CN213965259U - Citrus peel progressive extraction device - Google Patents

Citrus peel progressive extraction device Download PDF

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CN213965259U
CN213965259U CN202022795384.4U CN202022795384U CN213965259U CN 213965259 U CN213965259 U CN 213965259U CN 202022795384 U CN202022795384 U CN 202022795384U CN 213965259 U CN213965259 U CN 213965259U
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peel
tank
kernel
citrus
leaching
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曾祥奎
曾华
胡大学
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曾祥奎
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Abstract

The utility model relates to a citrus peel gradual extraction device, which comprises a citrus peel pretreatment system and a citrus peel gradual extraction system; the citrus peel progressive extraction system comprises a peel crusher, a peel slurry tank, a leaching tank, a storage tank group, a delivery pump, a plate type heat exchanger, a pipeline switching plate device and diatomite filtration. The utility model discloses the realization is carried out progressive extraction to citrus fruit, obtains peel essential oil, fruit juice, fruit stone, oranges and tangerines immersion fluid syrup, hesperidin, pectin and dietary fiber product in proper order, implements the utility model discloses, the oranges and tangerines peel draws and need not carry many times and shift the oranges and tangerines peel, and the dehydration operation is squeezed to the number of times, makes its easy and simple to handle, serialization, systematization, reduces the repetition work by a wide margin, reduces power and energy resource consumption, has also reduced the material loss of course of working by a wide margin, shortens product processing operation cycle simultaneously, has fine economic benefits.

Description

Citrus peel progressive extraction device
Technical Field
The utility model relates to a fruit peel retrieves and draws technical field, especially a citrus peel extraction element that advances gradually.
Background
The citrus planting area and the yield of China are in the first place of the whole world. However, the processing utilization rate of citrus is only 8% to 9% but less than 10%, and the utilization rate is much lower in citrus juice processing, which is very different from the global comprehensive level of 35% of citrus processing utilization rate. The processing utilization rate of the citrus in the countries developed by American and Brazilian citrus is as high as 70-80 percent, which is far from the processing utilization rate of the citrus. At present, the consumption market of citrus fruit juice with 14 hundred million population in China is rising year by year, the amount of the citrus fruit juice imported each year is about 8-10 ten thousand tons, and the reason is that the yield of citrus fruit in China is high, but the processing utilization rate of citrus is low; the market for citrus juice consumption is demanding but has to rely on importation.
The main reasons are four aspects: firstly, citrus fruit juice processing is an extension of citrus agriculture, and in order to keep sufficient citrus raw materials, citrus fruit juice needs to be built into a citrus orchard base, and needs to be supported by an agricultural industry policy in the aspect of base construction. In fact, citrus fruit juice enterprises are not supported by agricultural industry policies for developing citrus orchard base construction. Therefore, juice processing enterprises cannot build citrus orchard raw material bases of companies, and the manufacturing cost of citrus juice processing products is unbalanced with the manufacturing input cost of the products in the face of high and persistent citrus raw material prices; secondly, non-standardized orchard citrus raw materials purchased in the market hardly meet the technical requirements of products, so that the product quality is unstable, and influence cannot be formed in the market; thirdly, due to insufficient supply of citrus raw materials, the processing period of citrus juice is short, and enterprises are seriously restricted from realizing large-scale production; fourthly, the industrial structure is unreasonable, the processed product is single, and no rotary space exists in the face of market variation enterprises. For the reasons, the citrus juice processing enterprises without economic strength or unreasonable industrial structures are only in a predicament for a long time and even forced to stop production and disintegrate.
SUMMERY OF THE UTILITY MODEL
In order to solve the problems in the background art, the utility model provides a citrus peel gradual extraction device, which can recycle essential oil, juice and citrus fruit stones of citrus peel through the pretreatment of the citrus peel; the extraction operation of substances with higher value in the citrus peel is coherent in the process of extracting the citrus peel gradually, and citrus extract syrup, hesperidin, pectin and dietary fiber products can be obtained in sequence, so that the method has extremely important economic value.
The utility model provides a technical scheme that its technical problem adopted is: a citrus peel gradual extraction device comprises a citrus peel pretreatment system and a citrus peel gradual extraction system;
the orange peel pretreatment system comprises a kernel separation device, an orange peel grinding machine, a juicer, a peel crusher, a peel pulp tank and a screw pump; the fruit peel outlet of the juicer is arranged above the feed inlet of the kernel separation device; the discharge port of the kernel separation device is arranged above the feed port of the peel crusher; the discharge port of the peel crusher is arranged above the feed port of the peel pulp tank; the screw pump is connected to a conveying pipeline at a discharge port at the bottom of the peel pulp tank;
the citrus peel progressive extraction system comprises a first extraction tank, a second extraction tank, a third extraction tank, a storage tank group, a plate type heat exchanger, a pipeline switching plate, a diatomite filter, an ultrafiltration device, a low-temperature vacuum evaporator, a filter press, a dryer and a screw extruder;
the discharge port of the peel pulp tank is respectively connected with the tank tops of the first leaching tank, the second leaching tank and the third leaching tank through a conveying pipe provided with a screw pump;
the bottoms of the first leaching tank, the second leaching tank and the third leaching tank are respectively connected to the storage tank group through conveying pipelines, and the conveying pipelines are also provided with three-way valves and bypass pipes which are respectively connected to the plate-type heat exchanger and the pipeline switching plate;
the storage tank group is connected with the ultrafiltration device, the low-temperature vacuum evaporator, the diatomite filter and the filter press through a conveying pipeline; the pipeline switching plate is connected with the plate heat exchanger through a conveying pipeline; the conveying pipeline is provided with a centrifugal pump.
The first leaching tank, the second leaching tank and the third leaching tank are respectively provided with a water inlet pipe with a spray head.
Through the conversion of the pipeline switching plate connecting pipeline and the automatic valve conversion, the leaching liquor can be conveyed to meet the process requirements of each component extraction step, and the dryer and the screw extruder are combined to form the citrus peel dietary fiber puffing treatment system.
Further, the kernel separation device comprises a kernel separation sieve drum, a helical blade, a rotating shaft, a driving motor and a kernel collection plate; the driving motor is connected with a helical blade positioned in the kernel separation screen cylinder through a rotating shaft, and a kernel screen hole for separating kernels is formed in a cylinder body at the lower part of the kernel separation screen cylinder; the fruit core separating sieve is characterized in that an arc-shaped fruit core collecting plate is arranged below the fruit core separating sieve cylinder, a fruit peel feeding hole is formed in one end of the fruit core separating sieve cylinder, a fruit peel discharging hole is formed in the other end of the fruit core separating sieve cylinder, a fruit core collecting tank is arranged at the left end of the fruit core collecting plate, and a spraying pipe used for washing is arranged between the fruit core separating sieve cylinder and the fruit core collecting plate.
