CN210030574U - Vertical biomass pyrolysis reaction system - Google Patents
Vertical biomass pyrolysis reaction system Download PDFInfo
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- CN210030574U CN210030574U CN201920485386.8U CN201920485386U CN210030574U CN 210030574 U CN210030574 U CN 210030574U CN 201920485386 U CN201920485386 U CN 201920485386U CN 210030574 U CN210030574 U CN 210030574U
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- 239000000463 material Substances 0.000 claims abstract description 30
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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
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Abstract
The embodiment of the utility model provides a biomass vertical pyrolysis reaction system, which consists of a vertical pyrolysis reactor with a special structure and other matching devices; the system takes the solid heat carrier as a reaction heat transfer carrier, has the advantages of high thermal efficiency, uniform heating and the like, and can effectively improve the pyrolysis efficiency; through setting parameters such as spiral blades, stirring blades and the like in the vertical pyrolysis reactor, biomass and a heat carrier are fully mixed and quickly transferred, and meanwhile, the temperature of the heat carrier, the particle size of materials and the pyrolysis retention time are flexibly adjusted, so that the biomass pyrolysis reactor is suitable for treating various biomass raw materials, the yield of various pyrolysis products is conveniently adjusted, and the biomass pyrolysis reactor has the characteristics of high efficiency, low manufacturing cost and easiness in industrialization; the system also comprises a primary condensing tower for preventing coking, which effectively solves the coking problem of biomass in the traditional pyrolysis technology and can realize the long-period continuous and reliable operation of the system.
Description
Technical Field
The utility model belongs to the technical field of the living beings pyrolysis, in particular to adopt vertical pyrolytic reaction system of living beings of solid heat carrier circulation.
Background
Biomass refers to various organisms formed by photosynthesis, including all animals and plants and microorganisms. At present, biomass utilization mainly refers to various agricultural and forestry wastes such as straws, sawdust, rice hulls and the like. The main approaches of biomass include straw composting and returning to fields, utilization of industrial straw raw materials, utilization of straw feed and utilization of straw energy, wherein the advantages of high utilization efficiency, good benefit and the like of straw energy are widely regarded and researched. The biomass pyrolysis treatment technology is a thermal cracking method for straw raw materials through a high-efficiency pyrolysis device under the reaction conditions of oxygen deficiency and high temperature to produce products such as bio-combustible gas, bio-oil, pyroligneous liquor, biochar and the like, and the products are wide in utilization, high in added value and good in benefit compared with the traditional direct incineration treatment.
The vertical pyrolysis reactors developed for biomass pyrolysis at present are mainly fluidized beds, fixed beds, moving beds and the like. Because the pyrolysis process needs to be heated, in order to enable the biomass material to generate pyrolysis reaction in an oxygen-isolated environment, inert gas or solid is usually adopted as a heat carrier to provide required energy for the pyrolysis reaction, and various reactors used by the conventional pyrolysis technology have the problem of insufficient thermal efficiency to different degrees; meanwhile, currently, only a certain raw material can be treated in a proper particle size range, the raw material needs to be crushed or formed, and the economical efficiency of the production process is poor due to the difficulty in collecting the raw material of the biomass and the high cost of subsequent crushing, forming and the like.
SUMMERY OF THE UTILITY MODEL
The utility model discloses heating efficiency to exist among the current biomass pyrolysis technology all kinds of vertical pyrolytic reaction wares is low, living beings raw materials handles and leads to the cost to increase the scheduling problem, provides neotype vertical pyrolytic reaction system of living beings to solid heat carrier is as the reaction heat transfer carrier, based on the vertical pyrolytic reaction ware project organization of optimization, has that system equipment is simple, easy operation, the thermal efficiency is high, characteristics such as cost are low.
