CN104437032A - Synthetic raw material gas deep fine desulfurization process and fine desulfurization device - Google Patents
Synthetic raw material gas deep fine desulfurization process and fine desulfurization device Download PDFInfo
- Publication number
- CN104437032A CN104437032A CN201410632507.9A CN201410632507A CN104437032A CN 104437032 A CN104437032 A CN 104437032A CN 201410632507 A CN201410632507 A CN 201410632507A CN 104437032 A CN104437032 A CN 104437032A
- Authority
- CN
- China
- Prior art keywords
- gas
- synthetic raw
- raw gas
- devulcanizer
- sulfur
- 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
Landscapes
- Catalysts (AREA)
- Industrial Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a deep desulfurization method for preparing a synthetic raw material gas by taking a coal-based natural gas, a petroleum refining gas, a coke oven gas, a steel mill converter gas and the like as raw materials. The method comprises the step of enabling the raw material gas which is treated by rough desulfurization and contains hundreds of parts per million (ppm) of H2S and hundreds of ppm of organic sulfur (including COS, CS2, sulfur alcohol, sulfur ether, thiophene and the like) to pass through a plurality of stages of titanium-based molybdenum-cobalt catalysts, a plurality of stages of zinc oxide desulfurizing agents and a stage of multifunctional fine desulfurizing agent to enable the total sulfur to be less than or equal to 0.01ppm. Compared with the existing desulfurization accuracy (0.1ppm), the desulfurization accuracy of the deep desulfurization method enables the degree of purification to be increased by one order of magnitude and enables the service life of a methyl alcohol catalyst to be doubled. The invention also discloses a medium-temperature fine desulfurization device used by the synthetic raw material gas deep fine desulfurization method. For the industrial community, after the method and the device are used, the starting and stopping times of the device can be reduced, the raw material and the power consumption are reduced, the yield of the device is increased, and an effective measure capable of saving energy, reducing emission and increasing yield can be provided.
Description
Technical field
The present invention relates to gas cleaning in Chemical Engineering, belong to " energy-conservation, reduction of discharging " field, specifically a kind of synthetic raw gas degree of depth fine desulfurizing technology and device thereof.
Background technology
At present with coal gas in existing technology, the process that oven gas, petroleum refinery's gas, steel mill's converter gas and natural gas are the large and medium-sized Methanol Plant of waste synthetic raw gas, all there are fine de-sulfur in synthesis ammonia plant, artificial oil factory.Large-scale factory adopts low-temperature rectisol, NHD method, medium-sized employing fine desulfurization process by dry (comprising normal temperature and middle temperature fine de-sulfur).These methods the total sulfur≤0.1ppm in synthetic raw gas can be ensured the life-span of catalst for synthesis of methanol is 2 ~ 3 years, the life-span of synthetic ammonia catalyst is 5 ~ 7 years, synthetic oil catalyst life-span ﹤ 1 year.According to external experience, affect catalyst life (under same process condition) mainly sulfur poisoning, if the total sulfur in synthesis gas can be dropped to≤0.01 × 10
-6, i.e. 0.01ppm, the life-span of catalyst is by prolongation one times.Therefore, Exploitation Depth fine desulfurizing technology is industrial quarters new problem anxious to be resolved.
Propose the deep-purifying method of synthesis gas in document CN101224871B, the operating temperature that it is characterized by first technique is normal temperature, and secondly selected catalyst is hydrolyst, can only by COS, the CS in synthesis gas
2be hydrolyzed to H
2s and removing, cannot remove for organic sulfur such as mercaptan, thioether, thiophene etc. complicated in synthetic raw gas.The scope having this patent to use again can only after existing fine de-sulfur, namely in synthesis gas total sulfur≤0.lppm condition under.The use of such the method has had significant limitation.The present invention have found that wide accommodation, precision are high, the simple degree of depth desulfurizing process of flow process.
