Use of an apparatus for hydrolyzing biomass in hydrolyzing biomass

Abstract

The application relates to the field of biomass hydrolysis, and particularly discloses application of a device for hydrolyzing biomass in hydrolyzing biomass, wherein the device comprises a reactor, a catalyst liquid distributor and first and second stirrers; the reactor comprises an upper reactor body and a lower reactor body, the upper reactor body covers the lower reactor body, and the upper reactor body is provided with a feeding port and a discharging port at the top; the catalyst liquid distributor is connected to the lower part of the upper reactor body; the first and second stirrers are both connected to the upper reactor body and extend into the lower reactor body; the catalyst liquid distributor, the second stirrer, the feeding port and the first stirrer are sequentially and spacedly arranged along the rotation direction of the lower reactor body. The biomass powder is fed into the lower reactor body through the feeding port, the high-concentration inorganic acid is fed into the lower reactor body through the catalyst liquid distributor, the lower reactor body, the first stirrer and the second stirrer rotate, and the biomass powder is hydrolyzed by the high-concentration inorganic acid.

Description

TECHNICAL FIELD

[0001] The present application relates to the field of biomass hydrolysis, and in particular to an application of a device for hydrolyzing biomass in hydrolyzing biomass. BACKGROUND

[0002] Biomass is mainly composed of cellulose, hemicellulose and lignin components, and has a rich proportion of carbohydrates, which has important application value in the fields of energy, materials and chemical industry. Through the sugar platform approach, it is used to produce biofuels to replace traditional fossil energy, so as to achieve the purpose of energy substitution and greenhouse gas emission reduction. In addition, the use of non-food biomass effectively avoids the current development situation of "competing with people for food and competing with food for land".

[0003] At present, the production device and method applied to straw hydrolysis for sugar production still have many deficiencies. The immaturity of straw sugar production equipment leads to incomplete saccharification, lack of precision in process control, etc., making the sugar production process unstable, affecting product quality and thus failing to meet market demand. The most common method of straw sugar production is to use cellulase to enzymatically hydrolyze straw treated by chemical method, which is the way many enterprises use straw for industrialization. However, the buying and selling of cellulase has not yet formed an open market, and the complex enzyme system for treating lignocellulose is also not transparent, and the guarantee conditions for screening, storage and application are relatively high. At the same time, the invalid degradation of carbohydrates in traditional chemical pretreatment of biomass, the high load cost of special equipment for high temperature and high pressure, and the wastewater treatment problem caused by the use of a large amount of chemical reagents. Therefore, the solution to these problems of straw hydrolysis for sugar production requires more technical research and practice.

[0004] To overcome the key problems in the above-mentioned straw sugar production process, many researchers have proposed corresponding solutions. Chinese invention CN 117966502 A discloses a pretreatment method for lignin extraction from lignocellulosic raw materials, but this method needs to use a large amount of water to wash the materials in the industrial production process, resulting in a large amount of industrial wastewater; Chinese invention CN 117947224 A discloses a preparation method of biomass water-soluble sugar, but the hydrolysis temperature of this method is between 140℃ and 250℃, which requires a large amount of energy consumption and special high temperature and high pressure equipment, bringing great 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 processing period, greatly increasing the production cost of the process.

[0005] The information disclosed in this BACKGROUND section is only intended to increase the understanding of the general background of the application, and should not be considered as recognition or in any form as admitting that this information constitutes prior art known to those of ordinary skill in the art. SUMMARY

[0006] The technical problem solved by the first aspect of the present application is to provide a device for hydrolyzing biomass, which is suitable for hydrolyzing biomass with high-concentration inorganic acid and achieving high-efficiency production.

[0007] To solve the above technical problem, the first aspect of the present application discloses a device for hydrolyzing biomass, which comprises:

[0008] a reactor comprising an upper reactor body and a lower reactor body, the upper reactor body covering the lower reactor body and being provided with a feeding port and a discharging port at the top, the feeding port being configured to allow biomass powder to enter the lower reactor body, and the lower reactor body being configured to rotate relative to the upper reactor body around a vertical rotation axis;

[0009] an automatic weighing distributor connected to the feeding port and configured to distribute biomass powder in the lower reactor body through the feeding port;

[0010] a catalyst liquid distributor connected below the upper reactor body and configured to distribute high-concentration inorganic acid in the lower reactor body;

[0011] and a first stirrer and a second stirrer, both of which are connected to the upper reactor body and extend into the lower reactor body;

[0012] The catalyst liquid distributor, the second stirrer, the feeding port and the first stirrer are sequentially and spacedly arranged along the rotation direction of the lower reactor body.

[0013] In some embodiments, the catalyst liquid distributor comprises 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 out of the liquid distribution channel to the lower reactor body through the plurality of liquid distribution holes. The plurality of liquid distribution holes are spacedly arranged along the liquid distribution channel, and the spacing between adjacent two liquid distribution holes gradually decreases in an equidifference sequence along the radial direction away from the vertical rotation axis.

[0014] 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. The plurality of liquid distribution holes are formed on the pipe wall of the liquid distribution pipe.

[0015] In some embodiments, the device for hydrolyzing biomass comprises a connecting flange installed on the upper reactor body for connecting with an external catalyst supply device. The catalyst liquid distributor comprises a liquid distribution pipe adapter connecting the liquid distribution pipe and the connecting flange.

[0016] In some embodiments, the device for hydrolyzing biomass comprises an automatic weighing distributor connected to the inlet.

[0017] Specifically, the automatic weighing distributor comprises a weighing hopper shell, a second soft connection hopper, a biomass distributor shell, a guide hopper, a multi-blade unloading flap, a multi-blade distributing flap, and a weighing sensor. The weighing sensor is arranged outside the weighing hopper shell. The weighing hopper shell, the second soft connection hopper, the biomass distributor shell, and the guide hopper are sequentially connected from top to bottom to form a distribution channel through which the biomass powder can enter the inlet of the reactor upper body. The multi-blade unloading flap is arranged in a section of the weighing hopper shell in the distribution channel, and the multi-blade distributing flap is arranged in a section of the biomass distributor shell in the distribution channel, and both can rotate around their respective rotation axes.

[0018] By controlling the rotation speed of the multi-blade distributing flap in the automatic weighing distributor to regulate the rate at which the biomass powder enters the reactor lower body, the ratio of the rotation speed of the multi-blade distributing flap to the rate at which the biomass powder enters the reactor lower body is 2-8 rpm:1 kg / min.

[0019] Specifically, the rotation axis of the multi-blade unloading flap and the rotation axis of the multi-blade distributing flap both extend along the radial direction of the vertical rotation axis and are located in the same vertical plane. The rotation of the multi-blade unloading flap and the multi-blade distributing flap both forms a conical surface, and the two conical surfaces formed coincide with the projection area of the inlet in the top view direction and are located in the sector area in the reactor lower body.

[0020] Specifically, the multi-blade unloading flap and the multi-blade distributing flap divide the distribution channel into a storage and weighing section, a unloading section, and a smooth transition section. The storage and weighing section is used to receive, temporarily store, and weigh the biomass powder. The distribution channel communicates with the inlet of the reactor upper body through the lower port of the smooth transition section. The multi-blade unloading flap is located between the storage and weighing section and the unloading section and is configured to rotate to achieve the unloading of the biomass powder in the storage and weighing section to the unloading section. The multi-blade distributing flap is located between the unloading section and the smooth transition section and is configured to rotate to achieve the unloading of the biomass powder in the unloading section to the smooth transition section.

[0021] Specifically, the projection area is trapezoidal. The cross section of the storage and weighing section and the unloading section perpendicular to the vertical direction is rectangular. The area of the rectangle is greater than the area of the projection area.

[0022] Specifically, the device for hydrolyzing biomass comprises a first soft connection hopper connecting a weighing hopper shell in the automatic weighing distributor with an external biomass pneumatic conveying device.

[0023] Specifically, the automatic weighing distributor comprises a first bearing seat and a second bearing seat, and the multi-blade unloading flap is installed in the weighing hopper shell through the first bearing seat. The multi-blade distributing flap is installed in the biomass distributor shell through the second bearing seat.

[0024] Specifically, the device for hydrolyzing biomass comprises a distributor rack for fixedly supporting the automatic weighing distributor. The automatic weighing distributor comprises a weighing rack, and the weighing hopper shell is supported on the weighing rack through the weighing sensor. The weighing rack is fixedly supported on the distributor rack.

[0025] Specifically, the automatic weighing distributor comprises a driving mechanism configured to drive the multi-blade unloading flap and the multi-blade distributing flap to rotate, respectively. More specifically, the driving mechanism is a motor driving mechanism.

[0026] Specifically, a plurality of the first stirrers are arranged on a first radial line of the vertical rotation axis and are spaced apart, and a plurality of the second stirrers are arranged on another radial line of the vertical rotation axis and are spaced apart.

[0027] Specifically, the first stirrer and the second stirrer are structurally identical, comprising a stirring paddle, a stirrer support structure, a stirring driving mechanism, a coupling, and an auxiliary bearing. The stirrer support structure is fixedly installed on the upper end surface of the reactor upper body. The stirring driving mechanism is fixedly installed on the stirrer support structure. The coupling is arranged on the inner side of the stirrer support structure, and the output shaft of the stirring driving mechanism extends into the inner side of the stirrer support structure and connects the stirring paddle through the coupling. The stirring paddle is rotatably fixedly connected to the stirrer support structure through the auxiliary bearing.

[0028] More specifically, the stirring paddle is a hollow spiral paddle structure, comprising a stirring frame, a stirring shaft penetrating through the stirring frame, and hollow spiral paddles staggered along the circumferential direction of the stirring shaft and arranged in the stirring frame.

[0029] In some embodiments, the device for hydrolyzing biomass comprises an observation port and a breathing port, both of which are arranged on the reactor upper body.

[0030] In some embodiments, the apparatus for hydrolyzing biomass includes a material temperature measuring device mounted on the reactor upper body. The material temperature measuring device is configured to detect the temperature of the material in the reactor lower body.

[0031] In some embodiments, the apparatus for hydrolyzing biomass includes a slewing mechanism configured to support and drive the rotation of the reactor lower body relative to the reactor upper body about a vertical rotation axis.

[0032] In some embodiments, the slewing mechanism includes a drive gear and an external gear bearing, the external gear of the external gear bearing is coaxially fixedly connected with the reactor lower body, and the external gear of the external gear bearing is engaged with the drive gear.

[0033] In some embodiments, the apparatus for hydrolyzing biomass includes a slewing power source, the output shaft of the slewing power source is drivingly connected with the drive gear.

[0034] In some embodiments, the apparatus for hydrolyzing biomass includes a disc reactor rack for supporting the reactor. The disc reactor rack includes a reactor upper body structure support portion and a reactor lower body mounting structure portion. The reactor upper body is fixedly supported on the reactor upper body structure support portion. The inner ring of the external gear bearing is fixedly connected with the reactor lower body mounting structure portion through a mounting structure member.

[0035] In some embodiments, the reactor upper body includes a reactor upper body skeleton and a reactor upper body wall skin, the reactor upper body wall skin is fixedly connected to the reactor upper body skeleton.

[0036] In an embodiment, the reactor upper body includes an ear fixedly connected to the upper end outer circumferential portion of the reactor upper body skeleton, the ear is used to be fixedly connected with the reactor upper body structure support portion to achieve the fixed support of the reactor upper body on the reactor upper body structure support portion.

[0037] In an embodiment, the reactor lower body includes a reactor lower body body and a reactor lower body support structure, the reactor lower body body is made of light corrosion-resistant material. The reactor lower body body is configured to be accommodated in the reactor lower body support structure. The external gear of the external gear bearing is coaxially fixedly connected with the reactor lower body support structure to achieve the coaxial fixed connection of the external gear of the external gear bearing with the reactor lower body.

