Biomass pressurizing baking equipment

Abstract

The utility model discloses biomass pressurizing and baking equipment which comprises a pressurizing and baking reaction kettle used for drying and pressurizing and baking biomass raw materials, a steam generator used for preparing steam, and a desalting water tank used for providing raw material water for the steam generator and providing cooling water for a temperature and pressure reducer, the first heat exchanger is used for treating waste steam generated in the drying stage, the temperature and pressure reducer and the second heat exchanger are used for treating pressurized high-temperature steam generated in the baking stage, the third heat exchanger, the buffer tank and the combustible gas burner are used for treating pyrolysis gas generated in the baking stage, and the circulating water tank is used for providing cooling water for the three heat exchangers. After the equipment disclosed by the utility model is used for carrying out pressurized baking pretreatment on the biomass, the treatment difficulty and the treatment cost of the biomass are reduced, the generation of gasified tar is reduced in the treatment process, and clean, efficient and low-carbon conversion and utilization of biomass raw materials are realized.

Description

Technical Field

[0001] The utility model belongs to the technical field of biomass processing, relates to biomass processing equipment, and specifically relates to biomass pressure baking equipment. Background Art

[0002] Biomass energy is an ideal renewable energy source with the characteristics of being green, low-carbon and clean. After resource processing, it can be widely used in many fields such as life, industry, transportation, agriculture, etc. through power generation, heating and gas supply. It is a zero-carbon fuel that cannot be replaced by other renewable energy sources. In the current and future low-carbon energy structure, biomass energy will play a major role due to its unique characteristics. If combined with bioenergy and carbon capture and storage technology, biomass energy will create negative carbon emissions and make a huge contribution to carbon neutrality in various fields.

[0003] However, biomass is difficult to handle and has high processing costs due to its high moisture content, easy water absorption, low energy density, difficulty in grinding, large differences in properties, difficulty in transportation, and difficulty in storage. The processing process also produces a large amount of gasification tar pollutants, which does not meet the current demand for clean and green energy. This greatly limits the resource utilization of biomass. Summary of the invention

[0004] In view of the shortcomings of the prior art, the purpose of the utility model is to provide a biomass pressurized baking equipment to solve the technical problems in the prior art that biomass energy is difficult to process, has high processing costs, and is prone to produce gasification tar pollutants.

[0005] In order to solve the above technical problems, the utility model adopts the following technical solutions:

[0006] A biomass pressurized baking device comprises a pressurized baking reactor; the pressurized baking reactor comprises a reactor body, and the reactor body is provided with a heating steam inlet, a pressurized saturated steam outlet, a drying steam outlet and a pyrolysis gas outlet.

[0007] The heating steam inlet is connected to the steam outlet of the steam generator, and the water inlet of the steam generator is connected to the first water outlet of the desalted water tank.

[0008] The drying steam outlet is connected to the steam inlet end of the first heat exchanger, and the water outlet end of the first heat exchanger is connected to the sewage treatment system.

[0009] The pressurized saturated steam outlet is connected to the steam inlet end of the temperature and pressure reducing device, the steam outlet end of the temperature and pressure reducing device is connected to the steam inlet end of the second heat exchanger, and the water outlet end of the second heat exchanger is connected to the first return water end of the desalted water tank.

[0010] The second water outlet end of the demineralized water tank is also connected to the inlet steam and water end of the desuperheater and pressure reducer, and the outlet end of the desuperheater and pressure reducer is connected to the second water return end of the demineralized water tank.

[0011] The pyrolysis gas outlet is connected to the inlet steam end of the third heat exchanger, the outlet steam end of the third heat exchanger is connected to the inlet steam end of the buffer tank, and a combustible gas burner is arranged at the gas outlet end of the buffer tank.

[0012] The biomass pressurized baking equipment further includes a circulating water tank; the circulating water tank is connected to the first heat exchanger, the second heat exchanger and the third heat exchanger.

[0013] The utility model further has the following technical features:

[0014] A raw material inlet is further arranged on the reaction kettle body.

[0015] The first water outlet end of the demineralized water tank is connected to the inlet end of the first water outlet pipeline of the demineralized water tank, and the outlet end of the first water outlet pipeline of the demineralized water tank is connected to the inlet end of the steam generator; the outlet steam end of the steam generator is connected to the inlet steam end of the reaction kettle steam inlet pipeline, and the outlet end of the reaction kettle steam inlet pipeline is connected to the heating steam inlet of the pressurized baking reaction kettle.