The citrus seeds are gradually separated from citrus peels by using the stirring effect and the centrifugal effect generated by the continuous rotation of the helical blades in the conveying process of the fruit seed separating screen drum, fall onto the fruit seed collecting plate through the fruit seed screen holes at the lower part of the fruit seed separating screen drum, and are collected by the fruit seed collecting tank to obtain the citrus seeds. The citrus fruit kernels separated and recovered from citrus peels can be used as raw materials for food industry or other industrial processing through washing and drying treatment, and the dried citrus fruit kernels have the oil content of 20-25 percent and multiple purposes.
Further, a kernel separation sieve drum of the kernel separation device is obliquely arranged in such a way that a peel discharge opening end is higher than a peel feed opening end, and the preferred inclination angle is 45-60 degrees; under the produced stirring effect of helical blade's continuous rotation and centrifugal action, the oranges and tangerines kernel separates from the oranges and tangerines peel gradually, and the oranges and tangerines kernel gathers in the bottom of a kernel separation sieve section of thick bamboo under the action of gravity, falls to the kernel collecting plate through the kernel sieve mesh on the kernel separation sieve section of thick bamboo on, sprays the kernel on the kernel collecting plate through the shower and makes it enter into the kernel collecting vat and obtain collecting.
Furthermore, the kernel collecting plate is arc-shaped and parallel to the kernel separating screen drum, so that the citrus kernels can completely fall into the kernel collecting plate after passing through the kernel screen holes and are not easy to scatter.
Further, the arc-shaped kernel collecting plate covers the kernel sieve pore opening area of the cylinder body at the lower part of the kernel separating sieve cylinder, and when citrus kernels pass through the kernel sieve pores, the citrus kernels fall onto the kernel collecting plate, so that the citrus kernels can be conveniently collected in a centralized manner, and meanwhile, the phenomenon that the citrus kernels are scattered outside the kernel collecting plate can not occur.
Furthermore, the tank bottoms of the first leaching tank, the second leaching tank and the third leaching tank are conical, a conical filter screen plate is arranged in the tank bottom, and a space is arranged between the conical filter screen plate and the conical tank bottom; preferably, the conical filter screen plate is parallel to the bottom of the conical tank, and the distance is 60-90 mm. The chamber formed between the two provides a liquid level buffer space for the transmission of the leaching liquor, and when the leaching liquor separated from the tank bottom is filtered by the conical filter screen plate, the granular peel output in the leaching liquor is intercepted, so that the citrus peel is limited from entering the citrus peel leaching liquor.
Furthermore, filter screen plates are respectively arranged at the upper parts of the first leaching tank, the second leaching tank and the third leaching tank, the aperture of meshes of the filter screen plates is 10-16 mm, and the filter screen plates limit the upward floating of the citrus peel so as to ensure that the peel pulp is completely and effectively leached.
The implementation process comprises the following steps:
the citrus peel gradual extraction device is applied to perform gradual extraction on citrus peel, so as to sequentially obtain peel essential oil, fruit juice, fruit seeds, citrus extract syrup, hesperidin, pectin and dietary fiber products, and the specific process steps of the citrus peel gradual extraction are as follows:
a, pretreatment of citrus peel: the pretreatment of the citrus peel in the step A comprises the steps of citrus peel essential oil extraction, citrus juicing, fruit kernel separation and citrus peel crushing, and the specific method comprises the following steps:
a1 extraction of essential oil from pericarp: peeling citrus fruits by using a citrus peeling machine, destroying tissue cells on the surface of citrus peels, fully releasing peel essential oil from the peel cells, and recovering emulsion containing the peel essential oil to obtain citrus peel cold pressed essential oil; by separating and recycling the peel essential oil, the citrus peel essential oil can be prevented from entering the citrus peel leaching liquor to cause adverse effects on subsequent product processing and product quality;
a2 orange juicing: juicing the citrus after removing the peel essential oil in the step A1 by using a juicer, wherein the obtained citrus juice is used for processing citrus juice;
a3 kernel separation: the citrus peels after citrus juicing in the step A2 enter a fruit core separation device for fruit core separation, the citrus fruit cores and the citrus peels are separated by stirring and centrifuging generated by the rotation of the helical blades in the fruit core separation sieve cylinder, and the citrus fruit cores fall into a fruit core collection plate for collection through the fruit core sieve pores at the lower part of the fruit core separation sieve cylinder, so that the citrus fruit cores in the citrus peels are removed; collecting and washing the separated citrus fruit stones, soaking the fruit stones for 5min at normal temperature by using 5% hydrogen peroxide, then washing the fruit stones for 5min by using flowing softened water to remove the hydrogen peroxide, and drying the fruit stones until the water content is 8% -10% to obtain the citrus fruit stones; the citrus kernels are separated in the step, so that adverse effects on subsequent product processing and product quality can be avoided;
a4 pericarp breaking: and C, crushing the citrus peel separated from the kernel in the step A3 by using a peel crusher, spraying equivalent softened water into the peel crusher while crushing the citrus peel, wherein the crushed particle size of the citrus peel is 10-18 mm, converting the crushed citrus peel into fruit peel pulp, and conveying the fruit peel pulp into the first leaching tank, the second leaching tank and the third leaching tank. The softened water is sprayed during crushing, so that the crushing operation of the citrus peel is facilitated, and the fluidity of the peel pulp is improved.
