WO2022138850A1 - 塩素ガス分解用触媒、排出ガス処理装置および塩素ガスの分解方法 - Google Patents
塩素ガス分解用触媒、排出ガス処理装置および塩素ガスの分解方法 Download PDFInfo
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- WO2022138850A1 WO2022138850A1 PCT/JP2021/047971 JP2021047971W WO2022138850A1 WO 2022138850 A1 WO2022138850 A1 WO 2022138850A1 JP 2021047971 W JP2021047971 W JP 2021047971W WO 2022138850 A1 WO2022138850 A1 WO 2022138850A1
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- Prior art keywords
- chlorine gas
- gas
- exhaust gas
- catalyst
- oxide
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- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 title claims abstract description 162
- 239000003054 catalyst Substances 0.000 title claims abstract description 110
- 238000000354 decomposition reaction Methods 0.000 title claims abstract description 97
- 238000000034 method Methods 0.000 title claims description 43
- 229910044991 metal oxide Inorganic materials 0.000 claims abstract description 25
- 150000004706 metal oxides Chemical class 0.000 claims abstract description 25
- 229910052684 Cerium Inorganic materials 0.000 claims abstract description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 28
- 238000010438 heat treatment Methods 0.000 claims description 16
- IVMYJDGYRUAWML-UHFFFAOYSA-N cobalt(ii) oxide Chemical compound [Co]=O IVMYJDGYRUAWML-UHFFFAOYSA-N 0.000 claims description 15
- -1 perfluoro compound Chemical class 0.000 claims description 15
- 229910000428 cobalt oxide Inorganic materials 0.000 claims description 12
- 239000002131 composite material Substances 0.000 claims description 9
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- BMMGVYCKOGBVEV-UHFFFAOYSA-N oxo(oxoceriooxy)cerium Chemical compound [Ce]=O.O=[Ce]=O BMMGVYCKOGBVEV-UHFFFAOYSA-N 0.000 claims description 8
- 229910000420 cerium oxide Inorganic materials 0.000 claims description 7
- 229910052804 chromium Inorganic materials 0.000 claims description 5
- 229910052802 copper Inorganic materials 0.000 claims description 5
- 229910052742 iron Inorganic materials 0.000 claims description 4
- 229910052748 manganese Inorganic materials 0.000 claims description 4
- 229910052759 nickel Inorganic materials 0.000 claims description 4
- 239000002253 acid Substances 0.000 claims description 3
- 229910052749 magnesium Inorganic materials 0.000 claims description 3
- 229910052726 zirconium Inorganic materials 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 110
- HSJPMRKMPBAUAU-UHFFFAOYSA-N cerium(3+);trinitrate Chemical compound [Ce+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O HSJPMRKMPBAUAU-UHFFFAOYSA-N 0.000 description 54
- 150000004687 hexahydrates Chemical class 0.000 description 30
- 238000006243 chemical reaction Methods 0.000 description 26
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- 239000002994 raw material Substances 0.000 description 18
- 239000000243 solution Substances 0.000 description 16
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 13
- 239000000126 substance Substances 0.000 description 12
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 9
- 229910001873 dinitrogen Inorganic materials 0.000 description 9
- 239000002245 particle Substances 0.000 description 9
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- 239000007864 aqueous solution Substances 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 6
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- 229910000041 hydrogen chloride Inorganic materials 0.000 description 6
- MFUVDXOKPBAHMC-UHFFFAOYSA-N magnesium;dinitrate;hexahydrate Chemical compound O.O.O.O.O.O.[Mg+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O MFUVDXOKPBAHMC-UHFFFAOYSA-N 0.000 description 6
- 238000005259 measurement Methods 0.000 description 6
- NLKNQRATVPKPDG-UHFFFAOYSA-M potassium iodide Chemical compound [K+].[I-] NLKNQRATVPKPDG-UHFFFAOYSA-M 0.000 description 6
- QGUAJWGNOXCYJF-UHFFFAOYSA-N cobalt dinitrate hexahydrate Chemical compound O.O.O.O.O.O.[Co+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O QGUAJWGNOXCYJF-UHFFFAOYSA-N 0.000 description 5
- XTVVROIMIGLXTD-UHFFFAOYSA-N copper(II) nitrate trihydrate Substances [Cu+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O XTVVROIMIGLXTD-UHFFFAOYSA-N 0.000 description 5
- 238000005470 impregnation Methods 0.000 description 5
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- 239000000843 powder Substances 0.000 description 5
- 150000003839 salts Chemical class 0.000 description 5
- ZFYIQPIHXRFFCZ-QMMMGPOBSA-N (2s)-2-(cyclohexylamino)butanedioic acid Chemical compound OC(=O)C[C@@H](C(O)=O)NC1CCCCC1 ZFYIQPIHXRFFCZ-QMMMGPOBSA-N 0.000 description 4
- 229910002651 NO3 Inorganic materials 0.000 description 4
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 4
- GWXLDORMOJMVQZ-UHFFFAOYSA-N cerium Chemical compound [Ce] GWXLDORMOJMVQZ-UHFFFAOYSA-N 0.000 description 4
- 239000011651 chromium Substances 0.000 description 4
- 239000000498 cooling water Substances 0.000 description 4
- 239000010949 copper Substances 0.000 description 4
- 239000006185 dispersion Substances 0.000 description 4
- AOPCKOPZYFFEDA-UHFFFAOYSA-N nickel(2+);dinitrate;hexahydrate Chemical compound O.O.O.O.O.O.[Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O AOPCKOPZYFFEDA-UHFFFAOYSA-N 0.000 description 4
- IBMCQJYLPXUOKM-UHFFFAOYSA-N 1,2,2,6,6-pentamethyl-3h-pyridine Chemical compound CN1C(C)(C)CC=CC1(C)C IBMCQJYLPXUOKM-UHFFFAOYSA-N 0.000 description 3
- FTVZOQPUAHMAIA-UHFFFAOYSA-N O.O.[Zr+4].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O Chemical compound O.O.[Zr+4].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O FTVZOQPUAHMAIA-UHFFFAOYSA-N 0.000 description 3
- 239000003463 adsorbent Substances 0.000 description 3
- 229910052786 argon Inorganic materials 0.000 description 3
- PHFQLYPOURZARY-UHFFFAOYSA-N chromium nitrate Inorganic materials [Cr+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O PHFQLYPOURZARY-UHFFFAOYSA-N 0.000 description 3
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 3
- 238000002354 inductively-coupled plasma atomic emission spectroscopy Methods 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 3
- 239000011572 manganese Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N nickel Substances [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 3
- ZCYVEMRRCGMTRW-UHFFFAOYSA-N 7553-56-2 Chemical compound [I] ZCYVEMRRCGMTRW-UHFFFAOYSA-N 0.000 description 2
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- 229910020599 Co 3 O 4 Inorganic materials 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 229910021536 Zeolite Inorganic materials 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 229910017052 cobalt Inorganic materials 0.000 description 2
- 239000010941 cobalt Substances 0.000 description 2
- UFMZWBIQTDUYBN-UHFFFAOYSA-N cobalt dinitrate Chemical compound [Co+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O UFMZWBIQTDUYBN-UHFFFAOYSA-N 0.000 description 2
- 229910001981 cobalt nitrate Inorganic materials 0.000 description 2
- LBFUKZWYPLNNJC-UHFFFAOYSA-N cobalt(ii,iii) oxide Chemical compound [Co]=O.O=[Co]O[Co]=O LBFUKZWYPLNNJC-UHFFFAOYSA-N 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000010586 diagram Methods 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
- 229910001882 dioxygen Inorganic materials 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000000921 elemental analysis Methods 0.000 description 2
- 238000010304 firing Methods 0.000 description 2
- 239000001307 helium Substances 0.000 description 2
- 229910052734 helium Inorganic materials 0.000 description 2
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 2
- 229910001026 inconel Inorganic materials 0.000 description 2
- 238000009616 inductively coupled plasma Methods 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 229910052740 iodine Inorganic materials 0.000 description 2
- 239000011630 iodine Substances 0.000 description 2
- VCJMYUPGQJHHFU-UHFFFAOYSA-N iron(3+);trinitrate Chemical compound [Fe+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O VCJMYUPGQJHHFU-UHFFFAOYSA-N 0.000 description 2
- SZQUEWJRBJDHSM-UHFFFAOYSA-N iron(3+);trinitrate;nonahydrate Chemical compound O.O.O.O.O.O.O.O.O.[Fe+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O SZQUEWJRBJDHSM-UHFFFAOYSA-N 0.000 description 2
