CN111944555A - Homogeneous hydrogenation process for producing biodiesel from biomass oil - Google Patents

Homogeneous hydrogenation process for producing biodiesel from biomass oil Download PDF

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CN111944555A
CN111944555A CN202010796602.8A CN202010796602A CN111944555A CN 111944555 A CN111944555 A CN 111944555A CN 202010796602 A CN202010796602 A CN 202010796602A CN 111944555 A CN111944555 A CN 111944555A
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tower
oil
hydrogenation
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陈松
王康县
李广慈
任晓东
范芮堃
李学兵
王�忠
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Qingdao Institute of Bioenergy and Bioprocess Technology of CAS
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Qingdao Institute of Bioenergy and Bioprocess Technology of CAS
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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
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/42—Catalytic treatment
    • 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
    • C10G3/50—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids in the presence of hydrogen, hydrogen donors or hydrogen generating compounds
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • 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

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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 homogeneous phase hydrogenation process for producing biodiesel from biomass oil, which adopts a liquid catalyst homogeneous phase hydrogenation pretreatment process and a fixed bed hydrogenation coupling process to produce biodiesel under the condition of hydrogen, the biomass oil enters a homogeneous phase hydrogenation reactor to react in the states of hydrogen and liquid catalyst, a thermal high-pressure gas phase and side line distillate oil of a reduced pressure distillation tower enter the fixed bed hydrogenation reactor to react, the thermal high-pressure gas phase enters the reduced pressure distillation tower after being decompressed to separate out side line distillate oil, and oil generated by the reaction enters a product fractionating tower to separate into the biodiesel and the biodiesel.

