WO2017211079A1 - 一种从罗汉果中提取高纯度罗汉果苷v的方法 - Google Patents

一种从罗汉果中提取高纯度罗汉果苷v的方法 Download PDF

Info

Publication number
WO2017211079A1
WO2017211079A1 PCT/CN2017/070140 CN2017070140W WO2017211079A1 WO 2017211079 A1 WO2017211079 A1 WO 2017211079A1 CN 2017070140 W CN2017070140 W CN 2017070140W WO 2017211079 A1 WO2017211079 A1 WO 2017211079A1
Authority
WO
WIPO (PCT)
Prior art keywords
mogroside
han guo
enzymatic hydrolysis
luo han
filtrate
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/CN2017/070140
Other languages
English (en)
French (fr)
Inventor
龙伟岸
黄华学
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
JIANGXI HAIFU BIOENGINEERING CO Ltd
Original Assignee
JIANGXI HAIFU BIOENGINEERING CO Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by JIANGXI HAIFU BIOENGINEERING CO Ltd filed Critical JIANGXI HAIFU BIOENGINEERING CO Ltd
Priority to US16/307,309 priority Critical patent/US10743573B2/en
Publication of WO2017211079A1 publication Critical patent/WO2017211079A1/zh
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES, NOT OTHERWISE PROVIDED FOR; PREPARATION OR TREATMENT THEREOF
    • A23L27/00—Spices; Flavouring agents or condiments; Artificial sweetening agents; Table salts; Dietetic salt substitutes; Preparation or treatment thereof
    • A23L27/30—Artificial sweetening agents
    • A23L27/33—Artificial sweetening agents containing sugars or derivatives
    • A23L27/36—Terpene glycosides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/58—Multistep processes
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07J—STEROIDS
    • C07J17/00—Normal steroids containing carbon, hydrogen, halogen or oxygen, having an oxygen-containing hetero ring not condensed with the cyclopenta(a)hydrophenanthrene skeleton
    • C07J17/005—Glycosides
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
    • A23V2002/00—Food compositions, function of food ingredients or processes for food or foodstuffs
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
    • A23V2300/00—Processes
    • A23V2300/10—Drying, dehydrating
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
    • A23V2300/00—Processes
    • A23V2300/14—Extraction
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
    • A23V2300/00—Processes
    • A23V2300/24—Heat, thermal treatment
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
    • A23V2300/00—Processes
    • A23V2300/34—Membrane process
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
    • A23V2300/00—Processes
    • A23V2300/38—Multiple-step
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/06—Specific process operations in the permeate stream
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/08—Specific process operations in the concentrate stream
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/027—Nanofiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14—Ultrafiltration; Microfiltration
    • B01D61/145—Ultrafiltration

