CN114874795A - Device and method for extracting tar and biomass oil from biomass pyrolysis gas - Google Patents
Device and method for extracting tar and biomass oil from biomass pyrolysis gas Download PDFInfo
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- CN114874795A CN114874795A CN202210451096.8A CN202210451096A CN114874795A CN 114874795 A CN114874795 A CN 114874795A CN 202210451096 A CN202210451096 A CN 202210451096A CN 114874795 A CN114874795 A CN 114874795A
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- 239000002028 Biomass Substances 0.000 title claims abstract description 75
- 238000000197 pyrolysis Methods 0.000 title claims abstract description 56
- 238000000034 method Methods 0.000 title claims abstract description 24
- 238000009833 condensation Methods 0.000 claims abstract description 204
- 230000005494 condensation Effects 0.000 claims abstract description 203
- 238000003763 carbonization Methods 0.000 claims abstract description 195
- 239000011269 tar Substances 0.000 claims abstract description 95
- 239000012075 bio-oil Substances 0.000 claims abstract description 83
- 239000003921 oil Substances 0.000 claims abstract description 55
- 238000002485 combustion reaction Methods 0.000 claims abstract description 50
- 238000011084 recovery Methods 0.000 claims abstract description 40
- 239000002641 tar oil Substances 0.000 claims abstract description 19
- 238000003860 storage Methods 0.000 claims description 73
- 239000000463 material Substances 0.000 claims description 30
- 230000008569 process Effects 0.000 claims description 10
- 239000000523 sample Substances 0.000 claims description 8
- 238000010000 carbonizing Methods 0.000 claims description 3
- 238000000605 extraction Methods 0.000 claims description 2
- 238000001816 cooling Methods 0.000 abstract description 8
- 239000007789 gas Substances 0.000 description 116
- 239000003546 flue gas Substances 0.000 description 11
- 239000007788 liquid Substances 0.000 description 11
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 10
- 239000003610 charcoal Substances 0.000 description 9
- 230000005540 biological transmission Effects 0.000 description 8
- 239000000446 fuel Substances 0.000 description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 239000002994 raw material Substances 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
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- 229910052799 carbon Inorganic materials 0.000 description 2
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- 239000002910 solid waste Substances 0.000 description 2
- TVEXGJYMHHTVKP-UHFFFAOYSA-N 6-oxabicyclo[3.2.1]oct-3-en-7-one Chemical compound C1C2C(=O)OC1C=CC2 TVEXGJYMHHTVKP-UHFFFAOYSA-N 0.000 description 1
- 238000004177 carbon cycle Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
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Classifications
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- 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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C1/00—Working-up tar
-
- 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
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/133—Renewable energy sources, e.g. sunlight
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a device and a method for extracting tar and biomass oil from biomass pyrolysis gas, wherein the device comprises a first carbonization box, a second carbonization box connected with the first carbonization box, a third carbonization box connected with the second carbonization box, a condensation recovery device connected with the first carbonization box, and a high-temperature combustion box connected with the condensation recovery device, the second carbonization box and the third carbonization box, wherein the condensation recovery device comprises a first condensation chamber and a second condensation chamber. The invention collects tar and bio-oil in the mixed gas by a method of cooling and condensing the mixed gas in the condensing chamber by arranging two different condensing chambers, has the capability of collecting the tar and the bio-oil in a subarea manner, and two sets of different temperature cooling systems respectively control the temperatures of the first condensing chamber and the second condensing chamber, wherein the first condensing chamber and the second condensing chamber are both provided with pressurizing fans, so that the tar and the bio-oil are separated from the mixed gas by a condensing and pressurizing method.
Description
Technical Field
The invention relates to the technical field of extraction of tar and bio-oil, in particular to a device and a method for extracting tar and bio-oil from biomass pyrolysis gas.
Background
The amount of waste biomass such as crop straws, forestry wastes and the like in China is large and wide, and the traditional treatment methods such as local burning, landfill and the like not only pollute the environment, but also cause resource waste. The biomass solid waste has the characteristics of wide sources and recycling, and the waste biomass is converted into biomass oil, biomass charcoal and heat energy, so that the method is a green development road capable of fixing carbon, reducing emission and recycling resources. As the only renewable energy source capable of being directly converted into liquid fuels, biomass has attracted global attention due to its advantages of huge production, storage, and carbon cycle. Renewable biomass resources are converted into clean high-grade liquid fuel to partially replace petroleum, so that the excessive dependence on limited petroleum resources can be eliminated, the emission of pollutants and greenhouse gases can be greatly reduced, the environment is improved, and the ecology is protected.
Pyrolysis gas, tar, bio-oil and the like can be generated in the biomass carbonization process, the bio-oil can be recycled, and the main technology of domestic and bio-oil is to condense cold shock gas for high-temperature pyrolysis and then separate particles and bio-oil; or the cracking gas is classified and condensed by cold shock gas to collect the bio-oil, the problems of unstable quality, low heat value, high tar content and the like of the bio-oil generally exist in the process, and the popularization and the application of the bio-oil are influenced.
The development of efficient and environment-friendly equipment for extracting the high-purity bio-oil is beneficial to the realization of the aim of recycling the agricultural and forestry solid wastes in China.
Disclosure of Invention
The invention aims to solve the problems in the prior art, provides a device for extracting tar and biomass oil from biomass pyrolysis gas, and can effectively solve the problems in the background technology.
In order to achieve the purpose, the technical scheme of the invention is as follows:
draw device of tar and bio-oil in follow living beings pyrolysis gas, the device includes first carbomorphism case, the second carbomorphism case that links to each other with first carbomorphism case, the third carbomorphism case that links to each other with the second carbomorphism case, the condensation recovery unit who links to each other with first carbomorphism case and the high temperature combustion case that all links to each other with condensation recovery unit, second carbomorphism case and third carbomorphism case, condensation recovery unit includes first condensation chamber and second condensation chamber, first condensation chamber includes interior condensation chamber and outer condensation chamber, the second condensation chamber is located first condensation chamber top.
As preferred, the inside cavity of interior condensation chamber just is provided with gas delivery pipe, is provided with a plurality of condensation sheets on the lateral wall, outer condensation chamber comprises a plurality of corrugated sheet, outer condensation chamber lateral wall is "wavy" structure, the inside a plurality of condensation sheets and the oil collecting plate that is provided with of second condensation chamber, the oil collecting plate both ends are buckled, first carbomorphism case links to each other with condensation recovery unit, second carbomorphism case and third carbomorphism case, first carbomorphism case and high temperature combustion case all is in the same place through the pipe connection with second carbomorphism case, second carbomorphism case and third carbomorphism case.
