阅读说明：本技术 一种分离辣椒红素提取剩余物中糖酯的方法 (Method for separating sugar ester in capsorubin extraction residues ) 是由 高伟 路姣姣 齐立军 彭静维 连运河 于 2021-06-21 设计创作，主要内容包括：本发明涉及天然产物提取领域,特别是一种分离辣椒红素提取剩余物中糖酯的方法。本发明所述方法包括将辣椒红素提取剩余物溶于有机溶剂后通过耐有机溶剂纳滤膜对糖酯进行分离的操作；所述有机溶剂为乙酸乙酯、植物抽提溶剂或丙酮。本发明所述方法可实现辣椒红色素提取剩余物中糖酯与杂质成分的有效分离,通过一步操作即可实现糖酯的有效纯化,步骤简单,能耗低,易于实现工业化连续生产。(The invention relates to the field of natural product extraction, in particular to a method for separating sugar ester in capsorubin extraction residues. The method comprises the steps of dissolving capsorubin extraction residues in an organic solvent, and separating sugar ester by an organic solvent-resistant nanofiltration membrane; the organic solvent is ethyl acetate, plant extraction solvent or acetone. The method can realize effective separation of sugar ester and impurity components in the capsanthin extraction residues, can realize effective purification of the sugar ester by one-step operation, has simple steps and low energy consumption, and is easy to realize industrial continuous production.)

1. A method for separating sugar esters in capsorubin extraction residues is characterized by comprising the operation of dissolving the capsorubin extraction residues in an organic solvent and then separating the sugar esters through an organic solvent-resistant nanofiltration membrane;

the organic solvent is ethyl acetate, plant extraction solvent or acetone.

2. The method as claimed in claim 1, wherein the organic solvent resistant nanofiltration membrane is a composite membrane, and comprises a base membrane and a separation layer, wherein the base membrane is made of polyacrylonitrile, and the separation layer is an organic silicone coating coated on the surface of the base membrane.

3. The method according to claim 1, wherein the capsorubin extraction residue has a sugar ester content of 38 to 45%, a viscosity of 500 to 1000 Pa-s, and a color value of 80 to 160.

4. The method of claim 1, wherein said capsorubin extraction residue is prepared by:

1) extracting the capsicum particles by using an organic solvent to obtain an extracting solution, and removing the organic solvent in the extracting solution to obtain a capsorubin crude product;

2) purifying the capsorubin crude product by a hydration degumming method, and taking a water solution containing colloid;

3) and extracting the aqueous solution containing the colloid by using an organic solvent to obtain an extract, and removing the organic solvent in the extract to obtain the capsorubin extraction residue.

5. The method according to any one of claims 1 to 4, wherein the temperature of the system is controlled to be 0-40 ℃ in the process of passing through the organic solvent-resistant nanofiltration membrane; preferably 30 to 35 ℃.

6. The method according to any one of claims 1 to 4, wherein the operating pressure in the organic solvent resistant nanofiltration membrane treatment process is 1.3 to 2.8MPa, preferably 1.6 to 2.0 MPa.

7. The method according to any one of claims 1 to 4, wherein the mass percentage of the sugar ester mixture to be purified in the organic solvent is 3 to 30%.

Technical Field

The invention relates to the field of natural product extraction, in particular to a method for separating sugar ester in residual liquid of capsorubin extraction.

Background

The sugar ester is obtained by esterifying a fatty acid with a compound having a plurality of hydroxyl groups such as glucose or sucrose. Sugar esters can be classified into monoesters, diesters, and triesters, depending on the degree of esterification. Most sugar esters are non-toxic, non-irritating and odorless, but fatty acid esters with less than twelve carbon atoms have a bitter taste. Sugar ester is a kind of nonionic biosurfactant, widely used in food, medicine and cosmetic industries, and part of sugar ester and its derivatives also have antitumor and antibacterial activities.

