WO2018196476A1 - 一种鲜罗汉果脱色浓缩汁的制备工艺 - Google Patents

一种鲜罗汉果脱色浓缩汁的制备工艺 Download PDF

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WO2018196476A1
WO2018196476A1 PCT/CN2018/077304 CN2018077304W WO2018196476A1 WO 2018196476 A1 WO2018196476 A1 WO 2018196476A1 CN 2018077304 W CN2018077304 W CN 2018077304W WO 2018196476 A1 WO2018196476 A1 WO 2018196476A1
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resin
liquid
membrane
column
han guo
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PCT/CN2018/077304
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French (fr)
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黄华学
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广西甙元植物制品有限公司
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    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
    • A23L2/00—Non-alcoholic beverages; Dry compositions or concentrates therefor; Their preparation
    • A23L2/02—Non-alcoholic beverages; Dry compositions or concentrates therefor; Their preparation containing fruit or vegetable juices
    • A23L2/04—Extraction of juices
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
    • A23L2/00—Non-alcoholic beverages; Dry compositions or concentrates therefor; Their preparation
    • A23L2/02—Non-alcoholic beverages; Dry compositions or concentrates therefor; Their preparation containing fruit or vegetable juices
    • A23L2/08—Concentrating or drying of juices
    • A23L2/082—Concentrating or drying of juices by membrane processes
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
    • A23L2/00—Non-alcoholic beverages; Dry compositions or concentrates therefor; Their preparation
    • A23L2/70—Clarifying or fining of non-alcoholic beverages; Removing unwanted matter
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
    • A23L2/00—Non-alcoholic beverages; Dry compositions or concentrates therefor; Their preparation
    • A23L2/70—Clarifying or fining of non-alcoholic beverages; Removing unwanted matter
    • A23L2/72—Clarifying or fining of non-alcoholic beverages; Removing unwanted matter by filtration
    • A23L2/74—Clarifying or fining of non-alcoholic beverages; Removing unwanted matter by filtration using membranes, e.g. osmosis, ultrafiltration
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
    • A23L2/00—Non-alcoholic beverages; Dry compositions or concentrates therefor; Their preparation
    • A23L2/70—Clarifying or fining of non-alcoholic beverages; Removing unwanted matter
    • A23L2/80—Clarifying or fining of non-alcoholic beverages; Removing unwanted matter by adsorption
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
    • A23L33/00—Modifying nutritive qualities of foods; Dietetic products; Preparation or treatment thereof
    • A23L33/10—Modifying nutritive qualities of foods; Dietetic products; Preparation or treatment thereof using additives
    • A23L33/105—Plant extracts, their artificial duplicates or their derivatives

Definitions

  • the invention relates to the extraction of plant active ingredients, in particular to a production process of fresh Luo Han Guo decolorized concentrated juice.
  • Mangosteen As a plant species with homologous medicine and food, Mangosteen has special flavor and nutrients, as well as a unique taste.
  • the sweet component of fresh mangosteen is mainly triterpenoid saponin non-sugar sweet component: represented by Mogroside V and IV, the sweetness of glycoside V is 256-344 times that of sucrose, and the sweetness of IV is sucrose. 126 times, and the heat is only 1/50 of sucrose; another contains D-mannitol, which has a sweetness of 0.55-0.65 times that of sucrose.
  • fresh Luo Han Guo also contains a lot of glucose (glucose), fructose (fructose) and other sweet components; protein, amino acids, a small amount of flavonoids; also contains manganese, iron, nickel, selenium, tin, iodine, molybdenum and other 26 inorganic elements, Vitamin C (Vitamin C) and the like. Therefore, the deep processing of Luo Han Guo has attracted wide attention from scholars at home and abroad. At present, there are many research and development and production techniques for fresh mangosteen juice concentrate, but there are three main representative technologies:
  • the technology firstly breaks the fresh mangosteen fruit, and repeatedly soaks it with water of 40-95 ° C for 6-16 hours.
  • the filtrate is filtered by pretreatment, the temperature is lowered to 25-55 ° C, and the filtrate is pressed by a pressure pump at a pressure of 0.05-3.0 MPa. It is sequentially fed into the integrated membrane combination system, and is separated, purified and concentrated by microfiltration (MF), ultrafiltration (UF), reverse osmosis (RO), etc., to finally obtain 16-35 Baume of fresh Luo Han Guo concentrate. product.
  • MF microfiltration
  • UF ultrafiltration
  • RO reverse osmosis
  • the technology adopts the selected material and pretreatment, the cation column, the decolorization, the first acidification, the concentration and the second acidification, and the decolorized Luo Han Guo juice is white or yellowish transparent liquid, and the Baume degree is 10 or more or white.
  • the sugar content is above 60, and the composition of the juice is calculated by dry weight, wherein the content of the sweetmein is ⁇ 30%.
  • One of the techniques will wash the fresh fruit of Luo Han Guo and crush it to make a result. Then adjust the pH and temperature of the pulp, add the immobilized pulp enzyme, the pulp enzyme not only decomposes the pectin trunk, but also hydrolyzes the methyl galactonic acid residue in the pectin, lysing the plant cell wall, releasing more Juice while clarifying the juice. Then, the juice is ultrafiltered, deodorized, concentrated, sterilized, and packaged to obtain Luo Han Guo concentrated juice.
  • the second technique uses a screw press to crush fresh mangosteen, and the crushed fresh mangosteen fruit is digested and extracted by a four-stage cooking process, and the pectin in the steamed juice is hydrolyzed and precipitated by using a composite enzyme to clarify the juice and then use the juice.
  • the plate-frame diatomaceous earth filter press filters the clarified juice, sterilizes the juice by high-temperature instant sterilization, and concentrates the juice to 25Be by centrifugal film method and vacuum concentration pot, and finally cools the finished product to room temperature for packaging. .
  • the technology comprises three centrifugal filtration separation, combining three times separated juice, heating boiling to denature protein precipitation, removing odor precursor substance, plate and frame pressure filtration, adding preservative, microporous membrane filtration, nanofiltration concentration and the like.
  • the method uses a sterilized washing liquid with a pH of 11, 12 to wash the green hair of the fresh mangosteen skin, and then rinse it with deionized water or water. When the pH of the rinsed deionized water or clean water is 7, can. The washed Luo Han Guo is then broken into pieces. The crushed mangosteen is mixed with the formulation and water in a weight ratio of 1:1, 1.5, and 2.
