A biomass gasification fuel production process

Abstract

The present application relates to a kind of biomass gasification fuel production process, comprising the following steps, dry biomass powder is sent into low pressure bunker;Make biomass powder from low pressure bunker into lock hopper;Make the biomass powder in lock hopper into feed bin;Biomass powder and conveying gas into gas flow bed system are reacted with the oxygen admitted and converted into crude synthesis gas;Crude synthesis gas sent from gas flow bed system is admitted into synthesis gas purification system and is purified to obtain the required synthesis gas for fuel;Part of synthesis gas sent from synthesis gas purification system is sent into reaction system to prepare the required fuel product.Conveying gas uses synthesis gas or reaction tail gas or the mixed gas of above two, pressurized gas uses reaction tail gas or carbon dioxide gas after decarburization, low pressure bunker sealing gas uses carbon dioxide gas after decarburization or nitrogen or the mixed gas of two.The present application saves a lot of compression work and heat source and recovers effective component in reaction system tail gas, reduces raw material consumption, improves economic benefit.

Description

Technical Field

[0001] This invention relates to the field of biomass gas production technology, and in particular to a biomass gasification fuel production process. Background Technology

[0002] With increasingly stringent international requirements for carbon emission reduction, the demand for green energy is experiencing explosive growth. Biomass gasification to produce methanol and SAF has become a major production route for green energy. Biomass gasification is the primary energy consumption node in the production of green methanol and SAF. Currently, biomass gasification equipment mainly includes atmospheric pressure fixed bed, circulating fluidized bed, pressurized fluidized bed, and pressurized dry powder entrained flow bed. Pressurized dry powder entrained flow bed, with its advantages of high outlet temperature, high pressure, good heat recovery, and high effective component content of the reactant gas, is often the first choice for biomass gasification to produce fuel.

[0003] In existing biomass powder entrained flow bed conveying processes, biomass powder is fed into a gasifier through a low-pressure powder trough, a lock hopper, a feed bin, and a conveying mechanism. To transfer the biomass powder from the low-pressure powder trough to the high-pressure entrained flow bed, pressurizing gas and conveying gas are required. The pressurizing gas trough connects the lock hopper and the feed bin. The powder is transferred from the low-pressure to the high-pressure feed bin by pressurizing and depressurizing the lock hopper. The pressure in the feed bin is higher than that in the entrained flow bed. The bottom material is fed into the entrained flow bed by conveying gas through the conveying mechanism. The biomass material is burned with oxygen in the entrained flow bed in the gasifier, thereby converting the biomass into syngas at high temperature. The high-temperature syngas undergoes conversion, desulfurization, decarbonization, and adjustment of the hydrogen-carbon ratio before entering the reaction system to produce the required fuel.

[0004] In existing biomass pulverized gas flow systems, the conveying and pressurizing gases are carbon dioxide gas from decarbonization. Since most of the conveying and pressurizing gases enter the flow system, this carbon dioxide constantly circulates between biomass gasification and subsequent decarbonization. However, the decarbonized carbon dioxide gas has a low pressure (less than 0.1 MPa) and requires pressurization to be used as the conveying and pressurizing gas, increasing the compression work in this cycle. Furthermore, the removal of carbon dioxide consumes a large amount of heat, further increasing the decarbonization load. Especially when biomass gasification is followed by the addition of green hydrogen to produce green methanol or sustainable aviation fuel (SAF), as the amount of hydrogen added increases, the scale of biomass gasification conversion and decarbonization decreases, or even becomes unnecessary. When the amount of carbon dioxide removed cannot meet the requirements of the conveying and pressurizing gases, in order to avoid affecting the conveying of the pulverized gas, the unnecessary scale of conversion and decarbonization needs to be increased to meet the conveying demand, thus increasing unreasonable energy consumption.

[0005] Furthermore, in existing biomass gasification fuel production processes, when green hydrogen is added to produce green methanol, the tail gas from the reaction system contains a large amount of unreacted hydrogen and carbon monoxide, and its pressure is higher than that of the transport gas and pressurizing gas used in production. When green hydrogen is added to produce SAF (Self-Fuel Fuel) in the same biomass gasification process, the tail gas from the reaction system contains not only unreacted hydrogen and carbon monoxide, but also byproduct low-carbon components (methane to C7 components), and its pressure is typically greater than 1.0 MPa. Currently, these tail gases are depressurized before being used as fuel, and their effective components and pressure are not being effectively utilized. Summary of the Invention

[0006] The present invention aims to provide a biomass gasification fuel production process to overcome the shortcomings of the existing technology. The technical problem to be solved by the present invention is achieved through the following technical solution.

[0007] A biomass gasification process for producing fuel includes the following steps:

[0008] S1, Feeding; Dry biomass powder is fed into a low-pressure silo, and sealing gas is introduced into the low-pressure silo.

[0009] S2, feeding; depressurize the lock hopper so that the pressure inside the lock hopper is equal to the pressure inside the low-pressure silo, open the conveying valve I between the low-pressure silo and the lock hopper to allow biomass powder to enter the lock hopper from the low-pressure silo. After the lock hopper is full, close the conveying valve I between the low-pressure silo and the lock hopper.

[0010] S3, unloading; pressurize the lock hopper with pressurized air so that the pressure in the lock hopper is equal to the pressure in the feed hopper, open the conveying valve II between the lock hopper and the feed hopper so that the biomass powder in the lock hopper enters the feed hopper, and close the conveying valve II after unloading is completed;

[0011] S4, repeat S2 to S3 at a set time interval;

[0012] S5, Gas generation by the fluidized bed system: The pneumatic conveying mechanism sends the biomass powder in the feed hopper into the fluidized bed system through the conveying gas in the high-pressure conveying gas tank. At the same time, pressurizing gas is used to pressurize the feed hopper to maintain a constant pressure. The biomass powder and conveying gas entering the fluidized bed system react with the introduced oxygen to convert the biomass powder into crude syngas.

[0013] S6, Purify Synthesis Gas: The crude synthesis gas from the fluidized bed system is passed into the synthesis gas purification system for purification treatment to obtain the synthesis gas required for the production of synthetic products.

[0014] S7, Production of Synthetic Products; Part of the syngas sent from the syngas purification system is sent into the reaction system to produce the desired synthetic products; After the reaction system produces the synthetic products, it generates reaction tail gas.

[0015] in,

[0016] In S1, the sealing gas is either carbon dioxide gas removed from the syngas purification system or nitrogen gas supplied externally;

[0017] In S3 and S5, the pressurizing gas is the reaction tail gas generated by the reaction system, and / or the crude synthesis gas generated by the synthesis gas purification system, and / or the carbon dioxide gas removed by the synthesis gas purification system.

[0018] In S5, the transport gas is the syngas produced by the syngas purification system and / or the reaction tail gas produced by the reaction system.

[0019] Preferably, when the flow rate of the reaction tail gas generated by the reaction system can meet the needs of the pressurizing gas and the conveying gas, the reaction tail gas generated by the reaction system shall be used preferentially.

[0020] Preferably, when the flow rate of the reaction tail gas generated by the reaction system cannot meet the needs of the pressurizing gas and the transport gas, the syngas purified by the syngas purification system shall be used first.

[0021] Preferably, in S1, the sealing gas is preferably carbon dioxide gas removed by the syngas purification system, and if insufficient, it is supplemented by nitrogen gas from the outside.

[0022] Preferably, in S2, when depressurizing the lock hopper, the lock hopper is first pressure-equalized, and then pressure-equalized again; in S3, when pressurizing the lock hopper, the lock hopper is first pressure-equalized, and then pressurized with pressurizing gas.