In order to solve the technical problem, the embodiment of the utility model provides a vertical pyrolytic reaction system of living beings, including breaker, drying-machine, lifting machine, heating riser, material storehouse, vertical pyrolytic reaction ware, solid-solid separation ware, one-level condensing tower, second grade condensing tower, filter and adsorption tower, wherein:
the vertical pyrolysis reactor comprises a reactor barrel, and a heat carrier inlet, a material inlet and a pyrolysis gas outlet which are arranged on the reactor barrel, wherein the reactor barrel is in a hollow round platform structure with a large upper part and a small lower part, and a rotating shaft is arranged at the middle shaft of the reactor barrel; spiral blades are wound and fixed on the rotating shaft and are stirred along with the rotation of the rotating shaft; the heat carrier inlet and the material inlet are arranged on one side of the upper end of the reactor cylinder, the pyrolysis gas outlet is arranged on the opposite side of the upper end of the reactor cylinder, and the heat carrier inlet is higher than the material inlet; a solid outlet for discharging a solid heat carrier and pyrolysis solid products is also formed in the side part of the lower end of the reactor cylinder;
the biomass raw material sequentially passes through the crusher and the dryer, and the dryer is respectively connected with the hoister and the heating riser to convey biomass; after passing through the material bin, the biomass input into the elevator is input into the vertical pyrolysis reactor from the material inlet, the biomass input into the heating riser is used as fuel for combustion, and high-temperature flue gas generated by combustion is used for heating and lifting a solid heat carrier; the heating riser is connected with the heat carrier inlet to input a solid heat carrier into the vertical pyrolysis reactor, and biomass and the solid heat carrier are mixed and then subjected to pyrolysis reaction in the vertical pyrolysis reactor; the solid outlet is connected with the solid-solid separator to output a solid mixture, the solid-solid separator outputs biochar, and a solid heat carrier is input into the heating riser pipe connected with the solid-solid separator; the pyrolysis gas outlet is connected with a pyrolysis gas inlet at the top of the primary condensing tower, and high-temperature pyrolysis gas is sent into the primary condensing tower; the first-stage condensing tower inputs bio-oil obtained by condensing pyrolysis gas into the connected filter to filter out impurities, and inputs the residual pyrolysis gas into the connected second-stage condensing tower; and the secondary condensation tower outputs biogas, crude wood vinegar obtained by condensation is input into the adsorption tower to adsorb impurities, and the adsorption tower outputs wood vinegar.
Preferably, the spiral blades are sequentially fixed with a plurality of stirring blades along the extension direction of the blades, and the stirring blades are square or round raised ribs.
Preferably, a pyrolysis gas outlet of the vertical pyrolysis reactor is communicated with 1-5 side exhaust ports, and the side exhaust ports extend into the reactor barrel and are used for collecting internal pyrolysis gas and guiding the pyrolysis gas to the pyrolysis gas outlet to be discharged.
Preferably, the first-stage condensation tower is provided with a spraying oil inlet, the outlet of the filter is connected with the spraying oil inlet, and the bio-oil is input into the first-stage condensation tower for spraying.
Preferably, the solid-solid separator is connected with the adsorption tower, and the biochar is input into the adsorption tower to be used as an adsorbent for adsorbing impurities in the crude wood vinegar.
Preferably, a flue gas outlet of the heating riser pipe is connected with the dryer, and flue gas output from the heating riser pipe is input into the dryer to be used as a heat source for drying biomass.
Preferably, the pyrolysis gas inlet of the first-stage condensing tower is a conical opening with a small upper part and a large lower part, and a hot smoke hood is arranged outside the first-stage condensing tower and used for preserving heat of the pyrolysis gas inlet so as to prevent coking of the pyrolysis gas; the hot smoke cover comprises a smoke inlet and a smoke outlet; the flue gas inlet is arranged at the lower side part of the hot gas hood and is connected with the flue gas outlet of the heating lifting pipe to receive the flue gas from the heating lifting pipe; the flue gas outlet is arranged at the upper part of the hot smoke hood, is connected with the dryer, and outputs the flue gas in the hot smoke hood to the dryer to be used as a heat source for drying biomass.
The embodiment of the utility model provides a biomass pyrolytic reaction method uses aforementioned vertical pyrolytic reaction system of living beings to handle biomass feedstock, includes following step:
1. sending the biomass into a crusher to be crushed to a set particle size, and then sending the biomass into a dryer to pre-dry the biomass;
2. feeding the pre-dried biomass part into a vertical pyrolysis reactor, mixing with a solid heat carrier and carrying out pyrolysis reaction to generate high-temperature pyrolysis gas, feeding the rest biomass into a heating riser, and burning the biomass serving as fuel in the heating riser;
3. sending high-temperature pyrolysis gas generated in the vertical pyrolysis reactor into a primary condensing tower for spraying and condensing to obtain bio-oil;
4. feeding pyrolysis gas discharged from the first-stage condensing tower into a second-stage condensing tower for spray condensation to obtain crude pyroligneous liquor, feeding the crude pyroligneous liquor into an adsorption tower, and adsorbing impurities in the crude pyroligneous liquor to obtain pyroligneous liquor;
5. separating a solid mixture generated by reaction in the vertical pyrolysis reactor in a solid-solid separator to obtain biochar and a solid heat carrier;
6. and (3) feeding the solid heat carrier in the solid-solid separator into a heating riser, and feeding the heated and lifted solid heat carrier into a vertical pyrolysis reactor to be mixed with the biomass.
