CN115029388A - Method for co-producing ethanol and DDGS (distillers dried grains with soluble) by fermenting raw materials with wheat - Google Patents

Method for co-producing ethanol and DDGS (distillers dried grains with soluble) by fermenting raw materials with wheat Download PDF

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Publication number
CN115029388A
CN115029388A CN202110254695.6A CN202110254695A CN115029388A CN 115029388 A CN115029388 A CN 115029388A CN 202110254695 A CN202110254695 A CN 202110254695A CN 115029388 A CN115029388 A CN 115029388A
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China
Prior art keywords
wheat
mash
fermentation
ethanol
slurry
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Chinese (zh)
Inventor
林海龙
俞建良
刘晓峰
刘劲松
严明奕
熊强
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Meihekou Fukang Alcohol Co ltd
Sdic Biotechnology Investment Co ltd
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Meihekou Fukang Alcohol Co ltd
Sdic Biotechnology Investment Co ltd
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Priority to CN202110254695.6A priority Critical patent/CN115029388A/en
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    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P7/00—Preparation of oxygen-containing organic compounds
    • C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
    • C12P7/04—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic
    • C12P7/06—Ethanol, i.e. non-beverage
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23K—FODDER
    • A23K10/00—Animal feeding-stuffs
    • A23K10/30—Animal feeding-stuffs from material of plant origin, e.g. roots, seeds or hay; from material of fungal origin, e.g. mushrooms
    • A23K10/37—Animal feeding-stuffs from material of plant origin, e.g. roots, seeds or hay; from material of fungal origin, e.g. mushrooms from waste material
    • A23K10/38—Animal feeding-stuffs from material of plant origin, e.g. roots, seeds or hay; from material of fungal origin, e.g. mushrooms from waste material from distillers' or brewers' waste
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23K—FODDER
    • A23K20/00—Accessory food factors for animal feeding-stuffs
    • A23K20/10—Organic substances
    • A23K20/142—Amino acids; Derivatives thereof
    • A23K20/147—Polymeric derivatives, e.g. peptides or proteins
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P60/00—Technologies relating to agriculture, livestock or agroalimentary industries
    • Y02P60/80—Food processing, e.g. use of renewable energies or variable speed drives in handling, conveying or stacking
    • Y02P60/87—Re-use of by-products of food processing for fodder production

Abstract

The invention relates to the field of ethanol preparation, and in particular relates to a method for co-producing ethanol and DDGS feed by using wheat to perform raw material fermentation. The method comprises the following steps: mixing a mixed raw material containing the crushed products of the hulled wheat and other starchy raw materials with ingredient water, and pulping to obtain a powder pulp; optionally, adding a liquefying enzyme to the powder slurry to obtain liquefied mash; adding saccharifying enzyme and inoculating yeast into the powder slurry or the liquefied mash for fermentation to obtain fermentation liquor containing ethanol; distilling the fermentation liquor containing ethanol to obtain ethanol and waste mash, adding a carrier into the waste mash, and carrying out solid-liquid separation to obtain wet distiller grains and clear liquid; and concentrating the clear liquid to obtain concentrated clear liquid, and mixing the concentrated clear liquid and the wet distiller grains to prepare the DDGS feed. The invention can not cause the blockage of equipment or pipelines, improves the production efficiency of the device, increases the yield of the DDGS feed by using the carrier when producing the DDGS feed, and further solves the problems of high energy consumption and high cost of distillers' grains water evaporation and concentration.

Description

Method for co-producing ethanol and DDGS (distillers dried grains with soluble) by fermenting raw materials with wheat
Technical Field
The invention relates to the field of ethanol preparation, and in particular relates to a method for co-producing ethanol and DDGS (distillers dried grains with soluble) by using wheat to perform raw material fermentation.
Background
At present, almost all domestic production processes of alcohol plants comprise raw material crushing, size mixing, liquefaction, saccharification, fermentation, distillation and vinasse drying, and the final products are alcohol and DDGS. The specific process flow is shown in figure 1.
However, in the production of ethanol from wheat, because wheat is rich in gluten (usually 10-14% by weight of wheat), if gluten is not extracted before fermentation and the ethanol fermentation is directly performed, the high gluten content in the mash can block equipment such as process pipelines and hydrothermal injectors, and the production is unstable. Therefore, in the enterprise producing alcohol by using wheat as a raw material, wheat gluten is usually extracted after being crushed, and then the remaining starch is used as a raw material for alcohol production, so that three products, namely wheat gluten, alcohol and DDGS feed (containing yeast protein), are finally obtained. However, the enterprise that does not use wheat as the main alcohol production raw material will undoubtedly mean to adjust the alcohol production device and increase the production cost.
CN110468161A discloses a method for preparing ethanol by fermenting raw material with wheat as raw material, which can alleviate the problem of equipment blockage to some extent, but has low production efficiency and high energy consumption.
Disclosure of Invention
In order to overcome the problems in the prior art, the invention provides a method for co-producing ethanol and DDGS by fermenting raw materials with wheat.
