CN101121895A - Biological oil and method for preparing biological oil by using biomass magnetic stabilization fluidized bed reactor and medium-temperature rapid thermal cracking - Google Patents
Biological oil and method for preparing biological oil by using biomass magnetic stabilization fluidized bed reactor and medium-temperature rapid thermal cracking Download PDFInfo
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- CN101121895A CN101121895A CNA2007101473252A CN200710147325A CN101121895A CN 101121895 A CN101121895 A CN 101121895A CN A2007101473252 A CNA2007101473252 A CN A2007101473252A CN 200710147325 A CN200710147325 A CN 200710147325A CN 101121895 A CN101121895 A CN 101121895A
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- 239000002028 Biomass Substances 0.000 title claims abstract description 22
- 230000006641 stabilisation Effects 0.000 title claims abstract description 20
- 238000011105 stabilization Methods 0.000 title claims abstract description 20
- 238000000034 method Methods 0.000 title claims abstract description 17
- 238000004227 thermal cracking Methods 0.000 title abstract 4
- 239000012075 bio-oil Substances 0.000 claims abstract description 38
- 239000003921 oil Substances 0.000 claims abstract description 10
- 239000002994 raw material Substances 0.000 claims abstract description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 8
- 238000004821 distillation Methods 0.000 claims abstract description 5
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 4
- 239000010815 organic waste Substances 0.000 claims abstract description 3
- 239000000463 material Substances 0.000 claims description 30
- 239000007789 gas Substances 0.000 claims description 21
- 239000012530 fluid Substances 0.000 claims description 18
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 17
- 229910001882 dioxygen Inorganic materials 0.000 claims description 17
- 238000000197 pyrolysis Methods 0.000 claims description 15
- 239000003610 charcoal Substances 0.000 claims description 11
- 239000002245 particle Substances 0.000 claims description 11
- 238000005336 cracking Methods 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 238000002203 pretreatment Methods 0.000 claims description 4
- 238000012545 processing Methods 0.000 claims description 4
- 238000007670 refining Methods 0.000 claims description 4
- 206010002660 Anoxia Diseases 0.000 claims description 3
- 241000976983 Anoxia Species 0.000 claims description 3
- 206010021143 Hypoxia Diseases 0.000 claims description 3
- 230000007953 anoxia Effects 0.000 claims description 3
- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- 238000009826 distribution Methods 0.000 claims description 3
- 230000008676 import Effects 0.000 claims description 3
- 238000002360 preparation method Methods 0.000 claims description 3
- 238000003860 storage Methods 0.000 claims description 3
- 229910001122 Mischmetal Inorganic materials 0.000 claims description 2
- WMOHXRDWCVHXGS-UHFFFAOYSA-N [La].[Ce] Chemical compound [La].[Ce] WMOHXRDWCVHXGS-UHFFFAOYSA-N 0.000 claims description 2
- 230000033228 biological regulation Effects 0.000 claims description 2
- 150000001875 compounds Chemical class 0.000 claims description 2
- 229910052742 iron Inorganic materials 0.000 claims description 2
- 239000000843 powder Substances 0.000 claims description 2
- 239000004576 sand Substances 0.000 claims description 2
- 239000002023 wood Substances 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 abstract description 9
- 239000007787 solid Substances 0.000 abstract description 5
- 238000000926 separation method Methods 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract description 3
- 238000009833 condensation Methods 0.000 abstract description 2
- 230000005494 condensation Effects 0.000 abstract description 2
- 238000011161 development Methods 0.000 abstract description 2
- 230000007613 environmental effect Effects 0.000 abstract description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 abstract 1
- 125000002485 formyl group Chemical class [H]C(*)=O 0.000 abstract 1
- 239000010902 straw Substances 0.000 abstract 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 241000209149 Zea Species 0.000 description 2
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 2
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 235000005822 corn Nutrition 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000012159 carrier gas Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 230000009969 flowable effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 230000016507 interphase Effects 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 239000006249 magnetic particle Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910001120 nichrome Inorganic materials 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- -1 rare earth compound Chemical class 0.000 description 1
- 229910052761 rare earth metal Inorganic materials 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
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Abstract
The invention relates to bio-oil and a method for preparing the bio-oil by using the medium-temperature rapid thermal cracking of a biomass magnetic stabilization fluidized bed reactor, wherein the bio-oil is prepared byThe mass percentage of C is more than 71.1 percent, H is more than 7.3 percent, O is more than 16.6 percent, N is less than 0.1 percent, and the oil viscosity is more than 106mPa.s, density more than 1.10, pH value more than 2.5, and water content less than 20%. The method comprises the steps of utilizing biomass (straws, leaves, sawdust and organic wastes) to carry out medium-temperature rapid thermal cracking in a magnetically stabilized fluidized bed reactor, carrying out gas-solid separation and gas condensation on a cyclone separator, and obtaining the bio-oil after simple hydrogenation and distillation treatment of condensate, wherein the yield reaches 75%. The biological oil contains rich chemicals (phenol and aldehyde substances) and has high economic value. The invention adopts the medium-temperature rapid thermal cracking process of the magnetically stabilized fluidized bed to prepare the bio-oil, and replaces the common fluidized bed reactor. The technology takes biomass as a raw material, has the advantages of easily obtained raw materials, low price, simple process and good application and market prospects, can effectively solve environmental problems, increases the income of farmers, and conforms to the national sustainable development strategy.
