JP2011205976A - Method and apparatus for recovering water-soluble protein - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide an apparatus for efficiently recovering water-soluble protein contained in a processing solvent of animal food.SOLUTION: The apparatus 10 for recovery includes heaters 11a-11c arranged with electrodes 21 and 22 arranged in a pair. The aggregate of water-soluble protein in a processing solvent is produced by energizing the electrodes 21 and 22 in a condition of equally keeping a flow velocity in a cross section in a direction which the processing solvent L crosses a flow direction in a heating chamber 23. The aggregate becomes lump and is produced in the heating chamber 23 without adhering to the inner peripheral surface of the heaters 11a-11c, and the aggregate is recovered from the processing solvent L through a filter 27. Water-soluble protein having a different molecular weight is fractionally recovered by increasing the temperature of the heater on a downstream side rather than an upstream side.

Description

  The present invention relates to a technique for recovering a water-soluble protein contained in a processing solution for animal foods such as a seafood bleaching solution or a livestock dipping solution.

  When producing processed foods such as surimi foods for seafood, the seafood is washed or exposed. In a food processing factory, these treatment liquids cannot be discarded as they are, so they need to be purified by a waste liquid treatment facility and discharged to the outside. In the case of producing ham using raw meat such as pork and beef, an immersion liquid is used to soak the seasoning into the raw meat material. This immersion liquid is also a waste liquid after the immersion treatment, and is purified by a waste liquid treatment facility and discharged to the outside. For this reason, in a food processing factory that manufactures processed foods made from animal foods such as seafood and livestock meat, a waste liquid treatment facility is installed at a high cost to purify the processing liquid of the food materials. There is a need.

  The reason why the manufacturing cost and maintenance cost of the waste liquid treatment facility is high is that protein is contained in the treatment liquid of animal food. When protein is contained in the waste liquid, it is inevitable that the structure and processing steps of the waste liquid treatment facility become complicated, unlike the case where waste water containing only foreign matters such as dust is treated.

  Since treatment liquids for animal foods contain a large amount of water-soluble proteins, methods for separating and recovering water-soluble proteins from the treatment liquids have been studied. If the water-soluble protein can be recovered from the processing liquid, not only can the waste liquid treatment be performed quickly by a waste liquid processing facility with a simple structure, but the recovered water-soluble protein should be commercialized as a supplement to meet the demand. Is possible.

  There exists a thing described in patent document 1 as a water-soluble meat preparation which uses meat itself as a raw material by solubilizing the meat containing the myofibril which does not melt | dissolve in water. This prepared product is produced by adding a low-concentration saline to minced meat, stirring and pulverizing it, and centrifuging it to concentrate a solution from which aggregates have been removed.

JP 2003-144097 A

  A processing solution used for cleaning or exposing food materials in a food processing factory contains water-soluble proteins contained in animal foods. Since this water-soluble protein is denatured and becomes an aggregate when heated, the water-soluble protein can be separated and recovered from the treatment station by heat-treating the treatment liquid. Since the proteins that become aggregates have different molecular weights depending on the heating temperature, they can be recovered by being separated into proteins having different characteristics by changing the heating temperature of the treatment liquid.

  As a method of adjusting the temperature by heating the treatment liquid, a method of charging the treatment liquid into a heating container and heating the heating container using a heating means such as a gas burner can be considered. However, in such a method of heating the container from the outside, the processing liquid is heated from the outer part toward the central part by the heat conduction of the processing liquid itself. A large temperature difference has occurred. Therefore, subtle and accurate temperature control for separating and recovering proteins having different characteristics by heating the treatment liquid is not possible. As a method for eliminating a large temperature difference between the outer portion and the central portion of the heat treatment liquid, a method of sufficiently stirring the treatment liquid can be considered. However, even if stirring, the temperature difference with the outer edge part directly heated cannot be eliminated.

  As a heating method with relatively easy temperature control, a method of heating the treatment liquid using a heat exchanger in which hot water controlled to a target temperature is circulated is considered. However, in principle, since the heat is applied from the outside of the container, the temperature difference from the outer edge cannot be eliminated strictly. Furthermore, in such a heating system, a phenomenon occurs in which aggregates of denatured proteins called scum adhere to the inner surface of the heating container. In addition, since scum is generated at the outer edge where the protein is denatured and coagulated at the highest temperature, the occurrence of the phenomenon that aggregates adhere to the inner surface of the heating container cannot be prevented even if the processing solution is vigorously stirred. It was.

  As described above, when aggregates adhere to the inner surface of the heating container as scum, it is necessary to wash and remove them, and it is impossible to efficiently separate and recover the water-soluble protein.

  On the other hand, in the method of supplying the processing liquid into the heating chamber in the heater in which the electrodes are arranged and flowing the current between the electrodes to heat the processing liquid by Joule heat, the processing liquid itself is directly heated by the heat generation, The processing liquid in the processing chamber can be heated at a uniform temperature as a whole without stirring the processing liquid.

  However, in a conventional continuous heating device for solution using Joule heat, the agglomerates become fine particles due to the flowing solution and float in the processing liquid, causing the phenomenon that the agglomerates adhere to the inner surface of the heating vessel. It could not be prevented.

