CN109833645B - Oil cake extraction system - Google Patents
Oil cake extraction system Download PDFInfo
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- CN109833645B CN109833645B CN201910264769.7A CN201910264769A CN109833645B CN 109833645 B CN109833645 B CN 109833645B CN 201910264769 A CN201910264769 A CN 201910264769A CN 109833645 B CN109833645 B CN 109833645B
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- 239000002904 solvent Substances 0.000 claims abstract description 64
- 238000003860 storage Methods 0.000 claims abstract description 59
- 239000000843 powder Substances 0.000 claims abstract description 44
- 238000001704 evaporation Methods 0.000 claims abstract description 39
- 230000008020 evaporation Effects 0.000 claims abstract description 39
- 238000011084 recovery Methods 0.000 claims abstract description 31
- 239000002893 slag Substances 0.000 claims abstract description 15
- 238000004064 recycling Methods 0.000 claims abstract description 14
- 239000002994 raw material Substances 0.000 claims abstract description 13
- 238000002791 soaking Methods 0.000 claims description 124
- 239000011343 solid material Substances 0.000 claims description 60
- 238000007599 discharging Methods 0.000 claims description 46
- 239000003921 oil Substances 0.000 claims description 39
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- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 claims description 13
- 239000010779 crude oil Substances 0.000 claims description 12
- 238000007789 sealing Methods 0.000 claims description 11
- 239000003638 chemical reducing agent Substances 0.000 claims description 8
- 230000005540 biological transmission Effects 0.000 claims description 6
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- Extraction Or Liquid Replacement (AREA)
Abstract
The invention relates to an oil cake extraction system, wherein the outlet of a raw material temporary storage bin is connected with the solid inlet of a leacher through a quantitative auger, the wet outlet of the leacher is connected with a vertical steam-off machine through a wet slag conveyor, the inlet of a new solvent pump is connected with a fresh solvent pipe, the outlet of the new solvent pump is connected with the new solution inlet of the leacher, the concentrated solution outlet of the leacher is connected with the inlet of a concentrated solution extraction pump, the outlet of the concentrated solution extraction pump is connected with the inlet of a primary cyclone liquid separator through a mixed solution conveying pipe, the light phase outlet of the primary cyclone liquid separator is connected with the inlet of a secondary cyclone liquid separator, the light phase outlet of the secondary cyclone liquid separator is connected with the inlet of a solution temporary storage tank, the lower outlet of the solution temporary storage tank is connected with the reflux port of the solution temporary storage tank and an extraction liquid evaporation recovery system through a temporary storage tank conveying pump, and the recycling solvent outlet of the extraction liquid evaporation recovery system is connected with the inlet of the fresh solvent pipe. The system has the advantages of low investment, high extraction efficiency, full utilization of powder materials and great improvement of economic benefit.
Description
Technical Field
The invention relates to an extraction system, in particular to an oil cake extraction system which can be used for dynamic extraction in the industries of food, environmental protection, chemical industry and the like, and belongs to the technical field of extraction equipment.
Background
Extraction equipment in the market is various and includes fixed bed type, moving bed type, basket bucket type and filter cartridge type. The general principle is that the solid is naturally piled up to form a stable material bed or forced to form a stable material bed, the extracting solution or the washing solution is sprayed from the upper part of the material bed, and the liquid permeates the material layer to complete the mass transfer process.
The equipment has the requirement on the granularity of solid materials, the solid materials are in bulk or sheet form, and certain gaps are reserved among the piled particles so as to be beneficial to the permeation of extraction liquid or washing liquid. When the powder degree in the solid material is too large, the void ratio of the material bed is insufficient, the permeation rate is reduced or the material is not permeated, such as tea seed cake, palm kernel cake and other materials are leached.
In the working process of the existing leacher, most of solid materials are in laminar contact with the extraction liquid, and are insufficiently mixed with the extraction liquid; the extraction liquid automatically flows through the fall, the light phase is positioned at the upper part of the liquid layer, short circuit is easily generated in new solution, the extraction power is insufficient, and the extraction efficiency is low; the extraction path is seemingly longer, but the utilization rate of the upper layer screening surface of each leaching unit is very low. In addition, the concentrated extract liquid obtained by the powder extraction system contains a lot of powder particles, and the powder particles flow into a subsequent pipeline to cause the blockage of a liquid outlet pipe valve, so that the concentrated extract liquid must be filtered. After a period of time, the traditional filter can be blocked, the liquid flow is reduced, the filter element or grid plate is required to be cleaned manually at regular intervals, so that the loss of the solvent is high, the cleaning work is extremely dangerous due to inflammability and explosiveness of the solvent, the labor intensity is high, and the production stability is poor.
Disclosure of Invention
The invention aims to overcome the problems in the prior art and provide an oil cake extraction system which can omit screening, presoaking equipment, solvent circulation spraying and grid plate back flushing systems, and the powder materials are fully utilized, so that the economic benefit is greatly improved.
In order to solve the technical problems, the oil cake extraction system comprises a raw material temporary storage bin, a quantitative auger, a powder leacher and a wet slag conveyor, wherein an outlet of the raw material temporary storage bin is connected with an inlet of the quantitative auger, an outlet of the quantitative auger is connected with a solid material inlet of the leacher, a wet material outlet of the leacher is connected with an inlet of the wet slag conveyor, an inlet of a new solvent pump is connected with an outlet of a fresh solvent pipe, an outlet of the new solvent pump is connected with a new leaching inlet of the leacher, a concentrated solution outlet of the leacher is connected with an inlet of a concentrated solution extraction pump, an outlet of the concentrated solution extraction pump is connected with an inlet of a primary cyclone separator through a mixed solution conveying pipe, a light phase outlet of the primary cyclone separator is connected with an inlet of a secondary cyclone separator, and a light phase outlet of the secondary cyclone separator is connected with an inlet of a solution temporary storage tank; the lower outlet of the solution temporary storage tank is connected with the inlet of a temporary storage tank conveying pump, the outlet of the temporary storage tank conveying pump is connected with a return port of the solution temporary storage tank and a concentrated extract inlet of an extract evaporation recovery system, and a recycling solvent outlet of the extract evaporation recovery system is connected with the inlet of the fresh solvent pipe; the outlet of the wet slag conveyor is connected with the feed inlet of the vertical steam-off machine, and the discharge outlet of the vertical steam-off machine is provided with a cake slag discharge valve.
