HU212699B - A process and an arrangement for membrane filtration of a dispersion - Google Patents

Abstract

The present invention relates to a method and an arrangement for membrane filtration of a dispersion solution. The arrangement is provided with a continuous water phase dispersion feeding line (2 ", 2", 2n + 1), a supernatant filtrate removal material (6n_1, 6 ", 6n + 1) and a filtrate line (δ" '1). , 8n, 8n + 1) contains a membrane filtration unit (4n1, 4 ", 4n + 1), wherein the conduit (6", 6 ", 6n + 1) is the following membrane filter unit (4" -1, 4n, 4n + 1) is connected to an inlet or is connected to a feed line (2n_l, 2 ", 2n + 1) .The essence of the filtrate lines (8n_l, 8n, 8" + ") of one or more membrane filter units (4n_1, 4", 4 "+") (l) one or more of the concentrating units (10r < -1 >, 10 ", 10 " +1) separating the filtrate into the diluted fraction and the concentrated fraction, wherein the concentrating units (IO "-1, 10", 10n + 1) each with the effluent from the diluted fraction (12 "", 12 ", 12n + 1) and the second effluent carrying the concentrated fraction (14" - ", 14", 14 "+ l) where the second outlet (14 "_1, 14", 14 "+1) is a return line 2 FIG. 212 699 B Scope of the description: 28 pages (including 5 sheets)

Description

FIGURE 2

HU 212 699 B

Description: 28 pages (including 5 pages)

EN 212 699 Β (16 · ', 16, 16 * ¹ ) connected to the feed line (2' ¹ , 2 ⁿ , 2 ^{n +} ) of one or more membrane filter units (4 "', 4, 4 ^{n + 1} ). ¹ ) is connected. In the proposed process, a dispersion containing a continuous aqueous phase is processed with one or more membrane filter units by introducing a dispersion into the membrane filter unit, converting each membrane filter unit into a substance retained by the filter membrane and a filtrate obtained after the filter membrane. the material is wholly or partially introduced into one or more additional membrane filter units. In essence, the concentration of the filtrate obtained at the outlet of one or more membrane filters is increased, a concentrated fraction containing an increased concentration of dry matter or a portion thereof is produced and the concentrated fraction is fed to one or more membrane filter units as part of the feed dispersion.

The present invention relates to a method and arrangement for membrane filtration of a dispersion solution. The proposed arrangement comprises a membrane filter unit with a feed line, one or more dispersions comprising a continuous aqueous phase, a membrane filtration unit with an overflow filtrate removal material and a filtrate line, the outlet being arranged at the inlet of the next membrane filter unit or connected to the feed line. A process comprising the step of dispensing a continuous aqueous phase is processed by an arrangement comprising one or more membrane filter units in one or more filtration steps by introducing an initial or an inlet dispersion to the inlet of the membrane filter unit; converting the filtrate into a filtrate obtained after the membrane and, if necessary, retaining the whole or r in one or more further filtration steps.

The arrangement and method of the present invention are particularly suitable for controlling the concentration of solids derived from milk in dairy products made by concentrating its dry matter, in particular in the process of production by ultrafiltration of milk. Such dairy products obtained by the proposed process or arrangement are particularly advantageous in the manufacture of cheeses, including in particular fresh and unripe products, cottage cheese and soft and semi-hard cheeses in brine, such as for example cottage cheese, feta, economical production of semi-hard or soft cheeses of the domiati, mozzarella, cascade and kefalotiri types.

Before going on to the state of the art, the following definitions are provided by some of the terms used in the specification and claims to facilitate a better understanding of what has been said.

Membrane Filtration: Separation of a dispersion applied to the surface of a membrane for filtration, often referred to as the starting or inlet, into a retained fraction of components that do not penetrate the membrane orifices and a filtrate of material that has passed through the orifices. The retained fraction is usually a liquid dispersion with a higher density than the filtrate in which the solids are present in a higher concentration than the initial or inert dispersion. Membrane filtration includes membranes suitable for microfiltration, ultrafiltration, nanofiltration (MF, UF, NF, respectively, in the drawings and description), and reverse osmosis, or substantially equivalent hyperfiltration (also referred to below). in the drawings and in the description, RO and HF) are used respectively.

Retained fraction: material consisting of components of the initial dispersion that do not penetrate the membrane openings of the filtration membrane.

Filtrate: material consisting of the components of the initial dispersion which penetrate through the openings of the filtration membrane.

Microfiltration: Filtration with a membrane having pores of average size from 0.08 pm to 2.5 pm, or otherwise using a membrane with pores having a molecular weight of 150,000 to 5,000,000 allows passage.

Ultrafiltration: Filtration with a membrane having pores of average size from 0.002 pm to 0.4 pm, or otherwise using a membrane with pores of a molecular weight between 500 and 800,000 pore size.

Nanofiltration: Filtration with a membrane having pores of average size from 0.0007 pm to 0.007 pm, or otherwise using a membrane having a pore size that allows the passage of constituents having a molecular weight of 140 to 15,000.

Hyperfiltration or reverse osmosis separation: filtration through a membrane that allows reverse osmosis. When the conditions for reverse osmosis occur, the filtrate often consists of water only. There are conditions under which reverse filtration with osmotic separation yields a filtrate containing metal ions and water-soluble salts on one side of the membrane. It is difficult to determine pore size for membranes used in reverse osmosis, but the theoretical conclusion is that pore sizes are 0 pm and

HU 212 699 Β

They are in the range of 0.0015 µm, i.e., components with a molecular weight of up to 300 can penetrate the membrane, with a pore size of 0 µm having a molecular weight of 0.

Diafiltration: Filtration with a membrane, especially a membrane suitable for ultrafiltration or nanofiltration, in which water is added to the initial or inert dispersion prior to filtration. By performing diafiltration, the amount of soluble solids in the retained fraction can be reduced.

Initial Dispersion: The starting material for the membrane filtration process. There was no particular limitation on the composition and type of the initial dispersion, and the dispersed phase may comprise a dispersion of molecular dispersion, colloidal dispersion, and / or relatively large particle size.

It is a limitation of the present invention to provide a dispersion having a continuous (continuous) phase water-based liquid. Occasionally, the initial dispersion is referred to as an input dispersion if the dispersion delivered to the first inlet of a multiple module arrangement is to be distinguished from the dispersion processed by the other modules.

Permeable Solid Ingredients: Solids present in the initial or inert dispersion which are capable of penetrating the orifices of the membrane used for filtration, i.e., in the arrangement and process of the invention, substantially all of the constituents except the water removed from the dispersion in the filtrate. In the process and arrangement of the present invention, the membrane used for filtration determines which of the solid components of the initial or inert dispersion can be classified as permeable solids.

Before analyzing the known solutions, the general characteristics of membrane filtration of aqueous dispersions are described.

In the membrane filtration process, a filtrate of permeable solids and water is obtained at the outlet of the membrane openings. The other components of the initial dispersion, i.e. the retained fraction, remain on the surface of the membrane filter and cannot penetrate its material. The weight ratio of filtrate to retained fraction depends on a number of factors, including the pressure difference between the two inlet and outlet sides of the filtration membrane, the pore size, and the surface area sealed due to coating or contamination of the membrane active surface. Filtration may be carried out with membranes connected in series or in parallel. In some applications, such as ultrafiltration of semi-products obtained by processing milk or milk, the membrane filtration capacity is generally utilized by interconnecting membrane filtration units such that the retention phase recovered from the filter surface in the first membrane filtration unit forms an initial or in the retained phase received is passed to the third membrane filter unit, etc.

The retained phase derived from the membrane filter units itself is generally also a dispersion, i.e., the dispersed material and the continuous phase. If the dispersed material contains only particles that are unable to penetrate the membrane openings of the filtration while the continuous phase consists exclusively of permeable solid components and water, the continuous phase of the retained fraction is essentially a liquid phase mixture of the filtrate. A different situation is that when the particles in the dispersion are theoretically permeable to the membrane, they are bound to the larger particles and thus remain in the retained fraction, which results in a permeable solid in the filtrate. the proportion of the components is less than the value for the continuous phase in the retained fraction.

When it is also necessary for the relatively small particles or molecules to be present in the retained fraction, it is possible, at least in theory, to perform filtration such that the filtrate is produced with a small pore size membrane. A practical problem in this case is that by reducing the pore size, the filtration capacity of the membrane is reduced.

As a result of the above, the correct choice of pore sizes of membranes is essential for arrangements with membrane filter units. If the pores are chosen too large, many of the ingredients that are retained in the retained fraction may go into the filtrate.

If the components with relatively low molecular weight are low permeability! The membrane is contaminated relatively or even very rapidly as a result of which the filtration capacity is reduced.

It follows from the foregoing that there remains a need to develop an arrangement and process that provides the high filtration capacity required for industrial and other applications by retaining a relatively large proportion of the low molecular weight constituents desired to be retained in the retained fraction.

A solution for reducing the amount of soluble constituents in the continuous phase in the retained fraction is well known in which the continuous phase of the initial dispersion is diluted with water, i.e., diafiltration as defined above. With this solution, a larger amount of filtrate can be obtained while the amount of retained fraction remains unchanged. Upon dissolution of the permeable solids, their concentration in the continuous phase of the initial dispersion is reduced due to diafiltration, whereas in the retained phase, the concentration and thus the amount of permeable components are reduced.

Attempts to increase the amount of permeable solids in the retention phase have shown that the solids must be added to the initial dispersion to achieve the desired increase. Intended for use in the food industry3

However, when forming a fraction considered to be alien, the addition of any foreign material is generally avoided and in some cases, especially for dairy products, is explicitly prohibited in many countries.

Problems with the processing of aqueous dispersions of fat and protein by membrane filtration units are inherent in the food industry and are particularly problematic in the production of many dairy products when the raw material or semi-processed product, such as milk, dairy products or milk-like dispersions they are condensed in advance. For this purpose, an ultrafiltration arrangement is used in which ultrafiltration membranes are utilized. The latter are able to retain fat and proteins, while their pores are able to pass through lactose, low molecular weight protein substances, salts and water.

Cow's milk is a very important raw material for the dairy industry after homogenization as needed, and cheese (s) are made from a significant amount by conventional methods known per se. Milk is used or marketed as whole milk, ie with a solid content or reduced fat content compared to that obtained from milking, and dairy products made from milk enriched with cream separated from milk and thus have a higher fat content.

