CN102807626A - Method for preparing corn starch - Google Patents

Method for preparing corn starch Download PDF

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Publication number
CN102807626A
CN102807626A CN2011101460795A CN201110146079A CN102807626A CN 102807626 A CN102807626 A CN 102807626A CN 2011101460795 A CN2011101460795 A CN 2011101460795A CN 201110146079 A CN201110146079 A CN 201110146079A CN 102807626 A CN102807626 A CN 102807626A
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water
weight
corn
concentration
film evaporator
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CN102807626B (en
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岳国君
艾咏平
徐兆勇
娄新建
郜培
鲁艳秋
高占争
郝小明
罗虎
王旭
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China Grain Wuhan Scientific Research & Design Institute Co ltd
State Grain Reserve Wuhan Research and Design Institute Co.,Ltd.
Wuhan scientific research and Design Institute Co.,Ltd. of State Grain Reserve Bureau
Cofco Corp
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State Grain Reserve Wuhan Scientific Research And Design Institute
Cofco Corp
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Abstract

The invention provides a method for preparing corn starch. The method comprises the following steps of: removing sand and stones from a corn raw material; soaking shelled corn; concentrating an obtained corn soaking liquid; and separating rough starch milk to obtain diluted gluten and starch milk, wherein a method for removing sand and stones from the corn raw material comprises the following steps of: making the corn raw material flow from upstream on a high level to downstream on a low level along with water; submerging sand and stones in a flowing process; and limiting the submerged sand and stones to flow continually along with water; a method for treating gluten water comprises the following steps of: (1) concentrating gluten water firstly to obtain a first concentrated phase and a first water phase; and (2) concentrating the first concentrated phase secondly to obtain a second concentrated phase and a second water phase; and a method for concentrating the obtained core soaking liquid comprises the following steps of: concentrating the corn soaking liquid to 40-45 percent by weight by adopting a falling-film evaporator; and concentrating 40-45 percent by weight of a corn steep liquor to 48-52 percent by weight by adopting a scraper film evaporator. Due to the adoption of the method, the yield of gluten protein powder can be increased, and a high-concentration concentrated corn steep liquor can be produced as a byproduct.

Description

A kind of preparation method of W-Gum
Technical field
The present invention relates to a kind of preparation method of W-Gum.
Background technology
Corn can be sneaked into dust and rubble as farm crop inevitably in corn grain in plucking collection process.Therefore, in the corn processed process, at first need carry out dedusting to the maize raw material that contains corn grain and remove the stone processing.Usually, can adopt suitable screening and pneumatic separation device that dust of sneaking into and rubble are removed through screen cloth.But this mode belongs to dry cleaning, and processing power is limited.In addition, for the more firm earth that adheres on the corn grain with the onesize stone of corn grain, the removal effect of aforesaid method is not good enough.
Then; Need carry out follow-up processing to accomplishing pretreated corn grain, for example, the leaching process of starch is the chief component separating process of corn grain; The separation of each integral part of corn grain has two kinds of dry method and wet methods; And lock out operation main be to grind, therefore, the dry grinding and the branch of wet-milling are arranged.
Wherein, wet-milling is the general technology of current corn starch industry, is mainly the corn process fragmentation of passing through dipping, takes off embryo, correct grinding and screening, to tell plumule, fibrous residue, makes the process of rough milk of starch.After starch wearable riddler preface was extracted, the gained milk of starch still was a coarse starch milk, still contains a large amount of insoluble proteins and soluble substance, and the concentration of powder slurry is also rarer, need make with extra care and concentrate, for processing and deep processing at last provides purified smart milk of starch.
The purified method mainly is to utilize the principle of spinning, and coarse starch milk is separated, and tells light phase and heavy phase; Light mutually for containing the water of insoluble protein, i.e. seitan water, heavy phase is a milk of starch; Remove soluble substance remaining in the milk of starch with the pure water washing again, promptly get smart milk of starch.And isolated seitan water utilizes the method for spinning to concentrate once more, obtains enriched material and process water, after enriched material is dehydrated, promptly gets the gluten protein powder.Separate the process water that obtains, directly cyclically utilizing is in the washing process of technique for soaking corn or milk of starch.
But; Adopt the method for prior art to utilize the method for spinning to carry out spissated technology deficiency once more so that insoluble protein is fully separated to seitan water; Separation efficiency is lower; Cause the productive rate of gluten protein powder not high, and separate in the process water obtain and still contain a certain amount of insoluble protein, not only can cause the productive rate of gluten protein powder to reduce; If after the direct cyclically utilizing of process water was in technique for soaking corn and plumule, the fibre washing technique, the immersion effect of corn and quality product also can variation.
In addition, steeping water is one of significant by-products of wet milling process W-Gum production, also is the sub product that proposes at first in the starch production, is concentrated by corn steeping water to obtain, and is actually the extract of corn.Said corn steeping water outward appearance is the brown viscous liquid; Solids content is about 5-8 weight %, and the staple major part is corn soluble protein and degradation product thereof, like peptide class, each seed amino acid etc.; Also contain lactic acid, phytic acid ca magnesium salts, soluble saccharide in addition; Very high nutritive value is arranged, can be used for the microbiological culture media of fermentation industry, but most additive as animal-feed.
Because the concentration of corn steeping water is low, be not easy to store, transportation and using, therefore, need to concentrate and remove moisture, in order to save energy consumption, generally take the multiple-effect evaporation that reduces pressure, be concentrated into and contain dry-matter 40-45 weight %, be dense steeping water.Usually adopt the multiple-effect falling film vaporizer that steeping water is concentrated; Reduce the water cut in the steeping water as far as possible; To reduce the excess moisture that sprays into steeping water in the fiber feedstuff drying process; Cause energy consumption to strengthen, cause drying machine output to reduce, and make steeping water not join in the fiber feedstuff fully.Because falling-film evaporator adopts tubulation indirect heating material usually, if heated material concentration is too high, viscosity is big, is easy to cause the local dried wall of vaporizer heating tube, coking, scale formation, and stop up heating tube, make steam capability reduce greatly.So spissated steeping water concentration generally can only reach about 40-45 weight %.
Summary of the invention
The objective of the invention is to overcome the deficiency among the W-Gum preparation technology of prior art; And provide a kind of from raw materials pretreatment; The improvement of spissated whole W-Gum technology for preparing processing and the steeping water of the seitan water in the process to starch; And realize convenient, corn grain is carried out dedusting and removes stone handling, improving gluten protein powder productive rate and can be directly the process water reuse can be improved starch washing effect and the concentrated steeping water that can the by-product high density of corn soaking effect and cyclically utilizing to plumule, the fibre washing technique of process water cyclically utilizing to technique for soaking corn continuously, do not influence the successional W-Gum preparation method of W-Gum technology.
The invention provides a kind of preparation method of W-Gum, this method comprises the sandstone of removing in the maize raw material, soaks the corn grain that obtains; Concentrate the corn steep liquor obtain, and the corn grain that will pass through immersion carries out fragmentation, isolate plumule; The corn grain tissue that contains maize peel and endosperm that will take off behind the embryo grinds, and isolates fiber, the coarse starch milk that obtains is separated obtaining seitan water and milk of starch; And milk of starch washed, wherein:
Said method of removing the sandstone in the maize raw material comprises:
Make said maize raw material with water from being positioned at the elevated upper reaches towards the downstream flow that is positioned at low level, and said sandstone are sunk in flow process, the density of said corn grain is less than the density of said sandstone;
The said sandstone that restriction is sunk continue to flow with water;
The treatment process of said seitan water comprises seitan water concentrated, and said the spissated method of seitan water comprised:
(1) seitan water is carried out once concentration, obtain first concentrated phase and first water, the condition of once concentration makes the content of the first aqueous phase insoluble protein that obtains less than 0.3 weight %;
(2) first concentrated phase is carried out secondary concentration, obtain second concentrated phase and second water, it is more than the 10 weight % that the condition of secondary concentration makes the content of insoluble protein in second concentrated phase that obtains;
(3) second water is mixed with flocculant solution, the promoting the circulation of qi of going forward side by side is floating to be separated; Said flocculation agent is for making the insoluble protein flocculation and/or the settled material of second aqueous phase;
The said method that concentrates the corn steep liquor that obtains comprises evaporates corn steep liquor; The method of said evaporation comprises that the employing falling-film evaporator is concentrated into 40-45 weight % with corn steep liquor, and adopts scrapper thin film evaporator that the steeping water of the 40-45 weight % that obtains is concentrated into 48-52 weight %.
At first, in W-Gum technology, contriver of the present invention adopts wet method proportion separation principle that maize raw material is carried out pre-treatment, and when the maize raw material that will contain corn grain and sandstone mixed with water and flows, sandstone sank in flow process.Since said maize raw material with water from being positioned at the elevated upper reaches towards the downstream flow that is positioned at low level, thereby with the increase of distance of flow, sandstone can sink to lower position and the position that is limited in sinking on.In addition, because the density of corn grain is less than the density of sandstone, thereby corn grain can continue to flow or compare at least with the longer distance of water flows with sandstone with water in flow process.And as stated, along with the increase of distance of flow, subsidence position is lower, thereby has further delayed the sinking of corn grain.Therefore, use method of the present invention can make things convenient for, continuously corn grain carried out dedusting and removes the stone processing, and simple to operate, need and can not carry out the successive operation with complex apparatus.
Secondly, contriver of the present invention also finds, the W-Gum preparation technology who adopts prior art to seitan water utilize once more spinning the method deficiency so that insoluble protein fully separate; Separation efficiency is lower, and the content of the insoluble protein in the enriched material that therefore obtains is not high, causes the productive rate of gluten protein powder not high; In addition; Also contain a large amount of insoluble proteins in the process water that obtains after concentrating, if directly with the direct cyclically utilizing of process water to technique for soaking corn, owing to the protein content in the process water is higher; Therefore can't fully soak out and dissolve in the soluble protein in the corn in the water; And influence follow-up separating technology, same, the direct cyclically utilizing of the process water that prior art obtains in plumule, the fibre washing technique after; Also can't fully the soluble substance thorough washing in plumule, the fiber be come out, and can influence the quality of product.Adopting method of the present invention, earlier seitan water is carried out once concentration, the content of the first aqueous phase insoluble protein that control obtains is lower; Then; First concentrated phase is carried out secondary concentration, and the content of insoluble protein is higher in second concentrated phase that control obtains, thereby realizes effective separation of insoluble protein; After the insoluble protein in this second concentrated phase being separated and dehydrate, reach the purpose of the productive rate that improves the gluten protein powder greatly.In addition; The content of the first aqueous phase insoluble protein that control obtains is lower; Can make water reach the specification of quality of direct reuse, that is, with said water once more the reuse circulation corn is soaked and plumule, fiber is washed; Can reach basically and soak with fresh water and the effect of washing, and significantly improve the quality of smart milk of starch.The deficiency of the technology that the method that has remedied prior art is handled seitan water so that insoluble protein can fully separate.
