CN113234500A - Device and method for efficiently preparing biogas and purifying by combining solid-liquid separation with pressure swing adsorption - Google Patents
Device and method for efficiently preparing biogas and purifying by combining solid-liquid separation with pressure swing adsorption Download PDFInfo
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- CN113234500A CN113234500A CN202110356054.1A CN202110356054A CN113234500A CN 113234500 A CN113234500 A CN 113234500A CN 202110356054 A CN202110356054 A CN 202110356054A CN 113234500 A CN113234500 A CN 113234500A
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- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 10
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Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04B—CENTRIFUGES
- B04B11/00—Feeding, charging, or discharging bowls
- B04B11/06—Arrangement of distributors or collectors in centrifuges
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04B—CENTRIFUGES
- B04B15/00—Other accessories for centrifuges
- B04B15/06—Other accessories for centrifuges for cleaning bowls, filters, sieves, inserts, or the like
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04B—CENTRIFUGES
- B04B5/00—Other centrifuges
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04B—CENTRIFUGES
- B04B7/00—Elements of centrifuges
- B04B7/08—Rotary bowls
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04B—CENTRIFUGES
- B04B9/00—Drives specially designed for centrifuges; Arrangement or disposition of transmission gearing; Suspending or balancing rotary bowls
- B04B9/02—Electric motor drives
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/08—Production of synthetic natural gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/103—Sulfur containing contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M1/00—Apparatus for enzymology or microbiology
- C12M1/107—Apparatus for enzymology or microbiology with means for collecting fermentation gases, e.g. methane
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Abstract
The invention discloses a device and a method for efficiently preparing biogas and purifying by combining solid-liquid separation with pressure swing adsorption, wherein the device comprises a solid-liquid separation component, a gas production component, a gas collection component, a desulfurization drying tower, a filter tower, a primary adsorption tank, a secondary adsorption tank and an auxiliary vacuum tank, the solid-liquid separation component comprises a component frame, a centrifugal separation tank, a liquid collection tank mechanism, a slag discharge mechanism and a feeding distribution mechanism, the centrifugal separation tank is of a circular table-shaped shell structure with an opening at the bottom end, the side surface of the centrifugal separation tank is provided with a plurality of centrifugal separation holes communicated with the inside of the centrifugal separation tank, and the method comprises the following steps of S1: firstly, carrying out solid-liquid separation; s2: carrying out fermentation gas production on the solid and the liquid separated in the step S1 by using the gas production assembly; the process integrates three technologies of solid-liquid separation of livestock and poultry manure, fermentation of biogas slurry to produce biogas and purification of biogas, realizes efficient biogas production, optimizes the solid-liquid separation technology again, realizes efficient separation of solid-phase materials and liquid-phase materials, and greatly improves biogas production efficiency.
Description
Technical Field
The invention relates to the technical field of biogas production and purification, in particular to a device and a method for efficiently preparing biogas and purifying by combining solid-liquid separation with pressure swing adsorption.
Background
Biogas is a combustible gaseous mixture produced by microorganisms, the main component of which is methane, with a content of about 50-75%, followed by 25-45% carbon dioxide, in addition to other gases such as hydrogen sulfide, carbon monoxide, nitrogen, water vapor, oxygen, etc. The purification of the biogas mainly comprises the removal of hydrogen sulfide, carbon dioxide, sulfur dioxide, halogenated mixed gas and siloxane in the biogas.
The solid-liquid separation technology is used for separating the solid phase and the liquid phase of the livestock and poultry manure, so that the solid content and the water content of the solid phase in the liquid phase are reduced, the load and the treatment cost of subsequent solid phase and liquid phase treatment are reduced, and the biogas production efficiency can be greatly improved.
Pressure swing adsorption is an important process from biogas purification to natural gas, and means that the mixture gas is separated, purified and purified through a cyclic process of pressure adsorption and decompression or normal pressure desorption or flushing replacement regeneration at a certain temperature. PSA is seen to achieve adsorption and desorption by varying the pressure. The adsorption is usually carried out under a pressure environment, and the pressure swing adsorption provides a method combining pressurization and depressurization, and at a certain temperature, the pressure swing adsorption is usually an adsorption-desorption cyclic operation system consisting of pressurization adsorption and depressurization regeneration. The adsorption quantity of the adsorbent to the adsorbate is increased along with the increase of the pressure and is reduced along with the decrease of the pressure, and simultaneously, in the pressure reduction process, the adsorbed gas is released to regenerate the adsorbent, so that the separation or purification of the multi-component mixed gas is realized, the regeneration of the adsorbent can be carried out without supplying heat from the outside, and the pressure change can be partially compensated by a multi-tower pressure equalizing method in the adsorption-regeneration cycle operation, thereby reducing the pressure drop loss.
At present, most of farms adopt a mixed fermentation mode to prepare biogas, but the effect of preparing biogas by the mode is poor; the existing process for preparing the biogas by adopting the solid-liquid separation device also has the defect of low separation efficiency. The utilization rate of the fermented methane is relatively low due to the fact that the fermented methane contains more impurities; the process structure for purifying the biogas by utilizing the pressure swing adsorption principle is complex, so that the corresponding equipment has large volume and high energy consumption.
Disclosure of Invention
The invention aims to provide a device and a method for efficiently preparing and purifying biogas by combining solid-liquid separation with pressure swing adsorption, and aims to solve the problems.
In order to achieve the purpose, the invention provides the following technical scheme:
a device and a method for efficiently preparing biogas and purifying by combining solid-liquid separation with pressure swing adsorption comprise a solid-liquid separation component, a biogas production component for fermenting liquid components and solid components separated by the solid-liquid separation component to produce biogas, a biogas collection component for intensively storing the biogas produced by the biogas production component, a desulfurization drying tower for desulfurizing and drying the biogas stored in the biogas collection component, a filter tower for filtering the biogas treated by the desulfurization drying tower, a primary adsorption tank and a secondary adsorption tank for adsorbing and purifying the biogas, and an auxiliary vacuum tank for regenerating purification adsorbents in the primary adsorption tank and the secondary adsorption tank;
the solid-liquid separation assembly comprises an assembly frame, a centrifugal separation tank, a liquid collection tank mechanism, a slag discharge mechanism and a feeding distribution mechanism;
the assembly rack comprises a support base, a plurality of support columns extending upwards are fixedly arranged at the edge of the top of the support base, and top support rings are fixedly connected to the tops of the support columns;
the centrifugal separation tank is of a circular truncated cone-shaped shell structure with an opening at the bottom end, the side surface of the centrifugal separation tank is provided with a plurality of centrifugal separation holes communicated with the inside of the centrifugal separation tank, the top of the centrifugal separation tank is fixedly provided with a rotary support ring, the rotary support ring is in rotating fit with the inner side of the top support ring, and the top of the centrifugal separation tank is provided with a feeding shell connecting hole;
the upper end of the top support ring is fixedly connected with a first motor for driving the centrifugal separation tank to rotate, and the first motor drives the rotating support ring to rotate through a transmission part;
a second support ring is fixedly arranged at a position, close to the lower end, on the outer side of the centrifugal separation tank, a second support matching ring is fixedly connected to the inner sides of the support columns, and the second support ring is connected with the second support matching ring in a rotating matching manner;
the liquid collection tank mechanism comprises a liquid collection tank shell surrounding the side face of the centrifugal separation tank, the liquid collection tank shell is communicated with the interior of the centrifugal separation tank through the centrifugal separation hole, an annular liquid collection drainage tube is fixedly arranged at a position, close to the lower end, of the outer side of the liquid collection tank shell, the liquid collection drainage tube is communicated with the interior of the liquid collection tank shell, and the liquid collection tank shell is fixedly connected with the support columns through fixing rings;
the deslagging mechanism comprises a deslagging shell which is rotatably connected inside the centrifugal separation tank, the deslagging shell is of a circular-truncated-cone-shaped shell structure, a spirally-extending deslagging plate is fixedly arranged on the outer side surface of the deslagging shell, and a deslagging shell supporting ring is fixedly arranged inside the deslagging shell;
a second slag discharging shell supporting plate which is horizontally arranged is fixedly arranged inside the centrifugal separation tank, a slag discharging shell supporting column which extends downwards is fixedly arranged at the lower end of the slag discharging shell supporting plate, a slag discharging shell supporting matching ring is fixedly arranged at a position, close to the lower end, of the slag discharging shell supporting column, a slag discharging shell through hole is formed in the top of the slag discharging shell, the slag discharging shell supporting column penetrates into the slag discharging shell through hole, and the slag discharging shell supporting ring is connected to the slag discharging shell supporting matching ring in a rotating matching manner;
the lower end of the support column of the slag discharging shell is fixedly provided with a second motor for driving the slag discharging shell to rotate, and the second motor drives the support ring of the slag discharging shell to rotate through a transmission part;
the lower end of the centrifugal separation tank is provided with a slag collecting shell, the slag collecting shell is an annular hollow shell with a wide upper end and a narrow lower end, the upper end and the lower end of the slag collecting shell are both provided with openings, and the size of the upper end of the slag collecting shell is consistent with that of the lower end of the centrifugal separation tank;
the lower end of the feeding distribution mechanism is communicated with a gap between the inner side wall of the centrifugal separation tank and the outer side wall of the deslagging shell.