[0016] The dry steam outlet of the pressurized baking reaction kettle is connected to the inlet steam end of the dry steam pipeline, the outlet steam end of the dry steam pipeline is connected to the inlet steam end of the first heat exchanger, the outlet water end of the first heat exchanger is connected to the inlet end of the sewage discharge pipeline, and the outlet end of the sewage discharge pipeline is connected to the sewage treatment system.

[0017] The pressurized saturated steam outlet of the pressurized baking reaction kettle is connected to the inlet steam end of the pressurized saturated steam outlet pipeline, and the outlet steam end of the pressurized saturated steam outlet pipeline is connected to the inlet steam and water end of the desuperheater and pressure reducer; the outlet steam end of the desuperheater and pressure reducer is connected to the inlet steam end of the desuperheater and pressure reducer outlet pipeline, and the outlet end of the desuperheater and pressure reducer outlet pipeline is connected to the inlet steam end of the second heat exchanger; the second heat exchanger is connected to the inlet end of the second heat exchanger water return pipeline, and the outlet end of the second heat exchanger water return pipeline is connected to the first water return end of the demineralized water tank.

[0018] The second water outlet end of the demineralized water tank is connected to the inlet end of the second water outlet pipeline of the demineralized water tank, and the outlet end of the second water outlet pipeline of the demineralized water tank is connected to the pressurized saturated steam outlet pipeline; the outlet water end of the desuperheater and pressure reducer is connected to the inlet end of the desuperheater and pressure reducer water return pipeline, and the outlet end of the desuperheater and pressure reducer water return pipeline is connected to the first water return end of the demineralized water tank.

[0019] The pyrolysis gas outlet of the pressurized baking reactor is connected to the steam inlet end of the pyrolysis gas pipeline. The steam outlet end of the pyrolysis gas pipeline is connected to the steam inlet end of the third heat exchanger. The steam outlet end of the third heat exchanger is connected to the steam inlet end of the steam outlet pipeline of the third heat exchanger. The steam outlet end of the steam outlet pipeline of the third heat exchanger is connected to the steam inlet end of the buffer tank. The steam outlet end of the buffer tank is connected to the steam inlet end of the buffer tank gas outlet pipeline. A combustible gas burner is provided at the gas outlet end of the buffer tank gas outlet pipeline.

[0020] The first water outlet end of the circulating water tank is connected to the water inlet end of the first circulating water tank outlet pipeline. The water outlet end of the first circulating water tank outlet pipeline is connected to the water inlet end of the second heat exchanger. The water outlet end of the second heat exchanger is connected to the water inlet end of the first circulating water tank return pipeline. The water outlet end of the first circulating water tank return pipeline is connected to the first water return end of the circulating water tank.

[0021] The second water outlet end of the circulating water tank is connected to the water inlet end of the second circulating water tank outlet pipeline. The water outlet end of the second circulating water tank outlet pipeline is connected to the water inlet end of the first heat exchanger. The water outlet end of the first heat exchanger is connected to the water inlet end of the second circulating water tank return pipeline. The water outlet end of the second circulating water tank return pipeline is connected to the first water return end of the circulating water tank.

[0022] The third water outlet end of the circulating water tank is connected to the water inlet end of the third circulating water tank outlet pipeline. The water outlet end of the third circulating water tank outlet pipeline is connected to the water inlet end of the third heat exchanger. The water outlet end of the third heat exchanger is connected to the water inlet end of the third circulating water tank return pipeline. The water outlet end of the third circulating water tank return pipeline is connected to the first water return end of the circulating water tank.

[0023] Compared with the prior art, the utility model has the following technical effects:

[0024] (Ⅰ) The biomass pressurized baking equipment of the utility model can carry out pressurized baking treatment on biomass raw materials. The char product obtained after treatment has a more uniform element distribution, higher calorific value and lower oxygen content compared with the original biomass raw materials; Pressurized baking helps to improve the gasification characteristics of biomass and increase the yields of CO and H2. At the same time, in a pressurized steam atmosphere, the yield of gaseous tar in the pyrolysis gas generated after baking is lower, and the yield of pyrolysis gas is lower than that under normal pressure, while the yield and calorific value of solid char are higher; The char product obtained after pressurized baking treatment is more prone to fluidization. By suppressing the interlocking and potential coherence between particles, arching and bridging reactions during feeding as gasification raw materials can be avoided or reduced; After pressurized baking treatment, most of the hemicellulose, part of the lignin and cellulose in biomass are cracked to produce small molecule gases and tar, and the content is significantly reduced. The overall structure becomes more porous, brittle and easier to break, and the grindability is significantly improved, significantly reducing the crushing cost.

