EP2943556B1 - Process for the hydrogenation of carbon sulphide using a sulphidic cobalt molybdenum catalyst on an aluminium oxide carrier - Google Patents
Process for the hydrogenation of carbon sulphide using a sulphidic cobalt molybdenum catalyst on an aluminium oxide carrier Download PDFInfo
- Publication number
- EP2943556B1 EP2943556B1 EP14702755.1A EP14702755A EP2943556B1 EP 2943556 B1 EP2943556 B1 EP 2943556B1 EP 14702755 A EP14702755 A EP 14702755A EP 2943556 B1 EP2943556 B1 EP 2943556B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- cobalt
- hydrogenation
- catalysts
- molybdenum
- sulphidic
- 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.)
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- 239000003054 catalyst Substances 0.000 title claims description 56
- 238000005984 hydrogenation reaction Methods 0.000 title claims description 31
- 238000000034 method Methods 0.000 title claims description 27
- WHDPTDWLEKQKKX-UHFFFAOYSA-N cobalt molybdenum Chemical compound [Co].[Co].[Mo] WHDPTDWLEKQKKX-UHFFFAOYSA-N 0.000 title claims description 18
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 title description 41
- QGJOPFRUJISHPQ-UHFFFAOYSA-N Carbon disulfide Chemical compound S=C=S QGJOPFRUJISHPQ-UHFFFAOYSA-N 0.000 title description 11
- 239000007789 gas Substances 0.000 claims description 39
- 229910017052 cobalt Inorganic materials 0.000 claims description 22
- 239000010941 cobalt Substances 0.000 claims description 22
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 22
- DXHPZXWIPWDXHJ-UHFFFAOYSA-N carbon monosulfide Chemical class [S+]#[C-] DXHPZXWIPWDXHJ-UHFFFAOYSA-N 0.000 claims description 20
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 19
- PTISTKLWEJDJID-UHFFFAOYSA-N sulfanylidenemolybdenum Chemical compound [Mo]=S PTISTKLWEJDJID-UHFFFAOYSA-N 0.000 claims description 17
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 14
- -1 Co2+ ions Chemical class 0.000 claims description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 10
- 229910052961 molybdenite Inorganic materials 0.000 claims description 10
- CWQXQMHSOZUFJS-UHFFFAOYSA-N molybdenum disulfide Chemical compound S=[Mo]=S CWQXQMHSOZUFJS-UHFFFAOYSA-N 0.000 claims description 10
- 229910052982 molybdenum disulfide Inorganic materials 0.000 claims description 10
- JKQOBWVOAYFWKG-UHFFFAOYSA-N molybdenum trioxide Chemical compound O=[Mo](=O)=O JKQOBWVOAYFWKG-UHFFFAOYSA-N 0.000 claims description 10
- 239000000969 carrier Substances 0.000 claims description 8
- 239000003245 coal Substances 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 8
- 238000000197 pyrolysis Methods 0.000 claims description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 7
- 230000015572 biosynthetic process Effects 0.000 claims description 7
- 239000000470 constituent Substances 0.000 claims description 7
- 238000004519 manufacturing process Methods 0.000 claims description 7
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 7
- 238000003786 synthesis reaction Methods 0.000 claims description 7
- 239000001257 hydrogen Substances 0.000 claims description 6
- 229910052739 hydrogen Inorganic materials 0.000 claims description 6
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims description 6
- 239000013078 crystal Substances 0.000 claims description 5
- 239000012876 carrier material Substances 0.000 claims description 4
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims description 3
- 238000010521 absorption reaction Methods 0.000 claims description 2
- 239000007788 liquid Substances 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 description 16
- 239000000571 coke Substances 0.000 description 10
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical class [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 7
- 229910052751 metal Inorganic materials 0.000 description 6
- 239000002184 metal Substances 0.000 description 6
- 239000000047 product Substances 0.000 description 5
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 238000004939 coking Methods 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 3
- 229910002090 carbon oxide Inorganic materials 0.000 description 3
- JJWKPURADFRFRB-UHFFFAOYSA-N carbonyl sulfide Chemical compound O=C=S JJWKPURADFRFRB-UHFFFAOYSA-N 0.000 description 3
- 229910052750 molybdenum Inorganic materials 0.000 description 3
- 239000011733 molybdenum Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- JLDSOYXADOWAKB-UHFFFAOYSA-N aluminium nitrate Chemical compound [Al+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O JLDSOYXADOWAKB-UHFFFAOYSA-N 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 150000002739 metals Chemical class 0.000 description 2
