CN216419342U - Lignin separation system - Google Patents
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- CN216419342U CN216419342U CN202123026296.9U CN202123026296U CN216419342U CN 216419342 U CN216419342 U CN 216419342U CN 202123026296 U CN202123026296 U CN 202123026296U CN 216419342 U CN216419342 U CN 216419342U
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Abstract
The utility model discloses a lignin separation system, which comprises a reaction kettle, a solvent tank, a lignin separation tank, a first filter press, a water tank and a solvent/water tank; after the biomass raw material in the reaction kettle and the solvent and acid from one of the solvent tanks are stirred together and heated for decomposition, most lignin is dissolved in the solvent and then pumped into the other solvent tank, after the solvent in the initial solvent tank is pumped out, the solvent is reversely pumped from the other solvent tank to the initial solvent tank through the reaction kettle, the circulation is repeated for many times until the lignin is basically dissolved, then the liquid in the two solvent tanks is respectively introduced into the two lignin separation tanks, meanwhile, the water is respectively introduced into the two lignin separation tanks from the water tank, the lignin is separated out and separated from the solvent and enters a first filter press together with the liquid, the solid obtained by extrusion separation is the lignin, and the solvent and the water are introduced into the solvent/water tank. The utility model discloses process route is simple and easy, and equipment is simple, and lignin separation is efficient.
Description
Technical Field
The utility model relates to an agriculture and forestry biological data utilizes technical field, specifically is a lignin piece-rate system.
Background
The energy and environmental crisis is one of the major obstacles facing the sustainable development of human society in the 21 st century. The production of biomass fuels and bio-based products from the richest and cheapest renewable biomass feedstock on earth is one of the effective approaches to address the above obstacles.
The biomass comprises three main components of cellulose, hemicellulose and lignin, wherein the cellulose accounts for 35-45%, the hemicellulose accounts for 20-40% and the lignin accounts for 20-30%. Cellulose and hemicellulose can be hydrolyzed and saccharified to prepare a series of sugar platform compounds, including liquid fuels such as bioethanol and biobutanol, chemicals such as furfural and xylitol, and the like, and the cellulose can also be used for preparing functional cellulose materials. As a natural high molecular material, lignin molecules contain a large number of high-activity hydroxyl, phenolic hydroxyl, carbonyl and benzene ring structures, and are the only compounds capable of providing a large number of renewable aromatic groups in three renewable resources. In view of the above, the lignin is expected to be widely applied to vanillin, oil field chemicals, rubber reinforcing agents, functionalized aromatic hydrocarbons for producing fine chemicals or used as a high molecular raw material for preparing high molecular polymers such as resin, rubber and the like. However, natural lignin is often accompanied by a large amount of impurities such as cellulose, and it must be separated and purified before use, but its separation is difficult due to its complex, amorphous three-dimensional network structure.
Aiming at the existing industrial relevant separation equipment or method, the obtained product mostly destroys the aryl ether bond and generates a C-C condensation structure, so that the network structure of lignin collapses and the reactivity of lignin is lost, therefore, the method is a key problem for improving the lignin separation rate on the premise of not destroying the lignin activity. From the viewpoint of production process, the following disadvantages mainly exist: the reaction conditions are harsh, a chemical method needs to consume a large amount of other raw materials and can be carried out under a specified higher temperature and pressure, and an enzymatic hydrolysis method needs to provide a specified environment meeting the enzymatic activity; the cyclic utilization of production auxiliary raw materials is not realized during the system design, and the problems of resource waste and the like exist; low production efficiency and difficult continuous large-scale production. Patent CN107151560B discloses a lignin separation and steam cracking system and method thereof, which uses steam cracking to separate lignin and has the problems of high operation temperature, high system requirement, etc.
SUMMERY OF THE UTILITY MODEL
The utility model discloses the technical problem that solve lies in how to solve the problem that current lignin separation technique has separation condition to require height, production efficiency to hang down.
The utility model discloses a following technical means realizes solving above-mentioned technical problem:
a lignin separation system comprises a reaction kettle, a solvent tank, a lignin separation tank, a first filter press, a water tank and a solvent/water tank; the solvent tank and the lignin separation tank are respectively provided with two tanks; the solvent outlet/inlet of one solvent tank is communicated with a solvent inlet/outlet of the reaction kettle, and the solvent outlet/inlet of the reaction kettle is communicated with the solvent inlet/outlet of the other solvent tank; the discharge ports of the two solvent tanks are respectively communicated with the feed ports of the two lignin separation tanks, the discharge ports of the two lignin separation tanks are respectively communicated with the feed port of the first filter press, and the water inlets of the two lignin separation tanks are respectively communicated with the water tank; and the liquid outlet of the first filter press is communicated with the liquid inlet of the solvent/water tank.
