CN103146403A - Biomass pyrolysis system and method through self-sufficient energy - Google Patents
Biomass pyrolysis system and method through self-sufficient energy Download PDFInfo
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- CN103146403A CN103146403A CN201310095402XA CN201310095402A CN103146403A CN 103146403 A CN103146403 A CN 103146403A CN 201310095402X A CN201310095402X A CN 201310095402XA CN 201310095402 A CN201310095402 A CN 201310095402A CN 103146403 A CN103146403 A CN 103146403A
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The invention discloses a biomass pyrolysis system and method through self-sufficient energy. The biomass pyrolysis system comprises a feeding device, a pyrolysis device, a separating and cooling device, an air flue gas component and a generating power component, wherein the pyrolysis device is connected with the feeding device so as to perform pyrolysis on the biomass raw materials; the separating and cooling device is connected with the pyrolysis device so as to receive and separate coke and pyrolysis gas output by the pyrolysis device; the air flue gas component is connected with the separating and cooling device so as to combust the pyrolysis gas and the preheated air and respectively feed the gas back to the feeding device and the pyrolysis device; and the generating power component is connected with the air flue gas component so as to convert the heat of the pyrolysis gas and the preheated air into mechanical energy and supplement the power source of the pyrolysis device and the separating and cooling device. According to the biomass pyrolysis system, the energy of the biomass pyrolysis gas product is subjected to gradient utilization, and the system has the advantages of self-sufficient energy, low cost and the like.
Description
Technical field
The present invention relates to biomass pyrolytic and utilize technical field, especially relate to a kind of biomass pyrolysis system and method for energy-autarchic.
Background technology
There are 14.8 hundred million mu of saltings resources in China.Saltings kind plant and energy-source plant that exploitation are fallen into disuse can take full advantage of existing land resources, have important strategic importance to realizing rural economy, society, the unified development of ecological benefits.In existing Saline-alkali Field Control technology, utilizing biomass coke to carry out alkaline land improving and utilizing the raised fields desalinization of soil by flooding or leaching is not only can administer the saltings, but also can develop the effective way of biomass energy resource in conjunction with the saline-alkali water both culturing microalgae.But realize this two kinds of technology, material coke production and micro algae growth required carbon nutrition source is two subject matters of needing solution badly.
Biomass pyrolytic is produced the ordinary method of biomass coke and bio-oil.Generally, biomass pyrolytic is to be heated to decomposition generation gas-liquid solid product such as biomass coke, bio-oil and incondensable gas etc. under certain temperature under the inert atmosphere of anaerobic or anoxic.According to the difference of biomass heating rate in pyrolytic process, can be divided into slow pyrolysis, fast pyrogenation and flash pyrolysis.Fast pyrogenation and flash pyrolysis because the condensation of the high gaseous state intermediate product of heating rate is rapid, are the biomass liquefaction methods of commonly using.Although fast pyrogenation is a certain amount of biomass char of by-product also, slow pyrolysis produces more biomass coke.In these pyrolytic processs, bio-oil all forms after the pyrolysis product condensation, is at high temperature the intermediate product that mixes with non-condensation gas.
Multiple pyrolytic process and device have been developed at present, wherein much for the production of biomass coke, a kind of rotary type pyrolysis charring and boiler heat supplying integration apparatus are disclosed as patent of invention CN102032553A, patent CN101967386A discloses a kind of cylindrical self-combustion biomass char production furnace, patent CN102226092A discloses a kind of external heat screw propulsion low temperature pyrogenation charing method and equipment, patent CN101899311A discloses a kind of rotating furnace body charring furnace by the stack extension heating, etc.Existing biomass pyrolytic technique and device all need extra electric power to input with drive equipment to rotate and the running of induced draft fan gas blower, can't realize the energy-autarchic operation, therefore be not suitable near the field use.
Summary of the invention
The present invention is intended to solve at least one of technical problem that exists in prior art.For this reason, one object of the present invention is to propose a kind of biomass pyrolysis system of energy-autarchic.
Another object of the present invention is to propose a kind of method of biomass pyrolysis that adopts above-mentioned biomass pyrolysis system.
Biomass pyrolysis system according to first aspect present invention embodiment comprises: feeding unit, described feeding unit are used for the input biomass material; Pyrolysis installation, described pyrolysis installation is connected that with described feeding unit described biomass material is carried out pyrolysis; Separate refrigerating unit, described separation refrigerating unit is connected to receive with described pyrolysis installation and separates coke and the pyrolysis gas of described pyrolysis installation output; Air flue gas assembly, described air flue gas assembly is connected that with the described refrigerating unit that separates the air combustion after described pyrolysis gas and preheating is also fed back to respectively in described feeding unit and described pyrolysis installation; Generation driving force assembly, described generation driving force assembly and described air flue gas assembly are connected and convert mechanical energy to and replenish described pyrolysis installation, separate the propulsion source of refrigerating unit with the heat with the air combustion after described pyrolysis gas and preheating.
According to embodiment of the present invention biomass pyrolysis system, the energy of cascade utilization biomass pyrolytic gas product has energy-autarchic, low cost and other advantages.Device of the present invention utilizes the generation driving force assembly that the heat of the air combustion after pyrolysis gas and preheating is converted to mechanical energy and additional pyrolysis installation, separates the propulsion source of refrigerating unit, and efficient is high, can produce simultaneously biomass coke, electric energy and contain CO
2Flue gas is as the inorganic carbon nutrition source of micro algae growth.