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 230000000737 periodic effect Effects 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 235000011121 sodium hydroxide Nutrition 0.000 description 2
- ZSLUVFAKFWKJRC-IGMARMGPSA-N 232Th Chemical compound [232Th] ZSLUVFAKFWKJRC-IGMARMGPSA-N 0.000 description 1
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 1
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 1
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- 241000700735 Ground squirrel hepatitis virus Species 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 229910052776 Thorium Inorganic materials 0.000 description 1
- 229910052770 Uranium Inorganic materials 0.000 description 1
- QZYDAIMOJUSSFT-UHFFFAOYSA-N [Co].[Ni].[Mo] Chemical compound [Co].[Ni].[Mo] QZYDAIMOJUSSFT-UHFFFAOYSA-N 0.000 description 1
- 229910001854 alkali hydroxide Inorganic materials 0.000 description 1
- 150000008044 alkali metal hydroxides Chemical class 0.000 description 1
- ILRRQNADMUWWFW-UHFFFAOYSA-K aluminium phosphate Chemical compound O1[Al]2OP1(=O)O2 ILRRQNADMUWWFW-UHFFFAOYSA-K 0.000 description 1
- 229940001007 aluminium phosphate Drugs 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 229910001570 bauxite Inorganic materials 0.000 description 1
- 239000013590 bulk material Substances 0.000 description 1
- 150000001722 carbon compounds Chemical class 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 239000011651 chromium Substances 0.000 description 1
- KYYSIVCCYWZZLR-UHFFFAOYSA-N cobalt(2+);dioxido(dioxo)molybdenum Chemical compound [Co+2].[O-][Mo]([O-])(=O)=O KYYSIVCCYWZZLR-UHFFFAOYSA-N 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 235000019253 formic acid Nutrition 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 238000010335 hydrothermal treatment Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 229910001629 magnesium chloride Inorganic materials 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- DDTIGTPWGISMKL-UHFFFAOYSA-N molybdenum nickel Chemical compound [Ni].[Mo] DDTIGTPWGISMKL-UHFFFAOYSA-N 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 239000012264 purified product Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- VRRFSFYSLSPWQY-UHFFFAOYSA-N sulfanylidenecobalt Chemical compound [Co]=S VRRFSFYSLSPWQY-UHFFFAOYSA-N 0.000 description 1
- 150000004763 sulfides Chemical class 0.000 description 1
- 239000001117 sulphuric acid Substances 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 229930192474 thiophene Natural products 0.000 description 1
- 150000003577 thiophenes Chemical class 0.000 description 1
- ZCUFMDLYAMJYST-UHFFFAOYSA-N thorium dioxide Chemical compound O=[Th]=O ZCUFMDLYAMJYST-UHFFFAOYSA-N 0.000 description 1
- 229910052723 transition metal Inorganic materials 0.000 description 1
- 150000003624 transition metals Chemical class 0.000 description 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 1
- 229910052721 tungsten Inorganic materials 0.000 description 1
- 239000010937 tungsten Substances 0.000 description 1
- DNYWZCXLKNTFFI-UHFFFAOYSA-N uranium Chemical compound [U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U][U] DNYWZCXLKNTFFI-UHFFFAOYSA-N 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- GPPXJZIENCGNKB-UHFFFAOYSA-N vanadium Chemical compound [V]#[V] GPPXJZIENCGNKB-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- 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
Definitions
- the invention belongs to the field of coke making technology and relates to a new process for the removal of carbon sulphides from coke oven gas.
- Coke oven gas (synonym: coking gas) is obtained from dry distillation of hard coal in coke oven plants.
- the gas typically contains approx. 55 %-wt hydrogen, 25 %-wt methane, 10 %-wt nitrogen and 5 %-wt. carbon monoxide. Due to this, coke oven gas is generally qualified as a synthesis gas for chemical reactions; disadvantageous, however, are the contents of carbonyl sulphide and carbon disulphide, which must previously be removed as they act as catalyst poisons in subsequent reactions, for example. The consequence is that the catalysts must frequently be cleaned or even exchanged, which directly involves effort and cost and is also unwanted because of the turnaround of the plant.
- a common method to free industrial gas from unwanted carbon sulphides is the catalytic hydrolysis of such compounds as described in DE 26 47 690 A1 , EP 2 412 667 A1 , GB 1 332 337 A , US 4 336 233 A , US 4 863 489 A , WO 2004/105922 A1 , and WO 93/13184 A1 .
- One further method to free coke oven gas from unwanted carbon sulphides is to subject the gas to a catalytic hydrogenation and to convert the sulphur compounds into hydrogen sulphide. Although this gas is also unwanted, it can be washed out easily by means of aqueous lye, for example, ammonia solution.
