CN102816249A - 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 PDF

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CN102816249A
CN102816249A CN2012103235194A CN201210323519A CN102816249A CN 102816249 A CN102816249 A CN 102816249A CN 2012103235194 A CN2012103235194 A CN 2012103235194A CN 201210323519 A CN201210323519 A CN 201210323519A CN 102816249 A CN102816249 A CN 102816249A
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cyclone separator
mixed solution
top stream
underflow
water
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CN102816249B (en
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施韧
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Beijing Dongjun Xingbang Catering Management Co ltd
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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

The method and system of decrement rotational flow separation washing W-Gum
Technical field
The present invention relates to a kind of W-Gum protein isolates and washing process, and processing of the process water in the technology and close circulation technology, relate in particular to the method and system that a kind of decrement rotational flow separation is washed W-Gum.
Background technology
In the W-Gum production technique, after wearable, riddler's preface are extracted, get coarse starch milk, concentration is 10～12.5 ° Bx/20 ℃ (the physics specific density is 1.040～1.051, contents on dry basis 10.23%～12.74%).With the butt calculating composition is 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 the sedimentation centrifuge sedimentation at present; Remove impurity such as residual insoluble and soluble protein, ash content, sulfurous acid through the rotational flow station countercurrent washing of 10～15 grades of swirler-s then, obtain the smart milk of starch of 40～42 ° of final Bx.This " adverse current vortex method " become sophisticated washing starch technology; It is widely used in W-Gum industry, and this method technological principle is simple, so at design and manufacturing 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 significant defective, promptly because power consumption that separation progression causes more and problem consuming time.Producing 30 tons of starch units daily, average every grade of swirler-power consumption 10KWh, with the most widely used 12 stage countercurrent vortex methods at present, 120KWh per hour consumes energy.And; Since protein on stream the time long; 40～45 ℃ environment is again the temperature of enlivening most of microbial contamination; So need to keep certain SO2 content to play germicidal action simultaneously, cause SO2 residual quantity in the finished product starch and improve in order to the residual quantity of other non-metallic elements in the sulphur ore deposit of firing SO2.
Summary of the invention
The present invention is directed to the problem that exists in the above-mentioned prior art,, provide a kind of decrement rotational flow separation albumen to cooperate the method for dewatering system washing W-Gum, solved the length consuming time and the high problem that consumes energy in the prior art through test of many times and equipment development.
Another object of the present invention is to provide a kind of system of decrement rotational flow separation washing W-Gum.
Method of the present invention comprises the steps:
Step 1: after the Baume concentration of coarse starch milk in total storage tank is adjusted into 30～34 ° Bx/45 ℃,, get into cyclone separator W1 by the pressurization of starch Turo pump;
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 TIIIThe interflow after the mixing, gets into 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 removes moisture central solubility and small molecular protein through the pump blade type centrifugal discharging centrifuge dehydration, adds water and adjusts once more after ° Bx of degree Beaume to 30～34; Get into cyclone separator W2, carry out second stage rotational flow 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 the dehydration, adjusts for the third time after ° Bx of degree Beaume to 30～34, gets into cyclone separator W3, carries out third stage rotational flow separation;
