CN102816249B - Method and system for washing corn starch by reduced swirler separation - Google Patents
Method and system for washing corn starch by reduced swirler separation Download PDFInfo
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- CN102816249B CN102816249B CN201210323519.4A CN201210323519A CN102816249B CN 102816249 B CN102816249 B CN 102816249B CN 201210323519 A CN201210323519 A CN 201210323519A CN 102816249 B CN102816249 B CN 102816249B
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Abstract
The invention relates to a method and system for washing corn starch by reduced swirler separation. A three-stage diversion swirl system I is used for diverting crude starch milk, the protein solution from the top flow enters a three-stage diversion swirl system II, and through the three-stage diversion swirl system II, corn protein powder with the total protein content of 60-63% can be obtained only by refluxing instead of water treatment of the centrifuge. The invention uses 1.5 times of washing water consumption of the refluxing swirl method to achieve the goal of reducing the stages of swirlers on the premise of ensuring the washing effect. The invention greatly shortens the swirl washing time and the energy consumption of the swirl system; and the whole technique can shorten the swirl washing step time by 80% and reduce the energy for the swirl system by 72%.
Description
Technical field
The present invention relates to a kind of W-Gum protein isolate and washing process, and process water in technique processes and close circulation technology, relate in particular to a kind of method and system of decrement cyclonic separation washing W-Gum.
Background technology
In production of corn starch technique, after mill, riddler's order are extracted, obtain coarse starch milk, concentration is 10～12.5 ° Bx/20 DEG C (physics relative density is 1.040～1.051, contents on dry basis 10.23%～12.74%).Taking butt calculating composition as starch 89%～92%, protein 6%～8%, fat 0.5%～1%, solvend 0.1%～0.3%, ash content 0.2%～0.3%, thin slag 0.1g/L.
For this coarse starch milk, more general treatment process is to remove gluten protein through sedimentation centrifuge sedimentation at present, then remove the impurity such as residual insoluble and soluble protein, ash content, sulfurous acid by the rotational flow station countercurrent washing of 10～15 grades of swirlers, obtain 40～42 ° of final Bx essence starch milks.This " adverse current vortex method " become ripe washing starch technology, it is widely used in W-Gum industry, this method technological principle is simple, so at design and manufacture pipeline, starch Turo pump and overflow, underflow close to fasten and are tending towards ripe fixing, equipment cost and installation and debugging cost are also on a declining curve, but have a significant defect, owing to separating power consumption that progression causes more and problem consuming time.To produce 30 tons of starch equivalent weights daily, average every grade of swirler power consumption 10KWh, with the most widely used 12 stage countercurrent vortex methods at present, power consumption 120KWh per hour.And, due to protein on stream the time long, the environment of 40～45 DEG C is again the temperature of enlivening most of miscellaneous bacteria infection, so need to keep certain SO2 content to play germicidal action simultaneously, cause SO2 residual quantity in finished product starch and improve in order to the residual quantity of firing other non-metallic elements in the sulphur ore deposit of SO2.
Summary of the invention
The present invention is directed to above-mentioned problems of the prior art, through test of many times and equipment development, provide a kind of decrement cyclonic separation albumen to coordinate the method for dewatering system washing W-Gum, solved length consuming time and the high problem that consumes energy in prior art.
Another object of the present invention is to provide a kind of system of decrement cyclonic separation washing W-Gum.
