Three-section pure oxygen anti-condensation gasification furnace using straw as raw material

Abstract

According to the three-section pure oxygen anti-condensation gasification furnace using straws as raw materials, a first water jacket, a second water jacket and a third water jacket which are communicated with one another are arranged on the periphery of the gasification furnace to adapt to heat exchange temperatures at different height positions on a furnace body, so that a heat exchange medium is preheated in advance and gradually heated in the circulation process; the straw serving as fuel can achieve self efficient incineration, energy recovery and heat energy exchange, the bottleneck that gas tar is difficult to separate and recover is solved, the way that the straw is gasified and can be completely purified is opened, the energy conversion rate of produced fuel gas is high, and a boiler burner can better and smoothly conduct denitration to reach the emission standard. Straw serving as a gasification raw material is subjected to squeezing dehydration, stacking and airing for further dehydration, extrusion forming dehydration and other operations, the straw is put into a gasification furnace with an oxidation layer, a reduction layer, a slag layer and a dry distillation space layer with specific heights, the straw serves as the gasification raw material, and fuel gas containing high-concentration carbon monoxide and hydrogen is stably and efficiently produced.

Description

Technical Field

[0001] The invention relates to the technical field of gas boiler heat exchange equipment, in particular to a three-stage pure oxygen anti-condensation gasification furnace using straw as a raw material. Background Art

[0002] The high yield of agricultural crops and urbanized life have made straw waste increasingly prominent, affecting ecological balance and environmental protection. The current solution is to burn straw waste for power generation. The heat energy generated by incineration is mainly used for steam-steam turbine power generation, but the pollution after incineration requires huge investment in governance, which is inefficient and loss-making. However, most existing gasifiers use high-efficiency fuels such as coal or biomass. The heat energy generated by the combustion of straw waste cannot raise the temperature of the heat exchange medium to the specified temperature. The reason is that the gasified coal used in the existing gasifier contains about 80% carbon, volatile matter ≤13%, ash ≤11%, and the ignition point is above 600℃, while the carbon content of straw is about 25%, volatile matter 30-49%, ash 30%-50%, and the ignition point is 300℃. If the gasifier equipment and process using coal as raw material are used to gasify straw, it will not only fail to achieve normal and efficient heat exchange, but also fail to stably produce gas containing high concentrations of carbon monoxide and hydrogen. Summary of the invention

[0003] The purpose of the present invention is to provide a three-stage pure oxygen anti-condensation gasifier and a gasification operation process using straw as raw material. By arranging water jackets of different temperature types on the periphery of the gasifier, the internal heat exchange medium can be gradually heated. By using squeezed juice and extruded straw particles as gasification raw materials, efficient heat energy recovery can be carried out, the heat exchange medium can be heated to a specified temperature, and a stable output of fuel gas containing high concentrations of carbon monoxide and hydrogen can be produced, thereby solving the problems in the prior art.

[0004] The technical solution adopted by the present invention to solve its technical problems is: a three-stage pure oxygen anti-condensation gasification furnace using straw as raw material includes a furnace wall, and a first water jacket, a second water jacket and a third water jacket are installed on the outer periphery of the furnace wall. The first water jacket, the second water jacket and the third water jacket are arranged in sequence from bottom to top on the gasification furnace, and the upper part of the third water jacket and the lower part of the first water jacket are connected by a pipeline, and the upper part of the first water jacket and the lower part of the second water jacket are connected by a pipeline. A water supply pipeline is installed at the lower part of the third water jacket, and a high-temperature medium discharge pipeline is installed at the upper part of the second water jacket. The second water jacket is provided with a water supply pipeline, and a high-temperature medium discharge pipeline is installed at the upper part of the second water jacket. A water level gauge is also installed inside the jacket, wherein the total height of the first water jacket, the second water jacket and the third water jacket is 5.7m-20m, an ash pan slag discharge system is installed at the bottom of the furnace wall, a connected feeder is installed on the top of the furnace wall, a denitrification feeder is installed on the upper part of the feeder, a material detection layer rod is installed on the furnace wall on one side of the feeder, and a gas conduit connected to the furnace is installed on the furnace wall on the other side of the feeder, a normal temperature water inlet is installed at the lower part of the third water jacket, and the normal temperature water inlet is connected to the water supply pipeline, a low temperature water outlet is installed at the upper part of the third water jacket, and a low temperature water inlet is installed at the lower part of the first water jacket. A low-temperature water pipeline is connected between the low-temperature water outlet and the low-temperature water inlet, a medium-temperature water outlet is installed on the upper part of the first water jacket, a medium-temperature water inlet is installed on the lower part of the second water jacket, a medium-temperature water pipeline is connected between the medium-temperature water outlet and the medium-temperature water inlet, and a high-temperature medium discharge port is installed on the upper part of the second water jacket. Several spirally arranged temperature measuring devices are installed on the periphery of the gasifier, one end of the gas conduit is connected to the furnace wall, and a gravity dust removal tank is installed on the other end of the gas conduit. A connected dust storage tank is provided at the bottom of the gravity dust removal tank, and a connecting pipe and a connecting pipe are installed at one side of the gas outlet of the gravity dust removal tank. The connecting pipe is connected to the gas conduit. The gas processing device is a system for extracting hydrogen, synthesizing methane, methanol or a low-pressure burner. The low-pressure burner is provided with a tar sprayer. The upper end of the gas conduit is provided with a steam inlet chamber sleeve, which is connected to the gasification furnace outlet of the furnace wall through a first flange. The lower end of the gas conduit is provided with a drainage chamber sleeve, which is connected to the gravity dust removal tank through a second flange. The steam inlet chamber sleeve is provided with a connected steam inlet pipe, and the drainage chamber sleeve is provided with a connected drainage pipe. A plurality of semicircular tubes arranged in a circumference are longitudinally provided on the outer peripheral wall of the gas conduit, and the semicircular tubes are connected to the steam inlet chamber sleeve and the drainage chamber sleeve. One end of the gas conduit is connected to the furnace wall, and the other end of the gas conduit is provided with a burner, which is located in the combustion boiler. A water bag and a water supply pump are provided on the water supply pipeline, and a hot water pump and a heat exchange boiler are provided on the high-temperature medium discharge pipeline. The water supply pipeline and the high-temperature medium discharge pipeline are connected to the heat exchange steam drum together.The furnace diameter of the gasifier is 3.6 meters, and the total height of the three water jackets is 10-20 meters, of which the height of the first water jacket is 3-7 meters, the height of the second water jacket is 3-10 meters, and the height of the third water jacket is 1-7 meters. The volume of the first water jacket is 1.3-4.5 cubic meters, the volume of the second water jacket is 1.3-3 cubic meters, and the volume of the third water jacket is greater than 1.7 cubic meters. The height of the second water jacket is 7-10 meters. The gravity dust removal tank includes a dust removal tank body, a separation cylinder is installed at the upper end of the dust removal tank body, and the separation cylinder is connected to the bottom of the gas conduit. The lower end of the dust removal tank body is installed with a third flange, and the third flange is connected to the dust storage tank. An air outlet pipe is also opened on one side of the dust removal tank body, and the air outlet pipe is connected to the connecting pipe. The dust storage tank includes a dust storage tank body, and a connected dust exhaust pipe is installed on the outer periphery of the dust storage tank body, and a sewage discharge hole is also opened on the lower side of the dust storage tank body. The method for producing carbon monoxide and hydrogen in a three-stage pure oxygen anti-condensation gasification furnace using straw as a raw material comprises the following steps: ① When the straw is harvested, it is directly loaded into a vehicle and transported to a collection and processing center without falling to the ground; ② After the straw is sent to the processing center, it is squeezed and dehydrated within 2-3 days of harvesting to reduce its water content to ≤43%; ③ After the squeezing in step ② is completed, the slag climbs dozens of meters high through a conveyor and falls freely and gradually. The continuous falling allows the slag to form a hill from small to large. During the process of forming the hill for dozens of hours, the slag is dried in the sun, and the water evaporates 8-15% by wind, and the water content of the slag is reduced to 35-30%; ④ Two A set of double-roller tooth hole combined extrusion pellet machines extrude the residue to make pellets, wherein the first machine initially extrude medium φ16-20mm pellets with steam at a temperature of about 30°C, and the micro pellets emit steam to reduce the moisture content of the residue by 3-5% again. The semi-finished pellets made by the first machine enter the second extrusion pellet machine to make the semi-finished product moisture lower than about 30% and be extruded into φ16-20mm pellets again, or processed into φ30mm briquettes by rolling; ⑤ The pellets or briquettes made by dehydration and extrusion are put into the gasifier as raw materials, and high-temperature gasification makes the straw produce CO+H2=72%-82% gas. In the gasification process in step ⑤, the gasifying agent is pure oxygen, oxygen-enriched or air, and oxygen mixed with carbon dioxide or part of steam is preferably used for gasification. In the three-stage pure oxygen anti-condensation gasification furnace using straw as raw material, the thickness of the oxidation layer and the reduction layer is controlled at 5-12m, with a slag layer at the bottom and a retort layer at the top, and the gasification produces a stable CO+H2=72%-82% gas, which is used for hydrogen extraction or synthesis of green chemical products such as methane and methanol. The thickness of the oxidation layer and the reduction layer is controlled at 7-12m.

