A biomass graphene production device and process

Abstract

The invention discloses a biomass graphene production device and process, including a gasifier, a first cyclone dust collector, a first heating interlayer, a gas-liquid separator, a catalytic adsorption purifier, a flushing liquid ejector and a flushing gas storage tank connected in sequence, a negative pressure spiral low temperature pyrolysis purifier and a negative pressure spiral high temperature pyrolysis carbonization machine are respectively connected to the gas outlet of the flushing gas storage tank, and the negative pressure spiral low temperature pyrolysis purifier and the negative pressure spiral high temperature pyrolysis carbonization machine are respectively connected to the high temperature tail gas inlet of the heat exchanger, and a spray dryer is connected to the hot air outlet of the heat exchanger; the first heating interlayer is arranged on the spiral dryer, and the spiral dryer, the negative pressure spiral low temperature pyrolysis purifier, the negative pressure spiral high temperature pyrolysis carbonization machine, the graphite crusher, the negative pressure cavitation permeation tank, the high pressure puffing stripping machine, the stripping suspension storage tank, the delivery pump, the spray dryer and the cyclone collector are connected in sequence. The invention improves the energy utilization rate and yield when producing graphene.

Description

Technical Field

[0001] The present invention relates to the technical field of graphene production, and in particular to a biomass graphene production device and process. Background Art

[0002] As a new carbon-based material, graphene has excellent optical, electrical, thermal and mechanical properties, and has broad application prospects in the fields of electronic information, new materials, new energy, biomedicine, etc. It is becoming the focus of the global new technology and new industry revolution. With the rapid development of economic and industrial technology, graphene is receiving more and more attention.

[0003] At present, there are three main ways to prepare graphene materials. The first is to use natural mineral graphite as raw material, mainly including mechanical exfoliation, oxidation-reduction method, and liquid phase mechanical exfoliation method. The second is to use natural gas, methane and other combustible gas organic carbon sources as raw materials, chemical vapor deposition method, and the third is to use biomass solids as raw materials to synthesize biomass graphene. The above existing graphene preparation methods have the problems of complex preparation process, poor production safety, high production cost, harsh reaction conditions, low output and yield, etc., which are difficult to industrialize and greatly limit the application and development of graphene materials. Summary of the invention

[0004] The purpose of the present invention is to provide a biomass graphene production device and process to solve the problems existing in the above-mentioned prior art and improve the energy utilization rate and yield when producing graphene.

[0005] To achieve the above object, the present invention provides the following solutions:

[0006] The present invention provides a biomass graphene production device and process, comprising a gasifier (1), a first cyclone dust collector (105), a first heating interlayer (304), a gas-liquid separator (4), a catalytic adsorption purifier (6), a flushing liquid ejector (7) and a flushing gas storage tank (8) which are sequentially connected through pipelines; a negative pressure spiral low-temperature pyrolysis purifier (10) and a negative pressure spiral high-temperature pyrolysis carbonization machine (11) are respectively connected to the gas outlet of the flushing gas storage tank (8); the negative pressure spiral low-temperature pyrolysis purifier (10) and the negative pressure spiral high-temperature pyrolysis carbonization machine (11) are respectively connected to the high-temperature tail gas inlet of a heat exchanger (19); a spray dryer (17) is connected to the hot air outlet of the heat exchanger (19); and the tail gas catalytic adsorption purifier (6) is connected to the hot air outlet of the heat exchanger (19); The purifier (20) is connected to the cooling tail gas outlet of the heat exchanger (19); the first heating interlayer (304) is arranged on the spiral dryer (3); the spiral dryer (3), the negative pressure spiral low-temperature pyrolysis purifier (10), the negative pressure spiral high-temperature pyrolysis carbonization machine (11), the graphite crusher (12), the negative pressure cavitation permeation tank (13), the high pressure puffing stripping machine (14), the stripping suspension storage tank (15), the delivery pump (16), the spray dryer (17) and the cyclone collector (18) are connected in sequence; the water vapor outlet (301) of the spiral dryer (3) is also connected to the gasifier (1); and the liquid outlet of the gas-liquid separator (4) is connected to the biomass vinegar liquid storage tank (5).

[0007] Preferably, it further comprises a raw material crusher (2), the discharge port of the raw material crusher (2) being connected to the spiral feed hopper (302) on the spiral dryer (3); the gas outlet of the flushing gas storage tank (8) being connected to a combustible gas-air jet mixer (806), the negative pressure spiral low-temperature pyrolysis purifier (10) and the negative pressure spiral high-temperature pyrolysis carbonization machine (11) being respectively connected to the gas outlet of the combustible gas-air jet mixer (806); and a biomass vinegar liquid stop valve (501) being arranged on the liquid outlet pipe of the biomass vinegar liquid storage tank (5).

[0008] Preferably, a first screw feeder (101) is provided at the top feed port of the gasifier (1), a second screw feeder (1001) is provided at the left feed port of the negative pressure screw low-temperature pyrolysis purifier (10), a third screw feeder (1101) is provided at the left feed port of the negative pressure screw high-temperature pyrolysis carbonization machine (11), a first discharger (1007) is provided at the lower left discharge port of the negative pressure screw low-temperature pyrolysis purifier (10), and a second discharger (1107) is provided at the lower left discharge port of the negative pressure screw high-temperature pyrolysis carbonization machine (11).

[0009] Preferably, it also includes a second cyclone dust collector (9), the third pyrolysis volatile gas outlet (1002) on the negative pressure spiral low-temperature pyrolysis purifier (10) and the fourth pyrolysis volatile gas outlet (1102) on the negative pressure spiral high-temperature pyrolysis carbonization machine (11) are respectively connected to the fourth pyrolysis volatile gas inlet (902) on the second cyclone dust collector (9), and the air outlet at the top of the first cyclone dust collector (105) and the air outlet at the top of the second cyclone dust collector (9) are respectively connected to the second pyrolysis volatile gas inlet (305) on the spiral dryer (3).

[0010] Preferably, a spiral ash remover (110) is provided below the discharge port of the gasifier (1), a first regulating valve (104) is provided on the pipeline between the gas outlet at the top end of the first cyclone dust collector (105) and the second pyrolysis volatile gas inlet (305), a second regulating valve (107) is provided on the pipeline between the gasifier (1) and the water vapor outlet (301), and a third regulating valve (901) is provided on the pipeline between the gas outlet at the top end of the second cyclone dust collector (9) and the second pyrolysis volatile gas inlet (305).

[0011] Preferably, the bottom outlet of the first cyclone dust collector (105) is connected to the first water seal pressure relief device (108), and the first water seal pressure relief device (108) is provided with a first check valve (106) and a first sewage valve (109); the bottom outlet of the second cyclone dust collector (9) is connected to the second water seal pressure relief device (904), and the second water seal pressure relief device (904) is provided with a second check valve (903) and a second sewage valve (905).