Method of the present invention comprises the steps:
Step 1: the Baume concentration of coarse starch milk in total storage tank is adjusted into after 30～34 ° Bx/45 DEG C, is pressurizeed by starch Turo pump, enter cyclone separator W1;
Step 2: the top stream mixed solution of cyclone separator W1
tIfor, 4～8 ° of Bx of top stream concentration, protein butt mass percentage content 40%～50%, starch butt mass percentage content 50%～60%, top stream mixed solution
tItop stream mixed solution with cyclone separator W2
tII, cyclone separator W3 top stream mixed solution
tIIIinterflow, after mixing, enters cyclone separator W4, cyclone separator W5 and cyclone separator W6;
Step 3: the underflow mixed solution of cyclone separator W1
bIfor, 40～42 ° of Bx of underflow density, protein butt mass percentage content 0.4%～1%, starch butt mass percentage content 98.8%～99.4%, underflow mixed liquid B I is through pump blade type centrifugal discharging centrifuge dehydration, removes solubility and small molecular protein in the middle of moisture, after adding water and again adjusting degree Beaume to 30～34 ° Bx, enter cyclone separator W2, carry out second stage cyclonic separation;
Step 4: the underflow mixed solution of cyclone separator W2
bIImiddle protein contents on dry basis is reduced to 0.4%～0.6%, through adding water after dehydration, after adjusting for the third time degree Beaume to 30～34 ° Bx, enters cyclone separator W3, carries out third stage cyclonic separation;
Step 5: the top stream mixed solution after cyclone separator W3 separates
tIIIwith top stream mixed solution
tI, top stream mixed solution
tII, enter cyclone separator W4, cyclone separator W5, cyclone separator W6, underflow mixed solution
bI, underflow mixed solution
bIIand underflow mixed solution
bIIIin, the finished product starch milk that albumen butt mass percentage content is 0.2%～0.4%, enters baking operation and dries;
Step 6: the top stream mixed solution of cyclone separator W4, cyclone separator W5, cyclone separator W6
tIV, top stream mixed solution
tVand top stream mixed solution
tVIfor, the finished product Zein powder of starch butt mass percentage content 38% mixes breast, and Zein powder mixes breast through after centrifuge dehydration, enters baking operation, obtains finished product Zein powder;
Step 7: the underflow mixed solution of cyclone separator W4, cyclone separator W5, cyclone separator W6
bIV, underflow mixed solution
bVand underflow mixed solution
bVIbe back to total storage tank, wait for circulation cleaning.
Described cyclone separator W1, cyclone separator W2 and the underflow mixed solution of cyclone separator W3
bI, underflow mixed solution
bIIand underflow mixed solution
bIIIwater after dehydration, and all water through pump blade type centrifugal discharging centrifuge dehydration in technique, all add flocculation agent through ejector, and flocculating settling in process container for storing liquid, enters fine filtering step afterwards.
Separating centrifuge used in described fine filtering step, its filtration medium aperture 0.2 μ m, through the water after filtering, reclaims and is used as system wash water.By starch yield, production starch 30T per hour, need, after 144 hours, eliminate 5% systemic circulation water, adds new water and is in harmonious proportion.
In described step 2, protein butt mass percentage content is that mixed solution is flowed on top
tI> top stream mixed solution
tII> top stream mixed solution
tIII, top stream mixed solution
tIIImiddle protein butt mass percentage content is 22%.
In described step 3 and step 4, added water is the water refluxing after system is processed, and the water of backflow will ensure that pH value is stable at 4.3～4.7.
The cyclonic separation washing process temperature of W-Gum need keep 40～45 DEG C.
System architecture of the present invention is,
Cyclone separator W1, cyclone separator W2 and cyclone separator W3 mutually connect and form three level shunt eddy flow system I; Cyclone separator W4, cyclone separator W5 and cyclone separator W6 are mutually connected and are formed three level shunt eddy flow system II by " adverse current " form; Three level shunt eddy flow system I and three level shunt eddy flow system II connect; Three level shunt eddy flow system I are connected with total storage tank, process water tank and process container for storing liquid respectively with three level shunt eddy flow system II; Cyclone separator W1 is all connected with starch Turo pump and pump blade type centrifugal discharging centrifuge to cyclone separator W6.
Described process container for storing liquid is connected with separating centrifuge with ejector.
Described process water tank is connected with separating centrifuge with total storage tank.
Described cyclone separator W1 is all connected with and flows to valve and tensimeter to cyclone separator W6.
Advantageous effect of the present invention is as follows:
1, ensureing under the prerequisite of washing effect, reaching by having increased by 1.5 times of wash water consumptions to adverse current vortex method the object that reduces swirler progression.