[0023] Preferably, there is one locking hopper, which is connected to the pressure equalization tank;

[0024] In S2, when depressurizing the lock bucket, the lock bucket is first pressure-equalized through the pressure equalization tank, and then pressure is depressurized a second time. When equalizing the pressure of the lock bucket, the pressurization valve between the lock bucket and the pressure equalization tank is first opened, the lock bucket is pressure-equalized through the pressure equalization tank, and then pressure is depressurized a second time until the target set pressure is reached in the lock bucket.

[0025] In S3, when pressurizing the lock hopper, the lock hopper is first pressurized through the pressure equalization tank, and then pressurized through the pressurizing air. When pressurizing the lock hopper, the pressurizing air valve between the lock hopper and the pressure equalization tank is first opened, the lock hopper is pressurized through the pressure equalization tank, and then pressurized through the pressurizing air until the pressure inside the lock hopper is the same as the pressure inside the feed hopper.

[0026] Preferably, there are two lock hoppers, namely lock hopper I and lock hopper II, and lock hopper I and lock hopper II are respectively connected to the low-pressure silo, the low-pressure tank and the feed silo;

[0027] In S2, during feeding, firstly, the pressurizing valve between lock hopper I and lock hopper II is opened to equalize the pressure between them. The pressure in lock hopper I decreases to a certain value, and the pressure in lock hopper II increases to a certain value. Then, the pressurizing valve between lock hopper I and lock hopper II is disconnected to stop equalizing the pressure. Then, lock hopper I is depressurized a second time to make the pressure in lock hopper I comparable to the pressure in the low-pressure silo. Lock hopper II is then pressurized a second time to make the pressure in lock hopper II comparable to the pressure in the feed silo. Then, the conveying valve I between the low-pressure silo and lock hopper I is opened to allow biomass powder to enter lock hopper I from the low-pressure silo. After lock hopper I is full, the conveying valve I is closed, and the conveying valve II between lock hopper II and the feed silo is opened to allow the biomass powder in lock hopper II to enter the feed silo. After lock hopper II is unloaded, the conveying valve II is closed.

[0028] In S3, during unloading, the pressurizing valve between lock hopper I and lock hopper II is opened to equalize the pressure between them. The pressure in lock hopper I rises to a certain value, and the pressure in lock hopper II decreases to a certain value. Then, the pressurizing valve between lock hopper I and lock hopper II is disconnected to stop equalizing the pressure. Lock hopper I is then pressurized a second time using pressurizing air to make the pressure in lock hopper I comparable to the pressure in the feed hopper. Lock hopper II is then depressurized a second time to make the pressure in lock hopper II comparable to the pressure in the low-pressure hopper. The conveying valve II between lock hopper I and the feed hopper is opened to allow the biomass powder in lock hopper I to enter the feed hopper. After lock hopper I is unloaded, the conveying valve II is closed. The conveying valve I between the low-pressure hopper and lock hopper II is opened to allow the biomass powder to enter lock hopper II from the low-pressure hopper. After lock hopper II is full, the conveying valve I is closed.

[0029] Preferably, the lock bucket is connected to the low-pressure groove, and in S2, the lock bucket is depressurized a second time through the low-pressure groove.

[0030] Preferably, a vent valve is provided between the lock hopper and the low-pressure silo. In S2, the vent valve is opened to perform secondary pressure relief on the lock hopper, so that the pressure inside the lock hopper is released into the low-pressure silo.

[0031] In this invention, the reaction tail gas from the production of fuel products using biomass powder and hydrogen is used as the main conveying gas for the biomass powder entering the fluidized bed system. The biomass powder is fed into the fluidized bed system and combusted with introduced oxygen in a gasifier, thereby converting the biomass powder into crude syngas (mainly carbon monoxide, carbon dioxide, and hydrogen) at high temperature. After heat recovery, the high-temperature crude syngas undergoes conversion, desulfurization, and decarbonization to adjust the hydrogen-carbon ratio before entering the subsequent reaction system to produce the desired product. The conveying gas in the feed hopper is the desulfurized and decarbonized syngas, the tail gas produced by the reaction system, or a mixture of the two. The pressurizing gas for the lock hopper and feed hopper is the tail gas produced by the reaction system or the carbon dioxide gas from decarbonization. The sealing gas for the low-pressure hopper after drying is the carbon dioxide gas from decarbonization, nitrogen, or a mixture of both.

[0032] Compared to existing technologies, this invention utilizes syngas generated in the syngas purification system and tail gas generated in the reaction system as the conveying and pressurizing gases required for production. This eliminates or significantly reduces the circulation of carbon dioxide between the reaction system and the decarbonization stage, saving on carbon dioxide removal consumption. Furthermore, using higher-pressure syngas or reaction system tail gas saves considerable compression work compared to compressing low-pressure carbon dioxide conveying gas and recovers effective components from the reaction system tail gas, reducing raw material consumption and improving economic efficiency. By setting up a pressure equalization tank, the high-pressure gas in the unloaded lock hopper is released into the pressure equalization tank, and then the gas from the pressure equalization tank is used to pressurize the loaded lock hopper, thereby saving pressurizing gas. Attached Figure Description

[0033] Figure 1 This is a schematic block diagram of a structure according to an embodiment of the present invention;

[0034] Figure 2 This is a schematic block diagram of another embodiment of the present invention;

[0035] Figure 3 This is a schematic block diagram of another embodiment of the present invention;

[0036] Figure 4 This is a schematic block diagram of another embodiment of the present invention;

[0037] The reference numerals in the attached figures are as follows: C1, pneumatic conveying mechanism; C2, syngas compressor; C3, carbon dioxide compressor; C4, recovered gas booster; C5, reaction system tail gas compressor; M1, fluidized bed system; M2, syngas purification system; M3, reaction system; V1, low-pressure silo; V2, lock hopper; V2A, lock hopper I; V2B, lock hopper II; V3, feed silo; V4, high-pressure charging tank; V5, high-pressure conveying gas tank; V6, equalizing tank; V7, low-pressure tank. Detailed Implementation

[0038] It should be noted that, unless otherwise specified, the embodiments and features described in this application can be combined with each other. The present invention will now be described in detail with reference to the accompanying drawings and embodiments.

[0039] Example 1:

[0040] An improved process for producing fuel from biomass gasification includes the following steps:

[0041] S1, Feeding; Dry biomass powder is fed into low-pressure silo V1, and sealing gas is introduced into low-pressure silo V1;

[0042] S2, feeding; depressurize lock hopper V2 so that the pressure inside lock hopper V2 is equal to the pressure inside low-pressure silo V1, open conveying valve I between low-pressure silo V1 and lock hopper V2 to allow biomass powder to enter lock hopper V2 from low-pressure silo V1. After lock hopper V2 is full, close conveying valve I between low-pressure silo V1 and lock hopper V2.

[0043] S3, unloading; pressurize the lock hopper V2 with pressurized air so that the pressure in the lock hopper V2 is equal to the pressure in the feed hopper V3, open the conveying valve II between the lock hopper V2 and the feed hopper V3 so that the biomass powder in the lock hopper V2 enters the feed hopper V3, and close the conveying valve II after unloading is completed.

[0044] S4, repeat S2 to S3 at a set time interval;

[0045] S5, Gas generation by the fluidized bed system; the pneumatic conveying mechanism C1 sends the biomass powder in the feed hopper V3 into the fluidized bed system M1 through the conveying gas in the high-pressure conveying gas tank V5. At the same time, pressurizing gas is used to pressurize the feed hopper V3 to maintain a constant pressure. The biomass powder and conveying gas entering the fluidized bed system M1 react with the introduced oxygen to convert the biomass powder into crude syngas.