Summary of the invention
The problem to be solved in the present invention is: overcome the deficiencies in the prior art, and provide a kind of operation to simplify, desulfurized effect is good, can maximize the synthetic raw gas degree of depth fine desulfurizing technology saving desulfurization and postorder finalization chemical product cost.
For solving the problems of the technologies described above, the technical solution used in the present invention is: a kind of synthetic raw gas degree of depth fine desulfurizing technology, comprises the steps: that the synthetic raw gas entering operation is carried out pretreatment by (1), makes H in synthetic raw gas
2s content is down to <10ppm; (2) by H
2the synthetic raw gas of S content <10ppm carries out hydrogenation reaction through Ti-base catalyst, makes the organic sulfur conversion in synthetic raw gas be inorganic sulfur, i.e. H
2s; (3) again by synthetic raw gas through Zinc oxide desulfurizer, by H
2s removes from synthetic raw gas; (4) sulfide content in synthetic raw gas is made to reach trace according to the content of sulfide repetition different from kind step (2), (3); (5) containing trace sulfide synthetic raw gas through multi-function fine desulfurizing agent time, sulfide is removed further, thus reaches technic index requirement, be i.e. the total sulfur≤0.01ppm of synthetic raw gas.
Further, be oven gas, natural gas, refinery gas, coal gas, steel mill's converter gas as the source of the gas of synthetic raw gas in described step (1), after also comprising low-temperature rectisol purification and after NHD purification, the synthetic raw gas of total sulfur < 0.1ppm in gas.
Further, the Ti-base catalyst in described step (2) take titanium dioxide as carrier, the titanium base cobalt molybdenum containing cobalt oxide, molybdenum oxide or cobalt, molybdenum, nickel active constituent or titanium base cobalt molybdenum-nickel hydrogenation catalyst.
Further, in step (2), the light-off temperature of Ti-base catalyst is 120 ~ 150 DEG C.
Further, in step (2), the reaction pressure of hydrogenation reaction is 0.1 ~ 0.7MPa, and reaction temperature is 120 ~ 400 DEG C.
Another problem that the present invention will solve is: provide a kind of device applying above-mentioned synthetic raw gas degree of depth fine desulfurizing technology.
For solving the problems of the technologies described above, the technical solution used in the present invention is: the device applying above-mentioned synthetic raw gas degree of depth fine desulfurizing technology, comprise coarse iron oxide devulcanizer, gas-to-gas heat exchanger, go into operation heater, one-level hydrogenation reactor, stair oxidation zinc devulcanizer, secondary hydrogenation reactor, secondary oxidation zinc devulcanizer and multi-function fine devulcanizer, it is characterized in that: described coarse iron oxide devulcanizer by pipeline successively with gas-to-gas heat exchanger, go into operation heater, one-level hydrogenation reactor, stair oxidation zinc devulcanizer, secondary hydrogenation reactor, secondary oxidation zinc devulcanizer is connected, the outlet of described secondary oxidation zinc devulcanizer is connected with another entrance at gas-to-gas heat exchanger top by pipeline, another outlet bottom described gas-to-gas heat exchanger is connected by the entrance of pipeline with multi-function fine devulcanizer.
