US20110005975A1 - Method for removing mercury from hydrocarbon streams - Google Patents
Method for removing mercury from hydrocarbon streams Download PDFInfo
- Publication number
- US20110005975A1 US20110005975A1 US12/921,579 US92157909A US2011005975A1 US 20110005975 A1 US20110005975 A1 US 20110005975A1 US 92157909 A US92157909 A US 92157909A US 2011005975 A1 US2011005975 A1 US 2011005975A1
- Authority
- US
- United States
- Prior art keywords
- mercury
- weight
- absorbent
- oxide
- copper
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 title claims abstract description 57
- 229910052753 mercury Inorganic materials 0.000 title claims abstract description 56
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 42
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 41
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 36
- 238000000034 method Methods 0.000 title claims abstract description 35
- 239000002250 absorbent Substances 0.000 claims abstract description 33
- 230000002745 absorbent Effects 0.000 claims abstract description 33
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 19
- 239000001257 hydrogen Substances 0.000 claims abstract description 19
- 229910052802 copper Inorganic materials 0.000 claims abstract description 17
- 239000010949 copper Substances 0.000 claims abstract description 17
- 239000000463 material Substances 0.000 claims abstract description 16
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims abstract description 15
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 16
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 claims description 16
- 239000007788 liquid Substances 0.000 claims description 14
- QPLDLSVMHZLSFG-UHFFFAOYSA-N Copper oxide Chemical compound [Cu]=O QPLDLSVMHZLSFG-UHFFFAOYSA-N 0.000 claims description 10
- QDOXWKRWXJOMAK-UHFFFAOYSA-N dichromium trioxide Chemical compound O=[Cr]O[Cr]=O QDOXWKRWXJOMAK-UHFFFAOYSA-N 0.000 claims description 10
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 10
- QVQLCTNNEUAWMS-UHFFFAOYSA-N barium oxide Chemical compound [Ba]=O QVQLCTNNEUAWMS-UHFFFAOYSA-N 0.000 claims description 9
- 239000000377 silicon dioxide Substances 0.000 claims description 8
- 239000011787 zinc oxide Substances 0.000 claims description 8
- 235000012239 silicon dioxide Nutrition 0.000 claims description 7
- 239000005751 Copper oxide Substances 0.000 claims description 6
- 229910000431 copper oxide Inorganic materials 0.000 claims description 6
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 6
- 239000000395 magnesium oxide Substances 0.000 claims description 5
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 4
- 239000000725 suspension Substances 0.000 claims description 3
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 18
- 239000000203 mixture Substances 0.000 description 18
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 14
- 239000003054 catalyst Substances 0.000 description 12
- 239000000243 solution Substances 0.000 description 12
- 229910052751 metal Inorganic materials 0.000 description 7
- 239000002184 metal Substances 0.000 description 7
- 150000001875 compounds Chemical class 0.000 description 6
- 239000007789 gas Substances 0.000 description 6
- BRMYZIKAHFEUFJ-UHFFFAOYSA-L mercury diacetate Chemical compound CC(=O)O[Hg]OC(C)=O BRMYZIKAHFEUFJ-UHFFFAOYSA-L 0.000 description 6
- 238000002474 experimental method Methods 0.000 description 5
- 229910052709 silver Inorganic materials 0.000 description 5
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- 238000005984 hydrogenation reaction Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 4
- 239000008188 pellet Substances 0.000 description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical class [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 3
- 229910000497 Amalgam Inorganic materials 0.000 description 3
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 3
- 229910052782 aluminium Inorganic materials 0.000 description 3
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 3
- 229910052785 arsenic Inorganic materials 0.000 description 3
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- OMZSGWSJDCOLKM-UHFFFAOYSA-N copper(II) sulfide Chemical compound [S-2].[Cu+2] OMZSGWSJDCOLKM-UHFFFAOYSA-N 0.000 description 3
- 239000011521 glass Substances 0.000 description 3
- 229910052737 gold Inorganic materials 0.000 description 3
- 239000010931 gold Substances 0.000 description 3
- 150000002739 metals Chemical class 0.000 description 3
- KDLHZDBZIXYQEI-UHFFFAOYSA-N palladium Substances [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 3
- 239000004332 silver Substances 0.000 description 3
- OAKJQQAXSVQMHS-UHFFFAOYSA-N Hydrazine Chemical compound NN OAKJQQAXSVQMHS-UHFFFAOYSA-N 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 229910052946 acanthite Inorganic materials 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 2
- 229910000323 aluminium silicate Inorganic materials 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 125000004432 carbon atom Chemical group C* 0.000 description 2
- 238000004581 coalescence Methods 0.000 description 2
- 229910052593 corundum Inorganic materials 0.000 description 2
- HWMTUNCVVYPZHZ-UHFFFAOYSA-N diphenylmercury Chemical compound C=1C=CC=CC=1[Hg]C1=CC=CC=C1 HWMTUNCVVYPZHZ-UHFFFAOYSA-N 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000003949 liquefied natural gas Substances 0.000 description 2
- 239000003915 liquefied petroleum gas Substances 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 229910044991 metal oxide Inorganic materials 0.000 description 2
- 150000004706 metal oxides Chemical class 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 229910052763 palladium Inorganic materials 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910001845 yogo sapphire Inorganic materials 0.000 description 2
- 239000005995 Aluminium silicate Substances 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 239000005749 Copper compound Substances 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- MCMNRKCIXSYSNV-UHFFFAOYSA-N ZrO2 Inorganic materials O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- WRYNUJYAXVDTCB-UHFFFAOYSA-M acetyloxymercury Chemical compound CC(=O)O[Hg] WRYNUJYAXVDTCB-UHFFFAOYSA-M 0.000 description 1
- 125000002723 alicyclic group Chemical group 0.000 description 1
- 125000001931 aliphatic group Chemical group 0.000 description 1
- 150000001338 aliphatic hydrocarbons Chemical class 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 150000004703 alkoxides Chemical class 0.000 description 1