- a catalytic hydrogenation of gas mixtures is known in which carbonyl sulphide is hydrogenated using catalyst materials such as alumina, bauxite, activated clays, aluminium phosphate, thoria and magnesium chloride while carbon disulphide is hydrogenated using a catalyst containing at least one metal from Groups VI and/or VIII of the Periodic System of the Elements, either as such or in chemically bound form.
- catalyst materials such as alumina, bauxite, activated clays, aluminium phosphate, thoria and magnesium chloride
- carbon disulphide is hydrogenated using a catalyst containing at least one metal from Groups VI and/or VIII of the Periodic System of the Elements, either as such or in chemically bound form.
- Cobalt-molybdenum-aluminium catalysts for hydrogenation of carbonyl sulphide and carbon disulphide are also known from US 4 336 233 and EP 2 412 667 A1 , respectively.Related processes are already known according to prior
- German patent application DE 1545470 A1 suggests to hydrogenate carbon sulphides over cobalt molybdenum, nickel molybdenum or nickel cobalt molybdenum catalysts to hydrogen sulphide, which is then to be separated.
- the reaction temperature in the examples is above 550 °C.
- German patent application DE 2647690 A1 (Parsons ), which proposes to hydrogenate sulphur-bearing carbon compounds over catalysts on the basis of cobalt, molybdenum, iron, chromium, vanadium, thorium, nickel, tungsten and/or uranium and to remove the hydrogen sulphide obtained in an extraction column by means of an alkali hydroxide solution.
- the sulphides of the above metals are proposed as concrete catalysts.
- a disadvantage involved is, however, that in this case as well the catalysts require a minimum temperature of 260 °C and the hydrogenation must preferably be carried out at significantly higher temperatures, partly even above 400 °C. This is not desired especially for reasons of energy cost; in addition, such temperatures will change the composition of the gas, i.e. methanation will take place already.
- Aim of the present invention therefore was to improve the existing processes in so far as the carbon sulphides and organic sulphur compounds (e.g. thiophenes), if any, are transformed virtually quantitatively to hydrogen sulphide but at temperatures which are significantly lower. Furthermore, the process was intended to ensure keeping the mass ratio of carbon oxides to methane unchanged, i.e. preventing methanation.
- carbon sulphides and organic sulphur compounds e.g. thiophenes
- Subject matter of the invention is a process for the production of synthesis gas from hard coal, in which
- the sulphidic cobalt molybdenum catalysts known for hydrogenation of carbon sulphides feature a high activity and selectivity even below 280 and preferably below 260°C if they are deposited on aluminium oxide carrier material. Carbon sulphides are actually hydrogenated to hydrogen sulphide at at least 95 %-vol. without observing an influence of the hydrogenation on the ratio of carbon oxides to methane.
- Hydrogenation of the pyrolysis gases may be done in the manner customary, for which mainly fixed-bed reactors have proved best suited, as the catalysts are provided in the form of lumps as bulk layer or fixed packing. Since bulk material leads to channelling more easily and hence to an inhomogeneous flow distribution, preference is given to the embodiment in which the catalysts are arranged in packings inside the reactor.
- the advantage of the hydrogenation in the fixed-bed reactor is that high space/time yields can be achieved, which is why the process according to the invention can also be carried out at high GSHV values of approx. 500 to approx. 1500 and preferably approx. 1000 to approx. 1200 l/h.
- Another advantage is provided in that no special measures are required for the product discharge, as the reactants - i.e. pyrolysis gas and hydrogen - are preferably introduced jointly at the bottom of the reactor, pass through the catalyst bed leading to hydrogenation and leave the reactor as products at the top.
- a specific advantage of the process is that the sulphur compounds are hydrogenated over the catalysts to be used according to the invention, so that the reaction is possible at significantly more moderate conditions and effects the complete conversion of the carbon sulphides, without any signs of methanation.
- the reaction temperature ranges between 200 and 280 and with regard to an adequate reaction velocity preferably between 240 and 260 °C.
- the reactor may be heated from the outside - which results in a higher energy consumption - or the reaction components may be heated before introducing them into the reactor, with the mixing being possibly done in a nozzle which works, for example, by the Venturi principle.
- reaction may take place in the range of 1 to 15 bar, i.e. at atmospheric pressure or under pressure. Preference is given to an embodiment which uses a pressure in the range of approx. 5 to approx. 10 bar, as this is of benefit to yield and reaction velocity.
