CN209790931U - Oil cake extraction system - Google Patents

Abstract

The utility model relates to an oil cake extraction system, the export of raw materials temporary storage storehouse links to each other through the solid material entry of ration auger and leacher, the wet material export of leacher links to each other with vertical evapo-separated machine through wet sediment conveyer, the entry of new solvent pump links to each other with fresh solvent pipe, the export of new solvent pump links to each other with the new inlet that dissolves of leacher, the export of leacher dense solution links to each other with the entry of concentrated extraction liquid extraction pump, the export of concentrated extraction liquid extraction pump links to each other through the entry of mixed liquid conveyer pipe with one-level hydrocyclone, the export of the light phase of one-level hydrocyclone links to each other with the entry of second grade hydrocyclone, the export of the light phase of second grade hydrocyclone links to each other with the entry of solution temporary storage jar, the lower part export of solution temporary storage jar links to each other through the return flow mouth and the extraction liquid evaporation recovery system of solution temporary storage jar conveyer pump, the solvent export. The system has the advantages of low investment, high extraction efficiency, full utilization of powder materials and great improvement of economic benefits.

Description

Oil cake extraction system

Technical Field

The utility model relates to an extraction system especially relates to an oil cake extraction system, can be used to the dynamic extraction of trades such as food, environmental protection and chemical industry, belongs to extraction equipment technical field.

Background

Extraction equipment on the market is various, and comprises a fixed bed type, a movable bed type, a basket type and a filter drum type. The general principle is that the solid is naturally piled up to form a stable material bed or is forced to form a stable material bed, the extract liquor or the washing liquor is poured from the upper part of the material bed, and the liquid permeates the material layer to complete the mass transfer process.

The equipment has requirements on the granularity of solid materials, the solid materials are in bulk or in a sheet shape, and certain gaps are formed among the stacked 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 voidage of the material bed is insufficient, and the permeation rate is reduced or is not permeable, such as the leaching of materials such as tea seed cakes, palm kernel cakes and the like.

In the working process of the existing leacher, most of solid materials are in laminar flow contact with extraction liquid, and are not fully mixed with the extraction liquid; the extract liquid flows automatically through the fall, the light phase is positioned at the upper part of the liquid layer, and the short circuit is easy to occur in the new solution, so that the extraction power is insufficient, and the extraction efficiency is low; the extraction path appears to be longer, but the utilization of the upper screen surface of each group of leaching units is low. In addition, the concentrated extract obtained by extraction of the powder extraction system contains a lot of powder particles, and the thick extract flows into a subsequent pipeline to cause the blockage of a liquid outlet pipe valve, so that the thick extract must be filtered. After a traditional filter is used for a period of time, silting and blocking can occur, the liquid outlet flow is reduced, a filter element or a grid plate needs to be cleaned regularly and manually, so that the solvent loss is large, the cleaning work is extremely dangerous due to the inflammability and the explosiveness of the solvent, the labor intensity is high, and the production stability is poor.

SUMMERY OF THE UTILITY MODEL

An object of the utility model is to overcome the problem that exists among the prior art, provide an oil cake extraction system, can omit screening, preimpregnation equipment, solvent circulation and spray and grid tray back flush system, the powder material is whole to be utilized, improves economic benefits greatly.

For solving the technical problem above, the utility model discloses an oil cake extraction system, including raw materials temporary storage storehouse, quantitative auger, powder leacher and wet sediment conveyer, the export in 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 the entry of wet sediment conveyer, 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 the new mouth that dissolves of leacher, leacher concentrated solution export links to each other with the entry of concentrated solution extraction pump, the export of concentrated solution extraction pump links to each other with the entry of one-level hydrocyclone through mixed liquid conveyer pipe, the light phase export of one-level hydrocyclone links to each other with the entry of second-level hydrocyclone, the light phase export of second-level hydrocyclone links to each other with the entry of 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 the reflux port of the solution temporary storage tank and the concentrated extract inlet of an extract evaporation and recovery system, and the recycled solvent outlet of the extract evaporation and 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 type desolventizer-toaster, and the discharge outlet of the vertical type desolventizer-toaster is provided with a cake slag discharge valve.

