WO2004015035A1 - ガス化ガス用のcos処理装置とcos処理方法 - Google Patents
ガス化ガス用のcos処理装置とcos処理方法 Download PDFInfo
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- WO2004015035A1 WO2004015035A1 PCT/JP2003/009984 JP0309984W WO2004015035A1 WO 2004015035 A1 WO2004015035 A1 WO 2004015035A1 JP 0309984 W JP0309984 W JP 0309984W WO 2004015035 A1 WO2004015035 A1 WO 2004015035A1
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- WO
- WIPO (PCT)
- Prior art keywords
- cos
- catalyst
- gas
- removal
- gasification
- Prior art date
Links
- 238000002309 gasification Methods 0.000 title claims abstract description 15
- 238000000034 method Methods 0.000 title abstract description 9
- 239000003054 catalyst Substances 0.000 claims abstract description 93
- 238000006243 chemical reaction Methods 0.000 claims abstract description 53
- 238000012545 processing Methods 0.000 claims description 8
- 229910052717 sulfur Inorganic materials 0.000 claims description 8
- 238000003672 processing method Methods 0.000 claims description 6
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 4
- 229910052739 hydrogen Inorganic materials 0.000 claims description 4
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 abstract description 4
- QDOXWKRWXJOMAK-UHFFFAOYSA-N dichromium trioxide Chemical compound O=[Cr]O[Cr]=O QDOXWKRWXJOMAK-UHFFFAOYSA-N 0.000 abstract 2
- 239000007789 gas Substances 0.000 description 45
- 238000010248 power generation Methods 0.000 description 17
- 239000000446 fuel Substances 0.000 description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 13
- 238000000746 purification Methods 0.000 description 10
- 238000010521 absorption reaction Methods 0.000 description 6
- 239000012535 impurity Substances 0.000 description 6
- 239000007864 aqueous solution Substances 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 238000011144 upstream manufacturing Methods 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 4
- 229910052788 barium Inorganic materials 0.000 description 4
- 239000000428 dust Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000000295 fuel oil Substances 0.000 description 4
- 238000011068 loading method Methods 0.000 description 4
- -1 amine compound Chemical class 0.000 description 3
- 150000001412 amines Chemical class 0.000 description 3
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 239000002803 fossil fuel Substances 0.000 description 3
- 229910052602 gypsum Inorganic materials 0.000 description 3
- 239000010440 gypsum Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000010742 number 1 fuel oil Substances 0.000 description 3
- 150000003464 sulfur compounds Chemical class 0.000 description 3
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 229910052783 alkali metal Inorganic materials 0.000 description 2
- 150000001340 alkali metals Chemical class 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 230000006378 damage Effects 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 230000001737 promoting effect Effects 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 230000035882 stress Effects 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 241000238631 Hexapoda Species 0.000 description 1
- 206010037660 Pyrexia Diseases 0.000 description 1
- 229910010413 TiO 2 Inorganic materials 0.000 description 1
- WGLPBDUCMAPZCE-UHFFFAOYSA-N Trioxochromium Chemical compound O=[Cr](=O)=O WGLPBDUCMAPZCE-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- JRPBQTZRNDNNOP-UHFFFAOYSA-N barium titanate Chemical compound [Ba+2].[Ba+2].[O-][Ti]([O-])([O-])[O-] JRPBQTZRNDNNOP-UHFFFAOYSA-N 0.000 description 1
- 229910002113 barium titanate Inorganic materials 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 239000003990 capacitor Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 239000011651 chromium Substances 0.000 description 1
- 229910000423 chromium oxide Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 230000002542 deteriorative effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 229910000480 nickel oxide Inorganic materials 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- GNRSAWUEBMWBQH-UHFFFAOYSA-N oxonickel Chemical compound [Ni]=O GNRSAWUEBMWBQH-UHFFFAOYSA-N 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 125000004079 stearyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 230000004936 stimulating effect Effects 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
- 229910052815 sulfur oxide Inorganic materials 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 230000008646 thermal stress Effects 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/85—Chromium, molybdenum or tungsten
- B01J23/86—Chromium
- B01J23/866—Nickel and chromium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/88—Handling or mounting catalysts
- B01D53/885—Devices in general for catalytic purification of waste gases
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/34—Purifying combustible gases containing carbon monoxide by catalytic conversion of impurities to more readily removable materials
Definitions
- the present invention relates to an apparatus for removing cos (sulfide sulfonyl) from a gasified gas obtained from coal, heavy oil, or the like.
- low-quality fuels generally contain a large amount of sulfur compounds, and when this gas is burned as it is, the sulfur compounds are emitted as sulfur oxides into the atmosphere from the stack and become sources of environmental destruction such as acid rain. . Therefore, it has been practically used in ordinary thermal power generation to install a flue gas desulfurization device downstream of the boiler to remove the sulfur-containing compound, for example, as gypsum.