In order to achieve the above object, the present invention provides a method for co-producing ethanol and DDGS by raw material fermentation using wheat, the method comprising:
(1) mixing a mixed raw material containing a pulverized product of dehulled wheat and a pulverized product of rice with ingredient water to perform size mixing to obtain a flour paste;
(2) optionally, adding a liquefying enzyme into the slurry, and liquefying the slurry to obtain liquefied mash;
(3) adding saccharifying enzyme and inoculating yeast into the powder slurry or the liquefied mash for fermentation to obtain fermentation liquor containing ethanol;
(4) distilling the fermentation liquor containing the ethanol to obtain ethanol and waste mash, then adding a carrier into the waste mash, and carrying out solid-liquid separation to obtain wet distiller grains and clear liquid;
(5) concentrating the clear liquid to obtain concentrated clear liquid, mixing the concentrated clear liquid with the wet distiller grains, and drying to obtain DDGS feed;
wherein the carrier is a plant-derived raw material.
By the technical scheme of the invention, the following beneficial effects can be obtained:
(1) the method of the invention uses wheat raw material to be hulled and uses rice as alcohol fermentation raw material to ferment raw material, so that the existing alcohol production device can be used for producing alcohol by using wheat as raw material, and the blockage of equipment or pipelines can not be caused;
(2) the amino acid composition in the wheat gluten is unbalanced, the problem is solved to a certain extent by adding rice for fermentation, and other different hulled grains can be flexibly prepared by technical personnel in the field according to the matching requirement of nutrient components in the byproduct feed;
(3) in the process of producing the DDGS feed, the method of the invention uses the carrier from plant source, thereby not only fully utilizing the carrier, increasing the yield of the DDGS feed, meeting the requirements of protein and fiber in the feed, but also relatively reducing the amount of clear liquid, and further solving the problem of high energy consumption of evaporation and concentration of the distillers' grains water.
(4) The invention takes the hulled grains as the raw material, on one hand, the amount of the liquid preparation water used by the hulls is reduced, and on the other hand, the heat consumed by heating the distribution water is reduced; on the other hand, as the hulled grains are used, the utilization rate of the equipment is improved, and the production efficiency of the equipment is improved.
Drawings
FIG. 1 is a flow diagram of a prior art alcohol production process;
FIG. 2 is a flow chart of the alcohol production process provided by the present invention.
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
The invention provides a method for co-producing ethanol and DDGS by fermenting raw materials with wheat, which comprises the following steps:
(1) mixing a mixed raw material containing a pulverized product of dehulled wheat and a pulverized product of rice with ingredient water to perform size mixing to obtain a flour paste;
(2) optionally, adding a liquefying enzyme into the slurry, and liquefying the slurry to obtain liquefied mash;
(3) adding saccharifying enzyme and inoculating yeast into the powder slurry or the liquefied mash for fermentation to obtain fermentation liquor containing ethanol;
(4) distilling the fermentation liquor containing ethanol to obtain ethanol and waste mash, then adding a carrier into the waste mash, and carrying out solid-liquid separation to obtain wet distiller grains and clear liquid;
(5) concentrating the clear liquid to obtain concentrated clear liquid, mixing the concentrated clear liquid with the wet distiller grains, and drying to obtain DDGS feed;
wherein the carrier is a plant-derived raw material.
According to the present invention, the term "raw fermentation" refers to a process for the production of alcohol by the co-action of raw starch hydrolyzing enzymes with yeast on starchy materials at a temperature below the gelatinization temperature of the starch.
Step (1)
As will be understood by those skilled in the art, rice is a product made by cleaning, hulling, milling and the like, and is in a hulled state. That is, the raw materials used in the present invention are all raw materials without shells.
Although the above object can be achieved by husking wheat and mixing it with rice to perform raw material fermentation, and then introducing the plant-derived carrier before the subsequent solid-liquid separation, the amount of each raw material can be changed within a wide range. Preferably, the milled wheat product of the dehulled wheat is contained in the starting material mixture in an amount of 20 wt% or more, preferably 20 to 70 wt%, for example 20 wt%, 25 wt%, 30 wt%, 35 wt%, 40 wt%, 45 wt%, 50 wt%, 55 wt%, 60 wt%, 65 wt%, 70 wt%, more preferably 30 to 50 wt%.
The method of pulverizing wheat and rice to obtain a corresponding pulverized product is not particularly limited, and may be any of various pulverization methods commonly used in the art, and in order to improve the effect of the subsequent treatment, the pulverization method preferably includes pulverizing the material obtained by the impurity removal treatment and sieving the pulverized material through a 20-mesh sieve, preferably so that at least 85%, more preferably 95%, of the pulverized product (pulverized product of wheat, pulverized product of rice) can pass through the 20-mesh sieve.
The method of the impurity removal treatment is not particularly limited, and various methods of the impurity removal treatment commonly used in the art may be used, and for example, the method may include removing impurities such as stones, iron pieces, and woven fabrics from the respective raw materials. According to a particular embodiment of the invention, the raw materials are sieved, the mesh having such a pore size that the small-particle size raw materials with impurities are sieved off, while the large-particle size raw materials remain on the sieve. And then, removing impurities from the undersize product, mixing the undersize product with the oversize product, and crushing the obtained mixed material serving as the material obtained by impurity removal treatment.
According to the present invention, there is no particular limitation on how the mixed raw material is obtained, and the mixed raw material may be obtained by pulverizing dehulled wheat and rice separately and then mixing them, or may be obtained by mixing dehulled wheat and rice and then pulverizing them.