Compared with the prior art, the utility model discloses following beneficial effect has been obtained: the oil cake is the leftover after oil is pressed to prepare oil, such as tea seed cake, rapeseed cake, palm kernel pressed cake and the like; the pressed cake contains 5-10% of oil, and the rest is protein, cellulose and water, etc., and is generally used as coarse feed or fertilizer, so the economic value is low. After being crushed by a crusher, the oil cake is lifted to a high position by a bucket elevator and then is sent to a raw material temporary storage bin by a horizontal conveyor for temporary storage; then the oil cake is directly sent to a solid material inlet of an extractor of the powder extractor by the quantitative auger from the raw material temporary storage bin, the powder extractor adopts 'one pot stewing' type extraction, the extracted cake slag is discharged from a wet material outlet of the extractor, is sent out by a wet slag conveyor, is dried by a vertical evaporator and is discharged from a cake slag discharge valve. The new solvent pump sends new solvent into the new import of dissolving of leacher, after the concentrated solution that contains certain powder particle is taken out by concentrated extract extraction pump, send to one-level hydrocyclone separation through mixed liquid conveyer pipe and separate, get rid of the solid particle in the solution for the first time, get into the solution and keep in storage after the solid particle in the solution is got rid of again through second grade hydrocyclone separation, the solid particle stream that separates can leach the soaking groove of ware, concentrated solution after the sediment is from the export of solution keep in storage tank through keeping in storage tank conveyer pump and send it to the concentrated extract entry of extraction liquid evaporation recovery system. At the initial stage of system operation, the outlet solution of the temporary storage tank delivery pump can also return to the solution temporary storage tank through a temporary storage tank return pipe. The system omits screening and presoaking procedures, saves investment and installation sites of screening, storage and presoaking equipment, omits a complex and fussy solvent circulating spray system and a grid plate backwashing system, has good equipment tightness, eliminates potential safety hazards such as running, falling, dripping and leaking and the like, and has low operating cost. All the high-powder oil material cakes and the like can be fully utilized, such as 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 utilization rate of the powder is improved, and the profit level of oil cake enterprises can be greatly improved. The leaching system can be standardized, the investment is saved, the factory building is fast, the expansion is convenient and fast, the development bottleneck of the oil cake is hopefully broken through, and the industrial mass development is realized.

As the improvement of the utility model, the main heat medium entry of extraction liquid evaporation recovery system links to each other with the steam generation pipe, extraction liquid evaporation recovery system's solvent replenishment mouth links to each other with the n-hexane supply line, vertical evapo-separated machine's gaseous phase discharge port links to each other with extraction liquid evaporation recovery system's retrieval and utilization heat medium entry through retrieval and utilization heat medium pipe respectively, extraction liquid evaporation recovery system's crude oil delivery outlet links to each other with crude oil output tube. And (3) evaporating the concentrated extract liquid in the extract evaporation recovery system from a concentrated extract liquid inlet which is fed into the extract evaporation recovery system, discharging crude oil obtained by evaporation from a crude oil outlet, mixing recycled extract liquid obtained by evaporation with fresh n-hexane from the n-hexane supply pipe, discharging from a recycled solvent outlet, and feeding the mixed recycled extract liquid into a fresh solvent pipe for recycling. The raw steam is used as a main heat medium of the extraction liquid evaporation and recovery system, and the mixed steam discharged by the vertical evaporator is used as an auxiliary heat source, so that the extraction liquid can be preheated.

As a further improvement of the utility model, the powder leaching device comprises a rectangular box body, a plurality of parallel groove body clapboards are connected between the front wall board and the rear wall board of the box body, each groove body clapboard divides the inner cavity of the box body into a plurality of leaching tanks, the upper parts of each groove body clapboard are respectively provided with an overflow port, the overflow ports on the adjacent groove body clapboards are arranged in a staggered way in the front and rear direction, the height of each overflow port is gradually reduced from right to left, the discharge end of the right side leaching tank is connected with a leaching device new solution inlet, and the feed end of the left side leaching tank is connected with a leaching device 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 side, the discharging end of the right wall plate of the tank body is provided with a discharging chute extending upwards and rightwards, and the wet material outlet of the leacher is positioned at the upper end of the discharging chute; the bottom of each soaking groove is arc-shaped and is respectively provided with a soaking groove spiral, and the spiral directions of adjacent soaking grooves are opposite; and each guide chute is internally provided with a scraper lifting mechanism, and the discharge chute is internally provided with a scraper discharging mechanism. The material falls into the feed end of the leftmost soaking tank from the solid material inlet of the leacher, and the new solvent is sent into the new solvent inlet of the leacher by the new solvent pump and enters the rightmost soaking tank. The soaking and extracting processes are finished in the soaking tanks, and when the materials are pushed to the discharge ends of the soaking tanks, the materials are upwards fished out along the guide grooves, separated from the liquid level, and then drained by short drip to fall into the lower 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, fished out from the discharge end of the rightmost soaking tank along the discharge tank and discharged from a wet material outlet of the leacher, and then is sent out by a wet residue conveyor. The solid material and the solution always keep reverse flow, the material with the highest content contacts with the concentrated solution, the material with the lower content contacts with the dilute solution, the good osmotic pressure can be always kept, and the mass transfer efficiency is further improved. The solid material transversely advances along soaking the groove in turn, transversely advances after a section and is fished out and fall into fore-and-aft next-level soaking groove, obtains the stirring repeatedly, and material and solution all are the torrent state, can not appear laminar flow state, even the very little powder of void fraction also can be fully soaked by solution. The adjacent overflow ports are arranged in a staggered manner in the front and back directions, the solvent also flows in an S-shaped zigzag manner and is opposite to the advancing direction of the solid material, flows through the full length of each soaking tank, then flows into the next soaking tank by using potential difference overflow and turns back to flow through the full length of the soaking tank, the extraction stroke of the solid material and the solution is greatly prolonged, full extraction can be realized, and high-efficiency extraction is realized. The concentrated extract reaching the leftmost leaching tank is discharged from the concentrated liquor outlet of the leacher. The soaking liquid level is slightly higher than the solid phase, the solid and the liquid are mixed fully, the solvent consumption is low, the concentration of the obtained mixed liquid is high, and the energy consumption of evaporation separation is low. The bottom of the soaking groove is arc-shaped and is matched with the spiral of the soaking groove, so that dead zones at the bottom of the soaking groove can be avoided; the spiral of the soaking tank is responsible for conveying solid materials in the soaking tank and completing soaking extraction, the defect of insufficient mass transfer of the materials and the solvent in the simple soaking process is overcome through forced stirring of the spiral blades, and the spiral direction of the adjacent soaking tanks is opposite to make the materials advance in an S shape. The scraper lifting mechanism is used for fishing, draining and lifting the soaked solid materials for solid-liquid separation and solid-phase lifting; the scraper plate discharging mechanism is used for scooping up, draining and discharging the extracted solid materials. The spiral scraper can not only transport solid materials, but also stir the solid materials with strong force, the height of the material layer in the soaking box can be improved by more than one time, and the productivity in unit area is greatly improved; the extraction liquid naturally permeates from top to bottom, and is changed into spiral mechanical stirring, solid-liquid direct mixing immersion cleaning, the extraction power is large, and the extraction efficiency is high; the solvent amount that traditional leaching system participated in the circulation is 5 times of solid material, the utility model discloses well solid-liquid volume ratio is about 1.2-1.5 times, and initial throw solvent amount only has original quarter to third, saves a large amount of solvents greatly and the fund occupies.