  Furthermore, even when the Joule heating method is used, if the water-soluble protein is heat-denatured and aggregated and separated, and the uniformity of the solution is lost, the temperature distribution varies and uniform temperature control cannot be performed. This is not a big problem when simply collecting and collecting all proteins, but it becomes a problem when separating and collecting specific proteins using temperature differences. In addition, a large amount of processing liquid is used in food processing factories, and it is desirable to process the processing liquid continuously in order to process this.

  Therefore, the present invention provides a problem for accurately and uniformly heating a treatment solution for animal foods containing a large amount of water-soluble protein to an arbitrary temperature, and a problem for preventing the occurrence of scum that occurs at that time. To solve the problem.

  The water-soluble protein recovery method of the present invention is a water-soluble protein recovery method for separating and recovering water-soluble protein from a processing solution for animal food such as seafood, and is supplied to a heating chamber in a heater. The processing liquid is made to remain in the processing liquid through a plurality of electrodes arranged in pairs in the heating chamber in a state where the flow velocity in the cross section in the direction crossing the flow direction is kept constant. A heating step of energizing and heating the treatment liquid to the protein denaturation temperature; and a separation step of separating the water-soluble protein aggregates generated by the heat generation of the treatment liquid in the heating step from the treatment liquid by the separation means. And water-soluble protein is aggregated and recovered from the treatment liquid.

  The water-soluble protein recovery method of the present invention sequentially conveys the treatment liquid from the heater having a low heating temperature to the heater having a high heating temperature with respect to the plurality of heaters having different heating temperatures. The water-soluble protein that has become an aggregate in each of the heaters is separated by a separation means, and a plurality of types of water-soluble proteins having different molecular weights according to the denaturation temperature are separated and recovered from the treatment liquid. To do. In the method for recovering a water-soluble protein of the present invention, a treatment liquid is supplied into the heater from the lower side, and the water-soluble protein is aggregated integrally on the entire surface of the treatment liquid in the heater. It overflows from the surface of a heater, and is conveyed to the said separation means. The water-soluble protein recovery method of the present invention includes a tubular member that is formed of an insulating member and forms the heating chamber, and a heater that includes a plurality of annular electrodes provided in pairs with the tubular member. The processing liquid is supplied from the upstream end of the heater at a flow rate at which the processing liquid is in a turbulent state, and aggregated in the direction perpendicular to the processing liquid transport direction at the downstream end of the heater. A water-soluble protein is conveyed from the downstream end to the separation means.

  The water-soluble protein recovery device of the present invention is a water-soluble protein recovery device that separates and recovers a water-soluble protein from a processing solution for animal food such as seafood, and includes a plurality of pairs arranged in pairs. A heater having a heating chamber in which an electrode is disposed and the processing liquid is kept stationary or a flow rate in a cross section in a direction crossing the flow direction is uniformly maintained, and electric power is supplied to the processing liquid through the electrode, and the processing liquid A power supply unit that heats the water-soluble protein contained in the treatment liquid to a denaturing temperature, and a separation means that separates the water-soluble protein aggregates generated by the heat generation of the treatment liquid from the treatment liquid in the heater. And water-soluble protein is aggregated and recovered from the treatment liquid.

  The water-soluble protein recovery apparatus of the present invention comprises a low-temperature side heater for aggregating the water-soluble protein in the processing liquid, and the low-temperature side heating by heating the processing liquid at a higher temperature than the low-temperature side heater. A plurality of heaters having a high temperature side heater for aggregating the water-soluble protein having a higher denaturation temperature than the water-soluble protein aggregate produced by the vessel, and having different heating temperatures from each other; A plurality of separation means for separating the water-soluble protein aggregates from the treated processing solution from the processing solution, and separating a plurality of types of water-soluble proteins having different molecular weights depending on the denaturation temperature from the processing solution. It collects. The water-soluble protein recovery device of the present invention supplies a treatment liquid into the heater from the lower side, and the water-soluble protein is aggregated and aggregated over the entire surface of the treatment liquid in the heater. It overflows from the surface of the vessel and is conveyed to the separation means. In the water-soluble protein recovery apparatus of the present invention, the heater includes a tubular member formed of an insulating member and forming a heating chamber, and a plurality of annular electrodes provided in pairs with the tubular member, The processing liquid is supplied from the upstream end of the heater at a flow rate at which the processing liquid in the heating chamber becomes a turbulent state, and is integrated in a direction perpendicular to the processing liquid transport direction at the downstream end of the heater. The water-soluble protein thus produced is conveyed from the downstream end to the separation means.

  According to the present invention, the treatment liquid of animal food such as seafood is heated by generating heat by Joule heat, whereby the treatment liquid in the heater can be heated to a uniform and accurate temperature as a whole. As a result, aggregates of water-soluble proteins contained in the treatment liquid can be generated in a lump in the heater, and the aggregates do not adhere to the inner surface of the heater and are contained in the treatment liquid. Water-soluble protein can be efficiently recovered.