Preferably, the biomass is used as the waste heat of the flue gas generated by fuel combustion in the heating riser, and the biomass is pre-dried in a dryer and/or the pyrolysis gas inlet is insulated in the primary condensing tower, so that the waste heat of the high-temperature flue gas in the heating riser is recovered, and the energy utilization rate of the system is improved.
Preferably, the biological oil obtained in the first-stage condensation tower is filtered to remove impurities and then sent into the first-stage condensation tower again for spraying, so as to form the circulating spraying of the biological oil.
Preferably, the biochar obtained by separating the solid mixture in a solid-solid separator is packed into an adsorption tower as an adsorbent to adsorb impurities in the crude pyroligneous liquor fed into the adsorption tower, and the crude pyroligneous liquor is treated into pure pyroligneous liquor.
Preferably, the pyroligneous liquor obtained after adsorption of impurities in the crude pyroligneous liquor is re-fed into a secondary condensation tower for spraying to form a circulating spray of pyroligneous liquor.
The embodiment of the utility model provides an above-mentioned technical scheme disclose neotype living beings pyrolysis technology, utilize devices such as vertical pyrolysis reactor of special construction to constitute reaction system, adopt solid heat carrier as the reaction heat transfer carrier, compare with prior art, have following beneficial effect:
1. the solid heat carrier is adopted to provide pyrolysis reaction energy for biomass, so that the biomass pyrolysis device has the advantages of high thermal efficiency, uniform heating and the like, and can effectively improve the pyrolysis efficiency;
2. through reasonable setting of parameters such as spiral blades, stirring blades and the like of the vertical pyrolysis reactor, biomass and a heat carrier are fully mixed and quickly transferred, meanwhile, through flexible adjustment of the temperature of the heat carrier, the particle size of materials and pyrolysis residence time, straw biomass with different raw materials and different particle size ranges can be treated, the yield of different pyrolysis products is adjusted, and the pyrolysis process can be optimized so that the straw biomass pyrolysis reactor has the characteristics of high efficiency, low manufacturing cost and easiness in industrialization;
3. the anti-coking condensing tower is designed according to the easy coking of the biomass pyrolysis gas during cooling, so that the problem of coking of the biomass in the traditional pyrolysis technology is effectively solved, and the long-period continuous and reliable operation of the system can be realized.
Drawings
Fig. 1 is a system diagram of a biomass vertical pyrolysis reaction system provided by an embodiment of the present invention;
fig. 2 is a schematic structural diagram of a vertical pyrolysis reactor in a biomass vertical pyrolysis reaction system according to an embodiment of the present invention;
fig. 3 is a schematic structural diagram of a first condensation tower in a vertical biomass pyrolysis reaction system according to an embodiment of the present invention;
fig. 4 is a schematic flow chart illustrating steps of a biomass pyrolysis reaction method according to an embodiment of the present invention.
[ main component symbol description ]
1-a crusher; 2-a dryer;
31-a hoist; 32-a material bin;
4-heating the riser;
5-a vertical pyrolysis reactor; 51-reactor barrel; 52-axis of rotation; 53-helical leaves; 531-stirring leaves; 54-heat carrier inlet; 55-material inlet; 56-solids outlet; 57-outlet of pyrolysis gas; 571-side exhaust port;
6-first-stage condensation tower; 61-hot smoke hood; 611-a flue gas inlet; 612-a flue gas outlet; 62-inlet of pyrolysis gas; 63-concentration tube; 631-spray oil inlet; 632-a shower head; 64-inclined plates; 65-a slag removal port; 66-gas collecting hood; 67-condensation vent; 68-an oil outlet; 69-a liquid level meter;
7-a secondary condensation column;
8-solid separator;
91-a filter; 92-adsorption column.
Detailed Description
In order to make the technical problems, technical solutions and advantages to be solved by the present invention clearer, the following detailed description will be given with reference to the accompanying drawings and specific embodiments.
The utility model discloses to current problem, provide the vertical pyrolytic reaction technology of living beings to solid heat carrier is as reaction heat transfer carrier, based on the vertical pyrolytic reactor project organization of optimization, and this pyrolytic technology has that system equipment is simple, easy operation, the thermal efficiency is high, characteristics such as cost are low.
