Use of device for hydrolyzing biomass in hydrolysis of biomass

Abstract

The present invention relates to the field of biomass hydrolysis, and particularly discloses an application of a biomass hydrolysis apparatus in biomass hydrolysis, the biomass hydrolysis apparatus comprises: a reactor, the reactor comprises a reactor upper body and a reactor lower body, the reactor upper body covers the reactor lower body, and the top of the reactor upper body is provided with a feed inlet and a discharge outlet; the catalyst liquid distributor is connected below the reactor upper body; the first stirrer and the second stirrer are connected to the reactor upper body and extend into the reactor lower body; and the catalyst liquid distributor, the second stirrer, the feeding hole and the first stirrer are sequentially arranged at intervals along the rotating direction of the lower reactor body. The biomass powder is introduced into the reactor lower body through the feeding port, the high-concentration inorganic acid is introduced into the reactor lower body through the catalyst liquid distributor, the reactor lower body, the first stirrer and the second stirrer rotate, and the biomass powder is subjected to a hydrolysis reaction through the high-concentration inorganic acid.

Description

Technical Field

[0001] The invention relates to the field of biomass hydrolysis, and in particular to the application of a device for hydrolyzing biomass in the hydrolyzing biomass. Background Art

[0002] Biomass is mainly composed of cellulose, hemicellulose and lignin, and has a rich carbohydrate ratio. It has important application value in the fields of energy, materials and chemical industry. It is used to produce biofuels through the sugar platform to replace traditional fossil energy, thereby achieving the purpose of energy substitution and mitigating greenhouse gas emissions. In addition, the use of non-grain biomass effectively avoids the current development status of "competing with people for grain and competing with grain for land".

[0003] At present, there are still many shortcomings in the production devices and methods used for straw hydrolysis and sugar production. The immaturity of straw sugar production equipment leads to incomplete saccharification and lack of precision in process control, which makes the sugar production process unstable, affects product quality and cannot meet market demand. The most common method of straw sugar production is to use cellulase to enzymatically hydrolyze the chemically treated straw, which is the way many companies use straw for industrialization. However, the sale of cellulase has not yet formed an open market, and the complex enzyme system for treating lignocellulose is not yet transparent, and the guarantee conditions for screening, storage, and application are required to be high. At the same time, the ineffective degradation of carbohydrates in biomass pretreatment by traditional chemical methods, the high load cost brought by high temperature and high pressure special equipment, and the wastewater treatment problems brought by the use of a large number of chemical reagents. Therefore, the production device and method of straw hydrolysis and sugar production require more technical research and practice to solve these problems.

[0004] In order to overcome the key problems faced in the above-mentioned straw sugar production process, many researchers have proposed corresponding solutions. Chinese invention CN 117966502 A discloses a pretreatment method for extracting lignin from lignocellulose raw materials, but this method requires a large amount of water to wash the material during the industrial production process, generating a large amount of industrial wastewater; Chinese invention CN 117947224 A discloses a method for preparing water-soluble sugar from biomass, but the hydrolysis temperature of this method is between 140°C and 250°C, requiring a large amount of external energy consumption and special high-temperature and high-pressure equipment, which brings huge challenges to industrial production. Chinese invention CN 117925768 A discloses a combined pretreatment method for improving lignocellulose degradation and sugar conversion rate, but this method has a long treatment cycle, which greatly increases the production cost of the process flow.

[0005] The information disclosed in this background technology section is only intended to enhance the understanding of the overall background of the invention and should not be regarded as an acknowledgement or any form of suggestion that the information constitutes the prior art already known to ordinary technicians in this field. Summary of the invention

[0006] Purpose of the invention: The technical problem to be solved by the first aspect of the present invention is to provide a device for hydrolyzing biomass in view of the deficiencies in the prior art, which is suitable for hydrolyzing biomass using high-concentration inorganic acid to achieve efficient production.

[0007] In order to solve the above technical problems, the first aspect of the present invention discloses a device for hydrolyzing biomass, the device comprising: A reactor, comprising an upper reactor body and a lower reactor body, wherein the upper reactor body covers the lower reactor body and is provided with a feed inlet and a discharge inlet on the top, wherein the feed inlet is configured to allow biomass powder to pass into the lower reactor body, and the lower reactor body is configured to rotate relative to the upper reactor body around a vertical rotation axis; An automatic weighing distributor, connected to the feed port, configured to distribute the biomass powder through the feed port into the reactor lower body; a catalyst liquid distributor connected to the bottom of the reactor upper body and configured to distribute a high concentration of inorganic acid within the reactor lower body; and a first agitator and a second agitator, both connected to the reactor upper body and extending into the reactor lower body; The catalyst liquid distributor, the second agitator, the feed port and the first agitator are sequentially arranged at intervals along the rotation direction of the lower body of the reactor.

[0008] In some embodiments, the catalyst liquid distributor includes a liquid distribution channel and a plurality of liquid distribution holes. The liquid distribution channel extends radially along the vertical rotation axis. The high-concentration inorganic acid can flow from the liquid distribution channel through the plurality of liquid distribution holes to the lower body of the reactor. The plurality of liquid distribution holes are arranged at intervals along the liquid distribution channel, and the interval between two adjacent liquid distribution holes gradually decreases in an arithmetic progression along the radial direction away from the vertical rotation axis.

[0009] In some embodiments, the catalyst liquid distributor comprises a liquid distribution pipe, the liquid distribution channel is defined by the inner wall of the liquid distribution pipe, and the plurality of liquid distribution holes are provided on the wall of the liquid distribution pipe.

[0010] In some embodiments, the biomass hydrolysis device includes a connection flange, which is mounted on the reactor upper body and is used to connect to an external catalyst supply device. The catalyst liquid distributor includes a liquid distribution pipe adapter, which connects the liquid distribution pipe and the connection flange.

[0011] In some embodiments, the apparatus for hydrolyzing biomass comprises an automatic weighing distributor connected to the feed inlet.

[0012] Specifically, the automatic weighing distributor includes a weighing hopper shell, a second flexible connection hopper, a biomass distributor shell, an introduction hopper, a multi-blade unloading flap, a multi-blade distribution flap and a weighing sensor. The weighing sensor is arranged on the outside of the weighing hopper shell. The weighing hopper shell, the second flexible connection hopper, the biomass distributor shell and the introduction hopper are sequentially connected from top to bottom to form a distribution channel, and the biomass powder can enter the feed port of the reactor upper body through the distribution channel. The multi-blade unloading flap is arranged in the distribution channel in a section of the weighing hopper shell, and the multi-blade distribution flap is arranged in the distribution channel in a section of the biomass distributor shell, and both can rotate around their respective rotation axes.

[0013] The rate at which the biomass powder enters the lower body of the reactor is regulated by controlling the rotation speed of the multi-blade distribution flap in the automatic weighing distributor, and the ratio of the rotation speed of the multi-blade distribution flap to the rate at which the biomass powder enters the lower body of the reactor is 2-8rpm:1kg / min.

[0014] Specifically, the rotation axis of the multi-blade unloading flap and the rotation axis of the multi-blade distribution flap both extend radially along the vertical rotation axis and are located in the same vertical plane. The multi-blade unloading flap and the multi-blade distribution flap both rotate to form a conical surface, and the two formed conical surfaces overlap with the projection area of ​​the feed port in the top view direction and are located in the fan-shaped area in the lower body of the reactor.

[0015] Specifically, the multi-blade unloading flap and the multi-blade distribution flap divide the distribution channel into a storage weighing section, a material pouring section and a smooth transition section. The storage weighing section is used to receive, temporarily store and weigh the biomass powder. The distribution channel is connected to the feed port of the reactor upper body through the lower port of the smooth transition section. The multi-blade unloading flap is located between the storage weighing section and the material pouring section, and is configured to realize the unloading of the biomass powder in the storage weighing section to the material pouring section when rotating. The multi-blade distribution flap is located between the material pouring section and the smooth transition section, and is configured to realize the unloading of the biomass powder in the material pouring section to the smooth transition section when rotating.

[0016] Specifically, the projection area is a trapezoid. The cross-sections of the material storage weighing section and the material discharge section perpendicular to the vertical direction are both rectangular. The area of ​​the rectangle is larger than the area of ​​the projection area.

[0017] Specifically, the device for hydrolyzing biomass comprises a first flexible connection hopper, which connects a weighing hopper shell in the automatic weighing distributor with an external biomass pneumatic conveying device.

[0018] Specifically, the automatic weighing distributor comprises a first bearing seat and a second bearing seat, the multi-blade unloading flap is installed in the weighing hopper housing through the first bearing seat, and the multi-blade distribution flap is installed in the biomass distributor housing through the second bearing seat.

[0019] Specifically, the device for hydrolyzing biomass comprises a distributor frame for fixedly supporting the automatic weighing distributor. The automatic weighing distributor comprises a weighing frame, the weighing hopper housing is supported on the weighing frame through the weighing sensor, and the weighing frame is fixedly supported on the distributor frame.

[0020] Specifically, the automatic weighing material distributor includes a driving mechanism, and the driving mechanism is configured to respectively drive the multi-blade unloading flap and the multi-blade material distribution flap to rotate. More specifically, the driving mechanism is a motor driving mechanism.

[0021] Specifically, a plurality of the first agitators and a plurality of the second agitators are provided, the plurality of the first agitators are located on a first radial line of the vertical rotation axis and are spaced apart, and the plurality of the second agitators are located on another radial line of the vertical rotation axis and are spaced apart.

[0022] Specifically, the first agitator and the second agitator have the same structure, including a stirring paddle, a stirring support structure, a stirring drive mechanism, a coupling and an auxiliary bearing. The stirring support structure is fixedly mounted on the upper end surface of the reactor upper body. The stirring drive mechanism is fixedly mounted on the stirring support structure. The coupling is arranged on the inner side of the stirring support structure, and the output shaft of the stirring drive mechanism extends into the inner side of the stirring support structure and is connected to the stirring paddle through the coupling. The stirring paddle is rotatably fixedly connected to the stirring support structure through the auxiliary bearing.

[0023] More specifically, the stirring paddle is a hollow spiral blade structure, including a stirring frame, a stirring shaft passing through the stirring frame, and hollow spiral blades staggeredly distributed on the stirring frame along the circumference of the stirring shaft.

[0024] In some embodiments, the device for hydrolyzing biomass includes an observation port and a breathing port, and the observation port and the breathing port are both disposed on the upper body of the reactor.

[0025] In some embodiments, the device for hydrolyzing biomass includes a material temperature measuring device, which is installed on the upper body of the reactor and configured to detect the temperature of the material in the lower body of the reactor.

[0026] In some embodiments, the apparatus for hydrolyzing biomass includes a rotating mechanism configured to support and drive the reactor lower body to rotate relative to the reactor upper body around a vertical rotation axis.

[0027] In some embodiments, the rotating mechanism includes a driving gear and an external gear bearing, the external gear of the external gear bearing is coaxially fixedly connected to the lower body of the reactor, and the external gear of the external gear bearing is meshed with the driving gear.

[0028] In some embodiments, the apparatus for hydrolyzing biomass includes a rotary power source, and an output shaft of the rotary power source is drivingly connected to the drive gear.

[0029] In some embodiments, the device for hydrolyzing biomass includes a disc reactor frame for supporting the reactor. The disc reactor frame includes a reactor upper body structural support portion and a reactor lower body mounting structural portion. The reactor upper body is fixedly supported on the reactor upper body structural support portion. The inner ring of the external gear bearing is fixedly connected to the reactor lower body mounting structural portion through a mounting structural member.

[0030] In some embodiments, the reactor upper body includes a reactor upper body frame and a reactor upper body wall skin, and the reactor upper body wall skin is fixedly connected to the reactor upper body frame.

[0031] In one embodiment, the reactor upper body includes a support ear, which is fixedly connected to the upper end periphery of the reactor upper body skeleton, and the support ear is used to be fixedly connected to the reactor upper body structure support part to achieve fixed support of the reactor upper body on the reactor upper body structure support part.

[0032] In one embodiment, the reactor lower body comprises a reactor lower body main body and a reactor lower body support structure, and the reactor lower body main body is made of a lightweight corrosion-resistant material. The reactor lower body main body is configured to be accommodated in the reactor lower body support structure. The outer gear of the external gear bearing is coaxially fixedly connected to the reactor lower body support structure to achieve the coaxial fixed connection between the outer gear of the external gear bearing and the reactor lower body.

[0033] In one embodiment, the device for hydrolyzing biomass includes a rotary seal assembly, which is configured to enable the upper reactor body and the lower reactor body to be rotatably connected and sealed. In one embodiment of the rotary seal assembly, the rotary seal assembly is disposed on the top of the lower reactor body. In another embodiment of the rotary seal assembly, the rotary seal assembly is disposed at the bottom of the upper reactor body.