Sugar ester-containing by-products are produced during the production of capsanthin. For example, in the process of producing capsanthin by hydration degumming, the residual colloid water contains a large amount of sugar ester and other water-soluble substances, so that the viscosity and the precipitate are high, the fluidity is poor, and the treatment is difficult. In the existing production process of capsanthin, the yield of byproducts accounts for about 10 percent of the total capsanthin yield. If the sugar ester in the capsorubin byproduct can be extracted and further utilized, the additional value of the production of the capsorubin can be improved, but the method for separating the sugar ester in the prior art is generally complex and cannot be applied on a large scale.

Disclosure of Invention

In view of the above problems in the prior art, the present invention provides a method for separating sugar ester in residual liquid of capsorubin extraction, which is simple in operation.

The method comprises the steps of dissolving capsorubin extraction residues in an organic solvent, and separating sugar ester by an organic solvent-resistant nanofiltration membrane;

the organic solvent is ethyl acetate, plant extraction solvent or acetone.

The invention discovers for the first time that sugar esters in capsorubin extraction residues can be effectively separated from other components by processing the sugar esters by the method.

Preferably, the organic solvent resistant nanofiltration membrane is a composite membrane and comprises a base membrane and a separation layer, wherein the base membrane is made of polyacrylonitrile, and the separation layer is an organic silicone coating coated on the surface of the base membrane. The organic solvent resistant nanofiltration membrane has a good separation effect on sugar ester and the impurity components.

Preferably, the content of sugar ester in the capsorubin extraction residues is 38-45%, the viscosity is 50-1000 Pa.s, and the color value is 80-160.

Preferably, the residue of the capsanthin extract is prepared by the following method:

1) extracting the capsicum particles by using an organic solvent to obtain an extracting solution, and removing the organic solvent in the extracting solution to obtain a capsorubin crude product;

2) purifying the capsorubin crude product by a hydration degumming method, and taking a water solution containing colloid;

3) and extracting the aqueous solution containing the colloid by using an organic solvent to obtain an extract, and removing the organic solvent in the extract to obtain the capsorubin extraction residue.

Preferably, the organic solvent in the step 1) is one or two of acetone or n-hexane;

preferably, the mass ratio of the capsorubin crude product to the water in the step 2) is 1: 2-4;

preferably, the organic solvent in step 3) is ethyl acetate

The sugar ester content in the extraction residues is about 38-45%, the viscosity is 1000 Pa.s, the color value is 80-160, after the extraction residues are treated by an organic solvent-resistant nanofiltration membrane, the sugar ester enters a permeate liquid along with the membrane, after the organic solvent is removed by a trapped liquid, the sugar ester content is less than or equal to 10%, the viscosity is less than or equal to 200 P.s, the color value is 190-230, the quality of the product is similar to that of the capsanthin pigment obtained in the hydration degumming step, and the capsanthin pigment can be directly sold as a capsanthin product.

Preferably, the temperature of the system is controlled to be 0-40 ℃ in the process of passing through the organic solvent resistant nanofiltration membrane.

Further preferably, the temperature of the system is controlled to be 30-35 ℃.

Preferably, the operating pressure in the organic solvent resistant nanofiltration membrane treatment process is 1.3-2.8 MPa.

Further preferably, the temperature of the system is controlled to be 1.6-2.0 MPa.

Preferably, the mass percentage of the sugar ester mixture to be purified in the organic solvent is 3-30%. When the content of sugar ester is low, the separation efficiency is low and the cost is high; when the sugar ester content is more than 30%, the viscosity of the feed liquid is high, the feed liquid is not easy to dissolve, the operation difficulty is increased, and the separation effect is poor.

The invention has the following beneficial effects:

1) the method can realize effective separation of sugar ester and impurity components in the capsanthin extraction residues, realizes effective purification of the sugar ester, has simple steps and low energy consumption, and is easy to realize industrial continuous production.

2) The invention has ideal purification effect on sugar ester, and the purity of the purified sugar ester can reach about 90 percent.

