WO2011129534A9 - 수소화 탈왁스 공정을 위한 촉매 및 이의 제조 방법 - Google Patents
수소화 탈왁스 공정을 위한 촉매 및 이의 제조 방법 Download PDFInfo
- Publication number
- WO2011129534A9 WO2011129534A9 PCT/KR2011/002054 KR2011002054W WO2011129534A9 WO 2011129534 A9 WO2011129534 A9 WO 2011129534A9 KR 2011002054 W KR2011002054 W KR 2011002054W WO 2011129534 A9 WO2011129534 A9 WO 2011129534A9
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- WIPO (PCT)
- Prior art keywords
- catalyst
- zeolite
- phase transition
- group
- metal
- Prior art date
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- 239000003054 catalyst Substances 0.000 title claims abstract description 82
- 238000000034 method Methods 0.000 title claims abstract description 41
- 230000008569 process Effects 0.000 title claims abstract description 17
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 15
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 8
- 239000010457 zeolite Substances 0.000 claims abstract description 73
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 54
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 53
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 53
- 229910052751 metal Inorganic materials 0.000 claims abstract description 36
- 239000002184 metal Substances 0.000 claims abstract description 36
- 239000000463 material Substances 0.000 claims abstract description 31
- 230000007704 transition Effects 0.000 claims description 80
- 239000002994 raw material Substances 0.000 claims description 17
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 14
- 150000002739 metals Chemical class 0.000 claims description 13
- 239000000203 mixture Substances 0.000 claims description 13
- 239000000377 silicon dioxide Substances 0.000 claims description 13
- 230000009467 reduction Effects 0.000 claims description 12
- 239000004480 active ingredient Substances 0.000 claims description 8
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 8
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical group [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 7
- 238000001035 drying Methods 0.000 claims description 7
- 229930195733 hydrocarbon Natural products 0.000 claims description 7
- 150000002430 hydrocarbons Chemical class 0.000 claims description 7
- 239000000523 sample Substances 0.000 claims description 7
- 239000004215 Carbon black (E152) Substances 0.000 claims description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 5
- 229910052739 hydrogen Inorganic materials 0.000 claims description 5
- 239000001257 hydrogen Substances 0.000 claims description 5
- 239000003513 alkali Substances 0.000 claims description 4
- -1 amine compound Chemical class 0.000 claims description 4
- 229910052763 palladium Inorganic materials 0.000 claims description 4
- 229910052697 platinum Inorganic materials 0.000 claims description 4
- 239000013074 reference sample Substances 0.000 claims description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 3
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims description 3
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 3
- 229910052791 calcium Inorganic materials 0.000 claims description 3
- 239000011575 calcium Substances 0.000 claims description 3
- 238000010276 construction Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000007788 liquid Substances 0.000 claims description 3
- 229910052749 magnesium Inorganic materials 0.000 claims description 3
- 239000011777 magnesium Substances 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 229910052708 sodium Inorganic materials 0.000 claims description 3
- 239000011734 sodium Substances 0.000 claims description 3
- 230000002378 acidificating effect Effects 0.000 claims description 2
- 238000001354 calcination Methods 0.000 claims description 2
- 238000005406 washing Methods 0.000 claims description 2
- QEMXHQIAXOOASZ-UHFFFAOYSA-N tetramethylammonium Chemical compound C[N+](C)(C)C QEMXHQIAXOOASZ-UHFFFAOYSA-N 0.000 claims 1
- 238000006317 isomerization reaction Methods 0.000 abstract description 51
- 230000015572 biosynthetic process Effects 0.000 abstract description 44
- 238000003786 synthesis reaction Methods 0.000 abstract description 44
- 238000006243 chemical reaction Methods 0.000 abstract description 28
- DCAYPVUWAIABOU-UHFFFAOYSA-N hexadecane Chemical compound CCCCCCCCCCCCCCCC DCAYPVUWAIABOU-UHFFFAOYSA-N 0.000 abstract description 20
- 230000001588 bifunctional effect Effects 0.000 abstract description 13
- 238000005336 cracking Methods 0.000 abstract description 10
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- 229910052906 cristobalite Inorganic materials 0.000 abstract description 9
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- 239000002283 diesel fuel Substances 0.000 abstract description 3
- 239000000314 lubricant Substances 0.000 abstract description 3
- 239000002199 base oil Substances 0.000 abstract description 2
- 238000002411 thermogravimetry Methods 0.000 description 22
- 238000002441 X-ray diffraction Methods 0.000 description 21
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 18
