CN104371751A - Device and method for preparation of oil by biomass thermal cracking - Google Patents
Device and method for preparation of oil by biomass thermal cracking Download PDFInfo
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- CN104371751A CN104371751A CN201310473867.4A CN201310473867A CN104371751A CN 104371751 A CN104371751 A CN 104371751A CN 201310473867 A CN201310473867 A CN 201310473867A CN 104371751 A CN104371751 A CN 104371751A
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- cyclonic separator
- powdered carbon
- air outlet
- oil
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- 239000002028 Biomass Substances 0.000 title claims abstract description 65
- 238000000034 method Methods 0.000 title claims abstract description 13
- 238000002360 preparation method Methods 0.000 title abstract description 6
- 238000004227 thermal cracking Methods 0.000 title abstract 4
- 238000001816 cooling Methods 0.000 claims abstract description 66
- 238000002485 combustion reaction Methods 0.000 claims abstract description 9
- 238000006243 chemical reaction Methods 0.000 claims abstract description 6
- 238000011084 recovery Methods 0.000 claims abstract description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 182
- 229910052799 carbon Inorganic materials 0.000 claims description 182
- 239000003610 charcoal Substances 0.000 claims description 68
- 230000004888 barrier function Effects 0.000 claims description 62
- 239000000463 material Substances 0.000 claims description 62
- 239000012075 bio-oil Substances 0.000 claims description 50
- 238000007599 discharging Methods 0.000 claims description 50
- 239000003921 oil Substances 0.000 claims description 49
- 238000000197 pyrolysis Methods 0.000 claims description 46
- 238000011068 loading method Methods 0.000 claims description 33
- 238000003860 storage Methods 0.000 claims description 33
- 238000001035 drying Methods 0.000 claims description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 28
- 238000000926 separation method Methods 0.000 claims description 22
- 239000000428 dust Substances 0.000 claims description 17
- 239000002994 raw material Substances 0.000 claims description 17
- 239000003595 mist Substances 0.000 claims description 15
- 239000012535 impurity Substances 0.000 claims description 14
- 239000007921 spray Substances 0.000 claims description 13
- 239000012452 mother liquor Substances 0.000 claims description 9
- 238000010438 heat treatment Methods 0.000 claims description 7
- 239000000047 product Substances 0.000 claims description 7
- 239000006227 byproduct Substances 0.000 claims description 6
- 238000004891 communication Methods 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 6
- 238000010504 bond cleavage reaction Methods 0.000 claims description 4
- 230000007017 scission Effects 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 230000008676 import Effects 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 230000009897 systematic effect Effects 0.000 claims description 3
- 239000007795 chemical reaction product Substances 0.000 abstract description 5
- 230000000694 effects Effects 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 241001464837 Viridiplantae Species 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 229930002875 chlorophyll Natural products 0.000 description 1
- 235000019804 chlorophyll Nutrition 0.000 description 1
- ATNHDLDRLWWWCB-AENOIHSZSA-M chlorophyll a Chemical compound C1([C@@H](C(=O)OC)C(=O)C2=C3C)=C2N2C3=CC(C(CC)=C3C)=[N+]4C3=CC3=C(C=C)C(C)=C5N3[Mg-2]42[N+]2=C1[C@@H](CCC(=O)OC\C=C(/C)CCC[C@H](C)CCC[C@H](C)CCCC(C)C)[C@H](C)C2=C5 ATNHDLDRLWWWCB-AENOIHSZSA-M 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001727 in vivo Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000013022 venting Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
- C10B57/10—Drying
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1011—Biomass
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- 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
Abstract
The invention provides a device and a method for preparation of oil by biomass thermal cracking, the device comprises a negative pressure feeding system, a combustion reaction system and a recovery cooling system; a biomass feedstock is sucked into from an inlet of the negative pressure feeding system, and is discharged by an outlet of the negative pressure feeding system into the combustion reaction system for reaction, and a reaction product is flowed back to the recovery cooling system by the combustion reaction system and cooled and discharged. The device for preparation of oil by biomass thermal cracking is stable in performance, can run for a long time, and can improve the efficiency of preparation of the oil by biomass thermal cracking.
Description
Technical field
The present invention relates to preparation facilities and the method for bio oil, particularly relate to a kind of biomass through pyrolysis liquefaction Apparatus for () and method therefor.
Background technology
Biomass energy is that solar energy is converted into chemical energy storage energy in vivo by chlorophyll by green plants.Biomass pyrolytic refers under the condition of heat, biomass Volatile, and the process producing solid coke and liquid oil product.And mostly not mature enough for the equipment of preparing bio-oil at present, stability is strong, and the production run time is not grown just needs cleaning maintenance again to recover liquefaction function.Summary of the invention
The object of the invention is to the defect solving the existence of above-mentioned prior art, a kind of bio-oil Apparatus for () and method therefor of stable performance is provided.