- 235000012211 aluminium silicate Nutrition 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 229960000892 attapulgite Drugs 0.000 description 1
- 239000000440 bentonite Substances 0.000 description 1
- 229910000278 bentonite Inorganic materials 0.000 description 1
- SVPXDRXYRYOSEX-UHFFFAOYSA-N bentoquatam Chemical compound O.O=[Si]=O.O=[Al]O[Al]=O SVPXDRXYRYOSEX-UHFFFAOYSA-N 0.000 description 1
- 229910052797 bismuth Inorganic materials 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 229910000428 cobalt oxide Inorganic materials 0.000 description 1
- IVMYJDGYRUAWML-UHFFFAOYSA-N cobalt(ii) oxide Chemical compound [Co]=O IVMYJDGYRUAWML-UHFFFAOYSA-N 0.000 description 1
- 229910052681 coesite Inorganic materials 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 150000001879 copper Chemical class 0.000 description 1
- 150000001880 copper compounds Chemical class 0.000 description 1
- 229910052906 cristobalite Inorganic materials 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 238000010908 decantation Methods 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- -1 heterocyclic hydrocarbons Chemical class 0.000 description 1
- 231100000086 high toxicity Toxicity 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000010297 mechanical methods and process Methods 0.000 description 1
- 229910000000 metal hydroxide Inorganic materials 0.000 description 1
- 150000004692 metal hydroxides Chemical class 0.000 description 1
- 229910052976 metal sulfide Inorganic materials 0.000 description 1
- 229940008718 metallic mercury Drugs 0.000 description 1
- 229910000480 nickel oxide Inorganic materials 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- GNRSAWUEBMWBQH-UHFFFAOYSA-N oxonickel Chemical compound [Ni]=O GNRSAWUEBMWBQH-UHFFFAOYSA-N 0.000 description 1
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 description 1
- 229910052625 palygorskite Inorganic materials 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- XEBWQGVWTUSTLN-UHFFFAOYSA-M phenylmercury acetate Chemical compound CC(=O)O[Hg]C1=CC=CC=C1 XEBWQGVWTUSTLN-UHFFFAOYSA-M 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000010944 silver (metal) Substances 0.000 description 1
- 229940056910 silver sulfide Drugs 0.000 description 1
- XUARKZBEFFVFRG-UHFFFAOYSA-N silver sulfide Chemical compound [S-2].[Ag+].[Ag+] XUARKZBEFFVFRG-UHFFFAOYSA-N 0.000 description 1
- FSJWWSXPIWGYKC-UHFFFAOYSA-M silver;silver;sulfanide Chemical compound [SH-].[Ag].[Ag+] FSJWWSXPIWGYKC-UHFFFAOYSA-M 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 229910052682 stishovite Inorganic materials 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052718 tin Inorganic materials 0.000 description 1
- 239000011135 tin Substances 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
- 229910052905 tridymite Inorganic materials 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
- 239000011701 zinc Substances 0.000 description 1
Classifications
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- 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
- C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
- C10G25/003—Specific sorbent material, not covered by C10G25/02 or C10G25/03
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/11—Purification; Separation; Use of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
-
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
- B01D15/08—Selective adsorption, e.g. chromatography
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- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/0203—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising compounds of metals not provided for in B01J20/04
- B01J20/0233—Compounds of Cu, Ag, Au
- B01J20/0237—Compounds of Cu
-
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- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/04—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising compounds of alkali metals, alkaline earth metals or magnesium
- B01J20/041—Oxides or hydroxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01J20/08—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising oxides or hydroxides of metals not provided for in group B01J20/04 comprising aluminium oxide or hydroxide; comprising bauxite
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- B01J20/103—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate comprising silica
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J20/32—Impregnating or coating ; Solid sorbent compositions obtained from processes involving impregnating or coating
- B01J20/3202—Impregnating or coating ; Solid sorbent compositions obtained from processes involving impregnating or coating characterised by the carrier, support or substrate used for impregnation or coating
- B01J20/3204—Inorganic carriers, supports or substrates
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- B01J20/3236—Inorganic material layers containing metal, other than zeolites, e.g. oxides, hydroxides, sulphides or salts
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- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/345—Regenerating or reactivating using a particular desorbing compound or mixture
- B01J20/3458—Regenerating or reactivating using a particular desorbing compound or mixture in the gas phase
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- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/3483—Regenerating or reactivating by thermal treatment not covered by groups B01J20/3441 - B01J20/3475, e.g. by heating or cooling
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- 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
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/85—Chromium, molybdenum or tungsten
- B01J23/86—Chromium
- B01J23/868—Chromium copper and chromium
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- 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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/202—Hydrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/112—Metals or metal compounds not provided for in B01D2253/104 or B01D2253/106
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/60—Heavy metals or heavy metal compounds
- B01D2257/602—Mercury or mercury compounds
-
- 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
- B01J2220/00—Aspects relating to sorbent materials
- B01J2220/50—Aspects relating to the use of sorbent or filter aid materials
- B01J2220/56—Use in the form of a bed
-
- 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
- B01J23/72—Copper
Definitions
- the invention relates to a method of removing mercury and/or arsenic from a mercury-comprising hydrocarbon stream.
