CN104642717A - Lees protein feed production method - Google Patents
Lees protein feed production method Download PDFInfo
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- CN104642717A CN104642717A CN201310590453.XA CN201310590453A CN104642717A CN 104642717 A CN104642717 A CN 104642717A CN 201310590453 A CN201310590453 A CN 201310590453A CN 104642717 A CN104642717 A CN 104642717A
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Abstract
The present invention discloses a lees protein feed production method, which comprises a first drying step and a second drying step, wherein the first drying step and the second drying step are sequentially performed, the first drying step is used for drying a first material containing wet lees so as to obtain a first drying product, the second drying step is used for drying a second material, and the second material contains the first drying product and a soluble syrup. With the technical scheme, the DDS drying time is substantially shortened, and the production capacity is ensured while the quality of the final product DDGS feed is increased.
Description
Technical field
The present invention relates to a kind of production method of vinasse protein feed.
Background technology
Vinasse protein feed (DDGS) is the useless mash that corn processing production alcohol (comprising edible alcohol, industrial alcohol, alcohol fuel) produces, through centrifugation, dry product.According to statistics, the useless mash of 13-15 ton can be produced while often producing one ton of alcohol, the chemical oxygen consumption (COC) (COD) of vinasse is up to 50000mg/L, BOD (BOD) is up to 30000mg/L, greatly exceed alcohol industry COD350mg/L, BOD that GB (GB18918-2002) specifies is the discharge standard of 200mg/L, if directly enter water body by force, then can severe contamination water source and destruction ecological environment around.Therefore, drying is carried out to after maize alcohol stillage waste liquid evaporation and concentration, white drying protein feed can be obtained, i.e. full vinasse protein feed (DDGS), the most frequently used self-digestion mode (Qiao Jianfen of current corn fermentation preparing alcohol enterprise, Maize Alcohol Lees Liquid production white drying protein feed (DDGS), Shanxi Food Industry, 3:20-21).
The nutritional labeling of DDGS is larger by the impact of production technology (such as, the type of fermentation, distillation efficiency, baking temperature and time etc.).Wherein, due to the increase of temperature in dry run, (residual fat containing 6-12 % by weight in DDGS feed, when moisture is more than 5% to accelerate Maillard reaction and oxidation, fat oxidation is accelerated, and brown stain speed is also accelerated thus affected DDGS product quality; In addition, the oxidation of lutein can cause equally and darken) generation, therefore, the nutritional labeling of DDGS is especially with having the greatest impact by drying process.At present, market at home and abroad, the color of DDGS becomes the main reference factor of its quality, also becomes the mode of corn dry wine dregs of rice reality or the cognitive quality distinguishing separate sources.The color of DDGS has golden yellow and crineous, and golden yellow is best.The research such as Cromwell shows (Cromwell, G.L., K.L.Herkelman, and T.S.Stahly.1993.Physical, chemical, and nutritional characteristics of distillers dried grains with soluble for chicks andpigs.J.Anim.Sci.71:679-686), DDGS color and its nutritional labeling closely related, dark colour DDGS nutritive value is lower than the DDGS of light colour, and find dark colour DDGS usually with the paste smell of burning or smoke, this may be that in dry run, over-heating causes.And over-heating easily causes Maillard reaction, reduce the utilization rate of lysine.In addition, the effective content of lysine and the linear (R of its color in DDGS
2=0.67, p<0.05), the lysine content of light colour DDGS is 0.86%, and the lysine content of dark colour DDGS is only 0.62%.Long period does not have extensively to apply in pig industry DDGS in the past, and its reason is exactly that Maillard reaction in dry run have impact on the color of DDGS and reduces the digestibility of its lysine, and lysine is the first limiting amino acids of swine rations.(the Whitney such as Whitney, M.H., M.J.Spiehs, G.C.Shurson, and S.K.Baidoo.2001.Apparent ileal amino acid digestibility of corn distillers dried grains withsoluble.) research show, the lysine ileal digestibility of the golden yellow corn DDGS of high-quality is 53.6%, and pitchy lysine digestibility is 0.(the Fastinger such as Fastinger, N.D.and D.C.Mahan.2006.Determination of the ileal AA and energy.Digestibilities of corn distillersdried grains with soluble using grower-finisher pigs, J.Anim.Sci.84:1722-1728.) color of two kinds of DDGS is determined with Minolta CR410 colour photometer, L value is respectively 28 and 52.3, L value is lower, and its color is darker; Determination and analysis also finds, dark colour DDGS lysine content is only 0.48%, and standard ileal lysine digestibility is 43.6%, and in light colour DDGS, lysine content is 0.76%, and standard ileal lysine digestibility is 61.5%.
