WO2008035155A2 - Reaction system for production of diesel fuel from vegetable and animal oils - Google Patents
Reaction system for production of diesel fuel from vegetable and animal oils Download PDFInfo
- Publication number
- WO2008035155A2 WO2008035155A2 PCT/IB2007/002485 IB2007002485W WO2008035155A2 WO 2008035155 A2 WO2008035155 A2 WO 2008035155A2 IB 2007002485 W IB2007002485 W IB 2007002485W WO 2008035155 A2 WO2008035155 A2 WO 2008035155A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- oil
- reaction unit
- zsm
- tubular reaction
- tubular
- Prior art date
Links
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 118
- 239000008158 vegetable oil Substances 0.000 title claims abstract description 37
- 239000010775 animal oil Substances 0.000 title claims abstract description 26
- 235000013311 vegetables Nutrition 0.000 title abstract description 21
- 239000002283 diesel fuel Substances 0.000 title description 25
- 238000004519 manufacturing process Methods 0.000 title description 10
- 239000007788 liquid Substances 0.000 claims abstract description 60
- 239000000203 mixture Substances 0.000 claims abstract description 55
- 238000000034 method Methods 0.000 claims abstract description 51
- 230000008569 process Effects 0.000 claims abstract description 42
- 239000003054 catalyst Substances 0.000 claims abstract description 40
- 239000000446 fuel Substances 0.000 claims abstract description 36
- 239000003921 oil Substances 0.000 claims abstract description 34
- 239000012808 vapor phase Substances 0.000 claims abstract description 24
- 230000002378 acidificating effect Effects 0.000 claims abstract description 18
- 229910052751 metal Inorganic materials 0.000 claims abstract description 18
- 239000002184 metal Substances 0.000 claims abstract description 18
- 235000019198 oils Nutrition 0.000 claims description 33
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 18
- 235000015112 vegetable and seed oil Nutrition 0.000 claims description 16
- 239000003549 soybean oil Substances 0.000 claims description 14
- 235000012424 soybean oil Nutrition 0.000 claims description 14
- 229910052697 platinum Inorganic materials 0.000 claims description 12
- 229910021536 Zeolite Inorganic materials 0.000 claims description 9
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 9
- 239000010457 zeolite Substances 0.000 claims description 9
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 6
- 235000019482 Palm oil Nutrition 0.000 claims description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 4
- 239000002540 palm oil Substances 0.000 claims description 4
- 239000003784 tall oil Substances 0.000 claims description 4
- 235000006205 Balanites Nutrition 0.000 claims description 3
- 241000935123 Balanites Species 0.000 claims description 3
- 241000221089 Jatropha Species 0.000 claims description 3
- 235000019486 Sunflower oil Nutrition 0.000 claims description 3
- 235000005687 corn oil Nutrition 0.000 claims description 3
- 239000002285 corn oil Substances 0.000 claims description 3
- 229910001657 ferrierite group Inorganic materials 0.000 claims description 3
- 229910052763 palladium Inorganic materials 0.000 claims description 3
- 239000002600 sunflower oil Substances 0.000 claims description 3
- 240000002791 Brassica napus Species 0.000 claims description 2
- 235000006008 Brassica napus var napus Nutrition 0.000 claims description 2
- 235000019483 Peanut oil Nutrition 0.000 claims description 2
- 235000019484 Rapeseed oil Nutrition 0.000 claims description 2
- ZOJBYZNEUISWFT-UHFFFAOYSA-N allyl isothiocyanate Chemical compound C=CCN=C=S ZOJBYZNEUISWFT-UHFFFAOYSA-N 0.000 claims description 2
- 239000000828 canola oil Substances 0.000 claims description 2
- 235000019519 canola oil Nutrition 0.000 claims description 2
- 239000004359 castor oil Substances 0.000 claims description 2
- 235000019438 castor oil Nutrition 0.000 claims description 2
- 239000003240 coconut oil Substances 0.000 claims description 2
- 235000019864 coconut oil Nutrition 0.000 claims description 2
- 235000021323 fish oil Nutrition 0.000 claims description 2
- ZEMPKEQAKRGZGQ-XOQCFJPHSA-N glycerol triricinoleate Natural products CCCCCC[C@@H](O)CC=CCCCCCCCC(=O)OC[C@@H](COC(=O)CCCCCCCC=CC[C@@H](O)CCCCCC)OC(=O)CCCCCCCC=CC[C@H](O)CCCCCC ZEMPKEQAKRGZGQ-XOQCFJPHSA-N 0.000 claims description 2
- 239000010460 hemp oil Substances 0.000 claims description 2
- 239000010699 lard oil Substances 0.000 claims description 2
- 239000000944 linseed oil Substances 0.000 claims description 2
- 235000021388 linseed oil Nutrition 0.000 claims description 2
- 239000008164 mustard oil Substances 0.000 claims description 2
- 239000004006 olive oil Substances 0.000 claims description 2
- 235000008390 olive oil Nutrition 0.000 claims description 2
- 239000000312 peanut oil Substances 0.000 claims description 2
- 235000005713 safflower oil Nutrition 0.000 claims description 2
- 239000003813 safflower oil Substances 0.000 claims description 2
- 239000003760 tallow Substances 0.000 claims description 2
- 239000010698 whale oil Substances 0.000 claims description 2
- 239000011959 amorphous silica alumina Substances 0.000 claims 2
- 238000004064 recycling Methods 0.000 claims 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 7
- 229910052717 sulfur Inorganic materials 0.000 abstract description 7
- 239000011593 sulfur Substances 0.000 abstract description 7
- 239000000047 product Substances 0.000 description 37
- 235000019602 lubricity Nutrition 0.000 description 27
- 239000002253 acid Substances 0.000 description 12
- 150000001875 compounds Chemical class 0.000 description 11
- 235000014113 dietary fatty acids Nutrition 0.000 description 11
- 239000000194 fatty acid Substances 0.000 description 11
- 229930195729 fatty acid Natural products 0.000 description 11
- 150000004665 fatty acids Chemical class 0.000 description 10
- 229930195733 hydrocarbon Natural products 0.000 description 9
- 150000002430 hydrocarbons Chemical class 0.000 description 9
- 239000003225 biodiesel Substances 0.000 description 8
- 239000012263 liquid product Substances 0.000 description 7
- -1 methanol or ethanol Chemical compound 0.000 description 7
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 6
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 6
- 150000007513 acids Chemical class 0.000 description 6
- 238000009835 boiling Methods 0.000 description 6
- 239000010779 crude oil Substances 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 239000004215 Carbon black (E152) Substances 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 5
- 238000004821 distillation Methods 0.000 description 5
- 239000012074 organic phase Substances 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 241000196324 Embryophyta Species 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- 241001465754 Metazoa Species 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 230000009849 deactivation Effects 0.000 description 3
- 238000002290 gas chromatography-mass spectrometry Methods 0.000 description 3
- 238000006317 isomerization reaction Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 150000003626 triacylglycerols Chemical class 0.000 description 3
- ZCYVEMRRCGMTRW-UHFFFAOYSA-N 7553-56-2 Chemical compound [I] ZCYVEMRRCGMTRW-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical class [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- 230000002411 adverse Effects 0.000 description 2
- 150000004996 alkyl benzenes Chemical class 0.000 description 2
- 125000004432 carbon atom Chemical group C* 0.000 description 2
- 229910002090 carbon oxide Inorganic materials 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 125000004494 ethyl ester group Chemical group 0.000 description 2
- 239000003925 fat Substances 0.000 description 2
- 235000019197 fats Nutrition 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 229910052740 iodine Inorganic materials 0.000 description 2
- 239000011630 iodine Substances 0.000 description 2
- 239000000314 lubricant Substances 0.000 description 2
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 2
- 238000005457 optimization Methods 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000004088 simulation Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 150000004670 unsaturated fatty acids Chemical class 0.000 description 2
- 235000021122 unsaturated fatty acids Nutrition 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- WRIDQFICGBMAFQ-UHFFFAOYSA-N (E)-8-Octadecenoic acid Natural products CCCCCCCCCC=CCCCCCCC(O)=O WRIDQFICGBMAFQ-UHFFFAOYSA-N 0.000 description 1
- LQJBNNIYVWPHFW-UHFFFAOYSA-N 20:1omega9c fatty acid Natural products CCCCCCCCCCC=CCCCCCCCC(O)=O LQJBNNIYVWPHFW-UHFFFAOYSA-N 0.000 description 1
- QSBYPNXLFMSGKH-UHFFFAOYSA-N 9-Heptadecensaeure Natural products CCCCCCCC=CCCCCCCCC(O)=O QSBYPNXLFMSGKH-UHFFFAOYSA-N 0.000 description 1
- 241000251468 Actinopterygii Species 0.000 description 1
- 244000057001 Balanites aegyptiaca Species 0.000 description 1
- 235000009581 Balanites aegyptiaca Nutrition 0.000 description 1
