CN105028892A - Bean pulp low-temperature desolventizing system - Google Patents
Bean pulp low-temperature desolventizing system Download PDFInfo
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- CN105028892A CN105028892A CN201510491606.4A CN201510491606A CN105028892A CN 105028892 A CN105028892 A CN 105028892A CN 201510491606 A CN201510491606 A CN 201510491606A CN 105028892 A CN105028892 A CN 105028892A
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Abstract
The invention relates to a bean pulp low-temperature desolventizing system. A flash vacuum desolventizing machine is sequentially provided with a flash desolventizing section, a vacuum desolventizing section and a drying and cooling layer from top to bottom; the flash desolventizing section is provided with a solvent vapor inlet and a solvent vapor outlet, a steam jet vacuum pump is mounted on the upper part of a barrel of the vacuum desolventizing section, and the circumferential wall of the drying and cooling layer is provided with a cooling air inlet and a cooling air outlet; the solvent vapor outlet is connected with the air inlet of a solvent vapor cyclone, a bottom discharge hole of the solvent vapor cyclone is connected with the main inlet of a dust collection packing auger by means of an air blocking rotary valve, an outlet of the dust collection packing auger is connected with the upper part of the vacuum desolventizing section, an air outlet of the solvent vapor cyclone is connected with the air inlet of a dissolved steam wet collector, an air outlet of the dissolved steam wet collector is connected with the suction port of a dissolved steam fan, an outlet of the dissolved steam fan is connected with the tube pass inlet of a dissolved steam overheater, and the tube pass outlet of the dissolved steam overheater is connected with an solvent steam inlet. The system is great in output, high in production efficiency and low in energy consumption.
Description
Technical field
The present invention relates to a kind of edible bean cake process equipment, particularly relate to a kind of low temperature desolventizing system of dregs of beans.
Background technology
Containing very abundant phytoprotein in crude soya bean, wherein the highest with water-soluble protein content.Due to the easy heated denaturalization of protein, thus greatly reduce the use value of Soybean Meal.Carrying out low temperature desolventizing under lower than the denaturation temperature (80 DEG C) of protein can make the water-solubility protein in dregs of beans retain higher content.Low temperature desolventizing dregs of beans is commonly called as the important intermediate products that white peas or beans sheet is processing and eating soybean protein, can be made into various soy protein products through deep processing, as protein concentrate, protein isolate, histone and other functional soy albumen.Low temperature desolventizing can remove solvent the most up hill and dale, reduces production cost by recycling design, can also make the content that the water soluble protein in dregs of beans keeps higher.White peas or beans sheet is good with higher NSI (nitrogen solubility index) and complete laminated structure, the lower index such as residual molten, otherwise, lower with NSI, laminated structure destroyed, high, the residual molten height of fines content is bad.
Existing low temperature desolventizing technique is A, B cylinder precipitation, and wherein A cylinder is pre-precipitation, and the solvent (n-hexane) of 95-99% in the wet dregs of rice can be removed, B cylinder is whole precipitation, solvent strength can be down to 1200-1500ppm, is roughly equal to white peas or beans sheet 1.2-1.5kg solvent per ton.After quoad hoc, be difficult to reduce further containing molten amount in white peas or beans sheet, mainly B cylinder internal solvent steam is saturation state, solvent is caused to evaporate not thorough, white peas or beans sheet is bulk material simultaneously, and between sheet, gap is large, can hold 3kg air or 2.1 cubic metres of air between white peas or beans sheet gap per ton, if white peas or beans sheet is full of solvent vapo(u)r between gap, 8.0kg/ ton material can be reached.Process 1 ton of soybean in the industry at present, molten consumption, at 6-7kg, calculates by 1 ton of Soybean production, 0.7 ton of white peas or beans sheet, processes 1 ton of molten consumption of white peas or beans sheet and be about 8.6-10Kg, with coincideing of calculating above.
There is following weak point in traditional desolventizing machine: 1. precipitation chamber only has two, A cylinder and B cylinder airtight chamber internal solvent steam are difficult to form concentration gradient, barrel diameter is large, the solvent vapour that temperature is higher, density is less is easily along top area short-circuit cycle, not and fully heat exchange just discharges heat exchange chamber, causes precipitation not thorough; Residual molten height from the white peas or beans sheet that B cylinder is discharged, cannot reclaim containing a large amount of solvent vapo(u)r in white peas or beans sheet space, can only diffuse to air.
2. solvent stream can only contact with top layer material and the material kicked up, and most of solid accumulation, at cylinder body bottom, has no chance heat exchange; De-wet cake is deposited in cylinder body bottom, and bulk density is large, and material is mutually sheared, extruded under action of forced stirring, causes fines content to increase, and uses item matter and declines.
3. white peas or beans sheet drop temperature is at 60-62 DEG C, is rich in steam, and easily condensation forms water caking, and causes fines content in course of conveying to increase, and causes certified products yield to reduce.
4. the heat time is long, and in A, B cylinder, the heat time amounts up to 25-30 minute, is heated for a long time and causes soluble protein content to reduce, and uses item matter and declines.
5. level of integrated system is not high, individual equipment function singleness, and A, B cylinder low temperature desolventizing technique is shaped, is difficult to improve promote.
Increase C cylinder further precipitation if improve, solvent recovery amount can be increased, reduce molten consumption, but white peas or beans sheet fines content, NSI(nitrogen solubility index) etc. key index can reduce, product quality declines, and causes economic well-being of workers and staff to reduce.In addition, equipment, place investment can be increased, increase operating cost and production cost, so the necessity increasing C cylinder is inappropriate from income.Under the prerequisite ensureing product quality, effectively reducing the crucial costs such as the molten consumption of white peas or beans sheet, is problem demanding prompt solution in the industry.
Summary of the invention
The object of the invention is to, overcome problems of the prior art, provide a kind of low temperature desolventizing system of dregs of beans, integration degree is high, and operating cost is low.
For solving above technical problem, the low temperature desolventizing system of a kind of dregs of beans of the present invention, comprise flash vacuum desolventizing machine, the vertical cylinder top of described flash vacuum desolventizing machine is provided with combined feed mouth, the inner chamber of described cylindrical shell is provided with flash distillation precipitation section from top to bottom successively, vacuum desolvation section and dry cooling layer, described flash distillation precipitation section is provided with solvent vapo(u)r entrance and solvent vapo(u)r outlet, the cylindrical shell top of described vacuum desolvation section is provided with the steam jet vavuum pump of outwards bleeding, the bottom of described dry cooling layer is provided with total discharging opening, the circumferential wall of described dry cooling layer is provided with cooling air import and cooling air outlet, described solvent vapo(u)r outlet is connected with the air inlet of solvent vapo(u)r cyclone, the bottom discharging mouth of described solvent vapo(u)r cyclone is connected with the main-inlet of dust collection auger by lock cyclone rotary valve, the outlet of described dust collection auger is connected with the top of described vacuum desolvation section, the top outlet inlet of described solvent vapo(u)r cyclone is connected with the air inlet of molten vapour wet trap, the top outlet inlet of described molten vapour wet trap is connected with the suction inlet of molten vapour blower fan, the outlet of described molten vapour blower fan is connected with the tube side import of molten vapour superheater, the tube side outlet of described molten vapour superheater is connected with described solvent vapo(u)r entrance, the shell side import of described molten vapour superheater is connected with water vapour pipeline, and the shell-side outlet of described molten vapour superheater is connected with condensate pipe by drain valve.