Moreover contriver of the present invention finds that again though adopt the multiple-effect falling film vaporizer that steeping water is concentrated in the prior art usually, owing to receive all restrictions, spissated steeping water concentration generally can only reach about 40-45 weight %.In addition, scrapper thin film evaporator is because reasons in structure own can not be made too greatly, so its steam capability is limited, and prior art does not adopt scrapper thin film evaporator that steeping water is concentrated usually yet.And contriver of the present invention is surprised to find that; Adopt scrapper thin film evaporator and falling-film evaporator to form multi-effect evaporation system; Adopt falling-film evaporator that corn steep liquor is concentrated into 40-45 weight % earlier; Then utilize scrapper thin film evaporator as the high density concentrating unit, can be further be that the steeping water of 40-45 weight % is concentrated into 48-52 weight % with concentration.Avoided on the one hand when adopting falling-film evaporator that steeping water is concentrated; The dense steeping water of excessive concentration is because viscosity Da Yi stops up the problem of the heating tube of falling-film evaporator; And utilized the characteristics of scrapper thin film evaporator dexterously, as, what scrapper thin film evaporator adopted is the chuck heating; There is not obstructing problem; And can utilize the scraper plate in the scrapper thin film evaporator to force to stir, thereby can the concentration of steeping water be increased to suitable concentrated concentration (48-52 weight %), and obtain the higher steeping water liquid concentrator of concentration.Water-content reduces in the steeping water liquid concentrator of the high density that the present invention obtains, and therefore, can reduce the energy consumption of follow-up highly energy-consuming dehumidification system greatly.In addition, the high density steeping water that the present invention obtains is because drop temperature is high, and is better mobile, and available pipe is transported to follow-up drying plant and in time sprays in the fiber dry.
After the above-mentioned steps among the W-Gum preparation technology is improved and is made up, can realize the serialization production of W-Gum well, effectively improved the production efficiency of W-Gum.
Other features and advantages of the present invention will partly specify in embodiment subsequently.
Description of drawings
Accompanying drawing is to be used to provide further understanding of the present invention, and constitutes the part of specification sheets, is used to explain the present invention with embodiment of the present invention, but is not construed as limiting the invention.In the accompanying drawings:
Fig. 1 is the schematic top plan view of structure of a kind of embodiment that removes stone cistern of the method for removing the sandstone in the maize raw material that provides of embodiment of the present invention;
Fig. 2 is the synoptic diagram of structure of a kind of embodiment of method of removing the sandstone in the maize raw material of the present invention;
Fig. 3 is to use the embodiment of Fig. 2 to carry out removing in a large number the synoptic diagram that sandstone are handled;
Fig. 4 is the structural representation of the another kind of embodiment of method of removing the sandstone in the maize raw material of the present invention;
Fig. 5 is to use the embodiment of Fig. 4 to carry out removing in a large number the synoptic diagram that sandstone are handled;
Fig. 6 adopts multi-effect evaporation system that corn steep liquor is carried out spissated schema among the preparation method of W-Gum provided by the invention.
Description of reference numerals
10: remove stone cistern
11: sidewall 12: diapire 13: inlet 14: outlet 15: plate washer 20: fluid mixture 21: corn grain 22: rubble.
Embodiment
Be elaborated below in conjunction with the accompanying drawing specific embodiments of the invention.Should be understood that embodiment described herein only is used for explanation and explains the present invention, is not limited to the present invention.
Preparing method according to W-Gum provided by the invention; Wherein, Said method of removing the sandstone in the maize raw material comprises: make said maize raw material with water from being positioned at the elevated upper reaches towards the downstream flow that is positioned at low level; And said sandstone are sunk in flow process, the density of said corn grain is less than the density of said sandstone; The said sandstone that restriction is sunk continue to flow with water.
Preferably, the said sandstone 22 that said restriction is sunk continue the mobile method with water and comprise along the flow direction of water a plurality of obstacles are set that the said sandstone 22 that said obstacle restriction is sunk continue to flow with water.
The present invention does not limit the consumption of water is special, if with can form fluid after the maize raw material that contains corn grain and sandstone mixes with flowability.For example, can make maize raw material, have mobile fluid thereby form with water flows.But this mode is unfavorable for controlling the ratio of maize raw material and water, makes the fluid mobility of formation inconsistent.Preferably, maize raw material and water are at first mixed form uniform fluid mixture 20 (for example through stirring), fluid mixture 20 flowed and the separation sandstone.Wherein, to the consumption and the not special qualification of churning time of water, as long as can obtain flowability fluid mixture 20 preferably.For example the consumption of water can be 2-5 times of maize raw material gross weight, and the flow velocity of current can be 0.3-1.5m/s.
Explanation adopts method of the present invention that maize raw material is carried out pre-treatment to remove the concrete operations of the sandstone in the maize raw material below.
Can use suitable equipment or device to come the method for embodiment of the present invention.In preferred implementation of the present invention, to shown in Figure 5, can use method except that stone cistern 10 embodiment of the present invention like Fig. 1.The stone cistern 10 that removes of the present invention comprises two relative sidewalls 11; Diapire 12 between these two sidewalls; And the inlet 13 and outlet 14 that are separately positioned on the cell body two ends between said two sidewalls 11; The height of at least a portion of the diapire 12 from said inlet 13 to said outlet 14 reduces gradually, and the said diapire 12 of this at least a portion is provided with obstacle.In other words, inlet 13 and outlet 14 be respectively as the upstream and downstream of current, and current can rely on deadweight 13 to flow to outlet 14 from entering the mouth.
When fluid mixture 20 from entering the mouth 13 when outlet 14 is flowed because the density of sandstone 22 is much larger than water and greater than the density of corn grain 21, thereby sandstone 22 can sink in flow process on the diapire 12.Sink to the sandstone 22 on the diapire 12 through restriction, it can't be continued with water flows on diapire 12, thereby can sandstone 22 be limited in except that in the stone cistern 10.Though the density of corn grain 21 is compared sandstone 22 also greater than the density of water, it is slowly a lot of that the sinking velocity of corn grain 21 is wanted, thereby the longer distance that can before sinking to diapire 12, flow.Because diapire 12 13 reduces to outlet 14 with respect to the horizontal plane height from entering the mouth gradually, thereby has increased the distance that sinks to diapire 12 gradually, thereby can make corn grain 21 with the longer distance of water flows.In addition, even corn grain 21 sinks on the diapire 12, because of its density less, current wash away with wave action under can easily float, and can cross (for example cross hereinafter explanation plate washer 15) and continue with water flows.Therefore, can separate corn grain 21 and sandstone 22 easily, continuously.
In the present invention, said maize raw material can be realized through variety of way towards the downstream flow that is positioned at low level from being positioned at the elevated upper reaches with water.Specify through two kinds of embodiments below.
In a kind of preferred implementation of the present invention, can make said maize raw material with water along being tilted to down domatic mobile, said a plurality of obstacles be arranged on said domatic on.Particularly, as shown in Figures 2 and 3, in removing stone cistern 10, can make the said diapire 12 of at least a portion for downward-sloping domatic.
As stated, also " cross " obstacle for fear of the sandstone that sink 22 accumulations, preferably, said obstacle is a plurality of and the direction of edge from said inlet 13 to said outlet 14 is spaced.Through this layout, can prevent that sandstone 22 from " crossing " obstacle because of accumulation.In other words, even sandstone 22 " have been crossed " obstacle because of accumulation, but still can be stopped by other obstacle.Certainly, use the stone cistern 10 that removes of the present invention to remove sandstone continuously after the processing scheduled time, just when a large amount of sandstone 22 have all been piled up at each obstacle place, need stop to remove sandstone and handle and clear up, and then begin to handle except that sandstone.In addition, the dust in the sandstone 22 causes sinking velocity different with rubble because of density is different, thereby can on the different positions of diapire 12, sink.Therefore, the structure of this embodiment can also stop the sandstone 22 on the different positions that sinks to diapire 12.
Preferably, said domatic inclination angle (inclination angle with respect to the horizontal plane) is the 7-10 degree, and domatic through this slow inclination can guarantee that sandstone 22 13 all sink on the diapire 12 before flowing to outlet 14 from entering the mouth at current basically.
When the treatment capacity of mixture fluid 20 more after a little while, as shown in Figure 2, liquid level will be parallel to domatic.
When the treatment capacity of mixture fluid 20 is big, as shown in Figure 3, liquid level will be parallel to horizontal plane, in this case, and inlet 13 and export pressure difference between 14 will to strengthen fluidic mobile.
Preferably, said obstacle stops with the height that makes full use of obstacle perpendicular to said domatic.
In addition, can make the height of said outlet 14 be higher than the height of the obstacle adjacent with said outlet 14, thus utilize the height of outlet 14 stop maybe " crossing " last obstacle sandstone 22.
In addition, owing to the increase along with distance of flow, the amount of the sandstone of sinking reduces.Therefore, preferably, along the flow direction of liquid, the distance between adjacent two obstacles progressively increases, thereby when guaranteeing to remove the sandstone operation, reduces the quantity of obstacle, thereby reduces the cost that removes the sandstone operation.
In another embodiment of the invention, can make said maize raw material with the downward successively a plurality of step-flow in water edge, a said obstacle all is set on each step.Particularly, like Fig. 4 and shown in Figure 5, in removing stone cistern 10, can make the said diapire 12 of this at least a portion that reduces highly gradually be downward successively a plurality of steps.
In the ledge structure, horizontal component is called tread portion, and vertical component is called kickplate portion.Wherein, the edge that is connected with upwardly extending adjacent kickplate portion of tread portion is called combines the limit, and with tread portion be called free edge to the adjacent kickplate portion bonded edge that extends below.
Preferably, as shown in Figure 4, said obstacle is arranged on the free edge of tread portion of said ledge structure, thereby makes full use of the sandstone 22 that tread portion is held sinking.
In addition, preferably, said obstacle stops with the height that makes full use of obstacle perpendicular to the plane at said tread portion place.
In addition, preferably, the height of said obstacle is 1 with the ratio of said height: 1-1: 3, flow continuing thereby compile an amount of current in the tread portion of each step.
In this embodiment of the present invention; When the treatment capacity of mixture fluid 20 more after a little while; As shown in Figure 4, corn grain 21 with current from entering the mouth 13 towards outlet 14 process of flowing, also can produce and current form the liquid level that is parallel to tread at each step at each step.
When the treatment capacity of mixture fluid 20 is big, as shown in Figure 5, with forming complete and being parallel to the liquid level of horizontal plane.In this case, inlet 13 and export difference of altitude between 14 will to strengthen fluidic mobile.
Among the present invention, obstacle can be various suitable structures, stops or limits the sandstone 22 that sink on the diapire 12 and continue to flow with water as long as can play.In preferred implementation of the present invention, to shown in Figure 5, said obstacle is a plate washer 15 like Fig. 2.Plate washer 15 can be processed by the material with suitable intensity, stops sandstone 22 as long as can resist water impact, for example can be steel plate, slabstone or plastic plate.
Preferably, can make the edge at the top of said plate washer 15 have fillet, thus the corn grain 21 of being convenient to make sinking current wash away with wave action under float and cross plate washer 15.In addition, the breakage that this structure can also avoid corn grain 21 when crossing, to take place, thus keep the complete of corn grain 21.
In addition, preferably, the height of said plate washer 15 is 15-50cm, thus the corn grain 21 that sinks current wash away with wave action under float corresponding height and can realize crossing.This highly can be according to the size of corn kernel 21 and factors such as the speed design of current.