A kind of biomass through pyrolysis liquefaction equipment, comprises negative pressure feeding system, combustion reactions system, reclaims cooling system;
Described negative pressure feeding system comprises material loading cyclonic separator, storage compartment, Drying Bed, material loading blower fan, discharging blower fan, discharging cyclonic separator, pyrolysis hopper; Biomass material import is communicated with the opening for feed of material loading cyclonic separator, the air outlet of material loading cyclonic separator is communicated with the blast inlet of material loading blower fan, its discharge port is communicated with the feeding mouth of storage compartment, the discharge port of storage compartment is communicated with the feeding mouth of Drying Bed, the discharge port of Drying Bed is communicated with the opening for feed of discharging cyclonic separator, and the air outlet of discharging cyclonic separator is communicated with the blast inlet of discharging blower fan, its discharge port is communicated with the opening for feed of pyrolysis hopper;
Described combustion reactions system comprises burning bed, perpendicular bed, upper ball room, lower ball chamber, thermal barrier helix transporting device one, raw material helix transporting device, thermal barrier helix transporting device two, reactor; Described burning bed is communicated with the inlet mouth bottom perpendicular bed, the perpendicular air outlet at bed top is communicated with the feeding mouth of Drying Bed, the thermal barrier inlet communication of its heating medium outlet and upper ball room, the heating medium outlet of upper ball room and the discharge port of pyrolysis hopper are communicated to the feeding mouth of reactor jointly respectively by thermal barrier helix transporting device one and raw material helix transporting device, the discharge port of reactor is communicated with the opening for feed of lower ball chamber, and the discharge port of lower ball chamber is communicated with perpendicular bed by thermal barrier helix transporting device two bottom it;
Described recovery cooling system comprises: cooling tower, combustible gas ash discharge cyclonic separator, tail gas water seal, roots blower, oil pump, interchanger; The air outlet, top of lower ball chamber is communicated with the inlet mouth at cooling tower top, the air outlet of cooling tower is connected with the inlet mouth of combustible gas ash discharge cyclonic separator, the air outlet of combustible gas ash discharge cyclonic separator is communicated with tail gas water seal, one end, air outlet of tail gas water seal is in communication with the outside, one end is communicated with roots blower, and roots blower is communicated with burning bed; The discharge port of combustible gas ash discharge cyclonic separator is communicated with the oil-in bottom cooling tower; Bio oil oil outlet bottom cooling tower is communicated with the oil-in of oil pump, and the oil outlet of oil pump is communicated with the bio oil oiler of exchanger base, and the bio oil oil outlet of exchanger base is communicated with the spray of cooling tower inside; The low side of cooling tower is provided with the oil discharge outlet for discharging for unnecessary bio oil.
Further, also comprise burning powdered carbon storing chamber, be separated powdered carbon storing chamber, and revolve that powdered carbon storing chamber, two revolves powdered carbon storing chamber, separator, burning cyclonic separator, separation cyclone, are revolved cyclonic separator, two and revolved cyclonic separator, be separated blower fan; The carbon outleting port of described burning cyclonic separator is communicated with the carbon inlet port of burning powdered carbon storing chamber; The carbon outleting port of separation cyclone is communicated with the carbon inlet port being separated powdered carbon storing chamber; One revolves the carbon inlet port that cyclonic separator carbon outleting port and revolves powdered carbon storing chamber is communicated with; The carbon inlet port that two carbon outleting ports and two revolving cyclonic separator revolve powdered carbon storing chamber is communicated with; The inlet mouth of described burning cyclonic separator is communicated with the air outlet at perpendicular bed top, the air outlet of cyclonic separator of burning is communicated with the feeding mouth of Drying Bed; The delivery port of thermal barrier helix transporting device two is communicated with the opening for feed of separator, the discharge port of separator is communicated with the bottom of perpendicular bed, the air outlet at separator top is communicated with the inlet mouth of separation cyclone, the air outlet of separation cyclone is communicated with the inlet mouth being separated blower fan, is separated the air outlet of blower fan and is communicated with the inlet mouth of separator bottom; The inlet mouth that cyclonic separator is revolved in one air outlet and two of revolving cyclonic separator is communicated with; One inlet mouth revolving cyclonic separator is communicated with the air outlet at lower ball chamber top; Two air outlets of revolving cyclonic separator are communicated with the inlet mouth at cooling tower top.
Further, also comprise negative pressure row charcoal system, described negative pressure row charcoal system comprises negative pressure row charcoal cyclonic separator, negative pressure row charcoal storage charcoal room, twin screw e Foerderanlage, negative pressure row charcoal blower fan; Carbon outleting port and the negative pressure of described negative pressure row charcoal cyclonic separator arranges the carbon inlet port that charcoal stores up charcoal room and are communicated with, and negative pressure is arranged the carbon outleting port that charcoal stores up charcoal room and is communicated with the carbon inlet port of twin screw e Foerderanlage; Burning powdered carbon storing chamber, be separated powdered carbon storing chamber, and revolve the carbon outleting port that powdered carbon storing chamber, two revolves powdered carbon storing chamber and be all communicated with the extension being separated fan outlet, the end, extension being separated fan outlet is communicated with the inlet gas that negative pressure arranges charcoal cyclonic separator, and the air intake vent being connected to negative pressure row charcoal blower fan is returned in the air outlet of negative pressure row charcoal cyclonic separator.
Further, also comprise hay tank, described hay tank is connected between bio oil oil outlet bottom cooling tower and the oil-in of oil pump.
Further, also comprise dust-removal system, described dust-removal system comprises mist dust remover, water pump, dedusting cyclonic separator; Be communicated with the blast inlet of dedusting cyclonic separator after material loading blower fan and the air outlet of discharging blower fan converge, the air outlet of dedusting cyclonic separator is communicated with the bottom air inlet mouth of mist dust remover, the water outlet of the bottom of mist dust remover is communicated with the water-in of water pump, and the water outlet of water pump is communicated with by the spray of pipeline with mist dust remover inside.
A kind of biomass through pyrolysis method of making oil, comprises the following steps:
Step one, by the biomass material below 8 orders crossed through break process after material loading cyclonic separator separating impurity, biomass material enters in the storage compartment that is communicated with material loading cyclonic separator discharge port, then biomass material discharge from the discharge port of storage compartment after in Drying Bed through excess temperature be the high-temperature tail gas of 300 ~ 400 DEG C rapid drying with carry under one's arms after, by discharging cyclonic separator, raw material is discharged in pyrolysis hopper, then by raw material helix transporting device, biomass material is transported to reactor rapidly from pyrolysis hopper; Enter ball room after thermal barrier is heated to 750 ~ 800 DEG C by burning bed in perpendicular bed simultaneously, then by thermal barrier helix transporting device one, described thermal barrier is transported to rapidly in reactor;
Step 2, thermal barrier fully mix in reactor with biomass material, biomass material temperature within 1 ~ 2 second rises to 500 ~ 600 DEG C and heat scission reaction occurs, generate three kinds of products, be respectively: condensable gas, uncondensable combustible gas and powdered carbon; Wherein, condensable gas and uncondensable combustible gas are discharged as the air outlet of gaseous product from reactor head; And after powdered carbon and thermal barrier enter lower ball chamber from the discharge port of reactor, powdered carbon is collected as by product, and thermal barrier enters perpendicular bed by burning bed carries out heat to it;
Step 3, condensable gas and uncondensable combustible gas pass into the inlet mouth of cooling tower from the air outlet of reactor, then spray condensation is carried out by bio oil mother liquor, wherein condensable gas is condensed into new bio oil, and uncondensable combustible gas enters burning bed after discharging from the air outlet of cooling tower and air mixed is burnt for perpendicular bed provides heat energy, wherein, bio oil mother liquor is the bio oil of temperature step-down after interchanger cooling after discharging from the bio oil oil outlet bottom cooling tower.