[0005] The positive effect of the present invention is that the three-stage pure oxygen anti-condensation gasifier using straw as raw material is provided with a first water jacket, a second water jacket and a third water jacket connected to each other on the periphery of the gasifier, and the heat exchange temperature at different heights on the furnace body is adapted, so that the heat exchange medium can be preheated in advance and gradually heated up during the circulation process. The straw used as fuel can realize its own efficient incineration, energy recovery and heat exchange, solve the bottleneck of difficult separation and recovery of gas tar, open up the way for straw gasification and complete purification, and produce a high energy conversion rate of fuel gas, so that the boiler burner can denitrify better and smoothly to meet the emission standards. By pressing and dehydrating the straw used as the raw material for gasification, piling and drying for further dehydration, extrusion molding and dehydration, and placing it in a gasifier with a specific height of oxidation layer, reduction layer, slag layer, and dry distillation space layer, the straw can be used as the raw material for gasification to stably and efficiently produce fuel gas containing high concentrations of carbon monoxide and hydrogen. BRIEF DESCRIPTION OF THE DRAWINGS

[0006] Figure 1 It is a schematic diagram of the structure of the present invention; Figure 2 It is a schematic diagram of the structure of the gasifier connected to the combustion boiler; Figure 3 It is a schematic diagram of the heat exchange process of the heat exchange medium in the water jacket; Figure 4 It is a schematic diagram of the structure of an anti-condensation device provided on a gas conduit; Figure 5 yes Figure 4 Schematic diagram of the structure of the gas conduit; Figure 6 It is a schematic diagram of the cross-sectional structure of a steam inlet chamber sleeve arranged on a gas conduit; Figure 7 It is a schematic diagram of a structure in which a semicircular tube is arranged on the periphery of a gas conduit; Figure 8 It is a structural schematic diagram of a gravity dust removal tank and a dust storage tank; Fig. 9 This is a photo of the pellets produced by the double-roller gear extruder; Fig.10 and Fig.11 It is the 2013 straw pure oxygen gasification test report; Fig.12 This is the 2018 straw pure oxygen gasification test report. DETAILED DESCRIPTION

[0007] The three-stage pure oxygen anti-condensation gasification furnace using straw as raw material of the present invention is as follows: Figure 1-3 As shown, a furnace wall 1 is included, the interior of the furnace wall 1 is used for burning straw fuel, and a first water jacket 6, a second water jacket 7 and a third water jacket 8 are installed on the periphery of the furnace wall 1. The first water jacket 6, the second water jacket 7 and the third water jacket 8 are arranged in sequence from bottom to top on the gasifier, adapted to the heat exchange temperatures corresponding to different height positions on the gasifier, so as to realize the gradual heating and heat exchange of the heat exchange medium.

[0008] In order to achieve the connection between the water jackets, the upper part of the third water jacket 8 and the lower part of the first water jacket 6 are connected by a pipeline, and the upper part of the first water jacket 6 and the lower part of the second water jacket 7 are connected by a pipeline. A water replenishment pipeline 3 is installed at the lower part of the third water jacket 8, and a high-temperature medium discharge pipeline 4 is installed at the upper part of the second water jacket 7. After the heat exchange and temperature rise, the heat exchange medium will move upward in the water jacket. In the flow circulation process of the heat exchange medium gradually rising in temperature, it enters from the bottom position of the water jacket. After sufficient heat exchange, it flows out from the top of the water jacket and enters the next water jacket. Among them, the first water jacket 6 corresponds to medium-temperature heat exchange, the second water jacket 7 corresponds to high-temperature heat exchange, and the third water jacket 8 corresponds to low-temperature heat exchange. The heat exchange medium is heated in the third water jacket 8, the first water jacket 6 and the second water jacket 7 in turn.

[0009] A water level gauge 5 is also installed inside the second water jacket 7. The water level gauge 5 can monitor the water level inside the second water jacket 7 in real time. After the heat exchange medium is heated to form steam, the internal water level will decrease. At this time, the water level gauge 5 receives a signal and subsequently controls the water replenishment pipeline 3 to replenish the heat exchange medium into each water jacket.

[0010] Furthermore, an ash pan slag discharge system 2 is installed at the bottom of the furnace wall 1, and a connected feeder 12 is installed on the top of the furnace wall 1. The feeder 12 is used to feed straw and other fuels into the gasification furnace. A denitrification feeder 13 is installed on the upper part of the feeder 12. The denitrification agent is fed along with the feeding when the feeding is carried out, and the feeding of the denitrification agent is stopped synchronously when the feeding is stopped.

[0011] A detection layer stem 14 is installed on the furnace wall 1 on one side of the feeder 12. The detection layer stem 14 can detect the amount of straw fuel filled in the gasifier so as to replenish the fuel or perform subsequent combustion operations. A gas conduit 9 connected to the furnace is installed on the furnace wall 1 on the other side of the feeder 12. The combustible gas generated by the reaction in the gasifier can be discharged through the gas conduit 9.

[0012] Fig. 9 It is a double-roller gear extruder, which produces φ16mm-φ20mm straw pellets through the double-roller gear extrusion cavity. A single double-roller gear extruder can extrude 2000 tons of φ16mm-φ20mm straw pellets at one time and continuously, without any buttering or changing of adjusting parts. It is a limited selection equipment suitable for large-scale production and processing, and also lays the foundation for large-scale straw gasification.

[0013] One end of the gas conduit 9 is connected to the furnace wall 1, and a burner 10 is installed at the other end of the gas conduit 9. The burner 10 is located in the combustion boiler 11. The combustible gas discharged from the gasification furnace can enter the burner 10 for combustion and provide the combustion boiler 11 with the required heat exchange heat energy.

[0014] Furthermore, a normal temperature water inlet 27 is installed at the lower part of the third water jacket 8, and the normal temperature water inlet 27 is connected to the water supply pipeline 3, a low temperature water outlet 16 is installed at the upper part of the third water jacket 8, a low temperature water inlet 17 is installed at the lower part of the first water jacket 6, and a low temperature water pipeline 18 is connected between the low temperature water outlet 16 and the low temperature water inlet 17, a medium temperature water outlet 19 is installed at the upper part of the first water jacket 6, a medium temperature water inlet 20 is installed at the lower part of the second water jacket 7, and a medium temperature water pipeline 21 is connected between the medium temperature water outlet 19 and the medium temperature water inlet 20, and a high temperature medium discharge outlet 22 is installed at the upper part of the second water jacket 7.

[0015] During the circulation heating process, the third water jacket 8 at the top has the lowest temperature, and the second water jacket 7 at the middle has the highest temperature. Normal temperature water first enters the bottom of the third water jacket 8 from the water supply pipeline 3, and after preliminary heat exchange and heating, it is discharged from the low-temperature water outlet 16 into the low-temperature water pipeline 18, and enters the first water jacket 6 through the low-temperature water inlet 17. After secondary heating and heat exchange, it is discharged from the medium-temperature water outlet 19 at the top of the first water jacket 6 into the medium-temperature water pipeline 21, and enters the second water jacket 7 through the medium-temperature water inlet 20. After the final heating, it is discharged from the high-temperature medium discharge port 22 to achieve high-efficiency comprehensive heat exchange.

[0016] Furthermore, in order to achieve timely replenishment of the heat exchange medium, a water bag 23 and a water supply pump 24 are installed on the water supply pipeline 3. In order to enable the heat exchange medium after heating to achieve subsequent heat energy exchange, a hot water pump 25 and a heat exchange boiler 26 are installed on the high-temperature medium discharge pipeline 4.

[0017] Furthermore, in order to preheat the heat exchange medium entering the water supply pipeline 3 in advance, the water supply pipeline 3 and the high-temperature medium discharge pipeline 4 are connected to the heat exchange sub-steam drum 15 together, wherein the water supply pipeline 3 can be located in the tube side of the heat exchange sub-steam drum 15, and the heated heat exchange medium can be passed into the shell side of the heat exchange sub-steam drum 15, thereby realizing the preheating of the heat exchange medium in the heat exchange sub-steam drum 15.

[0018] Furthermore, in order to monitor the temperature of each water jacket in real time, several spirally arranged temperature detectors 28 are installed on the periphery of the gasifier. The arrangement of each temperature detector 28 can start from 0.4-0.9 meters from the top of the furnace. According to the pitch of 3 meters, two pitches are used, that is, 4 probe points are evenly arranged in each pitch within a range of 6 meters in height, and a total of 9 probe points are arranged. Multiple temperature detectors can be added radially at the temperature detection point, and the uniform temperature of the detection point can also be displayed by a table. The temperature displayed at the temperature detection point corresponds to the slag layer, gasification layer and reduction layer respectively. During operation, the corresponding slag discharge time can be adjusted through the temperature feedback of each temperature detector 28.

[0019] The first water jacket 6 pumps hot water into the third water jacket 8 for heating, the second water jacket 7 pumps high-temperature water into the first water jacket 6 to increase the temperature and generate high-temperature steam to be output through the heat exchange drum 15, the third water jacket 8 preheats the replenished water, and the heated water is promptly injected into the first water jacket 6. The reasonable combination of the three-stage water jacket (bore) is conducive to the efficient output of steam. According to the temperature of the gasification layer, the upper section is lower than the lower section, the lower section is lower than the middle section, and the middle section is at a high temperature position in the oxidation layer. The bottom of the middle section gradually cools down and enters the 500-300℃ area of ​​the lower section. The upper part of the middle section enters the upper section for dry distillation and absorption and cools down at about 300℃, so the middle section plays a role in generating high-pressure steam in stages. When the steam pressure of the water jacket (bore) reaches 0.4MPa, when the boiler is overpressured by 0.4MPa-1.3MPa, the pressure of the steam pump boosting and pumping into the boiler is increased, and the second water jacket 7 can also be directly pumped into the boiler with a hot water pump to effectively increase the gas production.

[0020] A denitrification feeding device is arranged on the top of the gasifier, which follows the feeding when feeding, and stops feeding the denitrification agent synchronously when feeding stops. The gas transmission conduit 9 on the top of the gasifier is connected to the output gas through the burner 10 into the gas boiler 11 for combustion to produce steam.

