CN109384855B

CN109384855B - Corn starch system of processing

Info

Publication number: CN109384855B
Application number: CN201811568772.XA
Authority: CN
Inventors: 鲍大权; 张洪彩; 袁媛; 吕志春; 胡明辉; 沈宾; 李旭东
Original assignee: Myande Group Co Ltd
Current assignee: Myande Group Co Ltd
Priority date: 2018-12-21
Filing date: 2018-12-21
Publication date: 2023-10-31
Anticipated expiration: 2038-12-21
Also published as: CN109384855A

Abstract

The invention discloses a corn starch processing system, wherein a germ outlet of a germ extraction device is connected with a germ packaging mechanism through a germ drying device; the corn grits outlet of the germ extraction device is connected with the enzymatic soaking device, the soaking corn outlet is connected with the feeding port of the crushing device, the discharging port of the crushing device is connected with the feeding port of the fiber washing device, the oversize product outlet of the fiber washing device is connected with the feeding port of the fiber dewatering and drying device, the discharging port of the fiber dewatering and drying device is connected with the feeding port of the fiber drying device, and the discharging port of the fiber drying device is connected with the fiber packaging mechanism. The sieve outlet of the fiber washing device is connected with the feed inlet of the disc centrifuge, the overflow port of the disc centrifuge is connected with the feed inlet of the protein concentration device through a thin gluten overflow pipe, the discharge port of the protein concentration device is connected with the feed inlet of the protein dehydration drying device, and the discharge port of the protein dehydration drying device is connected with the protein packaging mechanism. The system has high product yield, low investment and low energy consumption.

Description

Corn starch system of processing

Technical Field

The invention relates to a starch production system, in particular to a corn starch processing system, and belongs to the technical field of starch processing.

Background

The traditional corn processing starch adopts a wet processing technology, and comprises the following steps: 1. soaking by sulfurous acid; 2. grinding the materials by a two-stage coarse grinding (one-stage embryo extraction is carried out after each stage of coarse grinding) and a one-stage fine grinding; 3. extracting the fibers by fiber washing; 4. separating starch and protein by a centrifuge; 5. refining, dehydrating, drying and packaging starch; 6. dehydrating, drying and packaging the protein; 7. washing, dehydrating, drying and packaging the embryo; 8. dehydrating, drying and packaging the fiber. The process is mature, and the flow route is basically consistent.

The corn husk consists of semi-permeable membrane, which is changed into permeable membrane to permeate the soluble matter inside corn grains, and the corn is soaked in 0.15-0.25% sulfurous acid for 40-48 hr in conventional process to destroy the protein net of corn grains at 48-53 deg.c to separate the fiber from protein.

As the embryo is to be extracted, the traditional process only adopts 2-level coarse grinding and 1-level fine grinding, and the embryo is to be extracted after coarse grinding, and equipment such as a buffer tank, a delivery pump, an embryo cyclone and the like is needed in the middle. The embryo is extracted to be liquid, the embryo is dehydrated to about 53% by using a wringer, and then is dried to 7% by using a tube bundle dryer.

The starch separator is used for separating starch from protein, the protein content in the separated starch is less than or equal to 3.5%, and the protein content is reduced to below 0.4% by a washing cyclone. The starch milk is liquefied, saccharified and filtered in the sugar-removing workshop, and the filtered protein is generally directly sold.

When a vacuum drum suction filter is used for protein dehydration, a filter cloth is washed by using process water, the starch project is processed by 300 tons/day of corn, the washing water needs 35 m/h, and the treatment capacity of a thickener is increased in the part.

The vacuum drum and the vacuum pump of the evaporator need working fluid, the working fluid of 300 tons/day corn processing starch project needs 10m per hour, and the working fluid is generally directly discharged to a sewage treatment plant after being used by clear water.

The tube bundle dryer is used for feeding cold air, products are conveyed through negative pressure, the brake and the brake are discharged, tail gas is processed in a pulse mode, and the outlet of the fan is directly discharged.

In summary, the wet processing technology mainly has the following disadvantages: 1. the process flow is too long, so that more equipment is caused, the investment is high, and the power consumption is large; 2. the sulfurous acid needs to be soaked, the soaking time is long, the energy consumption is high, the water consumption is large, and the sewage quantity is also large.

Disclosure of Invention

The invention aims to overcome the problems in the prior art and provide a corn starch processing system which can omit acid making equipment, a middle storage tank, a conveying pump, a germ cyclone and the like, and the number and the volume of soaking tanks are greatly reduced, so that the steam consumption is reduced.

In order to solve the technical problems, the corn starch processing system comprises an embryo extracting device, wherein an embryo outlet of the embryo extracting device is connected with an inlet of an embryo drying device, and an outlet of the embryo drying device is connected with an embryo packaging mechanism; the corn grits outlet of the germ extraction device is connected with the feed inlet of the enzymatic soaking device, the corn outlet of the enzymatic soaking device is connected with the feed inlet of the crushing device through a corn soaking output pipe, the discharge outlet of the crushing device is connected with the feed inlet of the fiber washing device, the oversize outlet of the fiber washing device is connected with the feed inlet of the fiber dewatering and drying device, the discharge outlet of the fiber dewatering and drying device is connected with the feed inlet of the fiber drying device, and the discharge outlet of the fiber drying device is connected with the fiber packaging mechanism.

Compared with the prior art, the invention has the following beneficial effects: the germ is solid, the water content is about 15%, and the germ is dried to 7% by the germ drying device, so that germ dehydration equipment is reduced, drying equipment is greatly reduced, steam consumption is reduced, and the germ is packaged into a germ finished product by a germ packaging mechanism. The corn grits subjected to embryo extraction are metered and then enter an enzymatic soaking device, and soaked by utilizing soaking enzyme, so that the corn husks are damaged after embryo extraction, the soaking time can be controlled within 10 hours, and the soaking temperature is 28-32 ℃. Compared with the prior sulfurous acid soaking before embryo extraction, the method reduces acid making equipment, shortens soaking time greatly, and reduces the number and volume of soaking tanks greatly; the soaking temperature is also greatly reduced, and the steam consumption is reduced. The protein net of the corn kernels is destroyed after soaking, so that starch particles wrapped by the protein net are free, and the separation of fibers and proteins is facilitated; then the soaked corns are crushed by a crushing device, and then 1.2 times of process water is added to crush the corns into about twelve pieces. Because the embryo is extracted, equipment such as an intermediate storage tank, a delivery pump, an embryo cyclone and the like are not needed. And fourthly, enabling the crushed corn to enter a fiber washing device for seven-stage countercurrent screening washing, enabling the fiber to be left on a screen, enabling starch and protein to be washed under the screen, enabling corn fiber to enter from a first stage, enabling process water to enter from a seventh stage, enabling final fiber to be discharged from the seventh stage, enabling concentration to become starch milk after the starch is washed by the process water, and discharging from the first stage. And (5) the washed fiber contains about 90% of water, the fiber water is extruded to about 62% by a wringer, and then enters a tube bundle dryer for drying, and the dried fiber water is about 10% and is packaged into a fiber finished product by a fiber packaging mechanism.

As an improvement of the invention, the soaking liquid outlet of the enzymatic soaking device is connected with the inlet of the evaporation concentration device, and the outlet of the evaporation concentration device is connected with the corn steep liquor inlet of the fiber drying device. As the corn pulp is soaked by adopting an enzyme method, the pulp yield of each ton of corn is greatly reduced, and each ton of corn pulp is 0.3 ton of thin corn pulp with the concentration of about 5%, the thin corn pulp is concentrated by an evaporation concentration device, the concentration of the concentrated corn pulp reaches about 43%, the concentrated corn pulp is added into dried fibers, and the dried fibers are dried by a tube bundle dryer to form 10% pulp-added fibers, so that the corn pulp is recovered, the quality of the fibers is improved, and the added value of products is improved.