Further, powdered carbon described in step 2 carries out collection as by product and comprises: utilize thermal barrier helix transporting device two by before perpendicular for thermal barrier feeding bed, first by separator, powdered carbon is separated with thermal barrier, wherein, powdered carbon is sucked out in the air outlet at separator top, then by separation cyclone, powdered carbon is separated, the powdered carbon after separation enter be communicated with the carbon outleting port of separation cyclone be separated in powdered carbon storing chamber; And thermal barrier is by carrying out heat in the perpendicular bed of discharge port inflow of separator bottom, a small amount of powdered carbon that thermal barrier carries and tail gas are discharged by the air outlet at perpendicular bed top, and powdered carbon to be collected in the burning powdered carbon storing chamber that is communicated with it by the residue powdered carbon after discharge by the cyclonic separator that burns; The high-temperature tail gas of discharging from air outlet, perpendicular bed top is then blown into for drying biomass material from the feeding mouth of Drying Bed;
Condensable gas described in step 3 and uncondensable combustible gas are before entering the cooling tower, successively revolve to enter in cooling tower again after cyclonic separator and two revolves cyclonic separator twice cyclone dust removal through one and cool, wherein, one revolve powdered carbon that cyclonic separator is separated enter be communicated with it one revolve in powdered carbon storing chamber, two revolve powdered carbons that cyclonic separator is separated enters two revolving in powdered carbon storing chamber of being communicated with it.
Further, described burning powdered carbon storing chamber, be separated powdered carbon storing chamber, and revolve powdered carbon storing chamber, two and revolve powdered carbon that powdered carbon storing chamber reclaims to be collected in negative pressure row charcoal storage charcoal by negative pressure row charcoal systematic unity indoor, after the powdered carbon of negative pressure row charcoal storage charcoal indoor arrives predetermined output, discharged by the twin screw e Foerderanlage be communicated with it.
Further, described bio oil mother liquor is first through hay tank removing solid impurity after discharging from the bio oil oil outlet bottom cooling tower, then through the cooled bio oil of interchanger.
Further, the air outlet expellant gas of described discharging cyclonic separator and material loading cyclonic separator carries out dedusting by dust-removal system after converging.
Biomass through pyrolysis liquefaction equipment provided by the invention, its stable performance, the phenomenon that long-time running also can not cause equipment to block, thus improve the efficiency of biomass through pyrolysis liquefaction.
Accompanying drawing explanation
Fig. 1 is the embodiment of the present invention one biomass through pyrolysis liquefaction equipment structure chart;
Fig. 2 is the embodiment of the present invention two biomass through pyrolysis liquefaction equipment structure chart;
Fig. 3 is the embodiment of the present invention three biomass through pyrolysis liquefaction equipment structure chart;
Fig. 4 is the embodiment of the present invention four biomass through pyrolysis liquefaction equipment structure chart.
Embodiment
For making the object, technical solutions and advantages of the present invention clearly, below in conjunction with the accompanying drawing in the present invention, the technical scheme in the present invention is clearly and completely described, obviously, described embodiment is the present invention's part embodiment, instead of whole embodiments.Based on the embodiment in the present invention, those of ordinary skill in the art, not making the every other embodiment obtained under creative work prerequisite, belong to the scope of protection of the invention.
Accompanying drawing 1 is the embodiment of the present invention one biomass through pyrolysis liquefaction equipment structure chart, and as shown in Figure 1, this equipment comprises negative pressure feeding system, combustion reactions system, reclaims cooling system;
Wherein, described negative pressure feeding system comprises material loading cyclonic separator 12, storage compartment 13, Drying Bed 14, material loading blower fan 16, discharging blower fan 15, discharging cyclonic separator 17, pyrolysis hopper 18; Biomass material import is communicated with the opening for feed of material loading cyclonic separator 12, the air outlet of material loading cyclonic separator 12 is communicated with the blast inlet of material loading blower fan 16, its discharge port is communicated with the feeding mouth of storage compartment 13, the discharge port of storage compartment 13 is communicated with the feeding mouth of Drying Bed 14, the discharge port of Drying Bed 14 is communicated with the opening for feed of discharging cyclonic separator 17, and the air outlet of discharging cyclonic separator 17 is communicated with the blast inlet of discharging blower fan 15, its discharge port is communicated with the opening for feed of pyrolysis hopper 18.
Particularly, biomass material is inhaled into material loading cyclonic separator 12 from the entrance of negative pressure feeding system, be sucked out by the top of material loading blower fan 16 from material loading cyclonic separator 12 through material loading cyclonic separator 12 removal of impurities rear impurity, and biomass material enters in storage compartment 13 from the discharge port of material loading cyclonic separator 12, then raw material is dried from being admitted to Drying Bed 14 after the outlet of storage compartment 13 is discharged under the effect of high-temperature tail gas, raw material after oven dry enters discharging cyclonic separator 17 and carries out discharging under the effect of discharging blower fan 15, then raw material is discharged in pyrolysis hopper 18 by discharging cyclonic separator 17.
