CN111100703A - Method for hydrodeoxygenation of biological oil - Google Patents
Method for hydrodeoxygenation of biological oil Download PDFInfo
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- CN111100703A CN111100703A CN201811264070.2A CN201811264070A CN111100703A CN 111100703 A CN111100703 A CN 111100703A CN 201811264070 A CN201811264070 A CN 201811264070A CN 111100703 A CN111100703 A CN 111100703A
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- 238000000034 method Methods 0.000 title claims abstract description 55
- 239000003054 catalyst Substances 0.000 claims abstract description 60
- 238000006243 chemical reaction Methods 0.000 claims abstract description 32
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- 239000001257 hydrogen Substances 0.000 claims abstract description 22
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- 230000007423 decrease Effects 0.000 claims description 2
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- 239000002540 palm oil Substances 0.000 claims description 2
- 239000000312 peanut oil Substances 0.000 claims description 2
- 239000008165 rice bran oil Substances 0.000 claims description 2
- 239000008159 sesame oil Substances 0.000 claims description 2
- 235000011803 sesame oil Nutrition 0.000 claims description 2
- 235000020238 sunflower seed Nutrition 0.000 claims description 2
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- 235000019871 vegetable fat Nutrition 0.000 description 5
- 239000000295 fuel oil Substances 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
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- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 230000002411 adverse Effects 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000003225 biodiesel Substances 0.000 description 2
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 description 2
- 238000006317 isomerization reaction Methods 0.000 description 2
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- 230000002035 prolonged effect Effects 0.000 description 2
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- 150000004670 unsaturated fatty acids Chemical class 0.000 description 2
- 238000004073 vulcanization Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
- CSDREXVUYHZDNP-UHFFFAOYSA-N alumanylidynesilicon Chemical compound [Al].[Si] CSDREXVUYHZDNP-UHFFFAOYSA-N 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 239000002199 base oil Substances 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 229910052796 boron Inorganic materials 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
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- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
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- 229910052814 silicon oxide Inorganic materials 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 125000005480 straight-chain fatty acid group Chemical group 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 description 1
- UFTFJSFQGQCHQW-UHFFFAOYSA-N triformin Chemical compound O=COCC(OC=O)COC=O UFTFJSFQGQCHQW-UHFFFAOYSA-N 0.000 description 1
- 229910052721 tungsten Inorganic materials 0.000 description 1
- 229910052726 zirconium Inorganic materials 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- 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
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a method for hydrodeoxygenation of biological oil, which comprises the following steps: (1) the biological oil enters a thermal high-pressure separator to contact with a catalyst 1 filled in the thermal high-pressure separator to carry out olefin saturation and shallow hydrodeoxygenation reaction; (2) the gas phase effluent at the top of the hot high-pressure separator can be recycled as make-up hydrogen, and the liquid phase effluent enters a fractionating tower and is separated to obtain gasoline, diesel oil and unconverted oil; (3) the unconverted oil enters a hydrofining reactor to carry out deep hydrodeoxygenation reaction under the action of a catalyst 2, and the effluent enters a hot high-pressure separator. The method can ensure the activity stability of the catalyst and the long-period stable operation of the device while producing the low-freezing-point diesel blending component, and has low production cost and simple operation.
Description
Technical Field
The invention relates to a method for hydrodeoxygenation of biological oil, in particular to a method for producing high-quality diesel oil blending components by using animal and vegetable oil as a raw material through hydrodeoxygenation.
Background
Petroleum is a disposable resourceCan be recycled, and the yield and the storage capacity of the fertilizer are greatly reduced with the increase of the consumption of the fertilizer. Since new clean fuels are required for environmental regulations and industrial development by developing new renewable energy sources to replace the increasingly exhausted conventional energy sources, alternative and renewable energy sources are actively being explored and developed in various countries of the world. Animal and vegetable oil and fat are inexhaustible and are typical renewable energy sources, and the compositions of the biological oil and fat are similar, mainly comprise straight chain fatty acid triglyceride and are C16And C18There are many. Animal and vegetable oil and fat are composed of saturated fatty acid and unsaturated fatty acid, the content of unsaturated fatty acid in vegetable oil is higher, the content of saturated fatty acid in animal fat is higher, and if the animal and vegetable oil and fat are converted into small molecules for use, a new energy source for producing clean fuel is provided.