As a further improvement of the utility model, at least one baffle plate extending along the left and right directions is respectively arranged in each soaking groove, and the lower end of each baffle plate is respectively clamped above the spiral of the soaking groove through the upper concave arc of the baffle plate. The baffle plate can prevent the short-circuit outflow of the surface solution without fully contacting with the solid material, the upper concave arc of the baffle plate is clamped above the spiral of the soaking tank to convey and provide a channel for the material, the solution is forced to pass through the notch of the upper concave arc of the baffle plate, the solid material and the extraction liquid are stirred, mixed and contacted, the two phases are fully contacted in a turbulent flow state, and the soaking effect of the material and the solution is further improved; the solid and the liquid are in turbulent contact under the stirring action, the liquid phase has no chromatography, and the concentrations of the same phases are consistent. The plurality of baffle plates enable the solvent to flow in an S shape in the vertical direction in each soaking tank, so that the short circuit phenomenon of the solvent is avoided, the extraction power is obviously increased, and the extraction efficiency is high.

As the utility model discloses a further improvement, the big sprocket of fretwork is installed respectively to the screw axis discharge end of each soaking groove spiral, and corresponding scraper blade hoist mechanism's promotion drive chain lower extreme meshing evenly is equipped with a plurality of promotion scraper blades on the promotion drive chain on the big sprocket of fretwork. Partial materials can enter the discharge end of the soaking groove through the hollow part of the hollow large chain wheel, so that the material receiving area of the lifting scraper is increased, and the conveying capacity of the lifting scraper is increased. Soak groove spiral and scraper blade hoist mechanism synchronous revolution, promote the material that the scraper blade will push and come and drag for, promote from the solution, fall into next soaking groove, promote the conveying capacity of scraper blade and be greater than soaking groove spiral, can ensure not to cause the putty.

As a further improvement of the utility model, the upper end of each lifting driving chain is engaged on a small lifting chain wheel, each small lifting chain wheel is respectively arranged on a driving shaft, each driving shaft is also respectively provided with a linkage chain wheel, two adjacent driving shafts form a group, and the two linkage chain wheels are connected by the linkage chain; and a lifting large chain wheel is arranged at the shaft end of one driving shaft and is in transmission connection with a main chain wheel of a driving speed reducer through a main chain. The main chain wheel of the driving speed reducer drives the lifting large chain wheel to rotate through the main chain, the lifting large chain wheel drives the lifting small chain wheel and the linkage chain wheel to rotate through the driving shaft, the linkage chain drives the other driving shaft and the lifting small chain wheel to synchronously rotate, the two lifting small chain wheels drive the lifting scraper to operate and the soaking groove to spirally rotate through the lifting driving chain respectively, one driving speed reducer simultaneously drives the two soaking groove spirals to push solid materials leftwards and rightwards, and simultaneously drives the two scraper lifting mechanisms to synchronously drag for the materials, drain and lift the solid materials.

As a further improvement, the spiral shaft of each soaking groove spiral is supported at both ends respectively in the spiral shaft bearing, and each spiral shaft bearing is fixed respectively at the center of circular shrouding, and each circular shrouding covers respectively and fixes in the outside of soaking groove both ends spiral mounting hole. Tear circular shrouding and spiral bearing frame open and can will soak the whole spiral of groove and take out from the spiral mounting hole, will soak the groove spiral and penetrate from the spiral mounting hole earlier during the installation, then cover circular shrouding and pass through the bolt fastening, install spiral bearing frame again and fix.

