CN109837103A - A kind of biomass thermal chemical conversion integrated system and application - Google Patents
A kind of biomass thermal chemical conversion integrated system and application Download PDFInfo
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- CN109837103A CN109837103A CN201711224016.0A CN201711224016A CN109837103A CN 109837103 A CN109837103 A CN 109837103A CN 201711224016 A CN201711224016 A CN 201711224016A CN 109837103 A CN109837103 A CN 109837103A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Abstract
The present invention provides a kind of biomass thermal chemical conversion integrated system and application, the biomass thermal chemical conversion integrated system of the invention includes following components, biomass through pyrolysis/catalytic pyrolysis module, bio oil Hydrobon module, pyrolytic carbon reduction/catalysis restore CO in pyrolysis gas2CO module is prepared, CO adds hydrogen to prepare oil product module.Oil product or chemicals can be converted for almost all carbon component in biomass using thermochemical study integrated system of the invention.System of the present invention greatly improves the carbon atom utilization rate that biomass thermal chemical conversion utilizes process, reduces CO2It generates and discharges, improve the feature of environmental protection and economy of biomass thermal chemical conversion, there is good industrial applications prospect.
Description
Technical field
The invention belongs to eco-friendly power source technical fields, and in particular to a kind of biomass thermal chemical conversion integrated system and answer
With.
Background technique
The aggravation of fuels and chemicals demand, the increasingly harsh research for driving renewable energy clean utilization of environmental requirement
Process.Since rich reserves are easy to get, the advantages such as renewable receive more and more attention biomass resource.Thermochemical study is recognized
To be one of most effective biomass economy approach, become academic circles at present and industrial circle due to being with a wide range of applications
Research hotspot.Biomass fast pyrolysis is one of the major technique of biomass thermal chemical conversion, which refers to biomass
Raw material is under conditions of completely cutting off air or a small amount of air, using medium reaction temperature, very short steam residence time, to biomass
Carry out the process of quickly pyrolysis preparation bio oil.Contain a large amount of CO in the pyrolysis gas that biomass through pyrolysis generates2, produce simultaneously
A large amount of pyrolytic carbon is given birth to, which results in biomass resource carbon utilisation rate is lower.For traditional biomass used during fast thermal cracking
The low problem of carbon atom utilization rate, the invention proposes the integrated systems of the biomass thermal chemical conversion for improving biomass carbon utilization rate
The utilization of system, the system will greatly improve the carbon atom utilization rate of biomass during thermochemical study, while reduce greenhouse
Gas CO2Generation and discharge, improve the feature of environmental protection and economy of biomass thermal chemical conversion process.
Summary of the invention
The object of the present invention is to provide a kind of biomass thermal chemical conversion integrated system and applications, and the integrated system can
To improve the utilization rate of carbon atom in biomass, CO is reduced2It generates and discharges, while producing the clear gusoline without sulphur nitrogen-free and change
Product.
To achieve the goals above, the invention provides the following technical scheme:
A kind of biomass thermal chemical conversion integrated system, the system are made of following module: biomass through pyrolysis/urge
Change thermal cracking module, bio oil Hydrobon module, pyrolytic carbon reduction/catalysis restores CO in pyrolysis gas2CO module is prepared,
CO adds hydrogen to prepare oil product module.
The biomass through pyrolysis/catalytic pyrolysis module is by raw material storage warehouse, biomass pretreatment system, pyrolytic reaction
Device, carrier gas system, bio oil collection system, pyrolysis gas purification collection system, charcoal collection system and exhaust gas circulation system group
At.
The bio oil hydrofinishing module is by bio oil feed system, hydrogen air supply system, hydrofining reactor, production
Object separated collection system and exhaust gas circulation system composition.
CO in the pyrolytic carbon reduction/catalysis reduction pyrolysis gas2It prepares CO module and feed system, heat is pre-processed by charcoal
It vents one's spleen feed system, gasification reactor, ash content collection system, gas-phase product purification and collection system and exhaust gas circulation system group
At.