CN106190592A discloses a method for preparing biological lubricating oil by catalytic hydrogenation of biodiesel, wherein the biodiesel is contacted with a hydrogenation catalyst under the condition of catalytic hydrogenation reaction to generate hydrogenation saturation reaction and ester exchange reaction, and the reaction effluent is subjected to reduced pressure distillation to obtain the biological lubricating oil component. The method provided by the invention can obtain the biological lubricating oil component with stable performance, and has the advantages of simple process, good selectivity of target products and high yield.
CN101768469A discloses a combined hydrogenation method of mineral oil and animal and vegetable oil. In two hydrogenation reaction zones, high-sulfur mineral diesel oil fraction and animal and vegetable oil are respectively used as raw materials, and are subjected to hydrogenation treatment under different conditions, and the obtained products are mixed to obtain a low-sulfur even ultra-low-sulfur diesel oil product. The method provided by the invention can be used for treating high-sulfur mineral diesel oil fractions and vegetable oil. Can obtain clean diesel oil products with low sulfur content, high polycyclic aromatic hydrocarbon content and high cetane number under mild operation conditions. The equipment and the operation procedure of the regular sulfur supplement for the vegetable oil hydrotreating are omitted. The influence of water generated in the vegetable oil hydrogenation reaction on the activity of the hydrogenation catalyst is reduced, and the operation period of the device is prolonged.
CN101760234A discloses a hydrogenation method for improving the cetane number of secondary processing diesel oil. The secondary processing diesel oil is mixed with vegetable oil and/or animal fat, the mixed raw material is contacted with a hydrofining catalyst in the presence of hydrogen to carry out hydrogenation reaction, and the reaction effluent is cooled, separated and fractionated to obtain a diesel oil product, wherein the mixed raw material is taken as a reference. Because the mixing proportion of the vegetable oil is controlled, the influence of the water generated in the reaction on the activity of the hydrogenation catalyst is reduced, the operation period of the device is prolonged, and the yield of the obtained diesel oil product is high.
CN101348732A discloses a heavy oil hydrotreating method, especially a heavy oil hydrotreating method for improving diesel oil quality. Heavy distillate oil and animal and vegetable oil are used as raw oil, under the condition of hydrotreatment, the raw oil and hydrogen are mixed and pass through a hydrotreatment reaction zone, hydrogen-rich gas obtained by oil separation generated by hydrotreatment is recycled, and liquid obtained by separation is fractionated to obtain a diesel oil product and hydrogenated wax oil. The method can effectively improve the raw material source of the wax oil hydrotreatment device, greatly improve the quality of the hydrotreated diesel oil while ensuring the quality of the hydrotreated wax oil, and improve the storage stability of animal and vegetable oil as fuel oil.
EP1741767 and EP1741768 disclose a process for producing diesel oil fractions from animal or vegetable fats, mainly by subjecting the animal or vegetable fats to a hydrotreating process and then passing through an isomerization catalyst bed to obtain a low-freezing-point diesel oil fraction, but since water is generated during the hydrotreating process, the isomerization catalyst is very adversely affected, and the apparatus cannot be operated stably for a long period.
One of the main problems encountered in the hydrogenation process of the biological oil and fat by the method is that the stability of the catalyst is poor, the operation period is short, and the catalyst needs to be frequently stopped and replaced. Particularly, when the biological oil is used as the raw material alone or the mixing ratio of the biological oil is high, the operation period of the hydrogenation catalyst is influenced obviously, and the requirement of industrial application cannot be met.
CN103102916A discloses a two-stage hydrogenation method for producing low-condensation-point motor fuel, which comprises the following steps: the method comprises the steps of taking biological oil as raw oil, mixing the raw oil with hydrogen under a hydrogenation condition, allowing the raw oil and the hydrogen to pass through a first-stage hydrogenation reaction zone, separating a hydrogenation generated material flow to obtain hydrogen-rich gas, recycling the hydrogen-rich gas in the first stage, allowing the separated liquid to enter a second-stage hydrogenation modification reaction zone, separating the oil generated by the second-stage hydrogenation to obtain sub-hydrogen gas, recycling the sub-hydrogen gas in the second stage, and fractionating the separated liquid product to obtain naphtha and low-condensation-point diesel.