  Since the aggregation temperature differs depending on the molecular weight of the water-soluble protein contained in the treatment liquid, the water-soluble protein having a different molecular weight can be separated and recovered from the treatment liquid by changing the heating temperature of the treatment liquid.

  Disposing of a processing solution containing water-soluble protein was a waste liquid treatment facility, and the maintenance and management of the waste liquid processing facility was expensive. However, by collecting the water-soluble protein from the processing solution, The processing liquid can be processed by the waste liquid processing equipment having the structure, and the water-soluble protein recovered from the processing liquid can be commercialized as a supplement.

It is the schematic which shows the collection | recovery apparatus of the water-soluble protein which is one embodiment of this invention. It is a partially cutaway perspective view which expands and shows the heater shown by FIG. FIG. 3 is a cross-sectional view of FIG. 2. It is the schematic which shows the collection | recovery apparatus of the water-soluble protein which is other embodiment of this invention. It is the schematic which shows the collection | recovery apparatus of the water-soluble protein which is other embodiment of this invention. It is the schematic which shows the collection | recovery apparatus of the water-soluble protein which is other embodiment of this invention. (A) is a photograph showing the properties of the heated coagulated product when the treatment liquid is energized and heated without stirring, and (B) is a photograph showing the properties of the heated coagulum when the treatment solution is stirred and energized and heated. (C) is a photograph showing the properties of the heated coagulated product when the treatment liquid is heated in a warm bath without stirring. (A)-(C) are the photographs which show the adhesion state of the scum to the inner wall face of a heater at the time of carrying out an electrical heating of the process liquid on the conditions shown to FIG. 7 (A)-(C), respectively. (A)-(C) are temperature characteristic diagrams which show the temperature change of the process liquid during heating when the process liquid is energized and heated under the conditions shown in FIGS. 7 (A)-(C), respectively.

  As a form of recovering the water-soluble protein, there are a form in which the treatment liquid is energized and heated in a stationary or almost stationary state, and a form in which the treatment liquid is energized and heated while being conveyed and supplied to the heater.

  According to experiments, when the treatment liquid is heated in a uniform and stationary or almost stationary state as a whole, the temperature distribution of the treatment liquid becomes almost constant, and the water-soluble protein solidifies in the treatment liquid. Agglomerated as a result. Thereby, the aggregate did not adhere to the inner surface of the heater, and no scum was generated. On the other hand, when the treatment liquid was stirred by stirring or the like and energized and heated without making it stationary, aggregates separated from the solution, and a temperature difference and scum occurred.

  On the other hand, in the case of conducting heating while conveying the processing liquid, according to experiments, if the heating is performed while supplying the processing liquid into the heater at a speed at which the processing liquid is in a laminar flow state, aggregates adhere to the inner wall surface of the heater. On the other hand, it has been found that when the treatment liquid is supplied to the heater at a speed at which a turbulent state is obtained, aggregates do not adhere to the inner wall surface of the heater.

  Therefore, the treatment liquid is heated in a stationary or almost stationary state, or slowly transported and heated while maintaining the stationary structure of the solution, so that the protein is denatured without being separated from the solution, and purine-like coagulum is removed. Obtainable. When the treatment liquid is heated in a stationary state, continuous treatment can be performed by combining a plurality of batch treatment apparatuses.

  On the other hand, when heat treatment is performed while continuously transporting the treatment liquid, the treatment liquid is moved at a high speed at a flow rate at which the turbulent state is obtained, so that microscopically, although it is vigorously stirred, Homogeneous heating can be achieved even after aggregating and separating water-soluble proteins by simulating the flow while maintaining a homogeneous and static structure (with the flow velocity in the cross section crossing the flow direction kept uniform). .

  The present invention is a water-soluble protein recovery technique based on the above-described knowledge, and the present invention will be described in detail based on the drawings showing embodiments embodying the recovery technique.

  The recovery device 10 shown in FIG. 1 has three heaters 11, and in FIG. 1, the three heaters 11 are denoted by symbols a to c from the upstream side to the downstream side. Each heater 11 has a settling tank 13 in which a settling chamber 12 is formed, as shown in FIGS. The settling tank 13 has a rectangular parallelepiped shape, and includes front and rear side walls 14a and 14b, left and right side walls 14c, a top wall 14d, and a bottom wall 14e. A supply pipe 15 is attached to the top wall 14d in the vertical direction. The supply pipe 15 communicates with the sedimentation chamber 12 at the lower end, and an inlet 16 is provided at the upper end. The treatment liquid L used for washing or exposing animal food such as seafood is supplied from the inlet 16 and supplied to the settling chamber 12 in the settling tank 13. The processing liquid L supplied into the sedimentation chamber 12 is deposited temporarily in the processing liquid L in a state where the processing liquid L is temporarily stored therein, and is deposited on the bottom wall 14e. It will be.

  Next to the supply pipe 15, a heater main body 17 is attached to the top wall 14 d in the vertical direction, and the inside communicates with the sedimentation chamber 12. The heater body 17 has front and rear side walls 18a and 18b and left and right side walls 18c, and has a quadrilateral cross section. Plate-like electrodes 21 and 22 are attached to the inner surfaces of the front and rear side walls 18a and 18b of the heater main body 17 through an insulating member (not shown) so as to face each other. The electrodes 21 and 22 are formed of a conductor such as titanium or stainless steel, and are positioned higher than the top wall 14d of the settling tank 13 by a dimension H1, and the electrodes 21 and 22 in the internal space of the heater body 17 are provided. The space between is a heating chamber 23. The electrodes 21 and 22 may be attached to the inner surfaces of the left and right side walls 18c so as to face each other.