  • the object of the present invention is to overcome the deficiencies of the prior art, and to provide a production process of fresh Luo Han Guo decolorized concentrated juice; the process can produce high quality fresh Luo Han Guo decolorized concentrated juice product, the product is colorless and transparent, and the mouthfeel is excellent. No post-precipitation.
  • a production process of fresh Luo Han Guo decolorized concentrated juice comprising the following steps:
  • Luo Han Guo Take the newly purchased fresh and mature Luo Han Guo, put it into the raw material warehouse in a basket, close the doors and windows, leave only a small amount of vents open, and let it stand for 7 to 10 days.
  • the fresh Luo Han Guo epidermis turns from greenish green to green bean yellow, and the flesh can be licked.
  • the saccharification is completed;
  • the washed fresh Luo Han Guo is placed in a special Luo Han Guo feeding machine, and is lifted to the top of the multifunctional extraction tank by a conveyor belt.
  • Pre-purified water is added to the multi-functional extraction tank, and the fresh Luo Han Guo crushed material is continuously crushed by the Luo Han Guo special crusher under constant stirring.
  • the stirring is continued for 5 min, and then the standing temperature is allowed to stand for 20 min, that is, the discharging is started; when the discharging speed is decreased to 1/3 of the initial discharging speed, the purified water is additionally added, and the purified water is discharged while the percolation is extracted.
  • the dregs are transported to the extraction station via a conveyor belt to completely extract the mogroside. Collect all the discharge liquid to obtain the percolate extract;
  • the percolation extract is piped to the centrifugal station, centrifuged by a disc centrifuge, and the centrifugal slag is discarded to obtain a disc centrifuge containing turbidity without obvious impurities and precipitation;
  • the ceramic membrane clear liquid is pumped into the upstream tank of the ultrafiltration membrane, and the ultrafiltration membrane complete equipment is operated to collect the ultrafiltration membrane liquid;
  • the ultrafiltration membrane liquid is pumped into the high-position tank of the polyamide resin chromatography column, and the feed rate of the high-position tank and the discharge rate of the chromatography column are controlled to be 2.0-3.0 BV/h, and the resin column of the polyamide resin is decolored, and after the completion of the preparation. , further purifying the column with resin 2BV, combining the feed effluent and the water washing liquid to obtain a polyamide resin decolorizing liquid;
  • the polyamide resin decolorizing liquid is pumped into the high-position tank of the decolorizing resin column, and the high-level tank feeding and the column discharge flow rate are controlled to 2.0-3.0 BV/h, and the resin column loaded with the anionic decolorizing resin is decolored, and after the material is finished , further purifying the column with resin 2BV, combining the feed effluent and the water washing liquid to obtain a decolorizing resin decolorizing liquid;
  • the decolorizing resin decoloring liquid is pumped into the high-position tank of the cationic resin chromatography column, and the appropriate flow rate is controlled, and the pH adjusting liquid is obtained through a chromatography column packed with a cationic resin;
  • the pH adjustment liquid is pumped into the upstream tank of the reverse osmosis membrane, and the reverse osmosis membrane complete equipment is operated, and the membrane is concentrated under normal temperature and normal pressure to remove most of the water to obtain a membrane concentrate.
  • the membrane concentrate is pumped into a high-position tank of granular activated carbon chromatography column, and a toxic and harmful substance such as heavy metal and pesticide residue is removed through a column packed with granular activated carbon. After the feed is completed, the column is washed with granular activated carbon 2BV purified water, and combined. Feed effluent and water washing solution, to obtain residual liquid;
  • the ceramic membrane clear liquid is sucked into the inner circulation vacuum concentrator by vacuum, and the vacuum decompression and concentration equipment is turned on, and concentrated to a sugar degree of 60 to 65 Brix to obtain a concentrated juice;
  • the concentrated juice is transported to the aseptic workshop, the special sterilization equipment is turned on, the temperature is controlled at 80-85 ° C for 30 minutes, and the sterilization juice is obtained.
  • the vacuum sterilization machine is used to vacuum-pack the sterilization juice to obtain the finished Luo Han Guo decolorization and concentration. juice;
  • the obtained product retains the flavor and nutrients of fresh mangosteen fruit.
  • the color of the solution is nearly colorless and clear and transparent, and the mouthfeel is excellent. There is no post-precipitation.
  • the content of mogroside V is 2.5%-3.0%, and the sugar content is 60-65 Brix.
  • the purified water added is 1 time the weight of the fresh mangosteen.
  • the first ceramic membrane microfiltration clarified ceramic membrane pore size is 0.45 ⁇ m.
  • the ultrafiltration membrane liquid separation molecular weight is 0 to 20000.
  • the decolorizing polyamide resin has a particle size of 30 to 60 mesh, and 65 to 70 kg of the polyamide resin per 1000 L of the ultrafiltration membrane liquid.
  • the type of the decolorizing resin is D900 or LSD-835, and the standard is 40 to 45 kg of an anionic decolorizing resin per 1000 L of the polyamide resin decolorizing liquid.
  • the type of the cation exchange resin is D113 or 001 ⁇ 16 or D113FC, and the standard is 25 to 30 kg of a cation exchange resin per 1000 L of decolorizing resin decolorizing solution, and the pH of the effluent is 5.5 to 6.0.
  • the material for removing part of the heavy metal and the pesticide residue is granular activated carbon, and the use condition is column chromatography, and the standard is 60-80 kg of granular activated carbon per 1000 L of the membrane concentrated liquid.
  • the second ceramic membrane microfiltration clarified ceramic membrane pore size is 0.22 ⁇ m.
  • the vacuum decompression and concentration conditions are: controlling the degree of vacuum of 0.085 to 0.095 MPa, the temperature of 55 to 60 ° C, and concentrating to a sugar degree of 60 to 65 Brix.
  • Ultrafiltration is a relatively advanced membrane separation technology for removing pigments. It can be separated according to the relative molecular weight and molecular structure of chemical components.
  • the molecular structure of pigments is mostly planar, and most of them are difficult to pass through 20,000 molecular weight ultrafiltration membranes.
  • a part of the pigment can be removed by ultrafiltration;
  • the polyamide resin has a strong adsorption capacity for phenolic acid pigments, especially flavonoids, by molecular binding, and can remove most of the pigment;
  • the anion decolorizing resin is ion exchanged, and the phenolic acid is acidic.
  • the pigment has strong exchange adsorption capacity, and can remove the pigment which can not be completely removed by the first two kinds of decolorization methods;
  • the decolorization liquid decolorized by the anion decolorization resin is alkaline, which affects the flavor, taste and stability of Luo Han Guo, and is not introduced.
