CN108085039A - A kind of method that biomass by hydro-thermal liquefaction bio oil is modified - Google Patents
A kind of method that biomass by hydro-thermal liquefaction bio oil is modified Download PDFInfo
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- CN108085039A CN108085039A CN201711381188.9A CN201711381188A CN108085039A CN 108085039 A CN108085039 A CN 108085039A CN 201711381188 A CN201711381188 A CN 201711381188A CN 108085039 A CN108085039 A CN 108085039A
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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
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
-
- 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
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1011—Biomass
-
- 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
Abstract
The invention belongs to environmental protections and field of new energy technologies, and in particular to a kind of method that bio oil is modified；This method is using metallic aluminium and the aqueous portion reaction production hydrogen of biomass by hydro-thermal liquefaction bio oil, for bio oil modifying process, a kind of new bio oil method of modifying is provided, that is, improves the quality of bio oil, and realizes the recycling of hydrothermal liquefaction bio oil aqueous portion.
Description
Technical field
The invention belongs to environmental protections and field of new energy technologies, and in particular to a kind of biomass by hydro-thermal liquefaction bio oil changes
The method of property.
Background technology
Fossil energy consumes the energy crisis and environmental problem for causing the whole world excessively, and regenerative resource is subject to researcher
Extensive concern.Biomass is a kind of unique regenerative resource for being converted into liquid fuel, by its resourceful, cost
Low, CO2The features such as balance, becomes most promising alternative energy source.Biomass is mainly obtained by way of pyrolysis, hydrothermal liquefaction
It is compared to liquid fuel-bio oil with pyrolytic technique, hydrothermal liquefaction is because its raw material is applied widely, energy consumption is small, product calorific value
High, advantages of environment protection, it is considered to be most promising bio oil preparation method.
Although the biomass material for preparing bio oil is different, the main chemical compositions species of bio oil relatively,
It is mainly made of hundreds of compound, including alkane, phenol, aldehyde, ketone, acid, ester, ether, alcohol etc..The presence of wherein oxygenatedchemicals makes
Obtaining bio oil has poor fuel characteristic, is mainly shown as high viscosity, low heat value, stability are poor and corrosivity is strong etc..For example,
Polycondensation reaction easily occurs for aldehyde material, makes bio oil unstable, and the presence of aldehyde material causes bio oil with hydrophilic
Property, cause bio oil water content high and be not easy to remove；Content of the aldehydes matter in bio oil is higher, and mass fraction is up to
35%, aldehydes matter is easily aoxidized, and reduces the calorific value of bio oil, and some phenolic compounds (such as guaiacol) can also reduce biology
The stability of oil.Therefore, bio oil has to pass through modification, to improve its stability and chemical characteristic.
It is that bio oil is modified it is crucial that with the oxygen in minimum hydrogen consumption removing bio oil, while retain carbon therein.Mesh
Before, common bio oil method of modifying has catalytic pyrolysis, catalytic esterification, catalytic hydrogenation etc..The reaction temperature of catalytic pyrolysis is higher
(500-700 DEG C) be easy to cause catalyst coking and deactivation, and the yield of modification biological oil is relatively low.Catalytic esterification can only be certain
Carboxylic acids and part aldehydes is made to be converted into esters in degree, but oxygen content is still higher, it is necessary to further in bio oil after upgrading
It is hydrogenated with upgrading.
Catalytic hydrogenation is considered as most promising bio oil method of modifying, can be divided into direct hydrogen supply according to hydrogen supply mode
With hydrogen supply in situ, but hydrogenation process can consume substantial amounts of hydrogen, and every kilogram of bio oil complete hydrogenation deoxidation needs to consume 600-
The hydrogen of 1000L.Direct hydrogen supply can dramatically reduce the oxygen content of bio oil, but industrial hydrogen main source is change at present
The hydrogen manufacturing of stone fuel or water electrolysis hydrogen production.This just needs to consume mass energy, causes cost higher, and hydrogenation process is dangerous high.
