CN210438685U - Device for extracting wood vinegar through straw graded heating - Google Patents
Device for extracting wood vinegar through straw graded heating Download PDFInfo
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- CN210438685U CN210438685U CN201921107570.5U CN201921107570U CN210438685U CN 210438685 U CN210438685 U CN 210438685U CN 201921107570 U CN201921107570 U CN 201921107570U CN 210438685 U CN210438685 U CN 210438685U
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- 239000010902 straw Substances 0.000 title claims abstract description 90
- 238000010438 heat treatment Methods 0.000 title claims abstract description 34
- 239000000052 vinegar Substances 0.000 title description 8
- 235000021419 vinegar Nutrition 0.000 title description 8
- 239000002023 wood Substances 0.000 title description 8
- 238000000197 pyrolysis Methods 0.000 claims abstract description 149
- 238000003763 carbonization Methods 0.000 claims abstract description 107
- 238000001035 drying Methods 0.000 claims abstract description 62
- 238000003860 storage Methods 0.000 claims abstract description 37
- 238000001816 cooling Methods 0.000 claims abstract description 19
- 238000009826 distribution Methods 0.000 claims abstract description 10
- 239000000463 material Substances 0.000 claims description 39
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 13
- 239000000428 dust Substances 0.000 claims description 13
- 230000033228 biological regulation Effects 0.000 claims description 12
- 238000002485 combustion reaction Methods 0.000 claims description 12
- 239000011276 wood tar Substances 0.000 claims description 12
- 229910052799 carbon Inorganic materials 0.000 claims description 9
- 239000007788 liquid Substances 0.000 claims description 9
- 238000000034 method Methods 0.000 claims description 8
- 239000002131 composite material Substances 0.000 claims description 6
- 230000014759 maintenance of location Effects 0.000 abstract description 12
- 239000002028 Biomass Substances 0.000 abstract description 6
- 230000002035 prolonged effect Effects 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 60
- 238000004519 manufacturing process Methods 0.000 description 20
- 239000002994 raw material Substances 0.000 description 15
- 239000000047 product Substances 0.000 description 11
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 235000013162 Cocos nucifera Nutrition 0.000 description 2
- 244000060011 Cocos nucifera Species 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 239000003610 charcoal Substances 0.000 description 2
- 210000003608 fece Anatomy 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 244000144972 livestock Species 0.000 description 2
- 239000010871 livestock manure Substances 0.000 description 2
- 244000144977 poultry Species 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 229920002488 Hemicellulose Polymers 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 239000002537 cosmetic Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 235000011869 dried fruits Nutrition 0.000 description 1
- 229940117927 ethylene oxide Drugs 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 229920005610 lignin Polymers 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- -1 pyroligneous liquor Substances 0.000 description 1
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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
A device for extracting pyroligneous from straws by staged heating comprises a drying unit, a low-temperature pyrolysis unit, a high-temperature carbonization unit, a biochar cooling storage unit and a heat energy generation and distribution unit; the volume of the low-temperature pyrolysis furnace contained in the low-temperature pyrolysis unit is 1.5-3 times of the volume of the high-temperature carbonization furnace contained in the high-temperature carbonization unit, so that the retention time of the straws in the low-temperature pyrolysis furnace is prolonged, the low-temperature pyrolysis of the straws is more sufficient, and more high-quality pyroligneous liquor products are produced; meanwhile, the low-temperature pyrolysis unit is provided with two stages of series-connected tubular heat exchangers with different working temperatures, and biomass oil and pyroligneous liquor are separated by using temperature difference, so that the quality of the pyroligneous liquor is further improved.
Description
Technical Field
The utility model relates to a crop straw carbomorphism technical field, concretely relates to straw staged heating draws pyroligneous device.