- 239000002028 Biomass Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 229910003296 Ni-Mo Inorganic materials 0.000 description 1
- ZQPPMHVWECSIRJ-UHFFFAOYSA-N Oleic acid Natural products CCCCCCCCC=CCCCCCCCC(O)=O ZQPPMHVWECSIRJ-UHFFFAOYSA-N 0.000 description 1
- 239000005642 Oleic acid Substances 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 238000005899 aromatization reaction Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 150000001735 carboxylic acids Chemical class 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000004035 construction material Substances 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 150000001934 cyclohexanes Chemical class 0.000 description 1
- 238000006392 deoxygenation reaction Methods 0.000 description 1
- 239000008157 edible vegetable oil Substances 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000011121 hardwood Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- QXJSBBXBKPUZAA-UHFFFAOYSA-N isooleic acid Natural products CCCCCCCC=CCCCCCCCCC(O)=O QXJSBBXBKPUZAA-UHFFFAOYSA-N 0.000 description 1
- 238000005461 lubrication Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- DDTIGTPWGISMKL-UHFFFAOYSA-N molybdenum nickel Chemical compound [Ni].[Mo] DDTIGTPWGISMKL-UHFFFAOYSA-N 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- ZQPPMHVWECSIRJ-KTKRTIGZSA-N oleic acid Chemical compound CCCCCCCC\C=C/CCCCCCCC(O)=O ZQPPMHVWECSIRJ-KTKRTIGZSA-N 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 235000005985 organic acids Nutrition 0.000 description 1
- 230000008520 organization Effects 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000010773 plant oil Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000004537 pulping Methods 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000007363 ring formation reaction Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 230000009261 transgenic effect Effects 0.000 description 1
- 229910052723 transition metal Inorganic materials 0.000 description 1
- 150000003624 transition metals Chemical class 0.000 description 1
- 238000004148 unit process Methods 0.000 description 1
- 239000010913 used oil Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000001993 wax Substances 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
- C10L1/08—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for compression ignition
-
- 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
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/42—Catalytic treatment
- C10G3/44—Catalytic treatment characterised by the catalyst used
- C10G3/47—Catalytic treatment characterised by the catalyst used containing platinum group metals or compounds thereof
-
- 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
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/42—Catalytic treatment
- C10G3/44—Catalytic treatment characterised by the catalyst used
- C10G3/48—Catalytic treatment characterised by the catalyst used further characterised by the catalyst support
- C10G3/49—Catalytic treatment characterised by the catalyst used further characterised by the catalyst support containing crystalline aluminosilicates, e.g. molecular sieves
-
- 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
- C10G2300/10—Feedstock materials
- C10G2300/1011—Biomass
- C10G2300/1014—Biomass of vegetal origin
-
- 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
- C10G2300/10—Feedstock materials
- C10G2300/1011—Biomass
- C10G2300/1018—Biomass of animal origin
-
- 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
-
- 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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Definitions
- liquid fuels particularly diesel, jet and naphtha fuels, from vegetable and/or animal oils.
- NO x nitrogen oxide
- United Kingdom Patent Specification 1 524 781 discloses converting ester- containing vegetable oils into one or more hydrocarbons by pyrolysis at 300 to 700°C in the presence of a catalyst which comprises silica-alumina in admixture with an oxide of a transition metal of Groups IIA, IIIA, IVA, VA, VIA, VIIA or VIII of the periodic table, preferably in a fluidized bed, moving bed or fixed bed tubular reactor at atmospheric pressure.
- U.S. Patent No. 5,705,722 discloses a process for producing additives for diesel fuels having high cetane numbers and serving as fuel ignition improvers.
- biomass feedstock selected from (a) tall oil containing less than 0.5 wt % ash, less than 25 wt % unsaponifiables, up to 50 wt % diterpenic acids and 30 to 60 wt % unsaturated fatty acids, (b) wood oils from the pulping of hardwood species, (c) animal fats and (d) blends of said tall oil with plant or vegetable oil containing substantial amounts of unsaturated fatty acids or animal fats, is subjected to hydroprocessing by contacting the feedstock with gaseous hydrogen under hydroprocessing conditions in the presence of a hydroprocessing catalyst to obtain a product mixture. This product mixture is then separated and fractionated to obtain a hydrocarbon product boiling in the diesel fuel boiling range, this product being the high cetane number additive.
- U.S. Patent Publication No. 2004/0055209 discloses a fuel composition for diesel engines comprising 0.1-99% by weight of a component or a mixture of components produced from biological raw material originating from plants and/or animals and/or fish and 0-20% of components containing oxygen. Both components are mixed with diesel components based on crude oil and/or fractions from Fischer- Tropsch process.
- U.S. Patent Publication No. 2004/0230085 discloses a process for producing a hydrocarbon component of biological origin comprising at least two steps, the first one of which is a hydrodeoxygenation step and the second one is an isomerization step operated using the counter-current flow principle.
- Fuel properties important for potential diesel applications include: (i) lubricity; (ii) cetane number; (iii) density; (iv) viscosity; (v) lower heating value; (vi) sulfur; (vii) flash point; (viii) cloud point; (ix) Distillation Curve; (x) carbon residue; (xi) ash; and (xii) Iodine Value. Lubricity affects the wear of pumps and injection systems.
- Lubricity can be defined as the property of a lubricant that causes a difference in friction under conditions of boundary lubrication when all known factors except the lubricant itself are the same; thus, the lower the friction, the higher the lubricity.
- Cetane number rates the ignition quality of diesel fuels. Density, normally expressed as specific gravity, is defined as the ratio of the mass of a volume of the fuel to the mass of the same volume of water. Viscosity measures the fluid resistance to flow. Lower heating value is a measure of available energy in the fuel. Flash point is the lowest temperature at which a combustible mixture can be formed above the liquid fuel. Cloud point measures the first appearance of wax.
- Distillation Curve is characterized by the initial temperature at which the first drop of liquid leaves the condenser and subsequent temperatures at each 10 vol% of the liquid. Carbon residue correlates with the amount of carbonaceous deposits in a combustion chamber. Ash refers to extraneous solids that reside after combustion. Iodine Value measures the number of double bonds. [0010] A comparison of properties of biodiesel and EN standard EN590:2005 diesel can be found in Table 1.
- Boiling Point 0 C 180 to 340 315 to 350
- a process for producing a liquid fuel composition comprising providing oil selected from the group consisting of vegetable oil, animal oil, and mixtures thereof and hydrodeoxygenating and hydroisomerizing the oil.
- the hydrodeoxygenating and hydroisomerizing comprises feeding the oil to a tubular reaction unit containing a catalyst comprising an acidic component and a metal component, feeding effluent from the tubular reaction unit to a vapor-liquid separator, and feeding a vapor phase separated from the effluent from the tubular reaction unit to an adiabatic reaction unit comprising the same catalyst as in the tubular reaction unit comprising an acidic component and a metal component. Liquid separated from the effluent from the tubular reaction unit can be recycled to the tubular reaction unit.
- the tubular reaction unit is a multitubular reaction unit and/or operates in trickle-bed mode and the adiabatic reaction unit comprises a single tube.
- a reaction system for producing a liquid fuel composition comprising a tubular reaction unit containing a catalyst comprising an acidic component and a metal component, an adiabatic reaction unit containing the same catalyst as in the tubular reaction unit comprising an acidic component and a metal component, and a vapor-liquid separator disposed between the tubular reaction unit and the adiabatic reaction unit.
- the adiabatic reaction unit can be located downstream of the tubular reaction unit.
- the tubular reaction unit is a multi-tubular reaction unit and/or operates in trickle-bed mode and the adiabatic reaction unit comprises a single tube.