As a further improvement, the lower end of the discharge driving chain of the scraper discharge mechanism is meshed with the hollow large chain wheel, and a plurality of discharge scrapers are evenly arranged on the discharge driving chain. Partial materials can enter the discharge end of the rightmost soaking groove through the hollow part of the hollow large chain wheel, so that the material receiving area of the discharge scraper is increased, and the conveying capacity of the discharge scraper is improved. Soak groove spiral and scraper blade discharge mechanism synchronous revolution, the material that the ejection of compact scraper blade was come with the propelling movement is dragged for from solution, is promoted and is discharged the leacher, and the transport capacity of ejection of compact scraper blade is greater than soak groove spiral, can ensure not to cause the putty.

Drawings

The invention will be described in further detail with reference to the drawings and the detailed description, which are provided for reference and illustration purposes only and are not intended to limit the invention.

Fig. 1 is a flow chart of the oil cake extraction system of the utility model.

FIG. 2 is a front view of a powder extractor according to a first embodiment of 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 line B-B of 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 extractor box of fig. 2 with the top cover removed.

Fig. 9 is a perspective view of two adjacent steeping tanks of fig. 2.

Figure 10 is a perspective view of the leftmost infusion tank of figure 2.

Figure 11 is a perspective view of the filter cartridge of figure 10.

Fig. 12 is an enlarged view of a portion of the filter cartridge.

FIG. 13 is a schematic view of the second embodiment of the powder extractor of the present invention.

Fig. 14 is a top view of fig. 13.

In the figure: E0. a pulverizer; E1. a bucket elevator; E2. a horizontal conveyor; E3. temporarily storing the raw materials in a bin; E4. a quantitative auger; E5. a powder extractor; E6. a wet slag conveyor; E7. a primary hydrocyclone separator; E8. a secondary hydrocyclone separator; E9. a solution temporary storage tank; E10. a tail gas condenser; E11. an extract evaporation recovery system; e11a. a concentrated extract inlet; e11b. a recycled solvent outlet; ej11c. crude oil outlet; e 1d. primary refrigerant inlet; e11e. a recycling heating medium inlet; e11f. exhaust steam outlet; e11g. solvent make-up port; E12. a vertical evapo-separated machine; e12a. cake discharge valve; B1. a new solvent pump; B2. a concentrated extract liquid pump; B3. a temporary storage tank delivery 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. a normal hexane supply pipe; G7. a raw steam pipe; G8. recycling the heating medium pipe; q1. fresh solvent flow meter; q2. a thick solution flow meter; 1. a soaking tank; 1a, a solid material inlet of a leacher; 1a1. feed flow guide pipe; 1b, a wet material outlet of the leacher; 1c, a spiral mounting hole; 1d, a circular sealing plate; 1e, exhausting holes; 2. a tank body clapboard; 2a, an overflow port; 2b, a material guide groove; 2c, discharging a trough; 3. a baffle plate; 3a, a concave arc is arranged on the baffle plate; 4. the soaking groove is spiral; 4a screw shaft; 4b, main spiral sheets; 4c, hollowing out the large chain wheel; 4d, a spiral bearing seat; 4e, pushing the spiral right; 4f, left-pushing the helix; 5. a squeegee elevation mechanism; 5a, lifting a driving chain; 5b, lifting the scraper; 6. lifting the small chain wheel; 7. a drive shaft; 8. a link sprocket; 9. a linkage chain; 10. lifting the large chain wheel; 11. a main chain; 12. driving a speed reducer; 12a. a main sprocket; 13. a filter cartridge; grate bars; 13b, a filter cylinder outer helical band; 13c, a filter cartridge inner helical band; 14. a scraper plate discharging mechanism; 14a. a discharge drive chain; 14b, a discharge scraper; 15. a new solution inlet of the leacher; 16. and a concentrated solution 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 only for convenience of description and simplification of description, and do not mean that the device must have a specific orientation.

As shown in figure 1, the utility model discloses an oil cake extraction system includes rubbing crusher E0, bucket elevator E1, horizontal conveyor E2, raw materials temporary storage storehouse E3, ration auger E4, powder leacher E5 and wet residue conveyer E6, the export of raw materials temporary storage storehouse E3 links to each other with the entry of ration auger E4, the export of ration auger E4 links to each other with leacher solid material entry, leacher wet material export links to each other with wet residue conveyer E6's entry, wet residue conveyer E6's export links to each other with vertical evapo-separated machine E12's feed inlet, vertical evapo-separated machine E12's discharge gate is equipped with cake sediment bleeder valve E12a.

The inlet of a new solvent pump B1 is connected with a fresh solvent pipe G1, the outlet of a new solvent pump B1 is connected with a new dissolution inlet 15 of the leacher, the concentrated solution outlet 16 of the leacher is connected with the inlet of a concentrated solution extraction pump B2, the outlet of the concentrated solution extraction pump B2 is connected with the inlet of a primary hydrocyclone E7 through a mixed solution conveying pipe G2, the light phase outlet of the primary hydrocyclone E7 is connected with the inlet of a secondary hydrocyclone E8, the light phase outlet of the secondary hydrocyclone E8 is connected with the inlet of a solution temporary storage tank E9, and the bottom outlets of the primary hydrocyclone E7, the secondary hydrocyclone E8 and the temporary storage tank E9 are connected with the reflux port of a powder leacher E5.