In order to realize the technical scheme, the embodiment of the utility model provides a vertical pyrolysis reaction system of living beings. Fig. 1 shows the biomass vertical pyrolysis reaction system, which has the following basic structure:
the system comprises a crusher 1, a dryer 2, a lifter 31, a heating riser 4, a material bin 32, a vertical pyrolysis reactor 5, a solid-solid separator 8, a primary condensing tower 6, a secondary condensing tower 7, a filter 91 and an adsorption tower 92, wherein:
the biomass raw material is sent into a crusher 1 from an inlet of the crusher 1, an outlet of the crusher 1 is connected with an inlet of a dryer 2, and the biomass raw material sequentially passes through the crusher 1 and the dryer 2; the outlet of the dryer 2 is respectively connected with the elevator 31 and the heating lifting pipe 4, and the biomass is simultaneously conveyed into the elevator 31 and the heating lifting pipe 4.
The outlet of the hoister 31 is connected with the inlet of the material bin 32, the inlet of the material bin 32 is connected with the material inlet 55 of the vertical pyrolysis reactor 5, and the biomass in the hoister 31 is sent into the vertical pyrolysis reactor 5 through the material bin 32.
Biomass in the heating riser tube 4 is used as fuel to be combusted, and high-temperature flue gas generated by combustion is used for heating and lifting a solid heat carrier in the heating riser tube 4; a heat carrier outlet of the heating riser 4 is connected with a heat carrier inlet 54 of the vertical pyrolysis reactor 5, and the heated and lifted solid heat carrier is sent into the vertical pyrolysis reactor 5, so that the biomass and the solid heat carrier are mixed and then undergo pyrolysis reaction; the heating riser 4 is further provided with a flue gas outlet, and as a better implementation mode, in order to improve the energy utilization rate, the waste heat in the flue gas discharged by the heating riser 4 can be recycled, and the flue gas outlet of the heating riser 4 is sent into the dryer 2 to be used as a heat source for drying the biomass.
Pyrolysis reaction is carried out in the vertical pyrolysis reactor 5 to generate high-temperature pyrolysis gas and biochar; the pyrolysis gas outlet 57 of the vertical pyrolysis reactor 5 is connected to the pyrolysis gas inlet 62 at the top of the primary condensation tower 6, high-temperature pyrolysis gas is sent into the primary condensation tower 6, the solid outlet 56 is connected to the inlet of the solid-solid separator 8, and a solid mixture containing biochar and a solid heat carrier is sent into the solid-solid separator 8.
The solid-solid separator 8 separates the biochar and the solid heat carrier from the solid mixture, a heat carrier outlet of the solid-solid separator 8 is connected with a heat carrier inlet of the heating riser 4, the solid heat carrier is input into the heating riser 4 to be heated and lifted again and then is sent into the vertical pyrolysis reactor 5, the solid heat carrier forms heat carrier circulation in the vertical pyrolysis reactor 5, the solid-solid separator 8 and the heating riser 4, and heat is quickly transferred to the biomass; the biochar in the solid-solid separator 8 can be sent out as a product.
The first-stage condensing tower 6 condenses the high-temperature pyrolysis gas of the self-standing pyrolysis reactor 5 to generate bio-oil, the first-stage condensing tower 6 is connected with the filter 91, and the bio-oil is sent into the filter 91 to filter impurities; the filtered bio-oil can be sent out as a product, and as a better implementation mode, the outlet of the filter 91 can be connected to the spray oil inlet 631 of the primary condensation tower 6, and part of the bio-oil is input into the primary condensation tower 6 for circulating spray; the first-stage condensing tower 6 is connected with the second-stage condensing tower 7, and the pyrolysis gas is sent into the second-stage condensing tower 7.
The second-stage condensing tower 7 further condenses the pyrolysis gas from the first-stage condensing tower 6 to generate crude pyroligneous with impurities, and the residual pyrolysis gas can be used as biogas to be sent out; the second condensation tower 7 is connected to the adsorption tower 92, and the crude pyroligneous liquor is fed to the adsorption tower 92.
The crude pyroligneous liquor from the secondary condensation tower 7 in the adsorption tower 92 forms pure pyroligneous liquor after adsorbing impurities, the pyroligneous liquor can be sent out as a product, and as a better embodiment, the pyroligneous liquor can also be sent into the secondary condensation tower 7 for cyclic spraying; as another more preferable embodiment, the adsorption tower 92 may be connected to the solid-solid separator 8, and the biochar in the solid-solid separator 8 is filled into the adsorption tower 92 as an adsorbent.
