WO2011122331A1 - フィッシャー・トロプシュ合成反応用活性化触媒の製造方法、触媒スラリーの製造方法、並びに触媒スラリーのフィッシャー・トロプッシュ合成反応器への供給方法 - Google Patents
フィッシャー・トロプシュ合成反応用活性化触媒の製造方法、触媒スラリーの製造方法、並びに触媒スラリーのフィッシャー・トロプッシュ合成反応器への供給方法 Download PDFInfo
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- WO2011122331A1 WO2011122331A1 PCT/JP2011/056068 JP2011056068W WO2011122331A1 WO 2011122331 A1 WO2011122331 A1 WO 2011122331A1 JP 2011056068 W JP2011056068 W JP 2011056068W WO 2011122331 A1 WO2011122331 A1 WO 2011122331A1
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- Prior art keywords
- fischer
- catalyst
- reactor
- tropsch synthesis
- synthesis
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- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 216
- 239000003054 catalyst Substances 0.000 title claims abstract description 171
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 134
- 238000002360 preparation method Methods 0.000 title claims abstract description 7
- 239000002002 slurry Substances 0.000 title claims description 84
- 238000000034 method Methods 0.000 title claims description 36
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 78
- 239000007789 gas Substances 0.000 claims abstract description 64
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 59
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 42
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 39
- 229910052751 metal Inorganic materials 0.000 claims abstract description 36
- 239000002184 metal Substances 0.000 claims abstract description 34
- 230000009467 reduction Effects 0.000 claims abstract description 21
- 239000007788 liquid Substances 0.000 claims description 84
- 238000004519 manufacturing process Methods 0.000 claims description 42
- 230000004913 activation Effects 0.000 claims description 11
- 230000008569 process Effects 0.000 claims description 11
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 238000005984 hydrogenation reaction Methods 0.000 claims description 7
- 230000003213 activating effect Effects 0.000 claims description 4
- 239000007809 chemical reaction catalyst Substances 0.000 claims description 2
- 239000007858 starting material Substances 0.000 abstract 2
- 239000001993 wax Substances 0.000 description 46
- 238000004517 catalytic hydrocracking Methods 0.000 description 44
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 22
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 14
- 239000000446 fuel Substances 0.000 description 14
- 239000003345 natural gas Substances 0.000 description 11
- 238000006477 desulfuration reaction Methods 0.000 description 10
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- 229910002091 carbon monoxide Inorganic materials 0.000 description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 238000001994 activation Methods 0.000 description 8
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- 239000001257 hydrogen Substances 0.000 description 8
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- 239000003921 oil Substances 0.000 description 8
- 239000000047 product Substances 0.000 description 7
- 239000000377 silicon dioxide Substances 0.000 description 7
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 6
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- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 6
- 230000003197 catalytic effect Effects 0.000 description 6
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- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 229910017052 cobalt Inorganic materials 0.000 description 4
- 239000010941 cobalt Substances 0.000 description 4
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 4
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 3
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 description 3
- 238000004220 aggregation Methods 0.000 description 3
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- 238000007599 discharging Methods 0.000 description 3
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- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 3
- 238000011068 loading method Methods 0.000 description 3
- 229910044991 metal oxide Inorganic materials 0.000 description 3
- 150000004706 metal oxides Chemical class 0.000 description 3
- 229910052707 ruthenium Inorganic materials 0.000 description 3
- -1 silica alumina Chemical class 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
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- 150000003464 sulfur compounds Chemical class 0.000 description 3
- 230000002194 synthesizing effect Effects 0.000 description 3
- WFDIJRYMOXRFFG-UHFFFAOYSA-N Acetic anhydride Chemical compound CC(=O)OC(C)=O WFDIJRYMOXRFFG-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 229910021536 Zeolite Inorganic materials 0.000 description 2
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 150000001298 alcohols Chemical class 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000001354 calcination Methods 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 238000006114 decarboxylation reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 description 2
- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 230000002779 inactivation Effects 0.000 description 2
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- 229910052742 iron Inorganic materials 0.000 description 2
- 239000003350 kerosene Substances 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
- 239000000203 mixture Substances 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052763 palladium Inorganic materials 0.000 description 2
- 230000000737 periodic effect Effects 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 239000003381 stabilizer Substances 0.000 description 2
- 239000010457 zeolite Substances 0.000 description 2
- 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
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- QCWXUUIWCKQGHC-UHFFFAOYSA-N Zirconium Chemical compound [Zr] QCWXUUIWCKQGHC-UHFFFAOYSA-N 0.000 description 1
- 235000011054 acetic acid Nutrition 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
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- 230000000903 blocking effect Effects 0.000 description 1
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- 229910052799 carbon Inorganic materials 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 230000008859 change Effects 0.000 description 1
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- 238000011109 contamination Methods 0.000 description 1
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- 235000019253 formic acid Nutrition 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 229910052735 hafnium Inorganic materials 0.000 description 1
- VBJZVLUMGGDVMO-UHFFFAOYSA-N hafnium atom Chemical compound [Hf] VBJZVLUMGGDVMO-UHFFFAOYSA-N 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 150000003840 hydrochlorides Chemical class 0.000 description 1
- 230000001771 impaired effect Effects 0.000 description 1
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- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 229910052809 inorganic oxide Inorganic materials 0.000 description 1
- 229940057995 liquid paraffin Drugs 0.000 description 1
- 229910052744 lithium Inorganic materials 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 150000002823 nitrates Chemical class 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 235000005985 organic acids Nutrition 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 235000019260 propionic acid Nutrition 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- IUVKMZGDUIUOCP-BTNSXGMBSA-N quinbolone Chemical compound O([C@H]1CC[C@H]2[C@H]3[C@@H]([C@]4(C=CC(=O)C=C4CC3)C)CC[C@@]21C)C1=CCCC1 IUVKMZGDUIUOCP-BTNSXGMBSA-N 0.000 description 1
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- 238000000926 separation method Methods 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 150000003467 sulfuric acid derivatives Chemical class 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
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- 239000011787 zinc oxide Substances 0.000 description 1
- 229910052726 zirconium Inorganic materials 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/16—Reducing
- B01J37/18—Reducing with gases containing free hydrogen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
- C10G2/34—Apparatus, reactors
- C10G2/342—Apparatus, reactors with moving solid catalysts
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
- B01J23/46—Ruthenium, rhodium, osmium or iridium
- B01J23/462—Ruthenium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/74—Iron group metals
- B01J23/75—Cobalt
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
- B01J23/8913—Cobalt and noble metals
-
- B01J35/40—
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/0201—Impregnation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
- C10G2300/703—Activation
Definitions
- the present invention relates to a production method for producing an activated catalyst used in a Fischer-Tropsch synthesis reaction, a production method for producing a catalyst slurry containing the activated catalyst, and a catalyst slurry produced by the method.