In addition, also have following additional technical feature according to biomass pyrolysis system of the present invention:
According to one embodiment of present invention, described feeding unit comprises: the feeding warehouse that is used for the input biomass material; Blanking storehouse, described blanking position in storehouse be in the bottom of described feeding warehouse, is provided with reciprocal push structure in described blanking storehouse with to described biomass material continuous-feeding; And feed chamber, described feed chamber is connected to receive the biomass material that carry in described blanking storehouse with described blanking storehouse, and wherein said feed chamber is provided with the low-temperature flue gas entrance that is communicated with described air flue gas assembly.
Preferably, has pivotable dividing plate between described feeding warehouse and described blanking storehouse.
According to one embodiment of present invention, described pyrolysis installation comprises: interior stove cylinder, and described interior stove cylinder can be around its axial-rotation, and the burner of described interior stove cylinder and described feed chamber are tightly connected; Outer furnace tube, described outer furnace tube are set in coaxially the outside of described interior stove cylinder and seal by grommet with interior stove cylinder, described outer furnace tube fixed installation, and outer furnace tube stove tail place is provided with high-temperature flue gas entry and the burner place is provided with useless exhanst gas outlet.。
Alternatively, the burner of described interior stove cylinder is tightly connected by rotating grommet and described feed chamber.
Alternatively, described interior stove cylinder is configured to its central axis along from burner to the downward-sloping extension of the direction of stove tail.
Preferably, the pass of the inner diameter d of the height difference H between the burner of described interior stove cylinder and stove tail and described interior stove cylinder is: H/d=0.1-1.5.
Preferably, described interior stove cylinder along the pass of its axial length L and its inner diameter d is: L/d=5-15.
Further, the inwall of described interior stove cylinder is provided with many fins that radially protrude, the pass of the height h that described fin radially protrudes and the inner diameter d of described interior stove cylinder is: h/d=1/15-1/5, and the angle between the central axis of the length bearing of trend of described fin and described interior stove cylinder is 0-60 °.
Preferably, described many fins comprise the 3-12 bar fin that circumferentially is evenly arranged along described interior stove cylinder inwall.
Preferably, the pass of the inner diameter d of the gap s between the outer wall of the inwall of described outer furnace tube and described interior stove cylinder and described interior stove cylinder is: s/d=1/12-1/5.
Further, described pyrolysis installation also comprises: gear, and described geared sleeve is located at the two ends of described interior stove cylinder, and wherein said interior stove cylinder drives rotation by geartransmission.
According to one embodiment of present invention, described separation refrigerating unit comprises: cooling epimere, limit cooling upper chamber in described cooling epimere, the stove tail of described cooling upper chamber and described interior stove cylinder is tightly connected, and the top of described cooling upper chamber is formed with pyrolysis gas outlet; Cooling hypomere, described cooling hypomere are located at the bottom of described cooling epimere and limit the cooling lower chambers that is communicated with described cooling upper chamber, and the bottom of described cooling lower chambers is formed with coke export; And cooling heat exchanger, described cooling heat exchanger is located at described cooling bottom chamber.
Alternatively, described cooling upper chamber forms cuboid, and the cross section of the bottom of described cooling lower chambers forms down truncated cone shape.
According to one embodiment of present invention, described air flue gas assembly comprises: the first blower fan, and described the first blower fan is communicated with described cooling heat exchanger; The combustion chamber, described combustion chamber is communicated with to receive pyrolysis gas by the pyrolysis gas pipeline with the pyrolysis gas outlet of described cooling upper chamber, and described combustion chamber is communicated with described cooling heat exchanger by the first pipeline; The downstream that high-temperature heat-exchanging, described high-temperature heat-exchanging are located at described combustion chamber is to receive the high-temperature flue gas after described combustion chambers burn and high-temperature flue gas is carried out heat exchange; And flue gas shunting device, described flue gas shunting device is connected with described high-temperature heat-exchanging and described high-temperature flue gas is split into the two-way flue gas, first via flue gas in high-temperature heat-exchanging after heat exchange temperature be reduced to 500-700 ℃, the the second road flue gas in high-temperature heat-exchanging after heat exchange temperature be reduced to 150-250 ℃, described first via flue gas passes in described outer furnace tube, and described the second road flue gas is passed in described feed chamber.
Further, described air flue gas assembly also comprises: the second blower fan, described the second blower fan is connected between described high-temperature heat-exchanging and described feed chamber.
Further, described air flue gas assembly also comprises: the 3rd blower fan, described the 3rd blower fan are connected that with the described useless exhanst gas outlet of described outer furnace tube the first via flue gas between described outer furnace tube and described interior stove cylinder is discharged.
According to one embodiment of present invention, described generation driving force assembly comprises: stirling engine, wherein said high-temperature heat-exchanging is positioned at the hot junction of described stirling engine, and the heat of the air combustion of described stirling engine after with described pyrolysis gas and preheating converts mechanical energy to; Cryogenic heat exchanger, described cryogenic heat exchanger is located at the cold junction of described stirling engine, and described cryogenic heat exchanger is communicated with described the first blower fan by second pipe; Generator, described generator is connected with described stirling engine by transmission rig, and described generator provides power to described the first blower fan, described the second blower fan, described the second blower fan and described pyrolysis installation.
Further, described generation driving force assembly also comprises: store battery, described store battery are connected with described generator and are used for storing electric energy more than needed.
According to biomass pyrolysis system of the present invention, have the following advantages:
1, the energy that discharges after can cascade utilization biomass pyrolytic gas firing improves heat utilization efficiency and the hot merit efficiency of conversion of process system.Particularly, utilize stirling engine recovery high-temperature flue gas and higher-grade heat energy wherein to be used for generating, thereby make biomass pyrolytic need not to rely on the external energy input; The middle grade heat energy of high-temperature flue gas is used for the heating of biomass pyrolytic, and the low grade heat energy that pyrogenous origin coke waste heat and stirling engine cold junction discharge is used for preheated air.