As shown in fig. 2, which is an example of a vertical pyrolysis reactor 5, the vertical pyrolysis reactor 5 includes a reactor cylinder 51, and a heat carrier inlet 54, a material inlet 55 and a pyrolysis gas outlet 57 which are arranged on the reactor cylinder 51, the reactor cylinder 51 is in a hollow circular truncated cone structure with a large top and a small bottom, and a rotating shaft 52 is installed at a central axis position of the reactor cylinder 51; a spiral blade 53 is wound and fixed on the rotating shaft 52, and the spiral blade 53 is stirred along with the rotation of the rotating shaft 52; a heat carrier inlet 54 and a material inlet 55 are arranged on one side of the upper end of the reactor cylinder body 51, a pyrolysis gas outlet 57 is arranged on the opposite side, and the position of the heat carrier inlet 54 is higher than that of the material inlet 55; the side part of the lower end of the reactor cylinder 51 is also provided with a solid outlet 56 for discharging the solid heat carrier and pyrolysis solid products.
The vertical pyrolysis reactor 5 may take the following arrangement as a more preferred embodiment:
an included angle α between the vertical surface of the side part of the reactor cylinder body 51 and the lower bottom surface is 120-150 degrees, the side part of the reactor cylinder body 51 can be provided with 1-5 side exhaust ports 571 communicated with the pyrolysis gas outlet 57, the side exhaust ports 571 extend into the reactor cylinder body 51 and are used for collecting the pyrolysis gas inside and leading the pyrolysis gas to the pyrolysis gas outlet 57 for exhaust, the side exhaust ports 571 can be arranged to be round or square, and horizontally extend out 4-95 mm from the inner wall of the reactor cylinder body 51;
the rotating shaft 52 is arranged at the middle shaft position of the reactor cylinder body 51 and vertically penetrates through the reactor cylinder body 51 from top to bottom; a spiral blade 53 is wound and fixed on the rotating shaft 52, the spiral blade 53 can be fixed with the rotating shaft 52 by adopting a welding mode, and when the rotating shaft 52 rotates, blades of the spiral blade 53 stir by taking the rotating shaft 52 as a shaft to stir and push the biomass in the reactor cylinder 51; the distance between adjacent blades of the spiral blade 53 can be set to be 100-500 mm, and the distance between the edge of the spiral blade 53 and the inner side wall of the reactor cylinder 51 is 5-100 mm; for further promoting stirring effect, can weld a plurality of ribs in proper order on the spiral leaf 53 along blade extending direction and regard as stirring leaf 531, the rib is square or circular arch, bellied height can set up to 10~100mm, and the interval between the adjacent rib can set up to 100~300 mm.
In order to avoid coking of pyrolysis gas, the primary condensing tower 6 in the system can adopt a vertical spraying structure as shown in fig. 3, and the specific structure is as follows:
a small-top and large-bottom conical opening is formed in the center of the top of the primary condensing tower 6, a pyrolysis gas outlet 57 of the vertical pyrolysis reactor 5 is connected with the conical opening, pyrolysis gas is sent into the primary condensing tower 6, and the conical inlet is a pyrolysis gas inlet 62; the hot smoke hood 61 is arranged outside the pyrolysis gas inlet 62, and the hot smoke hood 61 is used for preserving heat of the pyrolysis gas inlet 62 to prevent the pyrolysis gas from coking; the hot smoke hood 61 is provided with a smoke inlet 611 and a smoke outlet 612, the smoke inlet 611 is arranged on the lower side part of the hot smoke hood 61 and is connected with the heating riser pipe 4 to receive high-temperature smoke from the heating riser pipe 4, and the high-temperature smoke is sent into the hot smoke hood 61 to serve as a heat source; the flue gas outlet 612 is arranged at the upper part of the hot smoke hood 61, and as a better embodiment, the flue gas outlet 612 can be connected with the dryer 2, and the flue gas in the hot smoke hood 61 is sent into the dryer 2 to be used as a heat source for drying biomass; as shown in fig. 3, as a better embodiment, a concentration pipe 63 surrounding a first-stage condensation tower 6 is arranged at a position 100-400 mm away from the lower part of a reheating smoke hood 61, a spray oil inlet 631 is arranged on the concentration pipe 63, the concentration pipe 63 is connected to the inside of the tower, a plurality of spray headers 632 are arranged on the concentration pipe 63 in the tower, spray oil enters from the spray oil inlet 631 and is sprayed by the spray headers 632, the spraying direction is a central downward direction, and the atomization angle is preferably set to be 100-150 °; an inclined plate 64 with an included angle of 40-60 degrees with the horizontal direction is arranged below the spray shower head 632, an opening is formed in the inclined plate 64 and used for filtering impurities, liquid descending upwards can leak downwards through the inclined plate 64, the opening rate of the inclined plate 64 can be 40-60%, and the aperture can be set to be 10-30 mm; a slag removing opening 65 is arranged at the lowest part of the inclined plate 64, the diameter of the slag removing opening 65 is preferably set to be 400-600 mm, and the slag removing opening is used for discharging impurities collected on the inclined plate 64; the gas-collecting hood 66 is arranged at the center position in the tower below the inclined plate 64, the inner diameter of the gas-collecting hood is 500-1000 mm, the gas-collecting hood is used for uniformly collecting pyrolysis gas in the tower, and one side of the upper part of the gas-collecting hood 66 is provided with a condensation exhaust port 67 communicated with the outside and used for outputting the collected pyrolysis gas to the outside of the tower; an oil outlet 68 is arranged on the side of the lower part of the first-stage condensation tower 6 and used for discharging biological oil generated in the tower, a liquid level meter 69 can be further arranged on the lower part of the tower, and the liquid level meter 69 is used for detecting the liquid level height in the tower and adjusting the flow of the oil outlet 68 according to the liquid level height.
