Novel high-temperature heat source waste heat utilization device

Abstract

The utility model provides a novel high-temperature waste heat utilization device which comprises a high-temperature heat source device, the high-temperature heat source device is connected with a biomass pyrolyzing furnace, a pyrolysis gas extraction port in one side of the biomass pyrolyzing furnace is connected with a tar decomposition device, and the tar decomposition device is connected with a methane decomposition device and a carbon dioxide heating device. The carbon dioxide heating device is connected with the lower part of the biomass pyrolyzing furnace; a biomass feeding pipeline is arranged at the top of the biomass pyrolyzing furnace; by means of the efficient heat recovery device, waste heat recovery of the high-temperature heat source device is achieved, and operation is easy; along with the rise of the temperature of each stage, macromolecular substances of the previous stage can be further pyrolyzed to generate micromolecular fuel gas, including CO, H2 and CH4, so that a relatively high CO and H2 generation rate is finally realized, and a raw material is provided for synthesis of green methanol.

Description

Technical Field

[0001] This application relates to the technical field of high-temperature waste heat utilization, and specifically relates to a new type of high-temperature heat source waste heat utilization device. Background Art

[0002] The utilization of high-temperature heat source waste heat mainly transfers the heat carried in the high-temperature heat source to the working medium (such as water, air, etc.) through various heat exchange devices (such as heat exchangers, etc.); then, the heated working medium can be processed in the following several ways according to specific requirements: 1. Directly used for other processes or equipment that require heat to achieve direct utilization of thermal energy; 2. Transfer the heat to other systems, such as driving a steam turbine to generate electricity, thereby converting thermal energy into electrical energy; 3. Store it for subsequent use; in this process, the key lies in effectively recovering and transferring the heat that might otherwise be wasted in the high-temperature heat source and utilizing it in a suitable way to improve the energy utilization efficiency and achieve the purpose of energy conservation and emission reduction.

[0003] For example, coking is an industry with high energy consumption and high pollution. As a key industry for national energy conservation and emission reduction, in the face of the increasingly severe situation of growing external resources, internal energy, and environmental pressures, how to efficiently recover and utilize the heat (coke sensible heat) generated during the coke production process is an important direction for future energy conservation and emission reduction.

[0004] The dry quenching coke waste heat power generation is a process method in which inert gas is used to cool the red coke during the coking process. The cooled coke is discharged from the bottom of the furnace, and the high-temperature inert gas after absorbing heat is introduced into the waste heat boiler and cooled by water. The high-temperature and high-pressure water vapor formed by the water absorbing heat and evaporating is used to drive the steam turbine to generate electricity. This power generation technology belongs to the traditional steam turbine Rankine cycle power generation technology and is the currently commonly used dry quenching coke waste heat utilization technology.

[0005] For example, a dry quenching coke system with the application number CN202223365407.3 discloses a technical solution, including a demineralized water tank and a feed water pipeline connected to the demineralized water tank. A heat exchanger and a coke powder cooling device are connected in series on the feed water pipeline, and the end of the feed water pipeline is connected to the dry quenching coke boiler; the coke powder cooling device includes a first pipeline and a second pipeline. The first pipeline is connected to the dust collector, and the high-temperature coke powder filtered out by the dust collector flows in the first pipeline; the second pipeline is connected to the feed water pipeline, and the demineralized water in the second pipeline is used to exchange heat with the high-temperature coke powder in the second pipeline; in this application, the demineralized water absorbs the heat of the high-temperature flue gas and coke powder in the dry quenching coke system in the heat exchanger and the coke powder cooling device respectively, and finally reaches the dry quenching coke boiler. Under the heating of the dry quenching coke boiler, high-temperature steam is formed and supplied to the gas users. The demineralized water has undergone three heat exchanges, with a higher utilization rate of the heat generated by the dry quenching coke system. The calcium and magnesium ions and other impurities are removed from the demineralized water, and it is not easy to block and corrode the pipeline, improving the service life of the device.

[0006] The working mode of the above-mentioned existing technology belongs to the traditional coke dry quenching waste heat utilization technology. However, there are the following disadvantages in this coke dry quenching waste heat utilization technology: 1. Large water consumption: A large amount of water is consumed to cool the high-temperature inert gas with water. The coke dry quenching technology industry is a high-water-consuming industry, and generally faces the problem of water shortage, and water resource shortage is a common problem; 2. Low heat utilization rate: The waste heat of the cooled inert gas and the high-temperature and high-pressure water vapor after absorbing heat is not fully utilized; 3. Both the heat exchange efficiency and the power generation efficiency are low: Using the steam Rankine cycle technology, the heat exchange of the high-temperature inert gas with water and the power generation efficiency using the water vapor after heat exchange are both low, and it cannot meet the current energy transformation requirements; 4. Large equipment floor space: Due to the large unit area of water vapor, the generator set of the traditional steam power generation system is large in volume, and an oxygen removal water supply pump station needs to be equipped to remove oxygen in the water to avoid equipment oxidation and corrosion, resulting in a large overall volume of the equipment; 5. Large carbon emissions: A large amount of carbon-containing gas is generated during the coking process, resulting in a high carbon emission.

[0007] For example, SO2 reactor power generation means that a large amount of heat will be generated in the SO2 reactor during the sulfur combustion process. By installing an appropriate heat exchange device, such as a heat exchanger, on the SO2 reactor, the waste heat of the reactor is transferred to the working medium (such as water or other fluids), so that the working medium is heated and generates high-temperature and high-pressure steam. These steams can drive the steam turbine to rotate, and the steam turbine drives the generator to rotate, thereby converting thermal energy into electrical energy. In this process, careful design and optimization are required for the collection, transmission, conversion and other links of waste heat to ensure efficient energy conversion and stable power generation process; Similarly, this power generation method belongs to the traditional power generation method and has the disadvantages 1, 2, 3, and 4 in the above-mentioned traditional coke dry quenching waste heat utilization technology.