  • the pH of the decolorizing solution is adjusted by the cation exchange resin as the optimum solution.
  • the decolorizing liquid is large in volume, and the vacuum concentration processing amount is small and the cost is high, the reverse osmosis membrane concentration technology is adopted, and steam is not consumed, and only electricity can be realized under normal temperature and normal pressure, thereby greatly saving the concentration cost;
  • the Luo Han Guo concentrated juice obtained in the process may have some heavy metals and pesticide residues remaining, while the granular activated carbon has a good adsorption effect on heavy metals and pesticide residues.
  • the residual liquid of the granular activated carbon may have a small amount of carbon particles and other turbid substances, and the cross-flow filtration of the 0.22 ⁇ m ceramic membrane and the microfiltration clarification have significant advantages of clarification and precipitation after removal, and therefore, a clear treatment liquid is obtained through the ceramic membrane.
  • Luo Han Guo decolorized concentrated juice The main components of Luo Han Guo decolorized concentrated juice are: mogroside V, mogroside IV, mogroside III, mogroside VI, 11-O-monanin V, D-mannitol, glucose, fructose.
  • the fresh Luo Han Guo decolorized concentrated juice produced by the process retains the flavor and nutrient composition of fresh Luo Han Guo fruit.
  • the color of the solution is close to colorless and clear and transparent, the mouthfeel is excellent, no post-precipitation, high quality, and can be widely used in food and beverage. , medicine and health care products industry;
  • the invention has simple production process, advanced technology, high degree of automation, high efficiency, low energy consumption, low production cost, stable product quality and high quality;
  • the invention can create obvious economic and social benefits, increase the employed population, earn foreign exchange through exports, and promote the agricultural industrialization and large-scale development of Guilin Luo Han Guo.
  • Figure 1 is a flow chart of the production process of the present invention.
  • Luo Han Guo 2000kg Take the newly purchased fresh and mature Luo Han Guo 2000kg, put it into the raw material warehouse in a basket, close the doors and windows, leave only a small amount of vents open, and let it stand for 8 days.
  • the fresh Luo Han Guo epidermis turns from greenish green to green bean yellow, and the flesh can be picked up.
  • the sugar is silk, the saccharification is completed.
  • a fresh mangosteen with no peeling, no mildew and no saccharification inside and outside the fruit was selected.
  • a total of 1991 kg was placed in a special fruit washing machine for Luo Han Guo, and the surface mud and dust and other impurities were washed away to obtain washed fresh mangosteen.
  • the percolation extract is piped to a centrifugal station, centrifuged by a disc centrifuge, and the centrifugal slag is discarded to obtain a disc centrifuge containing turbidity without significant impurities and precipitation.
  • the disc centrifuge is pumped into the upstream tank of the ceramic membrane, and the ceramic membrane complete equipment is turned on.
  • the ceramic membrane has a pore size of 0.45 ⁇ m, and the water-insoluble impurities and the turbid substance are removed, and 6000 L ceramic membrane clear liquid is obtained.
  • the ceramic membrane clear liquid is pumped into the upstream tank of the ultrafiltration membrane, and the ultrafiltration membrane complete equipment is operated to collect the molecular weight of 0 to 20000, and 6500L ultrafiltration membrane liquid is obtained.
  • the ultrafiltration membrane liquid is pumped into the high-position tank of the polyamide resin chromatography column, and the high-level tank feed and the column discharge flow rate are controlled to be 1600 L/h, and the resin having a weight of 425 kg and a particle size of 30-60 mesh polyamide resin is loaded.
  • the column is discolored. After the feed was completed, the column was washed with 700 L of purified water, and the feed effluent and the water washing solution were combined to obtain 7200 L of a polyamide resin decolorizing solution.
  • the polyamide resin decolorizing liquid was pumped into the high-position tank of the decolorizing resin column, and the high-position tank feeding and the column discharge flow rate was 900 L/h, and the resin column was decolorized by a resin column packed with an anionic decolorizing resin weighing 300 kg. After the completion of the feed, the column was washed with 600 L of purified water, and the feed effluent and the water washing solution were combined to obtain 7800 L of a decolorizing resin decolorizing solution.
  • the decolorizing resin decoloring liquid is pumped into the high-position tank of the cationic resin chromatography column, and the high-level tank feed and the column discharge flow rate are controlled to 1000 L/h, and the pH of the effluent is adjusted by loading a column with a weight of 200 kg of cation exchange resin. For 5.6, the pH solution was adjusted.
  • the pH adjustment liquid is pumped into the upstream tank of the reverse osmosis membrane, the reverse osmosis membrane complete equipment is turned on, the membrane is concentrated under normal temperature and normal pressure, most of the water is removed, and concentrated to 10 Brix to obtain 1850 L membrane concentrate.
  • the membrane concentrate is pumped into a high-position tank of granular activated carbon chromatography column, and a toxic and harmful substance such as heavy metals and pesticide residues is removed by a column packed with 130 kg of granular activated carbon. After the feed was completed, the column was washed with 260 L of purified water, and the feed effluent and the water washing solution were combined to obtain 2100 L of residual liquid.
  • the residual liquid is pumped into the upstream tank of the ceramic membrane, and the ceramic membrane complete equipment is turned on.
  • the ceramic membrane has a pore size of 0.22 ⁇ m, and the trace carbon residue, the water-insoluble impurities and the post-precipitated material are removed to obtain a ceramic membrane clear liquid.
  • the concentrated juice is transported to the aseptic workshop, the special sterilization equipment is turned on, the temperature is controlled at 85 ° C, and the time is 30 min for sterilization, and the sterilization juice is obtained; the sterilization juice is vacuum-packed with a vacuum packaging machine to obtain the finished Luo Han Guo decolorized concentrated juice.
  • the product retains the flavor and nutrients of fresh mangosteen fruit.
  • the color of the solution is nearly colorless and clear and transparent. It has excellent taste and no post-precipitation.
  • the content of mogroside V is 2.95% and the sugar content is 62 Brix.
  • a fresh mangosteen with no peeling, no mildew and no saccharification inside and outside the fruit was selected.
  • a total of 1489 kg was selected and placed in a special fruit washing machine for Luo Han Guo. The surface mud and dust and other impurities were washed away to obtain washed fresh mangosteen.
  • the percolation extract is piped to a centrifugal station, centrifuged by a disc centrifuge, and the centrifugal slag is discarded to obtain a disc centrifuge containing turbidity without significant impurities and precipitation.
