Combined method for producing bioethanol and an oilseed protein product

Abstract

The invention relates to a combined method, comprising a first method for producing bioethanol (10) and a second method for producing an oilseed protein product (31, 45), the first method comprising the steps of (a) providing a slurry (7), wherein the slurry (7) contains a carbohydrate-containing feedstock (1), in particular a grain, (b) fermenting the slurry (7) in order to obtain a fermented liquor (9) containing bioethanol (10), and (c) separating at least some of the bioethanol (10) from the fermented liquor (9); and the second method comprising the steps of (i) providing an oilseed feedstock (4), (ii) extracting the oilseed feedstock (4) using a first extraction agent (39), in order to obtain a first miscella (26) and a first extraction product (27), (iii) splitting the first extraction product (27) into a first mixture (30, 46) containing the oilseed protein product (31, 45) and a second mixture (32, 47) containing the oilseed secondary product (5), (iv) separating at least some of the oilseed protein product (31, 45) from the first mixture (30, 46), and optionally separating at least some of the oilseed secondary product (5) from the second mixture (32, 47); wherein the slurry (7) provided in step (a) of the first method contains at least some of the oilseed secondary product (5) obtained in the second method, wherein the first extraction agent (39) contains bioethanol (10) produced in the first method, wherein the first miscella (26) contains at least some of the first extraction agent (39), and wherein at least some of the first extraction agent (39) contained in the first miscella (26) is separated from the first miscella (26) and is used in step (c) of the first method.

Description

[0001] Combined process for the production of bioethanol and an oilseed protein product

[0002] The invention relates to a combined process for producing bioethanol and an oilseed protein product. Furthermore, the invention relates to a combined plant for producing the bioethanol and the oilseed protein product using the combined process, as well as to a feed obtainable by the combined process.

[0003] The use of bioethanol derived from renewable resources instead of petroleum-based ethanol has become increasingly important in recent years. For example, a process for producing ethanol from biomass is described in DE 10 2006 040 567 A1. The biomass is crushed and fermented to produce bioethanol. Demiray E. et al. (doi.org / 10.1016 / j.fuel.2020.119785) investigated the effect of soluble soy protein on the enzymatic hydrolysis of apple pomace for bioethanol production. They found that soluble soy protein enables twofold lower enzyme consumption and thus more economical enzymatic hydrolysis and bioethanol production.

[0004] Processes for processing oilseeds are also known from the prior art, in particular processes for processing soybeans to obtain soy protein products. For example, US Pat. No. 4,075,361 A teaches a process for producing an edible extract from an oilseed, wherein the oilseed is ground in the presence of a hot alkaline extraction solution, preferably containing sodium hydroxide. After the extraction step, the mixture of ground oilseed and extraction solution is neutralized with an acidic solution and then centrifuged.

[0005] US 4,457,869 A discloses a process for extracting an oilseed, in which the oilseed is contacted with an isopropanol-based solvent in an extractor to obtain a liquid miscella and a meal. The solvent is separated from the miscella and recovered by cooling and phase separation, and the solvent is separated from the meal and recovered by evaporation.

[0006] EP 3 295 803 A1 discloses a process for obtaining protein preparations from sunflower seeds. The sunflower husks are dehulled and then partially deoiled by pressing. Extraction steps are then carried out with a solvent, yielding a defatted, protein-containing flour as a protein preparation. A combination of two or more extraction solvents of different polarity can be used, e.g., water, acids, alcohols (e.g., isopropanol, ethanol, methanol), ketones (e.g., acetone), ethers, alkanes (n-hexane, isohexane). A lipophilic extraction can be performed first, followed by a hydrophilic extraction, or vice versa.

[0007] WO 2022 / 006165 A1 and WO 2022 / 183031 A1 relate to devices, systems, and methods for processing soybeans with an alcohol-based solvent to extract oil. The alcohol-based solvent can be ethanol (e.g., ethanol from renewable feedstocks, including organically grown feedstocks) or isopropyl alcohol.

[0008] DE 27 52595 A1 relates to a process for producing a protein concentrate. An oil-containing seed material (e.g., soybeans) is extracted in four consecutive steps using aqueous-alcoholic solutions (e.g., solutions of alcohol in water).

[0009] WO 2022 / 043248 A1 relates to a process for the industrial extraction of cold-pressed kernel oil. The kernels of an oil-bearing seed (e.g., soybeans) are dehulled and their hulls are separated from a low-hull fraction. The cold-pressed kernel oil is pressed from the low-hull fraction. A portion of the resulting press cake is recycled, mixed with the low-hull fraction, and pressed again. The remaining press cake is extracted with a solvent (e.g., hexane or ethanol) and dried to yield a protein concentrate.

[0010] US 2017 / 0233767 A1 concerns the production of ethanol from a fermented, solid product, which does not involve a combination of two processes. Bioethanol is obtained from the fermentation of plant raw materials. The resulting bioethanol can be used for energy generation within the process. The resulting product is therefore fundamentally different from soy proteins (SPC & SPI). Furthermore, the products obtained from this process necessarily contain yeast protein. Fukui et al. (Nutrition 20 (2004), 984-990) describe the ethanol washing of soy proteins. Sissons et al. (Br. J. Nutr. 42 (1979), 477-485) describe the effect of ethanol-extracted soybean feed on calves. Nehmeh et al. (Processes 10 (2022), 841) report on secondary metabolites during the extraction of oilseeds. Luque de Castro et al. (Analytica Chimica Acta 261 (1992), 425-434) report on the coupling of continuous separation methods with unsegmented flow systems.Abraham et al. (J. Am. Oil Chem. Soc. 68 (1991), 418-421) report on the process-based evaluation of ethanol extraction from cottonseeds. CN 105200094 A concerns ethanol production by microbial fermentation of lingocellulose feedstock.

[0011] During the production of oleaginous fruit protein products, particularly oleaginous fruit protein concentrate or oleaginous fruit protein isolate, an oleaginous fruit by-product is produced, which may include, in particular, oleaginous fruit molasses and / or oleaginous fruit protein liquor. Although this oleaginous fruit by-product can be used as an additive in animal feed, it is usually incinerated because the resulting quantities are too large to be fully utilized for animal feed purposes. There is a need for a process that enables the utilization of a larger quantity of the oleaginous fruit by-product generated during the production of oleaginous fruit protein products, thus increasing the sustainability of the process. The use of the waste product from oleaginous fruit protein production as a raw material for the production of bioethanol enables the production of second-generation bioethanol.On the other hand, it is also desirable to optimize bioethanol production processes – both in terms of their energy balance and CO2 footprint, but also in terms of the use of the resulting products or intermediates. Processes or combinations of processes that support or enable a production or energy cycle in the sense of a biorefinery are particularly desirable.

[0012] Accordingly, the invention relates to a combined process comprising a first process for producing bioethanol and a second process for producing an oilseed protein product, the first process comprising the steps

[0013] (a) providing a mash, the mash containing a carbohydrate-containing starting material, in particular a cereal,

[0014] (b) fermenting the mash to obtain a fermented broth containing bioethanol, and

[0015] (c) separating at least a portion of the bioethanol from the fermented broth; and the second process comprising the steps

[0016] (i) providing an oilseed crop product,

[0017] (ii) extracting the oilseed crop starting product with a first extraction agent to obtain a first miscella and a first extraction product,

[0018] (iii) separating the first extraction product into a first mixture containing the oilseed protein product and a second mixture containing the oilseed by-product,

[0019] (iv) separating at least a portion of the oleaginous protein product from the first mixture, and optionally separating at least a portion of the oleaginous by-product from the second mixture; wherein the mash provided in step (a) of the first process contains at least a portion of the oleaginous by-product obtained in the second process or at least a portion of the oleaginous by-product obtained in the second process is added during step (b), wherein the first extractant contains bioethanol produced in the first process, wherein the first miscella contains at least a portion of the first extractant, and wherein at least a portion of the first extractant contained in the first miscella is separated from the first miscella and used in step (c) of the first process.

[0020] The present invention therefore relates to the interactive combination of two essentially completely independent processes, which surprisingly allows many synergies to be utilized. The two processes can be designed relatively flexibly, particularly based on the most recent embodiments, since the targeted crosslinking of the two processes, as achieved according to the invention, takes place at points that correspond to the currently common individual processes. Thus, the first process can be carried out according to established process steps (as described, for example, in DE 10 2006 040 567 A1 and many other documents). The second process can essentially also be carried out according to common processes, provided the extraction is carried out using ethanol as the extractant, thereby establishing the inventive combination between the first and second processes (see, for example, WO 2022 / 006165 A1, WO 2022 / 183031 A1, WO 2022 / 043248 A1).According to US 2017 / 0233767 A1, bioethanol is obtained from the fermentation of plant raw materials. The resulting bioethanol can be used for energy generation within the process. The resulting product is therefore fundamentally different from soy proteins according to the present invention (SPC & SPI). Fukui et al. (Nutrition 20 (2004), 984-990) and Sissons et al. (Br. J. Nutr. 42 (1979), 477-485) describe products extracted with ethanol in the laboratory (SPI with ethanol; soy meal with ethanol). These products are not comparable to the feed obtained within the scope of the present invention, because according to these documents, the majority of the protein from the soy does not end up in the feed. The products according to Fukui et al. and Sissons et al. are more comparable to SPC and SPI, which are not known to be used as animal feed. The morphology shown in Fig. 2A by Nehmeh et al.The device shown in (Processes 10 (2022), 841) is used for the online analytical determination of, for example, bioethanol, for the purpose of online monitoring of the fermentation process (e.g., bioethanol production). Such analytical methods are not suitable for production, particularly because they do not allow for macroscopic separation or similar production steps. This analytical device also lacks crucial steps that are essential for the production of bioethanol or an oilseed protein product, such as suitable extraction devices or suitable separation units.

[0021] According to the invention, the oilseed by-product obtained in the second process is preferably used for the mash prepared in the first process and fermented together with the carbohydrate-containing starting material. This not only allows the oilseed by-product to be reused, but also increases the amount of bioethanol obtained in the first process. Furthermore, the combination of these two processes offers surprising energy and process-related advantages. For example, the thermal energy obtained in the combined process can also be used in the combined process, which can significantly improve process efficiency.Above all, the combination of the two processes makes it possible to use bioethanol produced in the first process as the first extraction agent in the second process and subsequently return it to the first process for purification, thus eliminating the need to dewater the first extraction agent. Furthermore, if the oilseed crop product provided in the second process contains dehulled oilseeds, the hulls separated from the oilseeds can be used in the first process and included in the mash produced. Since the hulls have an abrasive effect, they can reduce the contamination of plant components, which has a positive effect on the service life of the plants. The addition of the hulls to the mash also increases the value of the hulls, as they are otherwise difficult to sell on the market.

[0022] First process - production of bioethanol

[0023] In step (a) of the first process, the mash is provided, which contains the carbohydrate-containing starting material and preferably at least a portion of the oilseed by-product obtained in the second process. A carbohydrate-containing starting material is understood to mean a starting material that contains one or more carbohydrates, for example a cereal, potatoes, pulses, and / or beets. The carbohydrate-containing starting material is preferably a sugar product (e.g., sugar beet, sweet sorghum, sugar cane, fruit) or a starch product, wherein the starch product preferably contains a cereal (e.g., rice, wheat, corn, rye, barley), potatoes, and / or pulses (e.g., beans, lentils, peas, chickpeas). According to the present invention, a starch product is understood to mean a carbohydrate-containing starting material that contains one or more starch(s).Preferably, the carbohydrate-containing starting material is a grain, particularly preferably corn and / or wheat. A comparatively high yield of bioethanol can be obtained from this, especially if enzymatic degradation is carried out and / or if the materials (the fibers they contain) are ground beforehand.

[0024] The carbohydrate-containing starting material and / or the oilseed by-product (if present) are present in the mash at least partially in a mashed state. The mashed state is understood to mean a state in which the carbohydrate-containing starting material or the oilseed by-product contains an at least partially or completely digested (i.e., saccharified) and thus fermentable carbohydrate (in particular a starch), or a mixture of two or more such carbohydrates.

[0025] The mash provided in step (a) can be obtained by mashing the carbohydrate-containing starting material and optionally the oilseed by-product, preferably in the presence of water. Mashing can break down a carbohydrate, in particular a starch, contained in the carbohydrate-containing starting material and / or the oilseed by-product and render it fermentable. Mashing is preferably carried out at a temperature of 60 to 130°C, more preferably at 80 to 120°C. This not only enables efficient mashing, but also prevents thermal damage to the carbohydrate-containing starting material and the oilseed by-product. Preferably, mashing takes place for a period of 0.5 h or more, more preferably for 2 h or more. This allows the carbohydrate, in particular the starch, to be efficiently broken down. Particularly preferably, mashing takes place for a period of 1 to 4 h.Before mashing, saccharification (saccharification) can be performed, in which longer-chain carbohydrates are converted into individual (or at least shorter-chain) sugar molecules, leaving the monosaccharide molecules intact, such as the breakdown of starch into glucose monomers. Mashing can also be performed simultaneously or overlapping with saccharification. This can result in a good balance between process efficiency and saccharification.

[0026] Mashing can take place in the presence of one or more enzymes. The enzyme is preferably selected from the group comprising an alpha-amylase, a glucanase, a glucoamylase, a cellulase, a hemicellulase, a beta-glucanase, a xylanase, an arabinase, a galactosidase, and a protease, or a mixture thereof, with the enzyme particularly preferably being an alpha-amylase and / or a glucoamylase. The carbohydrate, in particular the starch, can then be efficiently digested. Before mashing, the carbohydrate-containing starting material can be comminuted, in particular ground, preferably by dry milling and / or wet milling. Dry milling refers to comminuting the carbohydrate-containing starting material in the dry state, i.e., without the addition of water. In wet milling, however, the carbohydrate-containing starting material is comminuted in the presence of a previously added liquid, in particular water.The oilseed by-product can be added to the carbohydrate-containing raw material after it has been crushed and before mashing.

[0027] During comminution, particularly during dry milling, the carbohydrate-containing starting material and oilseed shells are preferably comminuted together, with the oilseed shells particularly preferably being at least a portion of the shells separated from oilseeds, particularly soybeans, in step (i) of the second process. According to the invention, this enables a higher-value use of the oilseed shells, which are otherwise often burned, for single animal feed, such as "Dried Distillers Grains with Solubles" ("DDGS"), which is obtained as a by-product in the production of bioethanol from grains, with the resulting distillation residues being dried.