[0038] In an embodiment, the device for hydrolyzing biomass comprises a rotary sealing assembly configured to rotatably connect and seal the upper reactor body and the lower reactor body. In one embodiment of the rotary sealing assembly, the rotary sealing assembly is disposed on the top of the lower reactor body. In another embodiment of the rotary sealing assembly, the rotary sealing assembly is disposed on the lower portion of the upper reactor body.

[0039] In an embodiment, the lower reactor body is cylindrical.

[0040] In an embodiment, the entire reactor is disc-shaped.

[0041] In a second aspect, the application discloses the use of the device of the first aspect in hydrolyzing biomass.

[0042] In some embodiments, the use specifically comprises: feeding biomass powder into the lower reactor body through the feeding port, feeding high-concentration inorganic acid into the lower reactor body through the catalyst liquid distributor, rotating the lower reactor body, the first stirrer, and the second stirrer while keeping the upper reactor body stationary, hydrolyzing the biomass powder with the high-concentration inorganic acid, and discharging after the reaction stops.

[0043] In some embodiments, the discharging is to lower the rotation speed of the lower reactor body to below 15 rpm, and the discharger is inserted into the lower reactor body from the discharging port to take out the material; in some embodiments, when the bottom surface of the discharger contacts the bottom surface of the lower reactor body, the rotation speed of the lower reactor body can be increased, such as to 120 rpm for rapid rotation to discharge; in some embodiments, the discharger can use an existing discharger, such as the one described in Xiangshuai, Jianye Wang, Pengfei Li, et al. Structure Design of Screw Conveyor for Ammonium Metavanadate and Other Viscous Materials [J]. Soda Industry, 2024(02): 22-24.

[0044] In some embodiments, the biomass powder is fed into the reactor lower body through an automatic weighing distributor connected to the feed inlet; in some embodiments, the biomass powder is fed into the reactor lower body 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 rate of the biomass powder fed into the reactor lower body is controlled 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 in the automatic weighing distributor to the rate of the biomass powder fed into the reactor lower body is 2-8 rpm: 1 kg / min, such as 4 rpm: 1 kg / min, 5 rpm: 1 kg / min, 6 rpm: 1 kg / min; by controlling the rotation speed of the multi-blade distribution flap in the automatic weighing distributor to be 20-120 rpm, the rate of the biomass powder fed into the reactor lower body is controlled to be 5-20 kg / min; in some embodiments, the mass of the biomass powder stored in the second soft connection hopper is controlled by controlling the rotation speed of the multi-blade discharge flap in the automatic weighing distributor; in some embodiments, the rotation speed of the multi-blade discharge flap and the multi-blade distribution flap is independently selected from 20-120 rpm, such as 40 rpm, 60 rpm, 80 rpm, 100 rpm.

[0045] In some embodiments, the high-concentration inorganic acid is fed into the reactor lower body through the catalyst liquid distributor at a flow rate of 5-50 kg / min, such as 10 kg / min, 12.5 kg / min, 15 kg / min, 18 kg / min, 20 kg / min, 22 kg / min, 25 kg / min, 30 kg / min, 40 kg / min; in some embodiments, the pipe length of the liquid distribution channel is 1000-1400 mm, such as 1200 mm; in some embodiments, the inner diameter DN of the liquid distribution channel is 40-60 mm, such as 50 mm; in some embodiments, 200-400 liquid distribution holes are arranged in the liquid distribution channel at intervals, and the intervals between adjacent two liquid distribution holes gradually decrease in an arithmetic sequence in the radial direction away from the vertical rotation axis, such as 300 liquid distribution holes arranged in an arithmetic sequence; in some embodiments, the hole diameter of each liquid distribution hole is 1.5-3 mm.

[0046] In some embodiments, the biomass powder can be continuously or intermittently fed into the reactor lower body through the feed inlet, and the high-concentration inorganic acid can be continuously or intermittently fed into the reactor lower body through the catalyst liquid distributor.

[0047] In some embodiments, the biomass powder and the high-concentration inorganic acid are continuously fed; in this case, direct contact between the biomass powder not involved in the reaction and the high-concentration inorganic acid should be avoided to prevent carbonization of the biomass powder; in particular, the feeding rate of the biomass powder and the high-concentration inorganic acid and other parameters can be adjusted to avoid carbonization.

[0048] 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 rotations of the lower body of the reactor, such as once every 1 rotation, 2 rotations, 3 rotations or 4 rotations, to avoid direct contact between the biomass powder not involved in the reaction and the high-concentration inorganic acid, which can lead to carbonization of the biomass powder and formation of a large amount of side reactions; in some embodiments, the biomass powder and the high-concentration inorganic acid are cross-fed, first feeding the inorganic acid and then feeding the biomass powder. In this process, uniform and rapid interaction between the biomass powder and the inorganic acid can be achieved.

[0049] 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 or 190 rpm.

[0050] In some embodiments, the rotation speed of the first stirrer and the second stirrer is independently selected from 10-80 rpm, such as 20 rpm, 40 rpm or 60 rpm.

[0051] In some embodiments, the temperature of the reaction is room temperature, such as 20-30°C, such as 25°C; the temperature of the reaction can be monitored by a material temperature measuring device; if the temperature increases, the feeding of the biomass powder and the high-concentration inorganic acid can be temporarily suspended; the temperature change should be closely monitored during the production process to avoid high temperature as much as possible.

[0052] In some embodiments, the degree of hydrolysis of the biomass can be sampled and detected through the discharge port; for example, when the mixture in the reaction system has high fluidity, the mixture can be sampled and analyzed through the discharge port; after the reaction is completed, the reaction is stopped and the material is discharged.

[0053] In some embodiments, the hydrolysis of the biomass can be observed through the observation port; for example, when the reaction is in the initial stage and has good fluidity, the feeding rate of the biomass powder can be increased; when the reaction system has poor fluidity and does not improve significantly, the feeding rate of the high-concentration inorganic acid can be increased; when there is a tendency of carbonization, the feeding of the biomass powder and the high-concentration inorganic acid can be temporarily suspended; when the mixture in the reaction system has high fluidity at the end of the reaction, the degree of hydrolysis of the biomass can be sampled and detected through the discharge port.

[0054] In some embodiments, the diameter of the reactor lower body cavity is 0.6-20.6 meters, such as 2.6, 4.6, 6.6, 8.6, 10.6, 15.6 meters; in some embodiments, the height of the reactor lower body cavity is 0.2-5 meters, such as 0.6, 0.8, 1, 1.5, 2, 3, 4 meters; in some embodiments, the diameter and height of the reactor lower body cavity are 2.6 meters and 0.4 meters, respectively; in the process, the material can be kept uniformly mixed, and carbonization and other conditions rarely occur, and can be handled in time, and the production capacity is as high as 150-300 kg / 20 min. Further, when the diameter and height of the reactor lower body cavity are enlarged, the number of stirrers can be increased, the length of the catalyst liquid distributor can be increased, the rotation speed of the reactor lower body can be increased, and the feeding rate of the biomass powder and the acid can be increased, so that the production can be scaled up; specifically, when the rotation speed of the reactor lower body is increased from 120 rpm to 500 rpm, the rotation speed of the multi-blade distribution flap in the automatic weighing distributor is 80-480 rpm to control the rate of the biomass powder entering the reactor lower body to be 20-80 kg / min, the amount of acid is increased by 4 times, and the production capacity can be increased to 500 kg / 30 min; further scaling up, the production capacity can be as high as 3 tons / h.

[0055] In some embodiments, the biomass powder is obtained by passing through an 80-100 mesh screen.

[0056] 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 several 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 65 wt% or more, such as 70 wt%, 75 wt%, 80 wt%, 85 wt%, 90 wt%, 95 wt%, etc.; when the inorganic acid is hydrochloric acid, the concentration of the high-concentration inorganic acid is 25 wt%-35 wt%, such as 28 wt%, 30 wt%, 32 wt%.

[0057] In some embodiments, the biomass is any one or a combination of several of wheat straw, corn straw, rice straw, sorghum straw, cotton straw, sugarcane residue, corn cob, switchgrass, reed, and rapeseed.

[0058] 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 mass of the biomass powder.

[0059] In some embodiments, the ratio of the rate 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, 2.9:1.

[0060] In some embodiments, the temperature of the reaction is 20-35℃, such as room temperature.

[0061] In some embodiments, the reaction is under normal pressure.

[0062] In some embodiments, the time of the reaction is 10-60min, such as 15min, 20min, 25min, 30min, 35min, 40min, 45min, 50min.

[0063] In the present application, the rate of the biomass powder or the high concentration inorganic acid into the reactor lower body, unless otherwise specified, is the feeding rate of the biomass powder or the high concentration inorganic acid into the reactor lower body.

[0064] Advantages:

[0065] 1) The device provided by the present application is provided with a reactor lower body which can rotate relative to the reactor upper body around a vertical rotation axis, and when the reactor lower body rotates one round, the reactor lower body sequentially sweeps through a catalyst distributor, a second stirrer, a feeding port and a first stirrer, so that the area in the reactor lower body where high-concentration inorganic acid is scattered is mixed with hydrolysis liquid in the reactor lower body when the area is swept through the second stirrer with the rotation of the reactor lower body, and then the area is continuously swept through the distributor with biomass when the reactor lower body continues to rotate, and the area with biomass is mixed and stirred when the area is swept through the first stirrer, so that the direct contact between high-concentration inorganic acid and biomass is avoided to prevent rapid carbonization of the biomass, thereby improving the carbohydrate conversion rate. Meanwhile, for any sector area in the reactor lower body, when the reactor lower body rotates one round, the sector area sequentially experiences the processes of adding catalyst, mixing and stirring, adding biomass and mixing and stirring, and then if the reactor lower body is continuously rotated, the catalyst distributor is continuously and quantitatively distributed, and the automatic weighing distributor is continuously and quantitatively distributed, the device can realize the circulation of the above processes on the whole annular area of the reaction cavity, that is, realize the continuous production in a true sense. The prior art adopts a fixed reaction cavity, in order to avoid rapid carbonization, the catalyst distributor and the biomass distributor must be intermittently and alternately operated to realize the processes of adding catalyst, mixing and stirring, adding biomass and mixing and stirring on the whole fixed reaction cavity in time sequence. Therefore, compared with the prior art, the device of the present application can realize continuous production with continuous feeding, prevent rapid carbonization, improve the carbohydrate conversion rate, and improve the production efficiency.

[0066] 2) The device disclosed by the present application can realize continuous production and adjustable feeding ratio through the cooperation between the reactor, the automatic weighing distributor, the catalyst distributor and the stirrer.

[0067] 3) A large amount of PP material and lightweight design are used in the device disclosed by the present application, which can effectively reduce energy consumption. The reduction of operating cost brings great economic value.

[0068] 4) The straw powder of the present application is efficiently hydrolyzed at normal temperature and pressure to effectively obtain an oligosaccharide solution with high concentration and adjustable concentration, and the concentrations of cellobiose and xylobiose are as high as 3.05 g / l and 3.55 g / l, respectively, which can avoid the investment of a large amount of enzyme cost and provide a new option for the construction of a non-grain biological sugar platform.

[0069] 5) The device disclosed by the present application can effectively control the carbonization rate of cellulose and hemicellulose in the hydrolysis and conversion of biomass powder by controlling the contact ratio of biomass powder and high-concentration inorganic acid, and realize the production capacity of 3 tons of absolute dry straw powder / h in the hydrolysis production line, which is more stable, higher in effect and more superior in performance than the traditional device reaction process.

[0070] 6) The technical solution provided by this invention can significantly reduce the solid-liquid ratio to 0.35-1.4, reduce the amount of acid used by 0.5-1 times that 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. Attached Figure Description

[0071] The present invention will be further described in detail below with reference to the accompanying drawings and specific embodiments, and the advantages of the present invention in the above and / or other aspects will become clearer.