- FYDKNKUEBJQCCN-UHFFFAOYSA-N lanthanum(3+);trinitrate Chemical compound [La+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O FYDKNKUEBJQCCN-UHFFFAOYSA-N 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- MIVBAHRSNUNMPP-UHFFFAOYSA-N manganese(2+);dinitrate Chemical compound [Mn+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O MIVBAHRSNUNMPP-UHFFFAOYSA-N 0.000 description 2
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- JIPBPJZISZCBJQ-UHFFFAOYSA-N 1-[(2-methylpropan-2-yl)oxycarbonyl]-3-(pyridin-4-ylmethyl)piperidine-3-carboxylic acid Chemical compound C1N(C(=O)OC(C)(C)C)CCCC1(C(O)=O)CC1=CC=NC=C1 JIPBPJZISZCBJQ-UHFFFAOYSA-N 0.000 description 1
- NGDQQLAVJWUYSF-UHFFFAOYSA-N 4-methyl-2-phenyl-1,3-thiazole-5-sulfonyl chloride Chemical compound S1C(S(Cl)(=O)=O)=C(C)N=C1C1=CC=CC=C1 NGDQQLAVJWUYSF-UHFFFAOYSA-N 0.000 description 1
- 238000004438 BET method Methods 0.000 description 1
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 description 1
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 238000007605 air drying Methods 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- IYNQBRDDQSFSRT-UHFFFAOYSA-N chromium(3+) trinitrate hexahydrate Chemical compound O.O.O.O.O.O.[Cr+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O IYNQBRDDQSFSRT-UHFFFAOYSA-N 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- UBEWDCMIDFGDOO-UHFFFAOYSA-N cobalt(2+);cobalt(3+);oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[O-2].[Co+2].[Co+3].[Co+3] UBEWDCMIDFGDOO-UHFFFAOYSA-N 0.000 description 1
- 229940126543 compound 14 Drugs 0.000 description 1
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- 230000001186 cumulative effect Effects 0.000 description 1
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- 238000005516 engineering process Methods 0.000 description 1
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- 239000011521 glass Substances 0.000 description 1
- 229910052736 halogen Inorganic materials 0.000 description 1
- 150000002367 halogens Chemical class 0.000 description 1
- 150000004677 hydrates Chemical class 0.000 description 1
- 229910000040 hydrogen fluoride Inorganic materials 0.000 description 1
- MVFCKEFYUDZOCX-UHFFFAOYSA-N iron(2+);dinitrate Chemical compound [Fe+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O MVFCKEFYUDZOCX-UHFFFAOYSA-N 0.000 description 1
- 238000007561 laser diffraction method Methods 0.000 description 1
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- 239000000463 material Substances 0.000 description 1
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- 239000011812 mixed powder Substances 0.000 description 1
- 229910000480 nickel oxide Inorganic materials 0.000 description 1
- OQUOOEBLAKQCOP-UHFFFAOYSA-N nitric acid;hexahydrate Chemical compound O.O.O.O.O.O.O[N+]([O-])=O OQUOOEBLAKQCOP-UHFFFAOYSA-N 0.000 description 1
- GNRSAWUEBMWBQH-UHFFFAOYSA-N oxonickel Chemical compound [Ni]=O GNRSAWUEBMWBQH-UHFFFAOYSA-N 0.000 description 1
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- B01J37/341—Irradiation by, or application of, electric, magnetic or wave energy, e.g. ultrasonic waves ; Ionic sputtering; Flame or plasma spraying; Particle radiation making use of electric or magnetic fields, wave energy or particle radiation
- B01J37/343—Irradiation by, or application of, electric, magnetic or wave energy, e.g. ultrasonic waves ; Ionic sputtering; Flame or plasma spraying; Particle radiation making use of electric or magnetic fields, wave energy or particle radiation of ultrasonic wave energy
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Definitions
- the present invention relates to a chlorine gas decomposition catalyst, an exhaust gas treatment device using the catalyst, and a chlorine gas decomposition method.
- Chlorine gas may be contained in the gas emitted from the compound manufacturing process, various industrial processes, etc. Chlorine gas is toxic and needs to be removed, and has been removed by various means in the past.
- Patent Documents 1 and 2 disclose a method of removing chlorine gas by contacting an exhaust gas containing chlorine gas with an alkaline solution.
- Patent Documents 3 and 4 disclose a method of removing chlorine gas by adsorbing a halogen-based gas such as chlorine gas on an adsorbent (harmful agent) containing zeolite.
- Japanese Unexamined Patent Publication No. 2005-305414 Japanese Unexamined Patent Publication No. 2008-11339 Japanese Unexamined Patent Publication No. 2008-229610 Japanese Unexamined Patent Publication No. 2016-155072
- an object of the present invention is to provide a chlorine gas removing means, a chlorine gas removing method, etc., which can remove chlorine gas contained in exhaust gas or the like with high efficiency and do not need to be replaced frequently.
- the present invention relates to, for example, the following [1] to [16].
- the metal oxide (X) is a catalyst for decomposing chlorine gas containing an oxide (X1) of at least one element selected from the group consisting of Ce and Co.
- the oxide (X1) contains the composite oxide of Ce and at least one element M selected from the group consisting of Mg, Cr, Mn, Fe, Co, Ni, Cu and Zr [1] or [ 2] Chlorine gas decomposition catalyst.
- the catalyst for chlorine gas decomposition according to any one of [1] to [5], which comprises a carrier and the metal oxide (X) supported on the carrier.
- An exhaust gas treatment apparatus comprising a reactor into which an exhaust gas containing chlorine gas is introduced, wherein the reactor is provided with a catalyst for decomposing chlorine gas according to any one of [1] to [7].
- the exhaust gas treatment device according to any one of [8] to [10], comprising a device for supplying water to the exhaust gas.
- the exhaust gas treatment device according to any one of [8] to [11], comprising a heating device for heating the exhaust gas.
- the exhaust gas treatment device according to any one of [8] to [13], comprising a removing device for removing acid gas from the gas discharged from the reactor.
- the above [8] to [14] include a temperature detector for detecting the temperature of the exhaust gas supplied to the reactor and a control device for controlling the heating device based on the measured temperature of the temperature detector.
- a temperature detector for detecting the temperature of the exhaust gas supplied to the reactor
- a control device for controlling the heating device based on the measured temperature of the temperature detector.
- One of the emission treatment devices One of the emission treatment devices.
- [16] A method for decomposing chlorine gas, in which a gas containing chlorine gas is brought into contact with the chlorine gas decomposition catalyst according to any one of [1] to [7] above in the presence of water.
- chlorine gas decomposition catalyst of the present invention By using the chlorine gas decomposition catalyst of the present invention, chlorine gas contained in exhaust gas or the like can be removed with high efficiency. Further, the chlorine gas decomposition catalyst of the present invention can be used without frequent replacement.
- FIG. 1 is an XRD pattern of the chlorine gas decomposition catalyst produced in Example 1.
- FIG. 2 is an XRD pattern of the chlorine gas decomposition catalyst produced in Example 2.
- FIG. 3 is an XRD pattern of the chlorine gas decomposition catalyst produced in Example 3.
- FIG. 4 is an XRD pattern of the chlorine gas decomposition catalyst produced in Example 4.
- FIG. 5 is an XRD pattern of the chlorine gas decomposition catalyst produced in Example 5.
- FIG. 6 is an XRD pattern of the chlorine gas decomposition catalyst produced in Example 6.
- FIG. 7 is an XRD pattern of the chlorine gas decomposition catalyst produced in Example 7.
- FIG. 8 is an XRD pattern of the chlorine gas decomposition catalyst produced in Example 8.
- FIG. 9 is an XRD pattern of the chlorine gas decomposition catalyst produced in Example 9.
- FIG. 9 is an XRD pattern of the chlorine gas decomposition catalyst produced in Example 9.