  • the disc centrifuge is pumped into the upstream tank of the ceramic membrane, and the ceramic membrane complete equipment is turned on.
  • the ceramic membrane has a pore size of 0.45 ⁇ m, and the water-insoluble impurities and the turbid substance are removed, and 4500 L of the ceramic membrane clear liquid is obtained.
  • the ceramic membrane clear liquid is pumped into the upstream tank of the ultrafiltration membrane, and the ultrafiltration membrane complete equipment is operated to collect the molecular weight of 0 to 20000, and 4900L ultrafiltration membrane liquid is obtained.
  • the ultrafiltration membrane liquid is pumped into the high-position tank of the polyamide resin chromatography column, and the high-level tank feed and the column discharge flow rate are controlled to be 1250 L/h, and the resin having a weight of 350 kg and a particle size of 30-60 mesh polyamide resin is loaded.
  • the column is discolored. After the feed was completed, the column was washed with 600 L of purified water, and the feed effluent and the water washing liquid were combined to obtain 5500 L of a polyamide resin decolorizing solution.
  • the polyamide resin decolorizing solution was pumped into the high-position tank of the decolorizing resin column, and the high-position tank feed and the column discharge flow rate were controlled to be 700 L/h, and decolorized by a resin column packed with an anion decolorizing resin weighing 250 kg. After the feed was completed, the column was washed with 500 L of purified water, and the feed effluent and the water washing solution were combined to obtain 6000 L of decolorizing resin decolorizing solution.
  • the decolorizing resin decoloring liquid is pumped into the high-position tank of the cationic resin chromatography column, and the high-level tank feed and the column discharge flow rate are controlled to be 800 L/h, and the pH of the effluent is adjusted by loading a column with a weight of 150 kg of cation exchange resin. At 6.0, the pH solution was adjusted.
  • the pH adjustment liquid is pumped into the upstream tank of the reverse osmosis membrane, the reverse osmosis membrane complete equipment is turned on, the membrane is concentrated under normal temperature and normal pressure, most of the water is removed, and concentrated to 12 Brix to obtain 1260L membrane concentrate.
  • the membrane concentrate is pumped into a high-level tank of granular activated carbon chromatography column, and a toxic and harmful substance such as heavy metals and pesticide residues is removed by a column packed with 100 kg of granular activated carbon. After the feed was completed, the column was washed with 200 L of purified water, and the feed effluent and the water washing liquid were combined to obtain 1500 L of residual liquid.