[0034] In one embodiment, the lower body of the reactor is cylindrical.

[0035] In one embodiment, the reactor is overall disc-shaped.

[0036] In a second aspect, the present invention discloses the use of the device described in the first aspect in hydrolyzing biomass.

[0037] In some embodiments, the application specifically includes: passing biomass powder into the lower body of the reactor through the feed inlet, passing high-concentration inorganic acid into the lower body of the reactor through the catalyst liquid distributor, the upper body of the reactor remains stationary, the lower body of the reactor, the first agitator and the second agitator rotate, the biomass powder is hydrolyzed by the high-concentration inorganic acid, and the material is discharged after the reaction stops.

[0038] In some embodiments, the discharging is to reduce the rotation speed of the lower body of the reactor to below 15 rpm, and the discharging machine extends from the discharging port into the lower body of the reactor to take the material; in some embodiments, when the bottom surface of the discharging machine contacts the bottom surface of the lower body of the reactor, the rotation speed of the lower body of the reactor can be increased, such as increasing it to 120 rpm to quickly rotate and discharge the material; in some implementations, the discharging machine can adopt an existing discharging machine, such as Zeng Shuaiqiang, Wang Jianye, Li Pengfei, etc. Structural design of screw conveyor for viscous materials such as ammonium metavanadate [J]. Soda Ash Industry, 2024(02): 22-24.

[0039] In some embodiments, the biomass powder is introduced into the lower body of the reactor through an automatic weighing distributor connected to the feed port; in some embodiments, the biomass powder is introduced into the lower body of the reactor through the automatic weighing distributor at a rate of 5-20 kg / min, such as 5 kg / min, 7.5 kg / min, 10 kg / min, 15 kg / min, 20 kg / min; in some embodiments, the speed of the multi-blade distribution flap in the automatic weighing distributor is controlled to regulate the rate at which the biomass powder enters the lower body of the reactor, and the ratio of the speed of the multi-blade distribution flap in the automatic weighing distributor to the rate at which the biomass powder enters the lower body of the reactor is 2-8 rpm :1kg / min, such as 4rpm:1kg / min, 5rpm:1kg / min, 6kg / min; by controlling the rotation speed of the multi-blade distribution flap in the automatic weighing distributor to 20-120rpm, the rate at which the biomass powder enters the lower body of the reactor is regulated to be 5-20kg / min; in some embodiments, the mass of the biomass powder stored in the second soft-connected hopper can be controlled by controlling the rotation speed of the multi-blade unloading flap in the automatic weighing distributor; in some embodiments, the rotation speeds of the multi-blade unloading flap and the multi-blade distribution flap are independently selected from 20-120rpm, such as 40rpm, 60rpm, 80rpm, 100rpm.

[0040] In some embodiments, the high concentration inorganic acid is introduced into the lower body of the reactor through the catalyst liquid distributor at a flow rate of 5-50kg / min, such as 10kg / min, 12.5kg / min, 15kg / min, 18kg / min, 20kg / min, 22kg / min, 25kg / min, 30kg / min, 40kg / min; in some embodiments, the length of the liquid distribution channel is 1000-1400mm, such as 1200mm; in some embodiments, the inner diameter DN of the liquid distribution channel is 40-60mm, such as 50mm; in some embodiments, the liquid distribution channel is provided with 200-400 liquid distribution holes arranged at intervals, and the interval between two adjacent liquid distribution holes gradually decreases in an arithmetic progression along the radial direction away from the vertical rotation axis, such as 300 liquid distribution holes arranged in an arithmetic progression; in some embodiments, the aperture of each liquid distribution hole is 1.5-3mm.

[0041] In some embodiments, the biomass powder can be continuously or intermittently introduced into the lower body of the reactor through the feed port, and the high-concentration inorganic acid can be continuously or intermittently introduced into the lower body of the reactor through the catalyst liquid distributor.

[0042] In some embodiments, the biomass powder and the high concentration inorganic acid are fed continuously; in this case, it is necessary to avoid direct contact between the biomass powder that does not participate in the reaction and the high concentration inorganic acid to cause carbonization of the biomass powder; specifically, carbonization can be avoided by regulating parameters such as the feed rate of the biomass powder and the high concentration inorganic acid.

[0043] In some embodiments, the biomass powder and the high-concentration inorganic acid are cross-fed; in some embodiments, the biomass powder and the high-concentration inorganic acid are cross-fed once every 0.5-5 turns of the lower body of the reactor, such as every 1, 2, 3 or 4 turns, to avoid direct contact between the biomass powder that does not participate in the reaction and the high-concentration inorganic acid, resulting in carbonization of the biomass powder and forming a large number of side reactions; in some embodiments, the biomass powder and the high-concentration inorganic acid are cross-fed, and the inorganic acid is fed first, and then the biomass powder is fed. In this process, the biomass powder and the inorganic acid can interact evenly and quickly.

[0044] In some embodiments, the rotation speed of the lower body of the reactor is 50-200 rpm, such as 70 rpm, 80 rpm, 90 rpm, 100 rpm, 110 rpm, 120 rpm, 130 rpm, 140 rpm, 150 rpm, 160 rpm, 170 rpm, 180 rpm, and 190 rpm.

[0045] In some embodiments, the rotation speeds of the first agitator and the second agitator are independently selected from 10-80 rpm, such as 20 rpm, 40 rpm, and 60 rpm.

[0046] In some embodiments, the reaction temperature is room temperature, such as 20-30°C, such as 25°C; the reaction temperature can be monitored by a material temperature measuring device. If the temperature rises, the distribution of biomass powder and high-concentration inorganic acid can be temporarily suspended. During the production process, close attention should be paid to temperature changes to avoid high temperatures as much as possible.

[0047] In some embodiments, samples can be taken through the discharge port to detect the degree of hydrolysis of the biomass; if the mixture in the reaction system exhibits high fluidity, samples can be taken through the discharge port for analysis; after the reaction is complete, the reaction is stopped and the material is discharged.

[0048] In some embodiments, the hydrolysis of biomass is observed through an observation port; for example, when good fluidity exists at the initial stage of the reaction, the feeding rate of biomass powder is increased; when the fluidity of the reaction system is poor and there is no obvious improvement, the feeding rate of high-concentration inorganic acid is increased; when there is a carbonization trend, the feeding of biomass powder and high-concentration inorganic acid is temporarily suspended; when the mixture in the reaction system exhibits high fluidity at the end of the reaction, samples can be taken through the discharge port to detect the degree of hydrolysis of the biomass.

[0049] In some embodiments, the diameter of the inner cavity of the lower body of the reactor is 0.6-20.6 meters, such as 2.6, 4.6, 6.6, 8.6, 10.6, and 15.6 meters; in some embodiments, the height of the inner cavity of the lower body of the reactor is 0.2-5 meters, such as 0.6, 0.8, 1, 1.5, 2, 3, and 4 meters; in some embodiments, the diameter and height of the inner cavity of the lower body of the reactor are 2.6 meters and 0.4 meters, respectively; in this process, the materials can be kept mixed evenly, carbonization rarely occurs, and can be handled in time, with a production capacity of up to 150-300kg / 20min. Furthermore, when the diameter and height of the inner cavity of the lower body of the reactor are expanded, the rotation speed of the lower body of the reactor can be increased by increasing the number of agitators, increasing the length of the catalyst distributor, etc., thereby increasing the feeding rate of biomass powder and acid and scaling up production; specifically, if the rotation speed of the lower body of the reactor is increased from 120rpm to 500rpm, the rotation speed of the multi-blade distribution flap in the automatic weighing distributor is 80-480rpm to regulate the rate at which biomass powder enters the lower body of the reactor at 20-80kg / min, the amount of acid is increased by 4 times, and the production capacity can be increased to 500kg / 30min; with further scaling up, the production capacity can be as high as 3 tons / h.

[0050] In some embodiments, the biomass powder is obtained by passing through a 80-100 mesh sieve.

[0051] In some embodiments, the inorganic acid is added in the form of an inorganic acid aqueous solution, and the inorganic acid includes any one or a combination of sulfuric acid, hydrochloric acid, nitric acid and phosphoric acid. When the inorganic acid is sulfuric acid, nitric acid and phosphoric acid, the concentration of the high-concentration inorganic acid is 65wt% or more, such as 70wt%, 75wt%, 80wt%, 85wt%, 90wt%, 95wt%, etc.; when the inorganic acid is hydrochloric acid, the concentration of the high-concentration inorganic acid is 25wt%-35wt%, such as 28wt%, 30wt%, 32wt%.

[0052] In some embodiments, the biomass is any one or a combination of wheat straw, corn straw, rice straw, sorghum straw, cotton straw, bagasse, corn cob, switchgrass, reed and rapeseed.

[0053] In some embodiments, the mass of the acid is 0.3-1.2 times, such as 0.5-1 times, such as 0.6 times, 0.8 times, of the biomass powder.

[0054] In some embodiments, the rate ratio of the high concentration inorganic acid to the biomass powder into the lower body of the reactor is 0.5-3:1, such as 0.7:1, 0.9:1, 1.1:1, 1.3:1, 1.5:1, 1.7:1, 1.9:1, 2.1:1, 2.3:1, 2.5:1, 2.7:1, and 2.9:1.

[0055] In some embodiments, the reaction temperature is 20-35°C, such as room temperature.

[0056] In some embodiments, the reaction is carried out at normal pressure.

[0057] In some embodiments, the reaction time is 10-60 min, such as 15 min, 20 min, 25 min, 30 min, 35 min, 40 min, 45 min, 50 min.

[0058] The feeding in the present invention refers to the feeding of biomass powder or high-concentration inorganic acid into the lower body of the reactor. The feeding rate, unless otherwise specified, refers to the feeding rate of biomass powder or high-concentration inorganic acid into the lower body of the reactor.

[0059] Beneficial effects: 1) The device provided by the present invention is arranged so that the lower body of the reactor can rotate relative to the upper body of the reactor around the vertical rotation axis, and when the lower body of the reactor rotates once, the lower body of the reactor sequentially sweeps over the catalyst liquid distributor, the second agitator, the feed inlet and the first agitator, so that the area in the lower body of the reactor where the high concentration of inorganic acid is sprinkled is swept over the second agitator as the lower body of the reactor rotates and mixed with the hydrolyzate in the lower body of the reactor, and then the reactor area is swept over the liquid distributor with biomass as the lower body of the reactor continues to rotate, and the area with biomass is then swept over the first agitator for stirring and mixing, and in this process, the rapid carbonization of the biomass caused by the direct contact between the high concentration of inorganic acid and the biomass is avoided, thereby improving the carbohydrate conversion rate. At the same time, for any sector area in the lower body of the reactor, when the lower body of the reactor rotates one circle, the sector area sequentially undergoes the process of adding catalyst, stirring and mixing, adding biomass, stirring and mixing, and then if the lower body of the reactor is set to rotate continuously, the catalyst liquid distributor continuously and quantitatively distributes liquid, and the automatic weighing distributor continuously and quantitatively distributes materials, the device can realize the circulation of the above process for the entire annular area of ​​the reaction chamber, that is, to realize continuous production in the true sense. The prior art uses a fixed reaction chamber. In order to avoid rapid carbonization, the catalyst liquid distributor and the biomass distributor must work intermittently and alternately, so as to realize the process of adding catalyst, stirring and mixing, adding biomass, and stirring and mixing in the fixed reaction chamber as a whole in a time sequence. Therefore, compared with the prior art, the device of the present invention can realize continuous production of continuous feeding, and can improve the efficiency of production while preventing rapid carbonization and improving the conversion rate of carbohydrates.

[0060] 2) The device disclosed in the present invention can realize continuous production and adjustable feeding ratio through the coordination among the reactor, the automatic weighing distributor, the catalyst liquid distributor and the agitator.

[0061] 3) The device disclosed in the present invention uses a large amount of PP materials and lightweight design, which can effectively reduce energy consumption. The reduction in operating costs brings great economic value.

[0062] 4) The straw powder of the present invention is efficiently hydrolyzed at room temperature and pressure to effectively obtain a high-concentration and controllable oligosaccharide solution, with the concentrations of cellobiose and xylobiose reaching up to 3.05 g / l and 3.55 g / l, respectively, which can avoid the investment of a large amount of enzyme costs and provide a new option for the construction of a non-food bio-based sugar platform.

