CN104903428A - Process for the production of synthesis gas from hard coal - Google Patents
Process for the production of synthesis gas from hard coal Download PDFInfo
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- CN104903428A CN104903428A CN201480004324.0A CN201480004324A CN104903428A CN 104903428 A CN104903428 A CN 104903428A CN 201480004324 A CN201480004324 A CN 201480004324A CN 104903428 A CN104903428 A CN 104903428A
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- grams
- milliliter
- sulfide
- cobalt
- hydrogenation
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- 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
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
-
- 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
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Industrial Gases (AREA)
Abstract
A process for the production of synthesis gas from coke is suggested, in which (a) hard coal is subjected to dry pyrolysis, resulting in the production of a gas mixture containing hydrogen, methane, nitrogen and carbon monoxide as major constituents and carbon sulphides as minor constituents, (b) the gas mixture is subjected to hydrogenation at a temperature in the range of 200 DEG C to 280 DEG C over a sulphidic cobalt molybdenum catalyst provided on an aluminium oxide carrier material, and (c) the hydrogen sulphide obtained from hydrogenation is separated from the gas mixture.
Description
Technical field
The invention belongs to coke manufacturing technology domain variability and relate to from coke-oven gas, remove carbon sulfide novel process and new catalyzer and application thereof.
Background technology
Coke-oven gas (synonym: coke gas) is dry distillation acquisition from hard coal (hard coal) in coke furnace factory.As main component, this gas is usually containing the carbon monoxide of the hydrogen of the 55wt% that has an appointment (weight percent), the methane of 25wt%, the nitrogen of 10wt% and 5wt%.For this reason, coke-oven gas is normally qualified as the synthetic gas of chemical reaction, but disadvantage is the content of carbonyl sulfide (carbonyl sulphide) and carbon sulfide (carbon disulphide), it must be removed in advance, this is because they such as serve as catalyzer poison in reaction subsequently.Thus, catalyzer is constantly cleaned and is even replaced, and this is directly related to workload and cost and week then do not wish to occur due to factory.
A kind of method removing undesired carbon sulfide from coke-oven gas coal gas is stood catalytic hydrogenation and transforms sulphur compound to be hydrogen sulfide.Although this gas also undesired, it can be easy to be washed by means of moisture alkali lye such as ammonia solution.
According to prior art, relevant technique is known.Such as, German patent application DE 1545470 A1 (Pichler) suggestion hydrogenation carbon sulfide on cobalt molybdenum, nickel molybdenum or nickel cobalt-molybdenum catalyst is hydrogen sulfide, and then it can be separated.Temperature of reaction in this embodiment is higher than 550 DEG C.
For coke-oven gas hydrogenating desulfurization (hydrodesulphurisation), the use of catalyzer based on nickel, cobalt, molybdenum or palladium also can find in various Japanese patent application comparatively early, such as JP 59 145288 A2 (Shinnittetsu) or JP 59 230092 A1 (Hitachi).And these processing methodes accordingly.
Similar technique also can be known from German patent application DE 2647690 A1 (Parsons), which proposes the carbon compound of hydrogenation sulfur-bearing on the catalyzer on cobalt, molybdenum, iron, chromium, vanadium, thorium, nickel, tungsten and/or uranium basis and removes the hydrogen sulfide obtained in extraction column by means of alkali hydroxide soln.The sulfide of above-mentioned metal is proposed as concrete catalyzer.But involved shortcoming, in the case, catalyzer needs the temperature of minimum 260 DEG C and hydrogenation must preferably carry out, partly even higher than 400 DEG C showing at higher temperature.Be in the reason of energy cost, this is undesirable especially; In addition, by changing the component of gas, namely can there is methanation in this temperature.
Although prior art processes is changed carbon sulfide into hydrogen sulfide in the mode of high production capacity and is therefore changed the synthetic gas of coke-oven gas into enough high-quality, they all relate to substantial shortcoming, namely these techniques must be carried out at the very high temperature being equivalent to more than 280 DEG C, otherwise sufficiently high turnover ratio is difficult to realize.
Therefore, the object of the invention is to improve existing technique, if any, as long as carbon sulfide and organosulfur compound (such as thiophene) are converted hydrogen sulfide substantially quantitatively, and is showing at the temperature reduced.Further, the mass ratio that this technique is intended to guarantee to maintain oxycarbide and methane is constant, namely prevents methanation.