- FIG. 10 is an XRD pattern of the chlorine gas decomposition catalyst produced in Example 10.
- FIG. 11 is an XRD pattern of the chlorine gas decomposition catalyst produced in Example 11.
- FIG. 12 is an XRD pattern of the chlorine gas decomposition catalyst produced in Example 12.
- FIG. 13 is an XRD pattern of the chlorine gas decomposition catalyst produced in Example 13.
- FIG. 14 is an XRD pattern of the chlorine gas decomposition catalyst produced in Example 14.
- FIG. 15 is an XRD pattern of the chlorine gas decomposition catalyst produced in Example 15.
- FIG. 16 is an XRD pattern of the chlorine gas decomposition catalyst produced in Comparative Example 1.
- FIG. 17 is an XRD pattern of the chlorine gas decomposition catalyst produced in Comparative Example 2.
- FIG. 18 is a configuration diagram of one aspect of the exhaust gas treatment device of the present invention.
- the chlorine gas decomposition catalyst according to the present invention is a chlorine gas decomposition catalyst containing a metal oxide (X), and the metal oxide (X) is selected from the group consisting of Ce (cerium) and Co (cobalt). It is characterized by containing an oxide (X1) of at least one element thereof (that is, an oxide of Ce (cerium) and / or Co (cobalt) (X1)).
- the metal oxide (X) contains an oxide (X1) of at least one element selected from the group consisting of Ce and Co.
- the oxide (X1) is preferably (1) At least selected from the group consisting of cerium oxide and a composite oxide of Ce and at least one element M selected from the group consisting of Mg, Cr, Mn, Fe, Co, Ni, Cu and Zr. It contains one type of cerium oxide (2) cobalt oxide, or (3) both cerium oxide (1) and cobalt oxide (2).
- the metal oxide (X) is further composed of the element M (however, Co is excluded). It may contain an oxide (X2).
- the cerium oxide preferably contains CeO 2 .
- the metal element M is preferably at least one selected from the group consisting of Cr, Mn, Fe, Co, Ni and Cu, and more preferably Cr, Co and Cu.
- the ratio of the atom of the metal element M in the metal oxide (X) is preferably 0. It may be 001 to 2.0 mol, more preferably 0.1 to 1.8 mol.
- the metal oxide (X) is highly active with respect to the decomposition of chlorine gas. Therefore, the catalyst for chlorine gas decomposition according to the present invention is exhaust gas or the like. Chlorine gas contained in can be removed with high efficiency.
- the cobalt oxide (2) preferably contains Co 3 O 4 .
- the ratio of the cobalt oxide (2) in the embodiment (3) is preferably 2.0 mol or less of the cobalt atom in the cobalt oxide (2) with respect to 1 mol of the cerium atom in the cerium-based oxide (1). , More preferably 0.1 to 2.0 mol, more preferably 1.0 to 1.8 mol.
- the chlorine gas decomposition catalyst according to the present invention may further contain a carrier, that is, a chlorine gas decomposition catalyst containing the carrier and the metal oxide (X) supported on the carrier (hereinafter, “supported catalyst”). It may also be described as.).
- the chlorine gas decomposition catalyst, which is a supported catalyst generally has a large specific surface area, and is therefore preferable from the viewpoint of improving the catalytic activity.
- the shape and size of the carrier are not particularly limited, but for example, bead-shaped, pellet-shaped, powder-shaped, granular-shaped, and monolith-shaped structures are preferable. In particular, pellets are preferable.
- the carrier is preferably made of a porous material, and its specific surface area measured by the BET method is, for example, 100 to 500 cm 2 / g, preferably 100 to 300 cm 2 / g.
- constituent components of the carrier components that are inactive or have poor reactivity with respect to chlorine gas and hydrogen chloride generated by the decomposition reaction of chlorine gas are preferable, and for example, alumina (Al 2 O 3 ), silica (SiO 2 ), and Koji.
- alumina Al 2 O 3
- silica SiO 2
- Koji Koji
- Examples include light, zeolite and the like, preferably alumina.
- the average particle size (diameter) of the carrier is, for example, 1 to 10 mm, preferably 2 to 5 mm.
- a step of pulverizing and mixing a powder of metal oxide (X) (for example, cerium oxide powder, cobalt oxide powder), and optionally, the pulverized and mixed powder is calcined in air at 500 to 900 ° C. Examples thereof include a method for producing a catalyst for decomposing chlorine gas, which includes a step.
- a step (1) of preparing a carrier in which the carrier is impregnated with the raw material component of the metal oxide (X) that is, the carrier carrying the raw material component or a component containing a metal in the raw material component).
- Step of calcining the carrier to obtain a catalyst for chlorine gas decomposition Examples thereof include a method for producing a catalyst for decomposing chlorine gas containing.
- Examples of the raw material component of the metal oxide (X) include salts of Ce, Co, and other metal elements.
- the salt may be a hydrate.
- the salt examples include nitrate, chloride, bromide, sulfate, and carbonate, and among these, nitrate and chloride are preferable, and nitrate is more preferable.
- Specific examples of the nitrate include cerium (III) nitrate hexahydrate, cobalt (II) nitrate hexahydrate, nickel (II) nitrate hexahydrate, chromium (III) nitrate hexahydrate, and iron nitrate.
- III Nine hydrates, manganese (II) nitrate hexahydrate, magnesium nitrate hexahydrate, zirconium nitrate dihydrate, and copper (II) nitrate trihydrate.
- the raw material component of the metal oxide (X) may be the metal oxide (X) itself or a part of the oxide in the metal oxide (X).
- oxides include cobalt oxide (Co 3 O 4 ).
- the average particle size of the oxide as a raw material component for example, the value of D50 measured by the method adopted in the examples is preferably 0.1 to 10 ⁇ m.
- Method including (a), A step of dispersing the raw material component in water to prepare an impregnating solution (11b), and a step of contacting the impregnating solution with the carrier and then recovering the obtained carrier (12b).
- B or a step (11a) of preparing an impregnated solution by dissolving the raw material component in water.
- Method including (c) Is carried out by.
- the method (a) is preferably carried out.
- the method (b) is preferably carried out.
- the method (c) is preferably carried out.
- an impregnation method for example, a heat impregnation method, a normal temperature impregnation method, a vacuum impregnation method, a normal pressure impregnation method
- the pore filling method is preferable from the viewpoints of supporting the raw material component on the carrier with high dispersibility, improving the catalytic activity, and easiness of industrial implementation.
- the raw material component By contacting the impregnating liquid with the carrier, the raw material component can be stably supported on the surface of the carrier, and further in the pores when the carrier is made of a porous material, with high dispersibility. ..
- the contact between the impregnating liquid and the carrier may be performed under atmospheric pressure or reduced pressure.
- the contact between the impregnating liquid and the carrier may be carried out near room temperature (for example, 5 to 40 ° C.), or may be carried out at a higher temperature (for example, 40 to 85 ° C.) by heating.
- the recovered carrier is preferably dried. Drying can be performed by conventionally known means such as air drying and heating. Drying is performed, for example, under the following conditions.
- Step (2) Temperature at which the supported raw material components do not decompose (for example, room temperature to 300 ° C) Time: 0.5 to 50 hours Pressure: Normal pressure or under reduced pressure Atmosphere: Air, inert gas (for example, argon gas, nitrogen gas, helium gas), oxygen gas, or a mixed gas thereof ⁇ Step (2)> In the step (2), the carrier obtained in the step (1) is calcined to obtain a catalyst for chlorine gas decomposition.
- inert gas for example, argon gas, nitrogen gas, helium gas
- oxygen gas or a mixed gas thereof
- Firing is performed, for example, under the following conditions. Temperature: 300-1200 ° C, preferably 400-800 ° C Time: 0.5-10 hours, preferably 1-3 hours Pressure: Normal pressure, reduced pressure or pressurized Atmosphere: Air, inert gas (eg argon gas, nitrogen gas, helium gas), oxygen gas or a mixture thereof Gas
- inert gas eg argon gas, nitrogen gas, helium gas
- oxygen gas eg.g a mixture thereof
- the metal component is supported in the form of an oxide or a composite oxide in a highly dispersed state on the carrier.