CN102464995A discloses a hydrotreating method for producing motor fuel by biological oil, which comprises the following steps: one or more of the biological oil is raw oil; under the condition of hydrogenation operation, raw oil and hydrogen pass through a hydrogenation catalyst bed layer containing at least two hydrogenation active components with sequentially increased contents, the hydrogenation effluent is separated into a gas phase and a liquid phase, the gas phase is recycled, and the liquid phase enters a fractionating tower; fractionating in a fractionating tower to obtain naphtha, diesel oil and unconverted oil, wherein part of the diesel oil and/or part of the unconverted oil are recycled to the reaction system. Compared with the prior art, the method of the invention not only can effectively improve the storage stability of the biological grease as fuel oil, but also can realize the long-period stable operation of the device.
CN103102905A discloses a two-stage hydrogenation method for producing high-quality low-freezing-point motor fuel by using biological oil, which comprises the following steps: the biological oil raw material and hydrogen gas pass through a first-stage hydrogenation reaction zone at least comprising two hydrofining reactors, firstly pass through a reactor operated at low temperature, then pass through a reactor operated at high temperature, hydrogen-rich gas is recycled at the first stage, and liquid enters a second-stage hydrogenation modification reaction zone. The hydro-upgrading by-product hydrogen is recycled in the second stage, and the liquid product is fractionated to obtain naphtha and low-condensation-point diesel. Compared with the prior art, the method can ensure the activity stability of the catalyst and the long-period stable operation of the device while producing the motor fuel with low condensation point.
Although the method can effectively guarantee the activity of the catalyst and prolong the operation period of the device, at least more than two reactors and separators are needed, the investment cost of the device is high, and the operation is complex.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides the method for hydrodeoxygenation of the biological oil, which can ensure the activity stability of the catalyst and the long-period stable operation of the device while producing the low-freezing-point diesel oil blending component, and has the advantages of low production cost and simple operation.
The invention relates to a method for hydrodeoxygenation of biological oil, which comprises the following steps:
(1) the biological oil enters a thermal high-pressure separator to contact with a catalyst 1 filled in the thermal high-pressure separator to carry out olefin saturation and shallow hydrodeoxygenation reaction;
(2) the gas phase effluent at the top of the hot high-pressure separator can be recycled as make-up hydrogen, and the liquid phase effluent enters a fractionating tower and is separated to obtain gasoline, diesel oil and unconverted oil;
(3) the unconverted oil enters a hydrofining reactor to carry out deep hydrodeoxygenation reaction under the action of a catalyst 2, and the effluent enters a hot high-pressure separator.
In the method, the biological oil can comprise vegetable oil or animal oil, the vegetable oil comprises one or more of soybean oil, peanut oil, castor oil, rapeseed oil, corn oil, olive oil, palm oil, coconut oil, tung oil, linseed oil, sesame oil, cottonseed oil, sunflower seed oil, rice bran oil and the like, and the animal oil comprises one or more of beef tallow, lard, mutton oil, fish oil and the like.
In the method, the operating conditions of the thermal high-pressure separator are generally 3.0MPa to 20.0MPa of reaction pressure, 200:1 to 1000:1 of hydrogen-oil volume ratio and 0.1h of volume space velocity-1~10.0h-1The average temperature is 150-400 ℃; the preferable operation conditions are that the reaction pressure is 4.0MPa to 18.0MPa, the volume ratio of hydrogen to oil is 300:1 to 800:1, and the volume airspeed is 1h-1~8.0h-1The average reaction temperature is 200-350 ℃.
In the method, the operation conditions of the hydrofining reactor are generally 3.0MPa to 20.0MPa of reaction pressure, 200:1 to 1000:1 of hydrogen-oil volume ratio and 0.1h of volume space velocity-1~6.0h-1The average reaction temperature is 180-465 ℃; the preferable operation conditions are that the reaction pressure is 4.0MPa to 18.0MPa, the volume ratio of hydrogen to oil is 300:1 to 800:1, the volume space velocity is 0.2h < -1 > to 4.0h < -1 >, and the reaction is flatThe average reaction temperature is 200-445 ℃.
In the method, the operating temperature of the hot high-pressure separator is 50-300 ℃ lower than the reaction temperature of the hydrofining reactor, and preferably 100-200 ℃ lower than the reaction temperature of the hydrofining reactor.
In the method, shallow hydrodeoxygenation means that oxygen in the vegetable oil is removed at the reaction temperature of more than 200 ℃ to less than 300 ℃, and deep hydrodeoxygenation means that oxygen in the vegetable oil is removed at the reaction temperature of more than 300 ℃ to less than 400 ℃.