[0008] In view of the disadvantages and deficiencies of the existing technology in the high-temperature heat source waste heat utilization process, therefore, a new technical solution is needed to solve the above technical problems. Utility Model Content

[0009] The present application provides a novel high-temperature waste heat utilization device, including a high-temperature heat source device. The upper part of the high-temperature heat source device is connected to a biomass pyrolysis furnace through a gas phase pipeline. A slag discharge pipeline is arranged at the bottom of the biomass pyrolysis furnace. The pyrolysis gas extraction port on one side of the biomass pyrolysis furnace is connected to a tar decomposition device. The tar heating device is sequentially connected to a methane decomposition device and a carbon dioxide heating device. The carbon dioxide heating device is connected to the lower part of the biomass pyrolysis furnace; A biomass feed pipeline is arranged at the top of the biomass pyrolysis furnace.

[0010] As a preferred solution, a dryer is arranged on the biomass feed pipeline.

[0011] As a preferred solution, the gas pipeline is connected to the first gas pipeline, the first gas pipeline is connected to the tar decomposition device, the inert gas output end of the tar decomposition device is connected to the second gas pipeline, the second gas pipeline is connected to the dryer, and the output end of the dryer is connected to the high-temperature heat source device or the biomass pyrolysis furnace through a circulation pipeline. A condenser and a blower are arranged on the circulation pipeline.

[0012] As a preferred solution, one side of the biomass pyrolysis furnace is connected to the second gas pipeline through an inert gas extraction pipeline.

[0013] As a preferred solution, the gas pipeline is connected to the third gas pipeline, the third gas pipeline is connected to the carbon dioxide heating device, and the inert gas output end of the carbon dioxide heating device is connected to the second gas pipeline through the fourth gas pipeline.

[0014] As a preferred solution, the carbon dioxide heating device includes a first carbon dioxide heater, a second carbon dioxide heater, and a third carbon dioxide heater connected in sequence; the output end of the methane decomposition device is connected to the first input end of the first carbon dioxide heater, and the first output end of the first carbon dioxide heater is connected to the tar decomposition device; the second input end of the first carbon dioxide heater is connected to a carbon dioxide input pipeline, the second output end of the first carbon dioxide heater is connected to the first input end of the second carbon dioxide heater, and the first output end of the second carbon dioxide heater is connected to the third carbon dioxide heater; the third gas pipeline is connected to the second input end of the second carbon dioxide heater, and the second output end of the second carbon dioxide heater is connected to the second gas pipeline through the fourth gas pipeline.

[0015] As a preferred solution, the tar decomposition device includes a first tar heating device and a second tar heating device connected in sequence. The first output end of the first carbon dioxide heater is connected to the first input end of the second tar heating device, and the first output end of the second tar heating device is connected to the waste heat recovery device.

[0016] As a preferred solution, the biomass pyrolysis furnace includes a furnace body. A biomass feed port is arranged at the top of the furnace body, a slag discharge pipeline is arranged at the bottom of the furnace body, the interior of the furnace body includes a heat exchange section and a carbon dioxide reduction section, at least one carbon dioxide feed port is arranged on the side wall of the carbon dioxide reduction section, and a heater is also arranged on the side wall of the carbon dioxide reduction section.

[0017] A heating coil is arranged on the inner wall of the furnace body in the heat exchange section. The inner side of the heating coil is a biomass reaction channel. An inert gas inlet and an inert gas outlet communicated with the heating coil are arranged on the outer side of the furnace body.

[0018] A distributor is provided at the upper part of the heat exchange section. Heat exchange tubes are provided below the distributor. Biomass is introduced into the interior of the heat exchange tubes. An inert gas channel is formed between the outer walls of the heat exchange tubes. An inert gas inlet and an inert gas outlet are provided on the outer side of the furnace body.

[0019] The inert gas channel is divided into a plurality of inert gas channels by a partition layer. Each inert gas channel corresponds to an inert gas inlet and an inert gas outlet.

[0020] As a preferred solution, at a position of the heat exchange section close to the carbon dioxide reduction section, a carbon addition port is provided on the outer wall of the heat exchange section.

[0021] As a preferred solution, a plurality of biomass pyrolysis furnaces are connected in parallel for the biomass pyrolysis furnace.

[0022] As a preferred solution, a coke dry quenching furnace is used for the high-temperature heat source device. A red coke inlet pipeline is provided at the top of the coke dry quenching furnace. A cold coke extraction pipeline is provided at the bottom of the coke dry quenching furnace. A gas-phase pipeline and an inert gas pipeline are respectively connected to the top of the coke dry quenching furnace.

[0023] As a preferred solution, a SO2 reaction tank is used for the high-temperature heat source device. A SO2 outlet gas pipeline is connected to the top of the SO2 reaction tank. A heat exchanger is provided on the SO2 outlet gas pipeline for heat exchange with the introduced inert gas. The inert gas heated and raised in temperature after heat exchange enters the gas-phase pipeline. The heat exchanger is also connected to the gas-phase pipeline. An oxygen inlet pipeline and a raw material feeding pipeline are respectively connected to the SO2 reaction tank. A extraction pipeline is provided at the bottom of the SO2 reaction tank.

[0024] The present application has the following advantages:

[0025] 1. In the present application, three-stage heating pyrolysis is carried out through a biomass pyrolysis furnace, a tar decomposition device, and a methane decomposition device. As the temperature increases at each stage, the high-molecular substances in the previous stage will be further pyrolyzed to generate small-molecule fuel gases, including CO, H2, and CH4, finally achieving a relatively high production rate of CO and H2, providing raw materials for the synthesis of green methanol. For the tar decomposition device, high-temperature inert gas heating is used to promote the cracking of tar. An auxiliary electric heating device is introduced in the tar decomposition device and the methane decomposition device to further increase the temperature of the pyrolysis gas, optimize the cracking reaction conditions, and at the same time avoid the risk of tar solidification blocking the equipment.