Preferably, interior condensation chamber one end is sealed, and one end is opened, is provided with a plurality of gas outlets on the opening one end lateral wall, seals one end and is the top, and opening one end is the bottom, the gas outlet is put through with outer condensation chamber, outer condensation chamber top is provided with interface channel, interface channel and second condensation chamber put through.
Preferably, the condensation recovery device further comprises a first condensation chamber condenser, the first condensation chamber condenser is connected with the first condensation chamber, and the first condensation chamber condenser can enable the temperature of the first condensation chamber to be kept between 80 ℃ and 200 ℃.
Preferably, the condensation recovery device further comprises a second condensation chamber condenser, the second condensation chamber condenser is connected with the second condensation chamber, and the second condensation chamber condenser can keep the temperature of the second condensation chamber between 20 ℃ and 50 ℃.
Preferably, a tar storage chamber is arranged at the bottom of the first condensation chamber, a pressure sensor is arranged at the bottom of the tar storage chamber, the tar storage chamber is communicated with the inner condensation chamber and the outer condensation chamber, a connecting plate and an oil outlet hopper are arranged at the bottom of the inner condensation chamber, the connecting plate is communicated with the oil outlet hopper, and the outer edges of the connecting plate and the oil outlet hopper are both in a wave-shaped structure.
Preferably, a bio-oil storage chamber is arranged at the bottom of the second condensation chamber, the bio-oil storage chamber is communicated with the second condensation chamber, and a pressure sensor is arranged at the bottom of the bio-oil storage chamber.
Preferably, the condensation recovery device further comprises a tar storage tank and a bio-oil storage tank, wherein the tar storage tank and the bio-oil storage tank are respectively connected with the tar oil storage chamber and the bio-oil storage chamber, and the tar storage tank and the bio-oil storage tank are respectively provided with a centrifugal pump, an exhaust valve and an oil outlet pipe.
Preferably, a preheating cavity is further arranged between the high-temperature combustion box and the condensation recovery device, and an igniter is arranged at any position on the outer wall of the preheating cavity.
As preferred, the second carbomorphism case has a plurality of, first carbomorphism case, second carbomorphism case and the inside a plurality of carbomorphism nest of tubes that all are provided with of third carbomorphism incasement portion, the carbomorphism nest of tubes includes a plurality of carbomorphism pipes, the carbomorphism pipe quantity of every carbomorphism nest of tubes of group is the same, and arbitrary adjacent two sets of carbomorphism nest of tubes all link to each other, arbitrary carbomorphism pipe one end is provided with the motor, the inside screw rod propulsion shaft that is provided with of carbomorphism pipe, the motor links to each other with the screw rod propulsion shaft.
Preferably, a hot air pipeline is arranged between the first carbonization box and the second carbonization box, a plurality of pyrolysis gas discharge pipes are further arranged in the first carbonization box, the second carbonization box and the third carbonization box, and the pyrolysis gas discharge pipes are connected with the carbonization pipes.
Preferably, the high-temperature combustion box is connected with the second condensation chamber, an exhaust channel is arranged at the top of the high-temperature combustion box, igniters are arranged at any positions of the outer walls of the first carbonization box, the second carbonization box, the third carbonization box and the high-temperature combustion box, and temperature-sensitive probes are arranged at any positions of the inner walls of the first carbonization box, the second carbonization box, the third carbonization box and the high-temperature combustion box.
Preferably, the top of the connecting channel and the top of the second condensing chamber are both provided with one-way valves, and pressure sensors are arranged on any positions of the inner wall of the inner condensing chamber, the inner wall of the outer condensing chamber and the inner wall of the second condensing chamber.
Preferably, a pressurizing fan is arranged at the air inlet of the gas conveying pipe, the pressurizing fan is arranged at the top of the connecting channel, and the pressurizing fan at the top of the connecting channel is positioned above the one-way valve.
The device and the method for extracting tar and biomass oil from biomass pyrolysis gas comprise the following steps:
s1, preheating, namely preheating the first carbonization box through an igniter, and starting up when the temperature in the first carbonization box reaches 300-500 ℃;
s2, feeding, conveying the biomass material into a feed hopper through a conveying pipeline, and then falling into a carbonization tube group of a first carbonization box through the feed hopper;
s3, dehydrating and primarily carbonizing, wherein the biomass material is pushed at a certain speed through a screw rod pushing shaft, the temperature in the first carbonization tank reaches 300-500 ℃, and mixed gas is generated in the pushing process and comprises pyrolysis gas, tar, biological oil and the like;
s4, condensing tar for the first time, enabling the mixed gas to enter an inner condensing chamber of a condensation recovery device through a pipeline, enabling the temperature of the inner condensing chamber to be 80-200 ℃, enabling the tar to be condensed at a temperature lower than 200 ℃, enabling the tar to be condensed for the first time, and pressurizing through a pressurizing fan while condensing;
s5, condensing tar for the second time, enabling the mixed gas to enter an outer condensing chamber of a condensation recovery device through a gas outlet, enabling the temperature of the outer condensing chamber to be 80-200 ℃, enabling the tar to be condensed at a temperature lower than 200 ℃, enabling the tar to be condensed for the second time, and pressurizing through a pressurizing fan while condensing;
s6, condensing the bio-oil, enabling the mixed gas to enter a second condensing chamber of a condensation recovery device through a connecting channel, enabling the temperature of the second condensing chamber to be 20-50 ℃, enabling the bio-oil to be condensed at the temperature lower than 50 ℃, and pressurizing through a pressurizing fan while condensing;
and S7, burning, condensing and pressurizing the mixed gas, and feeding the mixed gas pipeline of the mixed gas into a high-temperature burning box for high-temperature burning.
Compared with the prior art, the invention has the following beneficial effects:
1. the invention collects tar and biological oil in the mixed gas by a method of cooling and condensing the mixed gas in the condensing chamber by arranging two different condensing chambers (a first condensing chamber and a second condensing chamber), and has the capacity of collecting the tar and the biological oil in a subarea manner.
