SK281336B6 - Process for producing hydrolyzate of the proteins waste of animal origin - Google Patents

Abstract

In order to create an alkaline environment in the alkaline enzymatic hydrolysis of animal protein protein waste, 0.5 to 3.0% of at least one alkali or alkaline earth oxide or hydroxide in combination with 1 to 1% by weight of waste is added prior to dosing of enzymes to waste in water. 8% amine with boiling point at atmospheric pressure up to 200 ° C, respectively. mixtures of such amines. The hydrolyzate obtained contains a basic protein component consisting mainly of a mixture of peptides and further admixture, in particular a low molecular weight salt. The content of impurities in the hydrolyzate, determined as the ash content by weight, does not exceed 6% of the total dry weight of the hydrolyzate. In particular, the hydrolyzate is useful as glue and jelly, as well as for the preparation of adhesives, for the preparation of flocculating solutions, as an additive for food products and the like.

Description

Technical field

The invention relates to a process for producing a protein waste hydrolyzate of animal origin. The hydrolyzate obtained is particularly useful in similar applications to glue and jelly, further to the preparation of adhesives, to the preparation of flocculating solutions, as an additive to food products and the like.

The actual production method consists in the alkaline enzymatic hydrolysis of protein waste of animal origin, in particular solid tannic waste, but also other types of animal waste, e.g. glaze, raw hides and slaughter waste.

BACKGROUND OF THE INVENTION

In addition to high-quality products, the meat and tanneries industry also produces a significant amount of protein waste of animal origin. In view of the increasingly stringent environmental requirements, more attention is being paid to the disposal and treatment of these wastes than in the past. In particular, the treatment and disposal of ecologically harmful types of protein wastes such as chromium tin wastes, such as chromium tin waste, is the subject of intensive research. whitenings.

If we do not take into account the depositing of these wastes in predefined landfills, the main directions of their treatment, respectively. Waste disposal are the directions dealing with the use of these wastes as fillers for insulating materials in construction, in their incineration, pyrolysis and acidic chemical or alkaline hydrolysis.

In the last decade, much attention has been paid in particular to the enzymatic hydrolysis of chrominated tartar, based on the action of alkaline proteases on the chrominated skin. These, as a rule, one-step processes are economically expensive and also the quality of the hydrolytic products obtained is very low. For this reason, two-step processes have been developed which make it possible to significantly reduce the cost of the expensive enzyme, while the quality of the resulting hydrolyzate in some parameters (molar mass, bloom value) is close to the quality of similar products obtained from the processing of idle raw wastes. and gleja.

The practical application of this procedure to cracks having a thickness greater than 0.05 mm and other types of protein waste with a larger particle size, however, greatly increases the reaction time, thus significantly increasing the processing costs and consequently increasing the cost of the isolated products unbearably. enzymatic hydrolysis.

Furthermore, in order to evaluate the effect of the prior art process, it is necessary to take into account that a different combination of magnesium oxide with alkali metal or alkaline earth hydroxides and alkali carbonates is used as the starting basic mixture. The proportion of expensive magnesium oxide is in the range of 3-7% by weight of the sowings, the proportion of other alkaline compounds varies from 0.5 to 2.0%. From an economic point of view, the prices of the chemicals making up the alkaline mixture are not negligible and can reach up to 30% of the total cost of production. In addition, the formed alkali salts pass into solution and thereby greatly increase the content of impurities in the hydrolyzate and, when expressed by weight of the ash formed, represent up to 20% of the total dry weight of the hydrolyzate. Since the ash content of the hydrolyzate dry matter is one of the decisive criteria for its further successful use in the production of quality goods, the composition of said hydrolyzate cannot in any case be regarded as optimal.

SUMMARY OF THE INVENTION

The method for producing the protein waste hydrolyzate of animal origin according to the invention, in principle based on the alkaline enzymatic hydrolysis of the protein waste of animal waste contributes to eliminating said deficiency. The principle of the invention consists in adding 0.5 to 3.0% of at least one oxide or hydroxide of the alkali metal and alkaline earth metal oxides and hydroxides to the waste water in the water prior to dosing the enzyme to the waste in water. in combination with 1.0 to 8.0% of an amine boiling at atmospheric pressure up to 200 ° C, respectively. mixtures of such amines.

Magnesium oxide or hydroxide is preferably used as the oxide or hydroxide of the alkali metal and alkaline earth oxides and hydroxides and hydroxides.

The amine is preferably at least one amine selected from the group consisting of isopropylamine, diisopropylamine, triethylamine and cyclohexylamine.

From the technological point of view, the process according to the invention can be carried out in one or two stages.