[0021] Furthermore, in order to improve the heat exchange efficiency of the overall device, the furnace diameter of the gasifier is 1.6 meters, and the total height of the three water jackets is 7.7-11.6 meters, of which the height of the first water jacket 6 is 2.2-5.6 meters, the height of the second water jacket 7 is 2.5-5 meters, and the height of the third water jacket 8 is 2-4 meters. The volume of the first water jacket 6 is 0.4-1.2 cubic meters, the volume of the second water jacket 7 is 0.5-1.1 cubic meters, and the volume of the third water jacket 8 is 0.57 cubic meters.

[0022] In addition, the furnace diameter of the gasifier can also be 0.8 meters, and the total height of the three water jackets is 5.7-9.7 meters, among which the height of the first water jacket 6 is 1.7-3.7 meters, the height of the second water jacket 7 is 2-4 meters, and the height of the third water jacket 8 is 1.2-3.2 meters. The volume of the first water jacket 6 is 0.15-0.34 cubic meters, the volume of the second water jacket 7 is 0.18-0.4 cubic meters, and the volume of the third water jacket 8 is 0.18 cubic meters.

[0023] The furnace diameter of the gasifier can also be 1.8-2.2 meters, and the total height of the three water jackets is 7.7-13.4 meters, of which the height of the first water jacket 6 is 2.2-6.2 meters, the height of the second water jacket 7 is 2.5-5.5 meters, and the height of the third water jacket 8 is 2-4 meters. The volume of the first water jacket 6 is 0.46-1.7 cubic meters, the volume of the second water jacket 7 is 0.6-1.7 cubic meters, and the volume of the third water jacket 8 is 0.8 cubic meters.

[0024] The furnace diameter of the gasifier can also be 2.4-3.2 meters, and the total height of the three water jackets is 8.3-15 meters, among which the height of the first water jacket 6 is 2.6-7.0 meters, the height of the second water jacket 7 is 2.7-6 meters, and the height of the third water jacket 8 is 1-5 meters. The volume of the first water jacket 6 is 0.7-2.7 cubic meters, the volume of the second water jacket 7 is 0.64-2.3 cubic meters, and the volume of the third water jacket 8 is 1.1 cubic meters.

[0025] The furnace diameter of the gasifier can also be greater than 3.6 meters, and the total height of the three water jackets is 10-20 meters, among which the height of the first water jacket 6 is 3-7 meters, the height of the second water jacket 7 is 3-10 meters, preferably 7-10 meters, and the height of the third water jacket 8 is 1-7 meters. The volume of the first water jacket 6 is 1.3-4.5 cubic meters, the volume of the second water jacket 7 is 1.3-3 cubic meters, and the volume of the third water jacket 8 is greater than 1.7 cubic meters.

[0026] The preferred ranges of the total height of the above three water jackets, the height of each level of water jacket and the accompanying pressurized water volume are described in the following table: The parameter range of the furnace diameter of the full-height water jacket is: the total height of the water jacket = the operating height of the water jacket or the furnace mountain, slag layer, reserved space priority parameters and water capacity range (m) in the furnace with the water jacket.

[0027]

[0028] In addition, the gas produced by the gasifiers with the cumulative total height of the three water jackets can be continuously operated by the intelligent burner for at least 24 months without extinguishing the fire.

[0029] Furthermore, if Figure 4-8 As shown, one end of the gas conduit 9 is connected to the furnace wall 1, and a gravity dust removal tank 29 is installed at the other end of the gas conduit 9. A dust storage tank 30 is provided at the bottom of the gravity dust removal tank 29. A connecting pipe 31 and a connecting pipe 32 are installed at one side of the gas outlet of the gravity dust removal tank 29. The connecting pipe 32 is connected to a gas processing device, which is a hydrogen extraction, methane synthesis, methanol system or a low-pressure burner 33. A tar sprayer 34 is provided on the low-pressure burner 33.

[0030] A steam inlet chamber sleeve 94 is installed at the upper end of the gas conduit 9, and the steam inlet chamber sleeve 94 is connected to the gasification furnace outlet 91 of the furnace wall 1 through a first flange 92. A drainage chamber sleeve 97 is installed at the lower end of the gas conduit 9, and the drainage chamber sleeve 97 is connected to the gravity dust removal tank 29 through a second flange 98. A connected steam inlet pipe 93 is installed on the steam inlet chamber sleeve 94, and a connected drainage pipe 99 is installed on the drainage chamber sleeve 97. A plurality of circumferentially arranged semicircular pipes 96 are longitudinally arranged on the outer peripheral wall of the gas conduit 9, and the semicircular pipes 96 are connected to the steam inlet chamber sleeve 94 and the drainage chamber sleeve 97.

[0031] The gravity dust removal tank 29 includes a dust removal tank body 292, a separation cylinder 291 is installed on the upper end of the dust removal tank body 292, the separation cylinder 291 is connected to the bottom of the gas conduit 9, a third flange 294 is installed on the lower end of the dust removal tank body 292, the third flange 294 is connected to the dust storage tank 30, and an air outlet pipe 293 is also opened on one side of the dust removal tank body 292, and the air outlet pipe 293 is connected to the connecting pipe 31.

[0032] The dust storage tank 30 includes a dust storage tank body 301 , a dust exhaust pipe 302 is installed on the outer periphery of the dust storage tank body 301 , and a sewage discharge hole 303 is opened on the lower side of the dust storage tank body 301 .

[0033] The separation cylinder 291 is connected and fixed with the drainage chamber sleeve 97, and the inner wall of the gas conduit 9 is heated to 180-300°C. The controlled gas enters the separation cylinder 291 and flows downward along the inner wall of the dust removal tank body 292, and flows upward through the outlet pipe 293, the connecting pipe 31 and the connecting pipe 32 to flow vertically to the low-pressure burner 33. The heavy tar and dust in the gas flowing downward from the separation cylinder 291 cannot flow upward along the tank wall due to gravity, and fall directly to the lower part of the dust storage tank 30. The tar mist and phenol water mist can enter the low-pressure burner 33 with the gas flow and burn at the same time, that is, the initial condensation state appears, and it is also a fuel with good fluidity, and it does not stick or block the pipe valve parts. These can enter the low-pressure burner 33 with the fluid, which is basically light oil and a small amount of phenol water vapor, and burn together and produce: the oil and gas that enter per ton of straw burning steam can increase the steam production effect by 0.6-0.75t.

[0034] The gas produced in the gasifier enters the gravity dust removal tank 29 through the gas conduit 9. After dust and ash removal, the gas enters the connecting pipe 31 and the connecting pipe 32, and is burned by the low-pressure burner 33 to obtain corresponding heat energy. The dust, ash and other debris discharged with the gas in the gasifier will enter the dust storage tank 30 under the action of gravity. In the above-mentioned combustion gas dust removal process, the high-temperature steam in the gasifier can enter the steam inlet chamber sleeve 94 through the steam inlet pipe 93, and enter each semicircular tube 96 to heat the outer periphery of the gas conduit 9. After heat exchange, the high-temperature steam enters the drainage chamber sleeve 97 to form water and is discharged through the drainage pipe 99.

[0035] The arrangement of the above structure can maintain the temperature of the inner wall of the gas conduit 9 at 180-300°C so that the tar and phenol water are always in a gaseous or misty state. That is, the tar component does not produce adhesion at a temperature of 180-300°C, and maintains a gaseous state flowing with the gas to avoid adhesion to the inner wall of the conduit, thereby playing a corresponding anti-condensation role.

[0036] A method for producing carbon monoxide and hydrogen in a gasifier using straw as a raw material, characterized in that it comprises the following steps: ① when the straw is harvested, it is directly loaded into a vehicle and transported to a collection and processing center without falling to the ground; ② After the straw is sent to the processing center, it is squeezed and dehydrated (juice) within 2-3 days of harvesting to reduce its moisture content to ≦43%; ③After the pressing in step ② is completed, the slag climbs dozens of meters high through the conveyor and falls freely and gradually. The continuous falling makes the slag form a hill from small to large. During the process of forming the hill for dozens of hours, the slag is dried in the sun, and the water evaporates by wind by 8-15%, and the water content of the slag drops to 35-30%; ④ Use two double-roller tooth hole combined extrusion pellet machines as a group to extrude the residue to make pellets. The first machine initially extrude medium φ16-20mm pellets with steam at a temperature of about 30℃, and the micro pellets emit steam to reduce the moisture content of the residue by 3-5% again. The semi-finished pellets made by the first machine enter the second extrusion pellet machine to make the semi-finished product with a moisture content of less than 30% and be extruded into φ16-20mm pellets again, or processed into φ30mm briquettes through rolling; ⑤ Put the dehydrated and extruded pellets or briquettes into the gasifier as raw materials, and high-temperature gasification makes the straw produce CO+H2=72%-82% gas.

[0037] Furthermore, in the gasification process in step ⑤, the gasifying agent is pure oxygen, oxygen-enriched oxygen or air, and preferably oxygen is mixed with carbon dioxide or part of steam for gasification.

[0038] Furthermore, in the three-stage pure oxygen anti-condensation gasification furnace using straw as raw material, the thickness of the oxidation layer and the reduction layer is controlled at 5-12m, preferably 7-12m, with a slag layer at the bottom and a retorting layer at the top. The gasification produces a stable CO+H2=72%-82% gas, which is used to extract hydrogen or synthesize green chemical products such as methane and methanol, as an inexhaustible green and clean energy.

[0039] The gasifier is a mixture of O2+CO2, which mainly realizes high-temperature gasification at 900-1050℃ or 1200℃. CO2 mainly comes from the inherent C02=14-25% of the output gas. The CO2 collected by the pure oxygen-fired boiler of the output gas is sufficient to be mixed with O2 to form a high-temperature gasifier for repeated use. It is actually a CO2 semi-medium medium. When the pure oxygen gasification temperature is 900-1050℃, CO2 can reduce CO by 50%, and when it is 1200℃, CO2 can reduce CO by 70%, which can save 10-15% of straw and generate 100-180m³ of O2. Pure oxygen gasification can use negative steam, which can pass through the ultra-thick slag layer to increase the temperature again to exceed the hot steam and enter the oxidation layer. In order to prevent the slag honeycomb from failing, stabilize the output of CO+H2=72%-82%, and reduce the swelling of the upper furnace particles due to wetting, CO2 is preferred.