2. The invention has two sets of different temperature cooling systems, which respectively control the temperature of the first condensing chamber and the second condensing chamber, can accurately control the temperature of the condensing chambers and separate tar and bio-oil from mixed gas.
3. The invention simultaneously adopts the methods of condensation liquefaction and pressurization liquefaction to recover the tar and the bio-oil, thereby improving the recovery rate of the tar and the bio-oil.
4. The mixed gas condensed by the condensing chamber enters the high-temperature combustion box from the condensing chamber to be combusted and converted into heat energy.
Drawings
FIG. 1 is a first general structural diagram of the present invention;
FIG. 2 is a schematic view of the internal structure of the present invention;
FIG. 3 is a schematic view of the overall structure of the present invention;
FIG. 4 is a partial cross-sectional view of the first embodiment of the present invention;
FIG. 5 is a partial cross-sectional view of the invention and a schematic gas flow;
FIG. 6 is a schematic view of the structure of the condensing unit of the present invention;
FIG. 7 is a schematic view of the construction of the external condensation chamber of the present invention;
FIG. 8 is a schematic view of the internal condensation chamber of the present invention;
FIG. 9 is an arrangement of internal condensation chambers according to the present invention;
FIG. 10 is a schematic view of the internal structure of a second condensation chamber according to the present invention;
FIG. 11 is a schematic view of the structure of a carbonization tube group according to the invention;
FIG. 12 is a cross-sectional view of a charring tube of the present invention.
In the figure: 1-first carbonization tank, 2-second carbonization tank, 3-third carbonization tank, 4-high temperature combustion tank, 5-first condensation chamber, 6-second condensation chamber, 7-inner condensation chamber, 8-outer condensation chamber, 9-gas conveying pipe, 10-condensation sheet, 11-corrugated plate, 12-oil collecting plate, 13-gas outlet, 14-connecting channel, 15-first condensation chamber condenser, 16-second condensation chamber condenser, 17-tar storage chamber, 18-connecting plate, 19-oil outlet hopper, 20-biological oil storage chamber, 21-tar storage tank, 22-biological oil storage tank, 23-centrifugal pump, 24-exhaust valve, 25-oil outlet pipe, 26-preheating cavity, 27-carbonization pipe, 28-motor, 29-screw rod pushing shaft, 30-pyrolysis gas discharge pipe, 31-exhaust port, 32-hot air pipeline, 33-exhaust pipeline, 34-igniter, 35-temperature sensing probe, 36-hot air pipeline, 37-flue gas pipeline, 38-feed hopper, 39-biochar transmission pipeline, 40-check valve, 41-pressurizing fan and 100-carbonization tube group.
The features and advantages of the present invention will be described in detail by embodiments in conjunction with the accompanying drawings.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is described in further detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention; furthermore, unless expressly stated or limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, as they may be fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements.
The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the application. Unless defined otherwise, technical or scientific terms used herein shall have the ordinary meaning as understood by one of ordinary skill in the art to which this invention belongs. The use of the terms "a" or "an" and the like in the description and in the claims of this application do not denote a limitation of quantity, but rather denote the presence of at least one. "plurality" includes two, and is equivalent to at least two. The word "comprising" or "comprises", and the like, means that the element or item listed as preceding "comprising" or "includes" covers the element or item listed as following "comprising" or "includes" and its equivalents, and does not exclude other elements or items. The terms "connected" or "coupled" and the like are not restricted to physical or mechanical connections, but may include electrical connections, whether direct or indirect. As used in this specification and the appended claims, the singular forms "a", "an", and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise. It should also be understood that the term "and/or" as used herein refers to and encompasses any and all possible combinations of one or more of the associated listed items. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Example 1:
as shown in fig. 1-12, the device for extracting tar and bio-oil from biomass pyrolysis gas comprises a first carbonization tank 1, a second carbonization tank 2 connected with the first carbonization tank 1, a third carbonization tank 3 connected with the second carbonization tank 2, a condensation recovery device connected with the first carbonization tank 1, and a high temperature combustion tank 4 connected with the condensation recovery device and the second carbonization tank 2 and the third carbonization tank 3, wherein the first carbonization tank 1, the second carbonization tank 2, the third carbonization tank 3, the first carbonization tank 1, the condensation recovery device, the second carbonization tank 2, the third carbonization tank 3 and the high temperature combustion tank 4 are all connected together through a pipeline, the condensation recovery device comprises a first condensation chamber 5 and a second condensation chamber 6, the first condensation chamber 5 comprises an inner condensation chamber 7 and an outer condensation chamber 8, the second condensation chamber 6 is located at the top of the first condensation chamber 5, wherein the first carbonization tank 1, the second carbonization tank 2 and the third carbonization tank 3 are all places for biomass carbonization, the condensation recovery device is used for extracting tar and bio-oil in mixed gas, the high-temperature combustion tank 4 is used for combusting redundant mixed gas to convert the cracked gas in the mixed gas into heat energy, the inner condensation chamber 7 is hollow and is provided with a gas conveying pipe 9, the first carbonization tank 1 is connected with the inner condensation chamber 7 through a pipeline, the side wall is provided with a plurality of condensation sheets 10, the outer condensation chamber 8 is composed of a plurality of corrugated plates 10, the side wall of the outer condensation chamber 8 is of a wave-shaped structure, the wave-shaped concave-convex fluctuation is formed, the cooling area of the outer condensation chamber 8 is increased, thereby the cooling area of the tar in the outer condensation chamber 8 is increased, the tar is condensed in the outer condensation chamber 8 as much as possible, the second condensation chamber 6 is internally provided with a plurality of condensation sheets 10 and oil collecting plates 12, 12 both ends of oil collecting plate are buckled, condensation piece 10 is located oil collecting plate 12, 7 one end in the condensation chamber is sealed, one end opening, be provided with a plurality of gas outlets 13 on the opening one end lateral wall, gas outlet 13 and the 8 switch-ons of outer condensation chamber, 8 tops in outer condensation chamber are provided with connecting channel 14, connecting channel 14 and the 6 switch-ons of second condensation chamber, second condensation chamber 6 passes through the pipe connection with high temperature combustion box 4 and is in the same place, second condensation chamber 6 is located 5 tops in first condensation chamber, wherein first condensation chamber 5 is used for the condensation of tar to collect, tar has twice condensation to collect the process, go on in condensation chamber 7 and outer condensation chamber 8 including respectively, second condensation chamber 6 is used for the condensation of bio-oil to collect.