According to the invention, the pulp mixing mode comprises the following steps: and preparing the mixed raw materials into starch slurry, namely powder slurry by using ingredient water. In the present invention, the ratio of the slurry in the slurry mixing step can be selected in a wide range, and preferably, the ratio of the slurry in the slurry mixing step is 1:1.3-4, for example, 1:1.3, 1:1.8, 1:2, 1:2.3, 1:2.5, 1:2.8, 1:3.5, 1:4, preferably 1: 2-3.
According to the present invention, the temperature of the slurry is preferably 30 to 70 ℃, and may be any value within the range of 30 ℃, 35 ℃, 40 ℃, 45 ℃, 50 ℃, 55 ℃, 57 ℃, 58 ℃, 59 ℃, 60 ℃, 61 ℃, 62 ℃, 63 ℃, 65 ℃, 70 ℃ and any two points, more preferably 55 to 65 ℃, and still more preferably 57 to 63 ℃.
According to the invention, the pH of the slip is preferably 4 to 5.5, and may be, for example, 4, 4.2, 4.4, 4.6, 4.8, 5, 5.2, 5.4, 5.5.
According to the present invention, in order to further overcome the problem of the imbalance of the amino acid composition in the wheat gluten, it is preferable that the mixed raw material may further contain pulverized products of other starchy raw materials (pulverized products of other grains which are dehulled) conventionally used in the field of ethanol production by fermentation, for example, corn, tapioca and sorghum, according to the need.
The method for obtaining the corresponding crushed product from the other grains after husking is not particularly limited, and may be various crushing treatment methods commonly used in the art, and in order to improve the effect of the subsequent treatment, the crushing treatment method preferably includes crushing the material obtained by impurity removal treatment and sieving the crushed material through a 20-mesh sieve, and preferably allows at least 85%, preferably at least 95%, of the crushed product to pass through the 20-mesh sieve.
The method of the impurity removal treatment is not particularly limited, and various methods of the impurity removal treatment commonly used in the art may be used, and for example, the method may include removing impurities such as stones, iron pieces, and woven fabrics from the respective raw materials. According to a particular embodiment of the invention, the raw materials are sieved, the mesh having such a pore size that the small-particle size raw materials with impurities are sieved off, while the large-particle size raw materials remain on the sieve. And then, removing impurities from the undersize product, mixing the undersize product with the oversize product, and crushing the obtained mixed material serving as the material obtained by impurity removal treatment.
According to the present invention, the mode of how to obtain the mixed raw material is not particularly limited, and the mixed raw material may be obtained by pulverizing dehulled wheat, rice and dehulled other grains, respectively, and then mixing them, or may be obtained by mixing dehulled wheat, rice and dehulled other grains, and then pulverizing them.
According to the present invention, it is understood that the terms "wheat", "maize", "cassava" and "sorghum" do not refer to the whole plant itself, but to the parts or organs thereof having a high starch content, i.e. wheat seeds, maize seeds, cassava tubers, sorghum seeds.
Step (2)
According to a preferred embodiment of the invention, the method comprises: and adding a liquefying enzyme into the slurry to liquefy the slurry. Preferably, the liquefying enzyme is an amylase, and the amylase used is a variety of amylases known in the art, for example, a fungal amylase, preferably an acid fungal amylase, which is commercially available, for example, from dupont under the product designation GC 626.
According to the invention, the amount of amylase used may vary within wide limits, preferably the amount of amylase used is 2-200U, more preferably 4-50U, e.g. 4U, 5U, 6U, 7U, 8U, 9U, 10U, 15U, 20U, 25U, 30U, 35U, 40U, 45U, 50U and any value within the range of any two points per gram of dry weight of the starch slurry.
According to the present invention, in order to further enhance the effect of the present invention, it is preferable that the liquefying enzyme further contains an acid protease, xylanase and pectinase.
According to the present invention, the acidic protease may be any acidic protease conventional in the art, and the amount may be selected from a wide range, and preferably, the amount of the acidic protease is 2-100U, more preferably 10-50U, for example, 10U, 15U, 20U, 25U, 30U, 35U, 40U, 45U, 50U, and any value within the range of any two points, relative to dry weight of the powder slurry per gram. It can be obtained commercially, for example, as an acid protease available from DuPont under the trade name Fermgen 2.5.
According to the invention, the xylanase may be any xylanase conventional in the art, and may be used in a wide range, preferably in an amount of 0.1-10U, more preferably 0.2-2U, e.g. 0.2U, 0.3U, 0.4U, 0.5U, 0.6U, 0.7U, 0.8U, 0.9U, 1U, 1.2U, 1.3U, 1.4U, 1.5U, 1.6U, 1.7U, 1.8U, 1.9U, 2U and any value within the range of any two points of composition per gram of the mash on a dry weight basis. It can be obtained commercially, for example, as a xylanase available from DuPont under the trade designation OPTIMASH BG.
According to the invention, the pectinase may be any pectinase conventional in the art, and the amount may be selected within the range that is preferred, preferably 0.1-2U, more preferably 0.2-1U, per gram dry weight of the mash, e.g. 0.2U, 0.4U, 0.6U, 0.8U, 1U and any value within the range between any two points. It can be obtained commercially, for example, as acid pectinase (30000U/ml activity specification) available from Shandong Longong Biotech, Inc.