[0072] Figure 1 This is a three-dimensional structural schematic diagram of an apparatus for hydrolyzing biomass disclosed in an embodiment of the present invention.

[0073] Figure 2 for Figure 1 The diagram shows the overall assembly structure of the reactor in the device for hydrolyzing biomass.

[0074] Figure 3 for Figure 2 The reactor shown is a top view.

[0075] Figure 4 for Figure 3 The reactor shown is a front view.

[0076] Figure 5 For Figure 3 Cross-sectional view of the reactor along the AA line.

[0077] Figure 6 for Figure 1 The diagram shows a three-dimensional structural schematic of the catalyst distributor in a device for hydrolyzing biomass.

[0078] Figure 7 for Figure 1 The diagram shows a three-dimensional structure of the automatic weighing feeder in the biomass hydrolysis device, installed on the feeder frame.

[0079] Figure 8 for Figure 7 The front view of the automatic weighing and spreading device is shown.

[0080] Figure 9 for Figure 8 The left view of the automatic weighing and spreading device shown.

[0081] Figure 10 for Figure 8 The image shows a top view of the automatic weighing and spreading device.

[0082] Figure 11 For Figure 9 Cross-sectional view of the automatic weighing and spreading device on the BB line.

[0083] Figure 12 A perspective view of a weigh hopper assembly.

[0084] Figure 13 A perspective view of a weigh hopper assembly. Figure 12 A vertical cross-sectional view of a weigh hopper assembly.

[0085] Figure 14 A perspective view of a material distribution assembly.

[0086] Figure 15 A vertical cross-sectional view of a material distribution assembly. Figure 14 A vertical cross-sectional view of a material distribution assembly.

[0087] Figure 16 A perspective view of an agitator in an apparatus for hydrolyzing biomass. Figure 1 A perspective view of an agitator in an apparatus for hydrolyzing biomass. A perspective view of an agitator in an apparatus for hydrolyzing biomass.

[0088] An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. Figure 17 An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. Figure 16 An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator.

[0089] An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. Figure 18 An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. Figure 16 An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator.

[0090] An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. Figure 19 An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. Figure 16 An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator.

[0091] An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. Figure 20 An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. Figure 1 An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator.

[0092] An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. Figure 21 An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. Figure 2 An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator.

[0093] An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. Figure 22 An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. Figure 2 An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator.

[0094] An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. Figure 23 An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator.

[0095] An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator. An assembly view of a secondary bearing, a coupling, and an agitator support structure in an agitator.

[0096] 100. Automatic weighing and distributing device; 110. Distributing channel; 1101. Storage and weighing section; 1102. Discharging section; 1103. Smooth transition section; 111. First flexible connection hopper; 1111. Upper guide flange; 1112. Flexible connection body; 1113. Fixed end mounting structure flange; 120. Weighing hopper assembly; 121. Weighing hopper shell; 122. Multi-blade discharge flap; 123. First bearing seat; 124. First motor mounting bracket; 125. First motor drive mechanism; 126. Weighing sensor; 127. Weighing frame; 131. Second flexible connection hopper; 140. Fabric feeding assembly; 141. Biomass feeder housing; 142. Multi-blade fabric feeding flap; 143. Second bearing seat; 144. Second motor mounting bracket; 145. Second motor drive structure; 151. Feed hopper; 200. Agitator; 201. First agitator; 202. Second agitator; 210. Agitator drive mechanism; 220. Agitator support structure; 230. Agitator paddle; 231. 232. Stirring frame; 233. Stirring shaft; 234. Hollow spiral blades; 245. Coupling; 256. Auxiliary bearing; 300. Reactor; 317. Upper body of reactor; 318. Feed inlet; 319. Upper body skeleton of reactor; 310. Upper body wall skin of reactor; 311. Support lugs; 322. Lower body of reactor; 323. Lower body support structure of reactor; 324. External gear bearing; 325. Mounting structure; 326. Rotary sealing assembly; 337. Reaction chamber 340. Vertical rotation axis; 410. Disc reactor frame; 411. Upper structure support of reactor; 412. Drive gear; 413. Rotation power source; 414. Lower structure of reactor; 420. Distributor frame; 500. Catalyst distributor; 510. Distribution pipe; 511. Distribution channel; 512. Distribution hole; 520. Distribution pipe adapter; 530. Connecting flange; 600. Material temperature measuring device; 700. Observation port; 800. Discharge port; 900. Breathing port. Detailed Implementation

[0097] Please see Figures 1 to 5 This application provides an apparatus for hydrolyzing biomass, which includes an automatic weighing and distributing device 100, a stirrer 200, a reactor 300, and a catalyst distributor 500.

[0098] Please see Figures 2 to 5 The reactor 300 is generally disc-shaped. The reactor 300 includes an upper reactor body 310 and a lower reactor body 320. The lower reactor body 320 has an upper opening, and the upper reactor body 310 covers the upper opening of the lower reactor body 320, forming a reaction chamber 330 together. See also... Figure 5The reactor lower body 320 and the reaction cavity 330 are both flat cylindrical in shape. The reactor lower body 320 is disc-shaped in shape. The reactor lower body 320 is configured to rotate relative to the reactor upper body 310 about a vertical rotation axis 340. The top of the reactor upper body 310 is provided with a feed inlet 311, which is disposed on one side of the vertical rotation axis 340 and has a fan-shaped or isosceles trapezoidal overall shape. The feed inlet 311 is configured to allow biomass to enter the reactor lower body 320. The top of the reactor upper body 310 is also provided with a discharge outlet 800, which is configured to allow a discharge machine to take material from the reactor lower body 320.

[0099] Referring to Figure 1 and Figure 2 , the automatic weighing distributor 100 is disposed above the reactor upper body 310 and connected at the feed inlet 311. The automatic weighing distributor 100 is configured to distribute biomass powder through the feed inlet 311 when the reactor lower body 320 rotates to the area swept by the reactor lower body 320.

[0100] Referring to Figure 5 , the catalyst liquid distributor 500 is connected below the reactor upper body 310 and is configured to distribute high-concentration inorganic acid in the reactor lower body 320.

[0101] Referring to Figure 1 , the stirrer 200 includes a first stirrer 201 and a second stirrer 202, both of which are mounted on the reactor upper body 310 and extend downward into the reactor lower body 320. The first stirrer 201 and the second stirrer 202 are respectively configured to rotate to stir the area swept by the reactor lower body 320 when the reactor lower body 320 rotates.

[0102] Referring to Figure 1 , Figure 2 and Figure 5 , the catalyst liquid distributor 500, the second stirrer 202, the feed inlet 311, and the first stirrer 201 are sequentially and spaced apart in the direction of rotation of the reactor lower body 320. When the reactor lower body 320 rotates one revolution, the reactor lower body 320 sequentially sweeps the catalyst liquid distributor 500, the second stirrer 202, the feed inlet 311, and the first stirrer 201.

[0103] The device disclosed in the embodiment is provided with a reactor lower body 320 which can rotate around a vertical rotation axis relative to a reactor upper body 310, and when the reactor lower body 320 rotates one round, the reactor lower body 320 sequentially sweeps through a catalyst distributor 500, a second stirrer 202, a feed inlet 311 and a first stirrer 201, so that the area in the reactor lower body where the high-concentration inorganic acid is scattered is mixed with the hydrolysis liquid in the reactor lower body by being swept through the second stirrer, and then the area in the reactor lower body is continuously swept through the distributor by the reactor lower body to be distributed with biomass, and the area distributed with biomass is immediately stirred and mixed by the first stirrer, in the process, the direct contact between the high-concentration inorganic acid and the biomass is avoided to cause rapid carbonization of the biomass, so as to improve the carbohydrate conversion rate.

[0104] In addition, the prior art adopts a fixed reaction cavity, and the processes of adding catalyst, stirring and mixing, adding biomass and stirring and mixing are performed on the whole fixed reaction cavity in a time sequence, in the process, in order to avoid rapid carbonization, the catalyst distributor and the biomass distributor must be intermittently and alternately operated. In the present application, for any one sector area in the reactor lower body 320, when the reactor lower body 320 rotates one round, the sector area sequentially experiences the processes of adding catalyst, stirring and mixing, adding biomass and stirring and mixing, if the reactor lower body 320 continuously rotates, the catalyst distributor 500 continuously and quantitatively distributes, and the automatic weighing distributor 100 continuously and quantitatively distributes, the device can realize the circulation of the above processes on the whole annular area of the reaction cavity, that is, realize the continuous production in a true sense. Compared with the prior art, the present application realizes the continuous production of both high-concentration inorganic acid and biomass in a continuous input mode while preventing rapid carbonization and improving the conversion rate, so as to improve the production efficiency.

[0105] In other words, the device disclosed in the present application can realize continuous production and adjustable feeding ratio by the cooperation between the reactor, the automatic weighing distributor, the catalyst distributor and the stirrers.

[0106] Preferably, please refer to Figure 1 , Figure 2 and Figure 5 , the first stirrer 201 is arranged close to the feed inlet 311, the second stirrer 202 is arranged close to the catalyst distributor 500, the first stirrer 201 is configured to immediately stir and mix the biomass scattered into the reaction cavity, and the second stirrer 202 is configured to immediately stir and mix the high-concentration inorganic acid scattered into the reaction cavity.

[0107] In some specific embodiments, please refer to Figure 5 and Figure 6The catalyst liquid distributor 500 comprises a liquid distribution channel 511 and a plurality of liquid distribution holes 512. The liquid distribution channel 511 extends along the radial direction of the vertical rotation axis 340. The high-concentration inorganic acid can flow out of the liquid distribution channel 511 through the liquid distribution holes 512 to the reactor lower body 320. Please refer to Figure 6 The plurality of liquid distribution holes 512 are arranged at intervals along the liquid distribution channel 511, and the intervals between adjacent two liquid distribution holes 512 gradually decrease in the radial direction away from the vertical rotation axis 340.

[0108] In some specific embodiments, please refer to Figure 6 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. The plurality of liquid distribution holes 512 are formed on the pipe wall of the liquid distribution pipe 510 and are in communication with the inside of the liquid distribution pipe 510.

[0109] In some specific embodiments, please refer to Figure 1 、 Figure 5 and Figure 6 The device for hydrolyzing biomass comprises a connecting flange 530 fixedly installed on the reactor upper body 310, and the connecting flange 530 is used to connect with an external catalyst supply device. The catalyst supply device comprises a plurality of catalyst supply pipelines respectively used to supply inorganic acid catalysts of different concentrations. The connecting flange 530 can selectively and alternatively communicate with any one of the plurality of catalyst supply pipelines in the catalyst supply device to introduce the inorganic acid catalyst of the required concentration into the catalyst liquid distributor 500.

[0110] Please refer to Figure 5 and Figure 6 The catalyst liquid distributor 500 comprises a liquid distribution pipe adapter 520 connecting the liquid distribution pipe 510 with the connecting flange 530, so as to realize the connection of the catalyst liquid distributor 500 with the reactor upper body 310 through the connecting flange 530.

[0111] In some specific embodiments, please refer to Figures 7 to 11 The automatic weighing distributor 100 comprises a weighing hopper shell 121, a second soft connection hopper 131, a biomass distributor shell 141, a guide hopper 151, a multi-blade discharge flap 122, a multi-blade distribution flap 142, and a weighing sensor 126. Please refer to Figure 11 The weighing sensor 126 is arranged outside the weighing hopper shell 121. The weighing hopper shell 121, the second soft connection hopper 131, the biomass distributor shell 141, and the guide hopper 151 are sequentially connected from top to bottom to form a distribution channel 110. Please refer to Figure 1The lower end of the feeding hopper 151 is arranged as a lower end of the material distribution passage 110, and extends into the feeding port 311 of the reactor upper body 310, so that the biomass can enter the feeding port 311 of the reactor upper body 310 through the material distribution passage 110. Please refer to Figure 11 The material distribution passage 110 is arranged in a vertical direction as a whole. Please refer to Figure 12 and Figure 13 The multi-blade material unloading flap 122 is arranged in the material distribution passage 110 and located in a section of the weighing hopper shell 121. Please refer to Figure 14 and Figure 15 The multi-blade material distribution flap 142 is arranged in the material distribution passage 110 and located in a section of the biomass material distributor shell 141, and the multi-blade material unloading flap 122 and the multi-blade material distribution flap 142 can rotate around their respective rotation axes.