[0063] 5) The device disclosed in the present invention effectively controls the carbonization rate of cellulose and hemicellulose in the hydrolysis conversion of biomass powder by controlling the contact ratio of biomass powder and high-concentration inorganic acid, and realizes a hydrolysis production line capacity of 3 tons of absolute dry straw powder / h. Compared with traditional devices, the reaction process is more stable, the effect is higher, and the performance is more superior.

[0064] 6) The technical solution provided by the present invention can significantly reduce the solid-liquid ratio to 0.35-1.4, reduce the acid dosage to 0.5-1 times of biomass powder, and the cellulose / acid ratio is as high as 0.8, thereby reducing the use of acid and the generation of wastewater. BRIEF DESCRIPTION OF THE DRAWINGS

[0065] The present invention will be further described in detail below in conjunction with the accompanying drawings and specific embodiments, and the above and / or other advantages of the present invention will become more clear.

[0066] Figure 1 The present invention is a schematic diagram of the three-dimensional structure of a device for hydrolyzing biomass disclosed in one embodiment of the present invention.

[0067] Figure 2 for Figure 1 The schematic diagram of the overall assembly structure of the reactor in the device for hydrolyzing biomass is shown.

[0068] Figure 3 for Figure 2 A top view of the reactor is shown.

[0069] Figure 4 for Figure 3 A front view of the reactor is shown.

[0070] Figure 5 For Figure 3 Cross-sectional view of the reactor of line AA.

[0071] Figure 6 for Figure 1 The schematic diagram of the three-dimensional structure of the catalyst liquid distributor in the device for hydrolyzing biomass is shown.

[0072] Figure 7 for Figure 1 The schematic diagram of the three-dimensional structure of the automatic weighing distributor in the device for hydrolyzing biomass is shown when it is installed on the distributor frame.

[0073] Figure 8 for Figure 7 The front view of the automatic weighing distributor is shown.

[0074] Fig. 9 for Figure 8 Left side view of the automatic weighing feeder shown.

[0075] Fig.10 for Figure 8 A top view of the automatic weighing distributor is shown.

[0076] Fig.11 For Fig. 9 Cross-sectional view of the automatic weighing feeder on line BB.

[0077] Fig.12 It is a schematic diagram of the three-dimensional structure of the weighing hopper assembly.

[0078] Fig.13 for Fig.12 A vertical cross-sectional view of a weigh hopper assembly is shown.

[0079] Fig.14 A schematic diagram of the three-dimensional structure of the cloth component.

[0080] Fig.15 for Fig.14 A vertical cross-section of the cloth assembly is shown.

[0081] Fig.16 for Figure 1 A schematic diagram of the three-dimensional structure of an agitator in a device for hydrolyzing biomass is shown.

[0082] Fig.17 for Fig.16 A schematic diagram of the assembly structure of the auxiliary bearing, coupling and agitator supporting structure in the agitator is shown.

[0083] Fig.18 for Fig.16 The main cross-sectional view of the assembly structure of the auxiliary bearing, coupling and agitator supporting structure in the agitator is shown.

[0084] Fig.19 for Fig.16 Schematic diagram of the structure of the stirring paddle in the stirrer shown.

[0085] Fig. 20 for Figure 1 The schematic diagram of the assembly structure of the disc reactor frame, driving gear and rotary power source in the device for hydrolyzing biomass is shown.

[0086] Fig.21 for Figure 2 A schematic diagram of the three-dimensional structure of the reactor upper body in the reactor shown.

[0087] Fig. 22 for Figure 2 A schematic diagram of the three-dimensional structure of the lower body of the reactor in the reactor shown.

[0088] Fig.23 This is a liquid phase diagram of the hydrolyzed oligosaccharide solution components according to the sixth embodiment of the present invention.

[0089] Description of the accompanying drawings: 100, automatic weighing distributor; 110, distribution channel; 1101, material storage weighing section; 1102, material discharging section; 1103, smooth transition section; 111, first soft connection hopper; 1111, upper material guide connection flange; 1112, soft connection body; 1113, fixed end mounting structure flange; 120, weighing hopper assembly; 121, weighing hopper shell; 122, multi-blade unloading flap; 123, first bearing seat; 124, first motor mounting frame; 125, first motor drive mechanism; 126, weighing sensor; 127, weighing frame; 131, second flexible connection hopper; 140, distribution assembly; 141, biomass distributor housing; 142, multi-blade distribution flap; 143, second bearing seat; 144, second motor mounting frame; 145, second motor drive structure; 151, introduction hopper; 200, agitator; 201, first agitator; 202, second agitator; 210, agitation drive mechanism; 220, agitator support structure; 230, agitator paddle; 231, Stirring frame; 232, stirring shaft; 233, hollow spiral blade; 240, coupling; 250, auxiliary bearing; 300, reactor; 310, reactor upper body; 311, feed inlet; 314, reactor upper body frame; 315, reactor upper body wall skin; 316, lug; 320, reactor lower body; 321, reactor lower body body; 322, reactor lower body support structure; 323, external gear bearing; 324, mounting structure; 325, rotating seal assembly; 330, reaction chamber ; 340, vertical rotation axis; 410, disc reactor frame; 411, reactor upper structure support; 412, driving gear; 413, rotary power source; 414, reactor lower mounting structure; 420, distributor frame; 500, catalyst liquid distributor; 510, liquid distribution pipe; 511, liquid distribution channel; 512, liquid distribution hole; 520, liquid distribution pipe adapter; 530, connecting flange; 600, material temperature measuring device; 700, observation port; 800, discharge port; 900, breathing port. DETAILED DESCRIPTION

[0090] See also Figures 1 to 5 The present application provides a device for hydrolyzing biomass, which includes an automatic weighing distributor 100, an agitator 200, a reactor 300 and a catalyst liquid distributor 500.

[0091] See also Figures 2 to 5 The reactor 300 is disc-shaped as a whole. The reactor 300 includes a reactor upper body 310 and a reactor lower body 320. The reactor lower body 320 is provided with an upper opening. The reactor upper body 310 covers the upper opening of the reactor lower body 320 and forms a reaction chamber 330 with the reactor lower body 320. Figure 5, the reactor lower body 320 and the reaction chamber 330 are both flat cylindrical as a whole. The reactor lower body 320 is disc-shaped as a whole. The reactor lower body 320 is configured to be rotatable around the vertical rotation axis 340 relative to the reactor upper body 310. A feed port 311 is provided at the top of the reactor upper body 310, and the feed port 311 is arranged on one side of the vertical rotation axis 340 and has an overall fan-shaped or isosceles trapezoidal shape. The feed port 311 is configured to allow biomass to pass into the reactor lower body 320. A discharge port 800 is also provided at the top of the reactor upper body 310, and the discharge port 800 is configured to allow a discharge machine to take materials from the reactor lower body 320.

[0092] See also Figure 1 and Figure 2 The automatic weighing distributor 100 is disposed above the reactor upper body 310 and connected to the feed port 311. The automatic weighing distributor 100 is configured to distribute the biomass powder through the feed port 311 in the area where the reactor lower body 320 sweeps the feed port 311 when the reactor lower body 320 rotates.

[0093] See also Figure 5 The catalyst liquid distributor 500 is connected to the bottom of the reactor upper body 310 and is configured to distribute high-concentration inorganic acid in the reactor lower body 320 .

[0094] See also Figure 1 The agitator 200 includes a first agitator 201 and a second agitator 202. The first agitator 201 and the second agitator 202 are both installed on the reactor upper body 310 and extend downward into the reactor lower body 320. The first agitator 201 and the second agitator 202 are respectively configured to rotate and stir the area swept by the reactor lower body 320 when the reactor lower body 320 rotates.

[0095] See also Figure 1 , Figure 2 and Figure 5 The catalyst distributor 500, the second agitator 202, the feed port 311 and the first agitator 201 are sequentially arranged at intervals along the rotation direction of the reactor lower body 320. When the reactor lower body 320 rotates one circle, the reactor lower body 320 sequentially sweeps over the catalyst distributor 500, the second agitator 202, the feed port 311 and the first agitator 201.

[0096] The device disclosed in this embodiment is arranged so that the reactor lower body 320 can rotate around the vertical rotation axis relative to the reactor upper body 310, and when the reactor lower body 320 rotates one circle, the reactor lower body 320 sequentially sweeps the catalyst liquid distributor 500, the second agitator 202, the feed inlet 311 and the first agitator 201, so that the area in the reactor lower body where high concentration of inorganic acid is sprinkled sweeps through the second agitator as the reactor lower body rotates and is mixed with the hydrolyzate in the reactor lower body, and then the reactor area sweeps through the liquid distributor where biomass is distributed as the reactor lower body continues to rotate, and the area where biomass is distributed is then swept through the first agitator for stirring and mixing, and in this process, rapid carbonization of the biomass caused by direct contact between the high concentration of inorganic acid and the biomass is avoided, thereby improving the carbohydrate conversion rate.

[0097] In addition, the prior art adopts a fixed reaction chamber, and the fixed reaction chamber as a whole is cycled in time sequence to add catalyst, stir and mix, add biomass, stir and mix. In this process, in order to avoid rapid carbonization, the catalyst liquid distributor and the biomass distributor must work alternately intermittently. In the present application, for any sector area in the reactor lower body 320, when the reactor lower body 320 rotates one circle, the sector area successively undergoes the process of adding catalyst, stirring and mixing, adding biomass, stirring and mixing. If the reactor lower body 320 rotates continuously, the catalyst liquid distributor 500 continuously distributes liquid quantitatively, and the automatic weighing distributor 100 continuously distributes material quantitatively, then the device can realize the cycle of the above process for the entire annular area of ​​the reaction chamber, that is, realize continuous production in the true sense. Compared with the prior art, the present application realizes continuous production of high-concentration inorganic acid and biomass while preventing rapid carbonization and improving conversion rate, thereby improving production efficiency.

[0098] In other words, the device disclosed in the present invention can achieve continuous production and adjustable feed ratio through the coordination between the reactor, the automatic weighing distributor, the catalyst liquid distributor and the agitator.

[0099] Preferably, see Figure 1 , Figure 2 and Figure 5 The first agitator 201 is disposed near the feed port 311, and the second agitator 202 is disposed near the catalyst liquid distributor 500. The first agitator 201 is configured to stir and mix the biomass spilled into the reaction chamber, and the second agitator 202 is configured to stir and mix the high-concentration inorganic acid spilled into the reaction chamber.

[0100] For some specific embodiments, see Figure 5 and Figure 6The catalyst liquid distributor 500 includes a liquid distribution channel 511 and a plurality of liquid distribution holes 512. The liquid distribution channel 511 extends radially along the vertical rotation axis 340. High-concentration inorganic acid can flow from the liquid distribution channel 511 through the liquid distribution holes 512 to the reactor lower body 320. Figure 6 A plurality of liquid distribution holes 512 are arranged at intervals along the liquid distribution channel 511 , and the interval between two adjacent liquid distribution holes 512 gradually decreases in an arithmetic progression along the radial direction away from the vertical rotation axis 340 .

[0101] In some specific embodiments, see Figure 6 The catalyst liquid distributor 500 includes a liquid distribution pipe 510. A liquid distribution channel 511 is defined by the inner wall of the liquid distribution pipe 510. A plurality of liquid distribution holes 512 are formed on the wall of the liquid distribution pipe 510 and are all connected to the inside of the liquid distribution pipe 510.

[0102] In some specific embodiments, see Figure 1 , Figure 5 and Figure 6 The device for hydrolyzing biomass includes a connecting flange 530, which is fixedly mounted on the reactor upper body 310 and is used to connect to an external catalyst supply device. The catalyst supply device includes a plurality of catalyst supply pipelines for supplying inorganic acid catalysts of different concentrations, and the connecting flange 530 can be selectively connected to any one of the plurality of catalyst supply pipelines in the catalyst supply device to pass the inorganic acid catalyst of the required concentration into the catalyst liquid distributor 500.

[0103] See also Figure 5 and Figure 6 The catalyst liquid distributor 500 includes a liquid distribution pipe adapter 520 , and the liquid distribution pipe adapter 520 connects the liquid distribution pipe 510 and the connecting flange 530 , thereby realizing that the catalyst liquid distributor 500 is connected to the reactor upper body 310 through the connecting flange 530 .