According to the present invention, the above-mentioned liquefying enzymes may be added to the slurry individually, and the order of addition is not limited, or the enzymes may be added to the slurry after mixing them together in a predetermined amount.
According to the present invention, the liquefaction temperature may be a starch liquefaction temperature in conventional raw meal fermentation, and preferably, the liquefaction temperature is 35 to 67 ℃, for example, 35 ℃, 40 ℃, 45 ℃, 50 ℃, 55 ℃, 57 ℃, 58 ℃, 59 ℃, 60 ℃, 61 ℃, 62 ℃, 63 ℃, 65 ℃, 67 ℃ or any value in a range of two points, more preferably 55 to 65 ℃, and still more preferably 57 to 63 ℃.
According to the invention, the pH of the liquefaction may be the pH conventionally used in fermentation of the feedstock, preferably the pH is 4-5.5, e.g. 4, 4.2, 4.4, 4.6, 4.8, 4.9, 5, 5.5 and any value within the range of any two points, more preferably the pH is 4.6-5.5, even more preferably 4.8-5.5.
According to the present invention, the time for liquefaction is preferably 0.5 to 3 hours, and for example, may be 0.5 hour, 1 hour, 1.5 hours, 2 hours, 2.5 hours, 3 hours, and more preferably 1.5 to 2.5 hours.
According to the present invention, in order to further promote the fermentation performance, preferably, the method further comprises adding a bacteriostatic agent to the powder slurry, wherein the bacteriostatic agent is not particularly limited, and can be various bacteriostatic agents commonly used in the art, and preferably, the bacteriostatic agent is one or more of virginiamycin, ansamicin and bleaching powder, and more preferably ansamicin.
The dosage of the bacteriostatic agent in the slurry can be changed in a wide range, and preferably, the addition amount of the bacteriostatic agent enables the concentration of the bacteriostatic agent in the slurry to be 2.5-20 ppm.
According to the invention, after liquefaction, the method of the invention further comprises reducing the temperature of the resulting liquefied mash to 25-40 ℃ to facilitate subsequent saccharification or fermentation.
Step (3)
The present invention may be a method of saccharifying a liquefied mash by adding a saccharifying enzyme to the liquefied mash and then holding the mixture for a certain period of time, or a method of fermenting while saccharifying by adding a saccharifying enzyme and yeast simultaneously, wherein the amount of the saccharifying enzyme is not particularly limited and may be an amount commonly used in the art. Preferably, the saccharifying enzyme is used in an amount of 50 to 5000U, more preferably 200-1500U, for example, 200U, 300U, 400U, 500U, 600U, 700U, 800U, 900U, 1000U, 1100U, 1200U, 1300U, 1400U, 1500U, and any value within the range of any two points per gram of the liquefied mash on a dry weight basis.
The saccharifying enzyme is also called glucosidase, and acts on the non-reducing end of the starch molecule, takes glucose as a unit, and sequentially acts on alpha-1, 4-glycosidic bonds in the starch molecule to generate glucose. It also hydrolyzes the alpha-1, 6-glycosidic bond of the maltose and amylopectin branch points to yield glucose. The enzyme producing strain is mainly Aspergillus niger (left Aspergillus, Aspergillus awamori), Rhizopus (Rhizopus niveus, Rhizopus delemar), Neurospora sp, and Monascus ruber. According to a specific embodiment of the invention, the gene encoding the saccharifying enzyme is derived from Aspergillus niger, which is commercially available, e.g.under the reference Stargen002 from DuPont.
According to the present invention, in order to further improve fermentation performance and reduce the addition of nitrogen source during fermentation, it is preferable that the method of the present invention further comprises adding an acid protease to the liquefied mash.
According to the present invention, the acidic protease may be any acidic protease conventional in the art, and the amount may be selected from a wide range, and preferably, the amount of the acidic protease is 2-100U, more preferably 10-50U, for example, 10U, 15U, 20U, 25U, 30U, 35U, 40U, 45U, 50U, and any value within the range of any two points, per gram of the dry weight of the powder slurry. It can be obtained commercially, for example, as an acid protease available from DuPont under the trade name Fermgen 2.5.
According to the present invention, in order to further promote the performance of fermentation, it is preferable that the method further comprises adding a bacteriostatic agent to the liquefied mash, wherein the bacteriostatic agent is not particularly limited, and may be various bacteriostatic agents commonly used in the art, and preferably, the bacteriostatic agent is one or more of virginiamycin, penicillin, ansamicin and bleaching powder, and more preferably, ansamicin.
Wherein the amount of the bacteriostatic agent in the liquefied mash can be varied within a wide range, preferably, the bacteriostatic agent is added in an amount such that the concentration of the bacteriostatic agent in the liquefied mash is 2.5-20 ppm.
According to the present invention, in order to further improve the fermentation performance, it is preferable that the method of the present invention further comprises adding nutrients to the liquefied mash, wherein the nutrients include ammonia, urea, zinc sulfate, magnesium sulfate, etc.
Wherein the dosage of the nutrient in the liquefied mash can be changed in a wide range, and preferably, the addition amounts of the ammonia water, the urea, the zinc sulfate and the magnesium sulfate are respectively 6-24mmol/L, 0.8-10mmol/L, 0.2-2mmol/L and 2-20mmol/L in the liquefied mash.