It is well known that ultrafiltration of milk in the manufacture of various types of cheese produces an intermediate product which is already characterized by the desired solids content of the final product. This operation is carried out in known ultrafiltration arrangements into interconnected modules which employ membrane-covered plates and together provide a membrane surface of the desired size in each module. The module is provided with passageways, the modules interconnected by wires, so that the fluid processed for compaction flows through substantially serially coupled modules, while in parallel with each other, the filtrate collected in each module flows into a collecting container. This ultrafiltration of milk essentially results in an increase in the concentration of protein, the concentration of fats also increases, while the basic mass of lactose and salts passes into the filtrate formed by ultrafiltration.

U.S. Pat. No. 4,497,836. U.S. Pat. No. 4,123,195 discloses a process for the preparation of a concentrate of whey used primarily in infant formulas and infant formulas by ultrafiltration of cheese whey resulting in a protein-rich fraction and a lactose-enriched filtrate. The filtrate was found to contain 9 to 12% solids in mineral salts due to whey. The concentration of the filtrate is increased by reverse osmosis and the mineral salt is removed, or by electrodialysis the salt is removed and subsequently concentrated by vacuum evaporation. The liberated filtrate is then mixed with the protein rich retention phase, i.e. the higher density material obtained by ultrafiltration, and the mixing ratio is adjusted to adjust the amount of lactose and mineral salts in the mixture. Thus, the process described requires ultrafiltration of the whey, whereby the mineral salts are separated from the filtrate, while lactose is retained as much as possible and added to the concentrated product obtained by ultrafiltration.

Lactose is a low molecular weight substance and therefore can only be recovered in the ultrafiltration process with a low concentration in the retained fraction. Thus, all or a significant portion of the lactose passes into the aqueous filtrate and is present there in dissolved form, so that the concentration of lactose in the retained fraction is much lower than its initial dispersion value.

In many cases, ultrafiltration of the dispersions is carried out in several steps, in several steps, when the filtrate obtained in one step is used as the initial dispersion in the next step. In many cases, ultrafiltration can be combined with diafiltration by adding water to the dispersion introduced in one or more steps.

If the dispersion obtained by ultrafiltration is, for example, a dairy product or a milk-based semi-product, the amount of lactose in the retained fraction may be reduced, for example by diafiltration, irrespective of the amount of fat and protein. Adding large amounts of water to the initial dispersion reduces the concentration of lactose in the aqueous phase. The aqueous phase remaining in the retained fraction contains a smaller amount of lactose. In other words, under these conditions, a relatively greater amount of lactose passes into the liquid phase of the filtrate.

Diafiltration can also be useful in adjusting the salt content of the retained phase, when the dissolved salts have to be removed.

The filtrate obtained from the processing of the filter membrane forms waste and by-products in many known processes and arrangements, which have serious problems due to the high concentration of soluble solids, including lactose, in their deposition and neutralization. When released into the environment, these liquids are highly contaminated by the presence of high concentrations of lactose and other components.

In addition, it is worth noting that some of the materials present in the filtrate are useful in many cases in the manufacture of products other than those originally intended, and it is highly desirable to develop a solution to selectively process at least a portion of thus could be kept in the retained phase.

European Patent Application EP-A1 460 339 (Applicant Perry et al.), In particular Part VII of the specification. Example 1 and Figure 1 describe a process and arrangement which does not contain aqueous dispersions such as lemon juice.

EN 212 699 Β suitable for the removal of desirable constituents, including citric acid. According to the disclosed process, the lemon juice is first subjected to microfiltration, whereby a retained phase containing its solid pasty constituents in a dispersed state and a filtrate free of the pasty constituents are obtained. The filtrate, which is liberated from the pulp-like components, is then subjected to electrodialysis and is thus liberated from the component to be removed, such as citric acid, without changing the water content of the filtrate. The resulting filtrate, optionally de-acidified and free of pasty ingredients, is collected in a transfer tank where it is mixed with the retained phase containing the pasty ingredients. With this method, the ingredients obtained by microfiltration can eventually be made into acid-free, reproduced lemon juice, which is obtained from the intermediate container.

The ability to perform regulatory functions is assured by optimizing the quantities of material designated for microfiltration and electrodialysis, and, for this purpose, feed lines from the transition vessel to the microfiltration unit are used for this purpose. This solution is known per se. However, the dewatering of the deacidified filtrate is not performed directly, but only after the filtrate is mixed with the retained phase, i.e. the weight ratio of the pulp dispersed in the filtrate to the continuous phase is substantially the same as that of the starting phase. it was typical of lemon juice before treatment. Since the deacidified filtrate is not part of the filtrate containing the increased proportion of permeable solids, it is not possible to obtain a retention fraction which is enriched in solids and contains soluble permeable constituents in a higher concentration than the initial one.

DE-A1 3 626 498 discloses a process for preventing the coating, blocking or contamination of a membrane used in ultrafiltration by returning the retained phase to the inlet, which may be carried out prior to the concentrating step and optionally sludge from the filtrate. at least a portion is removed and the pH adjusted as necessary. These latter operations are carried out by ion exchange, electrolysis or dialysis in such a way that part of the retained phase is also returned to the ultrafiltration membrane. The filtrate, which is mixed with the retained phase, has a reduced salt content and / or the pH is adjusted as needed to ensure that the proteins are less prone to clogging or contamination of the filter. When the conductivity of the mixing phase drops below a predetermined value, the concentration of the initial dispersion is adjusted by ultrafiltration so as to reduce the degree of contamination and clogging, thereby increasing the filtration capacity. This publication does not recommend that the filtrate be returned to the starting dispersion in its unaltered state, and the retained phase is returned to the process after a reduction in salinity and / or pH, as is clear from the description, thus increasing the permeable solids. is not considered to be the concentrated fraction of the filtrate containing.

It follows from the foregoing that the prior art solutions do not provide sufficient guidance to those skilled in the art to establish a process and arrangement to meet the aforementioned need. Therefore, it is our task to provide a process and arrangement that provides the high filtration capacity required for industrial and similar applications and provides opportunities for the relatively low molecular weight components, or at least a substantial portion thereof, not to pass through the filtrate but in the retention phase. remains. Our task may also be to increase the proportion of permeable solids in the retention phase during membrane filtration tasks.

The present invention is based on the discovery that the concentration of some solids in the filtrate obtained from the initial dispersion in the first membrane filter unit may be increased by centrifugation, evaporation, or filtration in a second membrane filter unit with a smaller pore size than the first membrane. fraction may be added to the dispersion fed to the starting or previous membrane filter unit. In this way, the solids content of the retained fraction can be increased or controlled, even if the pore size of the membrane receiving the initial dispersion is large enough to allow a significant portion of the solids retained to pass through the membrane.

In order to solve this problem, we have first of all developed a process and arrangement for membrane filtration suitable for the processing of aqueous dispersions to obtain the desired composition.

An embodiment of the present invention comprises a membrane filtration unit with a feed line carrying a dispersion containing one or more dispersions containing a continuous aqueous phase, a filtration conduit for supplying material obtained by removing filtrate and a filtrate conduit, wherein the drain is provided at the inlet of a subsequent membrane filtration unit. connected, it is essential according to the invention that the filtrate lines of one or more membrane filter units pass through one or more concentrating units separating the filtrate into a diluted fraction and a concentrated fraction, each concentrating unit having a first outlet carrying the diluted fraction and a second outlet carrying the concentrated fraction. provided with a second outlet connected by a feed line which is one or more membranes of a strong unit is connected with the feed pipe of.

In a highly preferred embodiment of the invention, a given membrane filter unit coupled to a concentrating unit is a

It is routed through its spill outlet to the feed line and is thus connected to one or more feed lines of the given membrane filter unit and / or to the inlet of at least one previous membrane filter unit.

The processing efficiency is improved if the arrangement according to the invention preferably comprises one or more groups of concentrating units, in particular first and second reverse osmosis units, wherein the one or more groups are connected to a common feed line by a concentrated material transfer line or outlet. provided.

Also, for processing purposes, an embodiment of the arrangement according to the invention comprising one or more groups of interconnected concentrating units, in particular first and second reverse osmosis units, is preferred, wherein the second outlet of the first concentrating unit, in particular the first reverse osmosis unit connected to the next concentrating unit, in particular the second reverse osmosis unit.

The efficiency and selectivity of membrane filtration is particularly strongly enhanced by the preferred embodiment of the arrangement according to the invention, wherein the concentrating unit is formed with first and second membrane units, in particular nanofiltration units and reverse osmosis units, wherein the second membrane unit is and the filtrate line of the first membrane unit, in particular the nanofiltration unit, is connected to the inlet of the second membrane unit, in particular the reverse osmosis unit. In this solution, soluble solids characterized by average molecular weight from the filtrate filter of the first membrane filter unit can be removed from the retained phase. and the relatively low molecular weight permeable solids can be recycled to the first membrane filtration unit such that the proportion of these permeable solids in the retention phase obtained in the first step can be significantly increased.

The usefulness of the arrangement according to the invention is enhanced by the preferred embodiment in which the membrane filter unit is designed as a unit equipped with a microfilter or ultrafilter.

The filtration process is effectively facilitated by the highly practical implementation of the arrangement according to the invention, wherein the concentrating unit is provided with a centrifuge, an evaporating unit and / or an additional membrane filter unit.

Also, the conditions for carrying out the filtration processes will be more favorable than the preferred embodiment of the arrangement according to the invention, wherein the concentrating unit is provided with an additional membrane filter unit having a pore size smaller than the membrane used in the membrane filter unit.

For various filtration tasks, the arrangement according to the invention is particularly well suited to the embodiment in which the membrane filter unit is formed with an ultrafiltration unit, the concentrating unit comprises a nanofiltration unit, the latter having a filtrate conduit and a filtrate conduit for transporting the filtrate. the outlet of the filtrate line is led to the inlet of the reverse osmosis unit, while the reverse osmosis unit is provided with a first outlet for transferring material separated from the filtrate and a second outlet for filtrate, and the second outlet is fed to a feed line into one or more feed lines of the membrane filter units.

Also for the purpose of the present invention, there is also provided a process for membrane filtration processing of aqueous dispersions, wherein a dispersion containing a continuous aqueous phase is processed in one or more filtration steps by an arrangement of one or more membrane filtration units, for each membrane filter unit, the starting or inlet dispersion is converted into a phase retained by the filter membrane and a filtrate obtained after the filter membrane and, if necessary, the retained material is processed in whole or in part in one or more further filtration steps. increasing the concentration of the filtrate obtained after the appropriate membrane filter in several filtration steps, thereby increasing the total solids present in the filtrate, or preparing a concentrated fraction containing a portion of the increased concentration and returning the concentrated fraction to the starting or inlet dispersion and processing it as part of the filtration step with one or more filter membranes.

