CN114075477A

CN114075477A - Device and process for simultaneously recovering water-soluble protein and colloid in refining process of edible tallow fat

Info

Publication number: CN114075477A
Application number: CN202010841348.9A
Authority: CN
Inventors: 胡洪舟
Original assignee: Individual
Current assignee: Individual
Priority date: 2020-08-20
Filing date: 2020-08-20
Publication date: 2022-02-22

Abstract

The invention belongs to the technical field of animal fat refining, and discloses a device for simultaneously recovering water-soluble protein and colloid in an edible tallow refining process, which comprises a raw material pretreatment device, a mixture separation device, a solid phase object and oil phase object treatment device and a water phase object treatment device; the raw material pretreatment device comprises a first-stage feeding conveyor, a chopper, a second-stage feeding conveyor, a preheating kettle and a hot water tank connected with the preheating kettle; the mixture separation device comprises a mixture delivery pump, an extrusion filter, a liquid phase delivery pump, a solid phase delivery pump, a settling kettle, a hot oil circulating pump, liquid-solid separation equipment and a mixed phase delivery pump; the solid phase and oil phase processing device comprises a secondary decocting kettle, oil/residue liquid-solid separation equipment, an oil press and a filter; the water phase substance treatment device comprises a protein separation tank, a composite negative pressure evaporator, a delivery pump and a spray dryer. The invention can prepare the edible beef tallow which is used in the chafing dish industry, does not have muddy soup, does not bubble and has the inherent strong flavor of the edible beef tallow.

Description

Device and process for simultaneously recovering water-soluble protein and colloid in refining process of edible tallow fat

Technical Field

The invention belongs to the technical field of animal fat refining, and relates to a device and a process for simultaneously recovering water-soluble protein and colloid in an edible tallow refining process.

Background

The beef tallow is boiled by equipment to become edible beef tallow, and then is widely used for making hotpot condiment, dairy products, shortening, baked products, essence and spice, seasoning sauce bags and the like, particularly on the hotpot condiment, the edible beef tallow can make the hotpot spicy but not dry, and is mild but not fired, so that the hotpot soup is red and bright, the taste is thick and fragrant, and the taste is mellow but not greasy.

At present, the general beef tallow oil refining basically adopts a dry process. On the premise of a dry refining process, different manufacturers adopt different refining methods, and the general flow is as follows: after animal fat is cut up, the animal fat is melted in vacuum at high temperature, the water content of the animal fat is evaporated, the oil residue is golden, then oil/residue separation is carried out, liquid oil is pumped to a finished product tank after being filtered, solid matters such as the oil residue are squeezed out by pressing to recover residual oil, and the oil residue is sold after being crushed and packaged. Specifically, refer to the invention patent with application publication No. CN 108559621 a (an environmental-friendly extraction method of animal fat). The disadvantages of this process are: a. after being cut into pieces, the animal fat is directly conveyed into a vacuum cooking kettle to be heated and heated, and is dehydrated under negative pressure, and because of the limitation of the heat exchange area of the vacuum cooking kettle, the evaporation efficiency of water is extremely low, which usually takes 2 to 4 hours, and wastes time and energy; the existing vacuum cooking kettle is not fully stirred, the phenomena of large blocks and burnt skin are generated, the evaporation of water in the internal water-containing material is difficult, the energy consumption in the cooking process is high, the acid value of the cooked oil is high, the color is deep, and various physical and chemical indexes are unqualified. b. Animal growth cycle is affected by nutrition, environment and animal age to cause different fat and lean, so that the content difference of water, oil and connective tissue in fat is large, water content increases along with decrease of oil content, water content of high-quality fat is about 15-20%, water content of fat with poor quality can reach 50-60%, animal fat is cut up and then put into a cooking kettle, and along with temperature rise, the fat tissue is gradually decomposed into three-phase substances which are respectively liquid-phase water and oil and solid-phase connective tissue. The nature of connective tissue is protein, and with the increase of temperature and water, hydrophilic protein is gradually decomposed, transited from large molecules to small molecules and dissolved in water. The longer the temperature rise time of the solid connective tissue in the vacuum cooking kettle is, the more the solid connective tissue is lost, the water in the kettle is changed from clear to turbid, and at the moment, the water-soluble protein content in the water phase of the vacuum cooking kettle can reach 8-10 percent. The mixture in the boiling kettle is gradually evaporated under the action of high temperature, three phases are changed into two phases, and the two phases are separated, and the pressed protein powder is taken out from the solid-phase oil residue phase. However, water-soluble proteins remain in the oil as the water evaporates, resulting in the following: 1) the hydrolyzed protein in the oil can be decomposed and deteriorated in the later production and use, so that the taste of the oil product is deteriorated, the acid value and the color of the oil product are increased, and the quality of the oil product is reduced. 2) Water-soluble protein in the oil can produce the coking gelatinization phenomenon under the high temperature effect of vacuum boiling kettle, and on the one hand, the gelatinization of protein can make the oil produce the bitter, and the taste becomes poor, and is turbid, and the color and luster aggravates, and on the other hand, the protein after the gelatinization still can release harmful substance benzopyrene, and benzopyrene is high carcinogenic, causes the injury to people's health. c. Because water and hydrophilic water-soluble protein and colloid contained in the beef tallow are not separated in the refining process, the degummed beef tallow is obtained by water washing degumming, drying and filtering after the cooking, but the inherent aroma flavor and taste of the beef tallow are seriously influenced by the water washing degumming, in addition, because the beef tallow still contains water-soluble protein, the protein gelatinization can leave a black pot ring on a hot pot after long-time boiling when the beef tallow is used as oil for hot pot bottom materials, and tableware is not easy to clean.

Therefore, aiming at the technical problems that the boiling time is long, the energy consumption is too high, the water-soluble protein and the colloid cannot be recovered in the boiling process in the prior art, so that the waste is caused and the quality of the beef tallow is influenced, a novel device and a novel process for simultaneously recovering the water-soluble protein and the colloid in the edible beef tallow fat refining process are needed to be provided.

Disclosure of Invention

The invention aims to provide a device and a process for simultaneously recovering water-soluble protein and colloid in the refining process of edible beef fat, wherein preheating and separation are carried out firstly and then boiling is carried out for the second time, so that the boiling time is shortened, the heat energy consumption and the power load of the second boiling are reduced, and the edible beef fat which is used in the hot pot industry and has no turbid soup, no bubbling and the inherent aroma and flavor of the edible beef fat can be prepared.

In order to achieve the purpose, the invention adopts the following technical scheme:

the invention provides a device for simultaneously recovering water-soluble protein and colloid in the refining process of edible tallow fat, which comprises a raw material pretreatment device, a mixture separation device, a solid phase object and oil phase object treatment device and a water phase object treatment device;

the raw material pretreatment device comprises a first-stage feeding conveyor, a chopper, a second-stage feeding conveyor, a preheating kettle and a hot water tank connected with the preheating kettle;

the mixture separation device comprises a mixture delivery pump connected with the outlet of the preheating kettle, an extrusion filter, a liquid phase delivery pump, a solid phase delivery pump, a settling kettle connected with the liquid phase delivery pump, a hot oil circulating pump connected with the settling kettle, liquid-solid separation equipment and a mixed phase delivery pump connected with the solid phase outlet and the oil phase outlet of the liquid-solid separation equipment;

the solid-phase substance and oil-phase substance treatment device comprises a secondary boiling kettle, oil/residue liquid-solid separation equipment, an oil press and a filter, wherein the secondary boiling kettle is connected with a hot oil circulating pump, a solid-phase conveying pump and a mixed-phase conveying pump;

the water phase substance treatment device comprises a protein separation tank connected with a water phase outlet of the liquid-solid separation equipment, a composite negative pressure evaporator connected with the protein separation tank, a delivery pump and a spray dryer.

Further, the extrusion filter comprises a cylinder body, the cylinder body penetrates through a spiral propelling shaft through the inside of a bearing seat, and spiral blades with gradually reduced screw pitches are arranged on the spiral propelling shaft; the cylinder body is divided into an accelerating propulsion section, a solid extrusion section, an expansion extrusion section, a conveying section and a discharging section along the solid propulsion direction, and the cylinder body is divided into a liquid extrusion section and a liquid shielding section along the liquid propulsion direction; a feed inlet is arranged above the cylinder body at the starting end of the accelerating propulsion section; a solid outlet is arranged below the cylinder body positioned at the tail end of the liquid phase shielding section; a liquid phase material collecting tank is arranged below the cylinder body positioned at the liquid phase material extrusion section, and a liquid phase material outlet is arranged below the cylinder body positioned at the tail end of the liquid phase material extrusion section; the spiral propelling shaft is connected with an output shaft of the speed reducing motor through a coupler.