- Mercury is present as impurity in numerous streams of materials which are obtained or processed in the chemical or petrochemical industry. These are often streams which are obtained in the processing or thermal utilization of fossil raw materials such as petroleum, natural gas or coal and in the utilization of wastes, since these raw materials or wastes comprise traces of mercury in elemental form or in chemically bound form. Streams comprising mercury as impurity are also obtained in processes in which mercury or mercury-comprising substances are used as reagent or catalyst. An example which may be mentioned is the electrolysis hydrogen obtained in the production of chlorine by the amalgam process. Because of the high toxicity of mercury, it is in most cases necessary to separate off this metal or compounds comprising this metal from the streams obtained in the processes concerned.
- mercury has the property of attacking apparatuses comprising aluminum by amalgam formation with destruction of the oxide layer on the surface of the aluminum, so that streams which pass through apparatuses or vessels made of aluminum have to be virtually mercury-free.
- catalysts comprising noble metals, as are used, for example, in petrochemical processes, are poisoned by traces of mercury.
- EP-A 0 761 830 discloses a simple, purely mechanical method in which finely divided mercury is collected by coalescence to form larger droplets of mercury which are easy to separate off.
- WO 2004/048624 describes a method of removing mercury by filtration through electrographite.
- DE-A 26 43 478 describes the separation of mercury from liquids by adsorption on activated carbon having a specific surface area of at least 250 m 2 /g.
- Carbon-based adsorbents are used, inter alia, for the removal of mercury from streams of materials, as described in U.S. Pat. No. 3,755,989.
- U.S. Pat. No. 4,500,327 describes sulfur-impregnated activated carbon for removing mercury from gaseous streams, while JP 52-53793 describes the use of iodide-comprising activated carbon for removing mercury from liquid streams.
- EP-A 0 385 742 describes a process for removing mercury from liquid hydrocarbon streams comprising hydrocarbons having up to 8 carbon atoms by bringing the streams into contact with metallic copper or copper compounds present on a support.
- DE-A 21 02 039 discloses a process for removing mercury from gases, in which the mercury-comprising gases are brought into contact with a composition comprising copper on a porous aluminum oxide support.
- U.S. Pat. No. 4,230,486 discloses a process for removing mercury from liquids by passing the liquids over an absorbent comprising metallic silver on a porous support such as activated carbon or a ceramic support.
- DE-A 42 21 207 teaches a process for removing mercury from alkaline metal hydroxide solution or alkaline metal alkoxide solution by passing the solutions over silver-coated fibers.
- DE-A 41 16 890 discloses absorbents for removing mercury, which comprise, in particular, Cu, Ag, Fe and Bi, or else Au, Sn, Zn and Pd and also mixtures of the metals mentioned in metallic or oxidic or sulfidic form on an activated carbon support having a BET surface area of from 300 to 1000 m 2 /g.
- U.S. Pat. No. 4,911,825 describes the removal of mercury and arsenic from hydrocarbon streams by bringing these into contact with a catalyst comprising nickel and palladium on aluminum oxide in the presence of hydrogen in a first step and into contact with an absorbent comprising sulfur or a metal sulfide, preferably copper sulfide or a combination of copper sulfide and silver sulfide, on a support in a second step.
- the process can also be carried out in a single stage over a mixture of the catalyst and the absorbent.
- FR-A 2 310 795 describes the removal of mercury from a gaseous natural gas stream using an absorbent comprising metallic gold, silver, copper or nickel on a support composed of silicon dioxide, aluminum oxide or an aluminosilicate having a BET surface area of from 40 to 250 m 2 /g.