Description

Homogeneous hydrogenation process for producing biodiesel from biomass oil
Technical Field
The invention belongs to the technical field of biological renewable energy sources, and particularly relates to a homogeneous phase hydrogenation process for producing biodiesel from biomass oil.
Background
The biomass oil is derived from plants, animals or microorganisms, is a renewable resource, the comprehensive utilization of the biomass oil is widely regarded worldwide, and various technical companies are dedicated to the research on producing high-quality clean energy by using the biomass oil as a raw material. The biomass oil has high oxygen content, so that the biomass oil has poor thermal stability and low heat value, and can be converted into high-grade fuel only by upgrading and modifying.
At present, the technology for upgrading biomass in the world and China mainly comprises catalytic hydrogenation, but biomass oil contains a large amount of lipid, unsaturated hydrocarbon, oxygen-containing hydrocarbon and heavy metal impurities, the impurities can cause coking, blockage and corrosion of hydrogenation heating equipment and coking of a hydrogenation fixed bed catalyst bed layer, pressure drop is increased, the catalyst is inactivated and the like, in addition, a large amount of water can be generated after the hydrogenation of the oxygen-containing hydrocarbon, the catalyst can be pulverized by the large amount of water to thoroughly block a reactor, and when the hydrogenation system causes the environment, the whole device can be frequently shut down to clean the equipment and replace the catalyst, and potential safety hazards exist.
CN102464998B relates to a method for producing high-quality diesel oil by catalytic hydrogenation of animal and vegetable oil and CN103374405B relates to a hydrogenation combination method for producing high-quality low-freezing-point diesel oil by biological oil, wherein a biomass oil raw material is mixed with hydrogen and then enters a solid catalyst fixed bed reactor for hydrogenation reaction, and the fixed bed reactor is blocked by lipid, unsaturated hydrocarbon, oxygen-containing hydrocarbon and the like in the animal and vegetable oil due to the method that the first-stage hydrogenation is the solid catalyst fixed bed reactor, so that the device is shut down.
CN102911696B relates to a hydrogenation method for producing motor fuel by biological oil, the biological oil and hydrogen are mixed and then enter a solid catalyst fixed bed reactor for hydrogenation reaction, the hydrogenation is also a solid catalyst fixed bed reactor, and no pretreatment facilities are provided, lipids, unsaturated hydrocarbons, oxygen-containing hydrocarbons and the like in the animal and vegetable oil can cause the fixed bed reactor to be blocked, and the shutdown of the device is caused.
CN103756716B relates to a living beings oil catalytic hydrogenation reaction unit and catalyst hydrogenation method thereof, and this device and method are that solid catalyst reacts in the bed, easily cause coking in the reactor, jam.
Aiming at the problems, the inventor conducts a great deal of experimental research on the biomass oil hydrogenation technology, and particularly invents a homogeneous phase hydrogenation process for producing biodiesel by using biomass oil.
Disclosure of Invention
In order to solve the problems, the invention provides a homogeneous hydrogenation process for producing biodiesel by using biomass oil, which comprises the following specific steps:
1. homogeneous hydrogenation of biomass oil: after biomass oil at 50-80 ℃ from a tank area is pressurized to 3.0-20.0MPa by a feed pump (1), the biomass oil is mixed with hydrogen and enters a mixer (2), then enters a feed heat exchanger (3) to exchange heat with a hydrofining reaction product to 100-300 ℃, then enters a feed heating furnace (4) to be heated to 220-420 ℃ and is mixed with a PPM-level oil-soluble composite molecular homogeneous phase liquid catalyst to enter a homogeneous phase reactor (5), the reaction temperature is 220-420 ℃, and the pressure is 3.0-20.0 MPa; the oil-soluble composite molecular homogeneous liquid catalyst is placed in a catalyst tank (18).
2. And (3) hydrofining of the biomass oil: the homogeneous reaction product enters a thermal high-pressure separator (6) for gas-liquid phase separation, the gas phase at the top of the thermal high-pressure separator (6) is mixed with the lateral line distillate oil of a decompression tower (11) and enters a hydrofining reactor (7) for hydrofining reaction, the hydrofining reactor is filled with a water-resistant hydrofining catalyst, the separation temperature of the thermal high-pressure separator (6) is 220-420 ℃, and the pressure is 3.0-20.0 MPa; the hydrofining reaction temperature is 150-: 0.1-10.0h-1(ii) a Feeding the hydrofining reaction product into a feeding heat exchanger (3) to exchange heat with the biomass oil raw material, heating the raw material to 100-300 ℃, cooling the hydrofining reaction product to 180-280 ℃, then feeding the hydrofining reaction product into an air cooler (12) to cool the hydrofining reaction product to 40-60 ℃, separating refined oil, circulating gas and low-pressure gas from the hydrofining reaction product in a cold high-pressure separator (13) and a low-pressure separator (14), feeding the circulating hydrogen at the top of the cold high-pressure separator (13) into a circulating hydrogen compressor (15) to pressurize, and mixing the pressurized circulating hydrogen with the biomass oil raw material; the separation temperature of the cold high-pressure separator (13) is 40-60 ℃, and the pressure is 2.0-20.0 MPa; the separation temperature of the low-pressure separator (14) is 40-60 ℃, and the pressure is 0.3-3.0 MPa.
