CN214300195U - Device for producing inulin by utilizing jerusalem artichoke or chicory - Google Patents
Device for producing inulin by utilizing jerusalem artichoke or chicory Download PDFInfo
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- CN214300195U CN214300195U CN202022805064.2U CN202022805064U CN214300195U CN 214300195 U CN214300195 U CN 214300195U CN 202022805064 U CN202022805064 U CN 202022805064U CN 214300195 U CN214300195 U CN 214300195U
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Abstract
The utility model discloses an utilize device of jerusalem artichoke or chicory production inulin, including ultrafiltration membrane system, first decoloration unit, receive the membrane system, first evaporative concentration unit, continuous chromatographic fractionation system, continuous ion exchange system, second decoloration unit, second evaporative concentration unit and the spray drying unit that connects gradually. And a dialysate outlet of the ultrafiltration membrane system is connected with a liquid inlet pipeline of the first decoloring unit, a concentrated solution outlet is connected with the first post-treatment pipe, a concentrated solution outlet of the nanofiltration membrane system is connected with a liquid inlet of the first evaporation concentration unit, and a dialysate outlet is connected with the second post-treatment pipe. Adopt the utility model discloses a device carries out inulin production, can be so that the consumption of water and active carbon significantly reduces, can reduce the use amount of acid-base in a large number simultaneously, and acid-base waste water reduces in a large number, reduces sewage treatment capacity.
Description
Technical Field
The utility model relates to the technical field of food production, in particular to a device for producing inulin by utilizing jerusalem artichoke or chicory.
Background
The jerusalem artichoke is commonly called jerusalem artichoke, is resistant to barren and drought, has low requirements on climate and soil conditions, and has strong adaptability. Can resist frost and various diseases. In China, many areas are planted, generally, 4000 kilograms of jerusalem artichoke tubers are produced per mu, the jerusalem artichoke tubers are good raw materials for processing and producing inulin, and 4.5 to 8.3 tons of inulin can be produced per hectare. Chicory is a one-year or two-year or short-term perennial herb of the compositae family, native to the eastern hemisphere, suitable for growing in the ocean climate, and has a yield per hectare of 9.8-16.1 tons compared to jerusalem artichoke.
Inulin belongs to a reserve polysaccharide in plants, and is fructan formed by connecting D-fructofuranose molecules with Ii (2-1) sugar-nutrient bonds, wherein each inulin molecule terminal is connected with a glucose residue by a (1.2) glycosidic bond, the polymerization Degree (DP) is usually 2-60, and the average polymerization degree is 10-12. At present, inulin is widely applied to the fields of food, medicine, chemical industry and the like. Inulin can be used as a fat substitute for low-energy food production, has the physiological functions of dietary fiber and probiotics, and is an excellent functional food base material. In Europe, inulin and related products have become a considerable industry with a wide prospect for development. A fixed bed is generally adopted in the traditional method for producing inulin, and the fixed bed has the defects of large floor area, more equipment investment, low utilization rate of ion exchange resin, large usage amount of acid, alkali, water and active carbon, large amount of waste water and the like.
Disclosure of Invention
To the technical problem who proposes in the background art, the utility model aims to provide an utilize device of jerusalem artichoke or chicory production inulin, adopt the device to carry out the inulin production, can be so that the consumption of water and active carbon significantly reduces, can reduce the use amount of acid-base simultaneously in a large number, acid-base waste water reduces in a large number, reduces sewage treatment capacity.
In order to realize the purpose, the utility model discloses a technical scheme as follows:
a device for producing inulin by using jerusalem artichoke or chicory comprises an ultrafiltration membrane system, a first decolorizing unit, a nanofiltration membrane system, a first evaporation concentration unit, a continuous chromatographic separation system, a continuous ion exchange system, a second decolorizing unit, a second evaporation concentration unit and a spray drying unit which are connected in sequence. And a dialysate outlet of the ultrafiltration membrane system is connected with a liquid inlet pipeline of the first decoloring unit, a concentrated solution outlet is connected with the first post-treatment pipe, a concentrated solution outlet of the nanofiltration membrane system is connected with a liquid inlet of the first evaporation concentration unit, and a dialysate outlet is connected with the second post-treatment pipe.
Furthermore, the ultrafiltration membrane system comprises a first-stage raw material tank, a first-stage valve, a first-stage delivery pump, an ultrafiltration membrane unit and a dialysate tank which are connected in sequence. And a dialysate outlet of the ultrafiltration membrane unit is connected with a dialysate tank, a concentrated solution outlet is connected with a primary raw material tank through a primary return pipe, and a primary heat exchange device is arranged on the primary return pipe. The dialysate tank is connected with the liquid inlet pipeline of the first decoloring unit.