2, do not add centrifugal settling operation, but directly use cyclone separator to separate coarse starch milk.
The adverse current eddy flow system that 3, can substitute ten Pyatyis, has significantly reduced the energy consumption of eddy flow washing time and eddy flow system.
4, the top of shunting stream mixing solutions, its dry biomass degree is only 10～12% of total dry matter mass percentage content, so, in order to the contracurrent system of washing shunting, though need 3 grades, but total power is only 10～12% of prior art total power, and main flow beyond shunting is reduced to 3 grades from 12 grades, and total power is 25% of prior art total power.
5, the cyclonic separation washing process of W-Gum need keep 40 DEG C, enlivens temperature, therefore the time is shorter and this temperature is foreign-bacteria active, the heat that lagging facility runs off is with regard to outside fewer, the probability that miscellaneous bacteria infects also diminishes, and whole technique, can reduce the eddy flow washing step time 80%.
Brief description of the drawings
Fig. 1 is system flow structural representation of the present invention.
In figure, 1, total storage tank, 2, starch Turo pump, 3, measurement controller, 4, pump blade type centrifugal discharging centrifuge, 5, ejector, 6, process container for storing liquid, 7, process water tank, P1, tensimeter, W1-W6, cyclone separator.
Embodiment
Embodiment
Method of the present invention comprises the steps:
Step 1: the Baume concentration of coarse starch milk in total storage tank is adjusted into after 30～34 ° Bx/45 DEG C, is pressurizeed by starch Turo pump, enter cyclone separator W1;
Step 2: the top stream mixed solution of cyclone separator W1
tIfor, 4～8 ° of Bx of top stream concentration, protein butt mass percentage content 40%～50%, starch butt mass percentage content 50%～60%, top stream mixed solution
tItop stream mixed solution with cyclone separator W2
tII, cyclone separator W3 top stream mixed solution
tIIIinterflow, after mixing, enters cyclone separator W4, cyclone separator W5 and cyclone separator W6; Protein butt mass percentage content is that mixed solution is flowed on top
tI> top stream mixed solution
tII> top stream mixed solution
tIII, top stream mixed solution
tIIImiddle protein butt mass percentage content is 22%.
Step 3: the underflow mixed solution of cyclone separator W1
bIfor, 40～42 ° of Bx of underflow density, protein butt mass percentage content 0.4%～1%, starch butt mass percentage content 98.8%～99.4%, underflow mixed solution
bIthrough pump blade type centrifugal discharging centrifuge dehydration, remove moisture central solubility and small molecular protein, the water that adding system refluxes after processing, the water refluxing will ensure that pH value is stable at 4.3～4.7, after again adjusting degree Beaume to 30～34 ° Bx, enter cyclone separator W2, carry out second stage cyclonic separation;
Step 4: the underflow mixed solution of cyclone separator W2
bIImiddle protein contents on dry basis is reduced to 0.4%～0.6%,, the water refluxing after adding system after dehydration is processed, the water of backflow will ensure that pH value is stable at 4.3～4.7, after adjusting for the third time degree Beaume to 30～34 ° Bx, enter cyclone separator W3, carry out third stage cyclonic separation;
Step 5: the top stream mixed solution after cyclone separator W3 separates
tIIIwith top stream mixed solution
tI, top stream mixed solution
tII, entering cyclone separator W4, cyclone separator W5, cyclone separator W6, W4, W5, W6 three swirler, be " adverse current vortex method " arrangement order; Underflow mixed solution
bI, underflow mixed solution
bIIand underflow mixed solution
bIIIin, the finished product starch milk that albumen butt mass percentage content is 0.2～0.4%, enters baking operation and dries;
Step 6: the top stream mixed solution of cyclone separator W4, cyclone separator W5, cyclone separator W6
tIV, top stream mixed solution
tVand top stream mixed solution
tVIfor, the finished product Zein powder of starch butt mass percentage content 40% mixes breast, and Zein powder mixes breast through after centrifuge dehydration, enters baking operation, obtains finished product Zein powder;
Step 7: the underflow mixed solution of cyclone separator W4, cyclone separator W5, cyclone separator W6
bIV, underflow mixed solution
bVand underflow mixed solution
bVIbe back to total storage tank, wait for circulation cleaning.
