CN1175085C - Biomass integrated thermocracking equipment for preparing liquid fuel - Google Patents
Biomass integrated thermocracking equipment for preparing liquid fuel Download PDFInfo
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- CN1175085C CN1175085C CNB021120080A CN02112008A CN1175085C CN 1175085 C CN1175085 C CN 1175085C CN B021120080 A CNB021120080 A CN B021120080A CN 02112008 A CN02112008 A CN 02112008A CN 1175085 C CN1175085 C CN 1175085C
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Abstract
The present invention discloses a biomass integrated thermal cracking device for preparing liquid fuel in a grading mode. A cyclone separator and a carbon filter are combined, which forms the present invention. Carbon is effectively recovered, and volatile ingredients are cleaned. Fuel oil which has the high quality is obtained by a grading condensation system which is composed of a high-middle temperature air-cooled heat exchanger, a high-middle temperature heat transfer oil heater and a high-middle-low temperature condenser, and simultaneously, heavy oil and liquid which contains more water are respectively processed. Therefore, the subsequent processing cost is reduced, and the output of the fuel oil which has the high quality is optimized. An automatic heat supply system which is composed of the high-middle temperature air-cooled heat exchanger, a carbon burning furnace and a reactor heat exchanger effectively utilizes residual heat generated by the automatic heat supply system. A combined type material feeding device can ensure that material is easily fed. A fluidized bed reactor whose cross section can be changed is adopted, which ensures the yield of biologic oil. Therefore, the present invention has the advantages of strong gas-solid phase heat transmission of a fluidized bed, high heat flow intensity, etc., and temperature rise of biomass at a flashing speed, quick separation of volatile ingredients and reutilization of solid carbon are realized.
Description
Technical field
The present invention relates to a kind of biomass integrated thermocracking equipment for preparing liquid fuel.
Background technology
The SO that causes rapid growth to energy demand, a large amount of combustion of fossil fuel to utilize in the process being discharged along with the sustainable development of Chinese national economy
2, NO
xMake ecotope be subjected to severe contamination Deng pollutent, simultaneously, as second largest CO in the world
2Discharging state, CO
2" Greenhouse effect " influence that a large amount of dischargings are aggravated has also obtained attention in China, in addition, because the instability of outburst of the several of oil crisis and oil price also impels the Application and Development of substituted liquid fluid fuel to put on schedule.Than fossil oils such as coals, biomass are a kind of renewable and clean energy resource resources, utilize because of biomass simultaneously to have CO in the process
2The zero release characteristics, thus for alleviating serious day by day " Greenhouse effect " special meaning is arranged.In the recovery energy field of biomass, the biomass through pyrolysis liquefaction technology is the cutting edge technology of the present research and development of biomass energy in the world.This technology can will be high-grade easy storage, easily transportation with the mode of production of successive technology and batch production based on the Wood Adhesives from Biomass of wood chip the like waste, energy density is high and substituted liquid fluid fuel (bio oil) easy to use, it not only can be directly used in the burning of equipment such as existing boiler and gas turbine, and can make the quality of the quality of liquid fuel by further modification processing near fuel powered by conventional energy such as diesel oil or gasoline, can therefrom extract Chemicals in addition with commercial value.Than the fossil oil of routine, bio oil is extremely small because of objectionable constituent such as its contained sulphur, nitrogen, can be considered the green fuel of 21st century.