Further, a solid material discharging and stirring assembly is arranged at the tail end of the spiral propelling shaft corresponding to the solid material outlet, the solid material discharging and stirring assembly comprises a solid material discharging and stirring plate and a fixed ring, and the solid material discharging and stirring plate is fixed on the spiral propelling shaft through the fixed ring.

Furthermore, be located the liquid phase thing and extrude the section the barrel outside is provided with the guard shield, the feed inlet position is higher than the guard shield, and the position that feed inlet below and guard shield suited sets up the splashproof plate washer of round platform shape, the diameter of splashproof plate washer is greater than the diameter of feed inlet.

Further, the preheating kettle and the secondary decocting kettle both adopt vacuum horizontal decocting kettles, each vacuum horizontal decocting kettle comprises a kettle body, a stirring main shaft penetrates through the kettle body through a bearing seat, a plurality of groups of stirring assemblies are arranged on the stirring main shaft, and each group of stirring assemblies are distributed on two sides of the stirring main shaft in a cross shape; the side wall of the driving end of the kettle body is provided with a material inlet and a material outlet, and the lower half part of the kettle body is provided with a semicircular heat-conducting oil coil pipe with two inlets and two outlets arranged in an S shape; the top of the kettle body is provided with a gas collector, the gas collector is provided with a vacuum pressure relief opening, a vacuum air exhaust opening and an air exhaust opening, and the top of the kettle body is fixed with a feeding hopper through a preheating feeding valve.

Further, every group the stirring subassembly includes support, stirring rake and scraper, the support is "ten" font and fixes on the stirring main shaft through the staple bolt, the stirring rake is fixed in the support both sides, and the support end is fixed with the scraper, scraper tool bit portion is close to the internal wall of cauldron.

Further, the device also comprises an odor treatment device and a heat energy recycling system.

The invention also provides a process for simultaneously recovering water-soluble protein and colloid in the refining process of edible tallow fat by using the device, which comprises the following steps:

a: pretreatment of raw materials

The animal fat frozen raw material is unpacked, sent into a chopper through a first-grade feeding conveyor to be cut into strip-shaped blocks with the size of 20-40mm, sent into a preheating kettle through a second-grade feeding conveyor to be preheated to the temperature of 80-100 ℃, and added with hot water with the temperature of 80-90 ℃ into the preheating kettle;

b: separation of the mixture

Conveying the preheated animal fat to an extrusion filter through a mixture conveying pump for solid-liquid two-phase separation, temporarily storing the separated liquid phase mixture, conveying the temporarily stored liquid phase mixture to a settling kettle through a liquid phase conveying pump for settling for 30-60min, and conveying the settled middle layer emulsified oil phase and the lower layer water phase containing hydrophilic water-soluble protein and colloid to liquid-solid separation equipment for liquid-solid three-phase separation;

c: solid phase and oil phase treatment

C, temporarily storing the solid-phase substances separated by the extrusion filter in the step B, and then conveying the solid-phase substances to a secondary decocting kettle by a solid-phase conveying pump for secondary heating and decocting; the residual upper oil phase in the settling kettle is sent to a heat exchanger through a hot oil circulating pump to be heated to 120-140 ℃ through circulating heat exchange, and the heated oil phase is sent to a secondary boiling kettle through the hot oil circulating pump to be boiled for the second time; temporarily storing the oil phase and the solid phase after the liquid, liquid and solid phases are separated in the step B, and then conveying the oil phase and the solid phase to a secondary decocting kettle by a mixed phase conveying pump for secondary decocting; after the secondary cooking is finished, sending the mixture to oil/residue liquid-solid separation equipment for oil/residue liquid-solid separation;

d: treatment of aqueous phase

B, temporarily storing the water phase after liquid-solid three-phase separation in a protein separation tank, adding a protein separating agent into the protein separation tank to enable protein and colloid to be agglomerated, feeding the agglomerated and polymerized protein thick slurry into a composite negative pressure evaporator, removing water through three-stage evaporation to form high-solid-content protein thick slurry, and conveying the protein thick slurry to a spray dryer through a conveying pump for spray drying to obtain protein powder;

e: oil residue and product oil

C, sending the solid phase subjected to oil/residue liquid-solid separation in the step C to an oil press to press residual oil to obtain low-fat protein oil residue; and removing fine oil residue from the liquid phase subjected to liquid-solid separation by using a filter to obtain the finished oil.

Further, the peculiar smell discharged from the secondary boiling kettle is treated by an odor treatment device and then discharged.

And D, further, the liquid phase subjected to oil/slag liquid-solid separation in the step E is pumped to be used as heating media of a preheating kettle and a secondary boiling kettle through a hot oil pump, and heat is recovered.

Compared with the prior art, the invention has the beneficial effects that:

according to the invention, materials are preheated and heated and hot water is added, so that on one hand, the basic temperature of subsequent material treatment is improved, and the pressurized extrusion operation of an extrusion filter is facilitated, and on the other hand, in the preheating and heating process, the hydrophilic protein and colloid contained in the hot water and the butter fat are fully dissolved and absorbed, and the hydrophilic protein and colloid contained in the oil phase substance are removed by a back-stage separation process; after the first solid-liquid separation, the liquid phase mixture is naturally settled, and the settled solution is in three forms: the upper oil layer is light yellow, the middle emulsified oil layer is milky white, the lower water-soluble protein dissolved water layer is tooth yellow, the interlayer definition is obvious through observation of a glass sight glass, the middle emulsified oil phase and the lower water phase containing hydrophilic water-soluble protein and colloid are subjected to secondary liquid, liquid and solid three-phase separation, and the lower water phase is not directly discharged as sewage, so that the sewage treatment pressure is reduced, the content of emulsified oil in materials entering a secondary boiling kettle is reduced, the phenomenon that the quality of oil products is influenced by the emulsified oil mixed into the finished oil is avoided, and the shelf life is prolonged; after natural sedimentation, the residual upper oil phase in the sedimentation kettle is conveyed to a heat exchanger through a hot oil circulating pump to exchange heat at a high speed and rise temperature, and then enters a secondary boiling kettle, so that the basic temperature of low-temperature materials in the boiling kettle is improved, the heat exchange efficiency is improved, as the low-temperature solid materials contain little moisture and high-temperature liquid oil is injected, the low-temperature solid materials and the high-temperature liquid oil exchange heat efficiently, and protein is dissolved in water but not dissolved in oil, and the temperature is continuously raised to refine to obtain the edible beef tallow which is used in the hot pot industry and has no turbid soup, no bubbles and the inherent strong flavor of the edible beef tallow; solid, secondary liquid, solid phase and oil phase after the separation of liquid and solid phases for the first time are sent to a secondary boiling kettle for boiling, so that the weight and moisture of materials entering the secondary boiling kettle are reduced, the boiling time is shortened, the heat energy consumption and the power load of the secondary boiling are reduced, meanwhile, because the materials for the secondary boiling are the oil phase after dehydration, the phenomenon of coking and gelatinization of water-soluble protein in a high-temperature environment is avoided, the release of toxic substance benzopyrene is reduced, the food safety is ensured, and the device can be used for producing food-grade oil; the solid matter of the animal fat after being dissolved is connective tissue, the connective tissue is composed of protein, the protein is soluble in water but not soluble in grease, and the material of the secondary cooking of the invention is dehydrated oil phase, which can block the hydrolysis of the connective tissue, namely block the decomposition of hydrophilic protein, reduce the loss of water-soluble protein and improve the nitrogen content of the connective tissue; adding a protein separating agent into a water phase after liquid, liquid and solid three-phase separation in a stirring process of a water-soluble protein separating tank, agglomerating and polymerizing protein and colloid contained in the water phase, separating clear water and agglomerated and polymerized protein thick slurry, directly discharging the clear water, efficiently evaporating water by a protein thick slurry transposition composite negative pressure evaporator, and recovering protein powder with the nitrogen content of more than 13% and the crude protein content of more than 81%, so that emulsified oil and hydrophilic water-soluble protein and colloid in the water phase are recovered as much as possible.