Water after described cyclone separator W1, cyclone separator W2 and the underflow mixed liquor I of cyclone separator W3, underflow mixed liquor I I and underflow mixed liquor I II dehydration, with all water through pump blade type centrifugal discharging centrifuge dehydration in technique, all add flocculation agent polyacrylamide through ejector, flocculating settling in process container for storing liquid, enters fine filtering step afterwards.
Separating centrifuge used in described fine filtering step, its filtration medium aperture 0.2 μ m, through the water after filtering, recovery is used as system wash water, by starch yield, and production starch 30T per hour, need, after 144 hours, eliminate 5% systemic circulation water, add new softening water and be in harmonious proportion.
The cyclonic separation washing process temperature of W-Gum need keep 40 DEG C.
System architecture of the present invention is,
Cyclone separator W1, cyclone separator W2 and cyclone separator W3 mutually connect and form three level shunt eddy flow system I; Cyclone separator W4, cyclone separator W5 and cyclone separator W6 mutually connect and form three level shunt eddy flow system II; Three level shunt eddy flow system I and three level shunt eddy flow system II connect; Three level shunt eddy flow system I are connected with total storage tank 1, process water tank 7 and process container for storing liquid 6 respectively with three level shunt eddy flow system II; Cyclone separator W1 is all connected with starch Turo pump, pump blade type centrifugal discharging centrifuge, flows to valve and tensimeter to cyclone separator W6.Described process container for storing liquid 6 is connected with pump blade type centrifugal discharging centrifuge with ejector 5.Described process water tank 7 is connected with pump blade type centrifugal discharging centrifuge with total storage tank 1.
principle of work of the present invention is as follows:
Decrement vortex method of the present invention is for traditional adverse current vortex method, every grade of swirler is all equivalent to the final stage swirler of adverse current vortex method---that is to say, what add after charging is the subsystem by enrolling whole washing system---filter the water purification of return-flow system instead of the next stage overflow water containing impurity such as albumen, and the starch milk of underflow, also need through dehydration with after removing as far as possible solubility or small molecular weight impurity contained in water, add again wash water, enter subordinate's charging.
As shown in the figure, so-called decrement eddy flow carries out " shunting " by three level shunt eddy flow system I to coarse starch milk.The top stream mixing solutions of shunting, its dry biomass degree is only 10～12% of total dry matter mass percentage content, so in order to the contracurrent system of washing shunting, though need three grades, total power is only 10～12% of prior art total power.And the protein soln that top flow point flows out, no longer enter system I, but because its dry-matter starch contained therein content still has 50%～58%, so still need to enter three level shunt eddy flow system II of conventional counter-current method composition, in three level shunt eddy flow system II, dry-matter total content is 12%～18%, therefore power consumption reduces, participate in water treatment without separating centrifuge, only need adverse current.Finally obtain total protein content and be 60%～63% Zein powder, after dewatered drying as maize gluten feed finished product.
By the shunting to the higher top stream of protein content, for the eddy flow of first stage provides the basic protein content condition that reduces eddy flow number of times, and every one-level is all the acid water purification washing using through albumen flocculation filtration treatment, and, three swirler device, every one-level underflow, through washing smart starch milk all after processed, separately add return-flow system water purification, be equivalent to the washing of a filteration, it is expelling water and rinsing, three grades of expelling water and rinsings add three swirler device, through experiment, can substitute the adverse current eddy flow system of ten Pyatyis completely, significantly reduce eddy flow washing time, energy consumption with eddy flow system.
The present invention washs rear starch quality standard test, protein content≤0.35%; Solvend≤0.02%.
Protein content kept stable, compared with existing adverse current eddy flow, has no increase and decrease and floats.But solubles content requires≤0.1% to reduce much than national standard, contained mineral substance in its starch, trace element, and SO
2residual quantity, be all minimized.