In the various technologies of biomass through pyrolysis liquefaction, multiple different testing apparatus and technological line have been adopted abroad, to reach the purpose that increases the bio oil productive rate and improve the energy utilization level.As quick cracking, hydrocracking, vacuum cracking, low temperature pyrolyzer, partial combustion cracking etc., but it is generally acknowledged that the quick cracking under normal pressure is still the most economic method of liquid fuel of producing, it generally can be divided into following a few class: (a) mechanical contact formula reactor, it mainly directly or indirectly contacts with biomass by a scorching hot reactor surface, thereby heat is delivered to biomass to be rapidly heated it to reach fast pyrolysis, the heat of ablation cracking reactor of Britain Aston university is typically arranged, the rotation awl biomass through pyrolysis to-oil reactor of Vortex reactor that NREL proposes and the design of Dutch Twente university etc.; (b) indirect type reactor, the principal character of this class reactor are to provide biomass through pyrolysis required heat by a pyritous surface or thermal source, and it mainly carries out the heat transmission by thermal radiation, as the thermal radiation reactor of U.S. Washington university; (c) mixing reactor, it mainly is by hot gas flow or gas-solid multiphase flow biomass to be carried out rapid heating, it can provide high heating rate and uniform relatively temperature of reaction, mobile carrier gas simultaneously fast is convenient to product of thermo-cracking and is in time separated out, as the fluid bed heat cracking system of Canadian Waterloo university, circulating fluid bed reactor that Canadian Ensyn proposes and the quick flow type pump with injection reactor of GTRI etc.The equipment scale of mechanical contact formula reactor is comparatively huge, and mechanical contact is worn and torn severe and made operation expense also higher simultaneously, therefore will be restricted in mass-producing is used.And the indirect type reactor since the limitations restrict of thermal source its application, this type of reactor is general main to provide the mechanism test required.Than preceding two types; the external biomass through pyrolysis liquefaction reaction device side of having developed and having attempted mass-producing overweights the 3rd class; especially use the biomass through pyrolysis reactor of fluidization, fluidized-bed process makes it become the technology that the thermo-cracking that development potentiality is arranged is at present most produced liquid fuel because of realizing high heating rate, the short gas phase residence time, simple and direct temperature control, charcoal recovery easily, lower investment and sophisticated method of design.
Summary of the invention
Purpose of the present invention is shortcoming such as not high and not classification of product liquid at energy utilization rate in the existing biomass through pyrolysis liquefaction process, has researched and developed a kind of biomass integrated thermocracking equipment for preparing liquid fuel.
The technical solution used in the present invention is:
Biomass integrated thermocracking equipment for preparing liquid fuel comprises that preparation connects the built-up type feeding device under the hopper, the built-up type feeding device connects the variable cross-section fluidized-bed reactor respectively, bailout gas, gas-holder, the variable cross-section fluidized-bed reactor, connect cyclonic separator respectively, bailout gas, gas-holder, with the interchanger outside reactor, connect the charcoal roasting kiln respectively, the raw material drying chamber, the storehouse that connects material respectively, raw material drying chamber, induced draft fan, one end of cyclonic separator and carbon filter is connected, after being connected, the other end of cyclonic separator and carbon filter connects the charcoal roasting kiln, carbon filter is through the high temperature condenser, the high temperature heat conductive oil well heater, first Heat-transfer Oil Pump connects the high temperature air cooler, the high temperature condenser also respectively with the high temperature air cooler, in warm condenser connect, in warm condenser through in warm hotline heater, warm air cooler during second Heat-transfer Oil Pump connects, in warm condenser also be connected with subcooling condenser, subcooling condenser has hot water outlet, cooling water inlet, and through the gas filter, gas pump connects gas-holder, connects the charcoal roasting kiln after an end of high temperature air cooler and middle temperature air cooler is connected, after being connected, the other end of high temperature air cooler and middle temperature air cooler connects gas blower.
The built-up type feeding device comprises the feed hopper that is connected with the preparation hopper, the feed spiral is housed under the discharge port of feed hopper, the material seeding airduct that one end is connected with gas-holder with bailout gas, the other end is connected with the variable cross-section fluidized-bed reactor is contained under the blanking airduct of feed spiral, the blanking airduct connects bailout gas and gas-holder, outside the material seeding airduct water jacket is housed.
The upper surface outlet of variable cross-section fluidized-bed reactor is connected with cyclonic separator, the air distribution plate of lower surface is connected with gas-holder with bailout gas through air compartment, variable cross-section fluidized-bed reactor inner chamber is gradual shrinkage freeboard of fluidized bed, emulsion zone from top to down, emulsion zone is equipped with the interchanger of reactor outward, and material inlet is positioned at the bottom of emulsion zone.
The useful effect that the present invention has:
1) it is technical sophisticated fluidization to be applied to biomass through pyrolysis, make full use of the fluidized-bed gas-solid advantages such as strong and heat flow rate per unit area is big of conducting heat mutually and realize the recycling of separating out fast of the flash intensification of biomass and fugitive constituent and solid carbon, realize the variable cross-section fluidized-bed reactor from heat supply, unique simultaneously variable cross-section design has guaranteed the productive rate of bio oil.