The invention provides an extrusion filter with a novel structure, wherein the screw pitch of a helical blade is gradually reduced along the advancing process of materials, namely the screw pitches of sections A to E are gradually reduced, and the pressure borne by the materials is increased due to the fact that the space is reduced when the materials enter the next section. The solid containing the liquid phase substance passes through an expansion extrusion section (section C) in the high-speed propelling process, the material is expanded and extruded to extrude most of the liquid phase substance in the solid due to the sudden diameter change of a cone of the section C, and the solid is spirally propelled to a discharge section E through a conveying section (section D) and discharged from a solid outlet; liquid phase matter extruded from the solid matter converges into the cylinder, and a liquid phase matter collecting tank is arranged below the cylinder and is discharged from a liquid phase matter outlet. Therefore, the solid substance which is subjected to the extrusion separation of water only contains a little part of water when entering the subsequent secondary cooking process, so that the energy consumption of evaporating water during cooking can be greatly reduced, the production cost is reduced, the cooking time can be reduced, and the production efficiency is improved.

The invention provides a vacuum cooking kettle with a novel structure, wherein stirring components are distributed on two sides of a stirring main shaft in a cross shape, each stirring component comprises a support, a stirring paddle and a scraper, the supports are fixed on the stirring main shaft in a cross shape, the stirring paddles are uniformly distributed on the stirring main shaft in a cross shape, on one hand, the stress of the stirring main shaft is more uniform, the service life of the stirring main shaft is prolonged, on the other hand, materials in the middle of the stirring kettle of the stirring paddles are stirred and turned more fully, the moisture in the materials can be removed efficiently under the negative pressure evaporation state, and the condition that the square frame type stirring paddles are caked due to the occurrence of stirring blind areas is avoided; intervals are arranged among the scrapers, and the scrapers are overlapped with the corresponding scrapers to clean the wall of the high-temperature kettle without dead angles, so that materials are prevented from being stuck to the inner wall of the high-temperature kettle, a heat exchange surface is guaranteed to be clean, and the heat exchange efficiency is improved; the semicircular heat-conducting oil coil pipe with two inlets and two outlets arranged in an S shape is arranged on the lower portion of the kettle body, on one hand, the heat exchange area of the kettle wall can be increased due to the S-shaped arrangement of the coil pipe, on the other hand, the coil pipe adopts a loop with one inlet and two outlets, the flow of heat-conducting oil is shortened, the flow speed of the heat-conducting oil is higher, the heat exchange efficiency is improved, the evaporation speed of water and the boiling speed are improved, electric energy is further saved, and the boiling cost is reduced.

Drawings

FIG. 1 is a schematic diagram of an apparatus for simultaneously recovering water-soluble protein and gum in the process of refining edible tallow fat according to the present invention.

FIG. 2 is a schematic view of the structure of an extrusion filter in the apparatus of the present invention.

FIG. 3 is a cross-sectional view taken along line A-A in FIG. 2 of an extrusion filter in the apparatus of the present invention.

FIG. 4 is a schematic view of the extrusion filter of the apparatus of the present invention in the direction B-B of FIG. 2.

FIG. 5 is a schematic top view of an extrusion filter of the apparatus of the present invention.

FIG. 6 is a schematic diagram of the top view of the material-setting assembly of the extrusion filter of the present invention.

FIG. 7 is a schematic structural view of a vacuum horizontal type cooking kettle in the device of the present invention.

FIG. 8 is a schematic view of the structure of the vacuum horizontal type cooking kettle in FIG. 6 in the direction of C-C in the device of the present invention.

FIG. 9 is a schematic view of the structure of the vacuum horizontal type decocting kettle in the device of the present invention along the direction D-D in FIG. 6.

FIG. 10 is a flow chart showing the process for simultaneously recovering water-soluble proteins in the process of refining animal fat according to the present invention.

Illustrated in the accompanying drawings: 1 is a raw material unpacking platform, 2 is a first-level material conveyor, 3 is a chopper, 4 is a second-level material conveyor, 5 is a preheating kettle, 6 is a mixture conveying pump, 7 is an extrusion filter, 8 is a hot water tank, 9 is a solid-phase temporary storage tank, 10 is a liquid-phase temporary storage tank, 11 is a liquid-phase conveying pump, 12 is a settling kettle, 13 is a heat exchanger, 14 is a hot oil circulating pump, 15 is a water-phase mixture buffer storage tank, 16 is a water-phase mixture primary conveying pump, 17 is a water-phase mixture temporary storage tank, 18 is a water-phase mixture secondary conveying pump, 19 is a liquid-solid separation device, 20 is a water-phase temporary storage tank, 21 is a protein separating agent stirring tank, 22 is a protein separation tank, 23-1 is a first-level negative pressure evaporator, 23-2 is a second-level negative pressure evaporator, 23-3 is a third-level negative pressure evaporator, 24 is a protein thick slurry temporary storage tank, 25 is a conveying pump, 26 is a spray dryer, 27 is a first vacuum pump, 28 is an oil phase and solid phase temporary storage kettle, 29 is a secondary cooking kettle, 30 is a solid phase delivery pump, 31 is a mixed phase delivery pump, 32 is oil/residue liquid-solid separation equipment, 33 is a hot oil temporary storage tank, 34 is a filter oil pump, 35 is a filter, 36 is a finished oil tank, 37 is an oil press, 38 is a condenser, 39 is a second vacuum pump, and 40 is an odor treatment device;

701 is a feed inlet, 702 is a splash baffle, 703 is a cylinder, 704 is a shield, 705 is a split flange, 706 is a partition plate, 707 is a spiral propulsion shaft, 708 is a solid discharging shifting plate, 710 is a driven end bearing seat, 711 is a driven end self-aligning bearing, 712 is a solid outlet, 713 is a liquid outlet, 714 is a liquid collecting tank, 715 is a driving end thrust bearing, 716 is a frame, 717 is a speed reducer bottom plate, 718 is a speed reducing motor, 719 is a coupler, 720 is a graphite sealing ring, 721 is a driving end bearing seat, and 723 is a baffle;

2901 is the switch board, 2902 is the material import, 2903 is preheating the feed valve, 2904 is the feeding hopper, 2905 is the gas collector, 2906 is the conduction oil export, 2907 is the manhole, 2908 is the conduction oil import, 2909 is the reinforcing plate, 2910 is the support, 2911 is the stirring main shaft, 2912 is the bin outlet, 2913 is the speed reducer, 2914 is the bottom plate, 2915 is the stirring rake, 2916 is the cauldron body, 2917 is the connecting support, 2918 is the scraper, 2919 is the shaft coupling, 2920 staple bolt.

Detailed Description

The following examples are intended to illustrate the invention, but are not intended to limit the scope of the invention. Unless otherwise specified, the technical means used in the examples are conventional means well known to those skilled in the art. The test methods in the following examples are conventional methods unless otherwise specified.

The device can be used for processing edible beef tallow, and the selected fat raw materials comprise: leaf fat, fat oil, net oil, etc. of cattle.

Example one

The device for simultaneously recovering water-soluble protein and colloid in the refining process of the edible tallow fat comprises a raw material pretreatment device, a mixture separation device, a solid phase object and oil phase object treatment device and a water phase object treatment device.

The raw material pretreatment device comprises a first-stage feeding conveyor 2, a chopper 3, a second-stage feeding conveyor 4, a preheating kettle 5 and a hot water tank 8 connected with the preheating kettle 5. Specifically, as shown in fig. 1, a stainless steel chain plate conveyor is adopted as the first-stage feeding conveyor 2, a screw conveyor is adopted as the second-stage feeding conveyor 4, one end of the first-stage feeding conveyor 2 is connected with the raw material unpacking platform 1, the other end of the first-stage feeding conveyor is connected with the inlet of the chopper 3, one end of the second-stage feeding conveyor 4 is connected with the outlet of the chopper 3, the other end of the second-stage feeding conveyor is connected with the inlet of the preheating kettle 5, and the outlet of the hot water tank 8 is connected with the inlet of the preheating kettle 5. Hot water of 80-90 ℃ is added into the

hot water tank

8, 1/4 of the weight of the hot water in the preheating kettle 5 is the weight of the beef tallow, and in the preheating and temperature rising process, the hydrophilic protein and the colloid contained in the hot water and the beef tallow are fully dissolved and absorbed, thereby being beneficial to the removal of the hydrophilic protein and the colloid contained in the oil phase substance by the later-stage separation process.