[0104] In some specific embodiments, see Figures 7 to 11 The automatic weighing distributor 100 includes a weighing hopper housing 121, a second flexible connection hopper 131, a biomass distributor housing 141, an inlet hopper 151, a multi-blade unloading flap 122, a multi-blade distribution flap 142 and a weighing sensor 126. Fig.11 The weighing sensor 126 is arranged outside the weighing hopper housing 121. The weighing hopper housing 121, the second flexible connection hopper 131, the biomass distributor housing 141 and the introduction hopper 151 are sequentially connected from top to bottom to form a distribution channel 110. Figure 1The lower end of the inlet hopper 151 is used as the lower end of the material distribution channel 110, which extends into the feed inlet 311 of the reactor upper body 310, so that the biomass can enter the feed inlet 311 of the reactor upper body 310 through the material distribution channel 110. Fig.11 The material distribution channel 110 is arranged along the vertical direction as a whole. Fig.12 and Fig.13 The multi-blade unloading flap 122 is arranged in the material distributing channel 110 and is located in a section of the weighing hopper housing 121, see Fig.14 and Fig.15 The multi-blade material distribution flap 142 is disposed in the material distribution channel 110 in a section of the biomass distributor housing 141 , and the multi-blade material discharge flap 122 and the multi-blade material distribution flap 142 can both rotate around their respective rotation axes.

[0105] See also Fig.11 The multi-blade unloading flap 122 and the multi-blade distribution flap 142 divide the distribution channel 110 into a storage weighing section 1101, a material pouring section 1102 and a smooth transition section 1103. The storage weighing section 1101 is used to receive, temporarily store and weigh biomass. The distribution channel 110 is connected to the feed port 311 of the reactor upper body 310 through the lower port of the smooth transition section 1103. The multi-blade unloading flap 122 is located between the storage weighing section 1101 and the material pouring section 1102, and is configured to control the rotation according to the measurement value of the weighing sensor 126 to realize the unloading of biomass in the storage weighing section 1101 to the material pouring section 1102. The multi-blade distribution flap 142 is located between the material pouring section 1102 and the smooth transition section 1103, and is configured to realize the unloading of biomass in the material pouring section 1102 to the smooth transition section 1103 when rotating.

[0106] This embodiment adopts a multi-blade material discharge flap 122, which is conducive to batch feeding.

[0107] In a preferred embodiment, see Figure 1 and Fig.11 The rotation axis of the multi-blade material unloading flap 122 and the rotation axis of the multi-blade material distribution flap 142 both extend radially along the vertical rotation axis 340 and are located in the same vertical plane. The multi-blade material unloading flap 122 and the multi-blade material distribution flap 142 both rotate to form a conical surface, and the two formed conical surfaces overlap with the projection area of ​​the feed port 311 in the top view direction and are located in the fan-shaped area in the reactor lower body 320.

[0108] In this embodiment, conical surfaces are formed by the rotation of the multi-blade unloading flap 122 and the multi-blade distribution flap 142, and the two formed conical surfaces coincide with the projection area of ​​the feed port 311 in the top view direction and are located in the fan-shaped area in the reaction chamber 330, so that the biomass can be evenly distributed in the fan-shaped area on the horizontal plane of the reaction chamber passed by the feed port rotating relative to the lower body of the reactor, and at the same time, when the biomass powder distribution rate is large, it is not easy to get clogged.

[0109] In this embodiment, a multi-blade unloading flap 122 and a multi-blade distribution flap 142 are arranged to rotate to form a conical surface, and the two formed conical surfaces coincide with the projection area of ​​the feed port 311 in the top view direction and are located in the fan-shaped area within the reactor lower body 320, so that the biomass is distributed in the fan-shaped area within the reactor lower body 320, avoiding waste caused by accumulation of biomass near the vertical rotation axis 340, which helps to improve the carbohydrate conversion rate.

[0110] In some specific embodiments, the projection area is a trapezoid. The small end of the trapezoid is closer to the vertical rotation axis 340 than the large end of the trapezoid. It should be understood that the projection area of ​​the present application can also be a fan-shaped. Fig.10 The cross-sections of the material storage weighing section 1101 and the material discharging section 1102 perpendicular to the vertical direction are both rectangular. The area of ​​the rectangle is larger than the area of ​​the projection area. Figure 7 The smooth transition section 1103 is configured to smoothly connect the pouring section 1102 with the feed port 311 .

[0111] See also Fig.13 and Fig.15 In the present application, both the multi-blade unloading flap 122 and the multi-blade material distribution flap 142 adopt a multi-blade flap structure, including a shaft and a plurality of blade plates, the plurality of blade plates are evenly distributed along the circumference of the shaft, and the blade plates extend along the radial direction of the shaft. The blade plates are arranged in a trapezoidal shape to form a conical surface when the multi-blade flap rotates. In some specific embodiments, see Fig.13 The multi-blade blanking flap 122 is provided with four blade plates evenly spaced along its circumference, see Fig.15 The multi-blade material distribution flap 142 is evenly spaced with twelve blades along its circumference. The angle between two adjacent blades is 30°, which is more conducive to the uniformity of batch feeding.

[0112] For some specific embodiments, see Fig.11 The automatic weighing distributor 100 includes a first bearing seat 123 and a second bearing seat 143. Both ends of the shaft of the multi-blade unloading flap 122 are installed in the weighing hopper housing 121 through the first bearing seat 123. Both ends of the shaft of the multi-blade distribution flap 142 are installed in the biomass distributor housing 141 through the second bearing seat 143.

[0113] In some specific embodiments, see Fig.11 The automatic weighing distributor 100 includes a first flexible connection hopper 111, and the first flexible connection hopper 111 connects the weighing hopper housing 121 and the external biomass pneumatic conveying device. The external biomass pneumatic conveying device is a prior art, so it is not described here. In some specific embodiments, please refer to Figure 8 , the first flexible connection hopper 111 includes an upper material guide connection flange 1111, a flexible connection body 1112 and a fixed end mounting structure flange 1113. Preferably, the material model selected for the upper material guide connection flange 1111 is 316L, and the flange surface is evenly distributed with circular holes for connecting to an external biomass pneumatic conveying device to achieve the connection between the first flexible connection hopper 111 and the external biomass pneumatic conveying device. Preferably, the flexible connection body 1112 is made of waterproof and breathable material. In order to reduce the weighing error and have a certain storage capacity, on the basis that the weighing hopper shell 121 has sufficient structural strength to support the multi-blade unloading flap 122, the height dimension of the weighing hopper shell 121 can be designed to be short enough, and the height dimension of the first flexible connection hopper 111 is designed to be large enough to accommodate enough biomass to be weighed. At this time, the first flexible connection hopper 111, the weighing hopper housing 121, the second flexible connection hopper 131, the biomass distributor housing 141, and the introduction hopper 151 together constitute the distribution channel 110. Preferably, the upper guide connection flange 1111 and the fixed end mounting structure flange 1113 are both designed in a rectangular structure.

[0114] It should be understood that the second soft connection hopper 131 can adopt the same structure as the first soft connection hopper 111 .

[0115] Preferably, the specific structure of the weighing hopper housing 121 is that threaded holes are evenly distributed on the upper and lower end surface flanges so as to be connected and installed with the first soft connection hopper 111 and the second soft connection hopper 131 .

[0116] In some specific embodiments, the automatic weighing distributor 100 includes a driving mechanism, which is configured to drive the multi-blade unloading flap 122 and the multi-blade material distribution flap 142 to rotate respectively. Figure 8 , the driving mechanism is a motor driving mechanism, such as a motor and a reducer. In some specific embodiments, see Fig.12 and Fig.14 The driving mechanism includes a first motor driving mechanism 125 for driving the multi-blade unloading flap 122 to rotate and a second motor driving mechanism 145 for driving the multi-blade material distribution flap 142 to rotate. In some specific embodiments, see Fig.12 and Fig.14The automatic weighing distributor 100 includes a first motor mounting frame 124 and a second motor mounting frame 144. The first motor driving mechanism 125 is fixedly mounted on the outer wall of the weighing hopper housing 121 through the first motor mounting frame 124. The second motor driving mechanism 145 is fixedly mounted on the outer wall of the biomass distributor housing 141 through the second motor mounting frame 144.

[0117] In some specific embodiments, for ease of assembly, see Fig.12 and Fig.13 The weighing hopper assembly 120 is composed of a weighing hopper housing 121, a multi-blade unloading flap 122, a first bearing seat 123, a first motor mounting frame 124 and a first motor driving mechanism 125. Fig.14 and Fig.15 The biomass distributor housing 141, the multi-blade distribution flap 142, the second bearing seat 143, the second motor mounting frame 144 and the second motor drive structure 145 together constitute the distribution assembly 140. Optionally, the first bearing seat 123 and the second bearing seat 143 can both use UCP series seated bearings, which are low in cost and easy to use.

[0118] In some specific embodiments, see Figure 7 The device for hydrolyzing biomass includes a distributor frame 420 for fixing and supporting the automatic weighing distributor 100. Figure 1 The distributor frame 420 is mounted on one side of the disc reactor frame 410. Figure 7 The automatic weighing distributor 100 includes a weighing frame 127 , a weighing hopper housing 121 is supported on the weighing frame 127 through a weighing sensor 126 , and the weighing frame 127 is fixedly supported on a distributor frame 420 .

[0119] In some specific embodiments, in order to ensure the mixing effect, see Figure 1 There are two first agitators 201 and two second agitators 202 , the two first agitators 201 are located on a first radial line of the vertical rotation axis 340 and are spaced apart, and the two second agitators 202 are located on another radial line of the vertical rotation axis 340 and are spaced apart.

[0120] It should be understood that in this embodiment, the number of the first agitators 201 and the number of the second agitators 202 are not limited to two, but can be extended as needed along the radial or circumferential direction of the vertical rotation axis 340. In addition, the number of the first agitators 201 and the number of the second agitators 202 can be the same or different.

[0121] In some specific embodiments, see Figures 16 to 18The first agitator 201 and the second agitator 202 are both agitators with the same structure, including a stirring drive mechanism 210, a stirring support structure 220, a stirring paddle 230, a coupling 240 and an auxiliary bearing 250. The stirring support structure 220 is fixedly mounted on the upper end surface of the reactor upper body 310. The stirring drive mechanism 210 is fixedly mounted on the stirring support structure 220. The coupling 240 is arranged on the inner side of the stirring support structure 220, and the output shaft of the stirring drive mechanism 210 extends into the inner side of the stirring support structure 220 and is connected to the stirring paddle 230 through the coupling 240. More specifically, the stirring drive mechanism 210 can be a motor drive mechanism.

[0122] In some specific embodiments, see Fig.17 and Fig.18 The stirring paddle 230 is rotatably fixedly connected to the stirring device support structure 220 through the auxiliary bearing 250. The stirring device 200 of this embodiment ensures the accuracy of the circular jump of the stirring paddle 230 during the operation process and increases the bending strength of the stirring paddle 230 by adding the auxiliary bearing 250.

[0123] In some specific embodiments, the stirring paddle 230 is a hollow spiral blade structure, see Fig.19 The stirring paddle 230 with a hollow spiral blade structure includes a stirring frame 231 , a stirring shaft 232 passing through the stirring frame 231 , and hollow spiral blades 233 staggeredly distributed in the stirring frame 231 along the circumferential direction of the stirring shaft 232 .

[0124] In some specific embodiments, see Figure 2 The device for hydrolyzing biomass includes an observation port 700, a discharge port 800 and a breathing port 900, which are all arranged on the top surface of the reactor upper body 310. In some specific embodiments, the breathing port 900 is made of a waterproof and breathable material, which can quickly discharge air and allow the biomass to quickly contact the catalyst, thereby improving the working efficiency. Preferably, see Figure 2 The breathing port 900 is arranged just above the liquid distributing pipe 510. In some specific embodiments, the observation port 700 is inlaid with a glass sheet to observe the reaction state of the material in the reaction chamber.

[0125] Preferably, see Figure 1 and Figure 2 The first agitator 201 , the feed port 311 , the second agitator 202 and the catalyst distributor 500 are all located on one side of the vertical rotation axis 340 , and the discharge port 800 is located on the other side of the vertical rotation axis 340 and opposite to the catalyst distributor 500 .

[0126] In some specific embodiments, see Figure 1The device for hydrolyzing biomass includes a material temperature measuring device 600, which is installed on the reactor upper body 310. The material temperature measuring device 600 is configured to detect the temperature of the material in the reactor lower body 320. The material temperature measuring device 600 can be an infrared temperature measuring device or a temperature measuring tube. Since the material temperature measuring device 600 does not involve the main invention of the present application, a temperature measuring device in the prior art can be selected, so the specific structure is not described in detail in the present application.

[0127] Specifically, in order to realize the rotation of the reactor lower body 320 relative to the reactor upper body 310 around the vertical rotation axis 340, the device for hydrolyzing biomass includes a rotating mechanism configured to support and drive the reactor lower body 320 to rotate relative to the reactor upper body 310 around the vertical rotation axis 340.

