

Background

Due to the rapid development of the society, the large-scale exploitation of natural gas, coal mine, oil field gas and shale gas is driven; the widespread use of fossil fuels such as coal and petroleum results in the production of large quantities of coke oven gas, coal gas, water gas, gas, synthetic ammonia semi-water gas and shift gas, oil refining tail gas, pyrolysis gas and synthesis gas; in addition, methane tanks, manure and garbage fermentation tanks; and a large amount of gas is released in environments such as a papermaking pulp tank. These gases contain a large amount of hydrogen sulfide and CS ₂ Organic sulfur such as COS, mercaptan, thioether and thiophene, and a large amount of HCN and NH ₃ . These gases, whether discharged directly into the atmosphere or indirectly after combustion, cause serious environmental pollution, such as the formation of a diffuse odor, acid rain and haze in the air, and the synergistic effect of these toxic gases causes cancers, respiratory diseases and skin diseases, etc., which directly endanger human health. If these gases are used as industrial raw gases, forIndustrial production is extremely harmful, for example, causing severe corrosion of equipment and buildings; in particular, the harm to industrial production of synthetic ammonia, organic synthesis and the like is more serious, for example, poisoning and deactivation of shift catalysts, synthetic ammonia catalysts, methanol catalysts, polymerization and cracking catalysts and the like are caused, copper consumption of a copper washing process of the synthetic ammonia is rapidly increased, the quality of products is reduced, the products are blackened and the like, wherein hydrogen sulfide is called cancer cells in the synthetic ammonia industry. Therefore, the development and research of desulfurization technology is becoming urgent and important.

The existing desulfurization technologies such as Claus process, alcohol amine process, MDEA process, G-V process, sulfolane process, A.D.A. process, hydroquinone process, vacuum carbonate process, tannin extract process, cobalt phthalocyanine process and the like mainly serve as primary desulfurization processes for removing hydrogen sulfide in industrial raw material gas but not CS in the gas ₂ The desulfurization methods have low desulfurization efficiency, high cost, serious crystallization blockage and serious corrosion, and meanwhile, part of desulfurization solution is often discharged to control the content of secondary salt in the desulfurization solution to improve the desulfurization effect, thereby causing direct environmental pollution; meanwhile, the methods use a large amount of toxic chemical reagents, cause secondary pollution and have undesirable comprehensive effect.

At the previous stage, we proposed "buffer solution method of ferrous hydroxide in acetic acid, sodium acetate and ammonia" [ see 1998 "journal of chemical industry", 49 (1), P48-58]And a gas decarbonization, desulfurization and decyanation method by using an iron-alkali solution catalysis method (see Chinese patent ZL 99100596.1)]And the like, we generally refer to such a desulfurization method as a "ferric alkali solution desulfurization method" or a "complex iron desulfurization method" or a "chelate iron desulfurization method" by a gas desulfurization method of absorbing hydrogen sulfide in a gas with an aqueous solution containing iron ions or complex iron and then oxidizing the absorbed hydrogen sulfide to elemental sulfur with air. In the actual operation process, the 'ferric alkali solution desulfurization method' or 'complex iron desulfurization method' or 'chelate iron desulfurization method' has high hydrogen sulfide removal efficiency, but the ferric alkali solution has poor stability, complex iron is easy to degrade, and a large amount of ferrous sulfide precipitates can be generated after the complex iron is contacted with hydrogen sulfide, so that the content of iron ions in the solution is rapidly reducedThe desulfurization effect is rapidly reduced, and the phenomenon of serious blockage of equipment such as a desulfurization tower is caused, so that the method is not suitable for the desulfurization of gas with high sulfur content. Meanwhile, the generated ferrous sulfide and the regenerated sulfur are mixed, and the mixture is like an earth explosive, and in the practical application process, the phenomena of spontaneous combustion and explosion occur. A great deal of practical demonstration shows that in all known iron compounds, even EDTA-Fe (ethylene diamine tetraacetic acid), NTA-Fe (aminotriacetic acid), and the like with the strongest stability are used, a great amount of ferrous sulfide precipitates to cause spontaneous combustion and explosion phenomena. In addition, because iron ions in the complexing iron are lost in the operation process, complexing ligands such as EDTA and NTA can form a large amount of salt crystals to cause crystallization blockage of equipment; meanwhile, the complex ligands can be slowly degraded into smaller organic acid salts and amine salts, and the organic acid salts and the amine salts are converted into strong surfactants, so that a large amount of virtual bubbles and flying bubbles are caused, the production is seriously influenced, and the production cannot be continued. Therefore, the 'iron-alkali solution' (complex iron) desulfurization method has great limitation and serious potential safety hazard. Therefore, for safety, we have not widely popularized and applied the "iron-base solution" (i.e. complex iron solution) desulfurization technique. In 1887, the Russian scientist Sergei Winogradsky discovered that beggaratoa (Beggiatoa) utilized hydrogen sulfide (H) ₂ S) as an energy source, CO ₂ As a mechanism of metabolism of the carbon source. After about 100 years, in 1984-1985, the research on oxidizing the sulfide in the wastewater by colorless sulfur oxidizing bacteria and oxygen in a dark environment by Cees Buisman of the Netherlands succeeded, and achieves the purpose of recovering sulfur, but the research only focuses on obtaining extracellular elemental sulfur. Later, the research mainly focuses on the application research field of sewage deodorization, the ThiOPAQ process technology is developed, in 1992, the ThiOPAQ technology is utilized by the people to remove hydrogen sulfide in the methane, and in 2002, the application in the field of natural gas desulfurization is realized in Canada.

Since 1995, our research team has been working on the field of gas biological desulfurization, and screened a sulfur-philic oxygen-consuming heat-resistant alkali-tolerant bacterium named "GDJ-3" from soil in a salt lake of inner Mongolia, which has a good homology with Alpha proteobacterium sp. (97%) and Ochrobactrum sp. (98%). The strain has good desulfurization effect and can be widely applied to the field of desulfurization of semi-water gas and shift gas for ammonia synthesis in China. For this reason, we developed "biochemical iron-alkali solution catalytic gas desulfurization method", and applied for and granted a national patent on 09.09.2002, and then we made a more detailed study on GDJ-3.

