Separation and purification system for co-production of glucuronic acid and D-chiro-inositol

Abstract

The utility model relates to the technical field of D-chiro-inositol, in particular to a separation and purification system for co-production of glucuronic acid and D-chiro-inositol. Comprising first filtering equipment, second filtering equipment, a cationic resin column, an anionic resin column, first concentration equipment, second concentration equipment, a buffer tank, a first ethanol storage tank, a first filtering device, a first filtrate storage tank, a filter cake storage tank, a second ethanol storage tank, a second filtering device, a second filtrate storage tank and a concentration device which are communicated with a feed liquid conveying pipeline, the device comprises a first drying device, a glucuronic acid storage tank, a second drying device and a D-chiro-inositol storage tank. The separation and purification system is reasonable in design, and compared with existing resin separation, the treatment capacity is large, operation is easy and convenient, and the yield and the separation efficiency are greatly improved.

Description

Technical Field

[0001] The utility model relates to the technical field of D-chiro-inositol, in particular to a separation and purification system for co-producing glucuronic acid and D-chiro-inositol. Background Art

[0002] D-Chiro Inos itol (DCI) is one of the nine isomers of inositol that is optically active and is also the biologically active isomer of vitamin B8. It exists at relatively high levels in plants such as buckwheat seeds, soybeans, and some insects, mostly in the form of methylated or glycosylated derivatives. It is a biodegradable product of buckwheat sugar alcohol. It has the function of sensitizing insulin and promoting liver fat metabolism, can significantly reduce blood sugar content, and has a significant therapeutic effect on diabetes. In addition, DCI also has the effects of improving Polycystic Ovarian Syndrome (PCOS), anti-oxidation, anti-aging, and scavenging free radicals, and has good utilization value.

[0003] Glucuronic acid, also known as glucuronic acid for short, is a compound formed by the oxidation of the primary alcohol hydroxyl group of glucose to a carboxyl group. It is widely distributed in animals and plants. In plants, it exists in gums such as gum arabic in the form of monoglucuronic acid and is an important component of pectin, mucus and higher polysaccharides. In animals, glucuronic acid forms a complex with glucosinolate and is stored in tissues. The aqueous solution of glucuronic acid is unstable and easily forms 3,6-glucuronolactone and is in a state of tautomerization equilibrium. When heated and in the presence of strong acid, D-glucuronic acid is also prone to decarboxylation to generate CO 2 , furan and other cracking products. Glucuronic acid can combine with toxins in the body to form non-toxic glucuronic acid conjugates and be excreted. It has the function of protecting the liver and detoxifying. It is used for hepatitis, cirrhosis, food and drug poisoning. Glucuronic acid is also an important component of connective tissue and can be used to treat arthritis and collagen diseases.

[0004] At present, the prior art discloses a process for co-producing D-chiro-inositol and glucuronic acid. The process is to use myo-inositol as a raw material, add inositol dehydrogenase and inositol monoketone isomerase, and the converted liquid after the reaction is filtered, and the collected filtrate is added with inositol oxidase, and a feed liquid containing D-chiro-inositol and glucuronic acid is obtained after the reaction, and then undergo resin adsorption, analysis and other operations to obtain D-chiro-inositol product and glucuronic acid; however, the process adopts resin separation when separating D-chiro-inositol and glucuronic acid, and then adopts an analytical agent for analysis, and the above separation method has low yield, small processing volume, low efficiency, and generates more sewage; therefore, in view of the above problems, it is necessary to establish a separation and purification system for co-producing D-chiro-inositol and glucuronic acid. Utility Model Content

[0005] The first technical problem to be solved by the utility model is: in view of the deficiencies in the prior art, a separation and purification system for co-producing glucuronic acid and D-chiro-inositol is provided, by which the effective separation of D-chiro-inositol and glucuronic acid can be achieved, thereby greatly improving the yield and separation efficiency.