- High quality liquid fuels in particular diesel and naphtha fuels, can be obtained from vegetable and/or animal oils in high yield by a process comprising hydrodeoxygenation and hydroisomerization.
- Triglycerides of fatty acids contained in the vegetable and/or animal oil are deoxygenated to form normal C 12 to C 18 or C 14 to C is paraffins, which are hydroisomerized in the same stage to form various isoparaff ⁇ ns. Minor cyclization and aromatization to alkyl cyclohexane and alkyl benzene may also occur.
- the deoxygenation can comprise removal of oxygen in the form of water and carbon oxides from the triglycerides.
- Hydrocracking is inhibited, so as to maintain the range of carbon number of hydrocarbons formed in the range of Ci 2 to C 18 or Ci 4 to Ci 8 .
- Hydrodeoxygenation of vegetable and/or animal oils alone would generate a mixture of long-chain straight Ci 2 to Ci 8 or Ci 4 to Ci 8 paraffins. While such long-chain straight Cj 2 to Ci 8 or Ci 4 to Ci 8 paraffins would be in the paraffin carbon number range of diesel fuels, the fuel properties of such long-chain straight Ci 2 to Ci 8 or Ci 4 to Ci 8 paraffins would be significantly different from those of diesel fuels. Therefore, production of diesel fuel requires hydroisomerization of the paraffins.
- the presently disclosed process for producing a liquid fuel composition comprises providing oil selected from the group consisting of vegetable oil, animal oil, and mixtures thereof and hydrodeoxygenating and hydroisomerizing the oil.
- oil selected from the group consisting of vegetable oil, animal oil, and mixtures thereof and hydrodeoxygenating and hydroisomerizing the oil.
- the liquid fuel composition produced by the presently disclosed process may further comprise 2- 10% lighter naphtha products boiling below 150°C as well as heavier distillate products.
- the hydrodeoxygenating and hydroisomerizing disclosed herein comprises feeding the oil to a tubular reaction unit containing a catalyst comprising an acidic component and a metal component, feeding effluent from the tubular reaction unit to a vapor-liquid separator, and feeding a vapor phase separated from the effluent from the tubular reaction unit to an adiabatic reaction unit comprising the same catalyst as in the tubular reaction unit comprising an acidic component and a metal component. While the effluent from the tubular reaction unit is primarily in a vapor phase, liquid separated from the effluent from the tubular reaction unit can be recycled to the tubular reaction unit.
- the tubular reaction unit which is contained within a shell, is a multi-tubular reaction unit and/or operates in trickle- bed mode and the adiabatic reaction unit comprises a single tube.
- the tube(s) e.g., 1,000 or even 5,000 tubes
- coolant contained in a shell jacketing the tube(s) for optimal temperature control.
- the vapor-liquid separator disposed downstream of the tubular reaction unit functions as a heat exchanger and sets the temperature of the vapor phase exiting the vapor-liquid separator, which is to be fed to the reaction unit following the vapor-liquid separator.
- the vapor phase leaves the vapor-liquid separator at a temperature of about 330 to 400°C.
- the reaction unit is adiabatic, and thus, in addition to setting the temperature of the vapor phase exiting the vapor-liquid separator, the vapor-liquid separator also sets the temperature of the reaction unit following the vapor-liquid separator and allows for optimization of the process.
- tubular reaction unit vapor-liquid separator, and adiabatic reaction unit may be contained within one or more reaction vessels.
- catalysts for the presently disclosed process are dual- functional catalysts comprising a metal component and an acidic component.
- metal components are platinum or palladium.
- the metal component is platinum.
- the acidic component can comprise an acidic function in a porous solid support.
- acidic components include, for example, amorphous silica aluminas, fluorided alumina, ZSM- 12, ZSM-21, ZSM-22, ZSM-23, ZSM-35, ZSM-38, ZSM-48, ZSM-57, SSZ-32, ferrierite, SAPO- 11, SAPO-31, SAPO-41, MAPO-11, MAPO-31, Y zeolite, L zeolite and Beta zeolite.
- the catalyst is Pt/SAPO-11, specifically 0.5-1 wt% Pt/S APO- 11 , more specifically 1 wt% Pt/SAPO- 11.
- the tubular reaction unit is operated at conditions comprising a liquid hourly space velocity (LHSV) in the range of 0.5-5 h '1 , for example, 0.6-3 h "1 , 0.7-1.2 h ' ⁇ or 1-2.5 h "1 , at a temperature varying between 300 and 450°C, for example, between 320 and 400°C, at a pressure varying between 10 and 60 atm, for example, 20-40 atm, and a H 2 /oil ratio of about 300- 1200 NL/L, for example, 500- 1000 NL/L.
- LHSV liquid hourly space velocity
- Lubricity is especially important with regard to modern diesel fuels, as modern engines have very high injection pressures in excess of 24,000 pounds per square inch. Good lubricity is necessary to prevent risk of catastrophic engine failure. In general, an acceptable lubricity refers to a lubricity that would allow modern engines to operate more efficiently.
- the diesel fuel has a maximum high-frequency reciprocating rig (HRFF) lubricity of 400 ⁇ m (according to International Organization for Standardization (ISO) standard 12156/1), in accordance with the recommendation of the World Wide Fuel Charter, Category 4.
- HRFF high-frequency reciprocating rig
- the lubricity is less than 300 ⁇ m according to ISO 12156/1, for exmaple, the lubricity is less than 200 ⁇ m according to ISO 12156/1.
- suitable vegetable oils include soybean oil, palm oil, corn oil, sunflower oil, oils from desertic plants such as, for example, jatropha oil and balanites oil, rapeseed oil, colza oil, canola oil, tall oil, safflower oil, hempseed oil, olive oil, linseed oil, mustard oil, peanut oil, castor oil, coconut oil, and mixtures thereof.
- vegetable oils include soybean oil, palm oil, corn oil, sunflower oil, jatropha oil, balanites oil, for example, from Balanites aegyptiaca, and mixtures thereof.
- the vegetable oil may be genetically modified oil, produced from transgenic crops.
- the vegetable oil may be crude vegetable oil or refined or edible vegetable oil. If crude vegetable oil is used, the vegetable oil can be pretreated, for example, to separate or extract impurities from the crude vegetable oil.
- Suitable animal oils include, for example, lard oil, tallow oil, train oil, fish oil, and mixtures thereof. Further, the vegetable and/or animal oil may be new oil, used oil, waste oil, or mixtures thereof.
- compositions derived from vegetable and/or animal oil can be used in the presently disclosed process.
- compositions derived from vegetable and/or animal oil refers to compositions which originate from or are the byproduct of processing vegetable and/or animal oil ⁇ e.g., vapor overhead stream from distilling vegetable and/or animal oil, residual non-vaporizable remaining portion, etc.).
- palm oil distillate containing greater than 70 wt% fatty acids can be used in the presently disclosed process.
- the diesel fuel composition produced by the presently disclosed methods comprises a mixture of Ci 2 to Ci 8 or Ci 4 to Ci 8 paraffins with a ratio of iso to normal paraffins from 0.5 to 8, for example, from 2 to 8, from 2 to 6, from 2 to 4, from 1 to 4, or from 4 to 7; less than 5 ppm sulfur, for example, less than 1 ppm sulfur; and acceptable lubricity.
- the diesel fuel composition can have a lubricity of less than 400 ⁇ m, for example, less than 300 ⁇ m or less than 200 ⁇ m, according to ISO 12156/1.
- the diesel fuel composition can comprise less than or equal to 0.6 wt%, for example, 0.1-0.6 wt%, of one or more oxygenated compounds, which, without wishing to be bound by any theory, are believed to contribute to the acceptable lubricity of the diesel fuel composition.
- the one or more oxygenated compounds comprise acid, for example, one or more fatty acids.
- the one or more oxygenated compounds e.g., acid
- fatty acids refers to long chain saturated and/or unsaturated organic acids having at least 8 carbon atoms, for example, 12 to 18 or 14 to 18 carbon atoms.
- oxygenated compounds for example, one or more fatty acids
- the low content of one or more oxygenated compounds, for example, one or more fatty acids, in the diesel fuel composition may contribute to the acceptable lubricity of a diesel fuel composition; such oxygenated compounds, present in the vegetable and/or animal oil feedstock, may survive the non-severe hydrodeoxygenation/hydroisomerization conditions employed in the presently disclosed process.