[0128] In some specific embodiments, the slewing mechanism includes a driving gear 412 and an external gear bearing 323. Figure 4 The outer gear of the outer gear bearing 323 is coaxially fixedly connected with the reactor lower body 320. The outer gear of the outer gear bearing 323 is meshed with the driving gear 412, which is not shown in the figure.

[0129] In this embodiment, the external gear bearing 323 can be a commercially available precision gear bearing module, which is used to provide excellent rotation accuracy for the reactor lower body 320 .

[0130] In some specific embodiments, the apparatus for hydrolyzing biomass includes a rotary power source 413, see Fig. 20 The output shaft of the rotary power source 413 is in driving connection with the driving gear 412. More specifically, the rotary power source 413 can be a motor drive mechanism.

[0131] In some specific embodiments, see Figure 1 The apparatus for hydrolyzing biomass includes a disc reactor frame 410 for supporting the reactor 300 .

[0132] See also Fig. 20 The disc reactor frame 410 includes a reactor upper structural support portion 411 and a reactor lower mounting structural portion 414. Figure 1 The reactor upper body 310 is fixedly supported on the reactor upper body structure support portion 411. Figure 4 The inner ring of the outer gear bearing 323 is fixedly connected with a mounting structure 324. The inner ring of the outer gear bearing 323 is fixedly connected with the reactor lower body mounting structure 414 through the mounting structure 324 to support the reactor lower body 320.

[0133] In some specific embodiments, see Fig. 20 , a rotary power source 413 is mounted to the disc reactor frame 410 .

[0134] In some specific embodiments, see Fig.21 The reactor upper body 310 includes a reactor upper body frame 314 and a reactor upper body wall skin 315, and the reactor upper body wall skin 315 is fixedly connected to the reactor upper body frame 314. In some specific embodiments, the reactor upper body frame 314 is made of 316L rectangular tubes to provide support for the reactor upper body 310.

[0135] In some specific embodiments, see Fig.21 The reactor upper body 310 includes a support ear 316, which is fixedly connected to the upper periphery of the reactor upper body frame 314. The support ear 316 is used to be fixedly connected to the reactor upper body structure support part 411 to achieve fixed support of the reactor upper body 310 on the reactor upper body structure support part 411.

[0136] In some specific embodiments, see Fig. 22 The reactor lower body 320 includes a reactor lower body main body 321 and a reactor lower body support structure 322. The reactor lower body main body 321 is made of a light corrosion-resistant material, and the reactor lower body main body 321 is configured to be accommodated in the reactor lower body support structure 322. The outer gear of the external gear bearing 323 is coaxially fixedly connected to the reactor lower body support structure 322 to achieve the coaxial fixed connection between the outer gear of the external gear bearing 323 and the reactor lower body 320. Optionally, the light corrosion-resistant material can be a PP material. The reactor lower body main body 321 of the PP material is connected to the reactor lower body support structure 322 using a special screw group to have excellent mechanical properties.

[0137] In some specific embodiments, see Fig. 22 The device for hydrolyzing biomass includes a rotary seal assembly 325, which is configured to enable a rotary connection and sealing fit between the reactor upper body 310 and the reactor lower body 320. In one embodiment of the rotary seal assembly, the rotary seal assembly 325 is disposed on the top of the reactor lower body 320. In another embodiment of the rotary seal assembly, the rotary seal assembly 325 is disposed at the lower part of the reactor upper body 310.

[0138] The rotary sealing assembly can be a rotary sealing assembly in the prior art, and the specific structure of the rotary sealing assembly does not involve the main invention point of the present application. Therefore, the present application does not elaborate on the specific structure of the rotary sealing assembly.

[0139] Furthermore, the above device is used to continuously and efficiently hydrolyze straw powder. The specific embodiments are as follows: The device, in particular: The diameter and height of the inner cavity of the reactor lower body 320 are 2600×400 mm respectively; the tube length of the liquid distribution channel 511 is 1200 mm, the diameter (inner diameter DN) is 50 mm, 300 liquid distribution holes 512 are arranged at intervals along the liquid distribution channel 511, and the interval between two adjacent liquid distribution holes 512 gradually decreases in an arithmetic progression along the radial direction away from the vertical rotation axis 340, and the apertures of these liquid distribution holes 512 are all 2 mm; the first agitator 201 and the second agitator 202 are 2 agitators respectively, with a total of 4 agitators; the temperature is detected by an infrared temperature measurement system, and when a temperature rise trend appears, the distribution of straw powder and high-concentration inorganic acid can be suspended.

[0140] The straw powder is powder that has passed through a 100-mesh sieve.

[0141] In the following specific application embodiments, the mass of straw powder stored in the second soft-connected hopper 131 can be controlled by adjusting the rotation speed of the multi-blade unloading flap 122; as in Example 1, the mass of straw powder stored in the second soft-connected hopper 131 is controlled to be 20-40kg, specifically 20-25kg, in cross-feeding; as in Example 2, the mass of straw powder stored in the second soft-connected hopper 131 is controlled to be 20-40kg, specifically 35-40kg, in continuous feeding.

[0142] The unit of the solid-to-liquid ratio in the following specific application examples is kg / L.

[0143] In the following examples, the National Renewable Energy Laboratory (NREL) method was used to detect the contents of cellulose, hemicellulose and lignin in biomass, and the cellulose conversion rate and hemicellulose conversion rate were calculated as follows: .

[0144] Wherein, C represents the percentage content of the corresponding component in the biomass, and M represents the mass of the corresponding substance. 原料-纤 Expressed as the cellulose content in the raw material, C 残渣-纤 Expressed as the cellulose content in the residue; C 原料-半纤 Expressed as the hemicellulose content in the raw material, C 残渣-半纤 Expressed as the hemicellulose content in the residue; M 原料 Expressed as the mass of raw material, M 残渣 It indicates the mass of the residue after the reaction is completed.

[0145] In the following examples, the cellulose content in the straw powder is 31.02%, and the hemicellulose content is 18.26%.

[0146] In the present invention, the percentages in the cellulose content and hemicellulose content are all mass percentages.

[0147] In the following examples, the solid-to-liquid ratio is the mass of straw powder / the mass of acid.

[0148] In the following examples, the cellulose / sulfuric acid ratio is (mass of straw powder×content of cellulose in straw powder) / (mass of aqueous sulfuric acid solution×mass concentration of aqueous sulfuric acid solution).

[0149] In the following examples, the sugar is detected by high performance liquid chromatography, and the specific chromatographic conditions include: RezexTM RCM-monosaccharide Ca+2 Size: LC Column 300*7.8mm, injection volume 20 microliters, column oven: 55°C; flow rate: 0.2 ml / min; time: 60min; mobile phase is pure water. Compared with organic acid columns, the detection method provided by the present invention can detect oligosaccharides (DP < 7).

[0150] Example 1 Cross-feeding of biomass powder and high concentration inorganic acid

[0151] The hydrolysis reaction specifically comprises the following steps: (1) The straw powder is introduced into the automatic weighing distributor 100, and the multi-blade feeding flap 122 in the automatic weighing distributor 100 is controlled so that the straw powder is stored in the second flexible connection hopper 131 after quantitative measurement; the multi-blade feeding flap 142 is further controlled so that the straw powder is stored in the second flexible connection hopper 131 or introduced into the reactor lower body 320 through the feed port 311 at a rate of 15 kg / min.

[0152] (2) A 70% w / w sulfuric acid aqueous solution is introduced into the reactor lower body 320 through the catalyst distributor 500 at a flow rate of 10.71 kg / min.

[0153] (3) The reactor lower body 320 is rotated at a rate of 120 rpm. The aqueous sulfuric acid solution is first introduced into the reactor lower body 320 through the catalyst distributor 500, and then the straw powder is introduced into the reactor lower body 320 through the automatic weighing distributor 100. The automatic weighing distributor 100 and the catalyst distributor 500 rotate alternately with each turn of the turntable, and two turns constitute one cycle. During the reaction, the rotation speed of the first agitator 201 and the second agitator 202 is 60 rpm. This entire process allows the straw powder and the catalyst to be uniformly distributed to the entire hydrolysis process while being distributed, and the two interact with each other uniformly and quickly.

[0154] (4) After the reactor lower body 320 was operated for 20 min, the reaction was stopped. After the reaction was completed, the material was taken out through the discharge port 800, washed and dried to obtain 93.24 kg of residue, in which the cellulose content was 17.29% and the hemicellulose content was 7.55%. After continuous high-efficiency hydrolysis, the cellulose conversion rate was 65.36% and the hemicellulose conversion rate was 74.29%.

[0155] This embodiment uses an external infrared temperature sensor system to collect temperature data in real time, ensuring that the temperature is maintained within the range of room temperature ±5°C and controlling the stability during the hydrolysis conversion process.

[0156] According to calculation, this embodiment processes 150 kg of corn stalk powder in 20 minutes of operation; uses 107.14 kg of 70% w / w sulfuric acid aqueous solution; the solid-liquid ratio is 1.4, the acid dosage is 0.5 times the mass of the stalk powder, and the cellulose / sulfuric acid ratio is 0.60. The oligosaccharides with DP < 7 obtained contain 3.05 g / l of cellobiose (glucobiose) and 3.55 g / l of xylobiose.

[0157] Example 2 Cross-feeding of biomass powder and high concentration inorganic acid

[0158] The hydrolysis reaction specifically comprises the following steps: (1) The straw powder is introduced into the automatic weighing distributor 100, and the multi-blade feeding flap 122 in the automatic weighing distributor 100 is controlled so that the straw powder is stored in the second flexible connection hopper 131 after quantitative measurement; the multi-blade feeding flap 142 is further controlled so that the straw powder is stored in the second flexible connection hopper 131 or introduced into the reactor lower body 320 through the feed port 311 at a rate of 15 kg / min.

[0159] (2) A 70% w / w sulfuric acid aqueous solution is introduced into the reactor lower body 320 through the catalyst distributor 500 at a flow rate of 10.71 kg / min.

[0160] (3) The lower body 320 of the reactor is rotated at a speed of 80 rpm. The aqueous sulfuric acid solution is first introduced into the lower body 320 of the reactor through the catalyst distributor 500, and then the straw powder is introduced into the lower body 320 of the reactor through the automatic weighing distributor 100. The automatic weighing distributor 100 and the catalyst distributor 500 rotate alternately with each turn of the turntable, and two turns constitute one cycle. During the reaction, the rotation speed of the first agitator 201 and the second agitator 202 is 40 rpm. This entire process allows the straw powder and the catalyst to be uniformly distributed to the entire hydrolysis process while being distributed, and the two interact with each other uniformly and quickly.

[0161] (4) After the reactor lower body 320 was operated for 20 min, the reaction was stopped. After the reaction was completed, the material was taken out through the discharge port 800, washed and dried to obtain 95.49 kg of residue, in which the cellulose content was 17.90% and the hemicellulose content was 8.17%. After continuous high-efficiency hydrolysis, the cellulose conversion rate was 63.27% and the hemicellulose conversion rate was 71.53%.

[0162] This embodiment uses an external infrared temperature sensor system to collect temperature data in real time, ensuring that the temperature is maintained within the range of room temperature ±5°C and controlling the stability during the hydrolysis conversion process.

[0163] According to calculation, this embodiment processes 150 kg of corn stalk powder in 20 minutes of operation; uses 107.14 kg of 70% w / w sulfuric acid aqueous solution; the solid-liquid ratio is 1.4, the acid dosage is 0.5 times the mass of the stalk powder, and the cellulose / sulfuric acid ratio is 0.60. The oligosaccharides with DP < 7 obtained contain 3.03 g / l of cellobiose (glucobiose) and 3.51 g / l of xylobiose.

[0164] Example 3 Continuous feeding of biomass powder and high concentration inorganic acid

[0165] The hydrolysis reaction specifically comprises the following steps: (1) The straw powder is introduced into the automatic weighing distributor 100, and the multi-blade feeding flap 122 in the automatic weighing distributor 100 is controlled so that the straw powder is stored in the second flexible connection hopper 131 after quantitative measurement; the multi-blade feeding flap 142 is further controlled so that the straw powder is stored in the second flexible connection hopper 131 or introduced into the reactor lower body 320 through the feed port 311 at a rate of 15 kg / min.

[0166] (2) A 70% w / w sulfuric acid aqueous solution is introduced into the reactor lower body 320 through the catalyst distributor 500 at a flow rate of 10.71 kg / min.

[0167] (3) The reactor lower body 320 is rotated at a rate of 120 rpm, and the automatic weighing distributor 100 and the catalyst liquid distributor 100 work continuously; during the reaction, the rotation speed of the first agitator 201 and the second agitator 202 is 60 rpm; this entire process allows the straw powder and the catalyst to be uniformly distributed to the entire hydrolysis process while being distributed to the material and liquid, and the two interact with each other uniformly and quickly.