Definitions

  • the present application relates to the field of extraction methods of mogroside V, and more particularly to a method for extracting high-purity mogroside V from Luo Han Guo.
  • Mangosteen Greek name: Siraitia grosvenorii
  • Traditional Chinese medicine is based on its fruit and contains medicinal ingredients such as mogroside, various amino acids and vitamins. It treats lung heat, cough, pharyngitis, tonsillitis, acute gastritis, constipation and so on.
  • Mangosteen also known as sweetener, is widely used as a sweetener because of its high sweetness and low calorie, and is often used as a substitute sugar for obese and diabetic patients.
  • Patent No. CN200910044558.9 provides a method for producing Luo Han Guo extract with a content of mogroside V of more than 60%: crushing ⁇ saccharification ⁇ water extraction ⁇ concentration ⁇ sedimentation centrifugation ⁇ ion exchange resin refining ⁇ macroporous resin refining ⁇ concentration ⁇ alumina Refinement ⁇ concentration ⁇ spray drying ⁇ finished product process.
  • the invention has a long process route, and requires macroporous resin and alumina in series purification in the separation and purification step, and the operation is complicated and the cost is high.
  • Patent No. CN200710003364.5 discloses a method for preparing a decolorized and debittered mangosteen extract: filtering and concentrating the extract, decolorizing with a decolorizing resin, eluting with ethanol, deodorizing with a deodorizing agent, and then concentrating, It is spray-dried and pulverized to obtain a decolorized and debittered mangosteen extract, and the content of the Luo Han Guo sweet ⁇ V is 60% or more (HPLC).
  • the invention also requires macroporous resin adsorption purification in the separation and purification step, and then elution with an organic solvent, the operation is complicated, the solvent is residual, and the cost is high.
  • Patent No. CN200710049737.2 provides a preparation method of milk white mangosteen extract containing mogroside V ⁇ 40% and mogroside ⁇ 98%: water extraction, concentration, enzymatic hydrolysis, macroporous adsorption resin purification, ion exchange resin decolorization, concentration Made by spray drying.
  • the invention also requires macroporous resin adsorption purification in the separation and purification step, and then elution with an organic solvent, the operation is complicated, the solvent is residual, and the cost is high.
  • the separation and purification of mogroside V is mainly carried out by macroporous resin adsorption, and then eluted with different solvents to obtain a certain content of crude extract of mogroside V.
  • the crude extract is desalted, decolored, finally dried, sieved and packaged to obtain a product;
  • the most widely used column chromatography method is the most widely used macroporous resin separation and purification.
  • the resin type is D101, AB-8, etc.
  • the separation and purification of macroporous resin is cumbersome, and the yield of mogroside V is low.
  • the elution requires the use of an organic solvent, causing solvent residue and environmental pollution.
  • Preparative chromatography and high-speed countercurrent chromatography have high product content, but the one-time investment cost is large, and the amount of organic solvent used is large, and there are still problems such as solvent residue and environmental pollution.
  • the present application provides a method for extracting high-purity mogroside V from Luo Han Guo, which can increase the purity of mogroside V extracted from fresh dried fruit of Lo Han Guo from 0.3-0.5% to 50% or more to solve the above technical problem.
  • the present application provides a method for preparing high-purity mogroside V from Luo Han Guo, the method comprising:
  • step (3) is obtained, and after cooling, it is sent to an enzymatic hydrolysis tank, and an enzyme reagent is added for enzymatic hydrolysis;
  • Nanofiltration The filtrate obtained in the step (5) is separated and purified by a nanofiltration membrane, concentrated to a small volume, and dialyzed with water until the conductivity of the filtrate meets the requirements, and a retentate is obtained;
  • Decolorization the retentate obtained in the step (6) is decolorized with a decolorizing resin, and the effluent flowing through the resin column after decolorization is collected to obtain a decolorizing liquid;
  • the decoloring liquid obtained in the step (7) is concentrated in a vacuum, the vacuum pressure is controlled to -0.1 to 0.06 MPa, the temperature is controlled at 40 to 50 ° C, and the solid content is 40 to 60% to obtain a concentrated liquid;
  • Microwave drying and pulverization the concentrated liquid of the step (8) is subjected to microwave drying, pulverized and sieved, and bagged.
  • the original The material is saccharified Luo Han Guo fresh fruit, no other impurities, the degree of breakage is the standard of crushing to 6-10 petals.
  • the extraction mode is continuous countercurrent extraction, and the countercurrent extraction is performed by using hot water of 95 to 99 ° C with a weight of 2 to 4 times of fresh fruit. , extraction time 1 ⁇ 2h.
  • the centrifuge mode is a horizontal centrifuge + a disc centrifuge or a horizontal centrifuge + a tubular centrifuge Combined mode, centrifugal speed control is 10000 ⁇ 50000r/min.
  • the enzymatic reagent used in the enzymatic hydrolysis is Novozyme liquid enzyme, and the enzyme reagent is added in an amount of 0.01 by volume of the extract liquid. ⁇ 0.03w/v%, enzymatic hydrolysis temperature 30 ⁇ 50°C, enzymatic hydrolysis time 2-4h, enzymatic hydrolysis pH ⁇ 6.
  • the ultrafiltration membrane in the fifth possible implementation manner of the first aspect, has a molecular weight of 8 to 100,000 Daltons, and the operating pressure is 1.0 to 2.0 MPa, and the temperature is controlled. 10 to 25 ° C, the conductivity of the filtrate is required to be ⁇ 500 ⁇ s / cm.
  • the nanofiltration membrane in the sixth possible implementation manner of the first aspect, has a molecular weight ranging from 600 to 5000 Daltons, and the pressure control during operation is 2.0 to 4.0 MPa, and the temperature is controlled. 10 ⁇ 25 ° C, nanofiltration concentrated to 10% ⁇ 30% of the solids of the liquid, the filtrate conductivity ⁇ 500 ⁇ s / cm can meet the requirements.
  • the decolorizing resin is D941, LSA-700, DA201-H.
  • the concentrator in the eighth possible implementation manner of the first aspect, in the step (8), may be a single-effect, double-effect or three-effect concentrator.
  • the microwave drying control vacuum pressure is -0.1 to 0.06 MPa
  • the drying temperature is 40 to 50 ° C
  • the final product moisture control is ⁇ 5. %.