- the diesel fuel composition may comprise alkyl cyclohexane, for example, less than 10 wt%, and/or alkyl benzene, for example, less than 15 wt%.
- the characteristics of the diesel fuel composition, and naphtha, produced by the presently disclosed methods may vary depending on the vegetable and/or animal oil starting product, process conditions, and catalyst used. In an embodiment, selection of vegetable and/or animal oil starting product, process conditions, and catalyst allows for high yield of high quality diesel fuel composition, with preferred properties, and minimized production of lighter components including, for example, naphtha, carbon oxides and C 1 to C 4 hydrocarbons.
- paraffinic diesel fuel compositions produced by the presently disclosed methods provide superior fuel properties, especially for low temperature performance (e.g., density, viscosity, cetane number, lower heating value, cloud point, and CFPP), to biodiesel, a mixture of methyl or ethyl esters.
- low temperature performance e.g., density, viscosity, cetane number, lower heating value, cloud point, and CFPP
- biodiesel a mixture of methyl or ethyl esters.
- fuel properties such as, for example, lubricity, may be controlled through variation of process conditions and/or catalyst(s).
- the initial boiling point (IBP) is in the range of 160°C-240°C and the 90 vol% distillation temperature is in the range of 300°C-360°C.
- the produced naphtha is highly pure and particularly suitable for use as a solvent and/or chemical feedstock, e.g., a cracking stock.
- Refined soybean oil was fed to a fixed-bed reactor packed with a granulated Ni-Mo catalyst operated at an LHSV of 1.0 h "1 , 375°C, 40 atm, and an H 2 /oil ratio of 1200 NL/L (Stage 1).
- the total liquid product was separated into two phases, water and an organic phase.
- the organic phase was fed to a fixed-bed reactor packed with a granulated 1 wt% Pt/S APO-11 catalyst operated at an LHSV of 3.0 h ⁇ ⁇ 380°C, 50 atm, and an H 2 /oil ratio of 500 NL/L (Stage 2).
- the organic phase from Stage 1 and the diesel product from Stage 2 were analyzed according to ASTM methods and their compositions were measured by GC-MS and confirmed by NMR. The results can be found in Table 3.
- the diesel product from Stage 2 exhibited a poorer lubricity (502 ⁇ m) as compared to that of the organic phase from Stage 1 (352 ⁇ m). Without wishing to be bound by any theory, it is believed that the increase in ratio of branched to linear paraffins in the diesel product from Stage 2, as compared to the organic phase from Stage 1 , resulted in a change of fuel properties. Comparative Example 2. Production of Diesel from Soybean Oil by a Two Stage Process
- the diesel product from Stage 1 exhibited acceptable properties, including a lubricity of 306 ⁇ m. As the composition of the diesel product from Stage 2 did not significantly differ from the diesel product from Stage 1, the properties of the diesel product from Stage 2 are similar to those of the diesel product from Stage 1. However, the diesel product from Stage 2 exhibited a poorer lubricity (437 ⁇ m) as compared to that of the diesel product from Stage 1 (306 ⁇ m), similar to the diesel production from Stage 2 of Comparative Example 1.
- water may act as an inhibitor to isomerization, which requires higher catalyst activity, and the removal of water between Stage 1 and Stage 2 in Comparative Example 1 and Comparative Example 2 may also remove acid, thereby affecting final product lubricity.
- Adding 0.1 wt% of oleic acid to the diesel product of Stage 2 improved its lubricity from 437 ⁇ m to 270 ⁇ m.
- the low content of one or more oxygenated compounds, such as one or more fatty acids, in the product of the process may contribute to the acceptable lubricity of the diesel product.
- Example 3 The reactor setup and the operating conditions of Example 3 were based on the results of kinetic studies and reactor simulations using soybean oil.
- concentrations of the soybean oil, acids, paraffins, olefins, cyclohexanes, aromatics and light compounds were measured as a function of residence time and temperature. Vapor-liquid equilibrium was provided by the reactor simulations. For a residence time of 15 to 25 minutes, the soybean oil was nearly completely converted. The acid content in the product(s) peaked at about 10 to 15 minutes, and then decreased with additional residence time.
- diesel fuel compositions produced in accordance with the presently claimed methods can comprise less than or equal to 0.6 wt% of one or more oxygenated compounds (e.g., acids).
- the effluent of the single wall-cooled reactor tube flowed through a gas-liquid separator maintained at 30 atm and 373°C, in which a very small amount of liquid (i.e., 0.2 wt% of the refined soybean oil fed to the single wall-cooled reactor tube) was separated from a vapor phase.
- the vapor phase from the separator flowed upward to a single tube, adiabatic, fixed-bed reaction unit packed with a granulated 1 wt% Pt/SAPO-11 catalyst operated at an LHSV of 1.4 h "1 , 373-375°C, 30 atm, and an H 2 /oil ratio of 550 NL/L.
- the diesel product from the adiabatic reaction unit was analyzed according to ASTM methods and its composition was measured by GC-MS. The results can be found in Table 5.
- the diesel product according to Example 3 exhibited acceptable properties, including a lubricity of 346 ⁇ m.
- the temperature of the adiabatic reaction unit following the vapor-liquid separator is set by the temperature of the vapor-liquid separator. Heat loss can cause a temperature drop in the vapor phase products from the tubular reaction unit. Assuming that heat loss is avoided, if the temperature of the vapor-liquid separator is low (i.e., lower than the temperature of the vapor phase products from the tubular reaction unit), the vapor phase products may undesirably condense to liquid prior to hydroisomerization in the adiabatic reaction unit.
- the temperature of the vapor-liquid separator can be set such that the temperature of the vapor- liquid separator is close to the temperature of the tubular reaction unit, and more specifically, the temperature of the vapor phase products from the tubular reaction unit.
- Most of the heat of the hydrodeoxygenation and hydroisomerization reaction is generated in the tubular reaction unit, which can be a wall-cooled reactor. Accordingly, the reaction unit downstream of the vapor-liquid separator can be run adiabatically.
- the vapor-liquid separator which can provide different conditions in the downstream adiabatic reaction unit than in the upstream tubular reaction unit, can also ensure that the downstream adiabatic reaction unit is run in vapor phase.
- the temperature of the adiabatic reaction unit following the vapor-liquid separator can be set in the range of about 350 to 400°C or about 360 to 385°C.
- the temperature of the vapor-liquid separator in Example 3 was maintained at 373°C and the temperature of the adiabatic reaction in Example 3 was operated at 373°C, to minimize condensation of vapor phase products to liquid prior to hydroisomerization in the adiabatic reaction unit.
- the vapor-liquid separator can be used to set the temperature of the adiabatic reaction unit following the vapor-liquid separator.
- the effluent from the single wall-cooled reactor tube is primarily in a vapor phase (e.g., vapor phase can comprise about 95 to 99.9 wt% of the effluent).
- the liquid separated from the vapor phase in the vapor-liquid separator can contain as much as 40 wt% acids.
- the catalyst contained in the reaction units is sensitive to coking and deactivation as a result of contact with heavy compounds (e.g., acids) in the liquid products. Thus, liquid products can negative affect selectivity of desired products and stability of the catalyst.
- separation of liquid from the vapor phase in the vapor-liquid separator i.e., the vapor phase to be fed to the adiabatic reaction unit
- tubular e.g., single wall-cooled reactor tube or multi-tubular
- adiabatic reaction units e.g., single wall-cooled reactor tube or multi-tubular
- a vapor-liquid separator disposed therebetween allows for improved performance and stability of the catalyst, especially the catalyst contained within the adiabatic reaction unit.
- the life of the catalyst contained within the adiabatic reaction unit can be extended as a result of using a vapor-liquid separator disposed between the tubular and adiabatic reaction units.
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Abstract
Abstract A process for producing a fuel composition from vegetable and/or animal oil comprises feeding the oil to a tubular reaction unit containing a catalyst comprising an acidic component and a metal component, feeding effluent from the tubular reaction unit to a vapor-liquid separator, and feeding a vapor phase separated from the effluent from the tubular reaction unit to an adiabatic reaction unit comprising the same catalyst as in the tubular reaction unit comprising an acidic component and a metal component. The produced fuel composition has acceptable lubricity and comprises a mixture of C12 to C18 or C14 to C18 paraffins having a ratio of iso to normal paraffins of 2 to 8 and less than 5 ppm sulfur.