B, extracting citrus extract syrup: adding softened water 2-3 times (by weight) of the peel pulp into a first leaching tank, completely immersing the peel pulp in the softened water, and standing and leaching for 20 min; transferring the leaching liquor in the first leaching tank to a second leaching tank, and standing and leaching the peel pulp in the second leaching tank for 20 min; transferring the leaching liquor in the second leaching tank to a third leaching tank, and standing and leaching the peel pulp for 20 min; collecting the leaching liquor in the third leaching tank, filtering by using a 120-160-mesh filter sieve, and removing suspended peel and pulp impurities in the leaching liquor to obtain a citrus peel washing sugar liquor;
pasteurizing the citrus peel washing sugar solution by adopting a plate heat exchanger, controlling the sterilization temperature to be 90-93 ℃ and the sterilization time to be 15-20 s, controlling the outlet temperature of the citrus peel washing sugar solution to be 50-55 ℃, adding 0.03-0.06 wt% of active carbon into the citrus peel washing sugar solution for decoloring, simultaneously adding pectinase, wherein the pectinase is obtained by dissolving pectinase dry powder in softened water by 5 times in advance, keeping the temperature to be 50-55 ℃ and carrying out enzymolysis for 40-60 min, and decomposing pectin in the citrus peel washing sugar solution; when the pectin enzymolysis test is negative, the enzymolysis reaches the end point, and the enzymolysis is stopped; when the enzymolysis reaches the end point, the suspended matters in the citrus peel washing sugar solution are mutually adsorbed and flocculated, and precipitate is formed and settled at the bottom, so that the citrus peel washing sugar solution is clarified;
taking out supernatant of the orange peel washing sugar solution after enzymolysis, separating suspended pulp and high molecular polymers in the orange peel washing sugar solution by adopting an ultrafiltration device, wherein the aperture of an ultrafiltration membrane core is 1-50 nm, the temperature is 50-55 ℃, the operating pressure is 0.50-0.56 Mpa, the circulation amount of ultrafiltration liquid is 8-12 times of the ultrafiltration separation capacity, water, monosaccharide, disaccharide and organic acid soluble solid substances penetrate through an ultrafiltration membrane, collecting transparent ultrafiltration permeating liquid, and concentrating the ultrafiltration permeating liquid by adopting a low-temperature vacuum evaporator until the soluble solid substances are 70.0-70.5 Brix to obtain clear orange extract syrup;
the finally obtained clarified orange extract syrup is a concentrated solution containing monosaccharide, disaccharide and organic acid soluble solids, and can be widely applied to the addition of ingredients for the production of seasonings in the food industry, the supply of carbon sources for the processing of brewed products and the like.
C, extracting hesperidin by primary biological enzymolysis: respectively adding softened water 2-3 times (by weight) of the peel pulp into the first leaching tank, the second leaching tank and the third leaching tank after the sugar solution is extracted in the step B, then adding cellulase 0.01-0.03% of the peel pulp, diluting and dissolving the cellulase into cellulase liquid by using softened water 5 times (by weight) before adding the cellulase, circularly heating the leaching solution in the leaching tanks by adopting a plate heat exchanger, and simultaneously fully mixing the cellulase liquid and the leaching solution; stopping circulation when the temperature of the leaching solution reaches 40-50 ℃, standing for enzymolysis for 3-4 h, and separating the leaching solution from three leaching tanks to obtain a primary hesperidin leaching solution;
d, continuously leaching hesperidin with hot water for the second time: after the hesperidin is extracted by the biological enzyme method in the step C, softened water 2 times (by weight) of peel slurry is added into a first leaching tank, the mixture is heated to 90 ℃ by using a plate heat exchanger and is leached for 20min, hot water leaching liquor in the first leaching tank is transferred into a second leaching tank, the temperature in the second leaching tank is controlled to be 85 ℃, the leaching is carried out for 20min, leaching liquor in the second leaching tank is transferred into a third leaching tank, the temperature is controlled to be 85 ℃, the leaching is carried out for 20min, leaching liquor is separated to obtain third hesperidin hot water leaching liquor, and the third hesperidin hot water leaching liquor is mixed with the first hesperidin leaching liquor extracted by the biological enzyme method in the step C to obtain a hesperidin leaching mixed liquor;
filtering the hesperidin leaching mixed solution by using a diatomite filter, removing insoluble impurities, concentrating by using a low-temperature vacuum evaporator, evaporating water by 70-80%, wherein the concentration ratio is 3: 1-5: 1, cooling the concentrated solution to 0-3 ℃, standing for 10 hours, and crystallizing and separating out hesperidin;
taking out the hesperidin crystal, washing with water, dissolving with 20 times (by weight) of 1% food-grade sodium hydroxide solution, and filtering with a 200-mesh filter sieve; adjusting pH to 10 with food-grade acidic pH regulator, and introducing carbon dioxide gas to precipitate hesperidin again to obtain hesperidin extract; filter-pressing and dehydrating by using a filter press, drying by using hot air at the temperature of 70-80 ℃ until the water content is lower than 5%, and crushing to obtain a hesperidin product;
e, extracting pectin: d, adding softened water in an amount which is 2-3 times (by weight) that of the peel pulp into the first leaching tank, the second leaching tank and the third leaching tank after the hesperidin is extracted in the step D, adjusting the pH value to 2 by adopting a food-grade acidic pH regulator, heating to 95-98 ℃, leaching for 60min, and separating out a leaching solution to obtain a pectin leaching stock solution; sequentially washing the fruit peel pulp in the three leaching tanks by softened water, and mixing the recovered washing liquid with the pectin leaching stock solution; outputting the peel pulp in the three leaching tanks to a filter press 26 by a screw pump 6 for squeezing and dewatering, simultaneously recovering a squeezing separation liquid of the peel pulp, and mixing the squeezing separation liquid with the fruit pulp leaching stock solution; mixing the three liquids, and filtering the mixture by using a 120-160-mesh filter sieve to obtain a pectin leaching liquor;
filtering the pectin leaching solution by a diatomite filter to remove insoluble impurities in the pectin leaching solution; then adding 0.1-0.3 wt% of active carbon, and stirring uniformly; controlling the temperature to be 60-65 ℃, standing for 60-90 min, and adsorbing and decoloring;
concentrating the pectin leaching solution by using an ultrafiltration device, separating water in the pectin leaching solution by using an ultrafiltration membrane, and intercepting pectin and active carbon by using the ultrafiltration membrane to obtain pectin concentrated solution containing the active carbon; filtering the pectin concentrated solution again by a diatomite filter to remove active carbon in the pectin concentrated solution to obtain liquid pectin;
slowly adding 90-95% food grade ethanol into the liquid pectin, stirring and adding until the ethanol concentration reaches 50%, standing for 30min to fully precipitate the pectin; taking out the precipitated pectin, crushing, adding 2-3 times (by weight) of 95% food-grade ethanol, and fully washing to remove residual water in the pectin; and (3) drying in vacuum at the temperature of 60-70 ℃, drying until the water content is lower than 10%, crushing, and screening by using a 80-100 mesh screen to obtain the pectin powder.