[0112] Please refer to Figure 11 The multi-blade material unloading flap 122 and the multi-blade material distribution flap 142 divide the material distribution passage 110 into a material storage and weighing section 1101, a material unloading section 1102, and a smooth transition section 1103. The material storage and weighing section 1101 is used to receive, temporarily store, and weigh the biomass. The material distribution passage 110 is in communication with the feeding port 311 of the reactor upper body 310 through the lower end of the smooth transition section 1103. The multi-blade material unloading flap 122 is located between the material storage and weighing section 1101 and the material unloading section 1102, and is configured to control rotation according to the measurement value of the weighing sensor 126 to achieve unloading of the biomass in the material storage and weighing section 1101 to the material unloading section 1102. The multi-blade material distribution flap 142 is located between the material unloading section 1102 and the smooth transition section 1103, and is configured to rotate to achieve unloading of the biomass in the material unloading section 1102 to the smooth transition section 1103.

[0113] In this embodiment, the multi-blade material unloading flap 122 is adopted, which is beneficial to batch feeding.

[0114] In a preferred embodiment, please refer to Figure 1 and Figure 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 along the radial direction of the vertical rotation axis 340 and are located in the same vertical plane. The rotation of the multi-blade material unloading flap 122 and the multi-blade material distribution flap 142 both forms a conical surface, and the two conical surfaces formed coincide with the projection area of the feeding port 311 in the top view direction and are located in the sector area in the reactor lower body 320.

[0115] In the embodiment, the multi-blade unloading flap 122 and the multi-blade distributing flap 142 are both formed into a conical surface, and the two conical surfaces are coincided with the projection area of the feed inlet 311 in the top view and located in the sector area in the reactor lower body 320, so that the biomass is distributed in the sector area in the reactor lower body 320, avoiding the waste caused by the accumulation of biomass near the vertical rotation axis 340, and helping to improve the conversion rate of carbohydrates.

[0116] In the embodiment, the multi-blade unloading flap 122 and the multi-blade distributing flap 142 are both formed into a conical surface, and the two conical surfaces are coincided with the projection area of the feed inlet 311 in the top view and located in the sector area in the reactor lower body 320, so that the biomass is distributed in the sector area in the reactor lower body 320, avoiding the waste caused by the accumulation of biomass near the vertical rotation axis 340, and helping to improve the conversion rate of carbohydrates.

[0117] 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 sector. Please refer to Figure 10 , the cross section of the storage and weighing section 1101 and the unloading section 1102 perpendicular to the vertical direction is a rectangle. The area of the rectangle is larger than the area of the projection area. Please refer to Figure 7 , the smooth transition section 1103 is configured to smoothly connect the unloading section 1102 and the feed inlet 311.

[0118] Please refer to Figure 13 and Figure 15 In the present application, the multi-blade unloading flap 122 and the multi-blade distributing flap 142 both adopt a multi-blade flap structure, including a shaft and a plurality of blade plates, the plurality of blade plates are uniformly 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, please refer to Figure 13 , the multi-blade unloading flap 122 is uniformly spaced by four blade plates along its circumference, please refer to Figure 15 , the multi-blade distributing flap 142 is uniformly spaced by twelve blade plates along its circumference. The included angle between two adjacent blade plates is 30°, which is more conducive to the uniformity of batch feeding.

[0119] In some specific embodiments, please refer to Figure 11 The automatic weighing and distributing device 100 includes a first bearing seat 123 and a second bearing seat 143, and the two ends of the shaft of the multi-blade unloading flap 122 are installed in the weighing hopper shell 121 through the first bearing seat 123. The two ends of the shaft of the multi-blade distributing flap 142 are installed in the biomass distributing device shell 141 through the second bearing seat 143.

[0120] In some embodiments, referring to Figure 11 , the automatic weighing distributor 100 comprises a first soft connection hopper 111, which connects the weighing hopper shell 121 with an external biomass pneumatic conveying device. The external biomass pneumatic conveying device is a prior art and thus is not described here. In some embodiments, referring to Figure 8 , the first soft connection hopper 111 comprises an upper material guiding connection flange 1111, a soft connection body 1112, and a fixed end mounting structure flange 1113. Preferably, the material of the upper material guiding connection flange 1111 is 316L, and the flange surface is uniformly distributed with round holes for connecting the external biomass pneumatic conveying device, so as to realize the connection between the first soft connection hopper 111 and the external biomass pneumatic conveying device. Preferably, the soft connection body 1112 is a 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 discharge 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 soft connection hopper 111 is designed to be large enough to accommodate a sufficient amount of biomass to be weighed. At this time, the first soft connection hopper 111, the weighing hopper shell 121, the second soft connection hopper 131, the biomass distributor shell 141, and the guide hopper 151 together constitute a material distribution channel 110. Preferably, the upper material guiding connection flange 1111 and the fixed end mounting structure flange 1113 are designed to be rectangular in structure.

[0121] It should be understood that the second soft connection hopper 131 can be designed with the same structure as the first soft connection hopper 111.

[0122] Preferably, the specific structure of the weighing hopper shell 121 is that the upper and lower end flanges are uniformly distributed with threaded holes, so as to be connected and mounted with the first soft connection hopper 111 and the second soft connection hopper 131.

[0123] In some embodiments, the automatic weighing distributor 100 comprises a driving mechanism configured to drive the multi-blade discharge flap 122 and the multi-blade distribution flap 142 to rotate, respectively. More specifically, referring to Figure 8 , the driving mechanism is a motor driving mechanism, such as a motor and a reducer. In some embodiments, referring to Figure 12 and Figure 14 , the driving mechanism comprises a first motor driving mechanism 125 for driving the multi-blade discharge flap 122 to rotate and a second motor driving structure 145 for driving the multi-blade distribution flap 142 to rotate. In some embodiments, referring to Figure 12 and Figure 14The automatic weighing distributor 100 comprises a first motor mounting frame 124 and a second motor mounting frame 144. The first motor driving mechanism 125 is fixedly installed on the outer sidewall of the weighing hopper shell 121 through the first motor mounting frame 124. The second motor driving mechanism 145 is fixedly installed on the outer sidewall of the biomass distributor shell 141 through the second motor mounting frame 144.

[0124] In some specific embodiments, in order to facilitate assembly, referring to Figure 12 and Figure 13 The weighing hopper assembly 120 is composed of the weighing hopper shell 121, the multi-blade unloading flap 122, the first bearing seat 123, the first motor mounting frame 124 and the first motor driving mechanism 125. Referring to Figure 14 and Figure 15 The distributing assembly 140 is composed of the biomass distributor shell 141, the multi-blade distributing flap 142, the second bearing seat 143, the second motor mounting frame 144 and the second motor driving mechanism 145. Optionally, the first bearing seat 123 and the second bearing seat 143 can both be UCP series bearing with seat, which is low in cost and convenient to use.

[0125] In some specific embodiments, referring to Figure 7 The device for hydrolyzing biomass comprises a distributor rack 420 for fixedly supporting the automatic weighing distributor 100. Referring to Figure 1 The distributor rack 420 is arranged on one side of the disc reactor rack 410. Referring to Figure 7 The automatic weighing distributor 100 comprises a weighing rack 127. The weighing hopper shell 121 is supported on the weighing rack 127 through a weighing sensor 126. The weighing rack 127 is fixedly supported on the distributor rack 420.

[0126] In some specific embodiments, in order to ensure the mixing effect, referring to Figure 1 The first stirrer 201 and the second stirrer 202 are both provided with two. The two first stirrers 201 are both located on a first radial line of the vertical rotation axis 340 and are spaced apart. The two second stirrers 202 are both located on another radial line of the vertical rotation axis 340 and are spaced apart.

[0127] It should be understood that the number of the first stirrer 201 and the number of the second stirrer 202 in the embodiment are not limited to two, but can be expanded along the radial direction or the circumferential direction of the vertical rotation axis 340 according to needs. In addition, the number of the first stirrer 201 and the number of the second stirrer 202 can be the same or different.

[0128] In some specific embodiments, referring to Figures 16 to 18, the first agitator 201 and the second agitator 202 are agitators of the same structure, and each comprises an agitator driving mechanism 210, an agitator support structure 220, an agitator blade 230, a coupling 240, and an auxiliary bearing 250. The agitator support structure 220 is fixedly installed on the upper end face of the reactor upper body 310. The agitator driving mechanism 210 is fixedly installed on the agitator support structure 220. The coupling 240 is arranged on the inner side of the agitator support structure 220, and the output shaft of the agitator driving mechanism 210 extends into the inner side of the agitator support structure 220 and connects the agitator blade 230 through the coupling 240. More specifically, the agitator driving mechanism 210 can be an electric motor driving mechanism.

[0129] In some specific embodiments, referring to Figure 17 and Figure 18 , the agitator blade 230 is rotatably fixedly connected to the agitator support structure 220 through the auxiliary bearing 250. The agitator 200 of the present embodiment is provided with the auxiliary bearing 250, which ensures the accuracy of the roundness of the agitator blade 230 during operation and increases the bending strength of the agitator blade 230.

[0130] In some specific embodiments, referring to Figure 19 , the agitator blade 230 is a hollow spiral blade structure, which comprises an agitator frame 231, an agitator shaft 232 arranged through the agitator frame 231, and hollow spiral blades 233 distributed along the circumference of the agitator shaft 232 and arranged in the agitator frame 231.

[0131] In some specific embodiments, referring to Figure 2 , the device for hydrolyzing biomass comprises an observation port 700, a discharge port 800, and a breathing port 900, which are all arranged on the top face of the reactor upper body 310. In some specific embodiments, the breathing port 900 is made of waterproof air-permeable material, which can quickly discharge air and make the biomass quickly contact with the catalyst, thereby improving the work efficiency. Preferably, referring to Figure 2 , the breathing port 900 is arranged directly above the liquid distribution pipe 510. In some specific embodiments, the observation port 700 is installed using a glass sheet inlay, which is used to observe the reaction state of the material in the reaction cavity.

[0132] Preferably, referring to Figure 1 and Figure 2 , the first agitator 201, the feed port 311, the second agitator 202, and the catalyst liquid distributor 500 are 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 liquid distributor 500.

[0133] In some specific embodiments, referring to Figure 1The device for hydrolyzing biomass includes a material temperature measuring device 600 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 is not related to the main application point of the present application, the temperature measuring device in the prior art can be selected, and therefore the specific structure is not described in detail in the present application.

[0134] 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 slewing 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.

[0135] In some specific embodiments, the slewing mechanism includes a drive gear 412 and an external gear bearing 323. Referring to Figure 4 , the external gear of the external gear bearing 323 is fixedly connected coaxially with the reactor lower body 320. The external gear of the external gear bearing 323 is engaged with the drive gear 412, which is not shown in the figure.

[0136] In the present embodiment, the external gear bearing 323 can be a commercially available precision gear bearing module, which is used to provide excellent slewing accuracy for the reactor lower body 320.

[0137] In some specific embodiments, the device for hydrolyzing biomass includes a slewing power source 413, referring to Figure 20 , the output shaft of the slewing power source 413 is in driving connection with the drive gear 412. More specifically, the slewing power source 413 can adopt a motor driving mechanism.

[0138] In some specific embodiments, referring to Figure 1 , the device for hydrolyzing biomass includes a disc reactor rack 410 for supporting the reactor 300.

