Biomass pretreatment continuous flow system and method based on solid acid packed bed tubular reactor

Abstract

The invention relates to the field of new energy technology systems, in particular to a biomass pretreatment continuous flow system based on a solid acid packed bed tubular reactor, which comprises a main reactor, an automatic control system, an air cooling system and a raw material supply and product collection system, the automatic control system comprises a heat conduction oil circulating system, a temperature monitoring control system, a material flow monitoring control system, a pressure monitoring control system and an electric control assembly, and the main reactor is a double-jacket type packed bed tubular reactor; the invention further relates to a biomass pretreatment continuous flow method based on the solid acid packed bed tubular reactor. The double-jacket type reaction tube promotes heat exchange, so that the temperature of the reaction chamber is more uniform, the cellulose conversion rate and the glucose yield are improved, the safety and the stability are enhanced, the fluid turbulence and the radial temperature uniformity are increased, the reaction flow distribution is improved, the blockage is prevented, the maintenance is easy, the datamation controllability is realized, and the reaction process is optimized.

Description

Technical Field

[0001] The present invention relates to the field of new energy technology, and in particular to a biomass pretreatment continuous flow system based on a solid acid packed bed tubular reactor and a method thereof. Background Art

[0002] Biomass energy is a very important renewable energy source. Among non-food biomass resources, lignocellulose has attracted more and more attention due to its rich storage content, abundant sources and short growth cycle. However, it is limited by the dense structure of lignocellulosic biomass, such as cellulose wrapped in hemicellulose and lignin, which is not easy to access, and anaerobic microorganisms are inefficient in hydrolyzing macromolecules. Therefore, it is necessary to depolymerize it into small molecular sugars through pretreatment to improve the accessibility of cellulose.

[0003] The traditional method is to use homogeneous acid to pretreat biomass in batch reactors. However, the use of homogeneous acid for pretreatment has problems such as strong corrosiveness, environmental unfriendliness, and difficulty in separation and recovery. Batch processing technology also has bottleneck problems such as slow temperature response and difficulty in continuous production, which restricts the continuous and efficient catalytic conversion of biomass.

[0004] The continuous flow system is a method to solve the above problems. The continuous flow reactor has the characteristics of high heat transfer efficiency, continuous production, low operating cost, stable product quality, etc., which is conducive to continuous and stable production on an industrial scale. Although there are many studies on catalytic conversion in microreactors, there are few systematic studies on the continuous catalytic conversion of biomass, and the continuous catalytic conversion of biomass cannot be achieved. Summary of the invention

[0005] The purpose of the present invention is to provide a biomass pretreatment continuous flow system and method based on a solid acid packed bed tubular reactor. Compared with the shortcomings of homogeneous acid, solid acid has the advantages of being environmentally friendly, highly active and selective, having stable physical and chemical properties, and being easy to recycle. In addition, due to the strong acidity, water resistance and porous structure of solid acid, the substrate is allowed to enter and contact the active sites in the pores of the solid material, resulting in efficient catalytic hydrolysis reaction. It has broad prospects for application in the hydrolysis of lignocellulosic biomass. Compared with batch reactions, continuous flow reactors have the characteristics of high heat transfer efficiency, continuous production, low operating costs and high product quality stability, and are more suitable for the requirements of continuous and stable production on an industrial scale, so as to solve the problems raised in the above-mentioned background technology.

[0006] To achieve the above object, the present invention provides the following technical solutions:

[0007] A biomass pretreatment continuous flow system based on a solid acid packed bed tubular reactor comprises a main reactor, an automated control system, an air cooling system, and a raw material supply and product collection system. The automated control system comprises a heat transfer oil circulation system, a temperature monitoring control system, a material flow monitoring control system, a pressure monitoring control system, and an electronic control component. The main reactor is a double-jacketed packed bed tubular reactor, which consists of an outer shell and three layers of pipes, namely an outer tube, a middle tube, and an inner tube, and four flow guide ducts.