The utility model discloses when using, stir and add the thermal decomposition back jointly by the living beings raw materials in the reation kettle with solvent and the acid that comes from one of them solvent tank, most lignin is dissolved in the solvent, then by suction to another solvent tank in, after the solvent has been taken out to initial solvent tank, with the solvent from the reverse suction of another solvent tank through reation kettle to initial solvent tank in, so circulation repeated suction is many times dissolved to lignin basically, let in two lignin knockout drums respectively with the liquid in two solvent tanks again, two lignin knockout drums are accesss to respectively by the basin simultaneously, lignin is by separating out in the solvent, together get into first pressure filter with liquid, the solid of extrusion separation out is the lignin, solvent and water let in the solvent/jar.
The utility model discloses combine chemistry and physics method, utilize solvent, acid and water to separate out lignin from biomass raw materials, through the setting of solvent groove, make the solvent get into another solvent groove through reation kettle from one of them solvent groove, during rethread reation kettle got back to original solvent groove, formed the system of a solvent circulation, make the solvent make a round trip many times through reation kettle like this to react with biomass raw materials in the reation kettle many times, dissolve until lignin, improve ligneous dissolution efficiency, the utility model discloses the process route is simple and easy, and equipment is simple, and lignin separation efficiency is high, easily realizes extensive industrialization.
Preferably, the reaction kettle is provided with a raw material inlet.
Preferably, the device further comprises a solvent buffer tank, wherein an outlet of the solvent buffer tank is communicated with another solvent inlet of the reaction kettle, and an inlet of the solvent buffer tank is communicated with another solvent outlet of the reaction kettle.
Preferably, the liquid inlets of the solvent buffer tank are respectively connected with the inlets of the two solvent tanks, and the solvent buffer tank is used for transferring the solution from the solvent buffer tank to the two solvent tanks.
Preferably, the water inlet of the reaction kettle is communicated to the water tank.
Preferably, the device also comprises an air compressor and an air storage tank; the air outlet of the air compressor is communicated with the air inlet of the reaction kettle, and the air inlet of the air compressor is communicated with the air outlet of the air storage tank.
Preferably, the reactor further comprises a second filter press, and an inlet of the second filter press is communicated with the solid-liquid discharge hole of the reaction kettle.
Preferably, the device further comprises a high-efficiency evaporator, wherein a liquid inlet of the high-efficiency evaporator is communicated with liquid outlets of the solvent/water tank, a water outlet of the high-efficiency evaporator is communicated to the water tank, and a solvent outlet of the high-efficiency evaporator is communicated with solvent recovery ports of the two solvent tanks.
The utility model discloses a theory of operation does: when in use, the biomass raw material is firstly crushed and then added into a reaction kettle through a raw material inlet; adding a solvent and acid into one solvent tank, pumping into a reaction kettle after uniformly stirring, stirring together and heating for decomposition, dissolving most lignin in the solvent, pumping into the other solvent tank, pumping the solvent from the other solvent tank to the initial solvent tank through the reaction kettle in a reverse manner after the solvent in the initial solvent tank is pumped out, circularly and repeatedly pumping for many times in the same manner until the lignin is basically dissolved, and stopping pumping the solvent; pumping the solvent in the solvent buffer tank into a reaction kettle, refluxing the solvent in the reaction kettle to the solvent buffer tank, stopping after a period of time, separating the residual small amount of lignin and bringing the lignin into the solvent buffer tank, and transferring the liquid mixed with the residual small amount of lignin into two solvent tanks from the solvent buffer tank; pumping water from the water tank to the reaction kettle, introducing compressed air from the air storage tank, extruding the residual residues in the reaction kettle by the aid of water and the compressed air, allowing the residues to flow out to a second filter press, extruding by the second filter press to obtain semi-cellulose solid, and introducing the water into the water tank again for use; respectively introducing liquid in the two solvent tanks into two lignin separation tanks, simultaneously introducing water in an amount equal to that of the solvent into the two lignin separation tanks by the water tank, fully stirring, separating out and separating the lignin from the solvent, introducing a solid-liquid mixture into a first filter press, extruding and separating out solid which is the lignin by the first filter press, and introducing the solvent and the water into the solvent/water tank; the liquid in the solvent/water tank is introduced into a high-efficiency evaporator, after evaporation treatment, the water flows back to the water tank for use, and the solvent is introduced into the two solvent tanks, so that a water and solvent recycling system is formed.