Step 5: through the top stream mixed solution after the cyclone separator W3 separation TIIIWith top stream mixed solution TI, top stream mixed solution TII, get into cyclone separator W4, cyclone separator W5, cyclone separator W6, the underflow mixed solution BI, the underflow mixed solution BIIAnd underflow mixed solution BIIIIn, albumen butt mass percentage content is 0.2%～0.4% finished product milk of starch, gets into the baking operation oven dry;
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 newborn, and Zein powder mixes breast through after the centrifuge dehydration, gets into baking operation, gets the finished product Zein powder;
Step 7: the underflow mixed solution of cyclone separator W4, cyclone separator W5, cyclone separator W6 BIV, the underflow mixed solution BVAnd underflow mixed solution BVIBe back to total storage tank, wait for circulation cleaning.
The underflow mixed solution of described cyclone separator W1, cyclone separator W2 and cyclone separator W3 BI, the underflow mixed solution BIIAnd underflow mixed solution BIIIAll all add flocculation agent through ejector through the water of pump blade type centrifugal discharging centrifuge dehydration in water after the dehydration and the technology, and flocculating settling in the process container for storing liquid gets into the fine filtering step afterwards.
Used separating centrifuge in the described fine filtering step, its filtration medium aperture 0.2 μ m through the water after filtering, reclaims and is used as system's wash water.By starch yield, per hour produce starch 30T, need after 144 hours, to eliminate 5% systemic circulation water, add new water and be in harmonious proportion.
In the described step 2, protein butt mass percentage content is top stream mixed solution 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 the step 4, added water is the water that refluxes after the system handles, and the water of backflow will guarantee that pH value is stable at 4.3～4.7.
The rotational flow separation washing process temperature of W-Gum need keep 40～45 ℃.
System architecture of the present invention does,
Cyclone separator W1, cyclone separator W2 and cyclone separator W3 connect each other and constitute three grades of shunting eddy flow I of system; Cyclone separator W4, cyclone separator W5 and cyclone separator W6 connect each other through " adverse current " form and constitute three grades of shunting eddy flow II of system; Three grades of shunting eddy flow I of system and three grades of shunting eddy flow II of system connect; Three grades of shunting eddy flow I of system link to each other with total storage tank, process water tank and process container for storing liquid respectively with three grades of shunting eddy flow II of system; Cyclone separator W1 all is connected with starch Turo pump and pump blade type centrifugal discharging centrifuge to cyclone separator W6.
Described process container for storing liquid links to each other with separating centrifuge with ejector.
Described process water tank links to each other with separating centrifuge with total storage tank.
Described cyclone separator W1 all is connected with to cyclone separator W6 and flows to valve and tensimeter.
Advantageous effect of the present invention is following:
1, under the prerequisite that guarantees washing effect, reached the purpose that reduces swirler-progression through having increased by 1.5 times of wash water consumptions to the adverse current vortex method.
2, do not add the centrifugal settling operation, but directly use cyclone separator that coarse starch milk is separated.
3, can substitute the adverse current eddy flow system of ten Pyatyis, reduce the energy consumption of eddy flow washing time and eddy flow system significantly.
4, the top of shunting stream mixing solutions; Its dry biomass degree is merely 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 merely 10～12% of prior art total power, and the main flow beyond the shunting is reduced to 3 grades from 12 grades, and total power is 25% of a prior art total power.
5, the rotational flow separation washing process of W-Gum need keep 40 ℃, enlivens temperature and this temperature is a foreign-bacteria active, so the time is short more; Outside the heat that lagging facility runs off is just fewer; The probability of microbial contamination also diminishes, and whole technology can reduce the eddy flow washing step time 80%.
 