Summary of the invention
Theme of the present invention is for the method by coke production synthetic gas, wherein
A () hard coal stands stem cracking, cause containing hydrogen, methane, nitrogen and carbon monoxide as the generation as the gaseous mixture of a small amount of component of main ingredient and carbon sulfide,
At the temperature of (b) gaseous mixture within the scope of 200 to 280 DEG C, the sulfide cobalt-molybdenum catalyst that provides on alumina supporting material carries out hydrogenation, and
C hydrogen sulfide that () obtains from hydrogenation is separated from described gaseous mixture.
Astoundingly, the known sulfide cobalt-molybdenum catalyst for carbon sulfide hydrogenation even lower than 280 DEG C and preferably lower than 260 DEG C at there is high reactivity and optionally feature, if they are deposited on alumina supporting material.Carbon sulfide in fact at least 95 (volume) % is hydrogenated and is reacted into hydrogen sulfide and does not observe hydrogenation to the impact of oxycarbide on the ratio of methane.This is a beyond thought result, because the instruction of document DE 2647690 A1 according to introductory song citation, people's expection also can promote with the catalyzer of sulphided form mainly containing cobalt and molybdenum the degree that undesired methanation be can not ignore to, if particularly reaction is carried out as usual under stress.
Coke coal gas is produced by hard coal cracking
In the process of hard coal dry distillation or cracking, under it occurs in 900 to 1400 DEG C of temperature, the volatiles of coal is released and forms porous coke, and it is now substantially only containing carbon.By condensate fractionation, unstripped gas is broken down into tar, sulfuric acid, ammonia, naphthalene (naphthalene), benzene and so-called coke coal gas.The latter is made up of hydrogen, methane, nitrogen and oxycarbide and can be further used in chemical reaction after fully processing to obtain synthetic gas.
Hydrogenation technique
The hydrogenation of cracked gas can carry out in a conventional manner, and to this, mainly fixed-bed reactor have proved optimal, because catalyzer is provided as bulk layers or fixing filler (packing) with bulk form.Because bulk material is more easy to form passage and is therefore formed with Non-Uniform Flow distribution, in this embodiment, preferably catalyzer is arranged in reactor in the mode of filler.
But the advantage of the hydrogenation in fixed-bed reactor is that the output of high space/time is achieved, Here it is why according to technique of the present invention also can about 500 to about 1500 ls/h (l/h) and preferably approximately 1000 carry out to high GHSV (gas hourly space velocity, gas (little) space-time () speed) value of about 1200 ls/h (l/h).Another advantage is for product withdraw without the need to special measure, because reactant-i.e. cracking coal gas and hydrogen-be preferably collectively incorporated in the bottom of reactor, through causing the catalyst bed of hydrogenation and leaving reactor as product at top.
As already mentioned in beginning, a specific advantages of this processing method is sulphur compound hydrogenation on the catalyzer that will use according to the present invention, makes to react to carry out under the condition of obvious milder and transforming completely of carbon sulfide and any sign without methanation becomes possibility.Range of reaction temperature between 200 to 280 DEG C, and preferably has sufficient speed of response between 240 to 260 DEG C.Reactor can from indirect heating, and this causes higher energy expenditure; Or reactive component can be heated before they are incorporated into reactor, it can mix by means of in the nozzle such as adopting the work of Venturi (Venturi) principle.
Further, reaction can namely at barometric point or add pressure and carry out in the scope of 1 to 15 bar.Present embodiment preferably adopts about 5 to the pressure in the scope of about 10 bar, because this is conducive to output and speed of response.
Catalyzer
Sulfide cobalt-molybdenum catalyst
Term " sulfide cobalt-molybdenum catalyst " mainly refers to containing moly-sulfide as actual catalyst and the cobalt catalyzer as promotor.That catalyzer is produced by the co-vulcanized of each oxide compound in known manner, wherein molybdenum oxide (MoO
3) be converted completely into molybdenumdisulphide (MoS
2).When the latter is applied on alumina supporter, itself or by flatly composition surface (" substrate engages ") or only engage an edge (" edge join ").After sulfuration, cobalt has three kinds of forms available: first as the Co be deposited on carrier
9s
8crystal, as at MoS
2on the edge of plate as Co
2+ion (" CoMo phase ") and as the Co on the tetrahedral site of aluminum oxide lattice
2+ion.Therefore, preferred catalyzer mainly by more than 50 (mole) %, preferably greater than 70 (mole) % and to form most preferably more than the moly-sulfide of 90 (mole) %, and comprise the cobalt of sulphided form as promotor, the quantity of its (mole) % is the difference with 100.Thus, in a similar preferred embodiment, described catalyzer does not comprise other metal any, does not especially have other transition metal.