Compared with the prior art, the invention has the following beneficial effects: the oil cake is the leftovers of oil after oil is squeezed, such as tea seed cake, rapeseed cake, palm kernel squeezed cake, etc.; the cake after oil extraction contains 5-10% of oil, and the balance of protein, cellulose, water and the like, and is usually used as coarse fodder or fertilizer, so that the economic value is low. After the oil cake is crushed by the crusher, the oil cake is lifted to a high position by a bucket elevator, and then is sent into a raw material temporary storage bin for temporary storage by a horizontal conveyor; and then the raw materials enter a quantitative auger from a temporary raw material storage bin, the quantitative auger directly sends oil cakes to a solid material inlet of a leacher of the powder leacher, one-pot stewing type extraction is adopted in the powder leacher, extracted cakes are discharged from a wet material outlet of the leacher, are sent out by a wet slag conveyor, and are discharged from a cake slag discharge valve after being dried by a vertical steam-off machine. The new solvent pump sends new solvent into the new solution inlet of the leacher, after the concentrated solution containing a certain amount of powder particles is pumped out by the concentrated extract pump, the concentrated solution is sent to the first-stage cyclone liquid separator for separation through the mixed liquid conveying pipe, the solid particles in the solution are removed for the first time, and then the solid particles in the solution are removed again through the second-stage cyclone liquid separator, and enter the solution temporary storage tank for storage, the separated solid particles flow into the soaking tank of the leacher, and the concentrated solution after precipitation is sent to the concentrated extract inlet of the extract evaporation recovery system from the outlet of the solution temporary storage tank through the temporary storage tank conveying pump. In the initial stage of system operation, the outlet solution of the temporary storage tank conveying pump can also return to the solution temporary storage tank through the temporary storage tank return pipe. The system omits screening and presoaking procedures, saves investment and installation sites of screening, storing and presoaking equipment, omits a complex and complicated solvent circulation spraying system and a grid plate back flushing system, has good equipment tightness, eliminates potential safety hazards such as running, leaking, and the like, and has low operation cost. All high-powder oil cakes and the like can be completely utilized, for example, residual oil in tea seed cakes, rapeseed cakes and palm kernel pressed cakes is extracted, so that the economic value of the cakes can be improved, and the additional storage and transportation cost is eliminated. The improvement of the utilization rate of the powder can greatly improve the profit level of oil cake enterprises. The leaching system can be standardized, investment is saved, factory construction is fast, capacity expansion is convenient and fast, the development bottleneck of oil cake is hopeful to be broken through, and large industrial development is realized.
As an improvement of the invention, a main heat medium inlet of the extraction liquid evaporation recovery system is connected with a raw steam pipe, a solvent supplementing port of the extraction liquid evaporation recovery system is connected with a normal hexane supplementing pipe, a gas phase discharging port of the vertical evaporator is respectively connected with a recycling heat medium inlet of the extraction liquid evaporation recovery system through a recycling heat medium pipe, and a crude oil output port of the extraction liquid evaporation recovery system is connected with a crude oil output pipe. The concentrated extract is sent into a concentrated extract inlet of an extract evaporation recovery system, evaporated in the extract evaporation recovery system, crude oil obtained by evaporation is discharged from a crude oil output port, and the recycled extract obtained by evaporation is mixed with fresh n-hexane from a n-hexane supply pipe, discharged from a recycled solvent outlet and fed into a fresh solvent pipe for recycling. The raw steam is used as a main heating medium of the extraction liquid evaporation recovery system, and the mixed steam discharged by the vertical type evaporator is used as an auxiliary heat source to preheat the extraction liquid.
As a further improvement of the invention, the powder leacher comprises a rectangular box body, a plurality of parallel groove body partition boards are connected between the front wall board and the rear wall board of the box body, each groove body partition board divides the inner cavity of the box body into a plurality of soaking grooves, the upper parts of the groove body partition boards are respectively provided with overflow ports, the overflow ports on the adjacent groove body partition boards are staggered in the front-rear direction, the height of each overflow port is gradually reduced from right to left, the discharge end of the right-most soaking groove is connected with a leacher new solution inlet, and the feed end of the left-most soaking groove is connected with a leacher concentrated solution outlet; the solid material inlet of the leacher is positioned above the feeding end of the leftmost soaking tank, the discharging end of each tank body partition plate is respectively provided with a guide chute for lifting and turning materials to the right, the discharging end of the right wall plate of the tank body is provided with a discharge chute extending upwards to the right, and the wet material outlet of the leacher is positioned at the upper end of the discharge chute; the bottoms of the soaking tanks are arc-shaped, the soaking tank spirals are respectively arranged, and the spiral directions of the adjacent soaking tank spirals are opposite; scraper lifting mechanisms are respectively installed in the guide tanks, and scraper discharging mechanisms are installed in the discharge tanks. The material falls into the feed end of the leftmost soaking tank from the solid inlet of the leacher, and the new solvent pump sends new solvent into the new solvent inlet of the leacher and into the rightmost soaking tank. The soaking and extracting process is completed in the soaking tanks, when the materials are pushed to the discharge ends of the soaking tanks, the materials are fished out upwards along the guide tanks, separated from the liquid level, and then are subjected to short draining and fall into the lower-level soaking tank on the right side. The advancing directions of the materials in the adjacent soaking tanks are opposite, so that the solid materials advance in an S-shaped zigzag manner. When the solid material enters the final-stage soaking tank, the solid material is fully soaked and mixed with the new solution, and then fished out from the discharge end of the right-most soaking tank along the discharge tank, discharged from the wet material outlet of the leacher, and sent out by the wet slag conveyor. The solid material and the solution always keep countercurrent, the material with the highest content contacts with the concentrated solution, and the material with lower content contacts with the dilute solution, so that good osmotic pressure can be always kept, and the mass transfer efficiency is further improved. The solid materials alternately advance along the soaking tank transversely, are fished out to fall into the longitudinal next-stage soaking tank after advancing transversely for one section, are repeatedly stirred, and are in turbulent flow states, so that laminar flow states of the materials and the solution can not occur, and even if the powder with small void ratio can be fully soaked by the solution. Adjacent overflow ports are arranged in a staggered manner in the front-rear direction, the solvent also flows in an S-shaped zigzag manner and is opposite to the advancing direction of the solid material, flows through the whole length of each soaking tank, then overflows into the next soaking tank by utilizing the potential difference and flows back through the whole length of the soaking tank, so that the extraction stroke of the solid material and the solution is greatly prolonged, the full extraction can be realized, and the efficient extraction is realized. The concentrated extract reaching the leftmost soaking tank is discharged from the concentrated extract outlet of the leacher. The liquid level of the soaking liquid is slightly higher than the solid phase, the solid and the liquid are fully mixed, the consumption of the solvent is less, the concentration of the obtained mixed liquid is high, and the evaporation separation energy consumption is less. The bottom of the soaking tank is arc-shaped and is in spiral fit with the soaking tank, so that dead zones at the bottom of the tank can be avoided; the spiral of the soaking tank is responsible for conveying solid materials in the soaking tank and completing soaking extraction, and the defect of insufficient mass transfer of the materials and the solvent in the simple soaking process is avoided by forced stirring of the spiral blades, so that the materials are reversely advanced in an S shape due to the spiral direction of the spiral of the adjacent soaking tank. The scraper lifting mechanism is used for fishing, draining and lifting the soaked solid materials and is used for solid-liquid separation and solid-phase lifting; the scraper discharging mechanism is used for fishing up, draining and discharging the extracted solid materials. The spiral scraper not only plays a role in conveying solid materials, but also can stir the solid materials strongly, the height of a material layer in the soaking box can be increased by more than one time, and the productivity per unit area is greatly improved; the natural permeation of the extract from top to bottom is changed into spiral mechanical stirring, the solid-liquid direct mixing and soaking are performed, the extraction power is high, and the extraction efficiency is high; the solvent quantity of the traditional leaching system participating in circulation is 5 times of that of solid materials, the solid-liquid volume ratio is about 1.2-1.5 times, the initial solvent quantity is only one fourth to one third of that of the original solvent, and a large amount of solvents and occupied funds are greatly saved.