[0008] Preferably, the flow guide conduit is fixed by a conduit chuck at the feed port and fixed by an annular fastener at the discharge port, a through hole is formed at the upper portion of the outer tube and connected to the first oil guide tube, a through hole is formed at the lower portion of the outer tube and connected to the fourth oil guide tube, the upper and lower portions of the inner tube are connected to the outer tube through the second oil guide tube and the third oil guide tube respectively, for exchanging heat transfer oil, the gap area between the inner wall of the middle tube and the outer wall of the inner tube is a reaction chamber, and the reaction chamber is filled with a fixed acid filler;

[0009] A feed pipe and a discharge pipe are respectively arranged at both ends of the main reactor. The feed pipe and the discharge pipe are threaded at the connection with the main reactor and are equipped with corresponding conical fasteners. Flange 1 and flange 2 are respectively arranged on the feed pipe and the discharge pipe. Flange 1 and flange 2 are connected to the inlet and outlet ports of the main reactor by bolts.

[0010] Preferably, a screen 1 is provided between the flange 1 and the feed port of the main reactor, and a screen 2 is provided between the flange 2 and the discharge port of the main reactor.

[0011] Preferably, the heat transfer oil circulation system comprises a heat transfer oil tank, a heat transfer oil heating device, a circulation pump, a bypass valve and a heat transfer oil pipeline, and the two ends of the heat transfer oil pipeline are respectively connected to the first oil pipe and the fourth oil pipe; the temperature monitoring and control system comprises an outlet end thermocouple and an inlet end thermocouple, and the outlet end thermocouple and the inlet end thermocouple are respectively installed at the inlet and outlet ports of the main reactor; the material flow monitoring and control system comprises a liquid phase pump and a precision flowmeter; the pressure monitoring and control system comprises a back pressure valve 1, a pressure dividing valve, a back pressure valve 2, and a pressure sensor 1 and a pressure sensor 2 at the two ports of the main reactor; the raw material supply and product collection system comprises a product collection system and a raw material supply system.

[0012] Preferably, the inner tube, the middle tube and the outer tube are three coaxial tubes, and the four flow guide tubes are symmetrically distributed on the circular cross-section of the reaction chamber.

[0013] Preferably, the inner wall of the middle tube is provided with threads, and a heat-insulating layer made of heat-insulating material is filled between the outer tube and the outer shell.

[0014] Preferably, the inlet and outlet ports of the main reactor are both disc-shaped and consistent in size with flange one and flange two, and have four symmetrically distributed through holes for inserting connecting parts. The surfaces of flange one and flange two each have four symmetrically distributed through holes, the center of which is a thin tube with a threaded end, and the diameter of the tube is consistent with that of the feed pipe and the discharge pipe.

[0015] A continuous flow method for biomass pretreatment based on a solid acid packed bed tubular reactor comprises the following steps:

[0016] S1. When the system is running, the heat transfer oil in the heat transfer oil tank is pumped out into the heat transfer oil pipeline by the circulating pump. During the pumping process, the heat transfer oil is heated by the heat transfer oil heating device, wherein the heat transfer oil heating device heats the heat transfer oil by industrial waste heat or solar energy heating. The heated high-temperature heat transfer oil flows into the lower part of the outer tube of the main reactor through the fourth oil guide pipe, flows into the inner tube through the third oil guide pipe, and after filling the inner tube, the heat transfer oil is collected into the upper part of the outer tube through the second oil guide pipe, and flows out through the first oil guide pipe;

[0017] S2. The raw materials in the raw material supply system are pumped into the feed pipe and into the reaction chamber through a liquid phase pump. The precision flow meter calculates the pumping amount, and the electronic control component controls the pumping amount of the liquid phase pump. During the reaction, the outlet thermocouple and the inlet thermocouple respectively detect the temperature of the outlet and inlet ends of the reaction chamber, and the electronic control component performs temperature control. The pressure sensor 1 and the pressure sensor 2 respectively detect the pressure at the outlet and inlet of the reaction chamber. The electronic control component adjusts the fluid pressure in the pipeline by controlling the valve opening of the back pressure valve 1, the back pressure valve 2, and the pressure dividing valve;

[0018] S3. The reaction product flows out through the discharge pipe, is cooled by the air cooling system, and finally flows into the product collection system.

[0019] Preferably, the method for the electronic control component to control the pumping amount of the liquid phase pump is as follows:

[0020] Use a precision flow meter to measure the pumping volume, and its reading is Q measured The electronic control component controls the pumping volume Q according to the preset set and the actual measured pumping volume Q measured To control the pumping amount of the liquid phase pump;

[0021] Control algorithm:

[0022] Calculation error: e Q =Q set -Q measured ;

[0023] The proportional-integral-derivative control algorithm is used to adjust the pump speed of the liquid phase pump. The output of the electronic control component is expressed as:

[0024]

[0025] Among them, K p is the proportional gain, K i is the integral gain, K d is the differential gain.