The advantage that the present invention has and effect are: the use of (1) titanium base cobalt molybdenum or titanium base cobalt molybdenum-nickel hydrogenation catalyst, can to the organic sulfur in the water-gas of composition complexity, oven gas, especially resemble the so complicated organic sulfur of thiophene and carry out hydrogenation degraded, operating mode applied very relaxes again, reaction temperature is low, air speed is large for it, occur without bad side reaction.(2) light-off temperature of hydrogenation conversion catalyst is low, be only 120 ~ 150 DEG C, its thermal source can be used heat or 0.5MPa steam, and hydrogenation conversion catalyst light-off temperature >=200 DEG C of the prior art, its thermal source needs the steam of heating furnace or 4.0MPa, the two is compared thermal source of the present invention and is easy to get, and reduces cost (comprising fixed investment firing equipment) and energy consumption.(3) titanium base cobalt molybdenum or titanium base cobalt molybdenum-nickel hydrogenation catalyst be not by O in gas
2, CO, CO
2the interference of content, has the ability of sulfuric-resisting salinization.(4) eliminate hydrogenation pre-converter, add multi-function fine devulcanizer, while guarantee effect of desulfidation and purification, operation is simplified; Due to more expensive than multifunction catalyst several times of pre-converting catalyst, thus reduce desulphurization cost, cost and the energy consumption of postorder chemical products after degree of depth fine de-sulfur, can be reduced.(5) result of degree of depth fine de-sulfur is that degree of purification reaches 0.01ppm, can make the life one times of catalyst for methanol.
Accompanying drawing explanation
Fig. 1 is process chart of the present invention.
In figure: 1, coarse iron oxide devulcanizer; 2, gas-to-gas heat exchanger; 3, go into operation heater; 4, one-level hydrogen reactor; 5, stair oxidation zinc devulcanizer; 6, secondary hydrogenation reactor; 7, secondary oxidation zinc devulcanizer; 8, multi-function fine devulcanizer.
Detailed description of the invention
Accompanying drawing is specific embodiment of the invention process chart, illustrates, but be not the restriction to protection scope of the present invention when be sulfur removal technology device flow process being secondary by figure and embodiment to the present invention.
Embodiment 1
A kind of device of synthetic raw gas degree of depth fine desulfurizing technology, as shown in Figure 1: comprise coarse iron oxide devulcanizer 1, gas-to-gas heat exchanger 2, go into operation heater 3, one-level hydrogenation reactor 4, stair oxidation zinc devulcanizer 5, secondary hydrogenation reactor 6, secondary oxidation zinc devulcanizer 7 and multi-function fine devulcanizer 8, coarse iron oxide devulcanizer 1 by pipeline successively with gas-to-gas heat exchanger 2, go into operation heater 3, one-level hydrogenation reactor 4, stair oxidation zinc devulcanizer 5, secondary hydrogenation reactor 6, secondary oxidation zinc devulcanizer 7 is connected, the outlet of described secondary oxidation zinc devulcanizer 7 is connected by pipeline another entrance with gas-to-gas heat exchanger 2 top, another outlet bottom described gas-to-gas heat exchanger 2 is connected by the entrance of pipeline with multi-function fine devulcanizer 8.
Can according to sulfur content in synthetic raw gas number and the complexity of sulfur speciation, sulfur removal technology device flow process can be one-level, secondary or multistage, and concrete which kind of technique that adopts should design depending on concrete operating mode.
Embodiment 2
Now for coke oven gas desulfurization, the technical process in the present invention is specifically addressed.Coke-stove gas is many containing organic sulfur in synthetic raw gas and the source of the gas that composition is complicated, simultaneously containing O
2, CO, CO
2component, atmosphere effect impact is fairly obvious.Coke-stove gas after thick desulfurization, through coarse iron oxide desulfurization reactor 1, by H in gas
2s content is down to <10ppm, again through gas-to-gas heat exchanger 2, go into operation heater 3, be warmed up to 120 ~ 150 DEG C (also can open temperature alive adjustment with catalyst), enter the one-level hydrogenation reactor 4 that titanium base cobalt molybdenum hydrogenation catalyst is housed again, pressure is 0.1 ~ 0.7MPa, temperature is 120 ~ 400 DEG C, carries out Organic sulfur hydro-conversion reaction with this understanding, by most organic sulfur (such as COS, CS
2, RSH, RSR, C
4h
4s etc.) hydro-conversion is H
2s, after going out one-level hydrogenation reactor 4, coke-stove gas enter Zinc oxide desulfurizer is housed stair oxidation zinc devulcanizer 5 by H
2s takes off≤0.03ppm, then enters secondary hydrogenation reactor 6, allows remaining organic sulfur again carry out hydroconversion reactions, and reacted unstripped gas enters secondary oxidation zinc devulcanizer 7, by organic sulfur and H
2s takes off trace.Coke-stove gas after secondary hydrogenation reaction and the desulfurization of secondary oxidation zinc is again through gas-to-gas heat exchanger 2 heat exchange, after cooling the temperature to normal temperature, enter the multi-function fine devulcanizer 8 that multi-function fine desulfurizing agent is housed again, remove the sulfide of denier further by the way transformed and adsorb, make the total sulfur≤0.01ppm of outlet synthetic raw gas.Hydrogenation removal of organic sulfur test data is as shown in table 1.
