CN212504676U - Molecular level apparatus for producing of inulin - Google Patents
Molecular level apparatus for producing of inulin Download PDFInfo
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- CN212504676U CN212504676U CN202021252703.0U CN202021252703U CN212504676U CN 212504676 U CN212504676 U CN 212504676U CN 202021252703 U CN202021252703 U CN 202021252703U CN 212504676 U CN212504676 U CN 212504676U
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Abstract
The utility model relates to a molecular level apparatus for producing of inulin belongs to natural plant and draws technical field. The utility model provides a molecular-level inulin production technology has utilized a molecular weight grading, separator, according to molecular weight what promptly, falls into several different grades, is greater than 2500 molecular weight, is greater than 1000 molecular weight, is greater than 500 molecular weight and is less than 500, is greater than the product of above four kinds of different grades of 200 molecular weight.
Description
Technical Field
The utility model relates to a molecular level apparatus for producing of inulin belongs to natural product and draws technical field.
Background
Inulin (inulin) is a functional health food edible fiber extracted from the rhizome of chicory (or Jerusalem artichoke) by hot dipping, and is widely used for special food, formula milk powder for the elderly and nutritional health food. The main function is to adjust the living and growing environment of intestinal beneficial bacteria, the market demand at home and abroad is large, high-grade products are imported, the variety at home is single, and the functionality can not meet the market demand in many aspects. The traditional production process can only separate out products with molecular weight of more than 500Da, and the rest products are used as fructo-oligosaccharide (food) syrup.
SUMMERY OF THE UTILITY MODEL
The utility model provides a production technology of molecular-level inulin has utilized a molecular weight classification, separator, according to molecular weight how much promptly, divide into several different grades, be greater than 1500 molecular weight, be greater than 1000 molecular weight, be greater than 500 molecular weight and be less than the product of four above different grades of 500 molecular weight, make its usage and functional difference, inulin liquid after the separation is through concentrated back, go the isotropic symmetry to carry out the homogeneity, feed liquid after the homogeneity is through pressure spray drying, become functional different product after, cooling sieve divides the packing finished product. The utility model discloses a separator comprises preprocessing device and four sections molecular separation devices, and every section produces the product of a molecular weight rank, and its order is big → well → little, and a set of molecular weight is the biggest at first, and last one-level molecular weight is minimum, according to required product difference, chooses for use the filter membrane of different nanometers, and last one-level is carried by the force pump in succession to next one-level four-stage, and last one-level is the nanofiltration or reverse osmosis unit of little trapped molecular weight and constitutes. The dialyzate is pre-concentrated and evaporated to DS75% to obtain the final product fructo-oligosaccharide food-grade syrup, and the concentrated solution is evaporated, concentrated and homogenized in a homogenizer, and then spray-dried under pressure to obtain inulin products with different molecular weights.
The more specific technical scheme is as follows:
a molecular-level production process of inulin comprises the following steps:
step 7, sequentially adopting four stages of membranes to concentrate the materials obtained in the step 6, and enabling penetrating fluid obtained in each stage to enter the next stage for concentration and filtration; the first-stage membrane concentration process obtains inulin with a first polymerization degree, the second-stage membrane concentration process obtains inulin with a second polymerization degree, the third-stage membrane concentration process obtains inulin with a third polymerization degree, and the fourth-stage membrane concentration process obtains inulin with a fourth polymerization degree.
In one embodiment, in step 3, the amount of water added during the extraction process may be 0.5-10 times, more preferably 1-3 times the weight of chicory (or jerusalem artichoke); in the water leaching process, the temperature is preferably 50-60 ℃, and the leaching time is preferably 10-60 min.
In one embodiment, in the 4 th step, the filtration is performed by using a microfiltration membrane, wherein the average pore size of the microfiltration membrane is in the range of 50-500 nm.
In one embodiment, in the step 4, a filter aid is also added into the feed liquid in the filtration process, the filter aid is diatomite, and the addition amount of the filter aid is 1-5wt% of the raw material liquid; the temperature during the filtration process is controlled at 20-60 ℃.