Preferably, the purification adsorbent is prepared from 15-26 parts by weight of alumina, 5-18 parts by weight of carbon molecular sieve, 8-17 parts by weight of sodium sulfate, 10-23 parts by weight of zeolite and 18-30 parts by weight of deionized water;
the preparation method of the purification adsorbent comprises the following steps:
1) adding deionized water into a hydrothermal kettle, then adding alumina and a carbon molecular sieve into the hydrothermal kettle, and uniformly stirring;
2) preparing sodium sulfate into a salt solution with the mass concentration of 30-45%, and adding the salt solution into a hydrothermal kettle;
3) and finally, adding zeolite into a hydrothermal kettle for reaction, controlling the temperature of the hydrothermal kettle to be 90-130 ℃, reacting for 20-50 min, and cooling the reaction material after the reaction is finished to obtain the purified adsorbent.
Description of the drawings: the purification adsorbent prepared according to the proportion has strong adsorption performance on carbon dioxide in the biogas, byproducts are not generated in the adsorption process, and the adsorption efficiency on the carbon dioxide is improved.
Preferably, the taper range of the centrifugal separation tank is 0.08-0.16.
Description of the drawings: the taper of the centrifugal separation tank is limited, so that the solid-liquid mixture in the centrifugal separation tank is prevented from being discharged when the solid-liquid mixture is not sufficiently separated, and the separation effect is ensured.
Preferably, an annular slag collecting baffle is fixedly arranged at the edge of the upper end of the slag collecting shell, and the slag collecting baffle surrounds the outer side of the edge of the lower end of the centrifugal separation tank.
Description of the drawings: the slag collecting baffle plate effectively prevents the leakage of solid components discharged from the lower end of the centrifugal separation tank.
Preferably, the feeding distribution mechanism comprises a feeding shell with a downward flared hollow opening, the feeding shell is fixedly connected in the feeding shell connecting hole, the feeding shell extends outwards and turns downwards, a horizontal outward discharging groove is formed in the position, close to the lower end, of the outer side of the feeding shell, a feeding guide plate extending spirally is arranged in the hollow interior of the feeding shell, a feeding interface is fixedly arranged at the top of the feeding shell, a feeding connecting pipe is connected with the feeding interface in a rotating fit manner, and the feeding connecting pipe is communicated and connected with a discharging hole of a feeding conveyor through a pipeline;
the circumferential rotation angle of the feeding guide plate extending from top to bottom is larger than and not more than degrees.
Description of the drawings: the feeding distribution mechanism can efficiently convey and distribute the solid-liquid mixture to the inner side wall of the centrifugal separation tank.
Preferably, the gas production assembly comprises a liquid fermentation tank and a solid fermentation tank, the liquid fermentation tank is provided with a liquid fermentation feed inlet, a liquid fermentation discharge outlet and a liquid fermentation exhaust outlet which are communicated with the interior of the liquid fermentation tank, and the solid fermentation tank is provided with a solid fermentation feed inlet, a solid fermentation discharge outlet and a solid fermentation exhaust outlet which are communicated with the interior of the solid fermentation tank;
the gas collection assembly comprises a gas collection tank, a gas collection tank gas inlet and a gas collection tank gas outlet which are communicated with the inside of the gas collection tank are arranged on the gas collection tank, and a pressure control valve is communicated with the gas collection tank gas outlet.
Description of the drawings: the liquid component and the solid component are fermented independently to produce gas, which is beneficial to adjusting relevant fermentation parameters according to respective actual conditions.
Preferably, the desulfurization drying tower comprises a desulfurization drying shell, the desulfurization drying shell is a flat cylindrical shell, a plurality of desulfurization drying air inlet pipes communicated with the interior of the desulfurization drying shell are fixedly arranged on one side end face of the desulfurization drying shell, an accommodating matching hole is formed in the other side end face of the desulfurization drying shell, a desulfurization accommodating ring is fixedly arranged in the accommodating matching hole, and a desulfurization drying assembly is arranged in the desulfurization accommodating ring;
the desulfurization drying air inlet pipe extends into the desulfurization drying shell, and the part of the desulfurization drying air inlet pipe, which is positioned in the desulfurization drying shell, is provided with a plurality of drying small ventilation holes;
the desulfurization drying assembly comprises an annular hollow desulfurizer containing shell, the desulfurizer containing shell is made of a breathable metal net, a desulfurizer is filled in the desulfurizer containing shell, the desulfurizer containing shell surrounds the outer side of the desulfurization drying air inlet pipe, a sealing cover is fixedly arranged at the outer end of the desulfurizer containing shell, and a plurality of small exhaust holes are formed in the side surface of the desulfurization containing ring;
the desulfurization drying shell is close to and has the filtration ring in the edge, it is hollow network structure to filter the ring, it has dry adsorbent to filter the ring intussuseption, filter the ring with form exhaust passage between the dry casing inside wall of desulfurization, the desulfurization is fixed be equipped with on the dry casing arc lateral wall a plurality of with the blast pipe that exhaust passage is linked together.
Description of the drawings: the desulfurization drying component can be conveniently taken down from the desulfurization containing ring, and the desulfurizer in the desulfurizer containing shell can be conveniently replaced.
Preferably, the filter tower comprises a filter tower shell, a filter air inlet and a filter air outlet which are communicated with the interior of the filter tower shell are fixedly arranged on the filter tower shell, and a filter core body is arranged in the filter tower shell;
the primary adsorption tank comprises a columnar primary adsorption shell which is communicated up and down, an air inlet shell is fixedly arranged at the lower end of the primary adsorption shell, the air inlet shell is a horn-shaped shell with an upward opening, an exhaust shell with a downward opening is fixedly arranged at the top of the primary adsorption shell, an adsorption exhaust port and a vacuum extraction port which are communicated with the inside of the exhaust shell are arranged at the top of the exhaust shell, an air inlet guide shell is fixedly arranged in the air inlet shell, a plurality of hexagonal densely-paved guide air inlet through holes are formed at the lower end of the air inlet guide shell, a plurality of hexagonal densely-paved guide air outlet through holes are formed at the top of the air inlet guide shell, the number of the guide air inlet through holes is the same as that of the guide air outlet through holes, and the guide air inlet through holes and the guide air outlet through holes are communicated in one-to-one smooth transition;
the one-level adsorbs the fixed spacing ring that is equipped with of casing inner wall near the lower extreme, the spacing ring top is piled up and is equipped with a plurality of absorption support rings, the fixed adsorbent that is equipped with in absorption support ring inboard holds the net, the adsorbent holds the net and is made by ventilative metal mesh, the adsorbent holds that the net intussuseption is filled with the purification adsorbent.
Description of the drawings: the air inlet flow guide shell plays a flow guide role, and leads the methane to the adsorbent containing net uniformly from bottom to top, so that the adsorption and purification effects of the purification adsorbent filled in the adsorbent containing net on the methane are more uniform and consistent, and the final methane treatment quality is ensured.
Preferably, the secondary adsorption tank comprises a secondary adsorption tank shell with an upward opening, a plurality of circles of air-isolating guide rings are arranged in the secondary adsorption tank shell, adjacent air-isolating guide rings are communicated with each other near the lower end or near the upper end, and the air-isolating guide rings are communicated with each other at intervals in different positions;
an annular sealing plate is arranged at the top between the adjacent gas-isolating guide rings, a hollow adsorption containing ring is arranged between the adjacent gas-isolating guide rings, a purification adsorbent is filled in the adsorption containing ring, the top of the adsorption containing ring is at a certain distance from the annular sealing plate, the bottom of the adsorption containing ring is at a certain distance from the inner bottom of the shell of the secondary adsorption tank, the upper end face and the lower end face of the adsorption containing ring are respectively provided with a plurality of adsorption ventilation holes communicated with the interior of the adsorption containing ring, and the top of each adsorption containing ring is fixedly connected with the annular sealing plate corresponding to the upper part of the adsorption containing ring;
an annular air inlet shell is fixedly arranged at the position, close to the lower end, of the outer side of the secondary adsorption tank shell, the annular air inlet shell is communicated with a space below the adsorption containing ring at the outermost side, an exhaust ring shell is fixedly arranged on the inner side wall of the adsorption containing ring at the innermost side, and the exhaust ring shell is communicated with a space below the adsorption containing ring at the innermost side;
the auxiliary vacuum tank is fixedly provided with a vacuum tank air inlet and a vacuum tank exhaust port which are communicated with the inside of the auxiliary vacuum tank, and the auxiliary vacuum tank is communicated and connected with the vacuum tank exhaust port and an air inlet of a vacuum air extractor; and a vacuum control valve is connected to the air inlet of the vacuum tank.
Description of the drawings: this structural design utilizes the route of ventilating of reciprocal turn-back for purifying effect to marsh gas is better, adsorb and hold the ring and can conveniently follow down up taking out, make things convenient for the later maintenance to change.