- WO 91/15559 discloses a method of removing mercury from liquid hydrocarbon streams by bringing them into contact with an absorbent produced by mixing of a pulverulent oxide, preferably an oxide selected from among nickel oxide, copper oxide and cobalt oxide, with a porous support material such as aluminum oxide, silicon dioxide, zeolites or clays and subsequent reduction.
- This object is achieved by a method of removing mercury from a mercury-comprising hydrocarbon stream, in which the hydrocarbon stream is brought into contact with an absorbent comprising copper on a porous oxidic support material, wherein the hydrocarbon stream is brought into contact with the absorbent in the presence of hydrogen.
- the absorbent used according to the invention comprises copper, preferably in reduced form, on a porous support material.
- the absorbent used according to the invention is effective as hydrogenation catalyst.
- Suitable porous support materials are amorphous and crystalline aluminosilicates, aluminum oxide, silicon dioxide, clays and metal oxides.
- Suitable clays are, for example, attapulgite, kaolin, bentonite, Fuller's earth.
- Suitable metal oxides are, for example, aluminum oxides and silicon dioxide and also magnesium oxide, zirconium dioxide, titanium dioxide, zinc oxide, chromium(III) oxide, barium oxide and mixtures thereof.
- a preferred aluminum oxide is ⁇ -aluminum oxide.
- the copper comprising hydrogenation-active absorbents used according to the invention can be obtained by mixing of copper oxide with a support material and subsequent conversion of copper into the metallic form by reduction, preferably in a stream of hydrogen.
- the absorbents used according to the invention can also be produced by impregnation of the support material with an aqueous solution of a copper salt, drying, if appropriate calcination and conversion of the copper into the metallic form by reduction, preferably by means of a hydrogen-comprising gas stream, although it is also possible to use a reducing agent such as hydrazine.
- the absorbent used according to the invention copper is generally present in reduced, i.e. metallic (elemental), form finely dispersed on the support material.
- the absorbents used according to the invention comprise from 10 to 50% by weight of copper on an oxidic support material.
- suitable compositions on the basis of which the absorbents used according to the invention are obtained are compositions comprising copper oxide, zinc oxide and aluminum oxide or compositions comprising copper oxide, magnesium oxide, barium oxide, chromium(III) oxide, zinc oxide and silicon dioxide.
- Particular preference is given to a mixture of from 10 to 60% by weight of copper oxide, from 0 to 40% by weight of zinc oxide, from 0 to 20% by weight of aluminum oxide, from 5 to 25% by weight of magnesium oxide, from 10 to 40% by weight of silicon dioxide, from 0 to 5% by weight of chromium(III) oxide and from 0 to 10% by weight of barium oxide.
- Hydrocarbon streams from which mercury can be removed according to the invention are any hydrocarbon streams which can be contaminated with mercury. These generally comprise aliphatic, aromatic, alicyclic and/or heterocyclic hydrocarbons having from 1 to 14 carbon atoms.
- hydrocarbon mixtures which can be freed of mercury according to the invention are LNG (liquefied natural gas), LPG (liquefied petroleum gas), naphtha and kerosene.
- pure hydrocarbons which can be purified according to the invention are ethylene and propylene and also aliphatic hydrocarbons.
- the mercury content of the hydrocarbons or hydrocarbon mixtures before carrying out the method of the invention can be up to 100 ppm, but is generally up to 1 ppm of Hg.
- Mercury is generally present in the form of organomercury compounds.
- the method of the invention can be carried out in the suspension mode or the fixed-bed mode. If it is carried out in the fixed-bed mode, it can be carried out in the upflow or downflow mode.
- the hydrocarbons or hydrocarbon mixtures comprising mercury or arsenic can be used in gaseous or liquid form.
- the hydrocarbons or hydrocarbon mixtures are preferably used in liquid form.
- Hydrogen is introduced together with the gaseous or liquid hydrocarbon or hydrocarbon mixture into a suitable reaction vessel and passed, generally in cocurrent, over the particulate absorbent present in a fixed bed. This can be carried out in the upflow or downflow mode. However, hydrogen and hydrocarbon or hydrocarbon mixture can also be passed over the bed of absorbent in countercurrent.
- the absorbent can also be present in suspension in the hydrocarbon or hydrocarbon mixture.
- the method is carried out at a temperature of from 30 to 250° C., preferably from 60 to 180° C., and a hydrogen pressure of from 1 to 20 bar.
- the pressure is preferably selected so that the hydrocarbon or the hydrocarbon mixture is present as a liquid.
- the amount of hydrogen introduced generally corresponds to a space velocity of from 10 to 650 standard I per kg of absorbent and hour.
- the absorbent After the absorbent is exhausted, it can be thermally regenerated by heating it in a stream of inert gas or a hydrogen-comprising gas stream, in general at temperatures of from 180 to 400° C., for example from 200 to 220° C., and condensing out vaporized mercury.
- example 2 The procedure of example 1 was repeated, but the solution was maintained at 25° C. Samples were taken at regular intervals and their mercury content was determined. The results are shown in table 2.
