CN102807626B

CN102807626B - Method for preparing corn starch

Info

Publication number: CN102807626B
Application number: CN201110146079.5A
Authority: CN
Inventors: 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
Original assignee: State Grain Reserve Wuhan Scientific Research And Design Institute; Cofco Corp
Current assignee: 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
Priority date: 2011-06-01
Filing date: 2011-06-01
Publication date: 2014-10-22
Anticipated expiration: 2031-06-01
Also published as: CN102807626A

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, as farm crop, inevitably can be sneaked into dust and rubble in plucking collection process in corn grain.Therefore,, in corn processed process, first need the maize raw material to containing corn grain carry out dedusting and remove stone and process.Conventionally, can adopt suitable screening and pneumatic separation device that the dust of sneaking into and rubble are removed by screen cloth.But this mode belongs to dry cleaning, and processing power is limited.In addition, for the more firmly earth adhering on corn grain with the onesize stone of corn grain, the removal effect of aforesaid method is not good enough.

Then, need to carry out follow-up processing to completing pretreated corn grain, for example, the leaching process of starch is the process of the chief component separation 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, have dividing of dry grinding and wet-milling.

Wherein, wet-milling is the technique of current corn starch industry universal, is mainly the corn process through dipping broken, de-embryo, fine grinding and screening, to separate plumule, fibrous residue, makes the process of rough starch milk.Starch is after mill riddler order is extracted, and gained starch milk is still coarse starch milk, still contains a large amount of insoluble proteins and soluble substance, and the concentration of powder slurry is also rarer, need to refine and concentrate, for finally processing and deep processing provides pure smart starch milk.

Refining method is mainly to utilize the principle of centrifugation, and coarse starch milk is carried out to separation, separates light phase and heavy phase, the light water for containing insoluble protein mutually, i.e. gluten water, heavy phase is starch milk, with pure water washing, remove soluble substance remaining in starch milk again, obtain smart starch milk.And isolated gluten water utilizes the method for centrifugation to concentrate again, obtain enriched material and process water, after enriched material is dehydrated, obtain gluten protein powder.The process water that separation obtains, can be back to use in the washing process of technique for soaking corn or starch milk by direct circulation.

But, adopt the method for prior art again to utilize the method for centrifugation to carry out concentrated technique deficiency so that insoluble protein is fully separated to gluten water, separation efficiency is lower, cause the productive rate of gluten protein powder not high, and still contain a certain amount of insoluble protein in the separated process water obtaining, not only can cause the productive rate of gluten protein powder to reduce, if after process water direct circulation is back to use in technique for soaking corn and plumule, fibre washing technique, the immersion effect of corn and quality product also can variation.

In addition, corn steep liquor is one of significant by-products of wet milling process production of corn starch, is also the byproduct proposing at first in Starch Production, by corn steeping water is concentrated, obtains, and is actually the extract of corn.Described corn steeping water outward appearance is brown viscous liquid, dry matter content is about 5-8 % by weight, main component major part is corn soluble protein and degradation product thereof, as peptide class, each seed amino acid etc., also contain in addition lactic acid, phytic acid ca magnesium salts, soluble saccharide, there is very high nutritive value, 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, transport and use, 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 the % by weight containing dry-matter 40-45, be dense corn steep liquor.Conventionally adopt multiple-effect falling film vaporizer to concentrate corn steep liquor, reduce the water content in corn steep liquor as far as possible, to reduce the excess moisture that sprays into corn steep liquor in fiber feedstuff drying process, cause energy consumption to strengthen, cause drying machine yield reducation, and corn steep liquor can not be joined in fiber feedstuff completely.Because falling-film evaporator adopts tubulation indirect heating material conventionally, if heated material concentration is too high, viscosity is large, is easy to cause evaporator heating pipe Local Dry wall, coking, scale formation, and stop up heating tube, steam capability is reduced greatly.Therefore concentrated corn steep liquor concentration generally can only reach 40-45 % by weight left and right.

Summary of the invention

The object of the invention is to overcome the deficiency in the W-Gum preparation technology of prior art, and provide a kind of from raw materials pretreatment, improvement to the processing of the gluten water in starch preparation process and the concentrated whole W-Gum technique of corn steep liquor, and realize conveniently, continuously corn grain carried out to dedusting and remove stone and process, improve gluten protein powder productive rate and can directly process water reuse can be improved again to process water cyclically utilizing to the corn soaking effect of technique for soaking corn and cyclically utilizing to plumule, the starch washing effect of fibre washing technique and concentrated corn steep liquor that can by-product high density, do not affect the successional W-Gum preparation method of W-Gum technique.

The invention provides a kind of preparation method of W-Gum, the method comprises the sandstone of removing in maize raw material, the corn grain that immersion obtains, the concentrated corn steep liquor obtaining, and the corn grain through soaking is carried out to fragmentation, isolate plumule, the corn grain tissue that contains maize peel and endosperm after de-embryo is ground, isolate fiber, the coarse starch milk obtaining is carried out to separation and obtain gluten water and starch milk, and starch milk is washed, wherein:

Described method of removing the sandstone in maize raw material comprises:

Make described maize raw material with water from being positioned at high-order upstream towards the downstream flow that is positioned at low level, and described sandstone are sunk in flow process, the density of described corn grain is less than the density of described sandstone;

The described sandstone that restriction is sunk continue to flow with water;

The treatment process of described gluten water comprises gluten water concentrated, described the concentrated method of gluten water is comprised:

(1) gluten water is carried out to once concentration, obtain the first concentrated phase and the first water, in the first water that the condition of once concentration makes to obtain, the content of insoluble protein is less than 0.3 % by weight;

(2) the first concentrated phase is carried out to secondary concentration, obtain the second concentrated phase and the second water, in the second concentrated phase that the condition of secondary concentration makes to obtain, the content of insoluble protein is more than 10 % by weight;

(3) the second water is mixed with flocculant solution, and carry out dissolved air flotation; Described flocculation agent is for making the material of the flocculation of insoluble protein in the second water and/or sedimentation;

The method of the described concentrated corn steep liquor obtaining comprises evaporates corn steep liquor, the method of described evaporation comprises that employing falling-film evaporator is concentrated into 40-45 % by weight by corn steep liquor, and adopts scrapper thin film evaporator that the corn steep liquor of the 40-45 % by weight obtaining is concentrated into 48-52 % by weight.

First, in W-Gum technique, the present inventor adopts wet method proportion separation principle to carry out pre-treatment to maize raw material, and when the maize raw material that contains corn grain and sandstone being mixed with water and flow, sandstone sink in flow process.Due to described maize raw material with water from being positioned at high-order upstream towards the downstream flow that is positioned at low level, thereby with the increase of the distance that flows, 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 flow or compare with sandstone at least with the longer distance of water flow with water in flow process.And as mentioned above, along with the increase of the distance that flows, subsidence position is lower, thereby has further delayed the sinking of corn grain.Therefore, use method of the present invention can facilitate, continuously corn grain carried out to dedusting and remove stone and process, and simple to operate, do not need with complicated equipment and can carry out continuous operation.

Secondly, the present inventor also finds, the W-Gum preparation technology who adopts prior art to gluten water again utilize centrifugation method deficiency so that insoluble protein fully separate, separation efficiency is lower, the content of the insoluble protein in the enriched material therefore obtaining is not high, cause the productive rate of gluten protein powder not high, in addition, in the process water obtaining after concentrated, also contain a large amount of insoluble proteins, if directly process water direct circulation is back to use to technique for soaking corn, because the protein content in process water is higher, therefore cannot fully the soluble protein in corn be soaked out and dissolve in water, and affect follow-up separating technology, equally, the process water direct circulation that prior art obtains is back to use plumule, after in fibre washing technique, also cannot be fully by plumule, soluble substance in fiber fully washs out, and can affect the quality of product.Adopting method of the present invention, first gluten water is carried out to once concentration, in the first water that control obtains, the content of insoluble protein is lower, then, the first concentrated phase is carried out to secondary concentration, and the content of controlling insoluble protein in the second concentrated phase obtaining is higher, thereby realizes effective separation of insoluble protein, by after the insoluble protein separation in this second concentrated phase dehydrating, reach the object of the productive rate that greatly improves gluten protein powder.In addition, in the first water that control obtains, the content of insoluble protein is lower, can make water reach the specification of quality of direct reuse,, by described water again reuse circulation corn is soaked and plumule, fiber is washed, can substantially reach and soak and the effect of washing with fresh water, and having significantly improved the quality of smart starch milk.Made up the technique that the method for prior art processes gluten water deficiency so that insoluble protein can fully separate.

Moreover the present inventor finds again, although conventionally adopt multiple-effect falling film vaporizer to concentrate corn steep liquor in prior art, owing to being subject to all restrictions, concentrated corn steep liquor concentration generally can only reach 40-45 % by weight left and right.In addition, scrapper thin film evaporator is because reasons in structure own can not be manufactured too greatly, so its steam capability is limited, and prior art does not adopt scrapper thin film evaporator to concentrate corn steep liquor conventionally yet.And the present inventor is surprised to find that, adopt scrapper thin film evaporator and falling-film evaporator to form multi-effect evaporation system, first adopt falling-film evaporator that corn steep liquor is concentrated into 40-45 % by weight, then utilizing scrapper thin film evaporator as high density concentrating unit, can be further that the corn steep liquor of 40-45 % by weight is concentrated into 48-52 % by weight by concentration.Avoided on the one hand when adopting falling-film evaporator to concentrate corn steep liquor, the dense corn steep liquor of excessive concentration is due to the problem of the heating tube of viscosity great Yi obstruction falling-film evaporator, and utilized dexterously the feature of scrapper thin film evaporator, as, what scrapper thin film evaporator adopted is chuck heating, there is not obstructing problem, and can utilize the scraper plate in scrapper thin film evaporator to carry out action of forced stirring, thereby the concentration of corn steep liquor can be increased to applicable concentrated concentration (48-52 % by weight), and obtain the corn steep liquor concentrated solution that concentration is higher.In the corn steep liquor concentrated solution of the high density that the present invention obtains, water-content reduces, and therefore, can greatly reduce the energy consumption of follow-up highly energy-consuming dehumidification system.In addition, the high density corn steep liquor that the present invention obtains is because drop temperature is high, and mobility is better, and available pipe is transported to follow-up drying plant and sprays in time in fiber dry.