Streamwise (promptly from entering the mouth 13 to outlet 14) is because therefore the sandstone 22 that carry and the sandstone 22 " crossed " because of accumulation fewer and feweri in the current, can make the height streamwise of said plate washer 15 reduce gradually.This structure can apply rational resistance at different positions to current through the plate washer 15 of different heights.In other words; In position near inlet 13; Because sandstone 22 are more, use higher plate washer 15 can stop a large amount of sandstone 22 on the one hand, can produce big resistance through 15 pairs of current of plate washer on the other hand; Thereby the current that make this place produce than great fluctuation process, float and cross with the corn grain 21 of assisting to sink.Near outlet 14 position, because sandstone 22 are less, use lower plate washer 15 just can stop sandstone 22, simultaneously because of having reduced resistance, thereby can improve current and carry corn kernel 21 towards exporting 14 mobile speed and flows to current.
Among this paper, the height of obstacle or plate washer 15 all refers to the distance of top to the diapire 12 of obstacle or plate washer 15.When being domatic, the height of obstacle or plate washer 15 is top to the domatic distance of obstacle or plate washer 15 at the said diapire 12 of said at least a portion; When the said diapire 12 of said at least a portion was downward a plurality of step, the height of obstacle or plate washer 15 was that the top of obstacle or plate washer 15 is to the tread portion place planar distance that this obstacle or plate washer 15 are set.
According to the preparation method of W-Gum provided by the invention, wherein, the treatment process of said seitan water comprises seitan water concentrated, and said the spissated method of seitan water comprised:
(1) seitan water is carried out once concentration, obtain first concentrated phase and first water, the condition of once concentration makes the content of the first aqueous phase insoluble protein that obtains less than 0.3 weight %;
(2) first concentrated phase is carried out secondary concentration, obtain second concentrated phase and second water, it is more than the 10 weight % that the condition of secondary concentration makes the content of insoluble protein in second concentrated phase that obtains.
(3) second water is mixed with flocculant solution, the promoting the circulation of qi of going forward side by side is floating to be separated; Said flocculation agent is for making the insoluble protein flocculation and/or the settled material of second aqueous phase.
Contriver of the present invention finds; Compare with the method that promptly obtains enriched material and process water after the once concentration of prior art; When seitan water is carried out once concentration; The content of the proteinaceous solid substance of first aqueous phase that control obtains is preferably 0.1-0.3 weight % less than 0.3 weight %, can guarantee earlier that promptly first aqueous phase only contains a spot of proteinaceous solid substance; Then; When first concentrated phase that obtains after the once concentration was carried out secondary concentration, the content of proteinaceous solid substance was preferably 10-12 weight % in second concentrated phase that control obtains more than 10 weight %; Contain a large amount of proteinaceous solid substances in second concentrated phase that has promptly guaranteed again to obtain; That is to say, adopt method of the present invention that seitan water is concentrated after, can obtain simultaneously quality content higher, proteinaceous solid substance less can direct reuse water; And need not again the water that obtains to be carried out subsequent disposal, obtain directly carrying out the higher concentrated phase of proteinaceous solid content of next step gluten protein powder preparation simultaneously.
According to the present invention; The content of the proteinaceous solid substance of first aqueous phase that control obtains is less than 0.3 weight %; Be preferably 0.1-0.3 weight %; The concentration ratio of first concentrated phase that can obtain during once concentration through control, the concentration ratio of said first concentrated phase is the feed volume of once concentration seitan water and the ratio of the first concentrated phase volume; The concentration of proteinaceous solid substance is lower in first concentrated phase, so promptly can guarantee the first aqueous phase low percentages of protein, and therefore, under the preferable case, the concentration ratio of first concentrated phase can be 2-3: 1, and 2.3-2.8 more preferably: 1.Vice versa; The content of proteinaceous solid substance is more than 10 weight % in second concentrated phase that control obtains; Be preferably 10-12 weight %; The concentration ratio of second concentrated phase that can obtain during secondary concentration through control, the feed volume of said secondary concentration first concentrated phase and the ratio of the second concentrated phase volume; The concentration of the proteinaceous solid substance of second aqueous phase is higher, can guarantee that promptly protein contnt is higher in second concentrated phase, and therefore, under the preferable case, the concentration ratio of second concentrated phase can be 3-4: 1, and 3.3-3.7 more preferably: 1.
According to the present invention, the spissated method of seitan water can for example, be utilized the principle of spinning for various concentrated modes well known in the art, adopt separating machine that seitan water is concentrated, enriched material flows out from underflow, and stream flows out process water from the top.Therefore, the method for the invention preferably adopts the method for spinning to carry out said once concentration and said secondary concentration.
According to the present invention; Spissated condition generally comprises the rotating speed of spinning and the temperature of feed rate and spinning etc.; The equal broad of the adjustable extent of above-mentioned condition; Also promptly, the condition of once concentration is as long as guarantee the proteinaceous solid content of first aqueous phase, and the condition of preferred once concentration gets final product the concentration ratio of the concentrated phase of winning in preferred range of the present invention; Simultaneously, the condition of secondary concentration is as long as guarantee the content of proteinaceous solid substance in second concentrated phase, and the condition of preferred secondary concentration makes the concentration ratio of second concentrated phase in preferred range of the present invention, get final product.Because the size of different centrifugal separation equipments, diameter difference, rotating speed are also just different, therefore, can select suitable equipment according to the needs of reality, its rotating speed has also confirmed that with regard to corresponding the while also just can be selected suitable inlet amount according to actual needs.The temperature of spinning generally can be 35-45 ℃.
Contriver of the present invention finds, flocculation agent is mixed with second water with the form of flocculant solution, can make it more even with the second water blended, makes the proteinaceous solid substance flocculation of this second aqueous phase and/or settled more abundant, complete.
According to the present invention, the solvent in the said flocculant solution can be the various solvents that can form solution with flocculation agent, and generally, the solvent in the said flocculant solution is a water.Said flocculation agent can be various can be with the flocculation of proteinaceous solid substance, the sedimentation of second aqueous phase; And make it from the effective isolating flocculation agent of second aqueous phase; Under the preferable case; Said flocculation agent can be ROHM and/or ZX-I and Poly aluminum Chloride (PAC), and also promptly, the aqueous solution of said flocculation agent is the aqueous solution of ROHM and/or ZX-I and the aqueous solution of Poly aluminum Chloride (PAC).
More preferably under the situation, said polyacrylic number-average molecular weight can be 6,000,000-1,000 ten thousand dalton, and the number-average molecular weight of said ZX-I can be 6,000,000-1,000 ten thousand dalton.Said Poly aluminum Chloride (PAC) is a kind of inorganic flocculating agent, and its molecular formula is [Al 2(OH) nCl 6-n] m, wherein, n is 1-5, m≤10, basicity B=n/6 * 100%.
Contriver of the present invention finds; Poly aluminum Chloride (PAC) makes the fine particle thing of said second aqueous phase accumulate in the suspended substance that it forms larger particles on every side more easily; And ROHM and/or ZX-I make the suspended substance sedimentation of larger particles more easily, therefore, and in the ban after the aqueous solution with second water and Poly aluminum Chloride (PAC); With the aqueous solution of the polyacrylic aqueous solution and/or ZX-I, can play better separating effect again.In addition; Contriver of the present invention also finds, the weight ratio of Poly aluminum Chloride (PAC) and ROHM and/or ZX-I is controlled at 2-5 in this flocculant solution, in the time of more preferably in the scope of 3-4.5; The layering of proteinaceous solid substance and water is more clear, and promptly separating effect is better.
Under the preferable case; After aqueous solution, before the aqueous solution of the polyacrylic aqueous solution and/or ZX-I, also comprise the step of stirring with second water and Poly aluminum Chloride (PAC); Gathering with the fine particle thing that fully makes the Poly aluminum Chloride (PAC) and second aqueous phase is more thorough; Destroy in order to be beneficial to the Poly aluminum Chloride (PAC) fine particle thing that fully flocculates, can not destroy again simultaneously the PM for particulate matter that has flocculated, the time of said stirring is preferably 0.5-5 minute.
In the present invention, the solubleness of flocculation agent in water is moderate, therefore; The adjustable extent broad of the mass and size concentration of said flocculant solution; As, can be 0.1-5% (m/v), from taking all factors into consideration of cost and effect; The mass and size concentration of the aqueous solution of the said polyacrylic aqueous solution and ZX-I is preferably 0.1-0.5% (m/v), and the mass and size concentration of the aqueous solution of said Poly aluminum Chloride (PAC) is preferably 1-5% (m/v).
According to method of the present invention; The adjustable extent broad of the consumption of said flocculant solution, for example, can be according to the consumption of how much regulating flocculant solution of the amount of the second aqueous phase insoluble protein; Under the preferable case; With every cubic metre second water is benchmark, and the consumption of said flocculant solution makes that the amount of flocculation agent is 5-100ppm, more preferably under the situation; The consumption of said flocculant solution makes that the amount of poly acryloyl acid and ZX-I flocculation agent is 5-50ppm, makes that the amount of flocculant of polymeric aluminium chloride is 20-100ppm.
If used flocculation agent is a poly acryloyl acid; Then the consumption of said flocculant solution makes that the amount of poly acryloyl acid flocculation agent is 5-50ppm; If used flocculation agent is a ZX-I; Then the consumption of said flocculant solution makes that the amount of ZX-I flocculation agent is 5-50ppm, if used flocculation agent is poly acryloyl acid and ZX-I, then the consumption of said flocculant solution makes that the total amount of poly acryloyl acid and ZX-I flocculation agent is 5-50ppm.
Above-mentioned m/v refers to mass and size concentration, and concrete implication comprises the quality of flocculation agent in every liter of flocculant solution.
According to the present invention, first water and flocculant solution blended condition can be comprised blended time and blended temperature, for example, the said blended time can be 1-10 minute, more preferably 1-5 minute; Said blended temperature can be 30-70 ℃, more preferably 40-60 ℃.In order to make second water and flocculant solution blended more even, said second water and mixing preferably of flocculant solution are under agitation carried out.
According to the present invention, do not limit second water and flocculant solution blended mode are special, for example, can be static mixing, also can be dynamic mixing, also or the combination of two kinds of hybrid modes.Wherein, said static mixing can for: second water and flocculant solution at container, as are left standstill and mix in the equipment and leave standstill; Said dynamic mixing can for: will in another transport pipe, converge with being incorporated in the flow process from second water of different transport pipes and flocculant solution and mix; Second water and flocculant solution are mixed through line mixer, and this mixture is delivered in the equipment of leaving standstill leaves standstill.
According to the present invention, with second water mix with flocculant solution and will by the flocculation and/or the isolating method of settled proteinaceous solid substance be the method for dissolved air flotation.The method of said dissolved air flotation is to utilize the micro-bubble of high dispersing to go to adhere to that second aqueous phase is flocculated and/or settled proteinaceous solid particle as carrier, makes its density float to the water surface on less than water, realizes process of solid-liquid separation.According to the present invention; The method of said dissolved air flotation comprises with second water and flocculant solution blended simultaneously or afterwards; In mixture, blast air, make by flocculation and/or the bubble adhesion that is formed of settled proteinaceous solid particle and with bubble floating.Wherein, As long as in mixture the condition of bubbling air can with by flocculation and/or settled proteinaceous solid particle by the bubble adhesion that forms by the air that feeds and with bubble floating; Forming the air supporting layer gets final product; Under the preferable case, the pressure of bubbling air can be the 0.2-0.4 MPa, and the size of bubble can be the 15-30 micron usually.Generally, the said air supporting time can be 1-10 minute, is preferably 4-7 minute.
