CN106190282A - A kind of biomass pyrolysis oil processing method - Google Patents
A kind of biomass pyrolysis oil processing method Download PDFInfo
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- CN106190282A CN106190282A CN201510224150.5A CN201510224150A CN106190282A CN 106190282 A CN106190282 A CN 106190282A CN 201510224150 A CN201510224150 A CN 201510224150A CN 106190282 A CN106190282 A CN 106190282A
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Abstract
A kind of biomass pyrolysis oil processing method, comprise the following steps: biomass pyrolysis oil is mixed by (1) with decompressed wax oil, obtain a kind of mixed material, in described mixed material, biomass pyrolysis oil and decompressed wax oil mass mixing ratio are 1: 10-10: 1, and described mixing makes described mixed material be homogeneous phase；(2) in presence of hydrogen, the material that step (1) is obtained and Hydrobon catalyst haptoreaction, described haptoreaction condition includes: pressure is 2-10 MPa, temperature is 250-380 DEG C, hydrogen-oil ratio is 100-400, oil ratio is 0.5-2, and product obtains hydrofined oil through oil-water separation.Compared with prior art, the method that the present invention provides can effectively suppress biomass pyrolysis oil coking in hydrogenation reaction.
Description
Technical field
The present invention relates to a kind of biomass pyrolysis oil processing method, particularly relate to a kind of with biomass pyrolytic
Oil is raw material production gasoline, the method for diesel oil distillate oil.
Background technology
Recently as the fast development of industry, growing to the demand of the energy.Meanwhile, along with environment
That pollutes is day by day serious, and the renewable alternative energy source of exploitation cleaning has become the task of top priority.Biomass pyrolytic
Oil, becomes the focus of people's research owing to having pollutant emission is few, cycle period is short feature.
Biomass pyrolysis oil be by biomass (rice husk, straw etc.) isolation air under conditions of, carry out
Fast pyrogenation reacts the product liquid (additionally, also including water and gaseous product etc.) obtained.
Oxygenates level in biomass pyrolysis oil is high, calorific value is low, pH value is low, corrosivity is strong, admittedly
Body impurity content is high so that it is difficult to use directly as fuel.Owing to biomass pyrolysis oil is thermodynamics
Uneven product, is susceptible to the chemical reactions such as polymerization, oxidation in heating process, it is impossible to use routine
Distillation mode is dehydrated.Use breaking emulsion and dewatering, electric dehydration and aqueous phase to increase the weight of the measures such as dehydration and also be difficult to dehydration.
Use and include that biomass pyrolysis oil can be refined by the method for hydrotreating, to promote biomass pyrolytic
The quality of oil.
201010228232 process for purification disclosing a kind of bio oil.The method first by bio oil in 140
DEG C of-300 DEG C catalytic hydrogenations 10 minutes to 120 minutes, obtain mixture, and separating obtained mixture obtains oil phase and produces
Thing；Again oil-phase product is mixed with paraffin oil, after 200 DEG C of-550 DEG C of catalytic cracking, obtain refined biological
Oil；Catalytic hydrogenation wherein uses Pd/ γ-Al2O3Or Pd/C.
201010236331 preparation methoies disclosing a kind of bio oil and biodiesel fuel combination.The party
40 parts of bio oil are joined in 60 parts of biodiesel by method with even speed, add 4 parts of emulsifyings and help
Agent, stirs the mixture for 20 minutes, then heats 15 minutes in the oil bath pan of 30 DEG C, simultaneously with often
The speed stirring of minutes 1200 turns, then stands and within 8 hours, obtains upper strata bio oil and biodiesel mixing combustion
Material, lower floor is the biological oil reservoir rich in pyrolysis lignin.
201110369628 to disclose a kind of bio-oil heavy constituent mixing with oil secondary operations mink cell focus
Method.The method include biomass heavy oil physical-chemical pretreatment, heavy oil emulsifying process, miscible, urge
Change is hydrocracked, product separation analysis process.
According to prior art, biomass pyrolysis oil easily occurs coking reaction to lose in hydrogenation reaction.
Summary of the invention
The technical problem to be solved in the present invention is, for biomass pyrolysis oil, coking easily occurs in hydrogenation reaction
The problem reacted and lose, it is provided that a kind of coking reaction has obtained the biomass pyrolysis oil processing side of suppression
Method.