Relative to prior art, the present invention achieves following beneficial effect: under the suction of molten vapour blower fan, first 75 DEG C of solvent vapo(u)rs that the flash distillation precipitation section of flash vacuum desolventizing machine is discharged enter solvent vapo(u)r cyclone, cyclonic separation solid dregs of rice end, the last bottom discharging mouth from solvent vapo(u)r cyclone of the solid dregs of rice enters the main-inlet of dust collection auger by lock cyclone rotary valve, solid dregs of rice end is sent into vacuum desolvation section and proceeded vacuum desolvation by dust collection auger; Then solvent vapo(u)r continues to enter in molten vapour wet trap and washs, little power in solvent vapo(u)r is captured, clean solvent vapo(u)r enters molten vapour superheater after molten vapour blower fan accelerates, in molten vapour superheater, solvent vapo(u)r walks tube side, water vapour walks the overheated solvent vapo(u)r that solvent vapo(u)r is heated as 150-160 DEG C by shell side, the flash distillation precipitation section of flash vacuum desolventizing machine is reentered from solvent vapo(u)r entrance, circulation like this, solvent vapo(u)r not only can be all recovered, and can UTILIZATION OF VESIDUAL HEAT IN.
As improvement of the present invention, the top of described molten vapour wet trap is provided with heat water-spraying's pipe, the bottom discharge mouth of described molten vapour wet trap is connected with the top entry of wastewater boilling tank, the middle part delivery port of described wastewater boilling tank is connected with the entrance of circulating pump, and described circulation delivery side of pump is connected with the entrance of heat water-spraying's pipe of described molten vapour wet trap; The lower circumference of described wastewater boilling tank is connected with water vapour pipeline, and the top vent of described wastewater boilling tank is connected with exhaust gas recovery system.Heat water-spraying's pipe on molten vapour wet trap top sprays 90 DEG C of hot water continuously, traps on the one hand, make solvent remain on gaseous state on the other hand, prevent solvent to run off dust; Hot water temperature after trapping dust decreases, wastewater boilling tank is entered from the bottom discharge mouth of molten vapour wet trap, in wastewater boilling tank, water vapour is by hot water heating to 90 DEG C, circulating pump is entered from the middle part delivery port of wastewater boilling tank, heat water-spraying's pipe that hot water is sent back to molten vapour wet trap by circulating pump carries out circulated sprinkling, and hot water and the heat that contains thereof are all reclaimed.After the dust in wastewater boilling tank reaches some, can be discharged by the sewage draining exit of bottom.
As a further improvement on the present invention, the outlet of described molten vapour blower fan is also connected with the shell side inlet of 1st effective evaporator, and the shell-side outlet of described 1st effective evaporator is connected with the entrance of atmospheric condenser; The bottom tube-side inlet of described 1st effective evaporator is connected with low concentration mixing oil pipe, the top of described 1st effective evaporator is connected with an effect vaporization chamber, a described effect top for vaporization chamber is connected with the entrance of vacuum condenser, and the bottom and of a described effect vaporization chamber is imitated concentrated blend pipe and is connected.Clean solvent vapo(u)r after solvent vapo(u)r cyclone and the dedusting of molten vapour wet trap, after molten vapour blower fan accelerates, some enters 1st effective evaporator, in 1st effective evaporator, the miscella of oil-containing 25% enters the bringing-up section tube side of 1st effective evaporator from low concentration mixing oil pipe and upwards flows, solvent vapo(u)r enters the bringing-up section shell side of 1st effective evaporator, enters atmospheric condenser continue condensation to the shell-side outlet from 1st effective evaporator after miscella heat release; Miscella is heated an effect vaporization chamber on rear arrival 1st effective evaporator top, and moisture evaporates in a large number and enters vacuum condenser from the top of an effect vaporization chamber, and the miscella of oil-containing 50% is discharged from an effect concentrated blend pipe.
As a further improvement on the present invention, described steam jet vacuum delivery side of pump is connected with the air inlet of mist cyclone, the bottom discharging mouth of described mist cyclone is connected with the auxiliary entrance of described dust collection auger by lock cyclone rotary valve, the top outlet inlet of described mist cyclone is connected with the air inlet of gaseous mixture wet trap, the outlet at bottom of described gaseous mixture wet trap is connected with the top entry of described wastewater boilling tank, the described top outlet inlet of gaseous mixture wet trap is connected with the shell side inlet of oil preheater, the shell-side outlet of described oil preheater is connected with described exhaust gas recovery system, the outlet of a described effect concentrated blend pipe is connected with the tube-side inlet of described oil preheater, and the tube side outlet of described oil preheater is connected with the bottom tube-side inlet of 2nd effect evaporator.First the 90 DEG C of water vapours extracted out from steam jet vacuum delivery side of pump and a small amount of solvent vapo(u)r enter mist cyclone, cyclonic separation solid dregs of rice end, the last bottom discharging mouth from mist cyclone of the solid dregs of rice enters the auxiliary entrance of dust collection auger by lock cyclone rotary valve, solid dregs of rice end is sent into vacuum desolvation section and proceeded vacuum desolvation by dust collection auger; Then mist continues to enter gaseous mixture wet trap and washs, and the little power in gaseous mixture is captured, and the shell side that clean gaseous mixture enters oil preheater heats miscella, reclaims heat; Imitate the miscella of the oil-containing 50% that concentrated blend pipe flows out after oil preheater heating from one, carry out 2nd effect evaporator and continue evaporation and concentration.
As a further improvement on the present invention, total discharging opening of described flash vacuum desolventizing machine is connected with the main charging aperture of finished product dregs of rice drag conveyor; The cooling air outlet of described flash vacuum desolventizing machine is connected with the air inlet of cooling air cyclone, and the bottom discharge mouth of described cooling air cyclone is connected with the auxiliary charging aperture of described finished product dregs of rice drag conveyor by lock cyclone rotary valve.The cooling air of discharging from cooling air outlet enters cooling air cyclone, cyclonic separation solid dregs of rice end, and the last bottom discharging mouth from cooling air cyclone of the solid dregs of rice enters the auxiliary charging aperture of finished product dregs of rice drag conveyor by lock cyclone rotary valve.