  • the residual liquid is pumped into the upstream tank of the ceramic membrane, and the ceramic membrane complete equipment is turned on.
  • the ceramic membrane has a pore size of 0.22 ⁇ m, and the trace carbon residue, the water-insoluble impurities and the post-precipitated material are removed to obtain a ceramic membrane clear liquid.
  • the ceramic membrane clear liquid is sucked into the inner circulation vacuum concentrator by vacuum, and the vacuum decompression and concentration equipment is turned on, and concentrated to a sugar degree of 61 Brix to obtain 236 kg of concentrated juice;
  • the concentrated juice is transported to the aseptic workshop, the special sterilization equipment is turned on, the temperature is controlled at 85 ° C, and the time is 30 min for sterilization, and the sterilization juice is obtained; the sterilization juice is vacuum-packed with a vacuum packaging machine to obtain the finished Luo Han Guo decolorized concentrated juice.
  • the product quality has been identified: the product retains the flavor and nutrients of fresh mangosteen fruit.
  • the color of the solution is close to colorless and clear and transparent, and the taste is excellent. There is no post-precipitation.
  • the content of mogroside V is 2.82% and the sugar content is 61 Brix.

Abstract

一种鲜罗汉果脱色浓缩汁的制备工艺，其步骤是：鲜罗汉果→糖化→选果和洗果→破碎→渗漉提取→碟式离心→0.45μm陶瓷膜微滤澄清→分子量超滤分离→聚酰胺树脂脱色→脱色树脂脱色→阳离子树脂调pH→反渗透膜浓缩→粒状活性炭柱去残留→0.22μm陶瓷膜微滤澄清→真空减压浓缩制膏→灭菌→真空包装→鲜罗汉果脱色浓缩汁。以及由上述工艺制备的鲜罗汉果脱色浓缩汁。

Description

一种鲜罗汉果脱色浓缩汁的制备工艺 技术领域
本发明涉及植物活性成分的提取，具体是一种鲜罗汉果脱色浓缩汁的生产工艺。
背景技术
罗汉果作为药食同源的植物品种，具有特殊的风味和营养成分，以及特有口感。鲜罗汉果中的甜味成分主要是三萜皂苷类非糖甜味成分：以罗汉果苷V(Mogroside V)和IV为代表，苷V甜度是蔗糖的256-344倍，IV甜度为蔗糖的126倍，而热量只有蔗糖的1/50；另含有D-甘露醇(D-mannitol)，其甜度为蔗糖的0.55-0.65倍。此外，鲜罗汉果中还含有大量葡萄糖(glucose)，果糖(fructose)等甜味成分；蛋白质、氨基酸、少量黄酮；又含锰、铁、镍、硒、锡、碘、钼等26种无机元素、维生素C(Vitamin C)等。故罗汉果的深加工引起国内外学者广泛关注。目前有关鲜罗汉果浓缩汁的研发和生产技术较多，但代表性技术主要有以下3种：
1、膜分离技术
该技术先将鲜罗汉果破碎，用40-95℃的水反复浸泡6-16小时，经预处理过滤得滤液，温度降至25～55℃，滤液经压力泵在0.05～3.0MPa压力下，按顺序送入集成膜组合系统，经微滤(MF)、超滤(UF)、反渗透(RO)等组合膜件逐级分离、纯化浓缩，最终得到16-35波美度的鲜罗汉果浓缩液产品。
2、树脂法
该技术将鲜罗汉果经选料及前处理、过阳离子柱、脱色、第一道酸化、浓缩和第二道酸化，得到的脱色罗汉果果汁为白色或类黄色透明液体，波美度为10以上或者白利糖度为60以上，果汁组成以干重计算，其中罗汉果甜甙体积含量≥30％。
3、酶解法
该技术之一将罗汉果鲜果清洗后，破碎打成果浆。然后调整果浆的pH值和温度，加入固定化果浆酶，该果浆酶不仅分解果胶主干，还能水解果胶中的甲基半乳糖酸残留，裂解植物细胞壁，释放出更多的果汁，同时使果汁澄清。然后将果汁超滤后进行脱臭处理，再浓缩、灭菌、包装得到罗汉果浓缩汁。
该技术之二用螺旋压榨机破碎鲜罗汉果,以四级蒸煮工艺将破碎了的鲜罗汉果蒸煮浸提取汁、运用复合酶使蒸煮得的果汁中的果胶酶解沉淀,使果汁澄清、然后用板框硅藻土压滤机对澄清后的果汁过滤,再以高温瞬时灭菌法将果汁灭菌、并以离心薄膜法和真空浓缩锅将果汁浓缩至25Be，最后使成品冷却至常温进行包装。
此外，还有一些简单的技术报导：
1、加添加剂制备罗汉果浓缩汁
该技术包括三次离心过滤分离、合并三次分离的果汁、加热沸腾使蛋白变性沉淀、脱除异味前体物质、板框压滤、加入防腐剂、微孔膜过滤、纳滤浓缩等步骤。
2、调配法制备罗汉果浓缩汁
该方法用pH值为11、12的灭菌洗涤液，将鲜罗汉果表皮的青毛洗去后，再用去离子水或清水冲洗，当冲洗后的去离子水或清水的pH值为7时即可。然后将经清洗干净的罗汉果破碎成碎块。破碎后的罗汉果与调配剂、水按1∶1，1.5、2的重量比进行调配。
以上所报导的生产鲜罗汉果浓缩汁的技术，有的是未实现鲜罗汉果浓缩汁的产业化，有的不能保留鲜罗汉果的风味和营养成分，有的有颜色，有的口感差，有后沉淀等。
发明内容