Table 1
From table 1, result is found out: (1) is as hydrogenation reaction temperature 250 DEG C, air speed 2800h
-1time, COS, CS
2and C
4h
4the conversion ratio of S reaches >98%.(2) as hydrogenation reaction temperature 250 DEG C, air speed 1500h
-1time, C
4h
4the conversion ratio of S reaches 100%, COS and CS
2conversion ratio reach >99.5%.(3) along with the rising of reaction temperature, when hydrogenation reaction temperature reaches 300 DEG C, air speed 1500h
-1time, all organic sulfurs are all converted into inorganic sulfur, and conversion ratio reaches 100%.
Visible, at a lower temperature, titanium base cobalt molybdenum hydrogenation catalyst hydrogenation removal of organic sulfur has good activity, and organic sulfur, almost can by all organic sulfur conversion after the reaction of titanium base cobalt molybdenum hydrogenation catalyst hydrogenation removal of organic sulfur.If pass through what titanium base cobalt molybdenum hydrogenation catalyst, what Zinc oxide desulfurizer again, and check on multi-function fine desulfurization, it has been exactly the deep desulfuration new technology extremely insured.
Embodiment 3
For desulfurization of water gas, the technical process in the present invention is specifically addressed again.Water-gas after thick desulfurization, through coarse iron oxide desulfurization reactor 1, by H in gas
2s content is down to <10ppm, again through gas-to-gas heat exchanger 2, go into operation heater 3, be warmed up to 120 ~ 150 DEG C (also can open temperature alive adjustment with catalyst), enter the one-level hydrogenation reactor 4 that titanium base cobalt molybdenum hydrogenation catalyst is housed again, pressure is 0.1 ~ 0.7MPa, temperature is 120 ~ 400 DEG C, carries out Organic sulfur hydro-conversion reaction with this understanding, by most organic sulfur (such as COS, CS
2, RSH, RSR, C
4h
4s etc.) hydro-conversion is H
2s, after going out one-level hydrogenation reactor 4, water-gas enter Zinc oxide desulfurizer is housed stair oxidation zinc devulcanizer 5 by H
2s takes off≤0.03ppm, then enters secondary hydrogenation reactor 6, allows remaining organic sulfur again carry out hydroconversion reactions, and reacted unstripped gas enters secondary oxidation zinc devulcanizer 7, by organic sulfur and H
2s takes off trace.Water-gas after secondary hydrogenation reaction and the desulfurization of secondary oxidation zinc is again through gas-to-gas heat exchanger 2 heat exchange, after cooling the temperature to normal temperature, enter the multi-function fine devulcanizer 8 that multi-function fine desulfurizing agent is housed again, remove the sulfide of denier further by the way transformed and adsorb, make the total sulfur≤0.01ppm of outlet synthetic raw gas.Hydrogenation removal of organic sulfur test data is as shown in table 2.
Table 2
From table 2, result is found out:, air speed not too high at hydrogenation reaction temperature, pressure is suitable, titanium base cobalt molybdenum hydrogenation catalyst, by organic sulfur, and particularly CS
2take off and do not detect, conversion ratio 100%, and COS takes off to 11 ~ 16ppm, conversion ratio >95%.If pass through what titanium base cobalt molybdenum hydrogenation catalyst, what Zinc oxide desulfurizer again, and check on multi-function fine desulfurization, it has been exactly the deep desulfuration new technology extremely insured.