Described combustion reactions system comprises burning bed 116, perpendicular bed 113, upper ball room 19, lower ball chamber 114, thermal barrier helix transporting device 1, raw material helix transporting device 110, thermal barrier helix transporting device 2 115, reactor 111, described burning bed 116 is communicated with the inlet mouth bottom perpendicular bed 113, the air outlet at perpendicular bed 113 top is communicated with the feeding mouth of Drying Bed 14, the thermal barrier inlet communication of its heating medium outlet and upper ball room 19, the heating medium outlet of upper ball room 19 and the discharge port of pyrolysis hopper 18 are communicated to the feeding mouth of reactor 111 jointly respectively by thermal barrier helix transporting device 1 and raw material helix transporting device 110, the discharge port of reactor 111 is communicated with the opening for feed of lower ball chamber 114, the discharge port of lower ball chamber 114 is communicated with perpendicular bed 113 by thermal barrier helix transporting device 2 115 bottom it,
Particularly, the raw material flowed out from described pyrolysis hopper 18 discharge port is transported to reactor 111 through raw material helix transporting device 110, biomass material fully mixes with the thermal barrier through heat and carries out heat scission reaction in reactor 111, the thermal barrier that after reaction, temperature reduces and reaction product flow into lower ball chamber 114 from the discharge port of reactor 111, and thermal barrier is delivered to perpendicular bed 113 at the discharge port of lower ball chamber 114 by thermal barrier helix transporting device 2 115; Simultaneously, thermal barrier carries out heat under the effect of burning bed 116 in perpendicular bed 113, high-temperature heat carrier after heating enters upper ball room 19 from the top of perpendicular bed 113, and high-temperature heat carrier is transported to reactor 111 at the discharge port of upper ball room 19 by thermal barrier helix transporting device 1; High-temperature tail gas after burning bed 116 heat hot carrier is discharged by the air outlet at perpendicular bed 113 top, and the biomass material of discharging from storage compartment 13 is blown into Drying Bed by pipeline by the high-temperature tail gas of discharge together; Described reaction product is condensable gas and uncondensable combustible gas, after reaction product enters lower ball chamber 114, discharges from the air outlet, top of lower ball chamber 114.
Described recovery cooling system comprises: cooling tower 117, combustible gas ash discharge cyclonic separator 118, tail gas water seal 119, roots blower 120, oil pump 122, interchanger 121; The air outlet, top of lower ball chamber 114 is communicated with the inlet mouth at cooling tower 117 top, the air outlet of cooling tower 117 is connected with the inlet mouth of combustible gas ash discharge cyclonic separator 118, the air outlet of combustible gas ash discharge cyclonic separator 118 is communicated with tail gas water seal 119, one end, air outlet of tail gas water seal 119 is in communication with the outside, one end is communicated with roots blower 120, and roots blower 120 is communicated with burning bed 116; The discharge port of combustible gas ash discharge cyclonic separator 118 is communicated with the oil-in bottom cooling tower 117; Bio oil oil outlet bottom cooling tower 117 is communicated with the oil-in of oil pump 122, and the oil outlet of oil pump 122 is communicated with the bio oil oiler bottom interchanger 121, and the bio oil oil outlet bottom interchanger 121 is communicated with the spray of cooling tower 117 inside; The low side of cooling tower 117 is provided with the oil discharge outlet 123 for discharging for unnecessary bio oil.
Particularly, the reaction product of discharging from the air outlet, top of lower ball chamber 114 passes into cooling tower 117, condensable gas is condensed into liquid biological oil, and the air outlet of uncondensable combustible gas in the middle part of cooling tower 117 is discharged, the uncondensable combustible gas after discharge passes into tail gas water seal 119 after the partial impurities of carrying in combustible gas removes by combustible gas ash discharge cyclonic separator 118; The pure combustible gas of discharging from tail gas water seal 119 returns to burning bed 116 by roots blower 120, burns for perpendicular bed 113 provides heat energy for burning bed 116 and air mixed; In cooling tower 117, condensed liquid biological oil content two outlet is discharged, and is respectively bio oil oil outlet, oil discharge outlet; Wherein, bio oil oil outlet is used for condensed bio oil again to cool, and cooled bio oil is again returned to the spray of cooling tower inside, for cooling the condensable gas of steam state entered in cooling tower; Oil discharge outlet is used for reclaiming liquid biological oil unnecessary in cooling tower for storage tank.Wherein, the bio oil that bio oil oil outlet is discharged bottom cooling tower is further cooled by oil pump press-in interchanger, further cooled bio oil is passed into the spray of cooling tower inside.
Biomass through pyrolysis liquefaction equipment provided by the invention, its stable performance, the phenomenon that long-time running also can not cause equipment to block, thus improve the efficiency of biomass through pyrolysis liquefaction.
Further, Fig. 2 is the embodiment of the present invention two biomass through pyrolysis liquefaction equipment structure chart, as shown in Figure 2, biomass through pyrolysis liquefaction equipment of the present invention also comprises burning powdered carbon storing chamber 22, is separated powdered carbon storing chamber 24, and revolves that powdered carbon storing chamber 29, two revolves powdered carbon storing chamber 220, separator 26, burning cyclonic separator 21, separation cyclone 23, are revolved cyclonic separator 27, two and revolved cyclonic separator 28, be separated blower fan 25; The carbon outleting port of described burning cyclonic separator 21 is communicated with the carbon inlet port of burning powdered carbon storing chamber 22, the carbon outleting port of separation cyclone 23 is communicated with the carbon inlet port being separated powdered carbon storing chamber 24, one revolves cyclonic separator 27 carbon outleting port is communicated with a carbon inlet port revolving powdered carbon storing chamber 29, and the carbon inlet port that two carbon outleting ports and two revolving cyclonic separator 28 revolve powdered carbon storing chamber 220 is communicated with; The inlet mouth of described burning cyclonic separator 21 is communicated with the air outlet at perpendicular bed 113 top, the air outlet of the cyclonic separator 21 that burns is communicated with the feeding mouth of Drying Bed 14; The delivery port of thermal barrier helix transporting device 2 115 is communicated with the opening for feed of separator 26, the discharge port of separator 26 is communicated with the bottom of perpendicular bed 113, the air outlet at separator 26 top is communicated with the inlet mouth of separation cyclone 23, the air outlet of separation cyclone 23 is communicated with the inlet mouth being separated blower fan 25, and the air outlet being separated blower fan 25 is communicated with the inlet mouth bottom separator 26; The inlet mouth that cyclonic separator 28 is revolved in one air outlet and two of revolving cyclonic separator 27 is communicated with; One inlet mouth revolving cyclonic separator 27 is communicated with the air outlet at lower ball chamber 114 top; Two air outlets of revolving cyclonic separator 28 are communicated with the inlet mouth at cooling tower 117 top.