Since then, the research of biological desulfurization in China is getting more and more hot, but the research is a theoretical research staying in a laboratory, and large-scale industrial application is not obtained. For example, the horse of south China university initially discusses the desulfurization mechanism of DS-3 strain (Rhodococcus erythropolis), and confirms that the strain has 64.08% and 85.86% final desulfurization rates for 08 diesel oil and refined diesel oil, respectively, and can remove Dibenzothiophene (DBT) and DBT derivatives, but has relatively poor ability to remove BT and BT derivatives. There are also many researchers who use Rhodococcus erythropolis (Rhodococcus erythropolis), thiobacillus ferrooxidans (Thiobacillus ferrooxidans), thiobacillus thiooxidans (Thiobacillus thiooxidans), gordonia sp, pseudomonas sp, arthrobacter (Acinetobacter sp.), desulfurovibrio (Desulforicus), corynebacterium sp, brevibacterium (Brevibacterium sp.), nocardia sp, paenibacillus polymyxa (Paenibacillus yxa), mycobacterium phlei GTIS10, paenibacillus (Paenibacillus sp.) A11-2, thermomyces acidocaldarius (Sulfobacillus), briytrium sp), DBT, and the like, respectively, but there are no research on the use of organic sulfur ore, sulfur removal of sulfur, and other sulfur-producing substances, and the like in petroleum ore, and no research on the use of organic sulfur ore, sulfur removal of DBT, and the like. Some researchers have introduced the removal of H from natural gas by Thiobacillus ferrooxidans and Thiobacillus denitrificans ₂ S, converting into elemental sulfur. Some researchers have also paid attention toThe use of Thiobacillus thioparus for the removal of H from gases is described ₂ S, forming simple substance sulfur, thiosulfate, polythionate, sulfite, sulfate and other intermediate products. Still other investigators have reviewed the use of Thiobacillus thiooxidans (Thiobacillus thiooxidans) for the removal of H from gases ₂ S, forming intermediate products such as elemental sulfur, thiosulfate, sulfate and the like. Some researchers reviewed the removal of H from gas with Xanthomonas (Xanthomonas sp.) ₂ S, oxidizing into intermediate products such as elemental sulfur, thiosulfate, sulfate and the like. Some researchers have also reviewed the removal of H from gases with Pseudomonas acidovorans ₂ S, forming intermediate products such as elemental sulfur, thiosulfate, sulfate and the like. Some researchers have also reviewed the use of Pseudomonas putida (Pseudomonas putida) for H removal from gases ₂ S, forming intermediate products such as elemental sulfur, thiosulfate, sulfate and the like. Some researchers have also reviewed H removal from gases with Chlorella (Chlorobium limicola) ₂ S, forming intermediate products such as elemental sulfur, thiosulfate, sulfate and the like. Some investigators have also reviewed the use of Thiospira frischneisseria (Thiomicrospira frisia) species for H removal from gas ₂ S, besides being oxidized into elemental sulfur, intermediate products such as thiosulfate and sulfate can be generated. Some researchers have also reviewed the use of sulfur micro-spira sp for H removal from gases ₂ S, besides being oxidized into elemental sulfur, intermediate products such as thiosulfate and sulfate can be generated. Some researchers have also reviewed the use of Thioflavia leucovora (Thiothrix nivea) strains for H removal from gases ₂ S, besides being oxidized into elemental sulfur, intermediate products such as thiosulfate and sulfate can be generated. Some researchers also reviewed degassing with bacteria such as Microbacterium filatum (Hypericum sp.), chlorophorbide (Chlorobium thiophanate), phlebia hippophae (Prosthenia austerucii), rhodospirillum halorapana abdelmalekii, microbacterium sulforaphicum (Thiobacillus cyclicum), thiobacillus neapolis (Thiobacillus neophilus), thiobacillus novaeolicus (Thiobacillus novalus), thiobacillus albugineus (Thiobacillus albugineus), thiobacillus albugineus (Thiobacillus albertuss), thiobacillus intermedius (Thiobacillus altertis), thiobacillus metabolically deficient Thiobacillus (Thiobacillus protophilus), and the likeH in (1) ₂ S, forming intermediate products such as thiosulfate, sulfate and the like besides elemental sulfur. Some researchers have reviewed the removal of H from gases by bacteria such as Thermothermus (Thermothermus azorensis), microaerobic spirillum (Thiolalispira microaerophila), thiobacillus novellus, arthrobacter oxydans, and the like ₂ S, forming intermediate products such as elemental sulfur, thiosulfate, sulfate and the like. Some researchers have reviewed the removal of H from gases by bacteria such as Agrobacterium sp ₂ S, forming intermediate products such as elemental sulfur, thiosulfate, sulfate and the like. Some researchers have also reviewed the removal of H from gas with Paracoccus versitus (Paracoccus versitus) ₂ S, forming intermediate products such as elemental sulfur, thiosulfate, sulfate and the like. Some researchers have reviewed the removal of H from gases by Chromobacterium (Chromobacterium), achromobacter (Achromobacter), desulfuromonas (Desulfuromonas), mycobacterium (Mycobacterium), arthrobacter (Arthrobacter), flavobacterium (Flavobacterium), xanthobacter (Xanthobacter), and the like ₂ S, forming intermediate products such as elemental sulfur, thiosulfate, sulfate and the like. Some researchers have also reviewed the use of Thiobacillus thioparus (Thiobacillus thiopams) and Thiolalkalivibrio (Thiolalkalivibrio) for H removal from gases ₂ S, forming intermediate products such as elemental sulfur, thiosulfate, sulfate and the like. The common feature of these bacterial desulfations is the "oxidative conversion of hydrogen sulfide to elemental sulfur, with the coproduction of thiosulfate, sulfite and sulfate". Therefore, when desulfurization is performed using these bacteria, the desulfurization efficiency gradually decreases as the concentration of by-products such as sulfate, thiosulfate, polythionate, and sulfite in the desulfurization solution gradually increases, and when the concentration thereof reaches a saturated state, crystallization of sulfate and the like occurs, which causes clogging of the apparatus.