After the above-mentioned steps in W-Gum preparation technology is improved and is combined, can realize well the serialization of W-Gum and produce, effectively improved the production efficiency of W-Gum.

Other features and advantages of the present invention partly in detail are described the embodiment subsequently.

Accompanying drawing explanation

Accompanying drawing is to be used to provide a further understanding of the present invention, and forms a part for specification sheets, is used from explanation the present invention, but is not construed as limiting the invention with the specific embodiment of the present invention one.In the accompanying drawings:

Fig. 1 is the schematic top plan view of structure of implementing a kind of embodiment except stone cistern of method of removing the sandstone in maize raw material provided by the invention;

Fig. 2 is the schematic diagram of structure of a kind of embodiment of method of removing the sandstone in maize raw material of the present invention;

Fig. 3 is used the embodiment of Fig. 2 to carry out the schematic diagram of processing except sandstone in a large number;

Fig. 4 is the structural representation of the another kind of embodiment of method of removing the sandstone in maize raw material of the present invention;

Fig. 5 is used the embodiment of Fig. 4 to carry out the schematic diagram of processing except sandstone in a large number;

Fig. 6 adopts multi-effect evaporation system to carry out concentrated schema to corn steep liquor in the preparation method of W-Gum provided by the invention.

Description of reference numerals

10: except stone cistern

11: sidewall 12: diapire 13: entrance 14: outlet 15: plate washer 20: fluid mixture 21: corn grain 22: rubble.

Embodiment

Below in conjunction with accompanying drawing, the specific embodiment of the present invention is elaborated.Should be understood that, embodiment described herein only, for description and interpretation the present invention, is not limited to the present invention.

According to the preparation method of W-Gum provided by the invention, wherein, described method of removing the sandstone in maize raw material comprises: make described maize raw material with water from being positioned at high-order upstream towards the downstream flow that is positioned at low level, and described sandstone are sunk in flow process, the density of described corn grain is less than the density of described sandstone; The described sandstone that restriction is sunk continue to flow with water.

Preferably, the described sandstone 22 that described restriction is sunk continue mobile method with water and comprise along the flow direction of water a plurality of obstacles are set, and the described sandstone 22 that described restriction of obstacle sinks continue to flow with water.

The present invention is not particularly limited the consumption of water, as long as can form the fluid with mobility after mixing with the maize raw material that contains corn grain and sandstone.For example, can make maize raw material with water flow, thereby form the fluid with mobility.But this mode is unfavorable for controlling the ratio of maize raw material and water, make the fluid mobility of formation inconsistent.Preferably, can make maize raw material and water first be mixed to form uniform fluid mixture 20 (for example, by stirring), then make fluid mixture 20 flow and separated sandstone.Wherein, the consumption of water and churning time are not particularly limited, as long as can obtain the good fluid mixture 20 of mobility.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.

The following describes and adopt method of the present invention to carry out pre-treatment to remove the concrete operations of the sandstone in maize raw material to maize raw material.

Can implement method of the present invention with suitable equipment or device.In the preferred embodiment of the present invention, as shown in Figures 1 to 5, can use except stone cistern 10 enforcement method of the present invention.The stone cistern 10 that removes of the present invention comprises two relative sidewalls 11, diapire 12 between these two sidewalls, and the entrance 13 and the outlet 14 that are separately positioned on the cell body two ends between described two sidewalls 11, the height of at least a portion of the diapire 12 from described entrance 13 to described outlet 14 reduces gradually, described in this at least a portion, on diapire 12, is being provided with obstacle.In other words, entrance 13 and outlet 14 are respectively as the upstream and downstream of current, and current can rely on deadweight to flow to outlet 14 from entrance 13.

When fluid mixture 20 from entrance 13 when outlet 14 is flowed, because the density of sandstone 22 is much larger than water and be greater than the density of corn grain 21, thereby sandstone 22 can sink on diapire 12 in flow process.By restriction, sink to the sandstone 22 on diapire 12, it cannot be continued with water flow on diapire 12, thereby sandstone 22 can be limited in except in stone cistern 10.Although the density of corn grain 21 is also greater than the density of water, compare sandstone 22, it is slowly a lot of that the sinking velocity of corn grain 21 is wanted, thereby the longer distance that can flow before sinking to diapire 12.Because diapire 12 reduces to outlet 14 height with respect to the horizontal plane gradually from entrance 13, thereby increased gradually the distance that sinks to diapire 12, thereby can make corn grain 21 with the longer distance of water flow.In addition, even if corn grain 21 sinks on diapire 12, because its density is 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 flow.Therefore, can be easily, separating corn grain 21 and sandstone 22 continuously.

In the present invention, described maize raw material can be realized by variety of way towards the downstream flow that is positioned at low level from being positioned at high-order upstream with water.Below by two kinds of embodiments, described in detail.

In a kind of preferred implementation of the present invention, can make described maize raw material with water along the hillslope overland flow under being tilted to, described a plurality of obstacles be arranged on described domatic on.Particularly, as shown in Figures 2 and 3, except in stone cistern 10, can make diapire 12 described at least a portion for downward-sloping domatic.

As mentioned above, for fear of the sandstone 22 that sink, pile up and also " cross " obstacle, preferably, described obstacle is a plurality of and is spaced along the direction from described entrance 13 to described outlet 14.By this layout, can prevent that sandstone 22 from " crossing " obstacle because of accumulation.In other words, even if 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 continuously sandstone after the processing scheduled time, namely, when a large amount of sandstone 22 have all been piled up at each obstacle place, need to stop processing and clearing up except sandstone, and then start to process except sandstone.In addition, the dust in sandstone 22 causes sinking velocity different because density is different with rubble, thereby can on the different positions of diapire 12, sink.Therefore, the structure of present embodiment can also stop the sandstone 22 on the different positions that sinks to diapire 12.

Preferably, described domatic inclination angle (inclination angle with respect to the horizontal plane) is 7-10 degree, and domatic by this slow inclination can guarantee that sandstone 22 all sank to diapire 12 flow to outlet 14 from entrance 13 at current before substantially.

When the treatment capacity of mixture fluid 20 is less, as shown in Figure 2, liquid level will be parallel to domatic.

When the treatment capacity of mixture fluid 20 is larger, as shown in Figure 3, liquid level will be parallel to horizontal plane, and in this case, the pressure difference between entrance 13 and outlet 14 will be strengthened flowing of fluid.

Preferably, described obstacle, perpendicular to described domatic, stops to make full use of the height of obstacle.

In addition, can make the height of described outlet 14 higher than the height of the obstacle adjacent with described outlet 14, thereby the height of utilization outlet 14 stop the sandstone 22 of possibility " crossing " last obstacle.

In addition, due to the increase along with the distance that flows, 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 reduces the quantity of obstacle when guaranteeing except sandstone operation, thereby reduces the cost except sandstone operation.

In another embodiment of the invention, can make described maize raw material with water along downward a plurality of step-flow successively, a described obstacle is all set on each step.Particularly, as shown in Figure 4 and Figure 5, except in stone cistern 10, diapire 12 is downward successively a plurality of steps described in this at least a portion that can make to reduce highly gradually.

In ledge structure, horizontal component is called tread portion, and vertical component is called kickplate portion.Wherein, the edge being connected with upwardly extending adjacent kickplate portion of tread portion is called in conjunction with limit, and the edge with being combined to the adjacent kickplate portion of downward-extension of tread portion is called to free edge.

Preferably, as shown in Figure 4, described obstacle is arranged on the free edge of tread portion of described ledge structure, thereby makes full use of the sandstone 22 that tread portion is held sinking.

In addition, preferably, described obstacle, perpendicular to the plane at described tread portion place, stops to make full use of the height of obstacle.

In addition, preferably, the height of described obstacle is 1 with the ratio of the height of described: 1-1: 3, thereby collect appropriate current in the tread portion of each step, flow continuing.

In this embodiment of the present invention, when the treatment capacity of mixture fluid 20 is less, as shown in Figure 4, corn grain 21 with current from entrance 13 towards outlet 14 mobile processes, 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 larger, as shown in Figure 5, will forms complete and be parallel to the liquid level of horizontal plane.In this case, the difference of altitude between entrance 13 and outlet 14 will be strengthened flowing of fluid.

In the present invention, obstacle can be various suitable structures, as long as can play, stops or limits the sandstone 22 that sink on diapire 12 and continue to flow with water.In the preferred embodiment of the present invention, as shown in Figures 2 to 5, described obstacle is plate washer 15.Plate washer 15 can be made by the material with suitable intensity, as long as can resist water impact, stops sandstone 22, for example, can be steel plate, slabstone or plastic plate.

Preferably, can make the edge at the top of described plate washer 15 there is fillet, thus be convenient to make the corn grain 21 that sinks 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 to occur when crossing, thus keep the complete of corn grain 21.

In addition, preferably, the height of described plate washer 15 is 15-50cm, thus the corn grain 21 sinking current wash away with wave action under float corresponding height and can realize and crossing.This highly can be according to the factor designs such as speed of the size of corn kernel 21 and current.

Streamwise (from entrance 13 to outlet 14), the sandstone 22 of " crossing " due to the sandstone 22 that carry in current with because of accumulation fewer and feweri, therefore, can make the height streamwise of described plate washer 15 reduce gradually.This structure can apply rational resistance at different positions to current by the plate washer 15 of different heights.In other words, in the position near entrance 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 larger resistance by 15 pairs of current of plate washer on the other hand, thereby make the current at this place produce larger fluctuation, to assist the corn grain 21 sinking float and cross.Near outlet 14 position, because sandstone 22 are less, use lower plate washer 15 just can stop sandstone 22, simultaneously because of having reduced the resistance to current, thereby can improve current and carry corn kernel 21 towards exporting 14 mobile speed and flows.

Herein, the height of obstacle or plate washer 15 all refers to that the top of obstacle or plate washer 15 is to the distance of diapire 12.At diapire described in described at least a portion 12 while being domatic, the height of obstacle or plate washer 15 is that the top of obstacle or plate washer 15 is to domatic distance; When diapire described in described at least a portion 12 is downward a plurality of step, the height of obstacle or plate washer 15 is that the top of obstacle or plate washer 15 is to the distance that the tread portion place plane of this obstacle or plate washer 15 is set.