Above embodiments of the invention have been described in detail, but described content being only preferred embodiment of the present invention, can not being considered to for limiting practical range of the present invention.All equalizations done according to the present patent application scope change and improve, and all should still belong within patent covering scope of the present invention.
Claims (6)
1. a synthetic raw gas degree of depth fine desulfurizing technology, is characterized in that: comprise the steps: that the synthetic raw gas entering operation is carried out pretreatment by (1), make H in synthetic raw gas
2s content is down to <10ppm; (2) by H
2the synthetic raw gas of S content <10ppm carries out hydrogenation reaction through Ti-base catalyst, makes the organic sulfur conversion in synthetic raw gas be inorganic sulfur, i.e. H
2s; (3) again by synthetic raw gas through Zinc oxide desulfurizer, by H
2s removes from synthetic raw gas; (4) sulfide content in synthetic raw gas is made to reach trace according to the content of sulfide repetition different from kind step (2), (3); (5) containing trace sulfide synthetic raw gas through multi-function fine desulfurizing agent time, sulfide is removed further, thus reaches technic index requirement, be i.e. the total sulfur≤0.01ppm of synthetic raw gas.
2. synthetic raw gas degree of depth fine desulfurizing technology according to claim 1, it is characterized in that: be oven gas, natural gas, refinery gas, coal gas, steel mill's converter gas as the source of the gas of synthetic raw gas in described step (1), after also comprising low-temperature rectisol purification and after NHD purification, the synthetic raw gas of total sulfur < 0.1ppm in gas.
3. synthetic raw gas degree of depth fine desulfurizing technology according to claim 1, it is characterized in that: the Ti-base catalyst in described step (2) take titanium dioxide as carrier, the titanium base cobalt molybdenum containing cobalt oxide, molybdenum oxide or cobalt, molybdenum, nickel active constituent or titanium base cobalt molybdenum-nickel hydrogenation catalyst.
4. the synthetic raw gas degree of depth fine desulfurizing technology according to claim 1 or 3, is characterized in that: in step (2), the light-off temperature of Ti-base catalyst is 120 ~ 150 DEG C.
5. the synthetic raw gas degree of depth fine desulfurizing technology according to claim 1 or 3, is characterized in that: in step (2), the reaction pressure of hydrogenation reaction is 0.1 ~ 0.7MPa, and reaction temperature is 120 ~ 400 DEG C.
6. the device of the synthetic raw gas degree of depth fine desulfurizing technology of an application rights requirement described in 1, comprise coarse iron oxide devulcanizer, gas-to-gas heat exchanger, go into operation heater, one-level hydrogenation reactor, stair oxidation zinc devulcanizer, secondary hydrogenation reactor, secondary oxidation zinc devulcanizer and multi-function fine devulcanizer, it is characterized in that: described coarse iron oxide devulcanizer by pipeline successively with gas-to-gas heat exchanger, go into operation heater, one-level hydrogenation reactor, stair oxidation zinc devulcanizer, secondary hydrogenation reactor, secondary oxidation zinc devulcanizer is connected, the outlet of described secondary oxidation zinc devulcanizer is connected with another entrance at gas-to-gas heat exchanger top by pipeline, another outlet bottom described gas-to-gas heat exchanger is connected by the entrance