CN112552947A - Processing method for producing biodiesel by hydrogenation of plant asphalt - Google Patents
Processing method for producing biodiesel by hydrogenation of plant asphalt Download PDFInfo
- Publication number
- CN112552947A CN112552947A CN202011248308.XA CN202011248308A CN112552947A CN 112552947 A CN112552947 A CN 112552947A CN 202011248308 A CN202011248308 A CN 202011248308A CN 112552947 A CN112552947 A CN 112552947A
- Authority
- CN
- China
- Prior art keywords
- oil
- hydrogenation
- biological
- steps
- heavy
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- 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
- C10G3/45—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof
- C10G3/46—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof in combination with chromium, molybdenum, tungsten 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
- C10G3/50—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
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/54—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids characterised by the catalytic bed
- C10G3/55—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids characterised by the catalytic bed with moving solid particles, e.g. moving beds
-
- 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
-
- 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
- Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
- Y02T50/00—Aeronautics or air transport
- Y02T50/60—Efficient propulsion technologies, e.g. for aircraft
- Y02T50/678—Aviation using fuels of non-fossil origin
Abstract
The invention relates to the technical field of petrochemical industry, in particular to a processing method for producing biodiesel by hydrogenating plant asphalt, which comprises the following steps: desalting, dehydrating and removing impurities from the raw oil; carrying out a first hydrogenation process on the treated raw material; separating the first hydrogenation product to obtain light hydrocarbons and heavy hydrocarbons; separating heavy hydrocarbons or further converting the heavy hydrocarbons; carrying out a second hydrogenation process on the light alkane and the hydrocracking product generated in the first hydrogenation process, and further carrying out hydrofining to remove oxygen in the first hydrogenation product; and fractionating the product of the second hydrogenation process to obtain biological light oil, biological aviation kerosene, biological diesel oil and biological heavy oil components. The processing method can process the plant asphalt to obtain the components of the biodiesel, the white oil, the liquid paraffin, the lubricating oil base oil, the biological light oil, the biological aviation kerosene, the biological heavy oil and the like, and has the advantages of simple steps, convenient operation and control, low energy consumption and high added value of products.
Description
Technical Field
The invention relates to the technical field of petrochemical industry, in particular to a processing method for producing biodiesel by hydrogenating plant asphalt.
Background
The plant asphalt is waste after fatty acid is extracted from plant oil residue through acidification, hydrolysis and distillation, and is called plant asphalt accounting for about 10% of the mass fraction of the plant oil residue due to the color of the plant asphalt like asphalt, and is mainly used for heavy oil combustion treatment at present. Analysis shows that the biodiesel also contains 60-70% of mixed fatty acid, 5-10% of phytosterol, about 5% of natural vitamin E and the like, and the mixed fatty acid is the main raw material phytosterol for producing the biodiesel and the vitamin E is high-grade natural oil chemicals, so that the biodiesel has very wide application and can be directly used as heavy oil to burn to cause great waste of precious natural resources.
Although the plant asphalt contains a certain amount of sterol and natural vitamin E, the plant asphalt has many kinds of impurities and high content, and the sterol has many kinds, different sterols, steroids, sterol esters and other compounds have close properties, so that the separation and purification process for extracting the high-purity sterol and the vitamin E is complex, the energy consumption of the purification process is high, the product market capacity is small, the product additional value is not high, most of the plant asphalt does not find a proper utilization way at present, and a treatment process for improving the additional value of the plant asphalt product is urgently needed.
Disclosure of Invention
In order to overcome the defects and shortcomings in the prior art, the invention aims to provide a processing method for producing biodiesel by hydrogenating plant asphalt.
The purpose of the invention is realized by the following technical scheme: a processing method for producing biodiesel by hydrogenating plant asphalt comprises the following steps:
(1) desalting, dehydrating and removing impurities from the raw oil;
(2) carrying out a first hydrogenation process on the treated raw material;
(3) separating the first hydrogenation product to obtain light hydrocarbons and heavy hydrocarbons;
(4) separating heavy hydrocarbons or further converting the heavy hydrocarbons;
A. separation treatment: separating heavy hydrocarbons to obtain a white oil fraction with low aromatic hydrocarbon content, a liquid paraffin fraction, a lubricating oil base oil fraction and a heavy residual oil fraction;
B. further conversion treatment: carrying out a hydrocracking process on the heavy residual oil fraction to crack the steroid macromolecules into micromolecules;
(5) carrying out a second hydrogenation process on the light alkane and the hydrocracking product generated in the first hydrogenation process, and further carrying out hydrofining to remove oxygen in the first hydrogenation product;
(6) and fractionating the product of the second hydrogenation process to obtain biological light oil, biological aviation kerosene, biological diesel oil and biological heavy oil components.