As a further improvement of the invention, the undersize outlet of the fiber washing device is connected with the feed inlet of a disc centrifuge, the overflow port of the disc centrifuge is connected with the feed inlet of a protein concentration device through a thin gluten overflow pipe, the discharge port of the protein concentration device is connected with the feed inlet of a protein dehydration drying device, and the discharge port of the protein dehydration drying device is connected with a protein packaging mechanism. The starch washed by the fiber washing device contains protein, the protein is separated by a disk centrifuge, the disk centrifuge utilizes different specific gravities, the starch has large specific gravity, the underflow is taken, and the concentration of the underflow starch milk is 16 Baume degrees. The protein volume weight is small, overflow is carried out, the concentration of overflow protein is 15g/l, the overflow protein enters a protein concentration device from a thin gluten overflow pipe to be concentrated to 90-110 g/l, then the moisture of the protein is reduced to 10% by a protein dehydration drying device, and the protein is packaged into a protein finished product by a protein packaging mechanism.

As a further improvement of the invention, the underflow outlet of the disc centrifuge is connected with the feed inlet of the starch refining device, the starch milk outlet of the starch refining device is connected with the feed inlet of the starch milk dehydration device, the discharge outlet of the starch milk dehydration device is connected with the inlet of the starch drying device, and the outlet of the starch drying device is connected with the starch packaging mechanism. The concentration of the underflow starch milk is 16 Baume degrees, the protein content is 3.5%, the underflow starch milk enters a starch refining device, the starch refining device generally adopts a 12-stage washing cyclone, fresh water enters from a final-stage washing cyclone by adopting a countercurrent washing principle, overflow of each stage cyclone returns step by step as washing water of a previous stage, starch can be fully recovered, the starch yield is improved, and the consumption of primary fresh water is reduced. The overflow of the first-stage washing cyclone enters a starch and gluten separator for re-separation. After refining, the concentration of the starch milk is increased to 20-22 Baume degrees, and the protein content is reduced to below 0.4%.

As a further improvement of the invention, the starch milk outlet of the starch refining device is also connected with a starch milk size mixing device, a liquefying device, a saccharifying device, a filtering device, a decoloring device, an ion exchange device and an evaporating device in sequence, and the outlet of the evaporating device is connected with a glucose filling mechanism; and a filtrate outlet of the filtering device is connected with a feed inlet of the protein dehydration drying device. Sequentially performing starch milk size mixing, liquefying, saccharifying, filtering, decolorizing, ion exchange and evaporating on the refined starch milk to obtain glucose, and filling and selling by a glucose filling mechanism; in the sugar manufacturing process, a small amount of protein obtained by filtration enters a protein dehydration drying device for recycling, so that the added value of the product is improved.

As a further improvement of the invention, the germ extraction device comprises a first bucket elevator for lifting new corns, wherein the outlet of the first bucket elevator is connected with the inlet of a destoner, the outlet of the destoner is connected with the inlet of a permanent magnet cylinder, the outlet of the permanent magnet cylinder is connected with the inlet of a temporary corn storage bin, the outlet of the temporary corn storage bin is provided with a corn conveyor, the outlet of the corn conveyor is connected with the inlet of a water wetting machine, the outlet of the water wetting machine is connected with the inlet of a second bucket elevator, the outlet of the second bucket elevator is connected with the inlet of a water wetting tank, the outlet of the water wetting tank is connected with the inlet of the water wetting tank conveyor, the outlet of the water wetting tank conveyor is connected with the inlet of the third bucket elevator, the outlet of the third bucket elevator is connected with the inlet of the germ removing machine, the germ outlet at the upper end of the germ removing machine is connected with a wet germ output pipe, and the corn grits outlet at the bottom of the germ removing machine is connected with a corn grits output pipe. The corn is lifted to a high position by a bucket elevator, firstly, impurities such as sediment and stones are removed by a stone removing machine, then, metal objects such as iron nails, iron sheets or screws are removed by a permanent magnet barrel, then, the materials are weighed by a corn flow balance, enter a corn temporary storage bin for temporary storage, are sent out by a corn conveyor, are added with water by a water wetting machine, so that the water content of the corn is improved to about 18%, are sent into a water wetting tank after being lifted by a bucket elevator II, are placed for about 12 hours, enable germs to fully absorb water, are discharged by the water wetting tank conveyor, are lifted to a high position by a bucket elevator III, and are then extracted by a degerming machine; the extracted solid embryo is discharged from a wet embryo output pipe, the embryo yield can reach 7%, the embryo purity is more than 70%, the water content of the embryo is about 15%, and then the embryo is dried by an embryo drying device until the water content is 7%, so that embryo dehydration equipment is reduced, drying equipment is greatly reduced, and steam consumption is also reduced. And discharging the corn grits after the germ extraction from the corn grits output pipe.

As a further improvement of the invention, the germ drying device comprises a germ tube bundle dryer, wherein a feeding port of the germ tube bundle dryer is connected with a germ outlet of the germ extraction device, a discharging port of the germ tube bundle dryer is connected with a germ air-conveying pipe through a germ air seal, a discharging port of the germ air-conveying pipe is connected with a feeding port of a germ brake, and a discharging port of the germ brake is connected with an inlet of a germ bin; the top air outlet of the germ brake dragon is connected with the inlet of the germ brake dragon exhaust fan, and the outlet of the germ brake dragon exhaust fan is connected with the reflux port of the germ tube bundle dryer through a germ reflux pipe; the top air outlet of the germ tube bundle dryer is connected with the air inlet of the dryer brake dragon, the top air outlet of the dryer brake dragon is connected with the inlet of the dryer brake dragon exhaust fan, and the outlet of the dryer brake dragon exhaust fan is connected with the drying tail gas discharge pipe. The wet embryo enters a feeding port of an embryo tube bundle dryer from a wet embryo output tube, steam enters from a steam tube, the moisture content of the embryo is dried from 15% to 7%, the steam releases heat and becomes condensed water, and the condensed water is discharged from a condensed water tube; the dry embryo enters an embryo air delivery pipe through an embryo air seal, is delivered into an embryo clerestory pipe, is discharged into an embryo storage bin, and then enters an embryo packing scale from a bottom discharge hole of the embryo storage bin to be packed into an embryo finished product. The pulse dust collector is omitted on the germ air delivery pipeline, so that the equipment investment cost is reduced; the tail gas exhausted from the top of the germ brake dragon contains a small amount of germs, and the germs are returned to the germ tube bundle dryer for recovery through the germ return pipe under the suction of the germ brake dragon exhaust fan, so that the yield of the germs is improved, the exhaust emission is reduced, the inlet air of the germ tube bundle dryer is changed from cold air to hot air, the heat in the exhaust air is completely recovered, and the energy consumption is greatly reduced. The wet tail gas discharged from the top of the germ tube bundle dryer enters a dryer brake dragon for separation and dust removal, and is extracted by a dryer brake dragon exhaust fan to enter a washing tower or is discharged to the atmosphere.