Namely therefore, produce light colour, also flavous DDGS feed has become the target that DDGS manufacturing enterprise pursues jointly.But because current domestic corn price is climbed to a higher point year by year, country reduces year by year to the subsidy of corn fermentation preparing alcohol enterprise, and U.S.'s DDGS product is dumped in a large number at home, and cause domestic corn deep processing enterprise profit on the low side, cost is higher in addition.Therefore, reduce as much as possible or control producing the energy consumption in DDGS, material consumption, ensure its quality again, be the task of top priority of current alcohol enterprise simultaneously.At present, the technique of domestic and international dry DDGS mainly contains three kinds: ring type drying, drum-type drying and tube bank are dry.
The feature of ring type drying is: the time of staying of DDGS in ring type drying system is general very short, and effectively can prevent the oxidation that DDGS is over-drying, effectively reduce material, thus can improve the quality of products.The feature of drum-type drying is: direct fired-air heats, inlet temperature is higher, residence time of material is shorter, the use of cooling device makes material cool sooner, effectively can reduce the generation of the oxidation of fat and the lutein contained in Maillard reaction in dry run and vinasse, thus reach the object improving DDGS quality.Tube bank drying is one of the most extensive drying process and equipment of current domestic use, and be characterized in: economical and practical, in various drying equipment, power consumption is minimum, hear rate is low.
But by above 3 kinds of drying processes, especially still need to be improved further with the quality of restraining the DDGS that drying process obtains.
Summary of the invention
The object of the invention is the second-rate defect of DDGS of producing to overcome prior art, a kind of production method can producing high-quality DDGS feed is provided.
The present inventor finds, the main cause that the DDGS quality that the technique that prior art produces DDGS feed obtains is lower is: existing drying process alcohol fermentation liquid is distilled out alcohol and obtains liquid phase (clear liquid) after carrying out Separation of Solid and Liquid, and described clear liquid is carried out concentrated after obtain concentrate (i.e. solubility syrup, DDS), again with isolated solid phase (i.e. wet vinasse, DDG) mix, and the feed that common for mixture drying is obtained.Due to the requirement in order to make the water content of product reach certain, need to carry out long drying to described mixture.Like this, the over-drying of product can be caused on the one hand, DDGS product be produced and sticks with paste the smell of burning and smoke; On the other hand, because long high temperature drying can accelerate the generation of Maillard reaction and fat and lutein oxidation, the serious color and luster that have impact on DDGS also reduces its nutritive value, thus reduces the quality of the DDGS finally obtained.
The present inventor is surprised to find that by large quantifier elimination, and in dry run, DDG is very little by the impact of dry time and temperature, and DDS is very responsive to the temperature and time of drying.Based on this, the present inventor adopts the method for two-part drying to carry out the drying of drunk fish, the drying of DDG is mainly carried out at first paragraph, add DDS at second segment, can greatly reduce like this drying time of the DDS added thus the generation of reduction Maillard reaction and fat and lutein oxidation.
Based on above-mentioned discovery, the invention provides a kind of production method of vinasse protein feed, the method comprises the first drying steps and the second drying steps that carry out successively, described first drying steps is used for carrying out drying to the first material containing wet vinasse, obtain the first desciccate, described second drying steps is used for carrying out drying to the second material, and described second material contains described first desciccate and solubility syrup.
Preferably, described first material is also containing described first desciccate.
Preferably, the dried material of described second material also containing described second drying steps gained.
Preferably, described first drying steps and the second drying steps all carry out in pipe bundle drier.
Pass through technique scheme, only dry by baking temperature and the less DDG of time effects in the first drying steps, add again in the second drying steps by baking temperature and the larger DDS of time effects, thus substantially reduce the drying time of DDS, effectively reduce the Maillard reaction and oxidation that occur in dry run.Thus effectively improve the quality of final products DDGS.And, in a preferred embodiment, regulated the moisture of charging in the first drying steps and the second drying steps by the method for back-mixing, and adopt lower-cost tube bank drying process, while not affecting DDGS quality, production cost is reduced greatly.