[0012] Preferably, the negative pressure cavitation osmosis tank (13) is provided with a negative pressure gauge (1305), a vent valve (1306), a dispersant input valve (1304) and a fourth regulating valve (1308); the negative pressure cavitation osmosis tank (13) is connected to a negative pressure pump (1302); a negative pressure valve (1301) is provided on the pipeline between the negative pressure cavitation osmosis tank (13) and the negative pressure pump (1302); a biomass graphite powder suction valve (1303) is provided on the pipeline between the negative pressure cavitation osmosis tank (13) and the graphite pulverizer (12); and a biomass graphite mixed liquid output valve (1307) is provided on the pipeline between the negative pressure cavitation osmosis tank (13) and the high-pressure puffing stripping machine (14).

[0013] Preferably, a high-pressure pump (1401) is provided on the pipeline between the biomass-graphite mixed liquid output valve (1307) and the high-pressure puffing and stripping machine (14), a pressure gauge (1402) and a pressure regulating valve (1403) are provided on the high-pressure puffing and stripping machine (14), and a first stop valve (1404) is provided on the pipeline between the high-pressure puffing and stripping machine (14) and the stripping suspension storage tank (15).

[0014] Preferably, a second stop valve (1502) is provided on the pipeline between the exfoliation suspension storage tank (15) and the delivery pump (16), a exfoliation suspension regulating valve (1701) is provided on the pipeline between the delivery pump (16) and the spray dryer (17), an atomizer (1702) and a thermometer (1703) are provided on the spray dryer (17), a fifth regulating valve (1705) is provided on the pipeline between the spray dryer (17) and the hot air outlet of the heat exchanger (19), and the cyclone collector (18) is connected to a third discharger (1802) and an induced draft fan (1801).

[0015] The present invention also provides a biomass graphene production process, comprising the following steps:

[0016] (1) starting the first screw feeder (101) at the upper end of the gasifier (1), feeding agricultural and forestry waste or domestic garbage with a diameter of 5-100 mm into the gasifier (1), starting the circulation pump (802) and the combustible gas blower (807), and igniting the gasifier (1); allowing the pyrolysis volatile gas in the gasifier (1) to enter the first cyclone dust collector (105) through the first pyrolysis volatile gas outlet (102) and the first pyrolysis volatile gas inlet (103); after removing dust in the first cyclone dust collector (105), the pyrolysis volatile gas is discharged through the pyrolysis volatile gas regulating valve provided at the upper end of the first cyclone dust collector (105); The first heating layer (304) is provided outside the spiral dryer (3), and the spiral dryer (3) is heated. The heated pyrolysis volatile gas enters the gas-liquid separator (4) through a second pyrolysis volatile gas outlet (303) provided on the left side of the lower part of the heating layer, through a pipeline and a third pyrolysis volatile gas inlet (401), and is cooled and separated into gas and liquid. The condensed liquid flows into a biomass vinegar liquid receiving tank provided at the lower end of the gas-liquid separator (4) for storage, and a biomass vinegar liquid product is obtained. The non-condensable gas in the gas-liquid separator (4) is discharged through a non-condensable gas outlet (402) provided on the right side of the upper part, through a pipeline and a non-condensable gas inlet (401). (601) enters the catalytic adsorption purifier (6) for catalytic adsorption purification treatment. Under the transmission of the circulation pump (802), the flushing liquid in the flushing gas storage tank (8) is sprayed and circulated at a high speed through the flushing liquid ejector (7). The purified combustible gas is sucked into the flushing liquid ejector (7) through the purified combustible gas outlet (602) provided at the lower end of the catalytic adsorption purifier (6), and is quickly mixed with the sprayed flushing liquid and washed into the flushing gas storage tank (8). After being washed with the biomass acetic acid aqueous flushing liquid, it enters the combustible gas air jet through the combustible gas outlet (804) provided at the top of the flushing gas storage tank (8). In the mixer (806), the combustible gas-air jet mixer (806) outlet is diverted through a tee to the first combustible gas pipeline (1006) and enters the first temperature-controlled combustion burners (1005) arranged at the lower part of the second heating interlayer (1004) arranged outside the negative pressure spiral low-temperature pyrolysis purifier (10) for intelligent ignition and temperature-controlled combustion, thereby heating the negative pressure spiral low-temperature pyrolysis purifier (10). The exhaust gas after combustion is collected into the heat exchanger (19) through the first exhaust gas exhaust pipeline (1003) to provide a heat source for the spray dryer. The cooling gas after heat exchange enters the exhaust gas catalytic purifier (20) for purification and then is discharged;Then, the combustible gas is diverted from the outlet of the combustible gas-air jet mixer (806) through a tee to the second combustible gas pipeline (1106) and enters the second temperature-controlled combustion burners (1105) arranged at the lower part of the third heating interlayer (1104) arranged outside the negative pressure spiral high-temperature pyrolysis carbonization machine (11) for intelligent ignition and temperature-controlled combustion, heating the negative pressure spiral high-temperature pyrolysis carbonization machine (11). The exhaust gas after combustion is collected into the heat exchanger (19) through the second exhaust gas exhaust pipeline (1103) to increase the heat source for the spray dryer. The cooling gas after heat exchange enters the exhaust gas catalytic purifier (20) for purification and then discharge. After observing that the gasification, separation, purification, combustion and heating systems are operating normally, the pyrolysis purification temperature of the negative pressure spiral low-temperature pyrolysis purifier (10) is set to the range of 200-500°C, and the pyrolysis carbonization temperature of the negative pressure spiral high-temperature pyrolysis carbonization machine (11) is set to the range of 300-1400°C;

[0017] (2) When the pyrolysis purification temperature and the pyrolysis carbonization temperature reach the set temperature, the second discharger (1107), the negative pressure spiral high temperature pyrolysis carbonization machine (11), the third spiral feeder (1101), the first discharger (1007), the negative pressure spiral low temperature pyrolysis purification machine (10), the second spiral feeder (1001), the spiral dryer (3) and the raw material crusher (2) are started in sequence; after observing that everything is running normally, the biomass solid raw material is first fed into the raw material crusher. The raw material is crushed in a material crusher (2) to obtain a powder raw material with a particle size of 60-200 meshes, the crushed raw material is dehydrated in a spiral dryer 3, enters a negative pressure spiral low temperature pyrolysis purifier (10) for purification through a second spiral feeder (1001), is discharged from a first discharger (1007), then enters a negative pressure spiral high temperature pyrolysis carbonization machine (11) for carbonization through a third spiral feeder (1101), and then is discharged from a second discharger (1107) to obtain graphite crystal powder;