In the method, the filling volume of the catalyst 1 filled in the hot high-pressure separator is 10-90%, preferably 30-60% of the filling volume of the hot high-pressure separator, and the distance from the top of a catalyst bed layer in the hot high-pressure separator to the top of the hot high-pressure separator is 5-50%, preferably 10-30% of the height of the hot high-pressure separator.
In the method, the catalyst 1 filled in the hot high-pressure separator is a spherical catalyst, and the particle diameter of the catalyst is 1-40 mm, preferably 2.0-20 mm; the preferred particle diameter decreases in the direction of the liquid phase effluent (from top to bottom) and in the direction of the gas phase effluent (from bottom to top). The gas phase effluent first passes through a catalyst bed layer with low porosity, so that light hydrocarbon carried in the gas phase effluent is condensed on the surface of the catalyst, the separation effect is improved, meanwhile, the retention time of the liquid phase effluent in the catalyst bed layer is gradually increased, the hydrogenation effect is ensured, and the pressure drop is prevented.
In the process of the present invention, the catalyst 1 in step (1) and the catalyst 2 in step (3) may be the same or different, and the latter is preferred; can be prepared using commercially available catalysts or by methods known in the art. The carrier adopted by the catalyst is generally alumina, amorphous silicon-aluminum, silicon oxide, titanium oxide and the like, other auxiliary agents such as P, Si, B, Ti, Zr and the like can be contained in the carrier, and the hydrogenation active component can be noble metal or non-noble metal. In the noble metal catalyst, the active component is generally Pt and/or Pt, and the weight content of the active component is generally 0.1-3%. The active component in the non-noble metal catalyst is one or more of W, Mo, Ni and Co, the active component can be in an oxidation state or a reduction state, and the content is generally 15-45% by weight of oxides. When a noble metal catalyst or a reduced non-noble metal catalyst is selected, hydrogen is used for treatment at the temperature of 200-500 ℃, preferably 220-450 ℃ before use; at any time, a medium containing sulfur and nitrogen is strictly injected into the system, so that the catalyst poisoning is avoided. The oxidation state non-noble metal catalyst is selected to be subjected to conventional vulcanization treatment before use, so that the hydrogenation active component is converted into a vulcanization state. The non-noble metal catalyst mainly comprises hydrogenation catalysts such as 3926, 3936, CH-20, FF-14, FF-18, FF-24, FF-26, FF-36, FH-98, FH-UDS and FZC-41 developed by the Fushu petrochemical research institute (FRIPP), hydrogenation catalysts such as HR-416 and HR-448 of IFP company, hydrogenation catalysts such as ICR174, ICR178 and ICR 179 of CLG company, hydrogenation catalysts such as HC-P, HC-K UF-210/220, hydrogenation catalysts such as TK-525, TK-555 and TK-557 of Topsor company, hydrogenation catalysts such as KF-752, KF-840, KF-848, KF-901 and KF-907 of AKZO company; the noble metal catalyst is developed and developed by HDO-18 catalyst such as Nashu petrochemical research institute (FRIPP), and can also be prepared by the method of CN00123141.3 and the like.
In the prior art, the vegetable oil hydrodeoxygenation method generally needs to be mixed with a large proportion of petroleum fractions for processing, otherwise, the running period cannot be ensured; or a plurality of reactors with different temperatures are connected in series for operation, thus increasing the equipment investment and the operation difficulty. According to the invention, by filling a small amount of catalyst in the thermal high-pressure separator and strictly controlling the filling mode, not only are the mutual adverse effects between the separation of the thermal high-pressure separator and the olefin saturation reaction in the thermal high-pressure separator solved, but also the separation and the olefin saturation reaction of the thermal high-pressure separator are promoted, the comprehensive effect is improved, the vegetable oil can be directly used as the raw material to produce high-quality diesel blending components, and the problem that a biological oil hydrogenation device cannot be stably operated for a long period is solved; meanwhile, the whole reaction system has simple process flow, low equipment investment and simple operation.
Drawings
FIG. 1 is a schematic diagram of a principle flow of the process of the present invention.
The vegetable oil 1 enters a hot high-pressure separator 2 from the upper part, the gas phase effluent 4 is recycled as make-up hydrogen, the liquid phase effluent 3 enters a separation tower 5, the separation is carried out to obtain gasoline 6, diesel oil 7 and unconverted oil 8, the unconverted oil 8 and hydrogen 9 are mixed and enter a hydrofining reactor 10, and the effluent 11 enters the hot high-pressure separator 2 from the lower part.