Preferably, the ultrafiltration membrane adopted by the ultrafiltration membrane unit is a ceramic membrane or an organic tubular membrane with the pore diameter of less than 0.1 um.
Furthermore, receive filter membrane system including the second grade head tank, second grade valve, second grade delivery pump, receive filter membrane unit and feed liquid jar that connect in order. The second grade head tank with the liquid outlet of first decoloration unit links to each other, receive the concentrate export of filter membrane separating unit and link to each other with the feed liquid jar, the dislysate outlet passes through the second grade back flow and links to each other with the second grade head tank, is equipped with second grade heat transfer device on the second grade back flow. The feed liquid tank is connected with a liquid inlet pipeline of the first evaporation concentration unit.
Further, the second grade head tank with first decoloration unit between be equipped with sheet frame filtration system, sheet frame filtration system's inlet with the liquid outlet pipeline of first decoloration unit links to each other, sheet frame filtration system's liquid outlet with second grade head tank pipeline links to each other.
Preferably, the aperture of the nanofiltration membrane adopted by the nanofiltration membrane unit is less than 1 kDa.
Furthermore, the continuous chromatographic separation system comprises a plurality of resin columns which are uniformly distributed along the circumferential direction and rotate according to a fixed period, and sodium type chromatographic separation resin or calcium type chromatographic separation resin for separating sugar solution and salt solution is respectively filled in each resin column.
Wherein, the continuous chromatographic separation system comprises 12 resin columns which are divided into 6 regions, and each region comprises the following components:
a feeding area: the device comprises 2 resin columns connected in series, feed liquid of a first evaporation concentration unit positively enters a feeding area, and the feed liquid adsorbed by the feeding area positively enters a secondary separation area for re-adsorption.
A secondary separation area: the system comprises 2 resin columns connected in series, one part of salt solution which is re-adsorbed by the secondary separation area reversely enters a salt top water area, and the rest salt solution is discharged through a pipeline for post-treatment.
A salt washing area: comprises 2 resin columns connected in series, and the feed liquid generated in the salt washing area and the feed liquid generated in the feeding area enter a secondary separation area together for re-adsorption.
A sugar washing area: comprises 4 resin columns connected in series, pure water is pumped into a sugar washing area in a forward direction, a part of sugar liquid washed out by the sugar washing area enters a salt washing area in the forward direction, and the rest of sugar liquid enters a continuous ion exchange system for further desalination.
A salt top water area: contains 1 resin column, and the feed liquid washed out from the top is recycled and reused through a pipeline.
Spare area: contains 1 resin column.
Furthermore, the continuous ion exchange system comprises a plurality of ion exchange columns which are uniformly distributed along the circumferential direction and rotate according to a fixed period, and the ion exchange columns are sequentially arranged according to the sequence numbers. Wherein the odd-numbered ion exchange columns are filled with cation resin, a plurality of odd-numbered ion exchange columns form a cation exchange system, the even-numbered ion exchange columns are filled with anion resin, and a plurality of even-numbered ion exchange columns form an anion exchange system.
The cation exchange system comprises 16 ion exchange columns which are divided into 6 regions, and each region comprises the following components:
a feeding area: comprises 2 ion exchange columns connected in parallel, sugar liquid generated by separation of a continuous chromatographic separation system positively enters a feeding area, and the feed liquid adsorbed by the feeding area positively enters a secondary separation area for re-adsorption.
A secondary separation area: the device comprises 4 ion exchange columns, wherein the 4 ion exchange columns comprise two sets of separation mechanisms connected in series, each set of separation mechanism is formed by connecting two ion exchange columns in parallel, one part of feed liquid after being re-adsorbed by a secondary separation area enters a material top water area in the forward direction, and the rest feed liquid is used as feed liquid of an anion exchange system.
A water material ejection area: comprises 3 ion exchange columns connected in series, pure water positively enters a water material lifting area, and feed liquid washed out by the water material lifting area and feed liquid separated by a feed area enter a secondary separation area for re-adsorption.
A regeneration zone: contains 3 ion exchange columns connected in series, acidic regeneration medium positively enters a regeneration zone, and feed liquid washed out by the regeneration zone is discharged out of a cation exchange system as waste acid.
Water top acid zone: comprises 3 ion exchange columns connected in series, pure water positively enters a water top acid area, and feed liquid washed out by the water top acid area and feed liquid generated by the ion exchange column at the front end of the regeneration area enter the ion exchange column at the rear end of the regeneration area together.
A material top water area: contains 1 ion exchange column, and the feed liquid washed out from the top is recycled and reused through a pipeline.
