CN103146403B - 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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- CN103146403B CN103146403B CN201310095402.XA CN201310095402A CN103146403B CN 103146403 B CN103146403 B CN 103146403B CN 201310095402 A CN201310095402 A CN 201310095402A CN 103146403 B CN103146403 B CN 103146403B
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 171
- 239000002028 Biomass Substances 0.000 title claims abstract description 124
- 238000000034 method Methods 0.000 title claims abstract description 29
- 239000003546 flue gas Substances 0.000 claims abstract description 126
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 125
- 238000001816 cooling Methods 0.000 claims abstract description 83
- 239000007789 gas Substances 0.000 claims abstract description 65
- 239000000571 coke Substances 0.000 claims abstract description 40
- 239000000047 product Substances 0.000 claims abstract description 11
- 239000013589 supplement Substances 0.000 claims abstract description 3
- 238000009434 installation Methods 0.000 claims description 51
- 239000000463 material Substances 0.000 claims description 40
- 238000002485 combustion reaction Methods 0.000 claims description 36
- 238000010438 heat treatment Methods 0.000 claims description 12
- 230000002411 adverse Effects 0.000 claims description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 8
- 239000001301 oxygen Substances 0.000 claims description 8
- 229910052760 oxygen Inorganic materials 0.000 claims description 8
- 230000005540 biological transmission Effects 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 230000004323 axial length Effects 0.000 claims description 3
- 238000010792 warming Methods 0.000 claims description 3
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
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- 235000011089 carbon dioxide Nutrition 0.000 description 2
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- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical compound C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 description 1
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Images
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
-
- 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
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Coke Industry (AREA)
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 make full use of existing land resources, has important strategic importance to realizing the unified development of rural economy, society, 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 saltings, but also can develop the effective way of biomass energy resource in conjunction with saline-alkali water both culturing microalgae.But realize this two kinds of technology, the required carbon nutrition source of material coke production and micro algae growth is two subject matters of needing solution badly.
Biomass pyrolytic is produced the ordinary method of biomass coke and bio-oil.Under normal circumstances, biomass pyrolytic is under the inert atmosphere of anaerobic or anoxic, to be heated under certain temperature to decompose and generate gas-liquid solid product as biomass coke, bio-oil and incondensable gas etc.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 conventional biomass liquefaction methods.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 pyrolysis product condensation, is at high temperature the intermediate product mixing with non-condensation gas.
Multiple pyrolytic process and device are developed at present, wherein much for the production of biomass coke, as patent of invention CN102032553A discloses a kind of rotary type pyrolysis charring and boiler heat supplying integration apparatus, 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 being heated by stack extension, etc.Existing biomass pyrolytic technique and device all need extra electric power to input the running with the rotation of drive equipment and induced draft fan gas blower, cannot realize energy-autarchic operation, are therefore not suitable for using near field.
Summary of the invention
The present invention is intended at least solve one of technical problem existing 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.
According to the biomass pyrolysis system of first aspect present invention embodiment, comprising: feeding unit, described feeding unit is used for inputting biomass material; Pyrolysis installation, described pyrolysis installation is connected that with described feeding unit described biomass material is carried out to pyrolysis; Separate refrigerating unit, described separation refrigerating unit is connected to receive and separate coke and the pyrolysis gas of described pyrolysis installation output with described pyrolysis installation; 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 the heat of the air combustion after described pyrolysis gas and preheating to be converted to mechanical energy and supplement described pyrolysis installation, separate the propulsion source of refrigerating unit.
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 that pyrolysis gas and the heat of the air combustion after preheating are converted to mechanical energy and supplementary pyrolysis installation, separate the propulsion source of refrigerating unit, and efficiency is high, can produce biomass coke, electric energy and containing CO simultaneously
2flue gas is as the inorganic carbon nutrition source of micro algae growth.