2) adopt cyclonic separator and carbon filter to combine secondary gas charcoal separation system, reach the purpose of solid matter in efficient recovery solid product charcoal and the high efficiency filter fugitive constituent.
3) by high temperature condenser, high temperature heat conductive oil well heater, high temperature air cooler, in warm condenser, middle temperature hotline heater, middle temperature air cooler and subcooling condenser form the fractional condensation system, as far as possible directly obtaining high-quality oil fuel simultaneously, be suitable for mink cell focus and contain handling respectively, thereby reduce subsequent disposal expense and the output that maximizes high-quality oil fuel than the liquid of juicy.
4) adopt the exhaust gas recirculation mode, return the cost that has reduced extra source of the gas as fluidizing agent by gas pump thereby can not cold crack vent one's spleen.
5) high temperature air cooler, middle temperature air cooler, charcoal roasting kiln and reactor interchanger have been formed reactor autothermal operation system efficiently, it will be utilized by the charcoal burning that secondary gas charcoal separation system separates, and makes that the required heat of biomass through pyrolysis can be supplied with voluntarily.The waste heat that the reactor autothermal operation system is produced has then been effectively utilized in the raw material drying chamber.
6) the built-up type feeding device has guaranteed the smooth feed at variable cross-section fluidized-bed reactor malleation feed place.
Description of drawings
Fig. 1 is a structural representation of the present invention;
Fig. 2 is the structural representation of built-up type feeding device;
Fig. 3 is the structural representation of variable cross-section fluidized-bed reactor.
Embodiment
As shown in Figure 1, the present invention includes the preparation hopper and connect built-up type feeding device 21 time, built-up type feeding device 2 connects variable cross-section fluidized-bed reactor 3 respectively, bailout gas 19, gas-holder 20, variable cross-section fluidized-bed reactor 3 connects cyclonic separator 5 respectively, bailout gas 19, gas-holder 20, connect charcoal roasting kiln 15 respectively with the interchanger 4 outside reactor, raw material drying chamber 17, the storehouse 16 that connects material respectively, raw material drying chamber 17, induced draft fan 21, one end of cyclonic separator 5 and carbon filter 6 is connected, after being connected, the other end of cyclonic separator 5 and carbon filter 6 connects charcoal roasting kiln 15, carbon filter 6 is through high temperature condenser 7, high temperature heat conductive oil well heater 8, the first Heat-transfer Oil Pump C1 connects high temperature air cooler 9, high temperature condenser 7 also respectively with high temperature air cooler 9, in warm condenser 12 connect, warm hotline heater 11 in back shaft 12 warps, warm air cooler 10 during the second Heat-transfer Oil Pump C2 connects, in warm condenser 12 also be connected with subcooling condenser 13, subcooling condenser 13 has hot water outlet a, cooling water inlet b, and through gas filter 14, gas pump C connects gas-holder 20, connects charcoal roasting kiln 15 after an end of high temperature air cooler 9 and middle temperature air cooler 10 is connected, after being connected, the other end of high temperature air cooler 9 and middle temperature air cooler 10 connects gas blower 22.