  • the extraction solvent of the invention is water, and the continuous countercurrent extraction method is used, compared with the extraction tank extraction method, not only the water consumption is small, the extraction time is shortened, but also the energy consumption is saved, and the continuous large-scale production is realized.
  • the permeate separated and purified by the nanofiltration membrane of the present invention and the water recovered by concentration can be returned as the extracting solution.
  • the agent not only saves water resources, but also has almost no sewage discharge, which plays a very good environmental protection effect.
  • the invention adopts the membrane technology to separate and purify, and has the advantages of separation and purification, obvious use of pure water solvent, and the like, and the organic solvent is discarded, which is simple in operation and safe and environmentally friendly, compared with other purification methods, such as adsorption and purification of macroporous resin.
  • the process is simple, inexpensive, and can achieve continuous large-scale industrial production.
  • Enzymatic hydrolysis 2158kg of centrifugation solution obtained in step (3) is put into the enzymolysis tank, and cellulase, pectinase and protease complex enzyme are added for enzymatic hydrolysis (complex enzyme is an imported Novozyme liquid enzyme), compound The enzyme addition amount was 0.01% of the volume of the extract, the enzymatic hydrolysis temperature was controlled at 32 ° C, the enzymatic hydrolysis time was controlled for 2 h, and the enzymatic hydrolysis pH was 4.5.
  • step (4) The enzymatic hydrolysate obtained in step (4) is passed through an ultrafiltration membrane of 8 to 100,000 Daltons, the pressure of the membrane is controlled to 1.2 MPa, and the temperature of the material is controlled by a cooling plate frame at 15 ° C; ultrafiltration to filtration When the liquid flow rate is one tenth of the initial flow rate, 500 L of pure water is added for dialysis, and the reaction is repeated three times until the filtrate conductivity is ⁇ 500 ⁇ s/cm, and the filtrate is collected.
  • Nanofiltration The 3,318 kg of the filtrate obtained in step (5) is separated and purified by a nanofiltration membrane with a molecular weight of 600 to 1000 Daltons.
  • the pressure of the membrane is controlled to 2.0 MPa, and the temperature of the material during dialysis is controlled at 15 ° C until filtration.
  • 500 L of pure water is added for dialysis, and the reaction is repeated three times until the filtrate conductivity is ⁇ 500 ⁇ s/cm, and the membrane retentate is collected to obtain a filtrate.
  • Microwave drying The concentrate is subjected to microwave drying, the vacuum pressure is controlled to -0.08 MPa, the drying temperature is 40 ° C, and the product moisture is finally controlled to ⁇ 5%; the final product is 16.38 Kg, and the mogroside V content is 50.1% (HPLC).
  • Enzymatic hydrolysis The 3080 kg of the centrifugation solution obtained in the step (3) is put into the enzymolysis tank, and the cellulase, pectinase and protease complex enzyme are added for enzymatic hydrolysis (the complex enzyme is an imported Novozyme liquid enzyme), and the compound is compounded.
  • the enzyme addition amount was 0.02% of the volume of the extract, the enzymatic hydrolysis temperature was controlled at 38 ° C, the enzymatic hydrolysis time was controlled for 3 h, and the enzymatic hydrolysis pH was 4.8.
  • step (4) the enzymatic hydrolysate obtained in step (4) is passed through an ultrafiltration membrane of 8 to 100,000 Daltons, the membrane pressure is controlled to 1.6 MPa, and the temperature of the material is controlled by a cooling plate frame to 15 ° C; ultrafiltration to filtration When the liquid flow rate is one tenth of the initial flow rate, 500 L of pure water is added for dialysis, and the reaction is repeated three times until the filtrate conductivity is ⁇ 500 ⁇ s/cm, and the filtrate is collected.
  • Nanofiltration The 4018 kg of the filtrate obtained in step (5) is separated and purified by a nanofiltration membrane with a molecular weight of 600 to 1000 Daltons.
  • the pressure of the membrane is controlled to 3.0 MPa, and the temperature of the material during dialysis is controlled at 15 ° C until filtration.
  • 500 L of pure water is added for dialysis, and the reaction is repeated three times until the filtrate conductivity is ⁇ 500 ⁇ s/cm, and the membrane retentate is collected to obtain a filtrate.
  • Microwave drying The concentrated liquid is subjected to microwave drying, the vacuum pressure is controlled to -0.085 MPa, the drying temperature is 45 ° C, and the product moisture is finally controlled to ⁇ 5%; the final product is 16.28 Kg, and the mogroside V content is 50.7% (HPLC).
  • Enzymatic hydrolysis 4176kg of centrifugation solution obtained in step (3) is put into the enzymolysis tank, and cellulase, pectinase and protease complex enzyme are added for enzymatic hydrolysis (complex enzyme is an imported Novozyme liquid enzyme), compound The enzyme addition amount was 0.03% of the volume of the extract, the enzymatic hydrolysis temperature was controlled at 44 ° C, the enzymatic hydrolysis time was controlled for 4 h, and the enzymatic hydrolysis pH was 5.3.
  • step (4) the enzymatic hydrolysate obtained in step (4) is passed through an ultrafiltration membrane of 8 to 100,000 Daltons, the pressure of the membrane is controlled to 2.0 MPa, and the temperature of the material is controlled by a cooling plate frame at 15 ° C; ultrafiltration to filtration When the liquid flow rate is one tenth of the initial flow rate, 500 L of pure water is added for dialysis, and the reaction is repeated three times until the filtrate conductivity is ⁇ 500 ⁇ s/cm, and the filtrate is collected.
  • Nanofiltration 5708 kg of the filtrate obtained in step (5) is separated and purified by a nanofiltration membrane with a molecular weight of 600 to 1000 Daltons.
  • the pressure of the membrane is controlled at 3.5 MPa, and the temperature of the material during dialysis is controlled at 15 ° C until filtration.
  • 500 L of pure water is added for dialysis, and the reaction is repeated three times until the filtrate conductivity is ⁇ 500 ⁇ s/cm, and the membrane retentate is collected to obtain a filtrate.
  • Step (6) The 280 kg of the nanofiltrate obtained in the step (6) is decolorized with a decolorizing resin, and the effluent flowing through the resin column after decolorization is collected, and the material is passed through the column and then pulverized with 2 column volumes of pure water to the effluent without sweetness. Collect all the effluent to obtain a decolorizing solution.
  • Microwave drying The concentrated liquid is subjected to microwave drying, the vacuum pressure is controlled to -0.09 MPa, the drying temperature is 50 ° C, and finally the product moisture is controlled to ⁇ 5%; the final product is 16.50 Kg, and the mogroside V content is 50.5% (HPLC).