In addition, also there is following additional technical feature according to biomass pyrolysis system of the present invention:
According to one embodiment of present invention, described feeding unit comprises: for inputting the feeding warehouse of biomass material; Blanking storehouse, described blanking position in storehouse is in the bottom of described feeding warehouse, is provided with reciprocal push structure with to described biomass material continuous-feeding in described blanking storehouse; And feed chamber, described feed chamber is connected with described blanking storehouse to receive the biomass material that carry in described blanking storehouse, and wherein said feed chamber is provided with the low-temperature flue gas entrance being communicated with described air flue gas assembly.
Preferably, between described feeding warehouse and described blanking storehouse, there is pivotable dividing plate.
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 is set in coaxially the outside of described interior stove cylinder and seals by grommet with interior stove cylinder, described outer furnace tube fixed installation, outer furnace tube stove tail place is provided with high-temperature flue gas entry and 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 the downward-sloping extension of direction from burner to 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 angle between the length bearing of trend of described fin and the central axis of described interior stove cylinder is 0-60 °.
Preferably, described many fins comprise the 3-12 bar fin being circumferentially evenly arranged along described interior stove cylinder inwall.
Preferably, the pass of the inner diameter d of the gap s between the inwall of described outer furnace tube and the outer wall of 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, in described cooling epimere, limit cooling upper chamber, 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 is located at the bottom of described cooling epimere and limits the cooling lower chambers being 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 is formed as cuboid, and the cross section of the bottom of described cooling lower chambers is formed as 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; Combustion chamber, described combustion chamber is communicated with to receive pyrolysis gas by 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; High-temperature heat-exchanging, described high-temperature heat-exchanging is located at the downstream of described combustion chamber to receive the high-temperature flue gas after described combustion chambers burn and high-temperature flue gas is carried out to 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 two-way flue gas, first via flue gas in high-temperature heat-exchanging after heat exchange temperature be reduced to 500-700 ℃, 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 is 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 described stirling engine converts the heat of the air combustion after described pyrolysis gas and preheating to mechanical energy; 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 is connected for storing electric energy more than needed with described generator.
According to biomass pyrolysis system of the present invention, have the following advantages:
1, the energy discharging 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 for generating, thereby make biomass pyrolytic without relying on external energy input; The middle grade heat energy of high-temperature flue gas is 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 for preheated air.
2. pyrolysis installation is made up of interior outer furnace tube, biomass are both by the high-temperature flue gas adverse current heating in outer furnace tube, in feed chamber and interior stove cylinder, have again low-temperature flue gas to play that following current is carried and heat effect, low-temperature flue gas on the one hand can be as protection gas in pyrolytic process simultaneously; 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 containing in biomass is all enriched in biomass coke substantially, the flue gas that the burning of pyrolysis gaseous state intermediate product produces there is no pollutent, because it contains appropriate carbonic acid gas, after suitably purifying, can be used as the carbon nutrition source of the both culturing microalgae of the saltings raised fields water surface.
According to the method for biomass pyrolysis of the energy-autarchic of second aspect present invention embodiment, adopt according to the biomass pyrolysis system of the energy-autarchic described in 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 are carrying under protection and are entering pyrolysis installation containing 150-250 ℃ of low-temperature flue gas following current of 2-3% oxygen, 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 containing tar gaseous product;
Cooling collection after the described coke obtaining in S3, step S2 and air indirect heat exchange;
Air after heat exchange in S4, step S3 reacts with the pyrolysis gas in described step S2 and perfect combustion, forms 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, after described coke and described air indirect heat exchange, be cooled to 40-80 ℃ and collection.
In step S3, the air themperature after described heat exchange is 100-200 ℃.
Between step S2 and S3, also comprise that step S21:500-700 ℃ high-temperature flue gas is reduced to 120-150 ℃ in adverse current temperature after heating, purifies cooling.
Additional aspect of the present invention and advantage in the following description part provide, and part will become obviously from the following description, or recognize by practice of the present invention.