- example 2 The procedure of example 1 was repeated. The temperature was thus 60° C. Samples were taken at regular intervals and their mercury content was determined. The results are shown in table 2.
- example 2 The procedure of example 1 was repeated, but the solution was heated to 100° C. Samples were taken at regular intervals and their mercury content was determined. The results are shown in table 2.
- Example 4 (25° C.) (60° C.) (100° C.) Time [h] Hg [ppm] Hg [ppm] Hg [ppm] 0 350 350 350 1 300 250 90 2 290 150 — 3 250 120 30 4 240 — — 5 220 72 — 6 205 51 2.3 7 — 37 — 8 — 28 — 22 80 — — 24 75 0.8 0.14 93 4.6 — —
- the experiments were carried out in a monoline reactor having an internal diameter of 6 mm and a total length of 5 m.
- the reactor comprised 4 segments connected to one another by means of a capillary.
- the reactor was operated in the downflow mode.
- the reactor segments were maintained at 60° C.
- the liquid hydrocarbon feed was mixed with hydrogen before the reactor inlet.
- the reactor output was cooled by means of a low-temperature condenser and the gas phase was separated from the liquid phase.
- the liquid phase was employed for determining the mercury content and the gas phase was disposed of via a mercury guard bed.
- a catalyst comprising 45% by weight of CuO, 16% by weight of MgO, 35% by weight of SiO 2 , 0.9% by weight of Cr 2 O 3 , 1.1% by weight of BaO and 0.6% by weight of ZnO in the form of 3 ⁇ 5 mm pellets were present in the reactor.
- a glass sphere having a diameter of 2 mm was present between each of the individual pellets.
- the catalyst was firstly activated in a stream of hydrogen at from 180 to 220° C.
- the reactor was subsequently cooled to 60° C. in a stream of hydrogen.
- the reactor was operated at atmospheric pressure.
Abstract
Method of removing mercury from a mercury-comprising hydrocarbon stream, in which the hydrocarbon stream is brought into contact with an absorbent comprising copper on a support material, wherein the hydrocarbon stream is brought into contact with the absorbent in the presence of hydrogen.
Description
- The invention relates to a method of removing mercury and/or arsenic from a mercury-comprising hydrocarbon stream.
- Mercury is present as impurity in numerous streams of materials which are obtained or processed in the chemical or petrochemical industry. These are often streams which are obtained in the processing or thermal utilization of fossil raw materials such as petroleum, natural gas or coal and in the utilization of wastes, since these raw materials or wastes comprise traces of mercury in elemental form or in chemically bound form. Streams comprising mercury as impurity are also obtained in processes in which mercury or mercury-comprising substances are used as reagent or catalyst. An example which may be mentioned is the electrolysis hydrogen obtained in the production of chlorine by the amalgam process. Because of the high toxicity of mercury, it is in most cases necessary to separate off this metal or compounds comprising this metal from the streams obtained in the processes concerned. Furthermore, mercury has the property of attacking apparatuses comprising aluminum by amalgam formation with destruction of the oxide layer on the surface of the aluminum, so that streams which pass through apparatuses or vessels made of aluminum have to be virtually mercury-free. In addition, catalysts comprising noble metals, as are used, for example, in petrochemical processes, are poisoned by traces of mercury.
- In Fuel Processing Technology 82 (2003), pp. 89-165, J. H. Pavlish et al. give an overview of methods of removing mercury from the offgas streams obtained in coal-fired power stations. In Hydrocarbon Processing, 1999, p. 61 ff., S. M. Wilhelm gives an overview of methods of removing mercury from liquid hydrocarbon streams. An overview of the removal of mercury in olefin plants is given by Steve Coleman et al.: Feedstock Contaminants in Ethylene Plants, 2005 Spring National Meeting Atlanta, Ga., Apr. 10-14, 2005.
- If metallic mercury is present in liquid form in streams of materials, the mercury is frequently removed by mechanical measures which exploit the high surface tension or the high specific gravity of mercury by decantation, by means of coalescence filters, activated carbon coated filters or the like. EP-A 0 761 830 discloses a simple, purely mechanical method in which finely divided mercury is collected by coalescence to form larger droplets of mercury which are easy to separate off. WO 2004/048624 describes a method of removing mercury by filtration through electrographite.
- The removal of mercury is often also carried out using methods in which the mercury is bound to an adsorbent. Thus, DE-A 26 43 478 describes the separation of mercury from liquids by adsorption on activated carbon having a specific surface area of at least 250 m2/g. Carbon-based adsorbents are used, inter alia, for the removal of mercury from streams of materials, as described in U.S. Pat. No. 3,755,989. U.S. Pat. No. 4,500,327 describes sulfur-impregnated activated carbon for removing mercury from gaseous streams, while JP 52-53793 describes the use of iodide-comprising activated carbon for removing mercury from liquid streams. U.S. Pat. No. 4,909,926 and U.S. Pat. No. 4,094,777 describe the use of active compositions comprising CuS or CuO or Ag2S on support materials such as aluminum oxide for removing mercury from streams of materials. EP-A 0 385 742 describes a process for removing mercury from liquid hydrocarbon streams comprising hydrocarbons having up to 8 carbon atoms by bringing the streams into contact with metallic copper or copper compounds present on a support.