As a further improvement of the invention, the enzymatic soaking device comprises a soaking tank and a corn conveying tank, wherein a soaking tank material inlet, a soaking tank enzyme preparation inlet and a soaking tank reflux port are arranged at the top of the soaking tank, the soaking tank material inlet is connected with a corn grits outlet of the embryo extraction device, the soaking tank enzyme preparation inlet is connected with an enzyme preparation pipe outlet, a soaking tank corn outlet and a soaking tank corn slurry outlet are arranged at the bottom of the soaking tank, the soaking tank corn outlet is connected with a top feed inlet of the corn conveying tank, a bottom discharge outlet of the corn conveying tank is connected with an inlet of a corn conveying pump, and an outlet of the corn conveying pump is connected with a corn soaking output pipe; the corn steep liquor outlet of the soaking tank is connected with the inlet of the circulating pump of the soaking tank, and the outlet of the circulating pump of the soaking tank is connected with the bottom feed inlet of the jacket heater; the top discharge port of the jacket heater is connected with a thin corn steep liquor output pipe and a soaking tank reflux pipe, the outlet of the thin corn steep liquor output pipe is connected with the feed inlet of the evaporator, and the outlet of the soaking tank reflux pipe is connected with the soaking tank reflux port. Discharging the corn grits after the embryo extraction from the corn grits output pipe, and entering a soaking tank; the enzyme preparation is discharged from the enzyme preparation pipe and also enters a soaking tank to be soaked with the corn grits, so that the protein net of the corn grains is destroyed, and the starch grains wrapped by the protein net are free, thereby being beneficial to separating fibers from protein. The soaked corn kernels are discharged from a corn outlet of the soaking tank, enter the corn conveying tank, and are conveyed into the dewatering curved sieve by the corn conveying pump along with water flow. The corn steep liquor produced after soaking is discharged from a corn steep liquor outlet of a soaking tank, is pumped into a jacket heater by a circulating pump of the soaking tank to be heated in a middle way, one part of the heated corn steep liquor returns to the soaking tank to circulate through a return pipe of the soaking tank, and the other part of the corn steep liquor is sent out through a thin corn steep liquor output pipe, and is concentrated by an evaporator to be subjected to fiber pulp pouring. The jacket heater adopts steam as a heat source, the steam becomes condensed water after heat release, and the condensed water is discharged from a condensed water pipe. The corn grits after embryo extraction are soaked by the enzyme preparation, the soaking time can be controlled within 10 hours, the soaking temperature is 28-32 ℃, the steam consumption can be reduced, and the number and the volume of soaking tanks are also greatly reduced.

As a further improvement of the invention, the crushing device comprises a degerming mill and a pin mill, the outlet of the soaked corn output pipe is connected with the feed inlet of a dewatering curved sieve, the material outlet of the dewatering curved sieve is connected with the inlet of a corn buffer tank, the outlet of the corn buffer tank is connected with the inlet of the degerming mill, the outlet of the degerming mill is connected with the inlet of the pin mill, the outlet of the pin mill is connected with the feed inlet of a post-grinding storage tank, and the outlet of the post-grinding storage tank is connected with the feed inlet of the fiber washing device through a screening conveying pump and a post-grinding material conveying pipe; the water outlet of the dewatering curved sieve is connected with a water return tank, the bottom outlet of the water return tank is connected with the top water inlet of the corn conveying tank through a water return tank bottom flow pipe, and the overflow port of the water return tank is connected with the water inlet of the fiber washing device through a water return tank overflow pipe; the inlets of the degerming mill and the pin mill are respectively connected with a process water pipe. The soaked corn discharged from the soaked corn output pipe enters a dewatering curved screen for dewatering, the dewatered corn enters a corn buffer tank for temporary storage, then enters a degerming mill for degerming milling, then enters a needle mill for fine milling, the fine milled material enters a post-milling storage tank for storage, and is pumped out by a screening conveying pump, and is sent into a fiber washing device for screening washing through a post-milling material conveying pipe. The water separated from the dewatering curved screen enters a water return tank to be collected, overflow water of the water return tank flows to a fiber washing device for recycling through an overflow pipe of the water return tank, and underflow of the water return tank is sent to a corn buffer tank for recycling through a bottom flow pipe of the water return tank. The water needed in the degerming mill and the needle mill grinding process is from the process water generated by the system, and the collected water is sent out by a process water pipe. Because the corn husks are destroyed after the dry embryo extraction, the corn husks can be finely ground after being soaked by an enzyme method and only subjected to primary embryo removal grinding, compared with the traditional technology, the secondary crushing is omitted, the water flow of the subsequent recovery process is used for the previous process, the water consumption is greatly reduced, and meanwhile, the sewage discharge is greatly reduced.

As a further improvement of the invention, the protein concentration device comprises a thin gluten storage tank, a concentrated gluten storage tank and a concentrator, wherein an overflow port of the disc centrifuge is connected with an inlet of the thin gluten storage tank through a centrifuge overflow pipe, a bottom outlet of the thin gluten storage tank is connected with an inlet of a thin gluten conveying pump, an outlet of the thin gluten conveying pump is connected with a feed inlet of the concentrator through a thin gluten conveying pipe, a discharge port of the concentrator is connected with an inlet of a concentration discharge distributor, a first outlet of the concentration discharge distributor is connected with an inlet of the concentrated gluten storage tank through a concentrator discharge pipe, a bottom outlet of the concentrated gluten storage tank is connected with an inlet of the concentrated gluten conveying pump, and an outlet of the concentrated gluten conveying pump is connected with the concentrated gluten conveying pipe; the second outlet of the concentrated discharging distributor is connected with the reflux port of the thin gluten storage tank through a concentrator reflux pipe, and the third outlet of the concentrated discharging distributor is connected with a protein concentrated drain pipe; the water outlet of the thickener is connected with the inlet of the process water tank through the protein concentration drain pipe, the bottom of the process water tank is connected with the inlet of the process water pump, and the outlet of the process water pump is connected with the process water pipe. The protein concentration in the diluted gluten overflowed from the disc centrifuge is 15g/l, the diluted gluten enters a diluted gluten storage tank through an overflow pipe of the centrifuge, is pumped out by a diluted gluten conveying pump, is sent into a rotary filter for filtering by a diluted gluten conveying pipe, and the filtered diluted gluten enters a thickener for concentration, and is separated by utilizing the difference of specific gravity of the protein and water, so that the protein concentration reaches 90-110 g/l. The concentrated gluten flowing out from the discharge hole of the thickener enters a concentrated gluten storage tank through a concentrated discharge distributor and a discharge pipe of the thickener, is pumped out by a concentrated gluten delivery pump, and enters a concentrated gluten delivery pipe to flow out after being cooled by a heat exchanger I. At the beginning of the operation of the thickener, the concentration of the discharged material is low, and the discharged material returns to the dilute gluten storage tank for circulation through the return pipe of the thickener. The drainage produced by the operation of the thickener or the test machine is discharged into a process water tank through a protein concentration drain pipe, pumped by a process water pump to enter a process water pipe, and sent to a degerming mill and a pin mill from the process water pipe for recycling. Impurities discharged by the rotary filter and water leakage of the thickener enter a concentrating section discharge pipe, and return to the fiber washing device from the concentrating section discharge pipe for recycling.

As a further improvement of the invention, the protein dewatering and drying device comprises a vacuum rotary drum suction filter, wherein the outlet of the concentrated gluten conveying pipe is connected with the feed inlet of the vacuum rotary drum suction filter, the discharge outlet of the vacuum rotary drum suction filter is connected with a wet protein output pipe, and the outlet of the wet protein output pipe is connected with the feed inlet of the protein tube bundle dryer; the bottom outlet of the dilute gluten storage tank is also connected with the inlet of a drum washing water pump, and the outlet of the drum washing water pump is connected with the backwash inlet of the vacuum drum suction filter through a suction filter backwash inlet pipe; the backwash outlet of the vacuum rotary drum suction filter is connected with the inlet of the thin gluten storage tank through a backwash outlet pipe of the suction filter. And (3) after the concentrated protein solution flows out of the concentrated gluten conveying pipe, the concentrated protein solution enters a vacuum rotary drum suction filter for dehydration, filter cloth attached to the outer surface of the hollow rotary drum is used as a filter medium, the protein solution with the concentration of 90-110 g/l is dehydrated to the concentration of 55-60% of water, and the protein solution is discharged through a wet protein output pipe and enters a protein tube bundle dryer for drying. The rotary drum washing pump pumps out the thin gluten in the thin gluten storage tank, and sends the thin gluten into a backwash inlet of the vacuum rotary drum suction filter through a backwash inlet pipe of the suction filter to clean filter cloth, and drainage water for washing the filter cloth returns to the thin gluten storage tank through a backwash outlet pipe of the suction filter, so that the treatment capacity of the thickener is not increased.