Background
The existing crop straw carbonization device mainly comprises a drying furnace and a carbonization furnace, wherein crop straws are heated in the carbonization furnace to a certain temperature, and crude fibers, cellulose, hemicellulose and lignin in the straws are thermally decomposed to generate products such as pyroligneous liquor, methanol, biomass oil, methane, ethylene, carbon monoxide, biochar and the like; wherein, methane, ethylene and carbon monoxide are introduced into a burner to burn, and provide a heat source for the crop straw carbonization device; the wood vinegar, the biomass oil and the biochar are main products after the crop straws are carbonized; in order to achieve higher main product yield and production efficiency, the optimal temperature of the carbonization furnace is generally set to be 450-600 ℃, and under the temperature and the action of oxygen, the impurity content of the wood vinegar liquid and the biomass oil is high and the quality is low; in addition, the variety of the produced biochar is single at the temperature, so that the comprehensive economic benefit of crop straw carbonization is influenced;
the national invention patent with the application number of CN201811142541.2 discloses a system and a method for the graded carbonization of livestock and poultry manure, wherein a carbonization furnace is divided into a low-temperature carbonization furnace and a high-temperature carbonization furnace and is used for separating carbon dioxide, water vapor and combustible gas so as to improve the heat value of the combustible gas; the utility model is mainly designed aiming at the characteristics of high water content of livestock and poultry manure, high carbon dioxide content in the carbonization process and fuel gas generated in the high-temperature carbonization furnace, and obviously cannot be applied to the carbonization of crop straws for the characteristics of high dust and low water content of the crop straws and combustible gas generated by the low-temperature carbonization furnace and the high-temperature carbonization furnace in the carbonization process;
the utility model patent of application No. 2019207064695.5 discloses a straw grading carbonization device, which is divided into a low-temperature pyrolysis carbonization furnace and a high-temperature pyrolysis carbonization furnace, and the straws are pyrolyzed and carbonized twice at low temperature and high temperature to finally produce high-quality biochar products; the production process of the device ensures the continuity of production, and the low-temperature and high-temperature pyrolysis carbonization time is basically the same, so that the low-temperature pyrolysis carbonization time is shorter, the yield of the pyroligneous liquor as a byproduct is lower, and the impurity content of the pyroligneous liquor generated by high-temperature pyrolysis carbonization is high, thereby finally influencing the yield and quality of the pyroligneous liquor; the wood vinegar has wide application and market prospect, and can be used in the fields of agriculture, food processing, cosmetics and the like, so that the improvement of the yield and the quality of the wood vinegar in the straw carbonization process has important economic value; in addition, the heat energy generated by the combustion of the pyrolysis gas generated by the device in the production process through the combustor is actually far greater than the heat energy required by the device for production, so that a large amount of heat energy can be directly discharged, the energy waste is caused, and the carbon dioxide emission is increased.
SUMMERY OF THE UTILITY MODEL
In order to overcome the defects in the background art, the utility model discloses a device for extracting pyroligneous by heating straw in stages, which comprises a drying unit, a low-temperature pyrolysis unit, a high-temperature carbonization unit, a biochar cooling storage unit and a heat energy generation and distribution unit; the volume of the low-temperature pyrolysis furnace contained in the low-temperature pyrolysis unit is 1.5-3 times of the volume of the high-temperature carbonization furnace contained in the high-temperature carbonization unit, so that the retention time of the straws in the low-temperature pyrolysis furnace is prolonged, the low-temperature pyrolysis of the straws is more sufficient, and more high-quality pyroligneous liquor products are produced; meanwhile, the low-temperature pyrolysis unit is provided with two stages of series-connected tubular heat exchangers with different working temperatures, and biomass oil and pyroligneous liquor are separated by using temperature difference, so that the quality of the pyroligneous liquor is further improved.
In order to realize the utility model aims at, the utility model adopts the following technical scheme: a device for extracting pyroligneous from straws by staged heating comprises a drying unit, a low-temperature pyrolysis unit, a high-temperature carbonization unit, a biochar cooling storage unit and a heat energy generation and distribution unit; the drying unit, the low-temperature pyrolysis unit and the high-temperature carbonization unit are connected with the material conveying device through pipelines; the low-temperature pyrolysis unit and the high-temperature carbonization unit are connected with the heat energy generation and distribution unit through pipelines; the high-temperature carbonization unit is connected with the biochar cooling storage unit through a material conveying device; the biochar cooling storage unit is connected with the drying unit through a pipeline; the method is characterized in that: the drying unit comprises a drying furnace; the low-temperature pyrolysis unit comprises a low-temperature pyrolysis furnace; the high-temperature carbonization unit comprises a high-temperature carbonization furnace; the volume of the low-temperature pyrolysis furnace is 1.5-3 times of that of the high-temperature carbonization furnace.
Further, the drying unit comprises a drying furnace and a dust remover; the drying furnace is obliquely arranged, a straw inlet, a hot air inlet, a cold air outlet and a straw outlet are arranged on the drying furnace, and the height of the straw inlet is greater than that of the straw outlet; the straw inlet is provided with a material conveying device; the hot air inlet is connected with the low-temperature pyrolysis unit, the high-temperature carbonization unit and the biochar cooling storage unit through pipelines; the cold air outlet is connected with a dust remover through a pipeline; the straw outlet is provided with a material conveying device; the dust remover is connected with a chimney.