[0040] The construction steps of the above method for preparing high-purity carbon monoxide and hydrogen can also be described as follows: 1. Storage and timely processing of fresh and wet straw ① When the straw is harvested, it is directly loaded into vehicles and transported to the collection and processing center without falling to the ground.

[0041] ② The straw is sent to the processing center for dehydration (juice) at a daily squeezing capacity of 100 tons, 400 tons, and 600 tons to ≦43%. After squeezing, the residue climbs dozens of meters high through a 30-60 meter conveyor and falls freely and gradually. The continuous falling residue forms a hill from small to large. When the bottom of the hill reaches a diameter of 40 meters, it is enough to store tens of thousands of tons of straw residue (raw materials). During the process of forming the hill for dozens of hours, the residue is dried, and the water evaporates by wind by 8-15%, and the moisture content of the residue drops to 35-30%. In order to store more residue, the 30-60 meter conveyor can move forward or backward, and swing left and right to allow limited land to accommodate tens of thousands or hundreds of thousands of tons of residue (straw), which is equivalent to using only 30 mu to replace the original straw to store dozens of times 2,000-3,000 tons of straw.

[0042] ③ According to ②, the straw after squeezing juice was placed in a hole for three years without rotting, spontaneous combustion, or blackening. It was fed to cows for a few days and was eaten by cows as usual. This created a reliable foundation for the storage of straw without weathering or rotting for three years. Its functions are: the straw is squeezed and dehydrated to be dense, and the presence of air and oxygen is greatly reduced. After three years, the temperature of the hole is about 30℃, which is not easy to spontaneously combust. Without squeezing and stacking, the temperature in the stack exceeds 60℃ and is prone to spontaneous combustion. Therefore, the straw should not fall to the ground and should be stored in time, and the dehydration and density must be significant. Sweeping and dehydrating the straw is not only for storage, but the key is to prevent spontaneous combustion and fire.

[0043] ④ The residue is preferably processed by two double-roll tooth hole combined extrusion pellet machines in a group. The first one initially extrude medium φ16-20mm pellets with steam at a temperature of about 30℃. The steam emitted by the pellets slightly reduces the moisture content of the residue by 3-5% again. The first one extrude is a semi-finished product, which directly enters the second extrusion pellet machine with a moisture content of less than 30% and is extruded into φ16-20mm pellets again. The pellets are plastic and have high hardness. The key is that the pellets are plastic and soaked in water for 20 hours, and they swell slightly but do not bloom obviously.

[0044] ⑤ Through the above ①②③④, large-scale and mechanized harvesting of straw that does not fall to the ground is achieved, and it is squeezed in time within 2-3 days to make it free of high moisture and stored for a long time, so that the extrusion pellet machine can be evenly released for several months to extrude it into φ16-20mm pellets, and it can also be rolled to process φ30mm briquettes. The extruded pellets lay the foundation for the output of CO+H2≥72%.

[0045] The straw particles processed in the above steps are subjected to pure oxygen high-temperature gasification in the gasifier, and the respective layers and functions are as follows: the straw anaerobic particles are gasified at high temperature to produce CO+H2=72%-82%, and the straw performance is about 25% carbon content, 30-49% volatile matter, 30%-50% ash content, and the ignition point value is 300°C. The difference between the gasified coal is about 80% carbon content, volatile matter ≦13%, ash content ≤11%, and the ignition point value is above 600°C.

[0046] The oxidation layer and reduction layer of the φ2-4m gasifier are the middle section of the high-temperature gasifier. Unlike coal, straw only contains 25% carbon, but its volatile matter is higher than 30-49%, its ash content is 30%-50%, and its key ignition point is 300℃. More than a decade of gasification has proved that the coal carbon gasification layer of 300mm and the reduction layer of 500mm are not the same thing for straw gasification.

[0047] The oxidation layer and reduction layer of straw gasification are always in a free state and fluctuate too much. For example: when the oxidation layer of straw gasification is 1200mm and the reduction layer is 3000mm, the outlet temperature exceeds 300℃ and the gas production CO+H2≤60% when running for more than 36 hours. If it is lower than 60%, it is a complete failure. Therefore, the high-temperature gasification oxidation layer and reduction layer of straw are set to 5-12m as the middle section of the gasifier. The oxidation layer and reduction layer are locked in the middle section of 5-12m high through the 5-12m height (thickness). It is more reliable to use 7-12m first. The oxidation layer is always floating. The oxidation process actually produces a large amount of high-temperature CO2. Since the straw contains only 25% carbon, a small amount of oxygen will flow into the upper layer due to the combustion gas. The high temperature of the coal-making oxidation layer is 4 times that of the coal-making oxidation layer = more than 1.2 meters. The reduction layer is both a reduction layer and a small amount of oxidation layer, which is equivalent to a weak oxidation layer. The actual layer thickness is X4 = 2.0 meters. The two items plus the insurance coefficient oxidation layer and reduction layer are 3.2X2 = 6.4 meters, reaching a thickness of 6.4 meters. The gasification intensity of the oxidation layer and reduction layer is 600-900m 3 / m 2 It can run stably and continuously for hundreds or thousands of hours to produce CO+H2=72%-82% (excluding CH4≥4%) gas.

[0048] According to the arrangement of the slag layer in the above-mentioned high-temperature gas furnace, the thickness of 1-5 meters is preferably 3-4 meters. The 3-4 meter thick slag is at a high temperature of 300-700℃. This high-temperature slag is used to heat the passing gasifier. Once the high-temperature gasifier enters the oxidation layer, it is ensured to be above 300℃ to prevent moisture from entering. The 3-4 meter thick slag layer regulates the changes of the oxidation layer and the reduction layer through continuous and slowly matching the slag discharge speed to stabilize it in the middle section of the furnace within the range of 5-12 meters.

[0049] The height of the distillation and space layers is about 6 meters, and 8-12 meters is preferred. The main function of the distillation space is 4-6 meters. The actual use height of the distillation layer (including waiting materials) is reduced by 1 meter, that is, 3-5 meters. The remaining 4-6 meters of space is mainly used to arrange the isolation tube with a height of 4-6 meters. The remaining space in the furnace will produce dust precipitation when unloading materials to prevent it from entering the gas pipeline.

[0050] When straw particles are gasified at high temperature in a gasifier, the required gasifying agent and temperature are as follows: the biomass gasification temperature is mostly 300-700°C, and the raw materials used are wood chips, building boards, and rice husks. The advantage of low-temperature gasification is that wood ash and charcoal can be discharged.

[0051] The high temperature of straw gasification at 900-1050℃ or 1200℃ is to produce CO+H2=72%-82% gas. Each ton of straw can produce 1100m 3 / t gas can extract hydrogen ≥ 600m 3 , methane ≥ 275m 3 above.

[0052] The principle of gasification agent and high temperature gasification is: Gasification agent: O2+CO2 mixture, mainly to achieve 900-1050℃ or 1200℃ high temperature gasification, CO2 mainly comes from the inherent C02=14-25% of the output gas, and the CO2 collected by the output gas pure oxygen-fired boiler is enough to be mixed with O2 to form a high temperature gasification agent for repeated use, which is actually a CO2 semi-medium medium. When the pure oxygen gasification temperature is 900-1050℃, CO2 can reduce CO by 50%, and when it is 1200℃, CO2 can reduce CO by 70%, which can save 10-15% of straw and generate 100-180m³ of O2. Pure oxygen gasification can use negative steam, and pass through the ultra-thick slag layer to increase the temperature again to exceed the hot steam to enter the oxidation layer. In order to prevent the slag honeycomb from failing, stabilize the output of CO+H2=72%-82%, and reduce the upper furnace particles from being humidified and puffed, CO2 is preferred.

[0053] During normal operation, the slag layer discharge gradually forms a continuous matching ash content of 30%-50%, that is, 0.3-0.5 tons of ash are produced for each ton of straw gasified. The workload is adjusted (corrected) at any time to automatically discharge slag, and the middle furnace oxidation layer (high temperature zone) is controlled at the lower third of the middle section of the furnace, so that there is a slag layer section of 3-4 meters at the bottom, and the upper 3-5 meters of raw material layer firmly controls the oxidation layer and reduction layer to stabilize in the middle section. In short, it is key to determine the continuous discharge of slag and the amount of digested straw in the oxidation layer and reduction layer, and the layer matching; this requires that the straw ash content is 30%-50%, so many people did not think of it, but simply applied the ash content ≤11% block coal gasification, and the technical breakthrough point is here.

[0054] The structure of the high-temperature gasifier can be described as follows: The high-temperature gasification of straw divides the oxidation layer reduction layer into one section, the dry distillation section, and the slag section into three sections to achieve high-yield, high-efficiency and stable output of CO+H2=72%-82% gas. The pure oxygen gasifier is made into a three-section principle, in which the furnace uses three (sections) of water jackets to form a high-temperature gasifier. The steel wall of the gasification furnace composed of the water jacket is always cooled by water, and the gasified raw materials in the furnace are heated without sticking to the wall. Among the three water jackets: the middle section is the high-temperature section, the lower section is the medium-temperature section, and the upper section is the low-temperature section. The middle section is in the high-temperature section of the oxidation-reduction layer. The water temperature in the water jacket can exceed 130°C to produce about 1.5 tons of steam. The upper section heats the water and evenly injects it into the lower section for heating. After heating, it is injected into the middle section to produce saturated steam.