- The formation of solid amalgams is also often used for the removal of mercury. The most suitable metals for this purpose are the metals of group XI of the Periodic Table (Cu, Ag, Au), which are usually used in the form of an absorption composition in which the metal is finely distributed on a support. Thus, DE-A 21 02 039 discloses a process for removing mercury from gases, in which the mercury-comprising gases are brought into contact with a composition comprising copper on a porous aluminum oxide support. U.S. Pat. No. 4,230,486 discloses a process for removing mercury from liquids by passing the liquids over an absorbent comprising metallic silver on a porous support such as activated carbon or a ceramic support. DE-A 42 21 207 teaches a process for removing mercury from alkaline metal hydroxide solution or alkaline metal alkoxide solution by passing the solutions over silver-coated fibers. DE-A 41 16 890 discloses absorbents for removing mercury, which comprise, in particular, Cu, Ag, Fe and Bi, or else Au, Sn, Zn and Pd and also mixtures of the metals mentioned in metallic or oxidic or sulfidic form on an activated carbon support having a BET surface area of from 300 to 1000 m2/g.
- U.S. Pat. No. 4,911,825 describes the removal of mercury and arsenic from hydrocarbon streams by bringing these into contact with a catalyst comprising nickel and palladium on aluminum oxide in the presence of hydrogen in a first step and into contact with an absorbent comprising sulfur or a metal sulfide, preferably copper sulfide or a combination of copper sulfide and silver sulfide, on a support in a second step. The process can also be carried out in a single stage over a mixture of the catalyst and the absorbent. FR-A 2 310 795 describes the removal of mercury from a gaseous natural gas stream using an absorbent comprising metallic gold, silver, copper or nickel on a support composed of silicon dioxide, aluminum oxide or an aluminosilicate having a BET surface area of from 40 to 250 m2/g. WO 91/15559 discloses a method of removing mercury from liquid hydrocarbon streams by bringing them into contact with an absorbent produced by mixing of a pulverulent oxide, preferably an oxide selected from among nickel oxide, copper oxide and cobalt oxide, with a porous support material such as aluminum oxide, silicon dioxide, zeolites or clays and subsequent reduction.
- It is an object of the invention to provide an improved method of removing mercury from a mercury-comprising hydrocarbon stream.
- This object is achieved by a method of removing mercury from a mercury-comprising hydrocarbon stream, in which the hydrocarbon stream is brought into contact with an absorbent comprising copper on a porous oxidic support material, wherein the hydrocarbon stream is brought into contact with the absorbent in the presence of hydrogen.
- It has been found that a very much better removal of mercury from the hydrocarbon streams is achieved in the presence of hydrogen using copper-comprising absorbents which comprise copper on a support and are effective as hydrogenation catalysts than in the absence of hydrogen.
- The absorbent used according to the invention comprises copper, preferably in reduced form, on a porous support material. The absorbent used according to the invention is effective as hydrogenation catalyst. Suitable porous support materials are amorphous and crystalline aluminosilicates, aluminum oxide, silicon dioxide, clays and metal oxides. Suitable clays are, for example, attapulgite, kaolin, bentonite, Fuller's earth. Suitable metal oxides are, for example, aluminum oxides and silicon dioxide and also magnesium oxide, zirconium dioxide, titanium dioxide, zinc oxide, chromium(III) oxide, barium oxide and mixtures thereof. A preferred aluminum oxide is γ-aluminum oxide.
- It is possible to use all customary copper-comprising hydrogenation catalysts in activated (reduced) form in the method of the invention.
- The copper comprising hydrogenation-active absorbents used according to the invention can be obtained by mixing of copper oxide with a support material and subsequent conversion of copper into the metallic form by reduction, preferably in a stream of hydrogen. The absorbents used according to the invention can also be produced by impregnation of the support material with an aqueous solution of a copper salt, drying, if appropriate calcination and conversion of the copper into the metallic form by reduction, preferably by means of a hydrogen-comprising gas stream, although it is also possible to use a reducing agent such as hydrazine.
- In the absorbent used according to the invention, copper is generally present in reduced, i.e. metallic (elemental), form finely dispersed on the support material. In general, the absorbents used according to the invention comprise from 10 to 50% by weight of copper on an oxidic support material. Examples of suitable compositions on the basis of which the absorbents used according to the invention are obtained are compositions comprising copper oxide, zinc oxide and aluminum oxide or compositions comprising copper oxide, magnesium oxide, barium oxide, chromium(III) oxide, zinc oxide and silicon dioxide. Particular preference is given to a mixture of from 10 to 60% by weight of copper oxide, from 0 to 40% by weight of zinc oxide, from 0 to 20% by weight of aluminum oxide, from 5 to 25% by weight of magnesium oxide, from 10 to 40% by weight of silicon dioxide, from 0 to 5% by weight of chromium(III) oxide and from 0 to 10% by weight of barium oxide.