Thus, the process of the present invention requires increasing the concentration and concentrating the filtrate, preferably by centrifugation and / or evaporation and / or membrane filtration. If membrane filtration is used to increase the concentration, it is highly desirable to carry out the process of the present invention wherein the membrane filtration unit utilizes an additional membrane having a pore size smaller than the pores of the membrane filtration unit providing the membrane filtration unit for the feed dispersion.

An effective increase in the concentration of the product obtained from the first ultrafiltration step is provided by a preferred embodiment of the process of the invention wherein the membrane filtration unit comprises an ultrafiltration membrane while increasing the concentration by one or more membrane filters with one or more membranes performing nanofiltration and / or reverse osmosis. unit. The membrane filters used in such combinations selectively adjust the proportions of the permeable solid components to be separated.

The process of the invention is particularly advantageous for use in the food industry, where according to general conditions, fat and / or protein is used as an initial or initial dispersion in the membrane filter.

EN 212 699 Β, in particular whole milk or semi-manufactured milk.

In order to adjust the composition of the product to be manufactured, it is very convenient to carry out the process according to the invention in which the initial or inert dispersion is subjected to membrane filtration by diafiltration. This measure, for example, makes it possible to reduce the proportion of undesirable permeable solids in the retained fraction by selectively concentrating the filtrate and re-feeding a predetermined portion of the permeable solids into the process to ensure their presence in the retained fraction.

It is highly desirable to carry out the process of the present invention wherein the concentration increase is accomplished by a combination of a nanofiltration membrane and a reverse osmosis membrane, the filtrate from the membrane being added as an input dispersion to the inlet side of the reverse osmosis membrane and after leaving the filtrate, the concentrated material is added to the inlet of the membrane filter unit receiving the initial or inlet dispersion with ultrafiltration.

The arrangement and process of the present invention provide the extremely important advantage that no foreign matter is introduced into the system during the process of product manufacture since the concentrated filtrate at elevated concentration contains only the ingredients already present in the introduced initial dispersion. It is therefore highly desirable to utilize the arrangement and method of the invention in the manufacture of food products and in the processing of such semi-products.

In view of the foregoing, we find it particularly advantageous to employ a variation of the solids content of the milk using ultrafiltrated milk, since the proportion of each solids can be individually controlled, above all for the total solids content and the solids content. the desired concentration of protein and lactose relative to fat content can be achieved relatively easily. Therefore, cheese varieties with different organoleptic characteristics can be produced directly in a wide variety of variants. As a result, the solid constituents of milk are more versatile than before and it is also possible to control the consistency of the cheese-type end product, since spreadability can be easily achieved by adjusting the proportion of lactose and protein. The more lactose the product contains, the better its spreadability. Another particularly advantageous advantage of the arrangement and method according to the invention is that the various parameters in the cheese making process can be adjusted without the need to introduce any foreign matter. Yet another significant advantage of the arrangement and method of the invention is that the excess semi-products (filtrates) are either very pure and therefore simply placed without any risk of environmental contamination or are so concentrated that they can be commercialized directly for use in animal husbandry lactose can be utilized or powdered.

Because of the foregoing, it is particularly advantageous to implement the process of the invention useful in the food industry by introducing milk into the inlet of the ultrafiltration membrane filtering unit to produce a concentrated dairy product and controlling the amount of milk-derived ingredients in the ultrafiltration unit processing the concentrated dairy product and controlling the amount of milk-derived solids in such a way that the filtrate from the initial or inert dispersion in the first filtration step with the membrane filter unit is optionally supplemented with at least a portion of the filtrate obtained by ultrafiltration or and the whole of the increased density material thus obtained, or a r separation of the second filtration step is fed back to a membrane filter unit equipped with an ultra filter and executing the recirculation step as necessary, repeated the desired proportion of the solid ingredients is achieved.

It is also very advantageous for food industry applications to carry out the process according to the invention in which part or all of the increased density material obtained by hyperfiltration, nanofiltration and / or evaporation from the ultrafiltration membrane filter unit and the filtrate obtained in the first filtration step is carried out by the ultrafiltration unit. to the second filtration step of the filtration process to achieve the desired proportion of solids. The same object can be achieved by the practical implementation of the process according to the invention by combining the increased density of the filtrate obtained from the filtrate obtained from the first filtration step with the ultrafiltration membrane filtration unit with a portion of the filtrate obtained in the second filtration step and mixing is returned to the second filtration step of the ultrafiltration unit filtration process.

Whole milk is separated (degreased) and pasteurized according to the method of the invention or prior to processing in the arrangement. The fat-containing fraction separated is optionally homogenized as a cream, or alternatively the whole milk is homogenized. By removing the cream, the fat content of the milk can be reduced naturally or, conversely, the fat content may be increased by the addition of cream. Ultrafiltration is used to increase the proportion of fat and protein in milk. During the filtration, a temperature of 4060 ° C is maintained and the conditions are adjusted so that the final concentration of the solids is ultimately 18 to 50% by weight, preferably 25 to 50% by weight. It may also be advantageous if the material remaining in the membrane filtration unit after ultrafiltration after the filtrate is separated is 15-35% by weight.

It is continued until a dry matter content of 25-31% by weight is reached.

In carrying out the process according to the invention, ultrafiltration is generally carried out in at least two steps, generally and in particular when adjusting the proportion of solids. In both the first and second steps and optionally in the further steps, ultrafiltration is carried out in a multi-module unit. The filtrate from the first step is concentrated by hyperfiltration (reverse osmosis), nanofiltration, or evaporation. The thickening can be carried out in batches or on a processing line. In order to adjust the protein and lactose concentration, the concentrated retention phase obtained in the hyperfiltration and nanofiltration systems is traced back to the part of the ultrafiltration system where the proportion of solids is the highest, i.e. the second and final stage. As a result, the proportion of water-soluble solids, and especially lactose, in the product obtained can be increased. Hyper-filtration (reverse osmosis) or evaporation increases the lactose content while also increasing the proportion of salts and ash-producing components. Nanofiltration can only increase the concentration of lactose, and the proportion of ash-forming components and salts in the process is reduced.

In a preferred embodiment of the process of the invention, the filtrate from the first stage of ultrafiltration is cooled from about 40 ° C to about 60 ° C to about 30 ° C and then at a pH of about 5.9 to about 6.1 after adjustment to the range of about 10% by weight and about 22% by weight by hyperfiltration. preferably, it is converted to a dry solids concentrate of from about 15% to about 19% by weight. The operating pressure of the retarded phase transfer valve is generally adjusted to a maximum of about 3 MPa.

Depending on the setting, the proportion of solids as a result of the compaction is from the initial approx

It is increased from 5.7% to about 10% by weight to the maximum value obtained with the applied pressure. If desired, the dry matter content can be adjusted to about any level from about 100% to about 22% by weight, preferably from about 15% to about 19% by weight in the retention phase as a result of reverse osmosis.

If nanofiltration is selected, the temperature range can be set within a relatively wide range depending on the filter unit used. The type and construction of the diaphragm determine the operating temperature. However, it is highly desirable to carry out the process of the present invention by converting the filtrate of the ultrafiltration membrane filtration unit to a dry solids concentrate by nanofiltration at a temperature of about 20 ° C to about 60 ° C.

When the concentrate is concentrated by evaporation, the filtrate obtained from the first ultrafiltration having a temperature in the range of about 40 ° C to about 60 ° C is introduced into an evaporator and under the conditions provided therein, the filtrate is concentrated by evaporation from about 10% to about 50% by weight. to about 20% by weight and about 40% by weight on a dry basis.

Thus, in the practice of the present invention, it is particularly advantageous to use milk as the initial dispersion and to adjust the proportion of proteins and fats in the concentrated product by adjusting the fat content of the milk.

The proposed procedure allows the addition of fats and protein to the desired proportions of lactose, ash constituents and salts. For this purpose, it is also very advantageous to carry out the process according to the invention by adjusting the proportion of lactose in the increased concentration product in a first filtration step in the ultrafiltration membrane filter unit by adjusting to a lower solids content in the ultrafiltration surface in the filtration step, increasing the amount of the higher density material obtained by hyperfiltration and / or nanofiltration and / or evaporation and / or adjusting the higher dry matter content of the higher density material obtained by hyperfiltration or nanofiltration, or vice versa; by adjusting the lower solids content of the phase and / or ultrafiltration second filtration step with a membrane filter unit equipped with the hiperszűréssel and / or nanofiltration and / densified material obtained by evaporation using a smaller amount and / or by adjusting the resulting densified material hiperszűréssel nanofiltration or less solids content is reduced or it.

The membranes used in the process of the present invention and in the proposed arrangement are suitable for thickening both filtrates and other liquid media. The membrane filter that receives the initial dispersion or the inlet leading to the filtration is hereinafter referred to as a type I filter membrane, while the concentration increasing membranes are referred to as a type II filter membrane.

The present invention is primarily intended for use in the food industry, but may be further extended.

DETAILED DESCRIPTION OF THE INVENTION The present invention will now be described in more detail with reference to the accompanying drawings, with reference to the accompanying drawings. In the drawing it is

Figure 1 is a schematic diagram of a basic unit for operating the arrangement of the present invention, showing a single membrane filter unit and associated concentrating unit,

Figure 2 is a combination of the base units shown in Figure 1 and according to the invention

A flowchart of the novel arrangement proposed in accordance with the present invention also suitable for carrying out process B, a

Figure 3 is a preferred embodiment of the basic unit required for carrying out the arrangement of the present invention, wherein the membrane filter unit is an ultrafiltration unit, while the concentrating unit comprises a nanofiltration unit and a reverse osmosis unit;

Fig. 4 is a circuit diagram of a preferred embodiment of the arrangement according to the invention showing a plurality of ultrafiltration units and a series of two reverse osmosis units as concentrating units, whereupon the filtrate flows from each ultrafiltration unit to the reverse osmosis units and the concentrated filtrate amount is traced back to the ultrafiltration units, suitably divided between them and dosed at appropriate locations in the serial connection,

Figure 5 is a preferred embodiment of the process of the invention

A flowchart of an embodiment of claim 18, wherein

Figure 6 is a preferred embodiment of the process of the present invention

A flowchart of an embodiment of claim 19.