Disclosure of Invention

In view of one or more of the problems with the prior art, the present invention provides the use of Campylobacter xanthus in desulfurization. Specifically, hydrogen sulfide and/or organic sulfur in sulfur-containing gas is absorbed by biological desulfurization liquid containing halofilm Campylobacter flavus; the biological desulfurization solution absorbing the hydrogen sulfide and/or organic sulfur is oxidized and regenerated by air/oxygen, sulfur is by-produced, and the regenerated biological desulfurization solution is recycled.

The invention provides an application of Campylobacter flavus in desulfurization of gas containing hydrogen sulfide and/or organic sulfur.

Preferably, the sulfur is hydrogen sulfide and/or organic sulfur in the sulfur-containing gas.

Preferably, the sulfur-containing gas is natural gas, coke oven gas, oil field gas, water gas, blast furnace gas, city gas, synthetic ammonia semi-water gas and shift gas, synthetic waste gas of a dye factory, waste gas of a chemical fiber factory or methane; and/or

The total sulfur content in the sulfur-containing gas is less than 99.9% by volume.

When the Campylobacter flavus inhabitation salt film is used for desulfurization, no special requirement is made on the total sulfur content in the sulfur-containing gas before desulfurization, but in order to achieve better desulfurization effect, the total sulfide content in the sulfur-containing gas is preferably less than 99.9% (volume ratio).

Preferably, directly adding the bacteria liquid of the campylobacter flavus to the desulfurization liquid to prepare a biological desulfurization liquid, and performing desulfurization; or directly adding spores of Campylobacter flavus into the desulfurization solution, and gradually growing the spores into vegetative cells in the desulfurization process to perform desulfurization.

Preferably, the concentration of the bacteria liquid of the Campylobacter flavus in the desulfurization liquid is1 × 10 ² ～1×10 ¹⁹ One/ml, preferably at a concentration of 1X 10 ⁶ ～1×10 ¹⁰ One per ml.

The pH value of the biological desulfurization solution is 2-12, and the pH value is preferably not less than 7 and not more than 9.

The invention does not limit the concentration of the desulfurization bacteria in the biological desulfurization solution, but the optimal concentration of the desulfurization bacteria in the biological desulfurization solution is1 x 10 ⁶ ～1×10 ¹⁰ Per ml; the pH value of the biological desulfurization solution is not particularly required, but is optimally kept within the range of 7-9 in order to prevent acid-base corrosion of equipment.

Preferably, the desulfurization is carried out by absorption under normal pressure; when the absorption is carried out under the normal pressure, the absorption temperature is 0-80 ℃.

More preferably, the absorption temperature is 15 to 25 ℃ in the absorption under normal pressure.

Preferably, after desulfurization, air/oxygen is introduced into the bacteria liquid of the Campylobacter flavus to regenerate the Campylobacter flavus, and sulfur is by-produced.

Preferably, the regeneration is carried out under normal pressure to regenerate the Campylobacter flavus; when the regeneration is carried out under the normal pressure, the regeneration temperature is 0-100 ℃.

More preferably, the regeneration temperature is 25 to 40 ℃ in the regeneration under the normal pressure.

When the campylobacter flavus inhabitation membrane is used for desulfurization, the process conditions are not strictly limited, and the process conditions can be normal pressure absorption, negative pressure absorption or pressurized absorption, but the normal pressure absorption is preferably adopted; when regenerating at normal pressure, the absorption temperature is 0-80 deg.C, and the regeneration temperature is 0-100 deg.C.

The previous researches show that in the campylobacter flavus desulfurization method, the bacteria can directly swallow sulfur-containing compounds into the bacteria, and then carry out aerobic digestion to convert the sulfur-containing compounds into elemental sulfur; the sulfur-containing compound may be hydrogen sulfide (H) ₂ S), carbon disulfide (CS) ₂ ) And sulfur-oxidized carbon (carbonyl sulfide COS), mercaptans (R-SH), thioethers (R-S-R'), and the like, which are volatile organic sulfur compounds. For convenience of presentation, we indicate as "< desulfurizing bacteria", so that the basic principle of the present invention is roughly summarized as follows:

when the gas contacts with the biological desulfurization solution, the following absorption reaction occurs:

⊙+H ₂ S→⊙-H ₂ S

⊙+COS→⊙-COS

⊙+CS ₂ →⊙-CS ₂

⊙+R-SH→⊙-R-SH

⊙+R-S-R’→⊙-R-S-R’

the sulfide-absorbed biological desulfurization solution is hereinafter referred to as "rich solution". The 'rich solution' is oxidized and regenerated by air under the action of the desulfurization bacteria, and the following regeneration reaction can occur:

⊙-H ₂ S+1/2O ₂ →S+H ₂ O+⊙

⊙-COS+1/2O ₂ →CO ₂ +S+⊙

⊙-CS ₂ +O ₂ →CO ₂ +2S+⊙

⊙-R-SH+1/2O ₂ →R-OH+S+⊙

⊙-R-S-R’+1/2O ₂ →R-O-R’+S+⊙

the rich solution after air oxidation is regenerated and converted into lean solution (i.e. biological desulfurization solution from which sulfide is removed), and the lean solution is recycled.

The main purpose of the invention is mainly the practicability of removing the sulfur-containing compounds in the gas, so the invention is directly applied to the actual production device, and the biological desulfurization solution can be recycled as long as the biological desulfurization solution is safe and stable and has high desulfurization efficiency; therefore, the detailed mechanism of the absorption reaction and regeneration reaction of bacterial desulfurization has not been studied in depth.

In order to realize the desulfurization process, the inventor of the application carries out direct production test on the existing desulfurization device in the coke oven gas desulfurization process of Tonglingtai special material company Limited. There are two types of coke oven gas desulfurization processes by holy taifu special materials limited: the first is normal pressure absorption, high tower regeneration flow (referred to as "high tower regeneration flow" for short); the second is a normal pressure absorption, jet absorption air regeneration process (referred to as "one tower process" for short).

The first is normal pressure absorption, high tower regeneration flow: directly adding desulfurization bacteria into desulfurization solution in two sets of desulfurization devices in high tower regeneration process of existing ammonia method desulfurization to control bacteria concentration to be 1 x 10 ⁶ ～1×10 ¹⁰ And (4) performing desulfurization test.