In one embodiment, in the 4 th step, a ceramic microfiltration membrane is used for the filtration process, and the operation steps of the filtration process comprise: (a) soaking the membrane layer of the ceramic microfiltration membrane in saturated Ca (OH)2Taking out the solution, and naturally airing; (b) using the ceramic microfiltration membrane of step (a) to 5wt% NaCO3Dialyzing and filtering the solution to generate CaCO in the pores of the membrane3(ii) a (c) Filtering the leaching solution by using the ceramic microfiltration membrane in the step (b) to generate a filter cake on the surface of the membrane; (d) dialyzing and filtering the dilute hydrochloric acid solution by using the microfiltration membrane in the step (c) to obtain CaCO3Dissolving; (e) continuing to filter the leach liquor using the microfiltration membrane of step (d).
In one embodiment, in the step 5, activated carbon is used for decolorization, and the decolorization temperature is controlled to be 75-80 ℃, preferably 80 ℃.
In one embodiment, in step 6, the ion exchange resin is one or more of a combination of strong acid cation exchange resin, strong base anion exchange resin and weak base anion exchange resin, and the eluent is deionized water.
In one embodiment, the ultrafiltration membrane with the molecular weight cut-off of 2500 is adopted in the first-stage membrane concentration process, the nanofiltration membrane with the molecular weight cut-off of 1000 is adopted in the second-stage membrane concentration process, the nanofiltration membrane with the molecular weight cut-off of 500 is adopted in the third-stage membrane concentration process, and the nanofiltration membrane with the molecular weight cut-off of more than 200 and less than 500 or the reverse osmosis membrane is adopted in the fourth-stage membrane concentration process.
In one embodiment, inulin of different polymerization degree levels is obtained after spray drying of the concentrate obtained in each stage of membrane concentration.
A molecular-scale production apparatus of inulin, comprising:
the leaching tank is used for leaching chicory;
the filter is connected with the leaching tank and is used for filtering and removing impurities from the leaching solution;
the decoloring tank is connected with the filter and is used for decoloring the filtrate obtained in the filter, and activated carbon is filled in the decoloring tank;
the ion exchange resin column is connected with the decoloring tank and is used for desalting the feed liquid processed by the decoloring tank by using ion exchange resin;
the first separation membrane is connected with the ion exchange resin column and is used for concentrating the inulin with the first polymerization degree on the eluent obtained in the ion exchange resin column;
the second separation membrane is connected to the permeation side of the first separation membrane and is used for concentrating the filtrate obtained in the first separation membrane into synanthrin with a second polymerization degree;
the third separation membrane is connected to the permeation side of the second separation membrane and is used for concentrating the synanthrin with the third polymerization degree on the filtrate obtained in the second separation membrane;
and the fourth separation membrane is connected to the permeation side of the third separation membrane and is used for concentrating the filtrate obtained in the third separation membrane into synanthrin with a third polymerization degree.
In one embodiment, the first separation membrane is an ultrafiltration membrane with a molecular weight cut off of 2500.
In one embodiment, the second separation membrane is a nanofiltration membrane with a molecular weight cut-off of 1000.
In one embodiment, the third separation membrane is a nanofiltration membrane with a molecular weight cut-off of 500.
In one embodiment, the fourth separation membrane is a nanofiltration or reverse osmosis membrane having a molecular weight cut-off of greater than 200 and less than 500.
In one embodiment, the apparatus further comprises a spray drying device connected to the concentrated side of any one of the first separation membrane, the second separation membrane, the third separation membrane, or the fourth separation membrane, for spray drying the concentrated solution.
In one embodiment, the ion exchange resin column is packed with any one of a strong acid cation exchange resin, a strong base anion exchange resin, or a weak base anion exchange resin.
In one embodiment, further comprising: and the eluent pipeline is used for adding eluent into the ion exchange resin column.
In one embodiment, further comprising: a crusher connected to the leaching tank for crushing the chicory (Jerusalem artichoke) put into the leaching tank.
In one embodiment, further comprising: and the cleaning tank is connected with a feed inlet of the crusher and is used for cleaning the chicory fed into the crusher 2.