[0026] Preferably, the temperature control method of the electric control component is as follows:

[0027] The outlet thermocouple and the inlet thermocouple are used to detect the temperature T in the reaction chamber respectively. out and T in The electronic control components are set according to the preset temperature T set and the actual measured temperature to adjust the heating of the thermal oil;

[0028] Control algorithm:

[0029] For the outlet and inlet, calculate the temperature error: eT out =T set -T out and eT in =T set -T in ;

[0030] The proportional-integral-differential control algorithm is used to adjust the output of the heating of the thermal oil. The output of the electronic control component is expressed as:

[0031]

[0032]

[0033] Among them, K p is the proportional gain, K i is the integral gain, K d is the differential gain;

[0034] The method for adjusting the fluid pressure in the pipeline by the electronic control component is as follows:

[0035] Use pressure sensor 1 and pressure sensor 2 to detect the pressure P at the outlet and inlet of the reaction chamber respectively. out and P in The electronic control component adjusts the fluid pressure in the pipeline by controlling the valve opening of the back pressure valve 1, the back pressure valve 2 and the pressure dividing valve;

[0036] Control algorithm:

[0037] For the outlet and inlet, calculate the pressure error separately: eP out =P set -P out and eP in =P set -P in ;

[0038] The proportional-integral-differential control algorithm is used to adjust the opening of the back pressure valve and the pressure dividing valve. The output of the electronic control component is expressed as:

[0039]

[0040]

[0041] Among them, K p is the proportional gain, K i is the integral gain, K d is the differential gain; the opening of the back pressure valve and the pressure dividing valve uP out and uP in Can be converted into valve control signal.

[0042] Compared with the prior art, the present invention has the following beneficial effects:

[0043] By setting the main reactor reaction tube as a double-jacketed structure, the outer tube and the inner tube can realize the circulation of heat transfer oil, and sufficient heat exchange will provide enough heat for the chemical reaction in the reaction chamber. At the same time, this sufficient heat exchange makes the temperature distribution in the reaction chamber more uniform compared with the existing straight tube reactor, which can effectively avoid the low cellulose conversion rate caused by uneven temperature distribution during the reaction of the existing reactor, and the decrease in glucose yield caused by the decomposition of product glucose;

[0044] By setting the middle tube and the inner tube as hollow cylindrical four-end threaded tubes with openings at both ends, the center of gravity shift during operation, such as in the case of three-end threaded tubes, can be effectively avoided, greatly improving safety and reaction stability;

[0045] The arrangement of threads on the inner wall of the reaction chamber is conducive to the formation of secondary flows such as centrifugal flow and vortex flow, thereby significantly increasing the turbulence of the fluid in the tube and making the radial temperature distribution more uniform.

[0046] By adding a flow guide conduit in the reaction chamber, an effective support is provided for the fixed acid filler composed of solid acid particles next to it, and a free passage with high porosity is generated around it, thereby improving the axial distribution of the reaction flow in the tube and avoiding the problem that the continuous flow system cannot work normally due to blockage inside the reaction tube. At the same time, the conduit chuck setting of the flow guide conduit makes it easy to disassemble and maintain;

[0047] Through the intervention of the automated control system, the reaction process can be digitally controlled. Real-time temperature, pressure and other values ​​can reflect the progress of the reaction system, and each value can be finely adjusted to adapt to the reaction process. BRIEF DESCRIPTION OF THE DRAWINGS

[0048] Figure 1 It is a system workflow diagram of the present invention;

[0049] Figure 2 is a cross-sectional view of the main reactor of the present invention;

[0050] Figure 3 It is a three-dimensional diagram of the main reactor of the present invention.