2. pyrolysis installation is made of interior outer furnace tube, biomass are both by the heating of the high-temperature flue gas adverse current in outer furnace tube, have again simultaneously low-temperature flue gas to play that following current is carried and heat effect in feed chamber and interior stove cylinder, low-temperature flue gas on the one hand can be as protection gas in pyrolytic process; On the other hand, a small amount of oxygen can in middle high temperature section and pyrolysis product generation oxidizing reaction, further improve pyrolysis temperature.
3. through pyrolysis, the ash content that contains in biomass all is enriched in biomass coke basically, the flue gas that the burning of pyrolysis gaseous state intermediate product produces there is no pollutent, because it contains appropriate carbonic acid gas, namely can be used as the carbon nutrition source of the both culturing microalgae of the saltings raised fields water surface after suitably purifying.
According to the method for biomass pyrolysis of the energy-autarchic of second aspect present invention embodiment, adopt the biomass pyrolysis system according to the described energy-autarchic of first aspect present invention embodiment, wherein, described method of biomass pyrolysis comprises the following steps:
S1, biomass material is added in feeding unit;
S2, described biomass material carry under protection the 150-250 that contains 2-3% oxygen ℃ of low-temperature flue gas following current and enter pyrolysis installation, under the outside adverse current heating of 500-700 ℃ of high-temperature flue gas, be warming up at 400-600 ℃ of temperature pyrolysis to form coke and to contain the tar gaseous product;
Cooling collection after the described coke that obtains in S3, step S2 and air indirect heat exchange;
Pyrolysis gas reaction and perfect combustion in air after heat exchange in S4, step S3 and described step S2 form high-temperature flue gas;
High-temperature flue gas in S5, step S5 is split into the first via and the second road flue gas, is cooled to respectively 500-700 ℃ and 150-250 ℃ in high-temperature heat-exchanging, and described first via flue gas and described the second road flue gas return for step S2.
In step S2, described biomass material is residence time 30s-5min in pyrolysis installation.
In step S3, be cooled to 40-80 ℃ and collection after described coke and described air indirect heat exchange.
In step S3, the air themperature after described heat exchange is 100-200 ℃.
Between step S2 and S3, comprise that also step S21:500-700 ℃ high-temperature flue gas is reduced to 120-150 ℃ in the adverse current temperature after heating, purifies cooling.
Additional aspect of the present invention and advantage part in the following description provide, and part will become obviously from the following description, or recognize by practice of the present invention.
Description of drawings
Above-mentioned and/or additional aspect of the present invention and advantage are from obviously and easily understanding becoming the description of embodiment in conjunction with following accompanying drawing, wherein:
Fig. 1 is the schematic diagram according to the biomass pyrolysis system of first aspect present invention embodiment;
Fig. 2 be in Fig. 1 A-A to sectional view;
Fig. 3 be in Fig. 2 B-B to sectional view;
Fig. 4 is the schematic diagram according to the method for biomass pyrolysis of second aspect present invention embodiment.
Reference numeral:
100, feeding unit;
110, feeding warehouse; 120, blanking storehouse; 121, reciprocal propulsive mechanism;
130, feed chamber; 131, low-temperature flue gas entrance; 140, dividing plate;
200, pyrolysis installation;
210, interior stove cylinder; 211, fin; 220, outer furnace tube; 230, gear;
300, separate refrigerating unit;
310, cooling epimere; 311, cooling upper chamber; 3111, pyrolysis gas outlet;
320, cooling hypomere; 321, cooling lower chambers; 3211, coke export;
330, cooling heat exchanger
400, air flue gas assembly;
410, the first blower fan; 420, combustion chamber; 421, pyrolysis gas pipeline; 422, the first pipeline;
430, high-temperature heat-exchanging; 440, flue gas shunting device; 450, the second blower fan; 460, the 3rd blower fan;
500, generation driving force assembly;
510, stirling engine; 520, cryogenic heat exchanger; 521, second pipe;
530, generator; 540, transmission rig
Embodiment
The below describes embodiments of the invention in detail, and the example of described embodiment is shown in the drawings, and wherein same or similar label represents same or similar element or the element with identical or similar functions from start to finish.Be exemplary below by the embodiment that is described with reference to the drawings, only be used for explaining the present invention, and can not be interpreted as limitation of the present invention.
In description of the invention, it will be appreciated that, orientation or the position relationship of the indications such as term " " center ", " on ", D score, 'fornt', 'back', " left side ", " right side ", " top ", " end ", " interior ", " outward " be based on orientation shown in the drawings or position relationship; be only the present invention for convenience of description and simplified characterization; rather than the device of indication or hint indication or element must have specific orientation, with specific orientation structure and operation, so can not be interpreted as limitation of the present invention.In addition, term " first ", " second " only are used for describing purpose, and can not be interpreted as indication or hint relative importance or the implicit quantity that indicates indicated technical characterictic.Thus, one or more these features can be expressed or impliedly be comprised to the feature that is limited with " first ", " second ".In description of the invention, except as otherwise noted, the implication of " a plurality of " is two or more.
In description of the invention, need to prove, unless clear and definite regulation and restriction are separately arranged, term " installation ", " being connected ", " connection " should be done broad understanding, for example, can be to be fixedly connected with, and can be also to removably connect, or connect integratedly; Can be directly to be connected, also can indirectly be connected by intermediary, can be the connection of two element internals.For the ordinary skill in the art, can particular case understand above-mentioned term concrete meaning in the present invention.