Preferably, the acidic regeneration medium is hydrochloric acid.
The anion exchange system comprises 16 ion exchange columns which are divided into 6 regions, and each region comprises the following components:
a feeding area: comprises 2 ion exchange columns connected in parallel, cation exchange effluent generated by the separation of a cation exchange system positively enters a feeding area, and feed liquid absorbed by the feeding area positively enters a secondary separation area for re-absorption.
A secondary separation area: the device comprises 4 ion exchange columns, wherein the 4 ion exchange columns comprise two sets of separation mechanisms connected in series, each set of separation mechanism is formed by connecting two ion exchange columns in parallel, one part of feed liquid after being re-adsorbed by a secondary separation area positively enters a material top water area, and the rest feed liquid serving as product liquid enters a second decoloring unit for decoloring.
A water material ejection area: comprises 3 ion exchange columns connected in series, pure water positively enters a water material lifting area, and feed liquid washed out by the water material lifting area and feed liquid separated by a feed area enter a secondary separation area for re-adsorption.
A regeneration zone: contains 3 ion exchange columns connected in series, the alkaline regeneration medium positively enters into the regeneration zone, and the feed liquid washed out by the regeneration zone is discharged out of the anion exchange system as waste alkali.
A water top alkali area: comprises 3 ion exchange columns connected in series, pure water positively enters a water top alkali area, and feed liquid washed out by the water top alkali area and feed liquid generated by the ion exchange column at the front end of the regeneration area enter the ion exchange column at the rear end of the regeneration area together.
A material top water area: contains 1 ion exchange column, and the feed liquid washed out from the top is recycled and reused through a pipeline.
Preferably, the alkaline regeneration medium is liquid alkali.
Further, the decolorizing media in the first decolorizing unit and the second decolorizing unit are both activated carbon.
The utility model discloses following beneficial effect has: providing a device for producing inulin by using jerusalem artichoke or chicory, and removing suspended matters from a crude inulin leaching liquor by adopting an ultrafiltration membrane; a nanofiltration membrane system is adopted to carry out monosaccharide and disaccharide removal treatment on the primary decolorizing plate frame filtrate; desalting, decoloring and monosaccharide removing the primary evaporated and concentrated feed liquid by using a continuous chromatographic separation system, and further desalting sugar liquid separated by continuous chromatography by using a continuous ion exchange system; and (4) carrying out secondary decolorization, secondary evaporation concentration and spray drying on the feed liquid subjected to desalination treatment to finally obtain the inulin. Adopt the utility model discloses a device carries out inulin production, can be so that the consumption of water and active carbon significantly reduces, can reduce the use amount of acid-base in a large number simultaneously, and acid-base waste water reduces in a large number, reduces sewage treatment capacity. The device of the utility model has the advantages of small occupied area, short production process period and high production efficiency.
Drawings
Fig. 1 is a schematic view of the structure of the device of the present invention.
FIG. 2 is a schematic structural view of an ultrafiltration membrane system.
Fig. 3 is a schematic structural view of a nanofiltration membrane system.
FIG. 4 is a schematic diagram of the structure of a continuous chromatographic separation system.
FIG. 5 is a schematic diagram of a continuous ion exchange system.
Description of the main component symbols: 1. an ultrafiltration membrane system; 101. a primary feed tank; 102. a first-stage valve; 103. a first-stage material conveying pump; 104. an ultrafiltration membrane unit; 105. a dialysate tank; 106. a primary return pipe; 107. a primary heat exchange device; 2. a first decoloring unit; 3. a nanofiltration membrane system; 301. a secondary feed tank; 302. a secondary valve; 303. a second-stage delivery pump; 304. a nanofiltration membrane unit; 305. a feed liquid tank; 306. a secondary return pipe; 307. a secondary heat exchange device; 4. a first evaporative concentration unit; 5. A continuous chromatographic separation system; 6. a continuous ion exchange system; 7. a second decoloring unit; 8. a second evaporation concentration unit; 9. A spray drying unit; 10. a plate and frame filtration system;
Detailed Description
The present invention will be further described with reference to the accompanying drawings and the following detailed description.
As shown in figures 1-5, the device for producing inulin by using jerusalem artichoke or chicory comprises an ultrafiltration membrane system 1, a first decolorizing unit 2, a nanofiltration membrane system 3, a first evaporation concentration unit 4, a continuous chromatographic separation system 5, a continuous ion exchange system 6, a second decolorizing unit 7, a second evaporation concentration unit 8 and a spray drying unit 9 which are connected in sequence. The dialysate export of ultrafiltration membrane system 1 links to each other with the inlet pipeline of first decoloration unit 2, and the concentrate is discharged by the pipeline and is carried out the post processing, and the concentrate export of receiving filter membrane system 3 links to each other with the inlet of first evaporative concentration unit 2, and the dialysate is discharged by the pipeline and is carried out the post processing. The decolorizing media in the first decolorizing unit 2 and the second decolorizing unit 7 are both activated carbon.