As shown in Figure 1, by traditional feed-types such as elevator or belt conveyings, biomass material is at first fed preparation hopper 1, after waiting to prepare hopper 1 and being full of raw material, close the top cover of preparation hopper 1, and open the preparation hopper 1 of originally closing and the valve between the built-up type feeding device 2, and the raw material of preparation hopper is slowly added in the built-up type feeding device 2, built-up type feeding device 2 is responsible for biomass material is sent in the variable cross-section fluidized-bed reactor 3 that is attached thereto.The raw material that enters variable cross-section fluidized-bed reactor 3 is reached about 500 ℃ preferable temperature of reaction by the flash heating in dense bed, the rapid decomposes of raw material discharges fugitive constituent, and in less than 1 second time, being fluidized the fast speed belt of wind from variable cross-section fluidized-bed reactor 3, pyrolysis solid product charcoal is also taken out of variable cross-section fluidized-bed reactor 3 by air clamp simultaneously.The charcoal and the fugitive constituent mixture that come out from reactor enter secondary gas charcoal separation system, the gas charcoal mixt at first enters cyclonic separator 5 and carries out flash trapping stage, wherein about charcoal of about 95% is separated by cyclonic separator 5, remaining charcoal and fugitive constituent enter follow-up carbon filter 6 together again, by gas-solid separator will be wherein remaining charcoal filter out, clean fugitive constituent enters follow-up fractional condensation system.The fractional condensation system is made up of the condenser and the heat-eliminating medium loop of different cooling temperatures, wherein the temperature of first step high temperature condenser 7 is set in 200 ℃, this temperature is equivalent to the final boiling point of gasoline, its effect is the higher product liquid of those boiling points to be cooled down earlier obtain having the oil fuel of heavy oil quality, can directly burn to utilize or carry out further cracking deep processing to become light-weight fuel oil; The temperature of warm condenser 12 is set in 101 ℃ in the second stage, its main purpose is the light-weight fuel oil that is collected in the gasoline boiling range scope, but the large quantity of moisture that biomass through pyrolysis generates can not be condensed because being higher than the boiling point of water simultaneously, the product of this section can be processed into high-quality power with oily by refinement; The temperature of last step subcooling condenser 13 is near room temperature, its effect is to comprise in the fugitive constituent in the biomass through pyrolysis process under the condensable composition condensation of water, the product liquid that this section collection obtains is because of containing than juicy, need adopt conventional fractionation handling procedure removal moisture wherein, the product behind the removal moisture can become light-weight fuel oil with the product liquid that middle temperature condenser 12 condensations obtain together or be used as industrial chemicals.The temperature of condensers at different levels is controlled by corresponding heat-eliminating medium loop temperature respectively and is guaranteed, wherein the used heat-eliminating medium of the cooling loop of high temperature condenser 7 and middle temperature condenser 12 correspondences adopts the strong thermal oil of thermostability, thermal oil is preheating to preset temperature by high temperature heat conductive oil well heater 8 in the condensation loop of correspondence and middle temperature hotline heater 11 respectively, treat that this device feeds intake after the operation, high temperature condenser 7 and middle temperature condenser 12 systemic heats are discharged by high temperature air cooler 9 and middle temperature air cooler 10 by the thermal oil medium in each self-condensation loop.And the heat-eliminating medium in subcooling condenser 13 corresponding loops is a water, can adopt disposable water-cooled or recirculated water cooling mode according to practical situations.From high temperature air cooler 9 and the hot blast that comes out of warm air cooler 10 feed in the charcoal roasting kiln 15 and carry out UTILIZATION OF VESIDUAL HEAT IN, the charcoal that gets off from secondary gas solid separation systematic collection feeds the hot flue gas of charcoal roasting kiln 15 burning generations, the interchanger 4 that the hot flue gas that generates feeds reactor is passed to the dense bed bed of variable cross-section fluidized-bed reactor 3 with heat, provides biomass through pyrolysis required heat.Feed the 17 pairs of raw materials in raw material drying chamber through the hot flue gas of part refrigerative together with the part freezing air and carry out drying, dried raw material is collected in feed bin 16.Can not cold crack venting one's spleen of coming out pump into gas-holder from the fractional condensation system, as combustible gas, other portion gas returns the fluidisation that variable cross-section fluidized-bed reactor 3 is used for the bed material to portion gas wherein through decarbonation technology.
As shown in Figure 1, the fractional condensation system realizes the purpose with product segmentation condensation, its condenser and medium loop by the different media temperature is formed, wherein the medium temperature of high temperature condenser 7 internal flows is the highest, design temperature is 200 ℃, be used for collecting product liquid with heavy oil quality, its initial temperature is preheating to corresponding temperature by corresponding high temperature heat conductive oil well heater 8, after treating normal operation, close the heating circuit of high temperature heat conductive oil well heater 8, open the medium flow cycle of high temperature air cooler 9 simultaneously, liberated heat in the biomass through pyrolysis product condensation process is discharged at high temperature air cooler 9 by thermal oil.The temperature of warm condenser 12 interior media is preheating to 101 ℃ by warm hotline heater 11 in corresponding earlier in the second stage, its main purpose is the light-weight fuel oil that is collected in the gasoline boiling range scope, but the large quantity of moisture that biomass through pyrolysis generates can not be condensed because being higher than the boiling point of water simultaneously, this section product condensation liberated heat is by middle temperature air cooler 10 dischargings, and the product of collecting can be processed into high-quality power with oily by refinement.The temperature of last step subcooling condenser 13 is near room temperature, its effect is to comprise in the fugitive constituent in the biomass through pyrolysis process under the condensable composition condensation of moisture, the product liquid that this section collection obtains is because of containing than juicy, need adopt conventional fractionation handling procedure removal moisture wherein, the product behind the removal moisture can become light-weight fuel oil with the product liquid that middle temperature condenser 12 condensations obtain together or be used as industrial chemicals.The warm air of high temperature air cooler 9 and middle temperature air cooler 10 feeds in the charcoal roasting kiln 15 and carries out UTILIZATION OF VESIDUAL HEAT IN in the fractional condensation system.