F, preparing dietary fiber: in the step E, outputting the peel pulp subjected to pectin extraction in the first extraction tank, the second extraction tank and the third extraction tank to a filter press by using a screw pump for squeezing and dewatering, pressing and dewatering the peel pulp by using the filter press to obtain peel wet cakes, and soaking and cleaning the peel wet cakes for 2-3 times by using softened water at the temperature of 50-60 ℃; soaking the raw materials in a 5% hydrogen peroxide solution at normal temperature for 20-30 min for decoloring; then washing with flowing softened water for 5min to remove hydrogen peroxide, and performing filter pressing and dewatering on the citrus peel again to obtain a citrus peel wet filter cake again; crushing the citrus peel wet filter cake, drying until the water content is 6-8%, and then performing activation treatment by adopting a screw extrusion technology to ensure that the citrus peel wet filter cake has biological activity, wherein the extrusion conditions are as follows: feeding water of 191.0g/kg, the terminal temperature of 140 ℃, the screw rotation speed of 60r/min, drying the activated dietary fiber again until the water content is less than 10%, crushing, and sieving by a 120-mesh filter sieve to obtain the dietary fiber.
In the step B, pectinase is adopted to decompose pectin in the water washing immersion liquid, the addition amount of the pectinase is determined through a pectin enzymolysis test, and the test method is as follows:
adding 10ml of acidified alcohol into a test tube, taking 5ml of water-washed sugar solution which is added with pectinase and subjected to enzymolysis for 1h, filtering by using filter paper, putting the filtered sugar solution into the test tube, slightly and vertically inverting the opening of the test tube for 3-5 times to fully mix the contents, judging the degradation degree of the pectin according to the size and the number of flocculation pieces and the speed of precipitation after mixing, indicating that the pectin starts to decompose when a small amount of coagulation occurs after mixing for 30s, standing for 15min, observing, and determining that the pectin decomposition test is negative if no white gel or floccule appears, namely the enzymolysis reaction reaches the end point.
The optimal data obtained by the pectin enzymolysis test is taken as a process guidance parameter. If the amount of pectinase is insufficient, the treatment can be performed by adding pectinase or prolonging the time of enzymolysis. In the subsequent production, the addition amount of pectinase is adjusted according to the change of the material properties, but other process conditions are not changed.
And D, filtering the hesperidin leaching mixed solution by using a diatomite filter to remove insoluble impurities, concentrating the hesperidin leaching mixed solution by using a low-temperature vacuum evaporator, evaporating 70-80% of water, keeping the concentration ratio of 3: 1-5: 1 times, cooling the concentrated solution to 0-3 ℃, standing for 10 hours to crystallize and separate out hesperidin, and discharging residual liquid after recovering crystals after returning the residual liquid to a leaching tank for reuse for 2-3 times, thereby improving the hesperidin leaching yield.
In the step E, an ultrafiltration device is adopted to concentrate the pectin leaching liquor, and the technological parameters of ultrafiltration separation operation are as follows: the aperture of the ultrafiltration membrane is 1-50 nm, the temperature of the feed liquid is 60-65 ℃, the operating pressure is 0.50-0.56 Mpa, and the circulation volume of the ultrafiltration feed liquid is 8-12 times of the ultrafiltration separation capacity; separating water in the pectin leaching solution through an ultrafiltration membrane, intercepting pectin and active carbon by the ultrafiltration membrane to form pectin concentrated solution containing the active carbon, and filtering the pectin concentrated solution again through a diatomite filter to remove the active carbon in the pectin concentrated solution to obtain liquid pectin; the quality of pectin products is greatly improved by adopting a process combining activated carbon adsorption decoloration and ultrafiltration concentration.
The device can be used for progressively extracting the effective components of any one of citrus, orange, grapefruit and lemon; the fruit peel can be fresh squeezed fruit peel or dried fruit peel.
The utility model has the advantages that: by gradually extracting citrus fruits, peel essential oil, fruit juice, fruit seeds, citrus immersion syrup, hesperidin, pectin and dietary fiber products are sequentially obtained, the citrus peel is continuously extracted, and continuous extraction of citrus peel washing syrup, hesperidin and pectin substances can be gradually completed under the condition that the citrus peel does not need to be transferred and conveyed for multiple times; compared with the traditional device, need not the multiple transfer of oranges and tangerines peel to carry and squeeze the dehydration operation several times at the extraction process, turn into the complicated extraction operation of tradition portably, serialization, systematization, reduce repetition work by a wide margin, reduced power and energy resource consumption, also reduced the material loss of course of working by a wide margin, shorten product processing operation cycle simultaneously, have fine economic benefits, have very important strategic meaning to promoting the continued economic development of our country's oranges and tangerines industry.
This device has adopted three leaching tanks, can leach in proper order at normal atmospheric temperature and retrieve the oranges and tangerines peel extraction sugar liquid, and the leaching can be guaranteed under the normal atmospheric temperature condition that the extraction process can not produce showing the influence to oranges and tangerines fruit cortex structure change.
The device can meet various different process requirements of each step through conversion of the pipeline switching plate connecting pipeline and automatic valve conversion, and can also upgrade the connecting pipeline into full-automatic control, so that the process operation is simplified, and the production efficiency is greatly improved.
The in-process that the kernel separator of this device can realize the oranges and tangerines kernel and carry at a kernel separation sieve section of thick bamboo, utilizes helical blade's the produced stirring effect of continuous rotation and centrifugal action, and the oranges and tangerines kernel separates from the oranges and tangerines peel gradually to on the kernel sieve mesh through a kernel separation sieve section of thick bamboo falls the kernel collecting plate, collect and obtain the oranges and tangerines kernel through the kernel collecting vat. The citrus fruit kernels recovered from citrus fruits can be used as raw materials for food industry or other industrial processing after washing and drying, and the dried citrus fruit kernels have the oil content of 20-25 percent and multiple purposes.
The device can realize the combined process of leaching liquor circulation and secondary leaching, greatly improve the concentration of soluble solid matters in the leaching liquor, save the heat energy consumption when the leaching liquor is evaporated and concentrated, and greatly improve the operating efficiency. Meanwhile, the discharge concentration of organic matters in the production discharge water is greatly reduced, so that the sewage treatment operation cost in production is effectively reduced, the citrus peel is gradually extracted, a rich and thick valuable product is obtained, the total utilization of the citrus peel is realized, and the environmental pollution risk caused by poor management of the citrus peel is eliminated.
The device realizes that essential oil of citrus peel and important substances of citrus fruit kernels can be obtained in the pretreatment process of the citrus peel by adopting a technology combining graded recovery and progressive extraction; products with high added values such as citrus extract syrup, hesperidin, pectin and the like can be obtained in the progressive extraction process, new resources are developed for the development of the food processing industry, and the recycling of the effective components of citrus peel is really realized from the aspect of resource utilization.