In hydrogen supply in situ, what the generation of hydrogen and the modifying process of bio oil carried out in same reaction vessel, avoiding problems straight
The problems such as connecing the hydrogen preparation, storage, harsh transport and hydroconversion condition of external hydrogen supply.Therefore hydrogen supply in situ is a kind of more economical
The hydrogen supply mode of safety.And hydrolyzable metal reaction is a kind of production hydrogen mode with bright prospects, the activity gold that can be reacted with water
Category has Be, Al, Zn, Mg, Ca, Li, Na, K etc., and aluminium is that the metals resources that reserves are most on the earth, theoretical hydrogen amount are big
(1244mL/g), and the concertedness of the hydrolysis of aluminium and bio oil modifying process is stronger.Therefore can be applied to as hydrogen source
The hydrogen supply modifying process in situ of bio oil.
Water is mutually as the liquefied by-product of biomass by hydro-thermal, containing more organic matter, including small molecular organic acid, small
Molecule alcohol and ketone etc., water and small molecular organic acid in water phase can be reacted with active metal generates hydrogen.Using water phase and
Metal reactive aluminum, you can highly effective hydrogen yield is modified for bio oil, and realizes the recycling of water phase.
The content of the invention
It is an object of the invention to be directed to hydrothermal liquefaction process to generate substantial amounts of industrial wastewater and existing bio oil hydrogenation
The external dangerous high, present situation of high cost of hydrogen supply in deoxidation modifying process provides a kind of new biomass by hydro-thermal liquefaction biology
Oily method of modifying.
This method is achieved through the following technical solutions：A kind of method that biomass by hydro-thermal liquefaction bio oil is modified, feature
It is, includes the following steps：
(1) by rice straw and deionized water with mass ratio 1:10 ratio is put into high temperature and pressure pilot scale reaction kettle,
Reaction temperature is 320 DEG C, obtains hydrothermal liquefaction bio oil and water phase under conditions of residence time 60min；In biomass water hydrothermal solution
During change, the main function of water is：Raw material dispersion；Inhibit the polycondensation reaction again of intermediate product；Hydrogen source is provided as hydrogen supply agent.
The yield of bio oil can be improved by suitably improving the ratio of rice straw/deionized water, but when ratio is more than 1/10, biology
The dissolution degree of matter in deionized water declines, and downward trend is presented in biological oily yield, and level of residue increases.
(2) between the hydrothermal liquefaction bio oil and water obtained aluminium powder, catalyst, step (1) is mutually put into certain proportion
In formula of having a rest high-temperature high-pressure reaction kettle, reaction kettle is sealed, afterwards with the air in inert gas replacement kettle；
(3) open power supply and intermittent high-temperature high-pressure reaction kettle is warming up to reaction temperature, and maintain certain reaction time；
(4) after reaction, lower chuck is unloaded, is cooled to room temperature intermittent high-temperature high-pressure reaction kettle by electric fan, it
After open air bleeding valve, with airbag collect gas；
(5) intermittent high-temperature high-pressure reaction kettle is opened, water-phase product and part residue is poured out, is respectively washed with organic solvent
Reaction kettle and kettle gut line, obtain the mixture of liquid phase and residue；
(6) solidliquid mixture that step (5) obtains is cleaned and depressurized to filter by acetone and obtain solid and product liquid,
Product liquid is put into removal absolute ethyl alcohol and acetone in rotary evaporator and obtains oil water mixture, solid product is through freeze-day with constant temperature
It is residue afterwards；
(7) oil water mixture that step (6) obtains is through dichloromethane extract and separate, respectively obtain the solvable phase of dichloromethane and
Water phase；The solvable phase of dichloromethane is removed into dichloromethane in constant temperature rotary evaporator, you can obtain modification biological oil.
Catalyst in the step (2) is dispersed catalyst n iS-MoS；The inert gas is high pure nitrogen.
Power supply is opened in the step (3), intermittent high-temperature high-pressure reaction kettle is warming up to 310~370 DEG C, keep reaction
Time is 60min, 5~30MPa of total pressure.
Organic solvent described in step (5) is absolute ethyl alcohol and the mixture of acetone.