- the present invention relates to a supply method to a Fischer-Tropsch synthesis reactor.
- synthesis gas mainly composed of carbon monoxide gas (CO) and hydrogen gas (H 2 )
- CO carbon monoxide gas
- H 2 hydrogen gas
- FT synthesis reaction Fischer-Tropsch synthesis reaction
- a synthesis reaction system for synthesizing a hydrocarbon compound by an FT synthesis reaction for example, a bubble column type slurry bed in which a synthesis gas is blown into a slurry in which solid catalyst particles are suspended in a liquid hydrocarbon and the FT synthesis reaction is performed.
- Patent Document 1 An FT reaction system is disclosed (Patent Document 1).
- the catalyst in the form of a catalyst slurry in which the catalyst is suspended in liquid hydrocarbon, and the slurry is brought into contact with the synthesis gas as the raw material
- the method usually, at the start-up time of the FT synthesis reactor, the catalyst is suspended in a liquid hydrocarbon to prepare a catalyst slurry and introduced into the reactor.
- GTL Gas To To Liquids
- hydrodesulfurization reactors for removing sulfur compounds in natural gas hydrocarbon compounds synthesized by FT synthesis reaction are hydrotreated Reactors for handling heated hydrogen gas and hydrocarbon compounds, such as reactors for the
- a catalyst used in the FT synthesis reaction a catalyst in which an active metal such as cobalt, iron, nickel or ruthenium is supported on a carrier such as an inorganic oxide is known.
- these catalysts are prepared by calcination after an active metal component is supported on a carrier, and further subjected to a reduction treatment with a reducing agent such as hydrogen gas to be activated for the FT synthesis reaction. Is done.
- the reduction treatment is often performed in equipment at a location different from the FT synthesis reaction equipment, for example, equipment at a catalyst production site.
- the activated catalyst is exposed to the atmosphere in the process of extracting the catalyst activated by the reduction treatment from the facility for performing the reduction treatment, transferring it to the FT synthesis reaction facility, and putting it into the FT synthesis reaction facility. Inactivation occurs.
- the surface of the activated catalyst is coated with a medium such as wax in a non-contact manner with the atmosphere, and simultaneously molded into a flake shape to prevent contact with the atmosphere.
- a method of handling such as transfer after stabilization for blocking (Patent Document 2).
- the present invention has been made in view of the above circumstances, and in a liquid fuel production system for implementing a GTL technology including a synthesis device that synthesizes a hydrocarbon compound by an FT synthesis reaction, a catalyst for an FT synthesis reaction is provided.
- An object of the present invention is to provide a method for producing an activated catalyst for an FT synthesis reaction by a simplified process which does not require special equipment for reduction treatment, a stabilization process by coating treatment, and equipment for the same. To do.
- a method for producing a catalyst slurry in which the activated catalyst is prevented from being deactivated without being subjected to a stabilization treatment and suspended in liquid hydrocarbon to form a slurry, and FT synthesis using the catalyst slurry It aims at providing the method of supplying this catalyst slurry to a reactor.
- the method for producing an activation catalyst for Fischer-Tropsch synthesis reaction of the present invention includes a step of reducing a Fischer-Tropsch synthesis reaction catalyst obtained by supporting an active metal on an inorganic carrier with a gas containing hydrogen gas.
- the reduction treatment is synthesized by a reactor that performs hydrodesulfurization of a hydrocarbon feedstock to produce synthesis gas that is a Fischer-Tropsch synthesis reaction feedstock, a reactor that performs a Fischer-Tropsch synthesis reaction, and a Fischer-Tropsch synthesis reaction. It is carried out in any of the reactors that carry out the hydroprocessing of the synthetic oil.
- the activation catalyst for Fischer-Tropsch synthesis reaction may be used in a slurry bed reactor.
- the activated catalyst is mixed with a liquid hydrocarbon to form a slurry, which can be easily added to a reactor for performing a Fischer-Tropsch synthesis reaction.
- the Fischer-Tropsch synthesis reaction can be carried out as it is.
- Fischer-Tropsch synthesis catalyst comprising Fischer-Tropsch synthesis reaction with active metal supported on an inorganic carrier, hydrodesulfurization of hydrocarbon feedstock to produce synthesis gas as Fischer-Tropsch synthesis reaction feedstock, Fischer-Tropsch synthesis
- An activation step of activating with a gas containing hydrogen gas in any one of a reactor for performing a reaction and a reactor for hydrotreating a synthetic oil synthesized by a Fischer-Tropsch synthesis reaction And a catalyst slurry preparation step of preparing a slurry by supplying a liquid hydrocarbon to any of the reactors in which the activated catalyst is accommodated.
- the method of supplying the catalyst slurry of the present invention to the Fischer-Tropsch synthesis reactor is as follows: Fischer-Tropsch synthesis catalyst comprising Fischer-Tropsch synthesis reaction with active metal supported on an inorganic carrier, hydrodesulfurization of hydrocarbon feedstock to produce synthesis gas as Fischer-Tropsch synthesis reaction feedstock, Fischer-Tropsch synthesis An activation step of activating with a gas containing hydrogen gas in any one of the reactors for performing a hydrogenation treatment of synthetic oil synthesized by the reaction; A catalyst slurry preparation step of preparing a slurry by supplying a liquid hydrocarbon to any of the reactors filled with the activated catalyst; And a transfer step of transferring the catalyst slurry to a reactor for performing a Fischer-Tropsch synthesis reaction via a pipe.
- the method for producing an activated catalyst for Fischer-Tropsch synthesis reaction of the present invention in a hydrocarbon production system utilizing FT synthesis reaction, special equipment for catalyst reduction treatment, activated catalyst coating treatment
- the activation process for the Fischer-Tropsch synthesis reaction is manufactured by a simplified process without the need for a stabilization process and a dedicated facility for the process.
- the method for producing the catalyst slurry for the Fischer-Tropsch synthesis reaction and the method for supplying the catalyst slurry to the Fischer-Tropsch synthesis reactor of the present invention no special equipment is required, and the activated catalyst is brought into contact with the atmosphere.
- the catalyst slurry can be easily produced while preventing inactivation, and the catalyst slurry can be easily introduced into the FT synthesis reactor.