[0018] (3) Start the graphite crusher (12), crush the obtained graphite crystal powder to a particle size of no more than 10 μm, start the negative pressure pump (1302), open the negative pressure valve (1301), open the dispersant suction valve to suck the dispersant into the negative pressure cavitation permeation tank (13) in proportion, close the dispersant suction valve, open the biomass graphite crystal suction valve, suck the ultrafine graphite crystals into the negative pressure cavitation permeation tank (13) in proportion, close the biomass graphite crystal suction valve, open the fourth air intake regulating valve (1308), slowly adjust the air intake flow rate, start the cavitation permeation operation, and after running for 20-40 minutes, close the fourth regulating valve (1308), open the vent valve (1306), and wait until the negative pressure gauge (1305) returns to 0, and then the cavitation permeation operation ends;

[0019] (4) switching to another negative pressure cavitation permeation tank (13) and continuously operating according to the above operation process;

[0020] (5) Turn on the high-pressure pump (1401), open the fourth regulating valve (1308), pump the graphite crystal mixture into the high-pressure puffing and stripping machine (14) through the high-pressure pump (1401), adjust the pressure regulating valve (1403), adjust the puffing pressure to the set range, observe the pressure gauge (1402) to see that the pressure should be within the set range of 20-200 MPa, and the suspension after stripping enters the suspension storage tank through the flow regulating valve and the pipeline, and the puffing and stripping operation begins. Under the high-pressure environment, the liquid density and gas supersaturation of the mixed liquid between the graphite crystal layers are increased, and the mixture is slowly released through the pressure regulating valve (1403). The instantaneous strong pressure drop, high-speed jet force and strong tensile stress produce impact effect, shear effect and cavitation effect, so that the graphite crystals are stripped and evenly suspended in the solvent;

[0021] (6) The induced draft fan (1801), the third discharger (1802), the atomizer (1702) and the fifth regulating valve (1705) are respectively turned on. After observing that the temperature of the thermometer (1703) reaches the set range of 160-360°C, the exfoliation suspension regulating valve (1701) and the delivery pump (16) are opened. After everything is running normally, the second stop valve (1502) is opened to start the spray drying operation to obtain a single layer or less than ten layers of graphene after drying. The obtained biomass graphene product enters the cyclone collector (18) through the biomass graphene powder outlet (1704). After being processed by the cyclone collector (18), a single layer or less than ten layers of biomass graphene product (1803) is obtained.

[0022] Compared with the prior art, the present invention has achieved the following technical effects:

[0023] The biomass graphene production device and process of the present invention improve the energy utilization rate and yield when producing graphene. The biomass graphene production device and process of the present invention have the following advantages: (1) The combustible gas produced by high-temperature pyrolysis and gasification of agricultural and forestry waste and domestic garbage as raw materials provides a heat source for negative pressure low-temperature pyrolysis purification and negative pressure high-temperature pyrolysis carbonization equipment, and then the combustible gas produced by the pyrolysis purification and pyrolysis carbonization process is recycled, that is, waste utilization, and the operating cost is reduced by more than 85%; (2) The remaining heat is then used to dehydrate and dry the raw materials and spray dry the products, which can not only achieve heat exchange to reduce the temperature of the combustible gas, but also fully utilize heat energy to reduce the operating cost, and the cost is reduced by 100%; (3) The water vapor after the raw material is dehydrated enters the gasifier as a catalyst to promote the conversion rate of the combustible gas, and the conversion rate can reach 98%; (4 ) Using negative pressure low temperature pyrolysis purification technology to pyrolyze and purify hemicellulose, cellulose and lignin to obtain a by-product biomass vinegar liquid, and then using negative pressure high temperature pyrolysis carbonization technology to remove oxygen-containing functional groups from biomass graphite, the van der Waals force between the sheets is completely destroyed, and carbonization and crystallization obtain biomass graphite crystals (5) Using negative pressure cavitation penetration technology to allow water-soluble dispersants to fully and quickly penetrate between the graphite crystal layers to expand them, and then using high pressure puffing peeling technology to quickly peel off the graphene sheets, peeling and stratifying to obtain uniformly dispersed single-layer or double-layer graphene, and obtaining dried single-layer or less than ten-layer graphene, which has few oxygen-containing functional groups, high electrical conductivity, small interlayer structural defects, nanosheet size of 4 to 25 μm, and specific surface area of ​​300 m 2 / g-800m 2 / g, with a thickness of 0.34nm-0.9nm and good dispersibility of biomass graphene powder; (6) waste gasification heating is used to make full use of waste heat, negative pressure pyrolysis purification carbonization, negative pressure cavitation penetration, and high pressure expansion peeling to produce single-layer or double-layer graphene, which has the advantages of low energy consumption, no pollution, low cost, high efficiency, easy operation, and small investment, and can realize large-scale continuous production. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0025] Figure 1 It is a structural schematic diagram of the biomass graphene production device of the present invention;

[0026] Wherein: 1. gasifier; 101. first spiral feeder; 102. first pyrolysis volatile gas outlet; 103. first pyrolysis volatile gas inlet; 104. first regulating valve; 105. first cyclone dust collector; 106. first check valve; 107. second regulating valve; 108. first water seal pressure relief device; 109. first blowdown valve; 110. spiral ash remover; 2. raw material crusher; 3. spiral dryer; 301. water vapor outlet; 302. raw material feed hopper; 303. second pyrolysis volatile gas outlet; 304. first heating interlayer; 305. second pyrolysis volatile gas inlet; 306. dry raw material outlet; 4. gas-liquid separator; 401. third pyrolysis volatile gas inlet; 402. non-condensable gas outlet; 4 03, cooling water outlet; 404, cooling water inlet; 5, biomass vinegar liquid storage tank; 501, biomass vinegar liquid stop valve; 6, catalytic adsorption purifier; 601, non-condensable gas inlet; 602, purified combustible gas outlet; 7, flushing liquid ejector; 8, flushing gas storage tank; 801, circulating flushing liquid outlet; 802, circulating pump; 803, circulating flushing liquid pipeline; 804, flushing combustible gas outlet; 805, torch; 806, combustible gas air jet mixer; 807, combustible gas blower; 9, second cyclone dust collector; 901, third regulating valve; 902, fourth pyrolysis volatile gas inlet; 903, second check valve; 904, second water seal pressure relief device; 905, second sewage valve; 10, negative pressure spiral low Temperature pyrolysis purifier; 1001, second spiral feeder; 1002, third pyrolysis volatile gas outlet; 1003, first tail gas exhaust pipeline; 1004, second heating interlayer; 1005, first temperature-controlled combustion burner; 1006, first combustible gas pipeline; 1007, first discharger; 11, negative pressure spiral high-temperature pyrolysis carbonization machine; 1101, third spiral feeder; 1102, fourth pyrolysis volatile gas outlet; 1103, second tail gas exhaust pipeline; 1104, third heating interlayer; 1105, second temperature-controlled combustion burner; 1106, second combustible gas pipeline; 1107, second discharger; 12, graphite crusher; 13, negative pressure cavitation permeation tank; 1301, negative pressure valve; 1302, negative pressure pump; 1303, biomass graphite powder suction valve; 1304, dispersant input valve; 1305, negative pressure gauge; 1306, vent valve; 1307, biomass graphite mixed liquid output valve; 1308, fourth regulating valve; 14, high-pressure puffing stripping machine; 1401, high-pressure pump; 1402, pressure gauge; 1403, pressure regulating valve; 1404, first stop valve; 15, stripping suspension storage tank; 1501, feed inlet; 1502, second stop valve; 16, delivery pump; 17, spray dryer; 1701, stripping suspension regulating valve; 1702, atomizer; 1703, temperature gauge; 1704, biomass graphene powder outlet; 1705, fifth regulating valve; 18, cyclone collector; 1801, induced draft fan;1802, third discharger; 1803, single-layer biomass graphene product; 19, heat exchanger; 1901, air inlet; 1902, hot air outlet; 1903, high-temperature exhaust gas inlet; 1904, cooling exhaust gas outlet; 20, exhaust gas catalytic purifier; 2001, exhaust port. ; DETAILED DESCRIPTION