The main features of the process according to the invention and the basic unit of the proposed arrangement are described in connection with Figure 1. In the base unit shown in Figure 1, the feed line 2 is connected to a membrane filter unit 4, to which the filtration membrane delivers the material to be processed by filtration. The membrane filter unit 4 is provided with a drain 6 and a filtrate line 8, wherein the filtrate line 8 is connected to the inlet of a concentrating unit 10 formed by a first outlet 12 and a second outlet 14. The first outlet 12 is also the outlet of the base unit of Figure 1, while the second outlet 14 extends through the feed line 16 into the feed line 2.

As a result of the separation of the membrane filter unit 4 in the apparatus of Figure 1, the retained phase in the drain 6 and the filtered material passing through the filtrate line 8 are obtained. The filtrate line 8 is connected to the concentrating unit 10, where further separation takes place, the fraction diluted through the first outlet 12 leaving the second outlet 14 for conveying the concentrated material. The concentration process can be carried out in any known manner, for example by centrifugation or evaporation, whereby the water content of the diluted fraction removed through the first outlet 12 can be removed by evaporation, or alternatively, membrane filtration using a membrane of the same or different type finally. The concentrate exiting through the second outlet 14, or at least part of it, is fed by the feed line 16 into the feed line 2 which is connected to the inlet of the membrane filter unit 4, and in the latter the mixed product of increased concentration is mixed with the introduced initial dispersion.

The principle of implementing the arrangement of FIG. 1 according to the present invention is preferably further developed as shown in FIG. 2, so that membrane filtration is again performed in a manner known per se in a plurality of units with suitably constructed filters. The arrangement according to the invention, detail shown in Figure 2, a prior constructed in accordance with Figure 1 a base unit 2 ^_l feed line starting or has been previously partially processed dispersion introduced 4 ^_1 membrane filter unit having six ^n_1 draining fraction retained until 8 ^'1 szűrletvezetéke filtered transmits material. 6 ^n_l drainage continuation of two supply line is arranged which is connected to a following ^4N membrane filter unit inlet. The permeate 8 ^{_l n_I} concentrating unit 10 is guided to the inlet, a first outlet of 12 ^n_1 diluted fractions, and a second outlet ¹ 14 for delivering an increased concentration of material, the feed line has two ^_l 16 'through ^one regenerative conduit connected.

Similarly, the membrane filter unit 4 ⁿ conveys the retained fraction 6 in the outlet, filtrated in the 8 ⁿ filtrate line, where the outlet 6 carrying the retained fraction is connected to the 2 ^{n + 1} feed line of a subsequent 4 ^{n + 1} membrane filter unit. The filtrate line 8 is connected to the inlet of a concentrating unit 10 having a first outlet 12 and a second outlet 14 connected to the supply line 2 via the feed line 16. The feed line 16 is connected to the horse feed line ¹ via a branch 18 through the isolation valve 18 and through this to the isolation valve 18 ^nl located in front of the membrane filtration unit 4 ^-1 .

The next 4 ⁺¹ membrane filter unit also has a 6 ^{n + 1} drain that delivers the retained fraction to the 2 ^{n + 2} feed line of the next membrane filter unit and the 8 ^{n + 1} filtrate line through which the filtered material is 10 ⁺¹ concentrate he leaves in unity. The conveyor 10 ^{n + l} diluted fraction concentrating unit 12 is provided with a first outlet ¹ ^ ¹ concentrations and conveying product with increased half 14 ^{+ l} second outlet and connected to the latter at 16 ^{+ l} regenerative conduit 2 ^{+ l} feed line. At one junction of the return line 16 ^{+ 1,} a line closable with a shut-off valve 18 ^{+2 for} the next membrane filter unit is inserted.

It follows from Figure 2 of the 4, 4 ^1, 4, 4 ^{+ l} membrane filter units each with 8, 8 ^_1, 8 ,, 8 is provided with ^{n + I} szűrletvezetékkel which 10, 10 ^-1, 10, 10 ⁺¹ concentrating unit it is also provided with a drain 6, 6 ", 6, 6 ^{+ 1} which feeds the retained fraction into the feed line 2, 2 ', 2, 2 ⁺¹ , 2 ⁺ 2 of the next membrane filter unit. 10, ΙΟ ^-1, 10, 10 ^{+ l} concentrating unit 12, 12 ^_1, 12, 12 ^{+ l} first outlet delivers filtrate was further processed no longer require or diluted fraction, while 14, 14 ^_l, 14, 14 ^{n + l} second outlet on 16, 16 ¹ ,

HU 212 699 Β

16, 16 ^{n + 1 can be} fed through feed line 2, 2 ^0-1 , 2, 2 ^{n + 1} feed line. 14, f4- ^1, 14, 14 ^{n + 1,} the second outlet as shown in one or more 18 ^1, 18, 18 ^{n + l,} 18 ^{n + 2,} isolating valve by opening one or more of the preceding 4, 4 * ¹ 4 , Can be traced back to a 4 ⁺¹ membrane filter unit.

Fig. 3 illustrates the construction of a similar base unit as shown in Fig. 1 for use in a second particularly preferred embodiment of the arrangement of the invention. At this basic unit, feed line 102 is led to an inlet of ultrafiltration unit 104. The ultrafiltration unit 104 is provided with a conduit 106 and a filtrate conduit 108, wherein the filtrate conduit 108 is led to the inlet of the nanofiltration unit 120 and through the filtrate conduit 122 to the reverse osmosis unit 126 and through the conduit 124 to another similar base unit or other processing unit. The reverse osmosis unit 126 is provided with first and second outlets 112 and 114, respectively, wherein the second outlet 114 is connected to the feed line 102 via a return line 116.

The pre-treated or initial dispersion is fed through feed line 102 to ultrafiltration unit 104 (UF in the figure) where the filtration operations are carried out while conveying the fraction retained through the outlet 106 and the filtrate through the filtrate line 108. The filtrate, or at least a portion thereof, is introduced into the nanofiltration unit 120 (denoted NF in the figure), which provides a fraction retained through the conduit 124 and at the same time obtains the filtrate from the filtrate line 122. The filtrate conduits 108 and 122 are each provided with a conduit with a disconnecting valve, through which the amount of material no longer required to be processed can be discharged. The filtrate from the nanofiltration unit 120 is transported to the reverse osmosis unit 126 (RO in the figure) which delivers filtrate through first outlet 112 and material for further processing via second outlet 114 to feed line 116, which is fed to feed line 102 it is connected to a drain via a filter. Thus, the retained fraction obtained in 126 reverse osmosis units is recycled to the processing process. By implementing the arrangement of the present invention with such a unit, solids that can pass through the ultrafiltration unit 104 but are still present on the membrane of the nanofiltration unit 120 can be removed while the portion of solid components passing through the membrane of the 120 nanofiltration unit is not removed. can pass through the return line 116 to the ultrafiltration unit 104 at an increased concentration. Like the one shown in Figure 2, the unit of Figure 3 can be connected in series to each other in the same manner as the base units described in Figure 1.

A practical embodiment of the arrangement according to the invention is described with reference to Figure 4. In this embodiment, the UF filter block for ultrafiltration consists of a series of interconnected ultrafiltration units of the same structure, the filtrate of which is received by an RO concentrator block consisting of reverse osmosis units, optionally containing two such reverse osmosis units. In the arrangement shown in the drawing, the inlet 201 passes through a reservoir 203, the outlet of which is connected via a feed line 202 to a first ultrafiltration unit 204. The first ultrafiltration unit 204 is provided with a recirculating circuit 205 constructed in a manner known per se, which is located on the feed and filtrate outlet side. A pump 207 is inserted into the recirculation circuit 205 to provide the necessary flow for speed and pressure adjustment, and is connected to a conduit 206 which transmits the retained phase formed in the first ultrafiltration unit 204 to the feed line 209. Through this, the retained phase flows to a second ultrafiltration unit 211. As shown in FIG. 4, the second ultrafiltration unit 211 and subsequent ultrafiltration units not separately depicted in the drawing but forming part of the serial connection are arranged in a manner similar to the first ultrafiltration unit 204 and incorporated into the flow system, one for each. recycling circle. Each recirculation circuit is equipped with a pump and a trap passing the retained phase in the ultrafiltration units.

The filtered material formed in the first ultrafiltration unit 204 is conveyed by a filtrate line 208 to a common filtrate line 213, to which the retained-phase leads of the further ultrafiltration units can be connected as needed. The common filtrate line 213 terminates in a first reverse osmosis unit 21, i.e. a concentrating unit. Like the ultrafiltration units, the first reverse osmosis unit 210 is installed in a known manner in a recirculation circuit 215 in which a pump 217 and a retention phase transfer line 214 are arranged. The first reverse osmosis unit 210 is provided with an outlet 212 which discharges the diluted fraction, optionally the filtrate obtained by reverse osmosis. The conduit connecting to the outlet 212 is provided for the inlet of a second reverse osmosis unit 219 which is similar in structure and arrangement to the first reverse osmosis unit 210. The recirculating circuits of the first reverse osmosis unit 210 and the second reverse osmosis unit 219 also have a terminal 221 which is connected to a return line 216 216 for returning the increased density filtered material to the ultrafiltration units. In the arrangement shown in FIG. 4, the feed line 216 is illustrated with respect to the third, fourth and fifth ultrafiltration units 211 following the second ultrafiltration unit 211, but is not required, and may be provided in other ways. The membrane used in ultrafiltration units is generally designed to allow materials of molecular weight up to 10,000 to 20,000 to be selected.

Figure 4 shows the following material streams: (A): initial dispersion which is aqueous based,

EN 212 699 anyag substance consisting of a water or an aqueous solution in a continuous phase;

(B): filtrate from ultrafiltrate;

(Bl); excess filtrate from ultrafiltration;

(B2): filtrate from the ultrafiltrate to the reverse osmosis unit;

(C); fraction retained by ultrafiltration;

(D): fraction retained by reverse osmosis; and (E): filtrate from reverse osmosis.

If the concentration increase in the process or arrangement of the present invention is accomplished by membrane filtration, this may be accomplished using the base unit shown in Figure 1, wherein the membrane filter unit 4 comprises a Type I filter membrane and the concentrate unit 10 has a Type II filter membrane. The initial dispersion is then applied to a type I filter membrane, such as an ultrafiltration membrane, and here the type I filtrate is obtained from the initial dispersion, whereby a phase retained from the membrane filter can be removed. Most or all of the type I filtrate is processed on the Π type filter membrane to provide additional membrane filtration by nanofiltration, reverse osmosis filtration, or ultrafiltration using a filter element with a pore size smaller than the type I filter membrane. As a result, a type II filtrate is obtained and the phase retained on the filter membrane can be processed as an increased concentration of material. The increased concentration material or part thereof is recycled to the process by mixing with the initial dispersion and enriching the retained fraction with the constituents of the concentrated material obtained from the filtrate.