[0028] During comminution, particularly wet milling, fiber, corn gluten and / or corn gluten feed (CGF) may be produced. At least some of this can be separated from the comminuted, carbohydrate-containing feedstock prior to mashing. The separated fiber, corn gluten and / or corn gluten feed can be added to a stillage (i.e., a non-fermentable residue) separated from the fermented broth. If the stillage is used as animal feed, the fiber, corn gluten and / or corn gluten feed can serve as a high-quality feed additive. Corn gluten is a protein concentrate resulting from the extraction of corn starch. CGF is the fiber fraction resulting from corn starch production, where this fiber is co-dried with CSL (corn steep liquor) to produce CGF. CSL is formed when the corn is steeped prior to the corn starch production process.Bioethanol is typically produced from ground corn and / or wheat flour. However, there are also processes where, for example, corn is first refined into starch, and then the starch is used to produce bioethanol. Bioethanol from wet-milled corn is the dominant production method in the USA, for example.

[0029] The mash provided in step (a) of the first process preferably contains at least a portion of the oilseed by-product of the second process. The mash may in particular contain at least a portion of the second mixture obtained in step (iii) (containing the oilseed by-product) and / or at least a portion of the oilseed by-product obtained in step (iv) (after its separation from the second mixture, and optionally after evaporation). The oilseed by-product may contain an oilseed molasses and / or an oilseed protein liquor, in particular a soy molasses and / or a soy protein liquor; this may depend on the design of the second process.

[0030] According to the invention, soy molasses preferably has the following composition: soy sugar (58-65%), typically oligosaccharides (stachyose 23-26%, raffinose 4-5%), disaccharides (sucrose 26-32%), monosaccharides (fructose 1.2-1.6%, glucose 0.9-1.3%), crude protein [N x 6.25] (including amino acids and peptides, etc.: 5-7%), crude lipid material (including phosphatides: 4-7%), minerals (ash, 3-7%), saponins (3-7%), isoflavones (6-15%), other organic components (including phenolic acids, leucoanthocyanins, etc.: to 100%). Alternatively, soy molasses can also be defined as follows: protein (guaranteed value: max. 12%), dry matter (55.0 ± 10%), fat (dry, max. 3.5%), carbohydrates (45.0% by difference); density at 60°C 1.2-1.3 g / mg; often also characterized with a typical energy value of 914 kJ (259 kcal / 100g).

[0031] If an oleaginous fruit protein concentrate is produced in the second process, the oleaginous fruit molasses can be contained in the oleaginous fruit by-product. If, however, an oleaginous fruit protein isolate is produced, the oleaginous fruit protein liquor can be contained in the oleaginous fruit by-product. The oleaginous fruit by-product preferably has a dry matter weight of 10 to 80 wt%, more preferably 15 to 50 wt%, even more preferably 20 to 40 wt%, and particularly preferably 25 to 35 wt%, based on the total weight of the oleaginous fruit by-product. This can facilitate process control during mashing and fermentation. This dry matter weight is understood to mean the dry matter weight of the oleaginous fruit by-product immediately before its use in the first process, optionally after evaporation.

[0032] Preferably, the mash provided in step (a) contains the oleaginous by-product in an amount of 30 wt% or less, more preferably 20 wt% or less, even more preferably 15 wt% or less, even more preferably 12 wt% or less, even more preferably 10 wt% or less, based on the weight of the carbohydrate-containing starting material. Exceeding this amount of oleaginous by-product may result in a deterioration in the fermentation properties of the mash. It is preferred if the mash provided in step (a) contains the oleaginous by-product in an amount of 1 to 30 wt%, preferably 1 to 20 wt%, more preferably 1 to 15 wt%, even more preferably 1 to 12 wt%, particularly preferably 5 to 10 wt%, based on the weight of the carbohydrate-containing starting material contained in the mash. Good fermentation kinetics can then be achieved, which improves process efficiency.The fermentation kinetics can be particularly optimal when the carbohydrate-containing starting material is a grain. The mash preferably has a ratio of oilseed by-product to carbohydrate-containing starting material, in particular grain, of 0.1:10 to 1.5:10, particularly preferably 1:10 (wt% / wt%). This results in particularly good fermentation behavior, i.e., both the carbohydrate-containing starting material and the oilseed by-product can be well fermented.

[0033] It is preferred if the mash provided in step (a) contains husks from oilseeds, in particular crushed husks from oilseeds. These husks are preferably at least a portion of husks separated from oilseeds, in particular soybeans, in step (i) of the second process. Since the husks have an abrasive effect, they can reduce the contamination of plant components, which has a positive impact on the service life of the plants. The addition of the husks to the mash also increases the value of the husks, as the husks are otherwise difficult to sell on the market. The husks are not or only partially fermentable and can be contained in the stillage separated from the fermented broth. When the stillage is used as animal feed, the husks can lead to a reduction in the protein content of the animal feed.However, the presence of the shells (especially the crushed shells) in the stillage has process-technical advantages, as the drying of the stillage can then be carried out more efficiently, as the (crushed) shells can absorb water well, especially if they are fibrous, whereby fibrous shells can form in particular by crushing the shells.

[0034] In step (b) of the first process, the mash is fermented (i.e., fermented). This converts sugar (e.g., maltose, glucose) into bioethanol. Carbon dioxide (CO2) may be produced as a by-product. Preferably, a microorganism, in particular a yeast (such as, for example, Saccharomyces cerevisiae, Saccharomyces pastorianus) and / or a bacterium (e.g., Zymomonas mobilis), is added to the mash before and / or in step (b). Fermentation can then take place particularly efficiently. Preferably, the mash is fermented at a temperature of 20 to 40°C, more preferably 28 to 36°C. Fermentation can then take place efficiently and without thermal damage. Preferably, the mash is fermented for a period of 25 hours or more, more preferably for 55 hours or more, particularly preferably for a period of 50 to 70 hours. This can result in a good bioethanol yield and, at the same time, good process efficiency.Fermentation produces a fermented broth containing bioethanol and stillage. Stillage is the non-fermentable residue, which contains the substances that were also present in the mash. Stillage preferably contains a protein, microorganism biomass, a fat, and / or a mineral (or a mixture of proteins, fats, and / or minerals), and preferably water. Stillage may contain non-fermentable carbohydrates; at least a large portion of these have been saccharified through mashing and thus rendered fermentable.

[0035] In step (c) of the first process, at least a portion of the bioethanol is separated from the fermented broth. Preferably, in step (c), at least a portion of the stillage contained in the fermented broth is also separated from the fermented broth. Separating the bioethanol and / or stillage preferably comprises thermal separation, in particular distillation. Since bioethanol evaporates at a lower temperature than water (which is also contained in the fermented broth), the bioethanol can be separated by thermal separation, in particular distillation, not only from the solids contained in the fermented broth (which are contained in the stillage), but also from at least a portion of the water contained in the fermented broth. By thermal separation, in particular distillation, the stillage can be separated from a bioethanol-water mixture.The bioethanol-water mixture preferably contains a proportion of bioethanol of 50 wt% or more, more preferably 85 wt% or more, even more preferably close to the azeotrope (95.6 wt%), i.e. 90 to 95.6 wt% based on the weight of the bioethanol-water mixture.

[0036] The separation of at least a portion of the bioethanol from the fermented broth in step (c) preferably comprises distillation and subsequent separation of the bioethanol-water mixture into bioethanol and water. This allows dewatering of the bioethanol. The separation of the bioethanol-water mixture into bioethanol and water can be carried out using a molecular sieve, a membrane process (using a membrane), and / or pressure swing adsorption (using an adsorbent). Preferably, the separation of the bioethanol-water mixture into bioethanol and water is carried out using a molecular sieve. This allows the bioethanol to be efficiently dewatered. The temperature during separation using the molecular sieve generally depends on the manufacturer, but is preferably in the range of 120 to 180°C, more preferably 160 to 170°C, and / or the pressure is preferably in the range of 2 to 6 bar, more preferably 3 to 5 bar.The molecular sieve preferably has a pore size of 0.25 to 0.35 nm, in particular 0.30 nm. By separating the bioethanol-water mixture, in particular by means of the molecular sieve, bioethanol with a purity of 99.0 wt% or more can be obtained in the first process, preferably 99.5 wt% or more, particularly preferably 99.9 wt% or more. The separation can also be carried out sustainably due to the regenerability and reusability of the molecular sieve. The water separated from the bioethanol is preferably treated (i.e., purified) so that it can be reused.

[0037] The molecular sieve is preferably dewatered to regenerate it using a cleaning or dewatering agent. This allows organic residues to be removed. This dewatering (regenerating) can be performed at regular intervals or as needed. The molecular sieve is preferably dewatered using an ethanol-containing cleaning agent (preferably as regenerate with the ethanol from the present process), wherein the cleaning agent preferably contains ethanol in an amount of 95% by weight or more, more preferably 97% by weight or more, even more preferably 99.9% by weight or more, particularly preferably 100% by weight, based on the weight of the cleaning agent. According to the invention, the use of the ethanol produced in the first process as regenerate for dewatering the molecular sieve is particularly preferred.This regenerate can be used directly (at least) for the second extraction stage, as it typically has an ethanol content of over 80 wt% and can therefore be used either directly or after dilution (preferably with water). This embodiment is particularly advantageous from an energy perspective, as it eliminates the need for (pre-)distillation of the dehydrating agent.

[0038] To clean the molecular sieve, approximately 0.1 to 0.2 m 3 Ethanol per m 3of bioethanol produced in the first process may be necessary. The ethanol-containing cleaning agent is used after its use to clean the molecular sieve, preferably in step (c) of the first process. The ethanol-containing cleaning agent can be added to the fermented broth, preferably after at least partial separation of water and / or stillage from the fermented broth, in particular after partial distillation of the fermented broth. The ethanol contained in the cleaning agent can then be separated from the fermented broth in step (c) of the first process together with the bioethanol contained in the fermented broth, so that the ethanol contained in the cleaning agent can also be at least partially recovered.The ethanol-containing (especially bioethanol-containing) cleaning agent can also be used as a second extraction agent, especially if the cleaning agent contains ethanol and water, in particular in a suitable ratio. This enables immediate reuse in the combined process, which is accompanied by energy savings, since dewatering of the ethanol can be eliminated. The cleaning agent can be stored, in particular in a storage container, before being added to the fermented broth or before being used as a second extraction agent. This makes it possible to remove at least a portion of the stored cleaning agent depending on requirements, availability, and / or capacity. Alternatively or in addition to cleaning the molecular sieve with an ethanol-containing cleaning agent, the molecular sieve is preferably cleaned, in particular rinsed, with carbon dioxide.For this purpose, at least a portion of the carbon dioxide produced during fermentation in step (b) of the first process can be utilized. The carbon dioxide produced as a byproduct during fermentation can therefore be reused in the combined process according to the invention, which is advantageous in terms of process efficiency. In particular, the utilization of carbon dioxide for ethanol production enabled by the process combination according to the invention is very important with regard to the sustainability of bioethanol production within the overall combined process.

[0039] It is preferred if the separation of at least a portion of the bioethanol from the fermented broth in step (c), in particular the separation of the bioethanol-water mixture into bioethanol and water, comprises a condensation of gaseous bioethanol and / or gaseous water. Thermal energy can be obtained in the process. This thermal energy can be used in the combined process, in particular for comminuting the oilseeds to obtain the oilseed starting product provided in step (i), for extracting the oilseed starting product with the first extractant in step (ii), and / or for separating the first extraction product into the first and second mixtures in step (iii). The inventive combination of the two processes can thus make a valuable contribution to sustainability and significantly improve the energy balance.For example, 0.4 to 0.6 t of steam (100 °C, 1 bar) can be obtained as thermal energy - this corresponds to approximately one third of the steam required to process one ton of oilseeds, especially soybeans.

[0040] The bioethanol separated from the fermented broth can be collected, in particular in a first collection container. Bioethanol produced in the first process is preferably used as the first extractant and / or as the second extractant in the second process, and / or further applications such as, for example, as an additive for fuels, in cosmetics, as a starting product for bio-based chemicals, etc. The stillage separated from the fermented broth in step (c) of the first process is preferably subsequently dried. Drying is preferably carried out at a temperature of 60°C or above, more preferably 100°C or above, particularly preferably at 100 to 140°C. This allows liquids, in particular water, and any volatile substances to be separated from the stillage. The stillage is preferably dried for 0.1 h or more, more preferably for 0.15 h or more, particularly preferably for 0.15 to 0.3 h.The dried stillage can be used as high-quality animal feed, e.g., as DDGS. For this purpose, the dried stillage is preferably pelletized. Afterward, it is preferably packaged, for example, in ready-to-sale containers. Alternatively or additionally, the stillage, or a portion thereof, can be used for energy recovery, for example, by conversion into biogas or biomethane. Gaseous water separated during drying of the stillage is preferably condensed, whereby thermal energy is recovered. The recovered thermal energy can be used in the combined process, in particular for conditioning during comminution of the oilseeds to obtain the oilseed starting product provided in step (i), for extracting the oilseed starting product with the first extraction agent in step (ii), and / or for separating the first extraction product into the first and second mixtures in step (iii).The inventive combination of the two processes can thus make a valuable contribution to sustainability and significantly improve the energy balance. The separated water is preferably treated so that it can be reused.

[0041] The stillage is preferably dried together with husks of oilseeds. The husks are preferably a portion of husks separated from oilseeds, particularly soybeans, in step (i) of the second process. These husks can be added to the stillage separated from the fermented broth in step (c) of the first process. Alternatively or additionally, the stillage may contain already crushed husks if the carbohydrate-containing starting material contained in the mash was crushed together with plant materials, particularly husks of oilseeds, grain, or beet pulp, particularly soybeans. The presence of (crushed) husks of oilseeds during the drying of the stillage offers process-related advantages: the drying of the stillage can then be more efficient because the (crushed) husks can absorb water well, especially if they are fibrous.The addition of the shells to the stillage also increases the value of the shells, as the shells would otherwise be difficult to sell on the market.

[0042] It is preferred if a portion of the oleaginous fruit by-product obtained in the second process is added to the stillage separated from the fermented broth, with the stillage and the added oleaginous fruit by-product preferably being dried together. This is particularly advantageous if the amount of oleaginous fruit by-product obtained in the second process is too large to be used entirely in step (a) of the first process and then fermented together with the carbohydrate-containing starting material; if the ratio of oleaginous fruit by-product to carbohydrate-containing starting material in the mash were too high, this could impair the fermentation properties of the mash.The addition of a portion of the oilseed by-product to the stillage offers the advantage that at least a portion of the oilseed by-product that cannot be fermented (particularly due to an excessive amount of oilseed by-product produced) can still be used in the combined process and processed into a valuable animal feed.