- 'sulphidic cobalt molybdenum catalysts' mainly refers to catalysts which contain molybdenum sulphide as the actual catalyst and cobalt as the promoter. Catalysts of that kind are produced in known manner by joint sulphidation of the respective oxides, where the MoO 3 is converted completely to MoS 2 . When the latter is applied to the aluminium oxide carrier, it is either bonded flat to the surface ('basal bonding') or to one edge only ('edge bonding').
- the cobalt is available in three forms: first as Co 9 S 8 crystals deposited on the carrier, as Co 2+ ions on the edges of the MoS 2 plates ('CoMo phase') and as Co 2+ ions on the tetrahedral positions in the aluminium oxide lattice.
- the catalysts are hence composed predominantly, i.e. of more than 50 %-mole, preferably of more than 70 %-mole and most preferably of more than 90 %-mole, of molybdenum sulphide and contain the cobalt in sulphidic form as a promoter, the quantity in %-mole resulting as the difference to 100. From this it follows that in a likewise preferred embodiment the catalysts do not contain any other metals, especially no other transition metals.
- Aluminium oxides of especially high specific surface area come into consideration as suitable carriers for the sulphidic cobalt molybdenum catalysts, the aluminium oxides preferably featuring the following characteristics:
- Aluminium oxide carriers of the type mentioned are sufficiently known from the state of the art.
- European patent documents EP 1385786 B1 and EP 1385787 B1 (Axens ), for example, describe a process for their manufacture, in which a hydrargillite-type aluminium oxide is ground, undergoes hydrothermal treatment with an aqueous solution of aluminium nitrate and formic acid at 200 °C for 6 hours, the resulting product then being calcined at 400 to 1300. The carrier material is then extruded and is thus ready for loading.
- the two documents mentioned are related to by reference.
- the hydrogenation gases are, for this purpose, preferably passed through an absorption column, where they are treated, for example, in counter current with an aqueous base such as caustic soda or ammonia.
- other devices may be used for the purification of gases as, for example, venturi scrubbers.
- the purified product is available without restriction as a high-quality synthesis gas for further chemical reactions.
- a further subject matter of the present invention is the use of sulphidic cobalt molybdenum catalysts provided on aluminum oxide carriers for the hydrogenation of carbon sulphides to hydrogen sulphide, wherein sulphidic cobalt molybdenum catalysts are used which contain molybdenum sulphide as the actual catalyst and cobalt as the promoter, wherein said catalysts are composed of more than 50 %-mole of molybdenum sulphide and said catalysts contain the cobalt in sulphidic form, the quantity in %-mole of said cobalt in sulphidic form resulting as the difference to 100, wherein molybdenum sulphide has been obtained by sulphidation of the respective oxide, wherein the MoO 3 has been converted completely to MoS 2 , wherein after sulphidation the cobalt is present in three forms: first as Co 9 S 8 crystals deposited on the carrier, as Co 2+ ions on the edges of the MoS 2 plates (
- the present invention also encompasses a method for preparing hydrogen sulphide, wherein carbon sulphides are subjected to hydrogenation in the presence of a working amount of sulphidic cobalt molybdenum catalysts provided on aluminium oxide carriers.
- the carbon sulphides are subjected to hydrogenation in the presence of cobalt molybdenum catalysts which, with reference to the metal components, predominantly consist of molybdenum sulphide and contain cobalt sulphide as a promoter only.
- cobalt molybdenum catalysts which, with reference to the metal components, predominantly consist of molybdenum sulphide and contain cobalt sulphide as a promoter only.
- aluminium oxide carriers meeting the following characteristics:
- a pilot plant for fixed-bed hydrogenation was equipped with a bulk layer of commercially available lumpy sulphidic cobalt molybdenum catalyst on an aluminium oxide carrier. Subsequently, different coking gases were introduced at the bottom of the column. The only difference between these so-called feed gases was the amount of carbon sulphides, in particular carbon disulphide.
- the hydrogenation was performed at a temperature of 220 °C and a pressure of 10 bar.
- the GHSV was about 1200 l/h.
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- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
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Description
- The invention belongs to the field of coke making technology and relates to a new process for the removal of carbon sulphides from coke oven gas.
- Coke oven gas (synonym: coking gas) is obtained from dry distillation of hard coal in coke oven plants. As main constituents, the gas typically contains approx. 55 %-wt hydrogen, 25 %-wt methane, 10 %-wt nitrogen and 5 %-wt. carbon monoxide. Due to this, coke oven gas is generally qualified as a synthesis gas for chemical reactions; disadvantageous, however, are the contents of carbonyl sulphide and carbon disulphide, which must previously be removed as they act as catalyst poisons in subsequent reactions, for example. The consequence is that the catalysts must frequently be cleaned or even exchanged, which directly involves effort and cost and is also unwanted because of the turnaround of the plant.