As a further improvement on the present invention, the flash distillation precipitation section of described flash vacuum desolventizing machine comprises upper and lower two-layer flash distillation precipitation layer, described cylindrical shell level is cut off by the chassis of each described flash distillation precipitation layer respectively, solvent vapo(u)r interlayer is respectively equipped with below the chassis of each described flash distillation precipitation layer, the sidewall of described solvent vapo(u)r interlayer is connected to described solvent vapo(u)r entrance, the chassis of each described flash distillation precipitation layer is evenly distributed with solvent vapo(u)r spray orifice, and the upper portion side wall of each described flash distillation precipitation layer is respectively equipped with the outlet of described solvent vapo(u)r; Be arranged with respectively above the chassis of each flash distillation precipitation layer and material is evenly spread out the flash distillation precipitation layer stirring wing of cloth on chassis; The chassis of upper flash distillation precipitation layer is radially provided with the flash distillation precipitation layer discharge gate of downward flash distillation precipitation layer discharge, described flash distillation precipitation layer discharge gate place is provided with middle rotary valve; The bottom sidewall of lower flash distillation precipitation layer is provided with flash distillation precipitation section discharging opening.Containing molten 30%, temperature 50 C
high containing wet cakefirst fall on the chassis of flash distillation precipitation layer, the overheated solvent vapo(u)r of 150-160 DEG C enters solvent vapo(u)r interlayer from solvent vapo(u)r entrance, upwards spray from each solvent vapo(u)r spray orifice chassis with the speed of 30-36m/s, enter high containing in the space of wet cake to flow with the speed of 15-20m/s, with height containing wet cake direct contact heat transfer, thickness of feed layer 600-700mm, under the stirring action of ejection of solvent steam and flash distillation precipitation layer stirring wing, the high wet cake that contains is in fluidisation state or half fluidisation state, with solvent vapo(u)r forced-convection heat transfer, make to be down to less than 15% containing molten, become
low containing the molten dregs of rice, the solvent vapo(u)r of 75 DEG C is discharged from solvent vapo(u)r outlet.Then material enters lower flash distillation precipitation layer through middle rotary valve, and the overheated solvent vapo(u)r continuing to enter with injection carries out forced-convection heat transfer, and make to be down to less than 1% containing molten, but vaporize not yet completely in conjunction with state solvent, flash distillation precipitation dregs of rice temperature rises to 80-85 DEG C, becomes
the middle temperature dregs of rice, discharge from flash distillation precipitation section discharging opening and enter vacuum desolvation section.
As a further improvement on the present invention, described vacuum desolvation section comprises stacked successively multi-layer vacuum precipitation layer from top to bottom, and the chassis of each described vacuum desolvation layer is followed successively by big disk from top to bottom, roundel interval arranges and the chassis of the two-layer vacuum desolvation layer of bottom is big disk; The periphery of each described big disk is connected on the inwall of described cylindrical shell, leaves gap between the periphery of each described roundel and the inwall of described cylindrical shell; Be respectively equipped with steam heating interlayer below the chassis of each described vacuum desolvation layer, the diapire of each described steam heating interlayer is connected to steam entry pipe and drip pipe; The top of each layer big disk except bottom is arranged with the centripetal flight carried by outer circumferential axle center by material respectively, and the axle center place of each layer big disk except bottom is respectively equipped with the vacuum desolvation layer discharge gate to lower floor's discharge; The top of bottom big disk and each layer roundel is arranged with the centrifugal flight carried to periphery by axle center by material respectively; The top of top layer vacuum desolvation layer is circumferentially provided with vacuum orifice and vacuum desolvation section feeding mouth, described vacuum orifice place is provided with described steam jet vavuum pump, described flash distillation precipitation section discharging opening with lock cyclone rotary valve by first between described vacuum desolvation section feeding mouth and be connected; Be provided with live (open) steam jet pipe in the cavity space of bottom vacuum desolvation layer, the bottom sidewall of bottom vacuum desolvation layer is provided with vacuum desolvation section discharging opening.Vacuum orifice continues suction makes vacuum desolvation section negative pressure,
the middle temperature dregs of riceenter vacuum desolvation section feeding mouth by the first lock cyclone rotary valve and fall on the excircle of the big disk of top layer vacuum desolvation layer, centripetal flight does centripetal screw motion, material is spread out cloth also to shift to circle centre position gradually on big disk, material and steam heating interlayer indirect heat exchange in the process, stirring of flight makes material thermally equivalent, and under certain vacuum degree, continue evaporation in conjunction with state solvent.Material on big disk falls into the center of the roundel of lower floor from the vacuum desolvation layer discharge gate of circle centre position, centrifugal flight does centrifugal screw motion, material is spread out cloth also to move to outer planet gradually on roundel, material and the further indirect heat exchange of steam heating interlayer in the process, then material falls to lower one deck big disk from the periphery of roundel.Circulation like this, until material drops on the center of bottom vacuum desolvation layer.At bottom vacuum desolvation layer, live (open) steam jet pipe sprays into appropriate superheated vapour in bottom chamber, superheated vapour upwards with dregs of beans reverse flow, solvent vapo(u)r in dregs of beans gap is diluted, dividing potential drop reduces, promote to evaporate further from embryo sheet tissue in conjunction with state solvent, spread, realize very brief stripping.Spray into the negative pressure that water vapour amount must control make vacuum desolvation section maintain-2000 ~-3000mm water column, prevent wetting+hot two conditions occur simultaneously, under the prerequisite of precipitation of remaining valid, prevent white peas or beans sheet generation thermal denaturation.Material is under the promotion of the centrifugal flight of bottom, and continue and steam heating interlayer indirect heat exchange, the solvent in white peas or beans sheet and moisture are able to rapid evaporation, and solvent strength is down to below 1000ppm, and the precipitation dregs of rice generating 60 DEG C ~ 65 DEG C are discharged from vacuum desolvation section discharging opening.
As a further improvement on the present invention, air blanketing is provided with below the chassis of described dry cooling layer, described air blanketing be circumferentially connected with described cooling air import, described dry cooling layer chassis on be evenly distributed with air jet orifices, the upper portion side wall of described dry cooling layer is provided with described cooling air outlet; The top of described dry cooling layer is circumferentially provided with dry cooling layer charging aperture, locks cyclone rotary valve be connected between described dry cooling layer charging aperture with described vacuum desolvation section discharging opening by second; Be arranged with respectively above the chassis of described dry cooling layer and material is evenly spread out the dry cooling layer stirring wing of cloth on chassis; The chassis of described dry cooling layer is radially provided with total discharging opening, and described total discharge outlet is provided with and rotates bin gate.First lock cyclone rotary valve and the second lock cyclone rotary valve can keep vacuum desolvation section to be negative pressure state,
the precipitation dregs of riceenter dry cooling layer charging aperture from the second lock cyclone rotary valve and fall into the chassis of dry cooling layer; According to moisture content and the temperature of the precipitation dregs of rice, cold wind is passed in air blanketing, evenly upwards spray from each air jet orifices, under the stirring action of dry cooling layer stirring wing, the precipitation dregs of rice are in fluidisation state or half fluidisation state again, with Forced Air Convection heat exchange, the drying of the precipitation dregs of rice is cooled to normal temperature, moisture content 8%, from total discharging opening with rotate bin gate and discharge continuously, complete solid phase desolvation process, obtain
the finished product dregs of rice.The finished product dregs of rice there will not be condensation, the group of rising and hygroscopic effect in follow-up workshop section, and stay in grade is excellent.