[0043] Second process - Production of the oilseed protein product

[0044] The oleaginous fruit protein product is preferably an oleaginous fruit protein isolate and / or an oleaginous fruit protein concentrate, particularly preferably a soy protein isolate and / or a soy protein concentrate. Oleaginous fruit protein isolate is a highly purified protein obtained from oleaginous fruits. Oleaginous fruit protein isolate typically contains at least 90% protein by weight and a comparatively low proportion of carbohydrate and / or fat. Oleaginous fruit protein concentrate has a similar composition to oleaginous fruit protein isolate, but may also have a lower protein content (approximately 40 to 90% by weight, preferably 50 to 90% by weight, especially 60 to 80% by weight) and a higher proportion of fiber, carbohydrate, and / or fat compared to oleaginous fruit protein isolate.

[0045] The oilseed by-product obtained in the second process preferably contains a carbohydrate or a mixture of two or more carbohydrates, wherein preferably at least one carbohydrate, in particular at least one starch, is saccharifiable. The oilseed by-product preferably contains at least 15% by weight of such a saccharifiable carbohydrate, more preferably at least 20% by weight, even more preferably at least 30% by weight, particularly preferably at least 40% by weight, based on the proportion of carbohydrates in the oilseed by-product and based on the dry matter weight of the oilseed by-product. Depending on the starting material, higher values ​​are also possible, in particular if short-chain carbohydrates, e.g. stachyose and raffinose, are present. A saccharifiable carbohydrate is understood to be a carbohydrate (in particular a starch) that can be broken down (i.e., saccharified) by mashing and thus made fermentable.Then, in step (b) of the first process, fermentation of the sugar produced by mashing (i.e., conversion of the sugar to ethanol) can take place. For example, if the oilseed by-product contains approximately 30% by weight of saccharifiable carbohydrates (based on the carbohydrate content of the oilseed by-product and the dry matter weight of the oilseed by-product), the combined process can increase the amount of bioethanol produced by the first process by approximately 2500 m³. 3per year if the ratio of oilseed by-product to carbohydrate-containing starting material in the mash is 1:10 (wt% / wt%). It is preferred if the oilseed by-product obtained in the second process also contains a protein (or a mixture of two or more proteins). Since proteins are not fermentable, they are contained in the stillage separated from the fermented broth. The stillage is thus particularly rich in protein, so that it can be used as a high-quality animal feed. In step (i) of the second process, an oilseed starting product is provided. The oilseed starting product is preferably obtained from oilseeds. Preferably, the provision of the oilseed starting product comprises processing the oilseeds, in particular separating shells from the oilseeds and / or comminuting the oilseeds.Examples of oilseeds are rapeseeds, sunflower seeds, linseeds, mustard seeds, peanut seeds, grape seeds, pumpkin seeds, soybeans, coconuts, avocados, coffee beans, oil palm seeds, oil palm fruits, olive kernels, and cottonseeds. The processability of oilseeds by extraction with alcohol-based solvents is known from WO 2022 / 006165 A1 and WO 2022 / 183031 A1. The oilseeds are preferably soybeans, sunflower seeds, and / or rapeseed seeds, particularly preferably soybeans. This allows a particularly high yield of oilseed protein product to be achieved in the second process. The oilseed starting product accordingly preferably contains comminuted and / or dehulled oilseeds; preferably comminuted and / or dehulled soybeans, comminuted and / or dehulled sunflower seeds, and / or comminuted and / or dehulled rapeseed seeds. particularly preferably crushed and / or hulled soybeans.If soybeans, in particular crushed and / or hulled soybeans, are used as oilseed crop starting product, a soy protein concentrate (SPC) and / or a soy protein isolate (SPI) can be obtained as oilseed crop protein product in the second process, wherein a soy molasses and / or a soy protein liquor (SPL) can be obtained as oilseed crop by-product.

[0046] At least a portion of the shells separated from the oilseeds is preferably used in the production of the mash provided in step (a) of the first process and / or dried together with the stillage. The further use of separated shells in the first process enables higher-value utilization of these shells. The comminution, in particular grinding and / or pressing, of the oilseeds preferably takes place at elevated temperature. Comminution preferably takes place at a temperature of 50°C or above, more preferably 70°C or above, even more preferably 90°C or above, particularly preferably 110°C or above. This allows the oilseeds to be (post-)dried at the same time; in particular, any water still contained in the oilseeds can be separated. This can increase the brittleness of the oilseeds and consequently improve the efficiency of comminution.The thermal energy required for crushing and / or pressing the oilseeds is preferably thermal energy obtained at least in part in the combined process, in particular thermal energy obtained during the separation of at least a portion of the bioethanol from the fermented broth in step (c) (in particular thermal energy obtained during the condensation of the bioethanol after separating the bioethanol-water mixture into bioethanol and water), and / or thermal energy obtained during the condensation of the water separated during the drying of the stillage. By utilizing thermal energy obtained in the combined process, the energy balance of the combined process can be significantly improved.

[0047] In step (ii) of the second process, the oil-fruit starting product is extracted with a first extraction agent to obtain a first miscella and a first extraction product. According to the invention, "miscella" (Latin for mixed) is understood - as is also the case in the art - to refer to a mixture of organic extraction agent (solvent) and oil, which is obtained as an intermediate product during the extraction of vegetable oils. This extraction preferably serves to defatt and / or deoil the oil-fruit starting product. The first extraction product therefore preferably contains an at least partially defatted and / or deoiled solid. The oil and / or fat contained in the oil-fruit starting product is accordingly preferably at least partially, more preferably largely (i.e.to 51 wt% or more, preferably to 80 wt% or more, more preferably to 90 wt% or more, even more preferably to 95 wt% or more, based on the total amount of oil and / or fat present in the oil crop starting product), particularly preferably in its entirety, in the first miscella.

[0048] The extraction in step (ii) of the second process is preferably carried out at elevated temperature, preferably at 50°C or above, more preferably at 60°C or above, even more preferably at 65°C to 100°C, in particular at 70 to 90°C. This allows deoiling and / or defatting to take place more quickly and completely. The thermal energy required for the extraction in step (ii) is preferably at least partly thermal energy obtained in the combined process, preferably thermal energy obtained during the separation of at least part of the bioethanol from the fermented broth in step (c) (in particular thermal energy obtained during the condensation of the bioethanol after the separation of the bioethanol-water mixture into bioethanol and water), and / or thermal energy obtained during the condensation of the water separated during the drying of the stillage.By utilising thermal energy generated in the combined process, the energy balance of the combined process can be significantly improved.

[0049] The first extraction agent is preferably ethanol, wherein the ethanol preferably has a purity of 99.0% by weight or higher, more preferably 99.5% by weight or higher, particularly preferably 99.9% by weight or higher (based on the weight of the first extraction agent). The use of ethanol, in particular with the stated purity, enables efficient defatting or deoiling of the oil crop starting product; if bioethanol is used, this can also improve sustainability. Preferably, the first extraction agent contains bioethanol produced in the first process, in particular bioethanol separated in step (c) of the first process; particularly preferably, the first extraction agent is bioethanol produced in the first process. Thus, bioethanol produced on site can be used without incurring transport costs.This additional linking of the two combined processes enables a further improvement in process efficiency and sustainability.

[0050] Preferably, at least a portion of the oil and / or fat contained in the first miscella is separated from the first miscella. This separation preferably comprises distillation and / or stripping. This allows separated oil and / or fat to be recovered and used for other applications. The distillation is preferably fractional distillation. This allows individual carbon fractions to be separated from one another, which enables their immediate reuse, for example as fuel. It is preferred if at least a portion of the first extractant contained in the first miscella is separated from the first miscella, preferably by distillation and / or stripping. The at least partial separation of the first extractant from the first miscella enables its reuse in the combined process.The separation of at least a portion of the oil and / or fat (including the separation into individual carbon fractions) and the separation of at least a portion of the first extractant from the first miscella can take place in the same distillation apparatus or in the same stripper. The separation of at least a portion of the oil and / or fat and at least a portion of the first extractant from the first miscella are independent of steps (iii) and (iv) of the second process. Therefore, this separation can be carried out in parallel with step (iii) and / or (iv) of the second process, or even following step (iii) or (iv).

[0051] The separation of at least a portion of the first extractant and optionally also at least a portion of the oil and / or fat from the first miscella is preferably carried out at an elevated temperature, at 50°C or above, more preferably at 60°C or above, even more preferably at 65°C to 100°C, in particular at 70 to 90°C. The thermal energy required for the separation is preferably at least partly thermal energy obtained in the combined process, preferably thermal energy obtained when separating at least a portion of the bioethanol from the fermented broth in step (c) (in particular thermal energy obtained when condensing the bioethanol after separating the bioethanol-water mixture into bioethanol and water), and / or thermal energy obtained when condensing the water separated when drying the stillage.

[0052] When the first extractant is ethanol, the separated first extractant preferably has an ethanol content of 85 wt% or more, more preferably 90 wt% or more, even more preferably 95 wt% or more, based on the weight of the separated first extractant. The ethanol content in the separated first extractant may be slightly lower than the ethanol content of the first extractant (which preferably has a purity of 99.0 wt% or more, as stated above); in particular, water may be separated together with the first extractant.

[0053] Preferably, the first extractant (containing ethanol) separated from the first miscella is used in step (c) of the first process; preferably, it is added to the fermented broth obtained in step (b) of the first process. Preferably, the separated first extractant is added to the fermented broth, preferably after at least partially separating water and / or stillage from the fermented broth, in particular after partially distilling the fermented broth. When adding the separated first extractant to the fermented broth (preferably after partially distilling it), the ethanol content of the fermented broth can preferably be increased by 1 wt% or more, more preferably by 1.5 wt% or more, even more preferably by 2 wt% or more.This allows the separation, in particular distillation, in step (c) to be carried out as efficiently as possible, especially since the ethanol content of the separated first extractant can be higher than the ethanol content of the fermented broth immediately after its fermentation. The use of the separated first extractant in step (c) of the first process makes it possible to separate at least a portion of the ethanol contained in the first extractant, together with at least a portion of the bioethanol obtained by fermentation in step (b), from the fermented broth. A separate dewatering step for the first extractant can thus be omitted, since this is carried out during step (c). This reduces the acquisition costs for the second process. Preferably, bioethanol produced in the first process is used as the first extractant, and at least a portion of the first extractant is used in step (c) of the first process.Thus, (bio)ethanol can circulate within the combined process. Alternatively or additionally, it is preferred if the separated first extraction agent (containing bioethanol) is used to separate the first extraction product into the first mixture and the second mixture, in particular as a second extraction agent. If necessary, water can be added to adjust the ethanol content according to the ethanol content suitable for the second extraction agent. This also enables circulation of (bio)ethanol within the combined process according to the invention. This circulation contributes significantly to improving the process efficiency and sustainability of the combined process.

[0054] The first extractant (containing ethanol, preferably bioethanol) separated from the first miscella can be stored prior to its use in the first process, in particular in the storage container, optionally together with the cleaning agent (also containing ethanol, preferably bioethanol) used to clean the molecular sieve (in step (c) of the first process). This makes it possible, depending on need, availability, and / or capacity, to remove at least a portion of the stored first extractant, or a mixture of the stored first extractant and the stored cleaning agent, for further use in the combined process.

[0055] In step (iii) of the second process, the first extraction product is separated into the first mixture containing the oleaginous fruit protein product and the second mixture containing the oleaginous fruit by-product. The design of the second process after step (ii) may vary depending on the oleaginous fruit protein product to be produced; in particular, a different process procedure may be required for the production of the oleaginous fruit protein isolate and the oleaginous fruit protein concentrate.

[0056] In the second process, the simultaneous production of the oleaginous fruit protein isolate and the oleaginous fruit protein concentrate can also occur. This can be achieved by using a first portion of the first extraction product to produce the oleaginous fruit protein concentrate and a second portion of the first extraction product to produce the oleaginous fruit protein isolate. The possibility of producing both of these oleaginous fruit protein products increases the flexibility of the combined process, especially since, depending on demand or order situation, either both oleaginous fruit protein products or just one of them can be produced simultaneously.

[0057] If the oleaginous protein product to be produced is an oleaginous protein concentrate, in particular a soy protein concentrate, the first extraction product in step (iii) is preferably extracted with a second extraction agent to separate it into the first mixture and the second mixture. The second mixture is also referred to as a second miscella. The first mixture contains the oleaginous protein concentrate and, optionally, a small amount of remaining second extraction agent. The second mixture contains an oleaginous by-product containing the oleaginous molasses. The oleaginous molasses typically contains carbohydrates, a small amount of proteins, fats, and fibers. Furthermore, the second mixture contains the majority of the second extraction agent.

[0058] The extraction in step (iii) of the second process is preferably carried out at elevated temperature, preferably at 25°C or above, more preferably at 30°C or above, even more preferably at 35 to 50°C. This allows the separation of the first extraction product into the first mixture and the second mixture to take place more quickly and effectively. The thermal energy required for the extraction in step (iii) is preferably at least partly thermal energy obtained in the combined process, preferably thermal energy obtained during the separation of at least a portion of the bioethanol from the fermented broth in step (c) (in particular thermal energy obtained during the condensation of the bioethanol after the separation of the bioethanol-water mixture into bioethanol and water), and / or thermal energy obtained during the condensation of the water separated during the drying of the stillage.By using thermal energy obtained in the combined process, the energy balance of the combined process can be significantly improved.

[0059] The second extraction agent preferably contains ethanol (in particular bioethanol) and water (e.g., 20 to 90 wt% or 40 to 90 wt%; Peng et al., Foods 10 (2021), 2222), wherein the ethanol content is preferably in the range of 55 to 90 wt%, more preferably 60 to 80 wt%, based on the weight of the second extraction agent. The ethanol contained in the second extraction agent preferably contains bioethanol produced in the first process, in particular bioethanol separated in step (c) of the first process; particularly preferably, the ethanol contained in the second extraction agent is bioethanol produced in the first process. This additional linking of the two combined processes enables a further improvement in process efficiency. By extraction with the second extraction agent, carbohydrates can be extracted from the first extraction product.These carbohydrates are then preferably at least partially, more preferably mostly, contained in the second miscella.

[0060] It is preferred if at least a portion of the second extractant is separated from the second mixture, preferably by distillation and / or stripping. The at least partial separation of the second extractant enables its reuse. On the one hand, the separated second extractant can subsequently be reused as the second extractant. The separation of at least a portion of the second extractant from the second mixture preferably takes place at an elevated temperature, preferably at 25°C or above, more preferably at 30°C or above, even more preferably at 35 to 50°C.The thermal energy required for the separation is preferably thermal energy obtained at least in part in the combined process, preferably thermal energy obtained when separating at least part of the bioethanol from the fermented broth in step (c) (in particular thermal energy obtained when condensing the bioethanol after separating the bioethanol-water mixture into bioethanol and water), and / or thermal energy obtained when condensing the water separated during drying of the stillage.