- A common method to free industrial gas from unwanted carbon sulphides is the catalytic hydrolysis of such compounds as described in
DE 26 47 690 A1 ,EP 2 412 667 A1 ,GB 1 332 337 A US 4 336 233 A ,US 4 863 489 A ,WO 2004/105922 A1 , andWO 93/13184 A1 - One further method to free coke oven gas from unwanted carbon sulphides is to subject the gas to a catalytic hydrogenation and to convert the sulphur compounds into hydrogen sulphide. Although this gas is also unwanted, it can be washed out easily by means of aqueous lye, for example, ammonia solution. For example, from
GB 1 018 630 A US 4 336 233 andEP 2 412 667 A1 , respectively.Related processes are already known according to prior art. German patent applicationDE 1545470 A1 (Pichler ), for example, suggests to hydrogenate carbon sulphides over cobalt molybdenum, nickel molybdenum or nickel cobalt molybdenum catalysts to hydrogen sulphide, which is then to be separated. The reaction temperature in the examples is above 550 °C. - The use of catalysts on a nickel, cobalt, molybdenum or palladium basis for the hydrodesul-phurisation of coke oven gas can also be found in various older Japanese patent applications, as, for instance,
JP 59 145288 A2 (Shinnittetsu JP 59 230092 A1 (Hitachi - A similar process is also known from German patent application
DE 2647690 A1 (Parsons ), which proposes to hydrogenate sulphur-bearing carbon compounds over catalysts on the basis of cobalt, molybdenum, iron, chromium, vanadium, thorium, nickel, tungsten and/or uranium and to remove the hydrogen sulphide obtained in an extraction column by means of an alkali hydroxide solution. The sulphides of the above metals are proposed as concrete catalysts. A disadvantage involved is, however, that in this case as well the catalysts require a minimum temperature of 260 °C and the hydrogenation must preferably be carried out at significantly higher temperatures, partly even above 400 °C. This is not desired especially for reasons of energy cost; in addition, such temperatures will change the composition of the gas, i.e. methanation will take place already. - Although prior-art processes serve to transform carbon sulphides to hydrogen sulphide at high yields and to thus convert coke oven gases into synthesis gases of sufficiently high quality, they all involve the substantial disadvantage that these processes must take place at very high temperatures of considerably more than 280 °C, as otherwise no adequate conversion rates will be achieved.
- Furthermore, from
GB 1 404 581 A US 4 085 199 A discloses the hydrogenation of sulphur compounds in the presence of sulphidized cobalt molybdate catalysts on alumina. - Aim of the present invention therefore was to improve the existing processes in so far as the carbon sulphides and organic sulphur compounds (e.g. thiophenes), if any, are transformed virtually quantitatively to hydrogen sulphide but at temperatures which are significantly lower. Furthermore, the process was intended to ensure keeping the mass ratio of carbon oxides to methane unchanged, i.e. preventing methanation.
- Subject matter of the invention is a process for the production of synthesis gas from hard coal, 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 to 280 °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,
- Surprisingly it was found that the sulphidic cobalt molybdenum catalysts known for hydrogenation of carbon sulphides feature a high activity and selectivity even below 280 and preferably below 260°C if they are deposited on aluminium oxide carrier material. Carbon sulphides are actually hydrogenated to hydrogen sulphide at at least 95 %-vol. without observing an influence of the hydrogenation on the ratio of carbon oxides to methane. This is an unexpected result, as on account of the experience according to document
DE 2647690 A1 quoted at the beginning one would have expected that catalysts which mainly contain cobalt and molybdenum in sulphidic form also facilitate unwanted methanation to a non-negligible degree, especially if the reaction is performed, as usual, under pressure. - During dry distillation or pyrolysis of hard coal, which takes place at 900 to 1400 °C, the volatile constituents of the coal are released and porous coke forms, which now essentially contain only carbon. By fractionated condensation the raw gas is decomposed into tar, sulphuric acid, ammonia, naphthalene, benzene and the so-called coking gas. The latter is composed of hydrogen, methane, nitrogen and carbon oxides and may, after adequate treatment to obtain synthesis gas, be used for further chemical reactions.
- Hydrogenation of the pyrolysis gases may be done in the manner customary, for which mainly fixed-bed reactors have proved best suited, as the catalysts are provided in the form of lumps as bulk layer or fixed packing. Since bulk material leads to channelling more easily and hence to an inhomogeneous flow distribution, preference is given to the embodiment in which the catalysts are arranged in packings inside the reactor.