The embodiment of the utility model provides a biomass pyrolytic reaction method uses aforementioned vertical pyrolytic reaction system of living beings to handle biomass feedstock, includes following step:
s1, sending the biomass into a crusher to be crushed to a set particle size, and then sending the biomass into a dryer to pre-dry the biomass;
s2, conveying the pre-dried biomass part into a vertical pyrolysis reactor, mixing the biomass part with a solid heat carrier and carrying out pyrolysis reaction to generate high-temperature pyrolysis gas, conveying the rest biomass into a heating riser, and burning the biomass serving as fuel in the heating riser;
s3, sending the high-temperature pyrolysis gas generated in the vertical pyrolysis reactor into a primary condensing tower for spray condensation to obtain bio-oil;
s4, feeding pyrolysis gas discharged from the primary condensation tower into a secondary condensation tower for spray condensation to obtain crude pyroligneous liquor, feeding the crude pyroligneous liquor into an adsorption tower, and adsorbing impurities in the crude pyroligneous liquor to obtain pyroligneous liquor;
s5, separating a solid mixture generated in the vertical pyrolysis reactor in a solid-solid separator to obtain biochar and a solid heat carrier;
s6, sending the solid heat carrier in the solid-solid separator into a heating riser, and sending the heated and lifted solid heat carrier into a vertical pyrolysis reactor to be mixed with the biomass.
The preferred embodiment of the above steps is as follows:
in the step S1, the biomass is sent into a crusher, the particle size range after crushing is 3-50 mm, and the material is dried until the moisture content is less than 10%.
In the step S2, the residence time of the biomass in the reactor is controlled to be 3-360S according to the properties and particle sizes of different types of biomass by adjusting the speed of a rotating shaft of the vertical pyrolysis reactor, and the gas outlet temperature of high-temperature pyrolysis gas generated by pyrolysis is 350-500 ℃; biomass is combusted in a heating riser to generate flue gas, the outlet temperature of the flue gas is 500-600 ℃, in order to improve the energy utilization rate and recover the waste heat of the flue gas, the flue gas discharged by the recovered heating riser is guided into a dryer to pre-dry the biomass, and can also be guided into a primary condensing tower to serve as a heat source to preserve heat of a pyrolysis gas inlet (specifically, as shown in fig. 3, a hot smoke hood is arranged around the pyrolysis gas inlet, and the flue gas is guided into the hot smoke hood) so as to fully utilize the waste heat of the high-temperature flue gas; preferably, 10-30% of the discharged flue gas is sent to a first-stage condensation tower to serve as a heat source, the flue gas discharged from the first-stage condensation tower and the rest of the discharged flue gas are gathered and then sent to a dryer, and the temperature of the flue gas entering the dryer is controlled to be 100-350 ℃.
And step S3, sending the high-temperature pyrolysis gas discharged by the vertical pyrolysis reactor into a primary condensing tower, reducing the temperature of the pyrolysis gas to 40-80 ℃ after spraying, condensing and separating out bio-oil in the primary condensing tower, filtering the bio-oil to remove mechanical impurities, and then sending the bio-oil out or sending the bio-oil into the primary condensing tower again to realize circulating spraying.
In step S4, the crude pyroligneous liquor is treated by an adsorption tower to remove tar and mechanical impurities contained therein to obtain pure pyroligneous liquor, which is sent out by a pump or sent into a secondary condensation tower again to use the pyroligneous liquor as circulating spray; the residual pyrolysis gas is discharged as biogas.