Oil cakes such as tea seed cakes, rapeseed cakes and palm kernel pressed cakes are crushed by a crusher E0, lifted to a high position by a bucket elevator E1, then conveyed 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, directly convey the oil cakes into a solid material inlet of a leacher of a powder leacher E5 by the quantitative auger E4, extract in the powder leacher E5 by a one-pot stewing method, discharge extracted cake dregs from a wet material outlet of the leacher, convey the extracted cake dregs by a wet dreg conveyor E6, dry by a vertical desolventizer E12, and discharge the dried cake dregs from a cake dreg discharge valve E12a.

Fresh solvent is fed into the new dissolution inlet 15 of the extractor by a new solvent pump B1, and the oil cake is contacted with the solvent in a powder extractor E5 to complete extraction. A fresh solvent flow meter Q1 is installed on an outlet pipeline of the new solvent pump B1, an outlet of a solution temporary storage tank E9 is connected with an inlet of a temporary storage tank conveying pump B3 through a temporary storage tank output pipe G4, an outlet of a temporary storage tank conveying pump B3 is connected with a concentrated extract liquid inlet E11a of an extract evaporation and recovery system E11 through a concentrated solution flow meter Q2 and a temporary storage tank output pipe G4, and a recycled solvent outlet E11B of the extract evaporation and recovery system E11 is connected with an inlet of the fresh solvent pipe G1. The outlet of the buffer tank feed pump B3 is also connected to the return port of solution buffer tank E9 by buffer tank return line G3.

Concentrated solution containing certain powder particles is pumped by a concentrated extract pump B2, and then is sent to a primary hydrocyclone E7 for separation through a mixed solution conveying pipe G2, solid particles in the solution are removed for the first time, and then are removed again through a secondary hydrocyclone E8, and then enter 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 left second soaking tank, so that the particle concentration at a concentrated solution outlet 16 of the leacher is reduced.

The precipitated concentrated solution is discharged from an outlet of the solution temporary storage tank E9 through a temporary storage tank output pipe G4, and is conveyed to a concentrated extract inlet E11a of an extract evaporation recovery system E11 through a temporary storage tank conveying pump B3. During the initial system operation, the outlet solution from the holding tank transfer pump B3 may also be returned to solution holding tank E9 via holding tank return line G3. A fresh solvent flow meter Q1 may monitor the flow rate of fresh solvent and a rich solution flow meter Q2 may monitor the flow rate of the output rich solution.

A main heat medium inlet E11d of an extract evaporation recovery system E11 is connected with a raw steam pipe G7, a solvent supplement port E11G of the extract evaporation recovery system E11 is connected with a normal hexane supply pipe G6, a gas phase discharge port of a vertical evaporator E12 is respectively connected with a recycling heat medium inlet E11E of the extract evaporation recovery system E11 through a recycling heat medium pipe G8, and a crude oil output port E11c of the extract evaporation recovery system E11 is connected with a crude oil output pipe G5.

Concentrated extract is evaporated in an extract evaporation recovery system E11 from a concentrated extract inlet E11a of an extract evaporation recovery system E11, crude oil obtained by evaporation is discharged from a crude oil outlet E11c, recycled extract obtained by evaporation is mixed with fresh n-hexane from a n-hexane supply pipe G6, and then discharged from a recycled solvent outlet E11b and enters a fresh solvent pipe G1 for recycling. The raw steam is used as a main heat medium of an extraction liquid evaporation and recovery system E11, and the mixed steam discharged by the vertical evaporator E12 is used as an auxiliary heat source, so that the extraction liquid can be preheated.

As shown in fig. 1 to 14, the powder extractor E5 includes a rectangular box, the top of the box is provided with an exhaust hole 1E and a manhole, the exhaust hole 1E and the exhaust port of the solution temporary storage tank E9 are both connected with a tail gas condenser E10, the exhaust steam outlet E11f of the extract evaporation recovery system E11 is also connected with a tail gas condenser E10, and the ethanol gas is recycled after being condensed and recovered. A plurality of parallel tank body partition plates 2 are connected between the front wall plate and the rear wall plate of the tank body, the inner cavity of the tank body is divided into a plurality of soaking tanks 1 by each tank body partition plate 2, the upper parts of the tank body partition plates 2 are respectively provided with an overflow port 2a, the overflow ports 2a on the adjacent tank body partition plates 2 are arranged in a staggered manner in the front-rear direction, the heights of the overflow ports 2a are gradually reduced from right to left, the discharge end of the right soaking tank is connected with a new leaching device inlet 15, and the feed end of the left soaking tank is connected with a leaching device concentrated solution outlet 16; a solid material inlet 1a of the leacher is arranged above the feeding end of the leftmost soaking tank, a guide chute 2b for lifting and turning materials to the right side is respectively arranged at the discharging end of each tank body clapboard 2, and a discharging chute 2c extending upwards to the right side is arranged at the discharging end of the right wall plate of the box body.

The bottom of each soaking tank 1 is arc-shaped and is respectively provided with a soaking tank spiral 4, the rotating directions of the adjacent soaking tank spirals 4 are opposite, and a left push spiral 4f is arranged in an odd number of tanks from a solid material inlet 1a of the solid material leacher to push the solid material to the front side wall direction of the powder leacher; and a right pushing screw 4e is arranged in the even number of grooves and pushes the solid materials to the direction of the rear side wall of the powder extractor. Each guide chute 2b is provided with a scraper lifting mechanism 5, and the discharge chute 2c is provided with a scraper discharging mechanism 14.