Accompanying drawing explanation
Above-mentioned and/or additional aspect of the present invention and advantage accompanying drawing below combination is understood becoming the description of embodiment obviously and easily, wherein:
Fig. 1 is according to the schematic diagram of 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 according to the schematic diagram of 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
Describe embodiments of the invention below in detail, the example of described embodiment is shown in the drawings, and wherein same or similar label represents same or similar element or has the element of identical or similar functions from start to finish.Be exemplary below by the embodiment being described with reference to the drawings, only 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 with operate, therefore can not be interpreted as limitation of the present invention.In addition, term " first ", " second " be only for describing object, 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 " multiple " is two or more.
In description of the invention, it should be noted that, unless otherwise clearly defined and limited, term " installation ", " being connected ", " connection " should be interpreted broadly, and for example, can be to be fixedly connected with, and can be also to removably connect, or connect integratedly; Can be to be directly 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.
Describe according to the biomass pyrolysis system of first aspect present invention embodiment below with reference to Fig. 1-Fig. 3.
As shown in Figure 1, according to the biomass pyrolysis system of the energy-autarchic of the embodiment of the present invention, comprising: feeding unit 100, pyrolysis installation 200, separation refrigerating unit 300, air flue gas assembly 400 and generation driving force assembly 500.
Feeding unit 100 is for inputting biomass material, biomass material is that biomass are through collecting and simple process, the raw material of the size obtaining 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.).
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 pyrolysis gas and the heat of the air combustion after preheating are converted to mechanical energy and supplementary pyrolysis installation 200, separate the propulsion source of refrigerating unit 300, and efficiency is high, can produce biomass coke and electric energy simultaneously.
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 for inputting biomass material, and for example feeding warehouse 110 can be configured to the funnel shaped that cross section reduces gradually from top to bottom, so that biomass material can easily enter.Alternatively, as shown in Figure 1, the cross section of feeding warehouse 110 is formed as rectangular shape.Blanking storehouse 120 is positioned at the bottom of feeding warehouse 110, in blanking storehouse 120, be provided with reciprocal push structure 121 with to biomass material continuous-feeding, wherein those skilled in the art know the structure of the reciprocal push structure 121 for continuous-feeding, are not described in detail at this.Preferably, between feeding warehouse 110 and blanking storehouse 120, there is pivotable dividing plate 140.Can prevent that thus flue gas from going out from feeding warehouse 110 anti-channelings.
Due to reciprocal propulsive mechanism 121 being housed in blanking storehouse 120, therefore biomass material is without pulverizing, only needs rough cutting, can put into feeding warehouse 110, by reciprocal propulsive mechanism 121 sent into feed chamber 130 in after entering blanking storehouse 120 under action of gravity.
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 fixedly mounts, and the stove tail place of outer furnace tube 220 is provided with high-temperature flue gas entry and burner place is provided with useless exhanst gas outlet.Wherein the burner of interior stove cylinder 210 (in the right end position as 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 the downward-sloping extension of direction from burner to stove tail, that is to say, the burner of interior stove cylinder 210 is higher than its stove tail (at the left position as 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 angle theta between the length bearing of trend of fin 211 and the central axis of interior stove cylinder 210 is 0-60 °.Preferably, many fins 211 comprise the 3-12 bar fin 211 being circumferentially evenly arranged along interior stove cylinder 210 inwalls.Further, in example as shown in Figure 1, the pass of the gap s between the inwall of outer furnace tube 220 and the outer wall of 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 is formed as cuboid.The top of cooling upper chamber 3211 is formed with pyrolysis gas outlet 3111, so that the pyrolysis gas of the stove tail output from interior stove cylinder 210 is discharged.Cooling hypomere 320 is located at the bottom of cooling epimere 310 and limits the cooling lower chambers 321 being communicated with cooling upper chamber 3211, and alternatively, the cross section of the bottom of cooling lower chambers 321 is formed as 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.
In the time of work, after the stove tail output-response of interior stove cylinder 210 comprise biomass coke and pyrolysis gas containing 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, after coke temperature is reduced to 40-90 ℃, discharges and collect from coke export 3211.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.