As a further improvement of the invention, a vacuum suction port of the vacuum drum suction filter is connected with an inlet of a vacuum tank, a bottom outlet of the vacuum tank is connected with an inlet of a suction water pump, an outlet of the suction water pump is connected with a suction water outlet pipe I and a suction water outlet pipe II, an outlet of the suction water outlet pipe I is connected with an inlet of the dilute gluten storage tank, and an outlet of the suction water outlet pipe II is connected with an inlet of the process water tank; the top outlet of the vacuum tank is connected with the vacuumizing port of the vacuum pump, the water outlet of the vacuum pump is connected with the inlet of the circulating water tank of the vacuum pump through the water outlet pipe of the vacuum pump, the outlet of the circulating water tank of the vacuum pump is connected with the inlet of the circulating water pump of the vacuum pump, and the outlet of the circulating water pump of the vacuum pump is connected with the water inlet of the vacuum pump through the water inlet pipe of the vacuum pump; and the overflow port and the discharge port of the vacuum rotary drum suction filter are connected with the inlet of the concentrated gluten storage tank through a vacuum rotary drum overflow discharge pipe. Under the suction action of the vacuum pump, the protein is intercepted on the filter cloth, the liquid phase enters the vacuum tank, the water in the vacuum tank is pumped out by the suction filtration water pump, and is sent into the dilute gluten storage tank for recycling through the suction filtration water outlet pipe I, or is sent into the process water tank for recycling through the suction filtration water outlet pipe II. The water outlet of the water ring type vacuum pump enters the vacuum pump circulating water tank through the vacuum pump water outlet pipe, is pumped out by the vacuumizing circulating water pump, and returns to the water inlet of the vacuum pump for recycling through the vacuum pump water inlet pipe after being cooled by the heat exchanger II. The overflowed and discharged liquid phase of the vacuum drum suction filter is returned to the concentrated gluten storage tank through a vacuum drum overflow discharge pipe for recycling.

Drawings

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

FIG. 1 is a flow chart of a corn starch processing system of the present invention.

FIG. 2 is a system diagram of an embryo extracting device according to the present invention.

FIG. 3 is a system diagram of a germ drying apparatus of the present invention.

FIG. 4 is a system diagram of an enzymatic soaking device according to the invention.

Fig. 5 is a system diagram of a crushing device according to the invention.

FIG. 6 is a system diagram of a protein concentration apparatus according to the present invention.

FIG. 7 is a system diagram of a protein dehydrator dryer according to the present invention.

In the figure: 1. a first bucket elevator; 2. a stone remover; 3. a permanent magnet cylinder; 4. corn flow balance; 5. temporary corn storage bins; 6. a corn conveyor; 7. a water wetting machine; 8. a second bucket elevator; 9. a water wetting tank; 10. a water-wetting tank conveyor; 11. thirdly, a bucket elevator; 12. a degerming machine; 13. a pulse dust collector I; 14. a pulse dust collector II; 15. a germ tube bundle dryer; 16. a germ air seal device; 17. germ brake dragon; 18. a germ bin; 18a, a germ packaging scale; 19. a dryer brake dragon; 20. a soaking tank; 20a, a corn outlet of a soaking tank; 20b, a corn steep liquor outlet of the soaking tank; 21. a jacket heater; 22. a corn conveying tank; 23. a dewatering curved screen; 24. a corn buffer tank; 25. a water return tank; 26. degerming mill; 27. needle mill; 28. a storage tank after grinding; 29. a thin gluten tank; 30. rotating the filter; 31. a thickener; 31a, a concentrated discharge distributor; 32. a concentrated gluten tank; 33. a first heat exchanger; 34. a process water tank; 35. a vacuum drum suction filter; 36. a vacuum tank; 37. a vacuum pump circulating water tank; 38. a second heat exchanger; F1. pulse dust collector exhaust fan I; F2. pulse dust collector exhaust fan two; F3. germ brake dragon exhaust fan; F4. a dryer brake Kelong exhaust fan; F5. an exhaust fan of the crushing section; B1. a soaking tank circulating pump; B2. a corn delivery pump; B3. screening a conveying pump; B4. a dilute gluten delivery pump; B5. a concentrated gluten delivery pump; B6. a process water pump; B7. a drum water washing pump; B8. suction filtration water pump; B9. a vacuum pump; B10. a vacuum pumping circulating water pump; G1. a wet germ output pipe; G2. a corn grits output pipe; G3. a germ air supply pipe; G4. a steam pipe; G5. a condenser water pipe; G6. a germ return line; G7. a dry tail gas discharge pipe; G8. an enzyme preparation tube; G9. a thin corn steep liquor output pipe; G10. a return pipe of the soaking tank; G11. soaking a corn output pipe; G12. an overflow pipe of the backwater tank; G13. a backwater tank bottom flow pipe; G14. a process water pipe; G15. a ground material conveying pipe; G16. an overflow pipe of the centrifugal machine; G17. a thin gluten delivery tube; G18. a concentrated gluten delivery tube; G19. a thickener discharge pipe; G20. a thickener return pipe; G21. a protein concentration drain pipe; G22. a wet protein output tube; G23. backwashing an inlet pipe of the suction filter; G24. backwashing outlet pipe of suction filter; G25. a vacuum drum overflow drain; G26. a vacuum pump inlet pipe; G27. a vacuum pump outlet; G28. suction filtration is carried out on the first water outlet pipe; G29. a second suction filtration water outlet pipe; G30. a concentrating section bleed line; G31. a cooling tower downcomer; G32. and a water supply pipe of the cooling tower.

Detailed Description

As shown in fig. 1, the corn starch processing system of the invention comprises an embryo extracting device, wherein an embryo outlet of the embryo extracting device is connected with an inlet of an embryo drying device, and an outlet of the embryo drying device is connected with an embryo packaging mechanism; the corn grits outlet of the germ extraction device is connected with the inlet of the metering device, the outlet of the metering device is connected with the feed inlet of the enzymatic soaking device, the corn outlet of the enzymatic soaking device is connected with the feed inlet of the crushing device through the soaked corn output pipe G11, the discharge outlet of the crushing device is connected with the feed inlet of the fiber washing device, the oversize outlet of the fiber washing device is connected with the feed inlet of the fiber dewatering and drying device, the discharge outlet of the fiber dewatering and drying device is connected with the feed inlet of the fiber drying device, and the discharge outlet of the fiber drying device is connected with the fiber packaging mechanism.

The embryo is firstly extracted by the embryo extracting device, the extracted embryo is solid, the moisture content is about 15%, and then the embryo is dried by the embryo drying device until the moisture content is 7%, so that embryo dehydration equipment is reduced, drying equipment is greatly reduced, steam consumption is also reduced, and the embryo is packaged into a finished embryo product by the embryo packaging mechanism. The corn grits after embryo extraction are metered and then enter an enzymatic soaking device, soaking is carried out by using soaking enzyme, and the soaking time can be controlled within 10 hours as the corn husks after embryo extraction are destroyed, and the soaking temperature is 28-32 ℃. The protein net of the soaked corn kernels is destroyed, so that the starch particles wrapped by the protein net are free, thereby being beneficial to separating fibers from protein; then the soaked corns are crushed by a crushing device, and then 1.2 times of process water is added to crush the corns into about twelve pieces. The broken corn enters a fiber washing device to carry out seven-stage countercurrent screening washing, fibers are left on a screen, starch and protein are washed under the screen, corn fibers enter from a first stage, process water enters from a seventh stage, finally fibers are discharged from the seventh stage, after the starch is washed by the process water, the concentration becomes high to starch milk, and the starch milk is discharged from the first stage. The washed fiber contains about 90 percent of water, the fiber water is extruded to about 62 percent by a wringing machine, and then enters a tube bundle dryer for drying, and the dried fiber water is about 10 percent and is packaged into a fiber finished product by a fiber packaging mechanism.