Further, the low-temperature pyrolysis unit comprises a low-temperature pyrolysis furnace, a first tubular heat exchanger, a second tubular heat exchanger, a wood tar storage tank and a wood vinegar storage tank; the low-temperature pyrolysis furnace is provided with a straw inlet, a low-temperature gas outlet, a pyrolysis gas outlet and a low-temperature carbon outlet; the straw inlet is connected with the straw outlet of the drying furnace through the material conveying device; the low-temperature gas outlet is connected with the dust remover through a pipeline; the pyrolysis gas outlet is connected with the first tubular heat exchanger through a pipeline; the first shell and tube heat exchanger is connected with the second shell and tube heat exchanger through a pipeline; the low-temperature carbon outlet is provided with a material conveying device;
the first tubular heat exchanger is provided with a pyrolysis gas inlet A, a wood tar outlet, a pyrolysis gas outlet A, a cold air inlet A and a hot air outlet A; the pyrolysis gas inlet A is connected with a pyrolysis gas outlet of the low-temperature pyrolysis furnace through a pipeline; the wood tar outlet is connected with a wood tar storage tank through a pipeline; the pyrolysis gas outlet A is connected with the second tube type heat exchanger through a pipeline; the cold air inlet A is connected with a fan A; the hot air outlet A is connected with a hot air inlet of the drying furnace through a pipeline;
the second shell and tube heat exchanger is provided with a pyrolysis gas inlet B, a pyroligneous liquid outlet, a pyrolysis gas outlet B, a cold air inlet B and a hot air outlet B; the pyrolysis gas inlet B is connected with the pyrolysis gas outlet A through a pipeline; the pyroligneous liquor outlet is connected with a pyroligneous liquor storage tank through a pipeline; the pyrolysis gas outlet B is connected with the heat energy generating and distributing unit through a pipeline; the cold air inlet B is connected with a fan B; the hot air outlet B is connected with a chimney through a pipeline;
the first tubular heat exchanger is provided with a temperature measuring device A, and the second tubular heat exchanger is provided with a temperature measuring device B; the fan A driving device is a variable frequency motor A which is electrically connected with a frequency converter A; the fan B driving device is a variable frequency motor B which is electrically connected with a frequency converter B; the temperature measuring device A is electrically connected with the frequency converter A; the temperature measuring device B is electrically connected with the frequency converter B; the output frequency of the frequency converter A is controlled by the difference between the actual temperature measured by the temperature measuring device A and the working temperature set by the first tubular heat exchanger; and the output frequency of the frequency converter B is controlled by the difference between the actual temperature measured by the temperature measuring device B and the working temperature set by the second shell and tube heat exchanger.
Further, the high-temperature carbonization unit comprises a high-temperature carbonization furnace; the high-temperature carbonization furnace is provided with a biochar inlet, a pyrolysis gas outlet and a biochar outlet; the biochar inlet is connected with a low-temperature carbon outlet of the low-temperature pyrolysis furnace through a material conveying device; the pyrolysis gas outlet is connected with the heat energy generating and distributing unit through a pipeline; the biochar outlet is provided with a material conveying device.
Further, the biochar cooling storage unit comprises a dividing wall type heat exchanger and a biochar storage tank; the dividing wall type heat exchanger is provided with a biochar inlet, a biochar outlet, a cold air inlet and a hot air outlet; the biochar inlet is connected with the biochar outlet of the high-temperature carbonization furnace through the material conveying device; the biochar outlet is connected with a biochar storage tank through a material conveying device; the cold air inlet is connected with a fan; the hot air outlet is connected with the hot air inlet of the drying oven through a pipeline.
Further, the heat energy generating and distributing unit comprises a burner, and a combustible gas inlet and a flow dividing regulation control device are arranged on the burner; the burner is connected with a pyrolysis gas outlet B of the second shell and tube heat exchanger through a pipeline; the shunting regulation control device is provided with a high-temperature hot gas outlet A and a high-temperature hot gas outlet B.
Furthermore, the low-temperature pyrolysis furnace and the high-temperature carbonization furnace are double-layer furnace bodies, the outer layer furnace body is of a fixed structure, the inner layer furnace body is of a rotating structure, and a high-temperature hot gas inlet and a low-temperature hot gas outlet are formed in the outer layer furnace body; heating spaces are formed between the outer layer furnace body and the inner layer furnace body of the low-temperature pyrolysis furnace and the high-temperature carbonization furnace; a high-temperature hot gas inlet of the low-temperature pyrolysis furnace is connected with a high-temperature hot gas outlet A of a shunting regulation control device on the combustion furnace through a pipeline; the high-temperature hot gas inlet of the high-temperature carbonization furnace is connected with a high-temperature hot gas outlet B of a shunting regulation control device on the combustion furnace through a pipeline; and the low-temperature hot gas outlets of the low-temperature pyrolysis furnace and the high-temperature carbonization furnace are connected with the hot air inlet of the drying furnace through pipelines.
