CN112159682A - Method for preparing low-condensation-point renewable alkane by hydrogenating waste animal and vegetable oil - Google Patents
Method for preparing low-condensation-point renewable alkane by hydrogenating waste animal and vegetable oil Download PDFInfo
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- 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
- C10G67/14—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 including at least two different refining steps in the absence of hydrogen
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- 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
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- C10G2300/1003—Waste materials
- C10G2300/1007—Used oils
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- 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
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4006—Temperature
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4012—Pressure
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
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Abstract
The invention discloses a method for preparing low-condensation-point renewable alkane by hydrogenating waste animal and vegetable oil, which comprises the following steps: uniformly mixing the waste animal and vegetable oil and renewable alkane with hydrogen to perform hydrogenation reaction; separating the obtained materials at high pressure to obtain gas, product oil and water; low-pressure separation is carried out on the product oil and water, and the product oil is stripped and desulfurized; distilling the desulfurized product oil at normal pressure to obtain renewable light hydrocarbon and renewable alkane, returning part of the renewable alkane to the initial stage, and carrying out hydrogenation isomerization reaction on the rest of the renewable alkane; and (3) carrying out high-pressure separation on the material obtained by the hydroisomerization reaction to separate gas and product oil, carrying out low-pressure separation on the product oil to separate dissolved gas in the product oil, fractionating the product oil to obtain renewable light hydrocarbon with the fractionation temperature of less than 120 ℃, and taking the rest material as low-condensation-point renewable alkane. The condensation point of the renewable alkane is effectively reduced to be below-15 ℃, the yield of the renewable alkane with low condensation point is higher than 80 wt.%, and the generated gaseous hydrocarbon is less.
Description
Technical Field
The invention belongs to the field of energy and chemical industry, and particularly relates to a method for preparing low-condensation-point renewable alkane by hydrogenating waste animal and vegetable oil.
Background
The quantity of waste grease produced in China every year is very large, and the waste grease and waste cooking oil recovered from large and medium cities are used for preparing the biodiesel, so that the production cost of the biodiesel can be reduced, the industrial waste oil and other waste oil can be comprehensively utilized, waste materials are changed into valuable materials, and the coordinated development of economy and environmental protection is realized.
The condensation point of the renewable alkane prepared by the waste animal and vegetable oil through hydrogenation is higher, and the value is lower. The hydrocracking pour point depressing technique generally adopted generates more gases and has lower yield of low pour point renewable alkane.
Disclosure of Invention
The technical problem to be solved by the invention is as follows: provides a method for preparing low-condensation-point renewable alkane by hydrogenating waste animal and vegetable oil with high yield.
In order to solve the technical problems, the technical scheme provided by the invention is as follows: a method for preparing low-condensation-point renewable alkane by hydrogenating waste animal and vegetable oil comprises the following steps:
a) waste animal and vegetable oil and renewable alkane are uniformly mixed to obtain a mixture;
b) mixing the mixture obtained in the step a) with hydrogen to carry out hydrogenation reaction in the presence of a hydrogenation catalyst;
c) performing high-pressure separation on the material obtained in the step b) through hydrogenation reaction to obtain gas, product oil and water through separation; gas circulates in the reaction device;
d) low-pressure separation is carried out on the product oil and the water obtained in the step c), steam stripping desulfurization is carried out on the product oil obtained by separation, and the water separated at low pressure is discharged;
e) carrying out normal pressure fractionation on the desulfurized product oil to fractionate renewable light hydrocarbon and renewable alkane, wherein part of the renewable alkane is refluxed to the step a) to be mixed with the waste animal and vegetable oil raw material, and the rest part is subjected to a hydroisomerization reaction in the presence of a hydroisomerization catalyst;
f) and e) carrying out high-pressure separation on the material obtained by the hydroisomerization reaction in the step e), separating gas and product oil, circulating the gas in a reaction device, carrying out low-pressure separation on the product oil, separating out dissolved gas in the product oil, fractionating the residual product oil, fractionating renewable light hydrocarbon with the fractionation temperature of less than 120 ℃, and obtaining low-condensation-point renewable alkane as the residual material.