The second is a normal pressure absorption and jet absorption air regeneration process: directly adding desulfurization bacteria into desulfurization solution in a set of desulfurization devices of a tower-type process of the existing ammonia method desulfurization to control the bacteria concentration to be 1 x 10 ⁶ ～1×10 ¹⁰ And (4) performing desulfurization test on the sample per ml.

The campylobacter flavus with the saliferous membrane has wide industrial application in the field of sulfur-containing gas desulfurization, can be used for desulfurization of natural gas, coke oven gas, oil field gas, water gas, blast furnace gas, urban gas, synthetic ammonia semi-water gas and conversion gas, synthetic waste gas of dye factories, waste gas of chemical fiber factories, biogas and other industrial raw gas or waste gas containing hydrogen sulfide and organic sulfur, and the total sulfur content of the sulfur-containing gas is less than 99.9 percent (volume ratio). Not only can remove hydrogen sulfide in the organic sulfur, but also has certain removal capacity for organic sulfur. And the traditional wet desulphurization method can not keep high desulphurization efficiency economically for a long time, but the desulphurization method can keep high desulphurization efficiency economically for a long time because the halophilic membrane campylobacter flavus can be regenerated and used.

Drawings

The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:

FIG. 1 is a schematic diagram of a laboratory desulfurization screening test apparatus.

FIG. 2 is a schematic diagram of an atmospheric absorption, high tower regeneration scheme in accordance with a first embodiment.

FIG. 3 is a schematic diagram of a regeneration process of the air by the atmospheric absorption and the spray absorption according to the second embodiment.

Detailed Description

A method of desulfurizing Campylobacter flavus of the present invention is described below with reference to specific embodiments for better illustrating the present invention and should not be construed as limiting the claims of the present invention.

The strain Flavellex salsolisticola used in the present invention was purchased from Ningbo Ming boat Biotech Co.

According to the information on the above purchased strains provided by Ningboming Biotechnology Co., ltd: the strain is named as Flavilex salsolisticola and belongs to the phylum Actinomycetales (actinobacillia)/class actinomycetes (actinobacillia)/order actinomycetes (actinomycetes)/family Campylobacter (actinomycetes)/genus Flaviviridae (Flaviformex). And "Other names" is written in the purchase information: KCTC 33148".

In addition, my sequenced 16S rRNA on this strain after purchase, with the following results: CCTGGGATCGCAAGCGCAAGGGCCCGTGAACGTGCGTGACCGCAGGGCCTGCGTGAACGTGCGTGCGGCCAAGGGCCCGTGAGGGCCCGTGAGGGCCCGTGAGGGCCCGTGAGGGCCCGTGAGGGCCCGTGAGGGCCCGTGAGGGCCCGTGAGGGCCCGTGAGGGCCCGTGAGGGCCCGTGAGGGCCCGTGAGCGTGAGCGTGAGCCTGAGGGCCCGTGAGGGCCCGTGAGGGCCCGTGAGCGTGAGCCCGTGAGGGCCCGTGAGGGCCCGTGAGGGCCCGTGAGGGCCCGTGAGCGTGAGCGTGAGCCTGAGGGCCCGTGAGCGTGAGCCTGAGCGTGAGCGTGAGCCCGTGAGCGTCCGTGAGGGCCCGTGAGGGCCCGTGAGGGCCCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTCCGTGAGCGTCCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTCCGCGTGAGCGCGCGCGCGCGCGCGCGCGCGTGAGCGCGCGTGAACGGGCCTGAGCGTGAGCGGGCCTGAGCGTGAGCGGGCCTGAGCGTGAGCGCGTGAGCGTGAGCGTCCGTGAGCGTGAGCGCGCGCGCGCGCGCGCGCGCGCGCGTCCGTGAGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGAGCGAGCGCGCGAGCGAGCGTCCGTCCGTCCGTCCGCGCGCGCGCGCGAGCGAGCGAGCGAGCGAGCGAGCGTCCGTCCGCGCGCGCGCGTCCGTGAGCGCGCGAGCGCGCGCGCGAGCGAGCGAGCGAGCGAGCGTGAGCGTGAGCGAGCGAGCGTGAGCGTCCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGAGCGCGCGCGCGCGCGCGCGCGCGCGCGCGTCCGTCCGCGAGCGTCCGTCCGTCCGTCCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTCCGTCCGTGAGCGTCCGTCCGTGAGCGTCCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGTGAGCGCGCGTGAGCGTGAGCGCGCGCGCGTGAGCGCGCGCGCGCGTGAGCGTGAGCGTCCGTGAGCGTGAGCGTGAGCGTGAGCGCGTGAGCGTGAGCGTGAGCGCGCGTGAACGCGCGTGAGCGTGAGCGTGAGCGTGAGCGCGCGCGCGTCCGTCCGCGCGCGCGCGCGCGCGCGCGTGAGCGTGAGCGTGAACGTGAGCGTGAGCGTGAGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGTGAGCGTGAGCGTGAGCGCGCGCGCGCGCGCGCGCGTGAGCGTGAGCGCGCGCGCGCGCGAGCGTGAGCGCGAGCGCGCGCGCGTGAGCGCGCGCGCGCGCGCGCGCGCGCGTGAGCGCGTCCGTGAACGCGCGTGAGCGTGAGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGTCCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGTGAGCGTCCGTCCGTCCGTCCGCGCGCGCGCGCGTGAGCGTGAGCGAGCGCGTGAGCGTGAGCGTGAGCGCGCGCGCGCGCGCGCGCGCGTCCGCGCGCGTCCGTCCGTGAGCGCGCGCGCGCGCGCGTGAGCGTGAGCGCGCGCGCGAGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGTCCGCGCGCGCGCGCGCGTGAGCGTGAGCGCGCGTGAGCGTGAGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGCGTCCGTCCGCGCGCGCGCGCGCGCGCGTCCGCGCGTGAACGTGAACGCGCGCGCGCGCGCGCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTGAACGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTGAACGTCCGTCCGTGAGCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGCGCGCGCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGTCCGCGCGCGTGAGCGTGAGCGCGCGTCCGTCCGTCCGTCCGTGAACGTGAACGTCCGTCCG

Compared with the gene sequence of the strain KCTC 33148, the similarity is 99.92 percent. Therefore, the Chinese name of the purchased strain should be Campylobacter salsibioticola (Flavellex sarstriicola). Hereinafter, it will be described as "Campylobacter xanthiformis (Flaviflexus salsibiricoscola)".