[0168] (4) After the reactor lower body 320 was operated for 20 min, the reaction was stopped. After the reaction was completed, the material was taken out through the discharge port 800, washed and dried to obtain 191.16 kg of residue, in which the cellulose content was 19.29% and the hemicellulose content was 9.96%. After continuous high-efficiency hydrolysis, the cellulose conversion rate was 60.37% and the hemicellulose conversion rate was 65.24%.

[0169] This embodiment uses an external infrared temperature sensor system to collect temperature data in real time, ensuring that the temperature is maintained within the range of room temperature ±5°C and controlling the stability during the hydrolysis conversion process.

[0170] According to calculation, this embodiment processes 300 kg of corn stalk powder in 20 minutes of operation; a total of 214.29 kg of 70% w / w sulfuric acid aqueous solution is used; the solid-liquid ratio is 1.40, the acid dosage is 0.5 times the mass of the stalk powder, and the cellulose / sulfuric acid ratio is 0.60. The oligosaccharides with DP < 7 obtained contain 2.82 g / l of cellobiose (glucobiose) and 3.11 g / l of xylobiose.

[0171] Example 4 Continuous feeding of biomass powder and high concentration inorganic acid

[0172] The hydrolysis reaction specifically comprises the following steps: (1) The straw powder is introduced into the automatic weighing distributor 100, and the multi-blade feeding flap 122 in the automatic weighing distributor 100 is controlled so that the straw powder is stored in the second flexible connection hopper 131 after quantitative measurement; the multi-blade feeding flap 142 is further controlled so that the straw powder is stored in the second flexible connection hopper 131 or introduced into the reactor lower body 320 through the feed port 311 at a rate of 15 kg / min.

[0173] (2) A 70% w / w sulfuric acid aqueous solution is introduced into the reactor lower body 320 through the catalyst distributor 500 at a flow rate of 10.71 kg / min.

[0174] (3) The lower body 320 of the reactor is rotated at a rate of 200 rpm, and the automatic weighing distributor 100 and the catalyst liquid distributor 100 work continuously; during the reaction, the rotation speed of the first agitator 201 and the second agitator 202 is 80 rpm; this entire process allows the straw powder and the catalyst to be uniformly distributed to the entire hydrolysis process while being distributed to the material and liquid, and the two interact with each other evenly and quickly.

[0175] (4) After the reactor lower body 320 was operated for 20 min, the reaction was stopped. After the reaction was completed, the material was taken out through the discharge port 800, washed and dried to obtain 178.36 kg of residue, in which the cellulose content was 15.23% and the hemicellulose content was 7.12%. After continuous high-efficiency hydrolysis, the cellulose conversion rate was 70.63% and the hemicellulose conversion rate was 76.82%.

[0176] This embodiment uses an external infrared temperature sensor system to collect temperature data in real time, ensuring that the temperature is maintained within the range of room temperature ±5°C and controlling the stability during the hydrolysis conversion process.

[0177] According to calculation, this embodiment processes 300 kg of corn stalk powder in 20 minutes of operation; a total of 214.29 kg of 70% w / w sulfuric acid aqueous solution is used; the solid-liquid ratio is 1.40, the acid dosage is 0.5 times the mass of the stalk powder, and the cellulose / sulfuric acid ratio is 0.60. The oligosaccharides with DP < 7 obtained contain 3.30 g / l of cellobiose (glucobiose) and 3.67 g / l of xylobiose.

[0178] Example 5

[0179] The hydrolysis reaction specifically comprises the following steps: (1) The straw powder is introduced into the automatic weighing distributor 100, and the multi-blade feeding flap 122 in the automatic weighing distributor 100 is controlled so that the straw powder is stored in the second flexible connection hopper 131 after quantitative measurement; the multi-blade feeding flap 142 is further controlled so that the straw powder is stored in the second flexible connection hopper 131 or introduced into the reactor lower body 320 through the feed port 311 at a rate of 15 kg / min.

[0180] (2) A 70% w / w sulfuric acid aqueous solution is introduced into the reactor lower body 320 through the catalyst distributor 500 at a flow rate of 21.43 kg / min.

[0181] (3) The reactor lower body 320 is rotated at a rate of 120 rpm. The aqueous sulfuric acid solution is first introduced into the reactor lower body 320 through the catalyst distributor 500, and then the straw powder is introduced into the reactor lower body 320 through the automatic weighing distributor 100. The automatic weighing distributor 100 and the catalyst distributor 500 rotate alternately with each turn of the turntable, and two turns constitute one cycle. During the reaction, the rotation speed of the first agitator 201 and the second agitator 202 is 60 rpm. This entire process allows the straw powder and the catalyst to be uniformly distributed to the entire hydrolysis process while being distributed, and the two interact with each other uniformly and quickly.

[0182] (4) After the reactor lower body 320 was operated for 20 min, the reaction was stopped. After the reaction was completed, the material was taken out through the discharge port 800, washed and dried to obtain 82.46 kg of residue, in which the cellulose content was 16.03% and the hemicellulose content was 6.19%. After continuous high-efficiency hydrolysis, the cellulose conversion rate was 71.59% and the hemicellulose conversion rate was 81.37%.

[0183] This embodiment uses an external infrared temperature sensor system to collect temperature data in real time, ensuring that the temperature is maintained within the range of room temperature ±5°C and controlling the stability during the hydrolysis conversion process.

[0184] According to calculation, this embodiment processes 150 kg of corn stalk powder in 20 minutes of operation; uses 214.29 kg of 70% w / w sulfuric acid aqueous solution; the solid-liquid ratio is 0.70, and the acid dosage is 1.0 times the mass of the stalk powder. The oligosaccharides with DP < 7 obtained contain 1.67 g / l of cellobiose (glucobiose) and 1.96 g / l of xylobiose.

[0185] Example 6

[0186] The hydrolysis reaction specifically comprises the following steps: (1) The straw powder is introduced into the automatic weighing distributor 100, and the multi-blade feeding flap 122 in the automatic weighing distributor 100 is controlled so that the straw powder is stored in the second flexible connection hopper 131 after quantitative measurement; the multi-blade feeding flap 142 is further controlled so that the straw powder is stored in the second flexible connection hopper 131 or introduced into the reactor lower body 320 through the feed port 311 at a rate of 15 kg / min.

[0187] (2) A 70% w / w sulfuric acid aqueous solution is introduced into the reactor lower body 320 through the catalyst distributor 500 at a flow rate of 42.86 kg / min.

[0188] (3) The reactor lower body 320 is rotated at a rate of 120 rpm. The aqueous sulfuric acid solution is first introduced into the reactor lower body 320 through the catalyst distributor 500, and then the straw powder is introduced into the reactor lower body 320 through the automatic weighing distributor 100. The automatic weighing distributor 100 and the catalyst distributor 500 rotate alternately with each turn of the turntable, and two turns constitute one cycle. During the reaction, the rotation speed of the first agitator 201 and the second agitator 202 is 60 rpm. This entire process allows the straw powder and the catalyst to be uniformly distributed to the entire hydrolysis process while being distributed, and the two interact with each other uniformly and quickly.

[0189] (4) After the reactor lower body 320 was operated for 20 min, the reaction was stopped. After the reaction was completed, the material was taken out through the discharge port 800, washed and dried, and 79.13 kg of residue was obtained. The cellulose content in the residue was 11.54%, and the hemicellulose content was 5.68%. After continuous high-efficiency hydrolysis, the cellulose conversion rate was 80.37%, and the hemicellulose conversion rate was 83.58%.

[0190] This embodiment uses an external infrared temperature sensor system to collect temperature data in real time, ensuring that the temperature is maintained within the range of room temperature ±5°C and controlling the stability during the hydrolysis conversion process.

[0191] According to calculation, this embodiment processes 150 kg of corn stalk powder in 20 minutes of operation; a total of 428.57 kg of 70% w / w sulfuric acid aqueous solution is used; the solid-liquid ratio is 0.35, and the acid dosage is 2.0 times the mass of the stalk powder. The oligosaccharides with DP < 7 obtained contain 0.94 g / l of cellobiose (glucobiose) and 1.03 g / l of xylobiose ( Fig.23 ).

[0192] Example 7

[0193] The hydrolysis reaction specifically comprises the following steps: (1) The straw powder is introduced into the automatic weighing distributor 100, and the multi-blade feeding flap 122 in the automatic weighing distributor 100 is controlled so that the straw powder is stored in the second flexible connection hopper 131 after quantitative measurement; the multi-blade feeding flap 142 is further controlled so that the straw powder is stored in the second flexible connection hopper 131 or introduced into the reactor lower body 320 through the feed port 311 at a rate of 15 kg / min.

[0194] (2) A 75% w / w sulfuric acid aqueous solution is introduced into the reactor lower body 320 through the catalyst distributor 500 at a flow rate of 20 kg / min.

[0195] (3) The reactor lower body 320 is rotated at a rate of 120 rpm. The aqueous sulfuric acid solution is first introduced into the reactor lower body 320 through the catalyst distributor 500, and then the straw powder is introduced into the reactor lower body 320 through the automatic weighing distributor 100. The automatic weighing distributor 100 and the catalyst distributor 500 rotate alternately with each turn of the turntable, and two turns constitute one cycle. During the reaction, the rotation speed of the first agitator 201 and the second agitator 202 is 60 rpm. This entire process allows the straw powder and the catalyst to be uniformly distributed to the entire hydrolysis process while being distributed, and the two interact with each other uniformly and quickly.

[0196] (4) After the reactor lower body 320 was operated for 20 min, the reaction was stopped. After the reaction was completed, the material was taken out through the discharge port 800, washed and dried, and 76.24 kg of residue was obtained. The cellulose content in the residue was 9.98%, and the hemicellulose content was 4.62%. After continuous high-efficiency hydrolysis, the cellulose conversion rate was 83.64%, and the hemicellulose conversion rate was 87.13%.

[0197] This embodiment uses an external infrared temperature sensor system to collect temperature data in real time, ensuring that the temperature is maintained within the range of room temperature ±5°C and controlling the stability during the hydrolysis conversion process.

[0198] According to calculation, this embodiment processes 150 kg of corn stalk powder in 20 minutes of operation; uses 200.00 kg of 75% w / w sulfuric acid aqueous solution; the solid-liquid ratio is 0.75, and the acid dosage is 1.0 times the mass of the stalk powder. The oligosaccharides with DP < 7 obtained contain 2.14 g / l of cellobiose (glucobiose) and 2.23 g / l of xylobiose.

[0199] Example 8

[0200] The hydrolysis reaction specifically comprises the following steps: (1) The straw powder is introduced into the automatic weighing distributor 100, and the multi-blade feeding flap 122 in the automatic weighing distributor 100 is controlled so that the straw powder is stored in the second flexible connection hopper 131 after quantitative measurement; the multi-blade feeding flap 142 is further controlled so that the straw powder is stored in the second flexible connection hopper 131 or introduced into the reactor lower body 320 through the feed port 311 at a rate of 15 kg / min.

[0201] (2) An 80% w / w aqueous sulfuric acid solution is introduced into the reactor lower body 320 through the catalyst distributor 500 at a flow rate of 18.75 kg / min.

[0202] (3) The reactor lower body 320 is rotated at a rate of 120 rpm. The aqueous sulfuric acid solution is first introduced into the reactor lower body 320 through the catalyst distributor 500, and then the straw powder is introduced into the reactor lower body 320 through the automatic weighing distributor 100. The automatic weighing distributor 100 and the catalyst distributor 500 rotate alternately with each turn of the turntable, and two turns constitute one cycle. During the reaction, the rotation speed of the first agitator 201 and the second agitator 202 is 60 rpm. This entire process allows the straw powder and the catalyst to be uniformly distributed to the entire hydrolysis process while being distributed, and the two interact with each other uniformly and quickly.

[0203] (4) After the reactor lower body 320 was operated for 20 min, the reaction was stopped. After the reaction was completed, the material was taken out through the discharge port 800, washed and dried to obtain 78.19 kg of residue, in which the cellulose content was 5.49% and the hemicellulose content was 1.35%. After continuous high-efficiency hydrolysis, the cellulose conversion rate was 90.78% and the hemicellulose conversion rate was 96.14%.

[0204] This embodiment uses an external infrared temperature sensor system to collect temperature data in real time, ensuring that the temperature is maintained within the range of room temperature ±5°C and controlling the stability during the hydrolysis conversion process.