As a further improvement on the present invention, axis along described cylindrical shell is provided with rotary main shaft, main shaft seal is respectively equipped with between described rotary main shaft and each layer, each described flash distillation precipitation layer stirring wing, centrifugal flight, centripetal flight and dry cooling layer stirring wing are separately fixed on described rotary main shaft, the lower end of described rotary main shaft is connected with the output shaft of reductor, and the power shaft of described reductor is connected with the armature spindle of fire-proof motor.Fire-proof motor drives reductor running, reductor drives rotary main shaft to rotate, rotary main shaft drives flash distillation precipitation layer stirring wing, centrifugal flight, centripetal flight and dry cooling layer stirring wing to rotate simultaneously, compact conformation, and material is being in fluidisation state or half fluidisation state, power of agitator consumes low, and white peas or beans sheet fines content is low.
As a further improvement on the present invention, the circumferential wall of each described flash distillation precipitation layer, vacuum desolvation layer and dry cooling layer is separately installed with access door, visor and thermometer.
Accompanying drawing explanation
Below in conjunction with the drawings and specific embodiments, the present invention is further detailed explanation, and accompanying drawing only provides reference and explanation use, is not used to limit the present invention.
Fig. 1 is the flow chart of the low temperature desolventizing system of dregs of beans of the present invention.
Fig. 2 is the front view of flash vacuum desolventizing machine in Fig. 1.
Fig. 3 is the right view of Fig. 2.
Fig. 4 is the stereogram one of Fig. 2.
Fig. 5 is the stereogram two of Fig. 2.
In figure: D1. wets dregs of rice drag conveyor; D2. rotating feeding valve; D3. solvent vapo(u)r cyclone; D3.1. the 3rd lock cyclone rotary valve; D4. molten vapour wet trap; D5. molten vapour blower fan; D6. molten vapour superheater; D7. dust collection auger; D8. wastewater boilling tank; D9. circulating pump; D10. 1st effective evaporator; D11. oil preheater; D12. mist cyclone; D12.1. the 4th lock cyclone rotary valve; D13. gaseous mixture wet trap; G1. water vapour pipeline; G2. condensate pipe; G3. low concentration mixing oil pipe; G4. an effect concentrated blend pipe; G5. condensate line; G6. compressed air hose; D14. cold wind blower fan; D15. cooling air cyclone; D15.1. the 5th lock cyclone rotary valve; D16. finished product dregs of rice drag conveyor; D17. atmospheric condenser; D18. vacuum condenser; D19. exhaust gas recovery system.
1. combined feed mouth; 2. flash distillation precipitation layer; 2a. solvent vapo(u)r interlayer; 2b. solvent vapo(u)r entrance; 2c. solvent vapo(u)r exports; 2d. flash distillation precipitation layer stirring wing; 2e. flash distillation precipitation layer discharge gate; 2f. flash distillation precipitation section discharging opening; 3. middle rotary valve; 4. the first lock cyclone rotary valve; 5. vacuum desolvation layer; 5a. steam heating interlayer; 5b. steam entry pipe; 5c. drip pipe; The centripetal flight of 5d.; The centrifugal flight of 5e.; 5f. vacuum desolvation section feeding mouth; 5g. vacuum desolvation section discharging opening; 5h. steam jet vavuum pump; 5j. live (open) steam jet pipe; 6. the second lock cyclone rotary valve; 7. dry cooling layer; 7a. air blanketing; The dry cooling layer charging aperture of 7b.; 7c. rotates bin gate; The import of 7d. cooling air; 7e. cooling air outlet; The dry cooling layer stirring wing of 7f.; 8. rotary main shaft; 9. desolventizing machine reductor; 10. fire-proof motor; 11. access doors; 12. visors; 13. thermometers.
Detailed description of the invention
As shown in Figures 2 to 5, flash vacuum desolventizing machine of the present invention comprises vertical cylindrical shell, and the top of cylindrical shell is provided with combined feed mouth 1, and the inner chamber of cylindrical shell is provided with flash distillation precipitation section, vacuum desolvation section and dry cooling layer 7 from top to bottom successively; Flash distillation precipitation section adopts overheated solvent vapo(u)r to carry out flash distillation precipitation to the wet dregs of rice.
The high wet cake that contains enters cylinder lumen from the combined feed mouth 1 at cylindrical shell top, first through flash distillation precipitation section, adopt overheated solvent vapo(u)r to carry out flash distillation precipitation as precipitation heat and mass carrier to the wet dregs of rice in flash distillation precipitation section, make the high wet cake that contains become low containing the molten dregs of rice, then become the middle temperature dregs of rice by low containing the molten dregs of rice.The middle temperature dregs of rice enter vacuum desolvation section and realize the shallow bed of material from thermal evaporation, and under suction function, solvent vapo(u)r diffuser efficiency obviously increases, and the solvent in the middle temperature dregs of rice and moisture are able to rapid evaporation, become the precipitation dregs of rice.The precipitation dregs of rice enter dry cooling layer 7, utilize air carry out drying to the precipitation dregs of rice and cool, and the dry cooled precipitation dregs of rice become the finished product dregs of rice and white peas or beans sheet, there will not be condensation and sizing, feed back phenomenon; Reduce the temperature of the finished product dregs of rice simultaneously, reduce the load of follow-up workshop section cooling.
Flash distillation precipitation section comprises upper and lower two-layer flash distillation precipitation layer 2, cylindrical shell level is cut off by the chassis of each flash distillation precipitation layer 2 respectively, solvent vapo(u)r interlayer 2a is respectively equipped with below the chassis of each flash distillation precipitation layer 2, the sidewall of solvent vapo(u)r interlayer 2a is connected to solvent vapo(u)r entrance 2b, the chassis of each flash distillation precipitation layer 2 is evenly distributed with solvent vapo(u)r spray orifice, and the upper portion side wall of each flash distillation precipitation layer 2 is respectively equipped with solvent vapo(u)r outlet 2c.
Be arranged with respectively above the chassis of each flash distillation precipitation layer 2 and material is evenly spread out the flash distillation precipitation layer stirring wing 2d of cloth on chassis.
The chassis of upper flash distillation precipitation layer is radially provided with the flash distillation precipitation layer discharge gate 2e of downward flash distillation precipitation layer discharge, flash distillation precipitation layer discharge gate 2e place is provided with middle rotary valve 3; The bottom sidewall of lower flash distillation precipitation layer is provided with flash distillation precipitation section discharging opening 2f.
Containing molten 30%, temperature 50 C
high containing wet cakefirst fall on the chassis of flash distillation precipitation layer, the overheated solvent vapo(u)r of 150-160 DEG C enters solvent vapo(u)r interlayer 2a from solvent vapo(u)r entrance 2b, upwards spray from each solvent vapo(u)r spray orifice chassis with the speed of 30-36m/s, with height containing wet cake direct contact heat transfer, thickness of feed layer 600-700mm, under the stirring action of ejection of solvent steam and flash distillation precipitation layer stirring wing 2d, the high wet cake that contains is in fluidisation state or half fluidisation state, with solvent vapo(u)r forced-convection heat transfer, make to be down to less than 15% containing molten, become
low containing the molten dregs of rice, the solvent vapo(u)r of 75 DEG C is discharged from solvent vapo(u)r outlet 2c.