[0025] In summary, after the biomass pressurized baking equipment of the present utility model is used to perform pressurized baking pretreatment on biomass, the processing difficulty and cost of biomass are reduced, and the generation of gasification tar is reduced during the processing, realizing the clean, efficient and low-carbon conversion and utilization of biomass raw materials.

[0026] (Ⅱ) The biomass pressurized baking equipment of the present utility model can adjust the heat source through a steam generator, and can realize the simultaneous drying and pressurized baking of biomass raw materials in a pressurized baking reaction kettle, with stronger adaptability to the moisture content of raw materials and a wider application range.

[0027] (Ⅲ) When using the present utility model to process biomass raw materials, the water vapor generated during the drying process can provide the required pressure in the reaction kettle, improve the heat transfer efficiency, shorten the drying time, and at the same time provide the pressure condition in the pressurized baking reaction kettle; multiple reaction kettles can be used for multi-stage energy utilization; the combustible gas generated by baking can be returned to the steam generator after combustion for preparing high-quality steam; through the above-mentioned cascade utilization of energy, the overall energy consumption of the equipment is effectively reduced, the energy efficiency of the whole process is improved, and green environmental protection is realized.

[0028] (Ⅳ) The biomass pressurized baking equipment of the present utility model has a simple structure, strong adaptability, large processing capacity, and good economy. Description of the Drawings

[0029] Figure 1 It is a schematic structural diagram of a pressurized baking reaction kettle.

[0030] Figure 2 It is a schematic overall structural diagram of the biomass pressurized baking equipment.

[0031] The meanings of the reference numerals and symbols in the figure are: 101 - reaction kettle main body, 102 - heating steam inlet, 103 - drying steam outlet, 104 - pressurized saturated steam outlet, 105 - pyrolysis gas outlet, 106 - raw material inlet.

[0032] 1 - Pressurized baking reactor, 2 - Steam generator, 3 - Demineralized water tank, 4 - First heat exchanger, 5 - Desuperheating and pressure reducing valve, 6 - Second heat exchanger, 7 - Third heat exchanger, 8 - Buffer tank, 9 - Combustible gas burner, 10 - Circulating water tank, 11 - First outlet pipe of demineralized water tank, 12 - Steam inlet pipe of reactor, 13 - Dry steam pipe, 14 - Drain pipe, 15 - Outlet pipe of pressurized saturated steam, 16 - Outlet pipe of desuperheating and pressure reducing valve, 17 - Return water pipe of second heat exchanger, 18 - Second outlet pipe of demineralized water tank, 19 - Return water pipe of desuperheating and pressure reducing valve, 20 - Pyrolysis gas pipe, 21 - Outlet pipe of third heat exchanger, 22 - Outlet pipe of buffer tank, 23 - First outlet pipe of circulating water tank, 24 - First return water pipe of circulating water tank, 25 - Second outlet pipe of circulating water tank, 26 - Second return water pipe of circulating water tank, 27 - Third outlet pipe of circulating water tank, 28 - Third return water pipe of circulating water tank.

[0033] The following further elaborates on the specific content of the present invention in conjunction with embodiments. Detailed implementation manners

[0034] It should be noted that all components and systems in the present utility model, without special instructions, adopt components and systems known in the art. For example:

[0035] The steam generator 2 adopts a conventional steam generator known in the prior art. The desuperheating and pressure reducing valve 5 adopts a conventional desuperheating and pressure reducing valve known in the prior art.

[0036] The first heat exchanger 4, the second heat exchanger 6, and the third heat exchanger 7 all adopt conventional double-pipe heat exchangers known in the prior art.

[0037] The sewage treatment system adopts a conventional sewage treatment system known in the prior art.

[0038] It should be noted that valves can be set on the pipelines in the present utility model according to actual needs.

[0039] The following gives specific embodiments of the present utility model. It should be noted that the present utility model is not limited to the following specific embodiments, and all equivalent transformations made on the basis of the technical solutions of this application fall within the protection scope of the present utility model.