- 238000001027 hydrothermal synthesis Methods 0.000 description 16
- 238000002474 experimental method Methods 0.000 description 12
- 230000004580 weight loss Effects 0.000 description 10
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- BANXPJUEBPWEOT-UHFFFAOYSA-N 2-methyl-Pentadecane Chemical compound CCCCCCCCCCCCCC(C)C BANXPJUEBPWEOT-UHFFFAOYSA-N 0.000 description 4
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 4
- DIOQZVSQGTUSAI-UHFFFAOYSA-N decane Chemical compound CCCCCCCCCC DIOQZVSQGTUSAI-UHFFFAOYSA-N 0.000 description 4
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- 229910001388 sodium aluminate Inorganic materials 0.000 description 4
- 239000004809 Teflon Substances 0.000 description 3
- 229920006362 Teflon® Polymers 0.000 description 3
- HUTDDBSSHVOYJR-UHFFFAOYSA-H bis[(2-oxo-1,3,2$l^{5},4$l^{2}-dioxaphosphaplumbetan-2-yl)oxy]lead Chemical compound [Pb+2].[Pb+2].[Pb+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O HUTDDBSSHVOYJR-UHFFFAOYSA-H 0.000 description 3
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- 150000002500 ions Chemical group 0.000 description 3
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- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 3
- 239000010970 precious metal Substances 0.000 description 3
- 229940043268 2,2,4,4,6,8,8-heptamethylnonane Drugs 0.000 description 2
- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 229910052784 alkaline earth metal Inorganic materials 0.000 description 2
- 150000003868 ammonium compounds Chemical class 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
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- 238000009835 boiling Methods 0.000 description 2
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- 230000000694 effects Effects 0.000 description 2
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- KUVMKLCGXIYSNH-UHFFFAOYSA-N isopentadecane Natural products CCCCCCCCCCCCC(C)C KUVMKLCGXIYSNH-UHFFFAOYSA-N 0.000 description 2
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- 238000012360 testing method Methods 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 239000001993 wax Substances 0.000 description 2
- BNGXYYYYKUGPPF-UHFFFAOYSA-M (3-methylphenyl)methyl-triphenylphosphanium;chloride Chemical compound [Cl-].CC1=CC=CC(C[P+](C=2C=CC=CC=2)(C=2C=CC=CC=2)C=2C=CC=CC=2)=C1 BNGXYYYYKUGPPF-UHFFFAOYSA-M 0.000 description 1
- 229910002012 Aerosil® Inorganic materials 0.000 description 1
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 1
- 229910002621 H2PtCl6 Inorganic materials 0.000 description 1
- 206010027476 Metastases Diseases 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 239000008186 active pharmaceutical agent Substances 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 150000001342 alkaline earth metals Chemical class 0.000 description 1
- 150000003973 alkyl amines Chemical class 0.000 description 1
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 239000007809 chemical reaction catalyst Substances 0.000 description 1
- 239000004927 clay Substances 0.000 description 1
- 229910052570 clay Inorganic materials 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 239000000306 component Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 229910021485 fumed silica Inorganic materials 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
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- 230000001050 lubricating effect Effects 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
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- 230000009401 metastasis Effects 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 125000001477 organic nitrogen group Chemical group 0.000 description 1
- 230000010363 phase shift Effects 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000000634 powder X-ray diffraction Methods 0.000 description 1
- 230000002250 progressing effect Effects 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical compound O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000005486 sulfidation Methods 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 229910001868 water Inorganic materials 0.000 description 1
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- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65
- C07C2529/72—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65 containing iron group metals, noble metals or copper
- C07C2529/74—Noble metals
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C9/00—Aliphatic saturated hydrocarbons
- C07C9/22—Aliphatic saturated hydrocarbons with more than fifteen carbon atoms
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/10—Lubricating oil
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Definitions
- the present invention relates to a metal-containing binary functional catalyst for a hydrodewaxing process and a method for preparing the same, and more specifically, to a carrier having an acid point, EU-2 zeolite having a controlled degree of phase transformation is used. It relates to a binary catalyst and a preparation method thereof.