- FIG. 1 is a schematic diagram showing an overall configuration of a liquid fuel synthesis system including a natural gas desulfurization apparatus, an FT synthesis reactor, and a hydrocarbon compound hydrotreating reactor according to an embodiment of the present invention. It is a schematic diagram which shows the processing unit used in one embodiment of the manufacturing method of the activation catalyst for Fischer-Tropsch synthesis reaction of this invention.
- FT synthesis reactor in which an activated catalyst for Fischer-Tropsch synthesis reaction (hereinafter also referred to as “activated FT synthesis catalyst”) manufactured according to the present invention is used. ”
- a natural gas desulfurization apparatus used for the production of this activated FT synthesis catalyst and the production of a catalyst slurry for the Fischer-Tropsch synthesis reaction hereinafter also referred to as“ catalyst slurry ”.
- catalyst slurry An example of a liquid fuel synthesis system based on GTL technology including a reactor and a hydrocarbon compound hydrotreating reactor will be described.
- FIG. 1 shows an example of a liquid fuel synthesis system.
- the liquid fuel synthesis system 1 includes a synthesis gas production unit 3, an FT synthesis unit 5, and an upgrading unit 7.
- the synthesis gas production unit 3 the natural gas which is a hydrocarbon raw material is reformed to produce synthesis gas containing carbon monoxide gas and hydrogen gas.
- the FT synthesis unit 5 a hydrocarbon compound is synthesized from the synthesis gas produced by the synthesis gas production unit 3 by an FT synthesis reaction.
- the hydrocarbon compound synthesized in the FT synthesis unit is hydrotreated and fractionated to produce liquid fuel products (naphtha, kerosene, light oil, wax, etc.).
- the synthesis gas production unit 3 mainly includes a desulfurization device 10, a reformer 12, an exhaust heat boiler 14, gas-liquid separators 16 and 18, a decarbonation device 20, and a hydrogen separation device 26.
- the desulfurization apparatus 10 includes a hydrodesulfurization reactor and the like, and removes sulfur compounds from natural gas as a raw material.
- the hydrodesulfurization reactor is filled with a known hydrodesulfurization catalyst, and a sulfur compound contained in natural gas is hydrogenated and converted into hydrogen sulfide in the presence of hydrogen gas.
- An adsorptive desulfurization apparatus filled with a desulfurization material that adsorbs hydrogen sulfide such as zinc oxide is provided at the subsequent stage of the hydrodesulfurization reactor, and hydrogen sulfide in natural gas is removed.
- the hydrodesulfurization reactor is a preferred example of the “reactor that performs hydrodesulfurization of a hydrocarbon raw material for producing synthesis gas that is a Fischer-Tropsch synthesis reaction raw material” according to the present invention.
- the natural gas supplied from the desulfurization apparatus 10 is reformed to produce a synthesis gas containing carbon monoxide gas (CO) and hydrogen gas (H 2 ) as main components.
- CO carbon monoxide gas
- H 2 hydrogen gas
- the exhaust heat boiler 14 the exhaust heat of the high-temperature synthesis gas produced by the reformer 12 is recovered, and high-pressure steam is obtained.
- the water heated by the heat exchange with the high-temperature synthesis gas in the exhaust heat boiler 14 is separated into gas (high-pressure steam) and liquid water.
- the condensed component is removed from the synthesis gas cooled by the exhaust heat boiler 14, and the gaseous component is supplied to the decarboxylation device 20.
- the decarboxylation device 20 uses an absorption liquid from the synthesis gas supplied from the gas-liquid separator 18 to remove the carbon dioxide gas, and regenerates the carbon dioxide gas from the absorption liquid containing the carbon dioxide gas for regeneration.
- Tower 24 uses an absorption liquid from the synthesis gas supplied from the gas-liquid separator 18 to remove the carbon dioxide gas, and regenerates the carbon dioxide gas from the absorption liquid containing the carbon dioxide gas for regeneration.
- Tower 24 uses an absorption liquid from the synthesis gas supplied from the gas-liquid separator 18 to remove the carbon dioxide gas, and regenerates the carbon dioxide gas from the absorption liquid containing the carbon dioxide gas for regeneration.
- the hydrogen separator 26 a part of the hydrogen gas contained in the synthesis gas is separated from the synthesis gas from which the carbon dioxide gas has been separated by the decarbonation device 20.
- the FT synthesis unit 5 mainly includes a bubble column type FT synthesis reactor 30, a gas-liquid separator 34, a separator 36, a gas-liquid separator 38, and a first rectifying tower 40.
- the FT synthesis reactor 30 is a reactor that synthesizes a hydrocarbon compound from synthesis gas by an FT synthesis reaction, and mainly includes a reactor main body 80 and a cooling pipe 81.
- the reactor body 80 is a substantially cylindrical metal container in which particles of solid activated FT synthesis catalyst are suspended in liquid hydrocarbon (product of FT synthesis reaction).
- a catalyst slurry is contained.
- a synthesis gas mainly composed of hydrogen gas and carbon monoxide gas is injected into the catalyst slurry.
- the synthesis gas blown into the catalyst slurry becomes bubbles and rises in the catalyst slurry from the lower side in the vertical direction of the reactor main body 80 toward the upper side.
- the synthesis gas dissolves in the liquid hydrocarbon and comes into contact with the catalyst particles to proceed with the synthesis of the hydrocarbon compound (FT synthesis reaction). Further, as the synthesis gas rises in the reactor main body 80 as bubbles, an upward flow (air lift) of the catalyst slurry is generated inside the reactor main body 80. Thereby, a circulating flow of the catalyst slurry is generated inside the reactor main body 80. The unreacted synthesis gas rising to the top of the reactor main body 80 is discharged from the top of the reactor main body 80 and supplied to the gas-liquid separator 38.
- This FT synthesis reactor 30 is, of course, a “reactor that performs a Fischer-Tropsch synthesis reaction” according to the present invention.
- water heated through the cooling pipe 81 disposed in the FT synthesis reactor 30 is separated into water vapor (medium pressure steam) and liquid water.
- the separator 36 is connected to the center of the FT synthesis reactor 30 and separates catalyst particles and liquid hydrocarbon products from the catalyst slurry.
- the gas-liquid separator 38 is connected to the FT synthesis reactor 30, and cools the gaseous light hydrocarbons produced by the unreacted synthesis gas and the FT synthesis reaction under the conditions in the reactor main body 80, and is a liquid hydrocarbon. to the gas-liquid separating a gas component containing component and unreacted synthesis gas and C 4 less gaseous hydrocarbon.
- the liquid hydrocarbons supplied from the FT synthesis reactor 30 via the separator 36, and the liquid hydrocarbons supplied from the FT synthesis reactor 30 via the gas-liquid separator 38, Is fractionated into each fraction according to the boiling point.