[0040] Embodiment:

[0041] This embodiment provides a biomass pressurized baking device, including a pressurized baking reactor 1; as Figure 1 shown, the pressurized baking reactor 1 includes a reactor main body 101, and a heating steam inlet 102, a pressurized saturated steam outlet 104, a dry steam outlet 103, and a pyrolysis gas outlet 105 are provided on the reactor main body 101.

[0042] As Figure 1 and Figure 2 shown, the heating steam inlet 102 is connected to the steam outlet end of the steam generator 2, and the water inlet end of the steam generator 2 is connected to the first water outlet end of the demineralized water tank 3; the dry steam outlet 103 is connected to the steam inlet end of the first heat exchanger 4, and the water outlet end of the first heat exchanger 4 is connected to the sewage treatment system; the pressurized saturated steam outlet 104 and the second water outlet end of the demineralized water tank 3 are both connected to the water and steam inlet end of the desuperheating and pressure reducing valve 5, and the steam outlet end of the desuperheating and pressure reducing valve 5 is connected to the steam inlet end of the second heat exchanger 6, and the water outlet end of the second heat exchanger 6 is connected to the first water return end of the demineralized water tank 3; the water outlet end of the desuperheating and pressure reducing valve 5 is connected to the second water return end of the demineralized water tank 3; the pyrolysis gas outlet 105 is connected to the steam inlet end of the third heat exchanger 7, the steam outlet end of the third heat exchanger 7 is connected to the steam inlet end of the buffer tank 8, and a combustible gas burner 9 is provided at the gas outlet end of the buffer tank 8; the biomass pressurized baking device further includes a circulating water tank 10; the circulating water tank 10 is connected to the first heat exchanger 4, the second heat exchanger 6 and the third heat exchanger 7.

[0043] In this embodiment, the pressurized baking reactor 1 is used for drying and pressurized baking treatment of biomass raw materials, the steam generator 2 is used for preparing steam as the reaction heat source, the demineralized water tank 3 is used for supplying raw water to the steam generator 2 and cooling water to the desuperheating and pressure reducing valve 5, the first heat exchanger 4 is used for treating the waste steam generated in the drying stage, the desuperheating and pressure reducing valve 5 and the second heat exchanger 6 are used for treating the pressurized high-temperature steam generated in the baking stage, the third heat exchanger 7, the buffer tank 8 and the combustible gas burner 9 are used for treating the pyrolysis gas generated in the baking stage, and the circulating water tank 10 is used for supplying cooling water to the three heat exchangers.

[0044] In this embodiment, the discharge of water vapor or pyrolysis gas generated by the pressurized baking reactor 1 can be adjusted by a three-way valve on the main pipeline.

[0045] In this embodiment, by changing the length of the reactor body of the pressurized baking reactor 1, the processing capacity requirements of different biomasses can be met.

[0046] As a specific scheme of this embodiment, as Figure 1 shown, a raw material inlet 106 is further provided on the reactor main body 101. Biomass materials are introduced into the reactor main body 101 through the raw material inlet 106.

[0047] As a specific scheme of this embodiment, as Figure 2As shown in the figure, the first water outlet end of the demineralized water tank 3 is connected to the water inlet end of the first demineralized water outlet pipeline 11, and the water outlet end of the first demineralized water outlet pipeline 11 is connected to the water inlet end of the steam generator 2; the steam outlet end of the steam generator 2 is connected to the steam inlet end of the reaction kettle steam inlet pipeline 12, and the steam outlet end of the reaction kettle steam inlet pipeline 12 is connected to the heating steam inlet 102 of the pressure baking reaction kettle 1.

[0048] In this embodiment, the water in the demineralized water tank 3 enters the steam generator 2 through the first demineralized water outlet pipeline 11 to provide raw water for steam preparation; the steam generator 2 is used to prepare saturated steam required for the drying stage and superheated steam required for the baking stage, and the steam prepared by the steam generator 2 is introduced into the pressure baking reaction kettle 1 through the reaction kettle steam inlet pipeline 12 and serves as the reaction heat source.