The temperature of rotary evaporator described in step (6) is 85 DEG C, and the temperature of freeze-day with constant temperature is 105 DEG C, drying time
For 12h, the aperture of organic filter membrane is 0.45 μm.
Beneficial effects of the present invention
1. the present invention is mainly modified bio oil, its stability and chemical characteristic are improved, makes modified bio oil can
For power-equipment.
2. the present invention realizes the recycling to hydrothermal liquefaction waste water, be conducive to its subsequent processing.
3. decomposing generate hydrogen at high temperature containing more small organic molecule in water phase, needed so that bio oil is hydrogenated with
It will.
It is workable, security is higher 4. the present invention is using aluminium and aqueous phase reactions original position hydrogen supply, avoid direct outside
The problems such as hydrogen that hydrogen supply faces is prepared, stored, transport and hydroconversion condition are harsh.
It is beneficial to perfect and supplement to the technology 5. the present invention is the innovation to bio oil hydrogenation modification technology；
6. hydrolysate (boehmite) of the metallic aluminium under bio oil modified condition can be used as high-temperature-resistant thermal-insulation material, energy saving
Environmental protection.
Description of the drawings
The present invention is further illustrated below in conjunction with the accompanying drawings.
Fig. 1 is the reacting flow chart of the method for the invention；
Specific embodiment
Carry out detailed description of the present invention specific embodiment below with reference to the accompanying drawings.
Embodiment 1：
With rice straw, obtained substantial amounts of hydrothermal liquefaction bio oil is spare in high temperature and pressure pilot scale reaction kettle；Hydrothermal liquefaction
The oxygen content of bio oil is 25.62%, calorific value 29.51MJ/kg.
By 4g aluminium powders, 10g hydrothermal liquefactions bio oil, 100g water phase and 0.3wt%NiS-MoS catalyst (the total matter of reactant
Amount) it is put into the intermittent high-temperature high-pressure reaction kettles of 500mL, reaction kettle is sealed, afterwards with the air in high pure nitrogen displacement kettle；
It opens power supply and reaction kettle is warming up to 310 DEG C, reaction time 60min.After reaction, lower chuck is unloaded, it will by electric fan
Reaction kettle is cooled to 30 DEG C or so, opens air bleeding valve afterwards, and gas is collected with airbag；Open reaction kettle, pour out water-phase product and
Part residue is respectively washed reaction kettle and kettle gut line with absolute ethyl alcohol and acetone mixed solvent, obtains total solidliquid mixture；
Said mixture is filtered through decompression, organic filter sizes are 0.45 μm, obtain solid and product liquid, product liquid is put into
Absolute ethyl alcohol is removed in 85 DEG C of constant temperature rotary evaporators and acetone obtains oil water mixture, and solid product is through 105 DEG C of freeze-day with constant temperature
It is residue after 12h.Oil water mixture obtained above through dichloromethane extract and separate, respectively obtain the solvable phase of dichloromethane and
Water phase；The solvable phase of dichloromethane is removed into dichloromethane in 45 DEG C of constant temperature rotary evaporators, you can obtain modification biological oil.This
The rate of oxygen that experiment obtains modification biological oil is 19.44%, calorific value 31.58MJ/kg.
Embodiment 2：
By 4g aluminium powders, 10g hydrothermal liquefactions bio oil, 100g water phase and 0.3wt%NiS-MoS catalyst (the total matter of reactant
Amount) it is put into the intermittent high-temperature high-pressure reaction kettles of 500mL, reaction kettle is sealed, afterwards with the air in high pure nitrogen displacement kettle；
It opens power supply and reaction kettle is warming up to 340 DEG C, reaction time 60min.After reaction, lower chuck is unloaded, it will by electric fan
Reaction kettle is cooled to 30 DEG C or so, opens air bleeding valve afterwards, and gas is collected with airbag；Open reaction kettle, pour out water-phase product and
Part residue is respectively washed reaction kettle and kettle gut line with absolute ethyl alcohol and acetone mixed solvent, obtains total solidliquid mixture；
Said mixture is filtered through decompression, organic filter sizes are 0.45 μm, obtain solid and product liquid, product liquid is put into
Absolute ethyl alcohol is removed in 85 DEG C of constant temperature rotary evaporators and acetone obtains oil water mixture, and solid product is through 105 DEG C of freeze-day with constant temperature
It is residue after 12h.Oil water mixture obtained above through dichloromethane extract and separate, respectively obtain the solvable phase of dichloromethane and
Water phase；The solvable phase of dichloromethane is removed into dichloromethane in 45 DEG C of constant temperature rotary evaporators, you can obtain modification biological oil.This
The rate of oxygen that experiment obtains modification biological oil is 18.05%, calorific value 32.4MJ/kg.