[0139] Referring to Figure 20 , the disc reactor rack 410 includes a reactor upper body structure support part 411 and a reactor lower body mounting structure part 414. Referring to Figure 1 , the reactor upper body 310 is fixedly supported on the reactor upper body structure support part 411. Referring to Figure 4 , the inner ring of the external gear bearing 323 is fixedly connected with a mounting structure 324. The inner ring of the external gear bearing 323 is fixedly connected with the reactor lower body mounting structure part 414 through the mounting structure 324 to support the reactor lower body 320.

[0140] In some specific embodiments, referring to Figure 20 , the slewing power source 413 is mounted to the disc reactor rack 410.

[0141] In some embodiments, referring to Figure 21 The reactor upper body 310 comprises a reactor upper body skeleton 314 and a reactor upper body wall skin 315 fixedly connected to the reactor upper body skeleton 314. In some embodiments, the reactor upper body skeleton 314 is made of 316L rectangular tubes to provide support for the reactor upper body 310.

[0142] In some embodiments, referring to Figure 21 The reactor upper body 310 comprises an ear 316 fixedly connected to the outer periphery of the upper end of the reactor upper body skeleton 314, which is used to be fixedly connected with the reactor upper body structure support part 411 to achieve the fixed support of the reactor upper body 310 on the reactor upper body structure support part 411.

[0143] In some embodiments, referring to Figure 22 The reactor lower body 320 comprises a reactor lower body body 321 made of a light corrosion-resistant material and a reactor lower body support structure 322, which is configured to accommodate the reactor lower body body 321. The outer gear of the outer gear bearing 323 is coaxially fixedly connected with the reactor lower body support structure 322 to achieve the coaxial fixed connection of the outer gear of the outer gear bearing 323 with the reactor lower body 320. Optionally, the light corrosion-resistant material can be a PP material. The reactor lower body body 321 made of PP material is connected with the reactor lower body support structure 322 by a special screw group to have excellent mechanical properties.

[0144] In some embodiments, referring to Figure 22 The device for hydrolyzing biomass comprises a rotary sealing assembly 325 configured to be rotatably connected and sealingly fitted between the reactor upper body 310 and the reactor lower body 320. In one embodiment of the rotary sealing assembly, the rotary sealing assembly 325 is arranged at the top of the reactor lower body 320. In another embodiment of the rotary sealing assembly, the rotary sealing assembly 325 is arranged at the lower part of the reactor upper body 310.

[0145] The rotary sealing assembly can be selected from the prior art, and the specific structure of the rotary sealing assembly is not the main point of the present application, so the specific structure of the rotary sealing assembly will not be described here.

[0146] Further, the above device is used for continuous and efficient hydrolysis of straw powder, and the specific implementation is as follows:

[0147] The device, specifically:

[0148] The diameter and height of the inner cavity of the reactor lower body 320 are 2600*400 mm; the pipe 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 along the liquid distribution channel 511 at intervals, the interval between adjacent two liquid distribution holes 512 gradually decreases along the radial direction away from the vertical rotation axis 340, and the hole diameter of the liquid distribution holes 512 is all 2 mm; the first agitator 201 and the second agitator 202 are respectively 2 agitators, and a total of 4 agitators; the temperature is detected by an infrared temperature measurement system, and when a temperature rising trend occurs, the distribution of the straw powder and the high-concentration inorganic acid can be paused.

[0149] The straw powder is a powder after passing through a 100-mesh screen.

[0150] In the following specific application examples, the mass of the straw powder stored in the second soft connection hopper 131 can be controlled by adjusting the rotating speed of the multi-blade discharge turning plate 122; for example, in the cross feeding of example 1, the mass of the straw powder stored in the second soft connection hopper 131 is controlled to be 20-40 kg, specifically 20-25 kg; for example, in the continuous feeding of example 2, the mass of the straw powder stored in the second soft connection hopper 131 is controlled to be 20-40 kg, specifically 35-40 kg.

[0151] In the following specific application examples, the unit of the solid-liquid ratio is kg / L.

[0152] In the following examples, the content of cellulose, hemicellulose and lignin in the biomass is detected by the NREL method of the National Renewable Energy Laboratory, and the cellulose conversion rate and the hemicellulose conversion rate are calculated as follows: .

[0153] Wherein, C represents the percentage content in the corresponding component in the biomass, and M represents the mass of the corresponding substance. Specifically, C 原料-纤 represents the cellulose component content in the raw material, C 残渣-纤 represents the cellulose component content in the residue; C 原料-半纤 represents the hemicellulose component content in the raw material, C 残渣-半纤 represents the hemicellulose component content in the residue; M 原料 represents the mass of the raw material, M 残渣 represents the mass of the residue after the reaction.

[0154] In the following examples, the content of cellulose in the straw powder is 31.02%, and the content of hemicellulose is 18.26%.

[0155] In the present application, the percentages in the cellulose content and the hemicellulose content are mass percentages.

[0156] In the following examples, the solid-to-liquid ratio is the mass of the straw powder / mass of the acid.

[0157] In the following examples, the cellulose / sulfuric acid ratio is (mass of the straw powder x content of cellulose in the straw powder) / (mass of the aqueous sulfuric acid solution x mass concentration of the aqueous sulfuric acid solution).

[0158] In the following examples, the sugar is detected by high-performance liquid chromatography, and the specific chromatographic conditions include: a calcium phenate column Rezex™ RCM-monosaccharide Ca+2 Size: LC Column 300*7.8 mm, a sample injection amount of 20 microliters, a column oven temperature of 55°C, a flow rate of 0.2 milliliter / min, a time of 60 min, and a mobile phase of pure water. Compared with an organic acid column, the detection method provided by the present application can detect oligosaccharides (DP < 7).

[0159] Example 1 Cross feeding of biomass powder and high-concentration inorganic acid

[0160] The hydrolysis reaction specifically includes the following steps:

[0161] (1) The straw powder is fed into the automatic weighing distributor 100, the multi-blade discharge flap 122 of the automatic weighing distributor 100 is controlled, so that the straw powder is quantitatively stored in the second soft connection hopper 131 after completion of the storage; the multi-blade distribution flap 142 is further controlled, so that the straw powder is stored in the second soft connection hopper 131 or is fed into the reactor lower body 320 at a rate of 15 kg / min through the feed port 311.

[0162] (2) The 70% w / w aqueous sulfuric acid solution is fed into the reactor lower body 320 at a flow rate of 10.71 kg / min through the catalyst liquid distributor 500.

[0163] (3) The reactor lower body 320 is rotated at a rate of 120 rpm, the aqueous sulfuric acid solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500, and then the straw powder is fed into the reactor lower body 320 through the automatic weighing distributor 100, the automatic weighing distributor 100 and the catalyst liquid distributor 500 are alternately operated once per revolution of the rotating disc, and two revolutions constitute a cycle; the rotation speed of the first stirrer 201 and the second stirrer 202 is 60 rpm during the reaction; this entire process enables the straw powder and the catalyst to be uniformly and rapidly distributed to the entire hydrolysis process while being distributed and liquidized, and the two interact uniformly and rapidly.

[0164] (4) After the reactor lower body 320 operates for 20 min, the reaction is stopped. After the reaction is completed, the material is taken out through the discharge port 800, washed with water and dried to obtain 93.24 kg of residue, and the content of cellulose in the residue is 17.29% and the content of hemicellulose is 7.55%. After continuous high-efficiency hydrolysis, the conversion rate of cellulose is 65.36% and the conversion rate of hemicellulose is 74.29%.

[0165] In this embodiment, an external infrared temperature measurement sensor system is used to collect temperature data in real time, so that the temperature is maintained within a range of room temperature ± 5°C, and the stability during the hydrolysis conversion process is controlled.

[0166] It is calculated that in this embodiment, 150 kg of corn straw powder is treated within 20 min of operation; 107.14 kg of 70% w / w sulfuric acid aqueous solution is used; the solid-liquid ratio is 1.4, the acid dosage is 0.5 times the mass of the straw powder, and the cellulose / sulfuric acid ratio is 0.60. The cellobiose (glucose) in the obtained oligosaccharide with DP < 7 is 3.05 g / l, and the xylotriose is 3.55 g / l.

[0167] Example 2 Cross feeding of biomass powder and high-concentration inorganic acid

[0168] The hydrolysis reaction specifically includes the following steps:

[0169] (1) The straw powder is fed into the automatic weighing distributor 100, the multi-blade discharge flap 122 of the automatic weighing distributor 100 is controlled, so that the straw powder is quantitatively stored in the second soft connection hopper 131 after completion of the storage; further control the multi-blade distribution flap 142, so that the straw powder is stored in the second soft connection hopper 131 or is fed into the reactor lower body 320 through the feed port 311 at a rate of 15 kg / min.

[0170] (2) The 70% w / w sulfuric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500 at a flow rate of 10.71 kg / min.

[0171] (3) The reactor lower body 320 is rotated at a speed of 80 rpm, the sulfuric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500, and then the straw powder is fed into the reactor lower body 320 through the automatic weighing distributor 100, the automatic weighing distributor 100 and the catalyst liquid distributor 500 are alternately operated once for each rotation of the rotating disc, and two rotations are one cycle; the rotation speed of the first stirrer 201 and the second stirrer 202 is 40 rpm during the reaction; this whole process enables the straw powder and the catalyst to be evenly and quickly distributed to the whole hydrolysis process while being distributed and liquidized, and the two interact uniformly and quickly.

[0172] (4) After the reactor lower body 320 operates for 20 min, the reaction is stopped. After the reaction is completed, the material is taken out through the discharge port 800, washed with water and dried to obtain 95.49 kg of residue, and the content of cellulose in the residue is 17.90% and the content of hemicellulose is 8.17%. After continuous high-efficiency hydrolysis, the conversion rate of cellulose is 63.27% and the conversion rate of hemicellulose is 71.53%.

[0173] In this embodiment, an external infrared temperature measurement sensor system is used to collect temperature data in real time, so that the temperature is maintained within a range of room temperature ± 5°C, and the stability during the hydrolysis conversion process is controlled.

[0174] It is calculated that in this embodiment, 150 kg of corn straw powder is treated within 20 min of operation; 107.14 kg of 70% w / w sulfuric acid aqueous solution is used; the solid-liquid ratio is 1.4, the acid dosage is 0.5 times the mass of the straw powder, and the cellulose / sulfuric acid ratio is 0.60. The cellobiose (glucose) in the obtained oligosaccharide with DP < 7 is 3.03 g / l, and the xylotriose is 3.51 g / l.

[0175] Example 3 Continuous feeding of biomass powder and high-concentration inorganic acid

[0176] The hydrolysis reaction specifically includes the following steps:

[0177] (1) The straw powder is fed into the automatic weighing distributor 100, the multi-blade discharge flap 122 of the automatic weighing distributor 100 is controlled, so that the straw powder is quantitatively stored in the second soft connection hopper 131 after completion; further control the multi-blade distribution flap 142, so that the straw powder is stored in the second soft connection hopper 131 or is fed into the reactor lower body 320 through the feed port 311 at a rate of 15 kg / min.

[0178] (2) The 70% w / w sulfuric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500 at a flow rate of 10.71 kg / min.

[0179] (3) The reactor lower body 320 is rotated at a speed of 120 rpm, and the automatic weighing distributor 100 and the catalyst liquid distributor 100 work continuously; the rotation speed of the first stirrer 201 and the second stirrer 202 during the reaction is 60 rpm; this whole process makes the straw powder and the catalyst evenly and quickly distributed to the whole hydrolysis process while being distributed and liquidized, and they interact uniformly and quickly.

[0180] (4) After the reactor lower body 320 operates for 20 min, the reaction is stopped. After the reaction is completed, the material is taken out through the discharge port 800, washed with water and dried to obtain 191.16 kg of residue, and the content of cellulose in the residue is 19.29% and the content of hemicellulose is 9.96%. After continuous high-efficiency hydrolysis, the conversion rate of cellulose is 60.37% and the conversion rate of hemicellulose is 65.24%.