The present invention relates to a kind of biomass pyrolysis oil processing method, comprise the following steps:
(1) biomass pyrolysis oil is mixed with decompressed wax oil, obtain a kind of mixed material, described mixing
In material, biomass pyrolysis oil and decompressed wax oil mass mixing ratio are 1: 10-10: 1, and described mixing makes
Described mixed material is homogeneous phase；
(2) in presence of hydrogen, the material that step (1) obtains is contacted instead with Hydrobon catalyst
Should, described haptoreaction condition includes: pressure is 2-10 MPa, and temperature is 250-380 DEG C, hydrogen oil
Ratio is 100-400, and oil ratio is 0.5-2, and product obtains hydrofined oil through oil-water separation；
Preferably, step (1) described biomass pyrolysis oil is 1: 5-with the mixing quality ratio of decompressed wax oil
5∶1。
Haptoreaction condition described in step (2) includes: pressure is 5-7 MPa, and temperature is 300-370
DEG C, hydrogen-oil ratio is 200-400, and oil ratio is 1.0-1.5.
The method provided according to the present invention, in the presence of being additionally included in hydrogen after described step (2),
The hydrofined oil that step (2) is obtained and the catalytic step of hydrocracking catalyst, described with add
Hydrogen catalyst for cracking haptoreaction condition includes: pressure is 4-8 MPa, and temperature is 320-380 DEG C, hydrogen
Oil ratio is 100-800, and oil ratio is 0.5-2.This product is isolated to gasoline and diesel oil distillate
Oil.
Preferably, include with described hydrocracking catalyst haptoreaction condition: pressure is 4-6 MPa,
Temperature is 340-370 DEG C, and hydrogen-oil ratio is 200-500, and oil ratio is 1.0-1.5.
In the present invention, described biomass pyrolysis oil raw material can be to use arbitrary prior art to obtain not
The biomass (such as rice husk, straw etc. or lignin, cellulose etc.) processed through any purification step exist
The product liquid that under conditions of isolation air, pyrolytic reaction obtains, it is also possible to be that described product liquid is used
Arbitrarily prior art carries out refining (as through including the step in filtration, esterification, emulsifying etc. or the essence of a few step
System processes), but the biomass including that oxygen content, alkene equal size still can not meet use requirement therein
Pyrolysis oil.
Described decompressed wax oil preferably refinery's vacuum distillation apparatus survey line product subtracts one, subtract two, the line that subtracts three
One or more mixture, preferably subtract one and or second line of distillation product.
In the present invention, be enough to make described biomass pyrolysis oil and decompressed wax oil mixture be equal in described mixing
On the premise of one phase, the method realizing this mixing is not limited by the present invention, such as, can use stirring
Method mix.
Inventor studies discovery, when described biomass pyrolysis oil and decompressed wax oil are mixed into homogeneous phase, uses
This mixture is charging when carrying out hydrofinishing, and the coking of biomass pyrolysis oil is substantially inhibited.
In the present invention, product includes gaseous product and product liquid, product liquid include water and
Oil, therefore, the separation described in step (2) includes gas-liquid separation and oil-water separation, and the gas after separation is
The oxygenatedchemicals of fraction low molecule quality and the gas group that can use as dry gas, liquefied gas
Point, oil water mixture separates water and oil-phase product after entering separator.
The gas that the separation of described step (3) generates after including reaction separates and separates with oil-phase product, separates
After gas can use as dry gas, liquefied gas, gained oil-phase product is separated respectively obtains vapour bavin
Oil distillate.
On the premise of being enough to realize various described separation, separation method is not limited by the present invention.As adopted
The method separating (high score) and/or low-pressure gas-liquid separation (low point) with high-pressure gas-liquid carries out gas-liquid separation,
Use the Liquid liquid Separation that the method for distillation is carried out, the oil-water separation using sedimentation or adsorption method to carry out, adopt
The solid-liquor separation etc. carried out by the method filtered.Described distillation generally can include one or more flash distillation, often
Pressure distillation and the operating unit of decompression distillation, to complete desired separation.
In the present invention, the purpose of described hydrofining reaction is to make biomass thermal by hydrofining reaction
Solve oxygenatedchemicals in oil and carry out hydrogenation deoxidation reaction, generate water after oxygenatedchemicals hydrogenation deoxidation and make biology
The polarity of matter pyrolysis oil reduces, and water is easier to remove from oil phase；Simultaneously containing few in biomass pyrolysis oil
They can be removed, for further by amount S, N, metal impurities element by hydrofining reaction
Processing provides quality raw materials.