本发明的目的在于克服现有技术的不足，而提供一种鲜罗汉果脱色浓缩汁的生产工艺；该工艺可以规模生产出高品质的鲜罗汉果脱色浓缩汁产品，产品无色透明，口感极好，无后沉淀。
实现本发明目的的技术方案是：
一种鲜罗汉果脱色浓缩汁的生产工艺，包括如下步骤：
1)糖化
取新购的新鲜成熟的罗汉果，成筐放入原料仓库中，关好门窗，仅留少量通风口开放，静置7～10天，至鲜罗汉果表皮由青绿色转绿豆黄色，并且果肉可拈起糖丝时，即完成糖化；
2)选果和洗果
挑选果皮无破损、果内外无霉变并已糖化好的鲜罗汉果，放入罗汉果专用洗果机中，洗去表面的泥砂以及灰尘等杂质，得到洗净的鲜罗汉果；
3)破碎
将洗净的鲜罗汉果放入罗汉果专用投料机，通过传送带提升至多功能提取罐的上方，预先在多功能提取罐中加入纯化水，在不断搅拌下通过罗汉果专用破碎机将鲜罗汉果破碎后的物料直接投入罗汉果提取专用的多功能提取罐中；
4)渗漉提取
投料完成以后，继续搅拌5min，然后常温静置20min，即开始放料；当放料速度下降至最初放料速度1/3时，补充加入纯化水，边加纯化水边放料，渗漉提取的药渣通过传送带输送至提取岗位，以完全提取罗汉果苷。收集所有放料液，得渗漉提取液；
5)碟式离心
将渗漉提取液通过管道输送至离心岗位，采用碟式离心机进行离心分离，离心渣弃去，得到浑 浊而无明显杂质和沉淀的碟式离心液；
6)第一次陶瓷膜微滤澄清
将碟式离心液泵入陶瓷膜上游罐，开启陶瓷膜成套设备运行，通过陶瓷膜去除水不溶杂质和产生浑浊的物质，得陶瓷膜清液；
7)分子量超滤分离
将陶瓷膜清液泵入超滤膜上游罐，开启超滤膜成套设备运行，收集超滤膜液；
8)聚酰胺树脂脱色
将超滤膜液泵入聚酰胺树脂层析柱的高位罐，控制高位罐进料及层析柱出料流速为2.0～3.0BV/h，通过聚酰胺树脂的树脂柱脱色，进完料以后，再用树脂2BV纯化水洗柱，合并进料流出液和水洗液，得聚酰胺树脂脱色液；
9)脱色树脂脱色
将聚酰胺树脂脱色液泵入脱色树脂柱的高位罐，控制高位罐进料及层析柱出料流速为2.0～3.0BV/h，通过装填有阴离子脱色树脂的树脂柱脱色，进完料以后，再用树脂2BV纯化水洗柱，合并进料流出液和水洗液，得脱色树脂脱色液；
10)阳离子树脂调pH
将脱色树脂脱色液泵入阳离子树脂层析柱高位罐，控制适当的流速，通过装填有阳离子树脂的层析柱，得调pH液；
11)反渗透膜浓缩
将调pH液泵入反渗透膜上游罐，开启反渗透膜成套设备运行，常温常压下进行膜浓缩，去除大部分水，得膜浓缩液。
12)粒状活性炭柱去残留
将膜浓缩液泵入粒状活性炭层析柱高位罐，通过装填有粒状活性炭的层析柱，去除部分重金属、农药残留等有毒有害物质，进完料以后，再用粒状活性炭2BV纯化水洗柱，合并进料流出液和水洗液，得去残留液；
13)第二次陶瓷膜微滤澄清
将去残留液泵入陶瓷膜上游罐，开启陶瓷膜成套设备运行，通过陶瓷膜去除微量炭渣、水不溶杂质和产生后沉淀的物质，得陶瓷膜清液；
14)真空减压浓缩
用真空将陶瓷膜清液吸入内循环减压浓缩器，开启真空减压浓缩设备运行，浓缩至糖度60～65Brix，得浓缩汁；
15)灭菌、真空包装
将浓缩汁输送至无菌车间，开启专用灭菌设备，控制温度80～85℃、时间30min进行灭菌，得灭菌汁；用真空包装机对灭菌汁进行真空包装，得成品罗汉果脱色浓缩汁；
经检验，所得产品保留鲜罗汉果的风味和营养成分，溶液颜色接近无色并澄清透明，口感极好，无后沉淀，罗汉果苷V含量2.5％～3.0％、糖度60～65Brix。
步骤3)中，加入的纯化水为投料鲜罗汉果重量的1倍。
步骤6)中，所述第一次陶瓷膜微滤澄清的陶瓷膜孔径为0.45μm。
步骤7)中，所述的超滤膜液分离截留分子量为0～20000。
步骤8)中，所述的脱色聚酰胺树脂粒度为30～60目，每1000L超滤膜液用聚酰胺树脂65～70kg。
步骤9)中，所述的脱色树脂的型号为D900或LSD-835，使用标准为每1000L聚酰胺树脂脱色液用阴离子脱色树脂40～45kg。
步骤10)中，所述的阳离子交换树脂的型号为D113或001×16或D113FC，使用标准为每1000L脱色树脂脱色液用阳离子交换树脂25～30kg，流出液的pH为5.5～6.0。
步骤12)中，所述的去除部分重金属和农药残留的材料为粒状活性炭，使用条件为柱层析，使用标准为每1000L膜浓缩液用粒状活性炭60～80kg。
步骤13)中，所述第二次陶瓷膜微滤澄清的陶瓷膜孔径为0.22μm。
步骤14)中，所述的真空减压浓缩条件为：控制真空度0.085～0.095MPa，温度55～60℃，浓缩至糖度60～65Brix。
本发明上述制备工艺根据鲜罗汉果所含化学成分的理化性质设计：
因鲜罗汉果在采摘时为避免运输损坏，均未全熟，以致新购的罗汉果需要充分放置几天即糖化，以便全熟；鲜罗汉果在运输过程难免有损坏，而在运输及糖化过程就会发霉变质，因此，需要将这部分霉坏果完全清理出来，以免影响罗汉果浓缩汁的产品品质；鲜罗汉果表面有泥砂和灰尘等杂质，可以通过清水洗去，以提升最终产品罗汉果浓缩汁的品质；罗汉果籽有一定苦味，会影响罗汉果浓缩汁的品质，因此，在破碎时，不宜将罗汉果籽打碎。
为了保留罗汉果的风味和营养成分，在将罗汉果汁和罗汉果渣分离的过程中，应尽可能在常温下进行，以免破坏营养成分，而渗漉提取能最大程度地提取罗汉果的风味和营养成分而不破坏，且溶剂用量少；碟式离心能将提取液中的大部分果肉和纤维通过离心去除，从而得到虽浑浊但无明显沉淀的前处理液；根据罗汉果的风味和营养成分溶于水而杂质不溶于水显浑浊的理化性质特点，结合陶瓷膜的错流过滤以及微孔0.45μm的优点，采用陶瓷膜澄清技术对碟式离心液进行澄清处理，得到澄清的处理液。
超滤是一种去除色素的比较先进的膜分离技术，可以根据化学成分的相对分子量和分子结构进行分离，而色素的分子结构多为平面型，多数难以透过20000分子量的超滤膜，因此，可以通过超滤去除一部分色素；聚酰胺树脂通过分子结合作用，对酚酸性色素尤其是黄酮类化合物具有较强的吸附能力，可以去除大部分色素；阴离子脱色树脂通过离子交换作用，对酚酸性色素具有很强的交换吸附能力，可以去除经前2种脱色方法仍不能完全去除的色素；经过阴离子脱色树脂脱色的脱色液显碱性，影响了罗汉果的风味、口感和稳定性，在不引入外来酸的条件下，通过阳离子交换树脂来调节脱色液的pH为最佳方案。
根据脱色液体积大，而真空浓缩处理量小且成本高的缺点，采用反渗透膜浓缩技术，不耗用蒸汽，只需要用电在常温常压下即可实现，极大地节省浓缩成本；前期工序所得的罗汉果浓缩汁，有可能残存部分重金属和农药残留，而粒状活性炭对重金属和农药残留具有较好的吸附作用，因此可通过粒状活性炭，采用柱层析的方法去除大部分残留；因经过粒状活性炭的脱残留液可能存在少量炭粒以及其他浑浊物质，而0.22μm陶瓷膜的错流过滤以及微滤澄清具有澄清和去除后沉淀的显著优点，因此，通过陶瓷膜得到澄清的处理液。