[0181] In this embodiment, an external infrared temperature measurement sensor system is used to collect temperature data in real time, so that the temperature is maintained within a range of room temperature ± 5°C, and the stability during the hydrolysis conversion process is controlled.

[0182] It is calculated that in this embodiment, 300 kg of corn straw powder is treated within 20 min of operation; 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 straw powder, and the cellulose / sulfuric acid ratio is 0.60. The cellobiose (glucose) in the obtained oligosaccharide with DP < 7 is 2.82 g / l, and the xylotriose is 3.11 g / l.

[0183] Example 4 Continuous feeding of biomass powder and high-concentration inorganic acid

[0184] The hydrolysis reaction specifically includes the following steps:

[0185] (1) The straw powder is fed into the automatic weighing distributor 100, the multi-blade discharge flap 122 of the automatic weighing distributor 100 is controlled, so that the straw powder is quantitatively stored in the second soft connection hopper 131 after completion; further control the multi-blade distribution flap 142, so that the straw powder is stored in the second soft connection hopper 131 or is fed into the reactor lower body 320 at a rate of 15 kg / min through the feed port 311.

[0186] (2) The 70% w / w sulfuric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500 at a flow rate of 10.71 kg / min.

[0187] (3) The reactor lower body 320 is rotated at a speed of 200 rpm, and the automatic weighing distributor 100 and the catalyst liquid distributor 100 work continuously; the rotation speed of the first stirrer 201 and the second stirrer 202 is 80 rpm during the reaction; this whole process makes the straw powder and the catalyst evenly and quickly distributed to the whole hydrolysis process while being distributed and liquidized, and they interact uniformly and quickly.

[0188] (4) After the reactor lower body 320 operates for 20 min, the reaction is stopped. After the reaction is completed, the material is taken out through the discharge port 800, washed with water and dried to obtain 178.36 kg of residue, the content of cellulose in the residue is 15.23%, and the content of hemicellulose is 7.12%. After continuous high-efficiency hydrolysis, the conversion rate of cellulose is 70.63%, and the conversion rate of hemicellulose is 76.82%.

[0189] In this embodiment, an external infrared temperature measurement sensor system is used to collect temperature data in real time, so that the temperature is maintained within a range of room temperature ± 5°C, and the stability during the hydrolysis conversion process is controlled.

[0190] It is calculated that in this embodiment, 300 kg of corn straw powder is treated within 20 min of operation; 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 straw powder, and the cellulose / sulfuric acid ratio is 0.60. The cellobiose (glucose) in the obtained oligosaccharide with DP < 7 is 3.30 g / l, and the xylotriose is 3.67 g / l.

[0191] Example 5

[0192] The hydrolysis reaction specifically includes the following steps:

[0193] (1) The straw powder is fed into the automatic weighing distributor 100, the multi-blade discharge flap 122 of the automatic weighing distributor 100 is controlled, so that the straw powder is quantitatively stored in the second soft connection hopper 131 after completion; further control the multi-blade distribution flap 142, so that the straw powder is stored in the second soft connection hopper 131 or is fed into the reactor lower body 320 through the feed port 311 at a rate of 15 kg / min.

[0194] (2) The 70% w / w sulfuric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500 at a flow rate of 21.43 kg / min.

[0195] (3) The reactor lower body 320 is rotated at a speed of 120 rpm, the sulfuric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500, and then the straw powder is fed into the reactor lower body 320 through the automatic weighing distributor 100, the automatic weighing distributor 100 and the catalyst liquid distributor 500 are alternately operated once for each rotation of the rotating disc, and two rotations are a cycle; the rotation speed of the first stirrer 201 and the second stirrer 202 is 60 rpm during the reaction; this whole process enables the straw powder and the catalyst to be evenly and quickly distributed to the whole hydrolysis process while being distributed and liquidized, and the two interact uniformly and quickly.

[0196] (4) After the reactor lower body 320 operates for 20 min, the reaction is stopped. After the reaction is completed, the material is taken out through the discharge port 800, washed with water and dried to obtain 82.46 kg of residue, the content of cellulose in the residue is 16.03%, and the content of hemicellulose is 6.19%. After continuous high-efficiency hydrolysis, the conversion rate of cellulose is 71.59%, and the conversion rate of hemicellulose is 81.37%.

[0197] In this embodiment, an external infrared temperature measurement sensor system is used to collect temperature data in real time, so that the temperature is maintained within a range of room temperature ± 5℃, and the stability during the hydrolysis conversion process is controlled.

[0198] It is calculated that in this embodiment, 150 kg of corn straw powder is treated within 20 min of operation; 214.29 kg of 70% w / w sulfuric acid aqueous solution is used; the solid-liquid ratio is 0.70, and the acid dosage is 1.0 times the mass of the straw powder. The cellobiose (glucose) in the obtained oligosaccharide with DP < 7 is 1.67 g / l, and the xylobiose is 1.96 g / l.

[0199] Example 6

[0200] The hydrolysis reaction specifically includes the following steps:

[0201] (1) The straw powder is fed into the automatic weighing distributor 100, the multi-blade discharge flap 122 of the automatic weighing distributor 100 is controlled, so that the straw powder is quantitatively stored in the second soft connection hopper 131 after completion; further control the multi-blade distribution flap 142, so that the straw powder is stored in the second soft connection hopper 131 or is fed into the reactor lower body 320 through the feed port 311 at a rate of 15 kg / min.

[0202] (2) The 70% w / w sulfuric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500 at a flow rate of 42.86 kg / min.

[0203] (3) The reactor lower body 320 is rotated at a speed of 120 rpm, the sulfuric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500, and then the straw powder is fed into the reactor lower body 320 through the automatic weighing distributor 100, the automatic weighing distributor 100 and the catalyst liquid distributor 500 are alternately operated once for each rotation of the rotating disc, and two rotations are a cycle; the rotation speed of the first stirrer 201 and the second stirrer 202 is 60 rpm during the reaction; this whole process enables the straw powder and the catalyst to be evenly distributed to the whole hydrolysis process at the same time of being distributed and liquidized, and the two interact uniformly and quickly.

[0204] (4) After the reactor lower body 320 operates for 20 min, the reaction is stopped. After the reaction is completed, the material is taken out through the discharge port 800, washed with water and dried to obtain 79.13 kg of residue, and the content of cellulose in the residue is 11.54% and the content of hemicellulose is 5.68%. After continuous high-efficiency hydrolysis, the conversion rate of cellulose is 80.37% and the conversion rate of hemicellulose is 83.58%.

[0205] In this embodiment, an external infrared temperature measurement sensor system is used to collect temperature data in real time, so that the temperature is maintained within a range of room temperature ± 5°C, and the stability during the hydrolysis conversion process is controlled.

[0206] It is calculated that in this embodiment, 150 kg of corn straw powder is treated within 20 min of operation; 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 straw powder. The cellobiose (glucose) in the obtained oligosaccharide with DP < 7 is 0.94 g / l, and the xylobiose is 1.03 g / l. Figure 23 ).

[0207] Example 7

[0208] The hydrolysis reaction specifically includes the following steps:

[0209] (1) The straw powder is fed into the automatic weighing distributor 100, the multi-blade discharge flap 122 of the automatic weighing distributor 100 is controlled, so that the straw powder is quantitatively stored in the second soft connection hopper 131 after completion of the quantitative storage; the multi-blade distribution flap 142 is further controlled, so that the straw powder is stored in the second soft connection hopper 131 or is fed into the reactor lower body 320 at a rate of 15 kg / min through the feed port 311.

[0210] (2) The 75% w / w sulfuric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500 at a flow rate of 20 kg / min.

[0211] (3) The reactor lower body 320 is rotated at a speed of 120 rpm, the sulfuric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500, and then the straw powder is fed into the reactor lower body 320 through the automatic weighing distributor 100, the automatic weighing distributor 100 and the catalyst liquid distributor 500 are alternately operated once for each rotation of the rotating disc, and two rotations are one cycle; the rotation speed of the first stirrer 201 and the second stirrer 202 is 60 rpm during the reaction; this whole process enables the straw powder and the catalyst to be evenly and quickly distributed to the whole hydrolysis process while being distributed and liquidized, and the two interact uniformly and quickly.

[0212] (4) After the reactor lower body 320 operates for 20 min, the reaction is stopped. After the reaction is completed, the material is taken out through the discharge port 800, washed with water and dried to obtain 76.24 kg of residue, and the content of cellulose in the residue is 9.98% and the content of hemicellulose is 4.62%. After continuous high-efficiency hydrolysis, the conversion rate of cellulose is 83.64% and the conversion rate of hemicellulose is 87.13%.

[0213] In this embodiment, an external infrared temperature measurement sensor system is used to collect temperature data in real time, so that the temperature is maintained within a range of room temperature ± 5°C, and the stability during the hydrolysis conversion process is controlled.

[0214] It is calculated that in this embodiment, 150 kg of corn straw powder is treated within 20 min of operation; 200.00 kg of 75% w / w sulfuric acid aqueous solution is used; the solid-liquid ratio is 0.75, and the acid dosage is 1.0 times the mass of the straw powder. The cellobiose (glucose) in the obtained oligosaccharide with DP < 7 is 2.14 g / l, and the xylobiose is 2.23 g / l.

[0215] Example 8

[0216] The hydrolysis reaction specifically includes the following steps:

[0217] (1) The straw powder is fed into the automatic weighing distributor 100, the multi-blade discharge flap 122 of the automatic weighing distributor 100 is controlled, so that the straw powder is quantitatively stored in the second soft connection hopper 131 after completion of the quantitative storage; the multi-blade distribution flap 142 is further controlled, so that the straw powder is stored in the second soft connection hopper 131 or is fed into the reactor lower body 320 at a rate of 15 kg / min through the feed port 311.

[0218] (2) The 80% w / w sulfuric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500 at a flow rate of 18.75 kg / min.

[0219] (3) The reactor lower body 320 is rotated at a speed of 120 rpm, the sulfuric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500, and then the straw powder is fed into the reactor lower body 320 through the automatic weighing distributor 100, the automatic weighing distributor 100 and the catalyst liquid distributor 500 are alternately operated once for each rotation of the rotating disc, and two rotations are one cycle; the rotation speed of the first stirrer 201 and the second stirrer 202 is 60 rpm during the reaction; this whole process enables the straw powder and the catalyst to be evenly and quickly distributed to the whole hydrolysis process while being distributed and liquidized, and the two interact uniformly and quickly.

[0220] (4) After the reactor lower body 320 operates for 20 min, the reaction is stopped. After the reaction is completed, the material is taken out through the discharge port 800, washed with water and dried to obtain 78.19 kg of residue, the content of cellulose in the residue is 5.49%, and the content of hemicellulose is 1.35%. After continuous high-efficiency hydrolysis, the conversion rate of cellulose is 90.78%, and the conversion rate of hemicellulose is 96.14%.

[0221] In this embodiment, an external infrared temperature measurement sensor system is used to collect temperature data in real time, so that the temperature is maintained within a range of room temperature ± 5°C, and the stability during the hydrolysis conversion process is controlled.

[0222] According to calculation, 150 kg of corn straw powder is treated within 20 min in this embodiment; 187.50 kg of 80% w / w sulfuric acid aqueous solution is used; the solid-liquid ratio is 0.8, and the acid dosage is 1.0 times the mass of the straw powder. In the obtained oligosaccharide with DP < 7, cellobiose (glucose) is 2.42 g / l, and xylobiose is 2.62 g / l.