- the exhaust gas treatment apparatus is provided with a container into which an exhaust gas containing chlorine gas is introduced, that is, a reactor, and the reactor is provided with a catalyst for decomposing chlorine gas according to the present invention. It is supposed to be.
- FIG. 18 is a configuration diagram of one aspect of the exhaust gas treatment device of the present invention.
- the exhaust gas perfluoro compound gas (hereinafter, also referred to as “PFC gas”) or acidic gas containing chlorine gas) is infused with water by a spray 2.
- a reactor 5 that introduces exhaust gas, pure water, and air that have passed through the scrubber 3 and the first scrubber 3 to decompose chlorine gas in the exhaust gas, and a cooler 7 that cools the exhaust gas that has passed through the reactor 5.
- the second scrubber 10 in which water is injected into the exhaust gas that has passed through the cooler 7 by the spray 9, the blower 11 for sending the treated exhaust gas that has passed through the second scrubber 10 out of the system, and the cooler 7. It is provided with a tank 13 for collecting the exhaust gas.
- the inside of the reactor 5 is filled with a chlorine gas decomposition catalyst 4, and a heater 6 is installed around the reactor 5.
- the reactor 5 can be appropriately set according to the type of exhaust gas, the scale of the exhaust gas treatment device, and the like.
- Examples of the exhaust gas include gases emitted from the compound manufacturing process, various industrial processes, and the like. Specific examples include an etching gas used in the manufacturing process of a semiconductor or a liquid crystal, or a cleaning gas used in a CVD apparatus, and these exhaust gases may contain a perfluoro compound. Examples of the perfluoro compound include CF 4 , CHF 3 , C 2 F 6 , C 3 F 8 , C 4 F 8 , SF 6 , and NF 3 .
- the reactor 5 may be provided with a catalyst for decomposing a perfluoro compound 14 (not shown) together with the catalyst for decomposing chlorine gas 4.
- the catalyst 14 for decomposing the perfluoro compound may be a conventionally known catalyst, for example, a nickel oxide catalyst.
- the reactor 5 including the chlorine gas decomposition catalyst 4 and the reactor 5 including the perfluoro compound decomposition catalyst 14 are not separated.
- Chlorine gas can be decomposed with high efficiency.
- the chlorine gas decomposition catalyst 4 and the perfluoro compound decomposition catalyst 14 may be filled inside the reactor 5, respectively, or may be provided on the inner wall of the reactor 5 as a catalyst layer. ..
- the chlorine gas decomposition catalyst 4 and the perfluoro compound decomposition catalyst 14 may be mixed and filled in the reactor 5, or may be separately filled in the reactor 5.
- the exhaust gas treatment device 1 according to the present invention preferably includes a device for supplying water to the exhaust gas to be introduced into the reactor 5. By providing this device, even when the exhaust gas originally does not contain water, the decomposition reaction of chlorine gas, which will be described later, can be smoothly performed.
- the exhaust gas treatment device 1 preferably includes a heating device 6 (for example, a heater) for heating the exhaust gas containing chlorine gas to a temperature at which the chlorine gas decomposition reaction is performed.
- the reactor 5 may be provided with a heating device 6 (for example, a heater installed around the reactor) for heating the inside of the reactor 5 to a temperature at which the decomposition reaction of chlorine gas is carried out.
- a heating device 6 for example, a heater
- the exhaust gas treatment device 1 preferably includes a cooling device 8 for cooling the gas discharged from the reactor 5.
- a cooling device 8 for cooling the gas discharged from the reactor 5.
- a device for bringing the cooling water into contact with the gas in the cooler 7 for example, a spray 8 for injecting water
- hydrogen chloride which is a decomposition product of chlorine gas contained in the gas
- hydrogen chloride which is a decomposition product of the perfluoro compound when the exhaust gas contains a perfluoro compound. It can be dissolved in cooling water and removed.
- the cooling water in which hydrogen chloride or the like is dissolved is discharged to the tank 13 by the pump 12.
- the exhaust gas treatment device 1 preferably removes an acid gas (hydrogen chloride gas, hydrogen fluoride gas) from the gas discharged from the reactor 5 and passed through the cooling device (for example, the second scrubber 10). ) Is provided.
- the exhaust gas treatment device controls the heating device 6 based on the temperature detector that detects the temperature of the exhaust gas supplied to the reactor 5, and the temperature measured by the temperature detector. It is equipped with a control device.
- Chlorine gas decomposition method The method for decomposing chlorine gas according to the present invention is characterized in that a gas containing chlorine gas is brought into contact with the chlorine gas decomposing catalyst according to the present invention in the presence of water.
- the ratio of chlorine gas in the gas containing chlorine gas is, for example, 0.1 to 10% by volume, preferably 0.1 to 1% by volume at 25 ° C. and 1 atm.
- the gas containing chlorine gas preferably contains water.
- the ratio of water in the gas containing chlorine gas is, for example, 1 to 40% by volume, preferably 10 to 25% by volume.
- the volume described here is a value converted in a standard state (0 ° C., 1.01 ⁇ 10 5 Pa).
- Examples of the gas other than chlorine gas and water vapor in the gas containing chlorine gas include nitrogen gas and argon gas.
- the decomposition reaction of chlorine gas is carried out under the following conditions, for example.
- chlorine gas particularly chlorine gas contained in exhaust gas, can be decomposed at a high decomposition rate.
- the raw materials used in the following examples and the like are as follows. ⁇ Cerium nitrate (III) hexahydrate (manufactured by Wako Pure Chemical Industries, Ltd.) ⁇ Cobalt oxide (Co 3 O 4 , manufactured by Fujifilm Wako Pure Chemical Industries, Ltd.) ⁇ Cobalt nitrate (II) hexahydrate (manufactured by Wako Pure Chemical Industries, Ltd.) ⁇ Nickel (II) nitrate hexahydrate (manufactured by Wako Pure Chemical Industries, Ltd.) -Chromium (III) nitrate nine hydrate (manufactured by Strem Chemicals) ⁇ Iron (III) nitrate nine hydrate (manufactured by Fujifilm Wako Pure Chemical Industries, Ltd.) ⁇ Manganese nitrate (II) hexahydrate (man
- the pore filling method that is, 39.0 g of the ⁇ -alumina porous body as a carrier is put into this aqueous solution (impregnated solution), and the ⁇ -alumina porous body and cerium nitrate are brought into contact with each other to bring the carrier (1) ( ⁇ -alumina) into contact with each other.
- a porous body on which cerium nitrate was supported.) was obtained.
- the carrier (1) was air-dried at room temperature for 1 hour, further dried at 60 ° C. for 24 hours, and then calcined in air at 500 ° C. for 2 hours to obtain a chlorine gas decomposition catalyst (1).
- a chlorine gas decomposition catalyst (1) 3.5 g of cobalt oxide is crushed with a planetary ball mill so that D50 becomes 1 ⁇ m in the particle size distribution measured by the average particle size distribution laser diffraction / scattering method, added to 53 mg of pure water, and irradiated with ultrasonic waves. The dispersion was obtained to obtain a dispersion liquid. This dispersion was used as an impregnating solution.
- D50 in the particle size distribution was measured as follows. A small spatula of cobalt oxide powder was placed in a small glass bottle, 2 mL of 98% ethanol was added thereto, and the mixture was ultrasonically dispersed for 5 minutes. This solution was put into a laser diffraction type particle size distribution measuring instrument (Microtrac MT-3000) manufactured by Microtrac Bell, and the volume-based cumulative particle size distribution was measured, and it was confirmed that the 50% particle size (D50) was 1 ⁇ m. ..
- a chlorine gas decomposition catalyst (2) was obtained in the same manner as in Example 1 except that the carrier (1) was changed to the carrier (2).
- Example 3 Same as Example 1 except that 24.4 g of cerium nitrate (III) hexahydrate was changed to 19.2 g of cerium nitrate (III) hexahydrate and 5.8 g of cobalt (II) nitrate hexahydrate. , Chlorine gas decomposition catalyst (3) was obtained.