[0061] When the second extractant contains ethanol (especially bioethanol), the second extractant separated from the second mixture preferably has an ethanol content of 55 wt% or more, more preferably 60 wt% or more, even more preferably 65 wt% or more, particularly preferably 70 wt% or more, based on the weight of the separated second extractant; the remaining portion (to obtain 100 wt%) is preferably water. This allows a suitable ratio of ethanol to water to efficiently carry out the second extraction. If the separated second extractant containing ethanol and water is reused as the second extractant, dehydration of the ethanol can be omitted. At least a portion of the second extractant is preferably reused as the second extractant.Optionally, the separated second extractant can be purified before reuse as a second extractant, wherein the purification preferably comprises filtration. On the other hand, if the separated second extractant contains ethanol (in particular bioethanol) and water, it can be used in step (c) of the first process. Preferably, the separated second extractant is added to the fermented broth obtained in step (b) of the first process, preferably after at least partially separating water and / or stillage from the fermented broth, in particular after partially distilling the fermented broth. Then, in step (c) of the first process, at least a portion of the ethanol used as the second extractant can be separated from the fermented broth together with at least a portion of the bioethanol obtained by fermentation in step (b).Accordingly, separate dewatering of the separated second extractant is eliminated, which is advantageous from a process engineering perspective. Particularly preferably, bioethanol produced in the first process is used as the second extractant, and at least a portion of the second extractant is subsequently used in step (c) of the first process. This allows for bioethanol to be circulated in the combined process, further improving sustainability and process efficiency.

[0062] The separated second extractant (containing ethanol and water) can be stored, in particular in the storage container, prior to its reuse as a second extractant and / or prior to its use in step (c) of the first process. This makes it possible to remove at least a portion of the stored second extractant as needed, depending on availability, and / or capacity. If the separated first extractant (containing ethanol) is also stored, the separated first extractant, the separated second extractant, and optionally the cleaning agent (containing ethanol) used to clean the molecular sieve (in step (c) of the first process) can be stored together, in particular if both the separated first and second extractants contain ethanol.

[0063] If the oilseed protein product to be produced is an oilseed protein isolate, in particular a soy protein isolate, preferably at least a portion of the first extractant contained in the first extraction product is separated from the first extraction product between steps (ii) and (iii). This separation is preferably carried out by evaporation. By at least partially separating the first extractant, in particular ethanol, from the first extraction product, the first extraction product can be better separated into the first and second mixtures in the subsequent step (iii). The thermal energy required for evaporation is preferably at least partially thermal energy obtained in the combined process, preferably thermal energy obtained during the separation of at least a portion of the bioethanol from the fermented broth in step (c), and / or thermal energy obtained during the condensation of the water separated during the drying of the stillage.This significantly improves the energy balance of the combined process. The evaporated first extractant can subsequently be condensed. The thermal energy obtained in this process can also be used in the combined process. The first extractant separated from the first extraction product, if it contains ethanol (especially bioethanol), is preferably used in step (c) of the first process. The separated first extractant is preferably added to the fermented broth obtained in step (b) of the first process, preferably after at least partial separation of water and / or stillage from the fermented broth, in particular after partial distillation of the fermented broth.Then, in step (c) of the first process, at least a portion of the ethanol, in particular bioethanol, used as the first extractant can be separated from the (preferably partially distilled) fermented broth, together with at least a portion of the bioethanol obtained by fermentation in step (b). Thus, (bio)ethanol can circulate in the combined process, contributing to improving the process efficiency and sustainability of the combined process.

[0064] If the oilseed protein product to be produced is an oilseed protein isolate, water is preferably added to the first extraction product in step (iii), the pH is preferably adjusted to 7-9.5, more preferably to 9, the undissolved residue is separated off, and then the pH of the first, now dissolved extraction product is adjusted essentially to the isoelectric point, preferably at pH 3 to pH 5, of the oilseed protein product in order to precipitate at least a portion of the oilseed protein isolate. Thus, the extraction is first carried out under neutral alkaline conditions, the residue is separated off, and finally the precipitation is carried out isoelectrically, optionally with appropriate pH adjustment. This allows the first extraction product to be separated into the first (precipitated) mixture and the second mixture. The first mixture contains the oilseed protein isolate and, optionally, a small amount of the water added beforehand in step (iii).The second mixture contains the oleaginous fruit by-product, which contains the oleaginous fruit protein liquor. Oleaginous fruit protein liquor typically contains carbohydrates, proteins, and fats, but (unlike oleaginous fruit molasses) no okara (or only a comparatively small proportion of okara). The fat content of this product is therefore preferably negligible and is therefore preferably below 2% by weight, more preferably below 1% by weight, in particular in the range of 0.5 to 0.2% by weight. Furthermore, the second mixture preferably contains the majority of the water added in step (iii). Okara is generally referred to as a by-product of soy product production, consisting of the fibers and proteins left over from the soybean during the production of soy products (such as soy milk or tofu). It contains proteins, fiber, vitamins (vitamin D), soy lecithin, linoleic acid, linolenic acid, phytosterols, tocopherol, and minerals such as calcium, phosphorus, and iron.Okara consists of 76 to 80% water, 3.5 to 4.0% protein, and 20 to 24% solids. In its moist state, okara contains 8 to 15% lipids, 12 to 14.5% crude fiber, 24% protein, and 17% of the protein of the original soybeans.

[0065] In step (iv) of the second process, at least a portion of the oilseed protein product, in particular soy protein product, is separated from the first mixture, and optionally at least a portion of the oilseed by-product, in particular soy by-product, is separated from the second mixture.

[0066] If the oilseed protein product to be produced is an oilseed protein concentrate, in step (iv) at least a portion of the oilseed protein concentrate is separated from the first mixture, in particular from the second extractant. The separation preferably comprises evaporating at least a portion of the second extractant. The thermal energy required for the evaporation is preferably at least partly the thermal energy obtained in the combined process, preferably the thermal energy obtained during the separation of at least a portion of the bioethanol from the fermented broth in step (c), and / or the thermal energy obtained during the condensation of the water separated during the drying of the stillage. This allows the energy balance of the combined process to be significantly improved. The evaporated second extractant can be condensed and subsequently reused.If the second extraction agent contains ethanol (in particular bioethanol), the separated second extraction agent is preferably added to the fermented broth obtained in step (b) of the first process; if appropriate, it is preferably condensed beforehand. Then, in step (c) of the first process, at least a portion of the ethanol, in particular bioethanol, contained in the second extraction agent can be separated from the fermented broth together with at least a portion of the bioethanol obtained by fermentation in step (b) of the first process. The produced bioethanol can subsequently be (re)used as the first and / or second extraction agent. Thus, bioethanol can circulate in the combined process. Before being added to the fermented broth, the second extraction agent separated from the oilseed protein concentrate can be stored, in particular in a storage container.If the second extractant is condensed after separation, thermal energy can be recovered. This can be used in the combined process, further improving the energy balance of the combined process.

[0067] The oleaginous fruit protein concentrate separated in step (iv) is preferably subsequently dried. This allows any remaining second extractant to be removed. Thermal energy obtained in the combined process is also preferably used, at least in part, for the drying, which preferably takes place at elevated temperature. Preferably, after step (iv) of the second process, in particular after drying, the oleaginous fruit protein concentrate contains an amount of second extractant (i.e., in particular ethanol) of 0.1% by weight or less, more preferably 0.01% by weight or less, even more preferably 0.001% by weight or less, based on the total weight of the oleaginous fruit protein concentrate. The oleaginous fruit protein concentrate thus preferably has a high purity and is ready for sale or consumption.The oleaginous fruit protein concentrate can be collected after step (iv) of the second process, in particular after drying, in particular in a second collection container. The second collection container can be of a suitable size for sale, or the oleaginous fruit protein concentrate can subsequently be transferred into a suitable container. The produced oleaginous fruit protein concentrate is preferably used as a high-quality food and / or animal feed.

[0068] If the oleaginous plant by-product contains an oleaginous plant molasses, preferably in step (iv) at least a portion of the oleaginous plant by-product containing the oleaginous plant molasses is separated from the second mixture (in particular from the second miscella). The separation preferably comprises stripping and / or decanting. Preferably, at least a portion of the separated oleaginous plant by-product is used in the first process and is contained in the mash provided in step (a), preferably at least partially in the mashed state. The oleaginous plant by-product may be evaporated prior to its use in the first process. This allows the water content of the oleaginous plant by-product to be reduced. The water separated from the oleaginous plant by-product is preferably treated (i.e., purified) so that it can be reused.

[0069] The separation of at least a portion of the oilseed by-product from the second mixture is preferably carried out at an elevated temperature, preferably at 25°C or above, more preferably at 30°C or above, even more preferably at 35 to 50°C. The thermal energy required for the separation is preferably at least partly thermal energy obtained in the combined process, preferably thermal energy obtained during the separation of at least a portion of the bioethanol from the fermented broth in step (c) (in particular thermal energy obtained during the condensation of the bioethanol after the separation of the bioethanol-water mixture into bioethanol and water), and / or thermal energy obtained during the condensation of the water separated during the drying of the stillage.

[0070] If the oil crop by-product contains oil crop molasses, preferably in step (iv) at least a portion of the second extractant is separated from the second mixture. The separation preferably comprises distilling, stripping, centrifuging, evaporating, and / or decanting. The second extractant separated from the second mixture, in particular from the oil crop by-product containing the oil crop molasses, can be reused. If the second extractant contains ethanol (in particular bioethanol), the second extractant separated by evaporation is preferably optionally condensed and used in step (c) of the first process.Preferably, the separated second extractant is added to the fermented broth obtained in step (b) of the first process, preferably after at least partially separating water and / or stillage from the fermented broth, in particular after partially distilling the fermented broth. Then, in step (c) of the first process, at least a portion of the ethanol, in particular bioethanol, contained in the second extractant can be separated from the (preferably partially distilled) fermented broth together with at least a portion of the bioethanol obtained by fermentation in step (b) of the first process. The bioethanol produced can subsequently be (re)used as the first and / or second extractant. Thus, bioethanol can circulate in the combined process.Before being added to the fermented broth, the second extractant separated from the second mixture can be stored, in particular in the storage container.

[0071] At least a portion of the second mixture can be used in the first process after separating at least a portion of the second extractant, and this portion of the second mixture can be contained in the mash provided in step (a). The second mixture can be evaporated prior to its use in the first process. This allows the water content of the second mixture to be reduced. Preferably, the second mixture used in the first process has a dry matter weight of 10 to 80 wt%, more preferably 15 to 50 wt%, even more preferably 20 to 40 wt%, particularly preferably 25 to 35 wt%, based on the total weight of the second mixture.Overall, at least a portion of the second mixture (after at least a portion of the second extractant has been separated) and / or at least a portion of the oleaginous by-product (after separating at least a portion of the oleaginous by-product from the second mixture) can be used in the first process and contained in the mash provided in step (a). Preferably, at least a portion of the oleaginous by-product is separated from the second mixture and used in the first process, so that this portion of the oleaginous by-product is contained in the mash provided in step (a). The separation of at least a portion of the oleaginous by-product and at least a portion of the second extractant from the second mixture, in particular the at least partial separation of the oleaginous by-product and the second extractant from one another, preferably takes place in the same distillation apparatus or in the same stripper.This simplifies the procedure.

[0072] If the oilseed protein product to be produced is an oilseed protein isolate, in particular a soy protein isolate, the separation of at least a portion of the oilseed protein isolate from the first mixture in step (iv) of the second process preferably comprises dewatering the oilseed protein isolate, in particular evaporating water, centrifuging, decanting, and / or sedimenting. Preferably, the oilseed protein isolate is washed with water before dewatering. This can improve the purity of the oilseed protein isolate. The separated oilseed protein isolate is preferably dried, in particular spray-dried. This allows any remaining water to be removed. Water separated from the first mixture, in particular from the oilseed protein isolate, in step (iv) is preferably treated for reuse.Preferably, after step (iv) of the second process, in particular after drying, the oleaginous fruit protein isolate contains a water content of 15% by weight or less, more preferably 10% by weight or less, even more preferably 8% by weight or less, in particular 2 to 7% by weight, based on the total weight of the oleaginous fruit protein isolate. The oleaginous fruit protein isolate thus preferably has a high purity and is accordingly ready for sale or consumption.

[0073] At least a portion of the second mixture (containing the oleaginous by-product) can be used in the first process, and this portion of the second mixture can be included in the mash provided in step (a). Preferably, however, in step (iv) of the second process, at least a portion of the oleaginous by-product (containing the oleaginous protein liquor) is separated from the second mixture. Separation preferably comprises dewatering the oleaginous by-product, in particular evaporating water, centrifuging, decanting, and / or sedimenting. This can reduce the water content of the oleaginous by-product. It is preferred if separating at least a portion of the oleaginous by-product from the second mixture comprises evaporating water. Water separated from the second mixture, in particular from the oleaginous by-product, in step (iv) is preferably treated for reuse.

[0074] The oilseed protein product, in particular soy protein product, produced in the second process can be collected, in particular in a second collection container. The oilseed protein product produced in the second process is preferably used as animal feed and / or as food.

[0075] If, in the second process, the oleaginous fruit protein isolate and the oleaginous fruit protein concentrate are produced simultaneously and / or consecutively (e.g., alternately), resulting in both an oleaginous fruit by-product containing the oleaginous fruit molasses and an oleaginous fruit by-product containing the oleaginous fruit protein liquor, preferably at least a portion of the oleaginous fruit by-product containing the oleaginous fruit molasses and at least a portion of the oleaginous fruit by-product containing the oleaginous fruit protein liquor, or at least a portion of the second mixture containing the respective oleaginous fruit by-product, are used together in the first process. In this case, the mash prepared in step (a) of the first process contains the oleaginous fruit protein liquor and the oleaginous fruit molasses. This allows the oleaginous fruit by-products produced in the combined process to be utilized to the greatest possible extent. Animal feed

[0076] The invention further relates to a feedstuff obtainable by the combined process according to the invention and containing shells of oilseeds, preferably crushed shells of oilseeds, in particular ground shells of oilseeds, wherein the oilseeds preferably contain soybeans, in particular soybeans, sunflower seeds, and / or rapeseeds. This results in an increased value of the shells of the oilseeds, since they are otherwise difficult to sell on the market and are therefore often burned.

[0077] The invention further relates to a feed obtainable by the combined process according to the invention and containing the oilseed by-product, in particular the oilseed molasses and / or the oilseed protein liquor. Preferably, the oilseed molasses is soy molasses, and / or the oilseed protein liquor is soy protein liquor.

[0078] Although in the combined process, the oilseed by-product resulting from the second process is used in the first process, if the amount of oilseed by-product is so large that, for capacity reasons, the entire amount cannot be mashed together with carbohydrate-containing starting material, the remainder of the oilseed by-product can be used as a feed additive and thus also be put to good use. Preferably, the feed also contains oilseed shells, more preferably crushed oilseed shells, in particular ground oilseed shells, where the oilseeds preferably contain soybeans, sunflower seeds, and / or rapeseeds, in particular where the oilseeds are soybeans. Thus, the oilseed shells can also be put to good use.