The utility model has the advantages that:
1. the utility model discloses combine chemistry and physics method, utilize solvent, acid and water to separate out lignin from biomass raw materials, through the setting of solvent groove, make the solvent get into another solvent groove through reation kettle from one of them solvent groove, during rethread reation kettle got back to original solvent groove, formed the system of a solvent circulation, make the solvent make a round trip many times through reation kettle like this to react with biomass raw materials in the reation kettle many times, dissolve until lignin, improve ligneous dissolution efficiency, the utility model discloses the process route is simple and easy, and equipment is simple, and lignin separation efficiency is high, easily realizes extensive industrialization.
2. The utility model discloses the recovery system of solvent and water that sets up for raw materials such as solvent, water and remaining acid that add in the production process all can be retrieved and recycled, reduce wasting of resources and environmental pollution, low in production cost is honest and clean.
Drawings
Fig. 1 is a schematic structural diagram of a lignin separation system according to an embodiment of the present invention.
The reference numbers illustrate:
1. a reaction kettle; 101. a raw material inlet; 2. a solvent tank; 201. a first solvent tank; 202. a second solvent tank; 3. a lignin separation tank; 301. a first lignin separation tank; 302. a second lignin separation tank; 4. a first filter press; 5. a water tank; 6. a solvent/water tank; 7. a solvent buffer tank; 8. an air compressor; 9. a gas storage tank; 10. a second filter press; 11. a high-efficiency evaporator.
Detailed Description
To make the purpose, technical solution and advantages of the embodiments of the present invention clearer, the embodiments of the present invention are combined to clearly and completely describe the technical solution in the embodiments of the present invention, and obviously, the described embodiments are some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.
Example one
As shown in fig. 1, the embodiment discloses a lignin separation system, which includes a reaction kettle 1, a solvent tank 2, a lignin separation tank 3, a first filter press 4, a water tank 5, a solvent/water tank 6, a solvent buffer tank 7, an air compressor 8, an air storage tank 9, a second filter press 10, and a high-efficiency evaporator 11.
As shown in fig. 1, the reaction kettle 1 of the present embodiment is provided with a raw material inlet 101, a solid-liquid discharge port, a compressed air inlet, a water inlet, a first solvent inlet/outlet, a second solvent inlet, a first solvent outlet/inlet, and a second solvent outlet, and the raw material inlet 101 is connected to an external conveyor belt.
As shown in fig. 1, the solvent tank 2 of the present embodiment includes two tanks, specifically, a first solvent tank 201 and a second solvent tank 202, where the first solvent tank 201 and the second solvent tank 202 are respectively provided with a solvent inlet/outlet, a liquid inlet, a liquid outlet, and a solvent recovery port;
the solvent outlet/inlet of the first solvent tank 201 is connected with the first solvent inlet/outlet of the reaction kettle 1 through a connecting pipeline, the solvent inlet/outlet of the second solvent tank 202 is connected with the first solvent outlet/inlet of the reaction kettle 1 through a connecting pipeline, and the solvent reaches the second solvent tank 202 after entering the reaction kettle from the first solvent tank 201, and then reaches the first solvent tank 201 after entering the reaction kettle from the second solvent tank 202, so that a solvent circulating system can be formed, the solvent passes through the reaction kettle 1 repeatedly in a reciprocating manner, and reacts with the biomass raw material in the reaction kettle 1 for multiple times until lignin is dissolved, and the wood dissolving efficiency is improved.
As shown in fig. 1, the lignin separation tank 3 of this embodiment includes two separation tanks, specifically, a first lignin separation tank 301 and a second lignin separation tank 302, and the first lignin separation tank 301 and the second lignin separation tank 302 are both provided with a water inlet, a feed inlet, and a discharge outlet;
the feed inlet of the first lignin separation tank 301 is connected with the liquid outlet of the first solvent tank 201 by a connecting pipeline, and the feed inlet of the second lignin separation tank 302 is connected with the liquid outlet of the second solvent tank 202 by a connecting pipeline, and is used for introducing the reacted liquid in the first solvent tank 201 and the second solvent tank 202 into the first lignin separation tank 301 and the second lignin separation tank 302 respectively.