The CO add hydrogen prepare oil product module by gas component modulation system, gas raw material air supply system, hydrogenator,
Product separation and collection system and exhaust gas circulation system composition.
The each module cooperative work of the system, promotes the promotion of carbon atom utilization rate, improves the utilization efficiency of thermal energy,
The generation and discharge for reducing greenhouse gases improve the economy and the feature of environmental protection of thermochemical study process.
The present invention also provides a kind of applications of biomass thermal chemical conversion integrated system, use above-mentioned biomass thermalization
Learn conversion integrated system, biomass material can successively be passed through thermal cracking/catalytic pyrolysis, pyrolysis oil Hydrobon,
Pyrolytic carbon restores pyrolysis gas and oxycarbide hydrogenation reaction, by cooperateing between each module of biomass thermal chemical conversion integrated system
Almost all carbon component in biomass is converted oil product and chemicals by cooperation.
The system is the work is performed in the following manner:
1) biomass material decomposes in biomass through pyrolysis/catalytic pyrolysis module generates bio oil, pyrolysis gas and heat
Solve charcoal；
2) the 1) in the pyrolysis oil that generates react in bio oil Hydrobon module with hydrogen, obtain oxygen-containing
Measure low stabilization oil product；Meanwhile the 1) in the pyrolysis gas that generates and pyrolytic carbon in pyrolytic carbon reduction/catalysis reduction pyrolysis gas
CO2It reacts in preparation CO module, obtains CO；
3) the 2) in the CO that generates add hydrogen to prepare oil product module in CO hydrogenation reaction occurs, obtains clean oil product or chemistry
Product.
A kind of biomass carbon component method for transformation, using above-mentioned biomass thermal chemical conversion integrated system；Specific steps are such as
Under:
S1: the biomass material for being stored in raw material storage warehouse, the particle that crushing and screening is 50-1000 microns, through 30- are chosen
Pyrolysis reactor is conveyed by biomass pretreatment system after 200 DEG C of drying.
S2: being passed through carrier gas into pyrolysis reactor from carrier gas system, (reaction initial stage carrier gas is N2Or vapor and N2
Mixture is carrier gas, the pyrolysis gas or CO generated after stable reaction using pyrolysis module2Recovery module generate tail gas or
The sweep gas mixture or their one of or several mixtures with vapor that person CO adds hydrogen module to generate are carrier gas).Heat
The operation temperature for solving reactor is 400-900 DEG C, gas residence time 0.5-3.0s.
S3: for the pyrolysis gas that pyrolytic process generates after circulating cooling gas-liquid separator, product liquid enters bio oil receipts
Collecting system, bio oil and water are collected in liquid collection tank, and the bio oil obtained after liquid separation is handled is stored in bio oil collection
Tank.Pyrolysis gas after cooling removes the particulate matter that may wherein carry secretly by primary purifying system, is then pressurized to through booster pump
0.5-8.0MPa is stored in pyrolysis gas purification collecting tank I.Remaining pyrolytic carbon is pyrolyzed to carry out simply through acetone and other organic solvent
Deoiling treatment loads the alkaline metal oxide of certain content, is stored in charcoal collecting tank after drying.
S4-1: the bio oil for being pyrolyzed acquisition is transported in pyrolysis oil hydrofining reactor by bio oil feed system,
Hydrogen is quantitatively passed through by hydrogen air supply system simultaneously, thick pyrolysis oil obtains stable biomass-based after catalytic hydrodeoxygenation
The liquid product of oil product, generation passes through product separated collection system, and oil product storage is in bio oil collecting tank P, gas phase tail gas warp
It crosses exhaust gas circulation system and imports hydrofining reactor again.