Preferably, in the step (1), the desalting adopts an electric desalting process, the dehydrating adopts a negative pressure distillation dehydrating process, and the impurity removal adopts centrifugal separation or plate-and-frame filtration.
Preferably, in the step (2), the first hydrogenation process adopts an upflow reactor suspended bed or a fluidized bed with good heat and mass transfer, or is combined with a downflow fixed bed reactor; or a downflow type fixed bed reactor can be independently adopted, the raw oil needs to be diluted by circulating oil, and the volume ratio of the circulating oil to the raw oil is (2-5): 1.
preferably, in the step (2), the operating pressure of the first hydrogenation process is 5-25MPa, the temperature is 350-450 ℃, and the volume ratio of hydrogen to oil is 800-1500: 1, the volume space velocity is 0.3-2.0h-1(ii) a The metals in the raw material can be removed through the first hydrogenation process, and the oxygen content in the raw material is reduced by 40-100%.
Preferably, in the step (2), the first hydrogenation process is catalyzed by mixing an oil-soluble catalyst and a solid catalyst, wherein the addition amount of the oil-soluble catalyst accounts for 0.01-0.10 wt% of the raw oil, and the addition amount of the solid catalyst accounts for 0.5-2.0 wt% of the raw oil.
According to the invention, the oil-soluble catalyst is used for realizing the high-efficiency dispersion and mixing of the catalyst, the hydrogenation performance of the active metal is fully exerted, the catalyst is promoted to exert better efficiency, the hydrocracking reaction rate is increased, the volume of a hydrogenation reactor is reduced, and the coking can be reduced; meanwhile, the solid catalyst is used, the characteristics of strong coke adsorption and bearing capacity of the solid catalyst are exerted, the adsorption of the coked substances and the metal organic matters in the hydrogenation reactor is realized, and the discharge of the coked substances and the metal organic matters in the hydrogenation reactor is promoted; the treated light oil product has high yield and good quality, the addition amount of active metal in the oil-soluble catalyst can be reduced, energy is saved, emission is reduced, the steps are simple, and the cost is low.
Preferably, the oil-soluble catalyst is a complex formed by metal molybdenum, iron, cobalt or nickel and an organic matter. More preferably, the oil-soluble liquid catalyst is at least one of an oil-soluble molybdenum amine complex, molybdenum naphthenate, molybdenum alkyl thiophosphate, molybdenum dialkyl dithiocarbamate, molybdenum dialkyl dithiophosphate, molybdenum 2-ethylhexanoate, molybdenum fatty acid, molybdenum isooctanoate, molybdenum alkyl thiocarbamate, and molybdenum organic acid. The oil soluble catalyst can be mutually soluble with the processed heavy oil or a certain section of distillate oil in the heavy oil, and can be decomposed into nano-scale metal sulfide particles in a hydrogenation reactor.
Preferably, the carrier of the solid catalyst is at least one of activated carbon, semi-coke, clay, natural diatomite and kaolin, the carrier is loaded with metal active components of molybdenum, iron, cobalt or nickel, and the particle size of the solid catalyst is 1-1000 μm. The solid catalyst of the invention adopts the carrier, has larger specific surface area, low cost and good adsorption effect.
Preferably, in the step (3), the separation method of the first hydrogenation product comprises the following processes:
a. a separation tank is adopted to realize gas-liquid separation;
b. distilling and separating the liquid phase to obtain light hydrocarbons and heavy hydrocarbons; the light hydrocarbons are below C10, and the heavy hydrocarbons include normal alkanes between C10-C20, normal hydrocarbons above C20, and steroid.
Preferably, in the step (4), the separation method of heavy hydrocarbons adopts a cooling filtration method. Because the steroid components have higher condensation points and lower solubility in solvent oil and water, the solvent oil can be adopted to carry out cooling extraction on the heavy hydrocarbon mixture, thereby realizing the separation of normal alkane and steroid compounds; the separated normal paraffins between C10 and C20 belong to white oil fraction with low aromatic hydrocarbon content; the normal hydrocarbons above C20 belong to liquid paraffin fraction; the steroid component produced after hydrogenation of sterols contains a large amount of lube base oil fractions.