of pipeline with multi-function fine devulcanizer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410632507.9A CN104437032A (en) | 2014-11-11 | 2014-11-11 | Synthetic raw material gas deep fine desulfurization process and fine desulfurization device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410632507.9A CN104437032A (en) | 2014-11-11 | 2014-11-11 | Synthetic raw material gas deep fine desulfurization process and fine desulfurization device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN104437032A true CN104437032A (en) | 2015-03-25 |
Family
ID=52884246
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410632507.9A Pending CN104437032A (en) | 2014-11-11 | 2014-11-11 | Synthetic raw material gas deep fine desulfurization process and fine desulfurization device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104437032A (en) |
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104707453A (en) * | 2015-03-26 | 2015-06-17 | 山西省国新能源发展集团有限公司 | Two-stage catalytic hydrodesulfurization device |
| CN104986732A (en) * | 2015-07-03 | 2015-10-21 | 赛鼎工程有限公司 | Method for preparing synthesis gas through coke oven gas and coal gas |
| CN105000533A (en) * | 2015-07-03 | 2015-10-28 | 赛鼎工程有限公司 | Method used for producing synthesis gas from coke oven gas and coal gas |
| CN105038866A (en) * | 2015-07-03 | 2015-11-11 | 临涣焦化股份有限公司 | Coke-oven gas fine desulfurization technology |
| CN105056753A (en) * | 2015-07-31 | 2015-11-18 | 青岛联信催化材料有限公司 | High pressure high-water/gas sulfur-containing raw gas organic sulfur conversion technology |
| CN106350122A (en) * | 2016-08-31 | 2017-01-25 | 武汉科林精细化工有限公司 | Fine desulfurization process for coke-oven gas |
| CN107456852A (en) * | 2017-07-04 | 2017-12-12 | 杨皓 | A kind of technique of carbon dioxide enriched gas conversion desulfurization |
| CN110144244A (en) * | 2019-06-13 | 2019-08-20 | 北京北科环境工程有限公司 | A kind of system and method for blast furnace gas desulfurization |
| CN110804468A (en) * | 2019-11-27 | 2020-02-18 | 浙江天禄环境科技有限公司 | Dry desulfurization process for synthesis gas |
| CN111054365A (en) * | 2018-10-16 | 2020-04-24 | 中国石油化工股份有限公司 | Fine desulfurizing agent, preparation method thereof and desulfurization process |
| CN111849562A (en) * | 2020-07-30 | 2020-10-30 | 中国石油化工股份有限公司 | Device and method for desulfurizing synthesis gas prepared by coal gasification |
| CN113318593A (en) * | 2021-05-13 | 2021-08-31 | 安徽威达环保科技股份有限公司 | Natural gas catalytic desulfurization purification device and process |
| CN114149835A (en) * | 2021-12-08 | 2022-03-08 | 浙江三龙催化剂有限公司 | Novel deoxidation and desulfurization process and application thereof |
| CN114196449A (en) * | 2021-12-08 | 2022-03-18 | 浙江三龙催化剂有限公司 | The pre-desulfurization process of blast furnace gas and its application |
| CN114433112A (en) * | 2020-11-06 | 2022-05-06 | 宁波中科远东催化工程技术有限公司 | Coke oven gas hydrodesulfurization catalyst and preparation method thereof |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4041130A (en) * | 1975-12-29 | 1977-08-09 | The Ralph M. Parsons Company | Process for desulfurization of coke oven gas |
| WO1999037741A1 (en) * | 1998-01-23 | 1999-07-29 | Exxon Research And Engineering Company | Production of low sulfur syngas from natural gas with c4+/c5+ hydrocarbon recovery |
| CN101054538A (en) * | 2007-02-02 | 2007-10-17 | 华东理工大学 | Iron-base desulfurizer for catalyzing, translating and absorbing carbonyl sulfur at middle-low temperature and preparation thereof |
| CN101337150A (en) * | 2008-08-07 | 2009-01-07 | 上海交通大学 | Preparation method of nano zinc oxide mesoporous desulfurizer |