Description
Technical field:
The present invention relates to a kind of bio oil and with the method for warm fast pyrolysis system bio oil in the biomass magnetic stabilization fluid bed bioreactor, belong in the biomass engineering the middle temperature Rapid Thermal in the biomass thermal chemical conversion and decompose the field.
Background technology:
The biomass fast pyrolysis liquefaction technology is one of cutting edge technology in world today's renewable energy source development field.Product can obtain the energy (being the highest means of present utilization ratio) of primordial matter 85%～90% based on bio oil.Bio oil also can be passed through further separation, extraction, synthetic high added value industrial chemicals except that as the fuel.
Reactor and modified version thereof are bored in the rotation that has that is used for the pyrolysis reactor input scale production of production bio oil at present, fluidized-bed reactor etc., but mostly have certain shortcoming.Rotation awl reactor as Dutch Twente university student's material technology group does not need carrier gas, and the device volume is little, bio oil productive rate height, but the equipment operation is complicated with maintenance, the energy consumption height.The fluidized-bed reactor of Canada Waterloo university, apparatus and process is simple, and response intensity is big, heat and mass speed height, the temperature field is even, but the bed material easily runs off, and easily lumps with material.
Summary of the invention:
The purpose of this invention is to provide a kind of bio oil and utilizing a kind of reactor is the method for warm fast pyrolysis system bio oil in the biomass magnetic stabilization fluid bed bioreactor, this invention is that to utilize a kind of new reactor be magnetic stabilization fluid bed bioreactor system bio oil, overcome the shortcoming of conventional flow fluidized bed reactor, realize the technology simple and stable, processing power is strong, oil productive rate height, characteristic of low energy consumption.Magnetic stabilization fluid bed is to be the bed material with the magnetic-particle, the stable bed that forms under the uniform magnetic field of axial time-independent space.The magnetic stabilization fluid bed many advantages that have fixed bed and fluidized-bed concurrently.It can use the small-particle solid and be unlikely to cause too high pressure to fall as fluidized-bed, alternate back-mixing has been controlled in the effect of externally-applied magnetic field effectively, and the flowable of fine particle makes the loading and unloading solid very convenient; Can avoid in the fluidized bed process solid particulate loss phenomenon that often occurs, also can avoid the hot localised points that may occur in the fixed bed, simultaneously can stable operation in relative broad range, can also brokenly lump and improve interphase mass transfer.
The objective of the invention is to realize in the following manner:
Contain C＞71.1%, H＞7.3%, O＞16.6%, N＜0.1% in the bio oil of the present invention by mass percentage, oil viscosity＞10
6MPa.s, density＞1.10, pH value＞2.5, water ratio＜20%.
Adopt international advanced middle temperature fast pyrolysis technology, with magnetic stabilization fluid bed (bed material: thin iron sand powder, particle diameter＜0.2mm.Externally-applied magnetic field: coil is set, realizes Digital Control, uniform magnetic field is provided.) be reactor system bio oil.Biomass fast by the magnetic stablizing bed material of high temperature, have reduced residence time of material under the rheomorphism of Poor oxygen gas, suppressed the product secondary and decomposed generation gas, and the bio oil productive rate has improved nearly 10%.