[0006] In order to solve the above technical problems, the technical solution of the utility model is:

[0007] A separation and purification system for co-producing glucuronic acid and D-chiro-inositol, comprising a first filtering device connected to a feed liquid conveying pipeline, wherein the filtrate outlet of the first filtering device is connected to a second filtering device; the filtrate outlet of the second filtering device is connected to a cationic resin column, and the liquid outlet of the cationic resin column is connected to an anionic resin column; the liquid outlet of the anionic resin column is connected to a first concentrating device, and the concentrated liquid outlet of the first concentrating device is connected to the second concentrating device; the concentrated liquid outlet of the second concentrating device is connected to a buffer tank, the liquid inlet of the buffer tank is connected to a first ethanol storage tank, and the material outlet of the buffer tank is connected to a first filtering device, The liquid outlet of the first filter device is connected to the first filtrate storage tank, and the material outlet of the first filter device is connected to the filter cake storage tank; the liquid inlet of the filter cake storage tank is connected to the second ethanol storage tank, the material outlet of the filter cake storage tank is connected to the second filter device, and the liquid outlet of the second filter device is connected to the second filtrate storage tank; the liquid outlets of the first filtrate storage tank and the second filtrate storage tank are connected to the concentrating device, the concentrated liquid outlet of the concentrating device is connected to the first drying device, and the material outlet of the first drying device is connected to the glucuronic acid storage tank; the material outlet of the second filter device is connected to the second drying device, and the material outlet of the second drying device is connected to the D-chiro-inositol storage tank.

[0008] As an improved technical solution, the first filtering device is a ceramic membrane filtering device with a pore size of 20-100 nm; the second filtering device is an ultrafiltration membrane filtering device with a molecular weight cutoff of 1000-10000 Da.

[0009] As an improved technical solution, the filler in the cationic resin column is SQD67, and the filler in the anionic resin column is LS-109D.

[0010] As an improved technical solution, the first concentration device is a nanofiltration membrane concentration device with a molecular weight cutoff of 150-200Da; the second concentration device is a multi-effect concentrator.

[0011] As an improved technical solution, the first filter device and the second filter device are both plate and frame filters.

[0012] As an improved technical solution, the first drying device is a double-cone dryer, and the second drying device is a vibrating fluidized bed.

[0013] After adopting the above technical solution, the beneficial effects of the utility model are:

[0014] The separation and purification system for co-producing glucuronic acid and D-chiro-inositol comprises a first filtering device connected to a feed liquid conveying pipeline, wherein the filtrate outlet of the first filtering device is connected to a second filtering device; the filtrate outlet of the second filtering device is connected to a cationic resin column, and the liquid outlet of the cationic resin column is connected to an anionic resin column; the liquid outlet of the anionic resin column is connected to a first concentrating device, and the concentrated liquid outlet of the first concentrating device is connected to the second concentrating device; the concentrated liquid outlet of the second concentrating device is connected to a buffer tank, the liquid inlet of the buffer tank is connected to a first ethanol storage tank, and the material outlet of the buffer tank is connected to the first filtering device. The liquid outlet of the first filter device is connected to the first filtrate storage tank, and the material outlet of the first filter device is connected to the filter cake storage tank; the liquid inlet of the filter cake storage tank is connected to the second ethanol storage tank, the material outlet of the filter cake storage tank is connected to the second filter device, and the liquid outlet of the second filter device is connected to the second filtrate storage tank; the liquid outlets of the first filtrate storage tank and the second filtrate storage tank are connected to the concentrator, the concentrated liquid outlet of the concentrator is connected to the first drying device, and the material outlet of the first drying device is connected to the glucuronic acid storage tank; the material outlet of the second filter device is connected to the second drying device, and the material outlet of the second drying device is connected to the D-chiro-inositol storage tank. In actual production, the conversion liquid containing D-chiro-inositol and glucuronic acid enters the interior of the first filtering device through a feed liquid conveying pipeline, the filtrate collected after filtration enters the second filtering device, the filtrate collected after filtration enters the interior of the cationic resin column, the collected effluent enters the interior of the anionic resin column, the collected effluent enters the first concentrating device, the concentrated liquid enters the second concentrating device, the concentrated liquid enters the cache tank, and the ethanol in the first ethanol storage tank also enters the interior of the cache tank. After heating and stirring for a period of time, the feed liquid in the cache tank enters the interior of the first filtering device, and is filtered. The filtered filtrate enters the first filtrate storage tank, the filtered filter cake enters the filter cake storage tank, and then the ethanol in the second ethanol storage tank also enters the filter cake storage tank. After heating and stirring for a period of time, the feed liquid in the filter cake storage tank enters the interior of the second filtering device, and the filtered filtrate enters the second filtrate storage tank. The filtrate in the first filtrate storage tank and the second filtrate storage tank enters the interior of the concentrator and is concentrated. The obtained concentrated liquid enters the interior of the first drying device, and the dried product enters the glucuronic acid storage tank for storage; the filter cake collected after filtering by the second filtering device passes through the interior of the second drying device, and the dried product is stored in the D-chiro-inositol storage tank. The above separation and purification system is reasonably designed, and compared with the existing resin separation, it has a large processing capacity, is simple and convenient to operate, and greatly improves the yield and separation efficiency.