As a further improvement of the invention, at least one baffle plate extending along the left-right direction is respectively arranged in each soaking tank, and the lower end of each baffle plate is respectively clamped above the spiral of the soaking tank through the concave arc on the baffle plate. The baffle plate can prevent the surface layer solution from flowing out in a short circuit without fully contacting with the solid material, the concave arc on the baffle plate is clamped above the spiral of the soaking tank to provide a channel for conveying the material, the solution is forced to pass through the notch of the concave arc on the baffle plate, the solid material is in stirring and mixing contact with the extracting solution, the two phases of turbulence are fully contacted, and the soaking effect of the material and the solution is further improved; the solid and the liquid are contacted in a turbulent flow under the stirring action, the liquid phase is free from chromatography, and the concentration of the same phase is consistent. The multiple baffles make the solvent flow in S shape in the up-down direction in each soaking tank, thereby avoiding the phenomenon of short circuit of the solvent, obviously increasing the extraction power and having high extraction efficiency.
As a further improvement of the invention, the discharge end of the spiral shaft of each soaking tank spiral is respectively provided with a hollow large chain wheel, the lower end of a lifting driving chain of a corresponding scraper lifting mechanism is meshed with the hollow large chain wheel, and a plurality of lifting scrapers are uniformly arranged on the lifting driving chain. Part of materials can enter the discharge end of the soaking tank through the hollowed-out part of the hollowed-out large chain wheel, so that the material receiving area of the lifting scraper is enlarged, and the conveying capacity of the lifting scraper is improved. The spiral of the soaking tank and the scraper lifting mechanism synchronously rotate, the material pushed by the lifting scraper is fished out from the solution and lifted, and falls into the next soaking tank, and the conveying capacity of the lifting scraper is larger than that of the spiral of the soaking tank, so that the material blockage can be avoided.
As a further improvement of the invention, the upper ends of the lifting driving chains are meshed with the lifting small chain wheels, the lifting small chain wheels are respectively arranged on the driving shafts, the driving shafts are also respectively provided with the linkage chain wheels, two adjacent driving shafts are in a group, and the two linkage chain wheels are in transmission connection through the linkage chain; the shaft end of one driving shaft is provided with a large lifting chain wheel, and the large lifting chain wheel is in transmission connection with a main chain of a driving speed reducer through a main chain. The main chain of the drive speed reducer drives the large lifting chain wheel to rotate through the main chain belt, the large lifting chain wheel drives the small lifting chain wheel and the linkage chain wheel to rotate through the driving shaft, the linkage chain drives the other driving shaft and the small lifting chain wheel to synchronously rotate, the two small lifting chain wheels drive the lifting scraping plates to operate and the soaking tank to rotate in a spiral mode through the lifting driving chain, the purpose that one drive speed reducer drives the two soaking tank spirals to push solid materials leftwards and rightwards simultaneously is achieved, and the two scraping plate lifting mechanisms are driven to drag out, drain and lift the solid materials synchronously simultaneously is achieved.
As a further improvement of the invention, the two ends of the spiral shaft of each soaking tank spiral are respectively supported in the spiral bearing seats, each spiral bearing seat is respectively fixed at the center of the round sealing plate, and each round sealing plate is respectively covered and fixed at the outer sides of the spiral mounting holes at the two ends of the soaking tank. The round sealing plate and the spiral bearing seat are removed, the whole spiral of the soaking tank can be pulled out from the spiral mounting hole, the spiral of the soaking tank penetrates through the spiral mounting hole during mounting, then the round sealing plate is covered and fixed through bolts, and then the spiral bearing seat is mounted and fixed.
As a further improvement of the invention, the lower end of the discharging driving chain of the scraper discharging mechanism is meshed with the hollow large chain wheel, and a plurality of discharging scrapers are uniformly arranged on the discharging driving chain. Part of materials can enter the discharging end of the right-most soaking tank through the hollowed-out part of the hollowed-out large chain wheel, so that the material receiving area of the discharging scraper is enlarged, and the conveying capacity of the discharging scraper is improved. The spiral of the soaking tank and the scraper discharging mechanism synchronously rotate, the material pushed by the discharging scraper is fished out from the solution, lifted and discharged out of the leacher, and the conveying capacity of the discharging scraper is larger than that of the spiral of the soaking tank, so that the blockage can be avoided.