Preferably, in the step B, the hydrocracking process adopts a hydrocracking catalyst which uses amorphous aluminosilicate or molecular sieve with acid centers as a carrier and supports active metals of molybdenum, nickel, cobalt or tungsten.
The invention has the beneficial effects that: the processing method can process the plant asphalt to obtain the components of the biodiesel, the white oil, the liquid paraffin, the lubricating oil base oil, the biological light oil, the biological aviation kerosene, the biological heavy oil and the like, and has the advantages of simple steps, convenient operation and control, low energy consumption and high added value of products.
Detailed Description
The present invention will be further described with reference to the following examples for facilitating understanding of those skilled in the art, and the description of the embodiments is not intended to limit the present invention.
Example 1
A processing method for producing biodiesel by hydrogenating plant asphalt comprises the following steps:
(1) desalting, dehydrating and removing impurities from the raw oil;
(2) carrying out a first hydrogenation process on the treated raw material;
(3) separating the first hydrogenation product to obtain light hydrocarbons and heavy hydrocarbons;
(4) separating heavy hydrocarbons or further converting the heavy hydrocarbons;
A. separation treatment: separating heavy hydrocarbons to obtain a white oil fraction with low aromatic hydrocarbon content, a liquid paraffin fraction, a lubricating oil base oil fraction and a heavy residual oil fraction;
B. further conversion treatment: carrying out a hydrocracking process on the heavy residual oil fraction to crack the steroid macromolecules into micromolecules;
(5) carrying out a second hydrogenation process on the light alkane and the hydrocracking product generated in the first hydrogenation process, and further carrying out hydrofining to remove oxygen in the first hydrogenation product;
(6) and fractionating the product of the second hydrogenation process to obtain biological light oil, biological aviation kerosene, biological diesel oil and biological heavy oil components.
In the step (1), the desalting adopts an electric desalting process, the dewatering adopts a negative pressure distillation dewatering process, and the impurity removal adopts centrifugal separation or plate-and-frame filtration.
In the step (2), the first hydrogenation process adopts an upflow reactor suspension bed or a fluidized bed with good heat and mass transfer, or is combined with a downflow fixed bed reactor for use; or a downflow fixed bed reactor can be independently adopted, the raw oil needs to be diluted by circulating oil, and the volume ratio of the circulating oil to the raw oil is 2: 1.
in the step (2), the operating pressure of the first hydrogenation process is 5MPa, the temperature is 350 ℃, and the volume ratio of hydrogen to oil is 800: 1, volume space velocity of 0.3h-1(ii) a The metals in the raw material can be removed through the first hydrogenation process, and the oxygen content in the raw material is reduced by 40%.
In the step (2), the first hydrogenation process adopts oil-soluble catalyst and solid catalyst to mix for catalysis, the adding amount of the oil-soluble catalyst accounts for 0.01 wt% of the raw oil, and the adding amount of the solid catalyst accounts for 0.5 wt% of the raw oil.
The oil-soluble catalyst is a complex formed by metal molybdenum and organic matters.
The carrier of the solid catalyst is active carbon or semi-coke, the carrier is loaded with a metal active component molybdenum, and the particle size of the solid catalyst is 1 μm. The solid catalyst adopts the carrier, has larger specific surface area, low cost and good adsorption effect.
In the step (3), the separation method of the first hydrogenation product comprises the following processes:
a. a separation tank is adopted to realize gas-liquid separation;
b. distilling and separating the liquid phase to obtain light hydrocarbons and heavy hydrocarbons; the light hydrocarbons are below C10, and the heavy hydrocarbons include normal alkanes between C10-C20, normal hydrocarbons above C20, and steroid.
In the step (4), a cooling filtration method is adopted as a heavy hydrocarbon separation method.
In the step B, the hydrocracking process adopts a hydrocracking catalyst which takes amorphous aluminosilicate or molecular sieve with acid centers as a carrier and loads active metal molybdenum, nickel, cobalt or tungsten.