[0055] Regarding the anti-condensation gasification of produced fuel gas: For the pure oxygen anti-condensation gasification furnace that produces straw CO+H2≧72%-82%, the outlet temperature of the upper furnace gas is difficult to reach 130°C due to the heat absorption of the material layer that is more than ten or twenty meters thick. The tar in the fuel gas, which basically maintains a temperature of 40-70°C, tends to be liquid and carries dust. After running for dozens of hours, it is easy to cause pipeline blockage.

[0056] For this purpose, Figure 4-Figure 8 The gas conduit 9 is provided with an anti-condensation device, and a plurality of evenly arranged semicircular tubes 96 are welded to the gas conduit 9 in the longitudinal direction. A steam inlet chamber sleeve 94 and a drainage chamber sleeve 97 are welded to the upper and lower ends of the gas conduit 9, and the gas conduit 9 is connected and fixed to the gasifier outlet 91 through a first flange 92 on the steam inlet chamber sleeve 94. Then, steam enters the steam inlet chamber sleeve 94 through the steam inlet pipe 93, and is injected into the semicircular tubes 96 through evenly distributed holes to heat the gas conduit 9 to 150-300°C (preferably 180-300°C). When the inner wall of the gas conduit 9 conducts heat, the transported gas with a temperature below 150°C is heated.

[0057] The above structure has the following functions: maintaining the inner wall of the gas conduit 9 at a temperature of 180-300°C so that the tar and phenol water are always in a gaseous or misty state, that is, the tar component does not produce adhesiveness at a temperature of 180-300°C, and is maintained in a gaseous state flowing with the gas, maintaining the gas conduit 9 and the semicircular tube 96 at 180-300°C, and promoting the gas to rise instead of falling under the action of the steam temperature, and smoothly input into the low-pressure burner 33. The semicircular tube 96 welded on the surface of the gas conduit 9 can use the semicircular tube height size as the diameter of the round tube size, and spirally wrap along the outer diameter of the tube to both ends to replace the semicircular tube performance.

[0058] After the steam inlet pipe 93 inputs the steam into the steam chamber sleeve 94, it is injected into each semicircular tube 96 to release heat through the inner wall of the gas conduit 9 until the drainage chamber sleeve 97 gradually cools down to produce hot water. A water discharge valve can be used on the drainage pipe 99 to discharge it into the boiler water injection system at any time.

[0059] The steam from the boiler heat exchanger can be preferably heated up again to 240-300°C, and the steam consumption is 0.15-0.5t / h when the pipe diameter is ф600-1200mm. The temperature of the steam mainly heats the inner wall of the gas conduit 9 to 240-300°C, so as to prevent the tar in the gas from developing into a viscous state and smoothly transport it to the low-pressure burner 33. The steam heat consumed by the gas conduit 9 is returned to the boiler through the burner through the gas heat absorption, and a small amount of phenol water disappears under the high temperature state in the boiler. In order to return the heat energy of the steam used for heat preservation to the furnace, the entire device must be provided with a 100-150mm thick reinforced insulation layer to prevent heat energy from overflowing.

[0060] The water jacket in the gasifier structure can be divided into two or three sections to realize an oxidation layer, and the reduction layer height (thickness) is greater than 1.0-4.5 times the furnace diameter. The limited carbon (about 25%) of the straw in the middle section of the furnace can be oxidized at high temperature in the thick layer, and the reduction can control the fire normally.

[0061] In high-temperature gasification, O2 and 30-90% CO2 are fully mixed as gasifying agents. When the temperature of the gasification layer is ≥1050℃, the reduction rate of CO2 can reach 50%, which not only reduces and adds one CO but also releases oxygen. It is equivalent to the known technology that saves 10-15% per ton of raw materials and releases hundreds of cubic meters of oxygen. The key is to reduce the generation of water vapor and the expansion and blooming of the upper straw particles in the furnace, avoiding the difficulty in handling excessive dirty (phenol) water and also causing the low cracking rate to absorb a large amount of heat energy. The selection of CO2 to replace steam reduction is basically in the drying process. It is easier to reasonably mix O2 or add CO2 as a gasifying agent to prevent the particles in the furnace from being soaked, expanded and bloomed.

[0062] Through the field test, the gasification output gas component content H2 or adding CO≧70% and CH4≥4% can extract more than 70% hydrogen after transformation, which is the basis for synthesizing methane, methanol and other clean green energy. The present invention uses straw as raw material for gasification, mainly because the straw itself contains volatile matter as high as 49%, and the carbon ignition point is too different, only about 25% (straw harvested in the same year). Through this invention, with the help of about 25% limited carbon, pure oxygen is used to increase the gasification temperature to 900-1350℃, and CO2 is perfectly comprehensively utilized to replace water vapor to produce H2 or add CO≧70%, CH4≥4%, CO2≦20%, which is the best raw material for synthesizing methanol and methane. It is better to extract ≧70% hydrogen CH4≥4% after transformation to become an inexhaustible synthetic raw material and non-fossil green energy.

[0063] The first water jacket 6, the second water jacket 7 and the third water jacket 8 can be combined into a full-height integrated water jacket furnace. The first water jacket 6 in the medium temperature section originally has a furnace mountain, and the slag layer is cooled to generate a medium-temperature heat source to generate medium-temperature hot water. The second water jacket 7 in the high temperature section originally has an oxidation layer, and the reduction layer releases heat to generate a high-temperature heat source to make the water high-temperature. Because the third water jacket 8 in the upper section of the low-temperature section specifically for gasifying straw needs to be set up with an ultra-large space of 1.0-4.5 times the furnace diameter, it can only become a furnace type that efficiently gasifies straw garbage if it stores raw materials that are multiple times larger than the second water jacket 7 in the middle section.

[0064] The third water jacket 8 of the upper section of 1.0-4.5 times can form a thickness greater than the oxidation layer and the reduction layer, which is about 1.0-4.5 times of the furnace. The reason for the extra thickening is that the ultra-thick retorting and drying layer can effectively hinder the uneven fire-spilling phenomenon of the ignition point value of the straw from occurring in the retorting layer and the drying layer, that is, the temperature of the oxidation layer is increased to reduce the reduced fuel gas CO2 and trace oxygen in the ultra-thick, especially ultra-thick retorting layer and the drying layer, and the oxygen is consumed, so that the gasification reduction layer in the whole furnace is reduced in the multi-layer ultra-thick retorting layer to continuously and stably reduce the up and down floating, and the up and down floating of the key reduction layer in the straw gasification furnace is reduced, and in a word, the thickness of the reduction layer is increased, and the excessive fire-spilling of trace oxygen in the retorting layer is minimized, that is, in popular terms, find a way not to burn biased in the furnace, that is, biased, there is a thick and thick raw material layer, which effectively hinders biased burning and finally burns flat naturally. The second water jacket 7 is an oxidation layer and a reduction layer in a high temperature layer, and the water temperature of the water jacket is ≥ 130°C. The third water jacket 8 is dry distilled and dried in a low temperature water jacket, and the water temperature is ≥ 70°C. The first water jacket 6 in the lower section is in the middle temperature of the slag layer, and the water temperature in the water jacket is ≥ 95°C. In this way, the water jackets are rationally and creatively separated according to the temperature layers in the gasifier. The water in the water jacket enters the upper section and becomes low temperature. The low temperature enters the first water jacket 6 to absorb the heat source of the slag layer for heating. The oxidation layer and the reduction layer of the second water jacket 7 in the middle section release heat for heating, and finally the water temperature in the second water jacket 7 in the middle section is > 130°C.

[0065] In order to reduce the floating of the reduction layer, it is necessary to thicken the dry distillation layer to 1.0-4.5 times the furnace diameter, directly forming the upper third water jacket 8, which is very high and thick, driving the lower first water jacket 6 and the middle second water jacket 7 to form a three-piece water jacket with high height. The upper extra-thick (high) material layer forms the third water jacket 8 to absorb low-temperature heat over a large area, so that the water temperature is >70℃ and enters the lower first water jacket 6 and the middle second water jacket 7, effectively sealing and strictly heat-insulating the gasification process of the gasifier to generate heat energy and convert it into high-temperature hot water or saturated steam >130℃ in three stages.

[0066] The operation of the above three-stage water jacket is to break the routine of gasification coal in combination with the actual gasification raw materials to release the oxidation layer, the reduction layer position and thickness, and the upper third water jacket 8 has multiple layers of thickened gasification raw materials to achieve the purpose of improving the gasification intensity, reducing the oxygen content of CO2 and fuel gas to form conditions that hinder crossfire, and the key is to play a role in reducing coarse dust in the furnace.

[0067] The present invention preferentially uses a low-temperature section, a medium-temperature section, and a high-temperature section arranged in sequence. The medium-temperature section (slag layer) and the high-temperature section are combined as needed to form a double-section water jacket. The original upper section can be replaced with an inner lining made of refractory materials or refractory bricks to increase the output gas temperature, mainly for heat preservation and tar prevention, so that the water-forming liquid is smoothly transported to the gas boiler and prevents pipeline adhesion, wall hanging, and blockage.

[0068] In order to process billions of straw and convert them into green energy gas with CO+H2≧75%-82%, a ф2.0-4.0 diameter fixed bed gasifier with three functions of high temperature, medium temperature and low temperature is selected. A single gasifier can process ≧120 tons of straw per day, and produce CO+H2≧75%-82%, and gas≧130,000m 3 , 5-10 gasifiers are distributed in counties, cities and districts as blocks, which consume 750-1500 tons of straw and produce 800,000-1.6 million m3 of CO+H2≧75%-82% gas. 3 , a total of 220,000 to 450,000 tons of straw are consumed throughout the year, basically all the straw in the area is consumed without falling to the ground or rotting. In other words, large-scale and stable industrialization will make full use of the annual straw.