The desired composition of the retained fraction can be adjusted based on several parameters. The entire amount or, if appropriate, only a portion of the retained fraction with increased concentration can be traced back to the process. The required concentration increase for the retained fraction can be accomplished in one or more steps in a number of ways. By increasing the concentration of the retained fraction in a multi-step process, different types of filter membranes and filter units of different pore sizes can be interconnected. Such multi-stage fractionation may be carried out in the aftertreatment of the initially generated concentrated stream or in the aftertreatment of the initially formed filtrate.

Examples of such processes include:

The filtrate obtained by ultrafiltration is subjected to a reverse osmosis process and some or all of the material thus concentrated is returned to the inlet of the ultrafiltration unit.

The filtrate obtained by ultrafiltration is processed by nanofiltration and all or part of the increased density of the resulting nanofiltration is recycled to the inlet of the ultrafiltration unit.

The filtrate obtained by ultrafiltration is subjected to nanofiltration and the filtrate obtained from the nanofiltration is further refined by reverse osmosis, and then all or part of the increased density material obtained from the reverse osmosis process is recycled to the inlet of the ultrafiltration unit.

By properly selecting a concentration increasing unit, including determining the size and pore size of the membrane, it is achieved that the desired substances are returned to the inlet of the primary, i.e., type I, filter membrane, in a selective and controllable manner and, as a result, recoverable material in the form of a retention phase in the filtration unit.

Recycling the desired fraction of the increased concentration filtrate into the process provides the opportunity to develop a number of new products or to improve the properties of known products. Accordingly, by utilizing the arrangement of the invention for processing milk, fractionation of the milk components can be effected efficiently so that the amount of lactose retained in the filter can be increased and accurately adjusted, while the amount of monovalent salt in the retained fraction does not increase or growth remains within acceptable limits. Alternatively, the proportion of monovalent salts may be increased, while avoiding an increase in lactose concentration. This latter goal can be achieved, for example, by a combination of a nanofiltration filter unit and a reverse osmosis process, wherein lactose is collected in the retention phase of the nanofiltration unit, while the monovalent salts are removed by filtration of the nanofiltration unit but returned to the reverse osmosis unit. and thus added to the filter unit containing the primary membrane as retention phase.

The favorable proportion of lactose and mineral constituents in the retained fraction is a very important feature of the invention, as it can adjust many important parameters of the final product, such as taste, consistency, gelling capacity, thermal stability, color, etc. and therefore, the process and arrangement of the present invention are capable of meeting a very widespread need for adjusting a favorable proportion of these ingredients.

It is also an advantage of the process and arrangement of the invention that the proportion of solids in the retained phase can be effectively adjusted by recycling material previously considered to be environmentally harmful byproducts, and thus achieving very good yields in terms of weight. the amount of by-products that were previously considered dangerous due to disposal difficulties.

In the development of the process and arrangement of the present invention, the ultrafiltration of milk and milk-based semi-products was first of all considered. However, the starting dispersion can be not only milk but any water-based mixture in which the continuous phase is water

HU 212 699 Β author. For example, the above materials may be supplemented with blood or waste water as substances which form a dispersion which can be processed according to the invention.

Thus, in a particularly preferred embodiment of the process according to the invention, the proportion of the fat constituents of the milk relative to the high concentration dairy products is adjusted and further details are given by referring to Figures 5 and 6.

In the process illustrated in the flowchart of Figure 5, the steps are as follows:

1. Treatment of the milk by centrifugation, homogenization of the cream as necessary and pasteurization of the cream for a period of 15 seconds at a temperature generally between about 72 ° C and 75 ° C.

2. First ultrafiltration (UFj) at a temperature of about 45 ° C to about 55 ° C to produce a filtrate B having a solids content of about 5.7% to about 10% by weight and a solids content of about 15% to about 35% by weight. C retains phase.

3. Hyperfiltration (reverse osmosis process) or nanofiltration (HF / NF in the drawing) or evaporation: filtrate B from the first ultrafiltration is concentrated to the desired solids content and removed as filtrate D. The retained phase as a concentrated material is divided into streams Ej and E ₂ , wherein the solids content of the concentrated material Ej + E ₂ is about 10% to about 20% by weight for hyperfiltration, about 10% to about 40% for nanofiltration and for evaporation. from about 10% to about 50% by weight.

4. A second ultrafiltration, wherein the retention phase E from hyperfiltration or nanofiltration is mixed with the retention phase C obtained from the first ultrafiltration and the resulting mixture F is recycled to the second ultrafiltration step, thereby retaining H with a solids content of about 25% to about 50%. phase. The filtrate G thus obtained is carried on with the retained phase or excess of the concentrated material in the stream E ₂ , and the mixture is used as an initial dispersion or powdered lactose is prepared.

In the process illustrated in the flowchart of Figure 6, the steps are as follows:

1. The milk treatment corresponds to the flowchart of FIG.

2. The first ultrafiltration is also performed according to the flowchart of FIG.

3. Hyperfiltration or Nanofiltration or Evaporation: The filtrate B from the first ultrafiltration is transported together with the recovered feed portion of the filtrate from the second ultrafiltration and the solids content is adjusted to the desired value. The filtrate D is drained from the system. The solids content of the retained phase E as concentrated material is shown in the flowchart of Figure 5.

4. During the second ultrafiltration, the retained phase E obtained by HF / NF hyperfiltration or nanofiltration, optionally by evaporation, is passed as a concentrated material together with filtrate C from the first ultrafiltration step, the two materials are mixed and blend F in the second ultrafiltration step. and concentrating it to a solids content of about 50% by weight to give H a retained phase.

In Denmark, cow's milk solids are composed of the following components in average proportions:

Protein, of which -NPN

- true protein

Lactose

Acid

Ash

Fat

3.40% by weight 0.25% by weight 3.15% by weight 4.70% by weight 0.30% by weight 0.63% by weight 4.20% by weight

If the goal is to produce a low fat concentrated dairy product, the excess fat in the milk is reduced by separating a portion of the cream.

In the case of ultrafiltration, the total amount of fat is retained in the retained phase, while at least 90% of the protein is retained, depending on the density and size of the pores opening from the membrane filter surface. Thus, the ratio of protein to fat in the concentrated dairy product is determined by the percentage of fat.

The desired solids content of the final product can be well adjusted during ultrafiltration. If a solids content of about 25 to about 31% by weight is required, the retention phase C for UF3 ultrafiltration uniformity is selected as follows. If the retention phase H is adjusted to about 30 wt% solids from the UF ₂ ultrafiltration unit (Examples 5-9), the retention phase C for the UF ultrafiltration unit is selected to be about 16 wt%. One of the most commonly used parameters when setting the lactose content of a product is the retention phase that forms the concentrated material fed to the UF ₂ ultrafiltration unit, i.e., the amount of current E combined with the retention phase C from the UF ultrafiltration unit and comparing this value to UF ₂ ultrafiltration obtained with a solids content of the retained phase H. By selecting a lower solids content ala45 for the UF ultrafiltration unit in retention phase C and / or introducing a higher flow rate Ej and / or adjusting the solids content to a higher level in the latter, the percentage of lactose in the final product can be increased. In the retention phase obtained in the UFj ultrafiltration unit, the lower solids content requires increasing the capacity of the unit for hyperfiltration, nanofiltration or evaporation. Therefore, these parameters are selected according to the most economical operation possible, taking into account the system size, the surface of the filter membranes and the performance required for filtration.

The process of the present invention will now be described in more detail with reference to some embodiments, in which several details of the system for implementing the example will be discussed with reference to the accompanying drawings.

HU 212 699 Β

Example 1

Ultrafiltration of milk was performed using the arrangement shown in Figure 4. The membranes used for filtration allowed up to 15,000 molecular weight components to pass through. The streams 5 indicated in Figure 4 are detailed in the attached table, which gives the mass flow rate in kg / h for each ingredient, the weight percentage of solids and the weight percentage of the most important ingredients, that is, the total weight. In compiling the table, the embodiment of the arrangement of the present invention shown in Figure 4 utilizing conventional ultrafiltration units was utilized. The concentration step and the re-feeding of the material containing permeable dry ingredients at elevated concentrations were not performed in this case.

Spreadsheet

Ingredients obtained by ultrafiltration of milk

Flowing material Flow rate of substance, kg / h Composition ,,% by weight in the arrangement according to the invention in the known arrangement (The milk 10000 Solids: 13.5 Fat: 4.6 Protein: 3.4 Lactose: 4.6 Solids: 12.5 Fat: 3.6 Protein: 3.4 Lactose: 4.6 (B) - The ultrafiltrate filtrate 9,222 Dry solids: 7.3 Fat: 0.0 Protein: 0.3 Lactose 6.2 Dry matter: 5.8 Fat: 0.0 Protein: 0.2 Lactose: 4.9 (B1) - Excess filtrate 4,430 as (B) (B2) -Filtration leading to reverse osmosis 4,792 as (B) (C) -The ultrafiltration retained fraction 2,594 Dry matter: 39.5 Fat: 17.7 Protein: 12.7 Lactose: 7.0 Dry matter: 39.5 Fat: 17.7 Protein: 17.3 Lactose: 3.4 (D) -The fraction retained by reverse osmosis 1816 Dry matter: 19.0 Fat: 0.0 Protein: 0.6 Lactose: 16.3 (E) -A filtrate from reverse osmosis 2 976 Dry matter: 0.1

From the results, it appears that the ultrafiltration retained material achieves a composition in which the 40 solids constituents are present in the desired amount or the fat, i.e.

39.5% by weight and 17.7% by weight, respectively, with a protein content of 12.7% by weight and is the most expensive ingredient in the present invention. On the other hand, protein 45 must be provided in a proportion of at least 16.3% by weight to obtain a product containing 39.5% by weight of solids and 17.7% by weight of fat in the ultrafiltration filtrate when conventional, i.e. permeable solid. we work with an ultrafiltration system that works without the recycling of components.

Example 2

By concentrating whole milk, it is intended to provide an example of controlling the proportion of solids in the preparation of a product which can be used in the manufacture of low-fat spread soft cheese without preservation.