Because the reactant generated in reactor is except condensable gas and uncondensable combustible gas, also containing powdered carbon.In order to improve the stability of equipment further, the present invention is provided with 5 carbon removal collection devices, be respectively by the burning carbon removal collection device formed with the burning powdered carbon storing chamber 22 that is communicated with of burning cyclonic separator 21, with being separated of being communicated with of separation cyclone 23 powdered carbon storing chamber 24 forms is separated carbon removal collection device, revolve with one that cyclonic separator 27 is communicated with one revolve that powdered carbon storing chamber 29 forms one revolve carbon removal collection device, revolve with two that cyclonic separator 28 is communicated with two revolve that powdered carbon storing chamber 220 forms two revolve carbon removal collection device; The material of discharging from lower ball chamber 114 comprises thermal barrier and powdered carbon, first powdered carbon and thermal barrier separate through separator by described thermal barrier and powdered carbon, thermal barrier slips into perpendicular bed from the bottom of separator, and powdered carbon enters after discharging from the top of separator and is separated carbon removal collection device and carries out carbon removal collection; In addition, because the thermal barrier entering perpendicular bed also carries a small amount of powdered carbon, these powdered carbons enter burning carbon removal collection device from the discharge port relief outlet at perpendicular bed top and carry out carbon removal collection; In addition, the condensable gas of discharging from reactor air outlet and uncondensable combustible gas also can carry part powdered carbon, are taken up in order of priority to revolve carbon removal collection device and two by one and revolve carbon removal collection device two-stage and carry out carbon removal collection.
Further, Fig. 3 is the embodiment of the present invention three biomass through pyrolysis liquefaction equipment structure chart, and as shown in Figure 3, described biomass through pyrolysis liquefaction equipment also comprises negative pressure row charcoal system; Described negative pressure row charcoal system comprises negative pressure row charcoal cyclonic separator 32, negative pressure row charcoal storage charcoal room 33, twin screw e Foerderanlage 34, negative pressure row charcoal blower fan 31; Carbon outleting port and the negative pressure of described negative pressure row charcoal cyclonic separator 32 arranges the carbon inlet port that charcoal stores up charcoal room 33 and are communicated with, and negative pressure is arranged the carbon outleting port that charcoal stores up charcoal room 33 and is communicated with the carbon inlet port of twin screw e Foerderanlage 34; Burning powdered carbon storing chamber 22, be separated powdered carbon storing chamber 24, and revolve the carbon outleting port that powdered carbon storing chamber 29, two revolves powdered carbon storing chamber 220 and be all communicated with the extension being separated blower fan 25 air outlet, the end, extension being separated blower fan 25 air outlet is communicated with the inlet gas that negative pressure arranges charcoal cyclonic separator 32, and the air intake vent being connected to negative pressure row charcoal blower fan 31 is returned in the air outlet of negative pressure row charcoal cyclonic separator 32.
Particularly, from described burning carbon removal collection device, be separated carbon removal collection device, and revolve carbon removal collection device, two and revolve the powdered carbon that carbon removal collection device collects and be collected in negative pressure row charcoal storage charcoal room 33 by negative pressure row charcoal blower fan 31 is unified, when the powdered carbon in negative pressure row charcoal storage charcoal room 33 collect predetermined upper in limited time, by twin screw e Foerderanlage 34 by negative pressure the powdered carbon arranged in charcoal storage charcoal room 33 discharge.Wherein, burning powdered carbon storing chamber 22, be separated powdered carbon storing chamber 24, and revolve on cylinder arm that powdered carbon storing chamber 29, two revolves powdered carbon storing chamber 220 and be equipped with Level control line, a lowest limit, a upper limit, when powdered carbon arrives between the lowest limit of storage charcoal room and the upper limit, open the switch of bottom, powdered carbon is all collected in negative pressure row charcoal storage charcoal room 33 under the effect of negative pressure row charcoal blower fan 31.
Further, Fig. 4 is the embodiment of the present invention four biomass through pyrolysis liquefaction equipment structure chart, as shown in Figure 4, in order to ensure from cooling tower 117 out can not blocking pipe for the bio oil of spraying cooling after interchanger 121 cools, the present invention also comprises hay tank 41, and described hay tank 41 is connected between bio oil oil outlet bottom cooling tower 117 and the oil-in of oil pump 122.
Further, as shown in Figure 4, the present invention also comprises dust-removal system, and described dust-removal system comprises mist dust remover 53, water pump 52, dedusting cyclonic separator 51; Be communicated with the blast inlet of dedusting cyclonic separator 51 after material loading blower fan 16 and the air outlet of discharging blower fan 15 converge, the air outlet of dedusting cyclonic separator 51 is communicated with the bottom air inlet mouth of mist dust remover 53, the water outlet of the bottom of mist dust remover 53 is communicated with the water-in of water pump 52, and the water outlet of water pump 52 is communicated with by the spray of pipeline with mist dust remover 53 inside.