Then material enters lower flash distillation precipitation layer through middle rotary valve 3, and the overheated solvent vapo(u)r continuing to enter with injection carries out forced-convection heat transfer, and make to be down to less than 1% containing molten, but vaporize not yet completely in conjunction with state solvent, flash distillation precipitation dregs of rice temperature rises to 80-85 DEG C, becomes
the middle temperature dregs of rice, discharge from flash distillation precipitation section discharging opening 2f and enter vacuum desolvation section.
Vacuum desolvation section comprises stacked successively multi-layer vacuum precipitation layer 5 from top to bottom, and the chassis of each vacuum desolvation layer 5 is followed successively by big disk from top to bottom, roundel interval arranges and the chassis of the two-layer vacuum desolvation layer of bottom is big disk.
The periphery of each big disk is connected on the inwall of cylindrical shell, leaves gap between the periphery of each roundel and the inwall of cylindrical shell; Be respectively equipped with steam heating interlayer 5a below the chassis of each vacuum desolvation layer 5, the diapire of each steam heating interlayer 5a is connected to steam entry pipe 5b and drip pipe 5c.
The top of each layer big disk except bottom is arranged with the centripetal flight 5d carried by outer circumferential axle center by material respectively, and the axle center place of each layer big disk except bottom is respectively equipped with the vacuum desolvation layer discharge gate to lower floor's discharge; The top of bottom big disk and each layer roundel is arranged with the centrifugal flight 5e carried to periphery by axle center by material respectively.
The top of top layer vacuum desolvation layer is circumferentially provided with vacuum orifice and vacuum desolvation section feeding mouth 5f, flash distillation precipitation section discharging opening 2f with lock cyclone rotary valve 4 by first between vacuum desolvation section feeding mouth 5f and be connected.
Be provided with live (open) steam jet pipe 5j in the cavity space of bottom vacuum desolvation layer, the bottom sidewall of bottom vacuum desolvation layer is provided with vacuum desolvation section discharging opening 5g.
Vacuum orifice continues suction makes vacuum desolvation section negative pressure,
the middle temperature dregs of riceenter vacuum desolvation section feeding mouth 5f by the first lock cyclone rotary valve 4 and fall on the excircle of the big disk of top layer vacuum desolvation layer, centripetal flight 5d does centripetal screw motion, material is spread out cloth also to shift to circle centre position gradually on big disk, material and steam heating interlayer 5a indirect heat exchange in the process, stirring of flight makes material thermally equivalent, and under certain vacuum degree, continue evaporation in conjunction with state solvent.Material on big disk falls into the center of the roundel of lower floor from the vacuum desolvation layer discharge gate of circle centre position, centrifugal flight 5e does centrifugal screw motion, material is spread out cloth also to move to outer planet gradually on roundel, material and the further indirect heat exchange of steam heating interlayer 5a in the process, then material falls to lower one deck big disk from the periphery of roundel.Circulation like this, until material drops on the center of bottom vacuum desolvation layer.
At bottom vacuum desolvation layer, live (open) steam jet pipe 5j sprays into appropriate superheated vapour in bottom chamber, superheated vapour upwards with dregs of beans reverse flow, solvent vapo(u)r in dregs of beans gap is diluted, dividing potential drop reduces, promote to evaporate further from embryo sheet tissue in conjunction with state solvent, spread, realize very brief stripping.Spray into the negative pressure that water vapour amount must control make vacuum desolvation section maintain-2000 ~-3000mm water column, prevent wetting+hot two conditions occur simultaneously, under the prerequisite of precipitation of remaining valid, prevent white peas or beans sheet generation thermal denaturation.
Material is under the promotion of the centrifugal flight 5e of bottom, and continue and steam heating interlayer 5a indirect heat exchange, the solvent in white peas or beans sheet and moisture are able to rapid evaporation, and solvent strength is down to below 1000ppm, generates
the precipitation dregs of ricedischarge from vacuum desolvation section discharging opening 5g.
Be provided with air blanketing 7a below the chassis of dry cooling layer 7, air blanketing 7a is circumferentially connected with cooling air import 7d, dry cooling layer 7 chassis on be evenly distributed with air jet orifices, the upper portion side wall of dry cooling layer 7 is provided with cooling air outlet 7e; The top of dry cooling layer 7 is circumferentially provided with dry cooling layer charging aperture 7b, locks cyclone rotary valve 6 be connected between dry cooling layer charging aperture 7b with vacuum desolvation section discharging opening 5g by second.
Be arranged with respectively above the chassis of dry cooling layer 7 and material is evenly spread out the dry cooling layer stirring wing 7f of cloth on chassis.
The chassis of dry cooling layer 7 is radially provided with total discharging opening, and total discharge outlet is provided with and rotates bin gate 7c.Rotate bin gate 7c and can adopt automatic material door disclosed in CN204009592U, can automatically adjust aperture size according to bed depth.Rotate bin gate 7c and can adopt automatic material door disclosed in CN204009592U, can automatically adjust aperture size according to bed depth.
First lock cyclone rotary valve 4 and the second lock cyclone rotary valve 6 can keep vacuum desolvation section to be negative pressure state,
the precipitation dregs of riceenter dry cooling layer charging aperture 7b from the second lock cyclone rotary valve 6 and fall into the chassis of dry cooling layer 7; According to moisture content and the temperature of the precipitation dregs of rice, cold wind is passed in air blanketing 7a, evenly upwards spray from each air jet orifices, under the stirring action of dry cooling layer stirring wing 7f, the precipitation dregs of rice are in fluidisation state or half fluidisation state again, with Forced Air Convection heat exchange, the drying of the precipitation dregs of rice is cooled to normal temperature, moisture content 8%, from total discharging opening with rotate bin gate 7c and discharge continuously, complete solid phase desolvation process, obtain
the finished product dregs of rice.The finished product dregs of rice there will not be condensation, the group of rising and hygroscopic effect in follow-up workshop section, and stay in grade is excellent.
Axis along cylindrical shell is provided with rotary main shaft 8, main shaft seal is respectively equipped with between rotary main shaft 8 and each layer, each flash distillation precipitation layer stirring wing 2d, centrifugal flight 5e, centripetal flight 5d and dry cooling layer stirring wing 7f are separately fixed on rotary main shaft 8, the lower end of rotary main shaft 8 is connected with the output shaft of desolventizing machine reductor 9, and the power shaft of desolventizing machine reductor 9 is connected with the armature spindle of fire-proof motor 10.Fire-proof motor 10 drives desolventizing machine reductor 9 to operate, desolventizing machine reductor 9 drives rotary main shaft 8 to rotate, rotary main shaft 8 drives flash distillation precipitation layer stirring wing 2d, centrifugal flight 5e, centripetal flight 5d and dry cooling layer stirring wing 7f to rotate simultaneously, compact conformation, and material is being in fluidisation state or half fluidisation state, power of agitator consumes low, and white peas or beans sheet fines content is low.
The circumferential wall of each flash distillation precipitation layer, vacuum desolvation layer 5 and dry cooling layer 7 is separately installed with access door 11, visor 12 and thermometer 13.