The key link that the present invention is different from traditional " adverse current vortex method " is, by shunting washing system I, coarse starch milk is divided into the top stream part of protein content 50% left and right and the underflow part of protein content 0.4%～1% left and right is divided two portions, so, by simplifying the carrying out washing treatment of eddy flow number of times to underflow part, and still use tradition " adverse current vortex method " to carry out carrying out washing treatment to top stream part, reduce the treatment time and reduce the object of processing power consumption thereby reach.
Claims (8)
1. a method for decrement cyclonic separation washing W-Gum, is characterized in that comprising the steps:
Step 1: the Baume concentration of coarse starch milk in total storage tank is adjusted into after 30～34 ° Bx/45 DEG C, is pressurizeed by starch Turo pump, enter cyclone separator W1;
Step 2: the top stream mixed solution of cyclone separator W1
tIfor, 4～8 ° of Bx of top stream concentration, protein butt mass percentage content 40%～50%, starch butt mass percentage content 50%～60%, top stream mixed solution
tItop stream mixed solution with cyclone separator W2
tII, cyclone separator W3 top stream mixed solution
tIIIinterflow, after mixing, enters cyclone separator W4, cyclone separator W5 and cyclone separator W6;
Step 3: the underflow mixed solution of cyclone separator W1
bIfor, 40～42 ° of Bx of underflow density, protein butt mass percentage content 0.4%～1%, starch butt mass percentage content 98.8%～99.4%, underflow mixed liquid B I is through pump blade type centrifugal discharging centrifuge dehydration, removes solubility and small molecular protein in the middle of moisture, after adding water and again adjusting degree Beaume to 30～34 ° Bx, enter cyclone separator W2, carry out second stage cyclonic separation;
Step 4: the underflow mixed solution of cyclone separator W2
bIImiddle protein contents on dry basis is reduced to 0.4%～0.6%, through adding water after dehydration, after adjusting for the third time degree Beaume to 30～34 ° Bx, enters cyclone separator W3, carries out third stage cyclonic separation;
Step 5: the top stream mixed solution after cyclone separator W3 separates
tIIIwith top stream mixed solution
tI, top stream mixed solution
tII, enter cyclone separator W4, cyclone separator W5, cyclone separator W6, underflow mixed solution
bI, underflow mixed solution
bIIand underflow mixed solution
bIIIin, the finished product starch milk that albumen butt mass percentage content is 0.2-0.4%, enters baking operation and dries;
Step 6: the top stream mixed solution of cyclone separator W4, cyclone separator W5, cyclone separator W6
tIV, top stream mixed solution
tVand top stream mixed solution
tVIfor, the finished product Zein powder of starch butt mass percentage content 40% mixes breast, and Zein powder mixes breast through after centrifuge dehydration, enters baking operation, obtains finished product Zein powder;
Step 7: the underflow mixed solution of cyclone separator W4, cyclone separator W5, cyclone separator W6
bIV, underflow mixed solution
bVand underflow mixed solution
bVIbe back to total storage tank, wait for circulation cleaning.
2. the method for decrement cyclonic separation washing W-Gum according to claim 1, is characterized in that described cyclone separator W1, cyclone separator W2 and the underflow mixed solution of cyclone separator W3
bI, underflow mixed solution
bIIand underflow mixed solution
bIIIwater after dehydration, and all water through pump blade type centrifugal discharging centrifuge dehydration in technique, all add flocculation agent through ejector, and buffer memory sedimentation in process container for storing liquid, enters fine filtering step afterwards.
3. the method for decrement cyclonic separation washing W-Gum according to claim 2, it is characterized in that separating centrifuge used in described fine filtering step, its filtration medium aperture 0.2 μ m, through the water after filtering, reclaim and be used as system wash water, by starch yield, production starch 30T per hour, need, after 144 hours, eliminate 5% systemic circulation water, add new water and be in harmonious proportion.