Description of drawings
Fig. 1 is a system flow structural representation of the present invention.
Among the figure, 1, total storage tank, 2, the starch Turo pump, 3, measurement controller, 4, pump blade type centrifugal discharging centrifuge, 5, ejector, 6, the process container for storing liquid, 7, the process water tank, P1, tensimeter, W1-W6, cyclone separator.
Embodiment
Embodiment
Method of the present invention comprises the steps:
Step 1: after the Baume concentration of coarse starch milk in total storage tank is adjusted into 30～34 ° Bx/45 ℃,, get into cyclone separator W1 by the pressurization of starch Turo pump;
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 TIIIThe interflow after the mixing, gets into cyclone separator W4, cyclone separator W5 and cyclone separator W6; Protein butt mass percentage content is top stream mixed solution 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 the pump blade type centrifugal discharging centrifuge dehydration; Remove moisture central solubility and small molecular protein; Adding system is handled the water that refluxes in the back, and the water of backflow will guarantee that pH value is stable at 4.3～4.7, adjusts once more after ° Bx of degree Beaume to 30～34; Get into cyclone separator W2, carry out second stage rotational flow separation;
Step 4: the underflow mixed solution of cyclone separator W2 BIIMiddle protein contents on dry basis is reduced to 0.4%～0.6%;, handle the water that refluxes in the back through adding system after the dehydration, the water of backflow will guarantee that pH value is stable at 4.3～4.7; Get into cyclone separator W3 after adjusting degree Beaume to 30～34 ° Bx for the third time, carry out third stage rotational flow separation;
Step 5: through the top stream mixed solution after the cyclone separator W3 separation TIIIWith top stream mixed solution TI, top stream mixed solution TII, getting into cyclone separator W4, cyclone separator W5, cyclone separator W6, W4, W5, W6 three swirler are " adverse current vortex method " arrangement order; The underflow mixed solution BI, the underflow mixed solution BIIAnd underflow mixed solution BIIIIn, albumen butt mass percentage content is 0.2～0.4% finished product milk of starch, gets into the baking operation oven dry;
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 newborn, and Zein powder mixes breast through after the centrifuge dehydration, gets into baking operation, gets the finished product Zein powder;
Step 7: the underflow mixed solution of cyclone separator W4, cyclone separator W5, cyclone separator W6 BIV, the underflow mixed solution BVAnd underflow mixed solution BVIBe back to total storage tank, wait for circulation cleaning.
Water after the underflow mixed liquor I of described cyclone separator W1, cyclone separator W2 and cyclone separator W3, underflow mixed liquor I I and the underflow mixed liquor I II dehydration; With all water that dewater through pump blade type centrifugal discharging centrifuge in the technology; All add the flocculation agent SEPIGEL 305 through ejector; Flocculating settling in the process container for storing liquid gets into the fine filtering step afterwards.
Used separating centrifuge in the described fine filtering step, its filtration medium aperture 0.2 μ m is through the water after filtering; Recovery is used as system's wash water, by starch yield, per hour produces starch 30T; Need after 144 hours, to eliminate 5% systemic circulation water, add new softening water and be in harmonious proportion.
The rotational flow separation washing process temperature of W-Gum need keep 40 ℃.
System architecture of the present invention does,
Cyclone separator W1, cyclone separator W2 and cyclone separator W3 connect each other and constitute three grades of shunting eddy flow I of system; Cyclone separator W4, cyclone separator W5 and cyclone separator W6 connect each other and constitute three grades of shunting eddy flow II of system; Three grades of shunting eddy flow I of system and three grades of shunting eddy flow II of system connect; Three grades of shunting eddy flow I of system and three grades of shunting eddy flow II of system link to each other with total storage tank 1, process water tank 7 and process container for storing liquid 6 respectively; Cyclone separator W1 all is 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 links to each other with pump blade type centrifugal discharging centrifuge with ejector 5.Described process water tank 7 links to each other with pump blade type centrifugal discharging centrifuge with total storage tank 1.
Principle of work of the present invention is following:
Decrement vortex method of the present invention is to be directed against traditional adverse current vortex method; Every grade of swirler-all is equivalent to the final stage swirler-of adverse current vortex method---that is to say; What add after the charging is through enrolling the subsystem of whole washing system---the water purification rather than the next stage that filter return-flow system contain the overflow water of impurity such as albumen, and the milk of starch of underflow, also need pass through dehydration to remove as far as possible after the solubility or small molecular weight impurity contained in the water; Add wash water again, get into subordinate's charging.
As shown in the figure, so-called decrement eddy flow promptly carries out " shunting " through three grades of shunting eddy flow I of system to coarse starch milk.The top stream mixing solutions of shunting, its dry biomass degree is merely 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 merely 10～12% of prior art total power.And flow point effusive protein soln in top no longer gets into the I of system, but still has 50%～58% because of its dry-matter starch contained therein content; So still need get into three grades of shunting eddy flow II of system that the conventional counter-current method is formed; Among three grades of shunting eddy flow II of system, the dry-matter total content is 12%～18%, so power consumption reduces; Need not separating centrifuge and participate in water treatment, only need adverse current.Finally obtain total protein content and be 60%～63% Zein powder, behind the dewatered drying promptly as the maize gluten feed finished product.
Through the shunting to the higher top of protein content stream, for the eddy flow of fs provides the basic protein content condition that reduces the eddy flow number of times, and each grade all is to use the acid water purification washing through albumen flocculation and filtration treatment; And, three swirler device, each grade underflow; After promptly all passing through processed through the smart milk of starch that washs, other adds the return-flow system water purification, is equivalent to the washing of a filteration; Be expelling water and rinsing, three grades of expelling water and rinsings add the three swirler device, through experiment; Can substitute the adverse current eddy flow system of ten Pyatyis fully, reduce the energy consumption of eddy flow washing time and eddy flow system significantly.
The present invention washs back starch quality standard test and is protein content≤0.35%; Solvend≤0.02%.
The protein content kept stable is compared with existing adverse current eddy flow, does not see that increase and decrease is unsteady.But solubles content requires≤0.1% to reduce much contained mineral substance in its starch, trace element, and SO than national standard 2Residual quantity, all be minimized.
The key link that the present invention is different from traditional " adverse current vortex method " does; Through shunting washing system I; Coarse starch milk is divided into the top stream part of protein contnt about 50% and the underflow of protein contnt about 0.4%～1% partly divides two portions, so, through simplifying the eddy flow number of times to underflow carrying out washing treatment partly; And still use tradition " adverse current vortex method " that top stream part is carried out carrying out washing treatment, reduce the treatment time and reduce the purpose of handling power consumption thereby reach.