Concrete processing step of the present invention is as follows:
(1) raw material pre-treatment:
With biomass is raw material, pulverizes, is dried to water ratio＜8at% then, makes the material particles of particle diameter less than 2mm;
(2) Poor oxygen gas preparation:
Air imports the Poor oxygen gas producer by air compressor, the Poor oxygen gas that produces enters the gas buffer jar, the gas that the gas buffer jar comes out is divided into two-way through spinner-type flowmeter: the main road that flow is bigger enters the reactor bottom preheating, enters reactor through gas distribution grid; The less route feed bin top of flow feeds, and together enters reactor along material;
(3) magnetic stabilization fluid bed reaction:
Biological particles enters by feeding screw with Poor oxygen gas and carries out fast pyrolysis in the magnetic stabilization fluid bed bioreactor, input rate is 5-10kg/h, the regulation and control magneticstrength makes the bed material just in time be restricted in the reactor, Poor oxygen gas being mixed together of fluidized bed material and material in reactor, and the lanthanum-cerium mischmetal compound that adds material quantity 1～3at% is as catalyzer, with reduce alkali (NaOH, KOH) and salt (NaCl, KCl, Na
2CO
3, K
2CO
3) composition, reactor is heated between 450-550 ℃, and material is degraded under the high temperature anoxia condition, generates cracking steam and charcoal, and pyrolytical condition: pressure is 1～1.4kPa, fluidising air velocity 0.20-0.30m/s;
(4) product collection:
Charcoal is collected by cyclonic separator and collection charcoal case; Oil vapour in the cracking steam is collected in the oil-collecting bottle by condenser, and condenser temperature maintains-1～1 ℃.Non-condensable gas in the cracking steam is through filter compression gas tank collection storage;
(5) product is refining:
The phlegma of oil vapour is through making catalyzer with CoMo, and at pressure 9～11Mpa, behind simple hydrogenation 3～5min, distillation is handled under the temperature 300-350 ℃ of condition, and 380～450 ℃ of distillation temperatures are made bio oil.
The cracking resultant is formed by mass percentage: bio oil 60-75%; Charcoal 10-13%; Gas 12-15% (N
240-50%, CO25-35%, CO
25-10%, CH
45-10%, other 10-20%).Bio oil viscosity＞10
6MPa.s, density＞1.10, pH value＞2.5, calorific value＞33MJ/kg, water ratio＜20% (massfraction).Bio oil ultimate analysis (massfraction): C＞71.1%, H＞7.3%, O＞16.6%, N＜0.1%.
Described biomass be stalk, leaf, wood chip and or organic waste.
The invention has the beneficial effects as follows: concentrated the advantage of fluidized-bed and fixed bed, technology is simple, and treatment capacity is big, and residence time of material is short, is heated evenly, and the bio oil productive rate is up to more than 70%.Make biomass pyrolytic reaction efficiency higher, production technique is more stable.And bio oil product calorific value height, sulfur-bearing, nitrogen, chlorine, heavy metal seldom, environmental protection.
Description of drawings:
Fig. 1 is a process flow sheet of the present invention.
Embodiment:
The biomass of utilizing of the present invention are as raw material, adopt the technology of warm fast pyrolysis system bio oil in the magnetic stabilization fluid bed bioreactor, raw material is through pre-treatment, middle temperature fast pyrolysis, cyclonic separator gas, the solid separation, condensation of gas, obtain bio oil (process flow sheet as shown in Figure 1) after refining.Be raw material with the corn cob now, particular content of the present invention described in detail:
(1) raw material pre-treatment:
Collect corn cob, pulverizing then, dry (water ratio＜8%) are also made the material particles of particle diameter less than 2mm.
(2) Poor oxygen gas preparation:
Air imports the Poor oxygen gas producer by air compressor, and the Poor oxygen gas of generation is pressed into surge tank.The gas that comes out from the gas buffer jar is divided into two-way through spinner-type flowmeter: the main road that flow is bigger enters the reactor bottom preheating, enters reactor through gas distribution grid; The less route feed bin top of flow feeds, and together enters reactor along material.