Advantageous effects
a. One product is divided into four products with different purposes according to different molecular weights so as to meet the requirements of different customers; b. the four-stage continuous molecular separation avoids the molecular degradation in the inulin production process, so that the yield of the macromolecular inulin is improved by 30 percent compared with the traditional process; c. each stage of interception process is also a concentration process, so that dehydration and concentration are simultaneously carried out in the production process, the steam consumption is reduced by 50%, and the production cost is lower; d. the new process thoroughly changes the production mode of the traditional process, implements a brand new extraction and separation mode, and performs fractional separation and extraction, so that the process is simpler, the system is more complete, and the effect is better.
Drawings
FIG. 1 is a process flow diagram of the present invention;
FIG. 2 is a flow diagram of the membrane separation section;
FIG. 3 is a diagram of the apparatus of the present invention;
FIG. 4 is a graph showing the flux change of the filtrate obtained by microfiltration;
wherein, 1, a cleaning tank; 2. a crusher; 3. a leaching tank; 4. a filter; 5. a decolorizing tank; 6. an eluent line; 7. ion exchange resin column; 8. a first separation membrane; 9. a second separation membrane; 10. a third separation membrane; 11. and a fourth separation membrane.
Detailed Description
The process steps of the utility model are shown in figure 1, and the detailed description is as follows:
and 3, carrying out hot water leaching on the chicory (or the jerusalem artichoke) which is cut into shreds in the step 2, wherein the added water amount can be 0.5-10 times of the weight of the chicory (or the jerusalem artichoke), and more preferably 1-3 times of the weight of the chicory (or the jerusalem artichoke). In the water leaching process, the temperature is preferably 50-75 ℃, and the leaching time is preferably 10-60 min.
And 4, after residues of the leaching liquor obtained by leaching in the step 3 are primarily removed, further filtering the leaching liquor, wherein the filtering can be carried out by adopting a microfiltration membrane, the microfiltration can remove larger colloids, proteins, suspended matters and the like in the leaching liquor, the adopted microfiltration membrane can be a membrane with the average pore diameter of 50-500nm, and the leaching liquor contains more macromolecular substances such as proteins, polysaccharides and the like, so that the pollution of the microfiltration membrane is easily caused, therefore, a filter aid can be added in the filtering process to form a filter cake layer on the surface of the microfiltration membrane and reduce the blocking pollution in membrane pores, wherein the used filter aid can be a diatomite filter aid, and the adding amount of the diatomite filter aid can be controlled to be 1-5wt% of the raw material liquid. The temperature during the filtration process is controlled at 20-70 ℃.
And 5, decoloring the filtrate obtained after filtration by using activated carbon, wherein the decoloring temperature is controlled to be 75-80 ℃, and preferably 80 ℃. In addition, because protein, colloid and other impurities can be brought into the leaching liquor during leaching, when the pollutants are filtered through the microfiltration membrane, the initial surface of the microfiltration membrane has no pollutants, so that the colloid can preferentially enter membrane pores, the membrane pores of the microfiltration membrane are easily blocked, and the pollutants in the membrane pores are not easily removed in a membrane surface washing manner, so that flux attenuation is caused; in another improved embodiment, the microfiltration membrane is first soaked in saturated Ca (OH)2In the solution, the pores of the membrane are soaked with saturated Ca (OH)2The solution is naturally dried, and then the microfiltration membrane is subjected to NaCO treatment3Slow dialysis filtration of the solution to produce CaCO in the pores of the membrane3Filtering the leaching solution containing the filter aid, wherein the generated CaCO exists in the membrane pores3Herein, thisThe filter aid is biased to generate filter cake on the membrane surface of the micro-filtration membrane during filtration, and after the filter cake is completely formed, the dilute hydrochloric acid is slowly used for dialysis filtration to ensure that CaCO in the membrane pores3Dissolving, and keeping the existence of filter cakes, so that the surface of the micro-filtration membrane not only keeps the filter cakes with the protection function formed by the filter aid, but also does not have blocking pollution in the membrane pores, so that the filtration flux is improved, and the flux attenuation problem caused by the pollution in the membrane pores is solved.