[0049] As a specific scheme of this embodiment, as Figure 2 shown in the figure, the dry steam outlet 103 of the pressure baking reaction kettle 1 is connected to the steam inlet end of the dry steam pipeline 13, the steam outlet end of the dry steam pipeline 13 is connected to the steam inlet end of the first heat exchanger 4, the water outlet end of the first heat exchanger 4 is connected to the water inlet end of the sewage discharge pipeline 14, and the water outlet end of the sewage discharge pipeline 14 is connected to the sewage treatment system.

[0050] In this embodiment, the water vapor generated in the drying stage enters the second heat exchanger 6 through the dry steam pipeline 13 for cooling, and the sewage generated after cooling is discharged to the sewage treatment system through the sewage discharge pipeline 14 for subsequent treatment.

[0051] As a specific scheme of this embodiment, as Figure 2 shown in the figure, the pressurized saturated steam outlet 104 of the pressure baking reaction kettle 1 is connected to the steam inlet end of the pressurized saturated steam outlet pipeline 15, and the steam outlet end of the pressurized saturated steam outlet pipeline 15 is connected to the water and steam inlet end of the desuperheating and pressure reducing valve 5; the steam outlet end of the desuperheating and pressure reducing valve 5 is connected to the steam inlet end of the desuperheating and pressure reducing valve outlet pipeline 16, and the steam outlet end of the desuperheating and pressure reducing valve outlet pipeline 16 is connected to the steam inlet end of the second heat exchanger 6; the second heat exchanger 6 is connected to the water inlet end of the second heat exchanger return water pipeline 17, and the water outlet end of the second heat exchanger return water pipeline 17 is connected to the first return water end of the demineralized water tank 3.

[0052] In this embodiment, the pressurized saturated steam generated after the superheated steam heat exchange in the baking stage first enters the pressurized saturated steam outlet pipe 15. At the same time, the water in the demineralized water tank 3 also enters the pressurized saturated steam outlet pipe 15 through the second outlet pipe 18 of the demineralized water tank and mixes with the pressurized saturated steam. Then, they flow into the desuperheating and pressure reducing valve 5 together for pressure reduction and temperature reduction, and finally enter the second heat exchanger 6 through the steam outlet pipe 16 of the desuperheating and pressure reducing valve to realize the waste heat recovery of the saturated steam. The desuperheating and pressure reducing valve 5 can reduce the load of the second heat exchanger 6 and lower the equipment requirements.

[0053] As a specific solution of this embodiment, as Figure 2 shown, the second outlet end of the demineralized water tank 3 is communicated with the inlet end of the second outlet pipe 18 of the demineralized water tank, and the outlet end of the second outlet pipe 18 of the demineralized water tank is communicated with the pressurized saturated steam outlet pipe 15; the outlet end of the desuperheating and pressure reducing valve 5 is communicated with the inlet end of the return water pipe 19 of the desuperheating and pressure reducing valve, and the outlet end of the return water pipe 19 of the desuperheating and pressure reducing valve is communicated with the first return end of the demineralized water tank 3.

[0054] In this embodiment, the water in the demineralized water tank 3 enters the desuperheating and pressure reducing valve 5 through the second outlet pipe 18 of the demineralized water tank to provide cooling water for the desuperheating and pressure reducing valve 5. The cooling water after heat exchange flows back into the demineralized water tank 3 through the return water pipe 19 of the desuperheating and pressure reducing valve to realize recycling.

[0055] As a specific solution of this embodiment, as Figure 2 shown, the pyrolysis gas outlet 105 of the pressurized baking reactor 1 is communicated with the inlet end of the pyrolysis gas pipe 20, the outlet end of the pyrolysis gas pipe 20 is communicated with the inlet end of the third heat exchanger 7, the outlet end of the third heat exchanger 7 is communicated with the inlet end of the steam outlet pipe 21 of the third heat exchanger, the outlet end of the steam outlet pipe 21 of the third heat exchanger is communicated with the inlet end of the buffer tank 8, and a combustible gas burner 9 is arranged at the outlet end of the buffer tank outlet pipe 22.