Detailed Description
The following examples further illustrate specific aspects of the present invention. The catalyst filled in the thermal high-pressure separator is an FH-40D hydrogenation catalyst developed by the comforting petrochemical research institute, the catalyst filled in the hydrofining reactor is an FF-46 hydrogenation catalyst, and soybean oil is used as a test raw material.
TABLE 1 Primary Properties of the base oils
TABLE 2 FH-40D and FF-46A hydrofining catalyst Primary physicochemical Properties
Table 3 example process conditions and test results
Table 4 examples process conditions and test results
The embodiment shows that the vegetable oil can directly produce diesel oil products or high-quality diesel oil blending components by the hydrogenation method of the technology, and can stably run for a long time.
Claims (12)
1. A method for hydrodeoxygenation of biological oil is characterized by comprising the following steps: the method comprises the following steps:
(1) the biological oil enters a thermal high-pressure separator to contact with a catalyst 1 filled in the thermal high-pressure separator to carry out olefin saturation and shallow hydrodeoxygenation reaction;
(2) the gas phase effluent at the top of the hot high-pressure separator can be recycled as make-up hydrogen, and the liquid phase effluent enters a fractionating tower and is separated to obtain gasoline, diesel oil and unconverted oil;
(3) the unconverted oil enters a hydrofining reactor to carry out deep hydrodeoxygenation reaction under the action of a catalyst 2, and the effluent enters a hot high-pressure separator.
2. The method of claim 1, wherein: the biological oil and fat is vegetable oil or animal oil and fat.
3. The method of claim 1, wherein: the vegetable oil is one or more of soybean oil, peanut oil, castor oil, rapeseed oil, corn oil, olive oil, palm oil, coconut oil, tung oil, linseed oil, sesame oil, cottonseed oil, sunflower seed oil and rice bran oil, and the animal oil is one or more of beef tallow, lard, mutton fat and fish oil.
4. The method of claim 1, wherein: the operating conditions of the hot high-pressure separator are that the pressure is 3.0MPa to 20.0MPa, the volume ratio of hydrogen to oil is 200:1 to 1000:1, and the volume airspeed is 0.1h-1~10.0h-1The temperature is 150-400 ℃.
5. The method of claim 4, wherein: the operating conditions of the hot high-pressure separator are that the pressure is 4.0MPa to 18.0MPa, the volume ratio of hydrogen to oil is 300:1 to 800:1, and the volume airspeed is 1h-1~8.0h-1And the temperature is 200-350 ℃.
6. The method of claim 1, wherein: the operating conditions of the hydrofining reactor are that the reaction pressure is 3.0MPa to 20.0MPa, the volume ratio of hydrogen to oil is 200:1 to 1000:1, and the volume airspeed is 0.1h-1~ 6.0h-1The average reaction temperature is 180-465 ℃.
7. The method of claim 1, wherein: the operating conditions of the hydrofining reactor are 4.0 MPa-18.0 MPa, the volume ratio of hydrogen to oil is 300: 1-800: 1, the volume space velocity is 0.2h < -1 > -4.0 h < -1 >, and the average reaction temperature is 200 ℃ to 445 ℃.
8. The method of claim 1, wherein: the operation temperature of the hot high-pressure separator is 50-300 ℃ lower than the reaction temperature of the hydrofining reactor.
9. The method of claim 1, wherein: the filling volume of the catalyst 1 filled in the hot high-pressure separator is 10-90% of the filling volume of the hot high-pressure separator, and the distance between the top of the catalyst bed layer in the hot high-pressure separator and the top of the hot high-pressure separator is 5-50% of the height of the hot high-pressure separator.
10. The method of claim 9, wherein: the method is characterized in that: the filling volume of the catalyst 1 filled in the hot high-pressure separator is 30-60% of the filling volume of the hot high-pressure separator, and the distance between the top of the catalyst bed layer in the hot high-pressure separator and the top of the hot high-pressure separator is 10-30% of the height of the hot high-pressure separator.
11. The method of claim 1, wherein: the catalyst 1 filled in the hot high-pressure separator is a spherical catalyst, and the particle diameter of the catalyst is 1-40 mm.
12. The method of claim 11, wherein: the particle diameter decreases in the direction of the liquid phase outflow.
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