[0026] 2. The inert gas can be recycled and returned to the dryer for continuous heat exchange to provide the heat required for the biomass to remove free water. The waste heat is utilized, achieving complete self-sufficiency in the thermal energy required by the dryer without the need for external heat sources, greatly reducing the operating cost. The cooled inert gas passes through the dryer to remove the free water from the water-containing biomass obtained from the farmland, subverting the mode of direct combustion power generation and single output of agricultural and forestry waste, promoting the advanced biomass pyrolysis technology, optimizing the pyrolysis process to improve the quality and added value of pyrolysis products, and mobilizing the enthusiasm of the biomass pyrolysis industry.

[0027] 3. By more efficiently recovering heat, this application is conducive to the recovery of waste heat energy from high-temperature heat source devices, improving the utilization rate of waste heat, with high separation efficiency, large processing capacity, and convenient production operation. Using the high-temperature waste heat for biomass pyrolysis can not only improve the conversion efficiency of biomass but also reduce the dependence on traditional energy sources and lower production costs. This combination helps to achieve energy diversification and cleanization, conforming to the global energy transformation and environmental protection trends.

[0028] 4. This application has a simple structure, convenient operation, is safe and reliable, and can achieve energy conservation, emission reduction, pollution-free, and optimal resource comprehensive utilization.

[0029] 5. The biomass pyrolysis furnace is simple and efficient, has a high level of automation, can continuously feed biomass, and work stably for a long time. The operation of the production line is not affected by external environmental factors such as weather. In terms of safety and environmental protection, the entire pyrolysis process is completed in a closed and evacuated equipment and pipeline, avoiding the problems of dust and VOC leakage and not generating secondary pollution. Under the premise of safety and environmental protection, it can achieve long-term full-load uninterrupted continuous and stable operation. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] Figure 1 is the process flow diagram of the high-temperature heat source device of this application using a coke dry quenching furnace;

[0031] Figure 2 is the process flow diagram of the high-temperature heat source device of this application using a SO2 reaction tank;

[0032] Figure 3 is the structural schematic diagram of the biomass pyrolysis furnace of this application;

[0033] 1, Coke dry quenching furnace; 2, SO2 reaction tank; 3, Red coke inlet pipeline; 4, Inert gas pipeline; 5, Cold coke extraction pipeline; 6, Biomass pyrolysis furnace; 7, Oxygen inlet pipeline; 8, Raw material feed pipeline; 9, SO2 outlet pipeline; 10, Heat exchanger; 11, Gas phase pipeline; 12, Slag discharge pipeline; 13, Pyrolysis gas extraction outlet; 14, Methane decomposition device; 15, Biomass feed pipeline; 16, Dryer; 17, Feed pump; 18, Gas phase pipeline one; 19, Gas phase pipeline two; 20, Circulation pipeline; 21, Condenser; 22, Blower; 23, Inert gas extraction pipeline; 24, Gas phase pipeline three; 25, Gas phase pipeline four; 26, Carbon dioxide heater one; 27, Carbon dioxide heater two; 28, Carbon dioxide heater three; 29, Carbon dioxide heater one input end one; 30, Carbon dioxide heater one output end one; 31, Tar heating device one; 32, Tar heating device two; 33, Tar heating device two input end one; 34, Tar heating device two output end one; 35, Waste heat recovery device; 36, Carbon dioxide heater one input end two; 37, Carbon dioxide input pipeline; 38, Carbon dioxide heater one output end two; 39, Carbon dioxide heater two input end one; 40, Carbon dioxide heater two output end one; 41, Carbon dioxide heater two input end two; 42, Carbon dioxide heater two output end two; 43, Furnace body; 44, Biomass feed inlet; 45, Carbon dioxide reduction section; 46, Heat exchange pipeline; 47, Biomass reaction channel; 48, Carbon dioxide feed inlet; 49, Electric heater; 50, Carbon supplement port; 51, Slag discharge pool; 52, Heating coil; 53, Distributor; 54, Heat exchange tube; 55, Inert gas channel; 56, Inert gas inlet; 57, Inert gas outlet; 58, Interlayer. Specific embodiments

[0034] The following is a detailed description of the specific embodiments of the present utility model in conjunction with the attached Figures 1-3 The specific embodiments of the present utility model will be described in detail. It should be noted that the specific embodiments described herein are only for explaining and understanding the present utility model, and are not used to limit the present utility model.

[0035] Example 1:

[0036] This embodiment provides a new type of high-temperature waste heat utilization device, including a high-temperature heat source device. The high-temperature heat source device adopts the coke dry quenching furnace 1, SO2 reaction tank 2, etc. in the prior art, such as Figure 1As shown in the figure, when the coke dry quenching furnace 1 is adopted, a red coke inlet pipe 3 is arranged at the top of the coke dry quenching furnace 1, and the red coke is put into the coke dry quenching furnace 1 through the red coke inlet pipe 3. Since inert gas usually does not react with carbon, in this embodiment, an inert gas pipeline 4 is arranged on one side of the coke dry quenching furnace 1 as an example; the inert gas pipeline 4 introduces inert gas to cool the red coke, and the inert gas is one of N2, CO, and Ar. In this embodiment, nitrogen is used as the inert gas; a cold coke extraction pipe 5 is arranged at the bottom of the coke dry quenching furnace 1, and the cooled coke after cooling is discharged from the cold coke extraction pipe 5 at the bottom of the coke dry quenching furnace 1. The high-temperature inert gas after absorbing heat is extracted from the top of the coke dry quenching furnace 1, part of which enters the biomass pyrolysis furnace 6, and part is directly used for traditional power generation; as Figure 2 As shown in the figure, when the SO2 reaction tank 2 is adopted, in the application scenario of the process of producing sulfuric acid from sulfur, there is also a high-temperature heat source that can be used to decompose biomass. The SO2 reaction tank 2 is used to realize the combustion of sulfur, and sulfur is burned in the combustion furnace to generate sulfur dioxide; two inlets are arranged on the SO2 reaction tank 2, which are respectively used to introduce sulfur-containing substances and oxygen, and the inlets are respectively an oxygen inlet pipeline 7 and a raw material feed pipeline 8. The oxygen inlet pipeline 7 is used to introduce oxygen, and the raw material feed pipeline 8 is used to introduce sulfur; an SO2 outlet pipeline 9 is also arranged on the SO2 reaction tank 2, which is used to discharge the reacted SO2 gas; in this embodiment, a heat exchanger 10 is adopted to heat up the inert gas. Specifically: a heat exchanger 10 is arranged on the SO2 outlet pipeline 9. The second input port of the heat exchanger is connected to the circulation pipeline 20, and the second output port of the heat exchanger is connected to the gas phase pipeline 11. A mixer is arranged on the circulation pipeline 20, and nitrogen enters the heat exchanger 10 through the mixer. Nitrogen exchanges heat with the extracted SO2 gas, and the heat of the sulfur dioxide gas is transferred to nitrogen through the heat exchange surface of the heat exchanger 10 to increase the temperature of nitrogen. The cooled sulfur dioxide gas is extracted for subsequent treatment, and the nitrogen after absorbing heat is introduced into the biomass pyrolysis furnace 6 to carry out an exothermic pyrolysis reaction on biomass particles; the high-temperature heat source device 1 is connected to the biomass pyrolysis furnace 6 through the gas phase pipeline 11. The biomass pyrolysis furnace 6 has simple equipment and high efficiency, and has a high level of automation. It can continuously feed biomass and work stably for a long time; a slag discharge pipe 12 is arranged at the bottom of the biomass pyrolysis furnace 6, and the generated biomass charcoal is extracted through the slag discharge pipe 12. The pyrolysis gas extraction port 13 on one side of the biomass pyrolysis furnace 6 is sequentially connected to a pyrolytic oil decomposition device, a methane decomposition device 14, and a carbon dioxide heating device. The carbon dioxide heating device is connected to the lower part of the biomass pyrolysis furnace 6. A biomass feed pipeline 15 is arranged at the top of the biomass pyrolysis furnace 6; in addition, the recycled CO2 is introduced into the carbon dioxide heating device, and is heat-exchanged and heated with a small amount of unreacted completely CH4, CO2, and the decomposed CO and H2. The heated CO2 enters the biomass pyrolysis furnace 6 and reacts with the carbon in the biomass pyrolysis furnace 6 to generate CO;

[0037] The tar decomposition device decomposes tar by heating, and the tar is decomposed into CH4 and other components. The purpose of the tar decomposition device is to decompose tar. The CH4 obtained by the decomposition of the tar decomposition device enters the methane decomposition device 14 for decomposition. The methane decomposition device 14 adopts an auxiliary electric heating device to further increase the temperature of the pyrolysis gas to about 1000 °C. CH4 + CO2 = 2CO + H2. The purpose is to convert methane gas and carbon dioxide into CO and H2 to increase the content of CO and H2. The pyrolysis gas enters the carbon dioxide heating device to heat CO2 and recover waste heat. The working principle of this embodiment is as follows: Biomass is introduced into the biomass pyrolysis furnace 6, and the high-temperature heat source inert gas generated by the high-temperature heat source device enters the biomass pyrolysis furnace 6 to carry out endothermic pyrolysis reaction on the biomass. The carbon generated by pyrolysis reacts with the supplemented CO2 to be reduced to CO, which also increases the output of CO and reduces the emission of CO2. The remaining slag is taken out through the slag discharge pipeline 12. The high-temperature and high-pressure tar, carbon monoxide, hydrogen, carbon dioxide, methane, etc. formed by the endothermic pyrolysis of biomass are sequentially processed through the tar decomposition device and the methane decomposition device 14. The CO2 recovered in the carbon dioxide heating device exchanges heat with the pyrolysis gas taken out from the methane decomposition device 14 to increase the temperature. The heated CO2 enters the biomass pyrolysis furnace 6 for carbon dioxide reduction, thereby reducing the carbon dioxide emission, alleviating the greenhouse effect, and mitigating the global climate change problem.

[0038] Embodiment 2:

[0039] In this embodiment, the inert gas generated by the high-temperature heat source device can be recycled. The cooled inert gas returns to the dryer 16, and the heat exchange is used to provide the heat for the biomass to remove the free water; the waste heat is utilized, realizing that the heat energy required by the dryer 16 is completely self-sufficient without an external heat source, greatly reducing the operating cost; it has the effect of improving the heat recovery utilization rate and the heat exchange efficiency.

[0040] Specifically, a dryer 16 and a feed pump 17 are provided on the biomass feed pipeline 15. The gas pipeline 11 is connected to the gas pipeline 18. The gas pipeline 18 is connected to the tar decomposition device. The inert gas output end of the tar decomposition device is connected to the gas pipeline 19. The gas pipeline 19 is connected to the dryer 16. The output end of the dryer 16 is connected to the high-temperature heat source device or the biomass pyrolysis furnace 6 through the circulation pipeline 20. A condenser 21 and a blower 22 are provided on the circulation pipeline 20. When the high-temperature heat source device adopts a coke dry quenching furnace 1, the circulation pipeline 20 is connected to the high-temperature heat source device. When the high-temperature heat source device adopts a SO2 reaction tank 2, the circulation pipeline 20 passes through the heat exchanger 10 and the gas pipeline 11 and is connected to the biomass pyrolysis furnace 6.