- isomerized C4-C7 hydrocarbons can be used in high octane gasoline production process.
- the C7-C15 hydrocarbon isomerization study is applicable to the production of high quality diesel oil with improved high cetane number and low temperature fluidity.
- the isomerization of normal-paraffins over C15 has been applied to the production of high-grade lubricants with high Viscosity Index.
- commercially available lubricating oils and jet oils require low pour points and melting points, and thus, a technique for converting wax components through an isomerization reaction is required to produce such oils in high quality.
- the bifunctional catalyst is composed of two active ingredients: a metal active ingredient (metal site) for hydrogenation / dehydrogenation reaction and a carrier (Acid Site) having a acid point for skeletal isomerization through carbenium ion generation. It is therefore called the bifunctional catalyst.
- the metal active component used in the bifunctional catalyst one or more metals are generally selected and used among Group 8 metals and Group 6 metals. In particular, precious metals such as Pt and Pd having excellent hydrogenation / dehydrogenation activity are mainly used.
- a carrier having an acid point used in a bifunctional catalyst a substance having various acid points such as silica-alumina, clay, and zeolite is mentioned. Especially, in the case of a zeolite material, the structure is stable even in harsh reaction conditions, and has a large surface area. Since it contains an acid point of, it is advantageous to be applied as an isomerization reaction catalyst.
- a method for preparing a catalyst for a hydrodewaxing process includes (a) preparing an EU-2 zeolite carrier having a controlled degree of transition such that a phase transition index (T) is 50 ⁇ T ⁇ 100. Doing;
- step (c) forming and drying / firing the catalyst of step (b).
- T (TGA reduction of the corresponding EU-2 sample in the synthesized state) / (TGA reduction of the pure EU-2 reference sample) X 100 (wherein the TGA reduction is 2 ° C./min from 120 ° C. to 550 ° C. in an air atmosphere. After heating up at a rate of 550 ° C. for 2 hours).
- the catalyst for the hydrodewaxing process according to the present invention for achieving another object of the present invention is a carrier having an acid point, the phase transition index (T) represented by the above formula is 50 ⁇ T ⁇ 100, the molar ratio of silica / alumina EU-2 zeolites of 1 to 200 carry a metal-active component of a hydrogenation function in which at least one component is selected from Group 8 metals and Group 6 metals.
- the bifunctional catalyst using EU-2 zeolite having a controlled degree of phase transformation according to the present invention as a carrier shows an improved isomerization selectivity compared to a zeolite having a ZSM-48 and EU-2 structure.
- the present invention can be used as a catalyst for the dewaxing process for the production of lubricating base oil, in addition to the normal-Paraffin using a bifunctional catalyst for various hydrocarbon fractions It is possible to apply to iso-paraffin conversion, that is, a catalyst for producing a high octane gasoline gasoline through isomerization reaction, a catalyst for improving the pour point of diesel oil.
- XRD X-ray diffraction pattern
- FIG. 2 is an X-ray diffraction pattern (XRD) of hydrothermally synthesized Pure EU-2 and EU-2 zeolite material having undergone phase transition with synthesis time.
- XRD X-ray diffraction pattern
- 3 is a graph showing iso-C16 yield as a function of n-C16 conversion.
- Figure 4 is a graph showing the relationship between the phase transition index and the isomerization yield according to an embodiment of the present invention.
- the present invention provides a dewaxing catalyst having excellent selectivity for isomerization reaction, and uses EU-2 zeolite having a controlled degree of phase transition as a carrier of the dewaxing catalyst.