Below with reference to the biomass pyrolysis system of Fig. 1-Fig. 3 description according to first aspect present invention embodiment.
As shown in Figure 1, the biomass pyrolysis system according to the energy-autarchic of the embodiment of the present invention comprises: feeding unit 100, pyrolysis installation 200, separate refrigerating unit 300, air flue gas assembly 400 and generation driving force assembly 500.
Feeding unit 100 is used for the input biomass material, biomass material is that biomass are through collecting and simple process, the raw material of the size that obtains below 5-10cm, wherein, biomass can comprise energy-source plant (as switchgrass, false indigo, salix monogolica and cogongrass etc.), agricultural wastes (as crop material, shell pericarp etc.) and forestry residuum (sawdust, branches and leaves, bark etc.).
Pyrolysis installation 200 is connected that with feeding unit 100 biomass material is carried out pyrolysis, separates refrigerating unit 300 is connected to receive with pyrolysis installation 200 and separation pyrolyzing device 200 is exported coke and pyrolysis gas.Air flue gas assembly 400 with separate refrigerating unit 300 and be connected with the air combustion after pyrolysis gas and preheating and feed back to respectively in feeding unit 100 and pyrolysis installation 200.Generation driving force assembly 500 and air flue gas assembly 400 is connected and converts mechanical energy and additional pyrolysis installation 200 to, separates the propulsion source of refrigerating unit 300 with the heat with the air combustion after pyrolysis gas and preheating.
According to embodiment of the present invention biomass pyrolysis system, the energy of cascade utilization biomass pyrolytic gas product has energy-autarchic, low cost and other advantages.Device of the present invention utilizes generation driving force assembly 500 that the heat of the air combustion after pyrolysis gas and preheating is converted to mechanical energy and additional pyrolysis installation 200, separates the propulsion source of refrigerating unit 300, and efficient is high, can produce simultaneously biomass coke and electric energy.
According to one embodiment of present invention, feeding unit 100 comprises: feeding warehouse 110, blanking storehouse 120 and feed chamber 130.Feeding warehouse 110 is used for the input biomass material, and for example feeding warehouse 110 can be configured to the funnel shaped that cross section from top to bottom reduces gradually, so that biomass material can easily enter.Alternatively, as shown in Figure 1, the cross section of feeding warehouse 110 forms rectangular shape.Blanking storehouse 120 is positioned at the bottom of feeding warehouse 110, be provided with reciprocal push structure 121 in blanking storehouse 120 with to the biomass material continuous-feeding, wherein those skilled in the art know the structure of the reciprocal push structure 121 that is used for continuous-feeding, are not described in detail at this.Preferably, has pivotable dividing plate 140 between feeding warehouse 110 and blanking storehouse 120.Can prevent that thus flue gas from going out from feeding warehouse 110 anti-channelings.
Feed chamber 130 is connected to receive the biomass material that carry in blanking storehouse 120 with blanking storehouse 120; wherein feed chamber 130 is provided with the low-temperature flue gas entrance 131 that is communicated with air flue gas assembly 400; thus, can be with a part of low-temperature flue gas in air flue gas assembly 400 the protection gas when feed chamber 130 passes into pyrolysis installation 200 as the biomass material pyrolysis.Alternatively, the quantity of low-temperature flue gas entrance 131 can be 1-6.
Owing in blanking storehouse 120, reciprocal propulsive mechanism 121 being housed, so biomass material need not to pulverize, and only needs rough cutting, can put into feeding warehouse 110, namely sent in feed chamber 130 by reciprocal propulsive mechanism 121 enter blanking storehouse 120 under action of gravity after.
As shown in Figure 1, pyrolysis installation 200 comprises: interior stove cylinder 210 and outer furnace tube 220, interior stove cylinder 210 can be around its axial-rotation, the burner of interior stove cylinder 210 and feed chamber 130 are tightly connected, outer furnace tube 220 is set in coaxially the outside of interior stove cylinder 210 and seals by grommet (scheming not shown) with interior stove cylinder 210, outer furnace tube 220 fixed installation, the stove tail place of outer furnace tube 220 is provided with high-temperature flue gas entry and the burner place is provided with useless exhanst gas outlet.Wherein the burner of interior stove cylinder 210 (namely as the right end position in Fig. 1) is tightly connected by rotating grommet and feed chamber 130.In some optional embodiment of the present invention, interior stove cylinder 210 is configured to its central axis along from burner to the downward-sloping extension of the direction of stove tail, that is to say, the burner of interior stove cylinder 210 is higher than its stove tail (namely as the left position in Fig. 1).Preferably, the pass of the inner diameter d of the height difference H between the burner of interior stove cylinder 210 and stove tail and interior stove cylinder 210 is: H/d=0.1-1.5.In addition, in some preferred examples, interior stove cylinder 210 along the pass of its axial length L and its inner diameter d is: L/d=5-15.
According to examples more of the present invention, as shown in Figures 2 and 3, the inwall of interior stove cylinder 210 is provided with many fins 211 that radially protrude, the pass of the height h that fin 211 radially protrudes and the inner diameter d of interior stove cylinder 210 is: h/d=1/15-1/5, and the angle theta between the central axis of the length bearing of trend of fin 211 and interior stove cylinder 210 is 0-60 °.Preferably, many fins 211 comprise the 3-12 bar fin 211 that circumferentially is evenly arranged along interior stove cylinder 210 inwalls.Further, in example as shown in Figure 1, the pass of the gap s between the outer wall of the inwall of outer furnace tube 220 and interior stove cylinder 210 and the inner diameter d of interior stove cylinder 210 is: s/d=1/12-1/5.