According to the present invention; Can adopt various existing airfloat equipments to realize solid-liquid separation; For example, can utilize air flotation slot to carry out dissolved air flotation, the principle of promptly utilizing different suspensions of material and absorption bubble (gas molecule) is with proteinaceous solid particle and water sepn.For example; The mixture of second water and the flocculant solution feed end by air flotation slot is got into; Air dissolved pump input gas electricity gets into the feed end of air flotation slot, and the gas that gets into air flotation slot forms the bubble diffusion by aeration head and plays in the liquid, and throw out and/or sediment that these bubbles will get into air flotation zone adhere to; And upwards floating along with flowing, water obtains clarification gradually.The proteinaceous solid particle that swims in the upper strata in a large number gathers and is called the higher liquid of concentration; Peeled by stripper plate from the air flotation slot discharge end then; And can filter; The air flotation slot middle part be clarifying water, the proteinaceous solid content of second water after the processing that obtains according to method of the present invention can be for below the 0.3 weight %.
According to the present invention, the method for separating the proteinaceous solid substance in second concentrated phase can adopt ordinary method known in those skilled in the art, for example, can carry out solid-liquid separation or directly carry out filtering separation through whizzer.Its concrete operation method and condition are conventionally known to one of skill in the art, here repeat no more.For example; In embodiment of the present invention, can adopt vacuum-type drum filter or plate-and-frame filter press to filter, filtering condition comprises sheet frame veneer model 125cm * 125cm, sheet frame MWP 0.4Mpa; Veneer filter cloth filtration area is generally 1.5 square metres, 758 model filter clothes.
According to the present invention, this method also comprises the step that dehydrates from second concentrated phase and/or the isolated proteinaceous solid substance of second aqueous phase.
Said method that dehydrates and condition all can adopt method well known in the art and condition to carry out.For example, the exsiccant mode can be seasoning, forced air drying, the drying mode of various routines such as vacuum-drying.Said exsiccant condition can comprise that drying temperature is more than 100 ℃, for example, and as 100-150 ℃; Can be 0.5-1.5 hour time of drying.
In the present invention, the light water that contains proteinaceous solid substance mutually that obtains after referring to the corn coarse starch milk separated of said seitan water.
Preparing method according to W-Gum provided by the invention; Wherein, The method that concentrates the corn steep liquor that obtains comprises evaporates corn steep liquor; The method of said evaporation comprises that the employing falling-film evaporator is concentrated into 40-45 weight % with the steeping water soak solution, and adopts scrapper thin film evaporator that the steeping water of the 40-45 weight % that obtains is concentrated into 48-52 weight %; Under the preferable case, adopt falling-film evaporator that the steeping water soak solution is concentrated into 40-42 weight %, and adopt scrapper thin film evaporator that the steeping water of the 40-42 weight % that obtains is concentrated into 48-50 weight %.
According to the present invention; As long as the method for said evaporation guarantees that after adopting falling-film evaporator that said steeping water soak solution is concentrated, making the concentration of the steeping water that obtains is 40-45 weight %; Be preferably 40-42 weight %; And guarantee adopting scrapper thin film evaporator with the 40-45 weight % that obtains, making the concentration of the spissated steeping water that obtains after the steeping water that is preferably 40-42 weight % concentrates is 48-52 weight %, is preferably 48-50 weight % and gets final product.
Under the preferable case, contriver of the present invention adopts scrapper thin film evaporator and falling-film evaporator to form multi-effect evaporation system, and said corn steep liquor is carried out multiple-effect evaporation.Wherein, said multiple-effect evaporation refers to the evaporation operation with several evaporator series operations, and steam thermal energy is repeatedly utilized, thereby improves the utilization ratio of heat energy.
Contriver of the present invention finds that adopting falling-film evaporator that number is imitated in the spissated evaporation of corn steep liquor can imitate for 3-4, and adopting the film-falling scraping plate vaporizer will pass through the further spissated evaporation of steeping water that the falling-film evaporator evaporation obtains, to imitate number be that 1-2 is imitated; Under the preferable case; Can adopt falling-film evaporator that the steeping water soak solution is carried out triple effect evaporation; Make the concentration of the steeping water that obtains reach 40-45 weight %, be preferably 40-42 weight %, then adopt one to imitate scrapper thin film evaporator the 40-45 weight % that obtains; Making the concentration of the spissated steeping water that obtains after the steeping water that is preferably 40-42 weight % concentrates is 48-52 weight %, is preferably 48-50 weight %.
According to a kind of embodiment of the present invention; Can adopt the method for quadruple effect evaporation that corn steep liquor is concentrated; That is, as shown in Figure 6, the first effect scrapper thin film evaporator and the second effect falling-film evaporator are connected; Second imitates falling-film evaporator connects with the triple effect falling-film evaporator, and the triple effect falling-film evaporator is connected with the quadruple effect falling-film evaporator.The method of said evaporation comprises corn steep liquor (IV is imitated charging) is pumped in the quadruple effect falling-film evaporator; Under 65-75 ℃ Heating temperature; To this corn steep liquor heating evaporation that circulates; Obtaining concentration is the quadruple effect steeping water feed liquid of 7-10 weight % and 50-55 ℃ four effect juice steams, and this quadruple effect steeping water feed liquid (IV is imitated feed liquid) is pumped in the second effect falling-film evaporator, under 98-105 ℃ Heating temperature; To this quadruple effect steeping water feed liquid heating evaporation that circulates, obtain concentration and be two effect juice steams that two of 18-20 weight % is imitated steeping water feed liquids and 85-90 ℃; This two effect steeping water feed liquid (II is imitated feed liquid) is pumped in the triple effect falling-film evaporator; Under 85-90 ℃ Heating temperature; This two is imitated steeping water feed liquid heating evaporation that circulates, and obtaining concentration is the triple effect steeping water feed liquid of 40-45 weight % and 65-75 ℃ three effect juice steams; This triple effect steeping water feed liquid (III is imitated feed liquid) is pumped into one imitates in the scrapper thin film evaporator; Under 120-130 ℃ Heating temperature; This triple effect steeping water feed liquid is evaporated, and obtaining concentration is the concentrated steeping water (I is imitated discharging) of 48-52 weight % and an effect juice steam of 98-110 ℃.
According to the present invention; The vacuum tightness that above-mentioned quadruple effect, triple effect, second effect and first are imitated when evaporating is corresponding one by one with the thermodynamic principles of the vaporization temperature foundation of each effect; For the ease of observing operation; Under the preferable case, the vacuum tightness of in the quadruple effect falling-film evaporator, evaporating can be 0.08MPa to 0.09MPa, more preferably 0.084MPa to 0.088MPa; The vacuum tightness of in the triple effect falling-film evaporator, evaporating can be 0.06MPa to 0.075MPa; Imitate the vacuum tightness of evaporating in the falling-film evaporator second and can be 0.03MPa to 0.04MPa; Imitate the pressure that evaporates in the scrapper thin film evaporator first and can be 0.01MPa to 0.05MPa, more preferably 0.01MPa-0.046MPa.Wherein, said vacuum tightness refers to be in the rare book degree of gas under the vacuum state.If the pressure in institute's measurement equipment is lower than atmospheric pressure, its pressure survey needs vacuum meter.Claim vacuum tightness from the numerical value that vacuum meter is read.Vacuum values is to express the numerical value that the system pressure actual numerical value is lower than atmospheric pressure, that is: vacuum tightness=(atmospheric pressure-psia).
In order to reduce the consumption of living steam, under the preferable case, the heating steam that is used for the second effect falling-film evaporator comes from the mixing steam that an effect juice steam perhaps is an effect juice steam and living steam; The heating steam that is used for the triple effect falling-film evaporator comes from two effect juice steams; The heating steam that is used for the quadruple effect falling-film evaporator comes from three effect juice steams; The heating steam that is used for the first effect scrapper thin film evaporator comes from living steam.Four effect juice steams can cool off through condensing surface with water coolant usually, and are connected with vacuum system.
That is, in the flow process of above-mentioned quadruple effect evaporation operation, first imitates scrapper thin film evaporator giving birth to steam as heating steam, and second imitates the heating steam as this effect of the juice vapour (being secondary steam) that all produces with its last effect to the quadruple effect falling-film evaporator.Especially, if the effect juice steam that the first effect scrapper thin film evaporator produces can not satisfy the heating requirements of the second effect falling-film evaporator, can replenish living steam and satisfy its heating requirements to produce enough juice vapour.Can guarantee that like this multi-effect evaporation system has enough steam capabilitys, and heating steam can utilize repeatedly, thereby can reduce the consumption of living steam significantly.
Wherein, heating steam and corn steep liquor or each imitate the steeping water liquid concentrator that obtains the flow direction can for and flow process, countercurrent flow, also can be the cross-flow flow process, be preferably the cross-flow flow process.
Under the preferable case; In order to make the steam capability maximum of falling-film evaporator; Before this method also is included in and goes into quadruple effect corn syrup liquid pump in the second effect falling-film evaporator; Quadruple effect steeping water feed liquid is preheated to the vaporization temperature of imitating near two, that is, can carries out second after quadruple effect steeping water feed liquid is preheated to 85-90 ℃ immediately and imitate in the falling-film evaporator and evaporate.According to the present invention; Said method with the corn steep liquor preheating can adopt the conventional various heat-exchange equipments in this area to heat; Under the preferable case, can adopt tubular heat exchange to heat, and said preheating can at least partly come from two effect juice steams with heating steam.
According to the present invention, said falling-film evaporator and scrapper thin film evaporator are this area evaporation equipment commonly used.The principle of work of said falling-film evaporator is: the shell side of vertical closed container internal heating tube bank is heating steam, and tube side is for being evaporated solution, and solution is membranaceous landing by being pumped to the container top distribution plate along the tubulation inwall; And by external steam heating vaporization; Get into the separate chamber in the bottom and carry out vapor-liquid separation, because vacuum action, juice vapour gets into the shell side of back single-effect evaporator; Liquid is then pumped into the container top heating again, and circulation constantly.The principle of work of said scrapper thin film evaporator is: be heating steam in the chuck of vertical closed container; Container is interior for being evaporated solution; And adopt scraper plate to force to stir; Make solution become membranaceous distribution, and, get into the separate chamber on container top and carry out vapor-liquid separation by the vaporization of the steam heating in the chuck at container inner wall.
In the present invention, just the treatment process of raw materials pretreatment and seitan water and the concentrating means of steeping water are improved, and all can be carried out according to the method for well known to a person skilled in the art for other step among the W-Gum preparation technology and condition.
For example, according to the present invention, corn grain soaked to adopt method known in those skilled in the art; For example; Under 50-55 ℃, be that the sulfurous acid aqueous solution of 0.1-0.35 weight % contacts 40-52 hour with corn particle and concentration, obtain corn steep liquor.Can make its each integral part loose with sulfurous acid soaking corn grain; Weaken mutual contact, sulfurous acid can also destroy the protein net, makes the semipermeable partition of corn grain epidermis become permeable membrane; Quicken and promote to permeate and diffusion; Make a large amount of water absorption and swellings of corn grain, softening, the great amount of soluble protein dissolution helps further being processed into steeping water in soak solution.The difference of solid content in the corn steep liquor that different soaking conditionses possibly cause obtaining, generally, the solid content of said corn steep liquor is 5-8 weight %.