[0223] Example 9

[0224] The hydrolysis reaction specifically includes the following steps:

[0225] (1) The straw powder is fed into the automatic weighing distributor 100, the multi-blade discharge flap 122 of the automatic weighing distributor 100 is controlled, so that the straw powder is quantitatively stored in the second soft connection hopper 131 after completion; further control the multi-blade distribution flap 142, so that the straw powder is stored in the second soft connection hopper 131 or is fed into the reactor lower body 320 through the feed port 311 at a rate of 10 kg / min.

[0226] (2) The 80% w / w sulfuric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500 at a flow rate of 12.50 kg / min.

[0227] (3) The reactor lower body 320 is rotated at a speed of 120 rpm, the sulfuric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500, and then the straw powder is fed into the reactor lower body 320 through the automatic weighing distributor 100, the automatic weighing distributor 100 and the catalyst liquid distributor 500 are alternately operated once for each rotation of the rotating disc, and two rotations are a cycle; the rotation speed of the first stirrer 201 and the second stirrer 202 is 60 rpm during the reaction; this whole process enables the straw powder and the catalyst to be evenly distributed to the whole hydrolysis process at the same time of being distributed and liquidized, and they interact uniformly and quickly.

[0228] (4) After the reactor lower body 320 operates for 30 min, the reaction is stopped. After the reaction is completed, the material is taken out through the discharge port 800, washed with water and dried to obtain 76.43 kg of residue, the content of cellulose in the residue is 5.22%, and the content of hemicellulose is 0.98%. After continuous high-efficiency hydrolysis, the conversion rate of cellulose is 91.43%, and the conversion rate of hemicellulose is 97.26%.

[0229] In this embodiment, an external infrared temperature measurement sensor system is used to collect temperature data in real time, so that the temperature is maintained within a range of room temperature ± 5°C, and the stability during the hydrolysis conversion process is controlled.

[0230] It is calculated that in this embodiment, 150 kg of corn straw powder is treated within 30 min of operation; 187.50 kg of 80% w / w sulfuric acid aqueous solution is used; the solid-liquid ratio is 0.80, and the acid dosage is 1.0 times the mass of the straw powder. The cellobiose (glucose) in the obtained oligosaccharide with DP < 7 is 2.44 g / l, and the xylobiose is 2.67 g / l.

[0231] Example 10

[0232] The hydrolysis reaction specifically includes the following steps:

[0233] (1) The straw powder is fed into the automatic weighing distributor 100, the multi-blade discharge flap 122 of the automatic weighing distributor 100 is controlled, so that the straw powder is quantitatively stored in the second soft connection hopper 131 after completion; further control the multi-blade distribution flap 142, so that the straw powder is stored in the second soft connection hopper 131 or is fed into the reactor lower body 320 through the feed port 311 at a rate of 7.50 kg / min.

[0234] (2) The 80% w / w sulfuric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500 at a flow rate of 9.38 kg / min.

[0235] (3) The reactor lower body 320 is rotated at a speed of 120 rpm, the sulfuric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500, and then the straw powder is fed into the reactor lower body 320 through the automatic weighing distributor 100, the automatic weighing distributor 100 and the catalyst liquid distributor 500 are alternately operated once for each revolution of the rotating disc, and two revolutions are a cycle; the rotation speed of the first stirrer 201 and the second stirrer 202 is 60 rpm during the reaction; this whole process enables the straw powder and the catalyst to be evenly distributed to the whole hydrolysis process at the same time of being distributed and liquidized, and they interact uniformly and quickly.

[0236] (4) After the reactor lower body 320 operates for 40 min, the reaction is stopped. After the reaction is completed, the material is taken out through the discharge port 800, washed with water and dried to obtain 75.37 kg of residue, and the content of cellulose in the residue is 4.82% and the content of hemicellulose is 0.71%. After continuous high-efficiency hydrolysis, the conversion rate of cellulose is 92.19% and the conversion rate of hemicellulose is 98.04%.

[0237] In this embodiment, an external infrared temperature measurement sensor system is used to collect temperature data in real time, so that the temperature is maintained within a range of room temperature ± 5°C, and the stability during the hydrolysis conversion process is controlled.

[0238] According to the calculation, in this embodiment, 150 kg of corn straw powder is treated within 40 min of operation; 187.50 kg of 80% w / w sulfuric acid aqueous solution is used; the solid-liquid ratio is 0.8, and the acid dosage is 1.0 times the mass of the straw powder. The cellobiose (glucose) in the obtained oligosaccharide with DP < 7 is 2.46 g / l, and the xylobiose is 2.67 g / l.

[0239] Example 11

[0240] The hydrolysis reaction specifically includes the following steps:

[0241] (1) The straw powder is fed into the automatic weighing distributor 100, the multi-blade discharge flap 122 of the automatic weighing distributor 100 is controlled, so that the straw powder is quantitatively stored in the second soft connection hopper 131 after completion; further control the multi-blade distribution flap 142, so that the straw powder is stored in the second soft connection hopper 131 or is fed into the reactor lower body 320 through the feed port 311 at a rate of 15 kg / min.

[0242] (2) 30% w / w hydrochloric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500 at a flow rate of 18.75 kg / min.

[0243] (3) The reactor lower body 320 is rotated at a speed of 120 rpm, the sulfuric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500, and then the straw powder is fed into the reactor lower body 320 through the automatic weighing distributor 100, the automatic weighing distributor 100 and the catalyst liquid distributor 500 are alternately operated once for each revolution of the rotating disc, and two revolutions are a cycle; the rotation speed of the first stirrer 201 and the second stirrer 202 is 60 rpm during the reaction; this whole process enables the straw powder and the catalyst to be evenly distributed to the whole hydrolysis process at the same time of being distributed and liquidized, and they interact uniformly and quickly.

[0244] (4) After the reactor lower body 320 operates for 20 min, the reaction is stopped. After the reaction is completed, the material is taken out through the discharge port 800, washed with water and dried to obtain 91.24 kg of residue, and the content of cellulose in the residue is 9.55% and the content of hemicellulose is 4.40%. After continuous high-efficiency hydrolysis, the conversion rate of cellulose is 81.27% and the conversion rate of hemicellulose is 85.34%.

[0245] In this embodiment, an external infrared temperature measurement sensor system is used to collect temperature data in real time, so that the temperature is maintained within a range of room temperature ± 5°C, and the stability during the hydrolysis conversion process is controlled.

[0246] It is calculated that in this embodiment, 150 kg of corn straw powder is treated within 20 min of operation; 187.50 kg of 30% w / w hydrochloric acid aqueous solution is used; the solid-liquid ratio is 0.8, the acid dosage is 0.375 times the mass of the straw powder, and the cellulose / hydrochloric acid ratio is 0.80. The cellobiose (glucose) in the obtained oligosaccharide with DP < 7 is 1.08 g / l, and the xylobiose is 1.19 g / l.

[0247] Example 12

[0248] The hydrolysis reaction specifically includes the following steps:

[0249] (1) The straw powder is fed into the automatic weighing distributor 100, the multi-blade discharge flap 122 of the automatic weighing distributor 100 is controlled, so that the straw powder is quantitatively stored in the second soft connection hopper 131 after completion of the storage; further control the multi-blade distribution flap 142, so that the straw powder is stored in the second soft connection hopper 131 or is fed into the reactor lower body 320 through the feed port 311 at a rate of 15 kg / min.

[0250] (2) The 72% w / w phosphoric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500 at a flow rate of 18.75 kg / min.

[0251] (3) The reactor lower body 320 is rotated at a speed of 120 rpm, the sulfuric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500, and then the straw powder is fed into the reactor lower body 320 through the automatic weighing distributor 100, the automatic weighing distributor 100 and the catalyst liquid distributor 500 are alternately operated once for each rotation of the rotating disc, and two rotations are one cycle; the rotation speed of the first stirrer 201 and the second stirrer 202 is 60 rpm during the reaction; this whole process enables the straw powder and the catalyst to be evenly and quickly distributed to the whole hydrolysis process while being distributed and liquidized, and the two interact uniformly and quickly.

[0252] (4) After the reactor lower body 320 operates for 20 min, the reaction is stopped. After the reaction is completed, the material is taken out through the discharge port 800, washed with water and dried to obtain 86.37 kg of residue, the content of cellulose in the residue is 8.23%, and the content of hemicellulose is 3.20%. After continuous high-efficiency hydrolysis, the conversion rate of cellulose is 84.73%, and the conversion rate of hemicellulose is 89.92%.

[0253] In this embodiment, an external infrared temperature measurement sensor system is used to collect temperature data in real time, so that the temperature is maintained within a range of room temperature ± 5°C, and the stability during the hydrolysis conversion process is controlled.

[0254] It is calculated that in this embodiment, 150 kg of corn straw powder is treated within 20 min of operation; 187.50 kg of 72% w / w phosphoric acid aqueous solution is used; the solid-liquid ratio is 0.8, and the acid dosage is 0.9 times the mass of the straw powder. The cellobiose (glucose) in the obtained oligosaccharide with DP < 7 is 1.13 g / l, and the xylobiose is 1.27 g / l.

[0255] Example 13

[0256] The hydrolysis reaction specifically includes the following steps:

[0257] (1) The straw powder is fed into the automatic weighing distributor 100, the multi-blade discharge flap 122 of the automatic weighing distributor 100 is controlled, so that the straw powder is quantitatively stored in the second soft connection hopper 131 after completion; further control the multi-blade distribution flap 142, so that the straw powder is stored in the second soft connection hopper 131 or is fed into the reactor lower body 320 through the feed port 311 at a rate of 15 kg / min.

[0258] (2) 80% w / w nitric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500 at a flow rate of 18.75 kg / min.

[0259] (3) The reactor lower body 320 is rotated at a speed of 120 rpm, the sulfuric acid aqueous solution is fed into the reactor lower body 320 through the catalyst liquid distributor 500, and then the straw powder is fed into the reactor lower body 320 through the automatic weighing distributor 100, the automatic weighing distributor 100 and the catalyst liquid distributor 500 are alternately operated once for each rotation of the rotating disc, and two rotations are a cycle; the rotation speed of the first stirrer 201 and the second stirrer 202 is 60 rpm during the reaction; this whole process enables the straw powder and the catalyst to be evenly distributed to the whole hydrolysis process at the same time of being distributed and liquidized, and they interact uniformly and quickly.

[0260] (4) After the reactor lower body 320 operates for 20 min, the reaction is stopped. After the reaction is completed, the material is taken out through the discharge port 800, washed with water and dried to obtain 89.51 kg of residue, the content of cellulose in the residue is 16.24%, and the content of hemicellulose is 8.08%. After continuous high-efficiency hydrolysis, the conversion rate of cellulose is 68.75%, and the conversion rate of hemicellulose is 73.61%.

[0261] In this embodiment, an external infrared temperature measurement sensor system is used to collect temperature data in real time, so that the temperature is maintained within a range of room temperature ± 5℃, and the stability during the hydrolysis conversion process is controlled.

[0262] It is calculated that in this embodiment, 150 kg of corn straw powder is treated within 20 min of operation; 187.50 kg of 80% w / w nitric acid aqueous solution is used; the solid-liquid ratio is 0.8, and the acid dosage is 1.0 times the mass of the straw powder. In the obtained oligosaccharide with DP < 7, cellobiose (glucose) is 0.92 g / l, and xylobiose is 0.99 g / l.

[0263] Comparative Examples 1-5

[0264] The hydrolysis device is replaced, and the straw powder is subjected to hydrolysis treatment, as follows:

[0265]

[0266] Note: The unit of liquid-solid ratio is L / kg.