As shown in fig. 1, the first filter press 4 of the present embodiment is provided with two liquid inlets, one liquid outlet and a product outlet; two liquid inlets on the first filter press 4 are respectively connected with the discharge ports of the first lignin separation tank 301 and the second lignin separation tank 302 by adopting the existing connecting pipelines; the product outlet of the first filter press 4 is connected with a valve for controlling the discharge of the lignin product.
As shown in fig. 1, a plurality of water inlets and water outlets are formed in the water tank 5 of this embodiment, and two of the water outlets of the water tank 5 are respectively connected to the water inlets of the first lignin separation tank 301 and the second lignin separation tank 302 by using the existing connecting pipes; the other water outlet of the water tank 5 is connected with the water inlet of the reaction kettle 1 by adopting the existing connecting pipeline and is used for introducing water into the reaction kettle 1.
As shown in fig. 1, the solvent/water tank 6 of this embodiment is provided with a liquid inlet and a liquid outlet, and the liquid inlet of the solvent/water tank 6 is connected to the liquid outlet of the first filter press 4 by using an existing connecting pipe.
As shown in fig. 1, the solvent buffer tank 7 of this embodiment is provided with two liquid outlets, a solvent inlet and a solvent outlet, the solvent inlet of the solvent buffer tank 7 is connected to another solvent outlet of the reaction kettle 1 by using an existing connecting pipeline, the solvent outlet of the solvent buffer tank 7 is connected to another solvent inlet of the reaction kettle 1 by using an existing connecting pipeline, and the two liquid outlets of the solvent buffer tank 7 are connected to the liquid inlets of the first solvent tank 201 and the second solvent tank 202 by using existing connecting pipelines, respectively, for transferring the solvent from the solvent buffer tank 7 to the two solvent tanks 2.
As shown in fig. 1, the air outlet of the air compressor 8 of this embodiment is communicated with the air inlet of the reaction kettle 1 by using the existing connecting pipeline, and the air inlet of the air compressor 8 is communicated with the air outlet of the air storage tank 9 by using the existing connecting pipeline, so as to introduce compressed air into the reaction kettle, thereby realizing solid-liquid separation.
As shown in fig. 1, a liquid inlet, a discharge port and a water outlet are formed in the second filter press 10 of this embodiment, the liquid inlet of the second filter press 10 is connected to the solid-liquid discharge port of the reaction kettle 1 by using an existing connecting pipe, a valve is installed at the discharge port of the second filter press 10 for controlling the discharge of cellulose or hemicellulose, and the water outlet of the second filter press 10 is connected to another water inlet of the water tank 5 by using an existing connecting pipe, so that the water returning tank 5 is recycled.
As shown in fig. 1, the high-efficiency evaporator 11 of this embodiment has a liquid inlet, a water outlet and two solvent outlets, the liquid inlet of the high-efficiency evaporator 11 is connected to the liquid outlet of the solvent/water tank 6 by using an existing connecting pipe, the water outlet of the high-efficiency evaporator 11 is connected to a water inlet of the water tank 5 by using an existing connecting pipe, so that the water flow returning tank 5 is recycled, and the two solvent outlets of the high-efficiency evaporator 11 are connected to the solvent recovery ports of the first solvent tank 201 and the second solvent tank 202 by using existing connecting pipes respectively.
The reation kettle 1, solvent groove 2, lignin knockout drum 3, first pressure filter 4, basin 5, solvent/water pitcher 6, solvent buffer tank 7, air compressor machine 8, gas holder 9, second pressure filter 10, high-efficient evaporimeter 11 that this embodiment discloses adopt current connecting tube to connect between each part, and the valve is installed respectively to the installation technology that adopts current valve and pipeline on the connecting tube for the intercommunication between each part is controlled.