[0079] Combined system

[0080] The invention further relates to a combined plant for producing bioethanol and an oilseed protein product using the combined process according to the invention, comprising a first plant for producing the bioethanol, comprising a fermenter for fermenting the mash, and a first separation unit for separating at least a portion of the bioethanol from the fermented broth; and a second plant for producing the oilseed protein product, comprising a first extraction device for extracting the oilseed starting product with the first extraction agent, a second separation unit for separating the first extraction product into the first mixture and the second mixture, a third separation unit for separating at least a portion of the oilseed protein product from the first mixture,and optionally a fourth separation unit for separating at least a portion of the oilseed by-product from the second mixture; wherein the second plant optionally comprises a fifth separation unit for separating at least a portion of the first extractant contained in the first miscella. The first separation unit of the first plant is connected downstream of the fermenter. Preferably, the first separation unit comprises a distillation apparatus. This allows at least a portion of the bioethanol to be separated not only from the fermented broth, but also from at least a portion of the water, thereby obtaining a bioethanol-water mixture. Furthermore, the first separation unit preferably comprises a molecular sieve, a membrane, and / or an adsorbent, particularly preferably a molecular sieve. This allows the bioethanol-water mixture to be separated into bioethanol and water. The molecular sieve,The membrane and / or the adsorbent are preferably arranged downstream of the distillation apparatus of the first separation unit. Preferably, a section of the first separation unit comprising the molecular sieve is connected to the fermenter such that carbon dioxide can be conducted from the fermenter to this section of the first separation unit. Alternatively or additionally, it is preferred if this section of the first separation unit comprising the molecular sieve is connected to the distillation apparatus of the first separation unit such that an ethanol-containing cleaning agent used to clean the molecular sieve can be conducted from the section of the first separation unit comprising the molecular sieve to the distillation apparatus. The ethanol-containing cleaning agent used can then be added to the fermented broth, preferably after at least partially separating water and / or stillage from the fermented broth.in particular after partial distillation of the fermented broth. Furthermore, it is alternatively or additionally preferred that the section of the first separation unit containing the molecular sieve be connected to the second separation unit, in particular to a second extraction device of the second separation unit. Then, ethanol-containing cleaning agent used to dewater (regenerate) the molecular sieve can be fed to the second extraction device for use as the second extraction agent.

[0081] The first plant preferably has a mashing apparatus for mashing a mixture containing the carbohydrate-containing starting material and the oilseed by-product. This is located upstream of the fermenter. The mashing apparatus is preferably connected to the fourth separation unit. The oilseed by-product obtained in the second process can then be fed directly from the fourth separation unit to the mashing apparatus.

[0082] The first system preferably comprises a comminution unit for comminution of the carbohydrate-containing starting material, and optionally of shells of oilseeds, in particular soybeans. The comminution unit can be a comminution unit for dry grinding and / or wet grinding. The comminution unit can comprise a mill and / or a pestle. The mill can comprise, for example, a conical, disc, and / or impact mill. This allows the carbohydrate-containing starting material to be efficiently comminuted. The comminution unit is located upstream of the fermenter and, optionally, the mashing apparatus.

[0083] Furthermore, it is preferred if the first plant has a dryer, in particular a feed dryer, for drying the stillage. The dryer is preferably connected to the first separation unit, in particular to the distillation apparatus of the first separation unit. The stillage separated in the first separation unit, in particular in the distillation apparatus, can then be fed to the dryer. If present, the dryer is preferably connected to the comminution unit of the first plant, in particular if the comminution unit is designed to comminute the carbohydrate-containing starting material in the wet state. Fibers, corn gluten, and / or corn gluten feed separated from the carbohydrate-containing starting material during comminution, in particular during wet milling, can then be dried together with the stillage.

[0084] The first plant, in particular the first separation unit, preferably has a first collecting container for collecting the bioethanol produced in the first process.

[0085] It is preferred if the first extraction device is connected to the first separation unit, in particular to the first collection container, in particular such that bioethanol produced in the first process and optionally collected in the first collection container can be fed to the first extraction device for use as the first extraction agent. This simplifies the process control, since bioethanol produced in the first plant can be fed directly to the first extraction device.

[0086] The second separation unit is connected downstream of the first extraction device. If the oilseed protein product to be produced is an oilseed protein concentrate, the second separation unit preferably has a second extraction device for separating the first extraction product into the first mixture and the second mixture. If the oilseed protein product to be produced is an oilseed protein isolate, the second separation unit preferably has a dryer and a precipitation device. The precipitation device is connected downstream of the dryer. The dryer can be used to separate at least a portion of the first extractant contained in the first extraction product from the first extraction product. The precipitation device can be used to separate the first extraction product into the first (precipitated) mixture and the second mixture.

[0087] The third separation unit is located downstream of the second separation unit. Preferably, the third separation unit comprises a dryer. The dryer can be configured to separate at least a portion of the oilseed protein product from the first mixture under reduced pressure (e.g., at 800 mbar or below) and / or at elevated temperature. The separated oilseed protein product can also be further dried in the dryer of the third separation unit to remove any remaining second extractant.

[0088] The fourth separation unit is connected to the second separation unit. It is configured to separate at least a portion of the oilseed by-product from the second mixture. The fourth separation unit preferably comprises a stripper, a distillation apparatus, a centrifuge, a decanter, a sedimenter, and / or an evaporator. If the oilseed by-product contains oilseed molasses, the fourth separation unit preferably comprises a distillation apparatus or a stripper configured to separate both a portion of the oilseed by-product and a portion of the second extractant from the second mixture. The separation can thus take place in the same distillation apparatus or stripper, which significantly simplifies the design of the combined plant and the process control.Preferably, the fourth separation unit is connected to the mashing apparatus and / or to the dryer, in particular the feed dryer, of the first plant. Then, oilseed by-product separated in the fourth separation unit can be fed to the first plant so that it can be contained in the mash prepared in step (a), and / or the oilseed by-product can be fed to the dryer and dried together with the stillage.

[0089] The second system preferably also comprises a fifth separation unit for separating at least a portion of the first extractant contained in the first miscella and / or for separating at least a portion of the oil and / or fat contained in the first miscella. The fifth separation unit is preferably connected to the first extraction device. The fifth separation unit preferably comprises a distillation apparatus or a stripper configured to separate both a portion of the first extractant and a portion of the oil and / or fat from the first miscella. The separation can thus take place in the same distillation apparatus or stripper, which significantly simplifies the design of the combined system and the process control.If the second separation unit has a second extraction device, the fifth separation unit is preferably connected to the second separation unit, in particular to the second extraction device. The first extractant separated from the first miscella can then be fed to the second separation unit for use as the second extractant. Additionally or alternatively, it is also preferred if the fifth separation unit is connected to the first separation unit, in particular to the distillation apparatus of the first separation unit.Then, the first extractant separated from the first miscella can be fed to the first separation unit, in particular the distillation apparatus, and added to the fermented broth obtained in step (b) of the first process, preferably after at least partial separation of water and / or stillage from the fermented broth, in particular after partial distillation of the fermented broth.

[0090] The second plant preferably comprises an evaporator configured to evaporate the second mixture and / or the oilseed by-product. This evaporator is preferably connected to the second separation unit and / or the fourth separation unit, as well as to the mashing apparatus, if present. Thus, the second mixture obtained in step (iii) of the combined process, in particular the second miscella, and / or the oilseed by-product can be evaporated prior to use in the first process.

[0091] It is preferred if the second plant has a processing unit for processing the provided oilseed starting product. The processing unit is connected upstream of the first extraction device. The processing unit preferably has a peeling unit for peeling the oilseed starting product and / or a comminution unit for comminution of the oilseed starting product. The comminution unit can have a mill and / or a pestle. The mill can, for example, have a conical, disc, and / or impact mill. This allows the oilseed starting product to be efficiently comminuted. The processing unit, in particular the peeling unit, of the second plant is preferably connected to the comminution unit of the first plant. Hulls separated from the oilseeds can then be fed to the comminution unit of the first plant and comminuted together with the carbohydrate-containing starting material.Alternatively or additionally, the processing unit, in particular the hulling unit, of the second plant is preferably connected to the dryer, in particular the feed dryer, of the first plant. Hulls separated from the oilseed crops, in particular soybeans, can then be dried together with the stillage.

[0092] The second plant, in particular the third separation unit, preferably comprises a second collecting container for collecting the oilseed protein product produced in the second process.

[0093] The combined system, in particular the first separation unit, preferably comprises a storage tank for storing separated first extractant, separated second extractant, and / or separated cleaning agent, each containing ethanol, preferably bioethanol. This storage tank is preferably connected to the distillation apparatus of the first separation unit. Furthermore, the storage tank is preferably connected to the section of the first separation unit containing the molecular sieve, to the second separation unit, to the third separation unit, to the fourth separation unit, and / or to the fifth separation unit.The storage container can store ethanol-containing cleaning agent used to clean the molecular sieve; the first extractant separated from the first miscella; the second extractant separated from the second mixture; and / or the second extractant separated from the oilseed protein product, in particular the oilseed protein concentrate, in particular prior to their further use in the combined process.

[0094] Preferably, the combined plant, in particular the first plant, comprises a wastewater treatment unit. The wastewater treatment unit is preferably connected to the first separation unit and / or to the dryer (in particular, the feed dryer) of the first plant. Water separated in these plant components can then be fed to the wastewater treatment unit for purification.

[0095] The first extraction device, the second separation unit, the third separation unit, the fourth separation unit, the fifth separation unit, and / or the processing plant is / are preferably connected to the first separation unit, in particular to the molecular sieve, and / or to the dryer, in particular to the feed dryer, of the first plant, in particular to a connecting element suitable for transporting thermal energy. The connecting element can comprise a pipe and / or a line, preferably with thermal insulation. Thermal energy obtained in the combined plant, in particular in the first plant, can then be used in the combined process, in particular in the second plant. The thermal energy can be transported by known methods. For example, the thermal energy can be transported by means of a heat transfer fluid, in particular water.

[0096] In a preferred embodiment, the second plant comprises two second separation units, two third separation units, optionally two fourth separation units, and optionally two second collection containers. The second plant is then configured to produce oleaginous fruit protein isolate and oleaginous fruit protein concentrate simultaneously and / or sequentially. For example, a first portion of the first extraction product can be used to produce the oleaginous fruit protein concentrate, in particular soy protein concentrate, and a second portion of the first extraction product can be used to produce the oleaginous fruit protein isolate, in particular soy protein isolate.

[0097] Whenever "ethanol" is mentioned in the present disclosure, "bioethanol" is also meant; this does not apply to the reverse case, ie, when "bioethanol" is mentioned, "ethanol" (which can also be obtained from petroleum, for example) is not meant.

[0098] In this disclosure, the term "connecting one system component to another" means that these two system components are fluidly connected. By means of the fluid connection, a fluid (e.g., bioethanol) can be transported directly between system components, which simplifies the process control.

[0099] Oilseed protein products obtainable according to the invention

[0100] According to a further aspect, the present invention relates to oleaginous protein products obtainable by the combined process according to the invention, in particular oleaginous protein concentrates, oleaginous protein isolates, oleaginous oil products, oleaginous lecithin products, or oleaginous fiber products. Particular preference is given to products obtainable from the use of soy-based starting materials, i.e., in particular, soy protein concentrates (SPCs), soy protein isolates (SPIs), soy oil products, soy lecithin products, or soy fiber products.

[0101] The oilseed protein products produced using the combination process according to the invention exhibit special features due to the extraction with bioethanol from the first process, which have a positive effect on the content and efficacy of the ingredients, such as phytoestrogens or inhibitors (trypsin inhibitors), or on the presence of known contaminants in the starting material (tropane alkaloids (from henbane, datura, or deadly nightshade, such as atropine and scopolamine) or mycotoxins (deoxynivalenol, T2 and HT2 toxins, or zearalenone)) in the final product. In particular, contaminants such as mycotoxins can accumulate in a stand-alone ethanol process because ethanol is constantly circulating. This accumulation is prevented or at least reduced by the inventive drain in the main product of the combination process in the ethanol process and is therefore advantageous in any case.In particular, the quality of the bioethanol used in the first process as an extraction agent allows a gentle and improved extraction of the oilseed protein products in the process according to the invention, whereby overall improved oilseed protein products can also be obtained.

[0102] The invention particularly relates to the following embodiments: 1. Combined process comprising a first process for producing bioethanol and a second process for producing an oilseed protein product, the first process comprising the steps

[0103] (a) providing a mash, the mash containing a carbohydrate-containing starting material,

[0104] (b) fermenting the mash to obtain a fermented broth containing bioethanol, and

[0105] (c) separating at least a portion of the bioethanol from the fermented broth; and the second process comprising the steps

[0106] (i) providing an oilseed crop product,

[0107] (ii) extracting the oilseed crop starting product with a first extraction agent to obtain a first miscella and a first extraction product,

[0108] (iii) separating the first extraction product into a first mixture containing the oilseed protein product and a second mixture containing the oilseed by-product,

[0109] (iv) separating at least a portion of the oleaginous protein product from the first mixture, and optionally separating at least a portion of the oleaginous by-product from the second mixture; preferably wherein the mash provided in step (a) of the first process contains at least a portion of the oleaginous by-product obtained in the second process.

[0110] 2. A combined process comprising a first process for producing bioethanol and a second process for producing an oilseed protein product, the first process comprising the steps

[0111] (a) providing a mash, the mash containing a carbohydrate-containing starting material,

[0112] (b) fermenting the mash to obtain a fermented broth containing bioethanol, and

[0113] (c) separating at least a portion of the bioethanol from the fermented broth; and the second process comprising the steps

[0114] (i) providing an oilseed crop product,

[0115] (ii) extracting the oilseed crop starting product with a first extraction agent to obtain a first miscella and a first extraction product,

[0116] (iii) separating the first extraction product into a first mixture containing the oilseed protein product and a second mixture containing the oilseed by-product,

[0117] (iv) separating at least a portion of the oilseed protein product from the first mixture, and optionally separating at least a portion of the oilseed by-product from the second mixture;wherein the mash provided in step (a) of the first process contains at least a portion of the oilseed by-product obtained in the second process or at least a portion of the oilseed by-product obtained in the second process is added during step (b), wherein the first extractant contains bioethanol produced in the first process, preferably wherein the first extractant is bioethanol produced in the first process, wherein the first miscella contains at least a portion of the first extractant, and wherein at least a portion of the first extractant contained in the first miscella is separated from the first miscella and used in step (c) of the first process, preferably wherein the separated first extractant is added to the fermented broth obtained in step (b) of the first process, in particular after at least partial separation of water and / or stillage from the fermented broth.;

[0118] 3. A combined process comprising a first process for producing bioethanol and a second process for producing an oilseed protein product, the first process comprising the steps

[0119] (a) providing a mash, the mash containing a carbohydrate-containing starting material,

[0120] (b) fermenting the mash to obtain a fermented broth containing bioethanol, and

[0121] (c) separating at least a portion of the bioethanol from the fermented broth; and the second process comprising the steps

[0122] (i) providing an oilseed crop product,

[0123] (ii) extracting the oilseed crop starting product with a first extraction agent to obtain a first miscella and a first extraction product,

[0124] (iii) separating the first extraction product into a first mixture containing the oilseed protein product and a second mixture containing the oilseed by-product,

[0125] (iv) separating at least a portion of the oleaginous plant protein product from the first mixture, and optionally separating at least a portion of the oleaginous plant by-product from the second mixture; wherein the provision of the oleaginous plant starting product in step (i) of the second process comprises separating oleaginous plant skins, and wherein the mash provided in step (a) of the first process contains at least a portion of the oleaginous plant by-product obtained in the second process and crushed oleaginous plant skins, the skins being at least a portion of the skins separated from the oleaginous plants in step (i) of the second process.