The mixture separation device comprises a mixture delivery pump 6 connected with an outlet of a preheating kettle 5, an extrusion filter 7, a liquid phase delivery pump 11, a solid phase delivery pump 30, a settling kettle 12 connected with the liquid phase delivery pump 11, a hot oil circulating pump 14 connected with the settling kettle 12, liquid-solid separation equipment 19 and a mixed phase delivery pump 31 connected with solid phase and oil phase outlets of the liquid-solid separation equipment 19. Specifically, as shown in FIG. 1, the mixture delivery pump 6 is selected from RJB-100-11 KW type of Hebei Shenghui pump company Limited, the liquid phase delivery pump 11 is selected from KCB200-4KW type of Hebei Shenghui pump company Limited, the solid phase delivery pump 30 is selected from RJB-100-250-15KW type of Hebei Shenghui pump company Limited, the mixed phase delivery pump 31 is selected from RJB-100-250-15KW type of Hebei Shenghui pump company Limited, the hot oil circulating pump 14 is selected from RY-65-160-7.5KW type of Hebei Shenghui pump company Limited, the water phase mixture primary delivery pump 16 is selected from RJB-100-200-11KW type of Hebei Shenghui pump company Limited, the inlet of the mixture delivery pump 6 is connected with the outlet of the preheating kettle 5, the outlet is connected with the feed inlet of the extrusion filter 7, the solid phase outlet of the extrusion filter 7 is connected with the solid phase temporary storage tank 9, the solid phase storage tank 9, A liquid phase outlet is connected with a liquid phase temporary storage tank 10, an outlet of a solid phase temporary storage tank 9 is connected with an inlet of a solid phase delivery pump 30, an inlet of a liquid phase delivery pump 11 is connected with an outlet of the liquid phase temporary storage tank 10, an outlet of the liquid phase delivery pump is connected with an inlet at the top of a settling kettle 12, a lower-layer water phase outlet at the bottom of the settling kettle 12 is connected with a water phase mixture buffer tank 15, an upper-layer oil phase outlet at the bottom of the settling kettle 12 is connected with an inlet of a hot oil circulating pump 14, an outlet of the hot oil circulating pump 14 is connected with a shell pass inlet of a heat exchanger 13 (the heat exchanger 13 adopts heat conducting oil or steam as a heating medium), a shell pass outlet of the heat exchanger 13 is connected with a hot oil inlet of the settling kettle 12, after the temperature is raised to 120-140 ℃ in a circulating manner, an outlet of the hot oil circulating pump 14 is switched to an inlet of a secondary boiling kettle 29, an inlet of a first-stage water phase mixture delivery pump 16 is connected with an outlet of the water phase mixture buffer tank 15, and an outlet is connected with a liquid-solid separation device 19 (a three-phase horizontal spiral centrifuge, LWS-350 model of Jiangsu giant energy machinery limited), the oil phase and the solid phase separated by the liquid-solid separation equipment 19 enter an oil phase and solid phase temporary storage kettle 28, the water phase enters a water phase temporary storage tank 20, and the outlet of the oil phase and the solid phase temporary storage kettle 28 is connected with the inlet of a mixed phase delivery pump 31.

Furthermore, in order to improve the processing capacity, the settled lower aqueous phase containing the water-soluble protein can be temporarily stored in the aqueous phase mixture temporary storage tank 15, and then pumped to the aqueous phase mixture temporary storage kettle 17 through the aqueous phase mixture primary conveying pump 16 for stirring and temporary storage, and when the aqueous phase mixture temporary storage kettle 17 is at the storage high position, pumped to the liquid-solid separation equipment 19 through the aqueous phase mixture secondary conveying pump 18. Specifically, the water phase mixture secondary delivery pumps 18 are all of types RJB-100-200 KW of Hebei Shenghui pump industry Co., Ltd, the inlets of the water phase mixture primary delivery pumps 16 are connected with the outlets of the water phase mixture temporary storage tanks 15, the outlets of the water phase mixture temporary storage tanks 17 are connected with the top inlets of the water phase mixture temporary storage tanks 17, and the inlets of the water phase mixture secondary delivery pumps 18 are connected with the bottom outlets of the water phase mixture temporary storage tanks 17, and the outlets of the water phase mixture secondary delivery pumps are connected with the liquid-solid separation equipment 19.

The solid phase and oil phase processing device comprises a secondary cooking kettle 29, an oil/residue liquid-solid separation device 32, an oil press 37 and a filter 35, wherein the secondary cooking kettle 29 is connected with a hot oil circulating pump 14, a solid phase delivery pump 30 and a mixed phase delivery pump 31. Specifically, as shown in fig. 1, the outlet of the solid phase delivery pump 30, the outlet of the hot oil circulating pump 14, and the outlet of the mixed phase delivery pump 31 are connected to the inlet of the secondary decocting kettle 29; an outlet of the secondary cooking kettle 29 is connected with an inlet of an oil/slag liquid-solid separation device 32 (a two-phase horizontal spiral centrifuge, the model LW-350 of Jiangsu giant energy machinery Co., Ltd.), an oil phase outlet of the oil/slag liquid-solid separation device 32 is connected with an inlet of a hot oil temporary storage tank 33, an outlet of the hot oil temporary storage tank 33 is connected with an inlet of an oil filter pump 34, an outlet of the filter oil pump 34 is connected with an inlet of a filter 35 (the model NYB-20 of Jiangsu giant energy machinery Co., Ltd.), an outlet of the filter 35 is connected with a finished oil tank 36, and a solid phase oil slag outlet of the oil/slag liquid-solid separation device 32 is connected with an oil press 37 (the model YZYYYX 140GX of Guangxin grain oil machinery Co., Ltd., Sichuan). The temperature of the secondary boiling in the secondary boiling kettle 29 is between 110 and 140 ℃ according to different raw materials. When the secondary decocting kettle 29 is heated and decocted, the secondary decocting kettle 29 is vacuumized under the action of a second vacuum pump 39 (SP-2 type of Song's vacuum equipment Co., Ltd., Liaoyang), the evaporation temperature of water is reduced, and water vapor is pumped into a condenser 38 to be condensed and recycled for reuse.

The water phase substance treatment device comprises a protein separation tank 22 connected with a water phase outlet of a liquid-solid separation device 19, a composite negative pressure evaporator connected with the protein separation tank 22, a delivery pump 25 and a spray dryer 26. Specifically, as shown in fig. 1, the aqueous phase separated by the liquid-solid separation device 19 contains protein and pectin and is sent to an aqueous phase temporary storage tank 20 for temporary storage, an outlet of the aqueous phase temporary storage tank 20 is connected with a protein separation tank 22, and the protein separation tank 22 is connected with a protein separating agent stirring tank 21 containing a protein separating agent. Adding the protein separating agent dissolved in the protein separating agent stirring tank 21 into the protein separating tank 22, wherein the adding amount of the protein separating agent is 2-8% of the weight of the protein water phase, so that the protein and the colloid are agglomerated, separating out clear water, directly discharging from the bottom of the protein separating tank 22, agglomerating and polymerizing the protein colloid thick slurry, and efficiently removing water by using a transposition composite negative pressure evaporator. A concentrated slurry outlet of the protein separation tank 22 is connected with a positive pressure chamber of the primary negative pressure evaporator 23-1, materials are quickly boiled in a high temperature state to generate a large amount of gas-liquid mixture, and after gas-liquid separation, secondary high-temperature water vapor is discharged to heating chambers of the secondary negative pressure evaporator 23-2 and the tertiary negative pressure evaporator 23-3 along an exhaust pipe to be used as heat sources, so that heat energy loss is reduced; liquid phase substances obtained after gas-liquid separation in the primary negative pressure evaporator 23-1 are injected into a negative pressure chamber of the secondary negative pressure evaporator 23-2 through a diversion trench, secondary evaporation is carried out in a negative pressure state, water vapor is condensed and recovered in a vacuum state and is pumped out through a first vacuum pump 27 (SP-2 type of Song vacuum Equipment Co., Ltd., Liaoyang) for recycling; liquid phase substances after gas-liquid separation in the first-stage negative pressure evaporator 23-1 are injected into a negative pressure chamber of the third-stage negative pressure evaporator 23-3 through a diversion trench, and are evaporated for three times in a negative pressure state. After the materials are evaporated for three times, a large amount of water is evaporated to form protein thick slurry with the solid content of more than 60%, the protein thick slurry enters a temporary storage tank 24 of the protein thick slurry, an outlet of the temporary storage tank 24 of the protein thick slurry is connected with an inlet of a conveying pump 25, and an outlet of the conveying pump 25 is connected with a spray dryer 26. According to the invention, through three-stage combined negative pressure evaporation, condensed distilled water can be reused to reduce emission, secondary steam generated in the material moisture evaporation process is effectively utilized to provide a heat source for the next-stage evaporator, the heat source consumption is reduced, and the heat efficiency is improved.