According 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 from 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 420 burnings of combustion chamber and high-temperature flue gas is carried out to heat exchange.Flue gas shunting device 440 is connected with high-temperature heat-exchanging 430 and high-temperature flue gas is split into two-way flue gas, the first via is cooled to 500-700 ℃ in interchanger, the second 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 with the useless exhanst gas outlet of outer furnace tube 220 with the first via flue gas between outer furnace tube 220 and interior stove cylinder 210 discharges.
Particularly, in the time of work, the preheated air that the pyrolysis gas passing into from pyrolysis gas pipeline 421 and the first pipeline 422 pass into, in the interior perfect combustion in combustion chamber 420, forms 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 that first via flue gas is shunted by flue gas shunting device 440 from 700-900 ℃ cools to 500-700 ℃, enter in the outer furnace tube 220 of pyrolysis installation 200, add hot-blast stove cylinder 210 by countercurrent flow, under the effect of the 3rd blower fan 460, leave pyrolysis installation.The flue gas of all the other 20-50% i.e. the second road flue gas is cooled to after 150-250 ℃ in the second blower fan 450 enters the feed chamber 130 being connected with pyrolysis installation 200 in high-temperature heat-exchanging 430, the protection gas when as 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, stirling engine 510 converts the heat of the air combustion after pyrolysis gas and preheating to mechanical energy, 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 generator 530 provides power to the gear 230 of the first blower fan 410, the second blower fan 450, the 3rd blower fan 460 and pyrolysis installation 200.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 by 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 multiple blower fans and pyrolysis installation 200 provides power, and electrical power storage more than needed is in store battery.
Describe according to the working process of the biomass pyrolysis system of the energy-autarchic of the embodiment of the present invention below with reference to Fig. 1.
First, biomass material adds after feeding warehouse 110, and the dividing plate 140 of feeding warehouse 110 is opened, and biomass material enters blanking storehouse I2 rear bulkhead and closes under action of gravity, under the promotion of reciprocal propulsive mechanism 121, enters feed chamber 130.In feed chamber 130, biomass material is at the heat drying containing 150-250 ℃ of low-temperature flue gas of 2-3% oxygen and under carrying, enter the burner of the interior stove cylinder 210 of pyrolysis installation.
Interior stove cylinder is by gear 230 driven rotary, stainless steel fin 211 lifting biomass on the one hand in cylinder, on the one hand heat being passed to biomass material from the inwall of interior stove cylinder 210 heats, because burner is higher than stove tail, make biomass material under action of gravity, stir to stove tail and move along with flue gas carries with fin 211.The high-temperature flue gas of 500-700 ℃ enters the space between pyrolysis installation outer furnace tube 220 and interior stove cylinder 210 from stove tail, heats inner furnace tube wall by convective heat exchange, and temperature is down to after 120-150 °, under the effect of the 3rd blower fan 460, discharges from burner.Biomass material is under the adverse current external heat effect of this high-temperature flue gas, and temperature rise pyrolysis discharge volatile matter and generate 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 containing 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, after coke temperature is reduced to 40-90 ℃, discharges and collect from coke export 3211.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, first by being positioned at, the cryogenic heat exchanger 520 of cold junction of stirling engine 510 is cooling obtains preheating for the first time from the working medium of stirling engine output, in cooling heat exchanger 330, obtain subsequently preheating for the second time, temperature rises to 100-200 ℃, enters combustion chamber 420 by the first pipeline 422.
Then, the preheated air that the pyrolysis gas passing into from pyrolysis gas pipeline 421 and the first pipeline 422 pass into, in the interior perfect combustion in combustion chamber 420, forms 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 that first via flue gas is shunted by flue gas shunting device 440 from 700-900 ℃ cools to 500-700 ℃, enter in the outer furnace tube 220 of pyrolysis installation 200, add hot-blast stove cylinder 210 by countercurrent flow, under the effect of the 3rd blower fan 460, leave pyrolysis installation.The flue gas of all the other 20-50% i.e. the second road flue gas is cooled to after 150-250 ℃ in the second blower fan 450 enters the feed chamber 130 being connected with pyrolysis installation 200 in high-temperature heat-exchanging 430, the protection gas when as biomass material pyrolysis.