Other features and advantages of the present invention are described in detail in detailed description of the invention part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide a further understanding of the present invention, and forms a part for description, is used from explanation the present invention, but is not construed as limiting the invention with detailed description of the invention one below.In the accompanying drawings:
Fig. 1 is the picture of the DDGS according to two-part drying means production of the present invention;
Fig. 2 is the picture of the DDGS produced according to the method for prior art;
Fig. 3 is the drying process schematic diagram of a kind of preferred embodiment of the present invention.
Description of reference numerals
1: the first pipe bundle drier charging aperture;
2: the first pipe bundle driers;
The back-mixing part of 3: the first pipe bundle driers;
The auger coupling part of 4: the first pipe bundle driers and the second pipe bundle drier;
The interpolation shower nozzle of 5:DDS;
6: the second pipe bundle driers;
The back-mixing part of 7: the second pipe bundle driers;
The discharging opening of 8: the second pipe bundle driers.
Detailed description of the invention
Below the specific embodiment of the present invention is described in detail.Should be understood that, detailed description of the invention described herein, only for instruction and explanation of the present invention, is not limited to the present invention.
The invention provides a kind of production method of vinasse protein feed, the method comprises the first drying steps and the second drying steps that carry out successively, described first drying steps is used for carrying out drying to the first material containing wet vinasse, obtain the first desciccate, described second drying steps is used for carrying out drying to the second material, and described second material contains described first desciccate and solubility syrup.
According to the present invention, described wet vinasse and solubility syrup are concept well known in the art, namely, described wet vinasse are solid content alcohol fermentation liquid being distilled out alcohol and obtains after carrying out Separation of Solid and Liquid, and described solubility syrup is the concentrate of clear liquid alcohol fermentation liquid being distilled out alcohol and obtains after carrying out Separation of Solid and Liquid.Wherein, the preparation method of described alcohol fermentation liquid, alcohol fermentation liquid is carried out distilling out the method for alcohol, the method for described Separation of Solid and Liquid and being conventionally known to one of skill in the art to the method that described clear liquid concentrates, do not repeat them here.
According to the present invention, have no particular limits the water content of wet vinasse dry in the first drying steps, under normal circumstances, after Separation of Solid and Liquid, the water content of the wet vinasse of gained is 68-72 % by weight.In the method for the invention, the wet vinasse of this water content directly can be carried out the first drying; Also the wet vinasse of this water content can be carried out predrying after carry out first dry again, pre-dried degree, such as, described wet vinasse can be dried to water content is 30 % by weight.Therefore, the water content of dry in the first drying steps wet vinasse can be 30-72 % by weight.
In the actual production of DDGS feed, in order to reduce or avoid material to the paste pipe phenomenon of drying equipment, preferably the water content of described first material is 30-45 % by weight, is more preferably 35-40 % by weight.Therefore, be 30-45 % by weight when described wet vinasse are dried to its water content, when being preferably 35-40 % by weight, can directly it can be used as the first material to carry out the first drying.Described pre-dried method is conventionally known to one of skill in the art, such as, can adopt the method for evaporation.
According to the present invention, in order to make, production technology is more simple, production cost is lower, and take into account the quality of gained DDGS simultaneously, according to one of the present invention preferred embodiment, only be greater than 45 % by weight by predrying for the wet vinasse of gained after described Separation of Solid and Liquid to its water content, more preferably do not carry out predrying to the wet vinasse of gained after described Separation of Solid and Liquid, in this case, described wet vinasse can be mixed with the first desciccate, carry out back-mixing by the first desciccate and wet vinasse.Preferably, in the first material, relative to the described wet vinasse of 100 weight portions, the content of described first desciccate is 70-150 weight portion.When not carrying out predrying to wet vinasse, in the first material, relative to the described wet vinasse of 100 weight portions, the content of described first desciccate is preferably 115-150 weight portion.The present inventor finds, because DDG is very little by the impact of dry time and temperature, therefore, this preferred embodiment in, both operating procedure was saved, reduce production cost, the quality of gained DDG can not be affected because of the first desciccate is carried out redrying again simultaneously, thus the quality of product can be ensured.
The present invention has no particular limits for the condition of the first drying steps, considering cost and product quality, and under preferable case, described first drying steps is 160-170 DEG C in temperature, and the time is 3-10min, carries out under the condition of preferred 3-4min.Under above-mentioned preferred condition, carry out the first drying, the water content of the first desciccate can either be ensured, the generation of Maillard reaction and oxidation in dry run can be reduced again.According to the practical production experience of the present inventor, carry out the first drying steps under the preferred water content and preferred drying condition of the first material after, the water content of gained first desciccate can be reduced to 10-12 % by weight.