Further, the material conveying device at the straw inlet of the drying furnace is a mesh belt type lifter and screw conveyor composite device; the material conveying device at the straw inlet of the low-temperature pyrolysis furnace is a mesh belt type elevator and screw conveyor composite device; the material conveying devices of the biochar inlet and the biochar outlet of the high-temperature carbonization furnace are pipeline furnace devices.
Furthermore, temperature measuring devices are arranged on the low-temperature pyrolysis furnace and the high-temperature carbonization furnace and are connected with a shunting adjustment control device of the combustion furnace through a lead.
When the device for extracting pyroligneous from straws by staged heating works, raw materials are sequentially conveyed to a drying furnace, a low-temperature pyrolysis furnace and a high-temperature carbonization furnace in a continuous feeding mode; the retention time of the raw materials in the drying furnace is 40-50 minutes; the temperature of the low-temperature pyrolysis furnace is controlled to be 200-250 ℃, and the retention time of the raw materials in the low-temperature pyrolysis furnace is 60-150 minutes; the temperature of the high-temperature carbonization furnace is controlled to be 600-900 ℃, and the retention time of the raw materials in the high-temperature carbonization furnace is 40-50 minutes; the temperature of the first tubular heat exchanger is controlled to be 110-130 ℃; the temperature of the first tubular heat exchanger is controlled to be 85-110 ℃.
Due to the adoption of the technical scheme, the utility model discloses following beneficial effect has: the utility model discloses a device for extracting pyroligneous liquid by heating straw in stages, which comprises a drying unit, a low-temperature pyrolysis unit, a high-temperature carbonization unit, a biochar cooling storage unit and a heat energy generation and distribution unit; the volume of the low-temperature pyrolysis furnace contained in the low-temperature pyrolysis unit is 1.5-3 times of the volume of the high-temperature carbonization furnace contained in the high-temperature carbonization unit, so that the retention time of the straws in the low-temperature pyrolysis furnace is prolonged, the low-temperature pyrolysis of the straws is more sufficient, and more high-quality pyroligneous liquor products are produced; meanwhile, the low-temperature pyrolysis unit is provided with two stages of tubular heat exchangers connected in series at different working temperatures, and biomass oil and pyroligneous liquor are separated by using temperature difference, so that the purity of the pyroligneous liquor is further improved; the device for extracting pyroligneous liquid by graded heating of straws of the utility model can control ash content of finally produced biochar products better due to more sufficient low-temperature pyrolysis of straws, thereby indirectly improving the quality of the biochar products; meanwhile, the device for extracting the pyroligneous liquor by graded heating of the straws reduces the amount of the pyrolysis gas generated in the production process, the heat energy generated by the combustion of the pyrolysis gas by a burner is basically balanced with the heat energy required by the device production, the waste of the heat energy is reduced, and the emission of carbon dioxide is also reduced; in addition the utility model discloses a straw heating in grades draws pyrolkigneous liquid device uses the mode of biological charcoal as the main product to become with traditional straw carbonization output and uses pyrolkigneous liquid to be the mode of main product, can produce high-quality pyrolkigneous liquid and biological charcoal product simultaneously, consequently very big improvement the economic value of straw carbonization.
Drawings
FIG. 1 is a schematic connection diagram of a device for extracting pyroligneous liquor by staged heating of straws.
In the figure: 1. a drying unit; 2. a low temperature pyrolysis unit; 3. a high temperature carbonization unit; 4. a biochar cooling storage unit; 5. a heat energy generating and distributing unit.
Detailed Description
The invention will be explained in more detail by the following examples, which disclose the invention and are intended to protect all technical improvements within the scope of the invention.