- Hydrocarbon streams from which mercury can be removed according to the invention are any hydrocarbon streams which can be contaminated with mercury. These generally comprise aliphatic, aromatic, alicyclic and/or heterocyclic hydrocarbons having from 1 to 14 carbon atoms. Examples of hydrocarbon mixtures which can be freed of mercury according to the invention are LNG (liquefied natural gas), LPG (liquefied petroleum gas), naphtha and kerosene. Examples of pure hydrocarbons which can be purified according to the invention are ethylene and propylene and also aliphatic hydrocarbons.
- The mercury content of the hydrocarbons or hydrocarbon mixtures before carrying out the method of the invention can be up to 100 ppm, but is generally up to 1 ppm of Hg. Mercury is generally present in the form of organomercury compounds.
- The method of the invention can be carried out in the suspension mode or the fixed-bed mode. If it is carried out in the fixed-bed mode, it can be carried out in the upflow or downflow mode. The hydrocarbons or hydrocarbon mixtures comprising mercury or arsenic can be used in gaseous or liquid form. The hydrocarbons or hydrocarbon mixtures are preferably used in liquid form. Hydrogen is introduced together with the gaseous or liquid hydrocarbon or hydrocarbon mixture into a suitable reaction vessel and passed, generally in cocurrent, over the particulate absorbent present in a fixed bed. This can be carried out in the upflow or downflow mode. However, hydrogen and hydrocarbon or hydrocarbon mixture can also be passed over the bed of absorbent in countercurrent. The absorbent can also be present in suspension in the hydrocarbon or hydrocarbon mixture. In general, the method is carried out at a temperature of from 30 to 250° C., preferably from 60 to 180° C., and a hydrogen pressure of from 1 to 20 bar. The pressure is preferably selected so that the hydrocarbon or the hydrocarbon mixture is present as a liquid. The amount of hydrogen introduced generally corresponds to a space velocity of from 10 to 650 standard I per kg of absorbent and hour.
- After the absorbent is exhausted, it can be thermally regenerated by heating it in a stream of inert gas or a hydrogen-comprising gas stream, in general at temperatures of from 180 to 400° C., for example from 200 to 220° C., and condensing out vaporized mercury.
- The invention is illustrated by the following examples.
- A solution of diphenylmercury (Ph2Hg) in 500 ml of octane, corresponding to 350 ppm of Hg, was heated to 60° C. in a glass flask. 1.5 standard I/h of hydrogen were passed into this solution while stirring. 5 g of an unreduced hydrogenation catalyst comprising 40% by weight of CuO, 40% by weight of ZnO and 20% by weight of Al2O3 in the form of 3×5 mm pellets (absorbent A) were added to this solution. Samples were taken from the solution after 2 h and 24 h and the mercury content of the samples was determined. The results are shown in table 1.
- A solution of diphenylmercury in 500 ml of octane, corresponding to 350 ppm of mercury, was heated to 60° C. in a glass flask. 5 g of the catalyst comprising 40% by weight of CuO, 40% by weight of ZnO and 20% by weight of Al2O3 which had previously been reduced and activated by means of H2 at 180° C. (absorbent B) in the form of 3×5 mm pellets were added to this solution. Hydrogen was not passed in. The solution was stirred. Samples were taken after 2 h and 24 h and their mercury content was determined. The results are shown in table 1.
- The procedure of comparative example 2 was repeated, but 1.5 standard I/h of hydrogen were passed in. Samples were taken at regular intervals and their mercury content was determined. The results are shown in table 1.
- The procedure of example 1 was repeated, but the reduced catalyst was added in pulverulent form (absorbent C). Samples were taken at regular intervals and their mercury content was determined. The results are shown in table 1.
-
TABLE 1 Comp. Ex. 1 Comp. Ex. 2 Example 1 Example 2 Time [h] Hg [ppm] Hg [ppm] Hg [ppm] Hg [ppm] 0 350 350 350 350 1 — 270 250 205 2 310 — 150 115 3 — — 120 75 4 — — — 60 5 — — 72 45 6 — 145 51 15 7 — — 37 — 8 — — 28 — 21 0.3 22 0.3 24 135 47 0.8 0.3 - The procedure of example 1 was repeated, but the solution was maintained at 25° C. Samples were taken at regular intervals and their mercury content was determined. The results are shown in table 2.
- The procedure of example 1 was repeated. The temperature was thus 60° C. Samples were taken at regular intervals and their mercury content was determined. The results are shown in table 2.
- The procedure of example 1 was repeated, but the solution was heated to 100° C. Samples were taken at regular intervals and their mercury content was determined. The results are shown in table 2.