[0126] 4. The combined process according to any one of embodiments 1 to 3, wherein the mash provided in step (a) is obtained by mashing the carbohydrate-containing starting material and the oilseed by-product, preferably in the presence of water. 5. The combined process according to any one of embodiments 1 to 4, wherein the carbohydrate-containing starting material is a cereal, preferably corn and / or wheat.

[0127] 6. The combined process according to any one of embodiments 1 to 5, wherein the mashing is carried out at a temperature of 60 to 130°C, preferably at 80 to 120°C; and / or wherein the mashing is carried out for a period of 0.5 h or more, preferably for 2 h or more, more preferably for 1 to 4 h.

[0128] 7. Combined process according to one of embodiments 1 to 6, wherein the mashing takes place in the presence of an enzyme, wherein the enzyme is preferably selected from the group comprising an alpha-amylase, a glucanase, a glucoamylase, a cellulase, a hemicellulase, a beta-glucanase, a xylanase, an arabinase, a galactosidase and a protease, or a mixture thereof, enzyme particularly preferably an alpha-amylase and / or a glucoamylase.

[0129] 8. Combined process according to any one of embodiments 1 to 5, wherein the carbohydrate-containing starting material is comminuted before mashing, preferably by means of dry grinding and / or wet grinding.

[0130] 9. The combined process according to embodiment 8, wherein the carbohydrate-containing starting material is comminuted by dry milling prior to mashing; and / or wherein the carbohydrate-containing starting material is comminuted by wet milling in the presence of water prior to mashing.

[0131] 10. The combined process according to embodiment 8 or 9, wherein the carbohydrate-containing starting material and oilseed shells are comminuted together prior to mashing, preferably by dry milling; preferably wherein the oilseed shells are at least a portion of shells separated from oilseeds in step (i) of the second process.

[0132] 11. The combined process according to any one of embodiments 8 to 10, wherein, prior to mashing, at least a portion of the fibers, corn gluten, and / or corn gluten feed obtained during comminution, in particular during wet milling, of the carbohydrate-containing starting material is separated from the comminuted, carbohydrate-containing starting material; preferably, wherein the separated fibers, corn gluten, and / or corn gluten feed are added to a slurry separated from the fermented broth.

[0133] 12. Combined process according to any one of embodiments 1 to 11, wherein the oilseed by-product contained in the mash provided in step (a) contains at least a portion of the second mixture obtained in step (iii) of the second process and / or at least a portion of the oilseed by-product obtained in step (iv).

[0134] 13. Combined process according to any one of embodiments 1 to 12, wherein the

[0135] Oilseed by-product containing an oilseed molasses and / or an oilseed protein liquor.

[0136] 14. Combined process according to any one of embodiments 1 to 13, wherein the

[0137] Oilseed by-product has a dry matter weight of 10 to 80 wt%, more preferably 15 to 50 wt%, even more preferably 20 to 40 wt%, particularly preferably 25 to 35 wt%, based on the total weight of the oilseed by-product.

[0138] 15. The combined process according to any one of embodiments 1 to 14, wherein the mash provided in step (a) contains the oil crop by-product in an amount of 30 wt% or less, more preferably 20 wt% or less, even more preferably 15 wt% or less, even more preferably 12 wt% or less, even more preferably 10 wt% or less, based on the weight of the carbohydrate-containing starting material.

[0139] 16. Combined process according to embodiment 15, wherein the mash provided in step (a) contains the oil crop by-product in an amount of 1 to 30 wt%, preferably 1 to 20 wt%, more preferably 1 to 15 wt%, even more preferably 1 to 12 wt%, most preferably 5 to 10 wt%, based on the weight of the carbohydrate-containing starting material.

[0140] 17. The combined process according to embodiment 16, wherein the mash has a ratio of oilseed by-product to carbohydrate-containing feedstock of 0.1:10 to 1.5:10 (w / w).

[0141] 18. Combined process according to any one of embodiments 1 to 17, wherein the mash provided in step (a) contains shells of oilseed crops, preferably crushed shells of oilseed crops, wherein the shells are preferably at least a part of shells separated from oilseed crops in step (i) of the second process.

[0142] 19. Combined process according to any one of embodiments 1 to 18, wherein a microorganism, in particular a yeast and / or a bacterium, is added to the mash before and / or in step (b).

[0143] 20. The combined process according to any one of embodiments 1 to 19, wherein the mash is fermented in step (b) at a temperature of 20 to 40°C, more preferably 28 to 36°C. 21. The combined process according to any one of embodiments 1 to 20, wherein the mash is fermented in step (b) for a period of 36 h or more, more preferably for 55 h or more, particularly preferably for a period of 50 to 70 h.

[0144] 22. The combined process according to any one of embodiments 1 to 21, wherein the fermented broth obtained in step (b) contains bioethanol and a stillage, wherein the stillage preferably contains a protein, biomass of the microorganism, a fat, and / or a mineral; preferably wherein in step (c) of the first process, at least a portion of the stillage contained in the fermented broth is separated from the fermented broth; particularly preferably wherein the separated stillage is subsequently dried.

[0145] 23. Combined process according to embodiment 22, wherein the separation of at least a portion of the bioethanol from the fermented broth in step (c), and optionally the separation of at least a portion of the stillage from the fermented broth in step (c), comprises a thermal separation, in particular a distillation.

[0146] 24. Combined process according to embodiment 23, wherein the distillation can separate the stillage from a bioethanol-water mixture, wherein the bioethanol-water mixture preferably contains a proportion of bioethanol of 70 wt% or more, more preferably 75 wt% or more, even more preferably 80 wt% or more, in particular 90 to 95.6 wt%, based on the weight of the bioethanol-water mixture.

[0147] 25. Combined process according to embodiment 24, wherein the separation of at least a portion of the bioethanol from the fermented broth in step (c) comprises distilling and subsequently separating the bioethanol-water mixture into bioethanol and water, wherein the separation of the bioethanol-water mixture into bioethanol and water is preferably carried out by means of a molecular sieve, a membrane process and / or pressure swing adsorption.

[0148] 26. Combined process according to embodiment 25, wherein the bioethanol-water mixture is separated into bioethanol and water by means of a molecular sieve, wherein the temperature during separation by means of the molecular sieve is preferably in the range of 120 to 180 °C, more preferably 160 to 170 °C, and / or wherein the pressure is preferably in the range of 2 to 6 bar, more preferably 3 to 5 bar.

[0149] 27. The combined process according to embodiment 26, wherein the cleaning of the molecular sieve is carried out with an ethanol-containing cleaning agent, preferably wherein the cleaning agent contains ethanol in an amount of 70 wt% or more, more preferably 80 wt% or more, even more preferably 90 wt% or more, particularly preferably 100 wt%, based on the weight of the cleaning agent; wherein the ethanol is particularly preferably bioethanol produced in the first process.

[0150] 28. Combined process according to embodiment 27, wherein the ethanol-containing cleaning agent, in particular the bioethanol-containing cleaning agent, is used after its use for cleaning the molecular sieve in step (c) of the first process and / or is used as a second extraction agent.

[0151] 29. Combined process according to any one of embodiments 26 to 28, wherein the purification of the molecular sieve is carried out with carbon dioxide, preferably wherein carbon dioxide formed during the fermentation in step (b) is used.

[0152] 30. Combined process according to any one of embodiments 1 to 29, wherein the separation of at least a portion of the bioethanol from the fermented broth in step (c) comprises condensing gaseous bioethanol and / or gaseous water, preferably wherein thermal energy obtained thereby is used in the second process, in particular for comminuting oilseeds to obtain the oilseed starting product provided in step (i), for extracting the oilseed starting product with the first extractant in step (ii) and / or for separating the first extraction product into the first and second mixtures in step (iii).

[0153] 31. The combined process according to any one of embodiments 22 to 30, wherein in step (c) at least a portion of a stillage contained in the fermented broth is separated; preferably wherein the separated stillage is subsequently dried.

[0154] 32. The combined process according to embodiment 31, wherein the separated stillage is dried for 0.1 h or more, more preferably for 0.15 h or more, particularly preferably for 0.15 to 0.3 h; and / or wherein the drying of the separated stillage is preferably carried out at a temperature of 60°C or above, more preferably of 100°C or above, particularly preferably at 100 to 140°C.

[0155] 33. The combined process according to embodiment 31 or 32, wherein separated, gaseous water is condensed during drying of the stillage, thereby obtaining thermal energy, which is preferably used in the combined process, in particular for comminuting oilseeds to obtain the oilseed starting product provided in step (i), for extracting the oilseed starting product with the first extractant in step (ii), and / or for separating the first extraction product into the first and second mixtures in step (iii). 34. The combined process according to any one of embodiments 31 to 33, wherein the separated stillage is dried together with oilseed shells, preferably with comminuted oilseed shells.

[0156] 35. Combined process according to embodiment 34, wherein a portion of the skins separated from the oilseed crops in step (i) of the second process is added to the separated stillage.

[0157] 36. Combined process according to any one of embodiments 31 to 35, wherein a portion of the oilseed by-product obtained in the second process is added to the separated stillage, preferably wherein the stillage and the added oilseed by-product are dried together.

[0158] 37. Combined process according to any one of embodiments 31 to 36, wherein the separated, preferably dried, stillage is used as animal feed and / or utilized for energy purposes.

[0159] 38. Combined process according to any one of embodiments 1 to 37, wherein water separated from the bioethanol in step (c) and / or water separated during drying of the stillage is treated.

[0160] 39. The combined process according to any one of embodiments 1 to 38, wherein the oleaginous fruit protein product is an oleaginous fruit protein concentrate and / or an oleaginous fruit protein isolate; preferably, wherein the oleaginous fruit protein isolate and the oleaginous fruit protein concentrate are produced in the second process, wherein a first portion of the first extraction product is used to produce the oleaginous fruit protein concentrate and a second portion of the first extraction product is used to produce the oleaginous fruit protein isolate.

[0161] 40. Combined process according to any one of embodiments 1 to 39, wherein the oilseed by-product obtained in the second process contains a carbohydrate (or a mixture of two or more carbohydrates), wherein preferably at least one carbohydrate, in particular at least one starch, is saccharifiable by mashing.

[0162] 41. The combined process according to embodiment 40, wherein the oilseed by-product contains at least 15% by weight of a saccharifiable carbohydrate, more preferably at least 20% by weight, even more preferably at least 25% by weight, particularly preferably at least 30% by weight, based on the proportion of carbohydrates in the oilseed by-product and based on the dry matter weight of the oilseed by-product. 42. The combined process according to any one of embodiments 1 to 41, wherein the oilseed by-product obtained in the second process contains a protein (or a mixture of two or more proteins).

[0163] 43. Combined process according to any one of embodiments 1 to 42, wherein the provision of the oilseed crop starting product in step (i) comprises separating shells from oilseed crops and / or comminuting the oilseed crops, preferably wherein the oilseed crop starting product contains hulled and / or comminuted soybeans, sunflower seeds and / or rapeseed seeds.

[0164] 44. Combined process according to any one of embodiments 1 to 43, wherein the oil crop starting product is obtained from oil crops, wherein the oil crops are soybeans, sunflower seeds and / or rapeseed seeds.

[0165] 45. Combined process according to embodiment 43 or 44, wherein at least a portion of the separated skins is used in the preparation of the mash provided in step (a) of the first process and / or is dried together with the stillage.

[0166] 46. ​​Combined process according to embodiment 44 or 45, wherein the comminution of the oilseeds takes place at elevated temperature, preferably at a temperature of 50°C or above, more preferably 70°C or above, even more preferably 90°C or above, particularly preferably 110°C or above.

[0167] 47. Combined process according to embodiment 46, wherein the thermal energy required for comminuting the oilseeds at elevated temperature is at least partly thermal energy obtained in the first process, in particular thermal energy obtained in separating at least part of the bioethanol from the fermented broth in step (c), and / or thermal energy obtained in condensing the water separated during drying of the stillage.

[0168] 48. Combined process according to any one of embodiments 1 to 47, wherein the first extraction product obtained in step (ii) contains an at least partially defatted and / or deoiled solid.

[0169] 49. Combined process according to any one of embodiments 1 to 48, wherein the extracting in step (ii) is carried out at elevated temperature, preferably at 50°C or above, more preferably at 60°C or above, even more preferably at 65°C to 100°C, in particular at 70 to 90°C.

[0170] 50. Combined process according to embodiment 49, wherein the thermal energy required for the extraction in step (ii) at elevated temperature is at least partly thermal energy obtained in the combined process, preferably thermal energy obtained in separating at least part of the bioethanol from the fermented broth in step (c), and / or thermal energy obtained in condensing the water separated during drying of the stillage.

[0171] 51. The combined process according to any one of embodiments 1 to 50, wherein the first extractant is ethanol, wherein the ethanol preferably has a purity of 99.0 wt% or above, more preferably 99.5 wt% or above, most preferably 99.9 wt% or above, based on the weight of the first extractant.

[0172] 52. The combined process according to embodiment 51, wherein the first extractant contains bioethanol produced in the first process, preferably wherein the first extractant is bioethanol produced in the first process.

[0173] 53. Combined process according to any one of embodiments 1 to 52, wherein at least a portion of an oil and / or fat contained in the first miscella is separated from the first miscella, wherein the separation preferably comprises distillation, in particular fractional distillation, and / or stripping.

[0174] 54. Combined process according to any one of embodiments 1 to 53, wherein at least a portion of the first extractant contained in the first miscella is separated from the first miscella, preferably by distillation and / or stripping.