A device for extracting pyroligneous by heating straw in stages comprises a drying unit 1, a low-temperature pyrolysis unit 2, a high-temperature carbonization unit 3, a biochar cooling storage unit 4 and a heat energy generation and distribution unit 5; the drying unit 1, the low-temperature pyrolysis unit 2 and the high-temperature carbonization unit 3 are connected with a material conveying device through pipelines; the low-temperature pyrolysis unit 2 and the high-temperature carbonization unit 3 are connected with the heat energy generation and distribution unit 5 through pipelines; the high-temperature carbonization unit 3 is connected with the biochar cooling storage unit 4 through a material conveying device; the biochar cooling storage unit 4 is connected with the drying unit 1 through a pipeline; the method is characterized in that: the drying unit 1 includes a drying oven; the low-temperature pyrolysis unit 2 comprises a low-temperature pyrolysis furnace; the high-temperature carbonization unit 3 comprises a high-temperature carbonization furnace; the volume of the low-temperature pyrolysis furnace is 1.5-3 times of that of the high-temperature carbonization furnace;
the drying unit 1 comprises a drying furnace and a dust remover; the drying furnace is obliquely arranged, a straw inlet, a hot air inlet, a cold air outlet and a straw outlet are arranged on the drying furnace, and the height of the straw inlet is greater than that of the straw outlet; the straw inlet is provided with a material conveying device; the hot air inlet is connected with the low-temperature pyrolysis unit 2, the high-temperature carbonization unit 3 and the biochar cooling storage unit 4 through pipelines; the cold air outlet is connected with a dust remover through a pipeline; the straw outlet is provided with a material conveying device; the dust remover is connected with a chimney;
the low-temperature pyrolysis unit 2 comprises a low-temperature pyrolysis furnace, a first tubular heat exchanger, a second tubular heat exchanger, a wood tar storage tank and a pyroligneous liquor storage tank; the low-temperature pyrolysis furnace is provided with a straw inlet, a low-temperature gas outlet, a pyrolysis gas outlet and a low-temperature carbon outlet; the straw inlet is connected with the straw outlet of the drying furnace through the material conveying device; the low-temperature gas outlet is connected with the dust remover through a pipeline; the pyrolysis gas outlet is connected with the first tubular heat exchanger through a pipeline; the first shell and tube heat exchanger is connected with the second shell and tube heat exchanger through a pipeline; the low-temperature carbon outlet is provided with a material conveying device;
the first tubular heat exchanger is provided with a pyrolysis gas inlet A, a wood tar outlet, a pyrolysis gas outlet A, a cold air inlet A and a hot air outlet A; the pyrolysis gas inlet A is connected with a pyrolysis gas outlet of the low-temperature pyrolysis furnace through a pipeline; the wood tar outlet is connected with a wood tar storage tank through a pipeline; the pyrolysis gas outlet A is connected with the second tube type heat exchanger through a pipeline; the cold air inlet A is connected with a fan A; the hot air outlet A is connected with a hot air inlet of the drying furnace through a pipeline;
the second shell and tube heat exchanger is provided with a pyrolysis gas inlet B, a pyroligneous liquid outlet, a pyrolysis gas outlet B, a cold air inlet B and a hot air outlet B; the pyrolysis gas inlet B is connected with the pyrolysis gas outlet A through a pipeline; the pyroligneous liquor outlet is connected with a pyroligneous liquor storage tank through a pipeline; the pyrolysis gas outlet B is connected with the heat energy generating and distributing unit 5 through a pipeline; the cold air inlet B is connected with a fan B; the hot air outlet B is connected with a chimney through a pipeline;
the first tubular heat exchanger is provided with a temperature measuring device A, and the second tubular heat exchanger is provided with a temperature measuring device B; the fan A driving device is a variable frequency motor A which is electrically connected with a frequency converter A; the fan B driving device is a variable frequency motor B which is electrically connected with a frequency converter B; the temperature measuring device A is electrically connected with the frequency converter A; the temperature measuring device B is electrically connected with the frequency converter B;
the high-temperature carbonization unit 3 comprises a high-temperature carbonization furnace; the high-temperature carbonization furnace is provided with a biochar inlet, a pyrolysis gas outlet and a biochar outlet; the biochar inlet is connected with a low-temperature carbon outlet of the low-temperature pyrolysis furnace through a material conveying device; the pyrolysis gas outlet is connected with the heat energy generating and distributing unit 5 through a pipeline; the biochar outlet is provided with a material conveying device;
the biochar cooling storage unit 4 comprises a dividing wall type heat exchanger and a biochar storage tank; the dividing wall type heat exchanger is provided with a biochar inlet, a biochar outlet, a cold air inlet and a hot air outlet; the biochar inlet is connected with the biochar outlet of the high-temperature carbonization furnace through the material conveying device; the biochar outlet is connected with a biochar storage tank through a material conveying device; the cold air inlet is connected with a fan; the hot air outlet is connected with a hot air inlet of the drying furnace through a pipeline;
the heat energy generating and distributing unit 5 comprises a burner, and a combustible gas inlet and a flow distribution adjusting and controlling device are arranged on the burner; the burner is connected with a pyrolysis gas outlet B of the second shell and tube heat exchanger through a pipeline; the shunting regulation control device is provided with a high-temperature hot gas outlet A and a high-temperature hot gas outlet B;
the low-temperature pyrolysis furnace and the high-temperature carbonization furnace are double-layer furnace bodies, the outer layer furnace body is of a fixed structure, the inner layer furnace body is of a rotating structure, and a high-temperature hot gas inlet and a low-temperature hot gas outlet are formed in the outer layer furnace body; heating spaces are formed between the outer layer furnace body and the inner layer furnace body of the low-temperature pyrolysis furnace and the high-temperature carbonization furnace; a high-temperature hot gas inlet of the low-temperature pyrolysis furnace is connected with a high-temperature hot gas outlet A of a shunting regulation control device on the combustion furnace through a pipeline; the high-temperature hot gas inlet of the high-temperature carbonization furnace is connected with a high-temperature hot gas outlet B of a shunting regulation control device on the combustion furnace through a pipeline; the low-temperature hot gas outlets of the low-temperature pyrolysis furnace and the high-temperature carbonization furnace are connected with the hot air inlet of the drying furnace through a pipeline;
the material conveying device at the straw inlet of the drying furnace is a mesh belt type elevator and screw conveyor composite device; the material conveying device at the straw inlet of the low-temperature pyrolysis furnace is a mesh belt type elevator and screw conveyor composite device; the material conveying devices at the biochar inlet and the biochar outlet of the high-temperature carbonization furnace are pipeline furnace devices;
the low-temperature pyrolysis furnace and the high-temperature carbonization furnace are provided with temperature measuring devices, and the temperature measuring devices are connected with a shunting regulation control device of the combustion furnace through wires.