- the upgrading unit 7 includes a wax fraction hydrocracking reactor 50, a middle fraction hydrotreating reactor 52, a naphtha fraction hydrotreating reactor 54, gas-liquid separators 56, 58 and 60, and a second rectification.
- a tower 70 and a naphtha stabilizer 72 are mainly provided.
- the wax fraction hydrocracking reactor 50 is connected to the bottom of the first fractionator 40.
- the middle distillate hydrotreating reactor 52 is connected to the center of the first rectifying column 40.
- the naphtha fraction hydrotreating reactor 54 is connected to the top of the first fractionator 40.
- Gas-liquid separators 56, 58, and 60 are provided corresponding to the reactors 50, 52, and 54, respectively.
- the second rectification column 70 the liquid hydrocarbons supplied from the gas-liquid separators 56 and 58 are fractionated according to the boiling point.
- the naphtha stabilizer 72 the liquid hydrocarbon compound contained in the naphtha fraction supplied from the gas-liquid separator 60 and the second rectifying column 70 is fractionated, and the light hydrocarbon compound of C 4 or less is flare gas. Hydrocarbon compounds having 5 or more carbon atoms are separated and recovered as naphtha of products.
- the wax fraction hydrocracking reactor 50 is a reactor for mainly hydrocracking (reducing molecular weight) the wax fraction supplied from the bottom of the first rectifying tower 40 in the presence of hydrogen gas. It is. Generally, the reactor is packed with a known hydrocracking catalyst in which a metal having hydrogenation activity is supported on a support containing a solid acid as a fixed bed. Specific examples of hydrocracking catalysts include platinum and / or palladium on a support containing a zeolite represented by USY zeolite and a composite metal oxide such as silica alumina, silica zirconia, and alumina boria. And those carrying metals belonging to Groups 8 to 10 of the periodic table.
- the middle distillate hydrotreating reactor 52 is mainly a hydrotreating of the middle distillate supplied from the central portion of the first rectifying column 40 in the presence of hydrogen gas (FT synthesis reaction by-product).
- This is a reactor for removal of oxygen-containing compounds such as olefins and alcohols) and hydroisomerization (conversion of normal paraffin, which is a main component of middle distillate, to isoparaffin).
- the reactor is packed with a known hydrorefining catalyst in which a metal having hydrogenation activity is supported on a support containing a solid acid.
- hydrorefining catalyst examples include a carrier containing a composite metal oxide such as silica alumina, silica zirconia, and alumina boria, and belongs to Groups 8 to 10 of the periodic table represented by platinum and / or palladium. The thing with which the metal was carry
- a composite metal oxide such as silica alumina, silica zirconia, and alumina boria
- the naphtha fraction hydrorefining reactor 54 is a hydrorefining (by-product of FT synthesis reaction) mainly obtained by hydrotreating the naphtha fraction supplied from the top of the first rectifying column 40 in the presence of hydrogen gas. (Removal of oxygen-containing compounds such as olefins and alcohols).
- the reactor is packed with a known hydrorefining catalyst in which a metal having a hydrogenation activity is supported on a support containing or not containing a solid acid.
- Specific examples of the hydrotreating catalyst include the same catalysts as those used in the middle distillate hydrotreating reactor 52.
- the “reactor that performs hydrotreating” refers to a reactor that purifies a hydrocarbon compound using hydrogen gas such as hydrocracking, hydrorefining, and hydroisomerization.
- the wax fraction hydrocracking reactor 50, the middle fraction hydrotreating reactor 52, and the naphtha fraction hydrotreating reactor 54 are the “synthetic oil synthesized by the Fischer-Tropsch synthesis reaction” according to the present invention. This is a preferred example of a “reactor that performs hydrotreatment”.
- the hydrodesulfurization reactor constituting the natural gas desulfurization apparatus 10 and the respective reactors for performing the hydrogenation treatment are usually filled with respective catalysts, and the respective reactions are performed. However, when the liquid fuel synthesizing system 1 stops operating and the catalyst filled in each reactor is extracted, for example, by exchanging the catalyst, any one of these reactors is treated as the method of the present invention. It becomes possible to use it.
- FIG. 2 the processing unit used for manufacture of the activated FT synthesis catalyst and manufacture of a catalyst slurry in the manufacturing method of the activated FT synthesis catalyst of the present embodiment will be described. The details will be described along with an example of using the wax fraction hydrocracking reactor 50 constituting the liquid fuel synthesis system 1 as the processing unit 100.
- the wax fraction hydrocracking reactor 50 is originally used as a reactor for hydrocracking the wax fraction, but it supplies heated hydrogen and liquid hydrocarbons. -Since it is possible to discharge the reactor, the operation of the reactor is stopped, and the charged hydrocracking catalyst is withdrawn. It can be preferably used as a processing apparatus.
- the treatment unit 100 includes a wax fraction hydrocracking reactor 50, a supply pipe 151 connected to the wax fraction hydrocracking reactor 50, and a heater 152 attached to the supply pipe 151.
- a mesh shelf 50a for loading a catalyst is installed inside the wax fraction hydrocracking reactor 50.
- the mesh shelf 50a has a mesh size that prevents the catalyst particles from passing therethrough.
- the side of the wax fraction hydrocracking reactor 50 is filled with a catalyst used for the FT synthesis reaction before the activation treatment (hereinafter also simply referred to as “FT synthesis catalyst”).
- a nozzle 50b is provided.
- the supply pipe 151 is a pipe used for supplying hydrogen gas and liquid hydrocarbons to the wax fraction hydrocracking reactor 50.
- the supply pipe 151 is connected to the hydrogen introduction pipe 151a and the liquid hydrocarbon introduction pipe 151b.
- the heater 152 for example, a heat exchanger, a heating furnace, or the like can be used.
- the wax fraction hydrocracking reactor 50 is preferably connected to a discharge pipe 153 for discharging a catalyst slurry to be described later in detail at a position directly above the mesh shelf 50a.
- hydrogen gas is supplied from the hydrogen introduction pipe 151a to the supply pipe 151, the hydrogen gas is heated by the heater 152, and the heated hydrogen gas is supplied to the wax fraction hydrocracking reactor 50. It has come to be. Further, liquid hydrocarbon is supplied from the liquid hydrocarbon introduction pipe 151b to the supply pipe 151, and this liquid hydrocarbon is heated by the heater 152 as necessary and supplied to the wax fraction hydrocracking reactor 50. It has become.