- the prior art aimed at preparing pure zeolites, but the present invention can improve the efficiency of the isomerization reaction according to the degree of phase transition of zeolites.
- the catalyst according to the present invention has a hydrogenation function in an EU-2 zeolite carrier having a phase transition index (T) of less than 100 and a value of 50 or more based on the EU-2 phase transition index proposed by the researchers. It is supported by a metal active ingredient.
- T phase transition index
- zeolite materials are prepared by mixing an organic template material with an aqueous alkali solution containing silica and alumina raw materials, and hydrothermally synthesizing them in a batch reactor such as an autoclave.
- a batch reactor such as an autoclave.
- the structure, purity and crystal size of the zeolite material are characterized by the relative concentration between raw materials such as silica, alumina, alkali or alkaline earth metal, water, whether or not aging before hydrothermal synthesis, hydrothermal synthesis temperature, hydrothermal synthesis time, It depends on various variables, such as whether the agitation during hydrothermal synthesis.
- EU-2 zeolite which is a kind of zeolite used in dewaxing catalyst, can also obtain pure EU-2 crystals after a certain time by controlling hydrothermal synthesis conditions. It gradually transforms, and the resulting phases include cristobalite and quartz, and one or more phases may occur together or change depending on the composition and time of the synthetic raw material.
- the present inventors synthesized EU-2 zeolites with different phase transitions by controlling hydrothermal synthesis time under the same synthesis conditions, and prepared a catalyst for dewaxing and comparing the isomerization performance. Rather, it was found that the isomerization performance of EU-2 zeolite, in which a phase transition proceeded to produce a material such as cristobalite or quartz, was excellent. It was confirmed that even when synthesized by changing the synthesis conditions such as silica and alumina ratio, the isomerization performance of the EU-2 zeolite with the advanced phase transition was superior to that of pure EU-2 zeolite, and the present invention is based on this.
- the presence of a substance represented by the purity and phase transition of the zeolite material itself is generally determined by XRD (X-ray Powder Diffraction) method, and the relative amount of material produced is compared by comparing the magnitude of characteristic XRD peak appearing by material. It can also be compared.
- the XRD method is particularly useful for determining the extent of EU-2 phase transition, as the XRD characteristic peaks of cristobalite and quartz can be observed simultaneously in addition to the XRD characteristic peaks of EU-2 materials.
- XRD characteristic peak of EU-2 zeolite obtained according to the synthesis time in the zeolite synthesis conditions of Example 1 to be described in accordance with an embodiment of the present invention is shown in FIG.
- the XRD peak (2 ⁇ ) corresponding to EU-2 is shown at 21.0 ° 23.0 °, and the main peak is shown by XRD analysis at 22.0 ° for cristobalite and 26.5 ° for quartz.
- EU-2 zeolite with high crystal purity As the synthesis time elapses, the phase transition occurs to the cristobalite and the quartz phase, and as the synthesis time is further increased, the quartz phase is greatly developed.
- Figure 2 shows the XRD characteristic Peak of the EU-2 zeolite obtained according to the synthesis time in the synthesis conditions different from Figure 1, as in Example 4, the composition of the mixture is described later.
- the transition of pure EU-2 zeolite peak to another phase proceeds.
- transition to the cristobalite phase is hardly observed.
- the phase transition proceeds rapidly to the quartz phase, it can be seen that the tendency and speed of the phase transition may change slightly as the synthesis conditions change.
- thermogravimetric analysis TGA
- T Phase 2 Transition Index
- TGA analysis condition TGA weight loss of the corresponding EU-2 sample in the synthesized state measured under the condition of 550 degrees 2 hours after raising the temperature from 120 degrees to 550 degrees at 2 degrees / min in air atmosphere
- the relative TGA of EU-2 based on the EU-2 sample with the highest crystal purity, from the fact that the TGA weight loss decreases as the phase transition of EU-2 synthesized with the same material and composition proceeds.
- the EU-2 phase transition index can be defined as described above. Furthermore, it should be noted that the phase transition index decreases proportionally with the synthesis time, but it is not absolutely consistent since it depends on the synthesis conditions.