Example 2
This embodiment is different from embodiment 1 described above in that:
in the step (2), the first hydrogenation process adopts an upflow reactor suspension bed or a fluidized bed with good heat and mass transfer, or is combined with a downflow fixed bed reactor for use; or a downflow fixed bed reactor can be independently adopted, the raw oil needs to be diluted by circulating oil, and the volume ratio of the circulating oil to the raw oil is 3.5: 1.
in the step (2), the operating pressure of the first hydrogenation process is 15MPa, the temperature is 400 ℃, and the volume ratio of hydrogen to oil is 1200: 1, volume space velocity of 1.2h-1(ii) a The metals in the raw material can be removed through the first hydrogenation process, and the oxygen content in the raw material is reduced by 70%.
In the step (2), the first hydrogenation process is catalyzed by mixing an oil-soluble catalyst and a solid catalyst, wherein the addition amount of the oil-soluble catalyst accounts for 0.05 wt% of the raw oil, and the addition amount of the solid catalyst accounts for 1.2 wt% of the raw oil.
The oil-soluble catalyst is a complex formed by metallic iron and organic matters.
The carrier of the solid catalyst is argil, the carrier is loaded with metal active component iron, and the particle size of the solid catalyst is 100 mu m.
Example 3
This embodiment is different from embodiment 1 described above in that:
in the step (2), the first hydrogenation process adopts an upflow reactor suspension bed or a fluidized bed with good heat and mass transfer, or is combined with a downflow fixed bed reactor for use; or a downflow fixed bed reactor can be independently adopted, the raw oil needs to be diluted by circulating oil, and the volume ratio of the circulating oil to the raw oil is 5: 1.
in the step (2), the operating pressure of the first hydrogenation process is 25MPa, the temperature is 450 ℃, and the volume ratio of hydrogen to oil is 1500: 1, volume space velocity of 2.0h-1(ii) a The metals in the raw material can be removed through the first hydrogenation process, and the oxygen content in the raw material is reduced by 100 percent.
In the step (2), the first hydrogenation process adopts oil-soluble catalyst and solid catalyst to mix for catalysis, the adding amount of the oil-soluble catalyst accounts for 0.10 wt% of the raw oil, and the adding amount of the solid catalyst accounts for 2.0 wt% of the raw oil.
The oil-soluble catalyst is a complex formed by metal cobalt or nickel and an organic matter.
The carrier of the solid catalyst is natural diatomite or kaolin, the carrier is loaded with metal active components cobalt or nickel, and the particle size of the solid catalyst is 1000 μm.
The processing method can process the plant asphalt to obtain the components of the biodiesel, the white oil, the liquid paraffin, the lubricating oil base oil, the biological light oil, the biological aviation kerosene, the biological heavy oil and the like, and has the advantages of simple steps, convenient operation and control, low energy consumption and high added value of products.
The above-described embodiments are preferred implementations of the present invention, and the present invention may be implemented in other ways without departing from the spirit of the present invention.
Claims (10)
1. A processing method for producing biodiesel by hydrogenating plant asphalt is characterized by comprising the following steps: the method comprises the following steps:
(1) desalting, dehydrating and removing impurities from the raw oil;
(2) carrying out a first hydrogenation process on the treated raw material;
(3) separating the first hydrogenation product to obtain light hydrocarbons and heavy hydrocarbons;
(4) separating heavy hydrocarbons or further converting the heavy hydrocarbons;
A. separation treatment: separating heavy hydrocarbons to obtain a white oil fraction with low aromatic hydrocarbon content, a liquid paraffin fraction, a lubricating oil base oil fraction and a heavy residual oil fraction;
B. further conversion treatment: carrying out a hydrocracking process on the heavy residual oil fraction to crack the steroid macromolecules into micromolecules;
(5) carrying out a second hydrogenation process on the light alkane and the hydrocracking product generated in the first hydrogenation process, and further carrying out hydrofining to remove oxygen in the first hydrogenation product;
(6) and fractionating the product of the second hydrogenation process to obtain biological light oil, biological aviation kerosene, biological diesel oil and biological heavy oil components.
2. The process of claim 1 for producing biodiesel from plant pitch by hydrogenation, wherein the process comprises the steps of: in the step (1), the desalting adopts an electric desalting process, the dewatering adopts a negative pressure distillation dewatering process, and the impurity removal adopts centrifugal separation or plate-and-frame filtration.