As a further improvement of the invention, each soaking tank spiral comprises a spiral shaft and a main spiral sheet wound on the periphery of the spiral shaft, a filter cylinder is arranged at the feed end of the spiral shaft below the solid material inlet of the leacher, a port of the filter cylinder facing one side of the main spiral sheet is closed, the other side of the filter cylinder is open, the concentrated liquid outlet of the leacher is inserted into the inner cavity of the filter cylinder, a plurality of axially extending grid bars are uniformly distributed on the circumference of the filter cylinder, and gaps between adjacent grid bars are narrow outside and wide inside. The powder is trapped on the outer surface of the filter cylinder after being filtered by the filter cylinder before flowing out, so that the content of powdery solid in the concentrated extract is reduced as much as possible, and the guarantee is provided for the subsequent hydrocyclone separation and evaporation; after the concentrated extract in the solid-liquid mixing medium is continuously and stably filtered out, the concentrated extract enters a concentrated extract outlet of a leacher and flows out, and the filtered concentrated extract can be stably and continuously filtered out and conveyed without blocking a liquid outlet pipe valve so as to conveniently enter a hydrocyclone separation system for fine filtration. Once the powder passes through the gap at the outermost side of the filter cylinder, the powder can smoothly fall into the bottom of the filter cylinder and is pushed out by the spiral belt in the filter cylinder to self-clean; avoiding powder particles from being blocked in gaps between adjacent grate bars and affecting the filtering capability.
As a further improvement of the invention, the outer circumference of the filter cylinder is wound with a filter cylinder outer spiral band, and the rotation direction of the filter cylinder outer spiral band is the same as that of the coaxial main spiral piece; the inner wall of the filter cylinder is provided with an inner spiral belt of the filter cylinder, and the rotation direction of the inner spiral belt of the filter cylinder is opposite to that of the coaxial main spiral sheet. The spiral belt outside the filter cylinder can push out the solid materials flowing along with the liquid to the side where the main spiral sheet is positioned, so that excessive materials are prevented from being deposited outside the filter cylinder. A small amount of solid powder enters the filter cartridge along with the extraction liquid, and is settled at the lower part of the inner wall of the filter cartridge, the inner spiral belt of the filter cartridge opposite to the main spiral sheet in rotation direction pushes sediment out of the filter cartridge from the open end, and the sediment is pushed out of the filtering section by the outer spiral belt of the filter cartridge, so that the self-cleaning process of the filter cartridge is completed. Thus realizing stable and reliable continuous filtration, leading the process of the oil cake extraction system to be complete, solving the difficult problem of separating high-powder-degree materials from liquid and leading the oil cake extraction system to have wide adaptability to various oils.
Drawings
The invention will now be described in further detail with reference to the drawings and the detailed description, which are provided for reference and illustration only and are not intended to limit the invention.
FIG. 1 is a flow chart of the oil cake extraction system of the present invention.
Fig. 2 is a front view of a first embodiment of a powder leacher in accordance with the present invention.
Fig. 3 is a cross-sectional view taken along A-A in fig. 2.
Fig. 4 is a cross-sectional view taken along B-B in fig. 2.
Fig. 5 is a cross-sectional view taken along line C-C of fig. 2.
Fig. 6 is a schematic view of fig. 2 with the front wall panel removed.
Fig. 7 is a perspective view of fig. 2.
Fig. 8 is a perspective view of the powder leacher tank of fig. 2 with the top cover removed.
Fig. 9 is a perspective view of two adjacent soaking tanks in fig. 2.
Fig. 10 is a perspective view of the leftmost soaking tank in fig. 2.
Fig. 11 is a perspective view of the filter cartridge of fig. 10.
Fig. 12 is an enlarged view of a portion of a filter cartridge.
FIG. 13 is a schematic view showing an operation of a second embodiment of the powder extractor according to the present invention.
Fig. 14 is a top view of fig. 13.
In the figure: E0. a pulverizer; E1. bucket elevator; E2. a horizontal conveyor; E3. a raw material temporary storage bin; E4. quantitative auger; E5. a powder leacher; E6. a wet slag conveyor; E7. a first-stage hydrocyclone; E8. a secondary hydrocyclone separator; E9. a solution temporary storage tank; E10. a tail gas condenser; E11. an extract evaporation recovery system; e11a. concentrated extract inlet; e11b. Recycled solvent outlet; e11c. Crude oil delivery outlet; e11d. a main heating medium inlet; e11e. recycling the heat medium inlet; e11f exhaust steam outlet; e11g. a solvent replenishment port; E12. vertical steam-off machine; e12a cake discharge valve; B1. a new solvent pump; B2. a concentrated extract pump; B3. a temporary storage tank transfer pump; G1. a fresh solvent tube; G2. a mixed liquid conveying pipe; G3. a temporary storage tank return pipe; G4. a temporary storage tank output pipe; G5. a crude oil output pipe; G6. n-hexane supply pipe; G7. a steam generating pipe; G8. recycling the heat medium pipe; q1. fresh solvent flow meter; q2, a concentrated solution flowmeter; 1. a soaking tank; 1a, a solid material inlet of a leacher; 1a1, a feeding honeycomb duct; 1b, a wet material outlet of the leacher; 1c, spiral mounting holes; 1d, a circular sealing plate; 1e, exhaust holes; 2. a tank body partition board; 2a, overflow port; 2b, a guide groove; 2c, a discharge chute; 3. a baffle plate; 3a, concave arcs on the baffle plates; 4. the soaking tank is spiral; 4a, a screw shaft; 4b, a main spiral sheet; 4c, hollowing out a large chain wheel; 4d, a spiral bearing seat; 4e, right pushing the spiral; 4f, pushing the spiral left; 5. a squeegee lifting mechanism; 5a, lifting a driving chain; 5b, lifting the scraping plate; 6. lifting the small chain wheel; 7. a drive shaft; 8. a linked sprocket; 9. a linkage chain; 10. lifting a large chain wheel; 11. a main chain; 12. driving a speed reducer; 12a, a main sprocket; 13. a filter cartridge; 13a, grate bars; 13b, a filter cartridge external screw belt; 13c, a spiral belt in the filter cartridge; 14. a scraper blade discharging mechanism; 14a, a discharging driving chain; 14b, a discharging scraper; 15. a new leaching inlet of the leacher; 16. and a concentrated liquor outlet of the leacher.
Detailed Description
In the following description of the present invention, the terms "upper", "lower", "front", "rear", "left", "right", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are merely for convenience in describing the present invention and simplifying the description, and do not mean that the device must have a specific orientation.