Described Hydrobon catalyst contains carrier and load hydrogenation active metals component on this carrier,
Described hydrogenation active metals component is selected from metal component and at least one VIII of at least one vib
The metal component of race, on the basis of catalyst, in described catalyst, the mass fraction of carrier is 65-95%,
The mass fraction of the metal component of the vib counted with oxide as 1-40%, in terms of oxide
The mass fraction of the metal component of VIII is 0.1-10%.On the basis of catalyst, the most described catalysis
In agent, the mass fraction of carrier is 78-94%, and the quality of the metal component of the vib in terms of oxide is divided
Number is for 5-25%, and the mass fraction of the metal component of the group VIII counted with oxide is as 0.5-7%.
In the present invention, aforesaid Hydrobon catalyst can be their hydrogenated refining reaction device fortune
The carbon mass fraction of the removal useless agent less than 5.0% after turning.When described Hydrobon catalyst is dead catalyst
Time, can reach the purpose reducing production cost.
In the present invention, described hydrocracking reaction is will be by biomass pyrolysis oil by hydrocracking reaction
The hydrocarbon ils component obtained is converted into corresponding petrol and diesel oil fraction, it is achieved biomass pyrolysis oil is converted into automobile-used combustion
The purpose of material.
Described hydrocracking catalyst contains carrier and load hydrogenation active metals component on this carrier,
Described hydrogenation active metals component is selected from metal component and at least one VIII of at least one vib
The metal component of race, on the basis of described catalyst, in described catalyst, the mass fraction of carrier is 65-
95%, the mass fraction of the metal component of the vib counted with oxide is as 1-40%, in terms of oxide
The mass fraction of the metal component of group VIII is 0.1-10%.On the basis of described catalyst, preferably institute
Stating the mass fraction of carrier in catalyst is 78-94%, the metal component of the vib in terms of oxide
Mass fraction is 5-25%, and the mass fraction of the metal component of the group VIII counted with oxide is as 0.5-
7%.
Heretofore described catalyst carrier preferably comprises aluminium oxide and Y type molecular sieve, with vehicle weight is
Benchmark, described Y type molecular sieve is 5%-35% with the mass ratio of aluminium oxide.On the basis of vehicle weight, enter
The one preferred described Y type molecular sieve of step is 15%-25% with the mass ratio of aluminium oxide.
In the present invention, described Hydrobon catalyst give up agent can be arbitrary prior art provide hydrogenation
Dead catalyst after refining reaction, biomass pyrolysis oil and decompressed wax oil fuel combination use useless agent carrying out
Hydrofining reaction procatalyst need not presulfurization.Common hydrogenation catalyst contains carrier and is supported on
Hydrogenation active metals component on this carrier, described hydrogenation active metals component is selected from least one VIB
The metal component of race and the catalyst of the metal component of at least one group VIII.Wherein, described carrier can
To be selected from arbitrarily can be as adding the heat-resistant inorganic oxide that hydrogen species catalyst carrier uses, such as, can
With one or more in aluminium oxide, silica-alumina, silicon oxide, titanium oxide, zirconium oxide,
It preferably is selected from one or more in aluminium oxide, silica-alumina, silicon oxide, more preferably aoxidizes
Aluminum, silica-alumina and their mixture.They can be commercially available commodity can also be use
Prepared by arbitrary existing method.
Described carrier can have variously-shaped according to concrete application scenario.Such as, described carrier can
Think spherical, bar shaped, annular, cloverleaf pattern, honeycombed and butterfly.
Described hydrogenation active metals component is selected from the non-noble metal components and at least of at least one group VIII
Kind of vib metals component, the metal component of preferred group VIII is nickel and/or cobalt, preferred the
The metal component of group vib is molybdenum and/or tungsten.
In the present invention, described hydrogenation catalyst can also provide catalyst containing any present invention that do not affects
Performance maybe can improve the material of catalyst performance that the present invention provides.As phosphorus, boron or fluorine etc. can be contained
One or both in component, count and on the basis of catalyst by element, and the content of above-mentioned auxiliary agent is less than
10 weight %, preferably 0.5-5 weight %.