3. And (3) carrying out reduced pressure distillation on the biomass oil: the liquid phase at the bottom of the hot high-pressure separator (6) enters the hot low-pressure separator (9) for gas-liquid phase separation after decompression, the separation temperature of the hot low-pressure separator (9) is 220-; the liquid at the bottom of the thermal low-pressure separator (9) enters a reduced-pressure heating furnace (10) to heat the medium to 230-. The operating temperature of the vacuum distillation tower (11) is as follows: the tower top is 30-110 ℃, and the tower bottom is 210- & ltSUB & gt 360 ℃; the operating pressure is: the top of the tower is 1-50KPa (absolute), the bottom of the tower is 4-60KPa (absolute), and the vacuum tower is a packed tower.
4. And (3) fractionating the biomass oil through reaction to generate oil: heating the oil phase at the bottom of the low-pressure separator (14) to 200-360 ℃ by a heating furnace (16), then feeding the oil phase into a product fractionating tower (17) for fractionation, feeding the oil-fractionated biodiesel generated by the reaction into a tank area for storage, and producing a small amount of biological naphtha; the operating temperature of the product fractionation column (17) is: the tower top is 60-180 ℃, and the tower bottom is 200-360 ℃; the operating pressure is: the top of the tower is 0-0.6MPa (table), the bottom of the tower is 0.1-0.8KPa (table), and the product fractionating tower is a tray tower or a packed tower, preferably a tray tower.
The method has the advantages that the step can realize continuous long-term operation of homogeneous hydrogenation of the biomass oil, and can well remove impurities such as lipids, unsaturated hydrocarbons, oxygenated hydrocarbons, heavy metals and the like in the biomass oil. And can ensure that the biomass oil homogeneous hydrogenation continuously operates, and the fixed bed hydrofining equipment is not coked, corroded or blocked, and the start-up time of the device for producing high-quality biodiesel by using the biomass oil is prolonged.
Drawings
FIG. 1 is a process flow diagram for producing high-quality biodiesel by homogeneous hydrogenation of biomass oil.
In the figure, 1 is a feed pump, 2 is a mixer, 3 is a feed heat exchanger, 4 is a feed heating furnace, 5 is a homogeneous reactor, 6 is a hot high-pressure separator, 7 is a hydrofining reactor, 8 is a distillate oil pump, 9 is a hot low-pressure separator, 10 is a vacuum heating furnace, 11 is a vacuum distillation tower, 12 is an air cooler, 13 is a cold high-pressure separator, 14 is a low-pressure separator, 15 is a recycle hydrogen compressor, 16 is a heating furnace, 16 is a product fractionating tower, and 18 is a catalyst tank.
Detailed Description
The basic principle of the step of producing the biodiesel by the biomass oil in the homogeneous hydrogenation process for producing the biodiesel by the biomass oil is as follows:
the biomass oil is mixed with hydrogen under the working condition of belt pressure and is subjected to hydrogenation reaction under the action of a PPM-level composite molecular homogeneous phase liquid catalyst, the reaction can be used for hydrocracking, hydrosaturation and hydrodeoxygenation of substances such as lipids, unsaturated hydrocarbons, oxygen-containing hydrocarbons and the like in the biomass oil, and a water-resistant semi-ceramic hydrorefining catalyst is researched and prepared aiming at the generation of water after the hydrodeoxygenation of the oxygen-containing hydrocarbons.
The invention will be described in detail below with reference to fig. 1 and the detailed description, but the invention is not limited to the example description.
The first embodiment is as follows:
mixing biomass oil with recycle hydrogen at an outlet of a recycle hydrogen compressor 14 through a feed pump 1, feeding the mixture into a mixer 2, feeding the uniformly mixed raw material into a raw material heat exchanger 3 to exchange heat with a hydrofining reaction product, feeding the mixture into a feed heating furnace 4 after the temperature is changed to 200 ℃, heating the raw material to 320 ℃, mixing the raw material with a composite molecular homogeneous catalyst, feeding the mixture into a homogeneous phase hydrogenation reactor 5 to perform hydrogenation reaction, wherein the reaction temperature is 320 ℃, and the pressure is 3.0 MPa; the reaction product from the homogeneous phase reactor 5 enters a thermal high-pressure separator 6, the liquid phase at the bottom of the thermal high-pressure separator 6 enters a thermal low-pressure separator 9 after being depressurized, the operating temperature of the thermal