Vacuum orifice place is provided with steam jet vavuum pump 5h.Utilizing Venturi effect, making the dry saturated steam of certain pressure walk to produce air-extraction function by forcibly pumped gas being carried secretly continuously during jet pipe at a high speed.
The high wet cake that contains enters cylinder lumen from the combined feed mouth 1 at cylindrical shell top, first through flash distillation precipitation section, adopt overheated solvent vapo(u)r to carry out flash distillation precipitation as precipitation heat and mass carrier to the wet dregs of rice in flash distillation precipitation section, make the high wet cake that contains become low containing the molten dregs of rice, then become the middle temperature dregs of rice by low containing the molten dregs of rice.The middle temperature dregs of rice enter vacuum desolvation section and realize the shallow bed of material from thermal evaporation, and under suction function, solvent vapo(u)r diffuser efficiency obviously increases, and the solvent in the middle temperature dregs of rice and moisture are able to rapid evaporation, become the precipitation dregs of rice of 60 DEG C ~ 65 DEG C.The precipitation dregs of rice enter dry cooling layer, utilize air carry out drying to the precipitation dregs of rice and cool, and the dry cooled precipitation dregs of rice become the finished product dregs of rice and white peas or beans sheet, there will not be condensation and sizing, feed back phenomenon; Reduce the temperature of the finished product dregs of rice simultaneously, reduce the load of follow-up workshop section cooling.Flash vacuum desolventizing machine device integration of the present invention is high, and single device substitutes A cylinder, B cylinder, vacuum desolvation machine and drying cooling device and promotes conveying equipment in a large number, can save power consumption 30%.Significantly reduce the floor space of equipment, reduce the cost of wheeling of material, reduce the fines content of material, operating cost is low.In desolvation process, avoid material and lower the temperature because of conveying, be conducive to the evaporation of solvent vapo(u)r under negative pressure state, diffusion.Improve white peas or beans sheet and go out quality, heated time is very brief, improves soluble protein index (NSI), eliminates the defective products such as caking, thus ensures the yield of the follow-up edible protein of high-quality.Reduce the surface area of equipment, be conducive to insulation, heat loss is little.Flash distillation precipitation section due to dregs of beans humidity high, the precipitation time is short, and therefore precipitation under the environment that temperature is higher, is conducive to raising the efficiency; The precipitation time of vacuum desolvation section is longer, and water capacity is low, under maintaining low-temperature vacuum environment, is conducive to the activity keeping protein.
As shown in Figure 1, the low temperature desolventizing system of dregs of beans of the present invention comprises above-mentioned flash vacuum desolventizing machine, containing molten 30%, temperature 50 C
high containing wet cake fromwet dregs of rice drag conveyor D1 discharges, and enters the combined feed mouth 1 at flash vacuum desolventizing machine top through rotating feeding valve D2.The solvent vapo(u)r outlet 2c of flash vacuum desolventizing machine is connected with the air inlet of solvent vapo(u)r cyclone D3, the bottom discharging mouth of solvent vapo(u)r cyclone D3 is connected with the main-inlet of dust collection auger D7 by the 3rd lock cyclone rotary valve D3.1, the outlet of dust collection auger D7 is connected with the top of vacuum desolvation section, the top outlet inlet of solvent vapo(u)r cyclone D3 is connected with the air inlet of molten vapour wet trap D4, the top outlet inlet of molten vapour wet trap D4 is connected with the suction inlet of molten vapour blower fan D5, the outlet of molten vapour blower fan D5 is connected with the tube side import of molten vapour superheater D6, the tube side outlet of molten vapour superheater D6 is connected with solvent vapo(u)r entrance 2b, the shell side import of molten vapour superheater D6 is connected with water vapour pipeline G1, and the shell-side outlet of molten vapour superheater D6 is connected with condensate pipe G2 by drain valve.
The shell side water vapour evaporation capacity for engine of molten vapour superheater D6 is controlled by pneumatic operated valve, and pneumatic operated valve provides source of the gas by compressed air hose G6, and the aperture of pneumatic operated valve is controlled by molten vapour superheater D6 tube side outlet solvent vapor (steam) temperature.
Under the suction of molten vapour blower fan D5, first 75 DEG C of solvent vapo(u)rs that the flash distillation precipitation section of flash vacuum desolventizing machine is discharged enter solvent vapo(u)r cyclone D3, cyclonic separation solid dregs of rice end, solid dregs of rice end locks by the 3rd the main-inlet that cyclone rotary valve D3.1 enters dust collection auger D7 from the bottom discharging mouth of solvent vapo(u)r cyclone D3, and solid dregs of rice end is sent into vacuum desolvation section and proceeded vacuum desolvation by dust collection auger D7; Then solvent vapo(u)r continues to enter in molten vapour wet trap D4 and washs, little power in solvent vapo(u)r is captured, clean solvent vapo(u)r enters molten vapour superheater D6 after molten vapour blower fan D5 accelerates, in molten vapour superheater D6, solvent vapo(u)r walks tube side, water vapour walks the overheated solvent vapo(u)r that solvent vapo(u)r is heated as 150-160 DEG C by shell side, the flash distillation precipitation section of flash vacuum desolventizing machine is reentered from solvent vapo(u)r entrance 2b, circulation like this, solvent vapo(u)r not only can be all recovered, and can UTILIZATION OF VESIDUAL HEAT IN.
The top of molten vapour wet trap D4 is provided with heat water-spraying's pipe, the bottom discharge mouth of molten vapour wet trap D4 is connected with the top entry of wastewater boilling tank D8, the middle part delivery port of wastewater boilling tank D8 is connected with the entrance of circulating pump D9, and the outlet of circulating pump D9 is connected with the entrance of heat water-spraying's pipe of molten vapour wet trap D4; The lower circumference of wastewater boilling tank D8 is connected with water vapour pipeline G1, and the top vent of wastewater boilling tank D8 is connected with exhaust gas recovery system D19.
Heat water-spraying's pipe on molten vapour wet trap D4 top sprays 90 DEG C of hot water continuously, traps on the one hand, make solvent remain on gaseous state on the other hand, prevent solvent to run off dust; Hot water temperature after trapping dust decreases, wastewater boilling tank D8 is entered from the bottom discharge mouth of molten vapour wet trap D4, in wastewater boilling tank D8, water vapour is by hot water heating to 90 DEG C, circulating pump D9 is entered from the middle part delivery port of wastewater boilling tank D8, heat water-spraying's pipe that hot water is sent back to molten vapour wet trap D4 by circulating pump D9 carries out circulated sprinkling, and hot water and the heat that contains thereof are all reclaimed.After the dust in wastewater boilling tank D8 reaches some, can be discharged by the sewage draining exit of bottom.
The outlet of molten vapour blower fan D5 is also connected with the shell side inlet of 1st effective evaporator D10, and the shell-side outlet of 1st effective evaporator D10 is connected with the entrance of atmospheric condenser D17; The bottom tube-side inlet of 1st effective evaporator D10 is connected with low concentration mixing oil pipe G3, the top of 1st effective evaporator D10 is connected with an effect vaporization chamber, the top of one effect vaporization chamber is connected with the entrance of vacuum condenser D18, and the bottom and of an effect vaporization chamber is imitated concentrated blend pipe G4 and is connected.