Preferably, the method for preparing and purifying the biogas by using the device for preparing and purifying the biogas efficiently by combining solid-liquid separation and pressure swing adsorption comprises the following steps:
s1: firstly, carrying out solid-liquid separation on the solid-liquid mixed livestock manure by using a solid-liquid separation component, discharging separated liquid from the liquid collection drainage tube, and discharging separated solid from the slag collection shell;
s2: fermenting the solid separated in the step S1 to generate gas by using the solid fermentation tank of the gas generation component, and fermenting the separated liquid to generate gas by using the liquid fermentation tank of the gas generation component;
s3: introducing the original gas produced by the fermentation of the liquid fermentation tank and the solid fermentation tank into the gas collection tank for temporary storage;
s4: introducing the biogas temporarily stored in the gas collecting tank into the desulfurization drying tower, and removing sulfides and moisture in the biogas by using a desulfurizer and a drying agent in the desulfurization drying tower to ensure that the water content of the desulfurized biogas is within the range of 2-9 mg/kg, thereby obtaining dry biogas;
s5: introducing the dried biogas obtained after the treatment in the step S4 into a filter tower to remove insoluble impurities in the dried biogas; adjusting the gas outlet pressure of the filter tower to be between 0.5 and 1.0Mpa to obtain compressed methane;
s6: pressure swing adsorption; intermittently introducing the compressed methane processed in the step S5 into a primary adsorption tank, and adsorbing impurity gases in the compressed methane by using a purification adsorbent in the primary adsorption tank to obtain primary purified methane;
wherein the flow range of the compressed methane is controlled to be 1-3 m3The intermittent air intake time is 3-5 min, the air intake temperature is 50-150 ℃, and the pressure of the primary purified methane is adjusted to 1.0-1.5 Mpa;
then intermittently introducing the biogas into a secondary adsorption tank, and compressing CO in the biogas by using the gravity of a purification adsorbent in the secondary adsorption tank2Adsorbing to obtain purified methane;
wherein the flow of the primary purified biogas is controlled to be 2-5 m3The air inlet intermittent time ranges from 1min to 3min, and the air inlet temperature ranges from 150 ℃ to 250 ℃;
s7: desorbing and regenerating, namely stopping introducing compressed methane into the primary adsorption tank when the purification adsorbent in the primary adsorption tank is saturated, and vacuumizing the primary adsorption tank and the secondary adsorption tank to desorb impurity gas on the purification adsorbent to realize regeneration of the purification adsorbent;
s8: and storing the purified methane in a centralized manner.
Preferably, the desulfurizer is prepared from 15-30 parts by weight of organic amine desulfurizer, 8-15 parts by weight of sulfoxide, 1-8 parts by weight of polyethylene glycol, 5-16 parts by weight of propylene carbonate and 20-35 parts by weight of deionized water;
description of the drawings: the desulfurizer prepared by the proportion has a longer service cycle, thereby reducing the replacement frequency of the desulfurizer and improving the working efficiency and the economic benefit.
The preparation method of the desulfurizer comprises the following steps: mixing and reacting an organic amine desulfurizer with sulfoxide and polyethylene glycol, controlling the pH value of the reaction to be 6-8 to generate a colloidal precipitate, oxidizing the colloidal precipitate with oxygen-enriched gas, and then filtering and separating; washing the filtered precipitate with water for 2-5 times; then, extruding and forming the material which is uniformly mixed with propylene carbonate and deionized water on a forming machine, and naturally drying to obtain the desulfurizer;
description of the drawings: the desulfurizer removes sulfides in the methane, thereby avoiding environmental pollution and improving the quality of the methane.
The drying agent is a composite drying agent which is prepared by compounding 16-33 parts of magnesium sulfate, 12-21 parts of sodium carbonate, 10-20 parts of calcium chloride, 8-23 parts of calcium carbonate, 7-19 parts of calcium hydride and 10-25 parts of deionized water in parts by weight;
description of the drawings: the drying agent in the proportion can efficiently dry various impurity gases in the biogas, and has higher drying efficiency.
The filter membrane in the filter tower is one of a polyamide fiber membrane, a polyimide hollow fiber membrane and a polyvinylidene fluoride hollow fiber membrane.
Compared with the prior art, the invention has the beneficial effects that:
(1) the invention has reasonable structural design and convenient operation, integrates three technologies of solid-liquid separation of the livestock and poultry manure, fermentation of biogas slurry to produce biogas and purification of biogas, and realizes high-efficiency biogas production;
(2) the process optimizes the solid-liquid separation technology again, realizes the high-efficiency separation of solid-phase materials and liquid-phase materials, and greatly improves the biogas production efficiency;
(3) the process optimizes the biogas purification technology again, and further optimizes the structure of the device on the premise of ensuring the purification efficiency;
(4) the process of the invention is used for purifying and purifying the biogas, the whole process flow has no emission of toxic and harmful gases, and the pollution to the environment is avoided and the green and harmonious development of the society is promoted on the premise of meeting the biogas purification standard.
Drawings
FIG. 1 is a front view of a solid-liquid separation module according to the present invention;
FIG. 2 is a schematic view of a liquid fermentation tank according to the present invention;
FIG. 3 is a schematic view of the structure of a solid-state fermentation tank according to the present invention;
FIG. 4 is a schematic diagram of the construction of a gas collection assembly of the present invention;
FIG. 5 is a front view of a desulfurization drying tower in accordance with the present invention;
FIG. 6 is a left side view of a desulfurization drying tower in accordance with the present invention;
FIG. 7 is a partial view A of FIG. 5;
FIG. 8 is a schematic view of the structure of a filtration column of the present invention;
FIG. 9 is a schematic view of the construction of a primary canister according to the present invention;
FIG. 10 is a bottom view of the air intake baffle housing of FIG. 9;
FIG. 11 is a top view of the air induction and flow guide housing of FIG. 9;
FIG. 12 is a front view of a secondary canister of the present invention;
FIG. 13 is a top view of a secondary canister of the present invention;
FIG. 14 is a partial view B of FIG. 12;
fig. 15 is a schematic view of the construction of an auxiliary vacuum tank in the present invention.
In the figure, 10-solid-liquid separation component, 11-component frame, 111-supporting base, 112-supporting column, 113-top supporting ring, 114-second supporting matching ring, 115-first motor, 12-centrifugal separation tank, 121-rotating supporting ring, 122-feeding shell connecting hole, 123-second supporting ring, 13-liquid collecting tank mechanism, 131-liquid collecting tank shell, 132-liquid collecting drainage tube, 14-slag discharging mechanism, 141-slag discharging shell, 142-slag discharging plate, 143-slag discharging shell supporting ring, 144-slag discharging shell supporting column, 145-slag discharging shell supporting matching ring, 146-slag discharging shell through hole, 147-second motor, 148-slag collecting shell, 1481-slag collecting baffle, 15-feeding distributing mechanism, 151-feeding shell, 152-discharging slotting, 153-feeding interface, 154-feeding connecting pipe, 155-feeding guide plate, 20-gas production component, 21-liquid fermentation tank, 211-liquid fermentation feeding port, 212-liquid fermentation discharging port, 213-liquid fermentation discharging port, 22-solid fermentation tank, 221-solid fermentation feeding port, 222-solid fermentation discharging port, 223-solid fermentation discharging port, 30-gas collection component, 31-gas collection tank, 311-gas collection tank air inlet, 312-gas collection tank air outlet, 32-pressure control valve, 40-desulfurization drying tower, 41-desulfurization drying shell, 411-containing matching hole, 42-desulfurization drying air inlet pipe, 421-drying ventilation small hole, 43-desulfurization containing ring, 43-desulfurization gas outlet pipe, and the like, 431-small exhaust hole, 44-desulfurization drying component, 441-desulfurizer containing shell, 442-sealing cover, 45-filtering ring, 451-exhaust channel, 452-exhaust pipe, 50-filtering tower, 51-filtering tower shell, 511-filtering air inlet, 512-filtering air outlet, 60-first-stage adsorption tank, 61-first-stage adsorption shell, 611-spacing ring, 62-air inlet shell, 63-air inlet guide shell, 631-guide air inlet through hole, 632-guide air outlet through hole, 64-adsorption support ring, 641-adsorbent containing net, 65-exhaust shell, 651-adsorption exhaust port, 652-vacuum exhaust port, 70-second-stage adsorption tank, 71-second-stage adsorption tank shell, 72-air isolating guide ring, 442-sealing cover, 73-adsorption containing ring, 731-adsorption vent hole, 74-annular sealing plate, 75-annular air inlet shell, 76-exhaust ring shell, 80-auxiliary vacuum tank, 81-vacuum tank air inlet, 811-vacuum control valve and 82-vacuum tank air outlet.
Detailed Description
The invention will now be described in detail with reference to fig. 1-15, for ease of description, the orientations described below will now be defined as follows: the up, down, left, right, and front-back directions described below correspond to the up, down, left, right, and front-back directions in the projection relationship of fig. 1 itself.