[0069] The test case results of the present invention are as follows: In 2010, the lower furnace of the double-stage furnace (commonly known as the semi-water jacket (chamber)) was used with a height of 2.3m, and the straw particles were oxidized with pure oxygen to obtain a gas composition of CO2≧27% , O2=2.1-3%, ash residual carbon rate 7-11%, difficult to ignite. Since CO2 and residual carbon rate are high and reduce the gasification energy conversion efficiency, gas containing oxygen O2=2.1-3% cannot be separated from tar and purified by high-voltage electrostatics.

[0070] In 2013, the lower furnace of the double-stage gasifier was changed to 3.3m (increased by 1.0 meter). The gas component CO2 of the gas obtained by pure oxygen gasification of straw decreased by ≤25%, O2=1.2-2.1%, and the residual carbon rate of ash was ≥7%. Since CO2 was still relatively high, the gasification rate was low, and the gas containing oxygen O2=1.2-2.1% could not be separated from tar and purified by electrostatic precipitator.

[0071] In 2018, the lower water jacket (chamber) of the double-stage gasifier was changed to 4.3m (another 1.0m higher), which is 2.0m higher than the general technology. The gas composition CO2≦21.6%, O2=0.6%, ash and slag carbon residue rate≦6%, and high-voltage electrostatic purification can be used smoothly. The gas from the gasifier is first electrostatically captured, and the ash and dust heavy adhesives (coarse tar) are melted into the tar. The gas attachments are no longer bonded and blocked, so that the electrostatic capture purification and separation system operate normally and stably. The tar content of the tar-purified gas is detected to be ≦10mg / m³, and then it is adsorbed to 2mg / m³, which finally solves the bottleneck of difficult separation and recovery of gas tar, and opens up the way for straw gasification and complete purification. The use of this gas to replace natural gas for gas boilers operates normally, and each ton of straw can produce more than 3.4 tons of steam.

[0072] In order to achieve the development of non-fossil energy in 2021-2023, it is proposed to use: a furnace chamber 10.5 or 2.0 meters high is divided into three sections of water jackets (chambers) to replace the gasification furnace chamber. The ash layer in the furnace is arranged in the lower section, and the oxidation layer and reduction layer are arranged in the middle section. The main purpose is to make the retort layer (including preheating) thicker and thicker, and the thickness is greater than 1.0-4.5 times the furnace diameter. Thickening reason: Straw and garbage in the gasifier and each time they are fed and unloaded, the volatiles first overflow, and the remaining solid black carbon oxidation layer reacts violently to produce high-temperature carbon dioxide and enter the reduction layer. That is to say, when the gasification process of the raw material is unstable, the high temperature of the oxidation layer is easy to cross the fire. For example: the furnace chamber with a diameter of 3.6 meters is 10.5 or 2.0 meters high, and the slag layer, oxygen layer, and reduction layer are controlled to be about 3-4 meters thick. In this way, there is a 3-5-meter retort layer that is lacking oxygen and cannot be heated. At the same time, the high temperature drops to medium temperature and cannot be ignited. The raw materials finally become natural to block the crossfire, and only the medium-temperature oxygen-deficient airflow flows in the retort layer.

[0073] The upper and lower combined height of the double-stage or three-stage water jacket (chamber) is about ten meters. The furnace is a steel plate structure, which is conducive to the normal and smooth sliding of the super-thick material layer in the furnace. The three-stage water jacket (chamber) is divided into upper, middle and lower sections under pressure. When the gasifier is running, the upper section preheats water to input the lower section for heating. The middle section is heated to high temperature to produce steam output, and the pressure can reach 1.3MPa. When the gas meets the gas boiler to produce 8 tons of steam, or the gasification intensity is 200-500m³ / ㎡ for oxygen and 400-1000m³ / ㎡ for air. The water jacket (chamber) produces 1.6-2 tons of steam at the same time, that is to say, the upper and lower sections of the three-section water jacket (chamber) wall are heated up by >150℃ (the temperature in the slag layer is 150℃-700℃), and the middle section wall is heated up by >240℃ (the temperature of the oxidation and reduction layers is 700℃-1300℃), and all the heat energy is absorbed again. The gas produced by the innovative way of operating the two functions replaces the natural gas boiler to produce steam. The pure oxidation gasification of each ton of orange stalk produces >4.2 tons of steam, and the air gasification produces >3.8 tons of steam. At present, about 2.5 tons can be found in China, and the thermal energy conversion efficiency is significantly improved. Due to the low temperature difference between the oxidation layer and the reduction layer of the double section, the fire jumps upward, and the CO2 content is not obvious.

[0074] The gasification layer and reduction layer of the straw gasification of the present invention are surprisingly large and messy. The main reason is that the ignition points of various raw materials in the straw garbage are very different. For example, the straw body and straw leaves, garbage solids and paper and plastics are violently oxidized after encountering oxygen, and are prone to excessive penetration. Therefore, the oxidation layer is many times higher than that of gasified coal, and the reduction layer is thicker. The furnace body is synthesized in three sections of water jackets, leaving sufficient reaction layer thickness. The position of the oxidation layer can not be accurately known by using a probe to detect the high temperature point. First, the high temperature point changes quickly, and second, it takes time to detect the point and cannot detect the temperature in time. The present invention adopts multi-point arrangement of electric induction to timely understand the temperature layer and quickly and automatically adjust.

[0075] Take the running Φ2.6m as an example: starting from 0.4-0.9m from the top of the furnace, use two pitches of 3m, that is, 3m X 2=6m in height, and evenly arrange 4 probe points in each pitch, for a total of 9 probe points. Multiple temperature probes can be added radially at the probe point, and the uniform temperature of the probe point can also be displayed by a table.

[0076] A double or three-stage water-jacketed (chamber) straw O2 or CO2-added gasifier for non-fossil energy hydrogen and heat production, with a range of requirements, through more than ten years of repeated straw gasification to high-jacketed (chamber) furnaces, multiple times higher-jacketed (chamber) water jackets to replace various existing furnaces. The distillation layer is 3-9 meters or more.

[0077] The nitrogen oxides in the gasified gas of straw waste can reach 240-900mg / m 3 , the denitrification agent is sprayed on the gas boiler with intelligent burner to reduce the concentration to 45-130mg / m 3, fluctuations are not easy to stabilize. The present invention proposes to use a feeder to uniformly inject an appropriate amount of denitrification agent during the feeding process of the gasifier. The gasification temperature and temperature layer difference are used to first denitrify in the furnace, and then the denitrification agent is injected into the burner for secondary denitrification, so that the straw gasification plus denitrification agent, the burner is sprayed with denitrification agent for the second time, and the nitrogen oxides are steadily reduced to 50mg / m 3 Within.

[0078] The water jacket (chamber) is raised to replace the furnace, and the dry layer is naturally thickened. The particularly thick dry layer plays a clever role in filtering the gasified gas from the lower part containing dust. The actual continuous operation from 2022 to 2023 proved that the dust generated was very small, and the electric coke collector can basically be left unattended. During maintenance, the manhole was opened to observe the pipeline, and there was no dust or tar attached to the space. The water jacket (chamber) is raised to replace the furnace, and the slag layer retention time is extended, and the residual carbon rate of the produced slag is extremely low.

[0079] After the straw is squeezed and dehydrated, the slag with a moisture content of ≤45% is freely scattered by the belt conveyor and gradually piled up into a hill over a long period of time. The process takes several hours or more than ten hours. After the moisture is naturally evaporated by 7-15%, it can be used as raw material or pressed into blocks (sheets). The briquettes with a diameter of about ф16-32mm or naturally pressed sheet raw materials are preferably used.

[0080] After squeezing the garbage, add an appropriate amount of relatively dry straw residue and mix it thoroughly to absorb the moisture of the garbage material to avoid drying in the environment.

[0081] A double-stage or three-stage water-jacketed (chamber) straw O2 or CO2-added gasifier for non-fossil energy hydrogen extraction and heat supply is characterized in that: the water jacket (chamber) of the gasifier is changed into a high water jacket (chamber) furnace chamber with upper, middle and lower sections to achieve very good results. The reason is not complicated. It is the well-known principle of the gasifier. The gradually cooled slag layer and the high-temperature air flow CO2 in the oxidation layer neutralizes and reduces CO2 and increases CO in the reduction layer. At this time, the oxygen content of the gas flow is extremely low. Only medium temperature (especially emphasizing lack of oxygen) enters the retorting layer, which will increase the ignition point of the coal itself to more than 600°C. A trace of oxygen cannot ignite the semi-coke of the coal after retorting. Therefore, the retorting layer is designed to be less than 2-3 meters. If it is too thick, it will easily stick together, which is not conducive to the gasification effect. However, the ignition value of straw garbage is uneven, and trace oxygen can easily ignite the raw materials with low ignition points in the retorting layer, gradually pulling the oxidation layer upward and burning. In 2010 and 2013, when the straw was gasified, the fire detection hole on the top of the gasifier was opened and the produced gas fire rake was not easy to ignite. Later, the lower furnace (water jacket (chamber)) was changed to a height of 4.3 meters, and no sparks were seen in the detection hole. The produced gas drove the internal combustion engine to generate electricity very smoothly, laying the foundation for gasification power generation. Regarding the uneven calorific value of orange stalk garbage, two fires occurred at the site of the present invention, which is sufficient to prove that the fire was mainly ignited by sparks from electric welding. The fire was fierce and four fire trucks put it out after a few hours. The scene was basically full of straw stalks, and the flammable straw leaves were not seen. It was also difficult to ignite the stalks with a match. After being processed into pressed blocks, the low calorific value in the gasification distillation layer was easily ignited by trace oxygen. Flames were often seen in the detection hole of the gasifier in 2010.