Alumina supporter
The aluminum oxide with high-specific surface area (specific surface area) is considered using as the suitable carrier for sulfide cobalt-molybdenum catalyst, and this aluminum oxide preferably has following characteristics:
The V of minimum 75 milliliters/100 grams, preferably 80 milliliter/100 grams, most preferably 85 milliliter/100 grams
37A;
The V of maximum 31 milliliters/100 grams, preferably 25 milliliter/100 grams, most preferably 15 milliliter/100 grams
0.1 μm;
The V of maximum 20 milliliters/100 grams, preferably 15 milliliter/100 grams, most preferably 10 milliliter/100 grams
0.2 μm; With
V
0.1 μmcompare V
0.2 μmratio be at least 1.5.
The alumina supporter of mentioned type is fully known in the art.Such as, European patent document EP 1385786 B1 and EP 1385787 B1 (Axens) describes their manufacturing process, wherein, gibbsite type (hydrargillite-type) aluminum oxide is polished, adopt aluminum nitrate and first aqueous acid, 200 DEG C of hydrothermal method process 6 hours, then products therefrom was calcined at 400 to 1300 DEG C.This solid support material is extruded subsequently and is therefore suitable for carrying.With regard to the character of this support of the catalyst and manufacture, these two sections of documents are all relevant reference.
Purifying
Leave the hydrogenation reaction product of reactor particularly fixed-bed reactor, the sulphur compound now containing hydrogen sulfide form, its content is usually in 50 scopes to 300ppm.H
2the existence of S is undesirable just as the existence of carbon sulfide, but for the latter, hydrogen sulfide relatively easily can be cleaned out and clean out in large quantities after all.For this purpose, those hydrogenation gases are preferably passed through absorption tower, and there, they such as process having in the adverse current as the aqueous solution of sodium hydroxide (caustic soda) or ammonia.Alternately, other device can be used to purify this gas, such as Venturi Scrubber.
When hydrogen sulfide part is separated, the product be purified is suitable and unrestricted as the high-quality synthetic gas for further chemical reaction.
Industrial applicibility
Another theme of the present invention relate to be set up on the alumina support, the application that becomes the sulfide cobalt-molybdenum catalyst of hydrogen sulfide for carbon sulfide hydrogenation.To this, preferably this kind of cobalt-molybdenum catalyst is used, and with reference to metal ingredient, it is mainly made up of moly-sulfide and comprises cobaltous sulfide (cobalt sulphide) as unique promotor.
For the carrier also preferential oxidation aluminium of cobalt-molybdenum catalyst, it has high specific surface area and has following characteristics simultaneously:
The V of (i) minimum 75 milliliters/100 grams, preferably 80 milliliter/100 grams, most preferably 85 milliliter/100 grams
37A;
(ii) V of maximum 31 milliliters/100 grams, preferably 25 milliliter/100 grams, most preferably 15 milliliter/100 grams
0.1 μm;
(iii) V of maximum 20 milliliters/100 grams, preferably 15 milliliter/100 grams, most preferably 10 milliliter/100 grams
0.2 μm; With
(iv) V
0.1 μmcompare V
0.2 μmratio be at least 1.5.
The present invention also comprises a kind of method for the preparation of hydrogen sulfide, and wherein carbon sulfide carries out hydrogenation being set up under sulfide cobalt-molybdenum catalyst working dose on the alumina support.
Preferred carbon sulfide carries out hydrogenation under cobalt-molybdenum catalyst exists, and with reference to described metal ingredient, this cobalt-molybdenum catalyst is mainly made up of moly-sulfide and comprises only as the cobaltous sulfide of promotor.Preferably alumina supporter meets following characteristics:
The V of (i) minimum 75 milliliters/100 grams, preferably 80 milliliter/100 grams, most preferably 85 milliliter/100 grams
37A;
(ii) V of maximum 31 milliliters/100 grams, preferably 25 milliliter/100 grams, most preferably 15 milliliter/100 grams
0.1 μm;
(iii) V of maximum 20 milliliters/100 grams, preferably 15 milliliter/100 grams, most preferably 10 milliliter/100 grams
0.2 μm; With
(iv) V
0.1 μmcompare V
0.2 μmratio be at least 1.5.