- the template material may be one or more materials selected from the group consisting of organic nitrogen-containing compounds, that is, Alkyl-amines, Tetrametyl ammonium compounds, Diquaternary ammonium compounds, and the like.
- the silica raw material may be one or more materials selected from the group consisting of silica sol, fumed silica, aerosil, tetraorthosilicate, and also ludox HS- Silica sol, such as 40 (Ludox HS-40) or Ludox AS-30.
- the alumina raw material may be at least one material selected from the group consisting of Sodium Aluminate, Aluminum Nitrate, Aluminum Sulfate, AlCl 3 , Al (OH) 3 and Al (OCH 3 ) 3 .
- the hydrothermal synthesis is preferably carried out in an alkaline state of pH 9 or more, more preferably hydrothermal synthesis is carried out at pH 12 or more.
- the synthesis time of the hydrothermal synthesis is related to the reaction temperature or the stirring conditions, but generally 1 hour or more is preferred and the reaction time may be adjusted according to the phase transition index of the obtained EU-2 zeolitic material.
- the phase transition index of the EU-2 zeolite material is preferably 50 ⁇ T ⁇ 100, more preferably the phase transition index (T) is adjusted in the range of 60 ⁇ T ⁇ 100, most preferably as shown in FIG. 4. , 60 ⁇ T ⁇ 98.
- the phase transition index (T) is less than 50 or 100, it is not preferable because impurities such as cristobalite or quartz are not included to the extent that they do not affect the improvement of the isomerization efficiency, or because the phase transition index T is included in an excessive amount to decrease the efficiency. .
- the method for preparing the catalyst may further include washing and drying the EU-2 zeolite, in which the degree of transition is controlled.
- the molar ratio of silica / alumina of the EU-2 zeolite carrier having the degree of phase transition controlled is from 1 to 500, more preferably from 20 to 200.
- the BET surface area of the EU-2 zeolite with controlled degree of phase transition provided by the present invention is preferably 100 m 2 / gr or more.
- the method for preparing a catalyst according to the present invention comprises the steps of supporting a metal active ingredient of a hydrogenation function on the EU-2 zeolite carrier synthesized as described above; And forming and drying / firing the resultant, wherein the catalyst composition according to the present invention has a phase transition index of less than 100 based on the EU-2 phase transition index proposed by the present researchers. It is a catalyst for isomerization reaction in which a metal active ingredient of a hydrogenation function is supported on an EU-2 zeolite carrier whose phase transition degree is controlled to have a value of 50 or more.
- the binary functional catalyst according to the present invention is used as a catalyst for the hydrowaxing process.
- the bifunctional catalyst according to the present invention uses an EU-2 zeolite carrier having a phase transition controlled as a carrier having an acidic point, an oxide such as alumina, silica, etc., and a metal having a hydrogenation function is a Group 8 metal or 6
- One or more metals may be selected from the group metals, preferably precious metals such as platinum and palladium.
- At least one metal selected from Group 8 metals or Group 6 metals is selected and supported on the ion exchanged phase transfer control EU-2 zeolite carrier, more preferably. It is to carry precious metals such as platinum and palladium.
- a method of supporting a metal a general impregnation method, an ion exchange method, or the like can be used.
- the catalyst in order to improve the isomerization reaction selectivity of the catalyst, it is possible to prepare the catalyst by adding at least one of Group 1 and Group 2 metal components as cocatalysts, and preferably, as the Group 1 and Group 2 components, sodium, magnesium, And calcium and one or more may be selected.
- a catalyst according to the present invention is prepared through a molding and drying / firing process, and the firing is generally performed at 350 to 600 ° C. for 1 to 24 hours.
- Drying, reduction, and pre-sulfidation may be required for activation and pretreatment of the catalyst, and such pretreatment may be omitted or changed as necessary.