S4-2: the gas in pyrolysis gas collecting tank I is passed through in pyrolytic carbon reduction pyrolysis gas by pyrolysis gas feed system
CO2In the gasification reactor of module, while charcoal by charcoal pretreatment feed system interval or is continuously conveyed into reaction
In device；Solid ash content is collected in ash content collecting tank.Richness CO gaseous mixture is obtained by gas-phase product purification and collection system processing, is increased
It is pressed onto 0.5-3.0MPa, is stored in gas storage tank J.The preferred fixed bed reactors of gasification reactor, operating condition are as follows: 700-
1200 DEG C, normal pressure.
S5: the gas in gas storage tank J is determined through carbonaceous gas air supply system and fresh hydrogen through hydrogen air supply system
Amount is passed through mixed gas tank, and it is anti-via gas raw material air supply system to be passed through CO adds hydrogen module plus hydrogen by the gas of said components modulation
It answers in device, the clear gusoline that product liquid obtains after gas-liquid separation and water-oil separating is stored in oily phase storage tank G, gaseous product
It is stored in after being pressurized in gas tank K.
S6: the gas in gas tank K is recycled to biomass pyrolysis device through exhaust gas circulation system or CO hydrogenation reaction fills
It is recycled in setting.
Based on the above technical solution, if in S1, alkalinous metal is catalyzed during preprocessing biomass raw material
Agent is loaded directly into biomass material, then the loading process of alkalinous metal is not needed in S3.
Based on the above technical solution, catalyst used in S6 is ferrum-based catalyst, cobalt-base catalyst, copper-based urges
Agent or nickel-base catalyst.
Preferably, biomass material described in S1 is stalk, corncob, rice husk and sawdust.
Preferably, S2 biomass fast pyrogenation reaction uses catalytic pyrolysis, and pyrolysis steam is passed directly into equipped with reformation
In the fixed bed reactors of catalyst, by steam condensation, gas-liquid separation are carried out after the reactor again.
Preferably, alkaline metal oxide described in S3 is K2The mixture of O, CaO or the two.
Preferably, CO hydrogenation reaction uses ferrum-based catalyst in S5, reduces high-purity H2Demand, reduce investment.
Oil product can be converted for almost all carbon component in biomass using thermochemical study integrated system of the invention
Or chemicals.System of the present invention is greatly improved biomass thermal chemical conversion and is utilized using the carbon atom of process
Rate reduces CO2It generates and discharges, improve the feature of environmental protection and economy of biomass thermal chemical conversion, there is good industry
Change application prospect.
Detailed description of the invention
Fig. 1 is a kind of process frame diagram of biomass carbon component conversion in the embodiment of the present invention；
Wherein 1 biomass through pyrolysis/catalytic pyrolysis module；CO in 2 pyrolytic carbon reduction/catalysis reduction pyrolysis gas2Preparation
CO module；3CO adds hydrogen to prepare oil product module；4 bio oil hydrofinishing modules；
11 raw material storage warehouses, 12 biomass pretreatment systems, 13 pyrolysis reactors, 14 charcoal collecting tanks, 15 carrier gas tanks,
16 gas-liquid separator X, 17 bio oil collecting tank P, 18 pyrolysis gas collecting tank I, 19 exhaust gas circulation system A；
21 charcoals pre-process feed system, 22 pyrolysis gas feed systems, 23 gasification reactors, 24 gas buffer tanks, 25
Purification pressure charging system, 26 gas storage tank J, 27 ash content collecting tanks, 28 exhaust gas circulation system B,
31 hydrogen air supply system D, 32 carbonaceous gas air supply systems, 33 mixed gas tanks, 34 gas buffer rooms, 35 hydrogenation reactions
Device, 36 gas-liquid separator Y, 37 oily phase storage tank G, 38 water phase storage tank H, 39 gas tank K, 40 exhaust gas circulation system C；
41 bio oil feed systems, 42 hydrogen-holders, 43 finishing reactors, 44 product separation systems, 45 oily phase storage tank S,
46 hydrogen air supply system E, 47 exhaust gas circulation system F.