[0082] After the operation test results of the 4.3m high water jacket (chamber) furnace in 2013, the ф3.6m gasifier is taken as an example: the water jacket (chamber) is composed of three sections, the first water jacket 6 in the lower section is 2.0m high, the second water jacket 7 in the middle section is about 4.5 meters high, the third water jacket 8 in the upper section is 4.0 meters high, the total height is 10.5 meters or plus 2.0 meters of unloading space, totaling more than 12.5 meters. The high temperature of the oxidation layer reduction layer is in the middle section of the water jacket (bore). The high-pressure steam produced is output from the upper part of the middle section. The upper section is preheated and driven into the lower section, and then heated and driven into the middle section to achieve the full furnace closed absorption furnace heat dissipation. The key is that the lower, middle and upper sections of the water jacket (bore) are processed into steel plate structures. The outer periphery of the water jacket (bore) is super thick and insulated. The exchange between the water jacket (bore) and the steel plate wall of the furnace hall makes the overall material in the furnace slide smoothly, that is, the exchange between the temperature difference between the water jacket (bore) and the wall prevents the high-temperature material from sticking to the wall. The key role is to always keep the furnace wall smooth. Set up a multi-point induction temperature probe to always control the oxidation layer in the middle of the middle section of the water jacket (bore), and the temperature of the measuring point at the bottom of the lower section of the water jacket (bore) shall not be higher than 400℃.

[0083] Pure oxygen is used to produce gas, which is compressed to remove carbon dioxide with a calorific value of 3000kco / m 3, used as clean fuel gas or pipeline transportation, CO2 back to the gasification furnace or become a product, while the fuel gas component H2 or CO = 76-82% is used to extract hydrogen or synthesize methane or methanol and other alcohol compounds according to the development of clean energy. The fuel gas produced by oxygen-enriched and air gasification is used for heating in gas-fired boilers, kilns, sintering, and can also be used for internal combustion engine power generation, etc., and can be used for civilian use after deep purification.

[0084] The thickness of the slag layer, oxidation layer and reduction layer of the high water jacket (chamber) hall furnace is about 2.0 meters for ф0.8-1.6 meters and 3.0-4.0 meters for ф1.8- to 3.6 meters according to the furnace diameter. The thickness of the preheating layer of the dry distillation is 1.5-4 times. The total height of the furnace diameter ф0.8-1.6 meters is 4.0-6.0 meters when viewed from the outside of the furnace body, and the total height of ф1.8-3.6 meters is 6.0-12 meters. According to the raw materials and operating conditions, the upper, middle and lower three-section water jacket can be combined into a whole section by using the lower section and the middle section, and the height of the combined water jacket should not be less than 2.4 meters. If the furnace diameter is small, the upper, middle and lower three sections can be selected as an integral section without segmentation, so as to meet the function of the three-section high water jacket as much as possible, that is, the output gas energy conversion rate is higher.

[0085] The nitrogen oxide content of the gas produced by straw waste gasification reaches 240-1000mg / m 3 , which makes it difficult to denitrate the boiler burner. In order to reduce the denitration, the denitrifier is injected as needed during the normal operation of the gasifier. It is mixed with the material in the furnace and the nitrogen oxides in the gas are reduced in advance under the action of temperature. The denitrifier dosage is 10-40kg per ton of material. Pure oxygen gasification can also be replaced by 3-5 times the amount of stone powder, or liquid denitrification can be used to spray into the gas outlet pipeline in a mist form. In this way, the nitrogen oxides in the gas produced are less than 150mg / m 3 , so that the boiler burner can denitrify more smoothly and reach the emission standard of 50mg / m 3 .

[0086] The pure oxygen gasification of rural straw waste and high-water jacket (chamber) furnace with low nitrogen for natural gas boiler operation from 2022 to 2023 proves a fact. Straw waste gasification is different from coal. The carbon content of coal gasification reaches 80%, while the carbon content of straw gasification is only about 20%. The limited carbon is concentrated for oxidation, temperature increase, heat preservation and reduction. Make full use of the volatile matter of straw waste to convert into energy, and pure oxygen gasification can take in an appropriate amount of CO2.

[0087] The gasifier using anthracite with volatile matter ≤11%, calorific value 6000kca / kg, ignition point ≥600℃, carbon content ≥80% generally sets the thickness of the oxidation layer to about 300mm and the reduction layer to about 500mm. They are arranged together with the slag layer in a 2-3m high water jacket in the lower section of the gasifier. In order to improve energy conversion, when the gasification intensity is ≥400m / ㎡, the steam generated by the lower water jacket is sprayed into the furnace to crack out some CO and H2. The technology, facilities and process flow have been in operation for nearly a hundred years.

[0088] Now straw is used: volatile matter ≥ 40%, calorific value 3000kca / kg, ignition point 300℃, carbon content ≤ 25% to replace anthracite with carbon content ≥ 80%. When the gasification intensity is 200m / ㎡, the oxidation layer and reduction layer cannot be controlled within the 300mm and 500mm layers. When the gasification intensity reaches ≥ 400m3 / ㎡, the oxidation layer and reduction layer basically become fire layers (oxidation layers), and the produced gas is difficult to ignite with a torch. Through repeated experiments, the original ideas, concepts and process procedures have been changed. The height of the oxidation layer and the reduction layer are realized as a super-thickened single layer of 1.0-4.5 times the furnace diameter as the middle section. The 1.0-4.5 times super-thickened oxidation layer and reduction layer are arranged in the middle section furnace. The gasification intensity is first achieved to reach ≧400m3 / ㎡, and the oxidation layer can reach a gasification high temperature of 900-1400℃. In this way, the reduction layer can be efficiently reduced and deoxidized to effectively reduce the oxygen content of the fuel gas to ≦0.9 / %, and the high-temperature fuel gas containing oxygen ≦0.9 / % enters the super-thick layer distillation section of the upper furnace to achieve hypoxia and avoid the fire layer from rising.

[0089] Since C02 is reduced to CO, the calorific value of the gas is significantly increased, and the intelligent burner can be used to operate reliably for hundreds or thousands of hours continuously and stably. It mainly solves the problem of low and uneven ignition point of straw, which causes fire. The thickness of the gasification layer and reduction layer is 1.0-4.5 times the furnace diameter, and the fire layer is firmly locked in the middle furnace. The oxygen content in the gas is reduced in the layer, and the generation of CO is reduced, so that the entire straw gasification can operate continuously. The oxidation layer and reduction layer of the middle furnace are 3-10 meters high, that is, the oxidation layer and reduction layer are at 2-10 meters, which is enough to cooperate with the slag retention time of the lower furnace to firmly lock the oxidation layer and reduction layer in the high temperature of the middle furnace.

[0090] The oxidation layer is realized by dividing into two or three sections of water jacket (chamber). The height (thickness) of the reduction layer is greater than 1.0-4.5 times the diameter of the furnace. The limited carbon (≦25%) of the straw in the middle section of the furnace can be oxidized at high temperature in the thick layer, and the reduction is normal to control the fire. Its gasification is a gasification agent that is fully mixed with O2 and 50-90% CO2. The reduction rate of CO2 can reach 50% when the temperature of the gasification layer is ≧1050℃. It not only reduces and adds one CO but also releases oxygen. It is equivalent to the known technology to save 10-15% per ton of raw materials and release hundreds of cubic meters of oxygen. The key is that there is no water vapor generated to cause the upper straw particles in the furnace to expand and bloom due to moisture, avoiding excessive dirty (phenol) water that is difficult to handle and also causing a low cracking rate to absorb a large amount of heat energy. The selection of CO2 to replace steam reduction is basically in the drying process. It is easier to reasonably mix O2 or add CO2 as a gasification agent to prevent the particles in the furnace from being soaked, expanded and bloomed.

[0091] The middle temperature water jacket, i.e. the first water jacket 6, has a furnace mountain and a slag layer whose thickness (height) is several to ten times greater than the coal gasification furnace operating rules, that is, 1.0-4.5 times the furnace diameter. The purpose is that the slag slowly and continuously sinks, and the gasifier passes through it to absorb the heat of the slag and increase the temperature. At the same time, the gasifier naturally forms honeycomb gaps through the slag to form a stable thermal turbulence uniform gasification layer. In addition, the low temperature water in the first water jacket 6 also absorbs heat to become middle temperature hot water and is pressed into the high temperature water jacket, i.e. the second water jacket 7.

[0092] The comprehensive thickness (height) of the oxidation layer and reduction layer of the high-temperature water jacket, i.e. the second water jacket 7, is greater than the carbon content ≧80%, and the ignition point ≥600℃. The oxidation (gasification) layer is ≈300mm, and it is reduced to multiple times of 500mm, that is, it reaches 1.0-4.5 times the furnace diameter. Its purpose is that the carbon content of the straw is only ≦25% and the CO2 is ≦20% after the gas passes through the extra-thick reduction layer, so that O2 or CO2 is added to produce gas CO or H2=65-82%. The oxidation layer and the reduction layer are in the high-temperature water jacket, i.e. the second water jacket 7, and the medium-temperature water is heated again, so that the hot water reaches a high temperature and produces high-temperature saturated steam.

[0093] The thickness (height) of the dry distillation layer and preheating layer of the straw fuel in the low-temperature water jacket, i.e. the third water jacket 8, is greater than 1.0-4.5 times the furnace diameter. The thick raw material will reduce the trace oxygen in the rising gas in the middle section 7 and deoxygenate it again to achieve dry distillation of the raw material, preheat and finally cool down. At the same time, the water in the low-temperature water jacket, i.e. the third water jacket 8, absorbs part of the heat to generate low-temperature hot water which is pressed into the medium-temperature water jacket, i.e. the first water jacket 6.

[0094] The present invention preferably uses a low temperature section, a medium temperature section, and a high temperature section arranged in sequence. The medium temperature section and the high temperature section are combined into a double-section water jacket as required.