- the hydrocarbon raw material is the hydrogenation dewaxing reaction conditions of the temperature of 250 to 420 °C, hydrogen partial pressure of 1 to 200 atm, liquid construction rate of 0.1 to 10 hours -1 , and 45 to 1780 m 3
- a hydrogenation gas ratio of / m 3 250 to 10,000 scf / B
- it can be used as a hydrodeswax catalyst.
- the final mixture was put into a hydrothermal synthesis reactor coated with Teflon material, and reacted at 165 ° C. for 2 days (48 hours) to obtain a zeolite material.
- the mixture is washed with distilled water sufficiently, dried at 60 ° C for 12 hours, and calcined at 550 ° C for 5 hours.
- the obtained material is a zeolite having only pure EU-2 crystal structure reported in the existing literature and patent.
- the hydrothermally synthesized EU-2 zeolite was ion exchanged with NH 4 + ions using an aqueous solution of 1N ammonium nitrate (Ammonium Nitrate).
- the ion-exchanged EU-2 zeolite was mixed with Psuedoboemite as a binder in a ratio of 1: 1, and an aqueous solution of H2PtCl6 was impregnated into the mixture of EU-2 zeolite and binder so as to be 0.6 wt% based on the Pt content.
- the impregnated catalyst was dried at 120 ° C. for 3 hours, and calcined at 500 ° C. for 3 hours to prepare a catalyst for isomerization reaction.
- the catalyst was prepared in the same manner by changing the synthesis time to only 4 days (96 hours) by the synthesis method as described above. At this time, the obtained material was confirmed to be X-ray diffraction analysis, the phase transition was progressing was a material containing the EU-2 and cristobalite structure.
- X-ray diffraction patterns of the obtained material are the same as '2 days', '4 days' of FIG. It can be seen that the synthesis time 2 days zeolite material is pure EU-2 zeolite having only EU-2 characteristic peak, and the synthesis time 4 days material is confirmed that the characteristic peaks of cristobalite and quartz are due to the phase change of EU-2 zeolite crystals.
- N-hexadecane conversion reaction experiments were carried out using the two catalysts for isomerization reaction obtained above.
- the experiment was carried out after the catalyst for isomerization thus obtained was charged in a fixed bed reactor having an outer diameter of 1/2 inch and activated at 260 ° C. for at least 1 hour to start the reaction experiment.
- the reaction experiment was started by injecting n-hexadecane feed into the reactor at a speed of 1gr / hr using a pump.
- the reaction conditions were controlled at 30 atm and hydrogen injection at 650cc / hr.
- the conversion of n-hexadecane can be controlled by adjusting the reaction temperature, and the selectivity of the cracking reaction and the selectivity of the isomerization reaction are also changed according to the conversion of n-hexadecane.
- the isomerization yield was higher than 60 or less than 100, more preferably from 60 to 98. As the phase transition index decreases further, the isomerization yield tends to decrease little by little compared to the maximum yield. When the phase transition index T is 50 or less as in EU-2 on the synthesis time 21 days, the isomerization yield is pure. It is rather reduced compared to EU-2 zeolite catalyst.
- the final mixture was added to a Teflon-coated hydrothermal synthesis reactor, and a phase transition EU-2 zeolite material was obtained according to the synthesis change under the same synthesis conditions as in Example 1, and the phase transition index of the obtained material and the catalyst were prepared as n-hexa.
- the results of the decane conversion reaction experiments are shown in the table below. Catalyst preparation and n-hexadecane conversion reaction experiments were performed in the same manner as in Example 1.
- the final mixture was added to a Teflon-coated hydrothermal synthesis reactor, and a phase transition EU-2 zeolite material was obtained according to the synthesis change under the same synthesis conditions as in Example 1, and the phase transition index of the obtained material and the catalyst were prepared as n-hexa.
- the results of the decane conversion reaction experiments are shown in the table below. Catalyst preparation and n-hexadecane conversion reaction experiments were performed in the same manner as in Example 1.
- the prepared catalyst has a Pour Point (flow point) at 48 ° C at a hydrogen pressure of 144 atmospheres, a hydrogenation dewaxing reaction condition, a liquid construction rate of 1 hr-1, a rate of 550 m 3 / m3 hydrogen treatment gas, and a reaction temperature of 340 ° C.