When the device for extracting the pyroligneous from the straws by staged heating is implemented, the production period is directly related to the volume settings of the drying furnace, the low-temperature pyrolysis furnace and the high-temperature carbonization furnace:
when the volume ratio of the drying furnace to the low-temperature pyrolysis furnace to the high-temperature carbonization furnace is set to be 1:1.5:1, namely the volume of the low-temperature pyrolysis furnace is 1.5 times that of the high-temperature carbonization furnace, the production cycle of the device for extracting pyroligneous liquor by graded heating of straws is 140-175 minutes, and the straws are basically pyrolyzed at low temperature in the low-temperature pyrolysis furnace, so that the production efficiency is high;
when the volume ratio of the drying furnace to the low-temperature pyrolysis furnace to the high-temperature carbonization furnace is set to be 1:2:1, namely the volume of the low-temperature pyrolysis furnace is 2 times that of the high-temperature carbonization furnace, the production cycle of the device for extracting the pyroligneous liquor by graded heating of the straws is 160-200 minutes, the straws are fully pyrolyzed in the low-temperature pyrolysis furnace, and the pyroligneous liquor has good balance between the yield of the pyroligneous liquor and the production efficiency;
when the volume ratio of the drying furnace to the low-temperature pyrolysis furnace to the high-temperature carbonization furnace is set to be 1:3:1, namely the volume of the low-temperature pyrolysis furnace is 3 times that of the high-temperature carbonization furnace, the production cycle of the device for extracting pyroligneous liquor by graded heating of straws is 200-250 minutes, the straws are completely pyrolyzed in the low-temperature pyrolysis furnace, the pyroligneous liquor yield is high, and the production efficiency is relatively low.
When the device for extracting the pyroligneous from the straws by staged heating is used for production, the temperature parameters of the drying furnace and the low-temperature pyrolysis furnace are set according to the difference of raw materials: when the raw material is crop straws, the temperature of the drying furnace is set to be 100 ℃, and the temperature of the low-temperature pyrolysis furnace is set to be 200 ℃; when the raw materials are dried fruit shells and coconut shells, the temperature of the drying furnace is set to be 120 ℃, and the temperature of the low-temperature pyrolysis furnace is set to be 250 ℃.
When the device for extracting pyroligneous from straws by staged heating is used for production, the temperature parameters of the high-temperature carbonization furnace are set according to the purpose of the produced biochar: when the produced biochar is used for fuel combustion, the temperature of a high-temperature carbonization furnace is set to be 500 ℃; when the produced biochar is used for filtering and adsorbing impurities, the temperature of a high-temperature carbonization furnace is set to be 750 ℃; when the produced biochar is used for farmland improvement, the temperature of the high-temperature carbonization furnace is set to 900 ℃.
Taking a straw graded heating and wood vinegar extracting device with a volume ratio of a drying furnace, a low-temperature pyrolysis furnace and a high-temperature carbonization furnace set to be 1:2:1 as an example, the method for producing the biological activated carbon for improving the farmland comprises the following process parameters when the production raw materials are crop straws: the temperature of the drying furnace is controlled at 100 ℃; the retention time of the raw materials in the drying furnace is 40 minutes; the temperature of the low-temperature pyrolysis furnace is controlled at 200 ℃, and the retention time of the raw materials in the low-temperature pyrolysis furnace is 80 minutes; the temperature of the high-temperature carbonization furnace is controlled at 900 ℃, and the retention time of the raw materials in the high-temperature carbonization furnace is 40 minutes.