According to the preparation method of W-Gum provided by the invention, wherein, the treatment process of described gluten water comprises gluten water concentrated, described the concentrated method of gluten water is comprised:

(2) the first concentrated phase is carried out to secondary concentration, obtain the second concentrated phase and the second water, in the second concentrated phase that the condition of secondary concentration makes to obtain, the content of insoluble protein is more than 10 % by weight.

(3) the second water is mixed with flocculant solution, and carry out dissolved air flotation; Described flocculation agent is for making the material of the flocculation of insoluble protein in the second water and/or sedimentation.

The present inventor finds, compare with the method that obtains enriched material and process water after the once concentration of prior art, when gluten water is carried out to once concentration, in the first water that control obtains, the content of proteinaceous solid substance is less than 0.3 % by weight, be preferably 0.1-0.3 % by weight, can first guarantee only to contain in the first water a small amount of proteinaceous solid substance, then, when the first concentrated phase obtaining after once concentration is carried out to secondary concentration, in the second concentrated phase that control obtains, the content of proteinaceous solid substance is more than 10 % by weight, be preferably 10-12 % by weight, in the second concentrated phase that has guaranteed again to obtain, contain a large amount of proteinaceous solid substances, that is to say, after adopting method of the present invention to concentrate gluten water, quality can be obtained simultaneously higher, the content of proteinaceous solid substance is less can direct reuse water, and without again the water obtaining being carried out to subsequent disposal, obtain directly carrying out the higher concentrated phase of proteinaceous solid content prepared by next step gluten protein powder simultaneously.

According to the present invention, in the first water that control obtains, the content of proteinaceous solid substance is less than 0.3 % by weight, be preferably 0.1-0.3 % by weight, the concentration ratio of first concentrated phase that can obtain when controlling once concentration, the concentration ratio of described the first concentrated phase is the feed volume of once concentration gluten water and the ratio of the first concentrated phase volume; In the first concentrated phase, the concentration of proteinaceous solid substance is lower, so can guarantee low percentages of protein in the first water, and therefore, under preferable case, the concentration ratio of the first concentrated phase can be 2-3: 1, and 2.3-2.8 more preferably: 1.Vice versa, in the second concentrated phase that control obtains, the content of proteinaceous solid substance is more than 10 % by weight, be preferably 10-12 % by weight, the concentration ratio of second concentrated phase that can obtain when controlling secondary concentration, the feed volume of described secondary concentration the first concentrated phase and the ratio of the second concentrated phase volume; In the second water, the concentration of proteinaceous solid substance is higher, can guarantee that in the second concentrated phase, protein content is higher, and therefore, under preferable case, the concentration ratio of the second concentrated phase can be 3-4: 1, and 3.3-3.7 more preferably: 1.

According to the present invention, the method that gluten water is concentrated can for example, be utilized to the principle of centrifugation for various concentrated modes well known in the art, adopt separating machine that gluten water is concentrated, enriched material flows out from underflow, and process water flows out from top stream.Therefore, the method for the invention preferably adopts the method for centrifugation to carry out described once concentration and described secondary concentration.

According to the present invention, concentrated condition generally comprises the rotating speed of centrifugation and the temperature of feed rate and centrifugation etc., the adjustable extent of above-mentioned condition is all wider, also be, the condition of once concentration is as long as guarantee proteinaceous solid content in the first water, and preferably the condition of once concentration makes the concentration ratio of the first concentrated phase in the preferred scope of the present invention; Meanwhile, the condition of secondary concentration is as long as guarantee the content of proteinaceous solid substance in the second concentrated phase, and preferably the condition of secondary concentration makes the concentration ratio of the second concentrated phase in the preferred scope of the present invention.Because size, the diameter of different centrifugal separation equipments are different, rotating speed is also just different, therefore, can select according to the actual needs suitable equipment, and its rotating speed has also been determined with regard to corresponding, also just can have been selected according to actual needs suitable inlet amount simultaneously.The temperature of centrifugation can be generally 35-45 ℃.

The present inventor finds, flocculation agent is mixed with the second water with the form of flocculant solution, and what can make it to mix with the second water is more even, proteinaceous solid substance in this second water is flocculated and/or sedimentation more abundant, complete.

According to the present invention, the solvent in described flocculant solution can be variously can form the solvent of solution with flocculation agent, and generally, the solvent in described flocculant solution is water.Described flocculation agent can be various can be by the flocculation of proteinaceous solid substance, sedimentation in the second water, and make its flocculation agent effectively separated from the second water, under preferable case, described flocculation agent can be polyacrylic acid and/or sodium polyacrylate and polymerize aluminum chloride, also, the aqueous solution of described flocculation agent is the aqueous solution of polyacrylic acid and/or sodium polyacrylate and the aqueous solution of polymerize aluminum chloride.

More preferably in situation, described polyacrylic number-average molecular weight can be 6,000,000-1,000 ten thousand dalton, and the number-average molecular weight of described sodium polyacrylate can be 6,000,000-1,000 ten thousand dalton.Described polymerize aluminum chloride 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%.

The present inventor finds, polymerize aluminum chloride more easily makes the fine particle thing in described the second water be gathered in it and forms the suspended substance of larger particles around, and polyacrylic acid and/or sodium polyacrylate more easily make the suspended substance sedimentation of larger particles, therefore, in the ban by after the aqueous solution of the second water and polymerize aluminum chloride, with the aqueous solution of the polyacrylic aqueous solution and/or sodium polyacrylate, can play better separating effect again.In addition, the present inventor also finds, when the weight ratio of polymerize aluminum chloride and polyacrylic acid and/or sodium polyacrylate in this flocculant solution is controlled to 2-5, 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 separating effect is better.

Under preferable case, after by the aqueous solution of the second water and polymerize aluminum chloride, before the aqueous solution of the polyacrylic aqueous solution and/or sodium polyacrylate, the step that also comprises stirring, fully to make the gathering of the fine particle thing in polymerize aluminum chloride and the second water more thorough, in order to be beneficial to the polymerize aluminum chloride fine particle thing that fully flocculates, can not destroy again the particulate matter of having flocculated, destroy, the time of described stirring is preferably 0.5-5 minute simultaneously.

In the present invention, the solubleness of flocculation agent in water is moderate, therefore, the adjustable extent of the mass body volume concentrations of described flocculant solution is wider, as, can be for 0.1-5% (m/v), for considering of cost and effect, the mass body volume concentrations of the aqueous solution of the described polyacrylic aqueous solution and sodium polyacrylate is preferably 0.1-0.5% (m/v), and the mass body volume concentrations of the aqueous solution of described polymerize aluminum chloride is preferably 1-5% (m/v).

According to method of the present invention, the adjustable extent of the consumption of described flocculant solution is wider, for example, can regulate according to the number of the amount of insoluble protein in the second water the consumption of flocculant solution, under preferable case, every cubic metre of second water of take is benchmark, it is 5-100ppm that the consumption of described flocculant solution makes the amount of flocculation agent, more preferably in situation, it is 5-50ppm that the consumption of described flocculant solution makes the amount of poly acryloyl acid and sodium polyacrylate flocculation agent, and the amount that makes flocculant of polymeric aluminium chloride is 20-100ppm.

If flocculation agent used is poly acryloyl acid, to make the amount of poly acryloyl acid flocculation agent be 5-50ppm to the consumption of described flocculant solution, if flocculation agent used is sodium polyacrylate, to make the amount of sodium polyacrylate flocculation agent be 5-50ppm to the consumption of described flocculant solution, if flocculation agent used is poly acryloyl acid and sodium polyacrylate, to make the total amount of poly acryloyl acid and sodium polyacrylate flocculation agent be 5-50ppm to the consumption of described flocculant solution.

Above-mentioned m/v refers to mass body volume concentrations, and concrete meaning comprises the quality of flocculation agent in every liter of flocculant solution.

According to the present invention, the condition that the first water is mixed with flocculant solution can comprise the time of mixing and the temperature of mixing, and for example, the time of described mixing can be 1-10 minute, more preferably 1-5 minute; The temperature of described mixing can be 30-70 ℃, more preferably 40-60 ℃.More even for what the second water was mixed with flocculant solution, described the second water and mixing preferably of flocculant solution are under agitation carried out.

According to the present invention, the mode that the second water is mixed with flocculant solution is not particularly limited, and for example, can be static mixing, can be also dynamic mixing, also or the combination of two kinds of hybrid modes.Wherein, described static mixing can be: by the second water and flocculant solution at container, as mixed in standing equipment and standing; Described dynamic mixing can be: the second water from different transport pipes and flocculant solution are converged in being incorporated in flow process and mixed in another transport pipe, or the second water and flocculant solution are mixed by line mixer, and by this mixture be delivered in standing equipment, carry out standing.

According to the present invention, the second water and flocculant solution are mixed and by the method being flocculated and/or the separated method of proteinaceous solid substance of sedimentation is dissolved air flotation.To be the micro-bubble that utilizes high dispersing go to adhere to as carrier the method for described dissolved air flotation in the second water, is flocculated and/or the proteinaceous solid particle of sedimentation, makes its density be less than water and float to the water surface, realizes the process of solid-liquid separation.According to the present invention, the method of described dissolved air flotation comprises when the second water is mixed with flocculant solution or afterwards, in mixture, blast air, make to be flocculated and/or bubble adhesion that the proteinaceous solid particle of sedimentation is formed with bubble floating.Wherein, as long as can will be flocculated and/or bubble adhesion that the proteinaceous solid particle of sedimentation is formed by the air by passing into bubble floating to the condition that passes into air in mixture, form air supporting layer, under preferable case, the pressure that passes into air can be 0.2-0.4 MPa, and the size of bubble can be 15-30 micron conventionally.Generally, the described 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, utilize the different suspensions of material with the principle of absorption bubble (gas molecule), proteinaceous solid particle is separated with water.For example, feed end by the mixture of the second water and flocculant solution by air flotation slot enters, air dissolved pump input gas electricity enters the feed end of air flotation slot, the gas that enters air flotation slot forms bubble diffusion by aeration head and plays in liquid, these bubbles adhere to the throw out and/or the sediment that enter air flotation zone, and upwards floating along with flowing, water is clarified gradually.The proteinaceous solid particle that swims in a large number upper strata gathers and is called the liquid that concentration is higher; then from air flotation slot discharge end, by stripper plate, peeled; and can filter; air flotation slot middle part be clarification water, the proteinaceous solid content of the second water after the processing obtaining according to method of the present invention can be for below 0.3 % by weight.