[0015] Since the first filter device is a ceramic membrane filter device with a pore size of 20-100 nm, and the second filter device is an ultrafiltration membrane filter device with a molecular weight cutoff of 1000-10000 Da, the first filter device and the second filter device can effectively remove whole cells and a small amount of protein molecules.

[0016] Since the filler in the cation resin column is SQD67 and the filler in the anion resin column is LS-109D, the cation resin column and anion resin column using the above fillers can effectively remove metal ions and pigments.

[0017] Since the first concentration device is a nanofiltration membrane concentration device with a molecular weight cutoff of 150-200Da; the second concentration device is a multi-effect concentrator. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] Figure 1 This is a schematic structural diagram of a separation and purification system for co-producing glucuronic acid and D-chiro-inositol according to the utility model;

[0019] Among them, 1-liquid conveying pipeline, 2-first filtering equipment, 3-second filtering equipment, 4-cationic resin column, 5-anion resin column, 6-first concentration equipment, 7-second concentration equipment, 8-buffer tank, 9-first ethanol storage tank, 10-first filtering device, 11-first filtrate storage tank, 12-filter cake storage tank, 13-second ethanol storage tank, 14-second filtering device, 15-second filtrate storage tank, 16-concentrating device, 17-first drying device, 18-glucuronic acid storage tank, 19-second drying device, 20-D-chiro-inositol storage tank. DETAILED DESCRIPTION

[0020] In order to make the purpose, technical solution and advantages of the utility model more clear, the utility model is further described in detail below in conjunction with the accompanying drawings and embodiments. It should be understood that the specific embodiments described here are only used to explain the utility model and are not used to limit the utility model.

[0021] A separation and purification system for co-producing glucuronic acid and D-chiro-inositol, such as Figure 1As shown, it includes a first filtering device 2 (a ceramic membrane filtering device with a pore size of 20-100nm) connected to a feed liquid conveying pipeline 1, the filtrate outlet of the first filtering device 2 is connected to a second filtering device 3 (an ultrafiltration membrane filtering device with a molecular weight cutoff of 1000-10000Da); the filtrate outlet of the second filtering device 3 is connected to a cationic resin column 4 (with a filler of SQD67), and the liquid outlet of the cationic resin column 4 is connected to an anion resin column 5 (with a filler of LS-109D); the liquid outlet of the anion resin column 5 is connected to a first concentrating device 6 (a nanofiltration membrane concentrating device with a molecular weight cutoff of 150-200Da), and the concentrated liquid outlet of the first concentrating device 6 is connected to a second concentrating device 7 (a multi-effect concentrator--a triple-effect concentrator); the concentrated liquid outlet of the second concentrating device 7 is connected to a buffer tank 8, and the liquid inlet of the buffer tank 8 is connected to a first ethanol storage tank 9, and the buffer The discharge port of tank 8 is connected to the first filtering device 10 (plate and frame filter), the liquid outlet of the first filtering device 10 is connected to the first filtrate storage tank 11, and the discharge port of the first filtering device 10 is connected to the filter cake storage tank 12; the liquid inlet of the filter cake storage tank 12 is connected to the second ethanol storage tank 13, the discharge port of the filter cake storage tank 12 is connected to the second filtering device 14 (plate and frame filter), and the liquid outlet of the second filtering device 14 is connected to the second filtrate storage tank 15; the liquid outlets of the first filtrate storage tank 11 and the second filtrate storage tank 15 are connected to the concentrating device 16 (concentrating kettle), the concentrated liquid outlet of the concentrating device 16 is connected to the first drying device 17 (double cone dryer), and the discharge port of the first drying device 17 is connected to the glucuronic acid storage tank 18; the discharge port of the second filtering device 15 is connected to the second drying device 19 (vibrating fluidized bed), and the discharge port of the second drying device 19 is connected to the D-chiro-inositol storage tank 20.

