CS230786B1 - A method of recovering protein substances from yeast sludge, milk whey and blood - Google Patents

Abstract

The subject of the invention is a method of obtaining protein substances from yeast sludge, whey and blood by their countercurrent precipitation in solution, with a desolvating agent, which may be methanol, ethanol, propanol, isopropanol or acetone. The present invention enables obtaining protein substances from yeast sludge, blood and whey by adjusting the colloidal solution of these substances with hydrochloric or sulfuric acid to a pH close to the isoelectric point and adding a desolvating agent in such an amount that all protein substances precipitate. If we want to obtain protein substances with a low degree of protein denaturation, we work at a temperature of -7 to -18 C. If we do not mind a certain degree of denaturation, we work at temperatures of 60 - 70 C. The precipitated proteins are freed from excess liquid by filtration on a filter press and dried. is reduced to the required dry matter at low temperatures, which is easily manageable due to the volatility of the desolvating agent. The desolvating agent is regenerated from the withdrawn liquid by rectification. The temperature from the dephlegmator, condenser and luther waters is used in the described operations or binding technologies. The produced protein substance still contains the residue of the desolvating agent in the stokes, which prevents microbial damage, which significantly increases the shelf life of the product. The residue of the agent is easily removed during further processing of the protein substance into raw material.

Description

-7- 230 788

The present invention relates to a process for obtaining proteinaceous substances from yeast sludge, milk whey and blood. The purpose of the present invention is to produce a durable protein preparation in a powder state with virtually no concentration of undesirable microorganisms present, which is a useful raw material for the production of food products or as a feed additive. for their protein enrichment »The recovery of proteinaceous materials from the aforementioned raw materials has now encountered the difficulties caused by the raw material being rapidly degraded by microbial degradation. The low utilizable protein content has reduced the possibility of economical use by the so far known technological process, as well as the properties of proteinaceous substances, such as hydrophilic colloids, have made any separation method difficult, while a significant portion of these raw materials is still unused for public use and pollutes the environment, even though it contains valuable components.

The proposed method of treatment removes the current difficulty of allowing all raw materials to be processed, even under premise, from the environment and storage for a short period of time.

The principle of the whole technology is that a desolvating agent (methanol, ethanol, isopropanol or acetone) is added to a suitable raw material in bound water on the colloid in such a way that the protein begins to fall out of the colloidal solution in the form of v_ .oiek. The flakes fall in the extraction colony counter to the other. agent and dewatered. The desolvation-extracting agent is removed for distillation by regeneration, while the proteinaceous material is discharged to a device which releases the reagent residue. The device can vary depending on the type of 230 786 - 2 - raw material and the overall concept of production. · The advantage of this method against the conventional spdso - bs known to date is that by properly setting the conditions under which desolvation can take place, we can obtain a variety of nature. · At low temperatures below - 7 ° C we obtain native preparations of proteinaceous substances · At suitable pH we can divide albumin from glo-bulgines · Precipitation can also be controlled by the concentration of desolvation agent at the site of the reagent with the raw material · energy intensity is quite lower than for drying, because in the distillation or concentration of the agent, we need less heat to evaporate the reagent than we would need to evaporate the water, due to the lower heat of the desolvation agent and, in addition, remove the heat from the impregnator, which, together with the heat of the lutra vdd, can be secondary used.

The high hygiene of the process is ensured by the fact that the desolvation agent, any of the above, prevents the development of microorganisms in the obtained product even at relatively low temperatures.

Individual protein acquisition technologies differ according to the type of raw material being processed, but the described principle remains ·

When processing blood from slaughter, the collected blood from the animal flows directly into the tank, where the desolvation agent, which is immediately conserved blood. Under well-defined conditions / temperature, addition of sodium citrate, at2 ./, slowly desolvate and flake out. · Blood can be transferred to a nearby center for processing.

Whey is still in the process of densifying and then desolvating and extracting sugars, lactoflavin and ash-wine ·

While the desolvation of yeast has been most refined, the beer yeast is acidified with a mineral acid of pH 2.6-3 and acidified into a plant where it meets the reagent in such a quantity as to concentrate it by centrifugation or filtration on vacuum rotary filters. the yeast-draining liquid contained about 56% by weight of the agent. The flocculated yeast pre-scavenges the freshly arriving agent, which is hot and water residue. 230 780

Centrifuged desolvated yeast is dried to remove reagent and packaged as a higher quality product such as Pangamine. reagent - usually ethanol - goes to regeneration · Lutr water goes to biological purifier ·

The wine yeast sludge is first deprived of the present tartaric acid and then after concentration to a centrifuge into the apparatus, somewhat countercurrently mixed with the desolvating agent. Water-cleared yeast goes to remove residual desolvation agent · Salted valuable substances are separated from lutra water. Example 1

Yeast wine sludge after removal of potassium tartrate is destroyed by excess water either by centrifugation or by filtration.