最后经过真空减压浓缩制汁以及灭菌和真空包装得到高品质鲜罗汉果脱色浓缩汁。
罗汉果脱色浓缩汁主要成分是：罗汉果苷V、罗汉果苷IV、罗汉果苷III、罗汉果苷VI、11-O-罗汉果苷V、D-甘露醇、葡萄糖、果糖。
本发明的优点：
(1)本工艺生产的鲜罗汉果脱色浓缩汁，保留了鲜罗汉果的风味和营养成分，溶液颜色接近无色并澄清透明，口感极好，无后沉淀，品质高，可以广泛应用于食品、饮料、医药和保健品行业；
(2)本发明生产工艺简单，技术先进，自动化程度高，高效率低耗能，生产成本低，产品质量稳定、品质高；
(3)本发明能创造明显的经济和社会效益，增加就业人口，出口创汇，促进桂林罗汉果的农业产业化、规模化发展。
附图说明
图1为本发明生产工艺流程图。
具体实施方式
通过下面给出的本发明的具体实施例，可以进一步清楚地了解本发明，但它们不是对本发明的限定。
实施例1
1)糖化
取新购的新鲜成熟的罗汉果2000kg，成筐放入原料仓库中，关好门窗，仅留少量通风口开放，静置8天，至鲜罗汉果表皮由青绿色转绿豆黄色，并且果肉可拈起糖丝时，即完成糖化。
2)选果和洗果
挑选果皮无破损、果内外无霉变并已糖化好的鲜罗汉果，共选出1991kg放入罗汉果专用洗果机中，洗去表面的泥砂以及灰尘等杂质，得到洗净的鲜罗汉果。
3)破碎
将洗净的鲜罗汉果放入罗汉果专用投料机，通过传送带提升至多功能提取罐的上方，预先在6.0m 3多功能提取罐中加入2000kg纯化水，在不断搅拌下通过罗汉果专用破碎机将鲜罗汉果破碎后的物料直接投入罗汉果提取专用的多功能提取罐中。
4)渗漉提取
投料完成以后，继续搅拌5min，然后常温静置20min，即开始放料。当放料速度由2000L/h下降至650L/h时，补充加入纯化水，边加纯化水边放料，合计加入4000kg纯化水。渗漉提取的药渣通过传送带输送至提取岗位，以完全提取罗汉果苷。收集所有放料液，得5500L渗漉提取液。
5)碟式离心
将渗漉提取液通过管道输送至离心岗位，采用碟式离心机进行离心分离，离心渣弃去，得到浑浊而无明显杂质和沉淀的碟式离心液。
6)0.45μm陶瓷膜微滤澄清
将碟式离心液泵入陶瓷膜上游罐，开启陶瓷膜成套设备运行，陶瓷膜孔径0.45μm，去除水不溶杂质和产生浑浊的物质，得6000L陶瓷膜清液。
7)分子量超滤分离
将陶瓷膜清液泵入超滤膜上游罐，开启超滤膜成套设备运行，收集分子量为0～20000的部分，得6500L超滤膜液。
8)聚酰胺树脂脱色
将超滤膜液泵入聚酰胺树脂层析柱的高位罐，控制高位罐进料及层析柱出料流速为1600L/h，通过装填有重量425kg，粒度30～60目聚酰胺树脂的树脂柱脱色。进完料以后，再用700L纯化水洗柱，合并进料流出液和水洗液，得7200L聚酰胺树脂脱色液。
9)脱色树脂脱色
将聚酰胺树脂脱色液泵入脱色树脂柱的高位罐，控制高位罐进料及层析柱出料流速为900L/h，通过装填有重量300kg的阴离子脱色树脂的树脂柱脱色。进完料以后，再用600L纯化水洗柱，合 并进料流出液和水洗液，得7800L脱色树脂脱色液。
10)阳离子树脂调pH
将脱色树脂脱色液泵入阳离子树脂层析柱高位罐，控制高位罐进料及层析柱出料流速为1000L/h，通过装填有重量200kg阳离子交换树脂的层析柱，调节流出液的pH为5.6，得调pH液。
11)反渗透膜浓缩
将调pH液泵入反渗透膜上游罐，开启反渗透膜成套设备运行，常温常压下进行膜浓缩，去除大部分水，浓缩至10Brix，得1850L膜浓缩液。
12)粒状活性炭柱去残留
将膜浓缩液泵入粒状活性炭层析柱高位罐，通过装填有重量130kg粒状活性炭的层析柱，去除部分重金属、农药残留等有毒有害物质。进完料以后，再用260L纯化水洗柱，合并进料流出液和水洗液，得2100L去残留液。
13)0.22μm陶瓷膜微滤澄清
将去残留液泵入泵入陶瓷膜上游罐，开启陶瓷膜成套设备运行，陶瓷膜孔径0.22μm，去除微量炭渣、水不溶杂质和产生后沉淀的物质，得陶瓷膜清液。
14)真空减压浓缩制汁
用真空将陶瓷膜清液吸入内循环减压浓缩器，开启真空减压浓缩设备运行，浓缩至糖度62Brix，得286kg浓缩汁；
15)灭菌、真空包装
将浓缩汁输送至无菌车间，开启专用灭菌设备，控制温度85℃、时间30min进行灭菌，得灭菌汁；用真空包装机对灭菌汁进行真空包装，得成品罗汉果脱色浓缩汁。
质量：产品保留鲜罗汉果的风味和营养成分，溶液颜色接近无色并澄清透明，口感极好，无后沉淀，罗汉果苷V含量2.95％、糖度62Brix。
实施例2
1)糖化
取新购的新鲜成熟的罗汉果1500kg，成筐放入原料仓库中，关好门窗，仅留少量通风口开放，静置10天，至鲜罗汉果表皮由青绿色转绿豆黄色，并且果肉可拈起糖丝时，即完成糖化。
2)选果和洗果
挑选果皮无破损、果内外无霉变并已糖化好的鲜罗汉果，共选出1489kg放入罗汉果专用洗果机中，洗去表面的泥砂以及灰尘等杂质，得到洗净的鲜罗汉果。
3)破碎
将洗净的鲜罗汉果放入罗汉果专用投料机，通过传送带提升至多功能提取罐的上方，预先在6.0m 3多功能提取罐中加入1500kg纯化水，在不断搅拌下通过罗汉果专用破碎机将鲜罗汉果破碎后的物料直接投入罗汉果提取专用的多功能提取罐中。
4)渗漉提取
投料完成以后，继续搅拌5min，然后常温静置20min，即开始放料。当放料速度由1500L/h下降至500L/h时，补充加入纯化水，边加纯化水边放料，合计加入3000kg纯化水。渗漉提取的药渣通过传送带输送至提取岗位，以完全提取罗汉果苷。收集所有放料液，得4100L渗漉提取液。
5)碟式离心
将渗漉提取液通过管道输送至离心岗位，采用碟式离心机进行离心分离，离心渣弃去，得到浑浊而无明显杂质和沉淀的碟式离心液。
6)0.45μm陶瓷膜微滤澄清
将碟式离心液泵入陶瓷膜上游罐，开启陶瓷膜成套设备运行，陶瓷膜孔径0.45μm，去除水不溶杂质和产生浑浊的物质，得4500L陶瓷膜清液。
7)分子量超滤分离
将陶瓷膜清液泵入超滤膜上游罐，开启超滤膜成套设备运行，收集分子量为0～20000的部分，得4900L超滤膜液。
8)聚酰胺树脂脱色
将超滤膜液泵入聚酰胺树脂层析柱的高位罐，控制高位罐进料及层析柱出料流速为1250L/h，通过装填有重量350kg，粒度30～60目聚酰胺树脂的树脂柱脱色。进完料以后，再用600L纯化水洗柱，合并进料流出液和水洗液，得5500L聚酰胺树脂脱色液。
9)脱色树脂脱色
将聚酰胺树脂脱色液泵入脱色树脂柱的高位罐，控制高位罐进料及层析柱出料流速为700L/h，通过装填有重量250kg的阴离子脱色树脂的树脂柱脱色。进完料以后，再用500L纯化水洗柱，合并进料流出液和水洗液，得6000L脱色树脂脱色液。