The working principle of the embodiment is as follows: the utility model provides a lignin separation system, when in use, S firstly crushes biomass raw materials to be crushed and then adds the crushed biomass raw materials into a reaction kettle 1 through a raw material inlet 101; adding a solvent and acid into one solvent tank 2, pumping into a reaction kettle 1 after uniformly stirring, dissolving most lignin in the solvent after jointly stirring and heating for decomposition, pumping into the other solvent tank 2, pumping the solvent from the other solvent tank 2 to the initial solvent tank 2 in a reverse direction after the solvent in the initial solvent tank 2 is pumped out, and repeating the pumping in such a way for multiple times until the lignin is basically dissolved, and stopping pumping the solvent; pumping the solvent in the solvent buffer tank 7 into the reaction kettle 1, refluxing the solvent in the reaction kettle 1 to the solvent buffer tank 7 again, stopping after a period of time, separating the residual small amount of lignin into the solvent buffer tank 7, and transferring the liquid mixed with the residual small amount of lignin into the two solvent tanks 2 from the solvent buffer tank 7; pumping water from the water tank 5 to the reaction kettle 1, introducing compressed air from the air storage tank 9, extruding residual residues in the reaction kettle 1 by water and compressed air, flowing the residues to a second filter press 10, extruding the residues by the second filter press 10 to obtain semi/cellulose solid, and introducing the water into the water tank 5 again for use; respectively introducing the liquid in the two solvent tanks 2 into two lignin separation tanks 3, simultaneously introducing water with the same amount as the solvent into the two lignin separation tanks 3 by a water tank 5, fully stirring, separating out and separating the lignin from the solvent, introducing a solid-liquid mixture into a first filter press 4, extruding and separating out the solid which is the lignin by the first filter press 4, and introducing the solvent and the water into a solvent/water tank 6; the liquid in the solvent/water tank 6 is introduced into a high-efficiency evaporator 11, after evaporation treatment, the water flows back to the water tank 5 for use, and the solvent is introduced into the two solvent tanks 2, so that a water and solvent recycling system is formed.
The solvent comprises phenol, ethylene glycol or butanediol; the acid comprises hydrochloric acid, p-toluenesulfonic acid or sulfuric acid; the volume ratio of the initial solvent to the acid in the solvent tank 2 is 20:1-150: 1; the water amount in the water tank 5 leading to the lignin separation tank 3 is 30-200% of the volume of the solvent in the tank; the heating temperature in the reaction kettle is 50-150 ℃; the flow rate of the compressed air is 50-500L/min, and the pressure is 0.5-5 kg.
Example two
The difference between this embodiment and the first embodiment is: in the embodiment, the rice straws are crushed to below 1.5 cm, and 200 kg of the crushed rice straws are poured into the reaction kettle 1 from the raw material inlet 101 through the conveying belt; adding 800 kg of ethylene glycol and 10 kg of p-toluenesulfonic acid into a first solvent tank 201, uniformly stirring, pumping into a reaction kettle 1, flowing from the reaction kettle 1 to a second solvent tank 202, simultaneously heating the reaction kettle 1 to 80 ℃, pumping the solvent into the reaction kettle 1 from the second solvent tank 202 after the solvent in the first solvent tank 201 is pumped out, and flowing to the first solvent tank 201, repeating the steps for many times until lignin is basically dissolved, and stopping pumping the solvent to ensure that the solvent completely enters the first solvent tank 201 and the second solvent tank 202; adding ethylene glycol into the solvent buffer tank 7, pumping into the reaction kettle 1, refluxing the solvent in the reaction kettle 1 to the solvent buffer tank 7, stopping after a period of time, separating the residual small amount of lignin into the solvent buffer tank 7, and transferring the liquid mixed with the residual small amount of lignin from the solvent buffer tank 7 to the first solvent tank 201 and the second solvent tank 202; pumping water into the reaction kettle 1 from the water tank 5, introducing 1 kg of compressed air with the flow of 200L/min and the pressure of 1 kg into the gas storage tank 9, extruding the residual residues in the reaction kettle 1 by water and the compressed air to flow out to a second filter press 10, extruding by the second filter press 10 to obtain semi-cellulose solid, and introducing the water into the water tank 5 again for use; introducing the solvents in the first solvent tank 201 and the second solvent tank 202 into a first lignin separation tank 301 and a second lignin separation tank 302 respectively, introducing water with the same amount as the solvents into the first lignin separation tank 301 and the second lignin separation tank 302 respectively through a water tank 5, fully stirring, separating out and separating the lignin from the solvents, introducing a solid-liquid mixture into a first filter press 4, extruding and separating out solids from the first filter press 4 to obtain the lignin, and introducing the solvents and the water into a solvent/water tank 6; the liquid in the solvent/water tank 6 is introduced into the high-efficiency evaporator 11, after evaporation treatment, the water flows back to the water tank 5 for use, and the solvent is introduced into the first solvent tank 201 and the second solvent tank 202, so that a water and solvent recycling system is formed.