The soaking liquid outlet of the enzyme method soaking device is connected with the inlet of the evaporation concentration device, and the outlet of the evaporation concentration device is connected with the corn steep liquor inlet of the fiber drying device. As the corn pulp is soaked by adopting an enzyme method, the pulp yield of each ton of corn is greatly reduced, and each ton of corn pulp is 0.3 ton of thin corn pulp with the concentration of about 5%, the thin corn pulp is concentrated by an evaporation concentration device, the concentration of the concentrated corn pulp reaches about 43%, the concentrated corn pulp is added into dried fibers, and the dried fibers are dried by a tube bundle dryer to form 10% pulp-added fibers, so that the corn pulp is recovered, the quality of the fibers is improved, and the added value of products is improved.

The undersize outlet of the fiber washing device is connected with the feed inlet of a disc centrifuge, the overflow port of the disc centrifuge is connected with the feed inlet of a protein concentration device through a thin gluten overflow pipe, the discharge port of the protein concentration device is connected with the feed inlet of a protein dehydration drying device, and the discharge port of the protein dehydration drying device is connected with a protein packaging mechanism. The starch washed by the fiber washing device contains protein, the protein is separated by a disk centrifuge, the disk centrifuge utilizes different specific gravities, the starch has large specific gravity, the underflow is taken, and the concentration of the underflow starch milk is 16 Baume degrees. The protein volume weight is small, overflow is carried out, the concentration of overflow protein is 15g/l, the overflow protein enters a protein concentration device from a thin gluten overflow pipe to be concentrated to 90-110 g/l, then the moisture of the protein is reduced to 10% by a protein dehydration drying device, and the protein is packaged into a protein finished product by a protein packaging mechanism.

The underflow outlet of the disc centrifuge is connected with the feeding port of the starch refining device, the starch milk outlet of the starch refining device is connected with the feeding port of the starch milk dewatering device, the discharging port of the starch milk dewatering device is connected with the inlet of the starch drying device, and the outlet of the starch drying device is connected with the starch packaging mechanism. The concentration of the underflow starch milk is 16 Baume degrees, the protein content is 3.5%, the underflow starch milk enters a starch refining device, the starch refining device generally adopts a 12-stage washing cyclone, fresh water enters from a final-stage washing cyclone by adopting a countercurrent washing principle, overflow of each stage cyclone returns step by step as washing water of a previous stage, starch can be fully recovered, the starch yield is improved, and the consumption of primary fresh water is reduced. The overflow of the first-stage washing cyclone enters a starch and gluten separator for re-separation. After refining, the concentration of the starch milk is increased to 20-22 Baume degrees, and the protein content is reduced to below 0.4%.

The process water outlet of the fiber dewatering and drying device is connected with the water inlet of the fiber washing device, and the process water generated by fiber dewatering is directly returned to the fiber washing device for recycling.

The overflow outlet of the starch refining device is connected with the feed inlet of the disc centrifuge, so that overflow water of the starch refining device returns to the disc centrifuge for re-separation, and starch in the overflow is recovered.

The siphon water outlet of the starch milk dehydration device is connected with the water inlet of the starch refining device, so that the process water generated by the starch milk dehydration is returned to the starch refining device for use.

The starch milk outlet of the starch refining device can be sequentially connected with a starch milk size mixing device, a liquefying device, a saccharifying device, a filtering device, a decoloring device, an ion exchange device and an evaporating device, and the outlet of the evaporating device is connected with a glucose filling mechanism; the filtrate outlet of the filtering device is connected with the feed inlet of the protein dehydration drying device. The refined starch milk can also be used for preparing sugar, and glucose is prepared by sequentially performing starch milk size mixing, liquefying, saccharification, filtering, decoloring, ion exchange and evaporation, and is filled and sold by a glucose filling mechanism; in the sugar manufacturing process, a small amount of protein obtained by filtration enters a protein dehydration drying device for recycling, so that the added value of the product is improved.

As shown in fig. 2, the germ extraction device comprises a bucket elevator 1 for lifting new corns, wherein the outlet of the bucket elevator 1 is connected with the inlet of a destoner 2, the outlet of the destoner 2 is connected with the inlet of a permanent magnet cylinder 3, the outlet of the permanent magnet cylinder 3 is connected with the inlet of a temporary corn storage bin 5, the outlet of the temporary corn storage bin 5 is provided with a corn conveyor 6, the outlet of the corn conveyor 6 is connected with the inlet of a water wetting machine 7, the outlet of the water wetting machine 7 is connected with the inlet of a bucket elevator 8, the outlet of the bucket elevator 8 is connected with the inlet of a water wetting tank 9, the outlet of the water wetting tank 9 is connected with the inlet of a water wetting tank conveyor 10, the outlet of the water wetting tank conveyor 10 is connected with the inlet of a bucket elevator three 11, the outlet of the bucket elevator three 11 is connected with the inlet of a germ removing machine 12, the germ outlet of the upper end of the germ removing machine 12 is connected with a wet germ output tube G1, and the corn grits outlet of the bottom of the germ removing machine 12 is connected with a corn grits output tube G2.

The corn is lifted to a high position by a bucket elevator 1, firstly, impurities such as sediment, stones and the like are removed by a stone removing machine 2, then, metal objects such as iron nails, iron sheets or screws and the like are removed by a permanent magnet cylinder 3, then, the materials are weighed by a corn flow scale 4, enter a temporary corn storage bin 5 for temporary storage, are sent out by a corn conveyor 6, are added with water by a water wetting machine 7, so that the water content of the corn is improved to about 18%, are lifted by a bucket elevator 8 and then are sent into a water wetting tank 9, are placed for about 12 hours, so that germs are fully absorbed by water, are discharged by a water wetting tank conveyor 10, are lifted to a high position by a bucket elevator III 11, and are then extracted by a embryo removing machine 12; the extracted solid embryo is discharged from the wet embryo output pipe G1, the embryo yield can reach 7%, the embryo purity is more than 70%, the embryo water content is about 15%, and then the embryo is dried by the embryo drying device until the water content is 7%, so that embryo dehydration equipment is reduced, drying equipment is greatly reduced, and steam consumption is also reduced. The corn grits after the germ extraction are discharged from the corn grits output pipe G2.

Dust generated by the stone remover 2 and the corn flow scale 4 enters the pulse dust remover I13 to remove dust, and is extracted and discharged by the pulse dust remover exhaust fan I F1. Dust generated by the degerming machine 12 enters the pulse dust collector II 14 to remove dust, and is extracted and discharged by the pulse dust collector exhaust fan II F2.

As shown in fig. 3, the germ drying device comprises a germ tube bundle dryer 15, wherein a feeding port of the germ tube bundle dryer 15 is connected with a germ outlet of the germ extraction device, a discharging port of the germ tube bundle dryer 15 is connected with a germ air supply pipe G3 through a germ air seal 16, a discharging port of the germ air supply pipe G3 is connected with a feeding port of a germ brake 17, and a discharging port of the germ brake 17 is connected with an inlet of a germ bin 18; the top air outlet of the germ brake dragon 17 is connected with the inlet of the germ brake dragon exhaust fan F3, and the outlet of the germ brake dragon exhaust fan F3 is connected with the reflux port of the germ tube bundle dryer 15 through a germ reflux pipe G6; the top air outlet of germ tube bundle dryer 15 links to each other with the air intake of desiccator brake Kelong 19, and the top air outlet of desiccator brake Kelong 19 links to each other with the entry of desiccator brake Kelong air exhauster F4, and the export of desiccator brake Kelong air exhauster F4 links to each other with dry tail gas discharge pipe G7.

The wet embryo enters a feeding port of the embryo tube bundle dryer 15 from the wet embryo output tube G1, steam enters from the steam tube G4, the moisture content of the embryo is dried from 15% to 7%, the heat of the steam is released to become condensed water, and the condensed water is discharged from the condensed water tube G5; the dry embryo enters an embryo air delivery pipe G3 through an embryo air seal 16, is delivered into an embryo clerestory 17 through the embryo air delivery pipe G3, is discharged into an embryo storage bin 18, and then enters an embryo packing scale 18a from a bottom discharge hole of the embryo storage bin 18 to be packed into an embryo finished product. The pulse dust collector is canceled on the germ air delivery pipe G3, so that the equipment investment cost is reduced; the tail gas discharged from the top of the germ brake dragon 17 contains a small amount of germs, and the germs are returned to the germ tube bundle dryer 15 for recovery through the germ return pipe G6 under the suction of the germ brake dragon exhaust fan F3, so that the yield of the germs is improved, the tail gas emission is reduced, the inlet air of the germ tube bundle dryer 15 is changed from cold air to hot air, the heat in the exhaust air is completely recovered, and the energy consumption is greatly reduced. The wet tail gas discharged from the top of the germ tube bundle dryer 15 enters a dryer brake dragon 19 for separation and dust removal, and is pumped out by a dryer brake dragon exhaust fan F4 to enter a washing tower or discharged to the atmosphere.