  An outlet 24 is provided at the upper end of the heater body 17 so as to protrude from the front side wall 18 a of the heater body 17. The processing liquid L in the settling chamber 12 flows into the heater body 17 from the settling chamber 12 and moves toward the upper end, overflows from the outlet 24 and flows out to the outside. The outflow speed of the processing liquid L from the outflow port 24 is set by the injection amount of the processing liquid L supplied to the injection port 16 from the outside. The cross-sectional area of the supply pipe 15 is set to be smaller than the cross-sectional area of the heater body 17, and the flow rate of the processing liquid L flowing upward in the heating chamber 23 of the heater body 17 is within the supply pipe 15. It becomes lower than the flow rate of the flowing processing liquid L.

  A power supply unit 25 is connected to the two electrodes 21 and 22 forming a pair, and a high-frequency current is supplied from the power supply unit 25 so that the two electrodes 21 and 22 have opposite polarities. As a result, while the processing liquid L moves upward in the heating chamber 23, Joule heat is generated and energized and heated.

  The heater body 17 communicates with the supply pipe 15 via the precipitation chamber 12, and the inlet 16 is provided so that the liquid level of the inlet 16 is higher than the liquid level of the outlet 24 by a dimension H2. It has been. The processing liquid L overflows from the outlet 24 due to the static pressure applied by the processing liquid L in the heating chamber 23 due to the height difference H2. By setting the height difference H2, the processing liquid L in the heating chamber 23 rises at a slow speed, and the entire cross section of the heating chamber 23 rises at a uniform speed. The volume of the precipitation chamber 12 is set to be larger than the volume of the heater body 17, and the portion of the vertical dimension H 1 between the precipitation chamber 12 and the heating chamber 23 in the heater body 17 is a rectifying chamber 26. In addition, since the processing liquid L passes through the portion of the rectifying chamber 26, the uniformity of the flow of the processing liquid L in the heating chamber 23 is further increased.

  In this manner, the processing liquid L flowing upward in the heating chamber 23 is maintained in a state where the flow velocity in the cross section of the heating chamber 23 in the direction crossing the flow direction thereof is uniformly maintained. When power is supplied from the power supply unit 25, the treatment liquid L in the heating chamber 23 generates heat due to Joule heat and is raised to the metamorphic temperature, and aggregates of water-soluble proteins are gathered on the upper end side of the heating chamber 23. It is generated as a state. Aggregates are gathered together in the heating chamber 23 to form a tofu or pudding lump so that scum does not adhere to the inner peripheral surfaces of the electrodes 21 and 22 and the heater body 17. In addition, since the temperature of the processing liquid L in the heating chamber 23 increases as it moves upward, the aggregated aggregate becomes stable due to the rising convection and is pushed upward by the pressure from below. And will move.

  As shown in FIG. 1, a filter 27 is arranged as a separating means adjacent to each heater 11, and the aggregated aggregate generated by the heater 11 is discharged from the outlet 24 together with the processing liquid L. Then, it is supplied to the filter 27 by the transport channel 28. However, the aggregate and the processing liquid L may be supplied directly from the outlet 24 to the filter 27. The recovery apparatus 10 shown in FIG. 1 has three heaters 11, and the treatment liquid L after the aggregates are recovered by the upstream filter 27 is sent to the lower heater 11 by the transport channel 29. It is supposed to be. Aggregates are captured by the respective filters 27 and the treatment liquid L containing the aggregates is separated into the aggregates and the treatment liquid L, and only the treatment liquid L is downstream by a pump 31 provided in the transport channel 29. It is supplied to the heater 11.

  Water-soluble proteins that become aggregates by heat denaturation have different heating temperatures depending on their molecular weights. As shown in FIG. 1, in the recovery device 10 having three heaters 11, the upstream side of the processing liquid L after the aggregates are recovered by the upstream filter 27 is heated via the transport channel 29. The heaters 11b and 11c can be sequentially sent from the heater 11a. Therefore, by setting the temperatures of the respective heating chambers 23 to different temperatures, the water-soluble protein aggregates captured by the respective filters 27 can have a molecular weight of each other without causing scum to adhere to the inner surface of the heater. Can be separated into different ones. For example, when the treatment liquid L is heated to 60 ° C. by the first-stage heater 11 a shown in FIG. 1, water-soluble proteins that aggregate at this temperature can be recovered from the treatment liquid L. When the treatment liquid L from which the aggregates have been removed is heated to 75 ° C. by the second stage heater 11b, the water-soluble protein that aggregates at this temperature can be recovered from the treatment liquid L. Furthermore, when the treatment liquid L from which the aggregates have been removed is heated to 90 ° C. by the third stage heater 11c, the water-soluble protein that aggregates at this temperature can be recovered from the treatment liquid L. Thus, to separate and collect the aggregate, the heating temperature is increased from the upstream side toward the downstream side heater.