- The advantage of the hydrogenation in the fixed-bed reactor, however, is that high space/time yields can be achieved, which is why the process according to the invention can also be carried out at high GSHV values of approx. 500 to approx. 1500 and preferably approx. 1000 to approx. 1200 l/h. Another advantage is provided in that no special measures are required for the product discharge, as the reactants - i.e. pyrolysis gas and hydrogen - are preferably introduced jointly at the bottom of the reactor, pass through the catalyst bed leading to hydrogenation and leave the reactor as products at the top.
- As already mentioned at the beginning, a specific advantage of the process is that the sulphur compounds are hydrogenated over the catalysts to be used according to the invention, so that the reaction is possible at significantly more moderate conditions and effects the complete conversion of the carbon sulphides, without any signs of methanation. The reaction temperature ranges between 200 and 280 and with regard to an adequate reaction velocity preferably between 240 and 260 °C. The reactor may be heated from the outside - which results in a higher energy consumption - or the reaction components may be heated before introducing them into the reactor, with the mixing being possibly done in a nozzle which works, for example, by the Venturi principle.
- Furthermore, the reaction may take place in the range of 1 to 15 bar, i.e. at atmospheric pressure or under pressure. Preference is given to an embodiment which uses a pressure in the range of approx. 5 to approx. 10 bar, as this is of benefit to yield and reaction velocity.
- The term 'sulphidic cobalt molybdenum catalysts' mainly refers to catalysts which contain molybdenum sulphide as the actual catalyst and cobalt as the promoter. Catalysts of that kind are produced in known manner by joint sulphidation of the respective oxides, where the MoO3 is converted completely to MoS2. When the latter is applied to the aluminium oxide carrier, it is either bonded flat to the surface ('basal bonding') or to one edge only ('edge bonding'). After sulphidation the cobalt is available in three forms: first as Co9S8 crystals deposited on the carrier, as Co2+ ions on the edges of the MoS2 plates ('CoMo phase') and as Co2+ ions on the tetrahedral positions in the aluminium oxide lattice. The catalysts are hence composed predominantly, i.e. of more than 50 %-mole, preferably of more than 70 %-mole and most preferably of more than 90 %-mole, of molybdenum sulphide and contain the cobalt in sulphidic form as a promoter, the quantity in %-mole resulting as the difference to 100. From this it follows that in a likewise preferred embodiment the catalysts do not contain any other metals, especially no other transition metals.
- Aluminium oxides of especially high specific surface area come into consideration as suitable carriers for the sulphidic cobalt molybdenum catalysts, the aluminium oxides preferably featuring the following characteristics:
- minimum V37A of 75 ml/100g, preferably 80 ml/100g and most preferably 85 ml/100g;
- maximum V0.1µm of 31 ml/100g, preferably 25 ml/100g and most preferably 15 ml/100gM;
- maximum V0.2µm of 20 ml/100g, preferably 15 ml/100g and most preferably 10 ml/100g; and
- ratio of V0.1µm to V0.2µm of at least 1.5.
- Aluminium oxide carriers of the type mentioned are sufficiently known from the state of the art. European patent documents
EP 1385786 B1 andEP 1385787 B1 (Axens ), for example, describe a process for their manufacture, in which a hydrargillite-type aluminium oxide is ground, undergoes hydrothermal treatment with an aqueous solution of aluminium nitrate and formic acid at 200 °C for 6 hours, the resulting product then being calcined at 400 to 1300. The carrier material is then extruded and is thus ready for loading. As far as the nature and manufacture of the catalyst carriers is concerned, the two documents mentioned are related to by reference. - The hydrogenation products leaving the reactor, particularly the fixed-bed reactor, now contain the sulphur compounds in the form of hydrogen sulphide, the content being typically within the range of 50 to 300 ppm. The presence of H2S is just as little desirable as that of the carbon sulphides but, in contrast to the latter, hydrogen sulphide can be washed out comparatively easily and, above all, quantitatively. The hydrogenation gases are, for this purpose, preferably passed through an absorption column, where they are treated, for example, in counter current with an aqueous base such as caustic soda or ammonia. Alternatively, other devices may be used for the purification of gases as, for example, venturi scrubbers.
- When the H2S portions have been separated, the purified product is available without restriction as a high-quality synthesis gas for further chemical reactions.