3) The method has the advantages that the purity and the concentration of the capsorubin in the residual liquid after the organic solvent resistant nanofiltration membrane is used are high, and the capsorubin can be directly sold as a product after the organic solvent is removed.

Detailed Description

The process of the invention is described below by means of specific embodiments. In addition, the embodiments should be considered illustrative, and not restrictive, of the scope of the invention, which is defined solely by the claims.

The capsorubin extraction residues referred to in the examples were prepared by the following method:

1) extracting the capsicum particles by using acetone to obtain an extracting solution, and evaporating to remove the acetone in the extracting solution to obtain a capsorubin crude product;

2) adding the capsorubin crude product into the capsorubin crude product according to the proportion of 1: 3, adding water into the solid-to-liquid ratio to carry out hydration treatment, standing the mixed solution, and taking a water solution containing colloid after layering;

3) and (3) extracting the aqueous solution containing the colloid by using ethyl acetate through liquid-liquid extraction, standing and layering to obtain an organic phase, and concentrating to remove the ethyl acetate to obtain the capsorubin extraction residue.

Example 1

The embodiment relates to a method for separating sugar ester in capsorubin extraction residues, which comprises the following steps:

dissolving the capsorubin extraction residue 700g (color value 145.2, viscosity 685 Pa.s, sugar ester content 43.7%) in 10L ethyl acetate, and filtering to remove solid insoluble substance; putting the feed liquid into a feed liquid tank of an organic solvent-resistant nanofiltration membrane device, starting a power supply, operating the device, keeping the temperature of the feed liquid at 30-35 ℃ and the operating pressure at 1.6-2.1MPa in the separation process, circulating the feed liquid at the upstream side of the membrane, collecting primary permeate at the downstream side, and closing the device when the collection amount of the primary permeate is 7L; adding 6L of ethyl acetate into the feed liquid tank, performing secondary separation, starting the device, keeping the temperature at 30-35 ℃, operating pressure at 1.6-2.1MPa, collecting secondary permeate at the downstream, and closing the equipment when the collection amount of the secondary permeate is 6L; adding 6L of ethyl acetate into the feed liquid tank, performing three-time separation, starting the device, keeping the temperature at 30-35 ℃, operating pressure at 1.6-2.1MPa, collecting three-time permeate at the downstream, and closing the device and discharging trapped fluid when the collection amount of the three-time permeate is 6L.

Respectively concentrating the three permeate solutions and the trapped solution to obtain a final material, wherein the first permeate solution is 123.5g (color value is 23.4, sugar ester purity is 98.3%, and the final material is solidified after standing); 102.3g of secondary permeate (color value is 18.7, sugar ester purity is 97.4%, and solidification is carried out after standing); 62.3g of the third permeate (color value 9.3, sugar ester purity 96.2%, viscosity 1052pa · s), and the total yield of the sugar ester after the third purification is 91.85% by calculation.

411.9g of trapped fluid (color value 233.7, sugar ester content 6.1%, viscosity 185Pa s), which can be sold directly as capsorubin finished product after organic solvent is removed.

Example 2

The embodiment relates to a method for separating sugar ester in capsorubin extraction residues, which comprises the following steps:

dissolving 2100g of capsorubin extraction residue (color value 145.2, viscosity 685Pa · s, sugar ester content 43.7%) in 30L of ethyl acetate, and filtering to remove solid insoluble substances; putting the feed liquid into a feed liquid tank of an organic solvent-resistant nanofiltration membrane device, starting a power supply, operating the device, keeping the temperature of the feed liquid at 30-35 ℃ and the operating pressure at 1.6-2.1MPa in the separation process, circulating the feed liquid at the upstream side of the membrane, collecting primary permeate at the downstream side, and closing the device when the collection amount of the primary permeate is 21L; adding 18L of ethyl acetate into the feed liquid tank, performing secondary separation, starting the device, keeping the temperature at 30-35 ℃, operating pressure at 1.6-2.1MPa, collecting secondary permeate at the downstream, and closing the equipment when the collection amount of the secondary permeate is 18L; adding 18L of ethyl acetate into the feed liquid tank, performing three-time separation, starting the device, keeping the temperature at 30-35 ℃, operating pressure at 1.6-2.1MPa, collecting three-time permeate at the downstream, and closing the equipment when the collection amount of the three-time permeate is 18L; adding 18L of ethyl acetate into the feed liquid tank, separating for four times, starting the device, keeping the temperature at 30-35 ℃, operating pressure at 1.6-2.1MPa, collecting four times of permeate at downstream, and closing the device and discharging trapped fluid when the collection amount of the four times of permeate is 18L.