In a one-step process, the protein waste in water is first added with an oxide or a hydroxide, respectively. a mixture of oxides and / or hydroxides in combination with an amine, respectively. mixture of amines. The resulting mixture was heated to 60-95 ° C for 1-6 hours with stirring while the enzyme was added and the mixture was heated for a further 1-4 hours with stirring. The hot mixture is then filtered and the hydrolyzate is recovered.

In the two-step process, the protein waste in water is also first added to the oxide or hydroxide, respectively. a mixture of oxides and / or hydroxides in combination with an amine, respectively. mixture of amines. The resulting mixture was heated to 60-95 ° C with stirring for 1 to 6 hours while the enzyme was added and the mixture was heated for a further 1-4 hours with stirring. The hot mixture is then filtered and the hydrolyzate is isolated by evaporation. The filter cake is stirred in water, heated to 60-95 ° C and, after the addition of the enzyme, further heated for a further 1-3 hours in the second hydrolysis stage. The hot mixture is then filtered again and the hydrolyzate is isolated by evaporation and the filter cake is dried for further processing after washing.

From an economic point of view, it is further advantageous to replace the amine and the amine, respectively. amines metered to form an alkaline environment, at least in part by condensate containing the recycled amine from the previous hydrolysis reaction.

The main benefit of the process according to the invention is the substantially lower content of impurities in the resulting hydrolyzate, which, expressed as weight fraction of ash, does not exceed 6% of the total dry weight of the hydrolyzate. This reduction is achieved by the fact that the mixture for forming the alkaline medium in the hydrolysis is not exclusively made up of alkaline hydroxides, as in the known production methods. An essential component of this mixture in the process according to the invention is the low molecular weight amine and the low molecular weight amine. a mixture of low molecular weight amines, which are applied in combination with an oxide, respectively. an alkali metal hydroxide, respectively. alkaline earth, but above all oxide, respectively. magnesium hydroxide. The amount of oxide, respectively. % of the hydroxide is then at least 100% lower than in the previously known processes.

SK 281336-6

A further advantage of the process according to the invention is that in the isolation of the hydrolysis products all of the amine or the amine used is passed through the process. amines to the condensate, which allows practically 100% recycling of amines, with a positive economic effect.

No less important is the fact that if larger sized particles are hydrolyzed, the hydrolysis reaction time is prolonged. If hydrolysis is carried out in the prior art, i.e. without the addition of amines, the hydrolysis time is too long, so that the practical treatment of such wastes becomes economically unacceptable.

An important benefit of the process according to the invention is also an increase in the overall efficiency of the dechromation and thus an increase in the yield of protein hydrolysates from 70 to 99.5%.

DETAILED DESCRIPTION OF THE INVENTION

Example 1

The mixture consisting of 100 kg of crisps (50% humidity), 500 kg of water, 7 kg of diisopropyl amine, 2 kg of magnesium oxide was heated in the reactor at 70 ° C for 4 hours. 10 g of the enzyme alkalase are then added to this mixture and heating is continued for a further 3 hours. Throughout the heating period, the mixture is stirred in the reactor with an anchor stirrer. After completion of the reaction, the hot mixture was filtered and the hydrolyzate from the first hydrolysis step was isolated therefrom.

The filter cake is mixed with 150 kg of water in the reactor, heated to 70 ° C, and after addition of 10 g of alkalase, the reaction mixture is hydrolyzed in the second stage for a further two hours while heating and stirring. The hot reaction mixture is then filtered again and the hydrolyzate is isolated from the second hydrolysis stage by scalding. The filter cake is washed with hot water and dried for further processing.

The admixture content, determined as the proportion by weight of ash in the dry matter of the hydrolyzate, is 5.8% by weight for the first stage hydrolyzate and 3.3% by weight for the second stage hydrolyzate, with a total dechromination efficiency of 99.5.

In the procedure used so far, i. j. in an alkali hydroxide environment, under comparable reaction conditions, the ash content of the hydrolyzate of the first stage is 21.3%, in the case of the hydrolyzate of the second stage, 7.2% and the dechromation efficiency in this case is only 73%.

Example 2

The entire hydrolysis procedure and the composition of the masterbatch are practically identical to Example no. 1. Only in the feed mixture of the first stage of hydrolysis is the primary amine added replaced by the recycled amine. The masterbatch is then, in addition to the components identical to Example no. 1 and recycled diisopropyl amine further comprises 0.2 kg of primary added diisopropylamine to compensate for recycled amine losses in filtration.