Clean solvent vapo(u)r after solvent vapo(u)r cyclone D3 and molten vapour wet trap D4 dedusting, after molten vapour blower fan D5 accelerates, some enters 1st effective evaporator D10, in 1st effective evaporator D10, the miscella of oil-containing 25% enters the bringing-up section tube side of 1st effective evaporator D10 from low concentration mixing oil pipe G3 and upwards flows, solvent vapo(u)r enters the bringing-up section shell side of 1st effective evaporator D10, condensation is continued to entering atmospheric condenser D17 from the shell-side outlet of 1st effective evaporator D10 after miscella heat release, a small amount of condensate liquid that bringing-up section shell side produces is discharged from the condensate line G5 bottom shell side, miscella is heated an effect vaporization chamber on rear arrival 1st effective evaporator D10 top, and moisture evaporates in a large number and enters vacuum condenser D18 from the top of an effect vaporization chamber, and the miscella of oil-containing 50% is discharged from an effect concentrated blend pipe G4.
The outlet of steam jet vavuum pump 5h is connected with the air inlet of mist cyclone D12, the bottom discharging mouth of mist cyclone D12 is connected with the auxiliary entrance of dust collection auger D7 by the 4th lock cyclone rotary valve D12.1, the top outlet inlet of mist cyclone D12 is connected with the air inlet of gaseous mixture wet trap D13, the outlet at bottom of gaseous mixture wet trap D13 is connected with the top entry of wastewater boilling tank D8, the top outlet inlet of gaseous mixture wet trap D13 is connected with the shell side inlet of oil preheater D11, the shell-side outlet of oil preheater D11 is connected with exhaust gas recovery system D19, the outlet of one effect concentrated blend pipe G4 is connected with the tube-side inlet of oil preheater D11, and the tube side outlet of oil preheater D11 is connected with the bottom tube-side inlet of 2nd effect evaporator.
First the 90 DEG C of water vapours extracted out from the outlet of steam jet vavuum pump 5h and a small amount of solvent vapo(u)r enter mist cyclone D12, cyclonic separation solid dregs of rice end, solid dregs of rice end locks by the 4th the auxiliary entrance that cyclone rotary valve D12.1 enters dust collection auger D7 from the bottom discharging mouth of mist cyclone D12, and solid dregs of rice end is sent into vacuum desolvation section and proceeded vacuum desolvation by dust collection auger D7; Then mist continues to enter gaseous mixture wet trap D13 and washs, and the little power in gaseous mixture is captured, and the shell side that clean gaseous mixture enters oil preheater D11 heats miscella, reclaims heat; Imitate the miscella of the oil-containing 50% that concentrated blend pipe G4 flows out after oil preheater D11 heats from one, carry out 2nd effect evaporator and continue evaporation and concentration.
Total discharging opening of flash vacuum desolventizing machine is connected with the main charging aperture of finished product dregs of rice drag conveyor D16; The outlet of cold wind blower fan D14 is connected with the cooling air import 7d of flash vacuum desolventizing machine, the cooling air outlet 7e of flash vacuum desolventizing machine is connected with the air inlet of cooling air cyclone D15, and the bottom discharge mouth of cooling air cyclone D15 is connected with the auxiliary charging aperture of finished product dregs of rice drag conveyor D16 by the 5th lock cyclone rotary valve D15.1.
The cooling air of discharging from cooling air outlet 7e enters cooling air cyclone D15, cyclonic separation solid dregs of rice end, and solid dregs of rice end locks by the 5th the auxiliary charging aperture that cyclone rotary valve D15.1 enters finished product dregs of rice drag conveyor D16 from the bottom discharging mouth of cooling air cyclone D15.
Claims (10)
1. the low temperature desolventizing system of a dregs of beans, comprise flash vacuum desolventizing machine, the vertical cylinder top of described flash vacuum desolventizing machine is provided with combined feed mouth, it is characterized in that: the inner chamber of described cylindrical shell is provided with flash distillation precipitation section from top to bottom successively, vacuum desolvation section and dry cooling layer, described flash distillation precipitation section is provided with solvent vapo(u)r entrance and solvent vapo(u)r outlet, the cylindrical shell top of described vacuum desolvation section is provided with the steam jet vavuum pump of outwards bleeding, the bottom of described dry cooling layer is provided with total discharging opening, the circumferential wall of described dry cooling layer is provided with cooling air import and cooling air outlet, described solvent vapo(u)r outlet is connected with the air inlet of solvent vapo(u)r cyclone, the bottom discharging mouth of described solvent vapo(u)r cyclone is connected with the main-inlet of dust collection auger by lock cyclone rotary valve, the outlet of described dust collection auger is connected with the top of described vacuum desolvation section, the top outlet inlet of described solvent vapo(u)r cyclone is connected with the air inlet of molten vapour wet trap, the top outlet inlet of described molten vapour wet trap is connected with the suction inlet of molten vapour blower fan, the outlet of described molten vapour blower fan is connected with the tube side import of molten vapour superheater, the tube side outlet of described molten vapour superheater is connected with described solvent vapo(u)r entrance, the shell side import of described molten vapour superheater is connected with water vapour pipeline, and the shell-side outlet of described molten vapour superheater is connected with condensate pipe by drain valve.
2. the low temperature desolventizing system of dregs of beans according to claim 1, it is characterized in that: the top of described molten vapour wet trap is provided with heat water-spraying's pipe, the bottom discharge mouth of described molten vapour wet trap is connected with the top entry of wastewater boilling tank, the middle part delivery port of described wastewater boilling tank is connected with the entrance of circulating pump, and described circulation delivery side of pump is connected with the entrance of heat water-spraying's pipe of described molten vapour wet trap; The lower circumference of described wastewater boilling tank is connected with water vapour pipeline, and the top vent of described wastewater boilling tank is connected with exhaust gas recovery system.
3. the low temperature desolventizing system of dregs of beans according to claim 1, is characterized in that: the outlet of described molten vapour blower fan is also connected with the shell side inlet of 1st effective evaporator, and the shell-side outlet of described 1st effective evaporator is connected with the entrance of atmospheric condenser; The bottom tube-side inlet of described 1st effective evaporator is connected with low concentration mixing oil pipe, the top of described 1st effective evaporator is connected with an effect vaporization chamber, a described effect top for vaporization chamber is connected with the entrance of vacuum condenser, and the bottom and of a described effect vaporization chamber is imitated concentrated blend pipe and is connected.