According to the present invention, the step of fermentation may be accomplished by methods well known to those skilled in the art, including batch fermentation and continuous fermentation. Among them, microorganisms capable of fermenting monosaccharides such as glucose and/or fructose, and oligosaccharides such as sucrose and/or galactose can be used in the fermentation process of the present invention, and since Saccharomyces cerevisiae is an alcohol-tolerant, less by-products, and high ethanol yield-producing microorganism commonly used in the Saccharomyces cerevisiae industry, it is preferable that the yeast used in the fermentation is Saccharomyces cerevisiae.
The yeast used for fermentation can be a commercially available yeast solid preparation (such as dried yeast powder) or yeast strains, Angel super high-activity dry yeast for brewing wine (purchased from Angel yeast of Hubei), Farkai high-temperature-resistant high-activity dry yeast for wine, Lesfu dry yeast and the like.
The yeast may be inoculated by conventional methods, preferably, the yeast seed liquid is inoculated per ton of the liquefied mashThe amount of yeast is 0.1-0.5kg, wherein the density of yeast in the yeast seed solution can be (2.0-3.0) x 10 8 One per ml. The yeast can be added in the form of seed liquid, and the seed liquid can be water solution of dry yeast or culture liquid after culture expansion, or activated seed liquid of dry yeast or commercial strains. Wherein, the counting of the microzyme can be realized by taking a certain amount of seed liquid, diluting the seed liquid appropriately and then counting the seeds by a microscope.
The fermentation conditions may be any conditions suitable for yeast growth, preferably at a temperature of 26-38 deg.C, more preferably 28-36 deg.C, even more preferably 29-33 deg.C, and a pH of preferably 3-5, more preferably 3.8-4.5. The fermentation time may be from the start of inoculation to the appearance of the death phase of yeast growth (i.e., the fermentation time is lag phase, log phase plus stationary phase), preferably the fermentation time is from 24 to 100 hours, more preferably from 50 to 96 hours, and even more preferably from 64 to 86 hours.
According to the present invention, the distillation may be carried out by a method conventional in the art, for example, rough distillation and rectification, and the present invention will not be described herein.
According to the invention, the carrier is added into the waste mash to carry out solid-liquid separation, so that on one hand, the separation performance of the material is improved, and the energy consumption for separation is reduced; on the other hand, the addition of the carrier absorbs part of water in the waste mash, reduces the yield of the clear liquid and further reduces the energy consumption for concentrating the clear liquid; on the other hand, the added value of the DDGS feed is also increased.
According to the present invention, preferably, the plant-derived raw material is selected from the group consisting of, but not limited to, hulls of grains, meal of grains, and stalks of grains; more preferably, the plant-derived raw material is one or more of corn bran, rice hull bran powder, wheat bran, soybean meal, corn germ meal and straw powder.
According to a specific embodiment of the invention, the plant-derived raw material is rice hull bran powder.
According to a specific embodiment of the invention, the plant-derived raw material is a mixture of rice hull bran powder and wheat bran, and the weight ratio of the mixture is 1: 0.5-2.
According to a specific embodiment of the invention, the plant-derived raw material is a mixture of rice hull bran powder, wheat bran and corn germ meal, and the weight ratio of the mixture is 1:0.5-2: 0.5-2.
The amount of the carrier used according to the present invention may vary within a wide range, and preferably is 5 to 40% by weight, for example, 5%, 10%, 15%, 20%, 25%, 30%, 35%, 40%, and preferably 20 to 30% by weight, relative to 100 parts by weight of dehulled wheat.
According to the present invention, the water content of the wet distiller's grains obtained by solid-liquid separation of the mash may be 45-70 wt%. The solid-liquid separation method may be various solid-liquid separation methods known in the art, and for example, the method may be centrifugation or filtration, the centrifugation may be a horizontal screw centrifuge or a disc centrifuge, and the filtration may be plate-and-frame filtration.
According to the invention, the degree of concentration of the clear liquid can be selected within a wide range, taking into account the time of concentration, the time of subsequent drying and the energy consumption, and the filtrate is preferably concentrated to a moisture content of 65-72% by weight. Wherein the concentration may be an evaporation concentration, and the temperature of the concentration may be 50-80 ℃.
According to the present invention, the mixing ratio of the concentrated clear solution and the wet distillers grains can use the ratio used in the existing DDGS preparation method, but in order to further improve the color of the prepared DDGS feed, the mixing ratio of the concentrated filtrate and the filter residue is preferably such that the moisture content of the mixed material is 55-68 wt%.
The drying conditions may be those conventionally used in the art for preparing DDGS feeds, for example, the drying temperature may be 120 ℃ to 150 ℃ and the drying time is preferably such that the water content of the prepared DDGS feed is not higher than 12% by weight.
According to a particularly preferred embodiment of the invention, the method for the coproduction of ethanol and DDGS by fermentation of raw material from wheat comprises:
(1) according to weight, 45-55 wt% of hulled wheat and 45-55 wt% of rice are mixed and crushed together, and the 20-mesh screening rate of the crushed raw materials reaches over 95%.