3. The process of claim 1 for producing biodiesel from plant pitch by hydrogenation, wherein the process comprises the steps of: in the step (2), the first hydrogenation process adopts an upflow reactor suspension bed or a fluidized bed with good heat and mass transfer, or is combined with a downflow fixed bed reactor for use; or a downflow type fixed bed reactor can be independently adopted, the raw oil needs to be diluted by circulating oil, and the volume ratio of the circulating oil to the raw oil is (2-5): 1.
4. the process of claim 1 for producing biodiesel from plant pitch by hydrogenation, wherein the process comprises the steps of: in the step (2), the operating pressure of the first hydrogenation process is 5-25MPa, the temperature is 350-450 ℃, and the volume ratio of hydrogen to oil is 800-1500: 1, the volume space velocity is 0.3-2.0h-1(ii) a The metals in the raw material can be removed through the first hydrogenation process, and the oxygen content in the raw material is reduced by 40-100%.
5. The process of claim 1 for producing biodiesel from plant pitch by hydrogenation, wherein the process comprises the steps of: in the step (2), the first hydrogenation process adopts oil-soluble catalyst and solid catalyst to mix for catalysis, the adding amount of the oil-soluble catalyst accounts for 0.01-0.10 wt% of the raw oil, and the adding amount of the solid catalyst accounts for 0.5-2.0 wt% of the raw oil.
6. The process of claim 5 for producing biodiesel from plant pitch by hydrogenation, wherein the process comprises the steps of: the oil-soluble catalyst is a complex formed by metal molybdenum, iron, cobalt or nickel and organic matters.
7. The process of claim 5 for producing biodiesel from plant pitch by hydrogenation, wherein the process comprises the steps of: the carrier of the solid catalyst is at least one of active carbon, semi-coke, argil, natural diatomite and kaolin, the carrier is loaded with metal active components of molybdenum, iron, cobalt or nickel, and the particle size of the solid catalyst is 1-1000 μm.
8. The process of claim 1 for producing biodiesel from plant pitch by hydrogenation, wherein the process comprises the steps of: in the step (3), the separation method of the first hydrogenation product comprises the following processes:
a. a separation tank is adopted to realize gas-liquid separation;
b. distilling and separating the liquid phase to obtain light hydrocarbons and heavy hydrocarbons; the light hydrocarbons are below C10, and the heavy hydrocarbons include normal alkanes between C10-C20, normal hydrocarbons above C20, and steroid.
9. The process of claim 1 for producing biodiesel from plant pitch by hydrogenation, wherein the process comprises the steps of: in the step (4), a cooling filtration method is adopted as a heavy hydrocarbon separation method.
10. The process of claim 1 for producing biodiesel from plant pitch by hydrogenation, wherein the process comprises the steps of: in the step B, the hydrocracking process adopts a hydrocracking catalyst which takes amorphous aluminosilicate or molecular sieve with acid centers as a carrier and loads active metal molybdenum, nickel, cobalt or tungsten.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011248308.XA CN112552947B (en) | 2020-11-10 | 2020-11-10 | Processing method for producing biodiesel by hydrogenating plant asphalt |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011248308.XA CN112552947B (en) | 2020-11-10 | 2020-11-10 | Processing method for producing biodiesel by hydrogenating plant asphalt |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN112552947A true CN112552947A (en) | 2021-03-26 |
| CN112552947B CN112552947B (en) | 2023-01-03 |
Family
ID=75041973
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011248308.XA Active CN112552947B (en) | 2020-11-10 | 2020-11-10 | Processing method for producing biodiesel by hydrogenating plant asphalt |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112552947B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113337310A (en) * | 2021-06-29 | 2021-09-03 | 海南盈科生物科技有限公司 | Method for preparing biodiesel by deep processing of biomass residual oil |
| CN113801693A (en) * | 2021-10-15 | 2021-12-17 | 海南盈科生物科技有限公司 | Combined hydrogenation method for fatty acid residue oil |
| CN114634826A (en) * | 2022-02-17 | 2022-06-17 | 神木富油能源科技有限公司 | Method and system for preparing jet fuel, white oil and lubricating oil base oil by hydrogenating waste oil |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102504866A (en) * | 2011-11-08 | 2012-06-20 | 海南临高化工实业有限公司 | Method for preparing biodiesel by mixing waste edible oil with mineral diesel oil and hydrogenization |