[0175] 55. The combined process according to embodiment 54, wherein the first extractant separated from the first miscella has an ethanol content of 85 wt% or higher, more preferably 90 wt% or higher, even more preferably 95 wt% or higher, based on the weight of the separated first extractant.

[0176] 56. The combined process according to embodiment 54 or 55, wherein the first extractant (containing ethanol, in particular bioethanol) separated from the first miscella is added to the fermented broth obtained in step (b) of the first process; and / or wherein the first extractant (containing ethanol, in particular bioethanol) separated from the first miscella is used to separate the first extraction product into the first mixture and the second mixture, in particular as a second extractant.

[0177] 57. The combined process according to any one of embodiments 1 to 56, wherein the second process produces an oilseed protein concentrate, preferably a soy protein concentrate. 58. The combined process according to embodiment 57, wherein the first extraction product in step (iii) is extracted with a second extraction agent to separate it into the first mixture and the second mixture.

[0178] 59. The combined process according to embodiment 58, wherein the extracting in step (iii) is carried out at elevated temperature, preferably at 25°C or above, more preferably at 30°C or above, even more preferably at 35 to 50°C.

[0179] 60. Combined process according to embodiment 59, wherein the thermal energy required for the extraction in step (iii) at elevated temperature is at least partly thermal energy obtained in the combined process, preferably thermal energy obtained in separating at least part of the bioethanol from the fermented broth in step (c), and / or thermal energy obtained in condensing the water separated during drying of the stillage.

[0180] 61. Combined process according to any one of embodiments 58 to 60, wherein the second extractant contains ethanol (in particular bioethanol) and water, wherein the ethanol content is preferably in the range from 40 to 90 wt%, more preferably from 55 to 90 wt%, in particular from 60 to 90 wt%, based on the weight of the second extractant.

[0181] 62. The combined process according to embodiment 61, wherein the ethanol contained in the second extractant is bioethanol produced in the first process.

[0182] 63. Combined process according to any one of embodiments 58 to 62, wherein at least a portion of the second extractant is separated from the second mixture, preferably by distillation and / or stripping.

[0183] 64. The combined process according to embodiment 63, wherein the second extractant separated from the second mixture has an ethanol content of 55 wt% or more, more preferably 60 wt% or more, even more preferably 65 wt% or more, most preferably 70 wt% or more, based on the weight of the separated second extractant.

[0184] 65. The combined process according to embodiment 63 or 64, wherein the second extractant separated from the second mixture is reused as the second extractant.

[0185] 66. The combined process according to embodiment 65, wherein the separated second extractant is purified before reuse as a second extractant, wherein the purification preferably comprises filtration. 67. The combined process according to any one of embodiments 63 to 66, wherein the separated second extractant contains ethanol (in particular bioethanol) and is used in step (c) of the first process, preferably wherein the separated second extractant is added to the fermented broth obtained in step (b) of the first process, preferably after at least partial separation of water and / or stillage from the fermented broth, in particular after partial distillation of the fermented broth.

[0186] 68. Combined process according to any one of embodiments 57 to 67, wherein in step (iv) at least a portion of the oilseed protein concentrate is separated from the first mixture, in particular from the second extractant, preferably by evaporation.

[0187] 69. Combined process according to embodiment 68, wherein thermal energy required for separating at least a portion of the oilseed protein concentrate from the first mixture, in particular from the second extractant, in particular by means of evaporation, is at least partly thermal energy obtained in the combined process, preferably thermal energy obtained during separation of at least a portion of the bioethanol from the fermented broth in step (c), and / or thermal energy obtained during condensation of the water separated during drying of the stillage.

[0188] 70. Combined process according to any one of embodiments 57 to 69, wherein the oilseed protein concentrate separated in step (iv) is dried.

[0189] 71. Combined process according to any one of embodiments 57 to 70, wherein in step (iv) at least a portion of the oilseed by-product containing the oilseed molasses is separated from the second mixture.

[0190] 72. The combined process of embodiment 71, wherein separating at least a portion of the oilseed by-product from the second mixture comprises stripping and / or decanting.

[0191] 73. Combined process according to any one of embodiments 57 to 72, wherein in step (iv) at least a portion of the second extractant is separated from the second mixture, preferably wherein the separation comprises distillation and / or stripping.

[0192] 74. The combined process according to embodiment 73, wherein at least a portion of the second mixture is used after separating at least a portion of the second extractant in the first process, and this portion of the second mixture is contained in the mash provided in step (a). 75. The combined process according to any one of embodiments 71 to 74, wherein the oilseed by-product separated from the second mixture and / or the second mixture is evaporated prior to use in the first process.

[0193] 76. Combined process according to any one of embodiments 71 to 75, wherein the oilseed crop by-product used in the first process and / or the second mixture used in the first process has a dry matter weight of 10 to 80 wt%, more preferably 15 to 50 wt%, even more preferably 20 to 40 wt%, particularly preferably 25 to 35 wt%, based on the total weight of the oilseed crop by-product and / or the second mixture.

[0194] 77. The combined process according to any one of embodiments 1 to 56, wherein the second process produces an oilseed protein isolate.

[0195] 78. Combined process according to embodiment 77, wherein between steps (ii) and (iii) at least a portion of the first extractant contained in the first extraction product is separated from the first extraction product, preferably by evaporation; preferably wherein the thermal energy required for the separation, in particular by evaporation, is at least partly thermal energy obtained in the combined process, preferably thermal energy obtained during the separation of at least a portion of the bioethanol from the fermented broth in step (c), and / or thermal energy obtained during the condensation of the water separated during the drying of the stillage.

[0196] 79. The combined process according to embodiment 78, wherein in step (iii) water is added to the first extraction product, and a pH of the first extraction product is adjusted substantially to the isoelectric point of the oilseed protein product to precipitate at least a portion of the oilseed protein isolate and thus separate the first extraction product into the first (precipitated) mixture and the second mixture.

[0197] 80. The combined process according to embodiment 78 or 79, wherein separating at least a portion of the oleaginous fruit protein isolate from the first mixture in step (iv) comprises dewatering the oleaginous fruit protein isolate, in particular evaporating water, centrifuging, decanting, and / or sedimenting; wherein the separated oleaginous fruit protein isolate is preferably dried.

[0198] 81. The combined process according to any one of embodiments 77 to 80, wherein in step (iv) of the second process, at least a portion of the oleaginous fruit by-product containing the oleaginous fruit protein liquor is separated from the second mixture, wherein the separation comprises dewatering the oleaginous fruit by-product. 82. The combined process according to embodiment 81, wherein the separation of at least a portion of the oleaginous fruit by-product containing the oleaginous fruit protein liquor from the second mixture comprises evaporating water, centrifuging, decanting, and / or sedimenting.

[0199] 83. Combined process according to any one of embodiments 77 to 82, wherein at least a portion of the second mixture and / or at least a portion of the oilseed by-product separated from the second mixture is used in the first process and is contained in the mash provided in step (a).

[0200] 84. Feed obtainable by the combined process according to any one of embodiments 1 to 83, and containing shells of oilseeds, preferably comminuted shells of oilseeds, in particular ground shells of oilseeds.

[0201] 85. Feed obtainable by the combined process according to any one of embodiments 1 to 83 and containing the oilseed by-product, in particular the oilseed molasses and / or the oilseed protein liquor.

[0202] 86. Feed according to embodiment 85, comprising shells of oilseeds, more preferably crushed shells of oilseeds, in particular ground shells of oilseeds.

[0203] 87. A combined plant for producing bioethanol and an oleaginous protein product using the combined process according to any one of embodiments 1 to 83, comprising a first plant for producing the bioethanol, comprising a fermenter for fermenting the mash, and a first separation unit for separating at least a portion of the bioethanol from the fermented broth; and a second plant for producing the oleaginous protein product, comprising a first extraction device for extracting the oleaginous starting product with the first extraction agent, a second separation unit for separating the first extraction product into the first mixture and the second mixture, a third separation unit for separating at least a portion of the oleaginous protein product from the first mixture, and optionally a fourth separation unit for separating at least a portion of the oleaginous by-product from the second mixture.

[0204] 88. A combined plant for producing bioethanol and an oilseed protein product using the combined process according to any one of embodiments 1 to 83, comprising a first plant for producing the bioethanol, comprising a fermenter for fermenting the mash, and a first separation unit for separating at least a portion of the bioethanol from the fermented broth; and a second plant for producing the oilseed protein product, comprising a first extraction device for extracting the oilseed starting product with the first extraction agent, a second separation unit for separating the first extraction product into the first mixture and the second mixture, a third separation unit for separating at least a portion of the oilseed protein product from the first mixture, and optionally a fourth separation unit for separating at least a portion of the oilseed by-product from the second mixture.wherein the second plant optionally comprises a fifth separation unit for separating at least a portion of the first extractant contained in the first miscella, preferably wherein the first extraction device and the fifth separation unit are connected to the first separation unit;

[0205] 89. A combined plant for producing bioethanol and an oilseed protein product using the combined process according to any one of embodiments 1 to 83, comprising a first plant for producing the bioethanol, comprising a fermenter for fermenting the mash, and a first separation unit for separating at least a portion of the bioethanol from the fermented broth; and a second plant for producing the oilseed protein product, comprising a first extraction device for extracting the oilseed starting product with the first extraction agent, a second separation unit for separating the first extraction product into the first mixture and the second mixture, a third separation unit for separating at least a portion of the oilseed protein product from the first mixture, and optionally a fourth separation unit for separating at least a portion of the oilseed by-product from the second mixture;wherein the first plant comprises a comminution unit for comminuting the carbohydrate-containing starting material and shells of oilseeds, and wherein the second plant comprises a processing unit for processing the provided oilseed starting product, wherein the processing unit comprises a peeling unit, preferably wherein the peeling unit of the processing unit of the second plant is connected to the comminution unit of the first plant. 90. Combined plant according to one of embodiments 87 to 89, wherein the first separation unit comprises a distillation apparatus; preferably wherein the first separation unit comprises a molecular sieve, a membrane, and / or an adsorbent, particularly preferably a molecular sieve; preferably wherein the molecular sieve, the membrane, and / or the adsorbent is connected downstream of the distillation apparatus.;

[0206] 91. Combined plant according to embodiment 90, wherein a section of the first separation unit comprising the molecular sieve is connected to the fermenter such that carbon dioxide can be conducted from the fermenter to this section of the first separation unit; and / or wherein the section of the first separation unit comprising the molecular sieve is connected to the distillation apparatus of the first separation unit such that an ethanol-containing cleaning agent used to clean the molecular sieve can be conducted from the section of the first separation unit comprising the molecular sieve to the distillation apparatus; and / or wherein the section of the first separation unit comprising the molecular sieve is connected to the second separation unit, in particular to a second extraction device of the second separation unit.

[0207] 92. Combined plant according to any one of embodiments 87 to 91, wherein the first plant comprises a mashing apparatus for mashing the carbohydrate-containing starting material and the oilseed by-product, wherein the mashing apparatus is preferably connected to the fourth separation unit.

[0208] 93. Combined plant according to one of embodiments 87 to 92, wherein the first plant comprises a comminution unit for comminuting the carbohydrate-containing starting material, and optionally shells of oilseeds.

[0209] 94. Combined plant according to one of embodiments 87 to 93, wherein the first plant comprises a dryer, in particular a feed dryer, for drying the stillage; preferably wherein the dryer, in particular a feed dryer, of the first plant is connected to the comminution unit of the first plant.

[0210] 95. Combined plant according to any one of embodiments 87 to 94, wherein the second separation unit comprises a second extraction device, or wherein the second separation unit comprises a dryer and a precipitation apparatus.

[0211] 96. The combined plant according to any one of embodiments 87 to 95, wherein the third separation unit comprises a dryer. 97. The combined plant according to any one of embodiments 87 to 96, wherein the fourth separation unit comprises a stripper, a distillation apparatus, a centrifuge, a decanter, a sedimenter, and / or an evaporator.

[0212] 98. Combined plant according to any one of embodiments 87 to 97, wherein the second plant comprises a fifth separation unit for separating at least a portion of the first extractant contained in the first miscella and / or for separating at least a portion of the oil and / or fat contained in the first miscella; preferably wherein the fifth separation unit comprises a distillation apparatus and / or a stripper.

[0213] 99. Combined plant according to one of embodiments 87 to 98, wherein the second plant comprises a processing unit for processing the provided oilseed starting product, preferably wherein the processing unit comprises a peeling unit and / or a comminution unit.

[0214] 100. Combined plant according to embodiment 99, wherein the processing unit, in particular the peeling unit, of the second plant is connected to the comminution unit of the first plant; and / or wherein the processing unit, in particular the peeling unit, of the second plant is connected to the dryer, in particular the feed dryer, of the first plant.

[0215] 101. Combined plant according to one of embodiments 87 to 100, wherein the processing unit of the second plant, the first extraction device, the second separation unit, the third separation unit, the fourth separation unit and / or the fifth separation unit is / are connected to the first separation unit (in particular to a section of the first separation unit which has the molecular sieve) and / or to the dryer (in particular feed dryer) of the first plant, in particular to a connecting element suitable for transporting thermal energy in order to use thermal energy obtained in the first plant in the second process.

[0216] 102. Combined plant according to any one of embodiments 87 to 101, comprising a storage tank for storing separated first extractant, separated second extractant, and / or separated cleaning agent, each containing ethanol, preferably bioethanol, wherein the storage tank is preferably connected to the first separation unit (in particular to the distillation apparatus of the first separation unit); and wherein the storage tank is preferably connected to the second separation unit, to the third separation unit, to the fourth separation unit, to the fifth separation unit, and / or to the section of the first separation unit comprising the molecular sieve. 103. Combined plant according to any one of embodiments 87 to 102, comprising a wastewater treatment unit, wherein the wastewater treatment unit is preferably connected to the first separation unit and / or to the dryer (in particular to the feed dryer) of the first plant.

[0217] 104. Combined plant according to any one of embodiments 87 to 103, wherein the first plant, in particular the first separation unit, comprises a first collection container for collecting the bioethanol produced in the first process; and / or wherein the second plant, in particular the third separation unit, comprises a second collection container for collecting the oilseed protein product produced in the second process.

[0218] 105. Combined plant according to one of embodiments 87 to 104, wherein the first extraction device is connected to the first separation unit, in particular to the first collection container.

[0219] 106. Combined plant according to any one of embodiments 87 to 105, wherein the second plant comprises two second separation units, two third separation units, optionally two fourth separation units and optionally two second collection vessels for producing oilseed protein isolate and oilseed protein concentrate simultaneously and / or sequentially.

[0220] 107. An oleaginous fruit protein product obtainable by a combined process according to any one of embodiments 1 to 83, in particular an oleaginous fruit protein concentrate, an oleaginous fruit protein isolate, an oleaginous fruit oil product, an oleaginous fruit lecithin product, or an oleaginous fruit fiber product obtainable by a combined process according to any one of embodiments 1 to 83.