  Water-soluble proteins captured by each filter 27 are periodically taken out from the filter 27 and sent to the next step such as a drying step.

  The recovery device 10 shown in FIG. 1 connects three heaters 11 in series so that each heater 11 heats the processing liquid L to a different temperature. When the treatment liquid L is heated to 90 ° C. at once, an aggregate containing all the water-soluble proteins that are aggregated at the temperature up to that point is generated. The recovery apparatus 10 that performs such a recovery process is configured to have one heater 11.

  In the recovery device 10 shown in FIG. 1, when the filter 27 is periodically removed, the heater 11 is removed from the transport channels 28 and 29, and the recovery process is stopped. In order to lengthen the continuous operation time of 11, it is necessary to enlarge the filter 27. On the other hand, by connecting the two filters 27 in parallel and alternately operating the two filters 27 that make a pair, the recovery process can be continuously performed even if the filter 27 is downsized. .

  FIG. 4 is a schematic view showing a recovery device according to another embodiment of the present invention. This recovery device has a configuration in which two filters 27a and 27b are connected in parallel. Is the same as that described above. As shown in FIG. 4, the conveyance channel 28 is provided with branch portions 28 a and 28 b via a channel switching valve 32, and the outlets 29 a and 29 b connected to the lower ends of the respective filters 27 a and 27 b. 29 b is connected to the transport channel 29 via a channel switching valve 33. Therefore, when one of the two filters 27a and 27b is taken out of the aggregate from the inside by operating the respective flow path switching valves 32 and 33, it is removed from the transport flow path 29 and the other filter is removed. Then, the processing liquid L is supplied to collect the aggregate. Thus, by alternately operating the two filters 27a and 27b, the processing liquid L can be continuously processed even if the respective filters 27a and 27b are downsized.

  FIG. 5 is a schematic view showing a recovery apparatus 10 according to another embodiment of the present invention. The recovery device 10 has two heaters 11d and 11e, and each heater 11d and 11e has a rectangular parallelepiped or cube shape. In the heaters 11d and 11e, two electrodes 21 and 22 are arranged so as to face each other in the same manner as the above-described heater, and a fixed amount of the processing liquid L is accommodated in the internal heating chamber 23. It is like that. Accordingly, in the recovery apparatus 10, the processing liquid L is heated and energized in a stationary state, not in a flowing state. Even when the process liquid L is not flowed into the heating chamber 23 and is heated while energized in a stationary state, aggregates are generated in a lump without scum adhering to the inner surface of the heater.

  In order to supply the processing liquid L directly to the two heaters 11d and 11e, branch channels 34a and 34b are connected to the common transport channel 34 via a channel switching valve 35. Furthermore, the outlets 36a and 36b provided on the bottom walls of the heaters 11d and 11e are connected to a common transport channel 36 via a channel switching valve 37, and the filter 27 is provided in the common transport channel 36. It is connected. Therefore, when the operation of generating aggregates by one heater and the operation of supplying the processing liquid L to the filter after the generation of aggregates are performed, the processing liquid L is supplied to the other heaters. By doing so, it is possible to continuously recover the water-soluble protein from the treatment liquid L. In the case shown in FIG. 5, the processing liquid L is supplied to one filter from two heaters, but in this embodiment as well, as shown in FIG. 4, two filters are paired in parallel. You may make it arrange | position.

  FIG. 6 is a schematic view showing a water-soluble protein recovery device according to another embodiment of the present invention, and this recovery device 10 has two heaters 11 denoted by symbols f and g. .

  Each heater 11 includes a tubular member 42 having a circular cross section in which a heating chamber 41 for guiding the processing liquid L is formed. The tubular member 42 includes a plurality of ring-shaped electrodes 43 and a plurality of electrodes disposed between them. The cylindrical body 44 is configured. Each electrode 43 is formed of a conductor such as titanium or stainless steel like the above-described electrodes 21 and 22, and each cylindrical body 44 is formed of an insulating material such as resin. Joint portions 45 and 46 on the inflow side and the outflow side are attached to both ends of the tubular member 42. A power supply unit 25 is connected to each electrode 43 via a cable, and a high-frequency current is supplied from the power supply unit 25 so that the pair of electrodes 43 adjacent to each other in the direction in which the processing liquid L flows have opposite polarities. Supplied. The number of electrodes 43 provided in each heater 11 shown in FIG. 6 is arbitrarily set according to the heating temperature and the like.

  A hopper 48 is connected to the joint portion 45 on the inflow side of the upstream heater 11f via a transport channel 47, and the processing liquid L introduced into the hopper 48 is supplied to the transport channel 47 with the heater 11f. And the pump 31 for supplying to the heater 11g is provided in the downstream. A filter 27 is connected to the outflow side joint portion 46 of the heater 11 f via a conveyance channel 28, and the discharge port of the filter 27 is connected to the inflow side joint portion of the downstream heater 11 g through the conveyance channel 29. 45. Further, a filter 27 is connected to the joint portion 46 on the outflow side of the heater 11g through the conveyance channel 28. Although the collection | recovery apparatus 10 shown in FIG. 6 has the two heaters 11, the collection | recovery apparatus 10 can be set to a various form by selecting the number of heaters variously.