Further, the not outer row in order to make the impurity produced in the process of preparation bio oil effectively process, not polluted air, be communicated with dedusting cyclonic separator 51 after material loading blower fan 16 is converged by both air outlets with the impurity of discharging blower fan 15 sucking-off by the present invention and carry out dedusting, then mist dust remover 53 is passed into by removing the gas after impurity through dedusting cyclonic separator 51, then water is compressed into the spray of mist dust remover 53 inside by water pump 52, by spray by mist dust remover 53 in gas carry out further dedusting, finally the gas after removing impurity is outwards discharged, thus the phenomenon avoided directly to air venting impurity, decrease the pollution to air.
The present invention also provides a kind of biomass through pyrolysis method of making oil, comprises the following steps:
Step one, by the biomass material below 8 orders crossed through break process after material loading cyclonic separator 12 separating impurity, biomass material enters in the storage compartment 13 that is communicated with material loading cyclonic separator 12 discharge port, then biomass material discharge from the discharge port of storage compartment 13 after Drying Bed 14 in through excess temperature be the high-temperature tail gas of 300 ~ 400 DEG C rapid drying and after carrying under one's arms, by discharging cyclonic separator 17, raw material is discharged in pyrolysis hopper 18, then by raw material helix transporting device 110, biomass material is transported to rapidly reactor 111 from pyrolysis hopper 18; Enter ball room 19 after thermal barrier is heated to 750 ~ 800 DEG C by burning bed 116 in perpendicular bed 113 simultaneously, then by thermal barrier helix transporting device 1, described thermal barrier is transported to rapidly in reactor 111;
Step 2, thermal barrier fully mix in reactor 111 with biomass material, biomass material temperature within 1 ~ 2 second rises to 500 ~ 600 DEG C and heat scission reaction occurs, generate three kinds of products, be respectively: condensable gas, uncondensable combustible gas and powdered carbon; Wherein, condensable gas and uncondensable combustible gas are discharged as the air outlet of gaseous product from reactor 111; And after powdered carbon and thermal barrier enter lower ball chamber 114 from the discharge port of reactor 111, powdered carbon is collected as by product, and thermal barrier enters perpendicular bed 113 by burning bed 116 carries out heat to it;
Step 3, condensable gas and uncondensable combustible gas pass into the inlet mouth of cooling tower 117 from the air outlet of reactor 111, then spray condensation is carried out by bio oil mother liquor, wherein condensable gas is condensed into new bio oil, and uncondensable combustible gas enters burning bed 116 after discharging from the air outlet of cooling tower 117 and air mixed is burnt for perpendicular bed 113 provides heat energy, wherein, bio oil mother liquor is the bio oil of temperature step-down after interchanger 121 heat exchange after discharging from the bio oil oil outlet bottom cooling tower 117.
Further, powdered carbon described in described step 2 carries out collection as by product and comprises: utilize thermal barrier helix transporting device 2 115 by before perpendicular for thermal barrier feeding bed 113, first by separator 26, powdered carbon is separated with thermal barrier, wherein, powdered carbon is sucked out in the air outlet at separator 26 top, then by separation cyclone 23, powdered carbon is separated, the powdered carbon after separation enter be communicated with the carbon outleting port of separation cyclone 23 be separated in powdered carbon storing chamber 24; And thermal barrier is by carrying out heat in the perpendicular bed 113 of discharge port inflow bottom separator 26; the residue powdered carbon that the thermal barrier of heat carries and high-temperature tail gas are discharged by the air outlet at perpendicular bed 113 top, and powdered carbon to be collected in the burning powdered carbon storing chamber 22 that is communicated with it by the residue powdered carbon after discharge by the cyclonic separator 21 that burns; The high-temperature tail gas of discharging from air outlet, perpendicular bed 113 top is then blown into for drying biomass material from the feeding mouth of Drying Bed 14;
Condensable gas described in step 3 and uncondensable combustible gas are before entering cooling tower 117, successively enter again in cooling tower 117 after one revolves cyclonic separator 27 and two revolve cyclonic separator 28 twice whirlwind carbon removal and cool, wherein, one revolve powdered carbon that cyclonic separator 27 is separated enter be communicated with it one revolve in powdered carbon storing chamber 29, two revolve powdered carbons that cyclonic separator 28 is separated enters two revolving in powdered carbon storing chamber 220 of being communicated with it.
Further, described burning powdered carbon storing chamber 22, be separated powdered carbon storing chamber 24, and revolve powdered carbon storing chamber 29, two and revolve the powdered carbon that powdered carbon storing chamber 220 reclaims and be collected in negative pressure row charcoal storage charcoal room 33 by negative pressure row charcoal systematic unity, after the powdered carbon in negative pressure row charcoal storage charcoal room 33 arrives predetermined output, discharged by the twin screw e Foerderanlage 34 be communicated with it.
Further, described bio oil mother liquor is first remove solid impurity through hay tank 41 after discharging from the bio oil oil outlet bottom cooling tower 117, then the oil after interchanger 121 heat exchange.
Further, described discharging cyclonic separator 17 and the air outlet expellant gas of material loading cyclonic separator 12 carry out dedusting by dust-removal system after converging.
Last it is noted that above embodiment is only in order to illustrate technical scheme of the present invention, be not intended to limit; Although with reference to previous embodiment to invention has been detailed description, those of ordinary skill in the art is to be understood that: it still can be modified to the technical scheme described in foregoing embodiments, or carries out equivalent replacement to wherein portion of techniques feature; And these amendments or replacement, do not make the essence of appropriate technical solution depart from the spirit and scope of various embodiments of the present invention technical scheme.