- An activated FT synthesis catalyst is produced by reducing the FT synthesis catalyst with the heated hydrogen gas.
- a known supported FT synthesis catalyst in which an active metal is supported on an inorganic carrier is used.
- the inorganic carrier porous oxides such as silica, alumina, titania, magnesia, zirconia are used, silica or alumina is preferable, and silica is more preferable.
- the active metal include cobalt, ruthenium, iron, nickel and the like. Cobalt and / or ruthenium are preferable, and cobalt is more preferable.
- the amount of the active metal supported is preferably 3 to 50% by mass, more preferably 10 to 40% by mass based on the mass of the carrier.
- the FT synthesis catalyst may carry other components for the purpose of improving the activity, or for the purpose of controlling the carbon number and distribution of the generated hydrocarbon.
- examples of other components include compounds containing metal elements such as zirconium, titanium, hafnium, sodium, lithium, and magnesium.
- the average particle size of the FT synthesis catalyst is such that when the catalyst is subjected to an FT synthesis reaction in a slurry bed reactor, it will flow easily in the reactor as a slurry suspended in liquid hydrocarbons. It is preferably ⁇ 150 ⁇ m.
- the active metal is supported on the carrier by a known method.
- the compound containing an active metal element used for loading include salts of mineral acids such as nitrates, hydrochlorides and sulfates of the active metal elements, salts of organic acids such as formic acid, acetic acid and propionic acid, and acetylacetate.
- a complex compound such as a narate complex can be given.
- the supporting method is not particularly limited, but an impregnation method typified by the Incipient Wetness method using a solution of the compound containing the active metal element is preferably employed.
- the carrier on which the compound containing the active metal element is supported is dried by a known method, and more preferably fired by a known method in an air atmosphere.
- the firing temperature is not particularly limited, but is generally about 300 to 600 ° C.
- the compound containing the active metal element on the support is converted into a metal oxide.
- the FT synthesis catalyst used in the method for producing an activated FT synthesis catalyst of the present invention is preferably such that the active metal atom is in an oxide state.
- the wax fraction hydrocracking reactor 50 is passed through a nozzle 50b provided in the wax fraction hydrocracking reactor 50.
- Examples thereof include a method of loading an FT synthesis catalyst on a mesh shelf provided inside.
- the reduction process is a process in which the active metal in the FT synthesis catalyst is reduced by a reducing gas in the wax fraction hydrocracking reactor 50 and activated.
- the reducing gas include hydrogen gas, gas containing hydrogen gas such as a mixed gas of hydrogen gas and inert gas such as nitrogen gas, carbon monoxide gas, etc., preferably hydrogen containing gas. More preferably, hydrogen gas is used.
- the temperature in the reduction treatment is not particularly limited, but is generally preferably 200 to 550 ° C. When the reduction temperature is lower than 200 ° C., the active metal atoms are not sufficiently reduced and the catalytic activity tends not to be sufficiently exhibited.
- the pressure in the reduction treatment is not particularly limited, but is generally preferably 0.1 to 10 MPa. When the pressure is less than 0.1 MPa, the active metal atoms tend not to be sufficiently reduced and the catalytic activity tends not to be sufficiently developed. When the pressure exceeds 10 MPa, the equipment cost increases due to the need to increase the pressure resistance of the apparatus. There is a tendency.
- the time for the reduction treatment is not particularly limited, but is generally preferably 0.5 to 50 hours. When the reduction time is less than 0.5 hours, the active metal atoms are not sufficiently reduced and the catalytic activity tends not to be sufficiently exhibited.
- the active metal atoms are caused by aggregation of the active metal. Catalytic activity tends to decrease and efficiency tends to decrease.
- the flow of reducing gas such as hydrogen gas is stopped, and an activated FT synthesis catalyst is obtained.
- the activated FT synthesis catalyst produced by the method for producing an activated FT synthesis catalyst is cooled to a predetermined temperature as necessary. Then, in a state where the catalyst is accommodated in the wax fraction hydrocracking reactor 50, the wax fraction hydrocracking reaction is performed from the liquid hydrocarbon introduction pipe 151b via the supply pipe 151 without being brought into contact with the atmosphere.
- the vessel 50 is supplied with liquid hydrocarbons.
- the liquid hydrocarbon may be liquid as long as it is supplied to the wax fraction hydrocracking reactor 50. For example, even if it is solid or semi-solid at room temperature, it is heated to wax fraction hydrocracking. It may be introduced into the reactor 50 and may be in a liquid state here.
- Liquid hydrocarbons may be liquid paraffin, petroleum hydrocarbon solvents, etc., but they can be used without being procured from the outside, in view of being substantially free of sulfur and aromatic hydrocarbons. From the viewpoints of being a component present in the FT synthesis reaction system, liquid hydrocarbons produced by the FT synthesis reaction are preferred.
- the liquid hydrocarbon produced by the FT synthesis reaction may be an unfractionated / unrefined crude oil obtained from the FT synthesis reaction step, and a naphtha fraction obtained by fractionating the crude oil, an intermediate A fraction obtained by hydrorefining the naphtha fraction or middle fraction, or a product obtained by hydrocracking the wax fraction, and each fraction obtained by fractionating these fractions. Or a mixture of the above fractions.
- the liquid hydrocarbon supplied from the liquid hydrocarbon supply pipe 151b through the supply pipe 151 is heated by the heater 152 as necessary and supplied to the wax fraction hydrocracking reactor 50.
- the liquid hydrocarbon to be used contains a wax fraction or a wax fraction, it is preferable to heat in order to maintain fluidity.
- the temperature at the outlet of the liquid hydrocarbon heater 152 is preferably from room temperature to 300 ° C., more preferably from room temperature to 250 ° C., depending on the composition of the liquid hydrocarbon.
- the temperature is preferably 80 to 300 ° C.
- the normal temperature is a temperature of about 5 to 35 ° C.
- Liquid hydrocarbons are supplied to the wax fraction hydrocracking reactor 50 and mixed with the activated FT synthesis catalyst contained therein, thereby forming a catalyst slurry.
- the catalyst slurry produced by the above-described catalyst slurry production method contains an activated FT synthesis catalyst and a liquid hydrocarbon, and can be subjected to an FT synthesis reaction by a bubble column type slurry bed FT synthesis reactor. Note that the amount of liquid hydrocarbon supplied to the wax fraction hydrocracking reactor 50 depends on the concentration of the activated FT synthesis catalyst in the catalyst slurry at the initial stage of the FT synthesis reaction.