[0041] The heat source of the above tar decomposition device introduces a stream of high-temperature nitrogen gas at 900 °C extracted from the top of the high-temperature heat source device. The inert gas after heat exchange with the tar decomposition device enters the dryer 16 to continue removing free water from the biomass in the dryer 16, and then returns to the high-temperature heat source device or the biomass pyrolysis furnace 6 for recycling after being cooled by the condenser 21, realizing the recycling of the inert gas.

[0042] Preferably, one side of the biomass pyrolysis furnace 6 is connected to the second gas pipeline 19 through the inert gas extraction pipeline 23. The inert gas after heating the biomass in the biomass pyrolysis furnace 6 is cooled and then extracted through the inert gas extraction pipeline 23 and mixed with the inert gas in the second gas pipeline 19; More preferably, the gas pipeline 11 is connected to the third gas pipeline 24, the third gas pipeline 24 is connected to the carbon dioxide heating device, the output end of the carbon dioxide heating device is connected to the second gas pipeline 19 through the fourth gas pipeline 25, and the inert gas extracted from the top of the high-temperature heat source device provides the required heat for the carbon dioxide heating device. The cooled inert gas is mixed with the inert gas in the second gas pipeline 19.

[0043] As can be seen from the above solution, the inert gas extracted from the top of the high-temperature heat source device in this application is divided into three parts. The first part directly enters the biomass pyrolysis furnace 6 to exchange heat with the biomass in the biomass pyrolysis furnace 6. The cooled inert gas enters the second gas pipeline 19 through the inert gas extraction pipeline 23; The second part of the inert gas enters the tar decomposition device for heat exchange, and the inert gas after heat exchange and cooling enters the second gas pipeline 19; The third part of the inert gas enters the carbon dioxide heating device for heat exchange, and the cooled inert gas enters the second gas pipeline 19; The three parts of the inert gas are cooled and mixed in the second gas pipeline 19. The mixed inert gas enters the dryer 16 for further heat exchange to provide the heat required for the biomass to remove free water. The waste heat is fully utilized, realizing the complete self-sufficiency of the heat energy required for drying without external heat sources, greatly reducing the operating cost, and having the effects of improving the heat recovery utilization rate and the heat exchange efficiency.

[0044] When the high-temperature heat source device uses the coke dry quenching furnace 1, the inert gas extracted from the top of the coke dry quenching furnace 1 is divided into four parts. In addition to the above three parts, there is also a part directly used for traditional power generation.

[0045] Example Three:

[0046] This embodiment will describe the carbon dioxide heating device. Specifically:

[0047] The carbon dioxide heating device includes a first carbon dioxide heater 26, a second carbon dioxide heater 27, and a third carbon dioxide heater 28 that are connected in sequence. The output end of the methane decomposition device 14 is connected to the first input end 29 of the first carbon dioxide heater, and the first output end 30 of the first carbon dioxide heater is connected to the tar decomposition device. A small amount of CH4, CO2 that are not completely decomposed in the methane decomposition device 14, as well as the decomposed CO and H2 enter the first carbon dioxide heater 26 to provide heat for the recycled CO2. After heat exchange, CH4, CO2, CO, and H2 enter the tar decomposition device to provide heat for the decomposition operation of this device. After cooling, CH4, CO2, CO, and H2 continue to enter equipment such as boilers for waste heat recovery. After the heat of the recovered heat is cooled, CO and H2 can be used as carbon monoxide hydrogenation to produce green methanol in the follow-up. More specifically, the tar decomposition device includes a first tar heating device 31 and a second tar heating device 32 that are connected in sequence. The first output end 30 of the first carbon dioxide heater is connected to the first input end 33 of the second tar heating device, and the first output end 34 of the second tar heating device is connected to the waste heat recovery device 35. The waste heat recovery device 35 uses equipment such as boilers.

[0048] A second input end 36 of the first carbon dioxide heater is connected to a carbon dioxide input pipeline 37. The carbon dioxide input pipeline 37 is used to introduce the recycled carbon dioxide. The second output end 38 of the first carbon dioxide heater is connected to the first input end 39 of the second carbon dioxide heater, and the first output end 40 of the second carbon dioxide heater is connected to the input end of the third carbon dioxide heater 28.

[0049] After the recycled carbon dioxide is heated by heat exchange with the pyrolysis gas in the first carbon dioxide heater 26, it enters the second carbon dioxide heater 27 for further heating. A part of the high-temperature nitrogen gas extracted from the top of the high-temperature heat source device enters the second carbon dioxide heater 27 to provide the required heat for the second carbon dioxide heater 27. After heat exchange and cooling in the second carbon dioxide heater 27, it enters the dryer 16 to continue to provide the required heat for the dryer 16. The carbon dioxide heated by the second carbon dioxide heater 27 continues to enter the third carbon dioxide heater 28, and the carbon dioxide heated by the third carbon dioxide heater 28 enters the high-temperature heat source device for a reduction reaction.

[0050] The above-mentioned third gas pipeline 24 is connected to the second input end 41 of the second carbon dioxide heater, and the second output end 42 of the second carbon dioxide heater is connected to the second gas pipeline 19 through the fourth gas pipeline 25. The inert gas extracted from the top of the high-temperature heat source device enters the second carbon dioxide heater 27 to provide heat for the second carbon dioxide heater 27. After cooling, the inert gas enters the second gas pipeline 19 and is mixed with the rest of the cooled inert gas. After mixing, it provides the required heat for the dryer 16.