Description
REACTION SYSTEM FOR PRODUCTION OF DIESEL FUEL FROM VEGETABLE AND ANIMAL OILS
Background Field of Art
[0001] Provided is a process and reaction system for the production of liquid fuels, particularly diesel, jet and naphtha fuels, from vegetable and/or animal oils.
Description of the Related Art [0002] Most combustible liquid fuels used for on road, off road, stationary engines, and combustion turbines and boilers in the world today are derived from crude oil. However, there are several limitations to using crude oil as a fuel source. For example, crude oil is in limited supply, includes a high content of aromatics, and contains sulfur and nitrogen-containing compounds that can adversely affect the environment. There is a great desire and need in the industry to provide combustible liquid fuels that are more environmentally friendly, display good engine performance, and which are available from alternative sources that are abundantly renewable. [0003] Vegetable and animal oils are an abundant and renewable source. The use of vegetable oil in diesel engines requires significant engine modification, including changing of piping and injector construction materials, otherwise engine running times are decreased, maintenance costs are increased due to higher wear, and the danger of engine failure is increased. The current conversion of vegetable and animal oils to combustible liquid fuels typically involves transesterifϊcation of the oils, which are triglycerides of Cn to C22 straight-chain carboxylic acids, with a lower alcohol such as methanol or ethanol, to form a mixture of methyl or ethyl esters called "biodiesel". This process is relatively complex, typical of the chemical industry rather than the petrochemical industry. Furthermore, the composition of biodiesel, which is completely different from that of diesel produced from crude oil, may have adverse effects on engine performance. Biodiesel exhibits poor low
temperature performance characteristics and increased nitrogen oxide (NOx) emissions compared to conventional fuels derived from crude oil. [0004] In the search for alternative and renewable sources, there is increasing interest in producing liquid fuels from biological raw materials for use as fuel by themselves or in mixture with the petroleum-derived fuels in use today. The patent literature describes methods for producing hydrocarbon mixtures from biological sources, including vegetable oils.
[0005] United Kingdom Patent Specification 1 524 781 discloses converting ester- containing vegetable oils into one or more hydrocarbons by pyrolysis at 300 to 700°C in the presence of a catalyst which comprises silica-alumina in admixture with an oxide of a transition metal of Groups IIA, IIIA, IVA, VA, VIA, VIIA or VIII of the periodic table, preferably in a fluidized bed, moving bed or fixed bed tubular reactor at atmospheric pressure. [0006] U.S. Patent No. 5,705,722 discloses a process for producing additives for diesel fuels having high cetane numbers and serving as fuel ignition improvers. In the process, biomass feedstock selected from (a) tall oil containing less than 0.5 wt % ash, less than 25 wt % unsaponifiables, up to 50 wt % diterpenic acids and 30 to 60 wt % unsaturated fatty acids, (b) wood oils from the pulping of hardwood species, (c) animal fats and (d) blends of said tall oil with plant or vegetable oil containing substantial amounts of unsaturated fatty acids or animal fats, is subjected to hydroprocessing by contacting the feedstock with gaseous hydrogen under hydroprocessing conditions in the presence of a hydroprocessing catalyst to obtain a product mixture. This product mixture is then separated and fractionated to obtain a hydrocarbon product boiling in the diesel fuel boiling range, this product being the high cetane number additive.
[0007] U.S. Patent Publication No. 2004/0055209 discloses a fuel composition for diesel engines comprising 0.1-99% by weight of a component or a mixture of components produced from biological raw material originating from plants and/or animals and/or fish and 0-20% of components containing oxygen. Both components are mixed with diesel components based on crude oil and/or fractions from Fischer- Tropsch process.
[0008] U.S. Patent Publication No. 2004/0230085 discloses a process for producing a hydrocarbon component of biological origin comprising at least two steps, the first one of which is a hydrodeoxygenation step and the second one is an isomerization step operated using the counter-current flow principle. A biological raw material containing fatty acids and/or fatty acid esters serves as the feed stock. [0009] Fuel properties important for potential diesel applications include: (i) lubricity; (ii) cetane number; (iii) density; (iv) viscosity; (v) lower heating value; (vi) sulfur; (vii) flash point; (viii) cloud point; (ix) Distillation Curve; (x) carbon residue; (xi) ash; and (xii) Iodine Value. Lubricity affects the wear of pumps and injection systems. Lubricity can be defined as the property of a lubricant that causes a difference in friction under conditions of boundary lubrication when all known factors except the lubricant itself are the same; thus, the lower the friction, the higher the lubricity. Cetane number rates the ignition quality of diesel fuels. Density, normally expressed as specific gravity, is defined as the ratio of the mass of a volume of the fuel to the mass of the same volume of water. Viscosity measures the fluid resistance to flow. Lower heating value is a measure of available energy in the fuel. Flash point is the lowest temperature at which a combustible mixture can be formed above the liquid fuel. Cloud point measures the first appearance of wax. Distillation Curve is characterized by the initial temperature at which the first drop of liquid leaves the condenser and subsequent temperatures at each 10 vol% of the liquid. Carbon residue correlates with the amount of carbonaceous deposits in a combustion chamber. Ash refers to extraneous solids that reside after combustion. Iodine Value measures the number of double bonds. [0010] A comparison of properties of biodiesel and EN standard EN590:2005 diesel can be found in Table 1.
Table 1
Fuel Property Biodiesel EN590
Diesel
Density @ 15°C, kg/m3 «885 «835
Viscosity @ 400C, mm2/s «4.5 «3.5
Cetane Number
90 vol% Distillation, 0C
Cloud Point, 0C
Lower Heating Value, MJ/kg
Lower Heating Value, MJ/Iiters
Polyaromatics, wt%
Oxygen, wt%
Sulfur, mg/kg
[0011] The American Society for Testing and Materials (ASTM) standards for commercial diesel (ASTM D975) and biodiesel (ASTM D6751) can be found in Table 2.
Table 2
Fuel Property Diesel Biodiesel
ASTM D975 ASTM D6751
Lower Heating Value, BTU/gal 129,050 118,170
Kinematic Viscosity @ 400C,
1.3-4.1 4.0-6.0 cSt
Specific Gravity @ 600C,
0.85 0.88 g/cm3
Carbon, wt% 87 77
Hydrogen, wt% 13 12
Oxygen, by dif. wt% 0 11
Sulfur, ppm 500 0
Boiling Point, 0C 180 to 340 315 to 350
Flash Point, 0C 60 to 80 100 to 170
Cloud Point, 0C -15 to 5 -3 to 12
Pour Point, 0C -35 to -15 -5 to 10
Cetane Number 40-55 48-65
Lubricity (HFRR), μm 300-600 <300
[0012] There remains a need for alternative processes for conversion of vegetable and animal oils to fuels and diesel fuel compositions derived from vegetable and animal oils having better and more acceptable properties.
Summary
[0013] Provided is a process for producing a liquid fuel composition comprising providing oil selected from the group consisting of vegetable oil, animal oil, and mixtures thereof and hydrodeoxygenating and hydroisomerizing the oil. The hydrodeoxygenating and hydroisomerizing comprises feeding the oil to a tubular reaction unit containing a catalyst comprising an acidic component and a metal component, feeding effluent from the tubular reaction unit to a vapor-liquid separator, and feeding a vapor phase separated from the effluent from the tubular reaction unit to an adiabatic reaction unit comprising the same catalyst as in the tubular reaction unit comprising an acidic component and a metal component. Liquid separated from the effluent from the tubular reaction unit can be recycled to the tubular reaction unit. In an embodiment, the tubular reaction unit is a multitubular reaction unit and/or operates in trickle-bed mode and the adiabatic reaction unit comprises a single tube. [0014] Additionally provided is a reaction system for producing a liquid fuel composition comprising a tubular reaction unit containing a catalyst comprising an acidic component and a metal component, an adiabatic reaction unit containing the same catalyst as in the tubular reaction unit comprising an acidic component and a metal component, and a vapor-liquid separator disposed between the tubular reaction unit and the adiabatic reaction unit. The adiabatic reaction unit can be located downstream of the tubular reaction unit. In an embodiment, the tubular reaction unit is a multi-tubular reaction unit and/or operates in trickle-bed mode and the adiabatic reaction unit comprises a single tube.