As shown in fig. 1, the oil cake extraction system comprises a crusher E0, a bucket elevator E1, a horizontal conveyor E2, a raw material temporary storage bin E3, a quantitative auger E4, a powder leacher E5 and a wet slag conveyor E6, wherein the outlet of the raw material temporary storage bin E3 is connected with the inlet of the quantitative auger E4, the outlet of the quantitative auger E4 is connected with the solid material inlet of the leacher, the wet material outlet of the leacher is connected with the inlet of the wet slag conveyor E6, the outlet of the wet slag conveyor E6 is connected with the feed inlet of a vertical evaporator E12, and the discharge port of the vertical evaporator E12 is provided with a cake slag discharge valve E12a.
The inlet of the new solvent pump B1 is connected with the fresh solvent pipe G1, the outlet of the new solvent pump B1 is connected with the new solution inlet 15 of the leacher, the concentrated solution outlet 16 of the leacher is connected with the inlet of the concentrated solution pump B2, the outlet of the concentrated solution pump B2 is connected with the inlet of the primary hydrocyclone E7 through the mixed solution conveying pipe G2, the light phase outlet of the primary hydrocyclone E7 is connected with the inlet of the secondary hydrocyclone E8, the light phase outlet of the secondary hydrocyclone E8 is connected with the inlet of the solution temporary storage tank E9, and the bottom outlets of the primary hydrocyclone E7, the secondary hydrocyclone E8 and the solution temporary storage tank E9 are connected with the reflux port of the powder leacher E5.
Oil cakes such as tea seed cakes, rapeseed cakes, palm kernel pressed cakes and the like are crushed by a crusher E0, lifted to a high position by a bucket elevator E1, then sent into a raw material temporary storage bin E3 by a horizontal conveyor E2 for storage, enter a quantitative auger E4 from the raw material temporary storage bin E3, the quantitative auger E4 directly sends the oil cakes into a solid material inlet of a leacher of a powder leacher E5, the powder leacher E5 adopts one-pot stewing type extraction, extracted cake residues are discharged from a wet material outlet of the leacher, sent out by a wet residue conveyor E6, dried by a vertical steam-stripping machine E12 and discharged from a cake residue discharge valve E12a.
The new solvent pump B1 sends new solvent into the new solvent inlet 15 of the leacher, and the oil cake contacts with the solvent in the powder leacher E5 to finish extraction. The outlet pipeline of the new solvent pump B1 is provided with a fresh solvent flowmeter Q1, the outlet of the solution temporary storage tank E9 is connected with the inlet of the temporary storage tank conveying pump B3 through a temporary storage tank output pipe G4, the outlet of the temporary storage tank conveying pump B3 is connected with the concentrated extract inlet E11a of the extract evaporation recovery system E11 through a concentrated solution flowmeter Q2 and the temporary storage tank output pipe G4, and the recycling solvent outlet E11B of the extract evaporation recovery system E11 is connected with the inlet of the fresh solvent pipe G1. The outlet of the temporary storage tank conveying pump B3 is also connected with the reflux port of the solution temporary storage tank E9 through a temporary storage tank reflux pipe G3.
After the concentrated solution containing a certain amount of powder particles is pumped out by a concentrated extract pump B2, the concentrated solution is sent to a first-stage hydrocyclone E7 for separation through a mixed solution conveying pipe G2, the solid particles in the solution are removed for the first time, then the solid particles in the solution are removed again through a second-stage hydrocyclone E8, the solution enters a solution temporary storage tank E9 for storage, the separated solid particle flow can enter a soaking tank of a powder leacher E5, and can enter a second soaking tank from the left, so that the particle concentration at a concentrated solution outlet 16 of the leacher is reduced.
The concentrated solution after precipitation is discharged from the outlet of the solution temporary storage tank E9 through the temporary storage tank output pipe G4 and is sent to the concentrated extract inlet E11a of the extract evaporation recovery system E11 through the temporary storage tank conveying pump B3. In the initial stage of the system operation, the outlet solution of the temporary storage tank transfer pump B3 may also return to the solution temporary storage tank E9 through the temporary storage tank return pipe G3. The fresh solvent flow meter Q1 can monitor the flow of fresh solvent and the concentrated solution flow meter Q2 can monitor the flow of output concentrated solution.
The main heat medium inlet E11d of the extraction liquid evaporation recovery system E11 is connected with a raw steam pipe G7, the solvent supplementing port E11G of the extraction liquid evaporation recovery system E11 is connected with a normal hexane supplementing pipe G6, the gas phase discharging port of the vertical evaporator-off machine E12 is respectively connected with the recycling heat medium inlet E11E of the extraction liquid evaporation recovery system E11 through a recycling heat medium pipe G8, and the crude oil output port E11c of the extraction liquid evaporation recovery system E11 is connected with a crude oil output pipe G5.
The concentrated extract is sent into the concentrated extract inlet E11a of the extract evaporation recovery system E11, the evaporation is carried out in the extract evaporation recovery system E11, the crude oil obtained by evaporation is discharged from the crude oil outlet E11c, and the recycled extract obtained by evaporation is mixed with the fresh n-hexane from the n-hexane supply pipe G6, then discharged from the recycled solvent outlet E11b and fed into the fresh solvent pipe G1 for recycling. The raw steam is used as a main heat medium of the extraction liquid evaporation recovery system E11, and the mixed steam discharged by the vertical evaporator E12 is used as an auxiliary heat source to preheat the extraction liquid.
As shown in fig. 1 to 14, the powder leacher E5 comprises a rectangular box body, the top of the box body is provided with an exhaust hole 1E and a manhole, the exhaust holes of the exhaust hole 1E and the solution temporary storage tank E9 are connected with the tail gas condenser E10, the exhaust steam outlet E11f of the extract evaporation recovery system E11 is also connected with the tail gas condenser E10, and the ethanol gas is recycled after condensation recovery. A plurality of tank body partition boards 2 which are parallel to each other are connected between the front wall board and the rear wall board of the tank body, each tank body partition board 2 divides the inner cavity of the tank body into a plurality of soaking tanks 1, the upper parts of the tank body partition boards 2 are respectively provided with overflow ports 2a, the overflow ports 2a on the adjacent tank body partition boards 2 are arranged in a staggered way in the front-rear direction, the height of each overflow port 2a is gradually reduced from right to left, the discharge end of the right-most soaking tank is connected with a leacher new solution inlet 15, and the feed end of the left-most soaking tank is connected with a leacher concentrated solution outlet 16; the upper part of the feeding end of the leftmost soaking tank is provided with a leacher solid material inlet 1a, the discharging end of each tank body partition plate 2 is respectively provided with a guide chute 2b for lifting and turning materials to the right side, and the discharging end of the right wall plate of the tank body is provided with a discharge chute 2c extending upwards to the right.