  As shown in FIG. 6, in the recovery apparatus 10 having the heater 11 using the ring-shaped electrode 43, the treatment liquid L is placed in the turbulent flow state in the heating chamber 41 of the tubular member 42. Will flow. When the processing liquid L is flowed into the heating chamber 41 at a flow rate at which the flow becomes a laminar flow, the flow rate at the center portion in the radial direction of the heating chamber 41 is the highest, and the flow rate at the inner peripheral surface side of the tubular member 42 is the lowest. In addition, the flow rate of the processing liquid L differs depending on the position in the radial direction. Thus, when the flow velocity of the inner peripheral surface of the tubular member 42 is lower than the central portion, aggregates of water-soluble proteins are generated from the treatment liquid L on the inner peripheral surface side, and aggregates are formed on the inner peripheral surface. Is inevitable.

  On the other hand, when the processing liquid L is supplied into the heating chamber 41 at a flow rate at which the processing liquid L becomes a turbulent flow, the flow rate in the cross section of the method crossing the heating chamber 41 becomes uniform as a whole. As a result, the treatment liquid L has a uniform heating temperature in each cross section, and the aggregates of water-soluble proteins are separated from the treatment liquid L flowing through the heating chamber 41, and the aggregates are gathered together. Is done. Since the aggregates are gathered together in the heating chamber 23 and become a tofu-like or pudding-like lump, the aggregates do not adhere to the inner peripheral surface of the tubular member 42 as scum.

  Agglomerates produced by the upstream heater 11f and agglomerated and the treatment liquid L are supplied to the filter 27 in a tocorotene manner, and the aggregates are separated and recovered. The treatment liquid L after the aggregates are separated by the upstream filter 27 is supplied to the downstream heater 11g and heated to a temperature higher than that of the upstream heater 11f, and the aggregates are downstream of the filter. 27 is separated and recovered. As shown in FIG. 6, in the recovery device 10 having two heaters 11, for example, the treatment liquid L is heated to about 60 ° C. by the first stage heater 11 f to aggregate in the water-soluble protein chamber. Can be removed by the first-stage filter 27, and then the treatment liquid L can be heated to 90 ° C. by the second-stage heater 11g to separate the aggregates.

  Also in the recovery apparatus 10 having the heater 11 made of such a tubular member 42, the number of heaters can be set to an arbitrary number. Moreover, two filters may be arranged in parallel as shown in FIG. 4 in order to separate the agglomerates from the treatment liquid L that has flowed out of the respective heaters 11. In each of the above-described embodiments, a filter is used as the separation unit, but a centrifuge may be used as the separation unit.

[Example 1]
A liquid obtained by adding 1 L of 0.05M phosphate buffer (pH 7.0) to 200 g of bonito blood, as a treatment solution, was stirred four times for 10 seconds with Hiscotron, and then centrifuged (12,000 G). Over 15 minutes, the supernatant was recovered to obtain an aqueous protein solution. NaCl was added to this so that it might become 0.45M, and it was set as the solution as a process liquid. As shown in FIG. 5, 300 mL of this solution was supplied without flowing the treatment liquid into a heater in which plate-like electrodes were arranged, and water-soluble protein was recovered by the following three methods.

  In the first method, the distance between the electrodes was set to 10 cm, the load voltage was set to 100 V, and the solution was heated while being left without being stirred. In the second method, the distance between the electrodes and the load voltage were the same as those in the first method, while the solution was heated while being stirred. Further, in the third method, the solution was placed in a 500 mL beaker and heated in a 90 ° C. water bath. In each method, the temperature of the solution accompanying heating was measured, and the properties of the heated coagulated product and the state of scum adhering to the inner wall surface of the heater and the electrode plate were examined.

  FIG. 7 is a photograph showing the properties of the heated coagulated product when energized and heated by each of the methods described above.

  When electrified and heated by the first method, as shown in FIG. 7A, the heated coagulated product became uniform in a pudding shape, whereas when electrified and heated by the second method, As shown in FIG. 7B and when the current was heated by the third method, the aggregates were dispersed in the form of particles as shown in FIG. 7C.

  FIG. 8 is a photograph showing the state of scum adhesion to the inner wall surface of the heater when energized and heated by each of the methods described above.

  As shown in FIG. 8 (A), the state of the wall surface after collecting the aggregate is cleanly separated because the aggregate is solidified in a pudding shape. Adhesion was not seen. On the other hand, in the second method, as shown in FIG. 8 (B), the coagulum separates from the solution into particles, and the aggregates grow with the fixed particles as nuclei. Many were attached. Similarly in the third method, as shown in FIG. 8C, a lot of scum adhered to the wall surface.

  FIG. 9 is a temperature characteristic diagram showing a change in the solution temperature during heating when energization heating is performed by each of the methods described above. 9A and 9B, the solid line indicates the temperature of the electrode surface, and the alternate long and short dash line indicates the temperature at the center of the solution. In FIG. 9C, the temperature of the middle layer portion of the solution center is shown, the broken line shows the temperature of the surface layer portion of the solution center, the two-dot chain line shows the temperature of the bottom layer portion on the wall side of the solution, and the solid line is the outside Indicates the temperature of the water bath for heating.