[0056] In this embodiment, partial pyrolysis gas is generated in the baking stage. The pyrolysis gas contains CO, CO 2 , CH 4 , O 2and a small amount of gaseous tar; the pyrolysis gas and gaseous tar generated during the baking stage enter the third heat exchanger 7 through the pyrolysis gas pipeline 20 for cooling, and the gas cooled by the third heat exchanger 7 enters the buffer tank 8 through the steam outlet pipeline 21 of the third heat exchanger; the buffer tank 8 is used to mix the pyrolysis gas evenly to ensure uniform gas outlet; the combustible gas burner 9 is used to burn the pyrolysis gas generated by baking; a sewage outlet is arranged below the buffer tank 8 for timely discharging the condensed water generated during the condensation process to ensure stable combustion of the combustible gas; the flue gas after being burned by the combustible gas burner 9 can be used to prepare the steam required for drying and baking, realizing the effective utilization of energy.

[0057] As a specific solution of this embodiment, as Figure 2 shown, the first water outlet end of the circulation water tank 10 is communicated with the water inlet end of the first circulation water outlet pipeline 23 of the circulation water tank, the water outlet end of the first circulation water outlet pipeline 23 of the circulation water tank is communicated with the water inlet end of the second heat exchanger 6, the water outlet end of the second heat exchanger 6 is communicated with the water inlet end of the first circulation water return pipeline 24 of the circulation water tank, and the water outlet end of the first circulation water return pipeline 24 of the circulation water tank is communicated with the first water return end of the circulation water tank 10.

[0058] In this embodiment, the water in the circulation water tank 10 enters the second heat exchanger 6 through the first circulation water outlet pipeline 23 of the circulation water tank to provide cooling water for the second heat exchanger 6, and the cooling water after absorbing the waste heat returns to the circulation water tank 10 through the first circulation water return pipeline 24 of the circulation water tank for continued use.

[0059] As a specific solution of this embodiment, as Figure 2 shown, the second water outlet end of the circulation water tank 10 is communicated with the water inlet end of the second circulation water outlet pipeline 25 of the circulation water tank, the water outlet end of the second circulation water outlet pipeline 25 of the circulation water tank is communicated with the water inlet end of the first heat exchanger 4, the water outlet end of the first heat exchanger 4 is communicated with the water inlet end of the second circulation water return pipeline 26 of the circulation water tank, and the water outlet end of the second circulation water return pipeline 26 of the circulation water tank is communicated with the first water return end of the circulation water tank 10.

[0060] In this embodiment, the water in the circulation water tank 10 enters the second heat exchanger 6 through the second circulation water outlet pipeline 25 of the circulation water tank to provide cooling water for the first heat exchanger 4, and the cooling water after absorbing the waste heat returns to the circulation water tank 10 through the second circulation water return pipeline 26 of the circulation water tank for continued use.

[0061] As a specific solution of this embodiment, as Figure 2 shown, the third water outlet end of the circulation water tank 10 is communicated with the water inlet end of the third circulation water outlet pipeline 27 of the circulation water tank, the water outlet end of the third circulation water outlet pipeline 27 of the circulation water tank is communicated with the water inlet end of the third heat exchanger 6, the water outlet end of the third heat exchanger 6 is communicated with the water inlet end of the third circulation water return pipeline 28 of the circulation water tank, and the water outlet end of the third circulation water return pipeline 28 of the circulation water tank is communicated with the first water return end of the circulation water tank 10.

[0062] In this embodiment, the water in the circulating water tank 10 enters the second heat exchanger 6 through the third outlet pipeline 27 of the circulating water tank to provide cooling water for the third heat exchanger 6. After absorbing the waste heat, the cooling water returns to the circulating water tank 10 through the third return pipeline 28 of the circulating water tank for continued use.

[0063] The working process of the utility model is as follows:

[0064] Step 1, loading:

[0065] Load the biomass raw materials into the pressurized baking reactor 1 until the filling amount of the biomass raw materials is 60% - 80% of the inner cavity volume of the entire reactor. When loading, a material truck is used for feeding. There are no other moving equipment in the reactor, which has better adaptability to temperature and pressure. The material truck for loading can be partitioned by baffles to avoid excessive accumulation of materials, which is not conducive to heat exchange. The material truck and baffles for loading are provided with holes of a certain size, which can accelerate heat transfer and improve heat transfer efficiency.

[0066] Step 2, drying of materials:

[0067] Start the steam generator 2 to prepare saturated steam, and then introduce the saturated steam into the pressurized baking reactor 1 for material drying. Coil heat exchange is used in the drying stage. The temperature of the saturated steam in the coil is 150 - 200 °C, ensuring that the temperature of the core of the material in the pressurized baking reactor 1 is 100 - 150 °C, and the pressure in the cavity of the pressurized baking reactor 1 is 0.5 - 2.5 MPa. The water vapor generated in the drying stage flows into the sewage treatment system after being cooled by the first heat exchanger 4.