-
2020
- 2020-11-10 CN CN202011248308.XA patent/CN112552947B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102504866A (en) * | 2011-11-08 | 2012-06-20 | 海南临高化工实业有限公司 | Method for preparing biodiesel by mixing waste edible oil with mineral diesel oil and hydrogenization |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113337310A (en) * | 2021-06-29 | 2021-09-03 | 海南盈科生物科技有限公司 | Method for preparing biodiesel by deep processing of biomass residual oil |
| CN113801693A (en) * | 2021-10-15 | 2021-12-17 | 海南盈科生物科技有限公司 | Combined hydrogenation method for fatty acid residue oil |
| CN114634826A (en) * | 2022-02-17 | 2022-06-17 | 神木富油能源科技有限公司 | Method and system for preparing jet fuel, white oil and lubricating oil base oil by hydrogenating waste oil |
| CN114634826B (en) * | 2022-02-17 | 2023-04-07 | 神木富油能源科技有限公司 | Method and system for preparing jet fuel, white oil and lubricating oil base oil by hydrogenating waste oil |
Also Published As
| Publication number | Publication date |
|---|---|
| CN112552947B (en) | 2023-01-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN112552947B (en) | Processing method for producing biodiesel by hydrogenating plant asphalt | |
| CN109294622B (en) | Process and device for realizing heavy oil lightening by using suspension bed hydrogenation | |
| CN101191081B (en) | Catalytic conversion method for hydrocarbon oil raw material | |
| CN103265971A (en) | Heterogeneous coal tar suspension bed hydrogenation method | |
| CN104962307B (en) | Method for producing light oil through coal liquefaction | |
| CN102796559A (en) | Method and apparatus for producing fuel oil by hydrocracking | |
| CN114045179B (en) | Multiphase flow residual oil hydro-upgrading and catalytic cracking combined process and system | |
| CN102041047B (en) | Heavy oil hydrogenation modifying method | |
| CN109111950B (en) | Method for producing liquid fuel by hydrogenating full-fraction tar | |
| CN104962314A (en) | System and method for producing raw material of needle coke by oil slurry | |
| CN110093186B (en) | Method for combined processing of catalytic cracking slurry oil | |
| CN109355100B (en) | Coal tar processing and coal co-refining combined process | |
| CN105296002B (en) | Coal tar cleaning puies forward the method and system that phenol back end hydrogenation produces fuel oil | |
| CN110093187B (en) | Method for combined processing of catalytic cracking slurry oil | |
| CN103102932A (en) | Hydrocarbon modification separation method | |
| CN113717754B (en) | Catalytic cracking process for producing high aromatic hydrocarbon oil and high yield liquefied gas | |
| CN113755208B (en) | High aromatic hydrocarbon oil material and preparation method and application thereof | |
| CN103789035B (en) | A kind of heavy benzene hydrogenation produces clean fuel oil method | |
| CN108102707B (en) | Processing method of high-calcium, high-nitrogen and high-viscosity residual oil | |
| CN113462432B (en) | Waste oil processing method and skid-mounted modular integrated device for waste oil processing | |
| CN109181762A (en) | A kind of multistage suspension bed hydroprocessing device and method of poor oil | |
| CN111154505B (en) | Coal tar hydrotreating process | |
| CN110358615B (en) | Device and method for regenerating waste lubricating oil | |
| CN111849552B (en) | Coal tar full-fraction hydrogenation upgrading method and system | |
| CN107880929B (en) | Atmospheric and vacuum distillation process and system for hydrogenation product of suspension bed |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20220831 Address after: No. 8, South 1st Row, Xinxing Road, Xinle City, Shijiazhuang City, Hebei Province, 050000 Applicant after: Shijiazhuang Ruitu Biotechnology Co.,Ltd. Address before: 570000 Room 201, building B, National University Science Park, Hainan Normal University, No.3 Haitao Avenue, Jiangdong new district, Haikou City, Hainan Province Applicant before: Hainan Bailang Biotechnology Co.,Ltd. |
|
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20220915 Address after: 201913 No. 495, Yuejin South Road, Xinhai Town, Chongming District, Shanghai (Guangming Rice Industry Economic Park) Applicant after: Shanghai Kered Energy Technology Co.,Ltd. Address before: No. 8, South 1st Row, Xinxing Road, Xinle City, Shijiazhuang City, Hebei Province, 050000 Applicant before: Shijiazhuang Ruitu Biotechnology Co.,Ltd. |
|
| GR01 | Patent grant | ||
| GR01 | Patent grant |