As shown in Figure 2, built-up type feeding device 2 plays a part biomass materials such as wood chip are sent into variable cross-section fluidized-bed reactor 3, it adopts screw feeder and the air conveying mode that combines, successfully overcome the deficiency of traditional gravity blanking mode, by the weight feed of feed spiral 2.1 assurances from feed hopper 2.5 raw materials, air conveyingly then will send into variable cross-section fluidized-bed reactor 3 fast by the raw material that feed spiral 2.1 provides, blanking airduct 2.4 in wherein air conveying guarantees that the raw material that feed spiral 2.1 comes out falls into material seeding airduct 2.2 smoothly, and material seeding airduct 2.2 then plays a part all even transferring raw material.Air conveying employing becomes the diameter design, each regional gas velocity is different, gas velocity in variable cross-section fluidized-bed reactor 3 ingresss can reach 10m/s, thereby can effectively prevent between the raw material and and built-up type feeding device 2 tube walls between adhesion, and and material seeding airduct 2.2 on the acting in conjunction of water jacket 2.3 water coolants guaranteed that the residence time of variable cross-section fluidized-bed reactor 3 ingress's raw materials is short to and can ignore its intensification at built-up type feeding device 2, avoided the be heated generation of the agglomerating phenomenon of bonding of raw material.After the proportioning of optimizing between variable cross-section fluidized-bed reactor 3 fluidized winds, material seeding airduct 2.2 material seeding wind and the blanking airduct 2.4 blanking wind, built-up type feeding device 2 can guarantee carrying out smoothly of biomass material feed.
As shown in Figure 3, variable cross-section fluidized-bed reactor 3 is main devices of biomass through pyrolysis, and it is made up of material inlet 3.1, air compartment 3.2, air distribution plate 3.3, emulsion zone 3.4, gradual shrinkage freeboard of fluidized bed 3.5 and reactor outlet 3.6.For productive rate that maximizes the liquid fuel product as far as possible and the quality of optimizing the liquid fuel product, structure of reactor wants to realize the quick and sufficient decomposes of biomass in reactor that a volatile matter that also will as far as possible biomass through pyrolysis be generated is separated out and unlikely secondary cracking fast in addition.The variable cross-section fluidized-bed reactor 3 that this patent proposes has adopted unique design, the material inlet 3.1 of reactor is positioned at the bottom of the emulsion zone 3.4 of variable cross-section fluidized-bed reactor 3, thereby made full use of the violent advantage of heat and mass in the emulsion zone 3.4, guaranteed that biomass can obtain quick and complete decomposes in emulsion zone 3.4, also can guarantee that the hot flue gas heat in the reactor interchanger 4 passes to the bed material of emulsion zone 3.4 simultaneously.In addition, this reactor has adopted the variable cross-section design, and the volatile matter that gradual shrinkage freeboard of fluidized bed 3.5 makes biomass through pyrolysis generate can be fast by reactor outlet 3.6 precipitating reactors and by secondary cracking.