Example 1:
a device and a method for efficiently preparing biogas and purifying by combining solid-liquid separation with pressure swing adsorption, as shown in fig. 1-15, comprising a solid-liquid separation component 10, a biogas production component 20 for fermenting liquid components and solid components separated by the solid-liquid separation component 10 to produce biogas, a biogas collection component 30 for intensively storing biogas produced by the biogas production component 20, a desulfurization drying tower 40 for desulfurizing and drying biogas stored in the biogas collection component 30, a filter tower 50 for filtering biogas treated by the desulfurization drying tower 40, a primary adsorption tank 60 and a secondary adsorption tank 70 for adsorbing and purifying biogas, and an auxiliary vacuum tank 80 for regenerating purification adsorbents in the primary adsorption tank 60 and the secondary adsorption tank 70;
as shown in fig. 1, the solid-liquid separation module 10 includes a module frame 11, a centrifugal separation tank 12, a liquid collection tank mechanism 13, a slag discharge mechanism 14, and a feed distribution mechanism 15;
as shown in fig. 1, the component rack 11 includes a supporting base 111, a plurality of supporting columns 112 extending upward are fixedly disposed at the top edge of the supporting base 111, and a top supporting ring 113 is fixedly connected to the tops of the supporting columns 112;
as shown in fig. 1, the centrifugal separation tank 12 is a truncated cone-shaped shell structure with an open bottom end, the side surface of the centrifugal separation tank 12 is provided with a plurality of centrifugal separation holes 120 communicated with the inside of the centrifugal separation tank 12, the top of the centrifugal separation tank 12 is fixedly provided with a rotary support ring 121, the rotary support ring 121 is rotatably matched with the inner side of the top support ring 113, the top of the centrifugal separation tank 12 is provided with a feeding shell connecting hole 122, and the taper range of the centrifugal separation tank 12 is 0.08-0.16;
as shown in fig. 1, a first motor 115 for driving the centrifugal separation tank 12 to rotate is fixedly connected to the upper end of the top support ring 113, and the first motor 115 drives the rotation support ring 121 to rotate through a transmission component;
as shown in fig. 1, a second support ring 123 is fixedly arranged at a position close to the lower end outside the centrifugal separation tank 12, a second support fitting ring 114 is fixedly connected to the inner sides of the plurality of support columns 112, and the second support ring 123 is connected with the second support fitting ring 114 in a rotating fitting manner;
as shown in fig. 1, the liquid collecting tank mechanism 13 includes a liquid collecting tank housing 131 surrounding the side of the centrifugal separation tank 12, the liquid collecting tank housing 131 is communicated with the inside of the centrifugal separation tank 12 through the centrifugal separation holes 120, an annular liquid collecting drainage tube 132 is fixedly arranged at a position near the lower end outside the liquid collecting tank housing 131, the liquid collecting drainage tube 132 is communicated with the inside of the liquid collecting tank housing 131, and the liquid collecting tank housing 131 is fixedly connected with the plurality of support pillars 112 through a fixing ring;
the slag discharging mechanism 14 comprises a slag discharging shell 141 rotatably connected inside the centrifugal separation tank 12, the slag discharging shell 141 is a circular truncated cone shaped shell structure, a spirally extending slag discharging plate 142 is fixedly arranged on the outer side surface of the slag discharging shell 141, and a slag discharging shell supporting ring 143 is fixedly arranged inside the slag discharging shell 141;
as shown in fig. 1, a second slag discharging shell supporting plate 140 which is horizontally arranged is fixedly arranged inside the centrifugal separation tank 12, a slag discharging shell supporting column 144 which extends downwards is fixedly arranged at the lower end of the slag discharging shell supporting plate 140, a slag discharging shell supporting matching ring 145 is fixedly arranged on the position, close to the lower end, of the slag discharging shell supporting column 144, a slag discharging shell through hole 146 is formed in the top of the slag discharging shell 141, the slag discharging shell supporting column 144 penetrates into the slag discharging shell through hole 146, and the slag discharging shell supporting ring 143 is connected to the slag discharging shell supporting matching ring 145 in a rotating matching manner;
the lower end of the slag discharge shell supporting column 144 is fixedly provided with a second motor 147 for driving the slag discharge shell 141 to rotate, and the second motor 147 drives the slag discharge shell supporting ring 143 to rotate through a transmission component;
a slag collecting shell 148 is arranged at the lower end of the centrifugal separation tank 12, the slag collecting shell 148 is an annular hollow shell with a wide upper end and a narrow lower end, the upper end and the lower end of the slag collecting shell 148 are both provided with openings, and the size of the upper end of the slag collecting shell 148 is consistent with that of the lower end of the centrifugal separation tank 12;
an annular slag collecting baffle 1481 is fixedly arranged at the edge of the upper end of the slag collecting shell 148, and the slag collecting baffle 1481 surrounds the outer side of the edge of the lower end of the centrifugal separation tank 12.
The lower end of the feeding distribution mechanism 15 is communicated with a gap between the inner side wall of the centrifugal separation tank 12 and the outer side wall of the slag discharge shell 141;
as shown in fig. 1, the feeding distribution mechanism 15 includes a feeding housing 151 with a downward flared hollow opening, the feeding housing 151 is fixedly connected to the feeding housing connection hole 122, the feeding housing 151 extends downward and turns outwards, a horizontal outward discharge slot 152 is formed outside the feeding housing 151 near the lower end, a spirally extending feeding guide plate 155 is formed inside the feeding housing 151, a feeding port 153 is fixedly formed at the top of the feeding housing 151, a feeding connection pipe 154 is connected to the feeding port 153 in a rotating fit manner, and the feeding connection pipe 154 is connected to the discharge port of the feeding conveyor in a communicating manner through a pipeline;
the circumferential rotation angle of the feeding guide plate 155 extending from top to bottom is greater than 90 ° and not more than 180 °.
As shown in fig. 2 and 3, the gas production assembly 20 comprises a liquid fermentation tank 21 and a solid fermentation tank 22, as shown in fig. 2, the liquid fermentation tank 21 is provided with a liquid fermentation inlet 211, a liquid fermentation outlet 212 and a liquid fermentation outlet 213 which are communicated with the inside thereof, as shown in fig. 3, the solid fermentation tank 22 is provided with a solid fermentation inlet 221, a solid fermentation outlet 222 and a solid fermentation outlet 223 which are communicated with the inside thereof;
as shown in fig. 4, the gas collecting assembly 30 includes a gas collecting tank 31, the gas collecting tank 31 has a gas collecting tank inlet 311 and a gas collecting tank outlet 312 communicated with the inside thereof, and the gas collecting tank outlet 312 is communicated with a pressure control valve 32.
As shown in fig. 5, the desulfurization drying tower 40 includes a desulfurization drying casing 41, the desulfurization drying casing 41 is a flat cylindrical casing, a plurality of desulfurization drying air inlet pipes 42 communicated with the inside of the desulfurization drying casing 41 are fixedly arranged on one side end surface of the desulfurization drying casing 41, an accommodating matching hole 411 is arranged on the other side end surface of the desulfurization drying casing 41, a desulfurization accommodating ring 43 is fixedly arranged in the accommodating matching hole 411, and a desulfurization drying assembly 44 is arranged in the desulfurization accommodating ring 43;
as shown in fig. 5, the desulfurization drying air inlet pipe 42 extends into the desulfurization drying shell 41, and as shown in fig. 7, a part of the desulfurization drying air inlet pipe 42, which is located inside the desulfurization drying shell 41, is provided with a plurality of drying ventilation holes 421;
the desulfurization drying assembly 44 comprises an annular hollow desulfurizing agent containing shell 441, the desulfurizing agent containing shell 441 is made of an air-permeable metal mesh, the inside of the desulfurizing agent containing shell 441 is filled with a desulfurizing agent, the desulfurizing agent containing shell 441 surrounds the outer side of the desulfurization drying air inlet pipe 42, a sealing cover 442 is fixedly arranged at the outer end of the desulfurizing agent containing shell 441, and as shown in fig. 7, the side surface of the desulfurization containing ring 43 is provided with a plurality of small exhaust holes 431;
as shown in fig. 6, a filtering ring 45 is provided in the vicinity of the edge of the desulfurization drying casing 41, the filtering ring 45 is a hollow mesh structure, the filtering ring 45 is filled with a drying adsorbent, as shown in fig. 5, an exhaust channel 451 is formed between the filtering ring 45 and the inner side wall of the desulfurization drying casing 41, and a plurality of exhaust pipes 452 communicated with the exhaust channel 451 are fixedly provided on the arc-shaped outer side wall of the desulfurization drying casing 41.
As shown in fig. 8, the filter tower 50 includes a filter tower shell 51, the filter tower shell 51 is fixedly provided with a filter air inlet 511 and a filter air outlet 512 which are communicated with the interior of the filter tower shell 51, and the interior of the filter tower shell 51 is provided with a filter core;
as shown in fig. 9, the primary adsorption tank 60 includes a columnar primary adsorption shell 61 penetrating up and down, the lower end of the primary adsorption shell 61 is fixedly provided with an air inlet shell 62, the air inlet shell 62 is a horn-shaped shell with an upward opening, the top of the first-stage adsorption shell 61 is fixedly provided with an exhaust shell 65 with a downward opening, the top of the exhaust shell 65 is provided with an adsorption exhaust port 651 and a vacuum pumping port 652 which are communicated with the inside of the exhaust shell 65, an air inlet guide shell 63 is fixedly arranged in the air inlet shell 62, as shown in fig. 10, the lower end of the air intake flow guiding housing 63 has a plurality of hexagonal flow guiding air intake through holes 631 densely paved, as shown in fig. 11, the top of the air inlet flow guiding housing 63 has a plurality of hexagonal densely-paved flow guiding air outlet through holes 632, the number of the flow guide air inlet through holes 631 is the same as that of the flow guide air outlet through holes 632, and the flow guide air inlet through holes 631 are in one-to-one smooth transition communication with the flow guide air outlet through holes 632;
as shown in fig. 9, a limiting ring 611 is fixedly disposed on the inner wall of the primary adsorption casing 61 near the lower end, a plurality of adsorption support rings 64 are stacked on the top of the limiting ring 611, an adsorbent containing net 641 is fixedly disposed on the inner side of the adsorption support rings 64, the adsorbent containing net 641 is made of a permeable metal net, and the purification adsorbent is filled in the adsorbent containing net 641.