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Proteomics, Peptides & Aminoacids (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Water Supply & Treatment (AREA)
  • Nutrition Science (AREA)
  • Food Science & Technology (AREA)
  • Polymers & Plastics (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Coloring Foods And Improving Nutritive Qualities (AREA)
  • Medicines Containing Plant Substances (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)

Abstract

本申请提供了一种从罗汉果中提取高纯度罗汉果苷V的方法，涉及一种罗汉果苷V的提取方法。其具体步骤包括：原料的预处理、提取、离心、酶解、超滤、纳滤、脱色、浓缩、微波干燥、粉碎。本发明采用了膜技术分离纯化，只使用纯水溶媒，舍弃有机溶剂，其操作简单、产品安全环保，工艺简单，物美价廉，能够实现连续化大规模工业生产。

Description

一种从罗汉果中提取高纯度罗汉果苷V的方法
本申请要求于2016年06月06日提交中国专利局、申请号为201610387839.4、发明名称为“一种从罗汉果中提取高纯度罗汉果苷V的方法”的中国专利申请的优先权，其全部内容通过引用结合在本申请中。
技术领域
本申请涉及罗汉果苷V的提取方法领域，尤其涉及一种从罗汉果中提取高纯度罗汉果苷V的方法。
背景技术
罗汉果(学名：Siraitia grosvenorii)是葫芦科多年生藤本植物。其叶心形，雌雄异株，夏季开花，秋天结果。中医以其果实入药，含有罗汉果甜苷、多种氨基酸和维生素等药用成分，主治肺热痰火咳嗽、咽喉炎、扁桃体炎、急性胃炎、便秘等。罗汉果又称为甜味素，因其甜度高、热量低而作为甜味剂广泛使用，常作为肥胖者和糖尿病患者的代用糖。
专利号CN200910044558.9中提供了一种罗汉果苷V含量大于60％的罗汉果提取物生产方法：破碎→糖化→水提取→浓缩→沉降离心→离子交换树脂精制→大孔树脂精制→浓缩→氧化铝精制→浓缩→喷雾干燥→成品的工艺流程。该发明工艺路线长，在分离纯化环节需要大孔树脂、氧化铝串联精制，操作复杂，成本高。
专利号CN200710003364.5中公开了一种脱色、脱苦的罗汉果提取物的制备方法：将提取液过滤、浓缩，用脱色树脂脱色后用乙醇洗脱，用脱味剂脱味，再经过浓缩、喷雾干燥，粉碎，得到脱色、脱苦的罗汉果提取物，其罗汉果甜甙V重量含量为60％以上(HPLC)。该发明在分离纯化环节也需要大孔树脂吸附纯化，然后有机溶剂洗脱，操作复杂，溶剂有残留，成本高。
专利号CN200710049737.2中提供了罗汉果苷V≥40％,罗汉果苷≥98％的牛奶白色罗汉果提取物的制备方法：水提取一浓缩一酶解一大孔吸附树脂精制一离子交换树脂脱色一浓缩一喷雾干燥制得。该发明在分离纯化环节也需要大孔树脂吸附纯化，然后有机溶剂洗脱，操作复杂，溶剂有残留，成本高。
目前罗汉果苷V分离纯化主要是用大孔树脂吸附，然后不同溶媒洗脱，得到一定含量的罗汉果苷V粗提物，粗提物进行脱盐、脱色，最后干燥、筛分、包装得产品；另有制备色谱及高速逆流色谱等。其中运用最广泛的是柱层析法，使用最多的是大孔吸附树脂分分离纯化，树脂型号如D101、AB-8等，但大孔树脂分离纯化操作繁琐，罗汉果苷V收率较低，且洗脱需要使用到有机溶剂，造成溶剂残留及环境污染等。制备色谱及高速逆流色谱，产品含量高，但一次性投资成本大，且有机溶剂使用量大，还是存在溶剂残留、环境污染等问题。
发明内容
本申请提供了一种从罗汉果中提取高纯度罗汉果苷V的方法，该主法能使罗汉果鲜果中提取的罗汉果苷V纯度从0.3～0.5％提升到50％以上，以解决以上的技术问题。
第一方面，本申请提供了一种从罗汉果中提取高纯度罗汉果苷V的制备方法，该方法包括：
(1)原料的预处理：将原料用破碎机破碎，每个鲜果破碎至6-10瓣为标准；
(2)提取：将步骤(1)所得原料采用连续逆流的提取方法，用热水连续逆流提取罗汉果苷V；提取液过200～400目不锈钢筛网，得滤液；
(3)离心：将步骤(2)所得提取液离心过滤，得离心液；
(4)酶解：将步骤(3)所得，降温到后送入酶解罐，加入酶试剂进行酶解；
(5)超滤：将步骤(4)所得酶解后离心液先过超滤膜，超滤至小体积，加水透析超滤膜，直到滤出液电导率符合要求为止，得滤出液；
(6)纳滤：将步骤(5)所得滤出液用纳滤膜进行分离纯化，浓缩至小体积，加水透析，直到滤出液电导率符合要求为止，得截留液；
(7)脱色：将步骤(6)所得截留液用脱色树脂进行脱色，经脱色后流过树脂柱的流出液收集，得脱色液；
(8)浓缩：将步骤(7)所得脱色液真空浓缩，真空压力控制-0.1～0.06MPa，温度控制40～50℃，浓缩至固形物为40～60％，得浓缩液；
(9)微波干燥、粉碎：将步骤(8)浓缩液进行微波干燥，粉碎过筛，装袋。
结合第一方面，在第一方面第一种可能的实现方式中，步骤(1)中，所述的原 料为经过糖化的罗汉果鲜果，无其他杂质，所述的破碎程度，为破碎至6-10瓣为标准。
结合第一方面，在第一方面第二种可能的实现方式中，步骤(2)中，所述提取方式为连续逆流提取，用2～4倍鲜果重量的95～99℃热水连续逆流提取，提取时间1～2h。
结合第一方面，在第一方面第三种可能的实现方式中，步骤(3)中，所述离心机方式为卧式离心机+碟式离心机或者卧式离心机+管式离心机的组合方式，离心转速控制10000～50000r/min。
结合第一方面，在第一方面第四种可能的实现方式中，步骤(4)中，所述酶解采用的酶试剂为诺维信液体酶，酶试剂添加量为提取料液体积的0.01～0.03w/v％，酶解温度30～50℃、酶解时间2-4h、酶解PH为3～6。
结合第一方面，在第一方面第五种可能的实现方式中，步骤(5)中，所述超滤膜分子量为8～10万道尔顿，运行时压力为1.0～2.0MPa、温度控制10～25℃、滤出液电导率要求≤500μs/cm为止。
结合第一方面，在第一方面第六种可能的实现方式中，步骤(6)中，所述纳滤膜分子量范围为600～5000道尔顿，运行时压力控制2.0～4.0MPa、温度控制10～25℃、纳滤浓缩至料液固形物10％～30％，滤出液电导率≤500μs/cm条件下均可达到要求。