The material enters the feed 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 extraction processes are completed in the soaking tanks 1, and when the materials are pushed to the discharge ends of the soaking tanks 1 by the soaking tank spiral 4, the materials are upwards fished out by the scraper lifting mechanism 5 along the guide groove 2b, separated from the liquid level, and then are drained by short drip to fall into the lower 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 the solid material is fished out from the discharge end of the rightmost soaking tank along the discharge groove 2c by the scraper discharge mechanism 14 and discharged out of the machine from the wet material outlet 1b of the leacher. The solid material and the solution always keep reverse flow, the material with the highest content contacts with the concentrated solution, the material with the lower content contacts with the dilute solution, the good osmotic pressure can be always kept, and the mass transfer efficiency is further improved. The solid material transversely advances along soaking groove 1 in turn, transversely advances after a section and is fished out and fall into fore-and-aft next-level soaking groove, obtains the stirring repeatedly, and material and solution all are the torrent state, can not appear laminar flow state, even the very little powder of void fraction also can be fully soaked by solution. The adjacent overflow ports 2a are arranged in a staggered manner in the front and back directions, the solvent also flows in an S-shaped zigzag manner and is opposite to the advancing direction of the solid material, flows through the full length of each soaking tank 1, then flows into the next soaking tank by using potential difference overflow and turns back the full length of the soaking tank, the extraction stroke of the solid material and the solution is greatly prolonged, full extraction can be realized, and high-efficiency extraction is realized. The concentrate reaching the leftmost leach tank is discharged from the leach concentrate outlet 16. The soaking liquid level is slightly higher than the solid phase, the solid and the liquid are mixed fully, the solvent consumption is low, the concentration of the obtained mixed liquid is high, and the energy consumption of evaporation separation is low.

The bottom of the soaking tank 1 is arc-shaped and is matched with the spiral 4 of the soaking tank, so that dead zones at the bottom of the tank can be avoided; soaking groove spiral 4 is responsible for the transport of solid material in soaking groove 1 and accomplishes and soak the extraction, through helical blade 'S compulsory stirring, avoids simply soaking the insufficient defect of in-process material and solvent mass transfer, and adjacent soaking groove spiral 4' S the opposite direction of turning makes the material be the S-shaped and gos forward. The scraper lifting mechanism 5 is used for fishing, draining and lifting the soaked solid materials for solid-liquid separation and solid-phase lifting; the scraper discharge mechanism 14 is used for scooping up, draining and discharging the extracted solid materials. The spiral scraper not only can transport solid materials, but also can stir the solid materials strongly.

As shown in fig. 8, each immersion tank 1 is provided with at least one baffle plate 3 extending in the left-right direction, and the lower end of each baffle plate 3 is clamped above the spiral of the immersion tank by a baffle plate upper concave arc 3a. The baffle plate 3 can prevent the surface solution from short-circuit outflow without fully contacting with the solid material, the upper concave arc 3a of the baffle plate is clamped above the spiral 4 of the soaking tank to convey and provide a channel for the material, the solution is forced to pass through the gap of the upper concave arc 3a of the baffle plate, the solid material and the extraction liquid are stirred, mixed and contacted, the two phases are fully contacted in a turbulent state, and the soaking effect of the material and the solution is further improved; the solid and the liquid are in turbulent contact under the stirring action, the liquid phase has no chromatography, and the concentrations of the same phases are consistent. The plurality of baffle plates 3 enable the solvent to flow in an S shape in the vertical direction in each soaking tank 1, thereby avoiding the short circuit phenomenon of the solvent, obviously increasing the extraction power and having high extraction efficiency.

As shown in fig. 9, a hollow large chain wheel 4c is respectively installed at the discharge end of the screw shaft of each soaking tank screw 4, the lower end of the lifting drive chain 5a of the corresponding scraper lifting mechanism 5 is engaged with the hollow large chain wheel 4c, and a plurality of lifting scrapers 5b are uniformly arranged on the lifting drive chain 5a. Partial materials can enter the discharge end of the soaking groove through the hollow part of the hollow 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 increased. Soak groove spiral 4 and 5 synchronous revolutions of scraper blade hoist mechanism, promote material that scraper blade 5b comes with the propelling movement and drag for from solution, promote, fall into next and soak the groove, promote scraper blade 5 b's conveying capacity and be greater than and soak groove spiral 4, can ensure not to cause the putty.

The upper end of each lifting driving chain 5a is meshed with a small lifting chain wheel 6, each small lifting chain wheel 6 is respectively arranged on a driving shaft 7, each driving shaft 7 is also respectively provided with a linkage chain wheel 8, two adjacent driving shafts 7 form a group, and the two linkage chain wheels 8 are in transmission connection through a linkage chain 9; the shaft end of one of the driving shafts 7 is provided with a lifting large chain wheel 10, and the lifting large chain wheel 10 is in transmission connection with a main chain wheel 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 drive the lifting scraper 5b to operate and the dipping groove screw 4 to rotate through the lifting driving chain 5a respectively, the driving speed reducer 12 simultaneously drives the two dipping groove screws 4 to push solid materials leftwards and rightwards, and simultaneously drives the two scraper lifting mechanisms 5 to synchronously drag the materials, drain and lift the solid materials.