According to the present invention, the corn grain that will pass through immersion takes off embryo, and the method for isolating plumule also can be carried out according to the method for well known to a person skilled in the art; For example, utilize corn degerming mill (TCM920), make the corn grain that gets into degerming mill under action of centrifugal force, get into the moving of band double wedge and decide between tooth plate; Because two dishes are done rotation relatively; And close outside dredging in recessed tooth is on dish, maize germ, scurf and endosperm are because of the fragmentation in various degree of the different quilts of physical property, and be separated from one another.Because the specific density of plumule and rest part is different, under action of centrifugal force, the free plumule is separated.
According to the present invention; The corn grain tissue that contains maize peel and endosperm that will take off behind the embryo grinds; Isolate the method for fiber and also can carry out, for example, utilize the pin mill to grind according to the method for well known to a person skilled in the art; At moving pin that receives high speed rotating and the fixed strong bump in repeated multiple times ground of deciding pin, most starch and fiber get loose and dissociate out.The thickness slag ratio generally can arrive 2.5-3: 1.Though the starch through after grinding has been unbound state, but still mixes with fibrous residue, owing to varying in size of several kinds of material particles; The screening plant that therefore, can utilize different sieve seams or aperture with fiber by separating in the farinaceous size, in said farinaceous size; The size of starch granules is generally the 5-30 micron; The particle size of fine-fibered is generally more than 65 microns in the fibrous residue, and the robust fibre slag becomes big sheet, and the seitan particle size is generally the 1-2 micron.Said screening plant can be various screening plants, for example, and pressure curved sieve or trommel, oscillating flat sieve, centrifugal screen etc.
According to the present invention, the coarse starch milk that obtains separated obtaining rare seitan and milk of starch, and the method that milk of starch washs can be carried out for method well known in the art.For example, the milk of starch in the coarse starch milk and the isolating principle of seitan mainly utilize specific density and the particle size of these two kinds of materials different and separate, and for example, can adopt settling process or centrifuging to separate.
Need to prove in addition; Each concrete technical characterictic described in above-mentioned embodiment under reconcilable situation, can make up through any suitable manner; For fear of unnecessary repetition, the present invention is to the explanation no longer separately of various possible array modes.
In addition, also can carry out arbitrary combination between the various embodiment of the present invention, as long as it is without prejudice to thought of the present invention, it should be regarded as the disclosed content of the present invention equally.
To further describe in detail the present invention through specific embodiment below, following examples only are used to explain the present invention, but are not used for limiting scope of the present invention.
Adopt disc separator that rare seitan is concentrated perhaps among the following embodiment and carry out solid-liquid separation, concentrated phase flows out from underflow, and stream flows out water from the top; The model of used disc-type separating centrifuge is DPF530.The model of air flotation slot is FXP300 * 5000, available from institute of Wuhan grain section.
The measuring method of the concentration of insoluble protein is an Oven Method in the process water that obtains after seitan water is concentrated.
Used two effects, triple effect and quadruple effect falling-film evaporator and this area falling-film evaporator commonly used among the following embodiment, available from the Yixing City,Grant dry and enrichment equipment Co., Ltd, model is JMZ-4.5, the moisture evaporation ability is 4500kg/h; Used one imitates the scrapper thin film evaporator that scrapper thin film evaporator and this area are used always, avenges unrestrained chemical plant factory available from Wuxi City Xishan, and model is LG-0.8, and the moisture evaporation ability is 160kg/h.
Embodiment 1
Present embodiment is used to explain the preparation method of W-Gum provided by the invention.
(1) raw materials pretreatment
Prepare the stone cistern that removes as shown in Figure 2, the said stone cistern 10 that removes comprises two relative sidewalls 11, the diapire 12 between these two sidewalls; And the inlet 13 and outlet 14 that are separately positioned on the cell body two ends between said two sidewalls 11; The height of the diapire 12 from said inlet 13 to said outlet 14 reduces gradually, and said diapire 12 is for being tilted to down domatic, and said domatic inclination angle (inclination angle with respect to the horizontal plane) is 10 to spend; The length of the horizontal direction of diapire 12 is 5 meters; With 8 baffle plates as obstacle be vertically set on said domatic on, the height of said plate washer reduces along the water flows direction gradually, the height of each baffle plate is 25cm.Said obstacle is spaced along the direction from said inlet 13 to said outlet 14,, is spaced apart 70cm between adjacent two obstacles along the flow direction of water.That is, inlet 13 and outlet 14 be respectively as the upstream and downstream of current, and current can rely on deadweight 13 to flow to outlet 14 from entering the mouth, and the height of said outlet 14 is higher than the height of the obstacle adjacent with said outlet 14.
Maize raw material (water cut 14 weight %) mixed with water obtain fluid mixture (consumption of water is 3 times of maize raw material gross weight); 13 inflows remove the stone cistern from entering the mouth; And it is mobile towards outlet 14; The flow rate control of current is being 1m/s, because the density of sandstone 22 is much larger than water and greater than the density of corn grain 21, thereby sandstone 22 can sink in flow process on the diapire 12.Sink to the sandstone 22 on the diapire 12 through restriction; It can't be continued on diapire 12 with water flows; And baffle plate can further stop sandstone " to be crossed " forward, thereby can sandstone 22 be limited in except that in the stone cistern 10, from exporting the corn grain after sandstone are removed in 14 collections.
(2) soak
To purify corn metering back, back and be delivered to steeping tank with waterpower, use concentration is that the sulfurous acid aqueous solution of 0.25 weight % carries out the adverse current immersion.Soaking filling is 10; Every tankage is 50 tons of maize raw materials after the above-mentioned purification, and the soak solution of steeping tank passes through a pump part self circulation, and a part is countercurrent flow with the adding corn; Be that initiate corn is used old soak; The corn that soaks is at most used new soak, and the soak time of corn is 48 hours, and soaking temperature is 50 ± 2 ℃.
(3) evaporation
According to Fig. 6; Three falling-film evaporators and a scrapper thin film evaporator are formed multiple-effect evaporator; The first effect scrapper thin film evaporator and the second effect falling-film evaporator are connected; Second imitates falling-film evaporator connects with the triple effect falling-film evaporator, and the triple effect falling-film evaporator is connected with the quadruple effect falling-film evaporator.
Will (every jar goes out 30m approximately by 50 ℃ of corn steep liquors extracting out in the steeping tank 3, dry matter content is 7 weight %), pump in the quadruple effect falling-film evaporator in the said multi-effect evaporation system that (control corn soaking flow quantity is 6m 3/ h); Under the vacuum tightness of 70 ℃ Heating temperatures, 0.068MPa; To the said corn steep liquor heating evaporation that circulates; Obtaining concentration is the quadruple effect steeping water feed liquid of 9 weight % and 52 ℃ four effect juice steams, this four effect juice steam is connected with vacuum pump through pipe bundle condenser, and (control feed liquid flow is 5-6m with the extraction of quadruple effect steeping water feed liquid 3/ h) and pump into second after being preheated to 85 ℃ and imitate in the falling-film evaporator; Under the vacuum tightness of 103 ℃ Heating temperatures, 0.015MPa; To the said quadruple effect steeping water feed liquid heating evaporation that circulates, obtain concentration and be two effect juice steams (part two is imitated the juice gas can be used for preheating quadruple effect steeping water feed liquid) that two of 20 weight % are imitated steeping water feed liquids and 88 ℃; Imitate the corn syrup liquid pumps with said two then and go into that (control feed liquid flow is 2-3m in the triple effect falling-film evaporator 3/ h); Under the vacuum tightness of 88 ℃ Heating temperatures, 0.034MPa; Adopt the two juice vapour of imitating to imitate the steeping water feed liquids heating evaporation that circulates to said two; Obtain output and be 1000kg/h, concentration and be triple effect steeping water feed liquid and 70 ℃ three effect juice steams about 42 weight %, and three effect juice steams to remake be the thermal source of quadruple effect falling-film evaporator; With said 1000kg/h, concentration is that triple effect corn syrup liquid pump about 42 weight % is gone into first and imitated in the scrapper thin film evaporator; And adopt 125 ℃ living steam, under the pressure of 0.24MPa; Said triple effect steeping water feed liquid is carried out heating evaporation, and obtaining output is that 840kg/h, concentration are the concentrated steeping water about 50 weight %.
(4) take off embryo
Corn after soaking is got into the wet corn hopper by the wet corn transferpump through rockover remover; Get into the one-level degerming mill again; Corn is broken into the 4-6 lobe; Contain shaping corn amount and be no more than 1 weight %, and tell the plumule of the 75-89 weight % of plumule total amount, discharge the starch of the 20-25 weight % of total starch content simultaneously;
Corn after the fragmentation is pumped to the plumule primary cyclone with plumule, and the effusive plumule in separator top removes washing system, and the underflow thing gets into the secondary degerming mill; Corn is broken for the 10-12 lobe; In this slurry, do not contain whole kernel corn, the plumule that is in bonding state is no more than 0.3 weight %, and the slurry of process secondary breaking is pumped into secondary plumule cyclone separator through plumule; Top stream thing gets into one-level germ separation device again, and underflow slurry is gone into the fine grinding operation.
(5) fine grinding
The underflow grout that process secondary cyclone separator is isolated behind the plumule passes through pressure curved sieve, and screen underflow is a coarse starch milk; Screen overflow gets into impact grinding (or pin mill) and carries out fine grinding, dissociates out with the free starch that itself and fiber are connect, and in the feasible slurry after grinding of the condition of pin mill, connects starch and is not more than 10 weight %.
Slurry after the fine grinding gets into the fiber wash groove, delivers to first step pressure curved sieve at these washing water with later washing the fibre.Screen underflow is isolated coarse starch milk, and through the countercurrent washing of the bent sieve of 6 stage pressures, washing process water adds before the last step sieve screen overflow again; Through compass screen surface, carrying the free starch that washs and moving forward step by step, before first step sieve in the rinse bath; Merge with the slurry after the fine grinding, get into first step pressure curved sieve jointly, tell coarse starch milk; The screen underflow coarse starch milk that this milk of starch and fine grinding fore worker are told converges, and gets into the starch separation circuit.Fiber on the compass screen surface, skin slag and washing water are gone against the stream, and,, after washing screening several times, discharge from the bent sieve of last step to each sieve is mobile later on from first sieve, dewater through screw extrusion press then.