In this embodiment, the condensation recovery device further includes a first condensing chamber condenser 15, the first condensing chamber condenser 15 is connected to the condensing sheet 10 in the first condensing chamber 5, the first condensing chamber condenser 15 can control the temperature of the condensing sheet 10, so that the temperature of the condensing sheet 10 is maintained between 80 ℃ and 200 ℃, so that the temperature of the first condensing chamber 5 is maintained between 80 ℃ and 200 ℃, the temperatures of the inner condensing chamber 7 and the outer condensing chamber 8 are both maintained between 80 ℃ and 200 ℃, tar is very sensitive to temperature, and starts to condense into liquid when the temperature is lower than 200 ℃, and tar in the mixed gas is condensed into liquid drops when encountering condensation on the inner wall of the inner condensing chamber 7, on the condensing sheet 10 and on the corrugated board 10 of the outer condensing chamber 8.
In this embodiment, the condensation recovery device further includes a second condensation chamber condenser 16, the second condensation chamber condenser 16 is connected to the condensation sheet 10 in the second condensation chamber 6, the second condensation chamber condenser 16 can control the temperature of the condensation sheet 10, so that the temperature of the condensation sheet 10 is maintained between 20 ℃ and 50 ℃, so that the temperature of the second condensation chamber 6 is maintained between 20 ℃ and 50 ℃, the bio-oil starts to condense into liquid under the condition that the bio-oil is lower than 50 ℃, and the bio-oil in the mixed gas meets the condensation on the inner wall of the second condensation chamber 6 and the condensation sheet 10 and condenses into liquid drops.
In this embodiment, a tar storage chamber 17 is disposed at the bottom of the first condensation chamber 5, a pressure sensor (not labeled in the figure) is disposed at the bottom of the tar storage chamber 17, the tar storage chamber 17 is communicated with the inner condensation chamber 7 and the outer condensation chamber 8, a connection plate 18 and an oil outlet bucket 19 are disposed at the bottom of the inner condensation chamber 7, the connection plate 18 is communicated with the oil outlet bucket 19, outer edges of the connection plate 18 and the oil outlet bucket 19 are both in a "wave" structure, the "wave" structure of the outer condensation chamber 8 is used in cooperation with the "wave" structure of the connection plate 18 and the oil outlet bucket 19, tar flows into the tar storage chamber 17 along the wall of the outer condensation chamber 8, the connection plate 18 and the oil outlet bucket 19, the bio-oil storage chamber 20 is communicated with the second condensation chamber 6, a pressure sensor (not labeled in the figure) is disposed at the bottom of the bio-oil storage chamber 20, the condensate recovery apparatus further includes a tar storage tank 21 and a bio-oil storage tank 22, the tar storage tank 21 and the bio-oil storage tank 22 are respectively connected with the tar storage chamber 17 and the bio-oil storage chamber 20 through pipes, the tar storage tank 21 and the bio-oil storage tank 22 are respectively provided with a centrifugal pump 23, an exhaust valve 24 and an oil outlet pipe 25, wherein the tar storage chamber 17 and the bio-oil storage chamber 20 are used for temporarily storing tar and bio-oil generated by condensation, the condensed tar drops into the tar storage chamber 17 along the condensation sheet 10 and the corrugated plate 10, the condensed bio-oil drops onto the oil collecting plate 12 along the condensation sheet 10 and then enters the bio-oil storage chamber 20 through the oil collecting plate 12, one end of the oil collecting plate 12 is bent upwards, the other end is bent downwards, and the bent section of the oil collecting plate 12 upwards prevents the bio-oil from flowing out from the end, so that the bio-oil drops into the bio-oil storage chamber 20 from the bent end of the oil collecting plate 12 downwards; the pressure sensor is connected with the computer host, a certain value is set, when the weight of the tar storage chamber 17 or the bio-oil storage chamber 20 exceeds 1.5kg, the pressure sensor transmits a signal to the computer host, the computer host controls the centrifugal pump 23 to work, tar or bio-oil in the tar storage chamber 17 or the bio-oil storage chamber 20 is pumped into the tar storage tank 21 or the bio-oil storage tank 22, and the tar or the bio-oil in the tar storage tank 21 or the bio-oil storage tank 22 is conveyed to the boiler through the oil outlet pipe 25 to be used as fuel or used as a raw material of other products; the vent valve 24 serves to equalize the gas pressure in the tar storage tank 21.
In this embodiment, the top of the connecting channel 14 and the top of the second condensing chamber 6 are both provided with a check valve 40, pressure sensors (not marked in the figure) are arranged at any positions of the inner walls of the inner condensing chamber 7, the outer condensing chamber 8 and the second condensing chamber 6, a pressurizing fan 41 is arranged at the air inlet of the gas conveying pipe 9, the top of the connecting channel 14 is provided with the pressurizing fan 41, the pressurizing fan 41 in the connecting channel 14 is positioned above the check valve 40, specifically, the pressure sensors are connected with a computer host, the check valve 40 is controlled by the computer host, the pressure sensors can transmit data to the computer host, the pressure sensors are provided with predetermined values, when the predetermined value in the first condensing chamber 5 and the second condensing chamber 6 exceeds 3kg, the computer host controls the check valve 40 to open, so that the gas can be unblocked, the pressurizing fans 41 in the first condensing chamber 5 and the second condensing chamber 6 have the function of pressurizing and liquefying functions and also increase the first condensing chamber 5 and the second condensing chamber 6 The effect of the gas pressure in the condensing chamber 6 is pressurized by the pressurizing fan 41, so that the one-way valve 40 can be opened, the setting of the one-way valve 40 increases the liquefaction time of the mixed gas, the mixed gas is condensed and liquefied while being pressurized and liquefied, and the recovery rate of tar and bio-oil is increased.
In this embodiment, a preheating chamber 26 is further provided between the high-temperature combustion box 4 and the condensation recovery device, an igniter 34 is provided at any position on the outer wall of the preheating chamber 26, the temperature of the condensed mixed gas becomes very low, and the mixed gas is required to be preheated again when entering the high-temperature combustion box 4, and at this time, a small amount of tar and bio-oil may be mixed in the mixed gas, so that the mixed gas needs to be heated again, so that the tar and the bio-oil can be in a gas state, and the tar and the bio-oil are prevented from being condensed in a pipeline.