The quality (composition) of the hydrolyzate and the overall efficacy of the dechromation are practically no different from Example no. First

Example 3

The mixture consisting of 200 kg of chaff waste based on scrap waste, 1000 kg of water, 5 kg of magnesium oxide, 10 kg of isopropylamine is heated in the reactor at 90 ° C for 5 hours. Then 10 g of the enzyme alkalase is added to this mixture and heating is continued for a further 3 hours. Throughout the heating period, the mixture is stirred in the reactor with an anchor stirrer. After completion of the reaction, the hot mixture is filtered to give 440 kg of hydrolyzate dispersion having a dry weight content of 5.2% by weight and 700 kg of a filter cake with a moisture content of 88%.

Subsequently, the hydrolyzate from the first hydrolysis step is isolated from the filtrate by evaporation; 680 kg of filter cake are mixed with 200 kg of water in the reactor, heated to 70 ° C and after addition of 10 g of alkalase, the second hydrolysis stage is continued with heating and stirring for 3 hours.

The hot reaction mixture is then filtered again to give 600 kg of hydrolyzate dispersion from the second hydrolysis stage with a solids (solids) content of 6.2% by weight. This is then recovered from the filtrate by evaporation. The filter cake is washed with hot water and dried for further processing.

The admixture content, determined as the proportion by weight of ash in the dry matter of the hydrolyzate, is 6.4% in the first stage hydrolyzate, 4.3% in the second stage hydrolyzate, and the total dechromination efficiency is 94%.

Example 4

The entire hydrolysis procedure and the feed composition are practically identical to Example 3. Only in the basic mixture of the first hydrolysis stage is the primary amine added replaced by the recycled amine.

The masterbatch is then, in addition to the components identical to Example no. 3 and recycled isopropyl amine further comprises 0.5 kg of primary isopropyl amine added to compensate for recycled amine losses in filtration.

The quality (composition) of the hydrolyzate and the overall efficiency of the dechromation are practically identical to Example no. Third

Note: Analogous results are obtained when triethylamine or cyclohexylamine are used instead of the indicated amines under the conditions indicated (see Examples 1 to 4).

Example 5

The mixture consisting of 100 kg of ground slaughter waste (intestines, unprocessed viscera, etc.), 300 kg of water, 3 kg of cyclohexylamine, 0.5 kg of magnesium oxide is heated in the reactor at 70 ° C for 2 hours. 10 g of the enzyme alkalase are then added to this mixture and heating is continued for a further 1 hour. Throughout the heating period, the mixture is stirred in the reactor with an anchor stirrer. Upon completion of the reaction, the hot mixture is filtered to remove mechanical impurities and the hydrolyzate is isolated from the filtrate (e.g. as an additive to smoked products).

Claims (6)

PATENT CLAIMS Process for the production of a protein waste hydrolyzate of animal origin comprising an essential protein component consisting primarily of a mixture of peptides and further admixtures, in particular low molecular weight salts, comprising alkaline enzymatic hydrolysis of protein waste, characterized in that add, by weight of waste, 0,5 to 3,0% of at least one oxide or hydroxide of the group of alkali and alkaline earth oxides and hydroxides in combination with 1 to 8% of amine boiling at atmospheric pressure up to 200 ° C, respectively. a mixture of such amines. SK 281336-6 Method according to claim 1, characterized in that the protein waste in the water is first added with an oxide or a hydroxide or with an organic solvent. a mixture of oxides and / or hydroxides in combination with an amine, respectively. amine mixture and the resulting mixture is heated to 60-95 ° C for 1-6 hours with stirring, then the enzyme is added and the mixture is heated for a further 1-4 hours with stirring, then the hot mixture is filtered and isolated from the filtrate. hydrolyzate. The production method according to claim 1, characterized in that the protein waste in water is first added with an oxide or a hydroxide, respectively. a mixture of oxides and / or hydroxides in combination with an amine, respectively. amine mixture and the resulting mixture is heated to 60-95 ° C for 1-6 hours with stirring, then the enzyme is added and the mixture is heated for a further 1-4 hours with stirring, then the hydrolyzate is filtered from the hot mixture, the filter cake is stirred in water, heated to 60-95 ° C and, after addition of the enzyme, further heated for 1 to 3 hours in the second hydrolysis stage, then the hydrolyzate is recovered from the hot mixture by filtration and the filter cake is dried for further washing the use. 4. A process according to claim 1, wherein the amine and the amine, respectively. the mixture of amines dosed to form the alkaline medium is at least partially replaced by condensate containing recycled amine from a previous hydrolysis reaction. A process according to claim 1, 2 or 3, characterized in that magnesium oxide or hydroxide is used as the oxide or hydroxide. A process according to claim 1, 2 or 3, characterized in that at least one amine selected from the group consisting of isopropylamine, diisopropylamine, triethylamine and cyclohexylamine is used as the amine.