Claims (10)

1. the method for a decrement rotational flow separation washing W-Gum is characterized in that comprising the steps:
Step 1: after the Baume concentration of coarse starch milk in total storage tank is adjusted into 30～34 ° Bx/45 ℃,, get into cyclone separator W1 by the pressurization of starch Turo pump;
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 TIIIThe interflow after the mixing, gets into 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 removes moisture central solubility and small molecular protein through the pump blade type centrifugal discharging centrifuge dehydration, adds water and adjusts once more after ° Bx of degree Beaume to 30～34; Get into cyclone separator W2, carry out second stage rotational flow 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 the dehydration, adjusts for the third time after ° Bx of degree Beaume to 30～34, gets into cyclone separator W3, carries out third stage rotational flow separation;
Step 5: through the top stream mixed solution after the cyclone separator W3 separation TIIIWith top stream mixed solution TI, top stream mixed solution TII, get into cyclone separator W4, cyclone separator W5, cyclone separator W6, the underflow mixed solution BI, the underflow mixed solution BIIAnd underflow mixed solution BIIIIn, albumen butt mass percentage content is the finished product milk of starch of 0.2-0.4%, gets into the baking operation oven dry;
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 newborn, and Zein powder mixes breast through after the centrifuge dehydration, gets into baking operation, gets the finished product Zein powder;
Step 7: the underflow mixed solution of cyclone separator W4, cyclone separator W5, cyclone separator W6 BIV, the underflow mixed solution BVAnd underflow mixed solution BVIBe back to total storage tank, wait for circulation cleaning.
2. decrement rotational flow separation according to claim 1 is washed the method for W-Gum, it is characterized in that the underflow mixed solution of described cyclone separator W1, cyclone separator W2 and cyclone separator W3 BI, the underflow mixed solution BIIAnd underflow mixed solution BIIIAll all add flocculation agent through ejector through the water of pump blade type centrifugal discharging centrifuge dehydration in water after the dehydration and the technology, and buffer memory sedimentation in the process container for storing liquid gets into the fine filtering step afterwards.
3. the method for decrement rotational flow separation washing W-Gum according to claim 2 is characterized in that used separating centrifuge in the described fine filtering step, its filtration medium aperture 0.2 μ m; Water through after filtering reclaims and is used as system's wash water, by starch yield; Per hour produce starch 30T; Need after 144 hours, eliminate 5% systemic circulation water, add new water and be in harmonious proportion.
4. the method for decrement rotational flow separation washing W-Gum according to claim 1 is characterized in that in the described step 2, and protein butt mass percentage content is top stream mixed solution 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 rotational flow separation washing W-Gum according to claim 1 is characterized in that in described step 3 and the step 4 that added water is the water that refluxes after the system handles, and the water of backflow will guarantee that pH value is stable at 4.3～4.7.
6. the method for decrement rotational flow separation washing W-Gum according to claim 1 is characterized in that the rotational flow separation washing process temperature of W-Gum need keep 40 ℃.
7. the system of decrement rotational flow separation washing W-Gum is characterized in that structure does, cyclone separator W1, cyclone separator W2 and cyclone separator W3 connect each other and constitute three grades of shunting eddy flow I of system; Cyclone separator W4, cyclone separator W5 and cyclone separator W6 connect each other and constitute three grades of shunting eddy flow II of system; Three grades of shunting eddy flow I of system and three grades of shunting eddy flow II of system connect; Three grades of shunting eddy flow I of system link to each other with total storage tank, process water tank and process container for storing liquid respectively with three grades of shunting eddy flow II of system; Cyclone separator W1 all is connected with starch Turo pump and pump blade type centrifugal discharging centrifuge to cyclone separator W6.
8. the system of decrement rotational flow separation washing W-Gum according to claim 7 is characterized in that described process container for storing liquid links to each other with separating centrifuge with ejector.
9. the system of decrement rotational flow separation washing W-Gum according to claim 7 is characterized in that described process water tank links to each other with separating centrifuge with total storage tank.
10. the system of decrement rotational flow separation according to claim 7 washing W-Gum is characterized in that described cyclone separator W1 all is connected with to cyclone separator W6 to flow to valve and tensimeter.
CN201210323519.4A 2012-09-05 2012-09-05 Method and system for washing corn starch by reduced swirler separation Expired - Fee Related CN102816249B (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103230844A (en) * 2013-05-21 2013-08-07 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

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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

Patent Citations (4)

* Cited by examiner, † Cited by third party
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

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103230844A (en) * 2013-05-21 2013-08-07 上海书康淘洗设备厂 Particle elutriation machine
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

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