Claims (1)
1. biomass integrated thermocracking equipment for preparing liquid fuel is characterized in that:
1) it comprises under preparation hopper (1) and connects built-up type feeding device (2), built-up type feeding device (2) connects variable cross-section fluidized-bed reactor (3) respectively, bailout gas (19), gas-holder (20), variable cross-section fluidized-bed reactor (3) connects cyclonic separator (5) respectively, bailout gas (19), gas-holder (20), connect charcoal roasting kiln (15) respectively with the interchanger (4) outside reactor, raw material drying chamber (17), the storehouse (16) that connects material respectively, raw material drying chamber (17), induced draft fan (21), cyclonic separator (5) is connected with an end of carbon filter (6), after being connected, the other end of cyclonic separator (5) and carbon filter (6) connects charcoal roasting kiln (15), carbon filter (6) is through high temperature condenser (7), high temperature heat conductive oil well heater (8), first Heat-transfer Oil Pump (C1) connects high temperature air cooler (9), high temperature condenser (7) also respectively with high temperature air cooler (9), in warm condenser (12) connect, in warm condenser (12) through in warm hotline heater (11), warm air cooler (10) during second Heat-transfer Oil Pump (C2) connects, in warm condenser (12) also be connected with subcooling condenser (13), subcooling condenser (13) has hot water outlet (a), cooling water inlet (b), and through gas filter (14), gas pump (C) connects gas-holder (20), connects charcoal roasting kiln (15) after an end of high temperature air cooler (9) and middle temperature air cooler (10) is connected, after being connected, the other end of high temperature air cooler (9) and middle temperature air cooler (10) connects gas blower (22);
2) said built-up type feeding device (2) comprises the feed hopper (2.5) that is connected with preparation hopper (1), feed spiral (2.1) is housed under the discharge port of feed hopper (2.5), one end is contained under the blanking airduct (2.4) of feed spiral (2.1) with the material seeding airduct (2.2) that bailout gas (19) is connected with gas-holder (20), the other end is connected with variable cross-section fluidized-bed reactor (3), blanking airduct (2.4) connects bailout gas (19) and gas-holder (20), and water jacket (2.3) is housed outside material seeding airduct (2.2);
3) upper surface of said variable cross-section fluidized-bed reactor (3) outlet (3.6) is connected with cyclonic separator (5), the air distribution plate of lower surface (3.3) is connected with gas-holder (20) with bailout gas (19) through air compartment (3.2), variable cross-section fluidized-bed reactor (3) inner chamber is gradual shrinkage freeboard of fluidized bed (3.5), emulsion zone (3.4) from top to down, the outer interchanger (4) that reactor is housed of emulsion zone (3.4), material inlet (3.1) is positioned at the bottom of emulsion zone (3.4).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021120080A CN1175085C (en) | 2002-06-07 | 2002-06-07 | Biomass integrated thermocracking equipment for preparing liquid fuel |
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| Application Number | Priority Date | Filing Date | Title |
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| CNB021120080A CN1175085C (en) | 2002-06-07 | 2002-06-07 | Biomass integrated thermocracking equipment for preparing liquid fuel |
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| CN1390915A CN1390915A (en) | 2003-01-15 |
| CN1175085C true CN1175085C (en) | 2004-11-10 |
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Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100357396C (en) * | 2005-01-05 | 2007-12-26 | 中国科学院过程工程研究所 | Method and device for thermolysis preparing liquid fuel from steam explosion stalk fermented residue |
| CN1962818B (en) * | 2005-11-08 | 2010-09-22 | 李效时 | Process for preparing bio-oil by using rapid thermal cleavage technology |
| CN101440311B (en) * | 2008-12-24 | 2012-10-17 | 张建超 | Biomass gas purification equipment and process |
| CN101962563B (en) * | 2010-10-30 | 2013-11-06 | 上海交通大学 | Device for preparing biofuel by quick thermal cracking of biomass |
| CN102168855A (en) * | 2011-04-27 | 2011-08-31 | 浙江物华天宝能源环保有限公司 | Pneumatic sludge feeding device of sludge incinerator |
| CN102408901B (en) * | 2011-10-12 | 2014-01-08 | 厦门大学 | Method for quick thermal cracking of biomass and device thereof |
| CN105602599B (en) * | 2015-10-20 | 2017-04-26 | 天津大学 | Method for preparing vehicular bio-fuel oil by using biomass all-components |
| CN110307582B (en) * | 2019-06-19 | 2021-01-19 | 西安石油大学 | Gas and hot water combined supply system for biomass coupling carbon five-auxiliary liquid |
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2002
- 2002-06-07 CN CNB021120080A patent/CN1175085C/en not_active Expired - Lifetime
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