Taking a device for heating and extracting pyroligneous liquor by straw in stages with the volume ratio of a drying furnace, a low-temperature pyrolysis furnace and a high-temperature carbonization furnace set to be 1:2:1 as an example, the device is used for producing biological activated carbon for filtering and adsorbing impurities, and the production raw materials are coconut shells, and the technological parameters are as follows: the temperature of the drying furnace is controlled at 120 ℃; the retention time of the raw materials in the drying furnace is 50 minutes; the temperature of the low-temperature pyrolysis furnace is controlled to be 250 ℃, and the retention time of the raw materials in the low-temperature pyrolysis furnace is 100 minutes; the temperature of the high-temperature carbonization furnace is controlled at 750 ℃, and the retention time of the raw materials in the high-temperature carbonization furnace is 50 minutes.
When the device for extracting the pyroligneous from the straws by staged heating is used for production, the temperature of the first tubular heat exchanger is set to be 120 ℃, and the temperature of the second tubular heat exchanger is set to be 90 ℃.
The part of the utility model not detailed is prior art.
Claims (9)
1. A device for extracting pyroligneous by heating straw in stages comprises a drying unit (1), a low-temperature pyrolysis unit (2), a high-temperature carbonization unit (3), a biochar cooling storage unit (4) and a heat energy generating and distributing unit (5); the drying unit (1), the low-temperature pyrolysis unit (2) and the high-temperature carbonization unit (3) are connected with a material conveying device through pipelines; the low-temperature pyrolysis unit (2) and the high-temperature carbonization unit (3) are connected with the heat energy generation and distribution unit (5) through pipelines; the high-temperature carbonization unit (3) is connected with the biochar cooling storage unit (4) through a material conveying device; the biochar cooling storage unit (4) is connected with the drying unit (1) through a pipeline; the method is characterized in that: the drying unit (1) comprises a drying oven; the low-temperature pyrolysis unit (2) comprises a low-temperature pyrolysis furnace; the high-temperature carbonization unit (3) comprises a high-temperature carbonization furnace; the volume of the low-temperature pyrolysis furnace is 1.5-3 times of that of the high-temperature carbonization furnace.
2. The device for extracting pyroligneous liquor by graded heating of straws as claimed in claim 1, which is characterized in that: the drying unit (1) comprises a drying furnace and a dust remover; the drying furnace is obliquely arranged, a straw inlet, a hot air inlet, a cold air outlet and a straw outlet are arranged on the drying furnace, and the height of the straw inlet is greater than that of the straw outlet; the straw inlet is provided with a material conveying device; the hot air inlet is connected with the low-temperature pyrolysis unit (2), the high-temperature carbonization unit (3) and the biochar cooling storage unit (4) through pipelines; the cold air outlet is connected with a dust remover through a pipeline; the straw outlet is provided with a material conveying device; the dust remover is connected with a chimney.
3. The device for extracting pyroligneous liquor by graded heating of straws as claimed in claim 1, which is characterized in that: the low-temperature pyrolysis unit (2) comprises a low-temperature pyrolysis furnace, a first tubular heat exchanger, a second tubular heat exchanger, a wood tar storage tank and a pyroligneous liquor storage tank; the low-temperature pyrolysis furnace is provided with a straw inlet, a low-temperature gas outlet, a pyrolysis gas outlet and a low-temperature carbon outlet; the straw inlet is connected with the straw outlet of the drying furnace through the material conveying device; the low-temperature gas outlet is connected with the dust remover through a pipeline; the pyrolysis gas outlet is connected with the first tubular heat exchanger through a pipeline; the first shell and tube heat exchanger is connected with the second shell and tube heat exchanger through a pipeline; the low-temperature carbon outlet is provided with a material conveying device;
the first tubular heat exchanger is provided with a pyrolysis gas inlet A, a wood tar outlet, a pyrolysis gas outlet A, a cold air inlet A and a hot air outlet A; the pyrolysis gas inlet A is connected with a pyrolysis gas outlet of the low-temperature pyrolysis furnace through a pipeline; the wood tar outlet is connected with a wood tar storage tank through a pipeline; the pyrolysis gas outlet A is connected with the second tube type heat exchanger through a pipeline; the cold air inlet A is connected with a fan A; the hot air outlet A is connected with a hot air inlet of the drying furnace through a pipeline;
the second shell and tube heat exchanger is provided with a pyrolysis gas inlet B, a pyroligneous liquid outlet, a pyrolysis gas outlet B, a cold air inlet B and a hot air outlet B; the pyrolysis gas inlet B is connected with the pyrolysis gas outlet A through a pipeline; the pyroligneous liquor outlet is connected with a pyroligneous liquor storage tank through a pipeline; the pyrolysis gas outlet B is connected with the heat energy generating and distributing unit (5) through a pipeline; the cold air inlet B is connected with a fan B; the hot air outlet B is connected with a chimney through a pipeline;
the first tubular heat exchanger is provided with a temperature measuring device A, and the second tubular heat exchanger is provided with a temperature measuring device B; the fan A driving device is a variable frequency motor A which is electrically connected with a frequency converter A; the fan B driving device is a variable frequency motor B which is electrically connected with a frequency converter B; the temperature measuring device A is electrically connected with the frequency converter A; the temperature measuring device B is electrically connected with the frequency converter B.
