CN104903428B - By the process of anthracite production synthesis gas - Google Patents
By the process of anthracite production synthesis gas Download PDFInfo
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- CN104903428B CN104903428B CN201480004324.0A CN201480004324A CN104903428B CN 104903428 B CN104903428 B CN 104903428B CN 201480004324 A CN201480004324 A CN 201480004324A CN 104903428 B CN104903428 B CN 104903428B
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- sulfide
- catalyst
- hydrogenation
- mole
- cobaltmolybdate
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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
The present invention relates to a kind of methods by coke production synthesis gas, wherein (a) anthracite is subjected to stem cracking, lead to the generation of admixture of gas；The admixture of gas contains the hydrogen as main component, methane, nitrogen and carbon monoxide and the carbon sulfide as a small amount of component；(b) admixture of gas carries out hydrogenation at a temperature in the range of 200 to 280 DEG C, on the sulfide cobaltmolybdate catalyst being arranged on alumina supporting material；And it (c) is separated from the admixture of gas from the hydrogen sulfide obtained in hydrogenation.
Description
Technical field
The invention belongs to coke manufacturing technology field and be related to from coke-stove gas remove carbon sulfide new process and
New catalyst and its application.
Background technique
Coke-stove gas (synonym: coke gas) is the dry distillation from anthracite (hard coal) in coke furnace factory
It obtains.As main component, the gas usually contain the hydrogen of about 55wt% (weight percent), 25wt% methane,
The nitrogen of 10wt% and the carbon monoxide of 5wt%.For this reason, coke-stove gas is usually to close as the synthesis gas of chemical reaction
Lattice, but it is disadvantageous in that carbonyl sulfide (carbonyl sulphide) and carbon sulfide (carbon
Disulphide content) must be removed in advance, this is because they for example serve as catalyst poison in subsequent reaction
Object.Catalyst must often be cleaned even being replaced as a result, this is directly related to workload and cost and due to factory
Turnover and it is undesirable.
A kind of method that undesired carbon sulfide is removed from coke-stove gas is that coal gas is subjected to catalytic hydrogenation simultaneously
And conversion sulphur compound is hydrogen sulfide.It, can be molten by means of aqueous lye such as ammonia although this gas is also undesired
Liquid and be easy to be cleaned out.
According to the prior art, relevant technique is known.For example, 1545470 A1 of German patent application DE
(Pichler) suggest that hydrogenation carbon sulfide is hydrogen sulfide on cobalt molybdenum, nickel molybdenum or nickel cobalt molybdenum catalyst, it then can be by
It separates.Reaction temperature in the embodiment is higher than 550 DEG C.
Hydrodesulfurization (hydrodesulphurisation) for coke-stove gas, based on nickel, cobalt, molybdenum or palladium
The use of catalyst can also be found in various Japanese patent applications earlier, such as 59 145288 A2 of JP
(Shinnittetsu) or 59 230092 A1 of JP (Hitachi).And these corresponding processes.
Similar technique can also know from 2647690 A1 of German patent application DE (Parsons), propose
On catalyst on the basis of cobalt, molybdenum, iron, chromium, vanadium, thorium, nickel, tungsten and/or uranium the carbon compound of hydrogenation sulfur-bearing and by
The hydrogen sulfide obtained in extraction column is removed in alkali hydroxide soln.The sulfide of above-mentioned metal is proposed as coagulation
Native catalyst.But related disadvantage, in the case, catalyst needs minimum 260 DEG C of temperature and hydrogenation must
It must preferably be carried out at significant higher temperature, partly even higher than 400 DEG C.The reason of in energy cost, this is special
It is undesirable；In addition, the temperature will change the component of gas, i.e., methanation can occur.
Although prior art processes are converted carbon sulfide as hydrogen sulfide in the way of high production capacity and therefore convert coke-oven coal
Gas is the synthesis gas of enough high-quality, they are directed to substantive disadvantage, i.e. these techniques must be equivalent to more than 280
DEG C very high temperature under carry out, otherwise sufficiently high conversion ratio is difficult to realize.
Therefore, the purpose of the present invention is to improve prior art, if any, as long as carbon sulfide and organosulfur compound
(such as thiophene) is substantially quantitatively converted hydrogen sulfide, and is at a temperature of significant reduced.Further, the technique purport
Ensuring to maintain the mass ratio of oxycarbide and methane constant, that is, is preventing methanation.