In the present invention, the water content of solubility syrup contained in the second material is had no particular limits, such as, directly carry out second dry after clear liquid after Separation of Solid and Liquid can being mixed with the first desciccate, also can mix with the first desciccate again after by its pre-concentration and carry out the second drying.The present inventor is found by large quantifier elimination, when being 50-85 % by weight by described clear liquid pre-concentration to water content, mix with the first desciccate again after preferred 77-80 % by weight, the ratio of mixing preferably makes the water content of the second material be 30-45 % by weight, be more preferably 35-40 % by weight (this water content can reduce or avoid material to the paste pipe of drying equipment), and then the second material is carried out the second drying, the total energy consumption produced can be made to reduce further, the nutrient composition content in final gained DDGS can be made again to be further improved, therefore, preferably, the water content of described solubility syrup is 50-85 % by weight, be more preferably 77-80 % by weight, the ratio mixed with the first desciccate preferably makes the water content of described second material be 30-45 % by weight, is more preferably 35-40 % by weight.
According to the present invention, although only namely solubility syrup and described first desciccate mixing can be reached the preferred water content of the second material.But the present inventor finds, when the water content of solubility syrup is preferably 77-80 % by weight, and contain in the second material, relative to the second material of 100 weight portions, the dried material of the second drying steps gained of 8-12 weight portion, and when ensureing the second above-mentioned preferred water content of material, can reduce production cost further, and the nutritional labeling of the DDGS of final gained can further be improved.Therefore, preferably, the water content of described solubility syrup is 77-80 % by weight, dried material also containing described second drying steps gained in described second material, back-mixing is carried out by the dried material of the second drying steps gained and the mixed material of DDS and the first desciccate, relative to the second material of 100 weight portions, the content of the dried material of described second drying steps gained is≤12 weight portions.
The present invention has no particular limits for the condition of the second drying steps, considering cost and product quality, and under preferable case, described second drying steps is 160-170 DEG C in temperature, and the time is 3-10min, carries out under the condition of preferred 3-4min.The second drying is carried out under above-mentioned preferred condition, the water content of the second desciccate can either be ensured, the generation of Maillard reaction and oxidation in the second material in dry run can be reduced again, and when above-mentioned preferably carry out back-mixing, the addition of the dried material of described second drying steps gained is not higher than 12 % by weight, therefore, the redrying of the dried material of the second drying steps gained can not affect the quality of gained DDGS substantially.According to the practical production experience of the present inventor, carry out the second drying steps under the preferred water content and preferred drying condition of the second material after, the water content of the second desciccate of gained can be reduced to less than 12 % by weight, can reach the requirement to its water content when storing DDGS.
According to the present invention, the not special requirement of equipment that is dry to first and the second drying can be well known in the art arbitrarily for the production of the drying equipment of DDGS.Such as, can be ring drier, cylindrical drier or pipe bundle drier.But ring type drying process and drum-type drying technique all adopt gas-firing to add hot-air as dry medium in dry run, and Gas Prices is expensive, for original added value with regard to lower DDGS feed and the lower medium-sized and small enterprises of profit, production cost is too high.Therefore, in order to reduce production cost, the first drying steps described in the present invention and the second drying steps preferably all carry out in power consumption and the lower pipe bundle drier of hear rate.Pipebundledrier is indirect contact drier, it utilizes heat transfer and heat radiation principle, steam is transmitted to heat by heat exchange tube wall the material to be dried of opposite side, is stirred and promote by the shovel board on pipe, material is moved to discharge end by feed end, discharges through discharging opening; Moisture after vaporization is discharged by blower fan, thus completes dry run.In the actual production of DDGS feed, pipe bundle drier feed water content preferably remains on certain limit, to avoid occurring to stick with paste pipe phenomenon.
For the ease of operation and the transfer time of reducing the first material and the second material as far as possible, according to one of the present invention preferred embodiment, as shown in Figure 3, it is made to join end to end by auger two pipe bundle driers, that is, the discharging opening being used for the first pipe bundle drier of the first drying is connected by the charging aperture of auger with the second pipe bundle drier being used for the second drying.The discharging opening of the second pipe bundle drier is connected with cyclone dust collectors, and described cyclone dust collectors are connected with packing shop by air delivery pipe.