[0027] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0028] The purpose of the present invention is to provide a biomass graphene production device and process to solve the problems existing in the above-mentioned prior art and improve the energy utilization rate and yield when producing graphene.

[0029] In order to make the above-mentioned objects, features and advantages of the present invention more obvious and easy to understand, the present invention is further described in detail below with reference to the accompanying drawings and specific embodiments.

[0030] like Figure 1As shown: This embodiment provides a biomass graphene production device, including a gasifier 1, a first cyclone dust collector 105, a first heating interlayer 304, a gas-liquid separator 4, a catalytic adsorption purifier 6, a flushing liquid ejector 7 and a flushing gas storage tank 8, which are connected in sequence through pipelines, a negative pressure spiral low-temperature pyrolysis purifier 10 and a negative pressure spiral high-temperature pyrolysis carbonization machine 11 are respectively connected to the gas outlet of the flushing gas storage tank 8, the negative pressure spiral low-temperature pyrolysis purifier 10 and the negative pressure spiral high-temperature pyrolysis carbonization machine 11 are respectively connected to the high-temperature exhaust gas inlet 1903 of the heat exchanger 19, a spray dryer 17 is connected to the hot air outlet 1902 of the heat exchanger 19, and the exhaust catalytic purifier 20 is connected to the cooling exhaust gas outlet 190 of the heat exchanger 19. 4 is connected, the heat exchanger 19 is also provided with an air inlet 1901, and the exhaust catalytic purifier 20 is provided with an exhaust port 2001; the first heating interlayer 304 is arranged on the spiral dryer 3, the spiral dryer 3, the negative pressure spiral low temperature pyrolysis purifier 10, the negative pressure spiral high temperature pyrolysis carbonization machine 11, the graphite crusher 12, the negative pressure cavitation permeation tank 13, the high pressure puffing stripping machine 14, the stripping suspension storage tank 15, the delivery pump 16, the spray dryer 17 and the cyclone collector 18 are connected in sequence, and the cyclone collector 18 is connected with the third discharger 1802 and the induced draft fan 1801; the water vapor outlet 301 of the spiral dryer 3 is also connected with the gasifier 1, and the liquid outlet of the gas-liquid separator 4 is connected with the biomass vinegar liquid storage tank 5. The gas-liquid separator 4 is provided with a cooling water inlet 404 and a cooling water outlet 403 to connect with the cold source. A flushing liquid ejector 7 is connected to the upper left side of the flushing gas storage tank 8, a flushing combustible gas outlet 804 is provided at the top, and a torch 805 is provided at the upper right part. A circulating flushing liquid outlet 801 is provided at the bottom of the flushing gas storage tank 8, and the circulating flushing liquid outlet 801 is connected to a circulating pump 802 and is connected to the flushing liquid ejector 7 through a circulating flushing liquid pipeline.

[0031] The biomass graphene production device of this embodiment also includes a raw material crusher 2, the discharge port of the raw material crusher 2 is connected to the raw material feed hopper 302 on the spiral dryer 3; the gas outlet of the flushing gas storage tank 8 is connected to the combustible gas air jet mixer 806, and the negative pressure spiral low-temperature pyrolysis purifier 10 and the negative pressure spiral high-temperature pyrolysis carbonization machine 11 are respectively connected to the gas outlet of the combustible gas air jet mixer 806; a biomass vinegar liquid stop valve 501 is provided on the liquid outlet pipe of the biomass vinegar liquid storage tank 5.

[0032] A first screw feeder 101 is provided at the top feed port of the gasifier 1, a second screw feeder 1001 is provided at the left feed port of the negative pressure screw low-temperature pyrolysis purifier 10, a third screw feeder 1101 is provided at the left feed port of the negative pressure screw high-temperature pyrolysis carbonization machine 11, a first discharger 1007 is provided at the lower left discharge port of the negative pressure screw low-temperature pyrolysis purifier 10, and a second discharger 1107 is provided at the lower left discharge port of the negative pressure screw high-temperature pyrolysis carbonization machine 11.

[0033] The biomass graphene production device of this embodiment also includes a second cyclone dust collector 9, the third pyrolysis volatile gas outlet 1002 on the negative pressure spiral low-temperature pyrolysis purifier 10 and the fourth pyrolysis volatile gas outlet 1102 on the negative pressure spiral high-temperature pyrolysis carbonization machine 11 are respectively connected to the fourth pyrolysis volatile gas inlet 902 on the second cyclone dust collector 9, and the air outlet at the top of the first cyclone dust collector 105 and the air outlet at the top of the second cyclone dust collector 9 are respectively connected to the second pyrolysis volatile gas inlet 305 on the spiral dryer 3.

[0034] A spiral ash remover 110 is provided below the discharge port of the gasifier 1, a first regulating valve 104 is provided on the pipeline between the gas outlet at the top of the first cyclone dust collector 105 and the second pyrolysis volatile gas inlet 305, a second regulating valve 107 is provided on the pipeline between the gasifier 1 and the water vapor outlet 301, and a third regulating valve 901 is provided on the pipeline between the gas outlet at the top of the second cyclone dust collector 9 and the second pyrolysis volatile gas inlet 305.