Summary of the invention
Subject of the present invention be for the method by coke production synthesis gas, wherein
(a) anthracite is subjected to stem cracking, leads to contain hydrogen, methane, nitrogen and carbon monoxide as main component and carbon
Generation of the sulfide as the admixture of gas of a small amount of component,
(b) vulcanization that admixture of gas provides at a temperature in the range of 200 to 280 DEG C, on alumina supporting material
Hydrogenation is carried out on object cobaltmolybdate catalyst, and
(c) it is separated from the admixture of gas from the hydrogen sulfide obtained in hydrogenation.
Astoundingly, it is known that the sulfide cobaltmolybdate catalyst for carbon sulfide hydrogenation even be lower than 280
DEG C and preferably shorter than 260 DEG C at have the characteristics that high activity and selectivity, if they are deposited over alumina supporting material
On.Carbon sulfide actually at least 95 (volume) % are hydrogenated reaction and do not observe hydrogenation to oxidation of coal at hydrogen sulfide
Influence of the object to the ratio of methane.This is one unexpected as a result, document DE 2647690 because being quoted from according to introductory song
The introduction of A1, people are expected also to promote undesired methanation to one with the catalyst that sulphided form mainly contains cobalt and molybdenum
A degree that can not ignore, especially if if reaction carries out under stress as usual.
Production coke coal gas is cracked by anthracite
During anthracite dry distillation or cracking, the volatile component quilt of coal at a temperature of 900 to 1400 DEG C occurs
Porous coke is discharged and formed, substantially contains only carbon now.By condensate fractionation, unstrpped gas be broken down into tar,
Sulfuric acid, ammonia, naphthalene (naphthalene), benzene and so-called coke coal gas.The latter is by hydrogen, methane, nitrogen and oxycarbide group
At and by sufficiently handling so that chemical reaction can be further used in after obtaining synthesis gas.
Hydrogenation technique
The hydrogenation of cracked gas can carry out in a conventional manner, and to this, mainly fixed bed reactors are had turned out to be
It is most suitable, because catalyst is provided as bulk layers with bulk form or fixes filler (packing).Because of bulk material
It more easily forms channel and is therefore formed and is distributed with Non-Uniform Flow, in this embodiment it is preferred that catalyst is to fill out
The mode of material is arranged in reactor.
But the advantages of hydrogenation in fixed bed reactors, is that the yield of high space time is achieved,
This is why process according to the invention can also at about 500 to about 1500 ls/h (l/h) and preferably approximately
1000 to about 1200 ls/h (l/h) high GHSV (gas hourly space velocity, gas (small) space-time
() speed) it carries out under value.Another advantage is for product withdraw without special measure, because reactant-cracks
Coal gas and hydrogen-are preferably collectively incorporated into the bottom of reactor, across the catalyst bed and conduct for leading to hydrogenation
Product leaves reactor at top.
As starting it has been mentioned that a specific advantages of the process are sulphur compounds according to the present invention
Hydrogenation on catalyst to be used, so that reaction carries out under conditions of obvious milder and carbon sulfide completely turns
Change and any sign without methanation is possibly realized.Range of reaction temperature between 200 to 280 DEG C, and preferably 240 to
There is sufficient reaction speed between 260 DEG C.Reactor can be externally heated, this leads to higher energy consumption；Or reaction
Component can be heated before introducing them into reactor, can be by means of for example, by using venturi (Venturi)
It is mixed in the nozzle of principle work.
Further, reaction can carry out under atmospheric pressure or pressurization in 1 to 15 bar of range.Present embodiment
Preferably using the pressure in the range of about 5 to about 10 bars, because this is to be conducive to yield and reaction speed.
Catalyst
Sulfide cobaltmolybdate catalyst
Term " sulfide cobaltmolybdate catalyst " refers mainly to contain molybdenum sulfide as actual catalyst and cobalt as promotor
Catalyst.That catalyst is the co-vulcanized generation by each oxide in known manner, wherein molybdenum oxide
(MoO3) it is converted completely into molybdenum disulfide (MoS2).When the latter is applied on alumina support, or flatly connect
It closes surface (" substrate engagement ") or only engages an edge (" edge join ").After vulcanization, there are three types of form is available for cobalt:
First as the Co being deposited on carrier9S8Crystal, as in MoS2On the edge of plate such as Co2+Ion (" CoMo phase ") and work
For the Co on the tetrahedral site of aluminium oxide lattice2+Ion.Accordingly, it is preferred that catalyst is mainly by more than 50
(mole) the molybdenum sulfide composition of %, preferably greater than 70 (mole) % and most preferably more than 90 (mole) %, and includes sulphur
For the cobalt of compound form as promotor, the quantity of (mole) % is the difference with 100.As a result, in a similar preferred implementation
In example, the catalyst does not include any other metal, particular without other transition metal.