[0051] Figure 1 In: 1. Product collection system; 2. Back pressure valve 1; 3. Pressure dividing valve; 4. Air cooling system; 5. Back pressure valve 2; 6. Pressure sensor 1; 7. Thermocouple at the outlet; 8. Main reactor; 9. Thermocouple at the inlet; 10. Pressure sensor 2; 11. Precision flow meter; 12. Automatic control system; 13. Raw material supply system; 14. Bypass valve; 15. Thermal oil tank;

[0052] Figure 2 Middle: 16, flange two; 17, flow guide tube; 18, outer shell; 19, insulation layer; 20, outer tube; 21, middle tube; 22, inner tube; 23, first oil guide tube; 24, second oil guide tube; 25, flange one; 26, bolt; 27, feed pipe; 28, screen one; 29, tube chuck; 30, fourth oil guide tube; 31, third oil guide tube; 32, screen two; 33, discharge pipe. DETAILED DESCRIPTION

[0053] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0054] Therefore, the following detailed description of the embodiments of the present invention provided in the accompanying drawings is not intended to limit the scope of the invention claimed for protection, but merely represents selected embodiments of the present invention. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0055] See also Figure 1-3The present invention provides a biomass pretreatment continuous flow system based on a solid acid packed bed tubular reactor, comprising a main reactor 8, an automatic control system 12, an air cooling system 4, and a raw material supply and product collection system. The automatic control system 12 includes a heat transfer oil circulation system, a temperature monitoring control system, a material flow monitoring control system, a pressure monitoring control system, and an electronic control component. The main reactor 8 is a double-jacketed packed bed tubular reactor, which is composed of an outer shell 18 and three layers of pipelines including an outer tube 20, a middle tube 21, and an inner tube 22, and four guide ducts 17. The inner tube 22, the middle tube 21, and the outer tube 20 are three coaxial tubes. The four guide ducts 17 are symmetrically distributed on the circular cross-section of the reaction chamber 21. The inner tube wall of the middle tube 21 is provided with threads. An insulation layer 19 composed of insulation material is filled between the outer tube 20 and the outer shell 18.

[0056] The outer tube 20 has a through hole at the top and is connected to the first oil guide pipe 23, the outer tube 20 has a through hole at the bottom and is connected to the fourth oil guide pipe 30, the upper and lower parts of the inner tube 22 are connected to the outer tube 20 through the second oil guide pipe 24 and the third oil guide pipe 31 respectively, so as to exchange heat transfer oil, the gap area between the inner wall of the middle tube 21 and the outer wall of the inner tube 22 is the reaction chamber, and the reaction chamber is filled with fixed acid filler, the flow guide tube 17 is fixed by the tube chuck 29 at the feed port and fixed by the annular fastener at the discharge port; the feed pipe 27 and the discharge pipe 33 are respectively arranged at both ends of the main reactor 8, and the feed pipe 27 and the discharge pipe 33 are connected to the main reactor 8 at the connection points with threads and corresponding conical fasteners. The feed pipe 27 and the discharge pipe 33 are provided with flange 1 25 and flange 2 16 respectively, and the flange 1 25 and flange 2 16 are connected with the feed port and discharge port of the main reactor 8 by bolts 26, and a screen 1 28 is provided between the flange 1 25 and the feed port of the main reactor 8, and a screen 2 32 is provided between the flange 2 16 and the discharge port of the main reactor 8. The feed port and discharge port of the main reactor 8 are both disc-shaped and have the same size as the flange 1 25 and the flange 2 16, and four through holes for inserting the connector are symmetrically opened thereon, and the surfaces of the flange 1 25 and the flange 2 16 are provided with four symmetrically distributed through holes, and the center position thereof is a thin tube with a thread at the end, and the diameter of the tube is consistent with the diameter of the feed pipe 27 and the discharge pipe 33.

[0057] The heat transfer oil circulation system includes a heat transfer oil tank 15, a heat transfer oil heating device, a circulation pump, a bypass valve 14 and a heat transfer oil pipeline, and the two ends of the heat transfer oil pipeline are respectively connected to the first oil pipe 23 and the fourth oil pipe 30; the temperature monitoring and control system includes an outlet thermocouple 7 and an inlet thermocouple 9, and the outlet thermocouple 7 and the inlet thermocouple 9 are respectively installed at the inlet and outlet ports of the main reactor 8; the material flow monitoring and control system includes a liquid phase pump and a precision flowmeter 11; the pressure monitoring and control system includes a back pressure valve 2, a pressure dividing valve 3, a back pressure valve 5, and a pressure sensor 6 and a pressure sensor 10 at the two ports of the main reactor 8; the raw material supply and product collection system includes a product collection system 1 and a raw material supply system 13.