Concentrating the four-time permeate and the trapped fluid respectively to obtain final material, wherein the first permeate is 370.5g (color value is 50.3, and sugar ester content is 98.2%, and then solidifying is carried out after standing); 306.9g of secondary permeating liquid (color value is 46.8, sugar ester content is 97.6 percent, and solidification is carried out after standing); 153.2g of third permeating liquid (color value 43.5, sugar ester content 96.8%, viscosity 1052Pa · s), 53.0g of fourth permeating liquid (color value 41.2, sugar ester content 95.2%, viscosity 602.3Pa · s); the total yield of sugar esters after four purifications was 93.94%.

1216.4g of trapped liquid (color value 216.5, sugar ester content 4.6%, viscosity 185 pas). The trapped fluid can be directly sold as a capsorubin finished product after the organic solvent is removed.

Example 3

The embodiment relates to a method for separating sugar ester in capsorubin extraction residues, which comprises the following steps:

dissolving 700g (color value 145.2, viscosity 685 Pa.s and sugar ester content 43.7%) of capsorubin extraction residue in 10L of plant extraction solvent, and filtering to remove solid insoluble substance; putting the feed liquid into a feed liquid tank of an organic solvent-resistant nanofiltration membrane device, starting a power supply, operating the device, keeping the temperature of the feed liquid at 30-35 ℃ and the operating pressure at 1.6-2.1MPa in the separation process, circulating the feed liquid at the upstream side of the membrane, collecting primary permeate at the downstream side, and closing the device when the collection amount of the primary permeate is 7L; adding 6L of ethyl acetate into the feed liquid tank, performing secondary separation, starting the device, keeping the temperature at 30-35 ℃, operating pressure at 1.6-2.1MPa, collecting secondary permeate at the downstream, and closing the equipment when the collection amount of the secondary permeate is 6L; adding 6L of ethyl acetate into the feed liquid tank, performing three-time separation, starting the device, keeping the temperature at 30-35 ℃, operating pressure at 1.6-2.1MPa, collecting three-time permeate at the downstream, and closing the device and discharging trapped fluid when the collection amount of the three-time permeate is 6L.

Respectively concentrating the three permeate solutions and the trapped solution to obtain a final material, wherein the first permeate solution is 121.3g (color value is 24.5, sugar ester purity is 97.5%, and the final material is solidified after standing); 99.5g of secondary permeate (color value of 20.3, sugar ester purity of 96.5%, solidification after standing); 62.3g of the third permeate (color value 10.5, sugar ester purity 95.3%, viscosity 1052pa · s), and the total yield of the sugar ester after the third purification is 89.46% by calculation.

416.9g of trapped fluid (color value 232.5, sugar ester content 7.8%, viscosity 185Pa s), which can be sold directly as capsorubin finished product after organic solvent is removed.

Comparative example 1

Compared with example 1, the capsorubin extraction residue was dissolved using other organic solvents, and methanol solvent was used.

The result shows that the methanol has poor dissolving effect on the material to be separated, the solubility of the material to be separated is less than 1 percent, and the effective separation of residual sugar ester in capsorubin extraction residues cannot be realized through an organic solvent resistant nanofiltration membrane.

Although the invention has been described in detail hereinabove by way of general description, specific embodiments and experiments, it will be apparent to those skilled in the art that many modifications and improvements can be made thereto based on the invention. Accordingly, such modifications and improvements are intended to be within the scope of the invention as claimed.