(3) magnetic stabilization fluid bed reaction:
Material enters by feeding screw with Poor oxygen gas and carries out fast pyrolysis in the magnetic stabilization fluid bed bioreactor.Input rate is 5kg/h.Regulate magneticstrength, the bed material just in time is limited in the reactor by externally-applied magnetic field, do not escape.Poor oxygen gas mixture of fluidized bed material and material together in reactor, and add a small amount of rare earth compound as catalyzer, to reduce alkali and salt component.Reactor is added nichrome wire and is heated to 500 ℃, and material under the high temperature anoxia condition thermal destruction takes place, and generates thermo-cracking steam and charcoal.The Poor oxygen gas that enters reactor leaves reactor with resultant, tangentially enters cyclonic separator.Pyrolytical condition: pressure is 1.25kPa, fluidising air velocity 0.25m/s.
(4) product collection:
Biomass charcoal is collected by cyclonic separator and collection charcoal case; Oil vapour is collected in the oil-collecting bottle by condenser (condenser temperature maintains 0 ℃).Gaseous product process filter is removed the tar of molecular surface, uses the compression gas tank collection storage.
(5) product is refining:
Product carries out hydrogenation reaction earlier, and CoMo makes catalyzer, pressure 10Mpa, 300 ℃ of temperature, time 3min.Distill refiningly subsequently, after the about 400 ℃ of processing of controlled temperature, make bio oil.
Resultant is formed (massfraction): bio oil 75%; Charcoal 12%; Gas 13%.Bio oil viscosity＞10
6MPa.s, density 1.40, pH value 2.9, calorific value 32MJ/kg, water ratio 10%.Bio oil ultimate analysis: C content 72.1%, H content 7.6%, O content 16.8%, N content 0.05%.
Claims (4)
1. a bio oil is characterized in that: contain C＞71.1%, H＞7.3%, O＞16.6%, N＜0.1% in the bio oil by mass percentage, oil viscosity＞10
6MPa.s, density＞1.10, pH value＞2.5, water ratio＜20%.
2. method with the described bio oil of warm fast pyrolysis system claim 1 in the biomass magnetic stabilization fluid bed bioreactor is characterized in that: concrete processing step is as follows:
(1) raw material pre-treatment:
With biomass is raw material, pulverizes, is dried to water ratio＜8at% then, makes the material particles of particle diameter less than 2mm;
(2) Poor oxygen gas preparation:
Air imports the Poor oxygen gas producer by air compressor, the Poor oxygen gas that produces enters the gas buffer jar, the gas that the gas buffer jar comes out is divided into two-way through spinner-type flowmeter: the main road that flow is bigger enters the reactor bottom preheating, enters reactor through gas distribution grid; The less route feed bin top of flow feeds, and together enters reactor along material;
(3) magnetic stabilization fluid bed reaction:
Biological particles enters by feeding screw with Poor oxygen gas and carries out fast pyrolysis in the magnetic stabilization fluid bed bioreactor, input rate is 5-10kg/h, the regulation and control magneticstrength makes the bed material just in time be restricted in the reactor, Poor oxygen gas being mixed together of fluidized bed material and material in reactor, and lanthanum-cerium mischmetal compound of interpolation material quantity 1～3at% is as catalyzer, reactor is heated between 450-550 ℃, material is degraded under the high temperature anoxia condition, generate cracking steam and charcoal, pyrolytical condition: pressure is 1～1.4kPa, fluidising air velocity 0.20-0.30m/s;
(4) product collection:
Charcoal is collected by cyclonic separator and collection charcoal case; Oil vapour in the cracking steam is collected in the oil-collecting bottle by condenser, and condenser temperature maintains-1～1 ℃.Non-condensable gas in the cracking steam is through filter compression gas tank collection storage;
(5) product is refining:
The phlegma of oil vapour is through making catalyzer with CoMo, and at pressure 9～11Mpa, behind simple hydrogenation 3～5min, distillation is handled under the temperature 300-350 ℃ of condition, and 380～450 ℃ of distillation temperatures are made bio oil.
3. the method with the described bio oil of warm fast pyrolysis system claim 1 in the biomass magnetic stabilization fluid bed bioreactor according to claim 2, it is characterized in that: adopt magnetic stabilization fluid bed middle temperature fast pyrolysis system bio oil of carrying out biomass, input rate is 5-10kg/h, bed material: thin iron sand powder, particle diameter＜0.2mm.