As shown in fig. 12, the secondary adsorption tank 70 includes a secondary adsorption tank shell 71 with an upward opening, the secondary adsorption tank shell 71 has a plurality of circles of air-blocking guide rings 72 therein, adjacent air-blocking guide rings 72 are communicated with each other near the lower end or near the upper end, and the communication modes at different positions are arranged at intervals;
an annular sealing plate 74 is arranged at the top between the adjacent gas-isolating guide rings 72, a hollow adsorption containing ring 73 is arranged between the adjacent gas-isolating guide rings 72, the adsorption containing ring 73 is filled with a purification adsorbent, the top of the adsorption containing ring 73 is spaced from the annular sealing plate 74, the bottom of the adsorption containing ring 73 is spaced from the inner bottom of the second-stage adsorption tank shell 71, as shown in fig. 14, the upper and lower end faces of the adsorption containing ring 73 are provided with a plurality of adsorption ventilation holes 731 communicated with the interior of the adsorption containing ring, and the top of each adsorption containing ring 73 is fixedly connected with the annular sealing plate 74 corresponding to the top of the adsorption containing ring 73;
as shown in fig. 13, an annular air inlet casing 75 is fixedly arranged at a position close to the lower end outside the secondary adsorption tank shell 71, the annular air inlet casing 75 is communicated with a space below the outermost adsorption containing ring 73, an exhaust annular casing 76 is fixedly arranged on the inner side wall of the innermost adsorption containing ring 73, and the exhaust annular casing 76 is communicated with a space below the innermost adsorption containing ring 73;
as shown in fig. 15, a vacuum tank air inlet 81 and a vacuum tank air outlet 82 which are communicated with the inside of the auxiliary vacuum tank 80 are fixedly arranged on the auxiliary vacuum tank, and the vacuum tank air outlet 82 is communicated with an air inlet of a vacuum air extractor; and a vacuum control valve 811 is connected to the vacuum tank air inlet 81.
Example 2:
the difference from embodiment 1 is that the taper of the centrifugal separation tank 12 is 0.12, and the circumferential rotation angle of the feed guide plate 155 extending from top to bottom is 130 °.
Example 3:
the difference from embodiment 1 is that the taper range of the centrifugal separation tank 12 is 0.16, and the circumferential rotation angle of the feed guide plate 155 extending from top to bottom is 180 °.
Example 4:
the method for preparing and purifying the biogas by utilizing the device for preparing and purifying the biogas efficiently by combining solid-liquid separation with pressure swing adsorption in the embodiment 1 comprises the following steps:
s1: firstly, the solid-liquid separation component 10 is used for carrying out solid-liquid separation on the solid-liquid mixed livestock manure, the separated liquid is discharged from the liquid collection drainage tube 132, and the separated solid is discharged from the slag collection shell 148;
s2: fermenting the solid separated in the step S1 to generate gas by using the solid fermentation tank 22 of the gas generation component 20, and fermenting the separated liquid to generate gas by using the liquid fermentation tank 21 of the gas generation component 20;
s3: introducing the raw gas produced by fermentation of the liquid fermentation tank 21 and the solid fermentation tank 22 into the gas collection tank 31 for temporary storage;
s4: introducing the biogas temporarily stored in the gas collecting tank 31 into the desulfurization drying tower 40, and removing sulfides and moisture in the biogas by using a desulfurizer and a drying agent in the desulfurization drying tower 40 to ensure that the water content of the desulfurized biogas is 2mg/kg, thereby obtaining dry biogas;
s5: introducing the dried biogas obtained after the treatment in the step S4 into a filter tower 50, and removing insoluble impurities in the dried biogas; adjusting the gas outlet pressure of the filter tower to 0.5Mpa to obtain compressed methane;
s6: pressure swing adsorption; intermittently introducing the compressed methane processed in the step S5 into the primary adsorption tank 60, and adsorbing impurity gases in the compressed methane by using a purification adsorbent in the primary adsorption tank 60 to obtain primary purified methane;
wherein the flow of the compressed methane is controlled to be 1m3H, the air inlet intermittent time is 3min, the air inlet temperature is 50-150 ℃, and the pressure of the primary purified methane is adjusted to 1.0 Mpa;
then intermittently introducing the gas into a secondary adsorption tank 70, and compressing CO in the biogas by using the gravity of the purification adsorbent in the secondary adsorption tank 702Adsorbing to obtain purified methane;
wherein the primary purified biogas is controlled to be 2m3The air inlet intermittent time is 1min, and the air inlet temperature is 150 ℃;
s7: desorbing and regenerating, namely stopping introducing compressed methane into the primary adsorption tank 60 when the purification adsorbent in the primary adsorption tank 60 is saturated, and vacuumizing the primary adsorption tank 60 and the secondary adsorption tank 70 to desorb impurity gas on the purification adsorbent so as to realize regeneration of the purification adsorbent;
s8: and storing the purified methane in a centralized manner.
The desulfurizer is prepared from 15 parts by weight of organic amine desulfurizer, 8 parts by weight of sulfoxide, 1 part by weight of polyethylene glycol, 5 parts by weight of propylene carbonate and 20 parts by weight of deionized water;
the preparation method of the desulfurizer comprises the following steps: mixing and reacting an organic amine desulfurizer with sulfoxide and polyethylene glycol, controlling the pH value of the reaction to be 6 to generate a colloidal precipitate, oxidizing the colloidal precipitate with oxygen-enriched gas, and then filtering and separating; washing the filtered precipitate with water for 2 times; then, extruding and forming the material which is uniformly mixed with propylene carbonate and deionized water on a forming machine, and naturally drying to obtain the desulfurizer;
the drying agent is a composite drying agent which is formed by compounding 16 parts of magnesium sulfate, 12 parts of sodium carbonate, 10 parts of calcium chloride, 8 parts of calcium carbonate, 7 parts of calcium hydride and 10 parts of deionized water in parts by weight;
the filter membrane in the filter tower is a polyamide fiber membrane.
The purification adsorbent is prepared from 15 parts of alumina, 5 parts of carbon molecular sieve, 8 parts of sodium sulfate, 10 parts of zeolite and 18 parts of deionized water in parts by weight;
the preparation method of the purification adsorbent comprises the following steps:
1) adding deionized water into a hydrothermal kettle, then adding alumina and a carbon molecular sieve into the hydrothermal kettle, and uniformly stirring;
2) preparing sodium sulfate into a salt solution with the mass concentration of 30%, and adding the salt solution into a hydrothermal kettle;
3) and finally, adding zeolite into a hydrothermal kettle for reaction, controlling the temperature of the hydrothermal kettle to be 90 ℃, reacting for 20min, and cooling the reaction material after the reaction is finished to obtain the purified adsorbent.
Example 5:
the method for preparing and purifying the biogas by utilizing the device for preparing and purifying the biogas efficiently by combining solid-liquid separation with pressure swing adsorption in the embodiment 1 comprises the following steps:
s1: firstly, the solid-liquid separation component 10 is used for carrying out solid-liquid separation on the solid-liquid mixed livestock manure, the separated liquid is discharged from the liquid collection drainage tube 132, and the separated solid is discharged from the slag collection shell 148;
s2: fermenting the solid separated in the step S1 to generate gas by using the solid fermentation tank 22 of the gas generation component 20, and fermenting the separated liquid to generate gas by using the liquid fermentation tank 21 of the gas generation component 20;
s3: introducing the raw gas produced by fermentation of the liquid fermentation tank 21 and the solid fermentation tank 22 into the gas collection tank 31 for temporary storage;
s4: introducing the biogas temporarily stored in the gas collecting tank 31 into the desulfurization drying tower 40, and removing sulfides and moisture in the biogas by using a desulfurizer and a drying agent in the desulfurization drying tower 40 to ensure that the water content of the desulfurized biogas is 5mg/kg, thereby obtaining dry biogas;
s5: introducing the dried biogas obtained after the treatment in the step S4 into a filter tower 50, and removing insoluble impurities in the dried biogas; adjusting the gas outlet pressure of the filter tower to 0.75Mpa to obtain compressed methane;
s6: pressure swing adsorption; intermittently introducing the compressed methane processed in the step S5 into the primary adsorption tank 60, and adsorbing impurity gases in the compressed methane by using a purification adsorbent in the primary adsorption tank 60 to obtain primary purified methane;
wherein the flow of the compressed methane is controlled to be 2m3H, the air inlet intermittent time is 4min, the air inlet temperature is 100 ℃, and the pressure of the primary purified methane is adjusted to 1.25 Mpa;
then intermittently introducing the gas into a secondary adsorption tank 70, and compressing CO in the biogas by using the gravity of the purification adsorbent in the secondary adsorption tank 702Adsorbing to obtain purified methane;
wherein the primary purified biogas is controlled to be 3m3The air inlet intermittent time is 2min, and the air inlet temperature is 200 ℃;
s7: desorbing and regenerating, namely stopping introducing compressed methane into the primary adsorption tank 60 when the purification adsorbent in the primary adsorption tank 60 is saturated, and vacuumizing the primary adsorption tank 60 and the secondary adsorption tank 70 to desorb impurity gas on the purification adsorbent so as to realize regeneration of the purification adsorbent;
s8: and storing the purified methane in a centralized manner.