Alumina support
Aluminium oxide with high-specific surface area (specific surface area) is considered as sulfide cobalt
The suitable carrier of molybdenum catalyst, the aluminium oxide preferably have the feature that
Minimum 75 milliliters/100 grams, preferably 80 milliliters/100 grams, most preferably 85 milliliters/100 grams of V37A；
Maximum 31 milliliters/100 grams, preferably 25 milliliters/100 grams, most preferably 15 milliliters/100 grams of V0.1μm；
Maximum 20 milliliters/100 grams, preferably 15 milliliters/100 grams, most preferably 10 milliliters/100 grams of V0.2μm；With
·V0.1μmCompare V0.2μmRatio be at least 1.5.
The alumina support of mentioned type is fully known in the art.For example, European patent document EP
1385786 B1 and 1385787 B1 of EP (Axens) describe their manufacturing process, wherein gibbsite type
(hydrargillite-type) aluminium oxide is ground, using the aqueous solution of aluminum nitrate and formic acid, in 200 DEG C of hydro-thermal method processing 6
Hour, then products therefrom is calcined at 400 to 1300 DEG C.The carrier material is then extruded and is consequently adapted to carry.Just
For the property and manufacture of the catalyst carrier, this two documents are all relevant bibliography.
Purifying
The hydrogenation reaction product of reactor especially fixed bed reactors is left, the vulcanization now containing vulcanization hydrogen form is closed
Object, content is usually in the range of 50 to 300ppm.H2The presence of S be just as the presence of carbon sulfide it is undesirable,
But for the latter, hydrogen sulfide can be cleaned out relatively easily and be cleaned out in large quantities after all.For
This purpose, those hydrogenation gases are preferably passed through absorption tower, and there, they for example have such as sodium hydroxide
It is handled in the adverse current of the aqueous solution of (caustic soda) or ammonia.Alternatively, other devices can be used to purify and be somebody's turn to do
Gas, such as Venturi Scrubber.
When vulcanization hydrogen partial has been separated, the product being purified is as the Gao Pin for further chemically reacting
Matter synthesis gas is suitable and unrestricted.
Industrial applicibility
Another theme of the invention be related to being set on the alumina support, for carbon sulfide hydrogenation at vulcanization
The application of the sulfide cobaltmolybdate catalyst of hydrogen.In this regard, preferred this kind of cobaltmolybdate catalyst is used, referring to metal component, master
If being made of molybdenum sulfide and including that cobalt sulfide (cobalt sulphide) is used as unique promotor.
Carrier for cobaltmolybdate catalyst is it is also preferred that aluminium oxide, with high specific surface area and at the same time having following spy
Sign:
(i) minimum 75 milliliters/100 grams, preferably 80 milliliters/100 grams, most preferably 85 milliliters/100 grams of V37A；
(ii) maximum 31 milliliters/100 grams, preferably 25 milliliters/100 grams, most preferably 15 milliliters/100 grams of V0.1μm；
(iii) maximum 20 milliliters/100 grams, preferably 15 milliliters/100 grams, most preferably 10 milliliters/100 grams of V0.2μm；With
(iv)V0.1μmCompare V0.2μmRatio be at least 1.5.
The present invention also includes a kind of method for being used to prepare hydrogen sulfide, and wherein carbon sulfide is being arranged on alumina support
On sulfide cobaltmolybdate catalyst working dose under carry out hydrogenation.
It is preferred that carbon sulfide carries out hydrogenation in the presence of cobaltmolybdate catalyst, referring to the metal component, which is urged
Agent is mainly made of and comprising only as the cobalt sulfide of promotor molybdenum sulfide.Preferably alumina support meets following
Feature:
(i) minimum 75 milliliters/100 grams, preferably 80 milliliters/100 grams, most preferably 85 milliliters/100 grams of V37A；
(ii) maximum 31 milliliters/100 grams, preferably 25 milliliters/100 grams, most preferably 15 milliliters/100 grams of V0.1μm；
(iii) maximum 20 milliliters/100 grams, preferably 15 milliliters/100 grams, most preferably 10 milliliters/100 grams of V0.2μm；With
(iv)V0.1μmCompare V0.2μmRatio be at least 1.5.
Embodiment
Example 1
Pilot factory for fixed bed hydrogenation reaction is equipped with commercially available massive sulphide cobalt on the alumina support
The bulk layers of molybdenum catalyst.Then, different coke coal gas is introduced in the bottom of tower.Between these so-called feed gas
Only difference is that the content of carbon sulfide especially carbon disulfide (carbon disulphide).Hydrogenation is at 220 DEG C
At a temperature of and 10 bars of pressure under carry out.Its GHSV is about 1200 ls/h.