And 6, after the decoloration treatment by the activated carbon, performing ion exchange resin treatment on the obtained material, wherein the ion exchange resin is used for removing salt impurities in the extracting solution, is not particularly limited, and can be selected from one or a combination of more of strong acid cation exchange resin, strong base anion exchange resin and weak base anion exchange resin. For example: the strongly acidic cation exchange resin may be selected from D001-F, the strongly basic anion exchange resin may be selected from D201, and the weakly basic anion exchange resin may be selected from D301. The elution process of the ion exchange resin can adopt deionized water for elution.
And 7, after the ion exchange resin is decolorized, the separation device consists of a pretreatment device and four sections of molecular separation devices, wherein each section produces a product with a molecular weight grade in the sequence of big → middle → small, the first group has the largest molecular weight and the last stage has the smallest molecular weight, different nano filter membranes are selected according to different required products, the upper stage to the lower stage are continuously conveyed by a pressure pump, and the last stage consists of a nanofiltration device and a reverse osmosis device. The preferred method in the utility model is as follows: the first stage adopts an ultrafiltration membrane with the molecular weight cut-off of 2500, the second stage adopts a nanofiltration membrane with the molecular weight cut-off of 1000, the third stage adopts a nanofiltration membrane with the molecular weight cut-off of 500, and the fourth stage adopts a nanofiltration membrane with the molecular weight cut-off of more than 200 and less than 500 or a reverse osmosis membrane; for the first stage to the third stage, the permeate from each stage is sent to the next stage for treatment; and (4) obtaining inulin with different polymerization degree grades after spray drying of each grade of concentrated solution.
The polymerization degree of inulin obtained in the first stage is 16 or more, the polymerization degree of inulin obtained in the second stage is 6 to 16, the polymerization degree in the third stage is 3 to 6, and the polymerization degree in the fourth stage is 2 or more.
Based on above method, the utility model provides a device is shown in fig. 3, include:
the leaching tank 3 is used for leaching chicory;
the filter 4 is connected with the leaching tank 3 and is used for filtering and removing impurities from the leaching liquor;
a decoloring tank 5 connected to the filter 4 for decoloring the filtrate obtained in the filter 4, wherein the decoloring tank 5 is filled with activated carbon;
the ion exchange resin column 7 is connected with the decoloring tank 5 and is used for desalting the feed liquid treated by the decoloring tank 5 by using ion exchange resin;
a first separation membrane 8 connected to the ion exchange resin column 7 for concentrating the eluate obtained from the ion exchange resin column 7 with inulin of a first polymerization degree;
a second separation membrane 9 connected to the permeate side of the first separation membrane 8, for concentrating the filtrate obtained in the first separation membrane 8 with inulin of a second degree of polymerization;
a third separation membrane 10 connected to the permeate side of the second separation membrane 9, for performing a concentration process of inulin having a third polymerization degree on the filtrate obtained in the second separation membrane 9;
and a fourth separation membrane 11 connected to the permeate side of the third separation membrane 10, for concentrating the filtrate obtained in the third separation membrane 10 into inulin of a third polymerization degree.
In one embodiment, the first separation membrane 8 is an ultrafiltration membrane with a molecular weight cut off of 2500.
In one embodiment, the second separation membrane 9 is a nanofiltration membrane with a molecular weight cut-off of 1000.
In one embodiment, the third separation membrane 10 is a nanofiltration membrane with a molecular weight cut-off of 500.
In one embodiment, the fourth separation membrane 11 is a nanofiltration or reverse osmosis membrane having a molecular weight cut-off of more than 200 and less than 500.
In one embodiment, the apparatus further comprises a spray drying device connected to the concentrated side of any one of the first separation membrane 8, the second separation membrane 9, the third separation membrane 10, or the fourth separation membrane 11, for spray drying the concentrated solution.
In one embodiment, the ion exchange resin column 7 is filled with any one of a strong acid cation exchange resin, a strong base anion exchange resin, or a weak base anion exchange resin.
In one embodiment, further comprising: an eluent pipeline 6 is used for adding eluent into the ion exchange resin column.
In one embodiment, further comprising: and the crusher 2 is connected to the leaching tank 3 and is used for crushing the chicory placed in the leaching tank 3.
