CN110982566A - Process for removing organic sulfur in natural gas - Google Patents
Process for removing organic sulfur in natural gas Download PDFInfo
- Publication number
- CN110982566A CN110982566A CN201911363426.2A CN201911363426A CN110982566A CN 110982566 A CN110982566 A CN 110982566A CN 201911363426 A CN201911363426 A CN 201911363426A CN 110982566 A CN110982566 A CN 110982566A
- Authority
- CN
- China
- Prior art keywords
- organic sulfur
- natural gas
- gas
- hydrogen sulfide
- desulfurized
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/103—Sulfur containing contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/14—Injection, e.g. in a reactor or a fuel stream during fuel production
- C10L2290/141—Injection, e.g. in a reactor or a fuel stream during fuel production of additive or catalyst
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/542—Adsorption of impurities during preparation or upgrading of a fuel
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/547—Filtration for separating fractions, components or impurities during preparation or upgrading of a fuel
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Gas Separation By Absorption (AREA)
- Industrial Gases (AREA)
Abstract
The invention relates to the technical field of natural gas purification in the oil field gas industry, in particular to a process for removing organic sulfur in natural gas, wherein the organic sulfur is carbonyl sulfur, mercaptan or thioether organic sulfur, the organic sulfur is subjected to catalytic hydrolysis or catalytic thermal cracking by a catalytic adsorption type organic sulfur desulfurizer to be converted into hydrogen sulfide, and then the hydrogen sulfide reacts with active components in the catalytic adsorption type organic sulfur desulfurizer to generate metal sulfide to be removed. The invention has simple process, low production cost, low energy consumption, high desulfurization precision and high desulfurization efficiency of 98 percent; safe and environment-friendly, and no waste liquid or waste gas is discharged in the process.
Description
Technical Field
The invention relates to the technical field of natural gas purification in the oil field gas industry, in particular to a process for removing organic sulfur in natural gas.
Background
Natural gas is a high quality, economical, clean energy source, and its composition is mainly methane, and contains a small amount of ethane. Compared with other energy sources, the natural gas has the advantages of convenient use, economy, safety, high heat generation, less pollution and the like. In addition, natural gas is also an important chemical raw material, and is widely applied to the production of methanol, ammonia, urea and downstream products with higher added values. However, natural gas has various gas qualities, most of which contain hydrogen sulfide, organic sulfur (COS, RSH, RSR), carbon dioxide, etc., and the sulfide contained therein not only causes corrosion of equipment and pipelines, but also poisons downstream catalysts. Meanwhile, in the process of liquefying natural gas into Liquefied Natural Gas (LNG), low-temperature condensation and pipeline blockage can be caused by the existence of organic sulfur. Therefore, it is necessary to remove it to within the specified values by an appropriate method. At present, wet desulphurization is mostly adopted for removing hydrogen sulfide in natural gas purification plants, the treatment capacity of the method is large, but the desulphurization precision is not high and organic sulfur cannot be effectively removed.
In order to solve the problem of fine desulfurization, the chinese patent application CN104548926A discloses an organic sulfur removal process, which comprises treating gas containing carbonyl sulfide with an organic sulfur hydrogenation catalyst in a hydrogen atmosphere to convert carbonyl sulfide into hydrogen sulfide, and then removing hydrogen sulfide under the action of a desulfurizing agent, thereby realizing high-efficiency removal of sulfide. However, the process needs high temperature and high pressure, and has harsh and complicated operating conditions, high price and high cost.
Therefore, how to realize the high-efficiency removal of organic sulfur in natural gas by using a simple process flow and a low-cost organic sulfur desulfurizer becomes a major research direction in the field.
Disclosure of Invention
The invention provides a process for removing organic sulfur in natural gas, which adopts a simple flow, uses a novel catalytic adsorption type organic sulfur desulfurizer to hydrolyze or crack organic sulfur which is difficult to remove, such as carbonyl sulfur, mercaptan, thioether organic sulfur and the like, and convert the organic sulfur into hydrogen sulfide, does not need to add hydrogen, and then removes the hydrogen sulfide under the action of the desulfurizer, thereby realizing the high-efficiency removal of the sulfide in the natural gas. The desulfurization efficiency of the process is as high as 98%, and the process is favorable for the production of LNG.