According to the present invention, the method for the proteinaceous solid substance in separated the second concentrated phase can adopt ordinary method known in those skilled in the art, for example, can be carried out solid-liquid separation or directly be carried out filtering separation by whizzer.Its concrete operation method and condition are conventionally known to one of skill in the art, here repeat no more.For example, in the specific embodiment of the present invention, can adopt vacuum-type drum filter or plate-and-frame filter press to filter, the condition of filtration comprises sheet frame veneer model 125cm * 125cm, sheet frame maximum working pressure (MWP) 0.4Mpa, veneer filter-cloth filtering area is generally 1.5 square metres, 758 model filter clothes.

According to the present invention, the method also comprises the step that isolated proteinaceous solid substance dehydrates from the second concentrated phase and/or the second water.

The described method dehydrating and condition all can adopt method well known in the art and condition to carry out.For example, dry mode can be seasoning, forced air drying, the drying mode of the various routines such as vacuum-drying.Described dry 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, described gluten water refers to Corn Crude starch milk to carry out the light water that contains mutually proteinaceous solid substance obtaining after separation.

According to the preparation method of W-Gum provided by the invention, wherein, the method of the concentrated corn steep liquor obtaining comprises evaporates corn steep liquor, the method of described evaporation comprises that employing falling-film evaporator is concentrated into 40-45 % by weight by corn steep liquor soak solution, and adopts scrapper thin film evaporator that the corn steep liquor of the 40-45 % by weight obtaining is concentrated into 48-52 % by weight; Under preferable case, adopt falling-film evaporator that corn steep liquor soak solution is concentrated into 40-42 % by weight, and adopt scrapper thin film evaporator that the corn steep liquor of the 40-42 % by weight obtaining is concentrated into 48-50 % by weight.

According to the present invention, as long as it is 40-45 % by weight that the method for described evaporation guarantees to make the concentration of the corn steep liquor that obtains after adopting falling-film evaporator that described corn steep liquor soak solution is concentrated, be preferably 40-42 % by weight, and guarantee adopting scrapper thin film evaporator by the 40-45 % by weight obtaining, after the corn steep liquor that is preferably 40-42 % by weight concentrates, making the concentration of the concentrated corn steep liquor that obtains is 48-52 % by weight, is preferably 48-50 % by weight.

Under preferable case, the present inventor adopts scrapper thin film evaporator and falling-film evaporator to form multi-effect evaporation system, and described corn steep liquor is carried out to multiple-effect evaporation.Wherein, described multiple-effect evaporation refers to the evaporation operation of several evaporator series operations, and steam thermal energy is repeatedly utilized, thereby improves the utilization ratio of heat energy.

The present inventor's discovery, employing falling-film evaporator can be imitated the concentrated evaporation effect number of corn steep liquor for 3-4, and adopting film-falling scraping plate vaporizer is 1-2 effect by evaporate the further concentrated evaporation effect number of corn steep liquor obtaining through falling-film evaporator; Under preferable case, can adopt falling-film evaporator that corn steep liquor soak solution is carried out to triple effect evaporation, make the concentration of the corn steep liquor that obtains reach 40-45 % by weight, be preferably 40-42 % by weight, then adopt an effect scrapper thin film evaporator by the 40-45 % by weight obtaining, after the corn steep liquor that is preferably 40-42 % by weight concentrates, making the concentration of the concentrated corn steep liquor that obtains is 48-52 % by weight, is preferably 48-50 % by weight.

According to a kind of embodiment of the present invention, can adopt the method for quadruple effect evaporation to concentrate corn steep liquor,, as shown in Figure 6, the first effect scrapper thin film evaporator is connected with the second effect falling-film evaporator, the second effect falling-film evaporator is connected with triple effect falling-film evaporator, and triple effect falling-film evaporator is connected with quadruple effect falling-film evaporator.The method of described evaporation comprises corn steep liquor (IV is imitated charging) is pumped in quadruple effect falling-film evaporator, under the Heating temperature of 65-75 ℃, this corn steep liquor is carried out to circulating-heating evaporation, obtaining concentration is the quadruple effect corn steep liquor feed liquid of 7-10 % by weight and four effect juice steams of 50-55 ℃, and this quadruple effect corn steep liquor feed liquid (IV is imitated feed liquid) is pumped in the second effect falling-film evaporator, under the Heating temperature of 98-105 ℃, this quadruple effect corn steep liquor feed liquid is carried out to circulating-heating evaporation, and obtaining concentration is two effect corn steep liquor feed liquids of 18-20 % by weight and two effect juice steams of 85-90 ℃; This two effect corn steep liquor feed liquid (II is imitated feed liquid) is pumped in triple effect falling-film evaporator, under the Heating temperature of 85-90 ℃, this two effects corn steep liquor feed liquid is carried out to circulating-heating evaporation, and obtaining concentration is the triple effect corn steep liquor feed liquid of 40-45 % by weight and three effect juice steams of 65-75 ℃; This triple effect corn steep liquor feed liquid (III is imitated feed liquid) is pumped in an effect scrapper thin film evaporator, under the Heating temperature of 120-130 ℃, this triple effect corn steep liquor feed liquid is evaporated, and obtaining concentration is the concentrated corn steep liquor (I is imitated discharging) of 48-52 % by weight and an effect juice steam of 98-110 ℃.

According to the present invention, vacuum tightness when above-mentioned quadruple effect, triple effect, the second effect and the first effect are evaporated is corresponding one by one with the thermodynamic principles of the vaporization temperature foundation of each effect, for the ease of observing operation, under preferable case, the vacuum tightness of evaporating in quadruple effect falling-film evaporator can be 0.08MPa to 0.09MPa, more preferably 0.084MPa to 0.088MPa; The vacuum tightness of evaporating in triple effect falling-film evaporator can be 0.06MPa to 0.075MPa, the vacuum tightness of evaporating in the second effect falling-film evaporator can be 0.03MPa to 0.04MPa, the pressure evaporating in the first effect scrapper thin film evaporator can be 0.01MPa to 0.05MPa, more preferably 0.01MPa-0.046MPa.Wherein, described vacuum tightness refers to the rare book degree of gas under vacuum state.If the pressure in institute's measurement equipment is lower than atmospheric pressure, its pressure survey needs vacuum meter.The numerical value of reading from vacuum meter claims vacuum tightness.Vacuum values means out that system pressure actual numerical value is lower than the numerical value of atmospheric pressure, that is: vacuum tightness=(atmospheric pressure-pounds per square inch absolute (psia)).

In order to reduce the consumption of raw steam, under preferable case, for the heating steam of the second effect falling-film evaporator, come from an effect juice steam or be an effect juice steam and the mixing steam of raw steam; Heating steam for triple effect falling-film evaporator comes from two effect juice steams; Heating steam for quadruple effect falling-film evaporator comes from three effect juice steams; Heating steam for the first effect scrapper thin film evaporator comes from raw steam.Four effect juice steams can be undertaken with water coolant cooling conventionally by condenser, and are connected with vacuum system.

That is, in the flow process of above-mentioned quadruple effect evaporation operation, the first effect scrapper thin film evaporator is usingd and is given birth to steam as heating steam, and the second effect to quadruple effect falling-film evaporator is all usingd the heating steam as this effect of juice vapour (being secondary steam) that its last effect produces.Especially, if the effect juice steam that the first effect scrapper thin film evaporator produces can not meet the heat request that adds of the second effect falling-film evaporator, can supplement raw steam and to produce enough juice vapour, meet it and add heat request.Can guarantee that like this multi-effect evaporation system has enough steam capabilitys, and heating steam can repeatedly utilize, thereby can significantly reduce the consumption of raw steam.

Wherein, the flow direction of the corn steep liquor concentrated solution that heating steam and corn steep liquor or each effect obtains can for and flow process, countercurrent flow, can be also cross-flow flow process, be preferably cross-flow flow process.

Under preferable case, in order to make the steam capability of falling-film evaporator maximum, before the method is also included in quadruple effect corn syrup liquid pump is entered in the second effect falling-film evaporator, quadruple effect corn steep liquor feed liquid is preheated to the vaporization temperature that approaches two effects, that is, after being preheated to 85-90 ℃, quadruple effect corn steep liquor feed liquid can carry out immediately evaporating in the second effect falling-film evaporator.According to the present invention, describedly can adopt the various heat-exchange equipments of this area routine to heat the method for corn steep liquor preheating, under preferable case, can adopt tubular heat exchange to heat, and described preheating can come from two effect juice steams at least partly with heating steam.

According to the present invention, described falling-film evaporator and scrapper thin film evaporator are the conventional evaporation equipment in this area.The principle of work of described falling-film evaporator is: in vertical closed container, the shell side of heating tube bundle is heating steam, tube side is for being evaporated solution, solution is membranaceous landing by being pumped to container top distribution plate along tubulation inwall, and by external steam heating vaporization, in bottom, enter separate chamber and carry out vapor-liquid separation, due to vacuum action, juice vapour enters the shell side of rear single-effect evaporator, liquid is again pumped into container top and is heated, and circulation constantly.The principle of work of described scrapper thin film evaporator is: in the chuck of vertical closed container, be heating steam, container is interior for being evaporated solution, and adopt scraper plate action of forced stirring, make solution become membranaceous distribution at container inner wall, and vaporized by the steam heating in chuck, on container top, enter separate chamber and carry out vapor-liquid separation.

In the present invention, just the concentration method of the treatment process of raw materials pretreatment and gluten water and corn steep liquor is improved, and all can carry out according to the method for well known to a person skilled in the art for other step in W-Gum preparation technology and condition.

For example, according to the present invention, corn grain is soaked and can adopt method known in those skilled in the art, for example, at 50-55 ℃, the sulfurous acid aqueous solution that is 0.1-0.35 % by weight by corn particle and concentration contacts 40-52 hour, obtains corn steep liquor.With sulfurous acid soaking corn grain, can make its each integral part loose, weaken mutual contact, sulfurous acid can also destroy protein net, make the semipermeable partition of corn grain epidermis become permeable membrane, accelerate and promote to permeate and diffusion, make a large amount of water absorption and swellings of corn grain, softening, great amount of soluble protein dissolution, in soak solution, is conducive to further be processed into corn steep liquor.The difference of solid content in the corn steep liquor that different soaking conditionses may cause obtaining, generally, the solid content of described corn steep liquor is 5-8 % by weight.