[0046] S6, Purify syngas; The crude syngas from the fluidized bed system M1 is passed into the syngas purification system M2 for purification to obtain the syngas required for the production of synthetic products.

[0047] S7, Production of Synthetic Products; Part of the syngas sent from the syngas purification system M2 is sent into the reaction system M3 to produce the desired synthetic products; After the reaction system M3 produces the synthetic products, it generates reaction tail gas.

[0048] in,

[0049] In S1, the sealing gas is either carbon dioxide gas removed from the synthesis gas purification system M2 or nitrogen gas supplied from the outside;

[0050] In S3 and S5, the pressurizing gas is the reaction tail gas generated by the reaction system M3, and / or the crude synthesis gas generated by the synthesis gas purification system M2, and / or the carbon dioxide gas removed from the synthesis gas purification system M2.

[0051] In S5, the transport gas is the syngas produced by the syngas purification system M2 and / or the reaction tail gas produced by the reaction system M3.

[0052] Furthermore, when the flow rate of the reaction tail gas generated by the reaction system M3 can meet the needs of the pressurizing gas and the transport gas, the reaction tail gas generated by the reaction system M3 shall be used preferentially.

[0053] Furthermore, when the flow rate of the reaction tail gas generated by the reaction system M3 cannot meet the needs of the pressurizing gas and the transport gas, the syngas purified by the syngas purification system M2 shall be used preferentially.

[0054] Furthermore, in S1, the sealing gas is preferably carbon dioxide gas removed from the syngas purification system M2, and if insufficient, it is supplemented by nitrogen gas from the outside.

[0055] Furthermore, in S2, when depressurizing the lock hopper V2, the lock hopper V2 is first pressure-equalized, and then pressure-depressurized a second time; in S3, when pressurizing the lock hopper V2, the lock hopper V2 is first pressure-equalized, and then pressurized by pressurizing gas.

[0056] Furthermore, the lock bucket V2 is connected to the low-pressure groove V7. In S2, the lock bucket V2 is depressurized a second time through the low-pressure groove V7.

[0057] Furthermore, a vent valve is provided between the lock hopper V2 and the low-pressure silo V1. In S2, the vent valve is opened to perform secondary pressure relief on the lock hopper V2, so that the pressure inside the lock hopper V2 is released into the low-pressure silo V1. The pressure of the low-pressure tank V7 is maintained by sending the gas in the low-pressure tank V7 to the recovery system for recycling.

[0058] In this embodiment, the biomass gasification fuel production process is completed in a biomass gasification production system, which includes a biomass silo system, a silo pressurization system, a gas conveying system, a fluidized bed system M1, a syngas purification system M2, and a reaction system M3.

[0059] The biomass silo system includes a low-pressure silo V1, a lock hopper V2, and a feed silo V3. The low-pressure silo V1 is connected to the lock hopper V2. Biomass powder enters the lock hopper V2 from the low-pressure silo V1. The lock hopper V2 is then pressurized by a pressure equalization tank V6 and a high-pressure aeration tank V4. After pressurization, the lock hopper V2 is connected to the feed hopper V3, and the biomass powder in the lock hopper V2 enters the feed hopper V3. The biomass powder in the feed hopper V3 then enters the airflow bed system M1 via a pneumatic conveying mechanism C1. Once all the biomass powder in the lock hopper V2 has entered the feed hopper V3, the lock hopper V2 is connected to the pressure equalization tank V6 and the low-pressure tank V7 to reduce the pressure to be equivalent to that in the low-pressure silo V1, and then it is re-feeded.

[0060] The silo pressurization system includes a high-pressure inflation tank V4, a pressure equalization tank V6, a low-pressure tank V7, and a recovery gas booster C4. The tail gas generated by the reaction system M3, the purified syngas from the syngas purification system M2, or the carbon dioxide from the decarbonization module enters the high-pressure charging tank V4, which is connected to the feed hopper V3. After all the biomass powder in the lock hopper V2 has entered the feed hopper V3, the lock hopper V2 is connected to the pressure equalization tank V6 for pressure equalization. Then it is connected to the low-pressure tank V7 to release the gas in the lock hopper V2, reducing the pressure in the lock hopper V2 to be equivalent to that in the low-pressure hopper V1. The low-pressure hopper V1 then begins to feed into the lock hopper V2. During this process, the lock hopper V2 remains connected to the low-pressure tank V7 to ensure that the pressure in the lock hopper V2 is equivalent to that in the low-pressure hopper V1. After the lock hopper V2 has finished feeding, it is then pressure equalized with the pressure equalization tank V6, and finally, the high-pressure charging tank V4 pressurizes the lock hopper V2. The gas in the low-pressure tank V7 is divided into two paths: one path is pressurized by the recovery gas booster C4 and enters the high-pressure charging tank V4 for recycling, and the other path is sent to the recovery system for recycling.

[0061] The gas delivery system includes a high-pressure gas delivery tank V5 and a pneumatic conveying mechanism C1. Syngas produced by the syngas purification system M2 or tail gas produced by the reaction system M3 enters the high-pressure gas delivery tank V5. The high-pressure gas delivery tank V5 is connected to the pneumatic conveying mechanism C1, and the biomass powder is delivered into the fluidized bed system M1 for gasification using the delivery gas.

[0062] The fluidized bed system M1 includes a gasifier. The biomass powder and conveying gas entering the fluidized bed system M1 are combusted with the oxygen introduced into the gasifier, thereby converting the biomass powder into crude syngas at high temperature. After heat recovery, washing, dust removal and cooling, the crude syngas is sent to the syngas purification system M2.

[0063] The syngas purification system M2 includes a shift converter, a desulfurization module, and a decarbonization module. The intermediate-temperature, saturated water-containing crude syngas from the fluidized bed system M1 is converted into hydrogen and carbon dioxide by the shift converter to adjust the hydrogen-to-carbon ratio required by the reaction system M3. After the shift converter, the gas undergoes desulfurization and decarbonization to obtain the syngas needed for fuel production, which is then fed into the subsequent reaction system M3. The decarbonized carbon dioxide serves as the sealing gas for the low-pressure silo V1; a portion of the syngas is pressurized and used as the conveying gas for the feed silo V3 and the pressurizing gas for the lock hopper V2 and the feed silo V3.

[0064] Syngas from the syngas purification system M2 is supplemented with hydrogen and pressurized before entering the reaction system M3, resulting in qualified products and reaction tail gas containing unreacted materials and generated byproducts. The reaction tail gas can be used as conveying gas for the feed hopper V3 and pressurizing gas for the lock hopper V2 and the feed hopper V3.

[0065] That is, the carbon dioxide and syngas removed by the syngas purification system M2 and the tail gas generated by the reaction system M3 can all be used as the pressurizing gas for the lock hopper V2 and the feed hopper V3; the syngas generated by the syngas purification system M2 and the reaction tail gas generated by the reaction system M3 can all be used as the conveying gas for the feed hopper V3; the carbon dioxide and nitrogen removed by the syngas purification system M2 can all be used as the sealing gas for the low-pressure hopper V1.