Preferably, the method for preparing the low-condensation-point renewable alkane by hydrogenating the waste animal and vegetable oil comprises the following steps:
a) waste animal and vegetable oil and renewable alkane are uniformly mixed to obtain a mixture; wherein the renewable alkane accounts for 10-90 wt% of the waste animal and vegetable oil;
b) mixing the mixture obtained in the step a) with hydrogen, entering a hydrogenation reactor, and carrying out hydrogenation reaction in the presence of a hydrogenation catalyst; the reaction conditions are as follows: liquid airspeed of 0.5-2 h-1The volume ratio of hydrogen to oil is 500: 1-2000: 1, the reaction pressure is 4-8 MPa, and the reaction temperature is 320-;
c) feeding the material obtained in the hydrogenation reaction in the step b) into a hydrogenation high-pressure separator, separating under the condition that the pressure is 4-8 Mpa, and separating to obtain gas, product oil and water; the gas enters a hydrogenation recycle hydrogen compressor and circulates in a reaction device;
d) feeding the product oil and water obtained in the step c) into a hydrogenation low-pressure separator, separating under the condition that the pressure is 0.5-1.5 MPa, feeding the separated product oil into a stripping tower for desulfurization, and discharging the separated water into a sewage tank;
e) the desulfurized product oil enters a hydrogenation fractionating tower for atmospheric fractionation, renewable light hydrocarbon is produced at the top of the hydrogenation fractionating tower, renewable alkane is produced at the bottom of the hydrogenation fractionating tower, part of the renewable alkane produced at the bottom of the hydrogenation fractionating tower reflows and is mixed with the waste animal and vegetable oil raw material, and the rest part enters an isomerization reactor through an isomerization feed pump and is subjected to hydrogenation isomerization reaction in the presence of a hydrogenation isomerization catalyst; the reaction conditions are as follows: liquid airspeed of 0.5-2 h-1The volume ratio of hydrogen to oil is 500: 1-2000: 1, the reaction pressure is 2-6 MPa, and the reaction temperature is 300-;
f) and (2) feeding the material at the outlet of the isomerization reactor into an isomerization high-pressure separator, separating gas and product oil under the pressure of 2-6 MPa, circulating the gas in a reaction device by an isomerization circulating hydrogen compressor, feeding the product oil into an isomerization low-pressure separator, separating dissolved gas and product oil under the pressure of 0.5-1.5 MPa, removing the dissolved gas to a torch, feeding the product oil into an isomerization fractionating tower, distilling the renewable light hydrocarbon with the temperature of less than 120 ℃ at the top of the tower, and distilling the low-condensation-point renewable alkane at the bottom of the tower.
The waste animal and vegetable oil is one or more of waste cooking oil, swill oil, palmitic acid oil, coconut oil and palm oil.
The hydrogenation catalyst consists of 1-30 wt% of active component and a catalyst carrier. The active components are two or three of nickel metal salt, molybdenum metal salt, cobalt metal salt and tungsten metal salt; the catalyst carrier is modified molecular sieve-alumina. The modified molecular sieve-alumina is molecular sieve modified Al2O3(ii) a The molecular sieve is selected from one or more of SAPO-34 type molecular sieve, ZSM-22 type molecular sieve, ZSM-23 type molecular sieve, NaX type molecular sieve, MCM-41 type molecular sieve, SAPO-11 type molecular sieve and ZSM-35 type molecular sieve. The content of the molecular sieve in the modified molecular sieve-alumina is 0.1 wt% -10 wt%.
The hydroisomerization catalyst consists of an active component with the content of 0.2 to 1.0 weight percent and a catalyst carrier; the active component is a platinum metal salt or a palladium metal salt; the catalyst carrier is modified molecular sieve-alumina. The modified molecular sieve-alumina carrier of the hydroisomerization catalyst is molecular sieve modified Al2O3A carrier; the molecular sieve is selected from one or more of SAPO-34 type molecular sieve, ZSM-22 type molecular sieve, ZSM-5 type molecular sieve, MCM-41 type molecular sieve, SAPO-11 type molecular sieve and ZSM-35 type molecular sieve. The content of the molecular sieve in the modified molecular sieve-alumina is 10 wt% -80 wt%.
Has the advantages that: the condensation point of the renewable alkane can be effectively reduced by adopting the process, the condensation point is reduced to be below-15 ℃, the yield of the renewable alkane with low condensation point is higher than 80 wt.%, and the generated gaseous hydrocarbon is less.