The desulfurizer is prepared from 22 parts by weight of organic amine desulfurizer, 11 parts by weight of sulfoxide, 5 parts by weight of polyethylene glycol, 10 parts by weight of propylene carbonate and 28 parts by weight of deionized water;
the preparation method of the desulfurizer comprises the following steps: mixing and reacting an organic amine desulfurizer with sulfoxide and polyethylene glycol, controlling the pH value of the reaction to be 7 to generate a colloidal precipitate, oxidizing the colloidal precipitate with oxygen-enriched gas, and then filtering and separating; washing the filtered precipitate with water for 3 times; then, extruding and forming the material which is uniformly mixed with propylene carbonate and deionized water on a forming machine, and naturally drying to obtain the desulfurizer;
the drying agent is a composite drying agent which is formed by compounding 25 parts of magnesium sulfate, 17 parts of sodium carbonate, 15 parts of calcium chloride, 15 parts of calcium carbonate, 13 parts of calcium hydride and 18 parts of deionized water in parts by weight;
the filter membrane in the filter tower is a polyimide hollow fiber membrane.
The purification adsorbent is prepared from 20 parts of alumina, 11 parts of carbon molecular sieve, 12 parts of sodium sulfate, 16 parts of zeolite and 24 parts of deionized water in parts by weight;
the preparation method of the purification adsorbent comprises the following steps:
1) adding deionized water into a hydrothermal kettle, then adding alumina and a carbon molecular sieve into the hydrothermal kettle, and uniformly stirring;
2) preparing sodium sulfate into a salt solution with the mass concentration of 40%, and adding the salt solution into a hydrothermal kettle;
3) and finally, adding zeolite into a hydrothermal kettle for reaction, controlling the temperature of the hydrothermal kettle to be 110 ℃, controlling the reaction time to be within 35min, and cooling the reaction material after the reaction is finished to obtain the purification adsorbent.
Example 6:
the method for preparing and purifying the biogas by utilizing the device for preparing and purifying the biogas efficiently by combining solid-liquid separation with pressure swing adsorption in the embodiment 1 comprises the following steps:
s1: firstly, the solid-liquid separation component 10 is used for carrying out solid-liquid separation on the solid-liquid mixed livestock manure, the separated liquid is discharged from the liquid collection drainage tube 132, and the separated solid is discharged from the slag collection shell 148;
s2: fermenting the solid separated in the step S1 to generate gas by using the solid fermentation tank 22 of the gas generation component 20, and fermenting the separated liquid to generate gas by using the liquid fermentation tank 21 of the gas generation component 20;
s3: introducing the raw gas produced by fermentation of the liquid fermentation tank 21 and the solid fermentation tank 22 into the gas collection tank 31 for temporary storage;
s4: introducing the biogas temporarily stored in the gas collecting tank 31 into the desulfurization drying tower 40, and removing sulfides and moisture in the biogas by using a desulfurizer and a drying agent in the desulfurization drying tower 40 to ensure that the water content of the desulfurized biogas is 9mg/kg, thereby obtaining dry biogas;
s5: introducing the dried biogas obtained after the treatment in the step S4 into a filter tower 50, and removing insoluble impurities in the dried biogas; adjusting the gas outlet pressure of the filter tower to 1.0Mpa to obtain compressed methane;
s6: pressure swing adsorption; intermittently introducing the compressed methane processed in the step S5 into the primary adsorption tank 60, and adsorbing impurity gases in the compressed methane by using a purification adsorbent in the primary adsorption tank 60 to obtain primary purified methane;
wherein the flow of the compressed methane is controlled to be 3m3H, the air inlet intermittent time is 5min, the air inlet temperature is 150 ℃, and the pressure of the primary purified methane is adjusted to 1.5 Mpa;
then intermittently introducing the gas into a secondary adsorption tank 70, and compressing CO in the biogas by using the gravity of the purification adsorbent in the secondary adsorption tank 702Adsorbing to obtain purified methane;
wherein, the flow of the primary purified biogas is controlled to be 5m3H, air inlet intermittent time of 3min, air inlet temperatureAt 250 ℃;
s7: desorbing and regenerating, namely stopping introducing compressed methane into the primary adsorption tank 60 when the purification adsorbent in the primary adsorption tank 60 is saturated, and vacuumizing the primary adsorption tank 60 and the secondary adsorption tank 70 to desorb impurity gas on the purification adsorbent so as to realize regeneration of the purification adsorbent;
s8: and storing the purified methane in a centralized manner.
The desulfurizer is prepared from 30 parts by weight of organic amine desulfurizer, 15 parts by weight of sulfoxide, 8 parts by weight of polyethylene glycol, 16 parts by weight of propylene carbonate and 35 parts by weight of deionized water;
the preparation method of the desulfurizer comprises the following steps: mixing and reacting an organic amine desulfurizer with sulfoxide and polyethylene glycol, controlling the pH value of the reaction to be 8 to generate a colloidal precipitate, oxidizing the colloidal precipitate with oxygen-enriched gas, and then filtering and separating; washing the filtered precipitate with water for 5 times; then, extruding and forming the material which is uniformly mixed with propylene carbonate and deionized water on a forming machine, and naturally drying to obtain the desulfurizer;
the drying agent is a composite drying agent which is formed by compounding 33 parts of magnesium sulfate, 21 parts of sodium carbonate, 20 parts of calcium chloride, 23 parts of calcium carbonate, 19 parts of calcium hydride and 25 parts of deionized water in parts by weight;
the filter membrane in the filter tower is a polyvinylidene fluoride hollow fiber membrane.
The purification adsorbent is prepared from 26 parts by weight of alumina, 18 parts by weight of carbon molecular sieve, 17 parts by weight of sodium sulfate, 23 parts by weight of zeolite and 30 parts by weight of deionized water;
the preparation method of the purification adsorbent comprises the following steps:
1) adding deionized water into a hydrothermal kettle, then adding alumina and a carbon molecular sieve into the hydrothermal kettle, and uniformly stirring;
2) preparing sodium sulfate into a salt solution with the mass concentration of 45%, and adding the salt solution into a hydrothermal kettle;
3) and finally, adding zeolite into a hydrothermal kettle for reaction, controlling the temperature of the hydrothermal kettle at 130 ℃, reacting for 50min, and cooling the reaction material after the reaction is finished to obtain the purification adsorbent.
In the practical application process of the present invention, the solid-liquid mixture enters the feeding interface 153 through the feeding connecting pipe 154, and the solid-liquid mixture in the feeding interface 153 enters the centrifugal separation tank 12 through the feeding shell 151;
the first motor 115 drives the rotating support ring 121 to rotate, the rotating support ring 121 drives the centrifugal separation tank 12 to rotate, the solid-liquid mixture is discharged between the outer side wall of the slag discharge shell 141 and the inner side wall of the centrifugal separation tank 12, the solid-liquid mixture is tightly attached to the inner side wall of the centrifugal separation tank 12 under the centrifugal action, the liquid components in the solid-liquid mixture are discharged into the liquid collection tank shell 131 through the centrifugal separation holes 120 under the centrifugal action, and the liquid components separated from the interior of the liquid collection tank shell 131 are discharged through the liquid collection drainage tube 132 and collected and stored in a centralized manner;
the second motor 147 drives the slag discharge shell support ring 143 to rotate, the slag discharge shell support ring 143 drives the slag discharge shell 141 to rotate, the slag discharge plate 142 on the outer side wall of the slag discharge shell 141 scrapes the solid-liquid mixture on the inner side wall of the centrifugal separation tank 12, the solid components separated from the liquid components by the solid-liquid mixture are discharged downwards under the action of the scraping action of the slag discharge plate 142, and the solid components enter the slag collection shell 148 and are then discharged from the lower end of the slag collection shell 148 and collected and stored in a centralized manner;
the liquid components are introduced into the liquid fermentation tank 21 for fermentation and gas production, the solid components are introduced into the solid fermentation tank 22 for fermentation and gas production, and the original biogas produced by fermentation of the liquid fermentation tank 21 and the solid fermentation tank 22 is discharged into the gas collection tank 31 for unified temporary storage;
the original biogas in the gas collecting tank 31 is firstly subjected to desulfurization and drying treatment by the desulfurization and drying tower 40, the original biogas is introduced into the desulfurization and drying gas inlet pipe 42, the original biogas in the desulfurization and drying gas inlet pipe 42 is discharged through the drying gas outlet holes 421, the original biogas passes through the desulfurizer accommodating shell 441, the desulfurizer inside the desulfurizer accommodating shell 441 performs desulfurization treatment on the original biogas, the desulfurized original biogas is discharged into the desulfurization and drying shell 41, the original biogas inside the desulfurization and drying shell 41 passes through the filter ring 45 and enters the exhaust channel 451, the dry adsorbent inside the filter ring 45 performs drying treatment on the original biogas, and the desulfurized and dried original biogas is discharged from the exhaust pipe 452;
filtering the raw biogas discharged from the exhaust pipe 452 by the filter tower 50 to remove insoluble impurities in the dry biogas;
the raw biogas treated by the filter tower 50 is treated by the primary adsorption tank 60, the raw biogas is introduced from the gas inlet shell 62, and uniformly flows upwards from the lower end inside the primary adsorption shell 61 under the flow guiding action of the gas inlet flow guiding shell 63, the raw biogas passes through the adsorbent accommodating net 641, the purified adsorbent filled inside the adsorbent accommodating net 641 adsorbs impurity gas in the raw biogas, and then the purified adsorbent is discharged from the adsorption gas outlet 651 on the gas discharge shell 65;
the raw methane processed by the primary adsorption tank 60 is processed by the secondary adsorption tank 70, the raw methane enters the secondary adsorption tank shell 71 through the annular air inlet shell 75 and turns back and forth to pass through the adsorption containing ring 73, and the purified adsorbent filled in the adsorption containing ring 73 is used for concentrating CO in the raw methane2Adsorption removal is carried out, and finally, purified methane is discharged from the exhaust ring shell 76 and stored in a concentrated manner;
when the purified adsorbent filled in the adsorbent accommodating net 641 in the primary adsorption tank 60 reaches adsorption saturation, stopping using the primary adsorption tank 60 to treat biogas, extracting air in the auxiliary vacuum tank 80 by using a vacuum air extractor in advance to make the interior of the auxiliary vacuum tank be in a vacuum state, connecting the vacuum extraction port 652 with the vacuum tank air inlet 81, quickly opening the vacuum control valve 811 to make the primary adsorption shell 61 and the interior of the auxiliary vacuum tank 80 be communicated, and quickly reducing the internal pressure of the primary adsorption shell 61 under the action of pressure difference to desorb impurity gas adsorbed on the purified adsorbent filled in the adsorbent accommodating net 641 so as to realize regeneration of the purified adsorbent;
when the purification adsorbent filled in the adsorption containing ring 73 in the second-stage adsorption tank 70 is saturated, the second-stage adsorption tank 70 is stopped to treat the biogas, compressed air is introduced into the annular air inlet shell 75, and the purification adsorbent filled in the adsorption containing ring 73 is desorbed by using clean compressed air, so that the regeneration of the purification adsorbent is realized.