The technical scheme for solving the technical problems is as follows:
the organic sulfur is carbonyl sulfur, mercaptan or thioether organic sulfur, and is catalytically hydrolyzed or catalytically cracked with catalytically adsorbing organic sulfur desulfurizing agent to convert into hydrogen sulfide, which reacts with the active components in the catalytically adsorbing organic sulfur desulfurizing agent to produce metal sulfide for elimination.
The method comprises the following steps:
1) enabling natural gas raw material gas to be desulfurized to enter a preprocessor in a state of 25 ℃ and 0.3MPa, and capturing and removing free water and solid impurities in the raw material gas;
2) heating the raw material gas to 350 ℃ at the pressure of 0.3MPa and the space velocity of 1000-3000 h-1The carbonyl sulfide passes through a desulfurization tower from top to bottom, the inside of a single tower of the desulfurization tower is filled with a filler which is a catalytic adsorption type organic sulfur desulfurizer, and after the carbonyl sulfide passes through the filler, the carbonyl sulfide reacts with water vapor under the catalytic action of the filler to generate hydrogen sulfide and carbon dioxide; for mercaptan or thioether organic sulfur, after the mercaptan or thioether organic sulfur passes through the filler, the mercaptan or thioether organic sulfur is thermally cracked under the action of the filler to generate hydrogen sulfide and olefin; and the hydrogen sulfide is absorbed by the filler, so that the hydrogen sulfide can be removed from the natural gas raw material gas.
Further, the active component is one or more of an iron compound, a copper compound, a nickel compound, a cobalt compound, a molybdenum compound or a zinc compound.
Further, the preprocessor in the step 1) is a vertical screen separator.
The vertical silk screen separator has one fixed silk screen assembly comprising silk screen and upper and lower support bars. The wire mesh material can adopt any one of polypropylene, polyethylene, polytetrafluoroethylene or stainless steel wires, the specific size can be designed in detail according to the component content of the feed gas, and the function of the wire mesh material is to separate free water and solid impurities possibly carried in the feed gas.
Further, the pretreated raw gas and the desulfurized natural gas exchange heat, the temperature of the raw gas is raised to 324 ℃ at most, and then the raw gas is heated by an electric heating furnace until the temperature of the raw gas reaches 350 ℃.
Further, after the desulfurized natural gas comes out of the desulfurization tower, heat exchange is carried out between the desulfurized natural gas and the pretreated raw material gas, the temperature of the desulfurized natural gas is reduced to 60 ℃, and the desulfurized natural gas is cooled to 40 ℃ through a sweetening purified gas cooler; and (4) feeding the cooled desulfurized natural gas into a pre-pressurization filter to remove liquid water and carried catalyst and desulfurizer impurities.
Further, after filtering, the desulfurized natural gas is compressed and pressurized by a reciprocating compressor, and after the desulfurized natural gas is pressurized to 5.2MPa, the desulfurized natural gas firstly passes through a compressor outlet cooler and a separator and then enters the first MDEA decarburization process of the liquefied natural gas flow.
Further, in the desulfurization process, a two-tower process is adopted. When the device is in operation, one organic sulfur desulfurizing tower is used for organic sulfur removal, and the other organic sulfur desulfurizing tower is standby. The purpose of setting the two-tower flow is to switch the standby tower when one organic sulfur desulfurization tower is in failure or the catalytic adsorbent is saturated in adsorption and the adsorption effect is not as good as the expected regeneration requirement, and the whole process adopts the automatic program control of a program valve. The production stop caused during the overhaul and regeneration of the desulfurization device is avoided, the operation continuity of the desulfurization device is ensured, and the production efficiency is improved.