Drawings
Fig. 1 is a schematic structural diagram of the present invention;
fig. 2 is a schematic structural view of the kernel separator of the present invention.
Parts and numbering in the figures:
1-a kernel separation device; 2-orange peel grinding machine; 3-a juice extractor; 4-a peel crusher; 5-peel pulp tank; 6-screw pump; 11-a kernel separation screen drum; 12-a helical blade; 13-a rotating shaft; 14-a drive motor; 15-kernel collection plate; 16-kernel sieve mesh; 17-peel feed inlet; 18-peel discharge port; 19-kernel collection tank; 20-a spray pipe; 21-plate heat exchanger; 22-pipeline switching plate; 23-diatomaceous earth filter; 24-an ultrafiltration device; 25-low temperature vacuum evaporator; 26-a filter press; 27-a dryer; 28-screw extruder; 111-storage tank group; 101-a first leaching tank; 102-a second leach tank; 103-a third leaching tank; 222-a water inlet pipe; 300-a filter screen plate; 333-conical filter screen plate; 600-centrifugal pump.
Detailed Description
As shown in fig. 1, a citrus peel gradual extraction device comprises a citrus peel pretreatment system and a citrus peel gradual extraction system;
the orange peel pretreatment system comprises a kernel separation device 1, an orange peel grinding machine 2, a juice extractor 3, a peel crusher 4, a peel slurry tank 5 and a screw pump 6; the fruit peel outlet of the juice extractor 3 is arranged above the feed inlet of the kernel separation device 1; the discharge hole of the kernel separation device 1 is arranged above the feed hole of the peel crusher 4; the discharge hole of the peel crusher 4 is arranged above the feed hole of the peel pulp tank 5; the screw pump 6 is connected to a conveying pipeline at a discharge port at the bottom of the peel pulp tank 5;
the citrus peel progressive extraction system comprises a first leaching tank 101, a second leaching tank 102, a third leaching tank 103, a storage tank group 111, a plate heat exchanger 21, a pipeline switching plate 22, a diatomite filter 23, an ultrafiltration device 24, a low-temperature vacuum evaporator 25, a filter press 26, a dryer 27 and a screw extruder 28;
the discharge port of the peel pulp tank 5 is respectively connected with the tank tops of a first leaching tank 101, a second leaching tank 102 and a third leaching tank 103 through a conveying pipe provided with a screw pump 6;
the bottoms of the first leaching tank 101, the second leaching tank 102 and the third leaching tank 103 are respectively connected to the storage tank group 111 through conveying pipelines, and the conveying pipelines are also provided with three-way valves and bypass pipes which are respectively connected to the plate heat exchanger 21 and the pipeline switching plate 22;
the storage tank group 111 is connected with an ultrafiltration device 24, a low-temperature vacuum evaporator 25, a diatomite filter 23 and a filter press 26 through a conveying pipeline; the pipeline switching plate 22 is connected with the plate heat exchanger 21 through a conveying pipeline; the transfer pipe is provided with a centrifugal pump 600.
The first leaching tank 101, the second leaching tank 102 and the third leaching tank 103 are respectively provided with a water inlet pipe 222 with a spray head.
The process requirements of each component extraction step can be met by the conveying of the leaching liquor through the conversion of the pipeline switching plate 22 and the automatic valve conversion, and the dryer 27 and the screw extruder 28 are combined to form the citrus peel dietary fiber puffing treatment system.
As shown in fig. 2, the kernel separating device 1 comprises a kernel separating screen drum 11, a helical blade 12, a rotating shaft 13, a driving motor 14 and a kernel collecting plate 15; the driving motor 14 is connected with the helical blade 12 positioned in the kernel separation screen drum 11 through the rotating shaft 13, and a kernel screen hole 16 for separating kernels is formed in the lower drum body of the kernel separation screen drum 11; an arc-shaped kernel collecting plate 15 is arranged below the kernel separating screen cylinder 11, one end of the kernel separating screen cylinder 11 is provided with a peel feeding hole 17, the other end of the kernel separating screen cylinder is provided with a peel discharging hole 18, the left end part of the kernel collecting plate 15 is provided with a kernel collecting tank 19, and a spraying pipe 20 for washing is arranged between the kernel separating screen cylinder 11 and the kernel collecting plate 15.
During the conveying process of the kernel separation screen drum 11, the citrus kernels are gradually separated from the citrus peels by utilizing the stirring effect and the centrifugal effect generated by the continuous rotation of the helical blades, fall onto the kernel collecting plate 15 through the kernel screen holes 16 at the lower part of the kernel separation screen drum 11, and are collected by the kernel collecting tank 19 to obtain the citrus kernels; citrus fruit kernels separated and recovered from citrus peel.
The kernel separation screen drum 11 of the kernel separation device 1 is formed by obliquely arranging a peel discharge port 18 end higher than a peel feed port 17 end, and the preferred inclination angle is 45-60 degrees; under the stirring effect and the centrifugal action that helical blade's continuous rotation produced, the oranges and tangerines kernel is separated from the oranges and tangerines peel gradually, and the oranges and tangerines kernel gathers in the bottom of a kernel separation sieve section of thick bamboo 11 under the action of gravity, falls to the kernel collecting plate 15 through the kernel sieve mesh 16 on the oranges and tangerines kernel separation sieve section of thick bamboo 11 on, sprays the oranges and tangerines kernel on the kernel collecting plate 15 through shower 20 and makes its action of gravity enter into in the kernel collecting vat 19 and obtain the collection.
The kernel collecting plate 15 is arc-shaped and parallel to the kernel separating screen drum 11, so that the citrus kernels can completely fall into the kernel collecting plate 15 after passing through the kernel screen holes 16 and are not easy to scatter.
The arc-shaped kernel collecting plate 15 covers the aperture area of the kernel screen hole 16 of the lower cylinder of the kernel separating screen cylinder 11, when the citrus kernels pass through the kernel screen hole 16 and then fall onto the kernel collecting plate 15, the centralized collection of the citrus kernels is facilitated, and the phenomenon that the citrus kernels are scattered outside the kernel collecting plate 15 can not occur.