(6) milk of starch is refining
Bent screening after sand separator, revolving filter are removed impurity, gets into elementary separating centrifuge (disc separator) from the thick starch that obtains from the fine grinding front and back, and it is rare seitan water that the overflow substance of discharging is flowed on the top, should carry out following processing by rare seitan water:
1) presses 350m 3The total flux of/h is on average sent into rare seitan water (concentration of proteinaceous solid substance is 1.7 weight %) and simultaneously rare seitan water is carried out once concentration in two disc separators (total feed of rare seitan water is 350m 3/ h, each inlet amount is 175m 3/ h, the rotating speed of spinning are respectively 3400 rev/mins, and the temperature of spinning is 45 ℃), the total flux that obtains first water is 200m 3/ the h (content of the proteinaceous solid substance of first aqueous phase is 0.3 weight %) and the total flux of first concentrated phase are 150m 3(the concentrated phase flow of each separating machine is respectively 75m to/h 3/ h) (proteinaceous solid content is 3.8 weight % in first concentrated phase); First concentrated phase sent into once more carry out secondary concentration in the disc separator (feed rate of first concentrated phase is 150m 3/ h, the rotating speed of spinning are 3500 rev/mins, and the temperature of spinning is 45 ℃), obtaining the second water flow is 106m 3/ the h and the second concentrated phase flow are 44m 3/ h (proteinaceous solid content is 12.1 weight % in second concentrated phase);
2) second concentrated phase that step 1) is obtained is inserted in the flame filter press and is filtered, and obtains filter cake (moisture 50 weight %); The filter cake that obtains is obtained feed (moisture content 10 weight %) 120 ℃ of oven dry, and the protein content that gets in the feed with the butt instrumentation is 62% (m/m);
3) be that 6,000,000 ZX-I flocculation agent is soluble in water with number-average molecular weight, make the mass and size specific concentration and be 0.05% solution; Poly aluminum Chloride (PAC) (n is 1-5, m≤10, basicity B=n/6 * 100%) is soluble in water, make the mass and size specific concentration and be 5% polymeric aluminum chlorides solution.And under 60 ℃; Second aqueous phase that obtains to step (1) adds above-mentioned two kinds of flocculant aqueous solutions; With every cubic metre second water is benchmark; The consumption of said ZX-I flocculant aqueous solution (25L) makes that the amount of ZX-I flocculation agent is 12.5ppm, and the consumption of the said flocculant of polymeric aluminium chloride aqueous solution (1L) makes that the amount of flocculant of polymeric aluminium chloride is 50ppm, mixes 1 minute; And the mixed solution that obtains inserted carry out dissolved air flotation in the air flotation slot (pressure of bubbling air is 0.3 MPa; The air supporting time is 5 minutes); Separate the proteinaceous solid particle in upper strata and mixed solution inserted in the flame filter press and filter; The content of the proteinaceous solid substance of aqueous phase that obtains is 0.22 weight %; The filter cake that obtains (water cut is 50 weight %) is obtained feed (moisture content 10 weight %) 120 ℃ of oven dry, and the protein content that gets in the feed with the butt instrumentation is 62% (m/m).
The starch concentration that obtains from elementary separating centrifuge underflow is 19-20 ° of Be '; And the moisture about 60 weight % of purified starch breast after 12 grades of swirler-washings; Protein contnt is less than 0.35 weight %; Smart milk of starch obtains the wet starch of moisture 38-40 weight % after dehydration, wet starch is sent into the pneumatic drier drying and obtained the commodity starch finished product.
Embodiment 2
Present embodiment is used to explain the preparation method of W-Gum provided by the invention.
Method according to embodiment 1 prepares W-Gum, and different is that in the step (6), the treatment process of said rare seitan water comprises:
1) presses 380m 3The total flux of/h is on average sent into rare seitan water (concentration of proteinaceous solid substance is 1.5 weight %) and simultaneously rare seitan water is carried out once concentration in two disc separators (total feed of rare seitan water is 380m 3/ h, each inlet amount is 190m 3/ h, the rotating speed of spinning are respectively 3300 rev/mins, and the temperature of spinning is 45 ℃), the total flux that obtains first water is 234m 3/ the h (content of the proteinaceous solid substance of first aqueous phase is 0.28 weight %) and the total flux of first concentrated phase are 146m 3(the concentrated phase flow of each separating machine is respectively 73m to/h 3/ h) (proteinaceous solid content is 3.5 weight % in first concentrated phase); First concentrated phase sent into once more carry out secondary concentration in the disc separator (feed rate of first concentrated phase is 146m 3/ h, the rotating speed of spinning are 3400 rev/mins, and the temperature of spinning is 45 ℃), obtaining the second water flow is 102m 3/ the h and the second concentrated phase flow are 44m 3/ h (proteinaceous solid content is 11 weight % in second concentrated phase);
2) second concentrated phase that step (1) is obtained is inserted in the flame filter press and is filtered, and obtains filter cake (moisture 50 weight %); The filter cake that obtains is obtained feed (moisture content 10 weight %) 120 ℃ of oven dry, and the protein content that gets in the feed with the butt instrumentation is 60% (m/m);
Method according to step 3) among the embodiment 1 is handled second water; The content of the proteinaceous solid substance of aqueous phase that obtains is 0.19 weight %; The filter cake that obtains (water cut is 50 weight %) is obtained protein fodder (moisture content 10 weight %) 120 ℃ of oven dry, and the protein content that gets in the feed with the butt instrumentation is 60% (m/m).
Embodiment 3
Present embodiment is used to explain the preparation method of W-Gum provided by the invention.
Method according to embodiment 1 prepares W-Gum, and different is that in the step (6), the treatment process of said rare seitan water comprises:
1) presses 360m 3The total flux of/h is on average sent into rare seitan water (concentration of proteinaceous solid substance is 1.6 weight %) and simultaneously rare seitan water is carried out once concentration in two disc separators (total feed of rare seitan water is 360m 3/ h, each inlet amount is 180m 3/ h, the rotating speed of spinning are respectively 3300 rev/mins, and the temperature of spinning is 45 ℃), the total flux that obtains first water is 231m 3/ the h (content of the proteinaceous solid substance of first aqueous phase is 0.31 weight %) and the total flux of first concentrated phase are 129m 3(the concentrated phase flow of each separating machine is respectively 64.5m to/h 3/ h) (content of proteinaceous solid substance is 3.9 weight % in first concentrated phase); First concentrated phase sent into once more carry out secondary concentration in the disc separator (feed rate of first concentrated phase is 129m 3/ h, the rotating speed of spinning are 3400 rev/mins, and the temperature of spinning is 45 ℃), obtaining the second water flow is 92m 3/ the h and the second concentrated phase flow are 37m 3/ h (content of proteinaceous solid substance is 12.3 weight % in second concentrated phase);
2) second concentrated phase that step (1) is obtained is inserted in the flame filter press and is filtered, and obtains filter cake (moisture 50 weight %); The filter cake that obtains is obtained feed (moisture content 10 weight %) 120 ℃ of oven dry, and the protein content that gets in the feed with the butt instrumentation is 61% (m/m);
Method according to step 3) among the embodiment 1 is handled second water; The content of the proteinaceous solid substance of aqueous phase that obtains is 0.24 weight %; The filter cake that obtains (water cut is 50 weight %) is obtained protein fodder (moisture content 10 weight %) 120 ℃ of oven dry, and the protein content that gets in the feed with the butt instrumentation is 61% (m/m).
Embodiment 4
Present embodiment is used to explain the preparation method of W-Gum provided by the invention.
Method according to embodiment 1 prepares W-Gum, and different is that in the step (6), the treatment process of said rare seitan water comprises:
1) presses 380m 3The total flux of/h is on average sent into rare seitan water (concentration of proteinaceous solid substance is 1.7 weight %) and simultaneously rare seitan water is carried out once concentration in two disc separators (total feed of rare seitan water is 380m 3/ h, each inlet amount is 190m 3/ h, the rotating speed of spinning are respectively 3300 rev/mins, and the temperature of spinning is 45 ℃), the total flux that obtains first water is 228m 3/ the h (content of the proteinaceous solid substance of first aqueous phase is 0.29 weight %) and the total flux of first concentrated phase are 152m 3(the concentrated phase flow of each separating machine is respectively 76m to/h 3/ h) (content of proteinaceous solid substance is 3.8 weight % in first concentrated phase); First concentrated phase sent into once more carry out secondary concentration in the disc separator (feed rate of first concentrated phase is 152m 3/ h, the rotating speed of spinning are 3400 rev/mins, and the temperature of spinning is 45 ℃), obtaining the second water flow is 110m 3/ the h and the second concentrated phase flow are 42m 3/ h (solid content is 11.8 weight % in second concentrated phase);
2) second concentrated phase that step (1) is obtained is inserted in the vacuum-type drum filter and is filtered, and obtains filter cake (moisture 50 weight %); The filter cake that obtains is obtained feed (moisture content 10 weight %) 120 ℃ of oven dry, and the protein content that gets in the feed with the butt instrumentation is 61% (m/m);
Method according to step 3) among the embodiment 1 is handled second water; The content of the proteinaceous solid substance of aqueous phase that obtains is 0.20 weight %; The filter cake that obtains (water cut is 50 weight %) is obtained protein fodder (moisture content 10 weight %) 120 ℃ of oven dry, and the protein content that gets in the feed with the butt instrumentation is 61% (m/m).
Embodiment 5
Present embodiment is used to explain the preparation method of W-Gum provided by the invention.
Method according to embodiment 1 prepares W-Gum, and different is, in the step (6), in the step 3) of the treatment process of said rare seitan water:
With number-average molecular weight is that 8,000,000 ROHM flocculation agent is soluble in water, makes the mass and size specific concentration and be 0.05% solution; Poly aluminum Chloride (PAC) (n is 1-5, m≤10, basicity B=n/6 * 100%) is soluble in water, make the mass and size specific concentration and be 5% polymeric aluminum chlorides solution.And under 40 ℃; Add above-mentioned two kinds of flocculant aqueous solutions to second aqueous phase; With every cubic metre second water is benchmark; The consumption of said ROHM flocculant aqueous solution (25L) makes that the amount of ROHM flocculation agent is 12.5ppm, and the consumption of the said flocculant of polymeric aluminium chloride aqueous solution (1L) makes that the amount of flocculant of polymeric aluminium chloride is 50ppm, mixes 3 minutes; And the mixed solution that obtains inserted carry out dissolved air flotation in the air flotation slot (pressure of bubbling air is 0.4 MPa; The air supporting time is 8 minutes); Separate upper strata seitan particle and mixed solution inserted in the flame filter press and filter; The content of the proteinaceous solid substance of aqueous phase that obtains is 0.21 weight %, and the filter cake that obtains (water cut is 50 weight %) is obtained protein fodder (moisture content 10 weight %) 120 ℃ of oven dry, and the protein content that gets in the feed with the butt instrumentation is 62% (m/m).
Embodiment 6
Present embodiment is used to explain the preparation method of W-Gum provided by the invention.
Method according to embodiment 1 prepares W-Gum, and different is, in the step (6), in the step 3) of the treatment process of said rare seitan water:
With every cubic metre second water is benchmark; The consumption of said ZX-I flocculant aqueous solution (30L) makes that the amount of ZX-I flocculation agent is 15ppm; The consumption of the said flocculant of polymeric aluminium chloride aqueous solution (0.9L) makes that the amount of flocculant of polymeric aluminium chloride is 45ppm; The content of the proteinaceous solid substance of aqueous phase that obtains after the filtration is 0.21 weight %; The filter cake that obtains (water cut is 50 weight %) is obtained protein fodder (moisture content 10 weight %) 120 ℃ of oven dry, and the protein content that gets in the feed with the butt instrumentation is 61% (m/m).
Embodiment 7
Present embodiment is used to explain the preparation method of W-Gum provided by the invention.