- Example 4 Same as Example 1 except that 24.4 g of cerium nitrate (III) hexahydrate was changed to 19.2 g of cerium nitrate (III) hexahydrate and 9.7 g of nickel (II) nitrate hexahydrate. , Chlorine gas decomposition catalyst (4) was obtained.
- Example 5 Same as Example 1 except that 24.4 g of cerium nitrate (III) hexahydrate was changed to 24.4 g of cerium nitrate (III) hexahydrate and 13.3 g of chromium (III) nitrate nine hydrate. , Chlorine gas decomposition catalyst (5) was obtained.
- Example 6 Same as Example 1 except that 24.4 g of cerium nitrate (III) hexahydrate was changed to 19.2 g of cerium nitrate (III) hexahydrate and 14.1 g of iron (III) nitrate hydrate. , Chlorine gas decomposition catalyst (6) was obtained.
- Example 7 Same as Example 1 except that 24.4 g of cerium nitrate (III) hexahydrate was changed to 24.2 g of cerium nitrate (III) hexahydrate and 9.4 g of manganese nitrate (II) hexahydrate. , Chlorine gas decomposition catalyst (7) was obtained.
- Example 8 Chlorine in the same manner as in Example 1 except that 24.4 g of cerium nitrate (III) hexahydrate was changed to 19.2 g of cerium nitrate (III) hexahydrate) and 20.6 g of magnesium nitrate hexahydrate. A gas decomposition catalyst (8) was obtained.
- Example 9 Chlorine gas in the same manner as in Example 1 except that 24.4 g of cerium nitrate (III) hexahydrate was changed to 24.4 g of cerium (III) nitrate hexahydrate and 7.8 g of zirconium nitrate dihydrate. A decomposition catalyst (9) was obtained.
- Example 10 24.4 g of cerium nitrate (III) hexahydrate, 19.2 g of cerium nitrate (III) hexahydrate, 5.8 g of cobalt (II) nitrate hexahydrate and 0.
- a chlorine gas decomposition catalyst (10) was obtained in the same manner as in Example 1 except that the amount was changed to 1 g.
- Example 11 13.8 g of cerium nitrate (III) hexahydrate, 3.5 g of cobalt (II) nitrate hexahydrate and 0.1 g of copper (II) nitrate trihydrate are dissolved in 53 mL of pure water, and an aqueous solution (impregnated solution) is used. ) was obtained.
- the pore filling method that is, 39.0 g of the ⁇ -alumina porous body as a carrier is put into this aqueous solution (impregnated solution), and the ⁇ -alumina porous body is brought into contact with cerium nitrate, cobalt nitrate and copper nitrate to support the carrier (the carrier (impregnated solution). 11a) was obtained.
- the carrier (11a) was air-dried at room temperature for 1 hour, further dried at 60 ° C. for 24 hours, and then calcined at 500 ° C. for 2 hours in the air to obtain a carrier (11b).
- a chlorine gas decomposition catalyst (11) was obtained in the same manner as in Example 1 except that the carrier (1) was changed to the carrier (11).
- Example 12 A catalyst for chlorine gas decomposition (12) was obtained in the same manner as in Example 3 except that 39.0 g of the ⁇ -alumina porous body was changed to 39.0 g of the silica porous body.
- Example 13 A catalyst for chlorine gas decomposition (13) was obtained in the same manner as in Example 3 except that 39.0 g of the ⁇ -alumina porous body was changed to 39.0 g of the cozylite porous body.
- Example 14 Same as Example 1 except that 24.4 g of cerium nitrate (III) hexahydrate was changed to 19.2 g of cerium nitrate (III) hexahydrate and 8.4 g of ittrium (III) nitrate hexahydrate. A catalyst for decomposing chlorine gas (14) was obtained.
- Example 15 24.4 g of cerium nitrate (III) hexahydrate to cerium nitrate (III) hexahydrate 19.
- a catalyst for chlorine gas decomposition (15) was obtained in the same manner as in Example 1 except that it was changed to 2 g and 6.1 g of lanthanum nitrate (III) hexahydrate.
- Example 16 Same as Example 1 except that it was changed to 13.8 g of cerium (III) nitrate hexahydrate, 3.5 g of cobalt (II) nitrate hexahydrate and 0.1 g of copper (II) nitrate trihydrate. A catalyst for decomposing chlorine gas (16) was obtained.
- Example 1 A catalyst for chlorine gas decomposition (17) was obtained in the same manner as in Example 1 except that 24.4 g of cerium nitrate (III) hexahydrate was changed to 16.3 g of nickel (II) nitrate hexahydrate. ..
- Example 2 A catalyst for chlorine gas decomposition (18) was obtained in the same manner as in Example 1 except that 24.4 g of cerium nitrate (III) hexahydrate was changed to 22.6 g of iron (III) nitrate hydrate. ..
- the measurement method by XRD is as follows.
- the obtained catalyst was crushed for 10 minutes using an agate mortar to obtain a powder for XRD measurement.
- An X-ray diffraction (XRD) figure was obtained.
- the Inconel reaction tube (volume 70 cc) was filled with the chlorine gas decomposition catalysts obtained in each Example and Comparative Example. At the time of reaction, the amount of each gas is such that the volume ratio of chlorine gas: nitrogen gas: water vapor in the reaction tube is 0.5 : 74.5: 25 (0 ° C, 1.01 ⁇ 105 Pa conversion). Was adjusted, and the mixed gas was supplied to the reaction tube at 5000 cc / min (0 ° C., 1.01 ⁇ 105 Pa conversion) under normal pressure.
- chlorine gas and nitrogen gas were mixed by adjusting the volume ratio by a mass flow controller, and the gas having the adjusted flow rate was introduced into the reaction tube.
- Pure water at room temperature is introduced into the preheating section (400 ° C.) with a pump while measuring the weight so as to have the above volume ratio from an inlet different from the inlet of the mixed gas, vaporized, and introduced into the reaction tube. Then, it was merged with the mixed gas of chlorine gas and nitrogen gas.
- the reaction tube was heated to 500 ° C. in an electric furnace, and sampling was performed by passing the gas at the outlet of the reaction tube through a potassium iodide aqueous solution 1 hour after the start of the reaction, and chlorine gas was quantified by the iodine titration method.
- the decomposition rate of chlorine gas defined by the following formula was measured.
- Decomposition rate (%) ⁇ (0.5-ratio of chlorine gas in outlet gas (volume%)) /0.5 ⁇ ⁇ 100 (However, the ratio of chlorine gas in the outlet gas is converted to the ratio in the standard state (0 ° C, 1.01 ⁇ 105 Pa).) It was confirmed that the composition of the gas discharged from the outlet of the reaction tube became almost constant by circulating the gas whose flow rate was adjusted for 1 hour until the reaction started. The same applies to the case of mixing PFC described later.
- C4 F 8 gas, chlorine gas, and nitrogen gas were mixed by adjusting the volume ratio by a mass flow controller, and the gas having the adjusted flow rate was introduced into the reaction tube.
- Pure water at room temperature is introduced into the preheating section (400 ° C.) with a pump while measuring the weight so as to have the above volume ratio from an inlet different from the inlet of the mixed gas, vaporized, and introduced into the reaction tube. Then, it was merged with the mixed gas of the above C 4 F 8 gas, chlorine gas and nitrogen gas.
- the reaction tube is heated to 750 ° C.
- Decomposition rate (%) ⁇ (0.5-ratio of chlorine gas in outlet gas (volume%)) /0.5 ⁇ ⁇ 100 (However, the ratio of chlorine gas in the outlet gas is converted to the ratio in the standard state (0 ° C, 1.01 ⁇ 105 Pa).) The results are shown in Table 2.