| CN102134519A (en) * | 2010-01-22 | 2011-07-27 | 上海寰球石油化学工程有限公司 | Combined process for natural gas desulfurization with high resource utilization ratio and good environmental protection effect |
| CN102497919A (en) * | 2009-09-15 | 2012-06-13 | 约翰森·马瑟公开有限公司 | Desulphurisation process |
-
2014
- 2014-11-11 CN CN201410632507.9A patent/CN104437032A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4041130A (en) * | 1975-12-29 | 1977-08-09 | The Ralph M. Parsons Company | Process for desulfurization of coke oven gas |
| WO1999037741A1 (en) * | 1998-01-23 | 1999-07-29 | Exxon Research And Engineering Company | Production of low sulfur syngas from natural gas with c4+/c5+ hydrocarbon recovery |
| CN101054538A (en) * | 2007-02-02 | 2007-10-17 | 华东理工大学 | Iron-base desulfurizer for catalyzing, translating and absorbing carbonyl sulfur at middle-low temperature and preparation thereof |
| CN101337150A (en) * | 2008-08-07 | 2009-01-07 | 上海交通大学 | Preparation method of nano zinc oxide mesoporous desulfurizer |
| CN102497919A (en) * | 2009-09-15 | 2012-06-13 | 约翰森·马瑟公开有限公司 | Desulphurisation process |
| CN102134519A (en) * | 2010-01-22 | 2011-07-27 | 上海寰球石油化学工程有限公司 | Combined process for natural gas desulfurization with high resource utilization ratio and good environmental protection effect |
Non-Patent Citations (1)
| Title |
|---|
| 张文效等: "精脱硫技术进展及钛基催化剂的应用探索", 《煤化工》, no. 5, 31 October 2014 (2014-10-31), pages 6 - 10 * |
Cited By (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104707453A (en) * | 2015-03-26 | 2015-06-17 | 山西省国新能源发展集团有限公司 | Two-stage catalytic hydrodesulfurization device |
| CN104986732A (en) * | 2015-07-03 | 2015-10-21 | 赛鼎工程有限公司 | Method for preparing synthesis gas through coke oven gas and coal gas |
| CN105000533A (en) * | 2015-07-03 | 2015-10-28 | 赛鼎工程有限公司 | Method used for producing synthesis gas from coke oven gas and coal gas |
| CN105038866A (en) * | 2015-07-03 | 2015-11-11 | 临涣焦化股份有限公司 | Coke-oven gas fine desulfurization technology |
| CN104986732B (en) * | 2015-07-03 | 2017-01-04 | 赛鼎工程有限公司 | Utilize the method that coke-stove gas and coal gas prepare synthesis gas |
| CN105056753A (en) * | 2015-07-31 | 2015-11-18 | 青岛联信催化材料有限公司 | High pressure high-water/gas sulfur-containing raw gas organic sulfur conversion technology |
| CN105056753B (en) * | 2015-07-31 | 2017-12-19 | 青岛联信催化材料有限公司 | A kind of high water/gas Sulfur Contained Raw Gas organic sulfur conversion technique of high pressure |
| CN106350122A (en) * | 2016-08-31 | 2017-01-25 | 武汉科林精细化工有限公司 | Fine desulfurization process for coke-oven gas |
| CN106350122B (en) * | 2016-08-31 | 2019-05-10 | 武汉科林精细化工有限公司 | A kind of coke oven gas fine desulfurization process |
| CN107456852A (en) * | 2017-07-04 | 2017-12-12 | 杨皓 | A kind of technique of carbon dioxide enriched gas conversion desulfurization |
| CN111054365A (en) * | 2018-10-16 | 2020-04-24 | 中国石油化工股份有限公司 | Fine desulfurizing agent, preparation method thereof and desulfurization process |
| CN111054365B (en) * | 2018-10-16 | 2023-04-18 | 中国石油化工股份有限公司 | Fine desulfurizing agent, preparation method thereof and desulfurization process |
| CN110144244A (en) * | 2019-06-13 | 2019-08-20 | 北京北科环境工程有限公司 | A kind of system and method for blast furnace gas desulfurization |
| CN110804468A (en) * | 2019-11-27 | 2020-02-18 | 浙江天禄环境科技有限公司 | Dry desulfurization process for synthesis gas |
| CN111849562A (en) * | 2020-07-30 | 2020-10-30 | 中国石油化工股份有限公司 | Device and method for desulfurizing synthesis gas prepared by coal gasification |