Concrete, see Fig. 3, in the process of drying, first DDG is delivered in the first pipe bundle drier 2 through the first pipe bundle drier charging aperture 1, and carry out back-mixing (when equipment just starts can not back-mixing or provide the first desciccate to carry out back-mixing by other equipment) with preferred proportion in the present invention by the back-mixing part 3 of the first pipe bundle drier and the first desciccate, then carry out the first drying steps and obtain the first desciccate.And the first desciccate is delivered in the second pipe bundle drier 6 by the auger coupling part 4 of the first pipe bundle drier and the second pipe bundle drier, by the back-mixing part 7 of the interpolation shower nozzle 5 and the second pipe bundle drier that are connected to the DDS on auger, the dried material of the first desciccate with DDS and the second drying steps gained is mixed with the preferred ratio of the present invention in the process of conveying, and the second drying steps is carried out in the second pipe bundle drier 6, product after second drying steps, also namely DDGS discharges from the discharging opening 8 of the second pipe bundle drier, thus prepare DDGS.The DDGS of preparation is delivered to packing shop by the discharging opening of cyclone dust collectors through air delivery pipe and packs.
According to the present invention, described in the first drying steps or the second drying steps for the first desciccate of back-mixing and the second desciccate, can be provided by existing first desciccate or the second desciccate when equipment brings into operation, when equipment stable operation, can be provided by the first desciccate of self output or the second desciccate.
In above-mentioned further preferred embodiment, the heat transfer area for the first pipe bundle drier and the second pipe bundle drier is 1200-1800m
2, electric current is 80-200A; The blade diameter of auger is 450-550mm, and auger motor is the level Four roller of 18-19KW, and its decelerator model is BWD6-23-185; Cyclone dust collectors diameter is 450-500mm, and gas speed is 13-15m/s, and resistance reduces to 1000-1020p.s, and process air quantity is 1400-1600m
3/ h.
Below will be described the present invention by embodiment.In following examples and comparative example:
First pipe bundle drier and the second pipe bundle drier are all purchased from the dry concentrator Co., Ltd of Yixing, Jiangsu Province Grant, and model is GZG1500, and heat transfer area is 1500m
2, electric current is 80 ~ 200A;
Be 500mm for connecting the packing auger blade diameter of the first pipe bundle drier and the second pipe bundle drier, motor is the level Four roller of 18.5KW, and its decelerator is purchased from Electromechanical Technology Co., Ltd on Shanghai ten thousand, and model is BWD6-23-185:
Cyclone dust collectors, diameter is 488mm, gas speed: 14m/s, resistance drop: 1011p.s, process air quantity: 1500m
3/ h;
Evaporation concentrator is purchased from the dry concentrator Co., Ltd of Yixing, Jiangsu Province Grant;
The measuring method of DDGS color:
In order to reduce objective condition, such as, the impact that the difference, the difference of direction of observation, the difference of size etc. of the difference of light source, the difference of background, observer judge DDGS color, adopts the digital method expressing color of International Commission on Illumination (CIE), L*a*b colour space method.The L*a*b colour space (also referred to as CIELAB) is one of colour space of the most general current measurement object color, is formulated in 1976 by CIE.Wherein L* represents brightness (0≤L≤100), a* and b* is chromaticity coordinate (-60≤a, b≤60).In chromaticity coordinate ,+a* represents red direction, and-a* represents green direction; + b* represents yellow direction, and-b* represents blue direction.Measuring instrument adopts Konica Minolta CM-700d portable colorimeter, carries out color quantizing measurement to the DDGS of different quality, wherein, and L value and b value is larger, a value is less shows that product color is better;
In all materials, the mensuration of moisture is carried out according to GB6435;
In the mensuration of the nutritional labeling in DDGS:
Adopt the method for GB/T6432 to measure the content of crude protein, content is higher shows that quality is better,
Adopt the method for GB/T6433 to measure the content of crude fat, content is higher shows that quality is better,
Adopt the method for GB/T6434 to measure coarse-fibred content, content is lower shows that quality is better,
Adopt the method for GB/T6438 to measure the content of coarse ash, content is lower shows that quality is better.
Embodiment 1
The present embodiment is for illustration of the production method of vinasse protein feed provided by the invention.
First drying steps:
By water content be 72 % by weight wet vinasse carry out predrying, the water content being dried to wet vinasse is 39.5 % by weight, obtains the first material.And be delivered in the first pipe bundle drier 2 by the charging aperture 1 of the first pipe bundle drier and carry out first dry, the condition of the first drying comprises: temperature is 160 DEG C, and the time is 3min, obtains the first desciccate that water content is 12 % by weight.