Furthermore, in order to recover the waste heat of the tail gas of the heat-conducting oil furnace in the heat-conducting oil heating system, a coil pipe passing through the tail gas is arranged in the protein separation tank 22, or a temporary protein mixture storage tank is additionally arranged between the protein separation tank 22 and the combined negative pressure evaporator, the coil pipe passing through the tail gas is arranged in the temporary protein mixture storage tank, the waste heat of the tail gas discharged by the heat-conducting oil furnace is utilized to heat the water phase mixture, the heat energy consumption of the combined negative pressure evaporator is reduced, and the energy consumption is saved.

As shown in fig. 1, the apparatus for simultaneously recovering water-soluble protein and gum in the refining process of edible tallow fat of the present invention further comprises an odor treatment apparatus 40 and a heat energy recycling system. Specifically, the odor components volatilized from the discharge port of the secondary decocting kettle 29 are pumped to an odor treatment device 40 (a spraying photo-oxygen deodorizer) for odor treatment, and the odor is discharged in an environment-friendly way after reaching the standard; the liquid phase separated by oil/slag liquid enters a hot oil temporary storage tank 33, and is pumped to be used as heating media of the preheating kettle 5 and the secondary boiling kettle 29 by a hot oil pump, so that heat is recovered.

As shown in fig. 2, the extrusion filter 7 of the present invention comprises a barrel 703, the barrel 703 penetrates through a screw propeller shaft 707 through the inside of a bearing seat, and the screw propeller shaft 707 is provided with a helical blade with a gradually decreasing pitch; the cylinder 703 is divided into an accelerating propulsion section (section A), a solid extrusion section (section B), an expansion extrusion section (section C), a conveying section (section D) and a discharging section (section E) along the solid propulsion direction, and the cylinder 703 is divided into a liquid extrusion section (section G) and a liquid shielding section (section F) along the liquid propulsion direction; a feed inlet 701 is arranged above the cylinder 703 at the starting end of the accelerating propulsion section (section A); a solid outlet 712 is arranged below the cylinder 703 at the tail end of the liquid phase shielding section (section F); a liquid phase collecting tank 714 is arranged below the barrel 703 at the liquid phase extrusion section (G section), and a liquid phase outlet 713 is arranged below the barrel 703 at the tail end of the liquid phase extrusion section (G section); the screw propeller shaft 707 is connected to an output shaft of the reduction motor 718 through a coupling 719.

The driving end of the screw propulsion shaft 707 refers to one end connected to the driving motor, the other end connected to the driving motor is a driven end of the screw propulsion shaft 707, the driving end of the screw propulsion shaft 707 is fixed on the driving end bearing seat 721 through the driving end thrust bearing 715, and the driven end of the screw propulsion shaft 707 is fixed on the driven end bearing seat 710 through the driven end self-aligning bearing 711. Specifically, the active end bearing seat 721 and the passive end bearing seat 710 are both flange-type bearing seats. Graphite sealing rings 720 are arranged between the active end bearing seat 721 and the passive end bearing seat 710 and between the spiral propeller shaft 707, so that the active and passive bearings are prevented from being polluted by materials. The sidewall of the liquid-phase collection tank 714 is inclined toward the liquid-phase outlet 713, and may be tapered, and correspondingly, the bottom of the liquid-phase collection tank 714 is provided with a hole, so that the separated liquid-phase material can flow into the liquid-phase outlet 713 and be discharged. If the material processing amount is large and the required equipment is long, the cylinder 703 is formed by splicing a plurality of sections of cylindrical cylinders, and the adjacent two sections of cylindrical cylinders are connected by adopting a split flange 705.

As shown in fig. 3, grooves are formed at intervals on the inner wall of the cylinder 703 at the liquid phase extrusion section (section G), the baffles 723 are mounted on the grooves, the baffles 723 can be made of stainless steel and are in a strip shape, the baffles 723 can be fixed on the inner wall of the cylinder 703 by welding, the baffles 723 are arranged at intervals, gaps are formed between adjacent baffles 723, and the material enters the gaps and is extruded in the process of high-speed rotation and propulsion of the screw propulsion shaft 707, so that the liquid phase in the animal fat is further separated.

As shown in fig. 2, a solid material discharge/kick-out member is provided at a position corresponding to the end of the screw shaft 707 of the solid material outlet 712, so that the separated solid material can be uniformly and constantly discharged from the solid material outlet 712. As shown in fig. 6, the solid material discharging and stirring assembly includes a solid material discharging and stirring plate 708 and a fixed ring, the solid material discharging and stirring plate 708 is fixed on the screw propulsion shaft 707 through the fixed ring, and the fixed ring and the screw propulsion shaft 707 are in interference fit.

As shown in fig. 2 and 5, a shield 704 is disposed outside the barrel 703 of the liquid material extrusion section (section G) to prevent the high-temperature liquid phase from splashing out of the extruder, and both ends of the shield 704 may be supported by a partition 706. At this time, in order to prevent the trouble of removing the shield 704 in case of the malfunction of the apparatus, the feed port 701 should be positioned higher than the shield 704. In addition, a truncated cone-shaped splash guard 702 is arranged at a position below the feed inlet 701 and corresponding to the shield 704 (the pipe of the feed inlet 701 penetrates through the bottom of the truncated cone-shaped splash guard 702), the diameter of the splash guard 702 is larger than that of the feed inlet 701, so that the extruded liquid phase is prevented from splashing out of the shield 704, and the inside and the outside of the shield 704 are isolated by the truncated cone-shaped splash guard 702, so that materials are prevented from entering a space between the shield 702 and the barrel 703.

According to the extrusion filter, the speed reducing motor base plate 717 is arranged below the speed reducing motor 718 through the rack 716, the screw pitches of the helical blades are gradually reduced along the advancing process of materials, namely the screw pitches of the sections A to E are gradually reduced, and the pressure borne by the materials is increased due to the fact that the space is reduced when the materials enter the next section. The solid containing the liquid phase substance passes through the expansion extrusion section (section C) in the high-speed propelling process, the material is extruded to extrude most of the liquid phase substance in the solid due to the sudden diameter change of the cone of the section C, and the solid is spirally propelled to the discharge section E through the conveying section (section D) and discharged from the solid outlet 712; the liquid phase material extruded from the solid matter is gathered under the cylinder 703 and is provided with a liquid phase material collecting tank 714, and is discharged from a liquid phase material outlet 713. Therefore, the solid substance which is subjected to the extrusion separation of water only contains a little part of water when entering the subsequent secondary cooking process, so that the energy consumption of evaporating water during cooking can be greatly reduced, the production cost is reduced, the cooking time can be reduced, and the production efficiency is improved.

According to the invention, a preheating kettle 5 and a secondary decocting kettle 29 both adopt vacuum horizontal decocting kettles, as shown in fig. 7-9, each vacuum horizontal decocting kettle comprises a kettle body 2916, a stirring main shaft 2911 penetrates through the kettle body 2916 through the inside of a bearing seat, a plurality of groups of stirring components are arranged on the stirring main shaft 2911, and each group of stirring components are distributed on two sides of the stirring main shaft 2911 in a cross shape; a material inlet 2902 and a material outlet 2912 are arranged on the side wall of the driving end of the kettle body 2916, and a semicircular heat-conducting oil coil pipe with two inlets and two outlets and arranged in an S shape is arranged on the lower half part of the kettle body 2916; a gas collector 2905 is arranged at the top of the kettle 2916, a vacuum pressure relief opening, a vacuum air exhaust opening and an air exhaust opening are arranged on the gas collector 2905, and a feeding hopper 2904 is further fixed at the top of the kettle 2916 through a preheating feeding valve 2903.