The invention has the beneficial effects that:
the invention provides a process for removing organic sulfur in natural gas, which can efficiently remove the organic sulfur in the natural gas, reduce the corrosion of sulfides to pipelines or equipment and the blockage during low-temperature condensation, meet the pipeline transportation standard of the natural gas and the liquefaction requirement of the natural gas, and has the following advantages:
(1) the process is simple, the equipment investment is low, the operation is convenient, and the equipment maintenance and production cost is reduced;
(2) the energy consumption is low, the high-temperature natural gas after organic sulfur conversion exchanges heat with the low-temperature feed gas, the heat load of a heating furnace is reduced, the cold load of a cooler is also reduced, and the investment and the operation cost of a feed gas desulfurization system are greatly reduced;
(3) the sulfur removal precision is high, and the desulfurization efficiency is up to 98 percent by utilizing and combining the existing various catalytic adsorption type desulfurizing agents;
(4) safe and environment-friendly, and no waste liquid or waste gas is discharged in the process.
Drawings
The present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.
FIG. 1 is a schematic diagram of the process for removing organic sulfur from natural gas according to the present invention.
Detailed Description
Example 1:
as shown in fig. 1, the natural gas raw material gas to be desulfurized enters a preprocessor at the state of 25 ℃ and 0.3MPa, and free water and solid impurities in the raw material gas are captured and removed; the catalyst and the adsorbent in the desulfurizing tower are protected, and the preprocessor is a vertical wire mesh separator.
And (3) exchanging heat between the pretreated raw material gas and the desulfurized natural gas, wherein the temperature of the raw material gas is raised to 324 ℃ at most, and then heating the raw material gas by using an electric heating furnace until the temperature of the raw material gas reaches 350 ℃.
The feed gas heat exchanger is arranged in front of the electric heating furnace, so that the heat of the desulfurized natural gas is recovered, the heat load of the heating furnace is reduced, and the cold load of the cooler is also reduced, thereby saving electric energy, reducing the consumption of cooling water, reducing energy consumption and greatly reducing the investment and operation cost of a feed gas desulfurization system.
Heating the raw material gas to 350 ℃ at the pressure of 0.3MPa and the space velocity of 1000-3000 h-1The carbonyl sulfide passes through a desulfurization tower from top to bottom, the inside of a single tower of the desulfurization tower is filled with a filler which is a catalytic adsorption type organic sulfur desulfurizer, and after the carbonyl sulfide passes through the filler, the carbonyl sulfide reacts with water vapor under the catalytic action of the filler to generate hydrogen sulfide and carbon dioxide;
under the action of catalyst, COS reacts with water vapor to produce hydrogen sulfide and carbon dioxide, and its reaction equation is shown in the following formula 1-1.
COS+H2O＝CO2+H2S (1-1)
For mercaptan or thioether organic sulfur, after the mercaptan or thioether organic sulfur passes through the filler, the mercaptan or thioether organic sulfur is thermally cracked under the action of the filler to generate hydrogen sulfide and olefin;
the mercaptan and thioether organic sulfur are thermally cracked under the action of catalyst to produce hydrogen sulfide and olefin, and their reaction equation is shown in the following formulas 1-2 and 1-3.
2RSH＝2H2S+(2R-2H) (1-2)
RSR＝H2S+(2R-2H) (1-3)
And the hydrogen sulfide is absorbed by the filler, so that the hydrogen sulfide can be removed from the natural gas raw material gas.
Organic sulfur is hydrolyzed or thermally cracked into hydrogen sulfide under the catalytic action of a desulfurizer, and then the hydrogen sulfide interacts with active components (metal oxides) in the desulfurizer to generate metal sulfides, so that the purpose of removal is achieved, and the reaction equation is as shown in the following formula 1-4.
H2S+MO＝MS+H2O (M represents metal) (1-4)
The active component in the example is a mixture of an iron compound, a copper compound and a nickel compound in a mass ratio of 1:1: 1.