In the step S5, discharging a solid heat carrier and biochar mixture from a solid outlet of the vertical pyrolysis reactor, and enabling the mixture to enter a solid-solid separator at the temperature of 350-500 ℃; the temperature of the solid heat carrier obtained after separation is 300-450 ℃, and the solid heat carrier enters the heating riser again to form heat carrier circulation; and (3) delivering the biochar obtained after separation, or partially filling the biochar into an adsorption tower to be used as an adsorbent for adsorbing and treating the crude wood vinegar.
In the step S6, the solid heat carrier is lifted in the heating lifting furnace by the flue gas at 800-1200 ℃ generated by biomass combustion and heated to 550-800 ℃, the solid heat carrier is usually made of ceramic balls or quartz sand, and the heated solid heat carrier is sent into the vertical pyrolysis reactor from the heat carrier inlet to be mixed with the biomass for heat transfer.
The following is a specific example of pyrolyzing solid organic matter by using the pyrolysis reaction system:
case one:
the biomass material is corn straw with the particle size of 5mm and the water content of 35 percent, the processing amount is 3t/h, the dried biomass material has the water content of 4 percent and enters a vertical pyrolysis reactor, the included angle α between the vertical surface of the side part of a reactor cylinder body and the lower bottom surface is 110 degrees, the blade interval of a spiral blade is 250mm, the interval between the spiral blade and the conical surface of the side part of the reactor cylinder body is 10mm, square raised ribs are welded on the spiral blade, the height of the ribs is 25mm, and the interval between the ribs is 200 mm;
the technological parameters are as follows:
the heating temperature of the solid heat carrier is 580 ℃, the pyrolysis retention time is controlled to be 8s, the temperature of a solid mixture at a solid outlet of the vertical pyrolysis reactor is 450 ℃, wherein: the yield of the biochar is 28 percent, the heat value is 15MJ/kg, the yield of the pyrolysis oil is 35 percent, the heat value is 16MJ/kg, the yield of the pyrolysis gas is 24 percent, the heat value is 13MJ/kg, and the balance is wood vinegar. The process has the advantages of rapid reaction, high oil gas yield and high heat value.
Case two:
the biomass material is corn straw with the particle size of 50mm and the water content of 35 percent, the processing amount is 3t/h, the dried biomass material has the water content of 8 percent and enters a vertical pyrolysis reactor, the included angle α between the vertical surface of the side part of a reactor cylinder body and the lower bottom surface is 135 degrees, the blade interval of a spiral blade is 350mm, the interval between the spiral blade and the conical surface of the side part of the reactor cylinder body is 50mm, square raised ribs are welded on the spiral blade, the height of the ribs is 100mm, and the interval between the ribs is 400 mm;
the technological parameters are as follows:
the heating temperature of the solid heat carrier is 650 ℃, the pyrolysis retention time is controlled to be 360s, the temperature of a solid mixture at a solid outlet of the vertical pyrolysis reactor is 430 ℃, wherein: the yield of the biochar is 34 percent, the heat value is 15.5MJ/kg, the yield of the pyrolysis oil is 28 percent, the heat value is 15.5MJ/kg, the yield of the pyrolysis gas is 19 percent, the heat value is 13.5MJ/kg, and the rest is wood vinegar. The yield of the biochar is obviously improved under the process, and the biochar is completely carbonized.
For the embodiments of the present invention, the common general knowledge of the known specific structures and characteristics in the schemes is not described too much; the embodiments are described in a progressive manner, technical features related to the embodiments can be combined with each other on the premise of not conflicting with each other, and the same and similar parts among the embodiments can be referred to each other.
In the description of the present invention, the terms "upper", "lower", "left", "right", "horizontal", "inner", "outer", etc. indicate the orientation or positional relationship based on the orientation or positional relationship shown in the drawings, and are only for convenience of description and simplification of the description, but do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and should not be construed as limiting the present invention. Unless expressly stated or limited otherwise, the terms "mounted," "connected," and "connected" are intended to be inclusive and mean, for example, that they may be fixedly connected, detachably connected, or integrally connected; the two components can be directly connected or indirectly connected through an intermediate medium, and the two components can be communicated with each other; furthermore, the terms "primary" and "secondary" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
The above embodiments are only used to illustrate the technical solution of the present invention and not to limit the same, although the present invention is described in detail with reference to the above embodiments, those skilled in the art can still modify or equally replace the specific embodiments of the present invention, and any modification or equivalent replacement that does not depart from the spirit and scope of the present invention is within the protection scope of the claims of the present invention.