Method according to embodiment 5 prepares W-Gum, and different is, in the step (6), in the step 3) of the treatment process of said rare seitan water:
With the flocculant aqueous solution and the second water blended mode is to add the aqueous solution of Poly aluminum Chloride (PAC) earlier, and mixes 2 minutes, and then adds the polyacrylic aqueous solution, mixes 1 minute.The content of the proteinaceous solid substance of aqueous phase that obtains after the filtration is 0.18 weight %; The filter cake that obtains (water cut is 50 weight %) is obtained protein fodder (moisture content 10 weight %) 120 ℃ of dryings, and the protein content that gets in the feed with the butt instrumentation is 62% (m/m).
Embodiment 8
Present embodiment is used to explain the preparation method of W-Gum provided by the invention.
Method according to embodiment 5 prepares W-Gum, and different is, in the step (6), in the step 3) of the treatment process of said rare seitan water:
With the flocculant aqueous solution and the second water blended mode is to add the aqueous solution of Poly aluminum Chloride (PAC) earlier, and mixes 2 minutes, and then adds the polyacrylic aqueous solution, mixes 1 minute; With every cubic metre second water is benchmark; The consumption (4L) of the aqueous solution of said Poly aluminum Chloride (PAC) (the mass and size specific concentration of Poly aluminum Chloride (PAC) is 2%) makes that the amount of flocculation agent is 80ppm, and the consumption (20L) of the said polyacrylic aqueous solution (polyacrylic mass and size specific concentration is 0.2%) makes that the amount of flocculation agent is 40ppm.The content of the proteinaceous solid substance of aqueous phase that obtains after the filtration is 0.19 weight %; The filter cake that obtains (water cut is 50 weight %) is obtained protein fodder (moisture content 10 weight %) 120 ℃ of dryings, and the protein content that gets in the feed with the butt instrumentation is 61% (m/m).
Embodiment 9
Present embodiment is used to explain the preparation method of W-Gum provided by the invention.
Method according to embodiment 5 prepares W-Gum, and different is, in the step (6), in the step 3) of the treatment process of said rare seitan water:
With the flocculant aqueous solution and the second water blended mode is to add the aqueous solution of Poly aluminum Chloride (PAC) earlier, and mixes 2 minutes, and then adds the polyacrylic aqueous solution, mixes 1 minute; With every cubic metre second water is benchmark; The consumption (3L) of the aqueous solution of said Poly aluminum Chloride (PAC) (the mass and size specific concentration of Poly aluminum Chloride (PAC) is 1%) makes that the amount of flocculation agent is 30ppm, and the consumption (15L) of the said polyacrylic aqueous solution (polyacrylic mass and size specific concentration is 0.1%) makes that the amount of flocculation agent is 15ppm.The content of the proteinaceous solid substance of aqueous phase that obtains after the filtration is 0.18 weight %; The filter cake that obtains (water cut is 50 weight %) is obtained protein fodder (moisture content 10 weight %) 120 ℃ of dryings, and the protein content that gets in the feed with the butt instrumentation is 60% (m/m).
Embodiment 10
Present embodiment is used to explain the preparation method of W-Gum provided by the invention.
Method according to embodiment 5 prepares W-Gum, and different is, in the step (6), in the step 3) of the treatment process of said rare seitan water:
With the flocculant aqueous solution and the second water blended mode is to add the aqueous solution of Poly aluminum Chloride (PAC) earlier, and mixes 2 minutes, and then adds the polyacrylic aqueous solution, mixes 1 minute; With every cubic metre second water is benchmark; The consumption (0.8L) of the aqueous solution of said Poly aluminum Chloride (PAC) (the mass and size specific concentration of Poly aluminum Chloride (PAC) is 5%) makes that the amount of flocculation agent is 40ppm, and the consumption (80L) of the said polyacrylic aqueous solution (polyacrylic mass and size specific concentration is 0.05%) makes that the amount of flocculation agent is 40ppm.The content of the proteinaceous solid substance of aqueous phase that obtains after the filtration is 0.21 weight %; The filter cake that obtains (water cut is 50 weight %) is obtained protein fodder (moisture content 10 weight %) 120 ℃ of dryings, and the protein content that gets in the feed with the butt instrumentation is 62% (m/m).
Embodiment 11
Present embodiment is used to explain the preparation method of W-Gum provided by the invention.
Method according to embodiment 1 prepares W-Gum, and different is: in the evaporation technology of step (3), and will (every jar goes out 25m approximately by 50 ℃ of corn steep liquors extracting out in the steeping tank 3, dry matter content is 8 weight %), pump in the quadruple effect falling-film evaporator in the said multi-effect evaporation system that (control corn soaking flow quantity is 6.2m 3/ h); Under the vacuum tightness of 70 ℃ Heating temperatures, 0.068MPa; To the said corn steep liquor heating evaporation that circulates; Obtaining concentration is the quadruple effect steeping water feed liquid of 10 weight % and 52 ℃ four effect juice steams, this four effect juice steam is connected with vacuum pump through pipe bundle condenser, and (control feed liquid flow is 5-6m with the extraction of quadruple effect steeping water feed liquid 3/ h) and pump into second after being preheated to 88 ℃ and imitate in the falling-film evaporator; Under the vacuum tightness of 105 ℃ Heating temperatures, 0.023MPa; To the said quadruple effect steeping water feed liquid heating evaporation that circulates, obtain concentration and be two effect juice steams (part two is imitated the juice gas can be used for preheating quadruple effect steeping water feed liquid) that two of 21 weight % are imitated steeping water feed liquids and 90 ℃; Imitate the corn syrup liquid pumps with said two then and go into that (control feed liquid flow is 2-3m in the triple effect falling-film evaporator 3/ h); Under the vacuum tightness of 90 ℃ Heating temperatures, 0.03MPa; Adopt the two juice vapour of imitating to imitate the steeping water feed liquids heating evaporation that circulates to said two; Obtain output and be 1180kg/h, concentration and be triple effect steeping water feed liquid and 70 ℃ three effect juice steams about 42 weight %, and three effect juice steams to remake be the thermal source of quadruple effect falling-film evaporator; With said 1180kg/h, concentration is that triple effect corn syrup liquid pump about 42 weight % is gone into first and imitated in the scrapper thin film evaporator; And adopt 130 ℃ living steam, under the pressure of 0.18MPa; Said triple effect steeping water feed liquid is carried out heating evaporation, and obtaining output is that 990kg/h, concentration are the concentrated steeping water about 51 weight %.
Embodiment 12
Present embodiment is used to explain the preparation method of W-Gum provided by the invention.
Method according to embodiment 1 prepares W-Gum, and different is: in the evaporation technology of step (3), and will (every jar goes out 35m approximately by 50 ℃ of corn steep liquors extracting out in the steeping tank 3, dry matter content is 6 weight %), pump in the quadruple effect falling-film evaporator in the said multi-effect evaporation system that (control corn soaking flow quantity is 5.8m 3/ h); Under the vacuum tightness of 65 ℃ Heating temperatures, 0.075MPa; To the said corn steep liquor heating evaporation that circulates; Obtaining concentration is the quadruple effect steeping water feed liquid of 8 weight % and 50 ℃ four effect juice steams, this four effect juice steam is connected with vacuum pump through pipe bundle condenser, and (control feed liquid flow is 5-6m with the extraction of quadruple effect steeping water feed liquid 3/ h) and pump into second after being preheated to 85 ℃ and imitate in the falling-film evaporator; Under the pressure of 99 ℃ Heating temperatures, 0MPa; To the said quadruple effect steeping water feed liquid heating evaporation that circulates, obtain concentration and be two effect juice steams (part two is imitated the juice gas can be used for preheating quadruple effect steeping water feed liquid) that two of 19 weight % are imitated steeping water feed liquids and 85 ℃; Imitate the corn syrup liquid pumps with said two then and go into that (control feed liquid flow is 2-3m in the triple effect falling-film evaporator 3/ h); Under the vacuum tightness of 85 ℃ Heating temperatures, 0.04MPa; Adopt the two juice vapour of imitating to imitate the steeping water feed liquids heating evaporation that circulates to said two; Obtain output and be 830kg/h, concentration and be triple effect steeping water feed liquid and 65 ℃ three effect juice steams about 42 weight %, and three effect juice steams to remake be the thermal source of quadruple effect falling-film evaporator; With said 830kg/h, concentration is that triple effect corn syrup liquid pump about 42 weight % is gone into first and imitated in the scrapper thin film evaporator; And adopt 120 ℃ living steam, under the pressure of 0.1MPa; Said triple effect steeping water feed liquid is carried out heating evaporation, and obtaining output is that 700kg/h, concentration are the concentrated steeping water about 50 weight %.
Comparative Examples 1
This Comparative Examples is used to explain the preparation method of the W-Gum of prior art.
Method according to embodiment 1 is carried out raw materials pretreatment and immersion with corn, and different is:
In the evaporation technology of step (3), adopt triple effect falling-film evaporator system that corn steep liquor is concentrated, that is, and will (every jar goes out 30m approximately by 50 ℃ of corn steep liquors extracting out in the steeping tank 3, dry matter content is 7 weight %), pump in the quadruple effect falling-film evaporator in the said multi-effect evaporation system that (control corn soaking flow quantity is 6m 3/ h); Under the vacuum tightness of 70 ℃ Heating temperatures, 0.068MPa; To the said corn steep liquor heating evaporation that circulates; Obtaining concentration is the quadruple effect steeping water feed liquid of 9 weight % and 52 ℃ four effect juice steams, this four effect juice steam is connected with vacuum pump through pipe bundle condenser, and (control feed liquid flow is 5-6m with the extraction of quadruple effect steeping water feed liquid 3/ h) and pump into second after being preheated to 85 ℃ and imitate in the falling-film evaporator; Under the vacuum tightness of 103 ℃ Heating temperatures, 0.015MPa; To the said quadruple effect steeping water feed liquid heating evaporation that circulates, obtain concentration and be two effect juice steams (part two is imitated the juice gas can be used for preheating quadruple effect steeping water feed liquid) that two of 20 weight % are imitated steeping water feed liquids and 88 ℃; Imitate the corn syrup liquid pumps with said two then and go into that (control feed liquid flow is 2-3m in the triple effect falling-film evaporator 3/ h); Under the vacuum tightness of 88 ℃ Heating temperatures, 0.034MPa; Adopt the two juice vapour of imitating to imitate the steeping water feed liquids heating evaporation that circulates to said two; Obtain output and be 1000kg/h, concentration and be triple effect steeping water feed liquid and 70 ℃ three effect juice steams about 42 weight %, and three effect juice steams to remake be the thermal source of quadruple effect falling-film evaporator.If in the triple effect falling-film evaporator, feed liquid is continued evaporation, make its concentration reach 48-52 weight %, then can be owing to viscosity of sludge is excessive; Mobile poor; And dried wall, coking phenomenon appear in heating tube, heating tube is stopped up in the long-time running meeting, and vaporizer can not normally be moved.