In this embodiment, there are several second carbonization boxes 2, several carbonization tube groups 100 are disposed inside the first carbonization box 1, the second carbonization box 2 and the third carbonization box 3, each carbonization tube group 100 includes several carbonization tubes 27, the number of the carbonization tubes 27 of each carbonization tube group 100 is the same, and any two adjacent carbonization tube groups 100 are connected, one end of any carbonization tube 27 is provided with a motor 28, a screw pushing shaft 29 is disposed inside the carbonization tube 27, the motor 28 is connected with the screw pushing shaft 29, and the rotation speed of the motor 28 is adjustable, wherein the carbonization tube group 100 in the first carbonization box 1 is connected with a feed hopper 38, the carbonization tube group 100 in the third carbonization box 3 is connected with a biological carbon transmission pipeline 39, specifically, the first carbonization box 1 is a place for preliminary carbonization of biomass material, the second carbonization box 2 is a place for main carbonization of biomass material, the third carbonization box 3 is a place for supplementary carbonization or temperature reduction, the biomass material all can produce a certain amount of mist when in the carbonization of three carbonization casees, mist includes pyrolysis gas, tar and biological oil etc., feeder hopper 38 is used for the feeding of biomass material, biological charcoal transmission pipeline 39 is used for transporting the biomass charcoal that produces at last, biomass material can impel in carbomorphism pipe 27 through motor 28 and screw rod propulsion shaft 29, can receive high temperature toast when biomass material impels in carbomorphism pipe 27 among first carbonization case 1, second carbonization case 2 and third carbonization case 3 to begin the carbomorphism, biological charcoal transmission pipeline 39 inner structure is unanimous with carbomorphism pipe 27, is used for transmitting the biological charcoal.
In this embodiment, a hot air pipeline 32 is disposed between the first carbonization box 1 and the second carbonization box 2, the first carbonization box 1, the inside of the second carbonization box 2 and the third carbonization box 3 are further provided with a plurality of cracked gas discharge pipes 30, the cracked gas discharge pipes 30 are connected with the carbonization pipes 27, a plurality of exhaust ports 31 are disposed on the cracked gas discharge pipes 30 in the second carbonization box 2 and the third carbonization box 3, wherein the hot air pipeline 32 is used for connecting the first carbonization box 1 and the second carbonization box 2, the mixed gas and heat in the second carbonization box 2 can enter the second carbonization box 2 through the hot air pipeline 32, and the mixed gas generated in the first carbonization box 1, the second carbonization box 2 and the third carbonization box 3 directly enters the condensation recovery device through the pipeline in the cracked gas discharge pipes 30 or enters the second carbonization box 2 and the third carbonization box 3.
In the embodiment, the high temperature combustion box 4 is connected with the second condensation chamber 6, the top of the high temperature combustion box 4 is provided with an exhaust passage, any position of the outer walls of the first carbonization box 1, the second carbonization box 2, the third carbonization box 3 and the high temperature combustion box 4 is provided with an igniter 34, any position of the inner walls of the first carbonization box 1, the second carbonization box 2, the third carbonization box 3 and the high temperature combustion box 4 is provided with a temperature-sensitive probe 35, wherein, some firearm 34 can be for first carbomorphism case 1, second carbomorphism case 2, third carbomorphism case 3 and high temperature combustion case 4 ignition preheat, and the temperature that the temperature is felt probe 35 and can detect first carbomorphism case 1, second carbomorphism case 2, third carbomorphism case 3 and high temperature combustion case 4 box inside feels the probe and can give the computer with the temperature transmission who detects, and the high temperature combustion case 4 burns almost no gas or heat energy and discharges in the air through exhaust passage.
In this embodiment, first carbomorphism case 1, second carbomorphism case 2, third carbomorphism case 3 and high temperature combustion case 4 all are provided with admission line 36, and the natural gas provides the energy of burning for first carbomorphism case 1, second carbomorphism case 2, third carbomorphism case 3 and high temperature combustion case 4 in entering into first carbomorphism case 1, second carbomorphism case 2, third carbomorphism case 3 and high temperature combustion case 4 from admission line 36.
In this embodiment, the top of the first carbonization tank 1, the second carbonization tank 2 and the third carbonization tank 3 is further provided with a flue gas pipeline 37, the cracked gas discharge pipe 30 in the first carbonization tank 1 is directly communicated with the flue gas pipeline 37, wherein one end of the pipeline connecting the first carbonization tank 1 and the condensing device is connected to the flue gas pipeline 37 of the first carbonization tank 1, and the other end is connected to the gas delivery pipe 9 of the inner condensation chamber 7; one end of a pipeline connecting the second carbonization box 2 and the high-temperature combustion box 4 is connected to the flue gas pipeline 37 of the second carbonization box 2, and the other end is connected to the high-temperature combustion box 4; one end of the pipeline connecting the third carbonization tank 3 and the high-temperature combustion tank 4 is connected to the flue gas pipeline 37 of the third carbonization tank 3, and the other end is connected to the high-temperature combustion tank 4.
In this embodiment, the hot air duct 32, the exhaust duct 33, the air inlet duct 36 and the smoke duct 37 are all provided with valves (not labeled in the figure), the valves are controlled by the computer host and can be automatically opened or closed, the temperature-sensitive probe 35 sets a certain value, and when the set value is exceeded, the computer host can control the hot air duct 32, the exhaust duct 33, the air inlet duct 36 and the smoke duct 37 to be opened.