Specific embodiment
In order to keep the purpose of the present invention, technical solution and advantage clearer, below by way of specific embodiment to the present invention
It is further elaborated.Following embodiment is only limitted to explain the present invention, does not limit the present invention.
The process of a kind of biomass thermal chemical conversion integrated system, a preferred embodiment of the system is as shown in Figure 1；By with
Under several modules composition: biomass through pyrolysis/catalytic pyrolysis module 1, bio oil Hydrobon module 4, pyrolytic carbon is also
CO in original/catalysis reduction pyrolysis gas2CO module 2 is prepared, CO adds hydrogen to prepare oil product module 3.
The biomass through pyrolysis/catalytic pyrolysis module 1 is by raw material storage warehouse 11, biomass pretreatment system 12, heat
Reactor 13, charcoal collecting tank 14, carrier gas tank 15, gas-liquid separator X 16, bio oil collecting tank P 17, pyrolysis gas is solved to collect
Tank I18 and exhaust gas circulation system A 19 is formed.
The bio oil hydrofinishing module 4 is by bio oil feed system 41, hydrogen-holder 42, finishing reactor 43, production
Object separated collection system (product separation system 44 and oily phase storage tank S 45), hydrogen air supply system E 46 and exhaust gas circulation system F
47 compositions.
CO in the pyrolytic carbon reduction/catalysis reduction pyrolysis gas2Preparation CO module 2 pre-processes feed system by charcoal
21, pyrolysis gas feed system 22, gasification reactor 23, gas-phase product purification and collection system (gas buffer tank 24, purification pressurization
System 25, gas storage tank J 26), ash content collecting tank 27 and exhaust gas circulation system B 28 form.
The CO adds hydrogen to prepare oil product module 3, and by gas component modulation system, (hydrogen air supply system D 31, carbonaceous gas are supplied
Gas system 32 and mixed gas tank 33), gas raw material air supply system (gas buffer room 34), hydrogenator 35, product separation and receive
Collecting system (gas-liquid separator Y 36, oily phase storage tank G 37, water phase storage tank H38, gas tank K 39) and exhaust gas circulation system C 40
Composition,.
The each module cooperative work of the system, promotes the promotion of carbon atom utilization rate, improves the utilization efficiency of thermal energy,
The generation and discharge for reducing greenhouse gases improve the economy and the feature of environmental protection of thermochemical study process.
The present invention also provides a kind of applications of biomass thermal chemical conversion integrated system, use above-mentioned biomass thermalization
Learn conversion integrated system, biomass material can successively be passed through thermal cracking/catalytic pyrolysis, pyrolysis oil Hydrobon,
Pyrolytic carbon restores pyrolysis gas and oxycarbide hydrogenation reaction, by cooperateing between each module of biomass thermal chemical conversion integrated system
Almost all carbon component in biomass is converted oil product and chemicals by cooperation.
The system is the work is performed in the following manner:
1) biomass material decomposes in biomass through pyrolysis/catalytic pyrolysis module generates bio oil, pyrolysis gas and heat
Solve charcoal；
2) the 1) in the pyrolysis oil that generates react in bio oil Hydrobon module with hydrogen, obtain oxygen-containing
Measure low stabilization oil product；Meanwhile the 1) in the pyrolysis gas that generates and pyrolytic carbon in pyrolytic carbon reduction/catalysis reduction pyrolysis gas
CO2It reacts in preparation CO module, obtains CO；
3) the 2) in the CO that generates add hydrogen to prepare oil product module in CO hydrogenation reaction occurs, obtains clean oil product or chemistry
Product.
A kind of method that biomass carbon component is converted into oil product and chemicals, it is integrated using above-mentioned biomass thermal chemical conversion
System；Specific embodiment is as follows:
Embodiment 1
S1: pyrolysis reactor 13 (selecting fluidized bed) temperature is risen to 600 DEG C.Choose the jade for being stored in raw material storage warehouse 11
Meter Xin is raw material, the particle for being 250-380 microns through 12 crushing and screening of biomass pretreatment system, with 2g/ after 80 DEG C of drying
The rate of min is continuously conveyed into pyrolysis reactor 13.