In one embodiment, further comprising: and the cleaning tank 1 is connected to a feed inlet of the crusher 2 and is used for cleaning the chicory fed into the crusher 2.
The utility model discloses a test method of the polymerization degree of inulin is based on the viscosity curve and determines, takes inulin of different polymerization degree grades, prepares into standard solution, draws the relation between solution viscosity and polymerization degree; and (4) measuring the viscosity of the solution of the sample to be measured according to the same method, and substituting the solution into a linear equation to obtain the polymerization degree of the inulin to be measured.
The inulin in the inulin of the utility model is non-reductive fructan, the glucose and the fructose in the inulin extract of the jerusalem artichoke are reducing sugar, and the method of subtracting the reducing sugar from the total sugar content is adopted when the inulin content is determined.
Inulin content (%) = ((C)General assembly-CAnd also) XLXdilution factor)/WSample (A)×100%
Wherein, CGeneral assemblyIs total sugar concentration (mg/mL); cAnd alsoAs reducing sugar concentration (mg/mL); l is the volume of solution (mL); wSample (A)Is the chicory sample size (mg).
Example 1
Cleaning chicory (jerusalem artichoke), and then shredding, wherein the solid-liquid ratio is 1: 1.5 adding hot water to carry out leaching, wherein the leaching temperature is controlled at 60 ℃, and the leaching time is 45 min; removing solid residues in the leaching liquor primarily, adding 1wt% of diatomite filter aid, filtering and removing impurities by using a ceramic microfiltration membrane with the average pore diameter of 200nm, wherein the membrane surface flow rate is 3m/s in the filtering process, collecting filtrate, adding the filtrate into a decoloring kettle for decoloring, decoloring the decoloring kettle by using active carbon, wherein the using amount of the active carbon is 1wt% of the weight of the material liquid, the decoloring temperature is 75 ℃, filtering the active carbon, cooling the material liquid to room temperature, feeding the material liquid into a weak base anion exchange resin D301 for extracting inulin, eluting by using deionized water, filtering and concentrating eluent by using an ultrafiltration membrane with the molecular weight cutoff of 2500, spray-drying concentrated solution to obtain first-stage inulin, feeding penetrating fluid into a nanofiltration membrane with the molecular weight cutoff of 1000 for filtering and concentrating, spray-drying concentrated solution to obtain second-stage inulin, feeding the penetrating fluid into the nanofiltration membrane with the molecular weight of 500 for filtering and concentrating, spray drying the concentrated solution to obtain the third-stage inulin, concentrating the penetrating fluid by using a reverse osmosis membrane, and spray drying the concentrated solution to obtain the fourth-stage inulin.
Example 2
Cleaning chicory, shredding, and mixing the raw materials according to a solid-liquid ratio of 1: 2, adding water for leaching, controlling the leaching temperature at 55 ℃ and the leaching time for 40 min; after primarily removing solid residues from the leaching liquor, adding about 2wt% of diatomite filter aid, filtering and removing impurities by using a ceramic microfiltration membrane with the average pore diameter of 50nm, wherein the membrane surface flow rate in the filtering process is 2m/s, collecting filtrate, adding the filtrate into a decoloring kettle for decoloring, decoloring the filtrate by using activated carbon in the decoloring kettle, wherein the using amount of the activated carbon is 3wt% of the weight of the material liquid, the decoloring temperature is 80 ℃, filtering the activated carbon, cooling the material liquid to room temperature, feeding the material liquid into a strong-acid cation exchange resin D001-F for extracting inulin, eluting by using deionized water, filtering and concentrating eluent by using an ultrafiltration membrane with the molecular weight cutoff of 2500, spray-drying concentrated liquid to obtain first-stage inulin, feeding penetrating liquid into a nanofiltration membrane with the molecular weight cutoff of 1000 for filtering and concentrating, spray-drying concentrated liquid to obtain second-stage inulin, feeding the penetrating liquid into the nanofiltration membrane with the molecular weight of, spray drying the concentrated solution to obtain the third-stage inulin, concentrating the penetrating fluid by using a reverse osmosis membrane, and spray drying the concentrated solution to obtain the fourth-stage inulin.