[0051] Example 4:

[0052] This embodiment describes the biomass pyrolysis furnace 6, specifically:

[0053] The biomass pyrolysis furnace 6 includes a furnace body 43. A biomass feed inlet 44 is provided at the top of the furnace body 43, and the biomass feed inlet 44 is connected to a biomass feed pipeline 15. A pyrolysis gas extraction outlet 13 is provided on one side of the furnace body 43. A slag discharge pipeline 12 is provided at the bottom of the furnace body 43. The interior of the furnace body 43 includes a heat exchange section and a carbon dioxide reduction section 45. At least one carbon dioxide feed inlet 48 is provided on the side wall of the carbon dioxide reduction section 45. The carbon dioxide heated by the carbon dioxide heater III 28 enters the carbon dioxide reduction section 45 through the carbon dioxide feed inlet 48. An electric heater 49 is also provided on the side wall of the carbon dioxide reduction section 45. At a position of the heat exchange section close to the carbon dioxide reduction section 45, a carbon addition port 50 is provided on the outer wall of the heat exchange section to timely supplement the carbon source. The carbon in the bottom of the tower reacts with CO2, generating the required CO and consuming CO2. The carbon source for supplementation is not limited to biomass carbon, and other types of external carbon sources can also be used.

[0054] As Figure 1 、 Figure 2 shown, heating coils 52 are provided on the inner wall of the furnace body 43 of the heat exchange section. The inner side of the heating coils 52 is a biomass reaction channel 47. An inert gas inlet 56 and an inert gas outlet 57 communicating with the heating coils 52 are provided on the outer side of the furnace body 43. The inert gas outlet 57 is connected to an inert gas extraction pipeline 23. Biomass enters through the biomass reaction channel 47, and the inert gas enters the heating coils 52 through the inlet. The inert gas heats the biomass to cause pyrolysis. This structure is suitable for heating biomass in a small-diameter reactor.

[0055] In addition, as Figure 3 shown, the heat exchange section can also adopt another form. A distributor 53 is provided in the upper part of the heat exchange section. Heat exchange tubes 54 are provided below the distributor 53. Biomass is introduced into the interior of the heat exchange tubes 54. An inert gas channel 55 is provided between the outer walls of the heat exchange tubes 54. An inert gas inlet 56 and an inert gas outlet 57 are provided on the outer side of the furnace body 43. The inert gas outlet 57 is connected to an inert gas extraction pipeline 23. Biomass enters the heat exchange tubes 54 through the distributor 53. Inert gas is introduced through the inert gas inlet 56. The high-temperature inert gas heats the biomass in the heat exchange tubes 54 to cause pyrolysis. This structure is suitable for heating biomass in a large-diameter reactor. The above two forms of heat exchange sections both adopt the form of external heating.

[0056] Preferably, the inert gas channel 55 is divided into a plurality of inert gas channels by a partition 58, each of which corresponds to an inert gas inlet 56 and an inert gas outlet 57, and the inert gas outlet 57 is located above the inert gas inlet 56; the provision of the partition 58 enables the inert gas to be heated in sections and facilitates the control of the temperature of each section.

[0057] Granular or block solid reactants or catalysts are continuously added to the top of the biomass pyrolysis furnace 6. As the reaction proceeds, the solid material gradually moves downward and is finally discharged continuously from the bottom. The high-temperature inert gas flows from bottom to top (countercurrent) to carry out heat transfer pyrolysis reaction; the electric heater 49 arranged on the side wall of the carbon dioxide reduction section 45 can ensure that the temperature of the biochar reaches above 900°C, and at the same time, 1000°C carbon dioxide is introduced through the carbon dioxide feed port 48 to increase the ratio of biochar converted into carbon monoxide.

[0058] Preferably, the carbon dioxide reduction section 45 is provided with a stirring device (not shown in the figure). By providing the stirring device, the char and CO2 can react fully while avoiding the problem of clogging of the slag discharge pipe 12.

[0059] Embodiment five:

[0060] The high temperature heat source device in this embodiment adopts a dry quenching furnace 1, which provides a specific application occasion:

[0061] In the coking process, 130℃ inert gas is used to cool the 1100℃ red coke, and the 400℃ cooled coke is discharged from the bottom of the dry quenching furnace 1. The 900℃ high-temperature nitrogen after absorbing heat is directly used for traditional power generation, and part of it enters the biomass pyrolysis furnace 6 through the gas phase pipeline 11; the straw particles are passed through the dryer 16 to remove 15% of the free water and then sent to the biomass pyrolysis furnace 6 through the biomass feed pipeline 15; the 900℃ high-temperature nitrogen is used to externally heat and decompose the straw particles, and the straw particles are heated from top to bottom in the biomass pyrolysis furnace. While moving downward, it is thermally decomposed at different temperatures to produce pyrolysis gas, tar and charcoal. The charcoal material moves downward along the biomass pyrolysis furnace. The recovered CO2 is transported to the carbon dioxide reduction section 45 at the bottom of the biomass pyrolysis furnace 6 after three-stage heating, and undergoes a reduction reaction with the charcoal. Specifically, the reduction section is heated to 1000°C to undergo a reduction reaction to obtain CO and residual ash. CO is extracted through the pyrolysis gas extraction port 13, and the residual ash is extracted through the slag discharge pipe 12 and enters the slag discharge pool 51 for subsequent treatment;

[0062] The tar and pyrolysis gas released from the top of the biomass pyrolysis furnace 6 enter the tar decomposition device. After being heated by nitrogen gas at 900°C, the tar cracks into small-molecule pyrolysis gas, which enters the methane decomposition device 14 and is decomposed again after being heated to 1000°C. The pyrolysis gas exchanges heat with the CO2 at 120°C recovered from the outside at the outlet, and then enters the tar decomposition device for heat exchange. After heat exchange, subsequent treatments such as heat recovery are carried out; the recovered CO2 is heated to 800°C by the carbon dioxide heater 1 26 and enters the carbon dioxide heater 2 27. The carbon dioxide heater 2 27 heats it to 850°C and enters the carbon dioxide heater 3 28. The nitrogen gas at 900°C enters the carbon dioxide heater 2 27. After heat exchange, it enters the gas pipeline 2 19, and the temperature of the mixed nitrogen gas is 600°C; the carbon dioxide heater 3 28 heats the carbon dioxide to 950°C and enters the carbon dioxide reduction section 45 through the carbon dioxide feed port 48, reacts with the carbon at the bottom of the biomass pyrolysis furnace to generate CO, and the ash is discharged into the slag pool through the slag discharge pipeline 12. The CO is extracted through the pyrolysis gas extraction port 13, and tar decomposition, methane decomposition, and carbon dioxide heating are carried out in sequence;