Drawings
FIG. 1 is a process flow diagram for preparing low condensation point renewable alkane by hydrogenating waste animal and vegetable oil;
in the figure, 1, a new hydrogenation hydrogen compressor, 2, a hydrogenation feeding pump, 3, a recycle hydrogenation hydrogen compressor, 4, a hydrogenation reactor, 5, a high-pressure hydrogenation separator, 6, a low-pressure hydrogenation separator, 7, a stripping tower, 8, a hydrogenation fractionating tower, 9, an isomeric feeding pump, 10, an isomeric new hydrogen compressor, 11, an isomeric recycle hydrogen compressor, 12, an isomeric reactor, 13, an isomeric high-pressure separator, 14, an isomeric low-pressure separator and 15, an isomeric fractionating tower are arranged.
Detailed Description
The method of the present invention will be further described with reference to the accompanying drawings, but the invention is not limited thereto.
The method for preparing the low-condensation-point renewable alkane by hydrogenating the waste animal and vegetable oil comprises the following specific steps of:
a) feeding the waste animal and vegetable oil and the renewable alkane through a hydrogenation feeding pump 2, and uniformly mixing to obtain a mixture; wherein the renewable alkane accounts for 10-90 wt% of the waste animal and vegetable oil;
b) mixing the mixture obtained in the step a) with hydrogen fed by a new hydrogenation compressor 1, feeding the mixture into a hydrogenation reactor 4, and carrying out hydrogenation reaction with the hydrogen in the presence of a hydrogenation catalyst; the hydrorefining reaction has the reaction conditions as follows: liquid airspeed of 0.5-2 h-1The volume ratio of hydrogen to oil is 500: 1-2000: 1, the reaction pressure is 4-8 MPa, and the reaction temperature is 320-;
c) feeding the material obtained in the hydrogenation reaction in the step b) into a hydrogenation high-pressure separator 5, and separating under the condition of 4-8 MPa to obtain gas, product oil and water; the gas enters a hydrogenation recycle hydrogen compressor 3 and circulates in the reaction device;
d) feeding the product oil and water obtained in the step c) into a hydrogenation low-pressure separator 6, separating under the pressure of 0.5-1.5 MPa, feeding the product oil obtained by separation into a stripping tower 7 for desulfurization, and discharging the water into a sewage tank;
e) the desulfurized product oil enters a hydrogenation fractionating tower 8 for atmospheric fractionation, renewable light hydrocarbon is ejected out of the hydrogenation fractionating tower 8, renewable alkane is ejected out of the tower bottom, part of the renewable alkane ejected out of the tower bottom of the hydrogenation fractionating tower 8 reflows and is mixed with the raw material, the rest of the renewable alkane enters an isomerization reactor 12 through an isomerization feed pump 9, and the mixture is stored in a hydrogenation isomerization catalystThen, carrying out hydroisomerization reaction with hydrogen fed by an isomerization fresh hydrogen compressor 10; the reaction conditions are as follows: liquid airspeed of 0.5-2 h-1The volume ratio of hydrogen to oil is 500: 1-2000: 1, the reaction pressure is 2-6 MPa, and the reaction temperature is 300-;
f) the method comprises the following steps that materials at the outlet of an isomerization reactor enter an isomerization high-pressure separator 13, gas and product oil are separated under the pressure of 2-6 MPa, the gas passes through an isomerization circulating hydrogen compressor 11 and is circulated in a reaction device, the product oil enters an isomerization low-pressure separator 14, dissolved gas and product oil are separated under the pressure of 0.5-1.5 MPa, the dissolved gas is removed from a torch, the product oil enters an isomerization fractionating tower 15, the fraction at the top of the tower is renewable light hydrocarbon with the temperature of less than 120 ℃, the fraction at the bottom of the tower is renewable alkane with the low condensation point, and the renewable alkane enters a product tank.