结合第一方面，在第一方面第七种可能的实现方式中，步骤(7)中，所述脱色树脂为D941、LSA-700、DA201-H。
结合第一方面，在第一方面第八种可能的实现方式中，步骤(8)中，所述浓缩器可采用单效、双效或三效浓缩器。
结合第一方面，在第一方面第九种可能的实现方式中，步骤(9)中，所述微波干燥控制真空压力-0.1～0.06MPa，干燥温度40～50℃，最终产品水分控制＜5％。
本发明具有以下优势：
1)本发明提取溶剂为水，采用连续逆流的提取方法，相比提取罐提取的方式，不仅用水量小，提取时间缩短，而且也节约能耗，实现连续化规模化生产。
2)本发明纳滤膜分离纯化的透过液以及浓缩回收出的水，可以返回作为提取溶 剂，不仅节约了水资源，而且几乎没有污水排放，起到很好的环保效果。
3)本发明采用了膜技术分离纯化，相比其他纯化方式，比如大孔树脂吸附纯化，具有分离纯化效果明显、只使用纯水溶媒等优点，舍弃有机溶剂，其操作简单、产品安全环保，工艺简单，物美价廉，能够实现连续化大规模工业生产。
具体实施方式
本说明书中各个实施例之间相同相似的部分互相参见即可。
实施例1
1)原料的预处理：将提出杂质的1000Kg鲜果原料用破碎机破碎，一边破碎一边加入到连续逆流提取机组里。
2)提取：同时逆向加入2000kg 96℃热纯水进行连续逆流提取，设定提取时间1h。
3)离心：将步骤(2)所得提取液用卧螺离心机离心，冷却到30℃，然后再过碟式离心机，得2158kg离心液，料液温度为32℃。
4)酶解：将步骤(3)所得2158kg离心液打入酶解罐，加入纤维素酶、果胶酶、蛋白酶复合酶进行酶解(复合酶为一种进口诺维信液体酶)，复合酶添加量为提取液体积的0.01％，酶解温度控制32℃，酶解时间控制2h，酶解PH为4.5。
5)超滤：将步骤(4)所得酶解液过8～10万道尔顿的超滤膜，膜的压力控制1.2MPa，通过冷却板框将物料温度控制15℃；超滤至滤出液流速为起始流速的十分之一时，加入500L纯水进行透析，重复三次，直到滤出液电导率≤500μs/cm为止，收集得滤出液。
6)纳滤：将步骤(5)所得3318kg滤出液用分子量600～1000道尔顿的纳滤膜进行分离纯化，膜的压力控制2.0MPa，透析时物料温度控制在15℃，至滤出液流速为起始流速的十分之一时，加入500L纯水进行透析，重复三次，直到滤出液电导率≤500μs/cm为止，收集膜内截留液，得纳滤液。
7)脱色：将步骤(6)所得268kg纳滤液用脱色树脂进行脱色，经脱色后流过树脂柱的流出液收集，物料过柱完毕后用2倍柱体积纯水赶到流出液无甜味，收集所有 流出液得脱色液。
8)浓缩：将步骤(7)所得280kg脱色液使用单效浓缩器真空浓缩，真空压力控制-0.086MPa，温度为45℃，得浓缩液30.5Kg。
9)微波干燥：将浓缩液进行微波干燥，控制真空压力-0.08MPa，干燥温度40℃，最终控制产品水分＜5％；得最终产品16.38Kg，罗汉果苷V含量50.1％(HPLC)。
实施例2。
1)原料的预处理：将提出杂质的1000Kg鲜果原料用破碎机破碎，一边破碎一边加入到连续逆流提取机组里。
2)提取：同时逆向加入3000kg 98℃热纯水进行连续逆流提取，设定提取时间1.5h。
3)离心：将步骤(2)所得提取液用卧螺离心机离心，冷却到35℃，然后再过碟式离心机，得3080kg离心液，料液温度为38℃。
4)酶解：将步骤(3)所得3080kg离心液打入酶解罐，加入纤维素酶、果胶酶、蛋白酶复合酶进行酶解(复合酶为一种进口诺维信液体酶)，复合酶添加量为提取液体积的0.02％，酶解温度控制38℃，酶解时间控制3h，酶解PH为4.8。
5)超滤：将步骤(4)所得酶解液过8～10万道尔顿的超滤膜，膜的压力控制1.6MPa，通过冷却板框将物料温度控制15℃；超滤至滤出液流速为起始流速的十分之一时，加入500L纯水进行透析，重复三次，直到滤出液电导率≤500μs/cm为止，收集得滤出液。
6)纳滤：将步骤(5)所得4018kg滤出液用分子量600～1000道尔顿的纳滤膜进行分离纯化，膜的压力控制3.0MPa，透析时物料温度控制在15℃，至滤出液流速为起始流速的十分之一时，加入500L纯水进行透析，重复三次，直到滤出液电导率≤500μs/cm为止，收集膜内截留液，得纳滤液。
7)脱色：将步骤(6)所得276kg纳滤液用脱色树脂进行脱色，经脱色后流过树脂柱的流出液收集，物料过柱完毕后用2倍柱体积纯水赶到流出液无甜味，收集所有流出液得脱色液。
8)浓缩：将步骤(7)所得284kg脱色液使用单效浓缩器真空浓缩，真空压力控制-0.086MPa，温度为45℃，得浓缩液31.2Kg。
9)微波干燥：将浓缩液进行微波干燥，控制真空压力-0.085MPa，干燥温度45℃，最终控制产品水分＜5％；得最终产品16.28Kg，罗汉果苷V含量50.7％(HPLC)。
实施例3。
1)原料的预处理：将提出杂质的1000Kg鲜果原料用破碎机破碎，一边破碎一边加入到连续逆流提取机组里。
2)提取：同时逆向加入4000kg 98℃热纯水进行连续逆流提取，设定提取时间1.5h。
3)离心：将步骤(2)所得提取液用卧螺离心机离心，冷却到42℃，然后再过碟式离心机，得4176kg离心液，料液温度为44℃。
4)酶解：将步骤(3)所得4176kg离心液打入酶解罐，加入纤维素酶、果胶酶、蛋白酶复合酶进行酶解(复合酶为一种进口诺维信液体酶)，复合酶添加量为提取液体积的0.03％，酶解温度控制44℃，酶解时间控制4h，酶解PH为5.3。
5)超滤：将步骤(4)所得酶解液过8～10万道尔顿的超滤膜，膜的压力控制2.0MPa，通过冷却板框将物料温度控制15℃；超滤至滤出液流速为起始流速的十分之一时，加入500L纯水进行透析，重复三次，直到滤出液电导率≤500μs/cm为止，收集得滤出液。
6)纳滤：将步骤(5)所得5708kg滤出液用分子量600～1000道尔顿的纳滤膜进行分离纯化，膜的压力控制3.5MPa，透析时物料温度控制在15℃，至滤出液流速为起始流速的十分之一时，加入500L纯水进行透析，重复三次，直到滤出液电导率≤500μs/cm为止，收集膜内截留液，得纳滤液。
7)脱色：将步骤(6)所得280kg纳滤液用脱色树脂进行脱色，经脱色后流过树脂柱的流出液收集，物料过柱完毕后用2倍柱体积纯水赶到流出液无甜味，收集所有流出液得脱色液。
8)浓缩：将步骤(7)所得291kg脱色液使用单效浓缩器真空浓缩，真空压力控制-0.09MPa，温度为45℃，得浓缩液32.1Kg。
9)微波干燥：将浓缩液进行微波干燥，控制真空压力-0.09MPa，干燥温度50℃，最终控制产品水分＜5％；得最终产品16.50Kg，罗汉果苷V含量50.5％(HPLC)。
以上所述的本发明实施方式并不构成对本发明保护范围的限定。