[0058] The present invention also provides a biomass pretreatment continuous flow method based on a solid acid packed bed tubular reactor, comprising the following steps:

[0059] S1. When the system is running, the heat-conducting oil in the heat-conducting oil tank 15 is pumped into the heat-conducting oil pipeline by the circulating pump. During the pumping process, the heat-conducting oil heating device heats the heat-conducting oil, wherein the heat-conducting oil heating device heats the heat-conducting oil by industrial waste heat or solar heating. The heated high-temperature heat-conducting oil flows from the fourth oil conduit 30 into the lower part of the outer tube 20 of the main reactor 8, and flows into the inner tube 22 through the third oil conduit 31. After filling the inner tube 22, the heat-conducting oil flows into the upper part of the outer tube 20 through the second oil conduit 24, and flows out through the first oil conduit 23.

[0060] S2, the raw materials in the raw material supply system 13 are pumped into the feed pipe 27 and into the reaction chamber through the liquid phase pump, the precision flow meter 11 calculates the pumping amount, and the electronic control component controls the pumping amount of the liquid phase pump. During the reaction, the outlet thermocouple 7 and the inlet thermocouple 9 respectively detect the temperature of the outlet and inlet ends of the reaction chamber, and the temperature is controlled by the electronic control component. The pressure sensor 1 6 and the pressure sensor 2 10 respectively detect the pressure at the outlet and inlet of the reaction chamber. The electronic control component adjusts the fluid pressure in the pipeline by controlling the valve opening of the back pressure valve 1 2, the back pressure valve 2 5, and the pressure dividing valve 3;

[0061] S3. The reaction product flows out through the discharge pipe 33, is cooled by the air cooling system 4, and finally flows into the product collection system 1.

[0062] During disassembly, the feed pipe 27 and the discharge pipe 33, as well as the bolts 26, are removed to separate the flange 1 25 and the flange 2 16 from the feed and discharge ports of the main reactor 8, and the screen 1 28 and the screen 2 32 are removed.

[0063] The method of the electronic control component controlling the pumping amount of the liquid phase pump is as follows:

[0064] The pumping amount is measured using a precision flow meter 11, and its reading is Q measuredThe electronic control component controls the pumping volume Q according to the preset set and the actual measured pumping volume Q measured To control the pumping amount of the liquid phase pump;

[0065] Control algorithm:

[0066] Calculation error: e Q =Q set -Q measured ;

[0067] The proportional-integral-derivative control algorithm is used to adjust the pump speed of the liquid phase pump. The output of the electronic control component is expressed as:

[0068]

[0069] Among them, K p is the proportional gain, K i is the integral gain, K d is the differential gain.

[0070] The temperature control method of the electronic control component is as follows:

[0071] The outlet thermocouple 7 and the inlet thermocouple 9 are used to detect the temperature T in the reaction chamber. out and T in The electronic control components are set according to the preset temperature T set and the actual measured temperature to adjust the heating of the thermal oil;

[0072] Control algorithm:

[0073] For the outlet and inlet, calculate the temperature error: eT out =T set -T out and eT in =T set -T in ;

[0074] The proportional-integral-differential control algorithm is used to adjust the output of the heating of the thermal oil. The output of the electronic control component is expressed as:

[0075]

[0076]

[0077] Among them, K p is the proportional gain, K i is the integral gain, K d is the differential gain;

[0078] The method for the electronic control component to adjust the fluid pressure in the pipeline is as follows:

[0079] The pressure sensor 1 6 and the pressure sensor 2 10 are used to detect the pressure P at the outlet and the inlet of the reaction chamber respectively. out and P in The electronic control component adjusts the fluid pressure in the pipeline by controlling the valve opening of the back pressure valve 1 2, the back pressure valve 2 5, and the pressure dividing valve 3;

[0080] Control algorithm:

[0081] For the outlet and inlet, calculate the pressure error separately: eP out =P set -P out and eP in =P set -P in ;

[0082] The proportional-integral-differential control algorithm is used to adjust the opening of the back pressure valve and the pressure dividing valve. The output of the electronic control component is expressed as:

[0083]

[0084]

[0085] Among them, K p is the proportional gain, K i is the integral gain, K d is the differential gain; the opening of the back pressure valve and the pressure dividing valve uP out and uP in Can be converted into valve control signal.

[0086] The double-jacketed reaction tube of the present invention promotes heat exchange, makes the temperature of the reaction chamber more uniform, and improves the cellulose conversion rate and glucose yield. The design of the four-head threaded tube enhances safety and stability. The inner wall threads of the middle tube increase fluid turbulence and radial temperature uniformity. The guide duct supports and fixes the acid filler while improving the reaction flow distribution, plays an anti-clogging role, and is easy to maintain. The automated control system realizes digital control and can be used to optimize the reaction process.