According to the present invention, corn grain through soaking is taken off to 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), the corn grain that makes to enter degerming mill enters with the moving of double wedge under the effect of centrifugal force to be determined between tooth plate, because two dishes are for the relative rotation, and recessed tooth is interior and dredges outer closely on dish, and maize germ, scurf and endosperm are because physical property difference is by fragmentation in various degree, separated from one another.Different due to the relative density of plumule and rest part, under the effect of centrifugal force, free plumule is separated.

According to the present invention, the corn grain tissue that contains maize peel and endosperm after de-embryo is ground, isolating the method for fiber also can carry out according to the method for well known to a person skilled in the art, for example, utilize pin mill to grind, be subject to moving pin and fixed strong shock the in repeated multiple times ground of determining pin of high speed rotating, most starch and fiber get loose and dissociate out.Thickness slag ratio generally can arrive 2.5-3: 1.Although the starch after grinding has been unbound state, but still mix with fibrous residue, due to varying in size of several material particles, therefore, can utilize the screening plant in different sieve seams or aperture that fiber is separated in farinaceous size, in described farinaceous size, the size of starch granules is generally 5-30 micron, in fibrous residue, the granular size of fine-fibered is generally more than 65 microns, and robust fibre slag becomes larger sheet, and seitan granular size is generally 1-2 micron.Described 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 obtaining is carried out to separation and obtain rare seitan and starch milk, and the method that starch milk is washed can be carried out for method well known in the art.For example, the principle separated with seitan of the starch milk in coarse starch milk mainly utilize the relative density of these two kinds of materials and granular size different and carry out separation, for example, can adopt settling process or centrifuging to carry out separation.

It should be noted that in addition, each concrete technical characterictic described in above-mentioned embodiment, in reconcilable situation, can combine by any suitable mode, for fear of unnecessary repetition, the present invention is to the explanation no longer separately of various possible array modes.

In addition, between various embodiment of the present invention, also can carry out arbitrary combination, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.

To the present invention, be further described in detail by specific embodiment below, following examples are only for the present invention is described, but are not used for limiting the scope of the invention.

In following embodiment, adopt disc separator rare seitan is concentrated or carry out solid-liquid separation, concentrated phase flows out from underflow, and water flows out from top stream; The model of disc-type separating centrifuge used is DPF530.The model of air flotation slot is FXP300 * 5000, purchased from Wuhan Liang Ke institute.

In the process water obtaining after gluten water is concentrated, the measuring method of the concentration of insoluble protein is Oven Method.

The conventional falling-film evaporator in two effects, triple effect and quadruple effect falling-film evaporator used and this area in following embodiment, purchased from Yixing City,Grant dry and enrichment equipment Co., Ltd, model is JMZ-4.5, moisture steam capability is 4500kg/h; The scrapper thin film evaporator that an effect scrapper thin film evaporator used and this area are conventional, purchased from Wuxi City Xishan Xue Lang chemical industry equipment factory, model is LG-0.8, moisture steam capability is 160kg/h.

Embodiment 1

The present embodiment is for illustrating 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 described stone cistern 10 that removes comprises two relative sidewalls 11, diapire 12 between these two sidewalls, and the entrance 13 and the outlet 14 that are separately positioned on the cell body two ends between described two sidewalls 11, the height of the diapire 12 from described entrance 13 to described outlet 14 reduces gradually, domatic under being tilted to of described diapire 12, described domatic inclination angle (inclination angle with respect to the horizontal plane) is 10 degree, the length of the horizontal direction of diapire 12 is 5 meters, using 8 baffle plates as obstacle, be vertically set on described domatic on, the height of described plate washer reduces gradually along water flow direction, the height of each baffle plate is 25cm.Described obstacle is spaced along the direction from described entrance 13 to described outlet 14, along the flow direction of water, between adjacent two obstacles, is spaced apart 70cm.That is, entrance 13 and outlet 14 are respectively as the upstream and downstream of current, and current can rely on deadweight to flow to outlet 14 from entrance 13, and the height of described outlet 14 is higher than the height of the obstacle adjacent with described outlet 14.

Maize raw material (water content 14 % by weight) and water are mixed to get to fluid mixture (consumption of water is 3 times of maize raw material gross weight), from entrance 13, flow into except stone cistern, and flow 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 be greater than the density of corn grain 21, thereby sandstone 22 can sink on diapire 12 in flow process.By restriction, sink to the sandstone 22 on diapire 12, it cannot be continued with water flow on diapire 12, and baffle plate can further stop sandstone " to be crossed " forward, thereby sandstone 22 can be limited in except in stone cistern 10, from exporting 14 collections, remove the corn grain sandstone.

(2) soak

By being delivered to steeping tank by waterpower after corn metering after purification, with the sulfurous acid aqueous solution that concentration is 0.25 % by weight, carry out adverse current immersion.Soaking filling is 10, every tankage is 50 tons of maize raw materials after above-mentioned purification, the soak solution of steeping tank is by a pump part self circulation, a part with add corn to be countercurrent flow, the old acid soak of the corn newly adding, soak the new acid soak of corn at most, 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 to multiple-effect evaporator, the first effect scrapper thin film evaporator is connected with the second effect falling-film evaporator, the second effect falling-film evaporator is connected with triple effect falling-film evaporator, and triple effect falling-film evaporator is connected with quadruple effect falling-film evaporator.

By 50 ℃ of corn steep liquors extracting out in steeping tank, (every tank approximately goes out 30m ³, dry matter content is 7 % by weight), pump in the quadruple effect falling-film evaporator in described multi-effect evaporation system that (controlling corn soaking flow quantity is 6m ³/ h), under the vacuum tightness of the Heating temperatures of 70 ℃, 0.068MPa, described corn steep liquor is carried out to circulating-heating evaporation, obtaining concentration is the quadruple effect corn steep liquor feed liquid of 9 % by weight and four effect juice steams of 52 ℃, this four effect juice steam is connected with vacuum pump by pipe bundle condenser, and (controlling feed liquid flow is 5-6m by the extraction of quadruple effect corn steep liquor feed liquid ³/ h) and after being preheated to 85 ℃, pump in the second effect falling-film evaporator, under the vacuum tightness of the Heating temperatures of 103 ℃, 0.015MPa, described quadruple effect corn steep liquor feed liquid is carried out to circulating-heating evaporation, obtain concentration and be two effect corn steep liquor feed liquids of 20 % by weight and two effect juice steams of 88 ℃ (part two effect juice gas can for preheating quadruple effect corn steep liquor feed liquid); Then described two effect corn syrup liquid pumps are entered in triple effect falling-film evaporator, (controlling feed liquid flow is 2-3m ³/ h), under the vacuum tightness of the Heating temperatures of 88 ℃, 0.034MPa, adopt the juice vapour of two effects to carry out circulating-heating evaporation to described two effect corn steep liquor feed liquids, obtaining output is that 1000kg/h, concentration are the triple effect corn steep liquor feed liquid of 42 % by weight left and right and three effect juice steams of 70 ℃, and three effect juice steams are re-used as the thermal source of quadruple effect falling-film evaporator; The triple effect corn syrup liquid pump that is 42 % by weight left and right by described 1000kg/h, concentration enters in the first effect scrapper thin film evaporator, and adopt the raw steam of 125 ℃, under the pressure of 0.24MPa, described triple effect corn steep liquor feed liquid is carried out to heating evaporation, and obtaining output is that 840kg/h, concentration are the concentrated corn steep liquor of 50 % by weight left and right.

(4) de-embryo

Corn after soaking is entered to wet corn hopper by wet corn transferpump through rockover remover, enter again one-level degerming mill, corn is broken into 4-6 lobe, containing shaping corn amount, be no more than 1 % by weight, and separate the plumule of the 75-89 % by weight of plumule total amount, discharge the starch of the 20-25 % by weight of total starch content simultaneously;

Corn after fragmentation is pumped to plumule primary cyclone with plumule, the plumule that flow out at separator top removes washing system, underflow thing enters secondary degerming mill, corn is broken for 10-12 lobe, in this slurry, not containing whole kernel corn, the plumule in bonding state is no more than 0.3 % by weight, and the slurry of process secondary breaking is pumped into secondary plumule cyclone separator through plumule, top stream thing reenters one-level germ separation device, and underflow slurry enters fine grinding operation.

(5) fine grinding

The underflow grout of isolating after plumule through swirl flow separator passes through pressure curved sieve, and screen underflow is coarse starch milk; Screen overflow enters impact grinding (or pin mill) and carries out fine grinding, and free out with the free starch that makes to greatest extent itself and fiber connect, the condition of pin mill makes in the slurry after grinding, and connects starch and is not more than 10 % by weight.

Slurry after fine grinding enters fibre washing bath, at this, delivers to first step pressure curved sieve with together with the washing water of later washing the fibre.Screen underflow is isolated coarse starch milk, screen overflow is again through the countercurrent washing of the bent sieve of 6 stage pressures, washing process water adds from last step sieve, by compass screen surface, is carrying the free starch washing and is moving forward step by step, until in the front rinse bath of first step sieve, merge with the slurry after fine grinding, jointly enter first step pressure curved sieve, separate coarse starch milk, the screen underflow coarse starch milk that this starch milk and fine grinding fore worker separate converges, and enters starch separation circuit.Fiber on compass screen surface, skin slag and washing water are gone against the stream, and from the first sieve to each sieve is mobile later, after washing screening several times, from the bent sieve of last step, discharge, and then through screw extrusion press, dewater.