Claims (10)
1. a biomass through pyrolysis liquefaction equipment, is characterized in that, comprises negative pressure feeding system, combustion reactions system, reclaims cooling system;
Described negative pressure feeding system comprises material loading cyclonic separator (12), storage compartment (13), Drying Bed (14), material loading blower fan (16), discharging blower fan (15), discharging cyclonic separator (17), pyrolysis hopper (18), biomass material import is communicated with the opening for feed of material loading cyclonic separator (12), the air outlet of material loading cyclonic separator (12) is communicated with the blast inlet of material loading blower fan (16), its discharge port is communicated with the feeding mouth of storage compartment (13), the discharge port of storage compartment (13) is communicated with the feeding mouth of Drying Bed (14), the discharge port of Drying Bed (14) is communicated with the opening for feed of discharging cyclonic separator (17), the air outlet of discharging cyclonic separator (17) is communicated with the blast inlet of discharging blower fan (15), its discharge port is communicated with the opening for feed of pyrolysis hopper (18),
Described combustion reactions system comprises burning bed (116), perpendicular bed (113), upper ball room (19), lower ball chamber (114), thermal barrier helix transporting device one (112), raw material helix transporting device (110), thermal barrier helix transporting device two (115), reactor (111), described burning bed (116) is communicated with the inlet mouth of perpendicular bed (113) bottom, the air outlet at perpendicular bed (113) top is communicated with the feeding mouth of Drying Bed (14), the thermal barrier inlet communication of its heating medium outlet and upper ball room (19), the heating medium outlet of upper ball room (19) and the discharge port of pyrolysis hopper (18) are communicated to the feeding mouth of reactor (111) jointly respectively by thermal barrier helix transporting device one (112) and raw material helix transporting device (110), the discharge port of reactor (111) is communicated with the opening for feed of lower ball chamber (114), the discharge port of lower ball chamber (114) is communicated with perpendicular bed (113) by thermal barrier helix transporting device two (115) bottom it,
Described recovery cooling system comprises: cooling tower (117), combustible gas ash discharge cyclonic separator (118), tail gas water seal (119), roots blower (120), oil pump (122), interchanger (121); The air outlet, top of lower ball chamber (114) is communicated with the inlet mouth at cooling tower (117) top, the air outlet of cooling tower (117) is connected with the inlet mouth of combustible gas ash discharge cyclonic separator (118), the air outlet of combustible gas ash discharge cyclonic separator (118) is communicated with tail gas water seal (119), one end, air outlet of tail gas water seal (119) is in communication with the outside, one end is communicated with roots blower (120), and roots blower (120) is communicated with burning bed (116); The discharge port of combustible gas ash discharge cyclonic separator (118) is communicated with the oil-in of cooling tower (117) bottom; The bio oil oil outlet of cooling tower (117) bottom is communicated with the oil-in of oil pump (122), the oil outlet of oil pump (122) is communicated with the bio oil oiler of interchanger (121) bottom, and the spray that the bio oil oil outlet of interchanger (121) bottom is inner with cooling tower (117) is communicated with; The low side of cooling tower (117) is provided with the oil discharge outlet (123) for discharging for unnecessary bio oil.
2. biomass through pyrolysis liquefaction equipment according to claim 1, it is characterized in that, also comprise burning powdered carbon storing chamber (22), be separated powdered carbon storing chamber (24), one revolve powdered carbon storing chamber (29), two revolve powdered carbon storing chamber (220), separator (26), burning cyclonic separator (21), separation cyclone (23), revolve cyclonic separator (27), two revolve cyclonic separator (28), be separated blower fan (25); The carbon outleting port of described burning cyclonic separator (21) is communicated with the carbon inlet port of burning powdered carbon storing chamber (22); The carbon outleting port of separation cyclone (23) is communicated with the carbon inlet port being separated powdered carbon storing chamber (24); One revolves the carbon inlet port that cyclonic separator (27) carbon outleting port and revolves powdered carbon storing chamber (29) is communicated with; The carbon inlet port that two carbon outleting ports and two revolving cyclonic separator (28) revolve powdered carbon storing chamber (220) is communicated with; The inlet mouth of described burning cyclonic separator (21) is communicated with the air outlet at perpendicular bed (113) top, the air outlet of the cyclonic separator (21) that burns is communicated with the feeding mouth of Drying Bed (14); The delivery port of thermal barrier helix transporting device two (115) is communicated with the opening for feed of separator (26), the discharge port of separator (26) is communicated with the bottom of perpendicular bed (113), the air outlet at separator (26) top is communicated with the inlet mouth of separation cyclone (23), the air outlet of separation cyclone (23) is communicated with the inlet mouth being separated blower fan (25), and the air outlet being separated blower fan (25) is communicated with the inlet mouth of separator (26) bottom; The inlet mouth that cyclonic separator (28) is revolved in one air outlet and two of revolving cyclonic separator (27) is communicated with; One inlet mouth revolving cyclonic separator (27) is communicated with the air outlet at lower ball chamber (114) top; Two air outlets of revolving cyclonic separator (28) are communicated with the inlet mouth at cooling tower (117) top.
3. biomass through pyrolysis liquefaction equipment according to claim 2, it is characterized in that, also comprise negative pressure row charcoal system, described negative pressure row charcoal system comprises negative pressure row's charcoal cyclonic separator (32), negative pressure row's charcoal storage charcoal room (33), twin screw e Foerderanlage (34), negative pressure row's charcoal blower fan (31); Carbon outleting port and the negative pressure of described negative pressure row's charcoal cyclonic separator (32) arranges the carbon inlet port that charcoal stores up charcoal room (33) and are communicated with, and negative pressure is arranged the carbon outleting port that charcoal stores up charcoal room (33) and is communicated with the carbon inlet port of twin screw e Foerderanlage (34); Burning powdered carbon storing chamber (22), be separated powdered carbon storing chamber (24), and revolve the carbon outleting port that powdered carbon storing chamber (29), two revolves powdered carbon storing chamber (220) and be all communicated with the extension being separated blower fan (25) air outlet, the end, extension being separated blower fan (25) air outlet is communicated with the inlet gas that negative pressure arranges charcoal cyclonic separator (32), and the air intake vent being connected to negative pressure row's charcoal blower fan (31) is returned in the air outlet of negative pressure row's charcoal cyclonic separator (32).