[0035] The bottom outlet of the first cyclone dust collector 105 is connected to the first water seal pressure relief device 108, on which the first check valve 106 and the first sewage valve 109 are provided; the bottom outlet of the second cyclone dust collector 9 is connected to the second water seal pressure relief device 904, on which the second check valve 903 and the second sewage valve 905 are provided.

[0036] The negative pressure cavitation permeation tank 13 is provided with a negative pressure gauge 1305, a vent valve 1306, a dispersant input valve 1304 and a fourth regulating valve 1308. The negative pressure cavitation permeation tank 13 is connected to a negative pressure pump 1302. A negative pressure valve 1301 is provided on the pipeline between the negative pressure cavitation permeation tank 13 and the negative pressure pump 1302. A biomass graphite powder suction valve 1303 is provided on the pipeline between the negative pressure cavitation permeation tank 13 and the graphite crusher 12. A biomass graphite mixed liquid output valve 1307 is provided on the pipeline between the negative pressure cavitation permeation tank 13 and the high-pressure puffing stripping machine 14.

[0037] A high-pressure pump 1401 is provided on the pipeline between the biomass graphite mixed liquid output valve 1307 and the high-pressure puffing stripping machine 14, a pressure gauge 1402 and a pressure regulating valve 1403 are provided on the high-pressure puffing stripping machine 14, and a first stop valve 1404 is provided on the pipeline between the high-pressure puffing stripping machine 14 and the stripping suspension storage tank 15.

[0038] A second stop valve 1502 is provided on the pipeline between the stripping suspension storage tank 15 and the delivery pump 16, a stripping suspension regulating valve 1701 is provided on the pipeline between the delivery pump 16 and the spray dryer 17, an atomizer 1702 and a thermometer 1703 are provided on the spray dryer 17, and a fifth regulating valve 1705 is provided on the pipeline between the spray dryer 17 and the hot air outlet 1902 of the heat exchanger 19.

[0039] This embodiment also provides a biomass graphene production process based on the above-mentioned biomass graphene production device, and the specific process is as follows:

[0040] The first spiral feeder 101 at the upper end of the gasifier 1 is started, and agricultural and forestry waste or domestic garbage with a diameter of 5-100 mm is put into the gasifier 1. The flushing liquid ejector 7 and the combustible gas-air jet mixer 806 are turned on, and the gasifier 1 is ignited, so that the pyrolysis volatile gas in the gasifier 1 enters the first cyclone dust collector 105 through the first pyrolysis volatile gas outlet 102 and the first pyrolysis volatile gas inlet 103. After the dust is removed in the first cyclone dust collector 105, the pyrolysis volatile gas regulating valve provided at the upper end of the first cyclone dust collector 105 enters the first heating interlayer 304 provided outside the spiral dryer 3, and the spiral dryer 3 is heated. The heated pyrolysis volatile gas The second pyrolysis volatile gas outlet 303 arranged at the left side of the lower part of the heating interlayer enters the gas-liquid separator 4 through the pipeline and the third pyrolysis volatile gas inlet 401, and is cooled and separated from the gas and liquid. The condensed liquid flows into the biomass vinegar liquid receiving tank arranged at the lower end of the gas-liquid separator 4 for storage to obtain a biomass vinegar liquid product; the non-condensable gas in the gas-liquid separator 4 enters the catalytic adsorption purifier 6 through the non-condensable gas outlet 402 arranged at the right side of the upper part through the pipeline and the non-condensable gas inlet 601, and is subjected to catalytic adsorption purification treatment. Under the transmission of the circulating pump 802, the flushing liquid in the flushing gas storage tank 8 is sprayed and circulated at a high speed through the flushing liquid ejector 7, and the purified combustible gas is discharged through the catalytic adsorption purifier 6 arranged at the lower end. The purified combustible gas outlet 602 is sucked into the flushing liquid ejector 7, and is quickly mixed with the injected flushing liquid for washing and enters the flushing gas storage tank 8. After being washed by the biomass acetic acid aqueous solution, it enters the combustible gas air jet mixer 806 through the combustible gas outlet 804 set at the top of the flushing gas storage tank 8. The combustible gas air jet mixer 806 outlet is diverted to the first combustible gas pipeline 1006 through a three-way diversion and enters the first temperature-controlled combustion burner heads 1005 set at the lower part of the second heating interlayer 1004 set outside the negative pressure spiral low-temperature pyrolysis purifier 10 for intelligent ignition and temperature control combustion, so as to heat the negative pressure spiral low-temperature pyrolysis purifier 10. The exhaust gas after combustion is discharged through the first exhaust gas discharge pipeline 1003 is introduced into the heat exchanger 19 to provide heat source for the spray dryer. The cooling gas after heat exchange enters the exhaust catalytic purifier 20 for purification and then discharged. Then it is diverted from the outlet of the combustible gas air jet mixer 806 through a three-way to the second combustible gas pipeline 1106 and enters the second temperature-controlled combustion burners 1105 arranged at the lower part of the third heating interlayer 1104 arranged outside the negative pressure spiral high-temperature pyrolysis carbonization machine 11 for intelligent ignition and temperature control combustion, heating the negative pressure spiral high-temperature pyrolysis carbonization machine 11. The exhaust gas after combustion is introduced into the heat exchanger 19 through the second exhaust gas exhaust pipeline 1103 to increase the heat source for the spray dryer. The cooling gas after heat exchange enters the exhaust catalytic purifier 20 for purification and then discharged. After observing that the gasification, separation, purification, combustion and heating systems are operating normally, the pyrolysis purification temperature of the negative pressure spiral low-temperature pyrolysis purifier 10 is set to the range of 200-500°C, and the pyrolysis carbonization temperature of the negative pressure spiral high-temperature pyrolysis carbonization machine 11 is set to the range of 300-1400°C.