| CN111849562B (en) * | 2020-07-30 | 2021-12-17 | 中国石油化工股份有限公司 | Device and method for desulfurizing synthesis gas prepared by coal gasification |
| CN114433112A (en) * | 2020-11-06 | 2022-05-06 | 宁波中科远东催化工程技术有限公司 | Coke oven gas hydrodesulfurization catalyst and preparation method thereof |
| CN113318593A (en) * | 2021-05-13 | 2021-08-31 | 安徽威达环保科技股份有限公司 | Natural gas catalytic desulfurization purification device and process |
| CN114149835A (en) * | 2021-12-08 | 2022-03-08 | 浙江三龙催化剂有限公司 | Novel deoxidation and desulfurization process and application thereof |
| CN114196449A (en) * | 2021-12-08 | 2022-03-18 | 浙江三龙催化剂有限公司 | The pre-desulfurization process of blast furnace gas and its application |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104437032A (en) | Synthetic raw material gas deep fine desulfurization process and fine desulfurization device | |
| CN106350122B (en) | A kind of coke oven gas fine desulfurization process | |
| Petersson | Biogas cleaning | |
| CN101649232B (en) | Synthesis process of natural gas employing methanation of coke oven gas | |
| CN101245262B (en) | Gas-steam combined cycle system and process based on coal gasification and methanation | |
| Chen et al. | Gasification kinetic analysis of the three pseudocomponents of biomass-cellulose, semicellulose and lignin | |
| Ciccoli et al. | Molten carbonate fuel cells fed with biogas: Combating H2S | |
| de Arespacochaga et al. | Evaluation of a pilot-scale sewage biogas powered 2.8 kWe Solid Oxide Fuel Cell: Assessment of heat-to-power ratio and influence of oxygen content | |
| CN104591083A (en) | Hydrogen preparation method | |
| CN105032157A (en) | Amine liquid desulphurization technology and device for removing hydrogen sulfide and carbonyl sulfide in acid gas | |
| Wang et al. | Preparation of biochar catalyst from black liquor by spray drying and fluidized bed carbonation for biodiesel synthesis | |
| CN103602357B (en) | Production process of liquefied natural gas | |
| CN113145103B (en) | Hydrodesulfurization catalyst and its preparation method and application | |
| CN101921641A (en) | Process for preparing synthetic natural gas from coke oven gas | |
| CN205740932U (en) | A kind of remove the device of organic sulphur components in liquefied natural gas | |
| Hiloidhari et al. | Biogas upgrading and life cycle assessment of different biogas upgrading technologies | |
| Zhang et al. | Sulfur evolution and capture behavior by a solid waste of red mud during chemical looping combustion of petroleum coke | |
| CN102464544A (en) | Hydrothermal treatment using porous nickel catalystReduction of CO2Or CO is methane | |
| CN102659102B (en) | Technology and device for preparing industrial carbon monoxide with water gas | |
| WO2023197065A1 (en) | Method for producing hydrogen using at least two biomethanes | |
| CN103113010A (en) | Method for synchronous implementation of methanation of coke oven gas and in-situ purification of marsh gas | |
| CN100377990C (en) | Sulfur-tolerant deoxygenation method for low temperature methanol cleaning process | |
| Garnaik et al. | Biomass-based CO 2 adsorbents for biogas upgradation with pressure swing adsorption | |
| CN203999538U (en) | A kind of natural-gas desulfurizer of preparing synthetic ammonia | |
| Groisil et al. | Acid gas simulation for recovering syngas and sulfur |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20150325 |
|
| RJ01 | Rejection of invention patent application after publication |