- the concentration of the activated FT synthesis catalyst in the catalyst slurry produced in the wax fraction hydrocracking reactor 50 is at least activated in the catalyst slurry used in the FT synthesis reaction at the initial stage of the FT synthesis reaction.
- the amount of liquid hydrocarbon to be supplied is adjusted so that the concentration of the FT synthesis catalyst is equal to or higher.
- the catalyst slurry produced by the method for producing catalyst slurry is transferred to the FT synthesis reactor 30.
- the catalyst slurry accommodated in the wax fraction hydrocracking reactor 50 may be once extracted to the outside and put into the FT synthesis reactor 30.
- the catalyst slurry may come into contact with the atmosphere, so that the activated FT synthesis catalyst may be deactivated, and when the catalyst slurry is heated, the fluidity is impaired due to a decrease in temperature. There is a fear. Therefore, it is preferable that the catalyst slurry is transferred directly to the FT synthesis reactor 30 through the piping without being extracted outside.
- the catalyst slurry is discharged from the wax fraction hydrocracking reactor 50 through the discharge pipe 153.
- the discharge pipe 153 is connected to the FT synthesis reactor 30 (not shown), a dedicated pipe for transferring the catalyst slurry is used to prevent contamination due to the catalyst remaining in the pipe after the catalyst slurry is transferred. It is preferable from the viewpoint.
- nitrogen gas is connected from a pipe 154 connected to the bottom of the wax fraction hydrocracking reactor 50 and normally used for discharging the spilled oil.
- An inert gas such as the above may be supplied to the wax fraction hydrocracking reactor 50.
- the catalyst slurry in the wax fraction hydrocracking reactor 50 is pumped, and at the same time, the catalyst slurry is mixed by gas bubbling, so that the catalyst slurry can be transferred in a more uniform state.
- the FT synthesis reactor 30 containing the catalyst slurry transferred from the wax fraction hydrocracking reactor 50, start-up work for starting the FT synthesis reaction is started.
- the catalyst slurry accommodated in the FT synthesis reactor 30 may be further mixed with liquid hydrocarbons for the purpose of adjusting the catalyst concentration, the slurry liquid level, and the like.
- the synthesis gas H 2 , CO
- a predetermined pressure for example, 1 to 5 MPaG
- the middle fraction hydrotreating reactor 52 and the naphtha fraction hydrotreating reactor 54 are also wax fraction hydrogen. It is a fixed bed reactor similar to the pyrolysis reactor 50 and handles heated hydrogen gas and liquid hydrocarbons. Therefore, in the case of these reactors, the same processing unit can be obtained by installing the incidental equipment similar to that described for the processing unit 100. Then, using the processing unit, an activated FT synthesis catalyst and a catalyst slurry can be produced by the same operation as described above.
- the hydrodesulfurization reactor constituting the natural gas desulfurization apparatus 10 installed in the synthesis gas production unit 3 of the liquid fuel production system 1 is also a fixed bed reactor, and the heated hydrogen gas and hydrocarbon compound are removed. In terms of handling, it is similar to the reactor that performs the hydrotreatment, and by installing an incidental facility similar to that described for the processing unit 100, a similar processing unit can be obtained. Then, using the processing unit, an activated FT synthesis catalyst and a catalyst slurry can be produced by the same operation as described above.
- the FT synthesis reactor 30 normally contains the catalyst slurry. However, the slurry is extracted, and only the FT synthesis catalyst is accommodated and reduced by heated hydrogen gas, thereby being activated. An FT synthesis catalyst can be produced. Further, a catalyst slurry is produced by supplying liquid hydrocarbons to the reactor containing the activated FT synthesis catalyst. In this case, as a matter of course, the FT synthesis reaction is carried out in the reactor without transferring the catalyst slurry.