Further, after the desulfurized natural gas comes out of the desulfurization tower, heat exchange is carried out between the desulfurized natural gas and the pretreated raw material gas, the temperature of the desulfurized natural gas is reduced to 60 ℃, and the desulfurized natural gas is cooled to 40 ℃ through a sweetening purified gas cooler; and (4) feeding the cooled desulfurized natural gas into a pre-pressurization filter to remove liquid water and carried catalyst and desulfurizer impurities.
Further, after filtering, the desulfurized natural gas is compressed and pressurized by a reciprocating compressor, and after the desulfurized natural gas is pressurized to 5.2MPa, the desulfurized natural gas firstly passes through a compressor outlet cooler and a separator and then enters the first MDEA decarburization process of the liquefied natural gas flow.
The catalyst used in the method can reach 98% of conversion efficiency of the organic sulfur, the desulfurizer has strong adsorption performance to the hydrogen sulfide, the organic sulfur conversion and the desulfurization are combined, and the hydrogen sulfide converted by the organic sulfur can be completely absorbed and removed by the reaction of the desulfurizer. In the desulfurization process, a two-tower flow is adopted, and the two towers alternately perform an adsorption process to adsorb and remove sulfides in the natural gas.
In summary, the natural gas organosulfur removal process of the invention comprises the following sections: 1. pretreating raw material gas, namely removing most of free liquid water drops and carried solid impurities in the raw material gas in a raw material gas separator; 2. exchanging heat between the natural gas raw material gas and the desulfurized natural gas to recover heat; 3. preheating feed gas by a heating furnace and feeding the preheated feed gas into a desulfurizing tower; 4. hydrolyzing carbonyl sulfide into hydrogen sulfide, thermally cracking mercaptan and thioether organic sulfur into hydrogen sulfide and olefin, and adsorbing and removing the hydrogen sulfide and the olefin by a desulfurizing agent; 5. after desulfurization, natural gas is subjected to heat exchange, cooling and filtration to remove liquid water and carried catalyst and desulfurizer impurities; 6. the compression system pressurizes the natural gas and enters a first MDEA decarburization unit in the liquefaction process.
Example 2:
unlike example 1, in which the active component is a cobalt compound, the catalyst used in this example can achieve 96% of the conversion efficiency of organic sulfur.
Example 3:
the difference from the example 1 is that the active component is a mixture of molybdenum compound and zinc compound according to the mass ratio of 1:1, and the catalyst used in the example can achieve the conversion efficiency of catalyzing organic sulfur up to 97.5%.
The above description is only a preferred embodiment of the present invention, and is not intended to limit the present invention in any way, and all simple modifications and equivalent variations of the above embodiment according to the present invention are within the scope of the present invention.
Claims (8)
1. The process for removing organic sulfur from natural gas is characterized by that the described organic sulfur is carbonyl sulfur, mercaptan or thioether organic sulfur, and adopts the catalytic adsorption type organic sulfur desulfurizing agent to make catalytic hydrolysis or catalytic thermal cracking reaction of organic sulfur to convert it into hydrogen sulfide, then the hydrogen sulfide can be reacted with active component in the catalytic adsorption type organic sulfur desulfurizing agent to produce metal sulfide, so that it can be removed.
2. The process for removing organic sulfur from natural gas as claimed in claim 1, wherein said active component is one or more of iron compound, copper compound, nickel compound, cobalt compound, molybdenum compound or zinc compound.
3. The process for removing organic sulfur from natural gas according to claim 1, which comprises the following steps:
1) enabling natural gas raw material gas to be desulfurized to enter a preprocessor in a state of 25 ℃ and 0.3MPa, and capturing and removing free water and solid impurities in the raw material gas;
2) heating the raw material gas to 350 ℃ at the pressure of 0.3MPa and the space velocity of 1000-3000 h-1The carbonyl sulfide passes through a desulfurization tower from top to bottom, the inside of a single tower of the desulfurization tower is filled with a filler which is a catalytic adsorption type organic sulfur desulfurizer, and after the carbonyl sulfide passes through the filler, the carbonyl sulfide reacts with water vapor under the catalytic action of the filler to generate hydrogen sulfide and carbon dioxide; for mercaptan or thioether organic sulfur, after the mercaptan or thioether organic sulfur passes through the filler, the mercaptan or thioether organic sulfur is thermally cracked under the action of the filler to generate hydrogen sulfide and olefin; and the hydrogen sulfide is absorbed by the filler, so that the hydrogen sulfide can be removed from the natural gas raw material gas.