The bottoms of the soaking tanks 1 are arc-shaped, the soaking tank spirals 4 are respectively arranged, the spiral directions of the adjacent soaking tank spirals 4 are opposite, and from the solid material inlet 1a of the solid material leacher, the left pushing spirals 4f are arranged in the odd number of tanks to push the solid material to the front side wall direction of the powder leacher; the even number of grooves are right pushing screws 4e which push the solid materials to the rear side wall direction of the powder leaching device. The scraper lifting mechanisms 5 are respectively installed in the guide tanks 2b, and the scraper discharging mechanisms 14 are installed in the discharge tanks 2c.
The material enters the feeding end of the leftmost soaking tank from the solid material inlet 1a of the leacher, and the new solvent enters the rightmost soaking tank. The soaking and extracting process is completed in the soaking tank 1, when the materials are pushed to the discharge end of each soaking tank 1 by the soaking tank spiral 4, the materials are fished out upwards by the scraper lifting mechanism 5 along the guide tank 2b, and the materials fall into the lower-level soaking tank on the right side after being separated from the liquid level by short-time draining. The advancing directions of the materials in the adjacent soaking tanks are opposite, so that the solid materials advance in an S-shaped zigzag manner. When the solid material enters the final soaking tank, the solid material is fully soaked and mixed with the new solution, and then is fished out by the scraper discharging mechanism 14 along the discharging tank 2c from the discharging end of the right-most soaking tank and discharged out of the machine from the wet material outlet 1b of the leacher. The solid material and the solution always keep countercurrent, the material with the highest content contacts with the concentrated solution, and the material with lower content contacts with the dilute solution, so that good osmotic pressure can be always kept, and the mass transfer efficiency is further improved. The solid materials alternately advance along the transverse direction of the soaking tank 1, are fished out to fall into a longitudinal next-stage soaking tank after advancing for a section transversely, are repeatedly stirred, are in turbulent flow states, are not in laminar flow states, and can be fully soaked by the solution even if the powder with small void ratio. The adjacent overflow ports 2a are arranged in a staggered manner in the front-rear direction, the solvent also flows in an S-shaped zigzag manner and is opposite to the advancing direction of the solid material, flows through the whole length of each soaking tank 1, then overflows into the next soaking tank by utilizing the potential difference and flows back through the whole length of the soaking tank, so that the extraction stroke of the solid material and the solution is greatly prolonged, the full extraction can be realized, and the efficient extraction is realized. The concentrate reaching the leftmost soaking tank is discharged from the leacher concentrate outlet 16. The liquid level of the soaking liquid is slightly higher than the solid phase, the solid and the liquid are fully mixed, the consumption of the solvent is less, the concentration of the obtained mixed liquid is high, and the evaporation separation energy consumption is less.
The bottom of the soaking tank 1 is arc-shaped and is matched with the soaking tank spiral 4, so that dead zones at the bottom of the tank can be avoided; the soaking tank spiral 4 is responsible for conveying solid materials in the soaking tank 1 and completing soaking extraction, and the defect of insufficient mass transfer of the materials and the solvent in the simple soaking process is avoided by forced stirring of spiral blades, so that the materials are reversely advanced in an S shape due to the opposite rotation directions of the adjacent soaking tank spiral 4. The scraper lifting mechanism 5 is used for fishing, draining and lifting the soaked solid materials and is used for solid-liquid separation and solid-phase lifting; the scraper discharging mechanism 14 is used for fishing out, draining and discharging the extracted solid materials. The spiral scraper not only plays a role in conveying solid materials, but also can be used for strongly stirring the solid materials.
As shown in fig. 8, at least one baffle plate 3 extending in the left-right direction is respectively arranged in each soaking tank 1, and the lower end of each baffle plate 3 is respectively clamped above the spiral of the soaking tank through a concave arc 3a on the baffle plate. The baffle plate 3 can prevent the surface layer solution from flowing out in a short circuit without fully contacting with the solid material, the concave arc 3a on the baffle plate is clamped above the soaking tank spiral 4 to provide a channel for conveying the material, the solution is forced to pass through the notch of the concave arc 3a on the baffle plate, the solid material is in stirring and mixing contact with the extraction liquid, and the two-phase turbulence state is fully contacted, so that the soaking effect of the material and the solution is further improved; the solid and the liquid are contacted in a turbulent flow under the stirring action, the liquid phase is free from chromatography, and the concentration of the same phase is consistent. The multi-channel baffle plates 3 enable the solvent to flow in an S shape in the up-down direction in each soaking tank 1, thereby avoiding the phenomenon of short circuit of the solvent, obviously increasing the extraction power and having high extraction efficiency.
As shown in fig. 9, the discharge ends of the spiral shafts of the soaking tank spirals 4 are respectively provided with a hollow large sprocket 4c, the lower ends of lifting driving chains 5a of corresponding scraper lifting mechanisms 5 are meshed with the hollow large sprocket 4c, and a plurality of lifting scrapers 5b are uniformly arranged on the lifting driving chains 5a. Part of the materials can enter the discharge end of the soaking tank through the hollowed-out part of the hollowed-out large chain wheel 4c, so that the material receiving area of the lifting scraper 5b is enlarged, and the conveying capacity of the lifting scraper 5b is improved. The soaking tank spiral 4 and the scraper lifting mechanism 5 synchronously rotate, the lifting scraper 5b drags the pushed materials out of the solution, the pushed materials fall into the next soaking tank, the conveying capacity of the lifting scraper 5b is larger than that of the soaking tank spiral 4, and the situation that blocking is caused can be avoided.