[0095] The invention creates hydrogen and synthesizes alcohols such as methanol through efficient gasification of agricultural and forestry solid wastes such as crop straws, so that the invention also creates technology and processes for gasification of plant stems, branches, shells, chaff, grass, leaves, reeds, and even garbage to extract hydrogen, and synthesize alcohols with low cost and green energy. These non-fossil resources can be transformed into inexhaustible green energy, and the most renewable energy can be converted into green hydrogen preparation and conversion with photovoltaic, wind, hydro and nuclear energy, realizing the green hydrogen energy era together.

[0096] In summary, a double-stage or three-stage water jacket (chamber) straw O2+CO2 gasification furnace for hydrogen extraction, alcohol synthesis and heat supply is characterized in that the straw with low carbon content, high volatile matter, low ignition point and unevenness can be processed into particles, blocks and slices, and a double-stage or three-stage water jacket (chamber) is used to build an ultra-thick slag layer, an ultra-thick gasification (oxidation) layer, and a double ultra-thick reduction and ultra-thick distillation layer to continuously make each layer function stably and smoothly. The straw is converted into CO+H2≧70%, CO2=15% or so, and CH4≧4% gas, becoming an inexhaustible green resource to constitute a variety of green resource products.

[0097] The technical solution of the present invention is not limited to the scope of the embodiments described in the present invention. The technical contents not described in detail in the present invention are all well-known technologies.

Claims

1. A three-stage pure oxygen anti-condensation gasification furnace using straw as raw material, characterized by: The invention comprises a furnace wall (1), wherein a first water jacket (6), a second water jacket (7) and a third water jacket (8) are installed on the outer periphery of the furnace wall (1); the first water jacket (6), the second water jacket (7) and the third water jacket (8) are arranged in sequence from bottom to top on the gasifier; the upper part of the third water jacket (8) and the lower part of the first water jacket (6) are connected via a pipeline; the upper part of the first water jacket (6) and the lower part of the second water jacket (7) are connected via a pipeline; a water supply pipeline (3) is installed at the lower part of the third water jacket (8); a high-temperature medium discharge pipeline (4) is installed at the upper part of the second water jacket (7); a water level gauge (5) is also installed inside the second water jacket (7); and the total height of the first water jacket (6), the second water jacket (7) and the third water jacket (8) is 5.7m-20m, an ash pan slag removal system (2) is installed at the bottom of the furnace wall (1), a connected feeder (12) is installed at the top of the furnace wall (1), a denitration feeder (13) is installed on the upper part of the feeder (12), a material detection layer rod (14) is installed on the furnace wall (1) on one side of the feeder (12), and a gas conduit (9) connected to the furnace is installed on the furnace wall (1) on the other side of the feeder (12), a normal temperature water inlet (27) is installed at the lower part of the third water jacket (8), the normal temperature water inlet (27) is connected to the water supply pipeline (3), and a low temperature water inlet (27) is installed on the upper part of the third water jacket (8). The first water jacket (6) has a low-temperature water inlet (17) installed at the bottom, a low-temperature water pipeline (18) connected between the low-temperature water outlet (16) and the low-temperature water inlet (17), a medium-temperature water outlet (19) installed at the top, a medium-temperature water inlet (20) installed at the bottom, a medium-temperature water outlet (19) and the medium-temperature water inlet (20) connected between the medium-temperature water outlet (19) and the medium-temperature water inlet (20), and a high-temperature medium discharge outlet (22) installed at the top of the second water jacket (7). The outer periphery of the gasifier is provided with a plurality of spirally arranged temperature measuring devices (28). The gas guide One end of the pipe (9) is connected to the furnace wall (1), and a gravity dust removal tank (29) is installed at the other end of the gas conduit (9). A dust storage tank (30) is provided at the bottom of the gravity dust removal tank (29). A connecting pipe (31) and a connecting pipe (32) are installed at one side of the gas outlet of the gravity dust removal tank (29). The connecting pipe (32) is connected to a gas processing device. The gas processing device is a hydrogen extraction, methane synthesis, methanol system or a low-pressure burner (33). The low-pressure burner (33) is provided with a tar sprayer (34). The upper end of the gas conduit (9) is installed with a steam inlet chamber sleeve (94). The steam inlet chamber sleeve ( The gasifier outlet (91) of the furnace wall (1) is connected to the gasifier outlet (94) via a first flange (92), a drainage chamber sleeve (97) is installed at the lower end of the gas conduit (9), and the drainage chamber sleeve (97) is connected to the gravity dust removal tank (29) via a second flange (98), a connected steam inlet pipe (93) is installed on the steam inlet chamber sleeve (94), and a connected drainage pipe (99) is installed on the drainage chamber sleeve (97), and a plurality of circumferentially arranged semicircular pipes (96) are longitudinally arranged on the outer peripheral wall of the gas conduit (9), and the semicircular pipes (96) are connected to the steam inlet chamber sleeve (94) and the drainage chamber sleeve (97).

2. The three-stage pure oxygen anti-condensation gasification furnace using straw as raw material according to claim 1, characterized in that: One end of the gas conduit (9) is connected to the furnace wall (1), and a burner (10) is installed at the other end of the gas conduit (9), and the burner (10) is located in the combustion boiler (11).

3. The three-stage pure oxygen anti-condensation gasification furnace using straw as raw material according to claim 1, characterized in that: The water supply pipeline (3) is equipped with a water bag (23) and a water supply pump (24), and the high-temperature medium discharge pipeline (4) is equipped with a hot water pump (25) and a heat exchange boiler (26).

4. The three-stage pure oxygen anti-condensation gasification furnace using straw as raw material according to claim 1, characterized in that: The water supply pipeline (3) and the high-temperature medium discharge pipeline (4) are connected to the heat exchange steam drum (15) together.

5. The three-stage pure oxygen anti-condensation gasification furnace using straw as raw material according to claim 1, characterized in that: The furnace diameter of the gasifier is 3.6 meters, and the total height of the three water jackets is 10-20 meters, wherein the height of the first water jacket (6) is 3-7 meters, the height of the second water jacket (7) is 3-10 meters, and the height of the third water jacket (8) is 1-7 meters. The volume of the first water jacket (6) is 1.3-4.5 cubic meters, the volume of the second water jacket (7) is 1.3-3 cubic meters, and the volume of the third water jacket (8) is greater than 1.7 cubic meters.

6. The three-stage pure oxygen anti-condensation gasification furnace using straw as raw material according to claim 5, characterized in that: The height of the second water jacket (7) is 7-10 meters.

7. The three-stage pure oxygen anti-condensation gasification furnace using straw as raw material according to claim 1, characterized in that: The gravity dust removal tank (29) comprises a dust removal tank body (292), a separation cylinder (291) is mounted on the upper end of the dust removal tank body (292), the separation cylinder (291) is connected to the bottom of the gas conduit (9), a third flange (294) is mounted on the lower end of the dust removal tank body (292), the third flange (294) is connected to the dust storage tank (30), and an air outlet pipe (293) is also provided on one side of the dust removal tank body (292), the air outlet pipe (293) is connected to the connecting pipe (31).

8. The three-stage pure oxygen anti-condensation gasification furnace using straw as raw material according to claim 1, characterized in that: The dust storage tank (30) comprises a dust storage tank body (301), a dust exhaust pipe (302) is installed on the outer periphery of the dust storage tank body (301), and a sewage discharge hole (303) is also opened on the lower side of the dust storage tank body (301).

9. A method for producing carbon monoxide and hydrogen using straw as raw material in a three-stage pure oxygen anti-condensation gasifier, characterized in that: The steps include: ① When the straw is harvested, it is directly loaded into vehicles and transported to the collection and processing center without falling to the ground; ② After the straw is sent to the processing center, it is squeezed and dehydrated (juice) within 2-3 days of harvesting to reduce its moisture content to ≦43%; ③After the pressing in step ② is completed, the slag climbs dozens of meters high through the conveyor and falls freely and gradually. The continuous falling makes the slag form a hill from small to large. During the process of forming the hill for dozens of hours, the slag is dried in the sun, and the water evaporates by wind by 8-15%, and the water content of the slag drops to 35-30%; ④ Use two double-roller tooth hole combined extrusion pellet machines as a group to extrude the residue to make pellets. The first machine initially extrude medium φ16-20mm pellets with steam at a temperature of about 30℃, and the micro pellets emit steam to reduce the moisture content of the residue by 3-5% again. The semi-finished pellets made by the first machine enter the second extrusion pellet machine to make the semi-finished product with a moisture content of less than 30% and be extruded into φ16-20mm pellets again, or processed into φ30mm briquettes through rolling; ⑤ Put the dehydrated and extruded pellets or briquettes into the gasifier as raw materials, and high-temperature gasification makes the straw produce CO+H2=72%-82% gas.

10. The method of producing carbon monoxide and hydrogen in a three-stage pure oxygen anti-condensation gasifier using straw as raw material according to claim 9, characterized in that: In the gasification process in step ⑤, the gasifying agent is pure oxygen, oxygen-enriched oxygen or air, and preferably oxygen is mixed with carbon dioxide or part of steam for gasification.

11. The method of producing carbon monoxide and hydrogen in a three-stage pure oxygen anti-condensation gasifier using straw as raw material according to claim 9, characterized in that: In the three-stage pure oxygen anti-condensation gasification furnace using straw as raw material, the thickness of the oxidation layer and the reduction layer is controlled at 5-12m. There is a slag layer at the bottom and a retorting layer at the top to produce a stable gas of CO+H2=72%-82%, which can be used to extract hydrogen or synthesize green chemical products such as methane and methanol.

12. A method for producing carbon monoxide and hydrogen in a three-stage pure oxygen anti-condensation gasifier using straw as raw material according to claim 11, characterized in that: The thickness of the oxidation layer and the reduction layer is controlled at 7-12m.

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