The driving end of the kettle 2916 is the end connected to the driving motor, and the other end connected to the driving motor is the passive end of the kettle 2916; the two sides of the kettle 2916 are welded and sealed by the active end sealing head plate and the passive end sealing head plate, and a jacket is wrapped outside the shell of the kettle 2916 to prevent hot gas from dissipating; the bearing seat is divided into a driving end bearing seat and a driven end bearing seat; and the bottom of the kettle 2916 is provided with steel plate tailor-welded equipment feet. A speed reducer 2913 is mounted on the outer side of the driving end of the kettle 2916 through a connecting bracket 2917, the output end of the speed reducer 2913 is connected with the stirring spindle 2911 through a coupler 2919, and the speed reducer 2913 drives the stirring spindle 2911 to rotate through the coupler 2919. The upper part of the side wall of the driving end of the kettle body 2916 is provided with a material inlet 2902, and the lower part is provided with a material outlet 2912. According to the invention, the semicircular heat-conducting oil coil pipe with two inlets and two outlets and arranged in an S shape is arranged at the lower part of the kettle body 2916, as shown in figure 8, the middle part of the side wall of the passive end of the kettle body 2916 is provided with the left heat-conducting oil outlet and the right heat-conducting oil outlet, and the bottom part of the side wall is provided with the heat-conducting oil inlet 2908, so that on one hand, the heat-conducting oil coil pipe is arranged in an S shape, the heat exchange area of the kettle wall can be enlarged, on the other hand, the coil pipe adopts a loop with one inlet and two outlets, the flow path of the heat-conducting oil is shortened, the flow rate of the heat-conducting oil is higher, the heat exchange efficiency is improved, the water evaporation and boiling speed are improved, the electric energy is further saved, and the boiling cost is reduced.

As shown in fig. 7 and 8, the kettle 2916 is formed by two unequal semicircular shells, wherein the semicircular diameter of the upper half is larger than that of the lower half. Each set of stirring assemblies comprises a bracket 2910, a stirring paddle 2915 and a scraper 2918, wherein the bracket 2910 is in a cross shape and is fixed on a stirring main shaft 2911 through a hoop 2920, the stirring paddle 2915 is fixed on two sides of the bracket 2910, the scraper 2918 is fixed at the tail end of the bracket 2910, and the head part of the scraper 2918 is close to the inner wall of the kettle 2916. Specifically, the end of the bracket 2910 fixes the scraper 2918 through the reinforcing plate 2909 and the bottom plate 2914, so as to enhance the acting force of the scraper 2918 during the operation, and the material of the scraper 2918 may be manganese steel. There is the interval between every scraper 2918 to overlap each other with corresponding scraper and do not have the dead angle clearance autoclave wall, prevent that the material from gluing on the autoclave inner wall, guarantee that the heat-transfer face is clean, improve heat exchange efficiency. In addition, because the diameter of the semicircle at the upper half part of the kettle 2916 is larger than that of the semicircle at the lower half part, a larger gap is left between the scraper 2918 rotating to the semicircle at the upper half part and the kettle wall, and the scraper 2918 is prevented from being locked by the notch at the opening part at the top of the kettle 2916.

As shown in fig. 7, the paddles 2915 are angled at 30 ° to 60 ° to the support 2910. The shape of the paddles 2915 is not particularly limited in the present invention, and the paddles 2915 may be triangular straight blade paddles, curved blade paddles, or other shapes. As an example, the paddles 2915 are angled at 45 ° to the support 2910, and 6 sets of stirring assemblies are provided. Support 2910 is "ten" font and fixes on stirring main shaft 2911 for stirring rake 2915 also is "ten" font equipartition on stirring main shaft 2911, can make stirring main shaft 2911 atress more even improvement life on the one hand, middle part material in on the other hand stirring rake 2915 stirred tank makes the material stirring turn more abundant, can be under the negative pressure evaporation state the high-efficient desorption of moisture content in the material, avoid using square frame formula stirring rake to appear the stirring blind area and the condition of caking. In addition, the stirring spindle 2911 may be formed by a single process to improve the concentricity of the stirring spindle 2911, and prevent damage to bearings and oil leakage due to misalignment of the stirring spindle 2911.

As shown in fig. 9, a gas collector 2905 is disposed on the top of the kettle 2916, a vacuum pressure relief port, a vacuum pumping port and a pumping port are disposed on the gas collector 2905, a one-way safety valve mounting interface and a vacuum meter mounting interface are further disposed on the gas collector 2905, the one-way safety valve mounting interface is used for mounting a safety valve for pressure relief, and the vacuum meter mounting interface is used for mounting a vacuum meter for detecting vacuum degree. The air suction opening is connected with an air suction fan through a pipeline, the vacuum air suction opening is connected with a vacuum pump through a pipeline, peculiar smell generated by materials is sucked out through the air suction opening by the air suction fan and then enters the gas collector 2905, the overflow is prevented, the peculiar smell gas can enter the spraying photo-oxygen deodorizer to be treated and then is discharged after reaching the standard, and the environmental pollution is reduced; after the feeding is completed, the vacuum pump is started to discharge air in the kettle, the kettle 2916 is in a vacuum state, water can be quickly removed through boiling in a negative pressure state under the heating of the heat-conducting oil, the boiling time is shortened, the boiling efficiency is improved, the electric quantity is saved, the boiling cost is reduced, and the obtained finished oil is low in acid value and light in color.

As shown in fig. 8, a flushing port inlet and a defoaming agent inlet are arranged at the upper part of the passive end side wall of the kettle 2916, the flushing port inlet is used for connecting a flushing medium pipeline to clean the kettle wall, and the defoaming agent inlet is used for adding a defoaming agent in the decocting process. Still be provided with on the driving end lateral wall of cauldron body 2916 and look the mirror lamp, be provided with observation window and lower observation window on the driven end lateral wall of cauldron body 2916, can observe the state of cooking of material in the cauldron more directly perceivedly. The top of the kettle 2916 near the passive end is provided with a manhole 2907 for equipment maintenance.

The top of the kettle 2916 is fixed with a feed hopper 2904 through a preheating feed valve 2903, which can be used as a preheating kettle 5 or a secondary boiling kettle 29, and has multiple purposes. When the animal fat material preheating kettle is used as a preheating kettle, a preheating feed valve 2903 is opened, the crushed animal fat material directly enters the kettle from a conveyor through a feed hopper 2904 to be preheated, and the oil/oil residue material after preheating can enter a rear-section extrusion filter 7 from a discharge port 2912 through a mixture conveying pump 6. When the device is used as a vacuum cooking kettle, the oil-solid mixed solution enters the kettle through the material inlet 2902.

The cooking process of the vacuum horizontal cooking kettle can be automatically controlled, and the control cabinet 2901 adopts a pneumatic automatic control distribution box integrating power temperature control and pneumatic valve control, and is internally provided with a single chip microcomputer. Three intelligent digital display temperature control meters are arranged on the control cabinet 2901 and used for displaying the temperature of the heat transfer oil inlet and outlet and the temperature of the raw materials boiled in the kettle. In order to ensure the safe operation of the stirring apparatus, the reducer 2913 cannot be started when the temperature in the kettle is below 50 ℃ according to the melting point of the high-melting animal oil. Pneumatic valves are arranged at the material inlet 2902, the preheating feed valve 2904, the flushing port inlet, the discharge port 2912, the vacuum pressure relief port, the vacuum air pumping port and the air pumping port, and the control cabinet 2901 can automatically control and jointly control the pneumatic valves at the above parts according to instructions and sequentially open and close the instructions.

According to the requirement of the cooking process, the exhaust vacuum and the exhaust fan with large exhaust amount can be switched in different refining stages due to the limitation of the exhaust amount of different vacuum pumps and exhaust fans. The pig fat oil is selected as a raw material, 55 tons of pig fat oil is processed every 12 hours as an example, the equipment volume of a vacuum horizontal boiling kettle is 4t, a matched motor is selected from XLED85-473-3KW of Guangzhou Tongmai reducer group, a vacuum pump is selected from SP-2 of Liaoyang Song vacuum equipment limited, and an exhaust fan is selected from 4-72-3.6C-3KW of Shanghai Zhongzhou Fan limited. The valve joint control process in the cooking process is as follows:

1) during feeding, because the temperature difference is big in raw materials and the cauldron, can produce a large amount of aqueous vapor and peculiar smell, open the feeding button on the switch board 2901, vacuum pressure release mouth valve is opened, and the vacuum bleed port valve is closed, through 15 seconds's delay control, preheats feed valve 2903 and the suction opening valve is opened, and the peculiar smell is taken out in the air exhauster work, and peculiar smell gas gets into gas collector 2905, prevents the overflow, and peculiar smell gas can get into and spray light oxygen deodorizer and handle the back and discharge up to standard.