Alternatively, pyrolysis installation 200 also comprises gear 230, and gear 230 is set in the two ends of interior stove cylinder 210, and wherein interior stove cylinder 210 drives rotation by geartransmission, and outer furnace tube 210 also can rotate thereupon thus.
As shown in Figure 1, separate refrigerating unit 300 and comprise cooling epimere 310, cooling hypomere 320 and cooling heat exchanger 330.Particularly, limit cooling upper chamber 3211 in cooling epimere 310, cooling upper chamber 3211 is tightly connected with the stove tail of interior stove cylinder 210, and alternatively, as shown in Figure 1, cooling upper chamber 3211 forms cuboid.The top of cooling upper chamber 3211 is formed with pyrolysis gas outlet 3111, discharging from the pyrolysis gas that the stove tail of interior stove cylinder 210 is exported.Cooling hypomere 320 is located at the bottom of cooling epimere 310 and limits the cooling lower chambers 321 that is communicated with cooling upper chamber 3211, and alternatively, the cross section of the bottom of cooling lower chambers 321 forms down truncated cone shape.The bottom of cooling lower chambers 321 is formed with coke export 3211.Cooling heat exchanger 330 is located in cooling lower chambers 321.
When work, after the stove tail output-response of interior stove cylinder 210 comprise biomass coke and pyrolysis gas contain the tar gaseous product, wherein biomass coke falls under gravity in cooling lower chambers 321, with cooling heat exchanger 330 contact heat-exchangings, transfer heat to the cooling air in cooling heat exchanger 330, discharge from coke export 3211 after coke temperature is reduced to 40-90 ℃ and collect.And in the gauge pressure at the stove tail place of interior stove cylinder 210 be-20Pa is to-100Pa, and pyrolysis gas is discharged from pyrolysis gas outlet 3111 under suction function.
In some embodiments of the present invention, air flue gas assembly 400 comprises: the first blower fan 410, combustion chamber 420, high-temperature heat-exchanging 430 and flue gas shunting device 440.As shown in Figure 1, the first blower fan 410 is communicated with cooling heat exchanger 330.Combustion chamber 420 is communicated with to receive pyrolysis gas by pyrolysis gas pipeline 421 with the pyrolysis gas outlet 3111 of cooling upper chamber 3211, and combustion chamber 420 is communicated with to receive the air after hot and cold heat exchanger 330 heat exchange with cooling heat exchanger 330 by the first pipeline 422.High-temperature heat-exchanging 430 is located at the downstream of combustion chamber 420 to receive the high-temperature flue gas after burning in combustion chamber 420 and high-temperature flue gas is carried out heat exchange.Flue gas shunting device 440 is connected with high-temperature heat-exchanging 430 and high-temperature flue gas is split into the two-way flue gas, the first via is cooled to 500-700 ℃ in interchanger, the second the tunnel is cooled to 150-250 ℃ in interchanger, first via flue gas passes in outer furnace tube 220, and the second road flue gas is passed in feed chamber 130.Further, air flue gas assembly 400 also comprises: the second blower fan 450 and the 3rd blower fan 460, the second blower fan 450 is connected between high-temperature heat-exchanging 430 and feed chamber 130, and the 3rd blower fan 460 is connected to discharge to the first via flue gas between outer furnace tube 220 and interior stove cylinder 210 with the useless exhanst gas outlet of outer furnace tube 220.
Particularly, in when work, preheated air 420 interior perfect combustions in the combustion chamber that the pyrolysis gas that passes into from pyrolysis gas pipeline 421 and the first pipeline 422 pass into form the high-temperature flue gas (excess of oxygen tolerance is 2-3%) of 700-900 ℃.High-temperature flue gas enters in high-temperature heat-exchanging 430 subsequently, wherein the flue gas of 50-80% is by 440 shuntings of flue gas shunting device after first via flue gas cools to 500-700 ℃ from 700-900 ℃, enter in the outer furnace tube 220 of pyrolysis installation 200, add hot-blast stove cylinder 210 by countercurrent flow, leave pyrolysis installation under the effect of the 3rd blower fan 460.The flue gas of all the other 20-50% i.e. the second road flue gas is cooled to 150-250 ℃ and enters by the second blower fan 450 in the feed chamber 130 that is connected with pyrolysis installation 200 in high-temperature heat-exchanging 430, the protection gas when being used as the biomass material pyrolysis.
In further embodiment of the present invention, generation driving force assembly 500 comprises: stirling engine 510, cryogenic heat exchanger 520 and generator 530.Wherein high-temperature heat-exchanging 430 is positioned at the hot junction of stirling engine 510, the heat of the air combustion of stirling engine 510 after with pyrolysis gas and preheating converts mechanical energy to, cryogenic heat exchanger 520 is located at the cold junction of stirling engine 510, cryogenic heat exchanger 520 is communicated with the first blower fan 410 by second pipe 521, generator 530 is connected with stirling engine 510 by transmission rig 540, and the gear 230 of 530 pairs of the first blower fans 410 of generator, the second blower fan 450, the 3rd blower fan 460 and pyrolysis installation 200 provides power.Alternatively, generation driving force assembly 500 also comprises store battery (scheming not shown), and store battery is connected with generator 530.Particularly, it is working medium that stirling engine 510 adopts helium or air, absorb the heat of high-temperature flue gas by high-temperature heat-exchanging 430, be mechanical energy with the thermal power transfer of high-temperature flue gas, by transmission rig 540 pushing generators 530, mechanical energy is converted to electric energy, for the gear 230 of the interior stove cylinder 210 of a plurality of blower fans and pyrolysis installation 200 provides power, and electrical power storage more than needed is in store battery.