As shown in fig. 4, the enzymatic soaking device comprises a soaking tank 20 and a corn conveying tank 22, wherein a soaking tank material inlet, a soaking tank enzyme preparation inlet and a soaking tank reflux port are arranged at the top of the soaking tank 20, the soaking tank material inlet is connected with a corn grits outlet of the embryo extraction device, the soaking tank enzyme preparation inlet is connected with an outlet of an enzyme preparation pipe G8, a soaking tank corn outlet 20a and a soaking tank corn slurry outlet 20B are arranged at the bottom of the soaking tank, the soaking tank corn outlet 20a is connected with a top feed inlet of the corn conveying tank 22, a bottom discharge port of the corn conveying tank 22 is connected with an inlet of a corn conveying pump B2, and an outlet of the corn conveying pump B2 is connected with a soaked corn output pipe G11; the corn steep liquor outlet 20B of the soaking tank is connected with the inlet of the circulating pump B1 of the soaking tank, and the outlet of the circulating pump B1 of the soaking tank is connected with the bottom feed inlet of the jacket heater 21; the top discharge port of the jacket heater 21 is connected with a thin corn steep liquor output pipe G9 and a soaking tank reflux pipe G10, the outlet of the thin corn steep liquor output pipe G9 is connected with the feed inlet of the evaporator, and the outlet of the soaking tank reflux pipe G10 is connected with the soaking tank reflux inlet.

Discharging the corn grits after the embryo extraction from the corn grits output pipe G2, and entering a soaking tank; the enzyme preparation is discharged from the enzyme preparation pipe G8 and also enters a soaking tank to be soaked with the corn grits, so that the protein net of the corn grains is destroyed, and the starch grains wrapped by the protein net are free, thereby being beneficial to separating fibers from protein. The soaked corn kernels are discharged from the corn outlet 20a of the soaking tank, enter the corn conveying tank 22, and are conveyed into the dewatering curved screen 23 by the corn conveying pump B2 along with water flow. Corn steep liquor generated after soaking is discharged from a corn steep liquor outlet 20B of the soaking tank, is sent into a jacket heater 21 by a soaking tank circulating pump B1 to be heated in a middle way, one part of the heated corn steep liquor is returned to the soaking tank for circulation through a soaking tank return pipe G10, and the other part of the corn steep liquor is sent out through a thin corn steep liquor output pipe G9, and is concentrated by an evaporator to be subjected to fiber slurry pouring. The jacket heater 21 uses steam as a heat source, and the steam releases heat to become condensed water, which is discharged from the condensed water pipe G5. The corn grits after embryo extraction are soaked by the enzyme preparation, the soaking time can be controlled within 10 hours, the soaking temperature is 28-32 ℃, the steam consumption can be reduced, and the number and the volume of soaking tanks are also greatly reduced.

As shown in fig. 5, the crushing device comprises a degerming mill 26 and a pin mill 27, an outlet of a soaked corn output pipe G11 is connected with a feed inlet of a dewatering curved sieve 23, a material outlet of the dewatering curved sieve 23 is connected with an inlet of a corn buffer tank 24, an outlet of the corn buffer tank 24 is connected with an inlet of the degerming mill 26, an outlet of the degerming mill 26 is connected with an inlet of the pin mill 27, an outlet of the pin mill 27 is connected with a feed inlet of a post-grinding storage tank 28, and an outlet of the post-grinding storage tank 28 is connected with a feed inlet of the fiber washing device through a screening conveying pump B3 and a post-grinding material conveying pipe G15; the water outlet of the dewatering curved screen 23 is connected with a water return tank 25, the bottom outlet of the water return tank 25 is connected with the top water inlet of the corn conveying tank 22 through a water return tank bottom flow pipe G13, and the overflow port of the water return tank 25 is connected with the water inlet of the fiber washing device through a water return tank overflow pipe G12; the inlets of the degerming mill 26 and the pin mill 27 are connected to the process water pipe G14, respectively.

The soaked corns discharged from the soaked corns output pipe G11 enter a dewatering curved screen 23 for dewatering, the dewatered corns enter a corn buffer tank 24 for temporary storage, then enter a degerming mill 26 for degerming milling, enter a pin mill 27 for fine milling, and the fine milled materials enter a post-milling storage tank 28 for storage and are pumped out by a screening conveying pump B3, and are sent into a fiber washing device for screening washing through a post-milling material conveying pipe G15. The water separated from the dewatering curved screen 23 enters a water return tank 25 for collection, overflow water of the water return tank 25 flows to a fiber washing device for recycling through a water return tank overflow pipe G12, and bottom flow of the water return tank 25 is sent to a corn buffer tank 24 for recycling through a water return tank bottom flow pipe G13. The water required in the grinding process of the degerming mill 26 and the pin mill 27 is from the process water generated by the system, and is sent out from the process water pipe G14 after being collected. Because the corn husks are destroyed after the dry embryo extraction, the corn husks can be finely ground after being soaked by an enzyme method and only subjected to primary embryo removal grinding, compared with the traditional technology, the secondary crushing is omitted, the water flow of the subsequent recovery process is used for the previous process, the water consumption is greatly reduced, and meanwhile, the sewage discharge is greatly reduced.

The exhaust port at the upper part of the dewatering curved screen 23 and the exhaust hood above the corn buffer tank 24 are connected with the crushing section exhaust fan F5, and the tail gas is extracted and discharged by the crushing section exhaust fan F5.

As shown in fig. 6, the protein concentration device comprises a thin gluten storage tank 29, a concentrated gluten storage tank 32 and a concentrator 31, wherein an overflow port of a disc centrifuge is connected with an inlet of the thin gluten storage tank 29 through a centrifuge overflow pipe G16, a bottom outlet of the thin gluten storage tank 29 is connected with an inlet of a thin gluten delivery pump B4, an outlet of the thin gluten delivery pump B4 is connected with a feed port of the concentrator 31 through a thin gluten delivery pipe G17, a discharge port of the concentrator 31 is connected with an inlet of a concentrated discharge distributor 31a, a first outlet of the concentrated discharge distributor 31a is connected with an inlet of the concentrated gluten storage tank 32 through a concentrator discharge pipe G19, a bottom outlet of the concentrated gluten storage tank 32 is connected with an inlet of a concentrated gluten delivery pump B5, and an outlet of the concentrated gluten delivery pump B5 is connected with a concentrated gluten delivery pipe G18; the second outlet of the concentrated discharge distributor 31a is connected with the reflux port of the thin gluten storage tank 29 through a concentrator reflux pipe G20, and the third outlet of the concentrated discharge distributor 31a is connected with a protein concentrated drain pipe G21; the water outlet of the thickener 31 is connected with the inlet of the process water tank 34 through a protein concentration drain pipe G21, the bottom of the process water tank 34 is connected with the inlet of a process water pump B6, and the outlet of the process water pump B6 is connected with a process water pipe G14.