Concentrated wine slurries are acidified with an added mineral acid / salt or sulfuric acid (pH = 2.3-2.9) and countercurrent water extraction is carried out with a desolvation agent - ethanol, either into a battery of extraction tanks or into an extraction column. The ethanol feed is controlled so that the leaving water / ethanol mixture contains about 55% ethanol by volume. The temperature in the extraction apparatus is maintained at 70-75 ° C.

The effluent goes to the rectification column for poor recovery of ethanol.

The effluent concentrate is freed of ethanol by centrifugation, compression and subsequent drying. The product contains 4 wt. / dry matter / ethanol that preserves it.

1.4 parts by weight of material per 1 part of water is required. The total ethanol demand is assumed to be 1.1 kg / loss and residual product / ethanol based. * Example 2

Blood from the slaughter line flows into containers where there is so much ethanol to make the ethanol content 20 - 22% by weight after filling the container

The contents of the container are pumped into the reaction vessel after it has been found to be wholesome and adjusted to - 4

pH = 4.3. Z30 7BB

The blood is already precipitated by addition of saline and ethanol

Pugat goes for ethanol recovery by rectification. The concentrate is dissolved in a small amount of alkaline water of NaOH, thereby removing residual dyes and re-precipitating the solution in a countercurrent device. The proteins obtained are packaged and handed over to the food industry after ethanol removal, as in the previous case.

1.85 liters of ethanol are needed per liter of water in the blood. The expected total losses on ethanol are 1.5-2% by weight. from the total amount of ethanol supplied. Example 3

Brewer's yeast sludge taken from the brewery / from the fermenting room / with a dry matter content of 5 to 15% by weight. are concentrated by centrifugation to 28% by weight. solids, or are filtered on filter presses / vacuum filters / to a dry weight of 27 to 30% by weight.

The resulting thick sludge is fed to a column where the countercurrent feeds ethanol at a concentration of 80 to 92% by weight. in a quantity of 1.6 - 2 kg per kg of bound water, ie 4.1 to 5.14 kg of ethanol are metered in per kg of dry matter at a temperature of 15 - 30 ° C.

Flocculated yeasts fall to the bottom of the column, where they are withdrawn and freed of ethanol by centrifugation and drying.

The yeast is freed from hot substances by this process, retaining the full value of the Group B vitamins and having a pleasant taste of the seed cores. from

They are suitable for the production of high-quality "Pangamine", vitamin and other preparations for vigorous products in medicine, food bugs.

The durability of the preparation is high with ethanol in nom. λ 230 788 Example 4

The hot brewing sludge after the hop boiling in the whirlpool is pumped to a column in which the pumped acetone of 80-90% is pumped in 1 kg of acetone per kg of bound water at a temperature of 15-30 ° C. - 25% by weight, it is necessary to counteract 0.75 to 0.80 kg of acetone per 1 kg of added lees.

Sludge in the column is sedimented against the incoming acetone in the flake and collected at the bottom of the column, purged and stripped of acetone by centrifugation and drying until removal of the acetone residue.

The dried sludge is simultaneously free of hot substances. The packs are hermetically sealed / hygroscopic and transported to the saline application ·

The preparation thus prepared is essentially barley gluteine, enzymatically partially cleaved, with lower peptides, a suitable proteinaceous supplement for food products or feed mixtures.

Similar technology can be used to process yeast yeast calyper milk whey · Example 5

The slaughter blood taken from the hollow knife flows into a container in which a mixture of propanol and isopropanol (1: 1) and sodium citrate is present in such a quantity as to contain isopropanol and propanol from 15 to 25% when the container is replenished with blood and sodium citrate content 0.8 to 1.2

The size of the container must be sufficient to receive blood from 1 piece / do-by-bed, to be swallowed.

After closing, the container is transported to the warehouse of the blood protein production plant. The contents of the containers are pumped into the tank, where the pH is adjusted to 3.2 to 4.8 with HCl. - even 1 kg per 1 kg of water, or isopropanol at 1 kg per 1,5 kg of water present ·

Blood flocculates and collects at the bottom of the column, draining it for separation and drying *

Claims (1)

Process for recovering proteinaceous substances from yeast sludge, milk whey and blood, characterized in that a desolvating agent is added to the aqueous dispersion of the concentrated raw materials, adjusted to a pH of 2.3 to 6.8 with a mineral acid such as sulfuric or hydrochloric acid. Preferred ethanol, acetone, isopropanol or the ^Λ propanol concentration from 80 to 98% by weight. in an amount of 0.6 to 2.5 kg per kg of colloid-bound water and the falling flakes are dewatered by countercurrent extraction, further addition of desolvating agent at a temperature of -20 to + 80 ° C, which is finally removed by centrifugation.