Example 2:
the device and the method for extracting tar and biomass oil from biomass pyrolysis gas comprise the following steps:
s1, preheating, namely preheating the first carbonization box 1 through the igniter 34, and starting when the temperature in the first carbonization box 1 reaches 300-500 ℃;
s2, feeding, conveying the biomass material into the feed hopper 38 through a conveying pipeline, and then dropping the biomass material into the carbonization tube group 100 of the first carbonization box 1 through the feed hopper 38;
s3, dehydrating and primarily carbonizing, wherein the biomass material is pushed at a certain speed through a screw rod pushing shaft 29, the temperature in the first carbonization box 1 reaches 300-500 ℃, and mixed gas is generated in the pushing process and comprises pyrolysis gas, tar, biological oil and the like;
s4, condensing tar for the first time, enabling the mixed gas to enter an inner condensing chamber 7 of a condensation recovery device through a pipeline, enabling the temperature of the inner condensing chamber 7 to be 80-200 ℃, enabling the tar to be condensed at a temperature lower than 200 ℃, enabling the tar to be condensed for the first time when meeting the condensation, and pressurizing through a pressurizing fan 41 while condensing;
s5, condensing tar for the second time, enabling the mixed gas to enter an outer condensing chamber 8 of the condensation recovery device through a gas outlet 13, enabling the temperature of the outer condensing chamber 8 to be 80-200 ℃, enabling the tar to be condensed at a temperature lower than 200 ℃, enabling the tar to be condensed for the second time, and pressurizing through a pressurizing fan 41 while condensing;
s6, condensing the bio-oil, enabling the mixed gas to enter a second condensation chamber 6 of the condensation recovery device through a connecting channel 14, enabling the temperature of the second condensation chamber 6 to be 20-50 ℃, enabling the bio-oil to be condensed at the temperature lower than 50 ℃, and pressurizing through a pressurizing fan 41 while condensing;
and S7, the mixed gas pipeline of the mixed gas after combustion, condensation and pressurization enters the high-temperature combustion box 4 for high-temperature combustion.
Example 3:
the working principle of the embodiment 1 is as follows:
after the equipment is ready for starting, a main power supply of the equipment is started, a self-checking program is started, after the self-checking is finished, an igniter 34 is started to ignite to preheat a first carbonization box 1 and a second carbonization box 2, the ignition weather of the igniter 34 is used as a heat source, natural gas enters the first carbonization box 1 and the second carbonization box 2 from an air inlet pipeline 36, when the temperatures of the first carbonization box 1 and the second carbonization box 2 rise to about 300-500 ℃, a temperature sensing probe 35 detects the temperature and transmits a preheating finishing signal to an equipment host, the host computer sends a starting ignition instruction, and the equipment carbonization system runs completely according to preset carbonization index parameters.
Firstly, a biomass material is input into a feed hopper 38 through a transmission pipeline and enters a carbonization pipe 27 from the feed hopper 38, the biomass material enters a first carbonization box 1 at a constant speed under the action of a screw pushing shaft 29 of the carbonization pipe 27 and a motor 28, at the moment, the temperature in the first carbonization box 1 is about 300-500 ℃, the biomass material can be continuously roasted in the propelling process, the biomass material can release a large amount of moisture and mixed gas during continuous roasting, the mixed gas comprises pyrolysis gas, tar, biological oil and the like, the pyrolysis gas in a mixed gas discharge pipe 30 in the mixed gas pyrolysis gas is not released in the first carbonization box 1, the mixed gas generated in the first carbonization box 1 is directly transmitted to a condensation recovery device through a pipeline for condensation reaction, a computer host controls a valve in a flue gas pipeline 37 in the first carbonization box 1 to be opened, and the mixed gas directly enters the flue gas pipeline 37 from the pyrolysis gas discharge pipe 30, then the gas enters a gas conveying pipe 9 through a flue gas pipeline 37 and a pipeline, finally the gas enters an inner condensing chamber 7 from the gas conveying pipe 9 for condensation reaction, at the moment, the temperature of the inner condensing chamber 7 is controlled to be 80-200 ℃ by a first condensing chamber condenser 15, tar in hot mixed gas is condensed by the inner condensing chamber 7, the tar is condensed into liquid under the condition that the temperature is lower than 200 ℃ because the tar is very sensitive to the temperature, the liquid is pressurized and liquefied by a pressurizing fan 41 in the condensation process, the mixed gas is subjected to first tar condensation in the inner condensing chamber 7, and the condensed tar is guided to flow into a tar storage chamber 17 along the inner wall of the inner condensing chamber 7 or a condensing sheet 10 for temporary storage; the mixed gas passing through the inner condensation chamber 7 enters the outer condensation chamber 8 through the gas outlet 13 to be condensed again, the temperature of the outer condensation chamber 8 is controlled to be 80-200 ℃ by the first condensation chamber condenser 15, the mixed gas is condensed into liquid under the condition of being lower than 200 ℃, the liquid is pressurized and liquefied by the pressurizing fan 41 in the condensation process, tar can be condensed on the corrugated board 10 and dripped into the tar storage chamber 17 along the corrugated board 10 to be temporarily stored, when the weight of the tar in the tar storage chamber 17 reaches 1.5kg, the mixed gas is pumped into the tar storage tank 21 through the guide pipe by the pressure sensor control centrifugal pump 23, and then is conveyed to a boiler by the oil outlet pipe 25 to be used as fuel or used as raw materials of other products.
When the preset value of the pressure sensor in the first condensation chamber 5 exceeds 3kg, the check valve 40 in the connecting channel 14 is opened, the gas exhausted from the first condensation chamber 5, namely the outer condensation chamber 7 is led to the second condensation chamber 6 through the connecting channel 14 to enter the second condensation chamber 6 for condensation of the bio-oil, the temperature of the second condensation chamber 6 is controlled to be 20-50 ℃ by the second condensation chamber condenser 15, the bio-oil is condensed into liquid under the condition of lower than 50 ℃, the bio-oil is pressurized and liquefied by the pressurizing fan 41 while being condensed, the bio-oil in the hot mixed gas is condensed by secondary condensation and pressurization, the effective separation of corresponding components in the hot mixed gas is realized, the obtained bio-oil drops through the condensation sheets 10 to be collected in the oil collecting plate 12 and flows into the bio-oil storage chamber 20 for temporary storage, when the weight of the bio-oil in the bio-oil storage chamber 20 reaches 1.5kg, a centrifugal pump 23 is controlled by a pressure sensor to be pumped into a bio-oil storage tank 22 through a bio-oil guide pipe, and then the bio-oil is conveyed to a boiler through an oil outlet pipe 25 to be used as fuel or used as raw materials of other products, most of mixed gas condensed by a first condensation chamber 5 and a second condensation chamber 6 is pyrolysis gas, when the preset value of the pressure sensor in the second condensation chamber 6 exceeds 3kg, a one-way valve 40 leading to a high-temperature combustion box 4 is opened, the pyrolysis gas enters the high-temperature combustion box 4 from the second condensation chamber 6 through a pipeline to be combusted, heat energy generated in the high-temperature combustion box 4 is 1000-1200 ℃, the heat energy can be converted into steam or generated electricity after being recovered, the heat energy firstly passes through a preheating cavity 26 before entering the high-temperature combustion box 4, the preheating cavity 26 is preheated, and an igniter 34 can ignite the preheating cavity 26.