The tank bottoms of the first leaching tank 101, the second leaching tank 102 and the third leaching tank 103 are conical, a conical filtering screen plate 333 is arranged in the tank bottom, a distance is arranged between the conical filtering screen plate 333 and the conical tank bottom, and preferably, the conical filtering screen plate 333 is parallel to the conical tank bottom, and the distance is 60-90 mm. The chamber formed between the two provides a liquid level buffer space for the transmission of the leaching liquor, and when the leaching liquor separated from the tank bottom is filtered by the conical filter screen plate 333, the output of granular peel in the leaching liquor is intercepted, and the citrus peel is limited from entering the citrus peel leaching liquor. The chamber formed between the two provides a liquid level buffer space for the transmission of the leaching liquor, and when the leaching liquor separated from the tank bottom is filtered by the conical filter screen plate 333, the output of granular peel in the leaching liquor is intercepted, and the citrus peel is limited from entering the citrus peel leaching liquor.
The upper parts of the first leaching tank 101, the second leaching tank 102 and the third leaching tank 103 are respectively provided with a filter screen plate 300, the aperture of meshes of the filter screen plate 300 is 10-16 mm, and the filter screen plate 300 limits the citrus peel to float upwards so as to ensure that the peel pulp is leached effectively.
The present invention will be further explained with reference to the drawings and examples.
Example 1
As shown in fig. 1, a citrus peel pretreatment system is used for pretreatment of citrus peel: the method comprises the steps of citrus peel essential oil extraction, citrus juicing, kernel separation and citrus peel crushing, and comprises the following specific steps:
a1 extraction of essential oil from pericarp: peeling citrus fruits by using a citrus peeling machine 2, destroying tissue cells on the surface of citrus peel, fully releasing peel essential oil from the peel cells, recovering an emulsion containing the peel essential oil, and centrifugally separating the emulsion containing the peel essential oil to obtain citrus peel cold pressing essential oil; by separating and recycling the peel essential oil, the citrus peel essential oil can be prevented from entering the citrus peel leaching liquor to cause adverse effects on subsequent product processing and product quality;
a2 orange juicing: juicing the citrus after removing the peel essential oil in the step A1 by using a juicer 3, wherein the obtained citrus juice is used for processing citrus juice;
a3 kernel separation: the citrus peels juiced from the citrus in the step A2 enter the citrus kernel separation device 1 for kernel separation, the citrus kernels and the citrus peels are separated by stirring and centrifuging generated by the rotation of the helical blades 12 in the kernel separation screen cylinder 11, and the citrus kernels fall into the kernel collection plate 15 through the kernel screen holes 16 at the lower part of the kernel separation screen cylinder 11 for collection, so that the citrus kernels in the citrus peels are removed; collecting and washing the separated citrus fruit stones, soaking the fruit stones for 5min at normal temperature by using 5% hydrogen peroxide, then washing the fruit stones for 5min by using flowing softened water to remove the hydrogen peroxide, and drying the fruit stones until the water content is 8% -10% to obtain the citrus fruit stones; the citrus kernels are separated in the step, so that adverse effects on subsequent product processing and product quality can be avoided;
a4 pericarp breaking: the citrus peel separated from the fruit kernels in the step A3 is crushed by the peel crusher 4, the same amount of softened water is sprayed into the peel crusher 4 while the citrus peel is crushed, the crushed particle size of the citrus peel is 10-18 mm, the crushed citrus peel is changed into fruit peel pulp, and the softened water is sprayed while the citrus peel is crushed, so that the orange peel crushing operation is facilitated, and meanwhile, the flowability of the fruit peel pulp is also improved.
Example 2
As shown in fig. 2, the citrus peel is subjected to progressive extraction by a citrus peel progressive extraction system to sequentially obtain citrus extract syrup, hesperidin, pectin and dietary fiber products, and the specific process steps of the citrus peel progressive extraction are as follows:
a, pretreatment of citrus peel: the peel pulp pretreated with the citrus peel of example 1 is transferred to a first leaching tank 101, a second leaching tank 102, and a third leaching tank 103, respectively;
b, extracting citrus extract syrup: adding softened water 2-3 times (by weight) of the peel pulp into the first leaching tank 101, completely immersing the peel pulp in the softened water, and standing and leaching for 20 min; transferring the leach liquor in the first leach tank 101 to the second leach tank 102 and leaving the leached pericarp slurry in the second leach tank 102 for 20 min; transferring the leaching liquor in the second leaching tank 102 to a third leaching tank 103 for standing and leaching the peel pulp for 20 min; collecting the leaching liquor in the third leaching tank 103, coarsely filtering by using a 120-160-mesh filter screen, and removing suspended peel and pulp impurities in the leaching liquor to obtain a citrus peel washing sugar liquor;
pasteurizing the citrus peel water-washing sugar solution by adopting a plate heat exchanger 21, controlling the sterilization temperature to be 90-93 ℃ and the sterilization time to be 15-20 s, controlling the outlet temperature of the citrus peel water-washing sugar solution to be 50-55 ℃, adding 0.03-0.06 wt% of active carbon into the citrus peel water-washing sugar solution for decoloring, and simultaneously adding pectinase, wherein the pectinase is obtained by dissolving pectinase dry powder in softened water by 5 times in advance, keeping the temperature to be 50-55 ℃ and carrying out enzymolysis for 40-60 min, and decomposing pectin in the citrus peel water-washing sugar solution; when the pectin enzymolysis test is negative, the enzymolysis reaches the end point, and the enzymolysis is stopped; when the enzymolysis reaches the end point, the suspended matters in the citrus peel washing sugar solution are mutually adsorbed and flocculated, and precipitate is formed and settled at the bottom, so that the citrus peel washing sugar solution is clarified;
taking out supernatant of the orange peel washing sugar solution after enzymolysis, separating suspended pulp and high molecular polymers in the orange peel washing sugar solution by using an ultrafiltration device 24, wherein the aperture of an ultrafiltration membrane core is 1-50 nm, the temperature is 50-55 ℃, the operating pressure is 0.50-0.56 Mpa, the circulation volume of ultrafiltration liquid is 8-12 times of the ultrafiltration separation capacity, water, monosaccharide, disaccharide and organic acid soluble solid substances penetrate through an ultrafiltration membrane, collecting transparent ultrafiltration permeate, and concentrating the permeate to a soluble solid substance of 70.0-70.5 Brix by using a low-temperature vacuum evaporator 25 to obtain clarified orange extract syrup;
the finally obtained clarified orange extract syrup is a concentrated solution containing monosaccharide, disaccharide and organic acid soluble solids, and can be widely applied to the addition of ingredients for the production of seasonings in the food industry, the supply of carbon sources for the processing of brewed products and the like.