Detailed Description [0015] High quality liquid fuels, in particular diesel and naphtha fuels, can be obtained from vegetable and/or animal oils in high yield by a process comprising
hydrodeoxygenation and hydroisomerization. Triglycerides of fatty acids contained in the vegetable and/or animal oil are deoxygenated to form normal C12 to C18 or C14 to C is paraffins, which are hydroisomerized in the same stage to form various isoparaffϊns. Minor cyclization and aromatization to alkyl cyclohexane and alkyl benzene may also occur. The deoxygenation can comprise removal of oxygen in the form of water and carbon oxides from the triglycerides. Hydrocracking is inhibited, so as to maintain the range of carbon number of hydrocarbons formed in the range of Ci2 to C18 or Ci4 to Ci8. [0016] Hydrodeoxygenation of vegetable and/or animal oils alone would generate a mixture of long-chain straight Ci2 to Ci8 or Ci4 to Ci8 paraffins. While such long- chain straight Cj2 to Ci8 or Ci4 to Ci8 paraffins would be in the paraffin carbon number range of diesel fuels, the fuel properties of such long-chain straight Ci2 to Ci8 or Ci4 to Ci8 paraffins would be significantly different from those of diesel fuels. Therefore, production of diesel fuel requires hydroisomerization of the paraffins. Accordingly, the presently disclosed process for producing a liquid fuel composition comprises providing oil selected from the group consisting of vegetable oil, animal oil, and mixtures thereof and hydrodeoxygenating and hydroisomerizing the oil. In addition to hydrocarbon products within the diesel boiling range, the liquid fuel composition produced by the presently disclosed process may further comprise 2- 10% lighter naphtha products boiling below 150°C as well as heavier distillate products.
[0017] The hydrodeoxygenating and hydroisomerizing disclosed herein comprises feeding the oil to a tubular reaction unit containing a catalyst comprising an acidic component and a metal component, feeding effluent from the tubular reaction unit to a vapor-liquid separator, and feeding a vapor phase separated from the effluent from the tubular reaction unit to an adiabatic reaction unit comprising the same catalyst as in the tubular reaction unit comprising an acidic component and a metal component. While the effluent from the tubular reaction unit is primarily in a vapor phase, liquid separated from the effluent from the tubular reaction unit can be recycled to the tubular reaction unit. In an embodiment, the tubular reaction unit, which is
contained within a shell, is a multi-tubular reaction unit and/or operates in trickle- bed mode and the adiabatic reaction unit comprises a single tube. [0018] As exothermic hydrodeoxygenation and double-bond saturation reactions take place in the tubular reaction unit, a significant amount of heat of reaction is removed from the tube(s) (e.g., 1,000 or even 5,000 tubes) of the tubular reaction unit, for example, by coolant contained in a shell jacketing the tube(s) for optimal temperature control. The vapor-liquid separator disposed downstream of the tubular reaction unit functions as a heat exchanger and sets the temperature of the vapor phase exiting the vapor-liquid separator, which is to be fed to the reaction unit following the vapor-liquid separator. In an embodiment, the vapor phase leaves the vapor-liquid separator at a temperature of about 330 to 400°C. As mild, vapor- phase hydroisomerization and similar reactions take place in the reaction unit following vapor-liquid separation, the reaction unit is adiabatic, and thus, in addition to setting the temperature of the vapor phase exiting the vapor-liquid separator, the vapor-liquid separator also sets the temperature of the reaction unit following the vapor-liquid separator and allows for optimization of the process. Use of both tubular and adiabatic reaction units allows for optimization of the hydrodeoxygenating and hydroisomerizing and improved performance and stability of the catalyst. The tubular reaction unit, vapor-liquid separator, and adiabatic reaction unit may be contained within one or more reaction vessels.
[0019] In an embodiment, catalysts for the presently disclosed process are dual- functional catalysts comprising a metal component and an acidic component. In an embodiment, metal components are platinum or palladium. In an embodiment, the metal component is platinum. The acidic component can comprise an acidic function in a porous solid support. In an embodiment, acidic components include, for example, amorphous silica aluminas, fluorided alumina, ZSM- 12, ZSM-21, ZSM-22, ZSM-23, ZSM-35, ZSM-38, ZSM-48, ZSM-57, SSZ-32, ferrierite, SAPO- 11, SAPO-31, SAPO-41, MAPO-11, MAPO-31, Y zeolite, L zeolite and Beta zeolite. In an embodiment, the catalyst is Pt/SAPO-11, specifically 0.5-1 wt% Pt/S APO- 11 , more specifically 1 wt% Pt/SAPO- 11.
[0020] The type and content of metal, acid strength, type and concentration of acid sites, solid porosity and pore size affect the type and quality of the diesel fuel produced. U.S. Patent Nos. 5,082,986, 5,135,638, 5,246,566, 5,282,958, and 5,723,716, the entire contents of which are hereby incorporated by reference, disclose representative process conditions using said catalysts for isomerization of different hydrocarbon feedstock. Further, typical processes and catalysts for dewaxing and hydroisomerization are described, for example, in U.S. Patent No. 6,702,937, the entire content of which is hereby incorporated by reference, and the references cited therein. [0021] The process is carried out at relatively mild conditions, for example, the tubular reaction unit is operated at conditions comprising a liquid hourly space velocity (LHSV) in the range of 0.5-5 h'1, for example, 0.6-3 h"1, 0.7-1.2 h'\ or 1-2.5 h"1, at a temperature varying between 300 and 450°C, for example, between 320 and 400°C, at a pressure varying between 10 and 60 atm, for example, 20-40 atm, and a H2/oil ratio of about 300- 1200 NL/L, for example, 500- 1000 NL/L. More severe conditions result in liquid fuel compositions with poorer lubricity, while more moderate to mild conditions result in liquid fuel compositions with better lubricity. [0022] Lubricity is especially important with regard to modern diesel fuels, as modern engines have very high injection pressures in excess of 24,000 pounds per square inch. Good lubricity is necessary to prevent risk of catastrophic engine failure. In general, an acceptable lubricity refers to a lubricity that would allow modern engines to operate more efficiently. In an embodiment, the diesel fuel has a maximum high-frequency reciprocating rig (HRFF) lubricity of 400 μm (according to International Organization for Standardization (ISO) standard 12156/1), in accordance with the recommendation of the World Wide Fuel Charter, Category 4. In an embodiment, the lubricity is less than 300 μm according to ISO 12156/1, for exmaple, the lubricity is less than 200 μm according to ISO 12156/1. [0023] Any vegetable and/or animal oil can be used in the presently disclosed process. For example, suitable vegetable oils include soybean oil, palm oil, corn oil, sunflower oil, oils from desertic plants such as, for example, jatropha oil and balanites oil, rapeseed oil, colza oil, canola oil, tall oil, safflower oil, hempseed oil,
olive oil, linseed oil, mustard oil, peanut oil, castor oil, coconut oil, and mixtures thereof. In an embodiment, vegetable oils include soybean oil, palm oil, corn oil, sunflower oil, jatropha oil, balanites oil, for example, from Balanites aegyptiaca, and mixtures thereof. The vegetable oil may be genetically modified oil, produced from transgenic crops. The vegetable oil may be crude vegetable oil or refined or edible vegetable oil. If crude vegetable oil is used, the vegetable oil can be pretreated, for example, to separate or extract impurities from the crude vegetable oil. Suitable animal oils include, for example, lard oil, tallow oil, train oil, fish oil, and mixtures thereof. Further, the vegetable and/or animal oil may be new oil, used oil, waste oil, or mixtures thereof.
[0024] The oil, or mixture of oils, used in the presently disclosed process can contain a high content of fatty acids {e.g., greater than or equal to 70 wt% fatty acids). Additionally, compositions derived from vegetable and/or animal oil that contains a high content of fatty acids can be used in the presently disclosed process. The phrase "compositions derived from vegetable and/or animal oil" refers to compositions which originate from or are the byproduct of processing vegetable and/or animal oil {e.g., vapor overhead stream from distilling vegetable and/or animal oil, residual non-vaporizable remaining portion, etc.). Thus, palm oil distillate containing greater than 70 wt% fatty acids can be used in the presently disclosed process.