- an activated FT synthesis catalyst of the present invention in a facility for a liquid fuel production system using an FT synthesis reaction, special equipment for reduction treatment of the FT synthesis catalyst, a stabilization process by coating treatment, and An activated FT synthesis catalyst is produced by a simplified process without the need for equipment. Further, subsequently, the catalyst slurry is prevented from being inactivated by contact with the atmosphere of the activated FT synthesis catalyst by the method for producing the catalyst slurry of the present invention and the method for supplying the catalyst slurry to the FT synthesis reactor. Produced and can be easily introduced into the FT synthesis reactor. This also allows the FT synthesis reaction to be carried out with the same catalytic activity and product selectivity as when using an activated FT synthesis catalyst that has been subjected to stabilization treatment.
Abstract
Description
本願は、2010年3月30日に出願された特願2010-79358について優先権を主張し、その内容をここに援用する。
FT合成反応により炭化水素化合物を合成する合成反応システムとしては、例えば、液体炭化水素に固体の触媒粒子を懸濁させたスラリーに合成ガスが吹き込まれてFT合成反応が行われる気泡塔型スラリー床FT反応システムが開示されている(特許文献1)。
特許文献1に記載のシステムのように、FT合成反応による炭化水素化合物の製造において、触媒を液体炭化水素に懸濁させた触媒スラリーの形態とし、該スラリーと原料である合成ガスとを接触させる方法を採用する場合には、通常、FT合成反応器のスタートアップ時に、触媒を液体炭化水素に懸濁させて触媒スラリーを調製し、これを反応器に導入する工程を有している。
前記活性化触媒がスラリー床反応器において使用されるものである場合は、活性化された触媒に液体炭化水素を混合してスラリーとした上で、フィッシャー・トロプシュ合成反応を行なう反応器に容易に移送することができ、また、そのままフィッシャー・トロプシュ合成反応を実施することができる。
無機担体に活性金属を担持してなるフィッシャー・トロプシュ合成反応用触媒を、フィッシャー・トロプシュ合成反応原料である合成ガスを製造するための炭化水素原料の水素化脱硫を行う反応器、フィッシャー・トロプシュ合成反応を行う反応器、フィッシャー・トロプシュ合成反応により合成された合成油の水素化処理を行う反応器のいずれかの反応器において、水素ガスを含むガスにより活性化する活性化工程と、
活性化された前記触媒が収容された前記いずれかの反応器に、液体炭化水素を供給してスラリーを調製する触媒スラリー調製工程と、を含む。
無機担体に活性金属を担持してなるフィッシャー・トロプシュ合成反応用触媒を、フィッシャー・トロプシュ合成反応原料である合成ガスを製造するための炭化水素原料の水素化脱硫を行う反応器、フィッシャー・トロプシュ合成反応により合成された合成油の水素化処理を行う反応器のいずれかの反応器において、水素ガスを含むガスにより活性化する活性化工程と、
活性化された前記触媒が充填された前記いずれかの反応器に、液体炭化水素を供給してスラリーを調製する触媒スラリー調製工程と、
前記触媒スラリーをフィッシャー・トロプシュ合成反応を行う反応器に配管を介して移送する移送工程と、を含む。
本発明のフィッシャー・トロプシュ合成反応用触媒スラリーの製造方法及び触媒スラリーのフィッシャー・トロプシュ合成反応器への供給方法によれば、特別な設備を必要とせず、前記活性化触媒の大気との接触による不活性化を防止しつつ、前記触媒スラリーが簡便に製造され、該触媒スラリーをFT合成反応器に容易に導入できる。
まず、本発明により製造されるフィッシャー・トロプシュ合成反応用活性化触媒(以下、「活性化FT合成触媒」ということもある)が使用されるフィッシャー・トロプシュ合成反応器(以下、「FT合成反応器」ということもある)、この活性化FT合成触媒の製造及びフィッシャー・トロプシュ合成反応用触媒スラリー(以下、「触媒スラリー」ということもある)の製造に使用される天然ガスの脱硫装置、FT合成反応器、炭化水素化合物の水素化処理反応器を含むGTL技術による液体燃料合成システムの一例について説明する。
この液体燃料合成システム1は、合成ガス製造ユニット3と、FT合成ユニット5と、アップグレーディングユニット7とを備えている。合成ガス製造ユニット3においては、炭化水素原料である天然ガスを改質して一酸化炭素ガスと水素ガスとを含む合成ガスを製造する。FT合成ユニット5においては、合成ガス製造ユニット3により製造された合成ガスからFT合成反応により炭化水素化合物が合成される。アップグレーディングユニット7においては、FT合成ユニットにおいて合成された炭化水素化合物が水素化処理及び分留されて液体燃料製品等(ナフサ、灯油、軽油、ワックス等)が製造される。
合成ガス製造ユニット3は、脱硫装置10と改質器12と排熱ボイラー14と気液分離器16,18と脱炭酸装置20と水素分離装置26とを主に備える。
脱硫装置10は、水素化脱硫反応器等を含み、原料である天然ガスから硫黄化合物が除去される。水素化脱硫反応器には、公知の水素化脱硫触媒が充填され、水素ガスの存在下に天然ガス中に含まれる硫黄化合物が水素化されて硫化水素に転化される。水素化脱硫反応器の後段には、例えば酸化亜鉛等の硫化水素を吸着する脱硫材が充填された吸着脱硫装置が備えられ、天然ガス中の硫化水素が除去される。
前記水素化脱硫反応器は、本発明に係る「フィッシャー・トロプシュ合成反応原料である合成ガスを製造するための炭化水素原料の水素化脱硫を行う反応器」の好適な一例である。
このFT合成反応器30は、当然のこととして、本発明に係る「フィッシャー・トロプシュ合成反応を行う反応器」である。
なお、前記の天然ガスの脱硫装置10を構成する水素化脱硫反応器、及び水素化処理を行うための各反応器は、通常はそれぞれの触媒が充填され、それぞれの反応が行なわれている。しかし、前記液体燃料合成システム1が運転を停止し、例えば触媒の交換等により、各反応器に充填された触媒が抜き出された場合には、これらの反応器のいずれかを本発明の方法に利用することが可能となる。
図2に、本実施形態例の活性化FT合成触媒の製造方法において、活性化FT合成触媒の製造及び触媒スラリーの製造に使用される処理ユニットについて説明する。この処理ユニット100として、上記液体燃料合成システム1を構成するワックス留分水素化分解反応器50を使用する例に沿って詳細を説明する。
前記加熱された水素ガスによりFT合成触媒を還元処理することにより、活性化FT合成触媒が製造される。
上記実施形態例の処理ユニット100を用いた活性化FT合成触媒の製造方法について説明する。
担持の方法としては特に限定されないが、前記の活性金属元素を含む化合物の溶液を用いた、Incipient Wetness法に代表される含浸法が好ましく採用される。
活性金属元素を含む化合物が担持された担体は、公知の方法により乾燥され、更に好ましくは空気雰囲気下に、公知の方法により焼成される。焼成温度としては特に限定されないが、一般的に300~600℃程度である。
前記焼成により、担体上の活性金属元素を含む化合物は金属酸化物に転化される。
本発明の活性化FT合成触媒の製造方法において使用するFT合成触媒は、前記の活性金属原子が酸化物の状態にあるものであることが好ましい。
還元処理における温度(還元温度)は特に限定されないが、一般的に200~550℃であることが好ましい。還元温度が200℃よりも低い場合、活性金属原子が充分に還元されず触媒活性が充分に発現しない傾向にあり、550℃を超える場合には、活性金属の凝集等に起因して触媒活性が低下する傾向にある。
還元処理における圧力は特に限定されないが、一般的に0.1~10MPaであることが好ましい。圧力が0.1MPa未満の場合には、活性金属原子が充分に還元されず触媒活性が充分に発現しない傾向にあり、10MPaを超える場合には、装置の耐圧を高める必要から設備コストが上昇する傾向にある。