After a plurality of minutes, the dried biomass material in the first carbonization box 1 enters the second carbonization box 2 through the pipeline (the second carbonization box 2 has two layers), the preheating temperature of the second carbonization box 2 is 300-500 ℃, the biomass material is baked to continuously release a large amount of pyrolysis gas in the advancing process, the pyrolysis gas enters the pyrolysis gas discharge pipe 30 from the carbonization pipe 27, then directly enters the second carbonization box 2 from the exhaust port 31 on the pyrolysis gas discharge pipe 30 to provide part of combustible gas for the continuous combustion in the second carbonization box 2, the pyrolysis gas starts to burn after reaching a preset concentration, the internal temperature of the second carbonization box 2 rises to 600-1000 ℃ instantly, the igniter 34 of the second carbonization box 2 stops igniting, the computer host controls the opening of the valve in the hot air pipeline 3, the hot air generated by the combustion of the pyrolysis gas enters the first carbonization box 1 from the second carbonization box 2 through the hot air pipeline 32, continuously providing a heat source for the first carbonization box 1, keeping the temperature in the first carbonization box 1 at 300-500 ℃ all the time, and stopping ignition of the igniter 34 of the first carbonization box 1; the biomass material entering the second carbonization box 2 continues to be pushed at a constant speed in the carbonization tube 27, anaerobic carbonization is started under the action of 600-1000 ℃, the biomass material enters the second layer of the second carbonization box 2 from the first layer of the second carbonization box 2 through the second blanking tube, anaerobic carbonization is continued, pyrolysis gas is continuously released for combustion, and redundant pyrolysis gas and heat energy enter the high-temperature combustion box 4 through the flue gas pipeline 37 for combustion.
When the incompletely reacted biomass material and biomass charcoal enter the third carbonization box 3 through the pipeline, because the temperature of the biomass material in the third carbonization box 3 is higher, the temperature of the biomass material in the third carbonization box 3 can not drop at a moment, a certain amount of pyrolysis gas can be continuously released from the biomass material propelled in the third carbonization box 3, at the moment, the third carbonization box 3 has the functions of supplementing carbonization and cooling, the pyrolysis gas enters the pyrolysis gas discharge pipe 30 from the carbonization pipe 27, then directly enters the third carbonization box 3 from the exhaust port 31 on the pyrolysis gas discharge pipe 30 to provide part of combustible gas for continuous combustion in the third carbonization box 3, the igniter 34 ignites the pyrolysis gas, the pyrolysis gas starts to combust, so that the temperature of the third carbonization box 3 is kept at about 200-400 ℃, and the redundant pyrolysis gas enters the high-temperature combustion box 4 through the flue gas pipeline 37, after the biomass material is completely carbonized into the biochar at the bottom layer of the third carbonization box 3, the biochar material finally enters the biochar transmission pipeline 39 from the carbonization pipe 27 at the bottom layer of the third carbonization box 3 to be mixed together, and then is conveyed to the storage tank to be stored in an oxygen-free sealing manner.
Example 4:
the rest of this embodiment is the same as embodiment 3, the difference lies in, the biomass material has been carbonized completely in second carbomorphism case 2, when the biomass material of complete carbonization enters into third carbomorphism case 3, because the biomass material of complete carbonization can not release the pyrolysis gas at propulsive in-process, this moment the firearm is out of work, third carbomorphism case 3 just can not start, third carbomorphism case 3 only plays the effect of cooling this moment, the temperature that flows living beings charcoal and gives off in carbomorphism pipe 27 is about 200 ~ 300 ℃, through the propulsion of a period of time, the temperature of living beings charcoal can begin to descend, it is in the same place to enter into biological charcoal transmission pipeline 39 from the carbomorphism pipe 27 group of three carbomorphism casees bottommost at last, then carry the anaerobic seal storage of storage tank.
The foregoing shows and describes the general principles and broad features of the present invention and advantages thereof. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, which are described in the specification and illustrated only to illustrate the principle of the present invention, but that various changes and modifications may be made therein without departing from the spirit and scope of the present invention, which fall within the scope of the invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (15)
1. Draw device of tar and bio-oil in follow living beings pyrolysis gas, a serial communication port, the device includes first carbomorphism case, the second carbomorphism case that links to each other with first carbomorphism case, the third carbomorphism case that links to each other with the second carbomorphism case, the condensation recovery unit who links to each other with first carbomorphism case and the high temperature combustion case that all links to each other with condensation recovery unit, second carbomorphism case and third carbomorphism case, condensation recovery unit includes first condensation chamber and second condensation chamber, first condensation chamber includes interior condensation chamber and outer condensation chamber, the second condensation chamber is located first condensation chamber top.
2. The device for extracting tar and bio-oil from biomass pyrolysis gas as claimed in claim 1, wherein the inner condensation chamber is hollow and provided with a gas delivery pipe, a plurality of condensation sheets are arranged on the side wall, the outer condensation chamber is composed of a plurality of corrugated plates, the side wall of the outer condensation chamber is in a wave-like structure, and a plurality of condensation sheets and oil collection plates are arranged inside the second condensation chamber.
3. The device for extracting tar and biomass oil from biomass pyrolysis gas as claimed in claim 2, wherein one end of the inner condensation chamber is sealed, the other end is open, a plurality of air outlets are arranged on the side wall of the open end, the air outlets are communicated with the outer condensation chamber, a connecting channel is arranged at the top of the outer condensation chamber, and the connecting channel is communicated with the second condensation chamber.
4. The device for extracting tar and biomass oil from biomass pyrolysis gas as claimed in claim 3, wherein the condensation recovery device further comprises a first condensation chamber condenser, the first condensation chamber condenser is connected with the first condensation chamber, and the first condensation chamber condenser can keep the temperature of the first condensation chamber between 80 ℃ and 200 ℃.
5. The device for extracting tar and biomass oil from biomass pyrolysis gas as claimed in claim 3, wherein the condensation recovery device further comprises a second condensation chamber condenser, the second condensation chamber condenser is connected with the second condensation chamber, and the second condensation chamber condenser can keep the temperature of the second condensation chamber between 20 ℃ and 50 ℃.