Example 1

The method for the enlarged culture of the campylobacter flavus in the salt-inhabiting membrane comprises the following steps:

the glycerol-preserved strains were recovered and cultured in a solid medium at 28 ℃ for 24 hours in an incubator. Scraping off the whole flora of Campylobacter salpingii (Flavellex salsiostigmala) on the cultured solid culture medium, pouring into a triangular flask containing 120ml of liquid culture medium, dispersing, and shaking uniformly to obtain the enrichment culture mother liquor. Adding 5ml of fresh enrichment culture mother liquor into 24 triangular flasks respectively filled with 120ml of liquid culture medium, wrapping triangular flask mouths, putting the triangular flasks into a bacteria culture shaking table, and culturing for 3-5 days at 28 ℃ and 150r/min to obtain the enrichment culture liquor. The proliferating bacteria liquid can be directly used for industrial production.

Liquid medium composition (g/L): 5.0 of peptone, 1.0 of yeast powder, 0.1 of ferric citrate, 19.45 of sodium chloride, 5.98 of magnesium chloride, 3.24 of sodium sulfate, 1.8 of calcium chloride, 0.55 of potassium chloride, 0.16 of sodium carbonate, 0.08 of potassium bromide, 0.034 of strontium chloride, 0.022 of boric acid, 0.004 of sodium silicate, 0.0024 of sodium fluoride, 0.0016 of sodium nitrate and 0.008 of disodium hydrogen phosphate, wherein the pH value is 7.6 +/-0.2 and 28 ℃.

The solid medium is simply a liquid medium to which an appropriate agar is added.

The applicant first carried out a laboratory desulfurization test on a campylobacter flaviflex salstrioticola bacterial solution (a proliferated bacterial solution obtained by the above culture) of the halophilic membrane yellow.

The laboratory desulfurization test apparatus is shown in FIG. 1.

FIG. 1 is a schematic diagram of a laboratory desulfurization test apparatus. Wherein, 1 is an absorption bottle, 2 is a bacterium liquid, 3 is a gas inlet, and 4 is a gas outlet.

Referring to fig. 1, the operating method for the laboratory desulfurization screening test was: about 150ml of Campylobacter flavus strain liquid 2 (prepared at a strain concentration of 10) ⁶ ～10 ⁷ Pieces/ml) is filled into a 250ml glass absorption bottle 1, gas containing hydrogen sulfide (the concentration of the hydrogen sulfide in nitrogen is about 10000ppm (volume ratio) and the flow rate is controlled at 80 ml/min) is led into the absorption bottle 1 from a gas inlet 3, and the hydrogen sulfide is absorbed by a bacterium liquid 2 after passing through a bacterium liquid 2 layer; the gas without hydrogen sulfide flows out from the gas outlet 4 and enters an absorption bottle filled with blue iodine-containing starch solution, and if the blue iodine-containing starch solution is colorless, the bacteria liquid 2 absorbs the blue iodine-containing starch solutionWhen saturated with hydrogen sulfide, absorption was stopped and the absorption time t (min) was recorded. Then, the bacterial liquid 2 saturated by absorbing hydrogen sulfide is regenerated, and the regeneration step is as follows: air (the flow rate is controlled to be about 200 ml/min) is introduced into the absorption bottle 1 from the gas inlet 3, and hydrogen sulfide in the bacterial liquid 2 is metabolized into elemental sulfur by bacteria after passing through the bacterial liquid 2 layer absorbing the hydrogen sulfide; after regeneration, the gas flows out from the gas outlet 4, is vented and is regenerated for 30min. The regenerated bacteria liquid 2 is used for absorbing hydrogen sulfide after elemental sulfur is removed: still repeating the above absorbing step; then, repeating the above regeneration steps, thus, absorbing and regenerating; and (3) absorbing and regenerating again, and then recording the saturation time t of absorption, the pH value before absorption (or the pH value after regeneration) and the pH value after absorption of each time. First, we carried out a reference experiment using 150ml of sodium carbonate solution having a concentration of 3g/L in the above manner, and the results of the experiment on the absorption of hydrogen sulfide by the reference solution are shown in Table 1. Then, the Campylobacter flavus bacterium composition solution 2 of the present invention (the bacterium concentration was adjusted to 10) was added to 150ml of a 3% sodium carbonate solution ⁶ ～10 ⁷ One/ml), repeating the above experiment, the experiment result of the present invention for absorbing hydrogen sulfide by the campylobacter flavus bacteria liquid is shown in table 2. (note in particular that the newly prepared 3% sodium carbonate solution has a high pH value and is unstable, so that the absorption time is long just before the start of the preparation, so that the previous unstable data are not needed, and only the experimental data after the pH value is slightly stable are adopted, the experimental temperature of the experiment is 35 ℃).

TABLE 1 150ml of 3g/L sodium carbonate solution in gas H ₂ The S concentration is 9995ppm (volume ratio), the flow is 80ml/min, the normal pressure is normal pressure, 35 ℃, the absorption saturation experiment result is obtained

TABLE 2 adding the yellow bend of the salt-centered film to a 3g/L solution of 150ml sodium carbonateA desulfurization solution (total bacterial concentration is 10) composed of aspergillus (Flavelexus salsolicatia) ⁶ ～10 ⁷ One/ml), H in gas ₂ The S concentration is 9995ppm (volume ratio), and the flow rate is 80ml/min

The experimental result of absorption saturation at normal pressure and 35 DEG C

As can be seen from the data in tables 1 and 2, the desulfurization solution containing Campylobacter flavus (Flavellex salstriostrea) has good desulfurization ability and has good ability to continue desulfurization after regeneration and recovery.

In order to reduce the test workload and ensure the test result to be real and effective, the production experiment of desulfurization is directly carried out on the coke oven gas desulfurization process device of the special material rich in cupling taifu company by using the flaviflex salsoliiostraticola (the proliferated bacteria liquid obtained above). The enterprise has two desulfurization processes: the first is normal pressure absorption, high tower regeneration flow (referred to as "high tower regeneration flow" for short); the second is a normal pressure absorption, jet absorption air regeneration process (referred to as a tower process for short); the actual process flow is as follows: two sets of identical high tower regeneration processes are connected in parallel for desulfurization (generally called 'primary desulfurization'), then coke oven gas after being connected in parallel for desulfurization is mixed together, and then the mixed gas enters a desulfurization device of a tower type tower process for further desulfurization (generally called 'secondary desulfurization').