Claims (10)
1. A device for efficiently preparing biogas and purifying by combining solid-liquid separation with pressure swing adsorption, which is characterized in that, the methane purifying device comprises a solid-liquid separation component (10), a methane production component (20) for fermenting liquid components and solid components separated by the solid-liquid separation component (10) to produce methane, a gas collection component (30) for storing methane produced by the methane production component (20) in a centralized manner, a desulfurization drying tower (40) for desulfurizing and drying methane stored in the gas collection component (30), a filtering tower (50) for filtering methane treated by the desulfurization drying tower (40), a primary adsorption tank (60) and a secondary adsorption tank (70) for adsorbing and purifying methane, and an auxiliary vacuum tank (80) for regenerating purification adsorbents in the primary adsorption tank (60) and the secondary adsorption tank (70);
the solid-liquid separation assembly (10) comprises an assembly frame (11), a centrifugal separation tank (12), a liquid collection tank mechanism (13), a slag discharge mechanism (14) and a feeding distribution mechanism (15);
the assembly rack (11) comprises a support base (111), a plurality of support columns (112) extending upwards are fixedly arranged at the edge of the top of the support base (111), and top support rings (113) are fixedly connected to the tops of the support columns (112);
the centrifugal separation tank (12) is of a circular truncated cone-shaped shell structure with an opening at the bottom end, the side surface of the centrifugal separation tank (12) is provided with a plurality of centrifugal separation holes (120) communicated with the inside of the centrifugal separation tank, the top of the centrifugal separation tank (12) is fixedly provided with a rotary support ring (121), the rotary support ring (121) is rotatably matched with the inner side of the top support ring (113), and the top of the centrifugal separation tank (12) is provided with a feeding shell connecting hole (122);
the upper end of the top supporting ring (113) is fixedly connected with a first motor (115) for driving the centrifugal separation tank (12) to rotate, and the first motor (115) drives the rotating supporting ring (121) to rotate through a transmission part;
a second support ring (123) is fixedly arranged at a position, close to the lower end, on the outer side of the centrifugal separation tank (12), a second support matching ring (114) is fixedly connected to the inner sides of the support columns (112), and the second support ring (123) is fixedly connected with the second support matching ring (114);
the liquid collection tank mechanism (13) comprises a liquid collection tank shell (131) surrounding the side face of the centrifugal separation tank (12), the liquid collection tank shell (131) is communicated with the inside of the centrifugal separation tank (12) through the centrifugal separation hole (120), an annular liquid collection drainage tube (132) is fixedly arranged at the position, close to the lower end, of the outer side of the liquid collection tank shell (131), the liquid collection drainage tube (132) is communicated with the inside of the liquid collection tank shell (131), and the liquid collection tank shell (131) is fixedly connected with the support columns (112) through fixing rings;
the slag discharging mechanism (14) comprises a slag discharging shell (141) which is rotatably connected inside the centrifugal separation tank (12), the slag discharging shell (141) is of a circular truncated cone-shaped shell structure, a spirally extending slag discharging plate (142) is fixedly arranged on the outer side surface of the slag discharging shell (141), and a slag discharging shell supporting ring (143) is fixedly arranged inside the slag discharging shell (141);
a second slag discharging shell supporting plate (140) which is horizontally arranged is fixedly arranged inside the centrifugal separation tank (12), a slag discharging shell supporting column (144) which extends downwards is fixedly arranged at the lower end of the slag discharging shell supporting plate (140), a slag discharging shell supporting matching ring (145) is fixedly arranged on the position, close to the lower end, of the slag discharging shell supporting column (144), a slag discharging shell through hole (146) is formed in the top of the slag discharging shell (141), the slag discharging shell supporting column (144) penetrates into the slag discharging shell through hole (146), and the slag discharging shell supporting ring (143) is connected to the slag discharging shell supporting matching ring (145) in a rotating matching manner;
the lower end of the slag discharge shell supporting column (144) is fixedly provided with a second motor (147) for driving the slag discharge shell (141) to rotate, and the second motor (147) drives the slag discharge shell supporting ring (143) to rotate through a transmission part;
a slag collecting shell (148) is arranged at the lower end of the centrifugal separation tank (12), the slag collecting shell (148) is an annular hollow shell with a wide upper end and a narrow lower end, the upper end and the lower end of the slag collecting shell (148) are both provided with openings, and the size of the upper end of the slag collecting shell (148) is consistent with that of the lower end of the centrifugal separation tank (12);
the lower end of the feeding distribution mechanism (15) is communicated with a gap between the inner side wall of the centrifugal separation tank (12) and the outer side wall of the slag discharge shell (141).
2. The device for high-efficiency biogas production and purification by combining solid-liquid separation with pressure swing adsorption according to claim 1, characterized in that: the purification adsorbent is prepared from 15-26 parts by weight of alumina, 5-18 parts by weight of carbon molecular sieve, 8-17 parts by weight of sodium sulfate, 10-23 parts by weight of zeolite and 18-30 parts by weight of deionized water;
the preparation method of the purification adsorbent comprises the following steps:
1) adding deionized water into a hydrothermal kettle, then adding alumina and a carbon molecular sieve into the hydrothermal kettle, and uniformly stirring;
2) preparing sodium sulfate into a salt solution with the mass concentration of 30-45%, and adding the salt solution into a hydrothermal kettle;
3) and finally, adding zeolite into a hydrothermal kettle for reaction, controlling the temperature of the hydrothermal kettle to be 90-130 ℃, reacting for 20-50 min, and cooling the reaction material after the reaction is finished to obtain the purified adsorbent.
3. The device for high-efficiency biogas production and purification by combining solid-liquid separation with pressure swing adsorption according to claim 1, characterized in that: an annular slag collecting baffle plate (1481) is fixedly arranged at the edge of the upper end of the slag collecting shell (148), and the slag collecting baffle plate (1481) surrounds the outer side of the edge of the lower end of the centrifugal separation tank (12).
4. The device for high-efficiency biogas production and purification by combining solid-liquid separation with pressure swing adsorption according to claim 1, characterized in that: the feeding distribution mechanism (15) comprises a feeding shell (151) with a downward flared hollow opening, the feeding shell (151) is fixedly connected in a feeding shell connecting hole (122), the feeding shell (151) is turned outwards and extends downwards, a horizontal outward discharging groove (152) is formed in the position, close to the lower end, of the outer side of the feeding shell (151), a spirally extending feeding guide plate (155) is arranged in the hollow interior of the feeding shell (151), a feeding interface (153) is fixedly arranged at the top of the feeding shell (151), a feeding connecting pipe (154) is connected with the feeding interface (153) in a rotating fit mode, and the feeding connecting pipe (154) is communicated and connected with a discharging hole of a feeding conveyor through a pipeline;
the circumferential rotating angle of the feeding guide plate (155) extending from top to bottom is larger than 90 degrees and not more than 180 degrees.
5. The device for high-efficiency biogas production and purification by combining solid-liquid separation with pressure swing adsorption according to claim 1, characterized in that: the gas production assembly (20) comprises a liquid fermentation tank (21) and a solid fermentation tank (22), wherein the liquid fermentation tank (21) is provided with a liquid fermentation feeding hole (211), a liquid fermentation discharging hole (212) and a liquid fermentation exhaust hole (213) which are communicated with the inside of the liquid fermentation tank, and the solid fermentation tank (22) is provided with a solid fermentation feeding hole (221), a solid fermentation discharging hole (222) and a solid fermentation exhaust hole (223) which are communicated with the inside of the solid fermentation tank;
the gas collection assembly (30) comprises a gas collection tank (31), a gas collection tank gas inlet (311) and a gas collection tank gas outlet (312) which are communicated with the inside of the gas collection tank (31) are arranged on the gas collection tank (31), and a pressure control valve (32) is communicated with the gas collection tank gas outlet (312).