[0066] Furthermore, in this embodiment, the pressurizing gas for the lock hopper V2 and the feed hopper V3, the conveying gas for the feed hopper V3, and the sealing gas for the low-pressure hopper V1 are determined based on the carbon dioxide flow rate removed from the syngas purification system M2 and the tail gas flow rate generated by the reaction system M3. When the exhaust gas flow rate generated by reaction system M3 can meet the pressurization gas requirements of lock hopper V2 and feed hopper V3, as well as the conveying gas requirements of feed hopper V3, the exhaust gas generated by reaction system M3 shall be used first. When the exhaust gas generated by reaction system M3 cannot meet the pressurization gas requirements of lock hopper V2 and feed hopper V3, as well as the conveying gas requirements of feed hopper V3, the syngas generated by syngas purification system M2 shall be used as the supplementary gas. When the carbon dioxide flow rate removed by syngas purification system M2 meets the pressurization gas flow rate requirements of lock hopper V2 and feed hopper V3, the carbon dioxide removed by syngas purification system M2 can be used as the pressurization gas of lock hopper V2 and feed hopper V3, and the exhaust gas generated by reaction system M3 and the syngas generated by syngas purification system M2 shall be used as the conveying gas of feed hopper V3. The sealing gas of low-pressure hopper V1 shall preferentially use the carbon dioxide removed by syngas purification system M2, and the insufficient part shall be supplemented by nitrogen.

[0067] In this embodiment, in order to ensure the hydrogen-to-carbon ratio required for the production of fuel products by the reaction system M3, the conversion and decarbonization scale of the syngas purification system M2 is maximized when no hydrogen is added to the syngas. At this time, the pressurizing gas for the lock hopper V2 and the feed hopper V3 can be decarbonized gas, or it can be the syngas produced by the syngas purification system M2 and the tail gas produced by the reaction system M3. The conveying gas for the feed hopper V3 is the syngas produced by the syngas purification system M2 and the tail gas produced by the reaction system M3. The sealing gas for the low-pressure hopper V1 is carbon dioxide.

[0068] When the amount of biomass powder remains constant, but the flow rate of hydrogen added to the syngas increases, the conversion and decarbonization scale of the syngas purification system M2 will decrease. When the flow rate of hydrogen added to the syngas increases to a certain scale, the conversion operation in the syngas purification system M2 will stop, and the syngas purification system M2 will only perform desulfurization and partial decarbonization operations. When the flow rate of hydrogen added to the syngas increases to the maximum value, the syngas purification system M2 will stop the conversion and decarbonization operations and only perform desulfurization operations. At this time, the pressurizing gas of the lock hopper V2 and the conveying gas of the feed hopper V3 are the syngas generated by the syngas purification system M2 and the tail gas generated by the reaction system M3, and the sealing gas of the low-pressure hopper V1 is nitrogen.

[0069] Furthermore, when the produced fuel product is methanol, the reaction tail gas generated by the reaction system M3 is methanol purge gas, methanol flash vapor, and pre-tower exhaust gas. The methanol flash vapor and pre-tower exhaust gas are pressurized and then incorporated into the methanol purge gas and sent to the high-pressure charging tank V4 as the charging gas for the lock hopper V2 and the feed bin V3, or sent to the high-pressure conveying gas tank V5 as the conveying gas for the feed bin V3. When the product is SAF aviation kerosene, the reaction tail gas generated by the reaction system M3 is low-carbon hydrocarbon purge gas, which is sent to the high-pressure charging tank V4 as the charging gas for the lock hopper V2 and the feed bin V3, or sent to the high-pressure conveying gas tank V5 as the conveying gas for the feed bin V3.

[0070] Furthermore, when the pressurizing gas is the reaction tail gas generated by the reaction system M3, the amount of reaction tail gas sent to the recovery system by the low-pressure tank V7 for recycling is determined according to the amount of inert gas (non-carbon and non-hydrogen components) in the reaction tail gas. When the inert gas content in the reaction tail gas is high, the amount of reaction tail gas recycled by the recovery system increases, and vice versa.

[0071] Furthermore, when the biomass powder raw material is changed to coal, the syngas produced by the syngas purification system M2 and the tail gas produced by the reaction system M3 can also be used as the pressurizing gas for the lock hopper V2 and the feed hopper V3, and as the conveying gas for the feed hopper V3.

[0072] Example 2:

[0073] Based on Example 1, the number of lock buckets V2 is one, and the lock bucket V2 is connected to the pressure equalization groove V6;

[0074] In S2, when depressurizing the lock bucket V2, the lock bucket V2 is first depressurized through the pressure equalization tank V6, and then depressurized a second time. When depressurizing the lock bucket V2, the pressurization valve between the lock bucket V2 and the pressure equalization tank V6 is first opened, and the lock bucket V2 is depressurized through the pressure equalization tank V6, and then depressurized a second time until the lock bucket V2 reaches the target set pressure.

[0075] In S3, when pressurizing the lock hopper V2, the lock hopper V2 is first pressurized through the pressure equalization tank V6, and then pressurized through the pressurizing air. When equalizing the pressure of the lock hopper V2, the pressurizing air valve between the lock hopper V2 and the pressure equalization tank V6 is first opened, and the lock hopper V2 is pressurized through the pressure equalization tank V6, and then pressurized through the pressurizing air until the pressure inside the lock hopper V2 is the same as the pressure inside the feed hopper V3.

[0076] Example 3:

[0077] Based on Example 1, there are two lock hoppers V2, namely lock hopper IV2A and lock hopper IIV2B. Lock hopper IV2A and lock hopper IIV2B are respectively connected to the low-pressure silo V1 and the feeding silo V3.

[0078] In S2, during feeding, firstly, the pressurizing valve between lock hoppers IV2A and IIV2B is opened to equalize the pressure between them. The pressure inside lock hopper IV2A decreases to a certain value, while the pressure inside lock hopper IIV2B increases to a certain value. Then, the pressurizing valve between lock hoppers IV2A and IIV2B is closed to stop the pressure equalization. Next, lock hopper IV2A is depressurized a second time to make its pressure equal to the pressure inside the low-pressure silo V1. This is done by using pressurizing air... Secondary pressurization is performed on lock hopper IIV2B to make the pressure inside lock hopper IIV2B equal to the pressure inside feed hopper V3. Then, the conveying valve I between low-pressure hopper V1 and lock hopper IV2A is opened to allow biomass powder to enter lock hopper IV2A from low-pressure hopper V1. After lock hopper IV2A is full, the conveying valve I is closed. Then, the conveying valve II between lock hopper IIV2B and feed hopper V3 is opened to allow biomass powder in lock hopper IIV2B to enter feed hopper V3. After lock hopper IIV2B is unloaded, the conveying valve II is closed.

[0079] In S3, during unloading, the pressurizing valve between lock hoppers IV2A and IIV2B is opened to equalize the pressure between them. The pressure inside lock hopper IV2A rises to a certain value, while the pressure inside lock hopper IIV2B decreases to a certain value. Then, the pressurizing valve between lock hoppers IV2A and IIV2B is closed, stopping the pressure equalization. Lock hopper IV2A is then repressurized using pressurizing air to make the pressure inside lock hopper IV2A equal to the pressure inside feed hopper V3. This process also affects the pressure distribution within the lock hoppers. IIV2B undergoes secondary depressurization to make the pressure inside the lock hopper IIV2B equal to the pressure inside the low-pressure silo V1. Then, the conveying valve II between the lock hopper IV2A and the feed silo V3 is opened, allowing the biomass powder in the lock hopper IV2A to enter the feed silo V3. After the lock hopper IV2A is unloaded, the conveying valve II is closed. Then, the conveying valve I between the low-pressure silo V1 and the lock hopper IIV2B is opened, allowing the biomass powder to enter the lock hopper IIV2B from the low-pressure silo V1. After the lock hopper IIV2B is full, the conveying valve I is closed.

[0080] In this embodiment, when the number of lock hoppers V2 is even, the pressure equalization tank V6 can be cancelled. Two lock hoppers V2 are used as a group, which are pressure equalization tanks for each other. That is, one lock hopper V2 that is filled with biomass powder from the low-pressure silo V1 is pressure equalized with another lock hopper V2 that has unloaded material into the feed silo V3. Then, they are connected to the high-pressure aeration tank V4 and the low-pressure tank V7 respectively.