Wherein, the first normal pressure absorption and high tower regeneration process: directly adding halomembrane campylobacter flavus into the desulfurization solution in two sets of desulfurization devices in the high tower regeneration process of ammonia desulfurization to control the bacterial concentration to be 1 x 10 ⁸ And (4) obtaining a biological desulfurization solution for desulfurization test.

The second normal pressure absorption and jet absorption air regeneration process comprises the following steps: directly adding halomembrane yellow campylobacter into the desulfurizing liquid in a set of desulfurizing device of tower-type process of ammonia desulfurization to control its bacterial concentration at 1X 10 ⁸ And (4) obtaining biological desulfurization solution for desulfurization test.

The first embodiment ("high tower regeneration scheme") is shown in figure 2.

FIG. 2 is a schematic diagram of an atmospheric absorption, high tower regeneration scheme according to the first embodiment. Wherein, 1 is coke oven gas before desulfurization, 2 is a desulfurizing tower, 3 is desulfurized coke oven gas, 4 is barren liquor, 5 is rich liquor, 6 is a desulfurizing liquor circulating tank, 7 is a desulfurizing pump, 8 is a high tower regeneration tower, 9 is air, 10 is an air compressor, 11 is sulfur foam, 12 is vent gas, 13 is a sulfur foam tank, 14 is a sulfur foam pump, 15 is a filter, 16 is sulfur paste, 17 is filtrate, 18 is a filtrate tank, and 19 is a filtrate pump.

Among them, the biological desulfurization solution in which the sulfide is absorbed is called "rich solution".

The 'rich solution' after air oxidation is regenerated and converted into 'lean solution', and the 'lean solution' is recycled.

Referring to fig. 2, coke oven gas 1 enters from the bottom of a desulfurizing tower 2 before desulfurization and is in countercurrent contact with barren liquor 4 sprayed from the top; sulfur-containing compounds in the coke oven gas 1 before desulfurization are absorbed by the barren solution 4, and the coke oven gas 1 before desulfurization is converted into desulfurized coke oven gas 3 (called as 'coke oven gas after primary desulfurization') which flows out from the top of the desulfurizing tower 2; the lean solution 4 having absorbed the sulfur-containing compounds is converted into a rich solution 5 at the bottom of the desulfurization tower 2; the rich liquid 5 flows out from the bottom of the desulfurizing tower 2, enters a desulfurizing liquid circulation tank 6, is sent into a high tower regeneration tower 8 from the bottom by a desulfurizing pump 7, air 9 is pressurized by an air compressor 10 and then also enters the high tower regeneration tower 8 from the bottom, in the high tower regeneration tower 8, the rich liquid 5 and the air 9 are fully mixed, sulfur-containing compounds in the rich liquid 5 are metabolized into elemental sulfur by bacteria by using oxygen to form sulfur foam 11, the sulfur foam 11 is floated to the top of the high tower regeneration tower 8 and then automatically overflows to a sulfur foam tank 13, and then is sent to a filter 15 by a sulfur foam pump 14 for filtering to obtain sulfur paste 16 and filtrate 17, the sulfur paste 16 can be sold as a byproduct, and the filtrate 17 enters a filtrate tank 18 and then is sent to the desulfurizing liquid circulation tank 6 by a filtrate pump 19 for recycling; the air 9 is changed into vent gas 12 after reacting in the high tower regeneration tower 8 and is released to the outside; after the air 9 is metabolized and regenerated by bacteria in the high tower regeneration tower 8, the rich solution 5 is converted into the lean solution 4, and the lean solution 4 automatically flows into the desulfurization tower 2 for recycling.

In the first embodiment, a coke oven gas desulfurization test is performed on two sets of parallel high tower regeneration primary desulfurization system devices of a coke oven gas desulfurization system of the special material of holy taifu company, the implementation flow is shown in fig. 2, and the equipment specifications and parameters are shown in table 3.

Wherein, the temperature in normal pressure absorption is 35 ℃, and the regeneration temperature in normal pressure regeneration is 40 ℃.

Table 3 specifications of each apparatus in the first embodiment

Device	Specification (mm)	Number of	Remarks for note
				Desulfurizing tower (2)	DN7000×32300	2 (parallel)
High tower regenerative tower (8)	DN5000×47000	2
				Doctor solution circulation tank (6)	DN4600L＝12440	2
Desulphurization pump (7)	Q＝2500m ³ /h，H＝60	3	Two switches on and one switch off
				Air compressor (10)	DN5000×5400	1
Sulfur foam tank (13)	DN3400，H＝6030	2
				Sulfur foam pump (14)	Q＝30m ³ /h，H＝50	2	One for one and one for one
Filter (15)	Filter area 150 square meter	2
				Filtrate tank (18)	DN2800×2125	1
Filtrate pump (19)	Q＝30m ³ /h，H＝35m	2	One for one and one for one

Before 12 months in 2018, the enterprise carries out desulfurization by using a desulfurization method (hereinafter, referred to as a 'PDS' method for short, the desulfurization method is a method for removing hydrogen sulfide widely used in industrial production in China) by using cobalt phthalocyanine as a catalyst, and the operation conditions of a tower No. 1 and a tower No. 2 are shown in tables 5 and 6. After 12 months from 2018, the enterprise adds the campylobacter flavus of the invention into the desulfurization solution of the existing desulfurization process, and the enterprise performs desulfurization by using the campylobacter flavus of the invention (hereinafter, abbreviated as "DDS" method), and the operation conditions of the tower # 1 and the tower # 2 in 2019, 2020 and 2021 are shown in tables 8 and 9, 11 and 12, and 14 and 15. From the operating point of view, the desulfurization efficiency of the DDS is higher than that of the PDS under the same conditions.

The second embodiment ("one-column flow scheme") is shown in FIG. 3.