Second drying steps:
Be 50 % by weight by DDS pre-concentration water content extremely by the DDS(of first desciccate of 20 % by weight and water content 50 % by weight in evaporation concentrator) be mixed to get the second material, and by the auger coupling part 4 of the first pipe bundle drier and the second pipe bundle drier be delivered in the second pipe bundle drier 6 carry out second dry.The ratio of mixing makes the water content of the second material be 38 % by weight.The condition of the second drying comprises: temperature is 165 DEG C, and the time is 3.5min, obtains the second desciccate that water content is 10 % by weight, i.e. DDGS.
Record the energy consumption in whole process and production capacity, and measure the content (the results are shown in Table 2) of crude protein, crude fibre and coarse ash in the color (the results are shown in Table 1) of DDGS feed and DDGS, gained DDGS color is similar to Example 2.
Embodiment 2
The present embodiment is for illustration of the production method of vinasse protein feed provided by the invention.
First drying steps:
By water content be 72 % by weight wet vinasse and the first desciccate of water content 12 % by weight of preparing of embodiment 1 first drying steps mixed by the back-mixing part 3 of the first pipe bundle drier, obtain the first material, with the described wet vinasse of 100 weight portions for benchmark, the consumption of described first desciccate is 115 weight portions, and after mixing, the water content of the first material is 40 % by weight.And be delivered in the first pipe bundle drier 2 by the charging aperture 1 of the first pipe bundle drier and carry out first dry, the condition of the first drying comprises: temperature is 160 DEG C, and the time is 3min, obtains the first desciccate that water content is 12 % by weight.
Second drying steps:
First desciccate of 20 % by weight and DDS and the second drying steps gained dried material are mixed to get the second material, and by the auger coupling part 4 of the first pipe bundle drier and the second pipe bundle drier be delivered in the second pipe bundle drier 6 carry out second dry.Wherein, be blended in described in the process of conveying by be connected to back-mixing part 7 that DDS on auger adds shower nozzle 5 and the second pipe bundle drier be the DDS of 80 % by weight and the water content of embodiment 1 second drying steps gained by the first desciccate and water content be 10 % by weight dried material carry out.Wherein, relative to the second material of 100 weight portions, the addition of the second drying steps gained dried material is 10 weight portions.The ratio of mixing makes the water content of the second material be 38 % by weight.The condition of the second drying comprises: temperature is 165 DEG C, and the time is 3.5min, obtains the second desciccate that water content is 10 % by weight, i.e. DDGS.
The DDGS of about 67 % by weight is delivered to packing shop by the second pipe bundle drier discharging 8 through air delivery pipe, and back-mixing is carried out in the porch that the DDGS of about 33 % by weight gets back to the second pipe bundle drier through the back-mixing part 7 of the second pipe bundle drier.Energy consumption after record stable operation in whole process and production capacity, and the content (the results are shown in Table 2) measuring crude protein, crude fat, crude fibre and coarse ash in the color (the results are shown in Table 1) of DDGS feed and DDGS, Fig. 1 is shown in by the picture of gained DDGS.
Embodiment 3
The present embodiment is for illustration of the production method of vinasse protein feed provided by the invention.
First drying steps:
By water content be 70 % by weight wet vinasse and the first desciccate of water content 12 % by weight of preparing of embodiment 1 first drying steps mixed by the back-mixing part 3 of the first pipe bundle drier, obtain the first material, with the described wet vinasse of 100 weight portions for benchmark, the consumption of described first desciccate is 150 weight portions, and after mixing, the water content of the first material is 35 % by weight.And be delivered in the first pipe bundle drier 2 by the charging aperture 1 of the first pipe bundle drier and carry out first dry, the condition of the first drying comprises: temperature is 170 DEG C, and the time is 4min, obtains the first desciccate that water content is 7 % by weight.The first desciccate that the material of this step back-mixing part is 7 % by weight by the water content obtained after stable operation provides, and the ratio of mixing makes the water content of the first material be 35 % by weight.