Below with reference to the working process of Fig. 1 description according to the biomass pyrolysis system of the energy-autarchic of the embodiment of the present invention.
At first, after biomass material added feeding warehouse 110, the dividing plate 140 of feeding warehouse 110 was opened, and biomass material enters blanking storehouse I2 rear bulkhead and closes under action of gravity, entered feed chamber 130 under the promotion of reciprocal propulsive mechanism 121.In feed chamber 130, biomass material is at the heat drying of the 150-250 that contains 2-3% oxygen ℃ low-temperature flue gas and enter the burner of the interior stove cylinder 210 of pyrolysis installation under carrying.
Interior stove cylinder is by gear 230 driven rotary, stainless steel fin 211 one side lifting biomass in cylinder, on the one hand heat being passed to biomass material from the inwall of interior stove cylinder 210 heats, due to burner higher than the stove tail, make biomass material under action of gravity, move to the stove tail along with flue gas carries to stir with fin 211.The high-temperature flue gas of 500-700 ℃ enters space between pyrolysis installation outer furnace tube 220 and interior stove cylinder 210 from the stove tail, heats inner furnace tube wall by convective heat exchange, after temperature is down to 120-150 °, discharges from burner under the effect of the 3rd blower fan 460.Biomass material is under the adverse current external heat effect of this high-temperature flue gas, and temperature rises and pyrolysis discharges volatile matter generation coke.Near the stove tail of interior stove cylinder 210, the temperature of biomass coke can reach 400-600 ℃.
After the stove tail output-response of interior stove cylinder 210 comprise biomass coke and pyrolysis gas contain the tar gaseous product, wherein biomass coke falls under gravity in cooling lower chambers 321, with cooling heat exchanger 330 contact heat-exchangings, transfer heat to the cooling air in cooling heat exchanger 330, discharge from coke export 3211 after coke temperature is reduced to 40-90 ℃ and collect.And in the gauge pressure at the stove tail place of interior stove cylinder 210 be-20Pa is to-100Pa, and pyrolysis gas is discharged from pyrolysis gas outlet 3111 under suction function.
Burn required air under the effect of the first blower fan 410, at first the cryogenic heat exchanger 520 of the cold junction by being positioned at stirling engine 510 is cooling obtains preheating for the first time after the working medium of stirling engine output, obtain subsequently preheating for the second time in cooling heat exchanger 330, temperature rises to 100-200 ℃, enters combustion chamber 420 by the first pipeline 422.
Then, preheated air 420 interior perfect combustions in the combustion chamber that the pyrolysis gas that passes into from pyrolysis gas pipeline 421 and the first pipeline 422 pass into form the high-temperature flue gas (excess of oxygen tolerance is 2-3%) of 700-900 ℃.High-temperature flue gas enters in high-temperature heat-exchanging 430 subsequently, wherein the flue gas of 50-80% is by 440 shuntings of flue gas shunting device after first via flue gas cools to 500-700 ℃ from 700-900 ℃, enter in the outer furnace tube 220 of pyrolysis installation 200, add hot-blast stove cylinder 210 by countercurrent flow, leave pyrolysis installation under the effect of the 3rd blower fan 460.The flue gas of all the other 20-50% i.e. the second road flue gas is cooled to 150-250 ℃ and enters by the second blower fan 450 in the feed chamber 130 that is connected with pyrolysis installation 200 in high-temperature heat-exchanging 430, the protection gas when being used as the biomass material pyrolysis.
Stirling engine 510 is converted to mechanical energy with the heat of the high-temperature flue gas of high-temperature heat-exchanging 430, by transmission rig 540 pushing generators 530, mechanical energy is converted to electric energy, for the gear 230 of the interior stove cylinder 210 of a plurality of blower fans and pyrolysis installation 200 provides power, and electrical power storage more than needed is in store battery.
According to biomass pyrolysis system of the present invention, have the following advantages:
1, the energy that discharges after can cascade utilization biomass pyrolytic gas firing improves heat utilization efficiency and the hot merit efficiency of conversion of process system, particularly.Utilize stirling engine recovery high-temperature flue gas and higher-grade heat energy wherein to be used for generating, thereby make biomass pyrolytic need not to rely on the external energy input; The middle grade heat energy of high-temperature flue gas is used for the heating of biomass pyrolytic, and the low grade heat energy that pyrogenous origin coke waste heat and stirling engine 510 cold junctions discharge is used for preheated air.
2. pyrolysis installation is made of interior outer furnace tube, biomass are both by the heating of the high-temperature flue gas adverse current in outer furnace tube 220, have again simultaneously low-temperature flue gas to play that following current is carried and heat effect in feed chamber 130 and interior stove cylinder 210, low-temperature flue gas on the one hand can be as protection gas in pyrolytic process; On the other hand, a small amount of oxygen can in middle high temperature section and pyrolysis product generation oxidizing reaction, further improve pyrolysis temperature.
3. through pyrolysis, the ash content that contains in biomass all is enriched in biomass coke basically, the flue gas that the burning of pyrolysis gaseous state intermediate product produces there is no pollutent, because it contains appropriate carbonic acid gas, namely can be used as the carbon nutrition source of the both culturing microalgae of the saltings raised fields water surface after suitably purifying.