Example 3
Cleaning chicory, shredding, and mixing the raw materials according to a solid-liquid ratio of 1: 1.2 adding water to carry out leaching, controlling the leaching temperature at 50 ℃ and the leaching time for 60 min; removing solid residues in the leaching liquor primarily, adding 2wt% of diatomite filter aid, filtering and removing impurities by using a ceramic microfiltration membrane with the average pore diameter of 200nm, wherein the membrane surface flow rate in the filtering process is 4m/s, collecting filtrate, adding the filtrate into a decoloring kettle for decoloring, decoloring the decoloring kettle by using active carbon, wherein the using amount of the active carbon is 2wt% of the weight of the material liquid, the decoloring temperature is 75 ℃, filtering the active carbon, cooling the material liquid to room temperature, sending the material liquid into a strong-base anion exchange resin D201 for extracting inulin, eluting by using deionized water, filtering and concentrating the eluent by using an ultrafiltration membrane with the molecular weight cutoff of 2500, spray-drying the concentrated solution to obtain the first-stage inulin, sending the penetrating fluid into a nanofiltration membrane with the molecular weight cutoff of 1000 for filtering and concentrating, spray-drying the concentrated solution to obtain the second-stage inulin, sending the penetrating fluid into the nanofiltration membrane with the molecular weight, spray drying the concentrated solution to obtain the third-stage inulin, concentrating the penetrating fluid by using a reverse osmosis membrane, and spray drying the concentrated solution to obtain the fourth-stage inulin.
Example 4
The difference from example 3 is that: the microfiltration membrane and the filtration process are pretreated when the microfiltration membrane is used for filtering the leaching liquor.
Cleaning chicory, shredding, and mixing the raw materials according to a solid-liquid ratio of 1: 1.2 adding water to carry out leaching, controlling the leaching temperature at 50 ℃ and the leaching time for 60 min; after the solid residue of the leaching liquor is primarily removed, adding about 2wt% of diatomite filter aid; the membrane surface of a ceramic microfiltration membrane with an average pore size of 200nm is first soaked in saturated Ca (OH)2Taking out from the solution, naturally drying in the air, repeating for three times, and then using 5wt% NaCO3Slowly dialyzing and filtering the solution to generate CaCO in the pores of the membrane3Filtering the leaching solution containing the filter aid to form stable filter cake on the surface of the micro-filtration membrane, slowly dialyzing and filtering with dilute hydrochloric acid to obtain CaCO in the membrane pores3Dissolving, continuing to filter the leaching liquor, wherein the membrane surface flow rate in the filtering process is 4m/s, collecting filtrate, adding the filtrate into a decoloring kettle for decoloring, decoloring by using active carbon in the decoloring kettle, wherein the active carbon is 2wt% of the weight of the filtrate, the decoloring temperature is 75 ℃, filtering the active carbon, cooling the filtrate to room temperature, sending the filtrate into a strong-base anion exchange resin D201 for extracting inulin, eluting by using deionized water, filtering and concentrating the eluent by using an ultrafiltration membrane with the cut-off molecular weight of 2500, spray-drying the concentrated solution to obtain first-stage inulin, sending the penetrating fluid into a nanofiltration membrane with the cut-off molecular weight of 1000 for filtering and concentrating, sending the penetrating fluid into a nanofiltration membrane with the cut-off molecular weight of 500 for filtering and concentrating, spray-drying the concentrated solution to obtain third-stage inulin, concentrating the penetrating fluid by using a reverse osmosis membrane, and spray-drying the concentrated solution to obtain fourth-grade inulin.
Purity of inulin
The purity of the inulin produced in each of the above examples is shown in the following table:
it can be seen from the above table, the utility model discloses in through the separation and purification back at different levels, can obtain the better inulin of purity, the inulin content of fourth level is the highest, mainly because corresponding impurity can be got rid of step by step in the technology of anterior segment.
Polymerization degree of inulin
The purity of the inulin produced in each of the above examples, as calculated by the viscosity curve method, is shown in the following table:
as can be seen from the above table, inulin at different polymerization degrees can be obtained after the grouping treatment by the quaternary film.