Specifications for the desired composition of the product are as follows:

The solids content is about 30% by weight 60

Fat content of solids including 1.20% by weight of salt at about 35% by weight

Protein about 11% by weight

Lactose about 7% by weight

To produce the desired composition of the product, a flowchart arrangement of Figure 5 was prepared with whole milk as the initial dispersion. The fat content of the whole milk was reduced to 3.25% by weight by separating the cream. The conditions for the first ultrafiltration were set to achieve a dry weight content of C retained fraction C of 27%. For the retention fraction C obtained at the first ultrafilter UFj, the E! the retained fraction was added to 20% by weight, while the filtrate G leaving the second ultrafiltration outlet of UF _{2 was} mixed with the excess retained fraction E ₂ obtained from the HF hyperfilter and then removed from the system as it is useful for feeding purposes, or powdered lactose. By carrying out the process, the following streams of material and composition were obtained:

HU 212 699 Β

Material First ultrafiltration hyper Filter Whole milk, Filtrate, B Withholding fraction, C Filtrate, D Withholding fraction, Ej + E ₂ Total quantity 1 11,000 7784.62 3215.38 5244.37 542.08 1897.14 + Protein, t% * 3.15 0.01 10.75 0 0.03 NPN,% t * 0.25 0.23 0.30 0.06 0.46 Lactose, t% * 4.70 5.13 3.66 0.02 16.31 Sav,% t * 0.30 0.20 0.54 0 0.71 Total ash,% t * 0.63 0.63 0.63 0.01 1.49 Fat, t% * 3.25 0 11.12 0 0 Solids, t% 12.28 6.2 27 0.09 19

Material Second ultrafiltration Feed, F Filtrate, G Withholding faction, H Total quantity, I 3858.46 643.08 3215.38 Protein, t% * 8.97 0.01 10.76 NPN,% t * 0.33 0.23 0.39 Lactose, t% * 5.77 7.88 6.92 Sav,% t * 0.57 0.30 0.68 Total ash,% t * 0.77 0.63 0.93 Fat, t% * 9.27 0 11.12 Solids, t% * 25.67 9.05 30.80

* i ^c á = weight%

Example 3

By concentrating whole milk, it is intended to provide an example of controlling the proportion of solids in the preparation of a product which can be used in the production of feta cheese in brine.

Specifications for the desired composition of the product are as follows:

Solid material

Fat content of solids including 3.50% by weight of salt Protein

Lactose

In order to obtain the product of the desired composition, the flowchart arrangement shown in Figure 5 is made up of about 40% by weight of about 40% by weight of about 11% by weight of about 10% by weight of whole milk. The conditions for the first ultrafiltration were set so that the C retained fraction had a dry weight content of 28%. Ej fraction retained in the UF, first received ultraszűrőnél C retentate fraction from the HF hiperszűrőből added 20% proportion, while leaving the UF _two second ultrafiltration, downstream G filtrate retained fraction derived from HF hiperszűrőből mixed _E2 excess and then removed from the system, since this for example, the mixture may be used for animal feed, so that it can be commercialized as such or be made into powdered lactose. By carrying out the process, the following streams of material and composition were obtained:

Material First ultrafiltration hyper Filter Whole milk, Filtrate, B Withholding fraction, C Filtrate, D Withholding fraction, Ej + E ₂ Total quantity, I 11,000 6594.71 4405.29 4442.75 881.06 1270.90 + Protein, i% * 3.15 0.01 7.85 0 0.03 NPN,% t * 0.25 0.23 0.28 0.06 0.46 Lactose, t% * 4.70 5.13 4.06 0.02 16.31 Sav,% t * 0.30 0.20 0.45 0 0.71 Total Ash, % by weight * 0.63 0.63 0.63 0.01 1.49 Fat. % by weight * 5.50 0 13.75 0 0 Solids, t% * 14.53 6.20 27 0.09 19

HU 212 699 Β

Material Second ultrafiltration Feed, F Filtrate, G Withholding faction, H Total quantity, I 5286.35 1919.25 3367.10 Protein, t% * 6.55 0.01 10.28 NPN,% by weight * 0.31 0.23 0.49 Lactose, t% * 6.10 7.88 9.57 Sav,% t * 0.49 0.30 0.77 Total ash,% t * 0.77 0.63 1.21 Fat, t% * 11.44 0 17.97 Solids, t% * 25.67 9.05 40.30

* t% = mass

Example 4

By concentrating whole milk, it is intended to provide an example of controlling the proportion of solids in the preparation of a product which can be used in the production of feta cheese in brine.

Specifications for the desired composition of the product are as follows:

Solids about 40% by weight

The fat content of solids including

3.50 wt% salt about 50 wt%

Protein about 7% by weight

Lactose about 8% by weight

To produce the desired composition of the product, a flowchart arrangement of Figure 5 was prepared with whole milk as the initial dispersion. The conditions for the first ultrafiltration were set so that the C retained fraction had a dry matter content of 30.12% by weight. The retention fraction C (obtained at the first ultrafiltration filter C) was added with 20% by weight of the retention fraction E ₍ from the HF hyperfilter), while the filtrate G leaving the second ultrafiltration effluent (UF _{2) was} mixed with the excess E ₂ retained fraction for example, this mixture can be used for animal feed purposes, and is therefore suitable for commercial sale as such, or can be made from powdered lactose.

Material First ultrafiltration hyper Filter Whole milk, Filtrate, B Withholding fraction, C Filtrate, D Withholding fraction, e, + e ₂ Total quantity 1 11,000 5099.92 5900.08 3435.73 1180.02 484.17 + Protein. % by weight * 3.15 0.01 5.86 0 0.03 NPN,% t * 0.25 0.23 0.27 0.06 0.46 Lactose. % by weight * 4.70 5.13 4.33 0.02 16.31 Sav,% t * 0:30 0.20 0.39 0 0.71 Total ash,% t * 0.63 0.63 0.63 0.01 1.49 Fat. % by weight * 10 0 18.64 0 0 Solid material. % by weight * 19.03 6.20 30.12 0.09 19

Material Second ultrafiltration Feed, F Filtrate, G Withholding faction, H Total quantity, I 7080.10 2022.89 5057.21 Protein, t% * 4.89 0.01 6.85 NPN,% t * 0.30 0.23 0.42 Lactose, t% * 6.33 7.88 8.86 Sav,% t * 0.44 0.30 0.62 Total ash,% t * 0.77 0.63 1.08 Fat, t% * 15.54 0 21.75 Solids, t% * 28.27 9.05 39.57

* t% = weight%

HU 212 699 Β

Example 5

By concentrating whole milk, it is intended to provide an example of controlling the proportion of solids in the preparation of a product which can be used in the production of feta cheese in brine.

Specifications for the desired composition of the product are as follows:

Solids about 42% by weight

The fat content of solids including

3.50% by weight salt about 45% by weight

Protein about 10% by weight

Lactose about 10% by weight

To obtain the desired composition of the product, see Figure 5.

Figure 1 is a flowchart arrangement wherein the initial dispersion was whole milk, the fat content of which was increased to 6.90% by weight with the addition of cream. The conditions for the first ultrafiltration were set to achieve a content of 28.58% by weight of dry substance 5 in the retained fraction C. The UF | retentate fraction obtained first ultraszűrőnél C E retained fraction from the HF hiperszűrőből added 20% proportion, while leaving the second ultrafiltration, downstream UF ₂ G filtrate obstructing HF hiperszűrőből eltávolí10 Totten, whereas this mixture is useful in feeding purposes, so it is itself capable commercially available or powdered lactose may be prepared. By carrying out the process, the following streams of material and composition were obtained:

Material First ultrafiltration hyper Filter Whole milk, Filtrate, B Withholding fraction, C Filtrate, D Withholding fraction, E | + E ₂ Total quantity 1 11,000 6217.39 4782.61 4188.56 956.52 1072.31 + Protein, t% * 3.15 0.01 7.23 0 0.03 NPN,% t * 0.25 0.23 0.28 0.06 0.46 Lactose, t% * 4.70 5.13 4.14 0.02 16.31 Sav,% t * 0.30 0.20 0.43 0 0.71 Total Ash, % by weight * 0.63 0.63 0.63 0.01 1.49 Fat, l% * 6.90 0 15.87 0 0 Solid material. t% 15.93 6.20 28.58 0.09 19

Material Second ultrafiltration Feed, F Filtrate, G Withholding faction, H Total quantity, I 5739.13 20,60.20 3678.93 Protein. % by weight * 6.03 0:01 9.41 NPN,% t * 0.31 0.23 0:48 Lactose, {%* 6.17 7.88 9.62 Sav,% t * 0.48 0.30 0.74 Total ash,% t * 0.77 0.63 1.21 Fat, t% * 13.23 0 20.63 Solid material. t% 26.98 9.05 42.09

*% by weight

Example 6

By concentrating whole milk, we intend to provide an example of controlling the proportion of solids in the preparation of a product which can be used in the manufacture of light feta cheese or spreadable cheese-like food in brine.

Specifications for the desired composition of the product are as follows:

Solids about 30% by weight

The fat content of solids including

2.50% by weight salt about 20% by weight

Protein about 10% by weight

Lactose about 12% by weight

To produce the desired composition of the product, a flowchart arrangement as shown in Figure 5 was prepared, wherein the starting dispersion was whole milk, the fat content of which was reduced to 2.20% by weight. The conditions of the first ultrafiltration were set to achieve a dry solids content of 16.26% by weight in the retained fraction C. The retention fraction C of UF obtained at the first ultrafiltration is derived from the HF hyperfilter16

The retained fraction was added at 20% by weight, while the filtrate G leaving the second ultrafiltration outlet of UF _{2 was} mixed with the excess retained fraction E ₂ from the HF hypofilter and then removed from the system as it is useful for feeding purposes, for example. therefore, it is suitable for commercial sale as such or can be made from powdered lactose. By carrying out the process, the following streams of material and composition were obtained:

Material First ultrafiltration hyper Filter Whole milk, Filtrate, B Withholding fraction, C Filtrate, D Withholding fraction, E] + E ₂ Total quantity 1 11,000 5500.00 5500.00 3705.26 1100.00 + 694.74 Protein, t% * 3.15 0.01 6.29 0 0.03 NPN,% t * 0.25 0.23 0.27 0.06 0.46 Lactose, t% * 4.70 5.13 4.27 0.02 16.31 Sav,% t * 0.30 0.20 0.40 0 0.71 Total ash, t% ' 0.63 0.63 0.63 0.01 1.49 Fat, t% * 2.20 0 4.40 0 0 Solids, t% 11.23 6.20 16.26 0.09 19

Material Second ultrafiltration Feed, F Filtrate, G Withholding faction, H Total quantity, I 6600.00 3032.43 3567.57 Protein, t% * 5.25 0.01 9.71 NPN,% t * 0.30 0.23 0.56 Lactose, t% * 6.28 7.88 11.61 Sav,% t * 0.45 0.30 0.84 Total ash,% t * 0.77 0.63 1.43 Fat, t% * 3.67 0 6.78 Solids, t% 16.72 9.05 30.93

* t% = weight ¹ ?