- a flue gas desulfurization device downstream of the boiler to remove the sulfur-containing compound, for example, as gypsum.
- the corrosion of the material is remarkable because the inlet temperature of the gas turbine is higher than the temperature of the poirer in ordinary thermal power generation.
- a water-soluble component is removed with a water scrubber, and H 2 S (hydrogen sulfide) is removed with an aqueous solution of amines.
- H 2 S hydrogen sulfide
- aqueous solutions of amines can remove H 2 S but not COS. Therefore, the hydrolysis reaction shown in equation (1) is carried out using a COS conversion catalyst to promote the reaction of conversion into the form of H 2 S that can be removed with an aqueous solution of amines.
- a catalyst containing titania see Japanese Patent No. 1463827 and Japanese Patent Application Laid-Open No. 11-180760
- JP-A-2000-248286 a catalyst containing chromium and alumina
- combustion catalysts are generally expensive because they carry noble metals, and are susceptible to poisoning by H 2 S, which tends to cause deterioration in performance. Had a problem such as a large stress applied to the device. Disclosure of the invention
- the present invention is characterized in that by installing an O 2 removal catalyst that promotes the reaction of the formula (2) upstream of the COS conversion catalyst, O 2 is removed and the performance of the COS conversion catalyst is prevented from deteriorating. ⁇
- the present invention H 2 S, H 2 0, a COS processing equipment for gasification gas containing ⁇ 2 and CO, 0 2 removal and catalyst, the gasification gas stream to the 0 2 removal catalyst
- a COS treatment device comprising: a COS conversion catalyst positioned downstream;
- H 2 S, H 2 0, 0 a COS processing method for gasification gas containing 2 and CO, first stearyl to remove ⁇ 2 by reaction with H 2 S and CO And a second step of converting the COS to H 2 S.
- FIG. 1 is an example of a flow of a wet gas purification apparatus to which the present invention is suitably used.
- FIG. 2 shows an arrangement of the O 2 removal catalyst and the COS conversion catalyst in Examples 1 and 2 of the present invention, in which both are provided in separate reactors. '
- FIG. 3 shows the arrangement of the O 2 removal catalyst and the COS conversion catalyst in Examples 1 and 2 of the present invention, in which both are provided in a single reactor.
- FIG. 4 is an example in which a dual-purpose COS conversion catalyst according to Embodiment 3 of the present invention is provided in a reactor.
- FIG. 5 shows a comparison result of the O 2 removal performance when the gas temperature was changed in Example 4 of the present invention.
- FIG. 1 is an example of a flow including a gasification furnace 3 and a wet gas purification device to which the present invention is suitably used.
- the gasification furnace 3 is a known one, and is supplied with low-quality fuel 1 such as coal or heavy oil, and oxygen, air, or oxygen-enriched air as a gasifying agent 2, and gasified gas 4 is taken out. It is. It is desirable to remove dust from the extracted gasified gas using a known dust collector 5.
- the first heat exchanger 6 between the dust collector 5 and the COS processing device 7 gives the heat of the gasified gas before purification to the gasified gas after purification.
- the type of the heat exchanger is not particularly limited, and a general multi-tube heat exchanger can be used.
- COS processor 7 a COS that can not be absorbed by the H 2 S absorption tower 11 described below, it is converted to H 2 S.
- COS processor 7 where having been loaded only COS conversion catalyst within reactance capacitor in the prior art, the combination of o 2 removal catalyzed and cos conversion catalyst in the present invention, or, the function of the o 2 removal combines It is characterized by loading a dual-purpose COS conversion catalyst.
- the o 2 removal catalyst is placed on the upper part of the CO s treatment unit, the COS conversion catalyst is placed on the lower part, gasified gas is introduced from the upper part, and the treated gas is taken out from the lower part.
- the o 2 removal catalyst is desirably installed under higher temperature conditions as described later in Examples.
- the reaction to the left becomes dominant when the temperature is high due to the equilibrium of the COS conversion reaction shown in equation (1). It is necessary to install in a more optimal use temperature range. From these results, it established without going through the heat exchanger immediately after ⁇ 2 removal catalyst more a high temperature e.g. dust collector 5, but also possible is an aspect in which installed separately from the cos conversion catalyst.
- o 2 removal catalyst performance for improved at high temperatures can be reduced catalyst loading required by installing a high temperature.
- the first heat exchanger 6 can also be installed in the next 0 2 removal catalyst.
- the number of pressure vessels for catalyst filling will increase, so the cost must be considered according to the properties of the gas to be treated. It is necessary to make an optimal arrangement.
- the method of loading the catalyst is not particularly limited, and a known loading method, for example, a method of placing a granular or honeycomb-shaped catalyst in an appropriate reactor can be used.