C, extracting hesperidin by primary biological enzymolysis: respectively adding softened water 2-3 times (by weight) of the peel pulp into the first leaching tank 101, the second leaching tank 102 and the third leaching tank 103 after the sugar solution is extracted in the step B, then adding cellulase 0.01-0.03% of the peel pulp, diluting and dissolving the cellulase into cellulase liquid by using softened water 5 times (by weight) before adding the cellulase, circularly heating the leaching solution in the leaching tanks by adopting a plate heat exchanger 21, and simultaneously fully mixing the cellulase liquid and the leaching solution; stopping circulation when the temperature of the leaching solution reaches 40-50 ℃, standing for enzymolysis for 3-4 h, and separating the leaching solution from three leaching tanks to obtain a primary hesperidin leaching solution;
d, continuously leaching hesperidin with hot water for the second time: after the hesperidin is extracted by the biological enzyme method in the step C, softened water 2 times (by weight) of peel slurry is added into a first leaching tank 101, the mixture is heated to 90 ℃ by using a plate heat exchanger 21 and is leached for 20min, hot water leaching liquor in the first leaching tank 101 is transferred into a second leaching tank 102, the temperature in the second leaching tank 102 is controlled to be 85 ℃ and is leached for 20min, leaching liquor in the second leaching tank 102 is transferred into a third leaching tank 103, the temperature is controlled to be 85 ℃ and is leached for 20min, leaching liquor is separated to obtain third hesperidin hot water leaching liquor, and the third hesperidin hot water leaching liquor is mixed with the first hesperidin leaching liquor extracted by the biological enzyme method in the step C to obtain a hesperidin leaching mixed liquor;
filtering the hesperidin leaching mixed solution by a diatomite filter 23, removing insoluble impurities, concentrating by using a low-temperature vacuum evaporator 25, evaporating 70-80% of water, wherein the concentration ratio is 3: 1-5: 1, cooling the concentrated solution to 0-3 ℃, standing for 10 hours, and crystallizing and separating out hesperidin;
taking out the hesperidin crystal, washing with water, dissolving with 20 times (by weight) of 1% food-grade sodium hydroxide solution, and filtering with a 200-mesh filter sieve; adjusting pH to 10 with food-grade acidic pH regulator, and introducing carbon dioxide gas to precipitate hesperidin again to obtain hesperidin extract; performing filter pressing and dehydration by using a filter press 26, drying by using hot air at the temperature of 70-80 ℃ until the water content is lower than 5%, and crushing to obtain a hesperidin product;
e, extracting pectin: d, adding softened water with the weight 2-3 times that of the peel pulp into the first leaching tank 101, the second leaching tank 102 and the third leaching tank 103 after the hesperidin is extracted, adjusting the pH value to 2 by adopting a food-grade acidic pH regulator, heating to 95-98 ℃, leaching for 60min, and separating out a leaching solution to obtain a pectin leaching stock solution; sequentially washing the fruit peel pulp in the three leaching tanks by softened water, and mixing the recovered washing liquid with the pectin leaching stock solution; outputting the peel pulp in the three leaching tanks to a filter press 26 by a screw pump 6 for squeezing and dewatering, simultaneously recovering a squeezing separation liquid of the peel pulp, and mixing the squeezing separation liquid with the fruit pulp leaching stock solution; mixing the three liquids, and performing coarse filtration by using a 120-160-mesh filter screen to obtain a pectin leaching liquor;
filtering the pectin leaching solution by a diatomite filter 23 to remove insoluble impurities in the pectin leaching solution; then adding 0.1-0.3 wt% of active carbon, and stirring uniformly; controlling the temperature to be 60-65 ℃, standing for 60-90 min, and adsorbing and decoloring;
concentrating the pectin leaching solution by using an ultrafiltration device 24, wherein water in the pectin leaching solution is separated by an ultrafiltration membrane, and pectin and active carbon are intercepted by the ultrafiltration membrane to form pectin concentrated solution containing active carbon; filtering the pectin concentrated solution again by a diatomite filter 23 to remove active carbon in the pectin concentrated solution to obtain liquid pectin;
slowly adding 90-95% food grade ethanol into the liquid pectin, stirring and adding until the ethanol concentration reaches 50%, standing for 30min to fully precipitate the pectin; taking out the precipitated pectin, crushing, adding 2-3 times (by weight) of 95% food-grade ethanol, and fully washing to remove residual water in the pectin; and (3) drying in vacuum at the temperature of 60-70 ℃, drying until the water content is lower than 10%, crushing, and screening by using a 80-100 mesh screen to obtain the pectin powder.
F, preparing dietary fiber: in the step E, the peel pulp which is subjected to pectin extraction in the first leaching tank 101, the second leaching tank 102 and the third leaching tank 103 is output to a filter press 26 by a screw pump 6 for squeezing and dewatering, the peel pulp which is squeezed and dewatered by the filter press 26 becomes peel wet cake, and the peel wet cake is soaked and cleaned for 2-3 times by softened water at 50-60 ℃; soaking the raw materials in a 5% hydrogen peroxide solution at normal temperature for 20-30 min for decoloring; then washing with flowing softened water for 5min to remove hydrogen peroxide, and performing filter pressing and dewatering on the citrus peel again to obtain a citrus peel wet filter cake again; crushing the citrus peel wet filter cake, drying until the water content is 6-8%, and then performing activation treatment by adopting a screw extrusion technology to ensure that the citrus peel wet filter cake has biological activity, wherein the extrusion conditions are as follows: feeding water of 191.0g/kg, the terminal temperature of 140 ℃, the screw rotation speed of 60r/min, drying the activated dietary fiber again until the water content is less than 10%, crushing, and sieving by a 120-mesh filter sieve to obtain the dietary fiber.
In the step B, pectinase is adopted to decompose pectin in the water washing immersion liquid, the addition amount of the pectinase is determined through a pectin enzymolysis test, and the test method is as follows:
adding 10ml of acidified alcohol into a test tube, taking 5ml of water-washed sugar solution which is added with pectinase and subjected to enzymolysis for 1h, filtering by using filter paper, putting the filtered sugar solution into the test tube, slightly and vertically inverting the opening of the test tube for 3-5 times to fully mix the contents, judging the degradation degree of the pectin according to the size and the number of flocculation pieces and the speed of precipitation after mixing, indicating that the pectin starts to decompose when a small amount of coagulation occurs after mixing for 30s, standing for 15min, observing, and determining that the pectin decomposition test is negative if no white gel or floccule appears, namely the enzymolysis reaction reaches the end point.
The optimal data obtained by the pectin enzymolysis test is taken as a process guide parameter, and if the addition amount of the pectinase is insufficient, the correction can be carried out by adding the pectinase or prolonging the enzymolysis time. In the subsequent production, the addition amount of pectinase is adjusted according to the change of the material properties, but other process conditions are not changed.