The heat of the high-temperature flue gas of high-temperature heat-exchanging 430 is converted to mechanical energy by stirling engine 510, 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 multiple 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 discharging 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 for generating, thereby make biomass pyrolytic without relying on external energy input; The middle grade heat energy of high-temperature flue gas is 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 for preheated air.
2. pyrolysis installation is made up of interior outer furnace tube, biomass are both by the high-temperature flue gas adverse current heating in outer furnace tube 220, in feed chamber 130 and interior stove cylinder 210, have again low-temperature flue gas to play that following current is carried and heat effect, low-temperature flue gas on the one hand can be as protection gas in pyrolytic process simultaneously; 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 containing in biomass is all enriched in biomass coke substantially, the flue gas that the burning of pyrolysis gaseous state intermediate product produces there is no pollutent, because it contains appropriate carbonic acid gas, after suitably purifying, can be used as the carbon nutrition source of the both culturing microalgae of the saltings raised fields water surface.
According to the method for biomass pyrolysis of a kind of energy-autarchic of second aspect present invention embodiment, adopt according to the biomass pyrolysis system of 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 enter pyrolysis installation 200 carrying containing 150-250 ℃ of low-temperature flue gas following current of 2-3% oxygen 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 containing tar gaseous product; Alternatively, biomass material is at the interior residence time 30s-5min of pyrolysis installation 200.
Cooling collection after the coke obtaining in S3, step S2 and air indirect heat exchange.Wherein, be cooled to 40-80 ℃ and collection after coke and air heat-exchange, collecting cooling artifact matter coke can be for soil improvement.Air themperature after heat exchange is 100-200 ℃.
Air after heat exchange in S4, step S3 reacts with the pyrolysis gas in step S2 and perfect combustion, forms 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, and 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, also comprise that step S21:500-700 ℃ high-temperature flue gas is reduced to 120-150 ℃ in 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 feature of this embodiment or example description.In this manual, the schematic statement of above-mentioned term is not necessarily referred to identical embodiment or example.And specific features, structure, material or the feature of description can be with suitable mode combination 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 not departing from principle of the present invention and aim, can carry out multiple variation, modification, replacement and modification to these embodiment, scope of the present invention is limited by claim and equivalent thereof.
Claims (20)
1. a biomass pyrolysis system for energy-autarchic, is characterized in that, comprising:
Feeding unit, described feeding unit is used for inputting biomass material, and described feeding unit comprises: for inputting the feeding warehouse of biomass material; Blanking storehouse, described blanking position in storehouse is in the bottom of described feeding warehouse, is provided with reciprocal push structure with to described biomass material continuous-feeding in described blanking storehouse; And feed chamber, described feed chamber is connected with described blanking storehouse to receive the biomass material that carry in described blanking storehouse, and wherein said feed chamber is provided with the low-temperature flue gas entrance being communicated with described air flue gas assembly;
Pyrolysis installation, described pyrolysis installation is connected that with described feeding unit described biomass material is carried out to pyrolysis, described pyrolysis installation comprises: interior stove cylinder, described interior stove cylinder can be around its axial-rotation, the burner of described interior stove cylinder and described feed chamber are tightly connected, and described interior stove cylinder is configured to its central axis along the downward-sloping extension of direction from burner to stove tail; Outer furnace tube, described outer furnace tube is set in coaxially the outside of described interior stove cylinder and seals by grommet with interior stove cylinder, described outer furnace tube fixed installation, described outer furnace tube stove tail place is provided with high-temperature flue gas entry and burner place is provided with useless exhanst gas outlet, and the pass of the height difference H between the burner of wherein said interior stove cylinder and stove tail and the inner diameter d of described interior stove cylinder is: H/d=0.1-1.5;
Separate refrigerating unit, described separation refrigerating unit is connected to receive and separate coke and the pyrolysis gas of described pyrolysis installation output with described pyrolysis installation;
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 the heat of the air combustion after described pyrolysis gas and preheating to be converted to mechanical energy and supplement described pyrolysis installation, separate the propulsion source of refrigerating unit.