FIG. 3 is a schematic diagram of a regeneration process of the air by the atmospheric absorption and the spray absorption according to the second embodiment. Wherein 3 is the coke oven gas after primary desulfurization, 20 is a tower type desulfurization tower, 21 is a tower type desulfurized coke oven gas, 22 is a tower type regeneration tank, 23 is a tower type barren liquor, 24 is a tower type pregnant solution, 25 is a desulfurization regeneration pump, 26 is an air injection absorber, 27 is air, 28 is vent gas, 29 is sulfur foam, 30 is a sulfur foam tank, 31 is a sulfur foam pump, 32 is a filter, 33 is filtrate, 34 is sulfur paste, 35 is a filtrate tank, and 36 is a filtrate pump.

Referring to fig. 3, the coke oven gas 3 after the first-stage desulfurization enters from the bottom of a tower-type desulfurization tower 20 and is in countercurrent contact with a tower-type barren solution 23 sprayed from the top; sulfur-containing compounds in the coke oven gas 3 subjected to the primary desulfurization are absorbed by a tower-type barren liquor 23, and the coke oven gas 3 subjected to the primary desulfurization is converted into tower-type desulfurized coke oven gas 21 which flows out from a gas outlet of a tower-type desulfurizing tower 20; the tower lean liquid 23 having absorbed the sulfur compounds is converted into a tower rich liquid 24 at the bottom of a tower desulfurization tower 20; a tower-type rich liquid 24 is pumped from the bottom of a tower-type desulfurization tower 20 by a desulfurization regeneration pump 25, enters an air injection absorber 26 after being pressurized, and absorbs air 27; a tower-type rich liquid 24 and air 27 are fully and uniformly mixed in an air jet absorber 26, and then enter the regeneration tank 22 from the bottom through a tail pipe of the air jet absorber 26; in the regeneration tank 22, a tower-type rich liquid 24 and air 27 are fully mixed, sulfur-containing compounds in the tower-type rich liquid 24 are metabolized into elemental sulfur by bacteria to form sulfur foam 29, then the sulfur foam automatically overflows to a sulfur foam tank 30, and then the sulfur foam is sent to a filter 32 by a sulfur foam pump 31 to be filtered, so that sulfur paste 34 and filtrate 33 are obtained through filtration; the sulfur paste 34 may be sold as a by-product; the filtrate 33 enters a filtrate tank 35 and is sent to a tower-type desulfurizing tower 20 by a filtrate pump 36 for recycling; the air 27 becomes the blow air 28 to be released to the outside; after the air 27 is regenerated in the regeneration tank 22, a tower rich liquid 24 is converted into a tower lean liquid 23, and automatically flows into a tower desulfurizing tower 20 from a desulfurizing liquid inlet for recycling.

In the second embodiment, a coke oven gas desulfurization test is performed on a tower type secondary desulfurization system device of a coke oven gas desulfurization system of the special material of holy taifu company, the implementation flow is shown in fig. 3, and the equipment specifications and parameters are shown in table 4.

Wherein, the temperature during normal pressure absorption is 35 ℃, and the regeneration temperature during normal pressure regeneration is 40 ℃.

TABLE 4 specification of each apparatus in the second embodiment

Device	Specification (mm)	Number of	Remarks to note
				A tower type desulfurizing tower (20)	DN9000×30000	1
A tower type regeneration tower (22)	DN9000/10000，H＝12900	1	At the top of a tower-type desulfurizing tower
				Desulphurization pump (25)	Q＝2500m ³ /h，H＝60	2	One for one and one for one
Ejector (26)	50m ³ /h	60 are	30 to 50 long openings
				Sulfur foam tank (30)	DN3400，H＝6030	1
Sulfur foam pump (31)	Q＝30m ³ /h，H＝50	2	One for one and one for one
				Filter (32)	Filter area 150 square meter	1
Filtrate tank (35)	DN2800×2125	1
				Filtrate pump (36)	Q＝30m ³ /h，H＝35m	2	One for one and one for one

Before 12 months in 2018, the enterprise carries out desulfurization by a desulfurization method (hereinafter referred to as a "PDS" method) by using cobalt phthalocyanine as a catalyst, and the operation condition of a desulfurization device of a tower process is shown in Table 7. After 12 months in 2018, the enterprise adds the campylobacter xanthus of the invention into the desulfurization solution of the existing desulfurization process (hereinafter, abbreviated as "DDS" method) for desulfurization, and the operation conditions of the desulfurization device of the tower process in 2019, 2020 and 2021 are shown in tables 10, 13 and 16. From the operating point of view, the desulfurization efficiency of DDS is far higher than that of PDS under the same conditions.

TABLE 5 run of column # 1 using PDS in 2018

TABLE 6 run of column # 2 using PDS in 2018

TABLE 7 run in 2018 with PDS in tower form

TABLE 8 run of tower # 1 using DDS in 2019

TABLE 9 run of tower # 2 using DDS in 2019

TABLE 10 run in 2019 with one tower DDS

TABLE 11 operation of # 1 tower with DDS in 2020

TABLE 12 operation of 2# column with DDS in 2020

TABLE 13 operation conditions in 2020 when DDS is used in one tower

TABLE 14 operation of DDS for column # 1 using 2021

TABLE 15 DDS operation of column # 2 using the year 2021

TABLE 16 operation of DDS in tower form in 2021

(Note: data in tables 5 to 16, operational data due to production abnormality is removed).

Finally, it should be noted that: although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that changes may be made in the embodiments and/or equivalents thereof without departing from the spirit and scope of the invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Sequence listing

<110> Beijing Boyuan Hengsheng technology Limited

TONGLING PACIFIC SPECIAL MATERIALS Co.,Ltd.

Beijing Hengtai Yuan Shenggao Tech Co Ltd

Jiangxi Yongfeng Boyuan Industrial Co.,Ltd.