Embodiment
Example 1
Pilot factory for fixed bed hydrogenation reaction is equipped with the bulk layers of commercially available massive sulphide cobalt-molybdenum catalyst on the alumina support.Subsequently, different coke coal gas is introduced in the bottom of tower.Sole difference between these so-called feed gas is the content of carbon sulfide particularly dithiocarbonic anhydride (carbon disulphide).Hydrogenation carries out at the temperature of 220 DEG C and under the pressure of 10 bar.Its GHSV is approximately 1200 ls/h.
Product gas analyzes sulphur in gas chromatograph and the cut of hydrogen sulfide and carbon sulfide measured by means of retention period.Table 1 summarizes result.Transformation efficiency refers to CS
2the hydrogenation of cut.
Table 1
(weight indicates with (volume) % the result of hydrogenation, except as otherwise noted)
The cut at least 95% of test result display carbon sulfide is converted into hydrogen sulfide.The ratio of other composition meanwhile in coke-oven gas keeps constant, does not namely have methanation problem.
Claims (18)
1. for the method by coke production synthetic gas, wherein
A () hard coal stands stem cracking, cause the generation of gaseous mixture; This gaseous mixture contains as the hydrogen of main ingredient, methane, nitrogen and carbon monoxide and the carbon sulfide as a small amount of component;
Hydrogenation is carried out at the temperature of (b) described gaseous mixture within the scope of 200 to 280 DEG C, being arranged on the sulfide cobalt-molybdenum catalyst on alumina supporting material; And
C hydrogen sulfide that () obtains from hydrogenation is separated by from described gaseous mixture.
2. method according to claim 1, is characterized in that, the synthetic gas with the carbon sulfide of 10 to 200ppm content is used.
3. method according to claim 1, is characterized in that, carries out in the temperature range of hydrogenation between 240 to 260 DEG C.
4. method according to claim 1, is characterized in that, hydrogenation carries out under the pressure of 1 to 15 bar.
5. method according to claim 4, is characterized in that, hydrogenation carries out under the pressure of 5 to 10 bar.
6. method according to claim 1, is characterized in that, hydrogenation carries out under the GHSV of 500 to 1500 ls/h.
7. method according to claim 1, is characterized in that, the cobalt-molybdenum catalyst not comprising other transition metal any is used.
8. method according to claim 1, is characterized in that, cobalt-molybdenum catalyst is used, and with reference to metal component, described cobalt-molybdenum catalyst is mainly made up of moly-sulfide and comprises only as the cobaltous sulfide of promotor.
9. method according to claim 1, is characterized in that, the aluminum oxide with high-specific surface area is used as the carrier of cobalt-molybdenum catalyst, and described aluminum oxide has following characteristics:
The V of (i) minimum 75 milliliters/100 grams, preferably 80 milliliter/100 grams, most preferably 85 milliliter/100 grams
37A;
(ii) V of maximum 31 milliliters/100 grams, preferably 25 milliliter/100 grams, most preferably 15 milliliter/100 grams
0.1 μm;
(iii) V of maximum 20 milliliters/100 grams, preferably 15 milliliter/100 grams, most preferably 10 milliliter/100 grams
0.2 μm; With
(iv) V
0.1 μmcompare V
0.2 μmratio be at least 1.5.
10. the method according to item at least one in claim 1 to 9, is characterized in that, described hydrogenation reaction is carried out in fixed-bed reactor.
11. methods according to claim 1, is characterized in that, the catalyzer used in fixed-bed reactor is provided as bulk layers or filler.
12. methods according to claim 1, is characterized in that, after leaving reactor, described hydrogenated products is transmitted through absorption tower, and hydrogen sulfide is cleaned out by means of alkaline liquid in described absorption tower.
13. arrange on the alumina support, the application of the sulfide cobalt-molybdenum catalyst of the hydrogenation that for carbon sulphidic conversion is hydrogen sulfide.
14. application according to claim 13, is characterized in that, described cobalt-molybdenum catalyst is used, and with reference to metal ingredient, described cobalt-molybdenum catalyst is mainly made up of moly-sulfide and comprises only as the cobaltous sulfide of promotor.
15. application according to claim 13, is characterized in that, have the carrier being used as cobalt-molybdenum catalyst of the aluminum oxide of high-specific surface area, described aluminum oxide meets following characteristics:
The V of (i) minimum 75 milliliters/100 grams, preferably 80 milliliter/100 grams, most preferably 85 milliliter/100 grams
37A;
(ii) V of maximum 31 milliliters/100 grams, preferably 25 milliliter/100 grams, most preferably 15 milliliter/100 grams
0.1 μm;
(iii) V of maximum 20 milliliters/100 grams, preferably 15 milliliter/100 grams, most preferably 10 milliliter/100 grams
0.2 μm; With
(iv) V
0.1 μmcompare V
0.2 μmratio be at least 1.5.