[0087] Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that various changes, modifications, substitutions and variations may be made to the embodiments without departing from the principles and spirit of the present invention, and that the scope of the present invention is defined by the appended claims and their equivalents.

Claims

1. A biomass pretreatment continuous flow system based on a solid acid packed bed tubular reactor, characterized in that: The invention comprises a main reactor (8), an automatic control system (12), an air cooling system (4), and a raw material supply and product collection system. The automatic control system (12) comprises a heat transfer oil circulation system, a temperature monitoring control system, a material flow monitoring control system, a pressure monitoring control system, and an electronic control component. The main reactor (8) is a double-jacketed packed bed tubular reactor, which comprises an outer shell (18), an outer tube (20), a middle tube (21), an inner tube (22) and three layers of pipelines, and four flow guide ducts (17).

2. The biomass pretreatment continuous flow system based on a solid acid packed bed tubular reactor according to claim 1, characterized in that: The flow guide conduit (17) is fixed at the feed port by a conduit chuck (29) and fixed at the discharge port by an annular fastener; the outer tube (20) has a through hole at the upper portion and is connected to the first oil guide tube (23); the outer tube (20) has a through hole at the lower portion and is connected to the fourth oil guide tube (30); the upper and lower portions of the inner tube (22) are connected to the outer tube (20) via the second oil guide tube (24) and the third oil guide tube (31) respectively, for exchanging heat transfer oil; the gap area between the inner wall of the middle tube (21) and the outer wall of the inner tube (22) is a reaction chamber, and the reaction chamber is filled with a fixed acid filler; A feed pipe (27) and a discharge pipe (33) are respectively provided at both ends of the main reactor (8). The feed pipe (27) and the discharge pipe (33) are both provided with threads at the connection points with the main reactor (8) and are equipped with corresponding conical fasteners. A flange plate 1 (25) and a flange plate 2 (16) are respectively provided on the feed pipe (27) and the discharge pipe (33). The flange plate 1 (25) and the flange plate 2 (16) are connected to the feed port and the discharge port of the main reactor (8) by bolts (26).

3. A biomass pretreatment continuous flow system based on a solid acid packed bed tubular reactor according to claim 2, characterized in that: A screen mesh 1 (28) is provided between the flange disc 1 (25) and the feed port of the main reactor (8), and a screen mesh 2 (32) is provided between the flange disc 2 (16) and the discharge port of the main reactor (8).

4. The biomass pretreatment continuous flow system based on a solid acid packed bed tubular reactor according to claim 2, characterized in that: The heat transfer oil circulation system comprises a heat transfer oil tank (15), a heat transfer oil heating device, a circulation pump, a bypass valve (14) and a heat transfer oil pipeline, wherein the two ends of the heat transfer oil pipeline are respectively connected to a first oil transfer pipe (23) and a fourth oil transfer pipe (30); the temperature monitoring and control system comprises an outlet end thermocouple (7) and an inlet end thermocouple (9), wherein the outlet end thermocouple (7) and the inlet end thermocouple (9) are respectively installed at the inlet and outlet ports of the main reactor (8); the material flow monitoring and control system comprises a liquid phase pump and a precision flow meter (11); the pressure monitoring and control system comprises a back pressure valve 1 (2), a pressure dividing valve (3), a back pressure valve 2 (5) and a pressure sensor 1 (6) and a pressure sensor 2 (10) at two ports of the main reactor (8); and the raw material supply and product collection system comprises a product collection system (1) and a raw material supply system (13).

5. The biomass pretreatment continuous flow system based on a solid acid packed bed tubular reactor according to claim 2, characterized in that: The inner tube (22), the middle tube (21) and the outer tube (20) are three coaxial tubes, and the four flow guide tubes (17) are symmetrically distributed on the circular cross section of the reaction chamber.

6. A biomass pretreatment continuous flow system based on a solid acid packed bed tubular reactor according to claim 2, characterized in that: The inner wall of the middle tube (21) is provided with threads, and a heat-insulating layer (19) made of heat-insulating material is filled between the outer tube (20) and the outer shell (18).