Example 7

By concentrating whole milk, it is intended to provide an example of controlling the proportion of solids in the preparation of products that can be used in the production of feta cheese in brine.

Specifications for the desired composition of the product are as follows:

Solids about 40% by weight

Fat content of solids including 4.20% by weight salt about 40% by weight

Protein about 15% by weight

Lactose about 6% by weight

To obtain the desired composition of the product, a flowchart arrangement of Figure 5 was prepared, wherein the starting dispersion was whole milk, the fat content of which was reduced to 4.00% by weight of the cream. The conditions of the first ultrafiltration were set to achieve a dry matter content of 30.11% by weight in the retained fraction C. The UF | the retention fraction C from the first ultrafilter was added to the retention fraction E from the HF hyperfilter in a proportion of 5 wt.

The filtrate G at the outlet of the second ultrafiltrate UF _{2 was} mixed with the excess retained fraction E ₂ from the HF hyperfilter and then removed from the system, since this mixture can be used for feed purposes, for example, as such or lactose powdered. By carrying out the process, the following streams of material and composition were obtained:

Material First ultrafiltration hyper Filter Whole milk, Filtrate, B Withholding fraction, C Filtrate, D Withholding fraction, E | + E ₂ Total quantity, I 11,000 7857.14 3142.14 5293.23 157.14 2406.77 + Protein, t% * 3.15 0.01 11.00 0 0.03

HU 212 699 Β

Material First ultrafiltration hyper Filter Whole milk, Filtrate, B Withholding fraction, C Filtrate, D Withholding fraction, E | + E ₂ NPN,% t * 0.25 0:23 0.30 0.06 0.46 Lactose, t% * 4.70 5.13 3.63 0.02 16.31 Sav,% t * 0.30 0.20 0.55 0 0.71 Total ash,% t * 0.63 0.63 0.63 0.01 1.49 Fat, t% * 4.00 0 14.00 0 0 Solids, t% 13.03 6.20 30.11 0.09 19.00

Material Second ultrafiltration Feed, F Filtrate, G Withholding faction, H Total quantity, I 3300,00 873.53 2426.47 Protein, t% * 10.48 0.01 14.25 NPN,% t * 0.31 0.23 0.42 Lactose, t% * 4:23 7.88 5.75 Sav,% t * 0.56 0.30 0.76 Total ash,% t * 0.67 0.63 0.91 Fat, t% * 13.33 0 18.13 Solids, t% 29.58 9.05 40.22

*% by weight

Example 8

By concentrating whole milk, it is intended to provide an example of controlling the proportion of solids in the preparation of a product which can be used in the production of feta cheese in brine.

Specifications for the desired composition of the product are as follows:

Solids about 40% by weight

The fat content of solids including

4.20% by weight salt about 40% by weight

Protein about 8% by weight

Lactose about 12% by weight

For the preparation of the desired composition, the flowchart arrangement shown in Figure 6 was prepared with whole milk as the initial dispersion. The conditions of the first ultrafiltration were set to achieve a solids content of 26.49% by weight in the retained fraction C. The UF | for the filtrate B obtained at the first ultrafiltration, from the Gi filtrate leaving the UF ₂ second ultrafilter outlet

6% by weight and retention fraction E from the HF hyperfilter were added to 40% by weight of UF retention fraction C from the first ultrafilter, while excess G _{2 of} the filtrate exiting the second ultrafiltration outlet of UF _{2 was} recovered, for example for feeding purposes. It can be utilized, that is, in itself, suitable for commercial sale, or it can be made from powdered lactose. By carrying out the process, the following streams of material and composition were obtained:

Material First ultrafiltration hyper Filter Whole milk, Filtrate, B Withholding fraction, C Filtrate, D Withholding fraction, E, + E ₂ Total quantity 1 11,000 5500.00 5500.00 3627.11 2200,00 Protein, t% * 3.15 0.01 6.29 0 0.03 NPN, t% ' 0.25 0.23 0.27 0.06 0.46 Lactose, t% * 4.60 5.40 3.80 0.02 16.31 Sav, t% ' 0.30 0.20 0.40 0 0.71 Total ash, t% ' 0.63 0.63 0.63 0.01 1.49 Fat, t% * 7.55 0 15,10 0 0 Solids, t% 16.48 6.47 26.49 0.09 19.00

HU 212 699 Β

Material Second ultrafiltration Feed, F Filtrate, G ₂ + G ₂ Withholding faction, H Total quantity, I 7700.0 327.11 2706.22 + 4666.67 Protein, t% * 4.50 0.01 7.43 NPN, (% * 0.32 0.23 0.54 Lactose, t% * 7.37 7.88 12.17 Sav,% t * 0.49 0.30 0.81 Total ash,% t * 0.88 0.63 1.44 Fat, t% * 10.79 0 17.80 Solids, t% 24.35 9.05 40.18

* t% = weight%

Example 9

By concentrating whole milk, it is intended to provide an example of controlling the proportion of solids in the preparation of a product which can be used in the production of feta cheese in brine.

Specifications for the desired composition of the product are as follows:

Solids about 40% by weight

The fat content of solids including

4.20% by weight salt about 40% by weight

Protein about 12% by weight

Lactose about 8% by weight

An arrangement for the preparation of the desired composition of the product was prepared using the flow chart depicted in Figure 5 with whole milk as the initial dispersion. The filtrate obtained by the first ultrafiltration was concentrated by evaporation, while the conditions of the second ultrafiltration were adjusted so as to obtain 20% by weight of dry matter in fraction C retained. The UF | retention fraction C obtained by ultrafiltration, from evaporation E | 20% by weight of the concentrate was added while the filtrate G leaving the second ultrafiltration outlet of UF _{2 was} mixed with excess concentrate E _{2 of} the concentrate concentrate and then removed from the system, since this mixture can be used for feeding purposes, lactose can be prepared. By carrying out the process, the following streams of material and composition were obtained:

Material First ultrafiltration hyper Filter Whole milk, Filtrate, B Withholding fraction, C Filtrate, D Withholding fraction, E] + E ₂ Total amount. I 11,000 7071.43 3928.57 4861.61 785.71 + 1424.11 Protein, t% * 3.15 0.01 8.80 0 0.03 NPN. % by weight * 0.25 0.23 0.29 0.02 0.67 Lactose, t% * 4.47 5.40 2.80 0 17.28 Sav,% t * 0.30 0.20 0.48 0 0.64 Total Ash, % by weight * 0.63 0.63 0.63 0.01 1.98 Fat, t% * 4.90 0 13.72 0 0 Solids, t% 13.70 6.47 26.71 0.03 20.61

Material Second ultrafiltration Feed, F Filtrate, G Withholding faction, H Total quantity, I 4714.29 1730.56 2983.73 Protein, t% * 7.34 0.01 11.60 NPN,% t * 0.25 0.23 0.55 Lactose, t% * 5.21 7.88 8.23 Sav,% t * 0.51 0.30 0.80 Total ash,% t * 0.86 0.63 1.35 Fat, t% * 11.43 0 18.06 Solids, t% 25.70 9.05 40.60

* t =% by weight

HU 212 699 Β

Example 10

By concentrating whole milk, it is intended to provide an example of controlling the proportion of solids in the preparation of a product which can be used in the production of feta cheese in brine.

Specifications for the desired composition of the product are as follows:

Solids about 30% by weight

The fat content of solids including

2.50% by weight salt about 20% by weight

Protein about 10% by weight

Lactose about 12% by weight

To produce the desired composition of the product, a flowchart arrangement of Figure 5 was prepared with whole milk as the initial dispersion. The conditions for the first ultrafiltration were set to achieve a dry weight content of C retained fraction C of 27%. The retention fraction C) obtained from the first ultrafilter was added to the retained fraction E) from the HF hyperfilter in a proportion of 16.07 wt%, while the filtrate G leaving the second ultrafiltration outlet of UF _{2 was} mixed with the excess E ₂ retained fraction from the HF since this mixture can be used, for example, for animal feed, so that it can be commercialized as such or be made into powdered lactose. By carrying out the process, the following streams of material and composition were obtained:

Material First ultrafiltration hyper Filter Whole milk, Filtrate, B Withholding fraction, C Filtrate, D Withholding fraction, e, + e ₂ Total quantity, I 11,000 5500.00 5500.00 3781.25 1485.00 + 233.75 Protein, t% * 3.15 0.01 6.29 0 0.03 NPN,% t * 0.25 0.23 0.27 0:02 0.67 Lactose, t% * 4.59 5.40 3.78 0 17.28 Sav,% t * 0.30 0.20 0.40 0 0.64 Total Ash, % by weight * 0.63 0.63 0.63 0:01 1.98 Fat. % by weight * 2.25 0 4.70 0 0 Solid material. t% 11.27 6.47 16.07 0.03 20.61

Material Second ultrafiltration Feed. F Filtrate, G Withholding faction. H Total quantity, I 6985.00 3104.44 3880.56 Protein. % by weight * 4.96 0.01 8.93 NPN,% t * 0.36 0.23 0.64 Lactose, t% * 6.65 7.88 11.97 Sav,% t * 0.45 0.30 0.81 Total ash,% t * 0.92 0.63 1.65 Fat, t% * 3.70 0 6.66 Solids, t% 17.03 9.05 30.66

* t% = mass

The process and arrangement of the present invention can be obtained by membrane filtration treatment of aqueous dispersions to obtain products containing a desired amount of various components in the initial dispersion. Preferably, the proposed process and arrangement is used in milk processing and the desired concentration of the selected ingredients in the resulting semi-finished and finished products can be adjusted with relative accuracy.

While the foregoing details of the invention have been described in more detail in preferred embodiments and embodiments, one skilled in the art will be able to provide many other variations based on the teachings and knowledge of the present disclosure, which are, however, within the scope of the appended claims.