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Abstract
Description
[1]
金属酸化物(X)を含む塩素ガス分解用触媒であって、
前記金属酸化物(X)はCeおよびCoからなる群から選択される少なくとも1種の元素の酸化物(X1)を含む
塩素ガス分解用触媒。
前記酸化物(X1)が酸化セリウムを含む前記[1]の塩素ガス分解用触媒。
[3]
前記酸化物(X1)がCeと、Mg、Cr、Mn、Fe、Co、Ni、CuおよびZrからなる群から選ばれる少なくとも1種の元素Mとの複合酸化物を含む前記[1]または[2]の塩素ガス分解用触媒。
前記金属酸化物(X)が、さらに前記元素M(ただし、Coを除く。)の酸化物を含む前記[3]の塩素ガス分解用触媒。
前記酸化物(X1)が酸化コバルトを含む前記[1]~[4]のいずれかの塩素ガス分解用触媒。
担体と、前記担体に担持された前記金属酸化物(X)とを含む、前記[1]~[5]のいずれかの塩素ガス分解用触媒。
排出ガス中に含まれる塩素ガスを分解するための前記[1]~[6]のいずれかの塩素ガス分解用触媒。
塩素ガスを含む排出ガスが導入される反応器を備え、前記反応器には前記[1]~[7]のいずれかの塩素ガス分解用触媒が備えられている、排出ガス処理装置。
前記排出ガスがパーフルオロ化合物を含む、前記[8]の排出ガス処理装置。
[10]
前記反応器にはパーフルオロ化合物分解用触媒が備えられている、前記[9]の排出ガス処理装置。
前記排出ガスに水を供給する装置を備える、前記[8]~[10]のいずれかの排出ガス処理装置。
前記排出ガスを加熱する加熱装置を備える、前記[8]~[11]のいずれかの排出ガス処理装置。
前記反応器から排出されるガスを冷却する冷却装置を備える、前記[8]~[12]のいずれかの排出ガス処理装置。
前記反応器から排出されたガスから酸性ガスを除去する除去装置を備える、前記[8]~[13]のいずれかの排出ガス処理装置。
前記反応器に供給される前記排出ガスの温度を検出する温度検出器と、前記温度検出器の測定温度に基づいて前記加熱装置を制御する制御装置とを備える、前記[8]~[14]のいずれかの排出ガス処理装置。
塩素ガスを含むガスを水の存在下で前記[1]~[7]のいずれかの塩素ガス分解用触媒と接触させる、塩素ガスの分解方法。
[塩素ガス分解用触媒]
本発明に係る塩素ガス分解用触媒は、金属酸化物(X)を含む塩素ガス分解用触媒であって、前記金属酸化物(X)はCe(セリウム)およびCo(コバルト)からなる群から選択される少なくとも1種の元素の酸化物(X1)(すなわち、Ce(セリウム)および/またはCo(コバルト)の酸化物(X1))を含むことを特徴としている。
前記金属酸化物(X)はCeおよびCoからなる群から選択される少なくとも1種の元素の酸化物(X1)を含む。
(1)酸化セリウム、ならびにCeとMg、Cr、Mn、Fe、Co、Ni、CuおよびZrからなる群から選ばれる少なくとも1種の元素Mとの複合酸化物からなる群から選択される、少なくとも1種のセリウム系酸化物
(2)酸化コバルト、または
(3)セリウム系酸化物(1)および酸化コバルト(2)の両方
を含む。
前記金属元素Mは、好ましくはCr、Mn、Fe、Co、NiおよびCuからなる群から選ばれる少なくとも1種であり、より好ましくはCr、Co、Cuである。
前記(3)の態様における酸化コバルト(2)の割合は、セリウム系酸化物(1)中のセリウム原子1モルに対し、酸化コバルト(2)中のコバルト原子が、好ましくは2.0モル以下、より好ましくは0.1~2.0モル、より好ましくは1.0~1.8モルとなる割合であってもよい。
本発明に係る塩素ガス分解用触媒は、さらに担体を含んでいてもよく、すなわち担体と前記担体に担持された前記金属酸化物(X)とを含む塩素ガス分解用触媒(以下「担持型触媒」とも記載する。)であってもよい。担持型触媒である塩素ガス分解用触媒は、一般に比表面積が大きくなるため、触媒活性を向上させるという観点から好ましい。
また、前記担体は、好ましくは多孔質材料からなり、そのBET法により測定される比表面積は、たとえば100~500cm2/g、好ましくは100~300cm2/gである。
(塩素ガス分解用触媒の製造方法)
本発明に係る塩素ガス分解用触媒のうち担体を含まないものの製造方法の例としては、
金属酸化物(X)の粉末(たとえば、酸化セリウム粉末、酸化コバルト粉末)を、粉砕かつ混合する工程、および
任意に、粉砕かつ混合された前記粉末を500~900℃で、空気中で焼成する工程を含む塩素ガス分解用触媒の製造方法
が挙げられる。
本発明に係る塩素ガス分解用触媒のうち前記担持型触媒の製造方法の例としては、
前記金属酸化物(X)の原料成分を前記担体に含浸させた担持体(すなわち、前記担体に、前記原料成分または前記原料成分中の金属を含む成分を担持したもの)を準備する工程(1)、
前記担持体を焼成して塩素ガス分解用触媒を得る工程(2)
を含む塩素ガス分解用触媒の製造方法
が挙げられる。
前記金属酸化物(X)の原料成分の例としては、Ce、Co、その他の金属元素のそれぞれの塩が挙げられる。前記塩は水和物であってもよい。
前記硝酸塩の具体例としては、硝酸セリウム(III)六水和物、硝酸コバルト(II)六水和物、硝酸ニッケル(II)六水和物、硝酸クロム(III)九水和物、硝酸鉄(III)九水和物、硝酸マンガン(II)六水和物、硝酸マグネシウム六水和物、硝酸ジルコニウム二水和物、および硝酸銅(II)三水和物が挙げられる。
前記原料成分を水に溶解させて含浸液を調製する工程(11a)、および
前記含浸液と前記担体とを接触させ、次いで得られた担持体を回収する工程(12a)
を含む方法(a)、
前記原料成分を水に分散させて含浸液を調製する工程(11b)、および
前記含浸液と前記担体とを接触させ、次いで得られた担持体を回収する工程(12b)
を含む方法(b)、または
前記原料成分を水に溶解させて含浸液を調製する工程(11a)、
前記原料成分を水に分散させて含浸液を調製する工程(11b)、および
2つの前記含浸液と前記担体とを接触させ、次いで得られた担持体を回収する工程(12c)
を含む方法(c)
により実施される。
前記原料成分として前記酸化物のみが使用される場合には、好ましくは前記方法(b)が実施される。
前記工程(12c)の態様の例としては、
2つの前記含浸液を混合し、得られた混合液と前記担体とを接触させ、次いで得られた担持体を回収する態様、および
一方の前記含浸液と前記担体とを接触させ、次いで得られた担持体を回収し、この担持体ともう一方の前記含浸液とを接触させ、次いで得られた担持体を回収する態様
が挙げられる。
前記含浸液と前記担体とを接触させることで、前記原料成分を担体の表面に、前記担体が多孔質材料からなる場合にはさらに細孔内に、高い分散性で安定に担持することができる。
前記含浸液と前記担体との接触は、室温付近(たとえば5~40℃)で行ってもよく、加熱によりさらに高い温度(たとえば40~85℃)で行ってもよい。
乾燥は、たとえば以下の条件下で行われる。
時間:0.5~50時間
圧力:常圧または減圧下
雰囲気:空気、不活性ガス(たとえば、アルゴンガス、窒素ガス、ヘリウムガス)、酸素ガス、またはこれらの混合ガス
<工程(2)>
工程(2)では、工程(1)で得られた担持体を焼成し、塩素ガス分解用触媒を得る。
温度:300~1200℃、好ましくは400~800℃
時間:0.5~10時間、好ましくは1~3時間
圧力:常圧、減圧または加圧
雰囲気:空気、不活性ガス(たとえば、アルゴンガス、窒素ガス、ヘリウムガス)、酸素ガスまたはこれらの混合ガス
この焼成により得られる触媒中で、金属成分は、酸化物または複合酸化物の形態で担体に高度に分散した状態で担持されている。
本発明に係る排出ガス処理装置は、塩素ガスを含む排出ガスが導入される容器、すなわち反応器を備え、前記反応器には本発明に係る塩素ガス分解用触媒が備えられていることを特徴としている。