  In the first method, as shown in FIG. 9A, there was no difference in temperature between the electrode surface and the center of the solution, and the electrode surface and the solution rose in the same manner. On the other hand, in the second method, as shown in FIG. 9C, the temperature of the electrode surface and the central part of the solution is the same as in the first method until the temperature at which protein begins to coagulate (58 ° C.). However, when the protein started to coagulate at 58 ° C. or higher, the coagulated protein was separated from the solution, so that the uniformity was lost and a difference in temperature increase was observed. Since the third method is external heating, the temperature rise is fast in the outside where heat is directly transmitted, but the temperature rise is very slow in the slow heat transfer, and the temperature difference is large depending on the part.

[Example 2]
By heating the fish meat bleaching solution as a processing solution, water-soluble protein was recovered from the solution. As the heater 11, a plate-like electrode disposed in the same manner as in the above-described embodiment is used, and the electrode is energized in a state in which 500 mL of solution is accommodated without flowing the treatment liquid into the heating chamber. Was heated. When heated until the temperature of the solution reached 50 ° C., aggregates were generated on the liquid surface side without adhering to the inner peripheral surface of the heater. The water-soluble protein thus heat-aggregated was collected by filtration through a filter. The new solution was heated to 55 ° C. with a similar heater, and the aggregated water-soluble protein was collected by filtration through a filter. This operation was repeated in increments of 5 ° C up to 90 ° C.

  The total protein and aggregated water-soluble protein in each solution were measured by the Burette method, and the ratio of the heat-aggregated protein to the total protein was determined as the aggregation rate of the aggregated protein. As a result, when the heating temperature was 60 ° C., 75 ° C., and 90 ° C., a difference was observed in the heating aggregation rate. Therefore, the molecular weight of the aggregated protein at these three temperatures was measured by SDS-PAGE electrophoresis. .

  In the electrophoresis pattern, a protein having a molecular weight of 29 KDa was observed at 60 ° C., and no protein having a molecular weight higher than that was present. On the other hand, at 75 ° C., a protein having a molecular weight of around 36.5 KDa was observed in addition to 29 KDa. Furthermore, at 90 ° C., proteins having molecular weights near 55 KDa and 97 KDa were present in addition to 29 KDa and 36.5 KDa. Thus, when the solution is Joule-heated, the water-soluble protein aggregates having different molecular weights can be fractionated and recovered from the treatment liquid L without depending on the heating temperature without adhering the water-soluble protein aggregates to the heater. did it.

  Accordingly, when three heaters 11 are connected in series as shown in FIG. 1 and the treatment liquid L is heated to 60 ° C. by the first-stage heater 11a, a water-soluble protein having a molecular weight of 29 KDa is treated. It can be separated and recovered from the liquid L. When the solution after the water-soluble protein having the molecular weight is separated by the filter 27 is heated to 75 ° C. by the second stage heater 11b, the water-soluble protein having the molecular weight of 36.5 KDa can be separated and recovered from the solution. . Subsequently, when the remaining solution is heated to 90 ° C. by the third stage heater 11c, water-soluble proteins having molecular weights of 55 KDa and 97 KDa can be separated and recovered from the processing liquid L.

[Example 3]
As a solution, a liquid in which 500 mL of 0.05 M phosphate buffer (pH 7.0) was added to 100 g of bonito blood was prepared, and this was stirred four times for 10 seconds with Hiscotron, and then centrifuged (12,000 G). Over 15 minutes, the supernatant was recovered, and NaCl was added to this to a concentration of 0.45 M to obtain a treatment solution L.

  This solution was heated with the same heater as in Example 1 described above until the liquid temperature reached 55 ° C., and then the heat-aggregated protein was recovered by centrifugation. This condensate is designated as 55 ° C. heat-aggregated protein.

  Next, 500 mL of another new bonito blood mixture exposure solution was supplied to the same heater and heated until the solution temperature reached 64 ° C., and then the heat-aggregated protein was collected by a centrifuge. Further, the remaining treatment liquid L after the heat-aggregated protein is recovered is heated with a similar heater until the liquid temperature reaches 90 ° C., and is maintained for 30 minutes, and then the heat-aggregated protein is centrifuged. Recovered with a separator. This is designated as 65-90 ° C. heat-aggregated protein.

  The molecular weights of the two kinds of proteins recovered in this way were measured by SDS-PAGE, and the concentration of each band was calculated by the image analysis software of Scion. Further, the iron content was measured by an atomic absorption method. As a result, the 55 ° C. heat-aggregated protein is composed of proteins with molecular weights around 97 KDa (concentration 16.9%), 40 KDa (concentration 40.9%) and 16 KDa (concentration 17.7%), and contains iron. The amount was 4.8 mg / 100 g. On the other hand, the 65-90 ° C. heat-condensed protein is mainly composed of a protein having a molecular weight in the vicinity of 16 KDa (concentration 66.9%), the iron content is 16.6 mg / 100 g, and the main component of this protein is myoglobin. it is conceivable that.