4. according to the arbitrary described biomass through pyrolysis liquefaction equipment of claim 1-3, it is characterized in that, also comprise hay tank (41), between the bio oil oil outlet that described hay tank (41) is connected to cooling tower (117) bottom and the oil-in of oil pump (122).
5. according to the arbitrary described biomass through pyrolysis liquefaction equipment of claim 1-3, it is characterized in that, also comprise dust-removal system, described dust-removal system comprises mist dust remover (53), water pump (52), dedusting cyclonic separator (51); Be communicated with the blast inlet of dedusting cyclonic separator (51) after material loading blower fan (16) and the air outlet of discharging blower fan (15) converge, the air outlet of dedusting cyclonic separator (51) is communicated with the bottom air inlet mouth of mist dust remover (53), the water outlet of the bottom of mist dust remover (53) is communicated with the water-in of water pump (52), and the water outlet of water pump (52) is communicated with by the spray that pipeline is inner with mist dust remover (53).
6. a biomass through pyrolysis method of making oil, is characterized in that, comprises the following steps:
Step one, by the biomass material below 8 orders crossed through break process after material loading cyclonic separator (12) separating impurity, biomass material enters in the storage compartment (13) that is communicated with material loading cyclonic separator (12) discharge port, then biomass material discharge from the discharge port of storage compartment (13) after Drying Bed (14) in through excess temperature be the high-temperature tail gas of 300 ~ 400 DEG C rapid drying and after carrying under one's arms, by discharging cyclonic separator (17), raw material is discharged in pyrolysis hopper (18), then by raw material helix transporting device (110), biomass material is transported to rapidly reactor (111) from pyrolysis hopper (18), enter upper ball room (19) after thermal barrier is heated to 750 ~ 800 DEG C by burning bed (116) in perpendicular bed (113) simultaneously, then described thermal barrier is transported to rapidly in reactor (111) by thermal barrier helix transporting device one (112),
Step 2, thermal barrier fully mix in reactor (111) with biomass material, biomass material temperature within 1 ~ 2 second rises to 500 ~ 600 DEG C and heat scission reaction occurs, generate three kinds of products, be respectively: condensable gas, uncondensable combustible gas and powdered carbon; Wherein, condensable gas and uncondensable combustible gas are discharged as the air outlet of gaseous product from reactor (111) top; And after powdered carbon and thermal barrier enter lower ball chamber (114) from the discharge port of reactor (111), powdered carbon is collected as by product, and thermal barrier enters perpendicular bed (113) by burning bed (116) carries out heat to it;
Step 3, condensable gas and uncondensable combustible gas pass into the inlet mouth of cooling tower (117) from the air outlet of reactor (111), then spray condensation is carried out by bio oil mother liquor, wherein condensable gas is condensed into new bio oil, and uncondensable combustible gas enters burning bed (116) after discharging from the air outlet of cooling tower (117) and air mixed is burnt for perpendicular bed (113) provides heat energy, wherein, bio oil mother liquor is the bio oil of temperature step-down after interchanger (121) cooling after discharging from the bio oil oil outlet of cooling tower (117) bottom.
7. biomass through pyrolysis method of making oil according to claim 6, it is characterized in that, powdered carbon described in step 2 carries out collection as by product and comprises: utilize thermal barrier helix transporting device two (115) by before perpendicular for thermal barrier feeding bed (113), first by separator (26), powdered carbon is separated with thermal barrier, wherein, powdered carbon is sucked out in the air outlet at separator (26) top, then by separation cyclone (23), powdered carbon is separated, powdered carbon after separation enter be communicated with the carbon outleting port of separation cyclone (23) be separated in powdered carbon storing chamber (24), and thermal barrier is by carrying out heat in the perpendicular bed (113) of discharge port inflow of separator (26) bottom, a small amount of powdered carbon that thermal barrier carries and tail gas are discharged by the air outlet at perpendicular bed (113) top, and powdered carbon to be collected in the burning powdered carbon storing chamber (22) that is communicated with it by the residue powdered carbon after discharge by the cyclonic separator (21) that burns, the high-temperature tail gas of discharging from perpendicular bed (113) air outlet, top is then blown into for drying biomass material from the feeding mouth of Drying Bed (14),
Condensable gas described in step 3 and uncondensable combustible gas are before entering cooling tower (117), successively revolve through one and after cyclonic separator (27) and two revolves cyclonic separator (28) twice cyclone dust removal, to enter that cooling tower (117) is middle to be cooled again, wherein, one revolve powdered carbon that cyclonic separator (27) is separated enter be communicated with it one revolve in powdered carbon storing chamber (29), two revolve powdered carbon that cyclonic separator (28) is separated enters two revolving in powdered carbon storing chamber (220) of being communicated with it.
8. biomass through pyrolysis method of making oil according to claim 7, it is characterized in that, described burning powdered carbon storing chamber (22), be separated powdered carbon storing chamber (24), and revolve powdered carbon storing chamber (29), two and revolve the powdered carbon that powdered carbon storing chamber (220) reclaims and be collected in negative pressure row's charcoal storage charcoal room (33) by negative pressure row charcoal systematic unity, after the powdered carbon in negative pressure row's charcoal storage charcoal room (33) arrives predetermined output, discharged by the twin screw e Foerderanlage (34) be communicated with it.
9. according to the arbitrary described biomass through pyrolysis liquefaction equipment of claim 6-8, it is characterized in that, described bio oil mother liquor is first through hay tank (41) removing solid impurity after discharging from the bio oil oil outlet of cooling tower (117) bottom, then through interchanger (121) cooled bio oil.
10. according to the arbitrary described biomass through pyrolysis liquefaction equipment of claim 6-8, it is characterized in that, after described discharging cyclonic separator (17) and the air outlet expellant gas of material loading cyclonic separator (12) converge, carry out dedusting by dust-removal system.
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