[0205] According to calculation, this embodiment processes 150 kg of corn stalk powder in 20 minutes of operation; uses 187.50 kg of 80% w / w sulfuric acid aqueous solution; the solid-liquid ratio is 0.8, and the acid dosage is 1.0 times the mass of the stalk powder. The oligosaccharides with DP < 7 obtained contain 2.42 g / l of cellobiose (glucobiose) and 2.62 g / l of xylobiose.

[0206] Example 9

[0207] The hydrolysis reaction specifically comprises the following steps: (1) The straw powder is introduced into the automatic weighing distributor 100, and the multi-blade feeding flap 122 in the automatic weighing distributor 100 is controlled so that the straw powder is stored in the second flexible connection hopper 131 after quantitative measurement; the multi-blade feeding flap 142 is further controlled so that the straw powder is stored in the second flexible connection hopper 131 or introduced into the reactor lower body 320 through the feed port 311 at a rate of 10 kg / min.

[0208] (2) An 80% w / w aqueous sulfuric acid solution is introduced into the reactor lower body 320 through the catalyst distributor 500 at a flow rate of 12.50 kg / min.

[0209] (3) The reactor lower body 320 is rotated at a rate of 120 rpm. The aqueous sulfuric acid solution is first introduced into the reactor lower body 320 through the catalyst distributor 500, and then the straw powder is introduced into the reactor lower body 320 through the automatic weighing distributor 100. The automatic weighing distributor 100 and the catalyst distributor 500 rotate alternately with each turn of the turntable, and two turns constitute one cycle. During the reaction, the rotation speed of the first agitator 201 and the second agitator 202 is 60 rpm. This entire process allows the straw powder and the catalyst to be uniformly distributed to the entire hydrolysis process while being distributed, and the two interact with each other uniformly and quickly.

[0210] (4) After the reactor lower body 320 was operated for 30 min, the reaction was stopped. After the reaction was completed, the material was taken out through the discharge port 800, washed and dried, and 76.43 kg of residue was obtained. The cellulose content in the residue was 5.22%, and the hemicellulose content was 0.98%. After continuous high-efficiency hydrolysis, the cellulose conversion rate was 91.43%, and the hemicellulose conversion rate was 97.26%.

[0211] This embodiment uses an external infrared temperature sensor system to collect temperature data in real time, ensuring that the temperature is maintained within the range of room temperature ±5°C and controlling the stability during the hydrolysis conversion process.

[0212] According to calculation, this embodiment processes 150 kg of corn stalk powder in 30 minutes of operation; uses 187.50 kg of 80% w / w sulfuric acid aqueous solution; the solid-liquid ratio is 0.80, and the acid dosage is 1.0 times the mass of the stalk powder. The oligosaccharides with DP < 7 obtained contain 2.44 g / l of cellobiose (glucobiose) and 2.67 g / l of xylobiose.

[0213] Example 10

[0214] The hydrolysis reaction specifically comprises the following steps: (1) The straw powder is introduced into the automatic weighing distributor 100, and the multi-blade feeding flap 122 in the automatic weighing distributor 100 is controlled so that the straw powder is stored in the second flexible connection hopper 131 after quantitative measurement; the multi-blade feeding flap 142 is further controlled so that the straw powder is stored in the second flexible connection hopper 131 or introduced into the reactor lower body 320 through the feed port 311 at a rate of 7.50 kg / min.

[0215] (2) An 80% w / w aqueous sulfuric acid solution is introduced into the reactor lower body 320 through the catalyst distributor 500 at a flow rate of 9.38 kg / min.

[0216] (3) The reactor lower body 320 is rotated at a rate of 120 rpm. The aqueous sulfuric acid solution is first introduced into the reactor lower body 320 through the catalyst distributor 500, and then the straw powder is introduced into the reactor lower body 320 through the automatic weighing distributor 100. The automatic weighing distributor 100 and the catalyst distributor 500 rotate alternately with each turn of the turntable, and two turns constitute one cycle. During the reaction, the rotation speed of the first agitator 201 and the second agitator 202 is 60 rpm. This entire process allows the straw powder and the catalyst to be uniformly distributed to the entire hydrolysis process while being distributed, and the two interact with each other uniformly and quickly.

[0217] (4) After the reactor lower body 320 was operated for 40 min, the reaction was stopped. After the reaction was completed, the material was taken out through the discharge port 800, washed and dried to obtain 75.37 kg of residue, in which the cellulose content was 4.82% and the hemicellulose content was 0.71%. After continuous high-efficiency hydrolysis, the cellulose conversion rate was 92.19% and the hemicellulose conversion rate was 98.04%.

[0218] This embodiment uses an external infrared temperature sensor system to collect temperature data in real time, ensuring that the temperature is maintained within the range of room temperature ±5°C and controlling the stability during the hydrolysis conversion process.

[0219] According to calculation, this embodiment processes 150 kg of corn stalk powder in 40 minutes of operation; uses 187.50 kg of 80% w / w sulfuric acid aqueous solution; the solid-liquid ratio is 0.8, and the acid dosage is 1.0 times the mass of the stalk powder. The oligosaccharides with DP < 7 obtained contain 2.46 g / l of cellobiose (glucobiose) and 2.67 g / l of xylobiose.

[0220] Embodiment 11

[0221] The hydrolysis reaction specifically comprises the following steps: (1) The straw powder is introduced into the automatic weighing distributor 100, and the multi-blade feeding flap 122 in the automatic weighing distributor 100 is controlled so that the straw powder is stored in the second flexible connection hopper 131 after quantitative measurement; the multi-blade feeding flap 142 is further controlled so that the straw powder is stored in the second flexible connection hopper 131 or introduced into the reactor lower body 320 through the feed port 311 at a rate of 15 kg / min.

[0222] (2) A 30% w / w hydrochloric acid aqueous solution is introduced into the reactor lower body 320 through the catalyst distributor 500 at a flow rate of 18.75 kg / min.

[0223] (3) The reactor lower body 320 is rotated at a rate of 120 rpm. The aqueous sulfuric acid solution is first introduced into the reactor lower body 320 through the catalyst distributor 500, and then the straw powder is introduced into the reactor lower body 320 through the automatic weighing distributor 100. The automatic weighing distributor 100 and the catalyst distributor 500 rotate alternately with each turn of the turntable, and two turns constitute one cycle. During the reaction, the rotation speed of the first agitator 201 and the second agitator 202 is 60 rpm. This entire process allows the straw powder and the catalyst to be uniformly distributed to the entire hydrolysis process while being distributed, and the two interact with each other uniformly and quickly.

[0224] (4) After the reactor lower body 320 was operated for 20 min, the reaction was stopped. After the reaction was completed, the material was taken out through the discharge port 800, washed and dried to obtain 91.24 kg of residue, in which the cellulose content was 9.55% and the hemicellulose content was 4.40%. After continuous high-efficiency hydrolysis, the cellulose conversion rate was 81.27% and the hemicellulose conversion rate was 85.34%.

[0225] This embodiment uses an external infrared temperature sensor system to collect temperature data in real time, ensuring that the temperature is maintained within the range of room temperature ±5°C and controlling the stability during the hydrolysis conversion process.

[0226] According to calculation, this embodiment processes 150 kg of corn stalk powder in 20 minutes of operation; uses 187.50 kg of 30% w / w hydrochloric acid aqueous solution; the solid-liquid ratio is 0.8, the acid dosage is 0.375 times the mass of the stalk powder, and the cellulose / hydrochloric acid ratio is 0.80. The oligosaccharides with DP < 7 obtained contain 1.08 g / l of cellobiose (glucobiose) and 1.19 g / l of xylobiose.

[0227] Example 12

[0228] The hydrolysis reaction specifically comprises the following steps: (1) The straw powder is introduced into the automatic weighing distributor 100, and the multi-blade feeding flap 122 in the automatic weighing distributor 100 is controlled so that the straw powder is stored in the second flexible connection hopper 131 after quantitative measurement; the multi-blade feeding flap 142 is further controlled so that the straw powder is stored in the second flexible connection hopper 131 or introduced into the reactor lower body 320 through the feed port 311 at a rate of 15 kg / min.

[0229] (2) A 72% w / w phosphoric acid aqueous solution is introduced into the reactor lower body 320 through the catalyst distributor 500 at a flow rate of 18.75 kg / min.

[0230] (3) The reactor lower body 320 is rotated at a rate of 120 rpm. The aqueous sulfuric acid solution is first introduced into the reactor lower body 320 through the catalyst distributor 500, and then the straw powder is introduced into the reactor lower body 320 through the automatic weighing distributor 100. The automatic weighing distributor 100 and the catalyst distributor 500 rotate alternately with each turn of the turntable, and two turns constitute one cycle. During the reaction, the rotation speed of the first agitator 201 and the second agitator 202 is 60 rpm. This entire process allows the straw powder and the catalyst to be uniformly distributed to the entire hydrolysis process while being distributed, and the two interact with each other uniformly and quickly.

[0231] (4) After the reactor lower body 320 was operated for 20 min, the reaction was stopped. After the reaction was completed, the material was taken out through the discharge port 800, washed and dried to obtain 86.37 kg of residue, in which the cellulose content was 8.23% and the hemicellulose content was 3.20%. After continuous high-efficiency hydrolysis, the cellulose conversion rate was 84.73% and the hemicellulose conversion rate was 89.92%.

[0232] This embodiment uses an external infrared temperature sensor system to collect temperature data in real time, ensuring that the temperature is maintained within the range of room temperature ±5°C and controlling the stability during the hydrolysis conversion process.

[0233] According to calculation, this embodiment processes 150 kg of corn stalk powder in 20 minutes of operation; uses 187.50 kg of 72% w / w phosphoric acid aqueous solution; the solid-liquid ratio is 0.8, and the amount of acid used is 0.9 times the mass of the stalk powder. The oligosaccharides with DP < 7 obtained contain 1.13 g / l of cellobiose (glucobiose) and 1.27 g / l of xylobiose.

[0234] Example 13

[0235] The hydrolysis reaction specifically comprises the following steps: (1) The straw powder is introduced into the automatic weighing distributor 100, and the multi-blade feeding flap 122 in the automatic weighing distributor 100 is controlled so that the straw powder is stored in the second flexible connection hopper 131 after quantitative measurement; the multi-blade feeding flap 142 is further controlled so that the straw powder is stored in the second flexible connection hopper 131 or introduced into the reactor lower body 320 through the feed port 311 at a rate of 15 kg / min.

[0236] (2) An 80% w / w nitric acid aqueous solution is introduced into the reactor lower body 320 through the catalyst distributor 500 at a flow rate of 18.75 kg / min.

[0237] (3) The reactor lower body 320 is rotated at a rate of 120 rpm. The aqueous sulfuric acid solution is first introduced into the reactor lower body 320 through the catalyst distributor 500, and then the straw powder is introduced into the reactor lower body 320 through the automatic weighing distributor 100. The automatic weighing distributor 100 and the catalyst distributor 500 rotate alternately with each turn of the turntable, and two turns constitute one cycle. During the reaction, the rotation speed of the first agitator 201 and the second agitator 202 is 60 rpm. This entire process allows the straw powder and the catalyst to be uniformly distributed to the entire hydrolysis process while being distributed, and the two interact with each other uniformly and quickly.

[0238] (4) After the reactor lower body 320 was operated for 20 min, the reaction was stopped. After the reaction was completed, the material was taken out through the discharge port 800, washed and dried to obtain 89.51 kg of residue, in which the cellulose content was 16.24% and the hemicellulose content was 8.08%. After continuous high-efficiency hydrolysis, the cellulose conversion rate was 68.75% and the hemicellulose conversion rate was 73.61%.

[0239] This embodiment uses an external infrared temperature sensor system to collect temperature data in real time, ensuring that the temperature is maintained within the range of room temperature ±5°C and controlling the stability during the hydrolysis conversion process.

[0240] According to calculation, this embodiment processes 150 kg of corn stalk powder in 20 minutes of operation; uses 187.50 kg of 80% w / w nitric acid aqueous solution; the solid-liquid ratio is 0.8, and the acid dosage is 1.0 times the mass of the stalk powder. The oligosaccharides with DP < 7 obtained contain 0.92 g / l of cellobiose (glucobiose) and 0.99 g / l of xylobiose.

[0241] Comparative Examples 1-5

[0242] Replace the hydrolysis device and hydrolyze the straw powder as follows:

[0243]

[0244] Note: The unit of liquid-to-solid ratio is L / kg.