- 0 2 removal catalyst the above (2) the chemical reaction is not particularly limited as Re der those actions that include stimulating, for example catalysts are available including the acid Ihikuromu or nickel oxide and barium titanate Nia, especially CR 2 0 3 and carrying honeycomb shape of T io 2 catalyst is preferably a Bariumu.
- the above (1) chemical reaction is not limited to Japanese as long as the function of promoting, for example the A 1 2 0 3 and T i 0 2 as a support, alumina and Group IV metal and barium catalysts and containing, alkali metal available catalyst comprises a catalyst or Paris ⁇ arm and T io 2 containing chromium oxide and alumina, among which, in particular T i 0 2 catalyst Ha second cam shape carrying barium are preferred .
- C r 2 0 3 of its preferred amount is from 0.
- 1 wt% or more 6 wt% or less relative to the total weight of the catalyst 6 wt particularly good Mashiku is 3 wt% or more when the T i 0 2 and carrier % or less and the T i 0 2 Les preferably the N i O when the carrier, the addition amount is 0. 1 wt% or more 15 wt% or less, particularly preferably with 1 OWT% or less 5 wt% or more
- the second heat exchanger 8 between the COS treatment device 7 and the gas cooling tower 9 also converts the heat of the gasified gas before purification into the gasified gas after purification. It has the function of giving.
- the gasified gas after purification passes first through the second heat exchanger 8 and then through the first heat exchanger 6, thereby becoming countercurrent to the gasified gas before purification, and flowing in parallel. Because the average temperature difference can be secured larger than when JP2003 / 009984
- the gasified gas before purification that has passed through the second heat exchanger 8 is subjected to water scrubber 10 to remove water-soluble impurities.
- another water scrubber 9 is preferably provided between the second heat exchanger 8 and the water scraper 10 so as to increase the solubility of water-soluble impurities in the circulating water of the water scraper 10.
- the water scraper 9 for example, one having the same structure as the water scrubber 10 can be used.
- the circulating water in which the impurities are dissolved is discharged out of the system by a discharge line (not shown), and makeup water corresponding to the discharged amount is collected from a makeup water line (not shown).
- Known water scrubbers 9 and 10 can be used.
- the gasified gas exiting the water scrubber 10 comes into gas-liquid contact with a fresh absorbing solution composed of an aqueous solution of an amine compound in the H 2 S absorption tower 11. Then, H 2 S in the gasified gas is absorbed by the aqueous solution of the amine compound. Gasified gas is extracted as a purified gas suitable as fuel for power generation equipment such as gas turbines and fuel cells. The heat is obtained from the gasified gas before purification by the second heat exchanger 8 and the first heat exchanger 6 described above, and the purified gas is heated and used as a fuel with higher power generation efficiency.
- the absorbing solution that has absorbed H 2 S is sent to the absorbing solution regenerating tower 12 and given heat from the absorbing solution regenerating heat source 14 to be separated into a fresh absorbing solution and high-concentration H 2 S 15.
- the fresh amine compound is returned to the H 2 S absorption tower 11 and recycled.
- High-concentration H 2 S 15 can be used as a raw material for elemental sulfur, gypsum, sulfuric acid, etc., and the sulfur content cannot be a source of environmental destruction.
- the H 2 S absorption tower 11, the absorption liquid regeneration tower 12, and the absorption liquid known ones can be used.
- Known devices and methods can be used for producing valuable resources such as simple elemental sulfur, gypsum, and sulfuric acid from high-concentration H 2 S 15.
- FIG. 2 is a diagram focusing on the COS treatment device 7 of the present invention
- FIG. 2 is a diagram illustrating a first reactor 21 having an O 2 removal catalyst 22 therein, and a flow downstream thereof.
- CO This is an example of a combination with a second reactor 21 ′ having an S conversion catalyst 23 inside.
- Figure 3 is provided with a 0 2 removal catalysts 22 to the upstream side of a single reactor 2 1 internal gasification gas flow, the downstream side is an example having a COS conversion catalyst 23.
- Figure 4 is an example in which a combined COS conversion catalyst 24 that combines ⁇ 2 removal function inside the reactor 21.
- FIG. 5 shows the results of comparing the O 2 removal performance of the ⁇ 2 removal catalyst with changing the gas temperature.
- the COS concentration at the outlet of the COS conversion catalyst was 110 ppm and the COS conversion rate was 0.642. there were.
- vol-% is volume percentage
- the cOS treatment apparatus and the COS treatment method for gasified gas according to the present invention provide a combined power generation system in which a low-quality fossil fuel such as coal or heavy oil is gasified, and a gas turbine using the gas fuel and a steam turbine are used in combination. It can be suitably used for power generation with excellent power generation efficiency in the field of thermal power generation, such as power generation by introducing hydrocarbon gas into fuel cells.