[0081] Example 4:

[0082] Based on Example 3, referring to Figure 1 As shown, taking the production of green methanol by supplementing sufficient green hydrogen in the biomass gasification fuel production as an example, the biomass flow rate is calculated based on 60 t / h of dried biomass powder, and 35,000 Nm³ of hydrogen is added. 3 / h, with an annual methanol production of 350,000 tons, and a reaction tail gas (methanol off-gas) volume of approximately 4500 Nm³. 3 / h, the density of biomass powder is approximately 500 kg / m³. 3The system employs a double-lock hopper (V2), with each hopper feeding once every 30 minutes. Each hopper has a volume of approximately 35 cubic meters. The gasifier in the fluidized bed system (M1) operates at a pressure of 3.0 MPa, and the feed hopper (V3) operates at a pressure of 4.0 MPa. The pressurizing gas is methanol release gas, and the conveying gas is a mixture of methanol release gas and syngas. The dried biomass powder enters the low-pressure hopper (V1), which is sealed with nitrogen. The conveying valve I between the low-pressure hopper (V1) and the hopper (IV2A) that has been depressurized and is now in the low-pressure tank (V7) is opened. Biomass powder flows from the low-pressure hopper (V1) into the hopper (IV2A). Once the hopper (IV2A) is full, it is disconnected from both the low-pressure hopper (V1) and the low-pressure tank (V7). Simultaneously, the hopper (IIV2B), also filled with biomass powder, unloads into the feed hopper (V3) and closes the conveying valve II. Then, open the pressurizing valve between lock hopper IV2A and lock hopper IIV2B to equalize the pressure. After equalization, the pressure is 2.6 MPa. Disconnect the pressurizing valve between lock hopper IV2A and lock hopper IIV2B, and then connect lock hopper IV2A to the high-pressure inflation tank V4, allowing the high-pressure inflation tank V4 to pressurize lock hopper IV2A to 4.0 MPa. When the pressure of lock hopper IV2A is the same as the pressure of feed hopper V3, open the conveying valve II between lock hopper IV2A and feed hopper V3, allowing the biomass powder in lock hopper IV2A to enter feed hopper V3. After lock hopper IV2A has finished unloading, close the conveying valve II. At the same time, lock hopper IIV2B completes the depressurization to the low-pressure tank V7 and feeds material from the low-pressure hopper V1. Then, open the pressurizing valve between lock hopper IIV2B and lock hopper IV2A to equalize the pressure, and repeat this cycle. The low-pressure tank V7 gas external recovery system has a pressure control slightly lower than that of the low-pressure silo V1. The pressurization gas consumption and release gas of lock hoppers IV2A and IIV2B is approximately 4200 Nm³. 3 / h, the external recovery system pressurizes approximately 3700 Nm³ of gas. 3 / h.

[0083] Methanol purge gas and compressed synthesis gas enter the high-pressure conveying gas tank V5, and then the biomass powder is sent from the feed hopper V3 to the fluidized bed system M1 via the pneumatic conveying mechanism C1, with a conveying gas flow rate of 15000 Nm³. 3 / h, of which the exhaust gas is 300Nm 3 / h, synthesis gas 14700 Nm 3 / h.

[0084] The crude syngas in the outflow bed system M1 has a pressure of approximately 2.9 MPa, a temperature of approximately 190°C, and a flow rate of approximately 80,000 Nm³. 3 / h (dry basis) enters the desulfurization module of the syngas purification system M2 for desulfurization. The syngas after sulfide removal in the syngas purification system M2 has a pressure of approximately 2.8 MPa and a temperature of approximately 40℃, and is divided into two streams, one with a flow rate of 14700 Nm³ / h. 3Syngas produced per hour is compressed to 4.0 MPa by syngas compressor C2 and then sent to high-pressure delivery gas tank V5, with the remaining flow rate at 65300 Nm³ / h. 3 / h synthesis gas and the added 35000Nm 3 The hydrogen-to-carbon ratio is adjusted to approximately 2.05, and then compressed to approximately 8.0 MPa before entering reaction system M3. Reaction system M3 produces approximately 350,000 tons / year of methanol. The methanol purge gas pressure is 7.5 MPa, the temperature is approximately 40°C, and the flow rate is approximately 4500 Nm³. 3 / h, divided into two paths, one with a flow rate of 4200 Nm 3 The purge gas, at a rate of / h, is reduced to 4.0 MPa and then sent to the high-pressure charging tank V4, with the remaining flow rate at 300 Nm³ / h. 3 The purge gas, at a rate of / h, is reduced to 4.0 MPa and then sent to the high-pressure delivery gas tank V5.

[0085] Compared with the existing technology that uses high-concentration carbon dioxide to transport biomass powder into a gas flow bed system to produce methanol, this embodiment reduces the steam consumption for conversion by about 15 t / h, the steam consumption for carbon dioxide removal by about 30 t / h, the consumption of circulating water by 1500 t / h, and the carbon dioxide compression work by 2700 kWh / h, while saving about 40 million RMB in investment for conversion and decarbonization.

[0086] Example 5:

[0087] Based on Example 1 or 2, refer to Figure 2 As shown, taking the production of green methanol from biomass gasification without the addition of green hydrogen as an example, with a biomass flow rate of 30 t / h of dried biomass powder, the annual methanol production is 110,000 tons, and the reaction tail gas, i.e., the methanol off-gas, is approximately 1500 Nm³. 3 / h, the density of biomass powder is approximately 500 kg / m³. 3It adopts a single lock hopper, with a feeding time of once every 30 minutes. The lock hopper has a volume of about 35 cubic meters. The gasifier operates at a pressure of 3.0 MPa, and the feed hopper V3 operates at a pressure of 4.0 MPa. The pressurizing gas is carbon dioxide gas decarbonized from the syngas purification system M2, and the conveying gas is methanol off-gas plus part of the syngas decarbonized from the syngas purification system M2. Dry biomass powder enters low-pressure silo V1, which is sealed with carbon dioxide gas. The conveying valve I between low-pressure silo V1 and the depressurized lock hopper V2 is opened, allowing the biomass powder to flow from V1 into V2. After V2 is full, the connection between V2 and V1 is disconnected. Then, the pressurization valve between V2 and the pressure equalization tank V6 is opened for pressure equalization. After equalization, the pressure is 2.6 MPa. The pressurization valve between V2 and V6 is then disconnected, and the connection between V2 and the high-pressure inflation tank V4 is opened, allowing the high-pressure inflation tank V4 to supply gas to V2. The process begins with pressurization to 4.0 MPa. When the pressure in lock hopper V2 equals that in feed hopper V3, the conveying valve II between lock hopper V2 and feed hopper V3 is opened, allowing biomass powder from lock hopper V2 to enter feed hopper V3. After material is discharged from lock hopper V2, conveying valve II is closed. Then, the pressurization valve between lock hopper V2 and pressure equalization tank V6 is opened for pressure equalization. The pressurization valve between lock hopper V2 and pressure equalization tank V6 is then closed. Next, the vent valve between lock hopper V2 and low-pressure hopper V1 is opened to release pressure below that of low-pressure hopper V1. Finally, the feed valve between low-pressure hopper V1 and lock hopper V2 is opened to feed material into lock hopper V2. This cycle is repeated. The pressurization process for lock hopper V2 consumes approximately 2100 Nm³ of carbon dioxide. 3 / h, approximately 1800 Nm³ of carbon dioxide gas is released. 3 / h.