[0025] The diesel fuel composition produced by the presently disclosed methods comprises a mixture of Ci2 to Ci8 or Ci4 to Ci8 paraffins with a ratio of iso to normal paraffins from 0.5 to 8, for example, from 2 to 8, from 2 to 6, from 2 to 4, from 1 to 4, or from 4 to 7; less than 5 ppm sulfur, for example, less than 1 ppm sulfur; and acceptable lubricity. Specifically, the diesel fuel composition can have a lubricity of less than 400 μm, for example, less than 300 μm or less than 200 μm, according to ISO 12156/1.
[0026] Additionally, the diesel fuel composition can comprise less than or equal to 0.6 wt%, for example, 0.1-0.6 wt%, of one or more oxygenated compounds, which, without wishing to be bound by any theory, are believed to contribute to the acceptable lubricity of the diesel fuel composition. In an embodiment, the one or
more oxygenated compounds comprise acid, for example, one or more fatty acids. In an embodiment, the one or more oxygenated compounds (e.g., acid), is present in an amount of less than or equal to 0.4 wt%, for example, 0.1-0.4 wt%. As used herein, the phrase "fatty acids" refers to long chain saturated and/or unsaturated organic acids having at least 8 carbon atoms, for example, 12 to 18 or 14 to 18 carbon atoms. Without wishing to be bound by any theory, it is believed that the low content of one or more oxygenated compounds, for example, one or more fatty acids, in the diesel fuel composition may contribute to the acceptable lubricity of a diesel fuel composition; such oxygenated compounds, present in the vegetable and/or animal oil feedstock, may survive the non-severe hydrodeoxygenation/hydroisomerization conditions employed in the presently disclosed process. The diesel fuel composition may comprise alkyl cyclohexane, for example, less than 10 wt%, and/or alkyl benzene, for example, less than 15 wt%. [0027] The characteristics of the diesel fuel composition, and naphtha, produced by the presently disclosed methods may vary depending on the vegetable and/or animal oil starting product, process conditions, and catalyst used. In an embodiment, selection of vegetable and/or animal oil starting product, process conditions, and catalyst allows for high yield of high quality diesel fuel composition, with preferred properties, and minimized production of lighter components including, for example, naphtha, carbon oxides and C1 to C4 hydrocarbons. The paraffinic diesel fuel compositions produced by the presently disclosed methods provide superior fuel properties, especially for low temperature performance (e.g., density, viscosity, cetane number, lower heating value, cloud point, and CFPP), to biodiesel, a mixture of methyl or ethyl esters. In contrast to the products of the process disclosed in U.S. Patent Publication No. 2004/0230085, disclosed herein are method for producing diesel fuel compositions with acceptable lubricities produced from vegetable and/or animal oil. More specifically, fuel properties, such as, for example, lubricity, may be controlled through variation of process conditions and/or catalyst(s). In general, with regards to the distillation curve of the diesel fuel composition produced by the presently disclosed methods, the initial boiling point (IBP) is in the range of 160°C-240°C and the 90 vol% distillation temperature is in
the range of 300°C-360°C. The produced naphtha is highly pure and particularly suitable for use as a solvent and/or chemical feedstock, e.g., a cracking stock.
Examples [0028] The following examples are intended to be non-limiting and merely illustrative.
Comparative Example 1. Production of Diesel from Soybean Oil Based on U.S. Patent Publication No. 2004/0230085
[0029] Refined soybean oil was fed to a fixed-bed reactor packed with a granulated Ni-Mo catalyst operated at an LHSV of 1.0 h"1, 375°C, 40 atm, and an H2/oil ratio of 1200 NL/L (Stage 1). The total liquid product was separated into two phases, water and an organic phase. The organic phase was fed to a fixed-bed reactor packed with a granulated 1 wt% Pt/S APO-11 catalyst operated at an LHSV of 3.0 h~\ 380°C, 50 atm, and an H2/oil ratio of 500 NL/L (Stage 2). The organic phase from Stage 1 and the diesel product from Stage 2 were analyzed according to ASTM methods and their compositions were measured by GC-MS and confirmed by NMR. The results can be found in Table 3.
Table 3
* Detection limit of 0.1 wt%
[0030] The diesel product from Stage 2 exhibited a poorer lubricity (502 μm) as compared to that of the organic phase from Stage 1 (352 μm). Without wishing to be bound by any theory, it is believed that the increase in ratio of branched to linear paraffins in the diesel product from Stage 2, as compared to the organic phase from Stage 1 , resulted in a change of fuel properties.
Comparative Example 2. Production of Diesel from Soybean Oil by a Two Stage Process
[0031] Refined soybean oil was fed to a fixed-bed reactor packed with a granulated 1 wt% Pt/SAPO-11 catalyst operated at an LHSV of 1.0 h"1, 380°C, 20 atm, and an H2/oil ratio of 1200 NL/L (Stage 1). The total liquid product was separated into two phases, water and diesel product. The diesel product from Stage
1 was fed to a fixed-bed reactor packed with a granulated 1 wt% Pt/SAPO-11 catalyst operated at an LHSV of 4.5 h"1, 360°C, 30 atm, and an H2/oil ratio of 1200 NL/L (Stage 2). The diesel product from Stage 1 and the diesel product from Stage
2 were analyzed according to ASTM methods and their compositions were measured by GC-MS and confirmed by NMR. The results can be found in Table 4.
Table 4
* Detection limit of 0.1 wt%
[0032] The diesel product from Stage 1 exhibited acceptable properties, including a lubricity of 306 μm. As the composition of the diesel product from Stage 2 did not significantly differ from the diesel product from Stage 1, the properties of the diesel product from Stage 2 are similar to those of the diesel product from Stage 1. However, the diesel product from Stage 2 exhibited a poorer lubricity (437 μm) as compared to that of the diesel product from Stage 1 (306 μm), similar to the diesel production from Stage 2 of Comparative Example 1. Without wishing to be bound by any theory, it is believed that water may act as an inhibitor to isomerization, which requires higher catalyst activity, and the removal of water between Stage 1 and Stage 2 in Comparative Example 1 and Comparative Example 2 may also remove acid, thereby affecting final product lubricity.
[0033] Adding 0.1 wt% of oleic acid to the diesel product of Stage 2 improved its lubricity from 437 μm to 270 μm. Thus, as noted above, without wishing to be
bound by any theory, it is believed that the low content of one or more oxygenated compounds, such as one or more fatty acids, in the product of the process may contribute to the acceptable lubricity of the diesel product.
Example 3. Production of Diesel from Soybean Oil in a Two Unit Process
[0034] The reactor setup and the operating conditions of Example 3 were based on the results of kinetic studies and reactor simulations using soybean oil. In the kinetic studies, concentrations of the soybean oil, acids, paraffins, olefins, cyclohexanes, aromatics and light compounds were measured as a function of residence time and temperature. Vapor-liquid equilibrium was provided by the reactor simulations. For a residence time of 15 to 25 minutes, the soybean oil was nearly completely converted. The acid content in the product(s) peaked at about 10 to 15 minutes, and then decreased with additional residence time. Again, diesel fuel compositions produced in accordance with the presently claimed methods can comprise less than or equal to 0.6 wt% of one or more oxygenated compounds (e.g., acids). In part due to the operating pressure, conversion of the soybean oil (e.g., for a residence time of 15 to 25 minutes) resulted in vapor phase products with only very small amounts of liquid products, which contain heavy compounds (e.g., C2o+ hydrocarbons). [0035] Accordingly, refined soybean oil was fed to a single (electrically heated) wall-cooled reactor tube, packed with a granulated 1 wt% Pt/SAPO-11 catalyst, and operated in trickle-bed mode at an LHSV of 3.5 h"1, 382°C, 30 atm, and an H2/oil ratio of 550 NL/L. The effluent of the single wall-cooled reactor tube flowed through a gas-liquid separator maintained at 30 atm and 373°C, in which a very small amount of liquid (i.e., 0.2 wt% of the refined soybean oil fed to the single wall-cooled reactor tube) was separated from a vapor phase. The vapor phase from the separator flowed upward to a single tube, adiabatic, fixed-bed reaction unit packed with a granulated 1 wt% Pt/SAPO-11 catalyst operated at an LHSV of 1.4 h"1, 373-375°C, 30 atm, and an H2/oil ratio of 550 NL/L. The diesel product from the adiabatic reaction unit was analyzed according to ASTM methods and its composition was measured by GC-MS. The results can be found in Table 5.