- A further subject matter of the present invention is the use of sulphidic cobalt molybdenum catalysts provided on aluminum oxide carriers for the hydrogenation of carbon sulphides to hydrogen sulphide,
wherein sulphidic cobalt molybdenum catalysts are used which contain molybdenum sulphide as the actual catalyst and cobalt as the promoter,
wherein said catalysts are composed of more than 50 %-mole of molybdenum sulphide
and said catalysts contain the cobalt in sulphidic form, the quantity in %-mole of said cobalt in sulphidic form resulting as the difference to 100,
wherein molybdenum sulphide has been obtained by sulphidation of the respective oxide, wherein the MoO3 has been converted completely to MoS2,
wherein after sulphidation the cobalt is present in three forms: first as Co9S8 crystals deposited on the carrier, as Co2+ ions on the edges of the MoS2 plates ('CoMo phase') and as Co2+ ions on the tetrahedral positions in the aluminum oxide lattice. - Also preferred as carriers for the cobalt molybdenum catalysts are aluminium oxides that feature a high specific area surface and at the same time feature the following characteristics:
- (i) minimum V37A of 75 ml/100g, preferably 80 ml/100g and most preferably 85 ml/100g;
- (ii) maximum V0.1µm of 31 ml/100g, preferably 25 ml/100g and most preferably 15 ml/100gM;
- (iii) maximum V0.2µm of 20 ml/100g, preferably 15 ml/100g and most preferably 10 ml/100g; and
- (iv) ratio of V0.1µm to V0.2µm of at least 1.5.
- The present invention also encompasses a method for preparing hydrogen sulphide, wherein carbon sulphides are subjected to hydrogenation in the presence of a working amount of sulphidic cobalt molybdenum catalysts provided on aluminium oxide carriers.
- The carbon sulphides are subjected to hydrogenation in the presence of cobalt molybdenum catalysts which, with reference to the metal components, predominantly consist of molybdenum sulphide and contain cobalt sulphide as a promoter only. Also preferred are aluminium oxide carriers meeting the following characteristics:
- (i) minimum V37A of at least 75 ml/100g, preferably 80 ml/100g and most preferably 85 ml/100g;
- (ii) maximum V0.1µm of 31 ml/100g, preferably 25 ml/100g and most preferably 15 ml/100gM;
- (iii) maximum V0.2µm of 20 ml/100g, preferably 15 ml/100g and most preferably 10 ml/100g; and
- (iv) ratio of V0.1µm to V0.2µm of at least 1.5.
- A pilot plant for fixed-bed hydrogenation was equipped with a bulk layer of commercially available lumpy sulphidic cobalt molybdenum catalyst on an aluminium oxide carrier. Subsequently, different coking gases were introduced at the bottom of the column. The only difference between these so-called feed gases was the amount of carbon sulphides, in particular carbon disulphide. The hydrogenation was performed at a temperature of 220 °C and a pressure of 10 bar. The GHSV was about 1200 l/h.
- The product gas was analysed for sulphur in the gas chromatograph and the fractions of hydrogen sulphide and carbon sulphides were determined by means of the retention periods. Table 1 sums up the results. The conversion rates refer to the hydrogenation of the CS2 fraction.
Table 1 Hydrogenation results (weight specified in %-vol. unless otherwise indicated) 1 2 3 4 Feed Prod. Feed Prod. Feed Prod. Feed Prod. Hydrogen 59.0 59.0 59.0 59.0 59.0 59.0 59.0 59.0 Methane 27.0 27.0 27.0 27.0 27.0 27.0 27.0 27.0 Nitrogen 5.0 5.0 5.0 5.0 5.0 5.0 5.0 5.0 Carbon monoxide 6.5 6.5 6.5 6.5 6.5 6.5 6.5 6.5 Carbon dioxide 2.5 2.5 2.5 2.5 2.5 2.5 2.5 2.5 COS (ppm) 1 10 0 0 0 0 0 10 CS2 (ppm) 117 0 94 0 95 0 54 0 H2S (ppm) 1 211 0 141 0 182 0 141 Conversion rate 95.5 100 100 93.4 - The test results show that the fraction of carbon sulphides is converted to at least 95% hydrogen sulphide. At the same time the proportion of the other constituents in the coke oven gas remained constant, i.e. no methanation was observed.
wherein said catalysts are composed of more than 50 %-mole of molybdenum sulphide and said catalysts contain the cobalt in sulphidic form, the quantity in %-mole of said cobalt in sulphidic form resulting as the difference to 100,
wherein molybdenum sulphide has been obtained by sulphidation of the respective oxide, wherein the MoO3 has been converted completely to MoS2,
wherein after sulphidation the cobalt is present in three forms: first as Co9S8 crystals deposited on the carrier, as Co2+ ions on the edges of the MoS2 plates ('CoMo phase') and as Co2+ ions on the tetrahedral positions in the aluminum oxide lattice.