The protein concentration in the diluted gluten overflowed from the disc centrifuge is 15G/l, the diluted gluten enters the diluted gluten storage tank 29 through the overflow pipe G16 of the centrifuge, is pumped out by the diluted gluten conveying pump B4, is sent into the rotary filter 30 for filtration through the diluted gluten conveying pipe G17, and the filtered diluted gluten enters the thickener 31 for concentration, and is separated by utilizing the difference of specific gravity of the protein and water, so that the protein concentration reaches 90-110G/l. The concentrated gluten flowing out from the discharge port of the thickener enters a concentrated gluten storage tank 32 through a concentrated discharge distributor 31a and a concentrated discharge pipe G19, is pumped out by a concentrated gluten delivery pump B5, is cooled by a first heat exchanger 33, and enters a concentrated gluten delivery pipe G18 to flow out. At the beginning of the operation of the thickener 31, the concentration of the discharged material is still low, and the discharged material is returned to the thin gluten storage tank 29 for circulation through the thickener return pipe G20. The drainage generated by the operation of the thickener 31 or the test machine is discharged into the process water tank 34 through the protein concentration drainage pipe G21, pumped out into the process water pipe G14 by the process water pump B6, and sent to the degerming mill 26 and the pin mill 27 from the process water pipe G14 for recycling. Impurities discharged by the rotary filter 30 and water leakage of the thickener 31 enter a concentrating section discharge pipe G30, and return to the fiber washing device from the concentrating section discharge pipe G30 for recycling.

As shown in fig. 7, the protein dewatering and drying device comprises a vacuum rotary drum suction filter 35, wherein the outlet of a concentrated gluten conveying pipe G18 is connected with the feed inlet of the vacuum rotary drum suction filter 35, the discharge outlet of the vacuum rotary drum suction filter 35 is connected with a wet protein output pipe G22, and the outlet of the wet protein output pipe G22 is connected with the feed inlet of the protein tube bundle dryer; the bottom outlet of the dilute gluten storage tank 29 is also connected with the inlet of a rotary drum water washing pump B7, and the outlet of the rotary drum water washing pump B7 is connected with the backwash inlet of a vacuum rotary drum suction filter 35 through a suction filter backwash inlet pipe G23; the backwash outlet of the vacuum drum suction filter 35 is connected to the inlet of the dilute gluten storage tank 29 through a suction filter backwash outlet pipe G24.

The concentrated protein solution flows out of the concentrated gluten conveying pipe G18 and enters the vacuum rotary drum suction filter 35 for dehydration, filter cloth attached to the outer surface of the hollow rotary drum is used as a filter medium, the protein solution with the concentration of 90-110G/l is dehydrated to the concentration of 55-60%, and is discharged through the wet protein output pipe G22 and enters the protein tube bundle dryer for drying. The drum washing pump B7 pumps out the thin gluten in the thin gluten storage tank 29, and sends the thin gluten into a backwashing inlet of the vacuum drum suction filter 35 through a suction filter backwashing inlet pipe G23 to clean filter cloth, and drainage water for washing the filter cloth returns to the thin gluten storage tank 29 through a suction filter backwashing outlet pipe G24, so that the treatment capacity of the thickener 31 is not increased.

The vacuum suction port of the vacuum drum suction filter 35 is connected with the inlet of the vacuum tank 36, the bottom outlet of the vacuum tank 36 is connected with the inlet of the suction filter water pump B8, the outlet of the suction filter water pump B8 is connected with a suction filter water outlet pipe G28 and a suction filter water outlet pipe G29, the outlet of the suction filter water outlet pipe G28 is connected with the inlet of the dilute gluten storage tank 29, and the outlet of the suction filter water outlet pipe G29 is connected with the inlet of the process water tank 34; the top outlet of the vacuum tank 36 is connected with the vacuumizing port of the vacuum pump B9, the water outlet of the vacuum pump B9 is connected with the inlet of the vacuum pump circulating water tank 37 through the vacuum pump water outlet pipe G27, the outlet of the vacuum pump circulating water tank 37 is connected with the inlet of the vacuumizing circulating water pump B10, and the outlet of the vacuumizing circulating water pump B10 is connected with the water inlet of the vacuum pump B9 through the vacuum pump water inlet pipe G26; the overflow and discharge ports of the vacuum drum suction filter 35 are connected to the inlet of the concentrated gluten tank 32 through a vacuum drum overflow discharge pipe G25.

Under the suction action of the vacuum pump B9, the protein is intercepted on the filter cloth, the liquid phase enters the vacuum tank 36, the water in the vacuum tank 36 is pumped out by the suction-filtration water pump B8 and is sent into the thin gluten storage tank 29 for recycling through the suction-filtration water outlet pipe G28, or is sent into the process water tank 34 for recycling through the suction-filtration water outlet pipe G29. The water discharged by the water ring type vacuum pump B9 enters the vacuum pump circulating water tank 37 through the vacuum pump outlet pipe G27, is pumped out by the vacuumizing circulating water pump B10, is cooled by the second heat exchanger 38, and returns to the water inlet of the vacuum pump B9 through the vacuum pump water inlet pipe G26 for recycling. The overflowed and discharged liquid phase of the vacuum drum suction filter 35 is returned to the concentrated gluten storage tank 32 for recycling through the vacuum drum overflow discharge pipe G25.

The water inlets of the first heat exchanger 33 and the second heat exchanger 38 are connected with the cooling tower sewer pipe G31, the water outlet is connected with the cooling tower upper water pipe G32, and the cooling water is cooled by the cooling tower and then returns to the heat exchanger for recycling.

Compared with the traditional corn starch processing system, the power consumption is saved by 10-15%, the steam consumption is saved by about 8%, and the sewage discharge amount is reduced by more than 20%.

The foregoing description is only of a preferred embodiment of the invention and is not intended to limit the scope of the invention. In addition to the embodiments described above, other embodiments of the invention are possible. All technical schemes formed by equivalent substitution or equivalent transformation fall within the protection scope of the invention. The technical features of the present invention that are not described may be implemented by or using the prior art, and are not described herein.

Claims

1. The utility model provides a corn starch processingequipment, includes and carries embryo device, its characterized in that: the germ outlet of the germ extraction device is connected with the inlet of the germ drying device, and the outlet of the germ drying device is connected with the germ packaging mechanism; the corn grits outlet of the embryo extraction device is connected with the feed inlet of the enzymatic soaking device, the corn grits with broken corn husks after embryo extraction are soaked by soaking enzyme, the soaking time is controlled within 10 hours, and the soaking temperature is 28-32 ℃; the corn outlet of the enzymatic soaking device is connected with the feeding port of the crushing device through a corn soaking output pipe; the discharging port of the crushing device is connected with the feeding port of the fiber washing device, the oversize product outlet of the fiber washing device is connected with the feeding port of the fiber dewatering and drying device, the discharging port of the fiber dewatering and drying device is connected with the feeding port of the fiber drying device, and the discharging port of the fiber drying device is connected with the fiber packaging mechanism;

the process water outlet of the fiber dehydration drying device is connected with the water inlet of the fiber washing device, so that the process water generated by fiber dehydration directly returns to the fiber washing device for recycling;

the soaking liquid outlet of the enzymatic soaking device is connected with the inlet of the evaporation concentration device, and the outlet of the evaporation concentration device is connected with the corn steep liquor inlet of the fiber drying device;