4. the method with the described bio oil of warm fast pyrolysis system claim 1 in the biomass magnetic stabilization fluid bed bioreactor according to claim 2, it is characterized in that: described biomass are stalk, leaf, wood chip and or organic waste.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2007101473252A CN101121895A (en) | 2007-08-15 | 2007-08-15 | Biological oil and method for preparing biological oil by using biomass magnetic stabilization fluidized bed reactor and medium-temperature rapid thermal cracking |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2007101473252A CN101121895A (en) | 2007-08-15 | 2007-08-15 | Biological oil and method for preparing biological oil by using biomass magnetic stabilization fluidized bed reactor and medium-temperature rapid thermal cracking |
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| Publication Number | Publication Date |
|---|---|
| CN101121895A true CN101121895A (en) | 2008-02-13 |
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ID=39084397
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|---|---|---|---|
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102199435A (en) * | 2011-04-19 | 2011-09-28 | 安徽理工大学 | Method for preparing guaiacol-enriched biological oil by catalytic pyrolysis of biomass |
| CN101353583B (en) * | 2008-09-19 | 2012-02-22 | 河南盛润创业投资管理有限公司 | Biomass processing method |
| CN102382683A (en) * | 2010-08-31 | 2012-03-21 | 北京金骄生物质化工有限公司 | Method for preparing biomass gas from plant branches and trunks |
| CN102533340A (en) * | 2011-12-15 | 2012-07-04 | 北京金骄生物质化工有限公司 | Method utilizing waste biomasses to prepare biogas |
| TWI394829B (en) * | 2009-01-09 | 2013-05-01 | Ind Tech Res Inst | Biomass fuel generator |
| CN104755590A (en) * | 2012-10-31 | 2015-07-01 | 国际壳牌研究有限公司 | Methods and systems for processing lignin through viscosity reduction during hydrothermal digestion of cellulosic biomass solids |
| CN105602599A (en) * | 2015-10-20 | 2016-05-25 | 天津大学 | Method for preparing vehicular bio-fuel oil by using biomass all-components |
| CN115595176A (en) * | 2022-08-24 | 2023-01-13 | 宁波中金石化有限公司（Cn） | Method for reducing solid-phase product content in pyrolysis catalytic product of residual oil-hydrocracking tail oil by using modified iron sand microspheres |
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2007
- 2007-08-15 CN CNA2007101473252A patent/CN101121895A/en active Pending
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101353583B (en) * | 2008-09-19 | 2012-02-22 | 河南盛润创业投资管理有限公司 | Biomass processing method |
| TWI394829B (en) * | 2009-01-09 | 2013-05-01 | Ind Tech Res Inst | Biomass fuel generator |
| CN102382683A (en) * | 2010-08-31 | 2012-03-21 | 北京金骄生物质化工有限公司 | Method for preparing biomass gas from plant branches and trunks |
| CN102382683B (en) * | 2010-08-31 | 2014-01-15 | 北京金骄生物质化工有限公司 | Method for preparing biomass gas from plant branches and trunks |
| CN102199435A (en) * | 2011-04-19 | 2011-09-28 | 安徽理工大学 | Method for preparing guaiacol-enriched biological oil by catalytic pyrolysis of biomass |
| CN102533340A (en) * | 2011-12-15 | 2012-07-04 | 北京金骄生物质化工有限公司 | Method utilizing waste biomasses to prepare biogas |
| CN104755590A (en) * | 2012-10-31 | 2015-07-01 | 国际壳牌研究有限公司 | Methods and systems for processing lignin through viscosity reduction during hydrothermal digestion of cellulosic biomass solids |
| CN104755590B (en) * | 2012-10-31 | 2016-08-24 | 国际壳牌研究有限公司 | Reduced by viscosity during the hydrothermal digestion of cellulose biomass solid and process the method and system of lignin |
| CN105602599A (en) * | 2015-10-20 | 2016-05-25 | 天津大学 | Method for preparing vehicular bio-fuel oil by using biomass all-components |
| CN115595176A (en) * | 2022-08-24 | 2023-01-13 | 宁波中金石化有限公司（Cn） | Method for reducing solid-phase product content in pyrolysis catalytic product of residual oil-hydrocracking tail oil by using modified iron sand microspheres |
| CN115595176B (en) * | 2022-08-24 | 2023-12-29 | 宁波中金石化有限公司 | Method for reducing content of solid-phase product in residual oil-hydrocracking tail oil pyrolysis catalytic product by utilizing modified iron sand microspheres |
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