2. biomass pyrolysis system according to claim 1, is characterized in that, between described feeding warehouse and described blanking storehouse, has pivotable dividing plate.
3. biomass pyrolysis system according to claim 1, is characterized in that, the burner of described interior stove cylinder is tightly connected by rotating grommet and described feed chamber.
4. biomass pyrolysis system according to claim 1, 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.
5. biomass pyrolysis system according to claim 1, 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 angle between the length bearing of trend of described fin and the central axis of described interior stove cylinder is 0-60 °.
6. biomass pyrolysis system according to claim 5, is characterized in that, described many fins comprise the 3-12 bar fin being circumferentially evenly arranged along described interior stove cylinder inwall.
7. biomass pyrolysis system according to claim 1, is characterized in that, the pass of the gap s between the inwall of described outer furnace tube and the outer wall of described interior stove cylinder and the inner diameter d of described interior stove cylinder is: s/d=1/12-1/5.
8. biomass pyrolysis system according to claim 1, 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.
9. according to the biomass pyrolysis system described in any one in claim 1-8, it 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 is located at the bottom of described cooling epimere and limits the cooling lower chambers being 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.
10. biomass pyrolysis system according to claim 9, is characterized in that, described cooling upper chamber is formed as cuboid, and the cross section of the bottom of described cooling lower chambers is formed as down truncated cone shape.
11. biomass pyrolysis systems according to claim 9, 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;
Combustion chamber, described combustion chamber is communicated with to receive pyrolysis gas by 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;
High-temperature heat-exchanging, described high-temperature heat-exchanging is located at the downstream of described combustion chamber to receive the high-temperature flue gas after described combustion chambers burn and high-temperature flue gas is carried out to 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 two-way flue gas, first via flue gas in high-temperature heat-exchanging after heat exchange temperature be reduced to 500-700 ℃, 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.
12. biomass pyrolysis systems according to claim 11, 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.
13. biomass pyrolysis systems according to claim 11, is characterized in that, described air flue gas assembly also comprises:
The 3rd blower fan, described the 3rd blower fan is 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.
14. biomass pyrolysis systems according to claim 10, 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 described stirling engine converts the heat of the air combustion after described pyrolysis gas and preheating to mechanical energy;
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.
15. biomass pyrolysis systems according to claim 14, is characterized in that, described generation driving force assembly also comprises:
Store battery, described store battery is connected for storing electric energy more than needed with described generator.
The method of biomass pyrolysis of 16. 1 kinds of energy-autarchics, adopts according to the biomass pyrolysis system of the energy-autarchic described in any one in claim 1-15, it 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 are carrying under protection and are entering pyrolysis installation containing 150-250 ℃ of low-temperature flue gas following current of 2-3% oxygen, 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 containing tar gaseous product;
Cooling collection after the described coke obtaining in S3, step S2 and air indirect heat exchange;
Air after heat exchange in S4, step S3 reacts with the pyrolysis gas in described step S2 and perfect combustion, forms high-temperature flue gas;
High-temperature flue gas in S5, step S4 is split into the first via and the second road flue gas, is cooled to respectively after 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.
17. method of biomass pyrolysis according to claim 16, is characterized in that, in step S2, described biomass material is residence time 30s-5min in pyrolysis installation.
18. method of biomass pyrolysis according to claim 16, is characterized in that, in step S3, are cooled to 40-80 ℃ and collection after described coke and described air indirect heat exchange.
19. method of biomass pyrolysis according to claim 16, is characterized in that, in step S3, the air themperature after described heat exchange is 100-200 ℃.
20. method of biomass pyrolysis according to claim 16, is characterized in that, between step S2 and S3, also comprise that step S21:500-700 ℃ high-temperature flue gas is reduced to 120-150 ℃ in adverse current temperature after heating, purifies cooling.
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