(2) Mixing the pulverized raw materials with water, and making slurry, wherein the ratio of material to liquid is 1:1.8-2.2, the temperature of the prepared slurry is 57-60 deg.C, and the pH is 3.5-4.5.
(3) The powder slurry is pretreated, and the pretreatment method comprises the following steps: adding 8-12U of acid fungal amylase, 38-42U of acid protease, 0.35-0.45U of xylanase, 0.8-1.2U of pectinase, 4.5-5.5ppm of ansamicin and 0.4-0.6mmol/L of urea into the powder slurry per gram of dry weight, adjusting pH to 3.5-4.5, maintaining the temperature at 57-60 deg.C, stirring for 1.2-1.8 hr, and cooling to 30-35 deg.C to obtain liquefied mash.
(4) Adding 480-520U of Aspergillus niger saccharifying enzyme, 28-32U of acid protease and 4.5-5.5ppm of ansamitocin into the cooled liquefied mash per gram of the liquefied mash by dry weight, and adding 0.1-0.3kg/t of yeast seed liquid (the cell concentration of the yeast seed liquid is 2.5-3.0 hundred million/ml) into the saccharified mash; adjusting pH to 3.5-4, performing intermittent fermentation at 28-30 deg.C, and finishing fermentation after 85-87 hr.
(5) Feeding fermented liquor into a distillation system to obtain alcohol and waste liquor;
(6) adding rice hull bran powder (the adding amount of the rice hull bran powder is 18-22 parts by weight relative to 100 parts by weight of the waste mash), then filtering by a plate frame to obtain wet distiller grains with the water content of 65-75% by weight and clear liquid, concentrating the clear liquid at 60-80 ℃ until the water content is 70-75% by weight (recording evaporation energy consumption), mixing with the wet distiller grains after concentration, and then drying together by a dryer at the temperature of 115 ℃ and 125 ℃ until the water content is 10-12% by weight to obtain the DDGS.
The present invention will be described in detail below by way of examples.
The present invention will be described in detail below by way of examples. In the following examples:
the acid amylase is an acid fungal amylase available from dupont under GC 626.
The acid protease is an acid protease available from DuPont under the trade designation Fermgen 2.5.
The xylanase is a xylanase purchased from DuPont under the trade designation OPTIMASH BG.
The pectinase is a pectinase with activity specification of 30000U/ml, which is purchased from Shandong Longong Dabioengineering Co.
The Aspergillus niger glucoamylase is a glucoamylase with a Stargen002 designation from DuPont.
Saccharomyces cerevisiae (Angel super Saccharomyces cerevisiae high activity dry yeast) is available from Angel Yeast, Inc. of Hubei.
Production efficiency: feeding amount (ton) × starch content (%) × liquor yield (%)/fermentation period (h)/fermentation tank volume (m) 3 )。
Example 1
This example illustrates the present invention for producing ethanol by fermentation and DDGS production
(1) According to the weight, 30 weight percent of hulled wheat and 70 weight percent of rice are mixed and crushed together, and the 20-mesh screening rate of the crushed raw materials reaches over 95 percent.
(2) Mixing the pulverized raw materials with water, and making slurry, wherein the ratio of material to liquid is 1:2.4, the temperature of the prepared slurry is 60-63 ℃, and the pH value is 5.0.
(3) The powder slurry is pretreated, and the pretreatment method comprises the following steps: adding 20U of acid fungal amylase, 35U of acid protease, 1U of xylanase, 0.6U of pectinase and 10ppm of ansamicin into the powder slurry per gram of dry weight, adjusting the pH to 5.0, maintaining the temperature at about 60-63 ℃, stirring for 2.5 hours, and then cooling to 32 ℃ to obtain liquefied mash.
(4) Adding 1000U of Aspergillus niger glucoamylase, 35U of acid protease, 5ppm of ampelopsin and 3mmol/L of urea into the cooled liquefied mash per gram of the liquefied mash by dry weight, and adding 0.2kg/t of yeast seed liquid (the cell concentration of the yeast seed liquid is 2.5-3.0 hundred million/ml) into the liquefied mash; adjusting pH to about 4.0, performing intermittent fermentation at 31 deg.C, and finishing fermentation after 68 hr;
(5) feeding fermented liquor into a distillation system to obtain alcohol and waste liquor;
(6) adding rice hull bran powder (the adding amount of the rice hull bran powder is 25 parts by weight relative to 100 parts by weight of hulled wheat) into the waste mash, filtering by using a plate frame to obtain wet distiller grains with the water content of 68% by weight and clear liquid, concentrating the clear liquid at 60-80 ℃ until the water content is 70% by weight (recording evaporation energy consumption), mixing the concentrated clear liquid with the wet distiller grains, and drying the concentrated clear liquid and the wet distiller grains together by using a dryer at 120 ℃ until the water content is 11% by weight to obtain the DDGS. The results are shown in Table 1.
Example 2
This example illustrates the present invention for producing ethanol by fermentation and DDGS production
(1) According to the weight, 50 weight percent of hulled wheat and 50 weight percent of rice are mixed and crushed together, and the 20-mesh screening rate of the crushed raw materials reaches over 95 percent.
(2) Mixing the pulverized raw materials with water, and making slurry at a ratio of 1:2, wherein the temperature of the prepared slurry is 57-60 deg.C, and pH is 4.0.