The upper end of each lifting driving chain 5a is meshed with a lifting small chain wheel 6, each lifting small chain wheel 6 is respectively arranged on each driving shaft 7, each driving shaft 7 is also respectively provided with a linkage chain wheel 8, two adjacent driving shafts 7 are in a group, and the two linkage chain wheels 8 are in transmission connection through a linkage chain 9; the shaft end of one driving shaft 7 is provided with a large lifting chain wheel 10, and the large lifting chain wheel 10 is in transmission connection with a main chain 12a of a driving speed reducer 12 through a main chain 11. The main chain wheel 12a of the driving speed reducer 12 drives the lifting large chain wheel 10 to rotate through the main chain 11, the lifting large chain wheel 10 drives the lifting small chain wheel 6 and the linkage chain wheel 8 to rotate through the driving shaft 7, the linkage chain 9 drives the other driving shaft 7 and the lifting small chain wheel 6 to synchronously rotate, the two lifting small chain wheels 6 respectively drive the lifting scraping plate 5b to operate and the soaking groove spiral 4 to rotate through the lifting driving chain 5a, the purpose that one driving speed reducer 12 simultaneously drives the two soaking groove spirals 4 to push solid materials leftwards and rightwards is achieved, and the two scraping plate lifting mechanisms 5 are simultaneously driven to synchronously drag out materials, drain and lift the solid materials is achieved.
Both ends of a screw shaft 4a of each soaking tank screw 4 are respectively supported in screw bearing seats 4d, each screw bearing seat 4d is respectively fixed at the center of a circular sealing plate 1d, and each circular sealing plate 1d is respectively covered and fixed at the outer sides of screw mounting holes 1c at both ends of the soaking tank. The whole soaking groove spiral 4 can be pulled out from the spiral mounting hole 1c by removing the circular sealing plate 1d and the spiral bearing seat 4d, the soaking groove spiral 4 penetrates into the spiral mounting hole 1c during mounting, then the circular sealing plate 1d is covered and fixed through bolts, and then the spiral bearing seat 4d is mounted and fixed.
The lower end of a discharging driving chain 14a of the scraper discharging mechanism 14 is meshed with the hollow large chain wheel 4c, and a plurality of discharging scrapers 14b are uniformly arranged on the discharging driving chain 14a. Part of the materials can enter the discharging end of the right-most soaking tank through the hollowed-out part of the hollowed-out large chain wheel 4c, so that the material receiving area of the discharging scraper 14b is enlarged, and the conveying capacity of the discharging scraper 14b is improved. The soaking tank spiral 4 and the scraper discharging mechanism 14 synchronously rotate, the discharging scraper 14b drags the pushed materials out of the solution, the pushed materials are lifted and discharged out of the powder leaching device, and the conveying capacity of the discharging scraper 14b is larger than that of the soaking tank spiral 4, so that the situation that blockage is caused can be avoided.
As shown in fig. 10 to 12, each soaking tank screw 4 comprises a screw shaft 4a and a main screw plate 4b wound on the periphery of the screw shaft, a filter cylinder 13 is mounted at the feed end of the leftmost screw shaft below the solid material inlet 1a of the leacher, a port of the filter cylinder 13 facing one side of the main screw plate 4b is closed, the other side is open, a concentrated liquid outlet 16 of the leacher is inserted into an inner cavity of the filter cylinder 13, a plurality of axially extending grate bars 13a are uniformly distributed on the circumference of the filter cylinder 13, and gaps between adjacent grate bars 13a are narrow outside and wide inside. The powder is trapped on the outer surface of the filter cylinder 13 after being filtered by the filter cylinder 13 before flowing out, so that the content of powdery solid in the concentrated extract is reduced as much as possible, and the guarantee is provided for the subsequent hydrocyclone separation and evaporation; after the concentrated extract in the solid-liquid intermixing medium is continuously and stably filtered out, the concentrated extract enters a concentrated extract outlet 16 of the leacher and flows out, and the filtered concentrated extract can be stably and continuously filtered out and conveyed without causing blockage of a liquid outlet pipe valve so as to conveniently enter a hydrocyclone separation system for fine filtration. Once the powder passes through the gap at the outermost side of the filter cylinder 13, the powder can smoothly fall into the bottom of the filter cylinder 13 and is pushed out by the spiral belt 13c in the filter cylinder to self-clean; avoiding powder particles from being blocked in gaps between adjacent grate bars 13a to influence the filtering capability.
The outer circumference of the filter cartridge 13 is wound with a cartridge outer spiral band 13b, and the rotation direction of the cartridge outer spiral band 13b is the same as that of the coaxial main spiral piece 4b. The outer spiral belt 13b of the filter cartridge can push out the solid materials flowing along with the liquid to the side where the main spiral sheet 4b is positioned, so as to avoid excessive materials from accumulating outside the filter cartridge 13.
The inner wall of the filter cartridge 13 is provided with an in-cartridge screw band 13c, and the rotation direction of the in-cartridge screw band 13c is opposite to that of the coaxial main screw piece 4b. A small amount of solid powder enters the filter cylinder 13 along with the extraction liquid, and is settled at the lower part of the inner wall of the filter cylinder 13, and an inner filter cylinder spiral belt 13c which is opposite to the main spiral sheet 4b in rotation direction pushes sediment out of the filter cylinder 13 from the open end, and then is pushed out of the filtering section by an outer filter cylinder spiral belt 13b, so that the self-cleaning process of the filter cylinder 13 is completed. Thus realizing stable and reliable continuous filtration, leading the process of the oil cake extraction system to be complete, solving the difficult problem of separating high-powder-degree materials from liquid and leading the oil cake extraction system to have wide adaptability to various oils.
As shown in fig. 2 and 7, the solid material inlet 1a of the leacher may be disposed at the left part of the top cover of the tank, and the feeding flow guide pipe 1a1 is connected below the solid material inlet 1a of the leacher to guide new solid material to the front side of the filter cartridge 13.
As shown in fig. 13 and 14, the leacher solid inlet 1a may be provided at the upper portion of the left side wall of the tank, and may be located at the front side of the filter cartridge 13 in the front-rear direction. The liquid level of the soaking tank at the rightmost side is highest, and overflows to the left side in sequence. In fig. 14, the large arrow indicates the solid material direction, the small arrow indicates the solution flow direction, and the whole flow is reversed.
The invention adopts one-pot stewing type leaching, is efficient and reliable, and can be used for leaching powdery materials and high-powder-degree materials. Can solve the problems of oil extraction and preparation bottleneck of oil cake, poor material permeability, easy dissolution, blockage of grid plates, shallow leaching material layer, large equipment investment, low production efficiency, high system failure rate and the like. For powdery offcuts which cannot be treated in the traditional leaching process, such as high-powder oil cake and semi-denatured puffing powder, the oil cake extraction system can be adopted to extract the materials with the characteristics and then extract grease, so that the economic value of the materials can be greatly improved, and the economic benefit and market competitiveness of enterprises can be improved.