S2: carrier gas (vapor and N are passed through into reactor from carrier gas tank 152Mixture).Gas residence time is 2s.
S3: after liquid/gas separator X 16, product liquid enters bio oil and collects system the pyrolysis steam that pyrolytic process generates
System, bio oil and water are collected in liquid collection tank, and the bio oil obtained after liquid separation is handled is stored in bio oil collecting tank
P17.Pyrolysis gas after cooling removes the particulate matter that may wherein carry secretly by primary purifying system, is pressurized to 1MPa and is stored in heat
It vents one's spleen in collecting tank I18.Remaining pyrolytic carbon is pyrolyzed after acetone washing, with K2CO3Aqueous solution impregnates charcoal (catalyst K2O
Mass content be biological carbonaceous amount 5wt%), be stored in after drying in charcoal collecting tank 14.
S4-1: the coarse biometric oil in bio oil collecting tank P is transported to pyrolysis oil by bio oil feed system 41 and adds hydrogen smart
In reactor 43 processed, while hydrogen is quantitatively passed through by hydrogen air supply system E 46, thick pyrolysis oil is after catalytic hydrodeoxygenation
Stable biomass-based oil product is obtained, the liquid product of generation is after product separation system 44, and oil product storage is in oily phase storage tank S
In 45.Gas phase tail gas imports hydrofining reactor 43 by exhaust gas circulation system F47 again.
S4-2: the gas in pyrolysis gas collecting tank I is passed through pyrolysis by pyrolysis gas feed system 22 (being depressurized to 3bar)
Charcoal restores CO in pyrolysis gas2In the gasification reactor 23 of module, at the same charcoal by charcoal pre-process and feed system 21 with
0.01g/min rate is continuously conveyed in reactor.Gasification reactor selects fixed bed, the operating condition of fixed bed reactors
Are as follows: 850 DEG C, normal pressure.Solid ash content is collected in ash content collecting tank 27.Richness CO gaseous mixture is obtained to purify and collect by gas-phase product
System processing is pressurized to 10bar and is stored in gas storage tank J26 later.
S5: the gas in gas storage tank J26 is through carbonaceous gas air supply system 32 and fresh hydrogen through hydrogen air supply system
D31 is quantitatively passed through mixed gas tank 33, CO, which is passed through, via gas raw material air supply system by the gas of said components modulation adds hydrogen module
Hydrogenator 35 in, the clear gusoline that product liquid obtains after gas-liquid separation and water-oil separating is stored in oily phase storage tank G
In 37, gaseous product is stored in gas tank K39 after being pressurized to 40bar.Hydrogenator selects fixed bed reactors, reactor
The mass content that the molar ratio of middle load co-precipitation FeMnK catalyst, Fe and Mn are 3, K is 2wt%.Catalyst first passes around
After 280 DEG C of activation 20h, it is to slowly warm up to 350 DEG C of progress CO hydrogenation reactions.
S6: the gas in gas tank K39 is recycled to charcoal reduction CO through exhaust gas circulation system2It is followed in fixed bed reactors
Ring uses.
Embodiment 2
S1: pyrolysis reactor 13 (selecting fluidized bed) temperature is risen to 650 DEG C.Choose the rice for being stored in raw material storage warehouse 11
Shell is raw material, the particle for being 250-380 microns through biomass pretreatment system crushing and screening, after 80 DEG C of drying, with 1g/min's
Rate is continuously conveyed into pyrolysis reactor 13.
S2: being passed through carrier gas into reactor from carrier gas system, (incipient stage carrier gas is N2, carrier gas adds for CO in subsequent process
Tail gas after hydrogen module reaction).Gas residence time is 2s.