6. The device for extracting tar and biomass oil from biomass pyrolysis gas as claimed in claim 4, wherein the bottom of the first condensation chamber is provided with a tar storage chamber, the bottom of the tar storage chamber is provided with a pressure sensor, the tar storage chamber is communicated with the inner condensation chamber and the outer condensation chamber, the bottom of the inner condensation chamber is provided with a connecting plate and an oil outlet bucket, the connecting plate is communicated with the oil outlet bucket, and the outer edges of the connecting plate and the oil outlet bucket are both in a wave-shaped structure.
7. The device for extracting tar and bio-oil from biomass pyrolysis gas according to claim 5, wherein a bio-oil storage chamber is arranged at the bottom of the second condensation chamber, the bio-oil storage chamber is communicated with the second condensation chamber, and a pressure sensor is arranged at the bottom of the bio-oil storage chamber.
8. The device for extracting tar and bio-oil from biomass pyrolysis gas as claimed in claim 7, wherein the condensation recovery device further comprises a tar storage tank and a bio-oil storage tank, the tar storage tank and the bio-oil storage tank are respectively connected with the tar oil storage chamber and the bio-oil storage chamber, and the tar storage tank and the bio-oil storage tank are respectively provided with a centrifugal pump, an exhaust valve and an oil outlet pipe.
9. The device for extracting tar and biomass oil from biomass pyrolysis gas as claimed in claim 8, wherein a preheating chamber is further arranged between the high temperature combustion box and the condensation recovery device, and an igniter is arranged at any position on the outer wall of the preheating chamber.
10. The device for extracting tar and biomass oil from biomass pyrolysis gas according to claim 8 or 9, wherein the number of the second carbonization boxes is several, the first carbonization box, the second carbonization box and the third carbonization box are all provided with a plurality of carbonization tube groups, each carbonization tube group comprises a plurality of carbonization tubes, the number of the carbonization tubes of each carbonization tube group is the same, any two adjacent carbonization tube groups are connected, one end of any carbonization tube is provided with a motor, a screw rod propulsion shaft is arranged in each carbonization tube, and the motor is connected with the screw rod propulsion shaft.
11. The apparatus of claim 10, wherein a hot air duct is disposed between the first carbonization tank and the second carbonization tank, a plurality of pyrolysis gas discharge pipes are disposed inside the first carbonization tank, the second carbonization tank, and the third carbonization tank, and the pyrolysis gas discharge pipes are connected to the carbonization pipes.
12. The device for extracting tar and biomass oil from biomass pyrolysis gas as claimed in claim 11, wherein the high temperature combustion box is connected with the second condensation chamber, the top of the high temperature combustion box is provided with an exhaust passage, any position of the outer walls of the first carbonization box, the second carbonization box, the third carbonization box and the high temperature combustion box is provided with an igniter, and any position of the inner walls of the first carbonization box, the second carbonization box, the third carbonization box and the high temperature combustion box is provided with a temperature-sensing probe.
13. The device for extracting tar and biomass oil from biomass pyrolysis gas as claimed in claim 12, wherein the top of the connecting channel and the top of the second condensation chamber are both provided with one-way valves, and the inner wall of the inner condensation chamber, the outer condensation chamber and the inner wall of the second condensation chamber are provided with pressure sensors at any position.
14. The device for extracting tar and bio-oil from biomass pyrolysis gas as claimed in claim 13, wherein a pressure fan is arranged at the gas inlet of the gas delivery pipe, the top of the connecting channel is provided with the pressure fan, and the pressure fan at the top of the connecting channel is positioned above the one-way valve.
15. The apparatus and method for extracting tar and bio-oil from pyrolysis gas of biomass according to claim 14, wherein the extraction method comprises:
s1, preheating, namely preheating the first carbonization box through an igniter, and starting up when the temperature in the first carbonization box reaches 300-500 ℃;
s2, feeding, conveying the biomass material into a feed hopper through a conveying pipeline, and then falling into a carbonization tube group of a first carbonization box through the feed hopper;
s3, dehydrating and primarily carbonizing, wherein the biomass material is pushed at a certain speed through a screw rod pushing shaft, the temperature in the first carbonization tank reaches 300-500 ℃, and mixed gas is generated in the pushing process and comprises pyrolysis gas, tar, biological oil and the like;
s4, condensing tar for the first time, enabling the mixed gas to enter an inner condensing chamber of a condensation recovery device through a pipeline, enabling the temperature of the inner condensing chamber to be 80-200 ℃, enabling the tar to be condensed at a temperature lower than 200 ℃, enabling the tar to be condensed for the first time, and pressurizing through a pressurizing fan while condensing;
s5, condensing tar for the second time, enabling the mixed gas to enter an outer condensing chamber of a condensation recovery device through a gas outlet, enabling the temperature of the outer condensing chamber to be 80-200 ℃, enabling the tar to be condensed at a temperature lower than 200 ℃, enabling the tar to be condensed for the second time, and pressurizing through a pressurizing fan while condensing;
s6, condensing the bio-oil, enabling the mixed gas to enter a second condensing chamber of a condensation recovery device through a connecting channel, enabling the temperature of the second condensing chamber to be 20-50 ℃, enabling the bio-oil to be condensed at the temperature lower than 50 ℃, and pressurizing through a pressurizing fan while condensing;
and S7, burning, and feeding the mixed gas pipeline of the condensed and pressurized mixed gas into a high-temperature burning box for high-temperature burning.
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| CN101851520A (en) * | 2010-04-29 | 2010-10-06 | 江苏中容电气有限公司 | Sludge pyrolysis gas fractional condensation method for recycling biological oil |
| CN204522365U (en) * | 2015-03-13 | 2015-08-05 | 扬州晨光特种设备有限公司 | Biomass fast pyrogenation steam-condensation fractionating device |
| CN106010602A (en) * | 2016-06-13 | 2016-10-12 | 浙江大学 | Biomass charring device and operating method thereof |
| CN210786298U (en) * | 2019-09-29 | 2020-06-19 | 杰瑞环保科技有限公司 | Pyrolysis gas grading treatment device |
| CN111676049A (en) * | 2020-05-19 | 2020-09-18 | 青岛科技大学 | Accurate high-efficient multistage condensation splitter |
| CN113384913A (en) * | 2021-06-07 | 2021-09-14 | 东南大学 | Pyrolysis bio-oil fractional condensation device and method with self-circulation cooling medium |
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