7. The biomass pretreatment continuous flow system based on a solid acid packed bed tubular reactor according to claim 2, characterized in that: The inlet and outlet ports of the main reactor (8) are both disc-shaped and have the same size as flange 1 (25) and flange 2 (16), and are symmetrically provided with four through holes for inserting connectors. The surfaces of flange 1 (25) and flange 2 (16) are both provided with four symmetrically distributed through holes, the center of which is a thin tube with a threaded end, and the diameter of the tube is consistent with the diameter of the feed tube (27) and the discharge tube (33).

8. A continuous flow method for biomass pretreatment based on a solid acid packed bed tubular reactor, characterized in that: The steps include: S1. When the system is running, the heat transfer oil in the heat transfer oil tank (15) is pumped into the heat transfer oil pipeline by the circulation pump. During the pumping process, the heat transfer oil is heated by the heat transfer oil heating device, wherein the heat transfer oil heating device heats the heat transfer oil by industrial waste heat or solar energy heating. The heated high-temperature heat transfer oil flows from the fourth oil guide pipe (30) into the lower part of the outer tube (20) of the main reactor (8), and flows into the inner tube (22) through the third oil guide pipe (31). After filling the inner tube (22), the heat transfer oil flows from the second oil guide pipe (24) into the upper part of the outer tube (20), and flows out from the first oil guide pipe (23); S2, the raw materials in the raw material supply system (13) are pumped into the feed pipe (27) and into the reaction chamber through the liquid phase pump, the precision flow meter (11) calculates the pumping amount, and the pumping amount of the liquid phase pump is controlled by the electronic control component, during the reaction process, the outlet end thermocouple (7) and the inlet end thermocouple (9) respectively detect the temperature of the outlet end and the inlet end of the reaction chamber, and the temperature is controlled by the electronic control component, the pressure sensor 1 (6) and the pressure sensor 2 (10) respectively detect the pressure at the outlet and the inlet of the reaction chamber, and the electronic control component adjusts the fluid pressure in the pipeline by controlling the valve opening of the back pressure valve 1 (2), the back pressure valve 2 (5) and the pressure dividing valve (3); S3. The reaction product flows out through the discharge pipe (33), is cooled by the air cooling system (4), and finally flows into the product collection system (1).

9. A biomass pretreatment continuous flow method based on a solid acid packed bed tubular reactor according to claim 8, characterized in that: The method for the electronic control component to control the pumping amount of the liquid phase pump is as follows: Use a precision flow meter (11) to measure the pumping volume, and its reading is Q measured The electronic control component controls the pumping volume Q according to the preset set and the actual measured pumping volume Q measured To control the pumping amount of the liquid phase pump; Control algorithm: Calculation error: e Q =Q set -Q measured ; The proportional-integral-derivative control algorithm is used to adjust the pump speed of the liquid phase pump. The output of the electronic control component is expressed as: Among them, K p is the proportional gain, K i is the integral gain, K d is the differential gain.

10. The continuous flow method for biomass pretreatment based on a solid acid packed bed tubular reactor according to claim 8, characterized in that: The temperature control method of the electric control component is as follows: The outlet thermocouple (7) and the inlet thermocouple (9) are used to detect the temperature T in the reaction chamber respectively. out and T in The electronic control components are set according to the preset temperature T set and the actual measured temperature to adjust the heating of the thermal oil; Control algorithm: For the outlet and inlet, calculate the temperature error: eT out =T set -T out and eT in =T set -T in ; The proportional-integral-differential control algorithm is used to adjust the output of the heating of the thermal oil. The output of the electronic control component is expressed as: Among them, K p is the proportional gain, K i is the integral gain, K d is the differential gain; The method for adjusting the fluid pressure in the pipeline by the electronic control component is as follows: Use pressure sensor 1 (6) and pressure sensor 2 (10) to detect the pressure P at the outlet and inlet of the reaction chamber respectively. out and P in The electronic control component adjusts the fluid pressure in the pipeline by controlling the valve opening of the back pressure valve 1 (2), the back pressure valve 2 (5) and the pressure dividing valve (3); Control algorithm: For the outlet and inlet, calculate the pressure error separately: eP out =P set -P out and eP in =P set -P in ; The proportional-integral-differential control algorithm is used to adjust the opening of the back pressure valve and the pressure dividing valve. The output of the electronic control component is expressed as: Among them, K p is the proportional gain, K i is the integral gain, K d is the differential gain; the opening of the back pressure valve and the pressure dividing valve uP out and uP in Can be converted into valve control signal.

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