In the present invention, described hydrocracking catalyst can be being hydrocracked of arbitrary prior art offer
Catalyst, such as, common hydrocracking catalyst contains carrier and load hydrogenation on this carrier is lived
Property metal component, described hydrogenation active metals component is selected from the metal component and extremely of at least one vib
The catalyst of the metal component of few a kind of group VIII, described carrier comprises aluminium oxide and Y type molecular sieve.
On the premise of being enough to realize described hydrofining reaction and hydrocracking reaction, the present invention is to reality
The device of existing described reaction is not particularly limited, such as, can carry out in fixed bed reactors, Ke Yi
Tank reactor is carried out.
The present invention carries out follow-up hydrogenation reaction after being mixed with decompressed wax oil by biomass pyrolysis oil, solves life
The problems such as material pyrolysis oil work in-process less stable, easy coking, can enter one by biomass pyrolysis oil
Step is converted into vehicle fuel, it is provided that a kind of biomass pyrolysis oil is converted into the processing method of purpose product.
Detailed description of the invention
The method providing the present invention is further described by the following examples, but the most therefore and
Limit the present invention.
Embodiment 1
Take biomass pyrolysis oil 50 grams (character of biomass pyrolysis oil is shown in Table 1), 200 grams of decompression waxes
Oil (character of decompressed wax oil is listed in table 2), uses the blender of 500 rpms of high speed rotating to enter
Row mixing 5 minutes, obtains mixing the mixed biologic oil of homogeneous phase.Hydrogenation autoclave device adds
Enter 10 grams of useless agent (the Industry Waste agent of RHC-130, carbon content is 4.0%) and aforesaid mixed biologic
Oil, introduces hydrogen and to be heated to initial pressure is 5.0MPa after sealing, reaction temperature is 280
DEG C, the response time is 1 hour, and at the end of reaction, pressure rises to 10.4MPa.Reaction will after terminating
Liquid product is positioned in separatory funnel 30 minutes (water is in lower floor) of standing, obtains through oil-water separation
23.1 grams of water, filter oil with catalyst mixture, obtain oil 203.5 grams, catalyst 14.5 grams.
Comparative example 1
Biomass pyrolysis oil described in Example 1 200 grams, useless agent 10 grams, according to embodiment 1
Identical method carries out hydrogenation reaction to biomass pyrolysis oil, and (in course of reaction, pressure rises to
12.2MPa).After reaction terminates, the upper strata of product is water, and lower floor is the oil of thickness and catalyst mixes
Compound, is isolated to 125 grams of water, the oil of thickness and catalyst mixture 59.2 grams.
Embodiment 2
The present embodiment in addition to initial pressure is 6.0MPa, the raw oil that used, catalyst and other
Operating condition is same as in Example 1, and at the end of reaction, pressure rises to 11.3MPa.Through oil-water separation
Obtain 23.9 grams of water, oil is filtered with catalyst mixture, obtain oil 211.9 grams, catalyst 17.2
Gram.
Embodiment 3
The present embodiment in addition to reaction temperature is 320 DEG C, the catalyst used and other operating conditions with
Same as in Example 1, at the end of reaction, pressure rises to 13.1MPa.Water is obtained through oil-water separation
28.8 grams, oil is filtered with catalyst mixture, obtain oil 195.0 grams, catalyst 15.2 grams.
Embodiment 4
The present embodiment primary response pressure is 7.0MPa, and reaction temperature is 320 DEG C, raw oil, urges
Agent and other operating conditions are same as in Example 1, and at the end of reaction, pressure rises to 15.3MPa.
Through oil-water separation, obtain 29.2 grams of water, oil is filtered with catalyst mixture, obtain oil 198.1
Gram, catalyst 13.1 grams.
Embodiment 5
125 grams and 125 grams decompressions of biomass pyrolysis oil described in Example 1 (with embodiment 1)
Wax oil (with embodiment 1), uses the blender of 500 rpms of high speed rotating to carry out mixing 5 points
Clock, obtains mixing the mixed biologic oil of homogeneous phase.10 grams of useless agent are added in hydrogenation autoclave device
(with embodiment 1) and aforesaid mixed biologic oil, introduces hydrogen and is heated to initial after sealing
Pressure is 5.0MPa, and reaction temperature is 320 DEG C, and the response time is 1 hour, presses at the end of reaction
Power rises to 13.6MPa.Liquid product is carried out oil according to embodiment 1 same procedure after terminating by reaction
Water separates, and is isolated to 67.2 grams of water, is filtered with catalyst mixture by oil, obtains oil 154.3
Gram, catalyst 19.2 grams.