6. The device for high-efficiency biogas production and purification by combining solid-liquid separation with pressure swing adsorption according to claim 1, characterized in that: the desulfurization drying tower (40) comprises a desulfurization drying shell (41), the desulfurization drying shell (41) is a flat cylindrical shell, a plurality of desulfurization drying air inlet pipes (42) communicated with the interior of the desulfurization drying shell (41) are fixedly arranged on one side end face of the desulfurization drying shell (41), an accommodating matching hole (411) is formed in the other side end face of the desulfurization drying shell (41), a desulfurization accommodating ring (43) is fixedly arranged in the accommodating matching hole (411), and a desulfurization drying assembly (44) is arranged in the desulfurization accommodating ring (43);
the desulfurization drying air inlet pipe (42) extends into the desulfurization drying shell (41), and the part of the desulfurization drying air inlet pipe (42) positioned in the desulfurization drying shell (41) is provided with a plurality of drying small ventilation holes (421);
the desulfurization drying assembly (44) comprises an annular hollow desulfurizing agent containing shell (441), the desulfurizing agent containing shell (441) is made of a breathable metal net, a desulfurizing agent is filled in the desulfurizing agent containing shell (441), the desulfurizing agent containing shell (441) surrounds the outer side of the desulfurization drying air inlet pipe (42), a sealing cover (442) is fixedly arranged at the outer end of the desulfurizing agent containing shell (441), and the side surface of the desulfurization containing ring (43) is provided with a plurality of small exhaust holes (431);
desulfurization drying casing (41) are close to and have filter ring (45) in the edge, filter ring (45) are hollow network structure, it is filled with dry adsorbent to filter ring (45) intussuseption, filter ring (45) with form exhaust passage (451) between desulfurization drying casing (41) inside wall, desulfurization drying casing (41) arc lateral wall go up fixed be equipped with a plurality of with blast pipe (452) that exhaust passage (451) is linked together.
7. The device for high-efficiency biogas production and purification by combining solid-liquid separation with pressure swing adsorption according to claim 2, characterized in that: the filter tower (50) comprises a filter tower shell (51), a filter air inlet (511) and a filter air outlet (512) which are communicated with the interior of the filter tower shell (51) are fixedly arranged on the filter tower shell (51), and a filter core body is arranged in the filter tower shell (51);
the one-level adsorption tank (60) includes that the column link up from top to bottom adsorbs casing (61), the one-level adsorbs casing (61) lower extreme is fixed to be equipped with and admits air casing (62), it is the loudspeaker form casing that the opening faces upward to admit air casing (62), the fixed exhaust casing (65) that is equipped with the opening down in one-level adsorption casing (61) top, exhaust casing (65) top has absorption gas vent (651) and vacuum extraction mouth (652) rather than inside being linked together, it admits air casing (62) internal fixation is equipped with into air water conservancy diversion casing (63), it has the closely water conservancy diversion air inlet through hole (631) that spreads of a plurality of hexagons to admit air water conservancy diversion casing (63) lower extreme, it has the closely water conservancy diversion air outlet through hole (632) that spread of a plurality of hexagons to admit air water conservancy diversion air inlet through hole (631) top, water conservancy diversion air inlet through hole (631) with the quantity of water conservancy diversion air outlet through hole (632) is the same, the flow guide air inlet through hole (631) is communicated with the flow guide air outlet through hole (632) in a one-to-one smooth transition way;
the one-level adsorption shell (61) inner wall is close to the fixed spacing ring (611) that is equipped with of lower extreme, spacing ring (611) top is piled up and is equipped with a plurality of absorption support rings (64), absorption support ring (64) inboard is fixed and is equipped with adsorbent and holds net (641), adsorbent holds net (641) and is made by ventilative metal mesh, adsorbent holds the inside packing of net (641) and has the purification adsorbent.
8. The device for high-efficiency biogas production and purification by combining solid-liquid separation with pressure swing adsorption according to claim 2, characterized in that: the secondary adsorption tank (70) comprises a secondary adsorption tank shell (71) with an upward opening, a plurality of circles of air-isolating guide rings (72) are arranged in the secondary adsorption tank shell (71), the adjacent air-isolating guide rings (72) are communicated with each other near the lower end or near the upper end, and the communication modes at different positions are arranged at intervals;
an annular sealing plate (74) is arranged at the top between the adjacent gas-isolating guide rings (72), a hollow adsorption containing ring (73) is arranged between the adjacent gas-isolating guide rings (72), a purification adsorbent is filled in the adsorption containing ring (73), a certain distance is formed between the top of the adsorption containing ring (73) and the annular sealing plate (74), a certain distance is formed between the bottom of the adsorption containing ring (73) and the inner bottom of the second-stage adsorption tank shell (71), a plurality of adsorption vent holes (731) communicated with the interior of the adsorption containing ring (73) are formed in the upper end surface and the lower end surface of the adsorption containing ring (73), and the top of each adsorption containing ring (73) is fixedly connected with the corresponding annular sealing plate (74) above the adsorption containing ring (73);
an annular air inlet shell (75) is fixedly arranged at a position, close to the lower end, on the outer side of the secondary adsorption tank shell (71), the annular air inlet shell (75) is communicated with a space below the adsorption containing ring (73) on the outermost side, an exhaust ring shell (76) is fixedly arranged on the inner side wall of the adsorption containing ring (73) on the innermost side, and the exhaust ring shell (76) is communicated with a space below the adsorption containing ring (73) on the innermost side;
a vacuum tank air inlet (81) and a vacuum tank exhaust port (82) which are communicated with the inside of the auxiliary vacuum tank (80) are fixedly arranged on the auxiliary vacuum tank, and the auxiliary vacuum tank is communicated and connected with the vacuum tank exhaust port (82) and an air inlet of a vacuum air extractor; and a vacuum control valve (811) is connected to the vacuum tank air inlet (81).
9. The method for purifying the biogas by utilizing the device for efficiently preparing the biogas by combining solid-liquid separation with pressure swing adsorption according to any one of claims 1 to 8, is characterized by comprising the following steps:
s1: firstly, a solid-liquid separation component (10) is utilized to carry out solid-liquid separation on the solid-liquid mixed livestock manure, the separated liquid is discharged from the liquid collection drainage tube (132), and the separated solid is discharged from the slag collection shell (148);
s2: fermenting the solid separated in the step S1 by using a solid fermentation tank (22) of the gas production assembly (20) to produce gas, and fermenting the separated liquid by using a liquid fermentation tank (21) of the gas production assembly (20) to produce gas;
s3: introducing the raw gas produced by fermentation of the liquid fermentation tank (21) and the solid fermentation tank (22) into the gas collection tank (31) for temporary storage;
s4: introducing the biogas temporarily stored in the gas collection tank (31) into the desulfurization drying tower (40), and removing sulfides and water in the biogas by using a desulfurizer and a drying agent in the desulfurization drying tower (40) to ensure that the water content of the desulfurized biogas is in a range of 2-9 mg/kg, thereby obtaining dry biogas;
s5: introducing the dried biogas obtained after the treatment in the step S4 into a filter tower (50) to remove insoluble impurities in the dried biogas; adjusting the gas outlet pressure of the filter tower to be between 0.5 and 1.0Mpa to obtain compressed methane;
s6: pressure swing adsorption; intermittently introducing the compressed methane processed in the step S5 into a primary adsorption tank (60), and adsorbing impurity gases in the compressed methane by using a purification adsorbent in the primary adsorption tank (60) to obtain primary purified methane;
wherein the flow range of the compressed methane is controlled to be 1-3 m3The intermittent air intake time is 3-5 min, the air intake temperature is 50-150 ℃, and the pressure of the primary purified methane is adjusted to 1.0-1.5 Mpa;
then intermittently introducing the gas into a secondary adsorption tank (70), and utilizing the gravity of the purification adsorbent in the secondary adsorption tank (70) to compress CO in the biogas2Adsorbing to obtain purified methane;
wherein the flow of the primary purified biogas is controlled to be 2-5 m3The air inlet intermittent time ranges from 1min to 3min, and the air inlet temperature ranges from 150 ℃ to 250 ℃;
s7: desorbing and regenerating, namely stopping introducing compressed methane into the primary adsorption tank (60) when the purification adsorbent in the primary adsorption tank (60) is saturated, and vacuumizing the primary adsorption tank (60) and the secondary adsorption tank (70) to desorb impurity gas on the purification adsorbent to realize regeneration of the purification adsorbent;
s8: and storing the purified methane in a centralized manner.
10. The method for high-efficiency biogas production and purification by combining solid-liquid separation with pressure swing adsorption according to claim 9, characterized in that: the desulfurizer is prepared from 15-30 parts by weight of organic amine desulfurizer, 8-15 parts by weight of sulfoxide, 1-8 parts by weight of polyethylene glycol, 5-16 parts by weight of propylene carbonate and 20-35 parts by weight of deionized water;
the preparation method of the desulfurizer comprises the following steps: mixing and reacting an organic amine desulfurizer with sulfoxide and polyethylene glycol, controlling the pH value of the reaction to be 6-8 to generate a colloidal precipitate, oxidizing the colloidal precipitate with oxygen-enriched gas, and then filtering and separating; washing the filtered precipitate with water for 2-5 times; then, extruding and forming the material which is uniformly mixed with propylene carbonate and deionized water on a forming machine, and naturally drying to obtain the desulfurizer;
the drying agent is a composite drying agent which is prepared by compounding 16-33 parts of magnesium sulfate, 12-21 parts of sodium carbonate, 10-20 parts of calcium chloride, 8-23 parts of calcium carbonate, 7-19 parts of calcium hydride and 10-25 parts of deionized water in parts by weight;
the filter membrane in the filter tower is one of a polyamide fiber membrane, a polyimide hollow fiber membrane and a polyvinylidene fluoride hollow fiber membrane.
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