Micro-filtration for removing impuritiesFlux change of process
In the processes of filtering and removing impurities from the leaching solution by using the microfiltration membrane in the embodiments 3 and 4, the flux attenuation curve is shown in fig. 4, and it can be seen from the figure that although the initial flux of the microfiltration membrane in the embodiment 4 is relatively low, the subsequent operation process is relatively stable, the early stage is relatively low mainly because the pretreatment of the microfiltration membrane is carried out, so that a stable filter cake is formed on the surface of the membrane, the blockage of membrane pores is prevented, and the subsequent operation process does not cause serious membrane pollution any more; in example 3, the initial flux is high, which is mainly due to the fact that the membrane is a new membrane, and the membrane pore blockage occurs in the initial filtration stage, so that the membrane pore blockage pollution and the filter cake pollution simultaneously occur, and the later flux is low.
Claims (10)
1. A molecular-level inulin production apparatus, comprising:
a leaching tank (3) for hot leaching chicory;
the filter (4) is connected with the leaching tank (3) and is used for filtering and removing impurities from the leaching liquor;
the decoloring tank (5) is connected with the filter (4) and is used for decoloring the filtrate obtained in the filter (4), and activated carbon is filled in the decoloring tank (5);
the ion exchange resin column (7) is connected with the decoloring tank (5) and is used for desalting the feed liquid processed by the decoloring tank (5) by using ion exchange resin;
a first separation membrane (8) connected to the ion exchange resin column (7) for concentrating the inulin having a first degree of polymerization in the eluate obtained from the ion exchange resin column (7);
a second separation membrane (9) connected to the permeate side of the first separation membrane (8) and used for concentrating the filtrate obtained in the first separation membrane (8) into inulin with a second degree of polymerization;
a third separation membrane (10) connected to the permeate side of the second separation membrane (9) and used for concentrating the filtrate obtained in the second separation membrane (9) into inulin with a third degree of polymerization;
and a fourth separation membrane (11) which is connected to the permeate side of the third separation membrane (10) and which is used for concentrating the filtrate obtained in the third separation membrane (10) into inulin having a third degree of polymerization.
2. Molecular scale production plant of inulin as claimed in claim 1, characterized in that the first separation membrane (8) is an ultrafiltration membrane with a molecular weight cut-off of 2500.
3. Molecular-scale inulin production plant according to claim 1, wherein the second separation membrane (9) is a nanofiltration membrane with a molecular weight cut-off of 1000.
4. Molecular scale production plant of inulin as claimed in claim 1, characterized in that the third separation membrane (10) is a nanofiltration membrane with a molecular weight cut-off of 500.
5. Molecular-scale inulin production apparatus according to claim 1, wherein the fourth separation membrane (11) is a nanofiltration or reverse osmosis membrane having a molecular weight cut-off of more than 200 and less than 500.
6. A molecular-scale inulin production apparatus according to claim 1, further comprising a spray-drying device connected to the concentrated side of any one of the first separation membrane (8), the second separation membrane (9), the third separation membrane (10) or the fourth separation membrane (11) for spray-drying the concentrated solution.
7. A molecular-scale inulin production apparatus as claimed in claim 1, wherein the ion exchange resin column (7) is filled with any one of strong acid cation exchange resin, strong base anion exchange resin or weak base anion exchange resin.
8. A molecular-scale inulin production apparatus as claimed in claim 1, further comprising: an eluent pipeline (6) is used for adding eluent into the ion exchange resin column.
9. A molecular-scale inulin production apparatus as claimed in claim 1, further comprising: a crusher (2) connected to the leaching tank (3) for crushing the chicory placed in the leaching tank (3).
10. A molecular-scale inulin production apparatus as claimed in claim 9, further comprising: the cleaning tank (1) is connected with a feeding port of the crusher (2) and is used for cleaning the chicory fed into the crusher (2).
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| CN202021252703.0U CN212504676U (en) | 2020-07-01 | 2020-07-01 | Molecular level apparatus for producing of inulin |
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| CN202021252703.0U CN212504676U (en) | 2020-07-01 | 2020-07-01 | Molecular level apparatus for producing of inulin |
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