In the step D, filtering the hesperidin extraction mixed solution by a diatomite filter 23, removing insoluble impurities, concentrating the hesperidin extraction mixed solution by using a low-temperature vacuum evaporator 25, evaporating 70-80% of water, enabling the concentration ratio to be 3: 1-5: 1, cooling the concentrated solution to 0-3 ℃, standing for 10 hours to crystallize and separate out hesperidin, returning residual liquid after recovering crystals to an extraction tank for repeated use for 2-3 times, and discharging to improve the hesperidin extraction yield.
In the step E, an ultrafiltration device 24 is adopted to concentrate the pectin leaching liquor, and the ultrafiltration separation operation process parameters are as follows: the aperture of the ultrafiltration membrane is 1-50 nm, the temperature of the feed liquid is 60-65 ℃, the operating pressure is 0.50-0.56 Mpa, and the circulation volume of the ultrafiltration feed liquid is 8-12 times of the ultrafiltration separation capacity; separating water in the pectin leaching solution through an ultrafiltration membrane, intercepting pectin and active carbon by the ultrafiltration membrane to form pectin concentrated solution containing the active carbon, and filtering the pectin concentrated solution again through a diatomite filter 23 to remove the active carbon in the pectin concentrated solution to obtain liquid pectin; the quality of pectin products is greatly improved by adopting a process combining activated carbon adsorption decoloration and ultrafiltration concentration.
The device can be used for progressively extracting the effective components of any one of citrus, orange, grapefruit and lemon; the fruit peel can be fresh squeezed fruit peel or dried fruit peel.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those skilled in the art; the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; such modifications and substitutions do not depart from the spirit and scope of the present invention in its corresponding aspects.

Claims (8)

1. A citrus peel gradual extraction device is characterized by comprising a citrus peel pretreatment system and a citrus peel gradual extraction system;
the orange peel pretreatment system comprises a kernel separation device (1), an orange peel grinding machine (2), a juice extractor (3), a peel crusher (4), a peel pulp tank (5) and a screw pump (6); the fruit peel outlet of the juice extractor (3) is arranged above the feed inlet of the kernel separation device (1); the discharge hole of the kernel separation device (1) is arranged above the feed hole of the peel crusher (4); the discharge hole of the peel crusher (4) is arranged above the feed hole of the peel pulp tank (5); the screw pump (6) is connected to a conveying pipeline at a discharge port at the bottom of the peel pulp tank (5);
the citrus peel progressive extraction system comprises a first extraction tank (101), a second extraction tank (102), a third extraction tank (103), a storage tank group (111), a plate heat exchanger (21), a pipeline switching plate (22), a diatomite filter (23), an ultrafiltration device (24), a low-temperature vacuum evaporator (25), a filter press (26), a dryer (27) and a screw extruder (28); the discharge port of the peel pulp tank (5) is respectively connected with the tank tops of the first leaching tank (101), the second leaching tank (102) and the third leaching tank (103) through a conveying pipe provided with a screw pump (6);
the bottoms of the first leaching tank (101), the second leaching tank (102) and the third leaching tank (103) are respectively connected to the storage tank group (111) through conveying pipelines, and the conveying pipelines are also provided with three-way valves and bypass pipes which are respectively connected to the plate heat exchanger (21) and the pipeline switching plate (22);
the storage tank group (111) is connected with the ultrafiltration device (24), the low-temperature vacuum evaporator (25), the diatomite filter (23) and the filter press (26) through a conveying pipeline; the pipeline switching plate (22) is connected with the plate heat exchanger (21) through a conveying pipeline; the conveying pipeline is provided with a centrifugal pump (600);
the first leaching tank (101), the second leaching tank (102) and the third leaching tank (103) are respectively provided with a water inlet pipe (222) with a spray head.
2. The progressive citrus peel extraction device as recited in claim 1, wherein said kernel separation device
(1) Comprises a kernel separation screen cylinder (11), a helical blade (12), a rotating shaft (13), a driving motor (14) and a kernel collecting plate (15); the driving motor (14) is connected with a helical blade (12) positioned in the kernel separation screen drum (11) through a rotating shaft (13), and a kernel screen hole (16) for separating kernels is formed in a drum body at the lower part of the kernel separation screen drum (11); an arc-shaped kernel collecting plate (15) is arranged below the kernel separating screen drum (11), one end of the kernel separating screen drum (11) is provided with a peel feeding hole (17), the other end of the kernel separating screen drum is provided with a peel discharging hole (18), the left end part of the kernel collecting plate (15) is provided with a kernel collecting tank (19), and a spraying pipe (20) for washing is arranged between the kernel separating screen drum (11) and the kernel collecting plate (15).
3. The progressive citrus peel extraction device as recited in claim 2, wherein said kernel separation device
(1) The fruit-stone separating screen cylinder (11) is arranged in a way that the end of a peel discharge hole (18) is higher than the end of a peel feed hole (17) in an inclined way
The oblique angle is 45-60 degrees.
4. The progressive citrus peel extraction device as recited in claim 2, wherein said stone collector plate is configured to collect stones
(15) Is arc-shaped and is parallel to the kernel separating screen cylinder (11).
5. The progressive citrus peel extraction device as recited in claim 4, wherein said arcuate kernel is curved
The collecting plate (15) covers the opening area of the kernel sieve pore (16) of the cylinder body at the lower part of the kernel separating sieve cylinder (11).
6. A citrus peel progressive extraction device as claimed in any one of claims 1 to 5, characterised in that said first step
The bottom of the first leaching tank (101), the bottom of the second leaching tank (102) and the bottom of the third leaching tank (103) are conical, a conical filter screen plate (333) is arranged in the bottom of the tank, and a space is arranged between the conical filter screen plate (333) and the conical tank bottom.
7. The progressive citrus peel extraction device as recited in claim 6, wherein said first extraction tank
(101) The second leaching tank (102) and the third leaching tank (103) are provided with a conical filter screen plate (333) which is parallel to the conical tank bottom, and the distance is 60-90 mm.
8. A device as claimed in any one of claims 1 to 5, wherein the first stage is a citrus peel progressive extraction device
The upper parts of the leaching tank (101), the second leaching tank (102) and the third leaching tank (103) are respectively provided with a filter screen plate
(300) The aperture of the mesh of the filter screen plate (300) is 10-16 mm.
CN202022795384.4U 2020-11-27 2020-11-27 Citrus peel progressive extraction device Active CN213965259U (en)

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