low-pressure separator 9 is 380 ℃, the pressure is 0.7MPa, the liquid phase at the bottom of the thermal low-pressure separator 9 enters a reduced-pressure heating furnace 10, the temperature is raised to 340 ℃, and then the liquid phase enters a reduced-pressure distillation tower 11, and the operating temperature of the reduced-pressure distillation tower 11 is as follows: the tower top is 70 ℃ and the tower bottom is 330 ℃; the operating pressure is: 12KPa at the top of the tower and 17KPa at the bottom of the tower, and fractionating side distillate and bottom tail oil in a reduced pressure distillation tower 11. The side line distillate oil is pressurized by a distillate oil pump 8 and mixed with the gas phase at the top of a hot high-pressure separator 6, enters a hydrofining reactor 7, is subjected to hydrofining reaction at the temperature of 320 ℃ and under the pressure of 2.5MPa, enters a feed heat exchanger 3 after the reaction to exchange heat with the biomass oil raw material, enters an air cooler 12 for cooling to 50 ℃ from the temperature of 320 ℃ of hot high-pressure gas phase, enters a cold high-pressure separator 13 to separate out recycle hydrogen, and the recycle hydrogen is pressurized to 3.6MPa by a recycle hydrogen compressor 15 and mixed with the raw material; the liquid at the bottom of the cold high-pressure separator 13 is depressurized and enters a low-pressure separator 14, the operating temperature of the low-pressure separator 14 is 50 ℃, the pressure is 0.7MPa, the low-fraction gas is separated and enters a downstream processing part, the low-fraction oil is heated to 230 ℃ by a heating furnace 16 and enters a product fractionating tower, the biodiesel distilled from the bottom enters a tank area for storage, and a small amount of biodiesel is produced at the top. This completes the steps of the homogeneous hydrogenation process for producing biodiesel from biomass oil.
Example two:
mixing biomass oil with recycle hydrogen at an outlet of a recycle hydrogen compressor 14 through a feed pump 1, feeding the mixture into a mixer 2, feeding the uniformly mixed raw material into a raw material heat exchanger 3 to exchange heat with a hydrofining reaction product, feeding the mixture into a feed heating furnace 4 after the temperature is changed to 220 ℃, heating the raw material to 340 ℃, mixing the raw material with a composite molecular homogeneous catalyst, feeding the mixture into a homogeneous phase hydrogenation reactor 5 to perform hydrogenation reaction, wherein the reaction temperature is 340 ℃, and the pressure is 6.0 MPa; the reaction product from the homogeneous phase reactor 5 enters a thermal high-pressure separator 6, the liquid phase at the bottom of the thermal high-pressure separator 6 enters a thermal low-pressure separator 9 after being depressurized, the operating temperature of the thermal low-pressure separator 9 is 390 ℃, the pressure is 1.0MPa, the liquid phase at the bottom of the thermal low-pressure separator 9 enters a reduced-pressure heating furnace 10, the temperature is increased to 360 ℃, and then the liquid phase enters a reduced-pressure distillation tower 11, and the operating temperature of the reduced-pressure distillation tower 11 is as follows: the tower top is 70 ℃, and the tower bottom is 350 ℃; the operating pressure is: 50KPa at the top of the tower and 60KPa at the bottom of the tower, and fractionating side line distillate oil and bottom tail oil in a reduced pressure distillation tower 11. The side line distillate oil is pressurized by a fractionation oil pump 8 and mixed with the gas phase at the top of a hot high-pressure separator 6, enters a hydrofining reactor 7, is subjected to hydrofining reaction at the temperature of 310 ℃ and under the pressure of 2.5MPa, enters a feed heat exchanger 3 after the reaction to exchange heat with the biomass oil raw material, enters an air cooler 12 for cooling to 50 ℃ from the temperature of 310 ℃ of the hot high-pressure gas phase, enters a cold high-pressure separator 13 to separate out recycle hydrogen, and the recycle hydrogen is pressurized to 6.8MPa by a recycle hydrogen compressor 15 and mixed with the raw material; the liquid at the bottom of the cold high-pressure separator 13 is depressurized and enters a low-pressure separator 14, the operating temperature of the low-pressure separator 14 is 50 ℃, the pressure is 1.0MPa, the low-fraction gas is separated and enters a downstream processing part, the low-fraction oil is heated to 260 ℃ by a heating furnace 16 and enters a product fractionating tower, the biodiesel distilled from the bottom enters a tank area for storage, and a small amount of biodiesel is produced at the top. This completes the steps of the homogeneous hydrogenation process for producing biodiesel from biomass oil.
After the biomass oil in the above table is subjected to the homogeneous hydrogenation process for producing biodiesel from the biomass oil in the first and second embodiments, the comparison conditions of the raw materials and the product are as follows:
Figure BDA0002625670800000051
the first and second examples show that the invention can produce biodiesel from biomass oil, and the produced biodiesel has high quality.