PATENT CLAIMS

Claims (26)

PATENT CLAIMS Arrangement 55 first membrane filtration dispersion liquid containing a dispersion of transmitting one or more continuous aqueous phase feed line (2, 2 ^n_l, 2 ^n, 2 ^{n + l)} at the top arranged filtrate obtained by removing material delivery outlet (6, 6 ^-1 , 6, 6 ^{n + l} ) and A ^{membrane with} 60 ^{filtrate lines} (8, 8 ^n_1 , 8, 8 ^{+ 1} ) GB 212 699 Β contains a filter unit (4, 4 "', 4, 4 ^{n + 1} ), where the drain (6, 6 ^n_l , 6 ⁿ , 6 ^{n + 1} ) is the next membrane filter unit (4, 4 ⁿ ~', 4 ⁿ , 4 ^{n + 1} ) or is connected to its feed line (2, 2 ^-1 , 2 ⁿ , 2 ^{n + 1} ), characterized in that the one or more membrane filter units (4, 4 ^-1 , 4) , 4 ^{n + 1} ) of filtrate lines (8, 8 ”, ¹ , 8, 8 ^{n + 1} ) in one or more concentrating units (10, ΙΟ ^-1 , 10, 10 ^{n + 1} ) separating the filtrate into diluted fractions and concentrated fractions guided, wherein the concentrating unit (10, 10 ^'1, 10, 10 ^{n + 1)} each having a first outlet transport the diluted fraction (12, 12 ^_1, 12, 12 ^{+ l)} and carrying the concentrated fraction is the second outlet (14, 14 ^-1 , 14, 14 ^wl ), wherein the second outlet (14, ^14-1 , 14, 14 ^{n + 1} ) is connected to a feed line (16, 16 ^-1 , 16 ⁿ , 16 ¹¹⁴¹ ) which is one or more membrane filter unit (4, 4) ~ 4 ⁿ , 4 ^{n + l} ) is connected to the feed line (2, 2 * ¹ , 2 ⁿ , 2 ^{n + 1} ). Arrangement according to claim 1, characterized in that a given membrane filter unit (4, 4 - ¹ , 4, 4 ^{n + 1} ) connected to a concentrating unit (10, 10 ', ¹ , 10, 10 ^{+ 1} ) is a concentrating unit (4, 4 - ¹ , 4, 4 ^{n + 1} ). at 10, 10 ^'1, 10, 10 ^{n + l)} second outlet is guided to the return conduits (16, 16 ^_l, 16, 16 ^{+ 1)} and thereby the respective membrane filter unit (4.4 ^_l, 4, ^{4N + l} ) is ^{connected to} one or more feed lines (2, 2, 1, 2, 2 ^{n + 1} ) and / or to the inlet of at least one previous membrane filter unit (4, 4 ^n_1 ). Arrangement according to Claim 1 or 2, characterized in that the concentrating units (10, ΙΟ ' ¹ , 10, 10 ^{n + 1} ), in particular the first and second reverse osmosis units (210, 219), are interconnected by one another. or a plurality of groups thereof, wherein the one or more groups are provided with a conduit (214) or outlet (221) connected to a common feed line (216). 4. Arrangement according to any one of claims 1 to 3, characterized in that it comprises one or more groups of concentrating units (10, 10 ^n_1 , 10, 10 ^{n + 1} ) connected in series, in particular the first and second reverse osmosis units (210, 219), wherein first concentrating unit (10, 10 * ^1, 10, 10 ^{+ 1),} in particular the second outlet of the first osmosis unit (210) (14, 14 ^-1, 14, 14 ^{n + l)} the following concentrating unit (10, 10 ^_1 , 10, 10 ^{n + 1} ), in particular a second reverse osmosis unit (219). 5. Arrangement according to any one of claims 1 to 3, characterized in that the concentrating unit (10, 10X 10, 10 ^{n + 1} ) is formed with first and second membrane units, in particular a nanofiltration unit (120) and an inverse osmotic unit (126), wherein the second membrane unit it has a pore size smaller than the first, and the filtrate line (108) of the first membrane unit, in particular the nanofiltration unit (120), is connected to the inlet of the second membrane unit, in particular the reverse osmosis unit (126). 6. Arrangement according to one of Claims 1 to 3, characterized in that the membrane filter unit (4, 4 ⁿ , 1, 4, 4 ^{+ 1} ) is designed as a microfilter or ultrafilter unit. Arrangement according to one of Claims 1 to 6, characterized in that the concentrating unit (10, 10 ** ^-1 , 10, 10 ^{n + 1} ) is formed by a centrifuge, an evaporating unit and / or an additional membrane filter unit. Arrangement according to claim 7, characterized in that the concentrating unit (10, ΙΟ ¹ , 10, 10 ^{n + 1} ) is provided with an additional membrane filter unit which is used in the membrane filter unit (4, 4 × 4, 4 ^{+ 1} ). with a pore size smaller than the membrane. 9. Arrangement according to any one of claims 1 to 3, characterized in that the membrane filter unit (4, 4 ^-1 , 4, 4 ^{n + 1} ) is formed by an ultrafiltration unit (104), the concentrating unit (10, 10 ^-1 , 10, 10 * ¹ ). comprising a nanofiltration unit (120), the latter having a conduit (124) for transferring material separated from the filtrate and a filtrate conduit (122) for transferring the filtrate, wherein the outlet of the filtrate conduit (122) is led to an inlet osmosis unit (126); a second outlet (114) for supplying material separated from the filtrate and a second outlet (114) for carrying the filtrate; and the second outlet (114) for one or more feed lines (2) to the membrane filter units (4.4, ^1.4 , 4 ⁺¹ ). , 2 ^-1 , 2, 2 ^{n + 1} , 102) is connected to an open feed line (116). 10. A process for membrane filtration of a dispersion solution, wherein a dispersion containing a continuous aqueous phase is processed by an arrangement comprising one or more membrane filter units in one or more filtration steps, wherein an initial or inlet dispersion is introduced into the membrane filtration unit inlet. converting the dispersion into a phase retained by the filtration membrane and into a filtrate obtained after the filtration membrane and, if necessary, processing the retained material in whole or in part in one or more further filtration steps, characterized by increasing the concentration of filtrate obtained in one or more filtration steps thereby producing a concentrated fraction containing the whole or part of the dry matter present in the filtrate in an increased concentration and the concentrated fraction it is recycled to the starting or inlet dispersion and processed as part of the filtration step with one or more filter membranes. 11. A process according to claim 10, wherein the concentration is increased by centrifugation and / or evaporation and / or membrane filtration. The process according to claim 10 or 11, wherein the concentration is increased by membrane filtration using an auxiliary membrane smaller than the membrane used in the membrane filtration unit to provide initial or inlet dispersion filtration. 13. A 10-12. A process according to any one of claims 1 to 6, wherein the filtration in the membrane filter receiving the initial or input dispersion is ultra21 The filtration is performed on one or more membrane filtration units equipped with one or more membrane filtration units that perform nanofiltration and / or reverse osmosis. 14. A 10-13. Process according to any one of claims 1 to 3, characterized in that the starting or input dispersion introduced into the membrane filter is a material containing fat and / or protein, in particular a dairy product. 15. A 10-14. A process according to any one of claims 1 to 3, characterized in that the membrane filtering of the starting or inlet dispersion is carried out by diafiltration. 16. A process according to any one of claims 1 to 3, wherein the concentration increase is accomplished by combining a nanofiltration membrane with a reverse osmosis membrane, the filtrate obtained from the membrane being added as an input dispersion to the inlet side of the reverse osmosis membrane and the reverse osmosis filtration membrane concentrated material is added to the inlet of the membrane filter unit receiving ultrafiltration receiving the starting or inlet dispersion. 17. A 10-16. A method according to any one of claims 1 to 6. characterized in that milk is introduced into the inlet of the membrane filter unit provided with the ultrafilter, processing to obtain a concentrated milk product and controlling the amount of solids from the milk by first filtrating the filtrate from the initial or inlet dispersion supplemented with at least a portion of the filtrate from step (a), subject to hyperfiltration or nanofiltration or evaporation, and all or part of the resulting higher density material is recycled to a second filtration ultrafiltration membrane filter and recycled as necessary to achieve the desired proportion of solids . 18. The method of claim 17, wherein some or all of the increased density material obtained from the filtrate from the first filtration step from the filtrate obtained from the ultrafiltration membrane is subjected to a second filtration step of the ultrafiltration unit filtration process. 19. The process of claim 17, wherein the high density material obtained by hyperfiltration, nanofiltration, and / or evaporation from the filtrate obtained from the filtrate from the first filtration step is combined with a portion of the filtrate obtained in the second filtration step. unit to the second filtration step. 20. A 17-19. A process according to any one of claims 1 to 5, characterized in that in the membrane filter unit provided with the ultrafilter, the first filtration step is continued until a solids content of 15-35% by weight, preferably 2531% by weight, is retained. 21. A process according to any one of claims 1 to 6, characterized in that the dry matter content of the product in the ultrafiltration membrane filter unit is continuously adjusted to 18-50% by weight, preferably 25-50% by weight. 22. A 17-21. Process according to any one of claims 1 to 3, characterized in that the filtrate obtained by the first filtration step in the ultrafiltration membrane filter unit is 10-22% by weight, preferably 15-19% by hyperfiltration in a medium characterized by a temperature of about 30 ° C and a pH of 5.9-6.1. % solids concentrate. 23. A process according to any one of claims 1 to 4, wherein the filtrate obtained by the first filtration step in the ultrafiltration membrane filtration unit is converted by nanofiltration at a concentration of 10-40% by weight in dry matter at about 20-60 ° C. 24. A 17-21. Process according to any one of claims 1 to 3, characterized in that the filtrate obtained in the first filtration step in the ultrafiltration membrane filtration unit is converted by evaporation to a dry matter concentrate containing 10-50% by weight, preferably 20640% by weight. 25. A 17-24. A process according to any one of claims 1 to 6, wherein the starting dispersion is milk and adjusting the proportion of proteins and fats in the concentrated product by adjusting the fat content of the milk. 26. A 17-25. A process according to any one of claims 1 to 6, wherein the proportion of lactose in the increased concentration product is adjusted by a first filtration step in the ultrafiltration membrane filtration unit, and / or a second filtration in the ultrafiltration membrane filtration unit and / or a second filtration in the ultrafiltration membrane filtration unit. by increasing the amount of the higher density material obtained by nanofiltration and / or evaporation and / or adjusting the higher dry matter content of the higher density material obtained by hyperfiltration or nanofiltration, or vice versa, or a membrane filter unit with ultrafiltration b In the second filtration step, it is reduced by using a smaller amount of the higher density material obtained by hyperfiltration and / or nanofiltration and / or evaporation and / or by adjusting the lower dry matter content of the higher density material obtained by hyperfiltration or nanofiltration.