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Combustion & Propulsion (AREA)
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Description
Claims
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US10/522,604 US7749455B2 (en) | 2002-08-09 | 2003-08-06 | Apparatus for treating COS for gas produced by gasification and method for treating COS |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2002-233680 | 2002-08-09 | ||
JP2002233680A JP4467872B2 (ja) | 2002-08-09 | 2002-08-09 | ガス化ガス用のcos処理装置とcos処理方法 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2004015035A1 true WO2004015035A1 (ja) | 2004-02-19 |
Family
ID=31711870
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2003/009984 WO2004015035A1 (ja) | 2002-08-09 | 2003-08-06 | ガス化ガス用のcos処理装置とcos処理方法 |
Country Status (4)
Country | Link |
---|---|
US (1) | US7749455B2 (ja) |
JP (1) | JP4467872B2 (ja) |
CN (1) | CN100580062C (ja) |
WO (1) | WO2004015035A1 (ja) |
Families Citing this family (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2006052424A2 (en) * | 2004-11-09 | 2006-05-18 | Fluor Technologies Corporation | Configurations and methods for sox removal in oxygen-containing gases |
JP5274802B2 (ja) * | 2006-09-15 | 2013-08-28 | 株式会社日本触媒 | 酸素除去方法 |
CN102000505A (zh) * | 2010-11-16 | 2011-04-06 | 湖北双雄催化剂有限公司 | 一种新型中温羰基硫水解方法 |
US9677018B2 (en) * | 2013-01-09 | 2017-06-13 | Thyssenkrupp Industrial Solutions Ag | Process for the production of synthesis gas from hard coal |
JP6122664B2 (ja) | 2013-03-05 | 2017-04-26 | 三菱重工業株式会社 | ガス精製装置およびガス精製方法 |
JP6161508B2 (ja) | 2013-10-23 | 2017-07-12 | 三菱重工業株式会社 | Cos転換触媒の触媒再生方法 |
JP6147663B2 (ja) | 2013-12-27 | 2017-06-14 | 三菱重工業株式会社 | Cos転換触媒の触媒再生方法 |
CN111744355B (zh) * | 2020-05-19 | 2022-02-01 | 福建省气柜设备安装有限公司 | 一种工业混合气体的脱硫方法及脱硫装置 |
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JPS5763388A (en) * | 1980-10-02 | 1982-04-16 | Osaka Gas Co Ltd | Removal of oxygen from coke oven gas |
JPS62256709A (ja) * | 1986-04-28 | 1987-11-09 | Kobe Steel Ltd | Coの精製方法 |
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GB1563251A (en) * | 1976-12-07 | 1980-03-26 | Shell Int Research | Process for working hydrogen suphidecontaining gases |
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2002
- 2002-08-09 JP JP2002233680A patent/JP4467872B2/ja not_active Expired - Lifetime
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2003
- 2003-08-06 US US10/522,604 patent/US7749455B2/en active Active
- 2003-08-06 WO PCT/JP2003/009984 patent/WO2004015035A1/ja active Application Filing
- 2003-08-06 CN CN03818595A patent/CN100580062C/zh not_active Expired - Lifetime
Patent Citations (7)
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JPS5763388A (en) * | 1980-10-02 | 1982-04-16 | Osaka Gas Co Ltd | Removal of oxygen from coke oven gas |
JPS62256709A (ja) * | 1986-04-28 | 1987-11-09 | Kobe Steel Ltd | Coの精製方法 |
EP0324526A1 (en) * | 1988-01-13 | 1989-07-19 | Comprimo B.V. | Process for converting and removing sulfur compounds from a CO containing gas |
US5660807A (en) * | 1993-06-09 | 1997-08-26 | Linde Aktiengesellschaft | Process for the removal of HCN from gas mixtures |
JPH11104451A (ja) * | 1997-10-03 | 1999-04-20 | Mitsubishi Heavy Ind Ltd | ガス精製方法及びガス精製装置 |
JP2000248286A (ja) * | 1999-03-02 | 2000-09-12 | Jgc Corp | コークス炉ガスの精製プロセス |
FR2830466A1 (fr) * | 2001-10-09 | 2003-04-11 | Axens | Utilisation d'une composition a base de ti02 comme catalyseur pour realiser l'hydrolyse des cos et/ou d'hcn dans un melange gazeux |
Also Published As
Publication number | Publication date |
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US7749455B2 (en) | 2010-07-06 |
JP4467872B2 (ja) | 2010-05-26 |
CN100580062C (zh) | 2010-01-13 |
US20060051263A1 (en) | 2006-03-09 |
CN1675337A (zh) | 2005-09-28 |
JP2004075712A (ja) | 2004-03-11 |
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