[0068] Step 3, baking of materials:

[0069] Start the steam generator 2 to prepare superheated steam, and then introduce the saturated steam into the pressurized baking reactor 1 for material baking. Coil heat exchange is used in the baking stage. The temperature of the superheated steam in the coil is 350 - 450 °C, ensuring that the temperature of the core of the material in the pressurized baking reactor 1 is 200 - 350 °C. Since the cavity of the pressurized baking reactor 1 is in a water vapor pressurized state after drying, at this time, the pressure in the cavity of the pressurized baking reactor 1 is 0.5 - 1.5 Mpa, and there is no need to introduce additional steam, and it can directly enter the baking stage. The pressurized saturated steam generated in the baking stage first enters the desuperheating and pressure reducing device 5, and after cooling and pressure reduction, it enters the second heat exchanger 6. The pyrolysis gas and gaseous tar generated in the baking stage are cooled by the third heat exchanger 7 and then sent to the buffer tank 8. The combustible gas in the buffer tank 8 can be directly burned by the combustible gas burner 9, or can be combined with the gasification process for secondary reaction.

[0070] Through the above working process, the utility model can pre-treat different biomasses, reduce the moisture content of the biomasses, and finally reduce the oxygen content in the prepared semi-coke product to 50% - 70% of the biomass raw material. The elemental composition of the semi-coke product is more homogenized, and the calorific value of the semi-coke product is increased by more than 25% compared with the original material, which is beneficial to the subsequent transportation and conversion processes. At the same time, baking can reduce the fiber content of the biomass, make the biomass particles more brittle and easier to grind, reduce the energy consumption in the crushing process, and save 50 - 85% of electric energy in preparing 0.1mm semi-coke powder compared with the biomass raw material.

Claims

1. A biomass pressure roasting device, characterized in that: The invention comprises a pressurized baking reactor (1); the pressurized baking reactor (1) comprises a reactor body (101), and the reactor body (101) is provided with a heating steam inlet (102), a pressurized saturated steam outlet (104), a drying steam outlet (103) and a pyrolysis gas outlet (105); The heating steam inlet (102) is connected to the steam outlet of the steam generator (2), and the water inlet of the steam generator (2) is connected to the first water outlet of the desalted water tank (3); The drying steam outlet (103) is connected to the steam inlet end of the first heat exchanger (4), and the water outlet end of the first heat exchanger (4) is connected to the sewage treatment system; The pressurized saturated steam outlet (104) is connected to the steam inlet end of the temperature reducing and pressure reducing device (5), the steam outlet end of the temperature reducing and pressure reducing device (5) is connected to the steam inlet end of the second heat exchanger (6), and the water outlet end of the second heat exchanger (6) is connected to the first water return end of the desalted water tank (3); The second water outlet end of the desalted water tank (3) is also connected to the water vapor inlet end of the temperature reducing and pressure reducing device (5), and the water outlet end of the temperature reducing and pressure reducing device (5) is connected to the second water return end of the desalted water tank (3); The pyrolysis gas outlet (105) is connected to the steam inlet end of the third heat exchanger (7), the steam outlet end of the third heat exchanger (7) is connected to the steam inlet end of the buffer tank (8), and the gas outlet end of the buffer tank (8) is provided with a combustible gas burner (9); The biomass pressure roasting equipment further comprises a circulating water tank (10); the circulating water tank (10) is connected to the first heat exchanger (4), the second heat exchanger (6) and the third heat exchanger (7).

2. The biomass pressure roasting equipment according to claim 1, characterized in that: The reactor body (101) is also provided with a raw material inlet (106).

3. The biomass pressure roasting equipment according to claim 1, characterized in that: The first water outlet end of the desalted water tank (3) is connected to the water inlet end of the first water outlet pipe (11) of the desalted water tank, and the water outlet end of the first water outlet pipe (11) of the desalted water tank is connected to the water inlet end of the steam generator (2); the steam outlet end of the steam generator (2) is connected to the steam inlet end of the reactor steam inlet pipe (12), and the steam outlet end of the reactor steam inlet pipe (12) is connected to the heating steam inlet (102) of the pressurized baking reactor (1).