Claims (10)

  1. 一种从罗汉果中提取高纯度罗汉果苷V的制备方法，其特征在于，其具体步骤如下：
    (1)原料的预处理：将原料用破碎机破碎，每个鲜果破碎至6-10瓣为标准；
    (2)提取：将步骤(1)所得原料采用连续逆流的提取方法，用热水连续逆流提取罗汉果苷V；提取液过200～400目不锈钢筛网，得滤液；
    (3)离心：将步骤(2)所得提取液离心过滤，得离心液；
    (4)酶解：将步骤(3)所得，降温到后送入酶解罐，加入酶试剂进行酶解；
    (5)超滤：将步骤(4)所得酶解后离心液先过超滤膜，超滤至小体积，加水透析超滤膜，直到滤出液电导率符合要求为止，得滤出液；
    (6)纳滤：将步骤(5)所得滤出液用纳滤膜进行分离纯化，浓缩至小体积，加水透析，直到滤出液电导率符合要求为止，得截留液；
    (7)脱色：将步骤(6)所得截留液用脱色树脂进行脱色，经脱色后流过树脂柱的流出液收集，得脱色液；
    (8)浓缩：将步骤(7)所得脱色液真空浓缩，真空压力控制-0.1～0.06MPa，温度控制40～50℃，浓缩至固形物为40～60％，得浓缩液；
    (9)微波干燥、粉碎：将步骤(8)浓缩液进行微波干燥，粉碎过筛，装袋。
  2. 根据权利要求1所述的一种从罗汉果中提取高纯度罗汉果苷V的制备方法，其特征在于：步骤(1)中，所述的原料为经过糖化的罗汉果鲜果，无其他杂质，所述的破碎程度，为破碎至6-10瓣为标准。
  3. 根据权利要求1所述的一种从罗汉果中提取高纯度罗汉果苷V的制备方法，其特征在于：步骤(2)中，所述提取方式为连续逆流提取，用2～4倍鲜果重量的95～99℃热水连续逆流提取，提取时间1～2h。
  4. 根据权利要求1所述的一种从罗汉果中提取高纯度罗汉果苷V的制备方法，其特征在于：步骤(3)中，所述离心机方式为卧式离心机+碟式离心机或者卧式离心机+管式离心机的组合方式，离心转速控制10000～50000r/min。
  5. 根据权利要求1所述的一种从罗汉果中提取高纯度罗汉果苷V的制备方 法，其特征在于：步骤(4)中，所述酶解采用的酶试剂为诺维信液体酶，酶试剂添加量为提取料液体积的0.01～0.03w/v％，酶解温度30～50℃、酶解时间2-4h、酶解PH为3～6。
  6. 根据权利要求1所述的一种从罗汉果中提取高纯度罗汉果苷V的制备方法，其特征在于：步骤(5)中，所述超滤膜分子量为8～10万道尔顿，运行时压力为1.0～2.0MPa、温度控制10～25℃、滤出液电导率要求≤500μs/cm为止。
  7. 根据权利要求1所述的一种从罗汉果中提取高纯度罗汉果苷V的制备方法，其特征在于：步骤(6)中，所述纳滤膜分子量范围为600～5000道尔顿，运行时压力控制2.0～4.0MPa、温度控制10～25℃、纳滤浓缩至料液固形物10％～30％，滤出液电导率≤500μs/cm条件下均可达到要求。
  8. 根据权利要求1所述的一种从罗汉果中提取高纯度罗汉果苷V的制备方法，其特征在于：步骤(7)中，所述脱色树脂为D941、LSA-700、DA201-H。
  9. 根据权利要求1所述的一种从罗汉果中提取高纯度罗汉果苷V的制备方法，其特征在于：步骤(8)中，所述浓缩器可采用单效、双效或三效浓缩器。
  10. 根据权利要求1所述的一种从罗汉果中提取高纯度罗汉果苷V的制备方法，其特征在于：步骤(9)中，所述微波干燥控制真空压力-0.1～0.06MPa，干燥温度40～50℃，最终产品水分控制＜5％。
PCT/CN2017/070140 2016-06-06 2017-01-04 一种从罗汉果中提取高纯度罗汉果苷v的方法 Ceased WO2017211079A1 (zh)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US16/307,309 US10743573B2 (en) 2016-06-06 2017-01-04 Method for extracting high-purity mogroside V from Siraitia grosvenorii