According to the method for biomass pyrolysis of a kind of energy-autarchic of second aspect present invention embodiment, adopt the biomass pyrolysis system according to first aspect present invention embodiment, wherein, method of biomass pyrolysis comprises the following steps:
S1, biomass material is passed in feeding unit 100.
S2, biomass material carry the 150-250 that contains 2-3% oxygen ℃ of low-temperature flue gas following current and enter pyrolysis installation 200 under protection, under the outside adverse current heating of 500-700 ℃ of high-temperature flue gas, be warming up at 400-600 ℃ of temperature pyrolysis to form coke and to contain the tar gaseous product; Alternatively, biomass material is at the interior residence time 30s-5min of pyrolysis installation 200.
Cooling collection after the coke that obtains in S3, step S2 and air indirect heat exchange.Wherein, be cooled to 40-80 ℃ and collection after coke and air heat-exchange, collect cooling artifact matter coke and can be used for soil improvement.Air themperature after heat exchange is 100-200 ℃.
Pyrolysis gas reaction and perfect combustion in air after heat exchange in S4, step S3 and step S2 form high-temperature flue gas.
High-temperature flue gas in S5, step S4 is split into the first via flue gas of 500-700 ℃ and the second road flue gas of 150-250 ℃ after high-temperature heat-exchanging, first via flue gas and the second road flue gas return for step S2.
According to one embodiment of present invention, between step S2 and S3, comprise that also step S21:500-700 ℃ high-temperature flue gas is reduced to 120-150 ℃ in the adverse current temperature after heating, purify cooling, then can be as the inorganic carbon nutrition source of both culturing microalgae.
In the description of this specification sheets, the description of reference term " embodiment ", " some embodiment ", " illustrative examples ", " example ", " concrete example " or " some examples " etc. means to be contained at least one embodiment of the present invention or example in conjunction with specific features, structure, material or the characteristics of this embodiment or example description.In this manual, the schematic statement of above-mentioned term not necessarily referred to identical embodiment or example.And the specific features of description, structure, material or characteristics can be with suitable mode combinations in any one or more embodiment or example.
Although illustrated and described embodiments of the invention, those having ordinary skill in the art will appreciate that: in the situation that do not break away from principle of the present invention and aim can be carried out multiple variation, modification, replacement and modification to these embodiment, scope of the present invention is limited by claim and equivalent thereof.
Claims (24)
1. the biomass pyrolysis system of an energy-autarchic, is characterized in that, comprising:
Feeding unit, described feeding unit are used for the input biomass material;
Pyrolysis installation, described pyrolysis installation is connected that with described feeding unit described biomass material is carried out pyrolysis;
Separate refrigerating unit, described separation refrigerating unit is connected to receive with described pyrolysis installation and separates coke and the pyrolysis gas of described pyrolysis installation output;
Air flue gas assembly, described air flue gas assembly is connected that with the described refrigerating unit that separates the air combustion after described pyrolysis gas and preheating is also fed back to respectively in described feeding unit and described pyrolysis installation;
Generation driving force assembly, described generation driving force assembly and described air flue gas assembly are connected and convert mechanical energy to and replenish described pyrolysis installation, separate the propulsion source of refrigerating unit with the heat with the air combustion after described pyrolysis gas and preheating.
2. biomass pyrolysis system according to claim 1, is characterized in that, described feeding unit comprises:
The feeding warehouse that is used for the input biomass material;
Blanking storehouse, described blanking position in storehouse be in the bottom of described feeding warehouse, is provided with reciprocal push structure in described blanking storehouse with to described biomass material continuous-feeding; With
Feed chamber, described feed chamber are connected to receive the biomass material that carry in described blanking storehouse with described blanking storehouse, wherein said feed chamber is provided with the low-temperature flue gas entrance that is communicated with described air flue gas assembly.
3. biomass pyrolysis system according to claim 2, is characterized in that, has pivotable dividing plate between described feeding warehouse and described blanking storehouse.
4. biomass pyrolysis system according to claim 2, is characterized in that, described pyrolysis installation comprises:
Interior stove cylinder, described interior stove cylinder can be around its axial-rotation, and the burner of described interior stove cylinder and described feed chamber are tightly connected;
Outer furnace tube, described outer furnace tube are set in coaxially the outside of described interior stove cylinder and seal by grommet with interior stove cylinder, described outer furnace tube fixed installation, and described outer furnace tube stove tail place is provided with high-temperature flue gas entry and the burner place is provided with useless exhanst gas outlet.
5. biomass pyrolysis system according to claim 4, is characterized in that, the burner of described interior stove cylinder is tightly connected by rotating grommet and described feed chamber.
6. biomass pyrolysis system according to claim 4, is characterized in that, described interior stove cylinder is configured to its central axis along from burner to the downward-sloping extension of the direction of stove tail.
7. biomass pyrolysis system according to claim 6, is characterized in that, the pass of the height difference H between the burner of described interior stove cylinder and stove tail and the inner diameter d of described interior stove cylinder is: H/d=0.1-1.5.
8. biomass pyrolysis system according to claim 6, is characterized in that, described interior stove cylinder along the pass of its axial length L and its inner diameter d is: L/d=5-15.
9. biomass pyrolysis system according to claim 6, it is characterized in that, the inwall of described interior stove cylinder is provided with many fins that radially protrude, the pass of the height h that described fin radially protrudes and the inner diameter d of described interior stove cylinder is: h/d=1/15-1/5, and the angle between the central axis of the length bearing of trend of described fin and described interior stove cylinder is 0-60 °.
10. biomass pyrolysis system according to claim 9, is characterized in that, described many fins comprise the 3-12 bar fin that circumferentially is evenly arranged along described interior stove cylinder inwall.