Claims (12)
- A process for the production of synthesis gas from hard coal, wherein(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 to 280 °C over a sulphidic cobalt molybdenum catalyst provided on an aluminum oxide carrier material, and(c) the hydrogen sulphide obtained from hydrogenation is separated from the gas mixture,wherein sulphidic cobalt molybdenum catalysts are used which contain molybdenum sulphide as the actual catalyst and cobalt as the promoter,
wherein said catalysts are composed of more than 50 %-mole of molybdenum sulphide and said catalysts contain the cobalt in sulphidic form, the quantity in %-mole of said cobalt in sulphidic form resulting as the difference to 100,
wherein molybdenum sulphide has been obtained by sulphidation of the respective oxide, wherein the MoO3 has been converted completely to MoS2,
wherein after sulphidation the cobalt is present in three forms: first as Co9S8 crystals deposited on the carrier, as Co2+ ions on the edges of the MoS2 plates ('CoMo phase') and as Co2+ ions on the tetrahedral positions in the aluminum oxide lattice. - The process of claim 1, wherein said catalysts are composed of more than 70 %-mole of molybdenum sulphide.
- The process of claim 2, wherein said catalysts are composed of more than 90 %-mole of molybdenum sulphide.
- The process of claim 1 wherein synthesis gases of a content of 10 to 200 ppm carbon sulphides are used.
- The process of Claim 1, wherein hydrogenation is carried out in a temperature range between 240 and 260 °C.
- The process of Claim 1, wherein hydrogenation is carried out at a pressure of 1 to 15 bar.
- The process of Claim 6, wherein hydrogenation is carried out at a pressure of 5 to 10 bar.
- The process of Claim 1, wherein that hydrogenation is carried out at a GHSV of 500 to 1500 l/h.
- The process according to at least one of claims 1 to 8, characterized in that hydrogenation is carried out in a fixed-bed reactor.
- The process of Claim 9, wherein the catalysts used in the fixed-bed reactor are provided as bulk layer or packing.
- The process of Claim 1, wherein the hydrogenation product, after leaving the reactor, is passed through an absorption column, where the hydrogen sulphide is washed out with a basic liquid.
- Use of sulphidic cobalt molybdenum catalysts provided on aluminum oxide carriers for the hydrogenation of carbon sulphides to hydrogen sulphide,
wherein sulphidic cobalt molybdenum catalysts are used which contain molybdenum sulphide as the actual catalyst and cobalt as the promoter,
wherein said catalysts are composed of more than 50 %-mole of molybdenum sulphide and said catalysts contain the cobalt in sulphidic form, the quantity in %-mole of said cobalt in sulphidic form resulting as the difference to 100,
wherein molybdenum sulphide has been obtained by sulphidation of the respective oxide, wherein the MoO3 has been converted completely to MoS2,
wherein after sulphidation the cobalt is present in three forms: first as Co9S8 crystals deposited on the carrier, as Co2+ ions on the edges of the MoS2 plates ('CoMo phase') and as Co2+ ions on the tetrahedral positions in the aluminum oxide lattice.
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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 |
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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 |
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 |
NL7013902A (en) * | 1970-09-21 | 1972-03-23 | ||
BE788068A (en) * | 1971-09-01 | 1973-02-28 | Shell Int Research | ERBINDINGEN UIT HET RUWE GAS VERKREGEN DOOR PARTIELE VERBRANDING VAN EEN KOOLSTOFHOUDENDE BRANDSTOF WERKWIJZE VOOR HET VERWIJDEREN VAN ROET EN ZWAVELV |
DE2551717C3 (en) * | 1975-11-18 | 1980-11-13 | Basf Ag, 6700 Ludwigshafen | and possibly COS from gases |
US4041130A (en) * | 1975-12-29 | 1977-08-09 | The Ralph M. Parsons Company | Process for desulfurization of coke oven 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 |
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 |
US4863489A (en) * | 1989-02-03 | 1989-09-05 | Texaco Inc. | Production of demercurized synthesis gas, reducing gas, or fuel gas |
NL9102195A (en) * | 1991-12-30 | 1993-07-16 | Veg Gasinstituut Nv | METHOD FOR TREATING GASES OBTAINED BY COAL GASIFICATION, RESIDUAL GASIFICATION, WASTE GASIFICATION OR OIL GASIFICATION |
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 |
EP1628744B1 (en) * | 2003-05-29 | 2008-07-09 | Shell Internationale Researchmaatschappij B.V. | 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 |
US8518356B2 (en) * | 2010-07-27 | 2013-08-27 | Air Products And Chemicals, Inc. | Method and apparatus for adjustably treating a sour gas |
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