2) When the feeding is completed, the feeding process enters a negative pressure dehydration stage, a feeding knob on the control cabinet 2901 is closed, the preheating feeding valve 2903 and the air suction opening valve are closed, the valve of the vacuum pressure relief opening is closed, the valve of the vacuum air suction opening is opened, the kettle body 2916 is in a vacuum state, and the material starts a vacuum negative pressure temperature rise refining process in the kettle by utilizing the characteristic that moisture boils at a low temperature under the negative pressure state through heat conduction oil heating. The water can be removed rapidly by boiling under the negative pressure, the boiling time is shortened, the boiling efficiency is improved, and the obtained finished oil has low acid value and light color.

Example two

As shown in fig. 10, the process for simultaneously recovering water-soluble protein and pectin in the refining process of edible tallow fat using the apparatus of the embodiment of the present invention comprises the following steps:

a: pretreatment of raw materials

The animal fat frozen raw material is unpacked, sent into a chopper 3 through a first-grade feeding conveyor 2 and cut into strip-shaped blocks with the length of 20-40mm, sent into a preheating kettle 5 through a second-grade feeding conveyor 4 to be preheated to the temperature of 80-100 ℃, and added with hot water with the temperature of 80-90 ℃ into the preheating kettle 5 at the same time of preheating. Hot water of 80-90 ℃ is added into the

hot water tank

B: separation of the mixture

The preheated animal fat is sent to an extrusion filter 7 by a mixture delivery pump 6 for solid-liquid two-phase separation, the separated liquid phase mixture is temporarily stored by a liquid phase temporary storage tank 10 and then sent to a sedimentation kettle 12 by a liquid phase delivery pump 11 for sedimentation for 30-60min, and the middle layer emulsified oil phase and the lower layer water phase containing hydrophilic water soluble protein and colloid are sent to a liquid-solid separation device 19 for liquid-solid three-phase separation after sedimentation.

C: solid phase and oil phase treatment

C, after the solid-phase substances separated by the extrusion filter 7 in the step B are temporarily stored in a solid-phase temporary storage tank 9, the solid-phase substances are conveyed to a secondary decocting kettle 29 through a solid-phase conveying pump 30 to be subjected to secondary heating and decocting; the residual upper oil phase in the settling kettle 12 is sent to a heat exchanger 13 through a hot oil circulating pump 14, the temperature is raised to 110-140 ℃ through circulating heat exchange, and the oil phase after temperature rise is sent to a secondary boiling kettle 29 through the hot oil circulating pump 14 for secondary boiling; the oil phase and the solid phase which are separated from the liquid phase, the liquid phase and the solid phase in the step B are temporarily stored in an oil phase and solid phase temporary storage kettle 28 and then are conveyed to a secondary decocting kettle 29 by a mixed phase conveying pump 29 for secondary decocting at the temperature of 140 ℃; after the secondary boiling is finished, the mixture is sent to an oil/residue liquid-solid separation device 32 for oil/residue liquid-solid separation. The peculiar smell discharged from the secondary stewing kettle 29 is discharged after being treated by the odor treatment device 40.

D: treatment of aqueous phase

And C, temporarily storing the water phase subjected to liquid-solid three-phase separation in the step B in a water phase temporary storage tank 20, then firstly feeding the water phase into a protein separation tank 22, adding a protein separating agent into the protein separation tank 22 to polymerize protein and colloid clusters, wherein the adding amount of the protein separating agent is 2-8% of the weight of the protein water phase, directly discharging separated clear water from the bottom of the protein separation tank 22, feeding the clustered and polymerized protein thick slurry into a composite negative pressure evaporator, removing water through three-stage evaporation to form high-solid-content protein thick slurry, and feeding the protein thick slurry into a spray dryer 24 through a conveying pump 23 to perform spray drying to obtain protein powder.

E: oil residue and product oil

C, sending the solid phase subjected to oil/residue liquid-solid separation in the step C to an oil press 37 to press residual oil to obtain low-fat protein oil residue; the liquid phase after liquid-solid separation enters a hot oil temporary storage tank 33, is pumped to a filter 35 through an oil filter pump 34 to remove fine oil residues to obtain finished oil, and is pumped to a finished oil tank 34 for storage. And refining the finished oil by using equipment to perform dephosphorization, degumming, deacidification, deodorization, decoloration and other treatments to reach the food grade standard.

The invention first preheats the materials, the animal fat after preheating and warming is extruded and filtered by an extrusion filter 7 for the first solid-liquid separation, the liquid phase mixture is naturally settled, the middle layer emulsified oil phase and the lower layer water phase containing water-soluble protein are separated for the second liquid, liquid and solid phases, and the invention has the following advantages: 1) firstly, preheating the materials and heating the materials and adding hot water, so that on one hand, the basic temperature of subsequent material treatment is improved, and the pressurized extrusion operation of an extrusion filter 7 is facilitated, and on the other hand, in the preheating and heating process, the hydrophilic protein and the colloid contained in the hot water and the butter fat are fully dissolved and absorbed, and the hydrophilic protein and the colloid contained in the oil phase substances are removed by a later-stage separation process; 2) after the first solid-liquid separation, the liquid phase mixture is naturally settled, and the settled solution is in three forms: the upper oil layer is light yellow, the middle emulsified oil layer is milky white, the lower water-soluble protein dissolved water layer is tooth yellow, the interlayer definition is obvious through observation of a glass sight glass, the middle emulsified oil phase and the lower water phase containing hydrophilic water-soluble protein and colloid are subjected to secondary liquid, liquid and solid three-phase separation, and the lower water phase is not directly discharged as sewage, so that the sewage treatment pressure is reduced, the content of emulsified oil in the material entering a secondary boiling kettle 29 is reduced, the phenomenon that the quality of an oil product is influenced by the emulsified oil mixed into the finished oil is avoided, and the shelf life is prolonged; 3) after natural sedimentation, the residual upper oil phase in the sedimentation kettle 12 is sent to a heat exchanger 13 through a hot oil circulating pump 14 for high-speed heat exchange and temperature rise, and then enters a secondary boiling kettle 29, so that the basic temperature of low-temperature materials in the boiling kettle is improved, the heat exchange efficiency is improved, as the low-temperature solid materials contain little moisture and high-temperature liquid oil is injected, the low-temperature solid materials and the high-temperature liquid oil exchange heat efficiently, and protein is dissolved in water but not dissolved in oil, and the temperature is continuously raised for refining to obtain the edible beef tallow with the inherent thick flavor of the edible beef tallow and no muddy soup used in the chafing dish industry; 4) solid, secondary liquid, solid phase and oil phase after three-phase separation of liquid and solid after the first solid-liquid separation are sent to a secondary boiling kettle 29 for boiling, so that the weight and water content of materials entering the secondary boiling kettle 29 are reduced, the boiling time is shortened, the heat energy consumption and the power load of secondary boiling are reduced, meanwhile, because the secondary boiling materials are the oil phase after dehydration, the phenomenon of coking and gelatinization of water-soluble protein in a high-temperature environment is avoided, the release of toxic substance benzopyrene is reduced, the food safety is ensured, and the device can be used for producing food-grade oil; 5) the solid matter of the animal fat after being dissolved is connective tissue, the connective tissue is composed of protein, the protein is soluble in water but not soluble in grease, and the material of the secondary cooking of the invention is dehydrated oil phase, which can block the hydrolysis of the connective tissue, namely block the decomposition of hydrophilic protein, reduce the loss of water-soluble protein and improve the nitrogen content of the connective tissue; 6) adding a protein separating agent into a water phase after liquid, liquid and solid three-phase separation in a stirring process of a water-soluble protein separating tank, agglomerating and polymerizing protein and colloid contained in the water phase, separating clear water and agglomerated and polymerized protein thick slurry, directly discharging the clear water, efficiently evaporating water by a protein thick slurry transposition composite negative pressure evaporator, and recovering protein powder with the nitrogen content of more than 13% and the crude protein content of more than 81%, so that emulsified oil and hydrophilic water-soluble protein and colloid in the water phase are recovered as much as possible.