Embodiment 6
Biomass pyrolysis oil described in Example 1 (with embodiment 1) 200 grams and 50 grams decompression wax
Oil (with embodiment 1), uses the blender of 500 rpms of high speed rotating to carry out mixing 5 points
Clock, obtains mixing the mixed biologic oil of homogeneous phase.10 grams of useless agent are added in hydrogenation autoclave device
(with embodiment 1) and aforesaid mixed biologic oil, introduces hydrogen and is heated to initial after sealing
Pressure is 5.0MPa, and reaction temperature is 320 DEG C, and the response time is 1 hour, presses at the end of reaction
Power rises to 14.6MPa.Liquid product is carried out oil according to embodiment 1 same procedure after terminating by reaction
Water separates, and is isolated to 114.5 grams of water, is filtered with catalyst mixture by oil, obtains oil
100.3 grams, catalyst 23.6 grams.
Before table 3 lists biomass pyrolysis oil raw material reaction and embodiment 1 and comparative example 1 reaction after
Through the different fractions section proportion of simulation distillation gained, the biomass pyrolysis oil raw material overwhelming majority is concentrated
In petrol and diesel oil fraction section, can be seen that from comparative example 1, the fraction of more than 500 DEG C is up to more than 64%,
Show that biomass pyrolysis oil is susceptible to condensation reaction when direct hydrogenation reacts, cause the degree of polymerization to increase
Adding, oil product converts to heavy direction.In embodiment 1, mix with decompressed wax oil with biomass pyrolysis oil
Thing is raw material, and biomass pyrolysis oil is converted mainly into gasoline, diesel oil, shows the contracting of biomass pyrolysis oil
Conjunction reaction is significantly suppressed.It addition, the oxygenatedchemicals warp of low-molecular-weight in biomass pyrolysis oil
It is converted into gaseous product after the reaction such as hydrogenation deoxidation, hydrotreating.
Table 1 biomass starting material pyrolysis oil properties
Table 2 decompressed wax oil fundamental property
Table 3 biomass pyrolysis oil hydrotreatment products oil phase is fractional distribution
Embodiment 7
The oil-phase product of embodiment 1-6 gained is collected, mixes, with this mixture for raw material 30
Hydrocracking reaction is carried out on milliliter hydrogenation fixed bed device.Use 18 gram 16～the RHC-3 of 20 mesh
Hydrocracking catalyst, in test use Carbon bisulfide mass fraction be 4% kerosene make sulfurized oil,
Catalyst vulcanizes 6 hours at 360 DEG C.Hydrocracking reaction condition is: reaction pressure 6.4MPa,
Temperature 370 DEG C, air speed 1.0-1, light oil volume ratio 300, react 2 hours, collect product liquid and enter
Row distillation cutting, obtains gasoline and diesel component, and product fundamental property such as table 4, table 5, from table 4
Find out that diesel component is a kind of quality product that can meet state's IV discharge standard.
Comparative example 2
With decompressed wax oil (with embodiment 1) as raw material, use catalyst same as in Example 7, reaction
Device and operating condition carry out hydrocracking reaction.Collect product liquid and carry out distillation cutting, obtain gasoline
And diesel component, diesel product fundamental property such as table 5.
The result be given by table 5 is it can be seen that use the method that the present invention provides, in biomass pyrolysis oil
Oxygenatedchemicals primarily enters diesel oil distillate after deoxidation, hydrocracking reaction.
Table 4 miscella hydrocracking reaction product gasoline diesel oil fundamental property
Table 5 hydrocracking reaction product diesel hydro carbons forms
Claims (12)
1. a biomass pyrolysis oil processing method, comprises the following steps:
(1) biomass pyrolysis oil is mixed with decompressed wax oil, obtain a kind of mixed material, described mixing
In material, biomass pyrolysis oil and decompressed wax oil mass mixing ratio are 1: 10-10: 1, and described mixing makes
Described mixed material is homogeneous phase；
(2) in presence of hydrogen, the material that step (1) obtains is contacted instead with Hydrobon catalyst
Should, described haptoreaction condition includes: pressure is 2-10 MPa, and temperature is 250-380 DEG C, hydrogen oil
Ratio is 100-400, and oil ratio is 0.5-2, and product obtains hydrofined oil through oil-water separation.