4. The process of claim 3, wherein the pretreater in step 1) is a vertical wire mesh separator.
5. The process for removing organic sulfur in natural gas according to claim 3, wherein the pretreated raw gas is subjected to heat exchange with the desulfurized natural gas, the temperature of the raw gas is raised to 324 ℃ at most, and then the raw gas is heated by an electric heating furnace until the temperature of the raw gas reaches 350 ℃.
6. The process for removing organic sulfur in natural gas according to claim 3, wherein the desulfurized natural gas is discharged from the desulfurization tower, and then exchanges heat with the pretreated raw gas, so as to reduce the temperature of the desulfurized natural gas to 60 ℃, and then is cooled to 40 ℃ by the mercaptan removal purified gas cooler; and (4) feeding the cooled desulfurized natural gas into a pre-pressurization filter to remove liquid water and carried catalyst and desulfurizer impurities.
7. The process of claim 6, wherein the desulfurized natural gas is compressed and pressurized by the reciprocating compressor after being filtered, and the desulfurized natural gas is pressurized to 5.2MPa, and then passes through the outlet cooler and the separator of the compressor, and then enters the first MDEA decarburization step of the liquefied natural gas flow.
8. The process for removing organic sulfur from natural gas according to claim 3, wherein a two-tower process is adopted in the desulfurization process.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911363426.2A CN110982566A (en) | 2019-12-26 | 2019-12-26 | Process for removing organic sulfur in natural gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911363426.2A CN110982566A (en) | 2019-12-26 | 2019-12-26 | Process for removing organic sulfur in natural gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110982566A true CN110982566A (en) | 2020-04-10 |
Family
ID=70077154
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911363426.2A Pending CN110982566A (en) | 2019-12-26 | 2019-12-26 | Process for removing organic sulfur in natural gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110982566A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111876210A (en) * | 2020-07-15 | 2020-11-03 | 中石化南京化工研究院有限公司 | Improve COS, CS in natural gas2Method for removing rate |
| CN113426289A (en) * | 2021-06-29 | 2021-09-24 | 松山湖材料实验室 | Hydrolysis adsorbent, blast furnace gas desulfurization method and desulfurization equipment |
| CN115125042A (en) * | 2021-03-25 | 2022-09-30 | 中国石油天然气股份有限公司 | Process for the fine removal of thiol-type organic sulfur |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105498678A (en) * | 2014-10-15 | 2016-04-20 | 中国石油化工股份有限公司 | Desulfurization adsorbent, preparation method thereof, and gas desulfurization method |
| CN106367146A (en) * | 2016-08-26 | 2017-02-01 | 成都巨涛油气工程有限公司 | Method of organic sulfur removal for natural gas |
| CN107008339A (en) * | 2017-04-26 | 2017-08-04 | 四川鸿鹄科技集团有限公司 | A kind of non-hydrogenation conversion catalyst of organic sulfur and preparation method thereof |
| EP3209408A4 (en) * | 2014-10-24 | 2018-07-04 | Research Triangle Institute, International | Integrated system and method for removing acid gas from a gas stream |
-
2019
- 2019-12-26 CN CN201911363426.2A patent/CN110982566A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105498678A (en) * | 2014-10-15 | 2016-04-20 | 中国石油化工股份有限公司 | Desulfurization adsorbent, preparation method thereof, and gas desulfurization method |
| EP3209408A4 (en) * | 2014-10-24 | 2018-07-04 | Research Triangle Institute, International | Integrated system and method for removing acid gas from a gas stream |
| CN106367146A (en) * | 2016-08-26 | 2017-02-01 | 成都巨涛油气工程有限公司 | Method of organic sulfur removal for natural gas |