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN201610387839.4A CN106008645B (zh) 2016-06-06 2016-06-06 一种从罗汉果中提取罗汉果苷v的方法
CN201610387839.4 2016-06-06

Publications (1)

Publication Number Publication Date
WO2017211079A1 true WO2017211079A1 (zh) 2017-12-14

Family

ID=57089595

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2017/070140 Ceased WO2017211079A1 (zh) 2016-06-06 2017-01-04 一种从罗汉果中提取高纯度罗汉果苷v的方法

Country Status (3)

Country Link
US (1) US10743573B2 (zh)
CN (1) CN106008645B (zh)
WO (1) WO2017211079A1 (zh)

Families Citing this family (28)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106279339B (zh) * 2016-08-09 2019-01-01 湖南华诚生物资源股份有限公司 一种高纯度罗汉果苷v的分离纯化方法
CN106977574A (zh) * 2017-03-29 2017-07-25 桂林实力科技有限公司 从罗汉果中提取罗汉果甙v的方法
CN107397103A (zh) * 2017-08-25 2017-11-28 湖南华诚生物资源股份有限公司 一种罗汉果脱色风味浓缩汁的制备方法
CN108514008A (zh) * 2018-04-08 2018-09-11 湖南艾达伦科技有限公司 一种罗汉果吐司及制备方法
CN108606149A (zh) * 2018-04-08 2018-10-02 湖南艾达伦科技有限公司 一种罗汉果冰激凌的制备方法
CN108402129A (zh) * 2018-04-08 2018-08-17 湖南艾达伦科技有限公司 一种罗汉果蛋糕及其制备方法
CN108606122A (zh) * 2018-04-08 2018-10-02 湖南艾达伦科技有限公司 一种罗汉果菊花轻饮及其制备方法
CN108514010A (zh) * 2018-04-08 2018-09-11 湖南艾达伦科技有限公司 一种泡芙及其制备方法
CN108497248A (zh) * 2018-04-11 2018-09-07 湖南华诚生物资源股份有限公司 一种罗汉果浓缩汁及罗汉果果粉的制备方法
CN108902844A (zh) * 2018-06-28 2018-11-30 湖南艾达伦科技有限公司 一种桂花雪梨复合风味茶酱及其制备方法
CN108740699A (zh) * 2018-06-28 2018-11-06 湖南艾达伦科技有限公司 一种罗汉果紫薯果泥及其制备方法
CN108771174A (zh) * 2018-06-28 2018-11-09 湖南艾达伦科技有限公司 一种红心芭乐果酱及其制备方法
CN108782771A (zh) * 2018-06-28 2018-11-13 湖南艾达伦科技有限公司 一种罗汉果红枣杏仁露及其制备方法
CN108783345A (zh) * 2018-06-28 2018-11-13 湖南艾达伦科技有限公司 一种罗汉果菊花枸杞果酱及其制备方法
CN108770941A (zh) * 2018-06-28 2018-11-09 湖南艾达伦科技有限公司 一种罗汉果奇亚籽豆奶及其制备方法
CN108432883A (zh) * 2018-06-28 2018-08-24 湖南艾达伦科技有限公司 一种罗汉果银杏豆奶及其制备方法
CN108936451A (zh) * 2018-08-31 2018-12-07 湖南艾达伦科技有限公司 一种罗汉果胡萝卜复合果泥及其制备方法
CN109170883A (zh) * 2018-08-31 2019-01-11 湖南艾达伦科技有限公司 一种罗汉果水蜜桃复合果泥及其制备方法
CN108902312A (zh) * 2018-08-31 2018-11-30 湖南艾达伦科技有限公司 一种罗汉果风味发酵乳及其制备方法
CN109077268A (zh) * 2018-08-31 2018-12-25 湖南艾达伦科技有限公司 一种罗汉果红枣复合果泥及其制备方法
CN109043347A (zh) * 2018-08-31 2018-12-21 湖南艾达伦科技有限公司 一种罗汉果营养棒及其制备方法
CN109170727A (zh) * 2018-10-22 2019-01-11 湖南艾达伦科技有限公司 一种玫瑰蔓越莓风味茶酱及其制备方法
CN109170731A (zh) * 2018-10-23 2019-01-11 湖南艾达伦科技有限公司 一种罗汉果桂圆红枣果酱及其制备方法
CN110669095B (zh) * 2019-10-14 2022-05-27 广西壮族自治区科学技术情报研究所 一种高纯度罗汉果苷v的提取方法
CN111296708A (zh) * 2020-02-24 2020-06-19 湖南华诚生物资源股份有限公司 一种采用固定化酶技术生产罗汉果提取物的方法
CN112023705B (zh) * 2020-09-02 2021-04-27 山东格润内泽姆环保科技有限公司 巴氏消毒型全膜法药液提取浓缩方法
CN113455550B (zh) * 2021-06-30 2022-06-24 湖南绿蔓生物科技股份有限公司 一种罗汉果豆腐及其制备方法
CN115124585B (zh) * 2022-08-02 2024-05-28 湖南华诚生物资源股份有限公司 一种罗汉果提取物的清洁生产方法