還元処理の時間は特に限定されないが、一般的に0.5~50時間であることが好ましい。還元時間が0.5時間未満の場合には、活性金属原子が充分に還元されず触媒活性が充分に発現しない傾向にあり、50時間を超える場合には、活性金属の凝集等に起因して触媒活性が低下する傾向にあり、また効率が低下する傾向にある。
還元処理の終了後、水素ガス等の還元性ガスの流通を停止し、活性化FT合成触媒が得られる。
上記実施形態例の処理ユニット100を用いた触媒スラリーの製造方法について説明する。
上記活性化FT合成触媒の製造方法によって製造された活性化FT合成触媒は、必要により所定の温度まで冷却される。そして該触媒がワックス留分水素化分解反応器50内に収容されている状態において、大気に接触させることなく、液体炭化水素導入管151bから供給管151を介して、ワックス留分水素化分解反応器50に液体炭化水素が供給される。ここで液体炭化水素とは、ワックス留分水素化分解反応器50に供給された状態で液体であればよく、例えば常温において固体又は半固体であっても、加熱されてワックス留分水素化分解反応器50に導入され、ここで液体の状態となっていればよい。
液体炭化水素供給管151bから供給管151を介して供給される液体炭化水素は、必要により加熱器152により加熱されてワックス留分水素化分解反応器50に供給される。特に、用いる液体炭化水素がワックス留分あるいはワックス留分を含有するものである場合には、流動性を維持するために加熱することが好ましい。液体炭化水素の加熱器152出口における温度は、液体炭化水素の組成にもよるが、常温~300℃が好ましく、常温~250℃がより好ましい。液体炭化水素がワックス成分を含有するものである場合には、80~300℃が好ましい。ここで、常温とは約5~35℃の温度である。なお、ワックス留分水素化分解反応器50への液体炭化水素の供給に際しては、ワックス留分水素化分解反応器50の底部に接続された、通常は流出油が排出される配管154、及び排出管153は閉止しておく。
上記触媒スラリーの製造方法により製造された触媒スラリーは、活性化FT合成触媒と液体炭化水素とを含み、気泡塔型スラリー床FT合成反応装置によるFT合成反応に供することができる。
なお、ワックス留分水素化分解反応器50に供給される液体炭化水素の量は、FT合成反応初期における触媒スラリー中の活性化FT合成触媒濃度に依存する。すなわち、ワックス留分水素化分解反応器50内で製造される触媒スラリー中の活性化FT合成触媒の濃度が、少なくとも、FT合成反応初期における、FT合成反応に使用される触媒スラリー中の活性化FT合成触媒の濃度以上となるように、供給する液体炭化水素の量を調整する。
上記触媒スラリーの製造方法によって製造された触媒スラリーは、FT合成反応器30へと移送される。
移送方法としては、ワックス留分水素化分解反応器50内に収容されている触媒スラリーを、一旦外部に抜き出し、FT合成反応器30へ投入してもよい。但し、その場合には、触媒スラリーが大気と接触することにより、活性化FT合成触媒が不活性化するおそれ、及び触媒スラリーが加熱されている場合にはその温度の低下により流動性が損なわれるおそれがある。よって、触媒スラリーの移送方法としては、外部に抜き出すことなく、配管を通じて直接FT合成反応器30へと移送することが好ましい。触媒スラリーのワックス留分水素化分解反応器50からの排出は、排出管153から行なわれることが好ましい。排出管153はFT合成反応器30に接続されているが(図示略)、触媒スラリー移送のための専用の配管であることが、触媒スラリー移送後の、配管に残留した触媒によるコンタミネーション防止の観点から好ましい。また、スラリー移送後に、排出管153に液体炭化水素を通じる(フラッシング)ことにより、残留する活性化触媒を除去することが好ましい。
その後、FT合成反応器30に、所定の圧力(例えば、1~5MPaG)に昇圧された合成ガス(H2、CO)が供給され、所定の温度170~300℃にされて、FT合成反応が開始される。FT合成反応においては、一酸化炭素ガス及び水素ガスから液体炭化水素が合成される。
3 合成ガス製造ユニット
5 FT合成ユニット
7 アップグレーディングユニット
10 脱硫装置
30 FT合成反応器
50 ワックス留分水素化分解反応器
52 中間留分水素化精製反応器
54 ナフサ留分水素化精製反応器
100 処理ユニット
151 供給管
151a 水素導入管
151b 液体炭化水素導入管
152 加熱器
153 排出管
Claims (4)
- 無機担体に活性金属を担持してなるフィッシャー・トロプシュ合成反応用触媒を、水素ガスを含むガスにより還元処理する工程を備え、
前記還元処理は、フィッシャー・トロプシュ合成反応原料である合成ガスを製造するための炭化水素原料の水素化脱硫を行う反応器、フィッシャー・トロプシュ合成反応を行う反応器、及びフィッシャー・トロプシュ合成反応により合成された合成油の水素化処理を行う反応器のいずれかにおいて実施されるフィッシャー・トロプシュ合成反応用活性化触媒の製造方法。 - 前記フィッシャー・トロプシュ合成反応用活性化触媒が、スラリー床反応器において使用される請求項1に記載のフィッシャー・トロプシュ合成反応用活性化触媒の製造方法。
- 無機担体に活性金属を担持してなるフィッシャー・トロプシュ合成反応用触媒を、フィッシャー・トロプシュ合成反応原料である合成ガスを製造するための炭化水素原料の水素化脱硫を行う反応器、フィッシャー・トロプシュ合成反応を行う反応器、フィッシャー・トロプシュ合成反応により合成された合成油の水素化処理を行う反応器のいずれかの反応器において、水素ガスを含むガスにより活性化する活性化工程と、
活性化された前記触媒が収容された前記いずれかの反応器に、液体炭化水素を供給してスラリーを調製する触媒スラリー調製工程と、
を備えるフィッシャー・トロプシュ合成反応用触媒スラリーの製造方法。 - 無機担体に活性金属を担持してなるフィッシャー・トロプシュ合成反応用触媒を、フィッシャー・トロプシュ合成反応原料である合成ガスを製造するための炭化水素原料の水素化脱硫を行う反応器、フィッシャー・トロプシュ合成反応により合成された合成油の水素化処理を行う反応器のいずれかの反応器において、水素ガスを含むガスにより活性化する活性化工程と、
活性化された前記触媒が充填された前記いずれかの反応器に、液体炭化水素を供給してスラリーを調製する触媒スラリー調製工程と、
前記触媒スラリーを、フィッシャー・トロプシュ合成反応を行う反応器に配管を介して移送する移送工程と、
を備える触媒スラリーのフィッシャー・トロプシュ合成反応器への供給方法。
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CN201180016594XA CN102917792A (zh) | 2010-03-30 | 2011-03-15 | 费托合成反应用活化催化剂的制造方法、催化剂浆料的制造方法及向费托合成反应器供给催化剂浆料的方法 |
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US13/637,379 US20130018114A1 (en) | 2010-03-30 | 2011-03-15 | Process for producing activated catalyst for fischer-tropsch synthesis reaction, process for producing catalyst slurry, and process for supplying catalyst slurry to fischer-tropsch synthesis reactor |
BR112012024443A BR112012024443A2 (pt) | 2010-03-30 | 2011-03-15 | processo para produzir catalizador ativado para reação de síntese de fischer-tropsch, processo para a produção de suspensão catalisadora, e processo para fornecimento de suspensão catalisadora para o reator de síntese de fischer-tropsch |
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JP5869397B2 (ja) * | 2012-03-28 | 2016-02-24 | 独立行政法人石油天然ガス・金属鉱物資源機構 | 気泡塔型スラリー床反応器のスタートアップ方法 |
KR101418910B1 (ko) * | 2012-11-02 | 2014-07-16 | 한국에너지기술연구원 | 경유 재순환 장치 및 그를 갖는 합성연료 제조 시스템 |
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FR3044565B1 (fr) * | 2015-12-08 | 2017-12-01 | Ifp Energies Now | Chargement d'un catalyseur dans une colonne a bulles pour la synthese fischer-tropsch |
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