16. 1 kinds, for the preparation of the method for hydrogen sulfide, is characterized in that, carbon sulfide carries out hydrogenation being set up under sulfide cobalt-molybdenum catalyst working dose on the alumina support.
17. methods according to claim 16, is characterized in that, described carbon sulfide carries out hydrogenation under cobalt-molybdenum catalyst exists, and with reference to metal ingredient, described cobalt-molybdenum catalyst is mainly made up of moly-sulfide and comprises only as the cobaltous sulfide of promotor.
18. methods according to claim 16, is characterized in that, described alumina supporter meets following characteristics:
The V of (i) minimum 75 milliliters/100 grams, preferably 80 milliliter/100 grams, most preferably 85 milliliter/100 grams
37A;
(ii) V of maximum 31 milliliters/100 grams, preferably 25 milliliter/100 grams, most preferably 15 milliliter/100 grams
0.1 μm;
(iii) V of maximum 20 milliliters/100 grams, preferably 15 milliliter/100 grams, most preferably 10 milliliter/100 grams
0.2 μm; With
(iv) V
0.1 μmcompare V
0.2 μmratio be at least 1.5.
Applications Claiming Priority (7)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102013000173.0 | 2013-01-09 | ||
| DE102013000173 | 2013-01-09 | ||
| DE102013010473.4 | 2013-06-03 | ||
| DE102013010473 | 2013-06-03 | ||
| DE102013009885.8 | 2013-06-06 | ||
| DE201310009885 DE102013009885A1 (en) | 2013-01-09 | 2013-06-06 | Manufacture of synthesis gas used for chemical reactions, involves forming gas mixture of hydrogen and methane by pyrolyzing dry coal, hydrogenating gas mixture using cobalt-molybdenum sulfide catalyst and separating hydrogen sulfide |
| PCT/EP2014/050190 WO2014108423A1 (en) | 2013-01-09 | 2014-01-08 | Process for the production of synthesis gas from hard coal |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104903428A true CN104903428A (en) | 2015-09-09 |
| CN104903428B CN104903428B (en) | 2019-01-18 |
Family
ID=51166541
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201480004324.0A Active CN104903428B (en) | 2013-01-09 | 2014-01-08 | By the process of anthracite production synthesis gas |
Country Status (6)
| Country | Link |
|---|---|
| EP (1) | EP2943556B1 (en) |
| JP (1) | JP2016505695A (en) |
| KR (1) | KR102055036B1 (en) |
| CN (1) | CN104903428B (en) |
| PL (1) | PL2943556T3 (en) |
| WO (1) | WO2014108423A1 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101641045B1 (en) * | 2015-09-30 | 2016-07-20 | 주식회사 포스코 | Oxidation prevention layer forming device for steel sheet and the method thereof |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1018630A (en) * | 1963-11-13 | 1966-01-26 | Shell Int Research | Process for the purification of hot gases obtained by partial combustion and containing soot and carbonyl sulphide |
| GB1332337A (en) * | 1970-09-21 | 1973-10-03 | Shell Int Research | Reducing total sulphur content of claus offgases |
| GB1404581A (en) * | 1971-09-01 | 1975-09-03 | Shell Int Research | Process for the removal of soot and sulphur compounds from the crude gas generated by the partial combustion of a carbonaceous fuel |
| DE2647690A1 (en) * | 1975-12-29 | 1977-07-14 | Parsons Co Ralph M | PROCESS FOR DESULFURIZATION OF COOKER GAS |
| US4085199A (en) * | 1976-06-08 | 1978-04-18 | Bethlehem Steel Corporation | Method for removing hydrogen sulfide from sulfur-bearing industrial gases with claus-type reactors |
| US4863489A (en) * | 1989-02-03 | 1989-09-05 | Texaco Inc. | Production of demercurized synthesis gas, reducing gas, or fuel gas |
| WO1993013184A1 (en) * | 1991-12-30 | 1993-07-08 | Gastec N.V. | Process for treating gases obtained by coal gasification, residue gasification, refuse gasification or oil gasification |