[0041] When the pyrolysis purification temperature and the pyrolysis carbonization temperature reach the set temperature, the biomass graphite powder windproof discharger, i.e., the first discharger 1007, the negative pressure spiral high temperature pyrolysis carbonization machine 11, the third spiral feeder 1101, the biomass graphite crystal windproof discharger, i.e., the second discharger 1107, the negative pressure spiral low temperature pyrolysis purification machine 10, the second spiral feeder 1001, the spiral dryer 3 and the raw material crusher 2 are started in sequence. After observing that everything is running normally, the biomass raw material is first put into the raw material crusher 2 for crushing. After the crushed particles have a diameter of 60-200 mesh, they are transported to the raw material feed hopper 302 set on the upper left side of the spiral dryer 3 and enter the spiral dryer 3. The spiral dryer 3 pushes the powder raw material to be evenly heated, dehydrated and dried. The water vapor obtained by drying passes through the water vapor outlet 301 set at the left end of the spiral dryer 3 through the pipeline and then enters the gasifier 1 through the second regulating valve 107 for catalytic cracking of harmful substances to enrich the combustible gas; the dried powder raw material is transported from the dry raw material outlet 306 at the right end of the spiral dryer 3 to the second spiral feeder 1001 set at the left end of the negative pressure spiral low-temperature pyrolysis purifier 10 and enters the negative pressure spiral low-temperature pyrolysis purifier 10. The powder raw material is evenly heated by the spiral of the negative pressure spiral low-temperature pyrolysis purifier 10, and low-temperature pyrolysis is performed in a negative pressure oxygen-free environment at a temperature of 200°C-500°C, so that the main components of biomass, hemicellulose, cellulose and lignin, are decomposed into acetic acid, 1- The volatile gases such as hydroxy-acetone, 1-hydroxy-2-butanone, levoglucosan, dehydrated cellobiose, o-methoxyphenol, H2, CO and CH4 enter the second cyclone dust collector 9 through the third pyrolysis volatile gas outlet 1002 through the three-way cyclone to remove dust, and then pass through the third regulating valve 901 set at the upper end of the second cyclone dust collector 9 and the first regulating valve 104 set at the upper end of the first cyclone dust collector 105 to mix and enter the first heating interlayer 3 set outside the spiral dryer 3. 04 to replenish heat energy; the biomass graphite powder that is purified and enriched in carbon is obtained by low-temperature pyrolysis and flows out through the pyrolysis biomass graphite powder windproof discharger, i.e., the first discharger 1007, and is transported through a pipeline to the third screw feeder 1101 arranged at the left end of the negative pressure spiral high-temperature pyrolysis carbonization machine 11 to enter the negative pressure spiral high-temperature pyrolysis carbonization machine 11. The powder raw material is evenly heated by the spiral of the negative pressure spiral high-temperature pyrolysis carbonization machine 11, and high-temperature pyrolysis is performed in a negative pressure oxygen-free environment at a temperature ranging from 300°C to 1400°C.The residual oxygen-containing functional groups are further decomposed to release volatile gases, which enter the second cyclone dust collector 9 through the fourth pyrolysis volatile gas outlet 1102 through the three-way cyclone to remove dust, and then the pyrolysis volatile gases from the third regulating valve 901 set at the upper end of the second cyclone dust collector 9 and the first regulating valve 104 set at the upper end of the first cyclone dust collector 105 are mixed and enter the first heating interlayer 304 set outside the spiral dryer 3 to supplement heat energy; high-temperature pyrolysis causes the biomass graphite to be carbonized and crystallized to weaken the interlayer van der Waals force and increase the interlayer spacing, and the biomass graphite crystals are obtained and flow out through the biomass graphite crystal windproof discharger, i.e., the second discharger 1107. The graphite pulverizer 12 is turned on, and the biomass graphite crystals are transported to the graphite pulverizer 12 for ultrafine grinding to obtain ultrafine graphite crystals with a crushed particle diameter of no more than 10 μm. Start the negative pressure pump 1302, open the negative pressure valve 1301, when the negative pressure gauge 1305 of the negative pressure cavitation permeation tank 13 reaches above -0.06Mpa, open the dispersant suction valve to suck the dispersant into the negative pressure cavitation permeation tank 13 in proportion, close the dispersant suction valve, open the biomass graphite crystal suction valve, suck the ultrafine graphite crystals into the negative pressure cavitation permeation tank 13 in proportion, close the biomass graphite crystal suction valve, open the fourth air intake regulating valve 1308, slowly adjust the air intake flow, start the cavitation permeation operation, and under the action of negative pressure, the fine airflow quickly enters the negative pressure cavitation permeation tank 13 In the liquid, a number of continuously rising tiny bubbles are generated. When the bubbles collapse, gas, liquid and solid three-phases collide with each other at high speed, resulting in dynamically enhanced cavitation effect, cavitation effect, turbulence effect, vortex and interface effect, increasing the mass transfer rate, expanding the permeation surface area, and allowing the dispersant to fully mix and penetrate into the graphite crystal layers to expand. After running for 20-40 minutes, close the fourth regulating valve 1308, open the vent valve 1306 and wait until the negative pressure gauge 1305 returns to 0. This cavitation permeation operation is terminated, and another negative pressure cavitation permeation tank 13 can be switched to run continuously according to the above operation process.The high-pressure pump 1401 is turned on, and the fourth regulating valve 1308 is opened. The graphite crystal mixed liquid is pumped into the high-pressure puffing and stripping machine 14 through the high-pressure pump 1401. The pressure regulating valve 1403 is adjusted to adjust the puffing pressure to the set range of 20-200Mpa. The pressure of the pressure gauge 1402 should be within the set range. The suspension after stripping enters the suspension storage tank through the flow regulating valve and the pipeline, and the puffing and stripping operation is started. Under the high-pressure environment, the liquid density and gas supersaturation of the mixed liquid between the graphite crystal layers are increased, and the mixture is slowly released through the pressure regulating valve 1403. The flow rate is increased to 100-400m / s, and the pressure is reduced to 0-5Mpa. The instantaneous strong pressure drop, high-speed jet force and strong tensile stress produce impact effect, shear effect and cavitation effect, so that the graphite crystals are stripped and layered uniformly suspended. Float in the solvent, respectively open the induced draft fan 1801, the third discharger 1802, the atomizer 1702 and the fifth regulating valve 1705, observe that the temperature of the thermometer 1703 reaches the set range of 160-360°C, open the exfoliation suspension regulating valve 1701 and the delivery pump 16, and after everything is running normally, open the second stop valve 1502, start the spray drying operation, and obtain a dried single-layer or ten-layer graphene. The obtained biomass graphene powder enters the cyclone collector 18 through the biomass graphene powder outlet 1704. After being processed by the cyclone collector 18, a single-layer or ten-layer biomass graphene product 1803 is obtained, which has less oxygen functional groups, high conductivity, small interlayer structural defects, nanosheet size of 4-25μm, and specific surface area of ​​300m. 2 / g-800m 2 / g, thickness of 0.34nm-0.9nm, good dispersibility of biomass graphene powder.

[0042] In the description of the present invention, it should be noted that the orientations or positional relationships indicated by the terms "top", "bottom", "left", "right", etc. are based on the orientations or positional relationships shown in the drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the devices or elements referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as limiting the present invention. In addition, the terms "first", "second", etc. are only used for descriptive purposes and cannot be understood as indicating or implying relative importance.