In the milk of starch process for refining of step (6), the treatment process of said rare seitan water comprises:
1) presses 350m 3The flow of/h is on average sent into total rare seitan water (proteinaceous solid concentration is 1.7 weight %) and simultaneously seitan water is concentrated in two disc separators that (the combined feed total feed flow of seitan water is 350m 3/ h, each inlet amount is 175m 3/ h, the rotating speed of spinning are respectively 3300 rev/mins, and the temperature of spinning is 45 ℃), the total flux that obtains process water is 310m 3(the process water flow of each separating machine is 155m to/h 3/ h) (proteinaceous solid content is 0.76 weight % in the process water) and the total flux of enriched material are 40m 3(the enriched material flow of each separating machine is 20m to/h 3/ h) (proteinaceous solid content is 9 weight % in the enriched material);
2) enriched material that step (1) is obtained is inserted in the flame filter press and is filtered, and obtains filter cake (moisture 50 weight %); The filter cake that obtains is obtained feed (moisture content 10 weight %) 120 ℃ of oven dry, and the protein content that gets in the feed with the butt instrumentation is 55% (m/m).
Contrast by the foregoing description 1-12 and Comparative Examples 1 can be found out; Adopt method of the present invention effectively to concentrate to seitan water; And be met the process water (proteinaceous solid content is less than 0.3 weight % in first water) of direct reuse standard simultaneously and contain the higher enriched material of proteinaceous solid content (proteinaceous solid content is greater than 11 weight % in second concentrated phase); On the one hand; Process water reuse circulation once more soaks corn and plumule, fiber is washed, and on the other hand, can improve the productive rate of gluten protein powder.In addition; Separate through adding the flocculation agent solid substance that the floating isolating method of promoting the circulation of qi can be further carries out second aqueous phase of secondary treatment with need of going forward side by side; Further obtain protein fodder, and, therefore handle more easily because the volume of second water is less relatively.
In addition; Adopt scrapper thin film evaporator and falling-film evaporator to form multi-effect evaporation system; Adopt falling-film evaporator that corn steep liquor is concentrated into 40-45 weight % earlier; Then utilize scrapper thin film evaporator as the high density concentrating unit, can be further be that the steeping water of 40-45 weight % is concentrated into 48-52 weight % with concentration.Avoided on the one hand when adopting falling-film evaporator that steeping water is concentrated; The dense steeping water of excessive concentration is because viscosity Da Yi stops up the problem of the heating tube of falling-film evaporator; And the characteristics of scrapper thin film evaporator have been utilized dexterously; Can the concentration of steeping water be increased to suitable concentrated concentration (48-52 weight %), and obtain the higher steeping water liquid concentrator of concentration.

Claims (23)

1. the preparation method of a W-Gum, this method comprises the sandstone of removing in the maize raw material, the soaking corn grain; Concentrate the corn steep liquor obtain, and the corn grain that will pass through immersion carries out fragmentation, isolate plumule; The corn particle that contains maize peel and endosperm that will take off behind the embryo grinds, and isolates fiber, the coarse starch milk that obtains is separated obtaining rare seitan and milk of starch; And milk of starch washed, it is characterized in that:
Said method of removing the sandstone in the maize raw material comprises:
Make said maize raw material with water from being positioned at the elevated upper reaches towards the downstream flow that is positioned at low level, and said sandstone are sunk in flow process, the density of said corn grain is less than the density of said sandstone;
The said sandstone that restriction is sunk continue to flow with water;
The treatment process of said seitan water comprises seitan water concentrated, and said the spissated method of seitan water comprised:
(1) seitan water is carried out once concentration, obtain first concentrated phase and first water, the condition of once concentration makes the content of the first aqueous phase insoluble protein that obtains less than 0.3 weight %;
(2) first concentrated phase is carried out secondary concentration, obtain second concentrated phase and second water, it is more than the 10 weight % that the condition of secondary concentration makes the content of insoluble protein in second concentrated phase that obtains;
(3) second water is mixed with flocculant solution, the promoting the circulation of qi of going forward side by side is floating to be separated; Said flocculation agent is for making the insoluble protein flocculation and/or the settled material of second aqueous phase;
The said method that concentrates the corn steep liquor that obtains comprises evaporates corn steep liquor; The method of said evaporation comprises that the employing falling-film evaporator is concentrated into 40-45 weight % with corn steep liquor, and adopts scrapper thin film evaporator that the steeping water of the 40-45 weight % that obtains is concentrated into 48-52 weight %.
2. preparation method according to claim 1, wherein, the sandstone that said restriction is sunk continue the mobile method with water and comprise along the flow direction of water a plurality of obstacles are set that the sandstone that said obstacle restriction is sunk continue to flow with water.
3. preparation method according to claim 2, wherein, the said maize raw material that contains corn grain and sandstone is mobile along being tilted to down domatic with liquid, said a plurality of obstacles be arranged on said domatic on; Said obstacle is perpendicular to said domatic.
4. preparation method according to claim 3, wherein, said domatic inclination angle is the 5-15 degree.
5. preparation method according to claim 3, wherein, along the flow direction of water, the distance between adjacent two obstacles progressively increases.
6. preparation method according to claim 2 wherein, makes the said maize raw material that contains corn grain and sandstone with the downward successively a plurality of step-flow in water edge, and a said obstacle all is set on each step.
7. preparation method according to claim 6, wherein, said obstacle is arranged on the free edge of tread portion of said step; Said obstacle is perpendicular to the plane at said tread portion place.
8. according to claim 6 or 7 described preparing methods, wherein, the height of said obstacle is 1 with the ratio of the height of said step: 1-1: 3.
9. according to the method for claim 2,3,6 or 7 described preparations, wherein, said obstacle is a baffle plate.
10. preparation method according to claim 9, wherein, the height streamwise of said plate washer reduces gradually.
11. preparation method according to claim 9, wherein, the height of said plate washer is 15-50cm.
12. preparation method according to claim 1, wherein, the flow velocity of said water is 0.3-1.5m/s; The consumption of said water be said maize raw material gross weight 2-5 doubly.
13. preparation method according to claim 1; Wherein, It is 0.1-0.3 weight % that the condition of once concentration makes the content of the proteinaceous solid substance of first aqueous phase that obtains, and it is 10-12 weight % that the condition of secondary concentration makes the content of proteinaceous solid substance in second enriched material that obtains.
14. according to claim 1 or 13 described preparing methods, wherein, it is 2-3 that the condition of once concentration makes the concentration ratio of first concentrated phase: 1, the concentration ratio of said first concentrated phase is the feed volume of once concentration seitan water and the ratio of the first concentrated phase volume; The condition of secondary concentration makes that the concentration ratio of second concentrated phase is 3-4: 1, and the concentration ratio of said second concentrated phase is the feed volume of secondary concentration first concentrated phase and the ratio of the second concentrated phase volume.
15. preparation method according to claim 1, wherein, said flocculant solution is the aqueous solution of flocculation agent, and the aqueous solution of said flocculation agent is the aqueous solution of ROHM and/or ZX-I and the aqueous solution of Poly aluminum Chloride (PAC).
16. preparation method according to claim 15, wherein, the mass and size concentration of the ROHM aqueous solution and ROHM sodium water solution is 0.1-0.5%, and the mass and size concentration of the Poly aluminum Chloride (PAC) aqueous solution is 1-5%; Said polyacrylic number-average molecular weight is 6,000,000-1,000 ten thousand dalton, and the number-average molecular weight of said ZX-I is 6,000,000-1,000 ten thousand dalton; The molecular formula of said Poly aluminum Chloride (PAC) is [Al 2(OH) nCl 6-n] m, wherein, n is 1-5, m≤10, basicity B=n/6 * 100%.
17. preparation method according to claim 16; Wherein, Second water and flocculant solution method of mixing are comprised earlier the aqueous solution with said second water and Poly aluminum Chloride (PAC), again with the aqueous solution of the polyacrylic aqueous solution and/or ZX-I; The mass ratio of Poly aluminum Chloride (PAC) and ROHM and/or ZX-I is 2-5.
18. preparation method according to claim 16; Wherein, With every cubic metre of pending water is benchmark, and the consumption of said flocculant solution makes that the amount of ROHM and ZX-I flocculation agent is 5-50ppm, makes that the amount of flocculant of polymeric aluminium chloride is 20-100ppm.
19. preparation method according to claim 1; Wherein, The method of said dissolved air flotation comprises with second water and flocculant solution blended simultaneously or afterwards; In mixture, blast air, make by flocculation and/or the bubble adhesion that is formed of settled seitan particle and with bubble floating, and separate said by flocculation and/or settled seitan particle; The pressure of bubbling air is the 0.2-0.4 MPa, and the air supporting time is 1-10 minute.
20. preparation method according to claim 1; Wherein, The method of said evaporation comprises that the employing falling-film evaporator is concentrated into 40-42 weight % with the steeping water soak solution, and adopts scrapper thin film evaporator that the steeping water of the 40-42 weight % that obtains is concentrated into 48-50 weight %.
21. according to claim 1 or 20 described preparing methods; Wherein, Adopting falling-film evaporator that number is imitated in the spissated evaporation of corn steep liquor is that 3-4 is imitated, and adopting the film-falling scraping plate vaporizer will pass through the further spissated evaporation of steeping water that the falling-film evaporator evaporation obtains, to imitate number be that 1-2 is imitated.
22. preparation method according to claim 21; Wherein, the method for said evaporation comprises corn steep liquor is pumped in the quadruple effect falling-film evaporator, under 65-75 ℃ Heating temperature; To this corn steep liquor heating evaporation that circulates; Obtaining concentration is the quadruple effect steeping water feed liquid of 7-10 weight % and 50-55 ℃ four effect juice steams, and this quadruple effect corn syrup liquid pump is gone in the second effect falling-film evaporator, under 98-105 ℃ Heating temperature; To this quadruple effect steeping water feed liquid heating evaporation that circulates, obtain concentration and be two effect juice steams that two of 18-20 weight % is imitated steeping water feed liquids and 85-90 ℃; This two is imitated corn syrup liquid pump and go in the triple effect falling-film evaporator, under 85-90 ℃ Heating temperature, this two is imitated steeping water feed liquid heating evaporation that circulates, obtaining concentration is the triple effect steeping water feed liquid of 40-45 weight % and 65-75 ℃ three effect juice steams;
This triple effect corn syrup liquid pump is gone into one imitate in the scrapper thin film evaporator, under 120-130 ℃ Heating temperature, this triple effect steeping water feed liquid is evaporated, obtaining concentration is the concentrated steeping water of 48-52 weight % and an effect juice steam of 98-110 ℃.
23. preparation method according to claim 22, wherein, the heating steam that is used for the second effect falling-film evaporator comes from the mixing steam that an effect juice steam perhaps is an effect juice steam and living steam; The heating steam that is used for the triple effect falling-film evaporator comes from two effect juice steams; The heating steam that is used for the quadruple effect falling-film evaporator comes from three effect juice steams.
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CN103059145A (en) * 2012-12-22 2013-04-24 泰安弘兴玉米开发有限公司 Method for producing corn protein powder
CN104151447A (en) * 2014-08-26 2014-11-19 淮安麦德森制药有限公司 Method for removing impurities from chondroitin sulfate enzymatic hydrolysate

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CN1054030C (en) * 1997-11-18 2000-07-05 河南莲花味之素有限公司 Process for extracting protein from waster water of starch
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103059145A (en) * 2012-12-22 2013-04-24 泰安弘兴玉米开发有限公司 Method for producing corn protein powder
CN104151447A (en) * 2014-08-26 2014-11-19 淮安麦德森制药有限公司 Method for removing impurities from chondroitin sulfate enzymatic hydrolysate

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