Table 1: the properties of the waste animal and vegetable oil in the embodiment are as follows:
| illegal cooking oil | Soybean oil | Palm fatty acid | Swill oil | |
| Density (20 ℃ C.)/(g/cm)3) | 0.908 | 0.915 | 0.874 | 0.920 |
| Viscosity at 40 deg.C/(mm)2/s) | 22.2 | 36.4 | 20.1 | 30.0 |
| Total acid value/(mgKOH/g) | 122.2 | 0.6 | 205.1 | 10.0 |
| C1 content/%) | 6.9 | 59.2 | 3.7 | 51.9 |
| S content/(μ g/g) | 24.5 | 23.3 | 22.8 | 16.6 |
Table 2: examples 1-3 Experimental conditions and Low freezing Point renewable alkane Performance
Claims (10)
1. A method for preparing low-condensation-point renewable alkane by hydrogenating waste animal and vegetable oil comprises the following steps:
a) waste animal and vegetable oil and renewable alkane are uniformly mixed to obtain a mixture;
b) mixing the mixture obtained in the step a) with hydrogen to carry out hydrogenation reaction in the presence of a hydrogenation catalyst;
c) performing high-pressure separation on the material obtained in the step b) through hydrogenation reaction to obtain gas, product oil and water through separation; gas circulates in the reaction device;
d) low-pressure separation is carried out on the product oil and the water obtained in the step c), steam stripping desulfurization is carried out on the product oil obtained by separation, and the water separated at low pressure is discharged;
e) carrying out normal pressure fractionation on the desulfurized product oil to fractionate renewable light hydrocarbon and renewable alkane, wherein part of the renewable alkane reflows to the step a) to be mixed with the waste animal and vegetable oil raw material, and the rest of the renewable alkane is subjected to hydrogenation isomerization reaction in the presence of a hydrogenation isomerization catalyst;
f) and e) carrying out high-pressure separation on the material obtained by the hydroisomerization reaction in the step e), separating gas and product oil, circulating the gas in a reaction device, carrying out low-pressure separation on the product oil, separating out dissolved gas in the product oil, fractionating the residual product oil, fractionating to obtain renewable light hydrocarbon with the boiling point of less than 120 ℃, and obtaining low-condensation-point renewable alkane as the residual material.
2. The method for preparing the low-condensation-point renewable alkane by hydrogenating the waste animal and vegetable oil according to claim 1, is characterized in that: the method comprises the following steps:
a) waste animal and vegetable oil and renewable alkane are uniformly mixed to obtain a mixture; wherein the renewable alkane accounts for 10-90 wt% of the waste animal and vegetable oil;
b) mixing the mixture obtained in the step a) with hydrogen, entering a hydrogenation reactor, and carrying out hydrogenation reaction in the presence of a hydrogenation catalyst; the reaction conditions are as follows: liquid airspeed of 0.5-2 h-1The volume ratio of hydrogen to oil is 500: 1-2000: 1, the reaction pressure is 4-8 MPa, and the reaction temperature is 320-;
c) feeding the material obtained in the hydrogenation reaction in the step b) into a hydrogenation high-pressure separator, separating under the condition that the pressure is 4-8 Mpa, and separating to obtain gas, product oil and water; the gas enters a hydrogenation recycle hydrogen compressor and circulates in a reaction device;
d) feeding the product oil and water obtained in the step c) into a hydrogenation low-pressure separator, separating under the condition that the pressure is 0.5-1.5 MPa, feeding the separated product oil into a stripping tower for desulfurization, and discharging the separated water into a sewage tank;
e) the desulfurized product oil enters a hydrogenation fractionating tower for atmospheric fractionation, renewable light hydrocarbon is produced at the top of the hydrogenation fractionating tower, renewable alkane is produced at the bottom of the hydrogenation fractionating tower, part of the renewable alkane produced at the bottom of the hydrogenation fractionating tower reflows and is mixed with the waste animal and vegetable oil raw material, and the rest part enters an isomerization reactor through an isomerization feed pump and is subjected to hydrogenation isomerization reaction in the presence of a hydrogenation isomerization catalyst; the reaction conditions are as follows: liquid airspeed of 0.5-2 h-1The volume ratio of hydrogen to oil is 500: 1-2000: 1, the reaction pressure is 2-6 MPa, and the reaction temperature is 300-;
f) and (2) feeding the material at the outlet of the isomerization reactor into an isomerization high-pressure separator, separating gas and product oil under the condition of pressure of 2-6 MPa, circulating the gas in a reaction device by an isomerization circulating hydrogen compressor, feeding the product oil into an isomerization low-pressure separator, separating dissolved gas and product oil under the condition of pressure of 0.5-1.5 MPa, removing the dissolved gas to a torch, feeding the product oil into an isomerization fractionating tower, fractionating renewable light hydrocarbon with the temperature of less than 120 ℃ at the top of the tower, and fractionating low-condensation-point renewable alkane at the bottom of the tower.