Beijing Honglong environmental protection Co Ltd

<120> application of Campylobacter flavus in desulfurization

<160> 1

<170> SIPOSequenceListing 1.0

<210> 1

<211> 1322

<212> DNA

<213> Curvularia flavus (Flaviflexus salsibostriata)

<400> 1

gtggattagt ggcgaacggg tgagtaacac gtgagtaacc tgcccctttc ttcgggataa 60

gcttgggaaa ctgggtctaa taccggatat tcagcggctg ccgcatggtg gttgttggaa 120

agatttattg ggaggggatg ggctcgcggc ctatcagctt gttggtgggg tgatggccta 180

ccaaggcgtc gacgggtagc cggcctgaga gggtgaccgg ccacactggg actgagatac 240

ggcccagact cctacgggag gcagcagtgg ggaatattgc acaatgagcg aaagcttgat 300

gcagcgacgc cgcgtgaggg atgacggctt tcgggttgta aacctctttc ggcagggaac 360

aagtccaggt tttggcctgg ttgagggtac ctgcataaga agcgccggct aactacgtgc 420

cagcagccgc ggtaatacgt agggcgcgag cgttgtccgg aattattggg cgtaaagagc 480

tcgtaggcgg cttgtcgcgt ctgctgtgaa aacgcggggc ttaactccgc gcttgcagtg 540

ggtacgggca ggcttgagtg tagtagggga gactggaatt cctggtgtag cggtggaatg 600

cgcagatatc aggaggaaca ccgatggcga aggcaggtct ctgggctata actgacgctg 660

aggagcgaaa gcatggggag cgaacaggat tagataccct ggtagtccat gccgtaaacg 720

ttgggcacta ggtgtggggg tttttgactt ctgcgccgta gctaacgcat taagtgcccc 780

gcctggggag tacggccgca aggctaaaac tcaaaggaat tgacgggggc ccgcacaagc 840

ggcggagcat gcggattaat tcgatgcaac gcgaagaacc ttaccaaggc ttgacataca 900

ctgcgatgtt ccagagatgg ggcagccttc ggggtggtgt acaggtggtg catggttgtc 960

gtcagctcgt gtcgtgagat gttgggttaa gtcccgcaac gagcgcaacc cttgtctcgt 1020

gttgccagca catgatggtg gggactcacg agagactgcc ggggttaact cggaggaagg 1080

tggggatgac gtcaaatcat catgcccctt atgtcttggg cttcacgcat gctacaatgg 1140

ccggtacaga gggttgcgat gtcgtaaggc tgagcgaatc ccttaaagcc ggtctcagtt 1200

cggattgggg tctgcaactc gaccccatga agtcggagtc gctagtaatc gcagatcagc 1260

aacgctgcgg tgaatacgtt cccgggcctt gtacacaccg cccgtcacgt cacgaaagtt 1320

gg 1322

Claims

1. Use of Campylobacter xanthus in the desulfurization of a gas containing hydrogen sulfide and/or organic sulfur.

2. Use according to claim 1, characterized in that: the desulfurization is to remove hydrogen sulfide and/or organic sulfur in the sulfur-containing gas.

3. Use according to claim 2, characterized in that: the sulfur-containing gas is natural gas, coke oven gas, oil field gas, blast furnace gas, city gas, gas, water gas, synthetic ammonia semi-water gas, shift gas, synthetic waste gas of a dye plant, sewage gas of a chemical fiber plant or methane; and/or

4. Use according to any one of claims 1 to 3, characterized in that: directly adding the bacteria liquid of the campylobacter xanthum into the desulfurization liquid to prepare a biological desulfurization liquid for desulfurization; or directly adding spores of Campylobacter flavus into the desulfurization solution, and gradually growing the spores into vegetative cells in the desulfurization process to perform desulfurization.

5. Use according to claim 4, characterized in that: the concentration of the Campylobacter flavus in the desulfurization solution is1 × 10 ² ~1×10 ¹⁹ Per ml; and/or

The pH value of the biological desulfurization solution is 2 to 12.

6. Use according to claim 5, characterized in that: the concentration of the campylobacter flavus in the desulfurization solution is1 multiplied by 10 ⁶ ~1×10 ¹⁰ Per ml; and/or

The pH value of the biological desulfurization solution is more than or equal to 7 and less than or equal to 9.

7. Use according to claim 1, characterized in that: absorbing at normal pressure for desulfurization; when the absorption is carried out under the normal pressure, the absorption temperature is 0 to 80 ℃.

8. Use according to claim 7, characterized in that: when the absorption is carried out under normal pressure, the absorption temperature is 15 to 25 ℃.

9. Use according to claim 1, 2, 3, 7 or 8, characterized in that: and after desulfurization, introducing air/oxygen into the bacteria liquid of the campylobacter flavus to regenerate the campylobacter flavus, and producing a byproduct of sulfur.

10. Use according to claim 4, characterized in that: and after desulfurization, introducing air/oxygen into the bacteria liquid of the campylobacter flavus to regenerate the campylobacter flavus, and producing a byproduct of sulfur.

11. Use according to claim 5, characterized in that: and after desulfurization, introducing air/oxygen into the bacteria liquid of the Campylobacter halophila to regenerate the Campylobacter halophila, and by-producing sulfur.

12. Use according to claim 6, characterized in that: and after desulfurization, introducing air/oxygen into the bacteria liquid of the campylobacter flavus to regenerate the campylobacter flavus, and producing a byproduct of sulfur.

13. Use according to claim 9, characterized in that: regenerating the campylobacter xanthus at normal pressure; and when the regeneration is carried out under the normal pressure, the regeneration temperature is 0-100 ℃.

14. Use according to claim 10, characterized in that: regenerating the campylobacter xanthus at normal pressure; and when the regeneration is carried out under the normal pressure, the regeneration temperature is 0-100 ℃.

15. Use according to claim 11, characterized in that: regenerating the campylobacter xanthus at normal pressure; and when the regeneration is carried out under the normal pressure, the regeneration temperature is 0-100 ℃.

16. Use according to claim 12, characterized in that: regeneration under normal pressure is selected for regeneration of the campylobacter xanthus; and when the regeneration is carried out under the normal pressure, the regeneration temperature is 0-100 ℃.

17. Use according to claim 13, characterized in that: and when the regeneration is carried out under the normal pressure, the regeneration temperature is 25 to 40 ℃.

18. Use according to claim 14, characterized in that: and when the regeneration is carried out under the normal pressure, the regeneration temperature is 25 to 40 ℃.

19. Use according to claim 15, characterized in that: and when the regeneration is carried out under the normal pressure, the regeneration temperature is 25 to 40 ℃.

20. Use according to claim 16, characterized in that: and when the regeneration is carried out under the normal pressure, the regeneration temperature is 25 to 40 ℃.