10)阳离子树脂调pH
将脱色树脂脱色液泵入阳离子树脂层析柱高位罐，控制高位罐进料及层析柱出料流速为800L/h，通过装填有重量150kg阳离子交换树脂的层析柱，调节流出液的pH为6.0，得调pH液。
11)反渗透膜浓缩
将调pH液泵入反渗透膜上游罐，开启反渗透膜成套设备运行，常温常压下进行膜浓缩，去除 大部分水，浓缩至12Brix，得1260L膜浓缩液。
12)粒状活性炭柱去残留
将膜浓缩液泵入粒状活性炭层析柱高位罐，通过装填有重量100kg粒状活性炭的层析柱，去除部分重金属、农药残留等有毒有害物质。进完料以后，再用200L纯化水洗柱，合并进料流出液和水洗液，得1500L去残留液。
13)0.22μm陶瓷膜微滤澄清
将去残留液泵入泵入陶瓷膜上游罐，开启陶瓷膜成套设备运行，陶瓷膜孔径0.22μm，去除微量炭渣、水不溶杂质和产生后沉淀的物质，得陶瓷膜清液。
14)真空减压浓缩制汁
用真空将陶瓷膜清液吸入内循环减压浓缩器，开启真空减压浓缩设备运行，浓缩至糖度61Brix，得236kg浓缩汁；
15)灭菌、真空包装
将浓缩汁输送至无菌车间，开启专用灭菌设备，控制温度85℃、时间30min进行灭菌，得灭菌汁；用真空包装机对灭菌汁进行真空包装，得成品罗汉果脱色浓缩汁。
产品质量经鉴定：产品保留鲜罗汉果的风味和营养成分，溶液颜色接近无色并澄清透明，口感极好，无后沉淀，罗汉果苷V含量2.82％、糖度61Brix。

Claims (10)

  1. 一种鲜罗汉果脱色浓缩汁的制备工艺，其特征在于，包括如下步骤：
    1)糖化
    取新购的新鲜成熟的罗汉果，成筐放入原料仓库中，关好门窗，仅留少量通风口开放，静置7～10天，至鲜罗汉果表皮由青绿色转绿豆黄色，并且果肉可拈起糖丝时，即完成糖化；
    2)选果和洗果
    挑选果皮无破损、果内外无霉变并已糖化好的鲜罗汉果，放入罗汉果专用洗果机中，洗去表面的泥砂以及灰尘等杂质，得到洗净的鲜罗汉果；
    3)破碎
    将洗净的鲜罗汉果放入罗汉果专用投料机，通过传送带提升至多功能提取罐的上方，预先在多功能提取罐中加入纯化水，在不断搅拌下通过罗汉果专用破碎机将鲜罗汉果破碎后的物料直接投入罗汉果提取专用的多功能提取罐中；
    4)渗漉提取
    投料完成以后，继续搅拌5min，然后常温静置20min，即开始放料；当放料速度下降至最初放料速度1/3时，补充加入纯化水，边加纯化水边放料，渗漉提取的药渣通过传送带输送至提取岗位，以完全提取罗汉果苷，收集所有放料液，得渗漉提取液；
    5)碟式离心
    将渗漉提取液通过管道输送至离心岗位，采用碟式离心机进行离心分离，离心渣弃去，得到浑浊而无明显杂质和沉淀的碟式离心液；
    6)第一次陶瓷膜微滤澄清
    将碟式离心液泵入陶瓷膜上游罐，开启陶瓷膜成套设备运行，用陶瓷膜去除水不溶杂质和产生浑浊的物质，得陶瓷膜清液；
    7)分子量超滤分离
    将陶瓷膜清液泵入超滤膜上游罐，开启超滤膜成套设备运行，收集超滤膜液；
    8)聚酰胺树脂脱色
    将超滤膜液泵入聚酰胺树脂层析柱的高位罐，控制高位罐进料及层析柱出料流速为2.0～3.0BV/h，通过聚酰胺树脂的树脂柱脱色，进完料以后，再用树脂2BV纯化水洗柱，合并进料流出液和水洗液，得聚酰胺树脂脱色液；
    9)脱色树脂脱色
    将聚酰胺树脂脱色液泵入脱色树脂柱的高位罐，控制高位罐进料及层析柱出料流速为2.0～3.0BV/h，通过装填有阴离子脱色树脂的树脂柱脱色，进完料以后，再用树脂2BV纯化水洗柱，合并进料流出液和水洗液，得脱色树脂脱色液；
    10)阳离子树脂调pH
    将脱色树脂脱色液泵入阳离子树脂层析柱高位罐，控制适当的流速，通过装填有阳离子树脂的层析柱，得调pH液；
    11)反渗透膜浓缩
    将调pH液泵入反渗透膜上游罐，开启反渗透膜成套设备运行，常温常压下进行膜浓缩，去除大部分水，得膜浓缩液；
    12)粒状活性炭柱去残留
    将膜浓缩液泵入粒状活性炭层析柱高位罐，通过装填有粒状活性炭的层析柱，去除部分重金属、农药残留等有毒有害物质，进完料以后，再用粒状活性炭2BV纯化水洗柱，合并进料流出液和水洗液，得去残留液；
    13)第二次陶瓷膜微滤澄清
    将去残留液泵入泵入陶瓷膜上游罐，开启陶瓷膜成套设备运行，用陶瓷膜去除微量炭渣、水不溶杂质 和产生后沉淀的物质，得陶瓷膜清液；
    14)真空减压浓缩
    用真空将陶瓷膜清液吸入内循环减压浓缩器，开启真空减压浓缩设备运行，浓缩至糖度60～65Brix，得浓缩汁；
    15)灭菌、真空包装
    将浓缩汁输送至无菌车间，开启专用灭菌设备，控制温度80～85℃、时间30min进行灭菌，得灭菌汁；用真空包装机对灭菌汁进行真空包装，得成品罗汉果脱色浓缩汁。
  2. 根据权利要求1所述的制备工艺，其特征在于，步骤3)中，加入的纯化水为投料鲜罗汉果重量的1倍。
  3. 根据权利要求1所述的制备工艺，其特征在于，步骤7)中，所述的超滤膜液分离截留分子量为0～20000。
  4. 根据权利要求1所述的制备工艺，其特征在于，步骤8)中，所述的脱色聚酰胺树脂粒度为30～60目，每1000L超滤膜液用聚酰胺树脂65～70kg。
  5. 根据权利要求1所述的制备工艺，其特征在于，步骤9)中，所述的脱色树脂的型号为D900或LSD-835，使用标准为每1000L聚酰胺树脂脱色液用阴离子脱色树脂40～45kg。
  6. 根据权利要求1所述的制备工艺，其特征在于，步骤10)中，所述的阳离子交换树脂的型号为D113或001×16或D113FC，使用标准为每1000L脱色树脂脱色液用阳离子交换树脂25～30kg，流出液的pH为5.5～6.0。
  7. 根据权利要求1所述的制备工艺，其特征在于，步骤12)中，所述的去除部分重金属和农药残留的材料为粒状活性炭，使用条件为柱层析，使用标准为每1000L膜浓缩液用粒状活性炭60～80kg。
  8. 根据权利要求1所述的制备工艺，其特征在于，在步骤6)和步骤13)中，所述的陶瓷膜的孔径分别为0.45μm和0.22μm。
  9. 根据权利要求1所述的制备工艺，其特征在于，步骤14)中，所述的真空减压浓缩条件为：控制真空度0.085～0.095MPa，温度55～60℃，浓缩至糖度60～65Brix。
  10. 用权利要求1-9之一所述的制备工艺制备的鲜罗汉果脱色浓缩汁。
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