Embodiment 3：
By 4g aluminium powders, 10g hydrothermal liquefactions bio oil, 100g water phase and 0.3wt%NiS-MoS catalyst (the total matter of reactant
Amount) it is put into the intermittent high-temperature high-pressure reaction kettles of 500mL, reaction kettle is sealed, afterwards with the air in high pure nitrogen displacement kettle；
It opens power supply and reaction kettle is warming up to 370 DEG C, reaction time 60min.After reaction, lower chuck is unloaded, it will by electric fan
Reaction kettle is cooled to 30 DEG C or so, opens air bleeding valve afterwards, and gas is collected with airbag；Open reaction kettle, pour out water-phase product and
Part residue is respectively washed reaction kettle and kettle gut line with absolute ethyl alcohol and acetone mixed solvent, obtains total solidliquid mixture；
Said mixture is filtered through decompression, organic filter sizes are 0.45 μm, obtain solid and product liquid, product liquid is put into
Absolute ethyl alcohol is removed in 85 DEG C of constant temperature rotary evaporators and acetone obtains oil water mixture, and solid product is through 105 DEG C of freeze-day with constant temperature
It is residue after 12h.Oil water mixture obtained above through dichloromethane extract and separate, respectively obtain the solvable phase of dichloromethane and
Water phase；The solvable phase of dichloromethane is removed into dichloromethane in 45 DEG C of constant temperature rotary evaporators, you can obtain modification biological oil.This
The rate of oxygen that experiment obtains modification biological oil is 16.23%, calorific value 33.36MJ/kg.
The key that bio oil is modified is the oxygen consumed with minimum hydrogen in removing bio oil, while retains carbon therein, medium temperature
Degree is to influence the key factor that bio oil is modified.It is oily using the method for the invention modification biological from embodiment, with
The rise of modification temperature, bio oil oxygen content are substantially reduced, and calorific value is improved.
The invention belongs to environmental protections and field of new energy technologies, and in particular to a kind of method that bio oil is modified；The party
Method, for bio oil modifying process, provides one using metallic aluminium and the aqueous portion of biomass water hydrothermal solution bio oil reaction production hydrogen
The new bio oil method of modifying of kind, that is, improve the quality of bio oil, and realizes the recycling profit of bio oil aqueous portion
With.
Although having been combined the preferred embodiment of the present invention above shows the present invention, those skilled in the art will
It will be appreciated that without departing from the spirit and scope of the present invention, the present invention can be carry out various modifications, replaced and changed
Become.Therefore, the present invention should not be limited by above-described embodiment, and should be limited by appended claims and its equivalent.
Claims (5)
1. a kind of method that biomass by hydro-thermal liquefaction bio oil is modified, which is characterized in that include the following steps：
(1) by rice straw and deionized water with mass ratio 1:10 ratio is put into high temperature and pressure pilot scale reaction kettle, is being reacted
Temperature is 320 DEG C, obtains hydrothermal liquefaction bio oil and water phase under conditions of residence time 60min；
(2) the hydrothermal liquefaction bio oil and water obtained aluminium powder, catalyst, step (1) is mutually put into intermittent in certain proportion
In high-temperature high-pressure reaction kettle, reaction kettle is sealed, afterwards with the air in inert gas replacement kettle；
(3) open power supply and intermittent high-temperature high-pressure reaction kettle is warming up to reaction temperature, and maintain certain reaction time；
(4) after reaction, lower chuck is unloaded, intermittent high-temperature high-pressure reaction kettle is cooled to room temperature by electric fan, is beaten afterwards
Begin to rehearse air valve, and gas is collected with airbag；
(5) intermittent high-temperature high-pressure reaction kettle is opened, water-phase product and part residue is poured out, reaction is respectively washed with organic solvent
Kettle and kettle gut line, obtain the mixture of liquid phase and residue；
(6) solidliquid mixture that step (5) obtains is cleaned and depressurized to filter by acetone and obtain solid and product liquid, by liquid
Body product is put into removal absolute ethyl alcohol and acetone in rotary evaporator and obtains oil water mixture, and solid product is after freeze-day with constant temperature
For residue；
(7) oil water mixture that step (6) obtains respectively obtains the solvable phase of dichloromethane and water through dichloromethane extract and separate
Phase；The solvable phase of dichloromethane is removed into dichloromethane in constant temperature rotary evaporator, you can obtain modification biological oil.