Both ends of a spiral shaft 4a of each soaking groove spiral 4 are respectively supported in spiral shaft bearing blocks 4d, each spiral shaft bearing block 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 spiral mounting holes 1c at both ends of the soaking groove. Tear circular shrouding 1d and screw bearing 4d down and can take out soaking groove spiral 4 is whole from spiral mounting hole 1c, during the installation earlier penetrates soaking groove spiral 4 from spiral mounting hole 1c, then covers circular shrouding 1d and passes through the bolt fastening, installs screw bearing 4d again and fixes.

The lower end of a discharge driving chain 14a of the scraper discharge mechanism 14 is meshed with the large hollow chain wheel 4c, and a plurality of discharge scrapers 14b are uniformly arranged on the discharge driving chain 14a. Partial materials can enter the discharge end of the rightmost soaking groove through the hollow part of the hollow large chain wheel 4c, so that the receiving area of the discharge scraper 14b is enlarged, and the conveying capacity of the discharge scraper 14b is improved. Soak groove spiral 4 and scraper blade discharge mechanism 14 synchronous revolution, ejection of compact scraper blade 14b with the material that the propelling movement was come drag for from solution, promote and discharge powder leaches the ware, ejection of compact scraper blade 14 b's transport capacity is greater than soak groove spiral 4, can ensure not to cause the putty.

As shown in fig. 10 to 12, each immersion groove screw 4 comprises a screw shaft 4a and a main screw plate 4b wound on the periphery of the screw shaft, a filter cartridge 13 is installed at the feed end of the leftmost screw shaft below the solid material inlet 1a of the extractor, the port of one side of the filter cartridge 13 facing the main screw plate 4b is closed, the other side of the filter cartridge 13 is open, the concentrated solution outlet 16 of the extractor is inserted into the inner cavity of the filter cartridge 13, a plurality of axially extending grid bars 13a are uniformly distributed on the circumference of the filter cartridge 13, and the gap between the adjacent grid bars 13a is narrow outside and wide inside. The powder is filtered by the filter cylinder 13 before flowing out, and the powder is retained on the outer surface of the filter cylinder 13, so that the content of powdery solid in the concentrated extract is reduced as much as possible, and the subsequent separation and evaporation of the rotary liquid are guaranteed; the concentrated extract liquid in the solid-liquid intermixing medium enters the concentrated liquid outlet 16 of the leacher to flow out after being continuously and stably filtered, and the filtered concentrated extract liquid can be stably and continuously filtered and conveyed without causing the blockage of a liquid outlet pipe valve so as to enter a rotary liquid separation system for fine filtration. Once the powder material crosses the gap at the outermost side of the filter cylinder 13, the powder material can smoothly fall into the bottom of the filter cylinder 13 and is pushed out by a spiral belt 13c in the filter cylinder for self-cleaning; avoiding the powder particles from being blocked in the gaps between the adjacent grate bars 13a and influencing the filtering capacity.

The outer periphery of the bowl 13 is wound with a bowl outer helical band 13b, and the direction of rotation of the bowl outer helical band 13b is the same as that of the coaxial main helical blade 4b. The filter cylinder outer spiral belt 13b can push out the solid materials flowing along with the liquid to one side where the main spiral sheet 4b is located, so that excessive materials are prevented from being deposited outside the filter cylinder 13.

The inner wall of the filter cylinder 13 is provided with a filter cylinder inner spiral belt 13c, and the spiral direction of the filter cylinder inner spiral belt 13c is opposite to the coaxial main spiral sheet 4b. A small amount of solid powder enters the filter cylinder 13 along with the extraction liquid and settles on the lower part of the inner wall of the filter cylinder 13, and the inner spiral belt 13c which is opposite to the rotation direction of the main spiral plate 4b pushes the settled matters out of the filter cylinder 13 from the open end and then out of the filter section by the outer spiral belt 13b of the filter cylinder, thereby completing the self-cleaning process of the filter cylinder 13. Therefore, stable and reliable continuous filtration is realized, the oil cake extraction system has a complete process, the problem of separation of high-powder materials from liquid is solved, and the oil cake extraction system has wide adaptability to various oil materials.

As shown in fig. 2 and 7, the solid inlet 1a of the extractor may be disposed at the left portion of the top cover of the tank, and a feeding guide pipe 1a1 is connected below the solid inlet 1a of the extractor to guide the fresh solid to the front side of the filter cartridge 13.

As shown in fig. 13 and 14, the extractor solid inlet 1a may be provided at the upper portion of the left side wall of the housing, and may be located at the front side of the filter cartridge 13 at a position in the front-rear direction. The right side of the soaking tank has the highest liquid level and overflows to the left side in sequence. In FIG. 14, the large arrows indicate the solid material flow direction, the small arrows indicate the solution flow direction, and the whole process is in a reverse flow direction.