The extraction rate of lignin obtained by the method of the embodiment is over 95 percent, and ethylene glycol, water and residual p-toluenesulfonic acid are recycled.
EXAMPLE III
The difference between this embodiment and the second embodiment is: the rice straw is changed into corn straw.
The lignin extraction rate obtained by the method of the embodiment exceeds 93 percent, and the ethylene glycol, the water and the residual p-toluenesulfonic acid are recycled.
Example four
The difference between this embodiment and the second embodiment is: replacing glycol with butanediol and p-toluenesulfonic acid with hydrochloric acid.
The extraction rate of lignin obtained by the method of the embodiment is over 90 percent, and ethylene glycol, water and residual p-toluenesulfonic acid are recycled.
The above embodiments are only used to illustrate the technical solution of the present invention, and not to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, it should be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; such modifications and substitutions do not depart from the spirit and scope of the present invention in its corresponding aspects.
Claims (8)
1. A lignin separation system, characterized by: comprises a reaction kettle, a solvent tank, a lignin separation tank, a first filter press, a water tank and a solvent/water tank; the solvent tank and the lignin separation tank are respectively provided with two tanks; the solvent outlet/inlet of one solvent tank is communicated with a solvent inlet/outlet of the reaction kettle, and a solvent outlet/inlet of the reaction kettle is communicated with a solvent inlet/outlet of the other solvent tank; the discharge ports of the two solvent tanks are respectively communicated with the feed ports of the two lignin separation tanks, the discharge ports of the two lignin separation tanks are respectively communicated with the feed port of the first filter press, and the water inlets of the two lignin separation tanks are respectively communicated with the water tank; and the liquid outlet of the first filter press is communicated with the liquid inlet of the solvent/water tank.
2. A lignin separation system according to claim 1, wherein: and a raw material inlet is formed in the reaction kettle.
3. A lignin separation system according to claim 1, wherein: the device also comprises a solvent buffer tank, wherein an outlet of the solvent buffer tank is communicated with another solvent inlet of the reaction kettle, and an inlet of the solvent buffer tank is communicated with another solvent outlet of the reaction kettle.
4. A lignin separation system according to claim 3, wherein: and liquid inlets of the solvent buffer tank are respectively connected with inlets of the two solvent tanks, and are used for transferring the solution from the solvent buffer tank to the two solvent tanks.
5. A lignin separation system according to claim 1, wherein: the water inlet of the reaction kettle is communicated to the inside of the water tank.
6. A lignin separation system according to claim 1, wherein: the device also comprises an air compressor and an air storage tank; the air outlet of the air compressor is communicated with the air inlet of the reaction kettle, and the air inlet of the air compressor is communicated with the air outlet of the air storage tank.
7. A lignin separation system according to claim 1, wherein: the device also comprises a second filter press, wherein an inlet of the second filter press is communicated with the solid-liquid discharge hole of the reaction kettle.
8. A lignin separation system according to claim 1, wherein: the device is characterized by further comprising a high-efficiency evaporator, wherein a liquid inlet of the high-efficiency evaporator is communicated with a liquid outlet of the solvent/water tank, a water outlet of the high-efficiency evaporator is communicated to the water tank, and a solvent outlet of the high-efficiency evaporator is communicated with solvent recovery ports of the two solvent tanks.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114933105A (en) * | 2022-05-10 | 2022-08-23 | 海南省智慧环境投资控股有限公司 | Domestic waste separation and concentration treatment device |
| CN116180479A (en) * | 2023-01-05 | 2023-05-30 | 北京石大油源科技开发有限公司 | Lignin and holocellulose separation device and separation method |
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2021
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114933105A (en) * | 2022-05-10 | 2022-08-23 | 海南省智慧环境投资控股有限公司 | Domestic waste separation and concentration treatment device |
| CN114933105B (en) * | 2022-05-10 | 2024-06-07 | 海南省智慧环境投资控股有限公司 | Domestic waste separation concentration processing apparatus |
| CN116180479A (en) * | 2023-01-05 | 2023-05-30 | 北京石大油源科技开发有限公司 | Lignin and holocellulose separation device and separation method |
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