The above-mentioned embodiments are merely preferred embodiments of the present invention, which are merely illustrative and not restrictive, and it should be understood that other embodiments may be easily made by those skilled in the art by replacing or changing the technical contents disclosed in the specification, and therefore, all changes and modifications that are made on the principle of the present invention should be included in the scope of the claims of the present invention.

Claims

1. The device for simultaneously recovering water-soluble protein and colloid in the refining process of the edible tallow fat is characterized by comprising a raw material pretreatment device, a mixture separation device, a solid phase object and oil phase object treatment device and a water phase object treatment device;

the raw material pretreatment device comprises a first-stage feeding conveyor (2), a chopper (3), a second-stage feeding conveyor (4), a preheating kettle (5) and a hot water tank (8) connected with the preheating kettle (5);

the mixture separation device comprises a mixture delivery pump (6) connected with an outlet of the preheating kettle (5), an extrusion filter (7), a liquid phase delivery pump (11), a solid phase delivery pump (30), a settling kettle (12) connected with the liquid phase delivery pump (11), a hot oil circulating pump (14) connected with the settling kettle (12), liquid-solid separation equipment (19), and a mixed phase delivery pump (31) connected with solid phase and oil phase outlets of the liquid-solid separation equipment (19);

the solid phase substance and oil phase substance processing device comprises a secondary cooking kettle (29) connected with a hot oil circulating pump (14), a solid phase delivery pump (30) and a mixed phase delivery pump (31), oil/residue liquid-solid separation equipment (32), an oil press (37) and a filter (35);

the water phase substance treatment device comprises a protein separation tank (22) connected with a water phase outlet of the liquid-solid separation equipment (19), a composite negative pressure evaporator connected with the protein separation tank (22), a delivery pump (25) and a spray dryer (26).

2. The device according to claim 1, characterized in that the extrusion filter (7) comprises a barrel (703), the barrel (703) penetrates through the spiral propeller shaft (707) through the inside of a bearing seat, and spiral blades with gradually reduced pitch are arranged on the spiral propeller shaft (707); the cylinder (703) is divided into an accelerating propulsion section, a solid extrusion section, an expansion extrusion section, a conveying section and a discharging section along the solid propulsion direction, and the cylinder (703) is divided into a liquid extrusion section and a liquid shielding section along the liquid propulsion direction; a feed inlet (701) is arranged above the cylinder (703) at the starting end of the accelerating propulsion section; a solid outlet (712) is arranged below the cylinder (703) positioned at the tail end of the liquid phase shielding section; a liquid phase collecting tank (714) is arranged below the cylinder (703) at the liquid phase extrusion section, and a liquid phase outlet (713) is arranged below the cylinder (703) at the tail end of the liquid phase extrusion section; the spiral propelling shaft (707) is connected with an output shaft of a speed reducing motor (718) through a coupling (719).

3. The device according to claim 2, wherein a solid material discharging and stirring assembly is arranged at the end position of the screw propulsion shaft (707) corresponding to the solid material outlet (712), the solid material discharging and stirring assembly comprises a solid material discharging and stirring plate (708) and a fixed ring, and the solid material discharging and stirring plate (708) is fixed on the screw propulsion shaft (707) through the fixed ring.

4. The device according to claim 2, characterized in that a shield (704) is arranged outside the barrel (703) of the liquid phase extrusion section, the feed inlet (701) is positioned higher than the shield (704), a truncated cone-shaped splash guard (702) is arranged below the feed inlet (701) and in a position corresponding to the shield (704), and the diameter of the splash guard (702) is larger than that of the feed inlet (701).

5. The device according to claim 1, wherein the preheating kettle (5) and the secondary decocting kettle (29) are vacuum horizontal decocting kettles, each vacuum horizontal decocting kettle comprises a kettle body (2916), a stirring main shaft (2911) penetrates through the kettle body (2916) through a bearing seat, a plurality of groups of stirring assemblies are arranged on the stirring main shaft (2911), and each group of stirring assemblies are distributed on two sides of the stirring main shaft (2911) in a cross shape; the side wall of the driving end of the kettle body (2916) is provided with a material inlet (2902) and a material outlet (2912), and the lower half part of the kettle body (2916) is provided with a semicircular heat-conducting oil coil pipe with two inlets and two outlets in S-shaped arrangement; the top of the kettle body (2916) is provided with a gas collector (2905), the gas collector (2905) is provided with a vacuum pressure relief port, a vacuum air suction port and an air suction port, and the top of the kettle body (2916) is further fixed with a feeding hopper (2904) through a preheating feeding valve (2903).

6. The device according to claim 5, wherein each group of the stirring assemblies comprises a bracket (2910), a stirring paddle (2915) and a scraper (2918), the bracket (2910) is in a cross shape and is fixed on the stirring main shaft (2911) through a hoop (2920), the stirring paddle (2915) is fixed on two sides of the bracket (2910), the scraper (2918) is fixed at the tail end of the bracket (2910), and the head part of the scraper (2918) is close to the inner wall of the kettle body (2916).

7. The apparatus according to claim 1, further comprising an odor treatment device (40) and a thermal energy recovery system.

8. A process for simultaneously recovering water soluble proteins and gums in an edible tallow fat refining process using the apparatus of any of claims 1 to 7, comprising the steps of:

a: pretreatment of raw materials

The animal fat frozen raw material is unpacked, sent into a chopper (3) through a first-grade feeding conveyor (2) and cut into strip-shaped blocks with the length of 20-40mm, sent into a preheating kettle (5) through a second-grade feeding conveyor (4) to be preheated to the temperature of 80-100 ℃, and added with hot water with the temperature of 80-90 ℃ into the preheating kettle (5) at the same time of preheating;

b: separation of the mixture

Sending the preheated animal fat to an extrusion filter (7) through a mixture delivery pump (6) for solid-liquid two-phase separation, temporarily storing the separated liquid phase mixture, sending the temporarily stored liquid phase mixture to a settling kettle (12) through a liquid phase delivery pump (11) for settling for 30-60min, sending the settled middle layer emulsified oil phase and the lower layer water phase containing hydrophilic water soluble protein and colloid to a liquid-solid separation device (19) for liquid-solid three-phase separation;

c: solid phase and oil phase treatment

C, temporarily storing the solid-phase substances separated by the extrusion filter (7) in the step B, and then conveying the solid-phase substances to a secondary decocting kettle (29) through a solid-phase conveying pump (30) for secondary heating and decocting; the residual upper oil phase in the settling kettle (12) is sent to a heat exchanger (13) through a hot oil circulating pump (14) and heated to 120-; c, temporarily storing the oil phase and the solid phase after the liquid phase, the liquid phase and the solid phase are separated in the step B, and then conveying the oil phase and the solid phase to a secondary decocting kettle (29) through a mixed phase conveying pump (31) for secondary decocting; after the secondary cooking is finished, sending the mixture to oil/residue liquid-solid separation equipment (32) for oil/residue liquid-solid separation;

d: treatment of aqueous phase

B, temporarily storing the water phase after liquid-solid three-phase separation in a protein separation tank (22), adding a protein separating agent into the protein separation tank (22) to enable protein and colloid to be agglomerated and polymerized, feeding the agglomerated and polymerized protein thick slurry into a composite negative pressure evaporator, removing water through three-stage evaporation to form high-solid-content protein thick slurry, and conveying the protein thick slurry to a spray dryer (24) through a conveying pump (23) for spray drying to obtain protein powder;

e: oil residue and product oil

C, sending the solid phase subjected to oil/residue liquid-solid separation in the step C to an oil press (37) to press residual oil to obtain low-fat protein oil residue; the liquid phase after liquid-solid separation is filtered by a filter (35) to remove fine oil residue, and the finished oil is obtained.

9. The process as claimed in claim 8, wherein the odor discharged from the secondary decocting kettle (29) is treated by an odor treatment device (40) and then discharged.

10. The process as claimed in claim 8, wherein the liquid phase separated from oil/residue in step E is pumped by hot oil to serve as a heating medium for the preheating kettle (5) and the secondary boiling kettle (29) to recover heat.