[0088] Part of the methanol off-gas and the decarbonized syngas from the purification system M2 enter the high-pressure conveying gas tank V5. Then, the biomass powder is conveyed from the feed hopper V3 to the fluidized bed system M1 via the pneumatic conveying mechanism C1, with a conveying gas flow rate of 7500 Nm³. 3 / h, of which the purge gas is 1000Nm 3 / h, synthesis gas 6500 Nm 3 / h.

[0089] The crude syngas in the outflow bed system M1 has a pressure of approximately 2.9 MPa, a temperature of approximately 190°C, and a flow rate of approximately 37,800 Nm³. 3 / h (dry basis), entering the conversion module of syngas purification system M2, where approximately 54% of carbon monoxide is converted into hydrogen and carbon dioxide, with a post-conversion flow rate of approximately 50,000 Nm³. 3 / h (dry basis), then through desulfurization and decarbonization to remove sulfides and approximately 12300 Nm. 3 / h carbon dioxide, 2100Nm 3The carbon dioxide, after being pressurized by the carbon dioxide compressor C3, is sent to the high-pressure charging tank V4, where most of the carbon dioxide is emitted locally. The flow rate of the syngas after carbon dioxide removal is approximately 37,700 Nm³. 3 The flow rate is approximately 2.05 / h, the hydrogen-to-carbon ratio is approximately 2.8 MPa, the pressure is approximately 2.8 MPa, and the temperature is approximately 40°C. It is divided into two streams, one with a flow rate of 6500 Nm³ / h. 3 The syngas is compressed to 4.0 MPa by syngas compressor C2 and then sent to high-pressure delivery gas tank V5, with the remaining flow rate being 31200 Nm³ / h. 3 The synthesis gas, compressed to approximately 6.0 MPa by a compressor, enters reaction system M3. Reaction system M3 produces approximately 110,000 tons / year of methanol. The purge gas pressure is 5.5 MPa, the temperature is approximately 40°C, and the flow rate is approximately 1500 Nm³. 3 / h, divided into two paths, one with a flow rate of 1000Nm 3 / h of vented gas, after being depressurized to 4.0 MPa, is sent into the high-pressure charging tank V4, with the remaining flow rate at 500 Nm³ / h. 3 / h venting gas recovery system.

[0090] Compared with the existing technology that uses high-concentration carbon dioxide to transport biomass into a gas flow bed to produce methanol, this embodiment reduces carbon dioxide vapor output by about 10 t / h, reduces circulating water consumption by 500 t / h, and reduces carbon dioxide compression work by 1350 kWh / h.

[0091] Example 6:

[0092] Based on Example 1 or 2, refer to Figure 3 As shown, taking the process of supplementing green hydrogen to produce SAF (green jet fuel) during biomass gasification for fuel production as an example, with a biomass flow rate of 30 t / h of dried biomass powder, the annual production of SAF products is approximately 100,000 tons, and the reaction tail gas, i.e., the low-carbon hydrocarbon release gas, is approximately 8500 Nm³. 3 / h, the density of biomass powder is approximately 500 kg / m³. 3A single-lock hopper is used, with feeding every 30 minutes. The hopper volume is approximately 35 cubic meters. The gasifier operating pressure is 3.0 MPa, and the feed hopper V3 operating pressure is 4.0 MPa. Both the pressurizing gas and the conveying gas are low-carbon hydrocarbon release gas from the reaction system M3. The dried biomass powder enters the low-pressure silo V1. The sealing gas for low-pressure silo V1 is carbon dioxide gas from the decarbonization module. The conveying valve I between low-pressure silo V1 and the lock hopper V2 (which has been depressurized and is now in the low-pressure tank V7) is opened, allowing the biomass powder to enter from low-pressure silo V1 into lock hopper V2. After lock hopper V2 is full, the connection between it and low-pressure silo V1 and low-pressure tank V7 is disconnected. Then, the pressurizing valve between lock hopper V2 and pressure equalization tank V6 is opened for pressure equalization. After pressure equalization, the pressure is 2.6 MPa. The pressurizing valve between lock hopper V2 and pressure equalization tank V6 is then disconnected, and the connection between lock hopper V2 and high-pressure charging tank V4 is opened to allow high-pressure charging. The air tank V4 pressurizes the lock hopper V2 to 4.0 MPa. When the pressure in lock hopper V2 is the same as the pressure in feed hopper V3, the conveying valve II between lock hopper V2 and feed hopper V3 is opened, allowing the biomass powder in lock hopper V2 to enter feed hopper V3. After lock hopper V2 unloads, conveying valve II is closed. Then, the pressurizing air valve between lock hopper V2 and pressure equalization tank V6 is opened for pressure equalization. After pressure equalization, the pressurizing air valve between lock hopper V2 and pressure equalization tank V6 is closed. Then, the vent valve of lock hopper V2 is opened to release pressure into low-pressure tank V7. After depressurization, the conveying valve I between low-pressure hopper V1 and lock hopper V2 is opened to feed material into lock hopper V2, and this cycle continues. The depressurized air stored in low-pressure tank V7 is divided into two paths, one at 1100 Nm³. 3 / h After being pressurized by the recovery gas booster C4, it is returned to the high-pressure filling tank V4 for reuse, with a flow rate of 700Nm. 3 The lock hopper V2 requires approximately 2100 Nm of pressurized air for recycling. 3 / h, of which approximately 1000 Nm 3 / h represents the off-gas from low-carbon hydrocarbons.

[0093] The pressurized low-carbon hydrocarbon purge gas from reaction system M3 enters high-pressure aeration tank V4, and then the biomass powder is conveyed from feed hopper V3 into fluidized bed system M1 via pneumatic conveying mechanism C1, with a conveying gas flow rate of 7500 Nm³. 3 / h.

[0094] The crude syngas in the outflow bed system M1 has a pressure of approximately 2.9 MPa, a temperature of approximately 190°C, and a flow rate of approximately 49,000 Nm³. 3 / h (dry basis), enters the desulfurization and decarbonization modules of the syngas purification system M2, where sulfides are removed and approximately 4000 Nm³ of gas is discharged. 3 The carbon dioxide concentration is approximately 45,000 Nm³ / h, and the syngas flow rate after carbon dioxide removal is approximately 45,000 Nm³ / h. 3 / h, hydrogen replenishment flow rate 35000 Nm 3 / h, total gas volume approximately 80000 Nm3 The hydrogen-to-carbon ratio is approximately 2.05, the pressure is approximately 2.8 MPa, and the temperature is approximately 40°C. After being compressed to approximately 3.5 MPa by a compressor, it enters reaction system M3. Reaction system M3 produces approximately 100,000 tons / year of aviation kerosene. Its low-carbon hydrocarbon purge gas pressure is 2.8 MPa, the temperature is approximately 40°C, and the flow rate is approximately 8500 Nm³. 3 / h, after being pressurized to 4.0Mpa by the tail gas compressor C5 of the reaction system, it is sent into the high-pressure charging tank V4.

[0095] Compared with the existing technology that uses high-concentration carbon dioxide to transport biomass powder into the fluidized bed system to produce SAF products, this embodiment reduces the steam consumption for conversion by about 4 t / h, the steam consumption for carbon dioxide removal by about 12 t / h, the consumption of circulating water by 600 t / h, and the carbon dioxide compression work by 1200 kWh / h. At the same time, it saves about 20 million yuan in investment for conversion and decarbonization. The conversion of low-carbon hydrocarbons in the low-carbon hydrocarbon purge gas into syngas can increase the production of SAF products by 15%, that is, increase the production of SAF products by 15,000 tons / year.