The utility model discloses a leaching of "a pot is stewed" formula, it is high-efficient and reliable, can be used to leaching of powdery material and high powder degree material. The method can solve the bottleneck of oil production by extraction of oil cake, and overcome the problems of poor material permeability, easy dissolution and blockage of grid plates, shallow leaching material layer, large equipment investment, low production efficiency, high system failure rate and the like. To the likepowder leftover bits and pieces that can't handle in traditional leaching process, like high powder degree oil cake, the popped powder of semi-degeneration, can adopt the utility model discloses an oil cake extraction system refines the grease behind this type of property material extraction, can promote the economic value of this type of material by a wide margin, promotes enterprise economic benefits and market competition.

The above description is only a preferred embodiment of the present invention, and not intended to limit the scope of the present invention. In addition to the above embodiments, the present invention may have other embodiments. All the technical solutions formed by adopting equivalent substitutions or equivalent transformations fall within the protection scope claimed by the present invention. The undescribed technical features of the present invention can be realized by or using the prior art, and are not described herein again.

Claims (8)

1. The utility model provides an oil cake extraction system, including the raw materials storehouse of keeping in temporarily, the ration auger, powder leaches ware and wet sediment conveyer, the export in the raw materials storehouse of keeping in temporarily links to each other with the entry of ration auger, the export of ration auger links to each other with the solid material entry of leacher, the wet material export of leacher links to each other with the entry of wet sediment conveyer, 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 the new inlet that dissolves of leacher, the concentrated solution export of leacher links to each other with the entry of concentrated extract pump, its characterized in that: the outlet of the concentrated extract liquid extraction pump is connected with the inlet of the primary hydrocyclone separator through a mixed liquid conveying pipe, the light phase outlet of the primary hydrocyclone separator is connected with the inlet of the secondary hydrocyclone separator, and the light phase outlet of the secondary hydrocyclone separator 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 the reflux port of the solution temporary storage tank and the concentrated extract inlet of an extract evaporation and recovery system, and the recycled solvent outlet of the extract evaporation and 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 type desolventizer-toaster, and the discharge outlet of the vertical type desolventizer-toaster is provided with a cake slag discharge valve.

2. An oil cake extraction system as claimed 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 supplement port of the extraction liquid evaporation recovery system is connected with a normal hexane supply pipe, the gas phase discharge port of the vertical type evaporator is connected with the recycling heat medium inlet of the extraction liquid evaporation recovery system through a recycling heat medium pipe, 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 claimed in claim 1, wherein: the powder leacher comprises a rectangular box body, wherein a plurality of parallel groove body partition plates are connected between the front wall plate and the rear wall plate of the box body, each groove body partition plate divides the inner cavity of the box body into a plurality of soaking grooves, the upper part of each groove body partition plate is respectively provided with an overflow port, the overflow ports on the adjacent groove body partition plates 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 rightmost soaking groove is connected with a new leaching device dissolving inlet, and the feed end of the leftmost soaking groove is connected with a concentrated solution outlet of the leacher; 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 side, the discharging end of the right wall plate of the tank body is provided with a discharging chute extending upwards and rightwards, and the wet material outlet of the leacher is positioned at the upper end of the discharging chute; the bottom of each soaking groove is arc-shaped and is respectively provided with a soaking groove spiral, and the spiral directions of adjacent soaking grooves are opposite; and each guide chute is internally provided with a scraper lifting mechanism, and the discharge chute is internally provided with a scraper discharging mechanism.

4. An oil cake extraction system as claimed in claim 3, wherein: at least one baffle plate extending along the left and right directions is respectively arranged in each soaking groove, and the lower end of each baffle plate is respectively clamped above the spiral of the soaking groove through the upper concave arc of the baffle plate.

5. An oil cake extraction system as claimed in claim 3, wherein: the discharge ends of the spiral shafts of the soaking grooves are respectively provided with a hollow large chain wheel, the lower ends of the lifting drive chains of the corresponding scraper lifting mechanisms are meshed with the hollow large chain wheels, and a plurality of lifting scrapers are uniformly arranged on the lifting drive chains.

6. An oil cake extraction system as claimed in claim 5, wherein: the upper end of each lifting driving chain is meshed with a small lifting chain wheel, each small lifting chain wheel is respectively arranged on a driving shaft, each driving shaft is also respectively provided with a linkage chain wheel, two adjacent driving shafts form a group, and the two linkage chain wheels are in transmission connection through the linkage chain; and a lifting large chain wheel is arranged at the shaft end of one driving shaft and is in transmission connection with a main chain wheel of a driving speed reducer through a main chain.

7. An oil cake extraction system as claimed in claim 3, wherein: the two ends of the spiral shaft of each soaking groove spiral are respectively supported in the spiral shaft bearing seats, each spiral bearing seat is respectively fixed at the center of the circular sealing plate, and each circular sealing plate respectively covers and is fixed at the outer sides of the spiral mounting holes at the two ends of the soaking groove.

8. An oil cake extraction system as claimed in claim 5, wherein: the lower end of a discharge driving chain of the scraper discharge mechanism is meshed with the hollow large chain wheel, and a plurality of discharge scrapers are uniformly arranged on the discharge driving chain.