The foregoing description is only of a preferred embodiment of the invention and is not intended to limit the scope of the invention. In addition to the embodiments described above, other embodiments of the invention are possible. All technical schemes formed by equivalent substitution or equivalent transformation fall within the protection scope of the invention. The technical features of the present invention that are not described may be implemented by or using the prior art, and are not described herein.
Claims (8)
1. The utility model provides an oil cake extraction system, including the raw materials temporary storage storehouse, quantitative auger, powder leaches ware and wet sediment conveyer, the export of raw materials temporary storage storehouse links to each other with the entry of quantitative auger, the export of quantitative auger links to each other with leacher solid material entry, leacher wet material export links to each other with wet sediment conveyer's entry, the entry of new solvent pump links to each other with the export of fresh solvent pipe, the export of new solvent pump links to each other with leacher new solution import, leacher thick liquid export links to each other with the entry of thick extraction liquid pump, its characterized in that: the outlet of the concentrated extract pump is connected with the inlet of the primary hydrocyclone through a mixed liquor conveying pipe, the light phase outlet of the primary hydrocyclone is connected with the inlet of the secondary hydrocyclone, and the light phase outlet of the secondary hydrocyclone is connected with the inlet of the solution temporary storage tank; the lower outlet of the solution temporary storage tank is connected with the inlet of a temporary storage tank conveying pump, the outlet of the temporary storage tank conveying pump is connected with a return port of the solution temporary storage tank and a concentrated extract inlet of an extract evaporation recovery system, and a recycling solvent outlet of the extract evaporation recovery system is connected with the inlet of the fresh solvent pipe; the outlet of the wet slag conveyor is connected with the feed inlet of the vertical steam-off machine, and the discharge outlet of the vertical steam-off machine is provided with a cake slag discharge valve;
the powder leacher comprises a rectangular box body, a plurality of parallel groove body partition boards are connected between front and rear wall boards of the box body, the inner cavity of the box body is divided into a plurality of soaking grooves by each groove body partition board, overflow ports are respectively arranged on the upper parts of the groove body partition boards, the overflow ports on the adjacent groove body partition boards are arranged in a staggered manner in the front-rear direction, the height of each overflow port is gradually reduced from right to left, the discharge end of the right-most soaking groove is connected with a leacher new solution inlet, and the feed end of the left-most soaking groove is connected with a leacher concentrated solution outlet; the solid material inlet of the leacher is positioned above the feeding end of the leftmost soaking tank, the discharging end of each tank body partition plate is respectively provided with a guide chute for lifting and turning materials to the right, the discharging end of the right wall plate of the tank body is provided with a discharge chute extending upwards to the right, and the wet material outlet of the leacher is positioned at the upper end of the discharge chute; the bottoms of the soaking tanks are arc-shaped, the soaking tank spirals are respectively arranged, and the spiral directions of the adjacent soaking tank spirals are opposite; the scraper lifting mechanisms are respectively arranged in the guide tanks, and the scraper discharging mechanisms are arranged in the discharge tanks;
at least one baffle plate extending along the left-right direction is arranged in each soaking tank, and the lower end of each baffle plate is clamped above the spiral of the soaking tank through the concave arc on the baffle plate.
2. An oil cake extraction system as defined in claim 1 wherein: the main heat medium inlet of the extraction liquid evaporation recovery system is connected with a raw steam pipe, the solvent supplementing port of the extraction liquid evaporation recovery system is connected with a normal hexane supplementing pipe, the gas phase discharging port of the vertical evaporator is connected with the recycling heat medium inlet of the extraction liquid evaporation recovery system through recycling heat medium pipes respectively, and the crude oil output port of the extraction liquid evaporation recovery system is connected with a crude oil output pipe.
3. An oil cake extraction system as defined in claim 1 wherein: the spiral shaft discharge end of each soaking tank spiral is respectively provided with a hollow large chain wheel, the lower ends of lifting driving chains of corresponding scraper lifting mechanisms are meshed with the hollow large chain wheels, and a plurality of lifting scrapers are uniformly arranged on the lifting driving chains.
4. An oil cake extraction system as defined in claim 3 wherein: the upper ends of the lifting driving chains are meshed with the lifting small chain wheels, the lifting small chain wheels are respectively arranged on the driving shafts, the driving shafts are also respectively provided with the linkage chain wheels, two adjacent driving shafts are in a group, and the two linkage chain wheels are in transmission connection through the linkage chain; the shaft end of one driving shaft is provided with a large lifting chain wheel, and the large lifting chain wheel is in transmission connection with a main chain of a driving speed reducer through a main chain.
5. An oil cake extraction system as defined in claim 1 wherein: the two ends of the spiral shaft of each soaking tank spiral are respectively supported in the spiral bearing seats, each spiral bearing seat is respectively fixed at the center of the round sealing plate, and each round sealing plate is respectively covered and fixed at the outer sides of spiral mounting holes at the two ends of the soaking tank.
6. An oil cake extraction system as defined in claim 3 wherein: the lower end of a discharging driving chain of the scraper discharging mechanism is meshed with the hollow large chain wheel, and a plurality of discharging scrapers are uniformly arranged on the discharging driving chain.
7. An oil cake extraction system according to any one of claims 1 to 6, wherein: each soaking tank spiral comprises a spiral shaft and a main spiral sheet wound on the periphery of the spiral shaft, a filter cylinder is arranged at the feed end of the spiral shaft below a solid material inlet of the leacher, the port of the filter cylinder facing one side of the main spiral sheet is closed, the other side of the filter cylinder is open, a concentrated liquid outlet of the leacher is inserted into an inner cavity of the filter cylinder, a plurality of axially extending grate bars are uniformly distributed on the circumference of the filter cylinder, and gaps between adjacent grate bars are narrow outside and wide inside.
8. An oil cake extraction system as defined in claim 7, wherein: the outer periphery of the filter cylinder is wound with a filter cylinder outer spiral strip, the rotation direction of the filter cylinder outer spiral strip is the same as that of the coaxial main spiral sheet, the inner wall of the filter cylinder is provided with a filter cylinder inner spiral strip, and the rotation direction of the filter cylinder inner spiral strip is opposite to that of the coaxial main spiral sheet.
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| CN109833646B (en) * | 2019-04-03 | 2024-01-19 | 迈安德集团有限公司 | Powder leaches ware |
| CN115746948B (en) * | 2022-10-19 | 2024-02-06 | 迈安德集团有限公司 | Palm kernel direct leaching system and leaching process |
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