4. The biomass pressure roasting equipment according to claim 1, characterized in that: The drying steam outlet (103) of the pressurized baking reactor (1) is connected to the steam inlet end of the drying steam pipeline (13), the steam outlet end of the drying steam pipeline (13) is connected to the steam inlet end of the first heat exchanger (4), the water outlet end of the first heat exchanger (4) is connected to the water inlet end of the sewage pipeline (14), and the water outlet end of the sewage pipeline (14) is connected to the sewage treatment system.

5. The biomass pressure roasting equipment according to claim 1, characterized in that: The pressurized saturated steam outlet (104) of the pressurized baking reactor (1) is connected to the steam inlet end of the pressurized saturated steam outlet pipe (15), and the steam outlet end of the pressurized saturated steam outlet pipe (15) is connected to the steam inlet end of the temperature reducing and pressure reducing device (5); the steam outlet end of the temperature reducing and pressure reducing device (5) is connected to the steam inlet end of the temperature reducing and pressure reducing device steam outlet pipe (16), and the steam outlet end of the temperature reducing and pressure reducing device steam outlet pipe (16) is connected to the steam inlet end of the second heat exchanger (6); the second heat exchanger (6) is connected to the water inlet end of the second heat exchanger return pipe (17), and the water outlet end of the second heat exchanger return pipe (17) is connected to the first return water end of the desalted water tank (3).

6. The biomass pressure roasting equipment according to claim 5, characterized in that: The second water outlet end of the desalted water tank (3) is connected to the water inlet end of the second water outlet pipe (18) of the desalted water tank, and the water outlet end of the second water outlet pipe (18) of the desalted water tank is connected to the pressurized saturated steam outlet pipe (15); the water outlet end of the desuperheater (5) is connected to the water inlet end of the desuperheater return pipe (19), and the water outlet end of the desuperheater return pipe (19) is connected to the first return end of the desalted water tank (3).

7. The biomass pressure roasting equipment according to claim 1, characterized in that: The pyrolysis gas outlet (105) of the pressurized roasting reactor (1) is connected to the steam inlet end of the pyrolysis gas pipeline (20), the steam outlet end of the pyrolysis gas pipeline (20) is connected to the steam inlet end of the third heat exchanger (7), the steam outlet end of the third heat exchanger (7) is connected to the steam inlet end of the third heat exchanger steam outlet pipeline (21), the steam outlet end of the third heat exchanger steam outlet pipeline (21) is connected to the steam inlet end of the buffer tank (8), the steam outlet end of the buffer tank (8) is connected to the steam inlet end of the buffer tank gas outlet pipeline (22), and a combustible gas burner (9) is provided at the gas outlet end of the buffer tank gas outlet pipeline (22).

8. The biomass pressure roasting equipment according to claim 1, characterized in that: The first water outlet end of the circulating water tank (10) is connected to the water inlet end of the first water outlet pipe (23) of the circulating water tank, the water outlet end of the first water outlet pipe (23) of the circulating water tank is connected to the water inlet end of the second heat exchanger (6), the water outlet end of the second heat exchanger (6) is connected to the water inlet end of the first water return pipe (24) of the circulating water tank, and the water outlet end of the first water return pipe (24) of the circulating water tank is connected to the first water return end of the circulating water tank (10).

9. The biomass pressure roasting equipment according to claim 1, characterized in that: The second water outlet end of the circulating water tank (10) is connected to the water inlet end of the second water outlet pipe (25) of the circulating water tank, the water outlet end of the second water outlet pipe (25) of the circulating water tank is connected to the water inlet end of the first heat exchanger (4), the water outlet end of the first heat exchanger (4) is connected to the water inlet end of the second water return pipe (26) of the circulating water tank, and the water outlet end of the second water return pipe (26) of the circulating water tank is connected to the first water return end of the circulating water tank (10).

10. The biomass pressure roasting equipment according to claim 1, characterized in that: The third water outlet end of the circulating water tank (10) is connected to the water inlet end of the third water outlet pipe (27) of the circulating water tank, the water outlet end of the third water outlet pipe (27) of the circulating water tank is connected to the water inlet end of the third heat exchanger (7), the water outlet end of the third heat exchanger (7) is connected to the water inlet end of the third water return pipe (28) of the circulating water tank, and the water outlet end of the third water return pipe (28) of the circulating water tank is connected to the first water return end of the circulating water tank (10).

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