S3: after gas-liquid separator X16, product liquid enters bio oil and collects system the pyrolysis steam that pyrolytic process generates
System, bio oil and water are collected in liquid collection tank, and the bio oil obtained after liquid separation is handled is stored in bio oil collecting tank
P17.Pyrolysis gas after cooling removes the particulate matter that may wherein carry secretly by primary purifying system, is pressurized to 1MPa and is stored in heat
It vents one's spleen in collecting tank I18.Remaining pyrolytic carbon is pyrolyzed after acetone washing, with Ca (NO3)2Aqueous solution impregnates charcoal (catalyst
The mass content of CaO is the 6wt% of biological carbonaceous amount), it is stored in after drying in charcoal collecting tank 14.
S4-1: the coarse biometric oil of bio oil collecting tank P17 is transported to pyrolysis oil by bio oil feed system 41 and adds hydrogen smart
In reactor 43 processed, while hydrogen is quantitatively passed through by hydrogen air supply system 46, thick pyrolysis oil obtains after catalytic hydrodeoxygenation
Stable biomass-based oil product is obtained, the liquid product of generation passes through product separation system 44, and oil product storage is in oily phase storage tank S45
In.Gas phase tail gas imports hydrofining reactor by exhaust gas circulation system F47 again.
S4-2: the gas in pyrolysis gas collecting tank I 18 is passed through heat by pyrolysis gas feed system 22 (being depressurized to 3bar)
Solve CO in charcoal reduction pyrolysis gas2In the fixed bed gasification reactor 23 of module, while charcoal is pre-processed and is fed by charcoal
System 21 is continuously conveyed in reactor with 0.01g/min rate.The operating condition of fixed bed reactors are as follows: 900 DEG C, normal pressure.
Solid ash content is collected in ash content collecting tank.Richness CO gaseous mixture is obtained by gas-phase product purification and collection system processing, is pressurized to
It is stored in gas storage tank J26 after 10bar.
S5: the gas in gas storage tank J26 is through carbonaceous gas air supply system 32 and fresh hydrogen through hydrogen air supply system
D31 is quantitatively passed through in mixed gas tank 33, is passed through CO via gas raw material air supply system by the gas of said components modulation and is added hydrogen mould
In the fixed bed hydrogenation reactor 35 of block, the clear gusoline that product liquid obtains after water-oil separating through gas-liquid is stored in oil and mutually stores up
In tank G37, gaseous product is stored in gas tank K39 after being pressurized to 40bar.Infusion process is loaded in fixed bed reactors
15Co1Mn/ZSM-5 catalyst, 250 DEG C of progress CO hydrogenation reactions.
S6: the gas in gas tank K39 is recycled in biomass pyrolysis device through exhaust gas circulation system to be recycled.
Embodiment 3
S1: choosing and being stored in the rice straw of raw material storage warehouse 11 is biomass material, broken through biomass pretreatment system
Broken screening is 250-380 micron of particle, and impregnating biological particles using potassium nitrate and calcium nitrate aqueous solution, (potassium oxide content is
2wt%, calcium oxide content 3wt%), it is continuously conveyed with the rate of 2g/min into pyrolysis reactor 13 after 80 DEG C of drying.
S2: the temperature to fluidized bed pyrolysis reactor 13 rises to 550 DEG C.Carrier gas is passed through into reactor from carrier gas system to lead to
Entering carrier gas, (incipient stage carrier gas is N2, carrier gas is that charcoal restores CO in subsequent process2Fixed bed reactors part loop tail
Gas), gas residence time 2s.
S3: after gas-liquid separator X16, product liquid enters bio oil and collects system the pyrolysis steam that pyrolytic process generates
System, bio oil and water are collected in liquid collection tank, and the bio oil obtained after liquid separation is handled is stored in bio oil collecting tank P17
In.Pyrolysis gas after cooling removes the particulate matter that may wherein carry secretly by primary purifying system, is pressurized to 1MPa and is stored in heat
It vents one's spleen in collecting tank I18.Remaining pyrolytic carbon is pyrolyzed to be stored in after acetone washing is dried in charcoal collecting tank 14.