  Therefore, by using a recovery device in which the heaters are arranged in two stages in series, a relatively high protein group and a relatively low molecular weight protein mainly composed of myoglobin are separated and recovered from the bleached bonito blood mixture. I was able to.

  The present invention is not limited to the above-described embodiment, and various modifications can be made without departing from the scope of the invention. The shape of the heater is not limited to the above-described form as long as the treatment liquid in the heating chamber can be uniformly heated as a whole.

DESCRIPTION OF SYMBOLS 10 Recovery device 11 Heater 12 Precipitation chamber 13 Precipitation tank 17 Heater main body 23 Heating chamber 25 Power supply unit 26 Rectification chamber 27 Filter 41 Heating chamber 42 Tubular member 43 Electrode

Claims (8)

A method for recovering water-soluble protein, wherein the water-soluble protein is separated and recovered from a processing solution of animal food such as seafood,
The processing liquid supplied into the heating chamber in the heater is placed in a pair in the heating chamber under a state where the processing liquid is kept stationary or the flow velocity in the cross section in the direction crossing the flow direction is kept uniform. A heating step of energizing the treatment liquid through a plurality of electrodes and heating the treatment liquid to a protein denaturation temperature;
A separation step of separating the water-soluble protein aggregates generated by the heat generation of the treatment liquid in the heating step from the treatment liquid by a separation means,
A method for recovering a water-soluble protein, comprising aggregating and recovering the water-soluble protein from the treatment liquid.   The water-soluble protein recovery method according to claim 1, wherein the treatment liquid is sequentially conveyed from the heater having a low heating temperature to the heater having a high heating temperature with respect to the plurality of heaters having different heating temperatures. In addition, the water-soluble protein that has become aggregates in each of the heaters is separated by a separation means, and a plurality of types of water-soluble proteins having different molecular weights according to the denaturation temperature are separated and recovered from the treatment liquid. A method for recovering a water-soluble protein.   The method for recovering a water-soluble protein according to claim 1 or 2, wherein a treatment liquid is supplied into the heater from the lower side, and the water is dissolved in an aggregate on the entire surface of the treatment liquid in the heater. A method for recovering a water-soluble protein, wherein the protein is overflowed from the surface of the heater and conveyed to the separation means.   The water-soluble protein recovery method according to claim 1 or 2, wherein the heater includes a tubular member made of an insulating member and forming the heating chamber, and a plurality of annular electrodes provided in pairs with the tubular member. The processing liquid is supplied from the upstream end of the heater at a flow rate at which the processing liquid in the heating chamber is in a turbulent state, and is integrated in a direction perpendicular to the transport direction of the processing liquid at the downstream end of the heater. A method for recovering a water-soluble protein, comprising transporting the aggregated water-soluble protein from the downstream end to the separation means. A water-soluble protein recovery device for separating and recovering a water-soluble protein from a processing solution for animal food such as seafood,
A heater having a heating chamber in which a plurality of electrodes arranged in pairs are arranged and the processing liquid is kept stationary or the flow velocity in the cross section in the direction crossing the flow direction is uniformly maintained;
A power supply unit that supplies power to the treatment liquid through the electrodes, heats the treatment liquid, and heats the water-soluble protein contained in the treatment liquid to a denaturing temperature;
Separation means for separating the water-soluble protein aggregates generated by the heat generation of the treatment liquid in the heater from the treatment liquid;
An apparatus for recovering water-soluble protein, comprising aggregating and recovering water-soluble protein from a treatment liquid.   The water-soluble protein recovery apparatus according to claim 5, wherein the low-temperature side heater is configured to aggregate the water-soluble protein in the processing liquid, and the processing liquid is heated at a temperature higher than the low-temperature side heater. A plurality of heaters each having a heating temperature different from each other, each having a high-temperature side heater that aggregates a water-soluble protein having a higher denaturation temperature than the water-soluble protein aggregate produced by the heater A plurality of separation means for separating water-soluble protein aggregates from the processing solution transported from the vessel, and separating and processing multiple types of water-soluble proteins having different molecular weights depending on the denaturation temperature An apparatus for recovering a water-soluble protein, which is recovered from a liquid.   The water-soluble protein recovery apparatus according to claim 5 or 6, wherein the treatment liquid is supplied into the heater from the lower side, and the water is soluble in agglomerated integrally with the entire surface of the treatment liquid in the heater. An apparatus for recovering a water-soluble protein, wherein the protein overflows from the surface of the heater and is conveyed to the separation means.   The water-soluble protein recovery apparatus according to claim 5 or 6, wherein the heater includes a tubular member made of an insulating member and forming a heating chamber, and a plurality of annular electrodes provided in pairs with the tubular member. And supplying the processing liquid from the upstream end of the heater at a flow rate at which the processing liquid in the heating chamber becomes a turbulent state, and is integrated in a direction perpendicular to the conveying direction of the processing liquid at the downstream end of the heater. The water-soluble protein collecting apparatus is characterized in that the aggregated water-soluble protein is conveyed from the downstream end to the separation means.