図18は、本発明の排出ガス処理装置の一態様の構成図である。本態様の排出ガス処理装置1は、排出ガス(塩素ガスを含む、パーフルオロ化合物ガス(以下「PFCガス」とも記載する。)または酸性ガス)に対して、スプレー2により注水が行われる第1スクラバー3、第1スクラバー3を通過した排出ガス、純水および空気を導入して排出ガス中の塩素ガスの分解反応を行う反応器5、反応器5を通過した排出ガスを冷却する冷却器7、冷却器7を通過した排出ガスにスプレー9により注水が行われる第2スクラバー10、第2スクラバー10を通過した処理済み排出ガスを系外に送り出すためのブロワー11、および冷却器7から回収された排水を回収するタンク13を備えている。
前記反応器5は、排出ガスの種類、排出ガス処理装置の規模等に応じて、適宜設定することができる。
前記反応器5には、前記塩素ガス分解用触媒4と共にパーフルオロ化合物分解用触媒14(図示せず)が備えられていてもよい。パーフルオロ化合物分解用触媒14は、従来公知の触媒、たとえばニッケル酸化物触媒であってもよい。
前記塩素ガス分解用触媒4、および前記パーフルオロ化合物分解用触媒14は、それぞれ前記反応器5の内部に充填されていてもよく、前記反応器5の内壁に触媒層として備えられていてもよい。
本発明に係る排出ガス処理装置1は、好ましくは、前記反応器5に導入する排出ガスに水を供給する装置を備えている。この装置を備えることにより、排出ガスが元来水を含まない場合であっても、後述する塩素ガスの分解反応を円滑に行うことができる。
たとえば、前記反応器5は、反応器5内を、塩素ガスの分解反応を行う温度に加熱するための加熱装置6(例えば反応器周囲に設置されたヒーター)を備えていてもよく、あるいは、前記排出ガス処理装置1は、塩素ガスを含む排出ガスを、前記反応器5に導入する前に塩素ガスの分解反応を行う温度に加熱するための加熱装置6(たとえばヒーター)を備えていてもよい。
前記排出ガス処理装置1は、好ましくは、前記反応器5から排出され前記冷却装置を通過したガスから酸性ガス(塩化水素ガス、フッ化水素ガス)を除去する除去装置(たとえば、第2スクラバー10)を備えている。
本発明に係る塩素ガスの分解方法は、塩素ガスを含むガスを水の存在下で本発明に係る塩素ガス分解用触媒と接触させることを特徴としている。
塩素ガスを含むガス中の塩素ガスの割合は、25℃かつ1気圧で、たとえば0.1~10体積%であり、好ましくは0.1~1体積%である。
塩素ガスの分解反応は、たとえば以下の条件下で行われる。
圧力:常圧若しくは加圧、好ましくは常圧
本発明に係る塩素ガスの分解方法によれば、高い分解率で塩素ガス、とりわけ排出ガス中に含まれる塩素ガスを分解することができる。
(原料)
以下の実施例等で用いられた原料は以下のとおりである。
・硝酸セリウム(III)六水和物(富士フイルム和光純薬(株)製)
・酸化コバルト(Co3O4、富士フイルム和光純薬(株)製)
・硝酸コバルト(II)六水和物(富士フイルム和光純薬(株)製)
・硝酸ニッケル(II)六水和物(富士フイルム和光純薬(株)製)
・硝酸クロム(III)九水和物(Strem Chemicals社製)
・硝酸鉄(III)九水和物(富士フイルム和光純薬(株)製
・硝酸マンガン(II)六水和物(富士フイルム和光純薬(株)製)
・硝酸マグネシウム六水和物(富士フイルム和光純薬(株)製)
・硝酸ジルコニウム二水和物(富士フイルム和光純薬(株)製)
・硝酸銅(II)三水和物(富士フイルム和光純薬(株)製)
・硝酸イットリウム(III)六水和物(富士フイルム和光純薬(株)製)
・硝酸ランタン(III)六水和物(富士フイルム和光純薬(株)製)
・γ-アルミナ多孔体(直径3mm、球状、γ-Al2O3)
・コージライト多孔体(直径3mm、球状、2MgO・2Al2O3・5SiO2)
・シリカ多孔体(直径3mm、球状、SiO2)
(触媒作製)
[実施例1]
硝酸セリウム(III)六水和物24.4gを純水53mLに溶解し、水溶液(含浸液)を得た。ポアフィリング法により、すなわちこの水溶液(含浸液)に担体としてのγ-アルミナ多孔体39.0gを入れて、γ-アルミナ多孔体と硝酸セリウムとを接触させ、担持体(1)(γ-アルミナ多孔体に硝酸セリウムが担持されたもの。)を得た。
[実施例2]
酸化コバルト3.5gを、遊星ボールミルで、平均粒度分布レーザー回折・散乱法で測定される粒度分布においてD50が1μmになるように破砕し、純水53mgの中に加え、超音波を照射して分散させて分散液を得た。この分散液を含浸液として用いた。
酸化コバルトの粉体を極小型スパーテル1杯分を小型のガラス瓶に入れ、そこに98%エタノール2mLを添加し、5分間超音波にて分散させた。この溶液をマイクロトラックベル社製レーザー回折式粒度分布測定器(マイクロトラックMT-3000)に投入し、体積基準累積粒度分布を測定し、50%粒子径(D50)が1μmである事を確認した。
[実施例3]
硝酸セリウム(III)六水和物24.4gを硝酸セリウム(III)六水和物19.2gおよび硝酸コバルト(II)六水和物5.8gに変更したこと以外は実施例1同様にして、塩素ガス分解用触媒(3)を得た。
硝酸セリウム(III)六水和物24.4gを硝酸セリウム(III)六水和物19.2gおよび硝酸ニッケル(II)六水和物9.7gに変更したこと以外は実施例1同様にして、塩素ガス分解用触媒(4)を得た。
硝酸セリウム(III)六水和物24.4gを硝酸セリウム(III)六水和物24.4gおよび硝酸クロム(III)九水和物13.3gに変更したこと以外は実施例1同様にして、塩素ガス分解用触媒(5)を得た。
硝酸セリウム(III)六水和物24.4gを硝酸セリウム(III)六水和物19.2gおよび硝酸鉄(III)九水和物14.1gに変更したこと以外は実施例1同様にして、塩素ガス分解用触媒(6)を得た。
硝酸セリウム(III)六水和物24.4gを硝酸セリウム(III)六水和物24.2gおよび硝酸マンガン(II)六水和物9.4gに変更したこと以外は実施例1同様にして、塩素ガス分解用触媒(7)を得た。
硝酸セリウム(III)六水和物24.4gを硝酸セリウム(III)六水和物)19.2gおよび硝酸マグネシウム六水和物20.6gに変更したこと以外は実施例1同様にして、塩素ガス分解用触媒(8)を得た。
硝酸セリウム(III)六水和物24.4gを硝酸セリウム(III)六水和物24.4gおよび硝酸ジルコニウム二水和物7.8gに変更したこと以外は実施例1同様にして、塩素ガス分解用触媒(9)を得た。
硝酸セリウム(III)六水和物24.4gを硝酸セリウム(III)六水和物19.2g、硝酸コバルト(II)六水和物5.8gおよび硝酸銅(II)三水和物0.1gに変更したこと以外は実施例1同様にして、塩素ガス分解用触媒(10)を得た。
硝酸セリウム(III)六水和物13.8g、硝酸コバルト(II)六水和物3.5gおよび硝酸銅(II)三水和物0.1gを純水53mLに溶解し、水溶液(含浸液)を得た。ポアフィリング法により、すなわちこの水溶液(含浸液)に担体としてのγ-アルミナ多孔体39.0gを入れて、γ-アルミナ多孔体と硝酸セリウム、硝酸コバルトおよび硝酸銅とを接触させ、担持体(11a)を得た。担持体(11a)を室温で1時間風乾燥し、さらに60℃で24時間乾燥した後、500℃で2時間、空気中で焼成し、担持体(11b)を得た。
[実施例12]
γ-アルミナ多孔体39.0gをシリカ多孔体39.0gに変更したこと以外は実施例3と同様にして、塩素ガス分解用触媒(12)を得た。
γ-アルミナ多孔体39.0gをコージライト多孔体39.0gに変更したこと以外は実施例3と同様にして、塩素ガス分解用触媒(13)を得た。
硝酸セリウム(III)六水和物24.4gを硝酸セリウム(III)六水和物19.2gおよび硝酸イットリウム(III)六水和物8.4gに変更したこと以外は実施例1と同様にして、塩素ガス分解用触媒(14)を得た。
硝酸セリウム(III)六水和物24.4gを硝酸セリウム(III)六水和物19.