[0063] The nitrogen gas that has exchanged heat with the straw particles in the biomass pyrolysis furnace 6, the nitrogen gas that has cooled down after exchanging heat with the tar decomposition device, and the nitrogen gas that has cooled down to below 500°C after exchanging heat with the carbon dioxide heating device jointly pass through the dryer 16, providing the heat required for the dryer 16. The dryer 16 is used to remove the free water from the water-containing biomass obtained from the farmland. The nitrogen gas that has cooled down to 200°C after exchanging heat with the dryer 16 is further cooled to 130°C by the condenser 21 and then returns to the dry quenching furnace 1 for recycling through the blower 22.

[0064] Chromatographic analysis is carried out on the pyrolysis products. The component composition range of the pyrolysis products is as follows: CO, 50 - 65%; H2, 15 - 30%; CH4, 10 - 30%; CO2, 15 - 20%; CnHm, 1 - 6%; the biomass carbon yield is about 10 - 25%; the composition of the pyrolysis products is related to factors such as pyrolysis temperature, heating rate, and residence time, as

[0065] shown in Table 1 Process Conditions of the Biomass Pyrolysis Process:

[0066]

[0067] This application adopts three-stage heating, gradually heating and pyrolyzing different pyrolysis substances step by step. The main components of the final pyrolysis gas are H2, CO, CO2, and CH4. While reducing the generation of other organic substances, it also avoids the risk of blockage of equipment by macromolecular substances such as tar. This process is simple to operate and stable in operation.

[0068] The raw materials of the above-mentioned biomass pyrolysis furnace 6 can also use wood chips with pyrolysis particles smaller than 100 mesh, etc.

[0069] This embodiment reduces carbon dioxide emissions by more efficiently recovering the sensible heat of red coke, achieving a carbon sequestration effect, facilitating the waste heat recovery of the coke dry quenching furnace 1, and facilitating production operations.

[0070] This application has the following advantages:

[0071] 1. By more efficiently recovering heat, this application is conducive to the waste heat recovery of high-temperature heat source devices and facilitates production operations. Using the high-temperature waste heat for biomass pyrolysis can not only improve the conversion efficiency of biomass but also reduce the dependence on traditional energy sources and lower production costs. This combination helps to achieve the diversification and cleanization of energy, meeting the global energy transformation and environmental protection trends.

[0072] 2. By recovering the waste heat of high-temperature heat source devices, this application reduces carbon dioxide emissions and achieves a carbon sequestration effect. It can achieve energy conservation, emission reduction, pollution-free, and optimal resource comprehensive utilization. Moreover, with internal heat integration in the overall process, the utilization rate of the sensible heat of coke is improved, the separation efficiency is high, and the processing capacity is large.

[0073] 3. The biomass pyrolysis furnace is simple and efficient, with a high level of automation. It can continuously feed biomass and operate stably for a long time. The operation of the production line is not affected by external environmental factors such as weather. In terms of safety and environmental protection, the entire pyrolysis process is completed in a closed and evacuated equipment and pipeline, avoiding problems such as dust and VOC leakage and not generating secondary pollution. Under the premise of safety and environmental protection, it can achieve long-term full-load uninterrupted continuous and stable operation.

[0074] 4. The inert gas can be recycled and returned to the dryer for continuous heat exchange to provide the heat required for the biomass to remove free water. The waste heat is utilized, achieving complete self-sufficiency of the heat energy required by the dryer without external heat sources, greatly reducing the operating cost. The cooled inert gas passes through the dryer to remove the free water from the water-containing biomass obtained from the farmland, subverting the direct combustion power generation and single-output mode of agricultural and forestry waste, promoting advanced biomass pyrolysis technology, optimizing the pyrolysis process to improve the quality and added value of pyrolysis products, and mobilizing the enthusiasm of the biomass pyrolysis industry. Moreover, the cascade utilization of inert gas at different temperatures is planned to maximize the effect of high-temperature heat sources in different process.

[0075] 5. This application conducts three-stage heating pyrolysis through a biomass pyrolysis furnace, a tar decomposition device, and a methane decomposition device. As the temperature increases in each stage, the high-molecular substances in the previous stage will further pyrolyze to produce small-molecule fuel gases, including CO, H2, and CH4, ultimately achieving a high production rate of CO and H2, providing raw materials for the synthesis of green methanol. The tar decomposition device promotes the cracking of tar by heating with high-temperature inert gas. An auxiliary electric heating device is introduced into the tar decomposition device and the methane decomposition device to further increase the temperature of the pyrolysis gas, optimize the cracking reaction conditions, and at the same time avoid the risk of tar solidification blocking the equipment.

[0076] 6. At the bottom of the bio-pyrolysis furnace, a CO2 reduction section is set up to create a high-temperature reducing atmosphere using the produced carbon, so that the supplemented CO2 can be effectively reduced. Carbon is timely supplemented through the carbon supplement port to generate more CO.

[0077] 7. This application does not use water vapor and O2 as gasifying agents, reducing the waste of bio-carbon sources and steam consumption, and lowering production costs.

[0078] In summary, this application uses biomass pyrolysis to solve the technical problems existing in current high-temperature waste heat utilization technologies, such as large water consumption, low heat utilization rate, low heat exchange efficiency and power generation efficiency, and large equipment floor space. It realizes high-temperature waste heat utilization and the "reduction, harmlessness, greening, resource utilization, reuse, and recycling" of biomass, enhances the profitability of biomass pyrolysis, and boosts the technological upgrading of the biomass industry.