(6) starch milk is refining

From bent screening before and after fine grinding, from the thick starch obtaining, through sand separator, revolving filter, remove after impurity, enter elementary separating centrifuge (disc separator), the overflow substance that top stream is discharged is rare gluten water, and this rare gluten water is carried out to following processing:

1) press 350m ³the total flux of/h is on average sent into rare gluten water (concentration of proteinaceous solid substance is 1.7 % by weight) and in two disc separators, rare gluten water is carried out to once concentration simultaneously (total feed of rare gluten water is 350m ³/ h, each inlet amount is 175m ³/ h, the rotating speed of centrifugation is respectively 3400 revs/min, the temperature of centrifugation is 45 ℃), the total flux that obtains the first water is 200m ³the total flux of/h (in the first water, the content of proteinaceous solid substance is 0.3 % by weight) and the first concentrated phase is 150m ³(the concentrated phase flow of each separating machine is respectively 75m to/h ³/ h) (in the first concentrated phase, proteinaceous solid content is 3.8 % by weight); The first concentrated phase is again sent into and in a disc separator, carried out secondary concentration (feed rate of the first concentrated phase is 150m ³/ h, the rotating speed of centrifugation is 3500 revs/min, the temperature of centrifugation is 45 ℃), obtaining the second water flow is 106m ³/ h and the second concentrated phase flow are 44m ³/ h (in the second concentrated phase, proteinaceous solid content is 12.1 % by weight);

2) by step 1) the second concentrated phase of obtaining inserts in flame filter press and filters, and obtains filter cake (moisture 50 % by weight); The filter cake obtaining is obtained to feed (moisture content 10 % by weight) 120 ℃ of oven dry, and the protein content that the butt instrumentation of take obtains in feed is 62% (m/m);

3) the sodium polyacrylate flocculation agent that is 6,000,000 by number-average molecular weight is soluble in water, makes mass volume ratio concentration and be 0.05% solution; Polymerize aluminum chloride (n is 1-5, m≤10, basicity B=n/6 * 100%) is soluble in water, make mass volume ratio concentration and be 5% polymeric aluminum chlorides solution.And at 60 ℃, in the second water obtaining to step (1), add above-mentioned two kinds of flocculant aqueous solutions, every cubic metre of second water of take is benchmark, it is 12.5ppm that the consumption of described sodium polyacrylate flocculant aqueous solution (25L) makes the amount of sodium polyacrylate flocculation agent, it is 50ppm that the consumption of the described flocculant of polymeric aluminium chloride aqueous solution (1L) makes the amount of flocculant of polymeric aluminium chloride, is uniformly mixed 1 minute; And the mixed solution obtaining is inserted and in air flotation slot, carried out dissolved air flotation (pressure that passes into air is 0.3 MPa, the air supporting time is 5 minutes), the separated proteinaceous solid particle in upper strata is also inserted mixed solution in flame filter press and is filtered, in the water obtaining, the content of proteinaceous solid substance is 0.22 % by weight, the filter cake obtaining (water content is 50 % by weight) is obtained to feed (moisture content 10 % by weight) 120 ℃ of oven dry, and the protein content that the butt instrumentation of take obtains in feed is 62% (m/m).

The starch concentration obtaining from elementary separating centrifuge underflow is 19-20 ° of Be ', and moisture approximately 60 % by weight of purified starch breast after 12 grades of swirler washings, protein content is less than 0.35 % by weight, essence starch milk obtains the wet starch of moisture 38-40 % by weight after dehydration, and wet starch is sent into the dry commodity starch finished product that obtains of pneumatic drier.

Embodiment 2

Method according to embodiment 1 is prepared W-Gum, different, and in step (6), the treatment process of described rare gluten water comprises:

1) press 380m ³the total flux of/h is on average sent into rare gluten water (concentration of proteinaceous solid substance is 1.5 % by weight) and in two disc separators, rare gluten water is carried out to once concentration simultaneously (total feed of rare gluten water is 380m ³/ h, each inlet amount is 190m ³/ h, the rotating speed of centrifugation is respectively 3300 revs/min, the temperature of centrifugation is 45 ℃), the total flux that obtains the first water is 234m ³the total flux of/h (in the first water, the content of proteinaceous solid substance is 0.28 % by weight) and the first concentrated phase is 146m ³(the concentrated phase flow of each separating machine is respectively 73m to/h ³/ h) (in the first concentrated phase, proteinaceous solid content is 3.5 % by weight); The first concentrated phase is again sent into and in a disc separator, carried out secondary concentration (feed rate of the first concentrated phase is 146m ³/ h, the rotating speed of centrifugation is 3400 revs/min, the temperature of centrifugation is 45 ℃), obtaining the second water flow is 102m ³/ h and the second concentrated phase flow are 44m ³/ h (in the second concentrated phase, proteinaceous solid content is 11 % by weight);

2) the second concentrated phase step (1) being obtained is inserted in flame filter press and is filtered, and obtains filter cake (moisture 50 % by weight); The filter cake obtaining is obtained to feed (moisture content 10 % by weight) 120 ℃ of oven dry, and the protein content that the butt instrumentation of take obtains in feed is 60% (m/m);

According to step 3 in embodiment 1) method process the second water, in the water obtaining, the content of proteinaceous solid substance is 0.19 % by weight, the filter cake obtaining (water content is 50 % by weight) is obtained to protein fodder (moisture content 10 % by weight) 120 ℃ of oven dry, and the protein content that the butt instrumentation of take obtains in feed is 60% (m/m).

Embodiment 3

1) press 360m ³the total flux of/h is on average sent into rare gluten water (concentration of proteinaceous solid substance is 1.6 % by weight) and in two disc separators, rare gluten water is carried out to once concentration simultaneously (total feed of rare gluten water is 360m ³/ h, each inlet amount is 180m ³/ h, the rotating speed of centrifugation is respectively 3300 revs/min, the temperature of centrifugation is 45 ℃), the total flux that obtains the first water is 231m ³the total flux of/h (in the first water, the content of proteinaceous solid substance is 0.31 % by weight) and the first concentrated phase is 129m ³(the concentrated phase flow of each separating machine is respectively 64.5m to/h ³/ h) (in the first concentrated phase, the content of proteinaceous solid substance is 3.9 % by weight); The first concentrated phase is again sent into and in a disc separator, carried out secondary concentration (feed rate of the first concentrated phase is 129m ³/ h, the rotating speed of centrifugation is 3400 revs/min, the temperature of centrifugation is 45 ℃), obtaining the second water flow is 92m ³/ h and the second concentrated phase flow are 37m ³/ h (in the second concentrated phase, the content of proteinaceous solid substance is 12.3 % by weight);

2) the second concentrated phase step (1) being obtained is inserted in flame filter press and is filtered, and obtains filter cake (moisture 50 % by weight); The filter cake obtaining is obtained to feed (moisture content 10 % by weight) 120 ℃ of oven dry, and the protein content that the butt instrumentation of take obtains in feed is 61% (m/m);

According to step 3 in embodiment 1) method process the second water, in the water obtaining, the content of proteinaceous solid substance is 0.24 % by weight, the filter cake obtaining (water content is 50 % by weight) is obtained to protein fodder (moisture content 10 % by weight) 120 ℃ of oven dry, and the protein content that the butt instrumentation of take obtains in feed is 61% (m/m).

Embodiment 4

1) press 380m ³the total flux of/h is on average sent into rare gluten water (concentration of proteinaceous solid substance is 1.7 % by weight) and in two disc separators, rare gluten water is carried out to once concentration simultaneously (total feed of rare gluten water is 380m ³/ h, each inlet amount is 190m ³/ h, the rotating speed of centrifugation is respectively 3300 revs/min, the temperature of centrifugation is 45 ℃), the total flux that obtains the first water is 228m ³the total flux of/h (in the first water, the content of proteinaceous solid substance is 0.29 % by weight) and the first concentrated phase is 152m ³(the concentrated phase flow of each separating machine is respectively 76m to/h ³/ h) (in the first concentrated phase, the content of proteinaceous solid substance is 3.8 % by weight); The first concentrated phase is again sent into and in a disc separator, carried out secondary concentration (feed rate of the first concentrated phase is 152m ³/ h, the rotating speed of centrifugation is 3400 revs/min, the temperature of centrifugation is 45 ℃), obtaining the second water flow is 110m ³/ h and the second concentrated phase flow are 42m ³/ h (in the second concentrated phase, solid content is 11.8 % by weight);

2) the second concentrated phase step (1) being obtained is inserted in vacuum-type drum filter and is filtered, and obtains filter cake (moisture 50 % by weight); The filter cake obtaining is obtained to feed (moisture content 10 % by weight) 120 ℃ of oven dry, and the protein content that the butt instrumentation of take obtains in feed is 61% (m/m);

According to step 3 in embodiment 1) method process the second water, in the water obtaining, the content of proteinaceous solid substance is 0.20 % by weight, the filter cake obtaining (water content is 50 % by weight) is obtained to protein fodder (moisture content 10 % by weight) 120 ℃ of oven dry, and the protein content that the butt instrumentation of take obtains in feed is 61% (m/m).

Embodiment 5

Method according to embodiment 1 is prepared W-Gum, different, in step (6), and the step 3 of the treatment process of described rare gluten water) in:

The polyacrylic acid flocculation agent that is 8,000,000 by number-average molecular weight is soluble in water, makes mass volume ratio concentration and be 0.05% solution; Polymerize aluminum chloride (n is 1-5, m≤10, basicity B=n/6 * 100%) is soluble in water, make mass volume ratio concentration and be 5% polymeric aluminum chlorides solution.And at 40 ℃, in the second water, add above-mentioned two kinds of flocculant aqueous solutions, every cubic metre of second water of take is benchmark, it is 12.5ppm that the consumption of described polyacrylic acid flocculant aqueous solution (25L) makes the amount of polyacrylic acid flocculation agent, it is 50ppm that the consumption of the described flocculant of polymeric aluminium chloride aqueous solution (1L) makes the amount of flocculant of polymeric aluminium chloride, is uniformly mixed 3 minutes; And the mixed solution obtaining is inserted and in air flotation slot, carried out dissolved air flotation (pressure that passes into air is 0.4 MPa, the air supporting time is 8 minutes), separated upper strata seitan particle is also inserted mixed solution in flame filter press and is filtered, in the water obtaining, the content of proteinaceous solid substance is 0.21 % by weight, the filter cake obtaining (water content is 50 % by weight) is obtained to protein fodder (moisture content 10 % by weight) 120 ℃ of oven dry, and the protein content that the butt instrumentation of take obtains in feed is 62% (m/m).