-
TABLE 2 Example 3 Example 4 Example 5 (25° C.) (60° C.) (100° C.) Time [h] Hg [ppm] Hg [ppm] Hg [ppm] 0 350 350 350 1 300 250 90 2 290 150 — 3 250 120 30 4 240 — — 5 220 72 — 6 205 51 2.3 7 — 37 — 8 — 28 — 22 80 — — 24 75 0.8 0.14 93 4.6 — — - The experiments were carried out in a monoline reactor having an internal diameter of 6 mm and a total length of 5 m. The reactor comprised 4 segments connected to one another by means of a capillary. The reactor was operated in the downflow mode. The reactor segments were maintained at 60° C. The liquid hydrocarbon feed was mixed with hydrogen before the reactor inlet. The reactor output was cooled by means of a low-temperature condenser and the gas phase was separated from the liquid phase. The liquid phase was employed for determining the mercury content and the gas phase was disposed of via a mercury guard bed.
- 80 g of a catalyst comprising 45% by weight of CuO, 16% by weight of MgO, 35% by weight of SiO2, 0.9% by weight of Cr2O3, 1.1% by weight of BaO and 0.6% by weight of ZnO in the form of 3×5 mm pellets were present in the reactor. A glass sphere having a diameter of 2 mm was present between each of the individual pellets. The catalyst was firstly activated in a stream of hydrogen at from 180 to 220° C. The reactor was subsequently cooled to 60° C. in a stream of hydrogen. The reactor was operated at atmospheric pressure.
- Octane which had been saturated over an organomercury compound was used as feed. In part of the experiments, phenylmercury acetate PhHgOAc was used as organomercury compound, and in another part of the experiments mercury acetate Hg(OAc)2 was used as organomercury compound. A number of batches having different mercury concentrations were used in each case. 100 standard I/h of the mercury-comprising octane and 2 standard I/h of hydrogen were metered in. The results of the experiments are summarized in table 3.
-
TABLE 3 Experiment Hg compound Hg concentration Hg concentration in the No. added in the feed [ppm] output [ppm] 1 PhHgOAc 80 0.004 2 PhHgOAc 90 0.002 3 PhHgOAc 80 0.004 4 PhHgOAc 60 0.001 5 Hg(OAc)2 6 0.001 6 Hg(OAc)2 1.4 0.001 7 Hg(OAc)2 0.6 0.001 8 Hg(OAc)2 2.8 0.001 9 Hg(OAc)2 1.2 0.001 10 PhHgOAc 90 0.001 11 PhHgOAc 120 0.003 12 PhHgOAc 75 0.004
Claims (8)
1.-8. (canceled)
9. A method of removing mercury from a mercury-comprising hydrocarbon stream, which comprises bringing a hydrocarbon stream into contact with an absorbent comprising copper on a support material, wherein the hydrocarbon stream is brought into contact with the absorbent in the presence of hydrogen, wherein the absorbent comprises from 10 to 60% by weight of copper oxide, from 0 to 40% by weight of zinc oxide, from 0 to 20% by weight of aluminum oxide, from 5 to 25% by weight of magnesium oxide, from 10 to 40% by weight of silicon dioxide, from 0 to 5% by weight of chromium(III) oxide and from 0 to 10% by weight of barium oxide.
10. The method according to claim 9 , wherein copper is present on a porous oxidic support material.
11. The method according to claim 9 , wherein the absorbent comprises from 10 to 60% by weight of copper.
12. The method according to claim 9 , wherein the hydrocarbon stream is present in liquid form.
13. The method according to claim 9 , wherein the absorbent is present as a fixed bed.
14. The method according to claim 13 , wherein the hydrocarbon stream is brought into contact with the absorbent in the upflow mode or the downflow mode.
15. The method according to claim 12 , wherein the absorbent is present in suspension in the hydrocarbon stream.
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US20090200207A1 (en) * | 2006-06-21 | 2009-08-13 | Stephan Hatscher | Absorption Composition and Process for Removing Mercury |
US20160177191A1 (en) * | 2013-08-07 | 2016-06-23 | Jx Nippon Oil & Energy Corporation | Method for removing mercury in hydrocarbon oil |
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CN102764655B (en) * | 2011-12-23 | 2015-03-04 | 盐城工学院 | Demercuration catalyst |
US9006508B2 (en) * | 2012-02-06 | 2015-04-14 | Uop Llc | Protected adsorbents for mercury removal and method of making and using same |
CN105148913B (en) * | 2015-10-08 | 2017-11-07 | 宁波海越新材料有限公司 | A kind of preparation method for the catalyst that MEK is prepared for sec-butyl alcohol |
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Also Published As
Publication number | Publication date |
---|---|
WO2009112440A1 (en) | 2009-09-17 |
JP5455939B2 (en) | 2014-03-26 |
CN101970614A (en) | 2011-02-09 |
EP2265695A1 (en) | 2010-12-29 |
JP2011513565A (en) | 2011-04-28 |
KR20100133394A (en) | 2010-12-21 |
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