Method the most according to claim 1, it is characterised in that biomass thermal in described mixed material
Solving oily and decompressed wax oil mixing quality ratio is 1∶5-5∶1。
Method the most according to claim 1, it is characterised in that the described contact of step (2) is anti-
Answering condition to include: pressure is 5-7 MPa, temperature is 300-370 DEG C, and hydrogen-oil ratio is 200-400, agent oil
Ratio is 1-1.5.
Method the most according to claim 1, it is characterised in that described Hydrobon catalyst contains
Carrier and load hydrogenation active metals component on this carrier, described hydrogenation active metals component is selected from extremely
The metal component of few a kind of vib and the metal component of at least one group VIII, with catalyst as base
Standard, in described catalyst, the mass fraction of carrier is 65-95%, the metal of the vib in terms of oxide
The mass fraction of component is 1-40%, and the mass fraction of the metal component of the group VIII in terms of oxide is
0.1-10%.
Method the most according to claim 4, it is characterised in that on the basis of catalyst, described in urge
In agent, the mass fraction of carrier is 78-94%, the quality of the metal component of the vib in terms of oxide
Mark is 5-25%, and the mass fraction of the metal component of the group VIII counted with oxide is as 0.5-7%.
6. according to the method described in any one of claim 1,4 or 5, it is characterised in that described hydrogenation essence
Catalyst processed is the useless agent that carbon mass fraction is less than the Hydrobon catalyst of 5%.
Method the most according to claim 1, it is characterised in that include after described step (2)
One in presence of hydrogen, is contacted instead with hydrocracking catalyst by the hydrofined oil that step (2) obtains
The step answered, described includes with hydrocracking catalyst haptoreaction condition: pressure is 4-8 MPa, temperature
Degree is for 320-380 DEG C, and hydrogen-oil ratio is 100-800, and oil ratio is 0.5-2.
Method the most according to claim 7, it is characterised in that described connect with hydrocracking catalyst
Tactile reaction condition includes: pressure is 4-6 MPa, and temperature is 340-370 DEG C, and hydrogen-oil ratio is 200-500,
Oil ratio is 1.0-1.5.
Method the most according to claim 7, it is characterised in that described hydrocracking catalyst contains
Carrier and load hydrogenation active metals component on this carrier, described hydrogenation active metals component is selected from extremely
The metal component of few a kind of vib and the metal component of at least one group VIII, with described catalyst
On the basis of, in described catalyst, the mass fraction of carrier is 65-95%, the vib in terms of oxide
The mass fraction of metal component is 1-40%, and the quality of the metal component of the group VIII in terms of oxide is divided
Number is 0.1-10%.
Method the most according to claim 9, it is characterised in that on the basis of described catalyst, institute
Stating the mass fraction of carrier in catalyst is 78-94%, the metal component of the vib in terms of oxide
Mass fraction is 5-25%, and the mass fraction of the metal component of the group VIII counted with oxide is as 0.5-
7%.
11. according to the method described in claim 9 or 10, it is characterised in that described catalyst carrier bag
Salic and Y type molecular sieve, on the basis of vehicle weight, the matter of described Y type molecular sieve and aluminium oxide
Amount ratio is 5%-35%.
12. methods according to claim 11, it is characterised in that on the basis of vehicle weight, institute
The mass ratio stating Y type molecular sieve and aluminium oxide is 15%-25%.
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| CN109628143A (en) * | 2018-12-20 | 2019-04-16 | 西北大学 | A kind of method that fast pyrogenation bio-oil refines production petrol and diesel oil with straight-run gas oil altogether |
| CN112745875A (en) * | 2019-10-31 | 2021-05-04 | 中国石油化工股份有限公司 | Processing method of biomass pyrolysis oil |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109628143A (en) * | 2018-12-20 | 2019-04-16 | 西北大学 | A kind of method that fast pyrogenation bio-oil refines production petrol and diesel oil with straight-run gas oil altogether |
| CN109628143B (en) * | 2018-12-20 | 2021-03-30 | 西北大学 | Method for producing gasoline and diesel oil by co-refining fast pyrolysis biomass oil and straight-run wax oil |
| CN112745875A (en) * | 2019-10-31 | 2021-05-04 | 中国石油化工股份有限公司 | Processing method of biomass pyrolysis oil |
| CN112745875B (en) * | 2019-10-31 | 2023-05-05 | 中国石油化工股份有限公司 | Processing method of biomass pyrolysis oil |
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Application publication date: 20161207 |