(3) The powder slurry is pretreated, and the pretreatment method comprises the following steps: adding 10U of acid fungal amylase, 40U of acid protease, 0.4U of xylanase, 1U of pectinase, 5ppm of ampelin and 0.5mmol/L of urea into the powder slurry per gram of dry weight, adjusting the pH to 4.0, maintaining the temperature at about 57-60 ℃, stirring for 1.5 hours, and cooling to 32 ℃ to obtain liquefied mash.
(4) Adding 500U of Aspergillus niger glucoamylase, 30U of acid protease and 5ppm of ampelopsin into the cooled liquefied mash per gram of the liquefied mash by dry weight, and adding 0.2kg/t of yeast seed liquid (the cell concentration of the yeast seed liquid is 2.5-3.0 hundred million/ml) into the liquefied mash; adjusting pH to about 3.8, performing intermittent fermentation at 29 deg.C, and finishing fermentation after 86 hr.
(5) Feeding fermented liquor into a distillation system to obtain alcohol and waste liquor;
(6) adding rice hull bran powder (the adding amount of the rice hull bran powder is 20 parts by weight relative to 100 parts by weight of the waste mash), filtering by using a plate frame to obtain wet distiller grains with the water content of 70% by weight and clear liquid, concentrating the clear liquid at 60-80 ℃ until the water content is 72% by weight (recording evaporation energy consumption), mixing the concentrated clear liquid with the wet distiller grains, and drying the concentrated clear liquid and the wet distiller grains together by using a dryer at 120 ℃ until the water content is 11.2% by weight to obtain the DDGS. The results are shown in Table 1.
Example 3
This example illustrates the method of producing ethanol and DDGS by fermentation provided by the present invention
(1) According to the weight, 40 percent of hulled wheat and 60 percent of rice are mixed and crushed together, and the 20-mesh screening rate of the crushed raw materials reaches over 95 percent.
(2) Mixing the pulverized raw materials with water, and making slurry, wherein the ratio of material to liquid is 1:3, the temperature of the prepared slurry is 58-61 deg.C, and the pH is 5.5.
(3) The powder slurry is pretreated, and the pretreatment method comprises the following steps: adding 30U of acid fungal amylase, 30U of acid protease, 1.5U of xylanase, 0.4U of pectinase, 15ppm of amphoterin and 1.5mmol/L of urea into the powder slurry per gram of dry weight, adjusting the pH to 5.5, maintaining the temperature at about 58-61 ℃, stirring for 2 hours, and cooling to 32 ℃ to obtain liquefied mash.
(4) Adding 1500U of Aspergillus niger glucoamylase, 40U of acid protease and 5ppm of ampelopsin into the cooled liquefied mash per gram of the liquefied mash by dry weight, and adding 0.2kg/t of yeast seed liquid (the cell concentration of the yeast seed liquid is 2.5-3.0 hundred million/ml) into the liquefied mash; adjusting pH to about 4.5, performing intermittent fermentation at 33 deg.C, and finishing fermentation after 64 hr.
(5) Feeding fermented liquor into a distillation system to obtain alcohol and waste liquor;
(6) adding rice hull bran powder (the adding amount of the rice hull bran powder is 30 parts by weight relative to 100 parts by weight of the waste mash), filtering by using a plate frame to obtain wet distiller grains with the water content of 65% by weight and clear liquid, concentrating the clear liquid at 60-80 ℃ until the water content is 68% by weight (recording evaporation energy consumption), mixing the concentrated clear liquid with the wet distiller grains, and drying the concentrated clear liquid and the wet distiller grains together by using a dryer at 120 ℃ until the water content is 10.5% by weight to obtain the DDGS. The results are shown in Table 1.
Example 4
This example illustrates the method of producing ethanol and DDGS by fermentation provided by the present invention
Ethanol was prepared according to the method of example 1, except that the used raw materials further included peeled corn, and the respective pulverized products of corn and rice were 35% by weight based on 100 parts by weight of wheat, corn and rice, and the results are shown in Table 1.
Example 5
This example illustrates the method of producing ethanol and DDGS by fermentation provided by the present invention
Ethanol was prepared according to the method of example 1 except that the carrier was a mixture of rice hull bran powder and wheat bran in a ratio of 1:1, and the results are shown in table 1.
Example 6
This example illustrates the method of producing ethanol and DDGS by fermentation provided by the present invention
Ethanol was prepared according to the method of example 1 except that the carrier was rice hull bran powder, wheat bran, corn germ meal in a ratio of 1: 1:1 the resulting materials were mixed and the results are shown in table 1.
Comparative example 1
This comparative example serves to illustrate a reference fermentative ethanol production and DDGS production process
Ethanol was prepared according to the method of example 1, except that both wheat and rice were husked and no carrier was introduced before solid-liquid separation, and the results are shown in Table 1.
Comparative example 2
This comparative example serves to illustrate the reference fermentative ethanol production and DDGS production process
Ethanol production was carried out according to the method of example 1, except that rice was replaced with an equal amount of peeled corn, and the results are shown in table 1.
Comparative example 3
This comparative example serves to illustrate the reference fermentative ethanol production and DDGS production process
Ethanol was prepared according to the procedure of example 1, except that no carrier was introduced before solid-liquid separation, and the results are shown in Table 1.