Claims (8)

1. A homogeneous hydrogenation process for producing biodiesel from biomass oil is characterized in that a liquid catalyst homogeneous hydrogenation pretreatment process and a fixed bed hydrogenation coupling process are adopted to produce biodiesel under the hydrogenation condition, and the related process steps are as follows: (A) homogeneous hydrogenation reaction of biomass oil: the biomass oil enters a homogeneous phase hydrogenation reactor to react in the states of hydrogen and a liquid catalyst; (B) fixed bed hydrogenation of the biomass oil: the hot high-pressure-distribution gas phase and the side-line distillate oil of the reduced pressure distillation tower enter a fixed bed hydrogenation reactor to react; (C) and (3) carrying out reduced pressure distillation on the biomass oil: the hot high-separation liquid phase is decompressed and then enters a reduced pressure distillation tower to separate side line distillate oil; (D) and (3) fractionating the biomass oil through reaction to generate oil: the oil generated by the reaction enters a product fractionating tower to be separated into biodiesel and biological naphtha.
2. The homogeneous hydrogenation pretreatment reaction according to claim 1, using a liquid catalyst characterized by a mixture of group IIIB, VIB and VIII elements.
3. The coupled hydrogenation process according to claim 1, comprising a homogeneous hydrogenation pretreatment and a fixed bed hydrofinishing post-treatment, wherein the hydrogenation state of the homogeneous hydrogenation reaction system is a pressure of 3.0-15.0MPa, the involved homogeneous hydrogenation temperature is 220-420 ℃, and the homogeneous hydrogenation reaction needs to be carried out in a liquid catalyst environment.
4. The hydrofining reaction system according to claim 1 is in a hydrogen state at a pressure of 2.0-20.0MPa, and the hydrofining temperature is 150-360 ℃, preferably 260-340 ℃, and the volume space velocity is: 0.1-10.0h-1。
5. The operating temperature of the vacuum distillation column 11 according to claim 1 is: the tower top is 30-110 ℃, and the tower bottom is 210- & ltSUB & gt 360 ℃; the operating pressure is: the top of the tower is 1-50KPa (absolute), the bottom of the tower is 4-60KPa (absolute), and the vacuum tower is a packed tower.
6. A homogeneous hydrogenation process according to claim 1, characterised in that the biomass oil total oxygen content (w%) is between 2% and 20%.
7. The biodiesel according to claim 1, which is a hydrogenated product and characterized by a density of 750-800 kg/m3The dry point of the distillation range is 315-340 ℃, and the 90 point is 280-315 DEG C
8. The product fractionation column of claim 1 operating at a temperature of: the tower top is 60-180 ℃, and the tower bottom is 200-360 ℃; the operating pressure is: the top of the tower is 0-0.6MPa (table), the bottom of the tower is 0.1-0.8MPa (table), and the product fractionating tower is a tray tower or a packed tower, preferably a tray tower.
CN202010796602.8A 2020-08-12 2020-08-12 Homogeneous hydrogenation process for producing biodiesel from biomass oil Pending CN111944555A (en)

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1766058A (en) * 2004-10-29 2006-05-03 中国石油化工股份有限公司 Coal tar whole fraction hydrotreatment process
CN101338213A (en) * 2007-08-17 2009-01-07 内蒙古金骄特种新材料有限公司 Biodesel and method for preparing same
CN102876348A (en) * 2011-07-11 2013-01-16 中国石油化工股份有限公司 Hydrogenation method for preparation of biodiesel
US20130292300A1 (en) * 2004-04-23 2013-11-07 Massachusetts Institute Of Technology Mesostructured zeolitic materials suitable for use in hydrocracking catalyst compositions and methods of making and using the same
CN105754639A (en) * 2014-12-17 2016-07-13 中国石油化工股份有限公司 Method for improving quality of biomass liquefaction product
CN110041963A (en) * 2019-04-22 2019-07-23 中国科学院青岛生物能源与过程研究所 A kind of technique of waste mineral oil homogeneous hydrogenation pretreatment and dechlorination

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20130292300A1 (en) * 2004-04-23 2013-11-07 Massachusetts Institute Of Technology Mesostructured zeolitic materials suitable for use in hydrocracking catalyst compositions and methods of making and using the same
CN1766058A (en) * 2004-10-29 2006-05-03 中国石油化工股份有限公司 Coal tar whole fraction hydrotreatment process
CN101338213A (en) * 2007-08-17 2009-01-07 内蒙古金骄特种新材料有限公司 Biodesel and method for preparing same
CN102876348A (en) * 2011-07-11 2013-01-16 中国石油化工股份有限公司 Hydrogenation method for preparation of biodiesel
CN105754639A (en) * 2014-12-17 2016-07-13 中国石油化工股份有限公司 Method for improving quality of biomass liquefaction product
CN110041963A (en) * 2019-04-22 2019-07-23 中国科学院青岛生物能源与过程研究所 A kind of technique of waste mineral oil homogeneous hydrogenation pretreatment and dechlorination

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Application publication date: 20201117