4. The device for extracting pyroligneous liquor by graded heating of straws as claimed in claim 1, which is characterized in that: the high-temperature carbonization furnace is provided with a biochar inlet, a pyrolysis gas outlet and a biochar outlet; the biochar inlet is connected with a low-temperature carbon outlet of the low-temperature pyrolysis furnace through a material conveying device; the pyrolysis gas outlet is connected with the heat energy generating and distributing unit (5) through a pipeline; the biochar outlet is provided with a material conveying device.
5. The device for extracting pyroligneous liquor by graded heating of straws as claimed in claim 1, which is characterized in that: the biochar cooling storage unit (4) comprises a dividing wall type heat exchanger and a biochar storage tank; the dividing wall type heat exchanger is provided with a biochar inlet, a biochar outlet, a cold air inlet and a hot air outlet; the biochar inlet is connected with the biochar outlet of the high-temperature carbonization furnace through the material conveying device; the biochar outlet is connected with a biochar storage tank through a material conveying device; the cold air inlet is connected with a fan; the hot air outlet is connected with the hot air inlet of the drying oven through a pipeline.
6. The device for extracting pyroligneous liquor by graded heating of straws as claimed in claim 1, which is characterized in that: the heat energy generating and distributing unit (5) comprises a combustor, and a combustible gas inlet and a flow distribution adjusting and controlling device are arranged on the combustor; the burner is connected with a pyrolysis gas outlet B of the second shell and tube heat exchanger through a pipeline; the shunting regulation control device is provided with a high-temperature hot gas outlet A and a high-temperature hot gas outlet B.
7. The device for extracting pyroligneous liquor by graded heating of straws as claimed in claim 1, which is characterized in that: the low-temperature pyrolysis furnace and the high-temperature carbonization furnace are double-layer furnace bodies, the outer layer furnace body is of a fixed structure, the inner layer furnace body is of a rotating structure, and a high-temperature hot gas inlet and a low-temperature hot gas outlet are formed in the outer layer furnace body; heating spaces are formed between the outer layer furnace body and the inner layer furnace body of the low-temperature pyrolysis furnace and the high-temperature carbonization furnace; a high-temperature hot gas inlet of the low-temperature pyrolysis furnace is connected with a high-temperature hot gas outlet A of a shunting regulation control device on the combustion furnace through a pipeline; the high-temperature hot gas inlet of the high-temperature carbonization furnace is connected with a high-temperature hot gas outlet B of a shunting regulation control device on the combustion furnace through a pipeline; and the low-temperature hot gas outlets of the low-temperature pyrolysis furnace and the high-temperature carbonization furnace are connected with the hot air inlet of the drying furnace through pipelines.
8. The device for extracting pyroligneous liquor by graded heating of straws as claimed in claim 1, which is characterized in that: the material conveying device at the straw inlet of the drying furnace is a mesh belt type elevator and screw conveyor composite device; the material conveying device at the straw inlet of the low-temperature pyrolysis furnace is a mesh belt type elevator and screw conveyor composite device; the material conveying devices of the biochar inlet and the biochar outlet of the high-temperature carbonization furnace are pipeline furnace devices.
9. The device for extracting pyroligneous liquor by graded heating of straws as claimed in claim 1, which is characterized in that: the low-temperature pyrolysis furnace and the high-temperature carbonization furnace are provided with temperature measuring devices, and the temperature measuring devices are connected with a shunting regulation control device of the combustion furnace through wires.
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| CN201921107570.5U CN210438685U (en) | 2019-07-16 | 2019-07-16 | Device for extracting wood vinegar through straw graded heating |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110240919A (en) * | 2019-07-16 | 2019-09-17 | 洛阳佳易新能源技术有限公司 | A kind of stalk progressive solution extracts wood vinegar device and production technology |
| CN111804277A (en) * | 2020-07-23 | 2020-10-23 | 黄瑞要 | Method for preparing charcoal activated carbon combustible gas bio-oil from crop straws |
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2019
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110240919A (en) * | 2019-07-16 | 2019-09-17 | 洛阳佳易新能源技术有限公司 | A kind of stalk progressive solution extracts wood vinegar device and production technology |
| CN111804277A (en) * | 2020-07-23 | 2020-10-23 | 黄瑞要 | Method for preparing charcoal activated carbon combustible gas bio-oil from crop straws |
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