Claims (7)
1. The utility model provides a vertical pyrolytic reaction system of living beings, includes breaker (1), drying-machine (2), lifting machine (31), heating riser (4), material storehouse (32), solid separator (8), one-level condensing tower (6), second grade condensing tower (7), filter (91) and adsorption tower (92), its characterized in that still includes vertical pyrolytic reaction ware (5), wherein:
the vertical pyrolysis reactor (5) comprises a reactor cylinder body (51), and a heat carrier inlet (54), a material inlet (55) and a pyrolysis gas outlet (57) which are arranged on the reactor cylinder body (51), wherein the reactor cylinder body (51) is of a hollow round table structure with a large upper part and a small lower part, and a rotating shaft (52) is arranged at the middle shaft position of the reactor cylinder body (51); a spiral blade (53) is wound and fixed on the rotating shaft (52), and the spiral blade (53) is stirred along with the rotation of the rotating shaft (52); the heat carrier inlet (54) and the material inlet (55) are arranged on one side of the upper end of the reactor barrel (51), the pyrolysis gas outlet (57) is arranged on the opposite side of the upper end of the reactor barrel, and the heat carrier inlet (54) is higher than the material inlet (55); a solid outlet (56) for discharging a solid heat carrier and pyrolysis solid products is further formed in the side portion of the lower end of the reactor cylinder (51);
the biomass raw material sequentially passes through the crusher (1) and the dryer (2), and the dryer (2) is respectively connected with the elevator (31) and the heating lifting pipe (4) to convey biomass; the biomass input into the hoister (31) passes through the material bin (32) and then is input into the vertical pyrolysis reactor (5) from the material inlet (55), and the biomass input into the heating lifting pipe (4) is used as fuel to be combusted to generate flue gas; the heating riser (4) is connected with the heat carrier inlet (54) to input a solid heat carrier into the vertical pyrolysis reactor (5), and biomass and the solid heat carrier are mixed and then subjected to pyrolysis reaction in the vertical pyrolysis reactor (5);
the solid outlet (56) is connected with the solid separator (8) to output a solid mixture, the solid separator (8) outputs biochar, and a solid heat carrier is input into the heating riser (4) which is connected with the solid separator;
the pyrolysis gas outlet (57) is connected with a pyrolysis gas inlet (62) at the top of the primary condensing tower (6) and sends high-temperature pyrolysis gas into the primary condensing tower (6); the first-stage condensing tower (6) inputs bio-oil obtained by condensing pyrolysis gas into the connected filter (91) to filter impurities, and inputs the residual pyrolysis gas into the connected second-stage condensing tower (7); the secondary condensation tower (7) outputs biogas, crude wood vinegar obtained by condensation is input into the adsorption tower (92) to adsorb impurities, and the adsorption tower (92) outputs wood vinegar.
2. The system according to claim 1, characterized in that a plurality of stirring blades (531) are sequentially fixed on the spiral blades (53) of the vertical pyrolysis reactor (5) along the extending direction of the blades, and the stirring blades (531) are square or circular raised ribs.
3. The system according to claim 1, wherein the pyrolysis gas outlet (57) of the vertical pyrolysis reactor (5) is communicated with 1-5 side exhaust ports (571), and the side exhaust ports (571) extend into the reactor barrel (51) and are used for collecting the pyrolysis gas inside and collecting and guiding the pyrolysis gas to the pyrolysis gas outlet (57) for discharging.
4. The system of claim 1, wherein the primary condensation tower (6) is provided with a spray oil inlet (631), the outlet of the filter (91) is connected with the spray oil inlet (631), and the bio-oil is input into the primary condensation tower (6) for spraying.
5. The system according to claim 1, characterized in that the solid-solid separator (8) is connected to the adsorption column (92) and biochar is fed into the adsorption column (92) as adsorbent.
6. The system according to any one of claims 1 to 5, characterized in that the flue gas outlet of the heating riser pipe (4) is connected with the dryer (2), and the flue gas output from the heating riser pipe (4) is input into the dryer (2) to be used as a heat source for drying biomass.
7. The system according to any one of claims 1 to 5, characterized in that the pyrolysis gas inlet (62) is a conical mouth with a small top and a big bottom, and a hot smoke hood (61) is arranged outside the conical mouth, and the hot smoke hood (61) insulates the pyrolysis gas inlet (62) to prevent coking of the pyrolysis gas; the hot hood (61) comprises a flue gas inlet (611) and a flue gas outlet (612); the flue gas inlet (611) is arranged at the lower side part of the hot gas hood (61) and is connected with the flue gas outlet of the heating lifting pipe (4) to receive the flue gas from the heating lifting pipe (4); the smoke outlet (612) is arranged at the upper part of the hot smoke hood (61), is connected with the dryer (2), and outputs smoke in the hot smoke hood (61) to the dryer (2) to be used as a heat source for drying biomass.
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