[0096] Example 7:

[0097] Based on Example 1 or 2, refer to Figure 4 As shown, taking the production of SAF (green jet fuel) from biomass gasification without the addition of green hydrogen as an example, with a biomass flow rate of 30 t / h of dried biomass powder, the annual production of SAF products is 43,000 tons, and the reaction tail gas, i.e., the low-carbon hydrocarbon release gas, is about 3400 Nm³. 3 / h, the density of biomass powder is approximately 500 kg / m³. 3It adopts a single lock hopper, with a feeding time of once every 30 minutes. The lock hopper volume is about 35 cubic meters. The gasifier operating pressure is 3.0 MPa, and the feed hopper V3 operating pressure is 4.0 MPa. The pressurizing gas is carbon dioxide gas decarbonized from the syngas purification system M2, and the conveying gas is low-carbon hydrocarbon off-gas from the reaction system M3 plus syngas decarbonized from the syngas purification system M2. Dry biomass powder enters the low-pressure silo V1, which is sealed with carbon dioxide gas. The conveying valve I between the low-pressure silo V1 and the lock hopper V2 (which has been depressurized) is opened, allowing the biomass powder to flow from the silo into the lock hopper V2. After the lock hopper V2 is full, its connection to the low-pressure silo V1 is disconnected. Then, the pressurization valve between the lock hopper V2 and the pressure equalization tank V6 is opened for pressure equalization. After equalization, the pressure is 2.6 MPa. The pressurization valve between the lock hopper V2 and the pressure equalization tank V6 is then disconnected. Finally, the lock hopper V2 is connected to the high-pressure inflation tank V4, allowing the high-pressure inflation tank V4 to supply pressure to the lock hopper V2. Pressurize to 4.0 MPa. When the pressure in lock hopper V2 is the same as the pressure in feed hopper V3, open conveyor valve II between lock hopper V2 and feed hopper V3. Biomass powder in lock hopper V2 enters feed hopper V3. After the material in lock hopper V2 is discharged, close conveyor valve II. Then, open the pressurizing valve between lock hopper V2 and pressure equalization tank V6 to equalize the pressure. Disconnect the pressurizing valve between lock hopper V2 and pressure equalization tank V6. Then, open the vent valve connecting lock hopper V2 to low-pressure hopper V1 to release pressure below that of low-pressure hopper V1. Then, open conveyor valve I between low-pressure hopper V1 and lock hopper V2 to feed material into lock hopper V2. This cycle continues. The pressurizing gas consumption of lock hopper V2 is approximately 2100 Nm³ of carbon dioxide. 3 / h, approximately 1800 Nm³ of carbon dioxide gas is released. 3 / h.

[0098] Part of the low-carbon hydrocarbon off-gas from reaction system M3 is mixed with part of the decarbonized syngas from syngas purification system M2. This mixture is then pressurized to 4.0 MPa by reaction system tail gas compressor C5 and enters high-pressure conveying gas tank V5. From there, biomass powder is conveyed from feed hopper V3 to fluidized bed system M1 via pneumatic conveying mechanism C1. The conveying gas flow rate is 7500 Nm³. 3 / h, of which 3000 Nm³ of low-carbon hydrocarbon purge gas 3 / h, synthesis gas 4500 Nm 3 / h.

[0099] The crude syngas in the outflow bed system M1 has a pressure of approximately 2.9 MPa, a temperature of approximately 190°C, and a flow rate of approximately 38,000 Nm³. 3 / h (dry basis), the conversion module of the syngas purification system M2 converts approximately 54% of the carbon monoxide into hydrogen and carbon dioxide, with a post-conversion flow rate of approximately 49,000 Nm³. 3 / h (dry basis), then through desulfurization and decarbonization to remove sulfides and approximately 14500 Nm. 3 / h carbon dioxide, 2100Nm 3 The carbon dioxide, after being pressurized by the carbon dioxide compressor C3, is sent to the high-pressure charging tank V4, where most of the carbon dioxide is emitted locally. The flow rate of the syngas after carbon dioxide removal is approximately 34,500 Nm³. 3 The flow rate is approximately 2.05 / h, the hydrogen-to-carbon ratio is approximately 2.8 MPa, the pressure is approximately 2.8 MPa, and the temperature is approximately 40°C. It is divided into two streams, one with a flow rate of 4500 Nm³ / h. 3 / h of syngas is used as transport gas to the reactor system's tail gas compressor C5 for pressurization, with the remaining flow rate at 30000 Nm³. 3 The syngas, compressed to approximately 3.5 MPa by a compressor, enters reaction system M3. Reaction system M3 produces approximately 43,000 tons / year of jet fuel, with the low-carbon hydrocarbon purge gas having a pressure of 2.8 MPa, a temperature of approximately 40°C, and a flow rate of approximately 3400 Nm³. 3 / h, divided into two paths, one with a flow rate of 3000 Nm 3 The mixture is combined with a portion of the syngas and pressurized to 4.0 MPa by the tail gas compressor C5 of the reaction system before being sent to the high-pressure delivery gas tank V5, with a flow rate of 400 Nm³ / h. 3 / h is sent to the recycling system for reuse.

[0100] Compared with the existing technology that uses high-concentration carbon dioxide to transport biomass powder into a gas flow bed to produce SAF products, this embodiment reduces the amount of carbon dioxide vapor removed by about 11 t / h, reduces the consumption of circulating water by 550 t / h, reduces the carbon dioxide compression work by 1100 kWh / h, and saves about 5 million yuan in decarbonization investment. The conversion of low-carbon hydrocarbons in the low-carbon hydrocarbon purge gas into syngas can increase the production of SAF products by 15%, which means an additional 0.6 million tons / year of SAF products.

[0101] It should be noted that the above detailed descriptions are exemplary and intended to provide further explanation of this application. Unless otherwise specified, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application pertains.

[0102] It should be noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to limit the exemplary embodiments described in this application. As used herein, the singular form is intended to include the plural form as well, unless the context clearly indicates otherwise. Furthermore, it should be understood that when the terms "comprising" and / or "including" are used in this specification, they indicate the presence of features, steps, operations, devices, components, and / or combinations thereof.

[0103] It should be noted that the terms "first," "second," etc., used in the specification, claims, and accompanying drawings of this application are used to distinguish similar objects and are not necessarily used to describe a specific order or sequence. It should be understood that such terms can be used interchangeably where appropriate so that the embodiments of this application described herein can be implemented in sequences other than those illustrated or described herein.

[0104] Furthermore, the terms “comprising” and “having”, and any variations thereof, are intended to cover non-exclusive inclusion. For example, a process, method, system, product, or apparatus that includes a series of steps or units is not necessarily limited to those steps or units that are explicitly listed, but may include other steps or units that are not explicitly listed or that are inherent to such process, method, product, or apparatus.

[0105] For ease of description, spatial relative terms such as "above," "on top of," "on the upper surface of," "above," etc., are used herein to describe the spatial positional relationship of a device or feature as shown in the figures to other devices or features. It should be understood that spatial relative terms are intended to encompass different orientations in use or operation beyond the orientation of the device as described in the figures. For example, if the device in the figures were inverted, a device described as "above" or "on top of" other devices or structures would subsequently be positioned as "below" or "under" other devices or structures. Thus, the exemplary term "above" can include both "above" and "below." The device may also be positioned in other different ways, such as rotated 90 degrees or in other orientations, and the spatial relative descriptions used herein will be interpreted accordingly.

[0106] In the detailed description above, reference has been made to the accompanying drawings, which form part of this document. In the drawings, similar symbols typically identify similar parts unless the context otherwise indicates otherwise. The illustrated embodiments described in the detailed specification, drawings, and claims are not intended to be limiting. Other embodiments may be used and other changes may be made without departing from the spirit or scope of the subject matter presented herein.