Claims

1. Application of a device for hydrolyzing biomass in hydrolyzing biomass, characterized in that: The device for hydrolyzing biomass comprises: A reactor (300) comprising a reactor upper body (310) and a reactor lower body (320), wherein the reactor upper body (310) covers the reactor lower body (320) and is provided with a feed inlet (311) and a discharge port (800) at the top, wherein the feed inlet (311) is configured to allow biomass powder to pass into the reactor lower body (320), and the reactor lower body (320) is configured to be rotatable relative to the reactor upper body (310) around a vertical rotation axis (340); A catalyst liquid distributor (500), connected below the reactor upper body (310) and configured to distribute a high-concentration inorganic acid in the reactor lower body (320); and a first stirrer (201) and a second stirrer (202), both connected to the reactor upper body (310) and extending into the reactor lower body (320); The catalyst liquid distributor (500), the second agitator (202), the feed port (311) and the first agitator (201) are sequentially arranged at intervals along the rotation direction of the reactor lower body (320); The biomass powder is introduced into the reactor lower body (320) through the feed port (311), and the high-concentration inorganic acid is introduced into the reactor lower body (320) through the catalyst liquid distributor (500). The reactor lower body (320), the first agitator (201), and the second agitator (202) are rotated, and the biomass powder is subjected to a hydrolysis reaction by the high-concentration inorganic acid. After the reaction stops, the biomass powder is discharged from the discharge port (800); The inorganic acid is any one or a combination of sulfuric acid, hydrochloric acid, nitric acid and phosphoric acid; When the inorganic acid is sulfuric acid, nitric acid or phosphoric acid, the concentration of the high-concentration inorganic acid is 65wt% or more; when the inorganic acid is hydrochloric acid, the concentration of the high-concentration inorganic acid is 25wt%-35wt%; The mass of the inorganic acid is 0.3-1.2 times that of the biomass powder.

2. The use according to claim 1, characterized in that: The biomass is any one or a combination of wheat straw, corn straw, rice straw, sorghum straw, cotton straw, bagasse, corn cob, switchgrass, reed and rapeseed.

3. The use according to claim 1, characterized in that: The rate ratio of the high-concentration inorganic acid to the biomass powder passing into the reactor lower body (320) is 0.5-3:

1.

4. The use according to claim 1, characterized in that: The rotation speed of the reactor lower body (320) is 50-500 rpm; the rotation speeds of the first agitator (201) and the second agitator (202) are independently selected from 10-80 rpm.

5. The use according to claim 1, characterized in that: The reaction temperature is 20-35°C.

6. The use according to claim 1, characterized in that: The catalyst liquid distributor (500) comprises: a liquid distribution channel (511), the liquid distribution channel (511) extending radially along the vertical rotation axis (340); and a plurality of liquid distribution holes (512), wherein the high-concentration inorganic acid can flow out from the liquid distribution channel (511) through the plurality of liquid distribution holes (512) to the reactor lower body (320); the plurality of liquid distribution holes (512) are arranged at intervals along the liquid distribution channel (511), and the interval between two adjacent liquid distribution holes (512) gradually decreases in an arithmetic progression along a radial direction away from the vertical rotation axis.

7. The use according to claim 6, characterized in that: The catalyst liquid distributor (500) comprises a liquid distribution pipe (510); the liquid distribution channel (511) is defined by the inner wall of the liquid distribution pipe (510); and the plurality of liquid distribution holes (512) are provided on the pipe wall of the liquid distribution pipe (510).

8. The use according to claim 7, characterized in that: The device for hydrolyzing biomass comprises a connecting flange (530), which is mounted on the reactor upper body (310) and is used to connect to an external catalyst supply device; The catalyst liquid distributor (500) comprises a liquid distribution pipe adapter (520), and the liquid distribution pipe adapter (520) connects the liquid distribution pipe (510) and the connecting flange (530).

9. The use according to any one of claims 1 to 8, characterized in that The device for hydrolyzing biomass comprises an automatic weighing distributor (100), and the automatic weighing distributor (100) is connected to the feed inlet (311).

10. The use according to claim 9, characterized in that: The automatic weighing distributor (100) comprises a weighing hopper housing (121), a second flexible connection hopper (131), a biomass distributor housing (141), an introduction hopper (151), a multi-blade unloading flap (122), a multi-blade distribution flap (142), and a weighing sensor (126); the weighing sensor (126) is arranged on the outside of the weighing hopper housing (121); the weighing hopper housing (121), the second flexible connection hopper (131), the biomass distributor housing (141), and the introduction hopper (151) are sequentially connected from top to bottom to form a distribution channel (110), and the biomass powder can enter the feed channel of the reactor upper body (310) through the distribution channel (110). The multi-blade material discharging flap (122) is arranged in the material distributing channel (110) in a section of the weighing hopper shell (121), and the multi-blade material distributing flap (142) is arranged in the material distributing channel (110) in a section of the biomass distributor shell (141), and both are rotatable around their respective rotation axes; the speed of the multi-blade material distributing flap (142) in the automatic weighing distributor (100) is controlled to regulate the rate at which the biomass powder enters the reactor lower body (320), and the ratio of the speed of the multi-blade material distributing flap (142) to the speed at which the biomass powder enters the reactor lower body (320) is 2-8 rpm: 1 kg / min.

11. The use according to claim 10, characterized in that: The rotation axis of the multi-blade material discharge flap (122) and the rotation axis of the multi-blade material distribution flap (142) both extend radially along the vertical rotation axis (340) and are located in the same vertical plane; the multi-blade material discharge flap (122) and the multi-blade material distribution flap (142) both form conical surfaces when they rotate, and the two formed conical surfaces overlap with the projection area of ​​the feed port (311) in the top view direction and are located in the fan-shaped area within the reactor lower body (320).

12. The use according to claim 11, characterized in that: The multi-blade unloading flap (122) and the multi-blade distribution flap (142) divide the distribution channel (110) into a storage and weighing section (1101), a discharge section (1102) and a smooth transition section (1103); the storage and weighing section (1101) is used to receive, temporarily store and weigh the biomass powder; the distribution channel (110) is connected to the feed port (311) of the reactor upper body (310) through the lower port of the smooth transition section (1103); The material discharging flap (122) is located between the material storage weighing section (1101) and the material discharging section (1102), and is configured to achieve the discharging of biomass powder in the material storage weighing section (1101) to the material discharging section (1102) when rotating; the multi-blade material distributing flap (142) is located between the material discharging section (1102) and the smooth transition section (1103), and is configured to achieve the discharging of biomass powder in the material discharging section (1102) to the smooth transition section (1103) when rotating.

13. The use according to claim 12, characterized in that: The projection area is trapezoidal; the cross-sections of the material storage weighing section (1101) and the material discharge section (1102) perpendicular to the vertical direction are both rectangular; and the area of ​​the rectangle is greater than the area of ​​the projection area.

14. The use according to claim 10, characterized in that: The device for hydrolyzing biomass comprises a first flexible connection hopper (111), wherein the first flexible connection hopper (111) connects a weighing hopper housing (121) in the automatic weighing distributor (100) with an external biomass pneumatic conveying device.

15. The use according to claim 10, characterized in that The automatic weighing distributor (100) comprises a first bearing seat (123) and a second bearing seat (143); the multi-blade material discharging flap (122) is installed in the weighing hopper housing (121) via the first bearing seat (123); and the multi-blade material distributing flap (142) is installed in the biomass distributor housing (141) via the second bearing seat (143).

16. The use according to claim 10, characterized in that: The device for hydrolyzing biomass comprises a distributor frame (420) for fixedly supporting the automatic weighing distributor (100); The automatic weighing distributor (100) comprises a weighing frame (127), the weighing hopper housing (121) is supported on the weighing frame (127) via the weighing sensor (126), and the weighing frame (127) is fixedly supported on the distributor frame (420).

17. The use according to claim 10, characterized in that: The automatic weighing material distributor (100) comprises a driving mechanism, wherein the driving mechanism is configured to respectively drive the multi-blade unloading flap (122) and the multi-blade material distribution flap (142) to rotate.

18. The use according to claim 17, characterized in that The driving mechanism is a motor driving mechanism.

19. The use according to any one of claims 1 to 6, characterized in that A plurality of the first agitators (201) and the second agitators (202) are provided, wherein the plurality of the first agitators (201) are located on a first radial line of the vertical rotation axis (340) and are spaced apart, and the plurality of the second agitators (202) are located on another radial line of the vertical rotation axis (340) and are spaced apart.

20. The use according to any one of claims 1 to 6, characterized in that The first agitator (201) and the second agitator (202) have the same structure, comprising: Agitator paddle (230); An agitator supporting structure (220) is fixedly mounted on the upper end surface of the reactor upper body (310); A stirring drive mechanism (210) fixedly mounted on the stirrer support structure (220); A coupling (240) is arranged on the inner side of the agitator support structure (220); the output shaft of the agitator drive mechanism (210) extends into the inner side of the agitator support structure (220) and is connected to the agitator paddle (230) via the coupling (240); and an auxiliary bearing (250), wherein the stirring paddle (230) is rotatably fixedly connected to the stirring device supporting structure (220) via the auxiliary bearing (250).

21. The use according to claim 20, characterized in that The stirring paddle (230) is a hollow spiral blade structure, comprising a stirring frame (231), a stirring shaft (232) passing through the stirring frame (231), and hollow spiral blades (233) staggeredly distributed in the stirring frame (231) along the circumference of the stirring shaft (232).

22. The use according to claim 1, characterized in that The device for hydrolyzing biomass comprises an observation port (700) and a breathing port (900), and the observation port (700) and the breathing port (900) are both arranged on the reactor upper body (310).

23. The use according to claim 22, characterized in that The device for hydrolyzing biomass comprises a material temperature measuring device (600), wherein the material temperature measuring device (600) is installed on the reactor upper body (310); the material temperature measuring device (600) is configured to detect the temperature of the material in the reactor lower body (320).

24. The use according to claim 1, characterized in that The device for hydrolyzing biomass comprises a rotating mechanism configured to support and drive the reactor lower body (320) to rotate relative to the reactor upper body (310) around a vertical rotation axis (340).

25. The use according to claim 24, characterized in that The rotary mechanism comprises: Drive gear (412); and an external gear bearing (323), wherein the external gear of the external gear bearing (323) is coaxially fixedly connected to the reactor lower body (320), and the external gear of the external gear bearing (323) is meshed with the driving gear (412).

26. The use according to claim 25, characterized in that The device for hydrolyzing biomass comprises a rotary power source (413), and an output shaft of the rotary power source (413) is drivingly connected to the driving gear (412).

27. The use according to claim 26, characterized in that The device for hydrolyzing biomass comprises a mounting structure (324) and a disc reactor frame (410) for supporting the reactor (300); the disc reactor frame (410) comprises a reactor upper body structural support portion (411) and a reactor lower body mounting structure portion (414); the reactor upper body (310) is fixedly supported on the reactor upper body structural support portion (411); the mounting structure (324) is fixedly connected to the inner ring of the external gear bearing (323), and the inner ring of the external gear bearing (323) is fixedly connected to the reactor lower body mounting structure portion (414) via the mounting structure (324).

28. The use according to claim 27, characterized in that The reactor upper body (310) comprises a reactor upper body frame (314) and a reactor upper body wall skin (315), wherein the reactor upper body wall skin (315) is fixedly connected to the reactor upper body frame (314).

29. The use according to claim 28, characterized in that The reactor upper body (310) comprises a support ear (316), wherein the support ear (316) is fixedly connected to the upper peripheral portion of the reactor upper body frame (314), and the support ear (316) is used to be fixedly connected to the reactor upper body structure support portion (411) to achieve fixed support of the reactor upper body (310) on the reactor upper body structure support portion (411).

30. The use according to claim 27, characterized in that The reactor lower body (320) comprises a reactor lower body main body (321) and a reactor lower body support structure (322); the reactor lower body main body (321) is made of a lightweight corrosion-resistant material, and the reactor lower body main body (321) is configured to be accommodated in the reactor lower body support structure (322); the external gear of the external gear bearing (323) is coaxially fixedly connected to the reactor lower body support structure (322), so as to achieve coaxially fixed connection between the external gear of the external gear bearing (323) and the reactor lower body (320).

31. The use according to claim 1, characterized in that The device for hydrolyzing biomass comprises a rotating sealing assembly (325), wherein the rotating sealing assembly (325) is configured to enable the upper reactor body (310) and the lower reactor body (320) to be rotationally connected and sealed.

32. The use according to claim 31, characterized in that The rotating seal assembly (325) is disposed on the top of the reactor lower body (320).

33. The use according to claim 31, characterized in that The rotating sealing assembly (325) is arranged at the lower part of the reactor upper body (310).

34. The use according to claim 1, characterized in that The reactor lower body (320) is cylindrical.

35. The use according to claim 1, characterized in that The reactor (300) is disc-shaped as a whole.

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