[0221] 108. The oilseed protein product of embodiment 106, wherein the product is a soy protein concentrate (SPC), a soy protein isolate (SPI), a soy oil product, a soy lecithin product, or a soy fiber product.

[0222] Figures

[0223] The invention is further described by the preferred embodiments shown in the following figures, to which, however, it is not limited.

[0224] Fig. 1 shows a schematic flow diagram of a combined process, where the first process produces bioethanol and the second process produces an oilseed protein concentrate. Fig. 2 shows a schematic flow diagram of a combined process, where the first process produces bioethanol and the second process produces an oilseed protein isolate.

[0225] Fig. 1 shows a schematic flow diagram of a combined process. As can be seen, a carbohydrate-containing starting material 1 is comminuted in a comminution unit 2. The comminution takes place by dry milling, wherein the carbohydrate-containing starting material 1 is mixed together with hulls 3, wherein the hulls 3 are at least a portion of hulls separated from oilseed crops in the second process, in order to obtain an oilseed crop starting product 4. Subsequently, the comminuted, carbohydrate-containing starting material 1 and the comminuted hulls 3, as well as an oilseed crop by-product 5 obtained in the second process, which contains an oilseed crop molasses, are added to a mashing apparatus 6, wherein the ratio of oilseed crop by-product 5 to carbohydrate-containing starting material 1 is 1:10 (wt% / wt%). In the mashing apparatus 6, mashing takes place in the presence of an alpha-amylase. The mash 7 is then added to a fermenter 8.Fermentation produces a fermented broth 9 containing bioethanol 10, a stillage 11, and water, with carbon dioxide 12 being produced as a by-product. The fermented broth 9 is fed to a first separation unit 13. The first separation unit 13 has a distillation apparatus 14 in which the stillage 11 is separated from a bioethanol-water mixture 15. The resulting bioethanol-water mixture 15 is then separated into bioethanol 10 and water 17 using a molecular sieve 16 of the first separation unit 13. The bioethanol 10 can be in a gaseous state and subsequently condensed to collect it in a first collection container 18 of the first separation unit 13. Thermal energy AT can be recovered in the process, which can be used in the combined process. The bioethanol 10 collected in the first collection container 18 has a purity of 99.0 wt% or more (based on the weight of the bioethanol 10).The water 17 separated from the bioethanol 10 can be fed to a wastewater treatment unit 19 for processing. The molecular sieve 16 can be cleaned after use with an ethanol-containing cleaning agent 20. The ethanol contained in the cleaning agent 20 can be bioethanol 10 produced in the first process. After use of the cleaning agent 20, it can be fed to a storage container 21 for storage. The stillage 11 contained in the fermented broth 9 is fed to a dryer 22, in particular a feed dryer, for drying. Hulls 3 obtained in the second process can also be added to the dryer 22, with which the stillage 11 (and the crushed hulls 3 already contained therein) can be dried. Alternatively or additionally, a portion of the oilseed by-product 5 obtained in the second process can be added to the dryer 22, with which the stillage 11 can be dried.The dried stillage 11 can be used as high-quality animal feed. Gaseous water 23 separated during the drying of the stillage 11 is subsequently condensed, whereby thermal energy AT is recovered. This water 23 can then be fed to the wastewater treatment unit 19 for processing. Furthermore, it can be seen from Fig. 1 that an oilseed starting product 4 is provided by processing in a processing unit 24. The processing unit 24 has a hulling unit and a comminution unit (not shown). The oilseed starting product 4 is first hulled in the hulling unit, with the separated hulls 3 being fed to the comminution unit 1 and, if appropriate, to the dryer 22. The hulled oilseed starting product 4 is then comminuted in the comminution unit of the processing unit 24.The comminution can take place at elevated temperature, wherein thermal energy AT obtained in the combined process can be used. The peeled oil fruit starting product 4 is then fed to the first extraction device 25, where it is extracted with bioethanol 10 supplied from the first collection container 18, which is used as the first extraction agent 39. The extraction can take place at elevated temperature, wherein thermal energy AT obtained in the combined process can be used. By extracting in the first extraction device 25, a first miscella 26 and a first extraction product 27 are obtained. The first extraction product 27 is subsequently fed to a second separation unit 28, which has a second extraction device.By extracting with a second extraction agent 29 containing bioethanol 10 and water, the first extraction product 27 is separated into a first mixture 30 containing an oleaginous fruit protein product 31, which is an oleaginous fruit protein concentrate, and a second mixture 32 (also referred to as a second miscella) containing the oleaginous fruit by-product 5. Extraction in the second extraction device can take place at elevated temperature, wherein thermal energy AT obtained in the combined process can be used. The second extraction agent 29 can be taken from the storage container 21. Alternatively, the bioethanol 10 can also be taken from the first collection container 18, and water can be added in an appropriate amount. The first mixture 30 is subsequently fed to a third separation unit 33 to separate at least a portion of the oleaginous fruit protein product 31 from the first mixture 30. The third separation unit 33 has a dryer.In the dryer, at least a portion of the second extractant 29 is evaporated, and the oilseed protein product 31 is subsequently dried to remove any remaining second extractant. Evaporation and drying take place at elevated temperature, and thermal energy AT obtained in the combined process can be utilized. Separated second extractant 29 is fed to the storage container 21, while the dried oilseed protein product 31 can be collected in a second collection container 34.

[0226] From Fig. 1, it can further be seen that the second mixture 32 containing the oleaginous by-product 5 is fed to a fourth separation unit 35 in order to separate at least a portion of the oleaginous by-product 5 from the second mixture 32. For this purpose, the fourth separation unit 35 has a stripper. By means of the stripper, at least a portion of the second extractant 29 can be separated from the second mixture 32 and subsequently fed to the storage tank 21 for reuse in the combined process. The oleaginous by-product 5 is then fed to the mashing apparatus 6. Alternatively, it could also be added to the comminuted carbohydrate-containing starting material 1 and the comminuted hulls 3 prior to addition to the mashing apparatus 6. The oleaginous by-product 5 can then be evaporated using an evaporator 36 to reduce its water content. The separated water 41 can be fed to the wastewater treatment unit 19.

[0227] Furthermore, Fig. 1 shows that the first miscella 26 from the first extraction device 25 is fed to a fifth separation unit 37. The fifth separation unit 37 has a stripper in which at least a portion of an oil and / or fat 38 and at least a portion of the first extraction agent 39 contained in the first miscella 26 are separated from the first miscella 26. The separated oil and / or fat 38 can be recovered and used for other applications. The separated first extraction agent 39 is fed to the storage container 21. Alternatively or additionally, the separated first extraction agent 39 could also be fed to the second extraction device of the second separation unit 28 for use as the second extraction agent 29, wherein the concentration can be adjusted with water if necessary.

[0228] Fig. 1 also shows that the storage vessel 21 is connected to the distillation apparatus 14. This makes it possible, depending on demand, availability and / or capacity, to feed a (bio)ethanol-containing mixture 40 stored in the storage vessel 21 to the distillation apparatus 14. The mixture 40 can then be processed together with the fermented broth 9 in step (c) of the first method. Preferably, the mixture 40 or a portion thereof is only fed to the distillation apparatus 14 after the fermented broth 9 has already been partially distilled and, accordingly, any water contained in the fermented broth 9 and / or the stillage 11 has / have already been at least partially separated from the fermented broth 9. At least a portion of the ethanol orBioethanol can be separated from the fermented broth 9 together with at least a portion of the bioethanol 10 contained in the (preferably partially distilled) fermented broth 9.

[0229] Fig. 2 shows another schematic flow diagram of a combined process. The combined process of Fig. 2 largely corresponds to that of Fig. 1; the following discussion is limited to the differences. The second process differs from the process shown in Fig. 1 in particular in that the second separation unit 28 has a dryer 42 and a precipitation apparatus 43. The first extraction product 27 obtained by extraction in the first extraction device 25 is fed to the dryer 42. As a result, at least a portion of the first extraction agent 39 contained in the first extraction product 27 (bioethanol 10 from the first collection container 18 was used as the first extraction agent 39) is separated from the first extraction product 27. This takes place by evaporating the bioethanol 10 at elevated temperature, whereby thermal energy AT obtained in the combined process can be used.The evaporated bioethanol 10 can subsequently be condensed; the thermal energy obtained thereby can be used in the combined process. The bioethanol 10 can subsequently be fed to the storage tank 21, particularly if it is contaminated. The first extraction product 27 remaining after the evaporation of at least a portion of the bioethanol 10 is subsequently transferred to the precipitation apparatus 43, to which water 44 is also added. This water 44 can, for example, be taken from the wastewater treatment unit 19. The pH of the first extraction product 27 is adjusted substantially to the isoelectric point of an oilseed protein product 45 to be produced, which is an oilseed protein isolate, in order to precipitate at least a portion of the oilseed protein product 45. As a result, the first extraction product 27 can be separated into the first (precipitated) mixture 46 and the second mixture 47.The first mixture 46 contains the oleaginous fruit protein product 45 and optionally a small amount of the water 44. The second mixture 47 contains an oleaginous fruit by-product 5 containing an oleaginous fruit protein liquor and the majority of the water 44.

[0230] As can further be seen from Fig. 2, the first mixture 46 is subsequently fed to the third separation unit 33 in order to separate at least a portion of the oleaginous protein product 45 from the first mixture 46. For this purpose, the third separation unit 33 has a dryer in which the oleaginous protein product 45 is dried. This takes place at elevated temperature, wherein thermal energy AT obtained in the combined process can be used. During drying, at least a portion of the water 44 can be separated and fed to the wastewater treatment unit 19. The dried oleaginous protein product 45 can be collected in the second collection container 34. The second mixture 47 is fed to the fourth separation unit 35 in order to separate at least a portion of the oleaginous by-product 5 from the second mixture 47. For this purpose, the fourth separation unit 35 has an evaporator. This allows the water content of the oleaginous by-product 5 to be reduced.Water 48 separated from the oilseed by-product 5 can be fed to the wastewater treatment unit 19 for treatment.

Claims

Claims 1. A combined process comprising a first process for producing bioethanol (10) and a second process for producing an oilseed protein product (31, 45), the first process comprising the steps (a) providing a mash (7), wherein the mash (7) contains a carbohydrate-containing starting material (1), in particular a grain, (b) fermenting the mash (7) to obtain a fermented broth (9) containing bioethanol (10), and (c) separating at least a portion of the bioethanol (10) from the fermented broth (9); and the second method comprising the steps (i) providing an oilseed crop starting product (4), (ii) extracting the oilseed starting product (4) with a first extraction agent (39) to obtain a first miscella (26) and a first extraction product (27), (iii) separating the first extraction product (27) into a first mixture (30, 46) containing the oilseed protein product (31, 45) and a second mixture (32, 47) containing the oilseed by-product (5), (iv) separating at least a portion of the oleaginous protein product (31, 45) from the first mixture (30, 46), and optionally separating at least a portion of the oleaginous by-product (5) from the second mixture (32, 47); wherein the mash (7) provided in step (a) of the first process contains at least a portion of the oleaginous by-product (5) obtained in the second process or at least a portion of the oleaginous by-product obtained in the second process is added during step (b), wherein the first extractant (39) contains bioethanol (10) produced in the first process, wherein the first miscella (26) contains at least a portion of the first extractant (39), and wherein at least a portion of the first extractant (39) contained in the first miscella (26) is separated from the first miscella (26) and used in step (c) of the first process.

2. Combined process according to claim 1, wherein the mash (7) provided in step (a) contains the oilseed by-product (5) in an amount of 1 to 20% by weight, based on the weight of the carbohydrate-containing starting material (1).

3. Combined process according to claim 1 or 2, wherein the provision of the oilseed starting product (4) in step (i) comprises separating shells from oilseeds and / or comminuting the oilseeds, wherein the oilseeds are preferably soybeans, sunflower seeds and / or rapeseed seeds.

4. Combined process according to one of claims 1 to 3, wherein the carbohydrate-containing starting material is corn and / or wheat.

5. Combined process according to one of claims 1 to 4, wherein the separated first extractant (39) is added to the fermented broth (9) obtained in step (b) of the first process, in particular after at least partial separation of water and / or a stillage (11) from the fermented broth (9).

6. Combined process according to one of claims 1 to 5, wherein the provision of the oilseed starting product (4) in step (i) of the second process comprises separating shells (3) from oilseeds, and wherein the mash (7) provided in step (a) of the first process contains crushed shells (3) of oilseeds, the shells (3) being at least a part of the shells (3) separated from the oilseeds in step (i) of the second process.

7. Combined process according to one of claims 1 to 6, wherein in step (c) at least a part of a stillage (11) contained in the fermented broth (9) is separated, the separated stillage (11) being subsequently dried.

8. Combined process according to claim 7, wherein a portion of the oilseed by-product (5) obtained in the second process is added to the separated stillage (11).

9. Feed obtainable by the combined process according to any one of claims 1 to 8 and containing the oilseed by-product (5).

10. A combined plant for producing bioethanol (10) and an oilseed protein product (31, 45) using the combined process according to any one of claims 1 to 8, comprising a first plant for producing the bioethanol (10), comprising a fermenter (8) for fermenting the mash (7), and a first separation unit (13) for separating at least part of the bioethanol (10) from the fermented broth (9);and a second plant for producing the oilseed protein product (31, 45), comprising a first extraction device (25) for extracting the oilseed starting product (4) with the first extraction agent (39), a second separation unit (28) for separating the first extraction product (27) into the first mixture (30, 46) and the second mixture (32, 47), a third separation unit (33) for separating at least a portion of the oilseed protein product (31, 45) from the first mixture (30, 46), and optionally a fourth separation unit (35) for separating at least a portion of the oilseed by-product (5) from the second mixture (32, 47); wherein the second plant optionally comprises a fifth separation unit (37) for separating at least a portion of the first extraction agent (39) contained in the first miscella (26).

11. Combined plant according to claim 10, wherein the first plant comprises a dryer (22), in particular a feed dryer, for drying the stillage (11).

12. Combined plant according to claim 10 or 11, wherein the fourth separation unit (35) is connected to the dryer (22).

13. Combined plant according to one of claims 10 to 12, wherein the first extraction device (25) is connected to the first separation unit (13).

14. Combined plant according to one of claims 10 to 13, wherein the first plant comprises a comminution unit (2) for comminuting the carbohydrate-containing starting material (1) and shells (3) of oilseeds, and wherein the second plant comprises a processing unit (24) for processing the provided oilseed starting product (4), wherein the processing unit (24) comprises a peeling unit.

15. Combined plant according to claim 14, wherein the peeling unit of the second plant is connected to the comminution unit (2) and / or to the dryer (22) of the first plant.

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