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Abstract
Description
도 1의 합성조건 | 도 2의 합성조건 | |||
합성시간(일) | TGA 무게감량(%) | EU-2 상 전이지수 (T) | TGA 무게감량(%) | EU-2 상 전이지수 (T) |
2 | 8.6 | 100.0 | 8.6 | 100.0 |
4 | 8.0 | 93.0 | 8.5 | 98.8 |
6 | 7.2 | 83.7 | 7.8 | 90.7 |
8 | 5.2 | 60.5 | 4.8 | 55.8 |
21 | 4.1 | 47.7 |
합성 시간(일) | XRD Peak | EU-2 상 전이 지수 (T) | 최대수율 (%) |
2 | Pure EU-2, 비교예 | 100.0 | 81.6 |
4 | 상 전이, 실시예 1 | 93.0 | 88.3 |
6 | 상 전이 | 83.7 | 87.0 |
8 | 상 전이 | 60.5 | 86.4 |
21 | 상 전이 | 47.7 | 72.5 |
합성 시간(일) | XRD Peak | EU-2 상 전이 지수 (T) | 최대수율 (%) |
2 | Pure EU-2 | 100.0 | 81.3 |
4 | 상 전이 | 97.6 | 85.2 |
합성 시간(일) | XRD Peak | EU-2 상 전이 지수 (T) | 최대수율(%) |
2 | Pure EU-2 | 100.0 | 80.6 |
6 | 상 전이 | 90.7 | 86.8 |
Feed | Product | |
API | 35.8 | |
Specific Gravity | 0.8458 | 0.834 |
Distillation, D2887 | ||
10% | 394.6 | |
90% | 451.0 | |
Sulfur, wtppm | 4.6 | <1.0 |
Nitrogen, wtppm | 2.0 | <1.0 |
Kinematic Viscosity@40′C, cSt | 35.1 | 35.88 |
Kinematic Viscosity@100′C, cSt | 6.543 | 6.429 |
Viscosity Index | 143 | 132 |
PP,′C | 48 | -14 |
Claims (12)
- (a) 상전이 지수(T)가 50 ≤ T <100가 되도록 전이 정도가 조절된 EU-2 제올라이트 담체를 준비하는 단계;(b) 상기 EU-2 제올라이트 담체에, 8족 금속 및 6족 금속 중에서 한 성분 이상이 선택되는 수소화 기능의 금속 활성성분을 담지하는 단계; 및(c) 상기 (b)단계의 촉매를 건조 및 소성시키는 단계를 포함하며,상기 T=(합성된 상태의 해당 EU-2 시료의 TGA 감량)/(순수한 EU-2 기준시료의 TGA 감량) X 100 (여기서 상기 TGA감량은 공기 분위기에서 120℃에서 550℃까지 2℃/분의 속도로 승온 후 550℃에서 2시간 유지하여 측정함)인 수소화 탈왁스 공정용 촉매의 제조방법.
- 청구항 1에 있어서, 상기 상전이 지수(T)는 60≤T≤98인 수소화 탈왁스 공정용 촉매의 제조방법.
- 청구항 1에 있어서, 상기 (a) 단계는,(i) 실리카 및 알루미나 원료물질의 알칼리 수용액을 주형물질과 혼합하는 단계;(ii) 상기 (i) 단계에서의 혼합물을 50 내지 250℃의 범위에서 반응시켜 제올라이트의 상전이 지수(T)가 50 ≤ T <100가 되도록 전이 정도를 조절하는 단계; 및(iii) 상기 (ii)단계의 제올라이트를 세척 및 건조시키는 단계;를 포함하는 수소화 탈왁스 공정용 촉매의 제조방법.
- 청구항 3에 있어서, 상기 주형물질은 아민화합물, 테트라메틸 암모늄 화합물, 및 디-4급 암모늄 화합물로 이루어진 그룹으로부터 선택된 하나 이상의 물질인 수소화 탈왁스 공정용 촉매의 제조방법.