| CN101050389A (en) * | 2007-05-11 | 2007-10-10 | 湖北省化学研究院 | Method for purifying HCN and COS in fuel gas produced from coal |
| CN100376313C (en) * | 2003-05-29 | 2008-03-26 | 国际壳牌研究有限公司 | A process for the removal of so2, hcn and h2s and optionally cos, cs2 and nh3 from a gas stream |
| EP2412667A1 (en) * | 2010-07-27 | 2012-02-01 | Air Products And Chemicals, Inc. | A method and apparatus for adjustably treating a sour gas |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1545470A1 (en) | 1966-10-05 | 1970-02-05 | Pichler Dr Phil Helmut | Process for converting coke oven gas into a gas that can be exchanged for natural gas |
| DE2551717C3 (en) * | 1975-11-18 | 1980-11-13 | Basf Ag, 6700 Ludwigshafen | and possibly COS from gases |
| US4248718A (en) | 1978-12-26 | 1981-02-03 | Chevron Research Company | Overbased lubricating oil additive |
| JPS59145288A (en) | 1983-02-07 | 1984-08-20 | Nippon Steel Chem Co Ltd | Hydrorefining of gas oil |
| FR2823193B1 (en) * | 2001-04-04 | 2004-02-13 | Pro Catalyse | ALUMINUM AGGLOMERATES, THEIR PREPARATION PROCESS, AND THEIR USES AS CATALYST SUPPORT, CATALYST OR ABSORBENT |
| FR2823194B1 (en) | 2001-04-10 | 2004-02-13 | Pro Catalyse | ALUMINUM AGGLOMERATES FOR USE, IN PARTICULAR, AS CATALYST SUPPORTS, CATALYSTS OR ADSORBENTS, AND THEIR PREPARATION METHODS |
-
2014
- 2014-01-08 JP JP2015551202A patent/JP2016505695A/en active Pending
- 2014-01-08 WO PCT/EP2014/050190 patent/WO2014108423A1/en active Application Filing
- 2014-01-08 KR KR1020157021202A patent/KR102055036B1/en active IP Right Grant
- 2014-01-08 PL PL14702755T patent/PL2943556T3/en unknown
- 2014-01-08 CN CN201480004324.0A patent/CN104903428B/en active Active
- 2014-01-08 EP EP14702755.1A patent/EP2943556B1/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1018630A (en) * | 1963-11-13 | 1966-01-26 | Shell Int Research | Process for the purification of hot gases obtained by partial combustion and containing soot and carbonyl sulphide |
| GB1332337A (en) * | 1970-09-21 | 1973-10-03 | Shell Int Research | Reducing total sulphur content of claus offgases |
| GB1404581A (en) * | 1971-09-01 | 1975-09-03 | Shell Int Research | Process for the removal of soot and sulphur compounds from the crude gas generated by the partial combustion of a carbonaceous fuel |
| DE2647690A1 (en) * | 1975-12-29 | 1977-07-14 | Parsons Co Ralph M | PROCESS FOR DESULFURIZATION OF COOKER GAS |
| US4085199A (en) * | 1976-06-08 | 1978-04-18 | Bethlehem Steel Corporation | Method for removing hydrogen sulfide from sulfur-bearing industrial gases with claus-type reactors |
| US4863489A (en) * | 1989-02-03 | 1989-09-05 | Texaco Inc. | Production of demercurized synthesis gas, reducing gas, or fuel gas |
| WO1993013184A1 (en) * | 1991-12-30 | 1993-07-08 | Gastec N.V. | Process for treating gases obtained by coal gasification, residue gasification, refuse gasification or oil gasification |
| CN100376313C (en) * | 2003-05-29 | 2008-03-26 | 国际壳牌研究有限公司 | A process for the removal of so2, hcn and h2s and optionally cos, cs2 and nh3 from a gas stream |
| CN101050389A (en) * | 2007-05-11 | 2007-10-10 | 湖北省化学研究院 | Method for purifying HCN and COS in fuel gas produced from coal |
| EP2412667A1 (en) * | 2010-07-27 | 2012-02-01 | Air Products And Chemicals, Inc. | A method and apparatus for adjustably treating a sour gas |
Also Published As
| Publication number | Publication date |
|---|---|
| EP2943556A1 (en) | 2015-11-18 |
| PL2943556T3 (en) | 2020-09-21 |
| EP2943556B1 (en) | 2020-04-08 |
| WO2014108423A1 (en) | 2014-07-17 |
| CN104903428B (en) | 2019-01-18 |
| KR20150103738A (en) | 2015-09-11 |
| JP2016505695A (en) | 2016-02-25 |
| KR102055036B1 (en) | 2019-12-11 |
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