Embodiment 6

Every cubic metre of second water of take is benchmark, it is 15ppm that the consumption of described sodium polyacrylate flocculant aqueous solution (30L) makes the amount of sodium polyacrylate flocculation agent, it is 45ppm that the consumption of the described flocculant of polymeric aluminium chloride aqueous solution (0.9L) makes the amount of flocculant of polymeric aluminium chloride, in the water obtaining after filtration, the content of proteinaceous solid substance is 0.21 % by weight, the filter cake obtaining (water content is 50 % by weight) is obtained to protein fodder (moisture content 10 % by weight) 120 ℃ of oven dry, and the protein content that the butt instrumentation of take obtains in feed is 61% (m/m).

Embodiment 7

Method according to embodiment 5 is prepared W-Gum, different, in step (6), and the step 3 of the treatment process of described rare gluten water) in:

The mode that flocculant aqueous solution is mixed with the second water is first to add the aqueous solution of polymerize aluminum chloride, and is uniformly mixed 2 minutes, and then adds the polyacrylic aqueous solution, is uniformly mixed 1 minute.In the water obtaining after filtration, the content of proteinaceous solid substance is 0.18 % by weight, the filter cake obtaining (water content is 50 % by weight) is dried and obtains protein fodder (moisture content 10 % by weight) at 120 ℃, and the protein content that the butt instrumentation of take obtains in feed is 62% (m/m).

Embodiment 8

The mode that flocculant aqueous solution is mixed with the second water is first to add the aqueous solution of polymerize aluminum chloride, and is uniformly mixed 2 minutes, and then adds the polyacrylic aqueous solution, is uniformly mixed 1 minute; Every cubic metre of second water of take is benchmark, it is 80ppm that the consumption (4L) of the aqueous solution of described polymerize aluminum chloride (the mass volume ratio concentration of polymerize aluminum chloride is 2%) makes the amount of flocculation agent, and it is 40ppm that the consumption (20L) of the described polyacrylic aqueous solution (polyacrylic mass volume ratio concentration is 0.2%) makes the amount of flocculation agent.In the water obtaining after filtration, the content of proteinaceous solid substance is 0.19 % by weight, the filter cake obtaining (water content is 50 % by weight) is dried and obtains protein fodder (moisture content 10 % by weight) at 120 ℃, and the protein content that the butt instrumentation of take obtains in feed is 61% (m/m).

Embodiment 9

The mode that flocculant aqueous solution is mixed with the second water is first to add the aqueous solution of polymerize aluminum chloride, and is uniformly mixed 2 minutes, and then adds the polyacrylic aqueous solution, is uniformly mixed 1 minute; Every cubic metre of second water of take is benchmark, it is 30ppm that the consumption (3L) of the aqueous solution of described polymerize aluminum chloride (the mass volume ratio concentration of polymerize aluminum chloride is 1%) makes the amount of flocculation agent, and it is 15ppm that the consumption (15L) of the described polyacrylic aqueous solution (polyacrylic mass volume ratio concentration is 0.1%) makes the amount of flocculation agent.In the water obtaining after filtration, the content of proteinaceous solid substance is 0.18 % by weight, the filter cake obtaining (water content is 50 % by weight) is dried and obtains protein fodder (moisture content 10 % by weight) at 120 ℃, and the protein content that the butt instrumentation of take obtains in feed is 60% (m/m).

Embodiment 10

The mode that flocculant aqueous solution is mixed with the second water is first to add the aqueous solution of polymerize aluminum chloride, and is uniformly mixed 2 minutes, and then adds the polyacrylic aqueous solution, is uniformly mixed 1 minute; Every cubic metre of second water of take is benchmark, it is 40ppm that the consumption (0.8L) of the aqueous solution of described polymerize aluminum chloride (the mass volume ratio concentration of polymerize aluminum chloride is 5%) makes the amount of flocculation agent, and it is 40ppm that the consumption (80L) of the described polyacrylic aqueous solution (polyacrylic mass volume ratio concentration is 0.05%) makes the amount of flocculation agent.In the water obtaining after filtration, the content of proteinaceous solid substance is 0.21 % by weight, the filter cake obtaining (water content is 50 % by weight) is dried and obtains protein fodder (moisture content 10 % by weight) at 120 ℃, and the protein content that the butt instrumentation of take obtains in feed is 62% (m/m).

Embodiment 11

Method according to embodiment 1 is prepared W-Gum, different: in the evaporation technology of step (3), by 50 ℃ of corn steep liquors extracting out in steeping tank, (every tank approximately goes out 25m ³, dry matter content is 8 % by weight), pump in the quadruple effect falling-film evaporator in described multi-effect evaporation system that (controlling corn soaking flow quantity is 6.2m ³/ h), under the vacuum tightness of the Heating temperatures of 70 ℃, 0.068MPa, described corn steep liquor is carried out to circulating-heating evaporation, obtaining concentration is the quadruple effect corn steep liquor feed liquid of 10 % by weight and four effect juice steams of 52 ℃, this four effect juice steam is connected with vacuum pump by pipe bundle condenser, and (controlling feed liquid flow is 5-6m by the extraction of quadruple effect corn steep liquor feed liquid ³/ h) and after being preheated to 88 ℃, pump in the second effect falling-film evaporator, under the vacuum tightness of the Heating temperatures of 105 ℃, 0.023MPa, described quadruple effect corn steep liquor feed liquid is carried out to circulating-heating evaporation, obtain concentration and be two effect corn steep liquor feed liquids of 21 % by weight and two effect juice steams of 90 ℃ (part two effect juice gas can for preheating quadruple effect corn steep liquor feed liquid); Then described two effect corn syrup liquid pumps are entered in triple effect falling-film evaporator, (controlling feed liquid flow is 2-3m ³/ h), under the vacuum tightness of the Heating temperatures of 90 ℃, 0.03MPa, adopt the juice vapour of two effects to carry out circulating-heating evaporation to described two effect corn steep liquor feed liquids, obtaining output is that 1180kg/h, concentration are the triple effect corn steep liquor feed liquid of 42 % by weight left and right and three effect juice steams of 70 ℃, and three effect juice steams are re-used as the thermal source of quadruple effect falling-film evaporator; The triple effect corn syrup liquid pump that is 42 % by weight left and right by described 1180kg/h, concentration enters in the first effect scrapper thin film evaporator, and adopt the raw steam of 130 ℃, under the pressure of 0.18MPa, described triple effect corn steep liquor feed liquid is carried out to heating evaporation, and obtaining output is that 990kg/h, concentration are the concentrated corn steep liquor of 51 % by weight left and right.

Embodiment 12

Method according to embodiment 1 is prepared W-Gum, different: in the evaporation technology of step (3), by 50 ℃ of corn steep liquors extracting out in steeping tank, (every tank approximately goes out 35m ³, dry matter content is 6 % by weight), pump in the quadruple effect falling-film evaporator in described multi-effect evaporation system that (controlling corn soaking flow quantity is 5.8m ³/ h), under the vacuum tightness of the Heating temperatures of 65 ℃, 0.075MPa, described corn steep liquor is carried out to circulating-heating evaporation, obtaining concentration is the quadruple effect corn steep liquor feed liquid of 8 % by weight and four effect juice steams of 50 ℃, this four effect juice steam is connected with vacuum pump by pipe bundle condenser, and (controlling feed liquid flow is 5-6m by the extraction of quadruple effect corn steep liquor feed liquid ³/ h) and after being preheated to 85 ℃, pump in the second effect falling-film evaporator, under the pressure of the Heating temperatures of 99 ℃, 0MPa, described quadruple effect corn steep liquor feed liquid is carried out to circulating-heating evaporation, obtain concentration and be two effect corn steep liquor feed liquids of 19 % by weight and two effect juice steams of 85 ℃ (part two effect juice gas can for preheating quadruple effect corn steep liquor feed liquid); Then described two effect corn syrup liquid pumps are entered in triple effect falling-film evaporator, (controlling feed liquid flow is 2-3m ³/ h), under the vacuum tightness of the Heating temperatures of 85 ℃, 0.04MPa, adopt the juice vapour of two effects to carry out circulating-heating evaporation to described two effect corn steep liquor feed liquids, obtaining output is that 830kg/h, concentration are the triple effect corn steep liquor feed liquid of 42 % by weight left and right and three effect juice steams of 65 ℃, and three effect juice steams are re-used as the thermal source of quadruple effect falling-film evaporator; The triple effect corn syrup liquid pump that is 42 % by weight left and right by described 830kg/h, concentration enters in the first effect scrapper thin film evaporator, and adopt the raw steam of 120 ℃, under the pressure of 0.1MPa, described triple effect corn steep liquor feed liquid is carried out to heating evaporation, and obtaining output is that 700kg/h, concentration are the concentrated corn steep liquor of 50 % by weight left and right.

Comparative example 1

This comparative example is for illustrating the preparation method of the W-Gum of prior art.

According to the method for embodiment 1, corn is carried out to raw materials pretreatment and immersion, different:

In the evaporation technology of step (3), adopt triple effect falling-film evaporator system to concentrate corn steep liquor, that is, by 50 ℃ of corn steep liquors extracting out in steeping tank, (every tank approximately goes out 30m ³, dry matter content is 7 % by weight), pump in the quadruple effect falling-film evaporator in described multi-effect evaporation system that (controlling corn soaking flow quantity is 6m ³/ h), under the vacuum tightness of the Heating temperatures of 70 ℃, 0.068MPa, described corn steep liquor is carried out to circulating-heating evaporation, obtaining concentration is the quadruple effect corn steep liquor feed liquid of 9 % by weight and four effect juice steams of 52 ℃, this four effect juice steam is connected with vacuum pump by pipe bundle condenser, and (controlling feed liquid flow is 5-6m by the extraction of quadruple effect corn steep liquor feed liquid ³/ h) and after being preheated to 85 ℃, pump in the second effect falling-film evaporator, under the vacuum tightness of the Heating temperatures of 103 ℃, 0.015MPa, described quadruple effect corn steep liquor feed liquid is carried out to circulating-heating evaporation, obtain concentration and be two effect corn steep liquor feed liquids of 20 % by weight and two effect juice steams of 88 ℃ (part two effect juice gas can for preheating quadruple effect corn steep liquor feed liquid); Then described two effect corn syrup liquid pumps are entered in triple effect falling-film evaporator, (controlling feed liquid flow is 2-3m ³/ h), under the vacuum tightness of the Heating temperatures of 88 ℃, 0.034MPa, adopt the juice vapour of two effects to carry out circulating-heating evaporation to described two effect corn steep liquor feed liquids, obtaining output is that 1000kg/h, concentration are the triple effect corn steep liquor feed liquid of 42 % by weight left and right and three effect juice steams of 70 ℃, and three effect juice steams are re-used as the thermal source of quadruple effect falling-film evaporator.If feed liquid is continued to evaporation in triple effect falling-film evaporator, make its concentration reach 48-52 % by weight, can be because viscosity of sludge is excessive, poor fluidity, and in heating tube, occur that dry wall, coking phenomenon, long-time running meeting stop up heating tube, can not normally move vaporizer.