[0107] The above description is merely a preferred embodiment of the present invention and is not intended to limit the invention. Various modifications and variations can be made to the present invention by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

Claims

1. A biomass gasification fuel production process, characterized in that: Includes the following steps: S1, Feeding; Dry biomass powder is fed into the low-pressure silo (V1), and sealing gas is introduced into the low-pressure silo (V1); S2, feeding; depressurize the lock hopper (V2) so that the pressure inside the lock hopper (V2) is equal to the pressure inside the low-pressure silo (V1), open the conveying valve I between the low-pressure silo (V1) and the lock hopper (V2) to allow biomass powder to enter the lock hopper (V2) from the low-pressure silo (V1). After the lock hopper (V2) is full, close the conveying valve I between the low-pressure silo (1) and the lock hopper (V2); S3, unloading; pressurize the lock hopper (V2) with pressurized air so that the pressure in the lock hopper (V2) is equal to the pressure in the feed hopper (V3), open the conveying valve II between the lock hopper (V2) and the feed hopper (V3) to allow the biomass powder in the lock hopper (V2) to enter the feed hopper (V3), and close the conveying valve II after unloading is completed; S4, repeat S2 to S3 at a set time interval; S5, Gas generation by the fluidized bed system; The pneumatic conveying mechanism (C1) sends the biomass powder in the feed hopper (V3) into the fluidized bed system (M1) through the conveying gas in the high-pressure conveying gas tank (V5). At the same time, the feed hopper (V3) is pressurized by pressurizing gas to maintain a constant pressure. The biomass powder and conveying gas entering the fluidized bed system (M1) react with the introduced oxygen to convert the biomass powder into crude syngas. S6, Purify Syngas; The crude syngas from the fluidized bed system (M1) is passed into the syngas purification system (M2) for purification to obtain the syngas required for producing synthetic products. S7, Production of Synthetic Products; Part of the syngas sent from the syngas purification system (M2) is sent into the reaction system (M3) to produce the desired synthetic products; After the reaction system (M3) produces the synthetic products, it generates reaction tail gas; in, In S1, the sealing gas is preferably carbon dioxide gas removed by the syngas purification system (M2), and if insufficient, it is supplemented by nitrogen gas from the outside. In S3 and S5, the pressurizing gas is the reaction tail gas generated by the reaction system (M3), and / or the crude synthesis gas generated by the synthesis gas purification system (M2), and / or the carbon dioxide gas removed by the synthesis gas purification system (M2); In S5, the transport gas is the syngas produced by the syngas purification system (M2) and / or the reaction tail gas produced by the reaction system (M3); When the flow rate of the reaction tail gas generated by the reaction system (M3) can meet the needs of pressurizing gas and conveying gas, the reaction tail gas generated by the reaction system (M3) shall be used first; when the flow rate of the reaction tail gas generated by the reaction system (M3) cannot meet the needs of pressurizing gas and conveying gas, the syngas purified by the syngas purification system (M2) shall be used first.

2. The biomass gasification fuel production process according to claim 1, characterized in that: In S2, when depressurizing the lock hopper (V2), the lock hopper (V2) is first pressure equalized, and then pressure is depressurized a second time; in S3, when pressurizing the lock hopper (V2), the lock hopper (V2) is first pressure equalized, and then pressurized by pressurizing gas.

3. The biomass gasification fuel production process according to claim 2, characterized in that: There is one lock bucket (V2), which is connected to the equalizing tank (V6); In S2, when depressurizing the lock hopper (V2), the lock hopper (V2) is first depressurized through the pressure equalization tank (V6), and then depressurized a second time. When depressurizing the lock hopper (V2), the pressurization valve between the lock hopper (V2) and the pressure equalization tank (V6) is first opened, and the lock hopper (V2) is depressurized through the pressure equalization tank (V6), and then depressurized a second time until the target set pressure is reached in the lock hopper (V2). In S3, when pressurizing the lock hopper (V2), the lock hopper (V2) is first pressurized through the pressure equalization tank (V6), and then pressurized through the pressurizing air. When pressurizing the lock hopper (V2), the pressurizing air valve between the lock hopper (V2) and the pressure equalization tank (V6) is first opened, and the lock hopper (V2) is pressurized through the pressure equalization tank (V6). Then the lock hopper (V2) is pressurized through the pressurizing air until the pressure inside the lock hopper (V2) is the same as the pressure inside the feed hopper (V3).

4. The biomass gasification fuel production process according to claim 2, characterized in that: There are two lock hoppers (V2), namely lock hopper I (V2A) and lock hopper II (V2B). Lock hopper I (V2A) and lock hopper II (V2B) are respectively connected to the low-pressure silo (V1), the low-pressure tank (V7) and the feed silo (V3); In S2, during feeding, firstly, the pressurizing valve between lock hopper I (V2A) and lock hopper II (V2B) is opened to equalize the pressure between them. The pressure in lock hopper I (V2A) decreases to a certain value, and the pressure in lock hopper II (V2B) increases to a certain value. Then, the pressurizing valve between lock hopper I (V2A) and lock hopper II (V2B) is closed to stop the pressure equalization. Next, lock hopper I (V2A) is depressurized a second time to make the pressure inside lock hopper I (V2A) equal to the pressure inside the low-pressure hopper (V1). The pressurized air then balances the pressure in the lock hopper. Bucket II (V2B) is pressurized a second time to make the pressure inside Bucket II (V2B) equal to the pressure inside the feed hopper (V3). Then, the conveying valve I between the low-pressure hopper (V1) and Bucket I (V2A) is opened to allow biomass powder to enter Bucket I (V2A) from the low-pressure hopper (V1). After Bucket I (V2A) is full, the conveying valve I is closed, and the conveying valve II between Bucket II (V2B) and the feed hopper (V3) is opened to allow biomass powder in Bucket II (V2B) to enter the feed hopper (V3). After Bucket II (V2B) is unloaded, the conveying valve II is closed. In S3, during unloading, the pressurizing valve between lock hopper I (V2A) and lock hopper II (V2B) is opened to equalize the pressure between them. The pressure in lock hopper I (V2A) rises to a certain value, and the pressure in lock hopper II (V2B) decreases to a certain value. Then, the pressurizing valve between lock hopper I (V2A) and lock hopper II (V2B) is closed, stopping the pressure equalization. Lock hopper I (V2A) is then repressurized using pressurizing air to make the pressure in lock hopper I (V2A) equal to the pressure in the feed hopper (V3), and the pressure in lock hopper II... (V2B) is depressurized a second time to make the pressure inside lock hopper II (V2B) equal to the pressure inside the low-pressure silo (V1). The conveying valve II between lock hopper I (V2A) and feed silo (V3) is opened to allow the biomass powder in lock hopper I (V2A) to enter feed silo (V3). After lock hopper I (V2A) is unloaded, the conveying valve II is closed. The conveying valve I between low-pressure silo (V1) and lock hopper II (V2B) is opened to allow the biomass powder to enter lock hopper II (V2B) from low-pressure silo (V1). After lock hopper II (V2B) is full, the conveying valve I is closed.

5. The biomass gasification fuel production process according to claim 1, characterized in that: The lock bucket (V2) is connected to the low-pressure tank (V7). In S2, the lock bucket (V2) is depressurized a second time through the low-pressure tank (V7).

6. The biomass gasification fuel production process according to claim 1, characterized in that: A vent valve is provided between the lock hopper (V2) and the low-pressure silo (V1). In S2, the vent valve is opened to perform secondary pressure relief on the lock hopper (V2), so that the pressure inside the lock hopper (V2) is released into the low-pressure silo (V1).

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