3. The method for preparing the low-condensation-point renewable alkane by hydrogenating the waste animal and vegetable oil and fat according to claim 1 or 2, wherein the method comprises the following steps: the waste animal and vegetable oil is one or more of waste cooking oil, swill oil, palmitic acid oil, coconut oil and palm oil.
4. The method for preparing the low-condensation-point renewable alkane by hydrogenating the waste animal and vegetable oil and fat according to claim 1 or 2, wherein the method comprises the following steps: the hydrogenation catalyst consists of 1-30 wt% of active component and a catalyst carrier.
5. The method for preparing the low-condensation-point renewable alkane by hydrogenating the waste animal and vegetable oil according to claim 4, wherein the method comprises the following steps: the active components are two or three of nickel metal salt, molybdenum metal salt, cobalt metal salt and tungsten metal salt; the catalyst carrier is modified molecular sieve-alumina.
6. The method for preparing the low-condensation-point renewable alkane by hydrogenating the waste animal and vegetable oil and fat according to claim 5, wherein the method comprises the following steps: the modified molecular sieve-alumina is molecular sieve modified Al2O3(ii) a The molecular sieve is selected from one or more of SAPO-34 type molecular sieve, ZSM-22 type molecular sieve, ZSM-23 type molecular sieve, NaX type molecular sieve, MCM-41 type molecular sieve, SAPO-11 type molecular sieve and ZSM-35 type molecular sieve.
7. The method for preparing the low-condensation-point renewable alkane by hydrogenating the waste animal and vegetable oil and fat as claimed in claim 6, wherein the method comprises the following steps: the content of the molecular sieve in the modified molecular sieve-alumina is 0.1 wt% -10 wt%.
8. The method for preparing the low-condensation-point renewable alkane by hydrogenating the waste animal and vegetable oil and fat according to claim 1 or 2, wherein the method comprises the following steps: the hydroisomerization catalyst consists of an active component with the content of 0.2 to 1.0 weight percent and a catalyst carrier; the active component is a platinum metal salt or a palladium metal salt; the catalyst carrier is modified molecular sieve-alumina.
9. The method for preparing the low-condensation-point renewable alkane by hydrogenating the waste animal and vegetable oil according to claim 8, wherein the method comprises the following steps: the modified molecular sieve-alumina carrier of the hydroisomerization catalyst is molecular sieve modified Al2O3A carrier; the molecular sieve is selected from one or more of SAPO-34 type molecular sieve, ZSM-22 type molecular sieve, ZSM-5 type molecular sieve, MCM-41 type molecular sieve, SAPO-11 type molecular sieve and ZSM-35 type molecular sieve.
10. The method for preparing the low-condensation-point renewable alkane by hydrogenating the waste animal and vegetable oil according to claim 8, wherein the method comprises the following steps: the content of the molecular sieve in the modified molecular sieve-alumina is 10 wt% -80 wt%.
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| CN103937527A (en) * | 2014-05-05 | 2014-07-23 | 抚顺新瑞催化剂有限公司 | Method for preparing diesel component with low condensation point through biomass oil hydrofining and isomerization-visbreaking |
| CN106256880A (en) * | 2015-06-18 | 2016-12-28 | 中国石油化工股份有限公司 | A kind of method being prepared jet fuel by animal and plant fat |
| CN109294746A (en) * | 2017-07-25 | 2019-02-01 | 中国石油化工股份有限公司 | A kind of method that grease type raw material adds hydrogen to prepare diesel oil distillate |
| CN109294623A (en) * | 2017-07-25 | 2019-02-01 | 中国石油化工股份有限公司 | A kind of grease type raw material prepares the method for hydrotreating of diesel oil distillate |
| CN110499178A (en) * | 2019-08-27 | 2019-11-26 | 易高生物化工科技(张家港)有限公司 | A kind of method that waste animal and vegetable oil adds hydrogen to prepare atoleine |
| CN110628511A (en) * | 2019-08-29 | 2019-12-31 | 易高生物化工科技(张家港)有限公司 | Method for preparing liquid paraffin by dechlorinating and hydrogenating waste animal and vegetable oil |
| CN110628512A (en) * | 2019-08-29 | 2019-12-31 | 易高生物化工科技(张家港)有限公司 | Hydrotreating method for chlorine-containing waste animal and vegetable oil |
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