Second drying steps:
First desciccate of 20 % by weight and DDS and the second drying steps gained dried material are mixed to get the second material, and by the auger coupling part 4 of the first pipe bundle drier and the second pipe bundle drier be delivered in the second pipe bundle drier 6 carry out second dry.Wherein, be blended in described in the process of conveying by be connected to back-mixing part 7 that DDS on auger adds shower nozzle 5 and the second pipe bundle drier be the DDS of 78 % by weight and the water content of embodiment 1 second drying steps gained by the first desciccate and water content be 10 % by weight dried material carry out.Wherein, relative to the second material of 100 weight portions, the addition of the second drying steps gained dried material is 12 weight portions.The ratio of mixing makes the water content of the second material be 35 % by weight.The condition of the second drying comprises: temperature is 170 DEG C, and the time is 4min, obtains the second desciccate that water content is 7 % by weight, i.e. DDGS.The second desciccate that the material of this step back-mixing part is 7 % by weight by the water content obtained after stable operation provides, and the ratio of mixing makes the water content of the second material be 35 % by weight.
The DDGS of about 67 % by weight is delivered to packing shop by the second pipe bundle drier discharging 8 through air delivery pipe, and back-mixing is carried out in the porch that the DDGS of about 33 % by weight gets back to the second pipe bundle drier through the back-mixing part 7 of the second pipe bundle drier.Energy consumption after record stable operation in whole process and production capacity, and the content (the results are shown in Table 2) measuring crude protein, crude fat, crude fibre and coarse ash in the color (the results are shown in Table 1) of DDGS feed and DDGS, gained DDGS color is similar to Example 2.
Embodiment 4
The present embodiment is for illustration of the production method of vinasse protein feed provided by the invention.
First drying steps:
By water content be 68 % by weight wet vinasse and the first desciccate of water content 12 % by weight of preparing of embodiment 1 first drying steps mixed by the back-mixing part 3 of the first pipe bundle drier, obtain the first material, with the described wet vinasse of 100 weight portions for benchmark, the consumption of described first desciccate is 125 weight portions, and after mixing, the water content of the first material is 37 % by weight.And be delivered in the first pipe bundle drier 2 by the charging aperture 1 of the first pipe bundle drier and carry out first dry, the condition of the first drying comprises: temperature is 165 DEG C, and the time is 3.5min, obtains the first desciccate that water content is 9 % by weight.The first desciccate that the material of this step back-mixing part is 9 % by weight by the water content obtained after stable operation provides, and the ratio of mixing makes the water content of the first material be 37 % by weight.
Second drying steps:
First desciccate of 20 % by weight and DDS and the second drying steps gained dried material are mixed to get the second material, and by the auger coupling part 4 of the first pipe bundle drier and the second pipe bundle drier be delivered in the second pipe bundle drier 6 carry out second dry.Wherein, be blended in described in the process of conveying by be connected to back-mixing part 7 that DDS on auger adds shower nozzle 5 and the second pipe bundle drier be the DDS of 77 % by weight and the water content of embodiment 1 second drying steps gained by the first desciccate and water content be 10 % by weight dried material carry out.Wherein, relative to the second material of 100 weight portions, the addition of the second drying steps gained dried material is 8 % by weight.The ratio of mixing makes the water content of the second material be 39 % by weight.The condition of the second drying comprises: temperature is 160 DEG C, and the time is 3min, obtains the second desciccate that water content is 11.5 % by weight, i.e. DDGS.The second desciccate that the material of this step back-mixing part is 11.5 % by weight by the water content obtained after stable operation provides, and the ratio of mixing makes the water content of the first material be 39 % by weight.
The DDGS of about 67 % by weight is delivered to packing shop by the second pipe bundle drier discharging 8 through air delivery pipe, and back-mixing is carried out in the porch that the DDGS of about 33 % by weight gets back to the second pipe bundle drier through the back-mixing part 7 of the second pipe bundle drier.Energy consumption after record stable operation in whole process and production capacity, and the content (the results are shown in Table 2) measuring crude protein, crude fat, crude fibre and coarse ash in the color (the results are shown in Table 1) of DDGS feed and DDGS, gained DDGS color is similar to Example 2.
Embodiment 5
The present embodiment is for illustration of the production method of vinasse protein feed provided by the invention.
The production of vinasse protein feed is carried out according to the method for embodiment 2, unlike: in the second drying steps, the second desciccate and the first desciccate are not carried out back-mixing, but the water content directly the first desciccate and DDS being mixed to the second material is 38 % by weight.Record the energy consumption in whole process and production capacity, and measure the content (the results are shown in Table 2) of crude protein, crude fat, crude fibre and the coarse ash in the color (the results are shown in Table 1) of DDGS feed and DDGS, gained DDGS color is similar to Example 2.