S4-1: the bio oil in bio oil collecting tank P17 is transported to pyrolysis oil by bio oil feed system 41 and adds hydrogen smart
In reactor 43 processed, while hydrogen is quantitatively passed through by hydrogen air supply system 46, thick pyrolysis oil obtains after catalytic hydrodeoxygenation
Stable biomass-based oil product is obtained, the liquid product of generation passes through product separation system 44, and oil product storage is in oily phase storage tank S45
In.Gas phase tail gas imports hydrofining reactor by exhaust gas circulation system again.
S4-2: the gas in gas storage tank 18 is passed through pyrolytic carbon by pyrolysis gas feed system 22 (being depressurized to 3bar)
Restore CO in pyrolysis gas2In the fixed bed gasification reactor 23 of module, while charcoal is pre-processed by charcoal and feed system
21 are continuously conveyed in reactor with 0.01g/min rate.The operating condition of fixed bed reactors are as follows: 800 DEG C, normal pressure.Solid
Ash content is collected in ash content collecting tank 27.Richness CO gaseous mixture is obtained by gas-phase product purification and collection system processing, is pressurized to
It is stored in gas storage tank J26 after 10bar.
S5: the gas in gas storage tank J26 is through carbonaceous gas air supply system 32 and fresh hydrogen through hydrogen air supply system
D31 is quantitatively passed through gas component modulation system, is passed through CO via gas raw material air supply system by the gas of said components modulation
Add in the fixed bed hydrogenation reactor 35 of hydrogen module, the clear gusoline that product liquid obtains after gas-liquid separation and water-oil separating is deposited
It is stored in oily phase storage tank G37, gaseous product is stored in gas tank K39 after being pressurized to 40 bar.It is loaded in fixed bed reactors
Oxalate precipitation process Cu-Co catalyst, 250 DEG C of progress CO hydrogenation reactions.
S6: the gas in gas tank K39 is recycled to CO through exhaust gas circulation system and hydrogen is added to prepare in oil product fixed bed reactors
It is recycled.
Above to the present invention have been described in detail, but the invention is not limited to specific embodiment parties described herein
Formula.It will be appreciated by those skilled in the art that in the case without departing from the scope of the present invention, other changes and deformation can be made.This hair
Bright range is defined by the following claims.
Claims (8)
1. a kind of biomass thermal chemical conversion integrated system, which is characterized in that the biomass thermal chemical conversion integrated system by with
Under several modules composition: biomass through pyrolysis/catalytic pyrolysis module, bio oil Hydrobon module, pyrolytic carbon reduction/
CO in catalysis reduction pyrolysis gas2CO module is prepared, CO adds hydrogen to prepare oil product module.
2. a kind of biomass thermal chemical conversion integrated system according to claim 1, which is characterized in that biomass hot tearing
Solution/catalytic pyrolysis module is collected by raw material storage warehouse, biomass pretreatment system, pyrolysis reactor, carrier gas system, bio oil
System, pyrolysis gas purification collection system, charcoal collection system and exhaust gas circulation system composition.
3. a kind of biomass thermal chemical conversion integrated system according to claim 1, which is characterized in that bio oil adds hydrogen smart
Molding block is by bio oil feed system, hydrogen air supply system, hydrofining reactor, product separated collection system and circulation of tail gas
System composition.
4. a kind of biomass thermal chemical conversion integrated system according to claim 1, which is characterized in that pyrolytic carbon reduction/
CO in catalysis reduction pyrolysis gas2It prepares CO module and feed system, pyrolysis gas feed system, gasification reaction is pre-processed by charcoal
Device, ash content collection system, gas-phase product purification and collection system and exhaust gas circulation system composition.