In the starch milk process for refining of step (6), the treatment process of described rare gluten water comprises:

1) press 350m ³the flow of/h is on average sent into total rare gluten water (proteinaceous solid concentration is 1.7 % by weight) and in two disc separators, gluten water is concentrated that (the combined feed total feed flow of gluten water is 350m simultaneously ³/ h, each inlet amount is 175m ³/ h, the rotating speed of centrifugation is respectively 3300 revs/min, the temperature of centrifugation 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) total flux of (in process water, proteinaceous solid content is 0.76 % by weight) and enriched material is 40m ³(the enriched material flow of each separating machine is 20m to/h ³/ h) (in enriched material, proteinaceous solid content is 9 % by weight);

2) enriched material step (1) being obtained is inserted in flame filter press and is filtered, and obtains filter cake (moisture 50 % by weight); The filter cake obtaining is obtained to feed (moisture content 10 % by weight) 120 ℃ of oven dry, and the protein content that the butt instrumentation of take obtains in feed is 55% (m/m).

Contrast by above-described embodiment 1-12 and comparative example 1 can be found out, adopt method of the present invention effectively to gluten water, to concentrate, and be met the process water (in the first water, proteinaceous solid content is less than 0.3 % by weight) of direct reuse standard simultaneously and contain the enriched material that proteinaceous solid content is higher (in the second concentrated phase, proteinaceous solid content is greater than 11 % by weight), on the one hand, process water again reuse circulation soaks and plumule, fiber is washed corn, on the other hand, can improve the productive rate of gluten protein powder.In addition, the solid substance that can further need be carried out by the method that adds flocculation agent and carry out dissolved air flotation in the second water of secondary treatment is separated, further obtain protein fodder, and because the volume of the second water is relatively little, therefore more easily process.

In addition, adopt scrapper thin film evaporator and falling-film evaporator to form multi-effect evaporation system, first adopt falling-film evaporator that corn steep liquor is concentrated into 40-45 % by weight, then utilizing scrapper thin film evaporator as high density concentrating unit, can be further that the corn steep liquor of 40-45 % by weight is concentrated into 48-52 % by weight by concentration.Avoided on the one hand when adopting falling-film evaporator to concentrate corn steep liquor, the dense corn steep liquor of excessive concentration is due to the problem of the heating tube of viscosity great Yi obstruction falling-film evaporator, and utilized dexterously the feature of scrapper thin film evaporator, the concentration of corn steep liquor can be increased to applicable concentrated concentration (48-52 % by weight), and obtain the corn steep liquor concentrated solution that concentration is higher.

Claims

1. the preparation method of a W-Gum, the method comprises the sandstone of removing in maize raw material, soaking corn grain, the concentrated corn steep liquor obtaining, and the corn grain through soaking is carried out to fragmentation, isolate plumule, the corn particle that contains maize peel and endosperm after de-embryo is ground, isolate fiber, the coarse starch milk obtaining is carried out to separation and obtain gluten water and starch milk, and starch milk is washed, it is characterized in that:

Described method of removing the sandstone in maize raw material comprises:

The described sandstone that restriction is sunk continue to flow with water;

2. preparation method according to claim 1, wherein, the sandstone that described restriction is sunk continue mobile method with water and comprise along the flow direction of water a plurality of obstacles are set, and the sandstone that described restriction of obstacle sinks continue to flow with water.

3. preparation method according to claim 2, wherein, described in contain corn grain and sandstone maize raw material with liquid along the hillslope overland flow under being tilted to, described a plurality of obstacles be arranged on described domatic on; Described obstacle is perpendicular to described domatic.

4. preparation method according to claim 3, wherein, described domatic inclination angle is 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, the maize raw material that contains corn grain and sandstone described in making along downward successively a plurality of step-flow, all arranges a described obstacle with water on each step.

7. preparation method according to claim 6, wherein, described obstacle is arranged on the free edge of tread portion of described step; Described obstacle is perpendicular to the plane at described tread portion place.

8. according to the preparation method described in claim 6 or 7, wherein, the height of described obstacle is 1:1-1:3 with the ratio of the height of described step.

9. according to the method for the preparation described in claim 2,3,6 or 7, wherein, described obstacle is baffle plate.

10. preparation method according to claim 9, wherein, the height streamwise of described plate washer reduces gradually.

11. preparation methods according to claim 9, wherein, the height of described plate washer is 15-50cm.

12. preparation methods according to claim 1, wherein, the flow velocity of described water is 0.3-1.5m/s; The consumption of described water be described maize raw material gross weight 2-5 doubly.

13. preparation methods according to claim 1, wherein, in the first water that the condition of once concentration makes to obtain, the content of proteinaceous solid substance is 0.1-0.3 % by weight, and in the second enriched material that the condition of secondary concentration makes to obtain, the content of proteinaceous solid substance is 10-12 % by weight.

14. according to the preparation method described in claim 1 or 13, and wherein, it is 2-3:1 that the condition of once concentration makes the concentration ratio of the first concentrated phase, and the concentration ratio of described the first concentrated phase is the feed volume of once concentration gluten water and the ratio of the first concentrated phase volume; It is 3-4:1 that the condition of secondary concentration makes the concentration ratio of the second concentrated phase, and the concentration ratio of described the second concentrated phase is the feed volume of secondary concentration the first concentrated phase and the ratio of the second concentrated phase volume.

15. preparation methods according to claim 1, wherein, the aqueous solution that described flocculant solution is flocculation agent, the aqueous solution of described flocculation agent is the aqueous solution of polyacrylic acid and/or sodium polyacrylate and the aqueous solution of polymerize aluminum chloride.

16. preparation methods according to claim 15, wherein, the mass body volume concentrations of the polyacrylic acid aqueous solution and polyacrylic acid sodium water solution is 0.1-0.5%, the mass body volume concentrations of the polymerize aluminum chloride aqueous solution is 1-5%; Described polyacrylic number-average molecular weight is 6,000,000-1,000 ten thousand dalton, and the number-average molecular weight of described sodium polyacrylate is 6,000,000-1,000 ten thousand dalton; The molecular formula of described polymerize aluminum chloride is [Al ₂(OH) _ncl _6-n] _m, wherein, n is 1-5, m≤10, basicity B=n/6 * 100%.

17. preparation methods according to claim 16, wherein, the method that the second water is mixed with flocculant solution comprises first the aqueous solution of described the second water and polymerize aluminum chloride, then with the aqueous solution of the polyacrylic aqueous solution and/or sodium polyacrylate; The mass ratio of polymerize aluminum chloride and polyacrylic acid and/or sodium polyacrylate is 2-5.

18. preparation methods according to claim 16, wherein, the every cubic metre of pending water of take is benchmark, and it is 5-50ppm that the consumption of described flocculant solution makes the amount of polyacrylic acid and sodium polyacrylate flocculation agent, and the amount that makes flocculant of polymeric aluminium chloride is 20-100ppm.

19. preparation methods according to claim 1, wherein, the method of described dissolved air flotation comprises when the second water is mixed with flocculant solution or afterwards, in mixture, blast air, make to be flocculated and/or bubble adhesion that the seitan particle of sedimentation is formed with bubble floating, and described in separation, be flocculated and/or the seitan particle of sedimentation; The pressure that passes into air is 0.2-0.4 MPa, and the air supporting time is 1-10 minute.

20. preparation methods according to claim 1, wherein, the method of described evaporation comprises that employing falling-film evaporator is concentrated into 40-42 % by weight by corn steep liquor soak solution, and adopts scrapper thin film evaporator that the corn steep liquor of the 40-42 % by weight obtaining is concentrated into 48-50 % by weight.

21. according to the preparation method described in claim 1 or 20, wherein, adopting falling-film evaporator that the concentrated evaporation of corn steep liquor is imitated to number is 3-4 effect, and adopting film-falling scraping plate vaporizer is 1-2 effect by the further concentrated evaporation effect number of the corn steep liquor that evaporation obtains through falling-film evaporator.

22. preparation methods according to claim 21, wherein, the method of described evaporation comprises corn steep liquor is pumped in quadruple effect falling-film evaporator, under the Heating temperature of 65-75 ℃, this corn steep liquor is carried out to circulating-heating evaporation, obtaining concentration is the quadruple effect corn steep liquor feed liquid of 7-10 % by weight and four effect juice steams of 50-55 ℃, and this quadruple effect corn syrup liquid pump is entered in the second effect falling-film evaporator, under the Heating temperature of 98-105 ℃, this quadruple effect corn steep liquor feed liquid is carried out to circulating-heating evaporation, obtaining concentration is two effect corn steep liquor feed liquids of 18-20 % by weight and two effect juice steams of 85-90 ℃, this two effects corn syrup liquid pump is entered in triple effect falling-film evaporator, under the Heating temperature of 85-90 ℃, this two effects corn steep liquor feed liquid is carried out to circulating-heating evaporation, obtaining concentration is the triple effect corn steep liquor feed liquid of 40-45 % by weight and three effect juice steams of 65-75 ℃,

This triple effect corn syrup liquid pump is entered in an effect scrapper thin film evaporator, under the Heating temperature of 120-130 ℃, this triple effect corn steep liquor feed liquid is evaporated, obtaining concentration is the concentrated corn steep liquor of 48-52 % by weight and an effect juice steam of 98-110 ℃.

23. preparation methods according to claim 22, wherein, come from an effect juice steam or are an effect juice steam and the mixing steam of raw steam for the heating steam of the second effect falling-film evaporator; Heating steam for triple effect falling-film evaporator comes from two effect juice steams; Heating steam for quadruple effect falling-film evaporator comes from three effect juice steams.