Claims

1. The application of a device for hydrolyzing biomass, characterized in that, The device for hydrolyzing biomass includes: The reactor (300) includes an upper reactor body (310) and a lower reactor body (320), the upper reactor body (310) covering the lower reactor body (320) and having an inlet (311) and an outlet (800) at the top, the inlet (311) being configured to allow biomass powder to be fed into the lower reactor body (320), and the lower reactor body (320) being configured to rotate relative to the upper reactor body (310) about a vertical axis of rotation (340); An automatic weighing feeder (100), connected to the feed inlet (311), is configured to distribute biomass powder through the feed inlet (311) into the area of ​​the lower body of the reactor (320) that sweeps across the feed inlet (311) when the lower body of the reactor (320) is rotated; A catalyst distributor (500) is connected below the upper body (310) of the reactor and is configured to distribute a high concentration of inorganic acid within the lower body (320) of the reactor. The first stirrer (201) and the second stirrer (202) are both connected to the upper body (310) of the reactor and extend into the lower body (320) of the reactor. The catalyst distributor (500), the second agitator (202), the feed inlet (311) and the first agitator (201) are arranged at intervals along the rotation direction of the lower body (320) of the reactor; The catalyst distributor (500) includes: Liquid distribution channel (511), which extends radially along the vertical rotation axis (340); The reactor also includes a plurality of liquid distribution holes (512), through which the high-concentration inorganic acid can flow from the liquid distribution channel (511) through the plurality of liquid distribution holes (512) to the lower body (320) of the reactor. The plurality of liquid distribution holes (512) are spaced apart along the liquid distribution channel (511), and the interval between two adjacent liquid distribution holes (512) gradually decreases in an arithmetic sequence along the radial direction away from the vertical axis of rotation. The automatic weighing and feeding device (100) includes a weighing hopper housing (121), a second flexible connecting hopper (131), a biomass feeder housing (141), an inlet hopper (151), a multi-blade feeding flap (122), a multi-blade feeding flap (142), and a weighing sensor (126). The weighing sensor (126) is located on the outside of the weighing hopper housing (121). The weighing hopper housing (121), the second flexible connecting hopper (131), the biomass feeder housing (141), and the inlet hopper (151) are connected sequentially from top to bottom to form a feeding channel (110), through which the biomass powder... The feed inlet (311) of the upper body (310) of the reactor can enter through the feeding channel (110); the multi-blade feeding flap (122) is located in the feeding channel (110) within a section of the weighing hopper shell (121), and the multi-blade feeding flap (142) is located in the feeding channel (110) within a section of the biomass feeder shell (141), and both can rotate around their respective rotation axes; the rate at which the biomass powder enters the lower body (320) of the reactor is controlled by adjusting the rotation speed of the multi-blade feeding flap (142) in the automatic weighing feeder (100); The rotation axis of the multi-blade feeding flap (122) and the rotation axis of the multi-blade feeding flap (142) both extend radially along the vertical rotation axis (340) and are located in the same vertical plane; the multi-blade feeding flap (122) and the multi-blade feeding flap (142) both form conical surfaces when rotated, and the two conical surfaces formed overlap with the projection area of ​​the feed inlet (311) in the top view direction and are located in a fan-shaped area within the lower body (320) of the reactor; the projection area is trapezoidal; The diameter and height of the inner cavity of the lower body (320) of the reactor are 0.6-2.6×0.2-0.6mm respectively; the length of the liquid distribution channel (511) is 1200mm and the diameter is 40-60mm. 200-400 liquid distribution holes (512) are arranged at intervals along the liquid distribution channel (511). The interval between two adjacent liquid distribution holes (512) gradually decreases in an arithmetic sequence along the radial direction away from the vertical rotation axis (340). The diameter of these liquid distribution holes (512) is 1.5-3mm; the first stirrer (201) and the second stirrer (202) are two stirrers each, for a total of four stirrers; The biomass powder is fed into the lower body (320) of the reactor at a rate of 7.5-15 kg / min through the feed inlet (311), and the high-concentration inorganic acid is fed into the lower body (320) of the reactor at a rate of 9.38-18.8 kg / min through the catalyst distributor (500). The biomass powder and the high-concentration inorganic acid are fed in a cross-feed manner, with the inorganic acid fed first and then the biomass powder fed. The lower body (320), the first stirrer (201), and the second stirrer (202) rotate. The biomass powder undergoes a hydrolysis reaction with the high-concentration inorganic acid. After the reaction stops, the biomass powder is discharged from the outlet (800). The rotation speed of the lower body (320) of the reactor is 110-130 rpm; the high concentration inorganic acid is 80-85 wt% sulfuric acid; the rotation speed of the first stirrer (201) and the second stirrer (202) is 60-80 rpm; The rate ratio of the high-concentration inorganic acid to the biomass powder introduced into the lower body (320) of the reactor is 1.1-1.3:1; The mass of the inorganic acid is 0.8-1.2 times that of the biomass powder; The reaction temperature is 20-35℃.

2. The application according to claim 1, characterized in that, The biomass is any one or a combination of several of the following: wheat straw, corn straw, rice straw, sorghum straw, cotton straw, sugarcane bagasse, corn cob, switchgrass, reeds, and rapeseed.

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

4. The application according to claim 1, characterized in that, The catalyst distributor (500) includes a distribution pipe (510); the distribution channel (511) is defined by the inner wall of the distribution pipe (510); and the plurality of distribution holes (512) are formed on the pipe wall of the distribution pipe (510).

5. The application according to claim 4, characterized in that, The device for hydrolyzing biomass includes a connecting flange (530) which is installed on the upper body (310) of the reactor and is used to connect to an external catalyst supply device. The catalyst distributor (500) includes a distribution pipe adapter (520) that connects the distribution pipe (510) to the connecting flange (530).

6. The application according to claim 1, characterized in that, The ratio of the rotational speed of the multi-blade fabric flap (142) to the rate at which the biomass powder enters the lower body (320) of the reactor is 2-8 rpm: 1 kg / min.

7. The application according to claim 1, characterized in that, The multi-bladed feeding flap (122) and the multi-bladed feeding flap (142) divide the feeding channel (110) into a storage and weighing section (1101), a pouring 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 feeding channel (110) is connected to the feed inlet (311) of the upper body (310) of the reactor through the lower port of the smooth transition section (1103); the multi-bladed... The feeding flap (122) is located between the storage weighing section (1101) and the pouring section (1102), and is configured to feed the biomass powder in the storage weighing section (1101) to the pouring section (1102) when rotating; the multi-blade feeding flap (142) is located between the pouring section (1102) and the smooth transition section (1103), and is configured to feed the biomass powder in the pouring section (1102) to the smooth transition section (1103) when rotating.

8. The application according to claim 7, characterized in that, The cross-sections of the material storage and weighing section (1101) and the material pouring section (1102) perpendicular to the vertical direction are both rectangular; the area of ​​the rectangle is larger than the area of ​​the projected area.

9. The application according to claim 1, characterized in that, The device for hydrolyzing biomass includes a first flexible connection hopper (111), which connects the weighing hopper shell (121) in the automatic weighing feeder (100) to an external biomass pneumatic conveying device.

10. The application according to claim 1, characterized in that, The automatic weighing and feeding device (100) includes a first bearing seat (123) and a second bearing seat (143). The multi-blade feeding flap (122) is installed in the weighing hopper housing (121) through the first bearing seat (123). The multi-blade feeding flap (142) is installed in the biomass feeder housing (141) through the second bearing seat (143).

11. The application according to claim 1, characterized in that, The device for hydrolyzing biomass includes a feeder frame (420) for fixing and supporting the automatic weighing feeder (100). The automatic weighing and feeding device (100) includes a weighing frame (127), the weighing hopper shell (121) is supported on the weighing frame (127) by the weighing sensor (126), and the weighing frame (127) is fixedly supported on the feeding device frame (420).

12. The application according to claim 1, characterized in that, The automatic weighing and distributing device (100) includes a drive mechanism configured to drive the multi-blade feeding flap (122) and the multi-blade distributing flap (142) to rotate respectively.

13. The application according to claim 12, characterized in that, The driving mechanism is a motor driving mechanism.

14. The application according to any one of claims 1 to 5, characterized in that, Multiple first stirrers (201) and multiple second stirrers (202) are provided. Multiple first stirrers (201) are located on a first radial line of the vertical rotation axis (340) and are distributed at intervals. Multiple second stirrers (202) are located on another radial line of the vertical rotation axis (340) and are distributed at intervals.

15. The application according to any one of claims 1 to 5, characterized in that, The first stirrer (201) and the second stirrer (202) have the same structure, including: Agitator (230); A stirrer support structure (220) is fixedly installed on the upper end face of the reactor body (310); A stirring drive mechanism (210) is fixedly installed on the stirrer support structure (220). A coupling (240) is disposed inside the agitator support structure (220), and the output shaft of the agitator drive mechanism (210) extends into the inside of the agitator support structure (220) and is connected to the agitator blade (230) through the coupling (240). And an auxiliary bearing (250), the stirring paddle (230) being rotatably fixed to the stirrer support structure (220) via the auxiliary bearing (250).

16. The application according to claim 15, characterized in that, The stirring paddle (230) is a hollow spiral blade structure, including a stirring frame (231), a stirring shaft (232) passing through the stirring frame (231), and hollow spiral blades (233) circumferentially distributed on the stirring frame (231) along the stirring shaft (232).

17. The application according to claim 1, characterized in that, The device for hydrolyzing biomass includes an observation port (700) and a breathing port (900), both of which are located on the upper body (310) of the reactor.

18. The application according to claim 17, characterized in that, The apparatus for hydrolyzing biomass includes a material temperature measuring device (600) installed on the upper body (310) of the reactor; the material temperature measuring device (600) is configured to detect the temperature of the material in the lower body (320) of the reactor.

19. The application according to claim 1, characterized in that, The apparatus for hydrolyzing biomass includes a rotary mechanism configured to support and drive the lower body (320) of the reactor to rotate relative to the upper body (310) about a vertical axis of rotation (340).

20. The application according to claim 19, characterized in that, The rotary mechanism includes: Drive gear (412); And an external gear bearing (323), the external gear of which is coaxially fixedly connected to the lower body (320) of the reactor, and the external gear of which meshes with the drive gear (412).

21. The application according to claim 20, characterized in that, The device for hydrolyzing biomass includes a rotary power source (413), the output shaft of which is connected to the drive gear (412).

22. The application according to claim 21, characterized in that, The apparatus for hydrolyzing biomass includes a mounting structure (324) and a disc reactor frame (410) for supporting the reactor (300); the disc reactor frame (410) includes a reactor upper body structure support (411) and a reactor lower body mounting structure (414); the reactor upper body (310) is fixedly supported on the reactor upper body structure support (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 (414) through the mounting structure (324).

23. The application according to claim 22, characterized in that, The reactor upper body (310) includes a reactor upper body skeleton (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 skeleton (314).

24. The application according to claim 23, characterized in that, The reactor upper body (310) includes a support (316), which is fixedly connected to the upper outer periphery of the reactor upper body frame (314). The support (316) is used to be fixedly connected to the reactor upper body structural support (411) so that the reactor upper body (310) is fixedly supported by the reactor upper body structural support (411).

25. The application according to claim 22, characterized in that, The reactor lower body (320) includes a reactor lower body body (321) and a reactor lower body support structure (322). The reactor lower body body (321) is made of a lightweight and corrosion-resistant material. The reactor lower body body (321) is configured to be housed in the reactor lower body support structure (322). The external gear of the external gear bearing (323) is coaxially and fixedly connected to the reactor lower body support structure (322) to achieve coaxial and fixed connection between the external gear of the external gear bearing (323) and the reactor lower body (320).

26. The application according to claim 1, characterized in that, The apparatus for hydrolyzing biomass includes a rotary sealing assembly (325) configured to rotatably connect and seal the upper body (310) of the reactor with the lower body (320).

27. The application according to claim 26, characterized in that, The rotary sealing assembly (325) is located at the top of the lower body (320) of the reactor.

28. The application according to claim 26, characterized in that, The rotating sealing assembly (325) is located at the lower part of the upper body (310) of the reactor.

29. The application according to claim 1, characterized in that, The lower part (320) of the reactor is cylindrical.

30. The application according to claim 1, characterized in that, The reactor (300) is generally disc-shaped.

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