5. a kind of biomass thermal chemical conversion integrated system according to claim 1, which is characterized in that CO adds hydrogen preparation oil
Product module is by gas component modulation system, gas raw material air supply system, hydrogenator, product separation and collection system and tail gas
Circulatory system composition.
6. a kind of biomass thermal chemical conversion integrated system according to claim 1, which is characterized in that the biomass
Include but are not limited to agricultural crop straw, trees, agriculture and forestry organic waste material, processing of farm products leftover bits and pieces, bagasse, furfural dregs, corn
Core, rice husk, shell or reed.
7. a kind of application of biomass thermal chemical conversion integrated system, which is characterized in that turned using above-mentioned biomass thermal chemistry
Change integrated system, biomass material is successively passed through to thermal cracking/catalytic pyrolysis, pyrolysis oil Hydrobon, pyrolytic carbon also
Former pyrolysis gas and oxycarbide hydrogenation reaction will be given birth to by coordinated between each module of biomass thermal chemical conversion integrated system
Almost all carbon component is converted into oil product and chemicals in substance.
8. a kind of application of biomass thermal chemical conversion integrated system according to claim 7, which is characterized in that the system
The work is performed in the following manner:
1) biomass material decomposes in biomass through pyrolysis/catalytic pyrolysis module generates bio oil, pyrolysis gas and pyrolytic carbon；
2) the 1) in the pyrolysis oil that generates react in bio oil Hydrobon module with hydrogen, it is low to obtain oxygen content
Stabilization oil product；Meanwhile the 1) in the pyrolysis gas and the pyrolytic carbon CO in pyrolytic carbon reduction/catalysis reduction pyrolysis gas that generate2System
It reacts in standby CO module, obtains CO；
3) the 2) in the CO that generates add hydrogen to prepare oil product module in CO hydrogenation reaction occurs, obtains clean oil product or chemicals.
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| CN111117683A (en) * | 2020-01-19 | 2020-05-08 | 中国林业科学研究院林产化学工业研究所 | Microwave continuous frequency modulation and biomass pyrolysis product cooperation gaseous hydrogenation device and use method thereof |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2011103047A2 (en) * | 2010-02-17 | 2011-08-25 | Uop Llc | Low oxygen biomass-derived pyrolysis oils and methods for producing the same |
| CN106497579A (en) * | 2016-10-14 | 2017-03-15 | 北京神雾环境能源科技集团股份有限公司 | A kind of system and method for domestic garbage resource |
| CN206624823U (en) * | 2017-03-17 | 2017-11-10 | 唐财安 | Rubbish biomass high-temperature low-pressure pyrolysis gasification system |
-
2017
- 2017-11-29 CN CN201711224016.0A patent/CN109837103A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2011103047A2 (en) * | 2010-02-17 | 2011-08-25 | Uop Llc | Low oxygen biomass-derived pyrolysis oils and methods for producing the same |
| CN106497579A (en) * | 2016-10-14 | 2017-03-15 | 北京神雾环境能源科技集团股份有限公司 | A kind of system and method for domestic garbage resource |
| CN206624823U (en) * | 2017-03-17 | 2017-11-10 | 唐财安 | Rubbish biomass high-temperature low-pressure pyrolysis gasification system |
Non-Patent Citations (2)
| Title |
|---|
| 刘建国等: "《可再生能源导论》", 28 February 2017, 中国轻工业出版社 * |
| 王钰等: "《煤化工生产技术》", 31 January 2017, 重庆大学出版社 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111117683A (en) * | 2020-01-19 | 2020-05-08 | 中国林业科学研究院林产化学工业研究所 | Microwave continuous frequency modulation and biomass pyrolysis product cooperation gaseous hydrogenation device and use method thereof |
| CN111117683B (en) * | 2020-01-19 | 2023-08-01 | 中国林业科学研究院林产化学工业研究所 | Microwave continuous frequency modulation synergistic biomass pyrolysis product gaseous hydrogenation device and application method thereof |
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