[0079] The devices, connection relationships, etc. not specifically described above all belong to the prior art, and the present utility model will not elaborate on them specifically here.

[0080] The preferred embodiments of this application have been described in detail above with reference to the drawings. However, this application is not limited to the specific details in the above embodiments. Within the technical concept of this application, various simple modifications can be made to the technical solutions of this application, and these simple modifications all fall within the protection scope of this application.

[0081] In addition, it should be noted that, in the case of no contradiction, the various specific technical features described in the above specific embodiments can be combined in any suitable way. To avoid unnecessary repetition, the various possible combination methods of this application will not be described separately.

[0082] Furthermore, any combination can be made among the various different embodiments of this application as long as it does not violate the idea of this application, and it should also be regarded as the content disclosed in this application.

Claims

1. A new type of high-temperature waste heat utilization device, including a high-temperature heat source device, characterized in that, The upper part of the high-temperature heat source device is connected to the biomass pyrolysis furnace (6) through a gas-phase pipeline (11). A slag discharge pipeline (12) is provided at the bottom of the biomass pyrolysis furnace (6). The pyrolysis gas extraction port (13) on one side of the biomass pyrolysis furnace (6) is connected to a tar decomposition device. The tar decomposition device is sequentially connected to a methane decomposition device (14) and a carbon dioxide heating device. The carbon dioxide heating device is connected to the lower part of the biomass pyrolysis furnace (6). A biomass feed pipeline (15) is provided at the top of the biomass pyrolysis furnace (6).

2. A novel high-temperature waste heat utilization device according to claim 1, characterized in that, A dryer (16) is provided on the biomass feed pipeline (15).

3. A novel high-temperature waste heat utilization device according to claim 2, characterized in that, The gas-phase pipeline (11) is connected to a first gas-phase pipeline (18). The first gas-phase pipeline (18) is connected to a tar decomposition device. The inert gas output end of the tar decomposition device is connected to a second gas-phase pipeline (19). The second gas-phase pipeline (19) is connected to the dryer (16). The output end of the dryer (16) is connected to the high-temperature heat source device or the biomass pyrolysis furnace (6) through a circulation pipeline (20). A condenser (21) and a blower (22) are provided on the circulation pipeline (20).

4. A novel high-temperature waste heat utilization device according to claim 3, characterized in that, One side of the biomass pyrolysis furnace (6) is connected to the second gas-phase pipeline (19) through an inert gas extraction pipeline (23).

5. A novel high-temperature waste heat utilization device according to claim 3, characterized in that, The gas-phase pipeline (11) is connected to a third gas-phase pipeline (24). The third gas-phase pipeline (24) is connected to a carbon dioxide heating device. The inert gas output end of the carbon dioxide heating device is connected to the second gas-phase pipeline (19) through a fourth gas-phase pipeline (25).

6. A novel high-temperature waste heat utilization device according to claim 5, characterized in that, The carbon dioxide heating device includes a first carbon dioxide heater (26), a second carbon dioxide heater (27), and a third carbon dioxide heater (28) connected in sequence. The output end of the methane decomposition device (14) is connected to a first input end of the first carbon dioxide heater (29). The first output end of the first carbon dioxide heater (30) is connected to the tar decomposition device. A second input end of the first carbon dioxide heater (36) is connected to a carbon dioxide input pipeline (37). The second output end of the first carbon dioxide heater (38) is connected to a first input end of the second carbon dioxide heater (39). The first output end of the second carbon dioxide heater (40) is connected to the third carbon dioxide heater (28). The third gas-phase pipeline (24) is connected to a second input end of the second carbon dioxide heater (41). The second output end of the second carbon dioxide heater (42) is connected to the second gas-phase pipeline (19) through the fourth gas-phase pipeline (25).

7. A novel high-temperature waste heat utilization device according to claim 6, characterized in that, The tar decomposition device includes a first tar heating device (31) and a second tar heating device (32) connected in sequence. The first output end of the first carbon dioxide heater (30) is connected to a first input end of the second tar heating device (33). The first output end of the second tar heating device (34) is connected to a waste heat recovery device (35).

8. A novel high-temperature waste heat utilization device according to claim 1, characterized in that, The biomass pyrolysis furnace (6) includes a furnace body (43). A biomass feed inlet (44) is provided at the top of the furnace body (43), and a slag discharge pipeline (12) is provided at the bottom of the furnace body (43). The interior of the furnace body (43) includes a heat exchange section and a carbon dioxide reduction section (45). At least one carbon dioxide feed inlet (48) is provided on the side wall of the carbon dioxide reduction section (45), and an electric heater (49) is also provided on the side wall of the carbon dioxide reduction section (45).

9. A novel high-temperature waste heat utilization device according to claim 1, characterized in that, The high-temperature heat source device uses a coke dry quenching furnace (1). A red coke inlet pipeline (3) is provided at the top of the coke dry quenching furnace (1), and a cold coke extraction pipeline (5) is provided at the bottom of the coke dry quenching furnace (1); the top of the coke dry quenching furnace (1) is respectively connected to a gas-phase pipeline (11) and an inert gas pipeline (4).

10. A novel high-temperature waste heat utilization device according to claim 1, characterized in that, The high-temperature heat source device uses a SO2 reaction tank (2). A SO2 outlet pipeline (9) is provided at the top of the SO2 reaction tank (2). A heat exchanger (10) is provided on the SO2 outlet pipeline (9), and the heat exchanger (10) is also connected to the gas-phase pipeline (11); the SO2 reaction tank (2) is respectively connected to an oxygen inlet pipeline (7) and a raw material feed pipeline (9), and a extraction pipeline is provided at the bottom of the SO2 reaction tank.

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