2gおよび硝酸ランタン(III)六水和物6.1gに変更したこと以外は実施例1と同にして、塩素ガス分解用触媒(15)を得た。
硝酸セリウム(III)六水和物13.8g、硝酸コバルト(II)六水和物3.5gおよび硝酸銅(II)三水和物0.1gに変更したこと以外は実施例1と同様にして、塩素ガス分解用触媒(16)を得た。
硝酸セリウム(III)六水和物24.4gを硝酸ニッケル(II)六水和物16.3gに変更したこと以外は実施例1と同様にして、塩素ガス分解用触媒(17)を得た。
硝酸セリウム(III)六水和物24.4gを硝酸鉄(III)九水和物22.6gに変更したこと以外は実施例1と同様にして、塩素ガス分解用触媒(18)を得た。
各実施例および比較例で得られた塩素ガス分解用触媒をXRD測定した結果、図1~19に示すように、各成分を含む酸化物もしくはそれらの成分を含む複合酸化物が確認できた。確認できなかった触媒については、元素分析(誘導結合プラズマ法(ICP-AES法))にて確認できた。
XRDによる測定法は、以下のとおりである。
得られた触媒を、メノウ乳鉢を用いて10分間解砕して、XRD測定用の粉末を得た。粉末X線回折測定装置(パナリティカルMPD スペクトリス株式会社製)を用い、得られたXRD測定用の粉末のX線回折測定(Cu-Kα線(出力45kV、40mA)、回折角度2θ=10~80°の範囲、ステップ幅:0.013°、入射側Sollerslit:0.04rad、入射側Anti-scatter slit:2°、受光側Sollerslit:0.04rad、受光側Anti-scatter slit:5mm)を行い、X線回折(XRD)図形を得た。
メノウ乳鉢で摩砕した触媒約0.01gを石英ビーカーに量りとり、HCl、H2SO4、HNO3のいずれかにより酸分解を行って溶解させた。放冷後100mLに定容し、ICP-AES法による定性分析を行い、触媒中に0.05重量%以上含まれる前記金属元素Mの量を、Ce原子1モルに対する割合に換算した。なお、分析はn=1で行った。(装置:Agilent 5110(Agilent technology))
(塩素ガス分解測定)
インコネル製反応管(体積70cc)に、各実施例および比較例で得られた塩素ガス分解用触媒を充填した。反応時、反応管内の塩素ガス:窒素ガス:水蒸気の体積比が0.5:74.5:25(0℃、1.01×105Pa換算)の混合ガスになるように、各ガス量を調整し、混合ガスを5000cc/分(0℃、1.01×105Pa換算)、常圧下で反応管に供給した。具体的には、マスフローコントローラーにて塩素ガスと窒素ガスとを、体積比を調整して混合し、この流量を調整したガスを反応管に導入した。混合ガスの流入口とは別の流入口から常温の純水を、上記の体積比になるよう重量を測定しながらポンプにて予熱部(400℃)に導入して気化させ、反応管に導入し、上記塩素ガスと窒素ガスの混合ガスに合流させた。反応管を電気炉で500℃に加熱し、反応開始1時間後の時点で反応管の出口のガスをヨウ化カリウム水溶液に流通させることによりサンプリングを行い、ヨウ素滴定法により塩素ガスを定量し、下式で定義される塩素ガスの分解率を測定した。
(ただし、出口ガス中の塩素ガスの割合は、標準状態(0℃、1.01×105Pa)での割合に換算したものである。)
なお流量を調整したガスを反応開始まで1時間流通させることにより、反応管の出口から排出されるガスの組成はほぼ一定になることを確認した。後述のPFC混合時の場合も同様である。
(PFC混合時の塩素ガス分解測定)
PFC混合時の塩素ガス分解率を測定するために、インコネル製反応管(体積70cc)に、実施例16で得られた塩素ガス分解用触媒を充填した。反応時、反応管内のC4F8ガス:塩素ガス:窒素ガス:水蒸気の体積比が0.5:0.5:84:15(0℃、1.01×105Pa換算)の混合ガスになるように、各ガス量を調整し、混合ガスを5000cc/分(0℃、1.01×105Pa換算)、常圧下で反応管に供給した。具体的には、マスフローコントローラーにてC4F8ガスと塩素ガスと窒素ガスとを、体積比を調整して混合し、この流量を調整したガスを反応管に導入した。混合ガスの流入口とは別の流入口から常温の純水を、上記の体積比になるよう重量を測定しながらポンプにて予熱部(400℃)に導入して気化させ、反応管に導入し、上記C4F8ガスと塩素ガスと窒素ガスの混合ガスに合流させた。反応管を、PFCガスであるC4F8ガスの高い分解率が得られるように、電気炉で750℃に加熱し、反応開始1時間後の時点で反応管の出口のガスをヨウ化カリウム水溶液に流通させることによりサンプリングを行い、ヨウ素滴定法により塩素ガスを定量し、下式で定義される塩素ガスの分解率を測定した。
(ただし、出口ガス中の塩素ガスの割合は、標準状態(0℃、1.01×105Pa)での割合に換算したものである。)
結果を表2に示す。
2…スプレー
3…第1スクラバー
4…塩素ガス分解用触媒
5…反応容器
6…加熱装置
7…冷却器
8…冷却装置(スプレー)
9…スプレー
10…第2スクラバー
11…ブロワー
12…ポンプ
13…タンク
Claims (16)
- 金属酸化物(X)を含む塩素ガス分解用触媒であって、
前記金属酸化物(X)はCeおよびCoからなる群から選択される少なくとも1種の元素の酸化物(X1)を含む
塩素ガス分解用触媒。 - 前記酸化物(X1)が酸化セリウムを含む請求項1に記載の塩素ガス分解用触媒。
- 前記酸化物(X1)がCeと、Mg、Cr、Mn、Fe、Co、Ni、CuおよびZrからなる群から選ばれる少なくとも1種の元素Mとの複合酸化物を含む請求項1または2に記載の塩素ガス分解用触媒。
- 前記金属酸化物(X)が、さらに前記元素M(ただし、Coを除く。)の酸化物を含む請求項3に記載の塩素ガス分解用触媒。
- 前記酸化物(X1)が酸化コバルトを含む請求項1~4のいずれか一項に記載の塩素ガス分解用触媒。
- 担体と、前記担体に担持された前記金属酸化物(X)とを含む、請求項1~5のいずれか一項に記載の塩素ガス分解用触媒。
- 排出ガス中に含まれる塩素ガスを分解するための請求項1~6のいずれか一項に記載の塩素ガス分解用触媒。
- 塩素ガスを含む排出ガスが導入される反応器を備え、前記反応器には請求項1~7のいずれか一項に記載の塩素ガス分解用触媒が備えられている、排出ガス処理装置。
- 前記排出ガスがパーフルオロ化合物を含む、請求項8に記載の排出ガス処理装置。
- 前記反応器にはパーフルオロ化合物分解用触媒が備えられている、請求項9に記載の排出ガス処理装置。
- 前記排出ガスに水を供給する装置を備える、請求項8~10のいずれか一項に記載の排出ガス処理装置。
- 前記排出ガスを加熱する加熱装置を備える、請求項8~11のいずれか一項に記載の排出ガス処理装置。
- 前記反応器から排出されるガスを冷却する冷却装置を備える、請求項8~12のいずれか一項に記載の排出ガス処理装置。
- 前記反応器から排出されたガスから酸性ガスを除去する除去装置を備える、請求項8~13のいずれか一項に記載の排出ガス処理装置。
- 前記反応器に供給される前記排出ガスの温度を検出する温度検出器と、前記温度検出器の測定温度に基づいて前記加熱装置を制御する制御装置とを備える、請求項8~14のいずれか一項に記載の排出ガス処理装置。
- 塩素ガスを含むガスを水の存在下で請求項1~7のいずれか一項に記載の塩素ガス分解用触媒と接触させる、塩素ガスの分解方法。
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