4. the method for decrement cyclonic separation washing W-Gum according to claim 1, is characterized in that in described step 2, and protein butt mass percentage content is that mixed solution is flowed on top
tI> top stream mixed solution
tII> top stream mixed solution
tIII, top stream mixed solution
tIIImiddle protein butt mass percentage content is 20%.
5. the method for decrement cyclonic separation washing W-Gum according to claim 1, is characterized in that
In described step 3 and step 4, added water is the water refluxing after system is processed, and the water of backflow will ensure that pH value stabilization is in 4.3～4.7.
6. the method for decrement cyclonic separation washing W-Gum according to claim 1, is characterized in that the cyclonic separation washing process temperature of W-Gum need keep 40 DEG C.
7. the system of decrement cyclonic separation washing W-Gum, is characterized in that structure is, cyclone separator W1, cyclone separator W2 and cyclone separator W3 mutually connect and form three level shunt eddy flow system I; Cyclone separator W4, cyclone separator W5 and cyclone separator W6 mutually connect and form three level shunt eddy flow system II; Three level shunt eddy flow system I and three level shunt eddy flow system II connect; Three level shunt eddy flow system I are connected with total storage tank, process water tank and process container for storing liquid respectively with three level shunt eddy flow system II; Cyclone separator W1 is all connected with starch Turo pump and pump blade type centrifugal discharging centrifuge to cyclone separator W6; Described process container for storing liquid is connected with pump blade type centrifugal discharging centrifuge with ejector; Described process water tank is connected with pump blade type centrifugal discharging centrifuge with total storage tank.
8. the system of decrement cyclonic separation washing W-Gum according to claim 7, is characterized in that described cyclone separator W1 is all connected with and flows to valve and tensimeter to cyclone separator W6.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210323519.4A CN102816249B (en) | 2012-09-05 | 2012-09-05 | Method and system for washing corn starch by reduced swirler separation |
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| CN201210323519.4A CN102816249B (en) | 2012-09-05 | 2012-09-05 | Method and system for washing corn starch by reduced swirler separation |
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| CN103230844B (en) * | 2013-05-21 | 2014-11-19 | 上海书康淘洗设备厂 | Particle elutriation machine |
| CN107439806A (en) * | 2017-07-26 | 2017-12-08 | 山东中谷淀粉糖有限公司 | A kind of method of wet method adjustment albumen powder protein content |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU986012A1 (en) * | 1980-08-04 | 1989-08-15 | Научно-производственное объединение по крахмалопродуктам | Multicyclone unit |
| SU1218534A1 (en) * | 1984-08-16 | 1990-10-15 | Научно-производственное объединение по крахмалопродуктам | Multicyclone unit |
| CN1070915A (en) * | 1992-10-13 | 1993-04-14 | 年文恒 | Novel process with the swirler corn starch separating |
| CN201292327Y (en) * | 2008-11-12 | 2009-08-19 | 山东阜丰生物科技开发有限公司 | Apparatus for separating corn plasmogen starch and protein |
-
2012
- 2012-09-05 CN CN201210323519.4A patent/CN102816249B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU986012A1 (en) * | 1980-08-04 | 1989-08-15 | Научно-производственное объединение по крахмалопродуктам | Multicyclone unit |
| SU1218534A1 (en) * | 1984-08-16 | 1990-10-15 | Научно-производственное объединение по крахмалопродуктам | Multicyclone unit |
| CN1070915A (en) * | 1992-10-13 | 1993-04-14 | 年文恒 | Novel process with the swirler corn starch separating |
| CN201292327Y (en) * | 2008-11-12 | 2009-08-19 | 山东阜丰生物科技开发有限公司 | Apparatus for separating corn plasmogen starch and protein |
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Effective date of registration: 20191225 Address after: Room 321, building a, Rongjing Lidu, No. 3, Rongjing East Street, Beijing Economic Development Zone, Daxing District, Beijing Patentee after: Beijing Dongjun Xingbang Catering Management Co.,Ltd. Address before: 110002, 1-8-1, 19 glorious Street, Heping District, Liaoning, Shenyang Patentee before: Shi Ren |
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