11. biomass pyrolysis system according to claim 4 is characterized in that, the pass of the gap s between the outer wall of the inwall of described outer furnace tube and described interior stove cylinder and the inner diameter d of described interior stove cylinder is: s/d=1/12-1/5.
12. biomass pyrolysis system according to claim 4 is characterized in that, described pyrolysis installation also comprises:
Gear, described geared sleeve is located at the two ends of described interior stove cylinder, and wherein said interior stove cylinder drives rotation by geartransmission.
13. according to claim 4-12, the described biomass pyrolysis system of any one, is characterized in that, described separation refrigerating unit comprises:
Cooling epimere limits cooling upper chamber in described cooling epimere, and the stove tail of described cooling upper chamber and described interior stove cylinder is tightly connected, and the top of described cooling upper chamber is formed with pyrolysis gas outlet;
Cooling hypomere, described cooling hypomere are located at the bottom of described cooling epimere and limit the cooling lower chambers that is communicated with described cooling upper chamber, and the bottom of described cooling lower chambers is formed with coke export; And
Cooling heat exchanger, described cooling heat exchanger are located at described cooling bottom chamber.
14. biomass pyrolysis system according to claim 13 is characterized in that, described cooling upper chamber forms cuboid, and the cross section of the bottom of described cooling lower chambers forms down truncated cone shape.
15. biomass pyrolysis system according to claim 13 is characterized in that, described air flue gas assembly comprises:
The first blower fan, described the first blower fan is communicated with described cooling heat exchanger;
The combustion chamber, described combustion chamber is communicated with to receive pyrolysis gas by the pyrolysis gas pipeline with the pyrolysis gas outlet of described cooling upper chamber, and described combustion chamber is communicated with described cooling heat exchanger by the first pipeline;
The downstream that high-temperature heat-exchanging, described high-temperature heat-exchanging are located at described combustion chamber is to receive the high-temperature flue gas after described combustion chambers burn and high-temperature flue gas is carried out heat exchange; And
The flue gas shunting device, described flue gas shunting device is connected with described high-temperature heat-exchanging and described high-temperature flue gas is split into the two-way flue gas, first via flue gas in high-temperature heat-exchanging after heat exchange temperature be reduced to 500-700 ℃, the the second road flue gas in high-temperature heat-exchanging after heat exchange temperature be reduced to 150-250 ℃, described first via flue gas passes in described outer furnace tube, and described the second road flue gas is passed in described feed chamber.
16. biomass pyrolysis system according to claim 15 is characterized in that, described air flue gas assembly also comprises:
The second blower fan, described the second blower fan is connected between described high-temperature heat-exchanging and described feed chamber.
17. biomass pyrolysis system according to claim 15 is characterized in that, described air flue gas assembly also comprises:
The 3rd blower fan, described the 3rd blower fan are connected that with the described useless exhanst gas outlet of described outer furnace tube the first via flue gas between described outer furnace tube and described interior stove cylinder is discharged.
18. biomass pyrolysis system according to claim 14 is characterized in that, described generation driving force assembly comprises:
Stirling engine, wherein said high-temperature heat-exchanging is positioned at the hot junction of described stirling engine, and the heat of the air combustion of described stirling engine after with described pyrolysis gas and preheating converts mechanical energy to;
Cryogenic heat exchanger, described cryogenic heat exchanger is located at the cold junction of described stirling engine, and described cryogenic heat exchanger is communicated with described the first blower fan by second pipe;
Generator, described generator is connected with described stirling engine by transmission rig, and described generator provides power to described the first blower fan, described the second blower fan, described the 3rd blower fan and described pyrolysis installation.
19. biomass pyrolysis system according to claim 18 is characterized in that, described generation driving force assembly also comprises:
Store battery, described store battery are connected with described generator and are used for storing electric energy more than needed.
20. the method for biomass pyrolysis of an energy-autarchic, in employing according to claim 1-19, the biomass pyrolysis system of the described energy-autarchic of any one, is characterized in that, described method of biomass pyrolysis comprises the following steps:
S1, biomass material is added in feeding unit;
S2, described biomass material carry under protection the 150-250 that contains 2-3% oxygen ℃ of low-temperature flue gas following current and enter pyrolysis installation, under the outside adverse current heating of 500-700 ℃ of high-temperature flue gas, be warming up at 400-600 ℃ of temperature pyrolysis to form coke and to contain the tar gaseous product;
Cooling collection after the described coke that obtains in S3, step S2 and air indirect heat exchange;
Pyrolysis gas reaction and perfect combustion in air after heat exchange in S4, step S3 and described step S2 form high-temperature flue gas;
High-temperature flue gas in S5, step S4 is split into the first via and the second road flue gas, and be cooled to respectively 500-700 ℃ and 150-250 ℃ in high-temperature heat-exchanging after, described first via flue gas and described the second road flue gas return for step S2.
21. method of biomass pyrolysis according to claim 20 is characterized in that, in step S2, described biomass material is residence time 30s-5min in pyrolysis installation.
22. method of biomass pyrolysis according to claim 20 is characterized in that, in step S3, is cooled to 40-80 ℃ and collection after described coke and described air indirect heat exchange.
23. method of biomass pyrolysis according to claim 20 is characterized in that, in step S3, the air themperature after described heat exchange is 100-200 ℃.
24. method of biomass pyrolysis according to claim 20 is characterized in that, between step S2 and S3, comprises that also step S21:500-700 ℃ high-temperature flue gas is reduced to 120-150 ℃ in the adverse current temperature after heating, purifies cooling.
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