[0043] The present specification uses specific examples to illustrate the principles and implementation methods of the present invention. The above examples are only used to help understand the method and core idea of ​​the present invention. At the same time, for those skilled in the art, according to the idea of ​​the present invention, there will be changes in the specific implementation methods and application scope. In summary, the content of this specification should not be understood as limiting the present invention.

Claims

1. A biomass graphene production device, characterized in that: The invention comprises a gasifier (1), a first cyclone dust collector (105), a first heating interlayer (304), a gas-liquid separator (4), a catalytic adsorption purifier (6), a flushing liquid ejector (7) and a flushing gas storage tank (8) which are connected in sequence through pipelines; a negative pressure spiral low-temperature pyrolysis purifier (10) and a negative pressure spiral high-temperature pyrolysis carbonization machine (11) are respectively connected to the gas outlet of the flushing gas storage tank (8); the negative pressure spiral low-temperature pyrolysis purifier (10) and the negative pressure spiral high-temperature pyrolysis carbonization machine (11) are respectively connected to the high-temperature exhaust gas inlet of a heat exchanger (19); a spray dryer (17) is connected to the hot air outlet of the heat exchanger (19); and an exhaust gas catalytic purifier (20) is connected to the heat exchanger (19). The cooling tail gas outlet of the exchanger (19) is connected; the first heating interlayer (304) is arranged on the spiral dryer (3); the spiral dryer (3), the negative pressure spiral low temperature pyrolysis purifier (10), the negative pressure spiral high temperature pyrolysis carbonization machine (11), the graphite crusher (12), the negative pressure cavitation permeation tank (13), the high pressure puffing stripping machine (14), the stripping suspension storage tank (15), the delivery pump (16), the spray dryer (17) and the cyclone collector (18) are connected in sequence; the water vapor outlet (301) of the spiral dryer (3) is also connected to the gasifier (1); the liquid outlet of the gas-liquid separator (4) is connected to the biomass vinegar liquid storage tank (5); It also includes a raw material crusher (2), the discharge port of the raw material crusher (2) is connected to the spiral feed hopper (302) on the spiral dryer (3); the gas outlet of the flushing gas storage tank (8) is connected to a combustible gas-air jet mixer (806), the negative pressure spiral low-temperature pyrolysis purifier (10) and the negative pressure spiral high-temperature pyrolysis carbonization machine (11) are respectively connected to the gas outlet of the combustible gas-air jet mixer (806); and a biomass vinegar liquid stop valve (501) is provided on the liquid outlet pipe of the biomass vinegar liquid storage tank (5); A first screw feeder (101) is provided at the top feed port of the gasifier (1), a second screw feeder (1001) is provided at the left feed port of the negative pressure screw low temperature pyrolysis purifier (10), a third screw feeder (1101) is provided at the left feed port of the negative pressure screw high temperature pyrolysis carbonization machine (11), a first discharger (1007) is provided at the lower left discharge port of the negative pressure screw low temperature pyrolysis purifier (10), and a second discharger (1107) is provided at the lower left discharge port of the negative pressure screw high temperature pyrolysis carbonization machine (11); It also includes a second cyclone dust collector (9), the third pyrolysis volatile gas outlet (1002) on the negative pressure spiral low-temperature pyrolysis purifier (10) and the fourth pyrolysis volatile gas outlet (1102) on the negative pressure spiral high-temperature pyrolysis carbonization machine (11) are respectively connected to the fourth pyrolysis volatile gas inlet (902) on the second cyclone dust collector (9), and the gas outlet at the top of the first cyclone dust collector (105) and the gas outlet at the top of the second cyclone dust collector (9) are respectively connected to the second pyrolysis volatile gas inlet (305) on the spiral dryer (3); A spiral ash remover (110) is provided below the discharge port of the gasifier (1); a first regulating valve (104) is provided on the pipeline between the gas outlet at the top of the first cyclone dust collector (105) and the second pyrolysis volatile gas inlet (305); a second regulating valve (107) is provided on the pipeline between the gasifier (1) and the water vapor outlet (301); and a third regulating valve (901) is provided on the pipeline between the gas outlet at the top of the second cyclone dust collector (9) and the second pyrolysis volatile gas inlet (305); The bottom outlet of the first cyclone dust collector (105) is connected to a first water seal pressure relief device (108), and the first water seal pressure relief device (108) is provided with a first check valve (106) and a first sewage discharge valve (109); the bottom outlet of the second cyclone dust collector (9) is connected to a second water seal pressure relief device (904), and the second water seal pressure relief device (904) is provided with a second check valve (903) and a second sewage discharge valve (905); The negative pressure cavitation osmosis tank (13) is provided with a negative pressure gauge (1305), a vent valve (1306), a dispersant input valve (1304) and a fourth regulating valve (1308); the negative pressure cavitation osmosis tank (13) is connected to a negative pressure pump (1302); a negative pressure valve (1301) is provided on the pipeline between the negative pressure cavitation osmosis tank (13) and the negative pressure pump (1302); a biomass graphite powder suction valve (1303) is provided on the pipeline between the negative pressure cavitation osmosis tank (13) and the graphite pulverizer (12); and a biomass graphite mixed liquid output valve (1307) is provided on the pipeline between the negative pressure cavitation osmosis tank (13) and the high-pressure puffing stripping machine (14); A high-pressure pump (1401) is provided on the pipeline between the biomass-graphite mixed liquid output valve (1307) and the high-pressure puffing stripping machine (14); a pressure gauge (1402) and a pressure regulating valve (1403) are provided on the high-pressure puffing stripping machine (14); and a first stop valve (1404) is provided on the pipeline between the high-pressure puffing stripping machine (14) and the stripping suspension storage tank (15); A second stop valve (1502) is provided on the pipeline between the peeling suspension storage tank (15) and the delivery pump (16), a peeling suspension regulating valve (1701) is provided on the pipeline between the delivery pump (16) and the spray dryer (17), an atomizer (1702) and a thermometer (1703) are provided on the spray dryer (17), and a fifth regulating valve (1705) is provided on the pipeline between the spray dryer (17) and the hot air outlet of the heat exchanger (19); the cyclone collector (18) is connected to a third discharger (1802) and an induced draft fan (1801).