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6124442A (en) * 1999-03-24 2000-09-26 Zhou; James H. Process for extracting triterpene glycosides from botanical sources
CN1683387A (zh) * 2005-03-16 2005-10-19 桂林莱茵生物科技股份有限公司 一种从罗汉果中提取罗汉果甜甙的方法
CN101177444A (zh) * 2006-11-11 2008-05-14 大闽食品（漳州）有限公司 一种从罗汉果中提取罗汉果甜甙的方法
CN101863946A (zh) * 2010-07-12 2010-10-20 湖南希尔天然药业有限公司 一种从干罗汉果中提取高含量罗汉果甜甙v的方法
EP2425721A1 (en) * 2010-09-03 2012-03-07 Purecircle SDN BHD High-purity mogrosides and process for their purification

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NZ549739A (en) * 2006-09-07 2009-01-31 Biovittoria Ltd Sweetening compositions and processes for preparing them
CN101007042B (zh) 2007-02-06 2010-05-19 桂林莱茵生物科技股份有限公司 一种脱色、脱苦的罗汉果提取物的制备方法
CN100572552C (zh) 2007-08-09 2009-12-23 桂林惠通生物科技有限公司 罗汉果苷v含量≥40%的罗汉果提取物及其制备方法
CN101690573B (zh) 2009-10-16 2012-01-25 长沙绿蔓生物科技有限公司 一种罗汉果苷v含量大于60%的罗汉果提取物生产方法
CN104558088A (zh) * 2015-01-23 2015-04-29 江西海富生物工程有限公司 一种从罗汉果中提取罗汉果苷v的方法
CN105218612B (zh) * 2015-09-30 2017-10-03 大闽食品（漳州）有限公司 一种提高罗汉果甜苷中罗汉果甜甙v纯度的方法

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6124442A (en) * 1999-03-24 2000-09-26 Zhou; James H. Process for extracting triterpene glycosides from botanical sources
CN1683387A (zh) * 2005-03-16 2005-10-19 桂林莱茵生物科技股份有限公司 一种从罗汉果中提取罗汉果甜甙的方法
CN101177444A (zh) * 2006-11-11 2008-05-14 大闽食品（漳州）有限公司 一种从罗汉果中提取罗汉果甜甙的方法
CN101863946A (zh) * 2010-07-12 2010-10-20 湖南希尔天然药业有限公司 一种从干罗汉果中提取高含量罗汉果甜甙v的方法
EP2425721A1 (en) * 2010-09-03 2012-03-07 Purecircle SDN BHD High-purity mogrosides and process for their purification

Also Published As

Publication number Publication date
US20190133166A1 (en) 2019-05-09
US10743573B2 (en) 2020-08-18
CN106008645B (zh) 2017-12-15
CN106008645A (zh) 2016-10-12

Similar Documents

Publication Publication Date Title
WO2017211079A1 (zh) 一种从罗汉果中提取高纯度罗汉果苷v的方法
CN100457765C (zh) 水苏糖的生产方法及利用地黄生产水苏糖和梓醇的方法
CN108752231B (zh) 从甜茶中提取茶氨酸以及同时提取甜茶苷和茶多酚的方法
CN109593034B (zh) 一种从银杏叶提取废液中制备莽草酸的方法
CN109674843B (zh) 一种干罗汉果综合利用的提取纯化方法
CN108516997A (zh) 一种从甜茶叶中提取甜茶苷的方法
CN103145869B (zh) 一种含有罗汉果多糖的提取物的制备方法
CN102702284A (zh) 高纯度甜茶苷的生产工艺
CN113637038B (zh) 一种从甜茶叶中提取无苦涩味甜茶苷和甜茶多酚的方法
CN106366092B (zh) 一种从东革阿里中分离宽缨酮的工业制备方法
CN115109112B (zh) 一种提高罗汉果甜苷v含量的罗汉果甜苷工业生产方法
CN107188911B (zh) 利用大豆糖蜜提取大豆低聚糖和大豆异黄酮的方法
CN102603478B (zh) 从赤藓糖醇多次结晶后的母液中分离提纯赤藓糖醇的方法
WO2018166029A1 (zh) 一种以亚临界水解吸附技术分离纯化罗汉果甜苷ⅴ的方法
CN109320400B (zh) 一种从罗汉果甜苷生产废液中提取天然甘露醇的方法
CN110917240B (zh) 一种从青钱柳中分离多种有效成分的连续化方法
CN104017028B (zh) 从异麦芽酮糖母液中分离异麦芽酮糖和海藻酮糖的方法
CN106589010A (zh) 一种同时生产l‑阿拉伯糖和d‑半乳糖的方法
WO2013159263A1 (zh) 一种用蔗髓为原料生产高纯度l-阿拉伯糖的方法
CN106832050B (zh) 从罗汉果生产废渣中分离果胶的方法
CN110078775B (zh) 高含量甜茶苷、甜茶多酚的环保生产方法
CN102212092A (zh) 一种高纯度栀子苷的制备方法
CN102669523B (zh) 功能性大豆低聚糖的制备方法
CN108516996B (zh) 罗汉果益生元的提取方法及同时提取罗汉果甜苷v的方法
JP6768970B2 (ja) ルブソシドの調製方法

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 17809520

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 17809520

Country of ref document: EP

Kind code of ref document: A1