2. the method that a kind of biomass by hydro-thermal liquefaction bio oil according to claim 1 is modified, which is characterized in that the step
Suddenly the catalyst in (2) is dispersed catalyst n iS-MoS；The inert gas is high pure nitrogen.
3. the method that a kind of biomass by hydro-thermal liquefaction bio oil according to claim 1 is modified, which is characterized in that the step
Suddenly power supply is opened in (3), intermittent high-temperature high-pressure reaction kettle is warming up to 310~370 DEG C, the holding reaction time is 60min, always
5~30MPa of pressure.
4. the method that a kind of biomass by hydro-thermal liquefaction bio oil according to claim 1 is modified, which is characterized in that step
(5) organic solvent described in is absolute ethyl alcohol and the mixture of acetone.
5. the method that a kind of biomass by hydro-thermal liquefaction bio oil according to claim 1 is modified, which is characterized in that step
(6) temperature of the rotary evaporator described in is 85 DEG C, and the temperature of freeze-day with constant temperature is 105 DEG C, and drying time 12h has machine filter
The aperture of film is 0.45 μm.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110713853A (en) * | 2019-10-24 | 2020-01-21 | 江苏大学 | Method for utilizing oily wastewater by combining electro-catalysis with algae |
| CN111808628A (en) * | 2020-07-23 | 2020-10-23 | 沈阳航空航天大学 | Method for improving effective hydrogen-carbon ratio of bio-oil based on aqueous phase reforming |
| CN113308265A (en) * | 2020-02-26 | 2021-08-27 | 中国石油化工股份有限公司 | Method for preparing biological crude oil by catalytic conversion method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101885986A (en) * | 2010-07-16 | 2010-11-17 | 华东理工大学 | Method for refining biological oil |
| CN106281394A (en) * | 2016-08-04 | 2017-01-04 | 江苏大学 | A kind of method that continuous way hydrothermal liquefaction prepares bio oil |
| CN107163973A (en) * | 2017-05-18 | 2017-09-15 | 沈阳航空航天大学 | A kind of biomass hydrogen supply liquefaction method for producing oil in situ |
-
2017
- 2017-12-20 CN CN201711381188.9A patent/CN108085039A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101885986A (en) * | 2010-07-16 | 2010-11-17 | 华东理工大学 | Method for refining biological oil |
| CN106281394A (en) * | 2016-08-04 | 2017-01-04 | 江苏大学 | A kind of method that continuous way hydrothermal liquefaction prepares bio oil |
| CN107163973A (en) * | 2017-05-18 | 2017-09-15 | 沈阳航空航天大学 | A kind of biomass hydrogen supply liquefaction method for producing oil in situ |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110713853A (en) * | 2019-10-24 | 2020-01-21 | 江苏大学 | Method for utilizing oily wastewater by combining electro-catalysis with algae |
| CN113308265A (en) * | 2020-02-26 | 2021-08-27 | 中国石油化工股份有限公司 | Method for preparing biological crude oil by catalytic conversion method |
| CN111808628A (en) * | 2020-07-23 | 2020-10-23 | 沈阳航空航天大学 | Method for improving effective hydrogen-carbon ratio of bio-oil based on aqueous phase reforming |
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Application publication date: 20180529 |