TABLE 1
Figure BDA0002964353290000171
Note: steam refers to the steam consumption of the evaporator and the dryer together
As can be seen from table 1, (1) the method of the present invention can produce alcohol using wheat as a raw material by hulling the wheat raw material and simultaneously performing raw material fermentation using rice as an alcohol fermentation raw material using the existing alcohol production apparatus without causing clogging of equipment or piping, while reducing production energy consumption and cost and improving production efficiency;
(2) the method of the invention uses the carrier from the plant source raw material in the process of producing the DDGS feed, thereby not only fully utilizing the carrier and increasing the yield of the DDGS feed, but also further solving the problem of high energy consumption of evaporation and concentration of the distillers' grains water.
(3) Although the feed yield was improved in comparative example 1 (by using unhulled grain in much greater amounts than the amount of added carrier in example 1), the protein content of the feed was lower than approximately 5% of that of example 1, the fiber content was too high, the product quality was poor, and the feed requirements were not met.
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including various technical features being combined in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.

Claims (10)

1. A method for co-producing ethanol and DDGS by fermenting raw materials with wheat is characterized by comprising the following steps:
(1) mixing a mixed raw material containing a pulverized product of dehulled wheat and a pulverized product of rice with ingredient water to perform size mixing to obtain a flour paste;
(2) optionally, adding a liquefying enzyme into the slurry, and liquefying the slurry to obtain liquefied mash;
(3) adding saccharifying enzyme and inoculating yeast into the powder slurry or the liquefied mash for fermentation to obtain fermentation liquor containing ethanol;
(4) distilling the fermentation liquor containing ethanol to obtain ethanol and waste mash, then adding a carrier into the waste mash, and carrying out solid-liquid separation to obtain wet vinasse and clear liquid;
(5) concentrating the clear liquid to obtain concentrated clear liquid, mixing the concentrated clear liquid with the wet distiller grains, and drying to obtain DDGS feed;
wherein the carrier is a plant source material.
2. The method of claim 1, wherein the temperature of the conditioning and liquefying is below the starch gelatinization temperature of wheat and rice.
3. The method according to claim 1 or 2, wherein in step (1), the content of the milled product of dehusked wheat in the mixed raw material is 20% by weight or more, preferably 20 to 70% by weight; and/or
The size of the milled product of dehulled wheat is such that at least 85% of the dehulled wheat milled product passes through a 20 mesh screen; the size of the ground product of rice is such that at least 85% of the ground product of dehulled rice passes through a 20 mesh screen.
4. A process according to any one of claims 1 to 3, wherein in step (1) the mixed feedstock also comprises a milled product of dehulled other grain selected from the group consisting of corn, tapioca and sorghum;
preferably, the particle size of the milled product of the dehulled other grain is such that at least 85% of the milled product of the dehulled other grain passes through a 20 mesh screen.
5. The method according to any one of claims 1 to 4, wherein in the step (1), the slurry-liquid ratio in the slurry mixing step is 1: 1.3-4; and/or
The temperature of the powder slurry is 30-70 ℃, and the pH value is 4-5.5.
6. The method according to any one of claims 1-5, wherein in step (2), the method comprises: adding a liquefying enzyme into the powder slurry to liquefy the powder slurry;
wherein the liquefying enzyme comprises raw material amylase, acid protease, xylanase and pectinase;
preferably, the dosage of the raw material amylase, the acidic protease and the xylanase is 2-200U, 2-100U, 0.1-10U and 0.1-2U, respectively per gram of the powder slurry by dry weight;
preferably, the method also comprises the step of adding a bacteriostatic agent into the powder slurry, wherein the addition amount of the bacteriostatic agent is that the concentration of the bacteriostatic agent in the powder slurry is 2.5-20 ppm;
preferably, the liquefaction conditions include: the pH value is 4-5.5, the temperature is 35-67 ℃, and the time is 0.5-3 hours.
7. The process according to any one of claims 1 to 6, wherein in step (3), the saccharifying enzyme is used in an amount of 50 to 5000U per gram of dry weight of the mash or the liquefied mash;
preferably, the method further comprises: adding an acid protease to the liquefied mash; the amount of said acid protease is 2-100U per gram of said liquefied mash on a dry weight basis;
preferably, the method further comprises: adding a bacteriostatic agent into the liquefied mash; the addition amount of the bacteriostatic agent is 2.5-20ppm in the liquefied mash;
preferably, the method further comprises: adding nutrients to the liquefied mash; the nutrient is selected from at least one of ammonia water, urea, zinc sulfate and magnesium sulfate;
preferably, the inoculation amount of the yeast seed liquid is 0.1-0.5kg per ton of the liquefied mash;
preferably, the fermentation conditions include: the temperature is 26-38 deg.C, pH is 3-5, and the time is 24-100 hr.
8. The method according to any one of claims 1-7, wherein the plant-derived feedstock is selected from the group consisting of hulls of grains, meal of grains, and stalks of grains.
9. The method of claim 8, wherein the plant-derived material is one or more of corn bran, rice hull bran meal, wheat bran, bean pulp, corn germ pulp, and straw meal.
10. The method according to any one of claims 7 to 9, wherein the carrier is used in an amount of 5 to 40% by weight relative to 100 parts by weight of the dehulled wheat.
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