| CN107008339A (en) * | 2017-04-26 | 2017-08-04 | 四川鸿鹄科技集团有限公司 | A kind of non-hydrogenation conversion catalyst of organic sulfur and preparation method thereof |
Non-Patent Citations (3)
| Title |
|---|
| 孙广庭等: "《中型合成氨厂生产工艺与操作问答》", 31 July 1985, 化学工业出版社 * |
| 辽宁省石油化学工业厅: "《辽宁化工产品大全》", 31 December 1994, 辽宁科学技术出版社 * |
| 鲍柳旭: "Co对ZnO/SiO2脱硫过程中COS生成的抑制作用研究", 《中国优秀硕士学位论文全文数据库 工程科技Ⅰ辑》 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111876210A (en) * | 2020-07-15 | 2020-11-03 | 中石化南京化工研究院有限公司 | Improve COS, CS in natural gas2Method for removing rate |
| CN115125042A (en) * | 2021-03-25 | 2022-09-30 | 中国石油天然气股份有限公司 | Process for the fine removal of thiol-type organic sulfur |
| CN115125042B (en) * | 2021-03-25 | 2023-08-22 | 中国石油天然气股份有限公司 | Process for refining and removing organosulfur from thiols |
| CN113426289A (en) * | 2021-06-29 | 2021-09-24 | 松山湖材料实验室 | Hydrolysis adsorbent, blast furnace gas desulfurization method and desulfurization equipment |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101434879B (en) | Method for preparing methyl alcohol synthesis gas and compressed natural gas from coke oven gas and coal | |
| CN103275777B (en) | Method for preparing hydrogen and liquefied natural gas through using gas retort raw gas | |
| CN107758617B (en) | Method for producing hydrogen by using biogas biomass | |
| CN101100622B (en) | Method and device for synthesizing natural gas by using coke oven gas | |
| CN108774107B (en) | Process for producing methanol by using gas of ore-smelting furnace | |
| CN110982566A (en) | Process for removing organic sulfur in natural gas | |
| CN102642810B (en) | Combined process for preparing Fischer-Tropsch synthetic oil raw material gas by utilizing coke-oven gas | |
| CN102050699B (en) | Process for co-producing methanol and ammonia by utilizing calcium carbide tail gas | |
| CN104119975A (en) | Method of combined production of methanol and liquefied natural gas in coking plant | |
| WO2020233030A1 (en) | Device and method for synergistic recover of sulfur and hydrogen resources from hydrogen sulfide acid gas | |
| CN111847381A (en) | Method and device for preparing hydrogen from industrial waste gas | |
| CN110228792B (en) | Deep decarburization process for synthesis gas | |
| CN109054893B (en) | System for hydrogen purification and wax oil hydrogenation coupling in coal hydrogen production | |
| CN108011119B (en) | Method and system for clean power generation and resource utilization of hydrogen-containing waste gas coupled fuel cell | |
| CN221217737U (en) | Device for purifying reducing gas from blast furnace or converter gas | |
| CN103952184B (en) | Catalytic coal gasifaction prepares the method and system of shaft furnace reducing gases | |
| CN111925847A (en) | Process for removing organic sulfur in natural gas by hydrogenation | |
| CN103343022A (en) | Negative-pressure desulfurization technology and equipment for coke gas | |
| CN104998517A (en) | Method for increasing concentrations of acid gas hydrogen sulfide and carbonyl sulfide in low-temperature methanol washing process | |
| CN114015481B (en) | Short-flow low-temperature methanol washing system and process thereof | |
| CN215250677U (en) | System for burnt tail gas transform of gasification, decarbonization system LNG | |
| CN210885331U (en) | Device for producing synthetic ammonia by utilizing sodium cyanide tail gas | |
| CN104974810A (en) | Method for producing liquefied natural gas (LNG) from semi-coke exhaust and calcium carbide furnace gas | |
| CN109679675B (en) | Method and system for producing low-carbon olefin by using semi-coke tail gas | |
| CN102659102A (en) | Technology and device for preparing industrial carbon monoxide with water gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20200410 |