2. A biomass graphene production process, characterized in that: The biomass graphene production device according to claim 1 comprises the following steps: (1) starting the first screw feeder (101) at the upper end of the gasifier (1), feeding agricultural and forestry waste or domestic garbage with a diameter of 5-100 mm into the gasifier (1), starting the circulation pump (802) and the combustible gas blower (807), and igniting the gasifier (1); allowing the pyrolysis volatile gas in the gasifier (1) to enter the first cyclone dust collector (105) through the first pyrolysis volatile gas outlet (102) and the first pyrolysis volatile gas inlet (103); after removing dust in the first cyclone dust collector (105), the pyrolysis volatile gas is discharged through the pyrolysis volatile gas regulating valve provided at the upper end of the first cyclone dust collector (105); The first heating layer (304) is provided outside the spiral dryer (3), and the spiral dryer (3) is heated. The heated pyrolysis volatile gas enters the gas-liquid separator (4) through a second pyrolysis volatile gas outlet (303) provided on the left side of the lower part of the heating layer, through a pipeline and a third pyrolysis volatile gas inlet (401), and is cooled and separated into gas and liquid. The condensed liquid flows into a biomass vinegar liquid receiving tank provided at the lower end of the gas-liquid separator (4) for storage, and a biomass vinegar liquid product is obtained. The non-condensable gas in the gas-liquid separator (4) is discharged through a non-condensable gas outlet (402) provided on the right side of the upper part, through a pipeline and a non-condensable gas inlet (401). (601) enters the catalytic adsorption purifier (6) for catalytic adsorption purification treatment. Under the transmission of the circulation pump (802), the flushing liquid in the flushing gas storage tank (8) is sprayed and circulated at a high speed through the flushing liquid ejector (7). The purified combustible gas is sucked into the flushing liquid ejector (7) through the purified combustible gas outlet (602) provided at the lower end of the catalytic adsorption purifier (6), and is quickly mixed with the sprayed flushing liquid and washed into the flushing gas storage tank (8). After being washed with the biomass acetic acid aqueous flushing liquid, it enters the combustible gas air jet through the combustible gas outlet (804) provided at the top of the flushing gas storage tank (8). In the mixer (806), the combustible gas-air jet mixer (806) outlet is diverted through a tee to the first combustible gas pipeline (1006) and enters the first temperature-controlled combustion burners (1005) arranged at the lower part of the second heating interlayer (1004) arranged outside the negative pressure spiral low-temperature pyrolysis purifier (10) for intelligent ignition and temperature-controlled combustion, thereby heating the negative pressure spiral low-temperature pyrolysis purifier (10). The exhaust gas after combustion is collected into the heat exchanger (19) through the first exhaust gas exhaust pipeline (1003) to provide a heat source for the spray dryer. The cooling gas after heat exchange enters the exhaust gas catalytic purifier (20) for purification and then is discharged;The combustible gas is then diverted from the outlet of the combustible gas-air jet mixer (806) through a tee to the second combustible gas pipeline (1106) and enters the second temperature-controlled combustion burners (1105) arranged at the lower part of the third heating interlayer (1104) arranged outside the negative pressure spiral high-temperature pyrolysis carbonization machine (11) for intelligent ignition and temperature-controlled combustion, thereby heating the negative pressure spiral high-temperature pyrolysis carbonization machine (11). The exhaust gas after combustion is introduced into the heat exchanger (19) through the second exhaust gas exhaust pipeline (1103) to increase the heat source for the spray dryer. The cooled gas after heat exchange enters the exhaust gas catalytic purifier (20) for purification and then discharged. After observing that the gasification, separation, purification, combustion and heating systems are operating normally, the pyrolysis purification temperature of the negative pressure spiral low-temperature pyrolysis purifier (10) is set to a range of 200-500°C, and the pyrolysis carbonization temperature of the negative pressure spiral high-temperature pyrolysis carbonization machine (11) is set to a range of 300-1400°C. (2) When the pyrolysis purification temperature and the pyrolysis carbonization temperature reach the set temperature, the second discharger (1107), the negative pressure spiral high temperature pyrolysis carbonization machine (11), the third spiral feeder (1101), the first discharger (1007), the negative pressure spiral low temperature pyrolysis purification machine (10), the second spiral feeder (1001), the spiral dryer (3) and the raw material crusher (2) are started in sequence; after observing that everything is running normally, the biomass solid raw material is first fed into the raw material crusher. The raw material is crushed in a material crusher (2) to obtain a powder raw material with a particle size of 60-200 meshes, the crushed raw material is dehydrated in a spiral dryer 3, enters a negative pressure spiral low temperature pyrolysis purifier (10) for purification through a second spiral feeder (1001), is discharged from a first discharger (1007), then enters a negative pressure spiral high temperature pyrolysis carbonization machine (11) for carbonization through a third spiral feeder (1101), and then is discharged from a second discharger (1107) to obtain graphite crystal powder; (3) Start the graphite crusher (12), crush the obtained graphite crystal powder to a particle size of no more than 10 μm, start the negative pressure pump (1302), open the negative pressure valve (1301), open the dispersant suction valve to suck the dispersant into the negative pressure cavitation permeation tank (13) in proportion, close the dispersant suction valve, open the biomass graphite crystal suction valve, suck the ultrafine graphite crystals into the negative pressure cavitation permeation tank (13) in proportion, close the biomass graphite crystal suction valve, open the fourth air intake regulating valve (1308), slowly adjust the air intake flow rate, start the cavitation permeation operation, and after running for 20-40 minutes, close the fourth regulating valve (1308), open the vent valve (1306), and wait until the negative pressure gauge (1305) returns to 0, and then the cavitation permeation operation ends; (4) switching to another negative pressure cavitation permeation tank (13) and continuously operating according to the above operation process; (5) Turn on the high-pressure pump (1401), open the fourth regulating valve (1308), pump the graphite crystal mixture into the high-pressure puffing and stripping machine (14) through the high-pressure pump (1401), adjust the pressure regulating valve (1403), adjust the puffing pressure to the set range, observe the pressure gauge (1402) to see that the pressure should be within the set range of 20-200 MPa, and the suspension after stripping enters the suspension storage tank through the flow regulating valve and the pipeline, and the puffing and stripping operation begins. Under the high-pressure environment, the liquid density and gas supersaturation of the mixed liquid between the graphite crystal layers are increased, and the mixture is slowly released through the pressure regulating valve (1403). The instantaneous strong pressure drop, high-speed jet force and strong tensile stress produce impact effect, shear effect and cavitation effect, so that the graphite crystals are stripped and evenly suspended in the solvent; (6) The induced draft fan (1801), the third discharger (1802), the atomizer (1702) and the fifth regulating valve (1705) are respectively turned on. After observing that the temperature of the thermometer (1703) reaches the set range of 160-360°C, the exfoliation suspension regulating valve (1701) and the delivery pump (16) are opened. After everything is running normally, the second stop valve (1502) is opened to start the spray drying operation to obtain a single layer or less than ten layers of graphene after drying. The obtained biomass graphene product enters the cyclone collector (18) through the biomass graphene powder outlet (1704). After being processed by the cyclone collector (18), a single layer or less than ten layers of biomass graphene product (1803) is obtained.

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