Table 5
[0036] The diesel product according to Example 3 exhibited acceptable properties, including a lubricity of 346 μm.
[0037] The temperature of the adiabatic reaction unit following the vapor-liquid separator is set by the temperature of the vapor-liquid separator. Heat loss can cause a temperature drop in the vapor phase products from the tubular reaction unit. Assuming that heat loss is avoided, if the temperature of the vapor-liquid separator is low (i.e., lower than the temperature of the vapor phase products from the tubular
reaction unit), the vapor phase products may undesirably condense to liquid prior to hydroisomerization in the adiabatic reaction unit. Therefore, the temperature of the vapor-liquid separator can be set such that the temperature of the vapor- liquid separator is close to the temperature of the tubular reaction unit, and more specifically, the temperature of the vapor phase products from the tubular reaction unit. Most of the heat of the hydrodeoxygenation and hydroisomerization reaction is generated in the tubular reaction unit, which can be a wall-cooled reactor. Accordingly, the reaction unit downstream of the vapor-liquid separator can be run adiabatically. The vapor-liquid separator, which can provide different conditions in the downstream adiabatic reaction unit than in the upstream tubular reaction unit, can also ensure that the downstream adiabatic reaction unit is run in vapor phase. [0038] For example, the temperature of the adiabatic reaction unit following the vapor-liquid separator can be set in the range of about 350 to 400°C or about 360 to 385°C. In particular, the temperature of the vapor-liquid separator in Example 3 was maintained at 373°C and the temperature of the adiabatic reaction in Example 3 was operated at 373°C, to minimize condensation of vapor phase products to liquid prior to hydroisomerization in the adiabatic reaction unit. Thus, the vapor-liquid separator can be used to set the temperature of the adiabatic reaction unit following the vapor-liquid separator. [0039] As noted above, the effluent from the single wall-cooled reactor tube is primarily in a vapor phase (e.g., vapor phase can comprise about 95 to 99.9 wt% of the effluent). The liquid separated from the vapor phase in the vapor-liquid separator can contain as much as 40 wt% acids. The catalyst contained in the reaction units is sensitive to coking and deactivation as a result of contact with heavy compounds (e.g., acids) in the liquid products. Thus, liquid products can negative affect selectivity of desired products and stability of the catalyst. Accordingly, separation of liquid from the vapor phase in the vapor-liquid separator (i.e., the vapor phase to be fed to the adiabatic reaction unit), protects catalyst in the adiabatic reaction unit and prevents deactivation thereof. Consequently, while catalyst in the upstream tubular reaction unit can be prone to deactivation as a result of contact with heavy compounds (e.g., acids) in the liquid products, separating
liquid product in the vapor-liquid separator prior to the downstream adiabatic reaction unit can avoid the need to regenerate catalyst in the downstream adiabatic reaction unit. Thus, use of both tubular (e.g., single wall-cooled reactor tube or multi-tubular) and adiabatic reaction units, and a vapor-liquid separator disposed therebetween, allows for improved performance and stability of the catalyst, especially the catalyst contained within the adiabatic reaction unit. In particular, the life of the catalyst contained within the adiabatic reaction unit can be extended as a result of using a vapor-liquid separator disposed between the tubular and adiabatic reaction units. [0040] While various embodiments have been described, it is to be understood that variations and modifications can be resorted to as will be apparent to those skilled in the art. Such variations and modifications are to be considered within the purview and scope of the claims appended hereto.
Claims
1. A process for producing a liquid fuel composition comprising: providing oil selected from the group consisting of vegetable oil, animal oil, and mixtures thereof; and hydrodeoxygenating and hydroisomerizing the oil, wherein the hydrodeoxygenating and hydroisomerizing comprises: feeding the oil to a tubular reaction unit containing a catalyst comprising an acidic component and a metal component; feeding effluent from the tubular reaction unit to a vapor-liquid separator; and feeding a vapor phase separated from the effluent from the tubular reaction unit to an adiabatic reaction unit comprising the same catalyst as in the tubular reaction unit comprising an acidic component and a metal component.
2. The process of claim 1 , wherein the tubular reaction unit comprises a multi-tubular reaction unit.
3. The process of claim 1, wherein hydrodeoxygenating occurs in the tubular reaction unit and hydroisomerizing occurs in the adiabatic reaction unit.
4. The process of claim 1, further comprising recycling liquid separated from the effluent from the tubular reaction unit to the tubular reaction unit.
5. The process of claim 1, wherein the tubular reaction unit operates in trickle-bed mode.
6. The process of claim 1, wherein the adiabatic reaction unit comprises a single tube.
7. The process of claim 1, comprising operating the tubular reaction unit at conditions comprising: a liquid hourly space velocity of 0.5 to 5 hr"1; a temperature of 300 to 450°C; a pressure of 10 to 60 atm; and a H2/oil ratio of 300 to 1200 NL/L.
8. The process of claim 1 , wherein the vapor phase has a temperature of about 330 to 4000C.
9. The process of claim 1 , comprising operating the adiabatic reaction unit at a temperature of about 350 to 400°C.
10. The process of claim 1, wherein the metal component is selected from the group consisting of platinum and palladium and the acidic component is selected from the group consisting of amorphous silica alumina, fluorided alumina, ZSM-12, ZSM-21, ZSM-22, ZSM-23, ZSM-35, ZSM-38, ZSM-48, ZSM-57, SSZ- 32, ferrierite, SAPO-11, SAPO-31, SAPO-41, MAPO-11, MAPO-31, Y zeolite, L zeolite, and beta zeolite.
11. The process of claim 9, wherein the catalyst is Pt/S APO- 11.
12. The process of claim 10, wherein the catalyst is 0.5-1 wt% Pt/S APO- 11.
13. The process of claim 1, wherein the vegetable oil is selected from the group consisting of soybean oil, palm oil, corn oil, sunflower oil, jatropha oil, balanites oil, rapeseed oil, colza oil, canola oil, tall oil, safflower oil, hempseed oil, olive oil, linseed oil, mustard oil, peanut oil, castor oil, coconut oil, and mixtures thereof.
14. The process of claim 1, wherein the animal oil is selected from the group consisting of lard oil, tallow oil, train oil, fish oil, and mixtures thereof.
15. A reaction system for producing a liquid fuel composition comprising: a tubular reaction unit containing a catalyst comprising an acidic component and a metal component; an adiabatic reaction unit comprising the same catalyst as in the tubular reaction unit comprising an acidic component and a metal component; and a vapor-liquid separator disposed between the tubular reaction unit and the adiabatic reaction unit.
16. The reaction system of claim 15, wherein the tubular reaction unit comprises a multi-tubular reaction unit.
17. The reaction system of claim 15, wherein the adiabatic reaction unit comprises a single tube.
18. The reaction system of claim 15, wherein the tubular reaction unit operates in trickle-bed mode.
19. The reaction system of claim 15, wherein the adiabatic reaction unit is located downstream of the tubular reaction unit.
20. The reaction system of claim 15, wherein the metal component is selected from the group consisting of platinum and palladium and the acidic component is selected from the group consisting of amorphous silica alumina, fluorided alumina, ZSM-12, ZSM-21, ZSM-22, ZSM-23, ZSM-35, ZSM-38, ZSM- 48, ZSM-57, SSZ-32, ferrierite, SAPO-I l, SAPO-31, SAPO-41, MAPO-I l, MAPO-31, Y zeolite, L zeolite, and beta zeolite.
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US20040230085A1 (en) * | 2002-09-06 | 2004-11-18 | Juha Jakkula | Process for producing a hydrocarbon component of biological origin |
US20060178540A1 (en) * | 2005-02-04 | 2006-08-10 | Garton Ronald D | Fixed bed reactor |
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JP2012507591A (en) * | 2008-11-06 | 2012-03-29 | エクソンモービル リサーチ アンド エンジニアリング カンパニー | Hydrotreatment of biodiesel fuels and blends |
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PL441706A1 (en) * | 2022-07-11 | 2024-01-15 | Sieć Badawcza Łukasiewicz - Instytut Ciężkiej Syntezy Organicznej Blachownia | Method of producing a biocomponent of liquid fuels |
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US20080066374A1 (en) | 2008-03-20 |
WO2008035155A3 (en) | 2009-08-27 |
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