Product gas carries out analysis to sulphur in gas chromatograph and the fraction of hydrogen sulfide and carbon sulfide is by means of protecting
The phase is stayed to be measured.Table 1 summarizes result.Conversion ratio refers to CS2The hydrogenation of fraction.
Table 1
The result of hydrogenation (weight is indicated with (volume) %, unless otherwise indicated)
Test result shows that the fraction at least 95% of carbon sulfide is converted into hydrogen sulfide.Its in coke-stove gas at the same time
The ratio of its ingredient is kept constant, that is, does not have methanation problem.
Claims (14)
1. a kind of method for by anthracite production synthesis gas, wherein
(a) anthracite is subjected to stem cracking, leads to the generation of coke-stove gas；The coke-stove gas mixture contains as main component
Hydrogen, methane, nitrogen and carbon monoxide and carbon sulfide as a small amount of component；
(b) coke-stove gas at a temperature in the range of 200 to 280 DEG C, in the sulphur being arranged on alumina supporting material
Hydrogenation is carried out on compound cobaltmolybdate catalyst；And
(c) it is separated from the coke-stove gas from the hydrogen sulfide obtained in hydrogenation,
Wherein, used sulfide cobaltmolybdate catalyst contains molybdenum sulfide as actual catalyst and cobalt as promotor,
The catalyst comprises more than 50 (mole) % molybdenum sulfides, and includes the cobalt of sulphided form, (mole) % quantity
For the difference with 100.
2. the method according to claim 1, wherein within the temperature range of hydrogenation is between 240 to 260 DEG C
It carries out.
3. the method according to claim 1, wherein hydrogenation carries out under 1 to 15 bar of pressure.
4. according to the method described in claim 3, it is characterized in that, hydrogenation carries out under 5 to 10 bars of pressure.
5. the method according to claim 1, wherein hydrogenation is at 500 to 1500 ls/h of GHSV
It carries out.
6. the method according to claim 1, wherein not including the cobaltmolybdate catalyst quilt of any other transition metal
It uses.
7. method described in claim 1, which is characterized in that referring to metal component, the cobaltmolybdate catalyst is by more than 70
(mole) the molybdenum sulfide composition of %.
8. method described in claim 1, which is characterized in that referring to metal component, the cobaltmolybdate catalyst is by more than 90
(mole) the molybdenum sulfide composition of %.
9. according to claim 1 to method described at least one of 8, which is characterized in that the hydrogenation is anti-in fixed bed
It answers in device and carries out.
10. according to the method described in claim 9, it is characterized in that, the catalyst used in fixed bed reactors is provided
As bulk layers or filler.
11. according to the method described in claim 9, it is characterized in that, the hydrogenated products are logical by transmission after leaving reactor
Absorption tower is crossed, hydrogen sulfide comes out in the absorption tower by means of akaline liquid is cleaned.
12. a kind of method for being used to prepare hydrogen sulfide, which is characterized in that sulphur on the alumina support is being set in carbon sulfide
Hydrogenation is carried out under compound cobaltmolybdate catalyst working dose, wherein used sulfide cobaltmolybdate catalyst contains molybdenum sulfide work
It is actual catalyst and cobalt as promotor, the catalyst comprises more than 50 (mole) % molybdenum sulfides, and includes sulfide
The cobalt of form, (mole) % quantity are the difference with 100.
13. according to the method for claim 12, which is characterized in that the carbon sulfide carries out in the presence of cobaltmolybdate catalyst
Hydrogenation, referring to metal component, the cobaltmolybdate catalyst is made of the molybdenum sulfide of 70 (mole) %.
14. according to the method for claim 12, which is characterized in that the carbon sulfide carries out in the presence of cobaltmolybdate catalyst
Hydrogenation, referring to metal component, the cobaltmolybdate catalyst is made of the molybdenum sulfide of 90 (mole) %.
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 CN104903428A (en) | 2015-09-09 |
| CN104903428B true CN104903428B (en) | 2019-01-18 |
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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 |
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| 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 |
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| EP2412667A1 (en) * | 2010-07-27 | 2012-02-01 | Air Products And Chemicals, Inc. | A method and apparatus for adjustably treating a sour gas |
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| 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
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| 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 |
| CN104903428A (en) | 2015-09-09 |
| KR20150103738A (en) | 2015-09-11 |
| JP2016505695A (en) | 2016-02-25 |
| KR102055036B1 (en) | 2019-12-11 |
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