- 청구항 1 또는 2에 있어서, 상기 (b)단계는, 1족 및 2족 금속 성분으로부터 하나 이상 선택되는 조촉매 성분을 첨가하는 단계를 더 포함하는 수소화 탈왁스 공정용 촉매의 제조방법.
- 청구항 5에 있어서, 상기 금속 성분은 나트륨, 마그네슘, 및 칼슘으로부터 하나 이상 선택되는 수소화 탈왁스 공정용 촉매의 제조방법.
- 산점을 갖는 담체로서 하기 식 1로 표시되는 상전이 지수(T)가 50 ≤ T <100이며, 실리카/알루미나의 몰비가 20 내지 200인 EU-2 제올라이트에, 8족 금속 및 6족 금속 중에서 한 성분 이상이 선택되는 수소화 기능의 금속 활성 성분이 담지된 수소화 탈왁스 공정용 촉매:<식 1> T=(합성된 상태의 해당 EU-2 시료의 TGA 감량)/(순수한 EU-2 기준시료의 TGA 감량) X 100 (여기서 상기 TGA감량은 공기 분위기에서 120℃에서 550℃까지 2℃/분의 속도로 승온 후 550℃에서 2시간 유지하여 측정함).
- 청구항 7에 있어서, 상기 상전이 지수(T)는 60≤ T ≤98인 수소화 탈왁스 공정용 촉매.
- 청구항 7에 있어서, 상기 금속활성 성분은 팔라듐 또는 백금인 수소화 탈왁스 공정용 촉매.
- 청구항 7에 있어서, 상기 촉매는 1족 및 2족 금속 성분으로부터 하나 이상 선택되는 조촉매 성분을 더 포함하는 수소화 탈왁스 공정용 촉매.
- 청구항 10에 있어서, 상기 금속 성분은 나트륨, 마그네슘, 및 칼슘으로부터 하나 이상 선택되는 수소화 탈왁스 공정용 촉매.
- 청구항 7 또는 10에 따른 수소화 탈왁스 공정용 촉매 존재 하에서, 탄화수소 원료에 대하여, 250 내지 420℃의 온도, 1 내지 200 기압의 수소분압, 0.1 내지 10 h-1 의 액체 시공 속도, 및 250 내지 10,000 scf/B의 수소 처리 기체 비율로 실시되는 수소화 탈왁스 방법.
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ES11769000T ES2813388T3 (es) | 2010-04-14 | 2011-03-25 | Catalizador para un procedimiento de desparafinado por hidrogenación y método para fabricar el mismo |
CN201180025628.1A CN102905786B (zh) | 2010-04-14 | 2011-03-25 | 用于加氢脱蜡工艺的催化剂及其制备方法 |
US13/640,788 US8772193B2 (en) | 2010-04-14 | 2011-03-25 | Catalyst for a hydrogenation dewaxing process and method for manufacturing same |
EP11769000.8A EP2559483B1 (en) | 2010-04-14 | 2011-03-25 | Catalyst for a hydrogenation dewaxing process and method for manufacturing same |
RU2012143524/04A RU2527283C2 (ru) | 2010-04-14 | 2011-03-25 | Катализатор для процесса гидродепарафинизации и способ его получения |
US14/306,447 US9518233B2 (en) | 2010-04-14 | 2014-06-17 | Catalyst for a hydrodgenation dewaxing process and method for manufacturing same |
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KR102068312B1 (ko) * | 2013-10-18 | 2020-01-20 | 에스케이이노베이션 주식회사 | 활성화된 eu-2 제올라이트 및 이의 용도 |
CN106994365A (zh) * | 2016-01-26 | 2017-08-01 | 中国石油化工股份有限公司 | 一种加氢脱蜡催化剂制备方法和由该方法制得的催化剂及其应用 |
KR101692547B1 (ko) | 2016-04-26 | 2017-01-03 | 에스케이이노베이션 주식회사 | 중질기유의 헤이즈 저감 방법 및 헤이즈가 저감된 수소 첨가 이성화 촉매계 |
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