The undersize outlet of the fiber washing device is connected with the feed inlet of a disc centrifuge, the overflow port of the disc centrifuge is connected with the feed inlet of a protein concentration device through a thin gluten overflow pipe, the discharge port of the protein concentration device is connected with the feed inlet of a protein dehydration drying device, and the discharge port of the protein dehydration drying device is connected with a protein packaging mechanism;

the underflow outlet of the disc centrifuge is connected with the feeding port of the starch refining device, the starch milk outlet of the starch refining device is connected with the feeding port of the starch milk dehydration device, the discharging port of the starch milk dehydration device is connected with the inlet of the starch drying device, and the outlet of the starch drying device is connected with the starch packaging mechanism;

the siphon water outlet of the starch milk dehydration device is connected with the water inlet of the starch refining device, so that the process water generated by the starch milk dehydration is returned to the starch refining device for use;

the overflow outlet of the starch refining device is connected with the feed inlet of the disc centrifuge, so that overflow water of the starch refining device returns to the disc centrifuge for re-separation, and starch in the overflow is recovered;

the enzymatic soaking device comprises a soaking tank and a corn conveying tank, wherein a soaking tank material inlet, a soaking tank enzyme preparation inlet and a soaking tank reflux inlet are formed in the top of the soaking tank, the soaking tank material inlet is connected with a corn grits outlet of the embryo extracting device, the soaking tank enzyme preparation inlet is connected with an enzyme preparation pipe outlet, a soaking tank corn outlet and a soaking tank corn slurry outlet are formed in the bottom of the soaking tank, the soaking tank corn outlet is connected with a top feeding port of the corn conveying tank, a bottom discharging port of the corn conveying tank is connected with an inlet of a corn conveying pump, and an outlet of the corn conveying pump is connected with a soaking corn output pipe; the corn steep liquor outlet of the soaking tank is connected with the inlet of the circulating pump of the soaking tank, and the outlet of the circulating pump of the soaking tank is connected with the bottom feed inlet of the jacket heater; the top discharge port of the jacket heater is connected with a thin corn steep liquor output pipe and a soaking tank return pipe, the outlet of the thin corn steep liquor output pipe is connected with the feed port of the evaporator, and the outlet of the soaking tank return pipe is connected with the soaking tank return port;

The crushing device comprises a degerming mill and a pin mill, the outlet of the soaked corn output pipe is connected with the feed inlet of the dewatering curved sieve, the material outlet of the dewatering curved sieve is connected with the inlet of the corn buffer tank, the outlet of the corn buffer tank is connected with the inlet of the degerming mill, the outlet of the degerming mill is connected with the inlet of the pin mill, the outlet of the pin mill is connected with the feed inlet of the post-grinding storage tank, and the outlet of the post-grinding storage tank is connected with the feed inlet of the fiber washing device through the screening conveying pump and the post-grinding material conveying pipe; the water outlet of the dewatering curved sieve is connected with a water return tank, the bottom outlet of the water return tank is connected with the top water inlet of the corn conveying tank through a water return tank bottom flow pipe, and the overflow port of the water return tank is connected with the water inlet of the fiber washing device through a water return tank overflow pipe; the inlets of the degerming mill and the pin mill are respectively connected with a process water pipe.

2. The corn starch processing apparatus of claim 1, wherein: the starch milk outlet of the starch refining device is also sequentially connected with a starch milk size mixing device, a liquefying device, a saccharifying device, a filtering device, a decoloring device, an ion exchange device and an evaporating device, and the outlet of the evaporating device is connected with a glucose filling mechanism; and a filtrate outlet of the filtering device is connected with a feed inlet of the protein dehydration drying device.

3. The corn starch processing apparatus of claim 1, wherein: the germ extraction device comprises a bucket elevator I for lifting new corns, an outlet of the bucket elevator I is connected with an inlet of a stone removing machine, an outlet of the stone removing machine is connected with an inlet of a permanent magnet cylinder, an outlet of the permanent magnet cylinder is connected with an inlet of a temporary corn storage bin, a corn conveyor is arranged at an outlet of the temporary corn storage bin, an outlet of the corn conveyor is connected with an inlet of a water wetting machine, an outlet of the water wetting machine is connected with an inlet of a bucket elevator II, an outlet of the bucket elevator II is connected with an inlet of a water wetting tank, an outlet of the water wetting tank is connected with an inlet of the water wetting tank conveyor, an outlet of the water wetting tank conveyor is connected with an inlet of the bucket elevator III, an outlet of the germ at the upper end of the germ removing machine is connected with a wet germ output pipe, and a corn grits outlet at the bottom of the germ removing machine is connected with a corn grits output pipe.

4. The corn starch processing apparatus of claim 1, wherein: the germ drying device comprises a germ tube bundle dryer, a feeding port of the germ tube bundle dryer is connected with a germ outlet of the germ extraction device, a discharging port of the germ tube bundle dryer is connected with a germ air conveying pipe through a germ air seal, a discharging port of the germ air conveying pipe is connected with a feeding port of a germ brake, and a discharging port of the germ brake is connected with an inlet of a germ bin; the top air outlet of the germ brake dragon is connected with the inlet of the germ brake dragon exhaust fan, and the outlet of the germ brake dragon exhaust fan is connected with the reflux port of the germ tube bundle dryer through a germ reflux pipe; the top air outlet of the germ tube bundle dryer is connected with the air inlet of the dryer brake dragon, the top air outlet of the dryer brake dragon is connected with the inlet of the dryer brake dragon exhaust fan, and the outlet of the dryer brake dragon exhaust fan is connected with the drying tail gas discharge pipe.

5. The corn starch processing apparatus of claim 1, wherein: the protein concentration device comprises a thin gluten storage tank, a thick gluten storage tank and a concentrator, wherein an overflow port of the disc centrifuge is connected with an inlet of the thin gluten storage tank through a centrifuge overflow pipe, a bottom outlet of the thin gluten storage tank is connected with an inlet of a thin gluten conveying pump, an outlet of the thin gluten conveying pump is connected with a feed inlet of the concentrator through a thin gluten conveying pipe, a discharge port of the concentrator is connected with an inlet of a concentrated discharge distributor, a first outlet of the concentrated discharge distributor is connected with an inlet of the thick gluten storage tank through a concentrator discharge pipe, a bottom outlet of the thick gluten storage tank is connected with an inlet of the thick gluten conveying pump, and an outlet of the thick gluten conveying pump is connected with the thick gluten conveying pipe; the second outlet of the concentrated discharging distributor is connected with the reflux port of the thin gluten storage tank through a concentrator reflux pipe, and the third outlet of the concentrated discharging distributor is connected with a protein concentrated drain pipe; the water outlet of the thickener is connected with the inlet of the process water tank through the protein concentration drain pipe, the bottom of the process water tank is connected with the inlet of the process water pump, and the outlet of the process water pump is connected with the process water pipe.

6. The corn starch processing apparatus of claim 5, wherein: the protein dehydration drying device comprises a vacuum rotary drum suction filter, wherein the outlet of the concentrated gluten conveying pipe is connected with the feed inlet of the vacuum rotary drum suction filter, the discharge outlet of the vacuum rotary drum suction filter is connected with a wet protein output pipe, and the outlet of the wet protein output pipe is connected with the feed inlet of the protein tube bundle dryer; the bottom outlet of the dilute gluten storage tank is also connected with the inlet of a drum washing water pump, and the outlet of the drum washing water pump is connected with the backwash inlet of the vacuum drum suction filter through a suction filter backwash inlet pipe; the backwash outlet of the vacuum rotary drum suction filter is connected with the inlet of the thin gluten storage tank through a backwash outlet pipe of the suction filter.

7. The corn starch processing apparatus of claim 6, wherein: the vacuum drum suction filter comprises a vacuum drum, a vacuum tank, a suction pump, a suction water outlet pipe, a dilute gluten storage tank, a process water tank, a water pump and a water pump, wherein a vacuum suction port of the vacuum drum suction filter is connected with an inlet of the vacuum tank, a bottom outlet of the vacuum tank is connected with an inlet of the suction pump, an outlet of the suction pump is connected with the suction water outlet pipe I and the suction water outlet pipe II, an outlet of the suction water outlet pipe I is connected with the inlet of the dilute gluten storage tank, and an outlet of the suction water outlet pipe II is connected with the inlet of the process water tank; the top outlet of the vacuum tank is connected with the vacuumizing port of the vacuum pump, the water outlet of the vacuum pump is connected with the inlet of the circulating water tank of the vacuum pump through the water outlet pipe of the vacuum pump, the outlet of the circulating water tank of the vacuum pump is connected with the inlet of the circulating water pump of the vacuum pump, and the outlet of the circulating water pump of the vacuum pump is connected with the water inlet of the vacuum pump through the water inlet pipe of the vacuum pump; and the overflow port and the discharge port of the vacuum rotary drum suction filter are connected with the inlet of the concentrated gluten storage tank through a vacuum rotary drum overflow discharge pipe.