[0022] In actual production, the conversion liquid containing D-chiro-inositol and glucuronic acid enters the interior of the first filtering device through the feed liquid conveying pipeline, the filtrate collected after filtration enters the second filtering device, the filtrate collected after filtration enters the interior of the cationic resin column, the collected effluent enters the interior of the anionic resin column, the collected effluent enters the first concentrating device, the concentrated liquid enters the second concentrating device, the concentrated liquid enters the cache tank, and the ethanol in the first ethanol storage tank also enters the interior of the cache tank, and then is heated by the heat medium in the cache tank jacket. After being stirred for a period of time by the stirring component inside the cache tank, the feed liquid in the cache tank enters the interior of the first filtering device, and the filtered filtrate enters The first filtrate storage tank, the filtered filter cake enters the filter cake storage tank, and then the ethanol in the second ethanol storage tank also enters the filter cake storage tank, and is heated by the heat medium in the filter cake storage tank jacket, and after being stirred for a period of time by the stirring component inside the filter cake storage tank, the feed liquid in the filter cake storage tank enters the interior of the second filtering device, and the filtered filtrate enters the second filtrate storage tank. The filtrate in the first filtrate storage tank and the second filtrate storage tank enters the interior of the concentrator, and is heated and concentrated by the heat medium in the concentration kettle jacket. The obtained concentrated liquid enters the interior of the first drying device, and the dried product enters the glucuronic acid storage tank for storage; the filter cake collected after filtering by the second filtering device passes through the interior of the second drying device, and the dried product is stored in the D-chiro-inositol storage tank. The above separation and purification system is reasonably designed, and compared with the existing resin separation, it has a large processing capacity, is simple and convenient to operate, and greatly improves the yield and separation efficiency.

[0023] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions and improvements made within the spirit and principles of the present invention should be included in the protection scope of the present invention.

Claims

1. A separation and purification system for co-producing glucuronic acid and D-chiro-inositol, characterized in that: The invention comprises a first filtering device connected with a feed liquid conveying pipeline, wherein the filtrate outlet of the first filtering device is connected with a second filtering device; the filtrate outlet of the second filtering device is connected with a cation resin column, and the liquid outlet of the cation resin column is connected with an anion resin column; the liquid outlet of the anion resin column is connected with a first concentrating device, and the concentrated liquid outlet of the first concentrating device is connected with a second concentrating device; the concentrated liquid outlet of the second concentrating device is connected with a buffer tank, the liquid inlet of the buffer tank is connected with a first ethanol storage tank, the material outlet of the buffer tank is connected with a first filtering device, the liquid outlet of the first filtering device is connected with a first filtrate storage tank, and the material outlet of the first filtering device is connected with a filter cake storage tank; the liquid inlet of the filter cake storage tank is connected with a second ethanol storage tank, the material outlet of the filter cake storage tank is connected with a second filtering device, and the liquid outlet of the second filtering device is connected with a second filtrate storage tank; the liquid outlets of the first filtrate storage tank and the second filtrate storage tank are connected with a concentrating device, the concentrated liquid outlet of the concentrating device is connected with a first drying device, and the material outlet of the first drying device is connected with a glucuronic acid storage tank; the material outlet of the second filtering device is connected with a second drying device, and the material outlet of the second drying device is connected with a D-chiro-inositol storage tank.

2. A separation and purification system for co-producing glucuronic acid and D-chiro-inositol according to claim 1, characterized in that: The first filtering device is a ceramic membrane filtering device with a pore size of 20-100 nm; the second filtering device is an ultrafiltration membrane filtering device with a molecular weight cutoff of 1000-10000 Da.

3. A separation and purification system for co-producing glucuronic acid and D-chiro-inositol according to claim 1, characterized in that: The filler in the cationic resin column is SQD67, and the filler in the anionic resin column is LS-109D.

4. A separation and purification system for co-producing glucuronic acid and D-chiro-inositol according to claim 1, characterized in that: The first concentration device is a nanofiltration membrane concentration device with a molecular weight cutoff of 150-200Da; the second concentration device is a multi-effect concentrator.

5. A separation and purification system for co-producing glucuronic acid and D-chiro-inositol according to claim 1, characterized in that: The first filter device and the second filter device are both plate and frame filters.

6. A separation and purification system for co-producing glucuronic acid and D-chiro-inositol according to claim 1, characterized in that: The first drying device is a double cone dryer, and the second drying device is a vibrating fluidized bed.

Images