Comparative example 1
The production method of the vinasse protein feed that this comparative example provides for illustration of prior art.
This comparative example adopts a step seasoning to carry out the production of DDGS feed.Also be, be the wet vinasse of 72 % by weight by water content, water content be 80 % by weight DDS and water content be 10 % by weight the second desciccate mix according to the amount ratio in embodiment 2, then drying is carried out, dry temperature is 165 DEG C, and the dry time makes the water content of the DDGS obtained be 10 % by weight.Record the energy consumption in whole process and production capacity, and measure the content (the results are shown in Table 2) of crude protein, crude fat, crude fibre and coarse ash in the color (the results are shown in Table 1) of DDGS feed and DDGS, Fig. 2 is shown in by the picture of gained DDGS.
Table 1
Remarks, 2 ° refer to angle standard observer; D65 refers to standard sources D65(daylight, colour temperature: 6540k)
Table 2
By upper table 1 and 2 and Fig. 1 and Fig. 2 can find out, the color of the DDGS adopting technical method of the present invention to produce, for golden yellow, is obviously better than the DDGS that comparative example 1 is produced, and can take into account the quality of energy consumption, production capacity and final DDGS simultaneously.By embodiment 2 is compared with embodiment 1 can find out with embodiment 5, adopt the preferred method of the present invention can reduce energy consumption further, improve the quality of final gained DDGS.Further, the present invention preferably carries out the production of DDGS in the pipe bundle drier that power consumption is lower, while ensuring the quality of products, reduce further production cost.
Further, the present invention preferably carries out drying in tube bank drier, compares with drum-type drying with ring type drying, on the basis ensureing DDGS color and luster and nutritional labeling, significantly can reduce production cost.
More than describe the preferred embodiment of the present invention in detail; but the present invention is not limited to the detail in above-mentioned embodiment, within the scope of technical conceive of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.
It should be noted that in addition, each the concrete technical characteristic described in above-mentioned detailed description of the invention, in reconcilable situation, can be combined by any suitable mode.In order to avoid unnecessary repetition, the present invention illustrates no longer separately to various possible combination.
In addition, also can be combined between various different embodiment of the present invention, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (10)
1. the production method of a vinasse protein feed, the method comprises the first drying steps and the second drying steps that carry out successively, described first drying steps is used for carrying out drying to the first material containing wet vinasse, obtain the first desciccate, described second drying steps is used for carrying out drying to the second material, and described second material contains described first desciccate and solubility syrup.
2. method according to claim 1, wherein, described wet vinasse are solid content alcohol fermentation liquid being distilled out alcohol and obtains after carrying out Separation of Solid and Liquid, and described solubility syrup is the concentrate of clear liquid alcohol fermentation liquid being distilled out alcohol and obtains after carrying out Separation of Solid and Liquid.
3. method according to claim 1 and 2, wherein, the water content of described wet vinasse is 30-72 % by weight; The water content of the first material is 30-45 % by weight.
4. according to the method in claim 1-3 described in any one, wherein, the water content of described wet vinasse is 68-72 % by weight, and described first material is also containing described first desciccate, relative to the described wet vinasse of 100 weight portions, the content of described first desciccate is 115-150 weight portion.
5. according to the method in claim 1-4 described in any one, wherein, the first drying steps is 160-170 DEG C in temperature, and the time is carry out under the condition of 3-10min.
6. according to the method in claim 1-5 described in any one, wherein, the water content of described solubility syrup is 50-85 % by weight, and the water content of described second material is 30-45 % by weight, is preferably 35-40 % by weight.
7. according to the method in claim 1-6 described in any one, wherein, the water content of described solubility syrup is 77-80 % by weight, the dried material of described second material also containing described second drying steps gained, relative to the second material of 100 weight portions, the content of the dried material of described second drying steps gained is 8-12 weight portion.
8. according to the method in claim 1-7 described in any one, wherein, the second drying steps is 160-170 DEG C in temperature, and the time is carry out under the condition of 3-10min.
9. method according to claim 1, wherein, described first drying steps and the second drying steps all carry out in pipe bundle drier.
10. the vinasse protein feed that the method in claim 1-9 described in any one is produced.
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| CN109566851A (en) * | 2018-12-22 | 2019-04-05 | 河南飞天农业开发股份有限公司 | A kind of preparation method of plant compound protein |
| CN112998131A (en) * | 2021-04-07 | 2021-06-22 | 南京理工大学 | Method for improving color of corn ethanol process byproduct DDGS |
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