4. the low temperature desolventizing system of dregs of beans according to claim 1, it is characterized in that: described steam jet vacuum delivery side of pump is connected with the air inlet of mist cyclone, the bottom discharging mouth of described mist cyclone is connected with the auxiliary entrance of described dust collection auger by lock cyclone rotary valve, the top outlet inlet of described mist cyclone is connected with the air inlet of gaseous mixture wet trap, the outlet at bottom of described gaseous mixture wet trap is connected with the top entry of described wastewater boilling tank, the described top outlet inlet of gaseous mixture wet trap is connected with the shell side inlet of oil preheater, the shell-side outlet of described oil preheater is connected with described exhaust gas recovery system, the outlet of a described effect concentrated blend pipe is connected with the tube-side inlet of described oil preheater, and the tube side outlet of described oil preheater is connected with the bottom tube-side inlet of 2nd effect evaporator.
5. the low temperature desolventizing system of dregs of beans according to claim 1, is characterized in that: total discharging opening of described flash vacuum desolventizing machine is connected with the main charging aperture of finished product dregs of rice drag conveyor; The cooling air outlet of described flash vacuum desolventizing machine is connected with the air inlet of cooling air cyclone, and the bottom discharge mouth of described cooling air cyclone is connected with the auxiliary charging aperture of described finished product dregs of rice drag conveyor by lock cyclone rotary valve.
6. the low temperature desolventizing system of dregs of beans according to any one of claim 1 to 5, it is characterized in that: the flash distillation precipitation section of described flash vacuum desolventizing machine comprises upper and lower two-layer flash distillation precipitation layer, described cylindrical shell level is cut off by the chassis of each described flash distillation precipitation layer respectively, solvent vapo(u)r interlayer is respectively equipped with below the chassis of each described flash distillation precipitation layer, the sidewall of described solvent vapo(u)r interlayer is connected to described solvent vapo(u)r entrance, the chassis of each described flash distillation precipitation layer is evenly distributed with solvent vapo(u)r spray orifice, the upper portion side wall of each described flash distillation precipitation layer is respectively equipped with the outlet of described solvent vapo(u)r, be arranged with respectively above the chassis of each flash distillation precipitation layer and material is evenly spread out the flash distillation precipitation layer stirring wing of cloth on chassis, the chassis of upper flash distillation precipitation layer is radially provided with the flash distillation precipitation layer discharge gate of downward flash distillation precipitation layer discharge, described flash distillation precipitation layer discharge gate place is provided with middle rotary valve, the bottom sidewall of lower flash distillation precipitation layer is provided with flash distillation precipitation section discharging opening.
7. the low temperature desolventizing system of dregs of beans according to claim 6, it is characterized in that: described vacuum desolvation section comprises stacked successively multi-layer vacuum precipitation layer from top to bottom, the chassis of each described vacuum desolvation layer is followed successively by big disk from top to bottom, roundel interval arranges and the chassis of the two-layer vacuum desolvation layer of bottom is big disk; The periphery of each described big disk is connected on the inwall of described cylindrical shell, leaves gap between the periphery of each described roundel and the inwall of described cylindrical shell; Be respectively equipped with steam heating interlayer below the chassis of each described vacuum desolvation layer, the diapire of each described steam heating interlayer is connected to steam entry pipe and drip pipe; The top of each layer big disk except bottom is arranged with the centripetal flight carried by outer circumferential axle center by material respectively, and the axle center place of each layer big disk except bottom is respectively equipped with the vacuum desolvation layer discharge gate to lower floor's discharge; The top of bottom big disk and each layer roundel is arranged with the centrifugal flight carried to periphery by axle center by material respectively; The top of top layer vacuum desolvation layer is circumferentially provided with vacuum orifice and vacuum desolvation section feeding mouth, described vacuum orifice place is provided with described steam jet vavuum pump, described flash distillation precipitation section discharging opening with lock cyclone rotary valve by first between described vacuum desolvation section feeding mouth and be connected; Be provided with live (open) steam jet pipe in the cavity space of bottom vacuum desolvation layer, the bottom sidewall of bottom vacuum desolvation layer is provided with vacuum desolvation section discharging opening.
8. the low temperature desolventizing system of dregs of beans according to claim 7, it is characterized in that: below the chassis of described dry cooling layer, be provided with air blanketing, described air blanketing be circumferentially connected with described cooling air import, described dry cooling layer chassis on be evenly distributed with air jet orifices, the upper portion side wall of described dry cooling layer is provided with described cooling air outlet; The top of described dry cooling layer is circumferentially provided with dry cooling layer charging aperture, locks cyclone rotary valve be connected between described dry cooling layer charging aperture with described vacuum desolvation section discharging opening by second; Be arranged with respectively above the chassis of described dry cooling layer and material is evenly spread out the dry cooling layer stirring wing of cloth on chassis; The chassis of described dry cooling layer is radially provided with total discharging opening, and described total discharge outlet is provided with and rotates bin gate.
9. the low temperature desolventizing system of dregs of beans according to claim 8, it is characterized in that: the axis along described cylindrical shell is provided with rotary main shaft, main shaft seal is respectively equipped with between described rotary main shaft and each layer, each described flash distillation precipitation layer stirring wing, centrifugal flight, centripetal flight and dry cooling layer stirring wing are separately fixed on described rotary main shaft, the lower end of described rotary main shaft is connected with the output shaft of reductor, and the power shaft of described reductor is connected with the armature spindle of fire-proof motor.
10. the low temperature desolventizing system of dregs of beans according to claim 7, is characterized in that: the circumferential wall of each described flash distillation precipitation layer, vacuum desolvation layer and dry cooling layer is separately installed with access door, visor and thermometer.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110542304A (en) * | 2019-09-27 | 2019-12-06 | 中国环境科学研究院 | zero emission of desolventizer-toaster waste gas, pollutant and solvent recovery system |
| CN115287121A (en) * | 2022-09-14 | 2022-11-04 | 山东凯斯达机械制造有限公司 | Method for utilizing secondary steam generated by low-temperature desolventizing and mixed oil evaporation |
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| CN202164285U (en) * | 2011-06-21 | 2012-03-14 | 武汉九楚亘泰萃取技术有限公司 | Energy-saving continuous type wet meal desolvation machine |
| CN103690719A (en) * | 2013-09-26 | 2014-04-02 | 青岛盛嘉信息科技有限公司 | Traditional Chinese medicine composition for treating intractable insomnia |
| CN204949379U (en) * | 2015-08-12 | 2016-01-13 | 迈安德集团有限公司 | Low temperature exsolution system of dregs of beans |
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| CN202164285U (en) * | 2011-06-21 | 2012-03-14 | 武汉九楚亘泰萃取技术有限公司 | Energy-saving continuous type wet meal desolvation machine |
| CN103690719A (en) * | 2013-09-26 | 2014-04-02 | 青岛盛嘉信息科技有限公司 | Traditional Chinese medicine composition for treating intractable insomnia |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110542304A (en) * | 2019-09-27 | 2019-12-06 | 中国环境科学研究院 | zero emission of desolventizer-toaster waste gas, pollutant and solvent recovery system |
| CN110542304B (en) * | 2019-09-27 | 2024-03-01 | 中国环境科学研究院 | Zero emission and solvent recovery system for waste gas and pollutant of steam stripping machine |
| CN115287121A (en) * | 2022-09-14 | 2022-11-04 | 山东凯斯达机械制造有限公司 | Method for utilizing secondary steam generated by low-temperature desolventizing and mixed oil evaporation |
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