The ultrafiltration membrane system 1 comprises a primary raw material tank 101, a primary valve 102, a primary feed pump 103, an ultrafiltration membrane unit 104 and a dialysate tank 105 which are connected in sequence. The dialysate outlet of the ultrafiltration membrane unit 104 is connected with a dialysate tank 105, the concentrate outlet is connected with a primary raw material tank 101 through a primary return pipe 106, and a primary heat exchange device 107 is arranged on the primary return pipe 106. The dialysate tank 105 is connected to the inlet line of the first decolorizing unit 2. Preferably, the ultrafiltration membrane used in the ultrafiltration membrane unit 104 is a ceramic membrane or an organic tubular membrane having a pore size of less than 0.1 um.
The nanofiltration membrane system 3 comprises a secondary raw material tank 301, a secondary valve 302, a secondary delivery pump 303, a nanofiltration membrane unit 304 and a liquid tank 305 which are connected in sequence. The second-stage raw material tank 301 is connected with the liquid outlet of the first decolorizing unit 2, the concentrated solution outlet of the nanofiltration membrane separation unit 304 is connected with the liquid tank 305, the dialysate outlet is connected with the second-stage raw material tank 301 through a second-stage return pipe 306, and the second-stage return pipe 306 is provided with a second-stage heat exchange device 307. The feed liquid tank 305 is connected to the liquid inlet pipe of the first evaporation concentration unit 4. Preferably, the nanofiltration membrane unit 304 employs nanofiltration membranes having a pore size of less than 1 kDa.
Be equipped with plate frame filtration system 10 between second grade head tank 301 and the first decoloration unit 2, the inlet of plate frame filtration system 10 links to each other with the liquid outlet pipeline of first decoloration unit 2, and plate frame filtration system 10's liquid outlet links to each other with second grade head tank 301 pipeline.
The continuous chromatographic separation system 5 comprises a plurality of resin columns which are uniformly distributed along the circumferential direction and rotate according to a fixed period, and sodium type chromatographic separation resin or calcium type chromatographic separation resin for separating sugar solution and salt solution is respectively filled in each resin column. The continuous chromatographic separation system comprises 12 resin columns numbered from 1 to 12, which are divided into 6 regions, and each region is composed of the following components:
1) a secondary separation area: feed liquid that 7, 8 # columns of feeding zone were established ties and are come out mixes the back through the pipeline and gets into 9 # columns with the feed liquid that 6 # columns came out to 9, 10 # columns establish ties together, and the solution after the separation is discharged through the pipeline and is carried out post treatment.
2) A feeding area: the raw material liquid enters a No. 7 column, the No. 7 column and the No. 8 column are connected in series, and the material liquid discharged from the No. 8 column and the material liquid discharged from the No. 6 column are separated for the second time.
3) A salt washing area: and (3) feeding a part of the sugar liquid from the column No. 4 into a column No. 5, connecting the sugar liquid with the columns No. 5 and No. 6 in series, and performing secondary separation on the washed sugar liquid and the sugar liquid from the column No. 8.
4) A sugar washing area: the pure water enters the column No. 1 in the forward direction and is connected with the columns No. 2, 3 and 4 in series, the washed sugar solution enters the subsequent treatment through a pipeline, and enters the secondary separation area again after the leaching is finished, and the steps are repeated.
5) A salt top water area: and part of the salt solution from the No. 10 column reversely enters the No. 11 column, and the water washed from the top is recycled and reused through a pipeline.
6) Spare area: column 12 is the spare column.
The continuous ion exchange system 6 comprises a plurality of ion exchange columns which are uniformly distributed along the circumferential direction and rotate according to a fixed period, and the ion exchange columns are sequentially arranged according to the numbers 1-32. Wherein the odd-numbered ion exchange columns are filled with cation resin, and a plurality of odd-numbered ion exchange columns form a cation exchange system. Anion resin is filled in the even number ion exchange columns, and an anion exchange system is formed by a plurality of even number ion exchange columns.
The cation exchange system comprises 16 odd-numbered ion exchange columns which are divided into 6 regions, and each region comprises the following components:
1) a secondary separation area: the feed liquid from the feeding area No. 7 and No. 9 columns and the feed liquid from the No. 5 column are mixed and then enter No. 11 and No. 13 columns through pipelines in parallel, the No. 15 and No. 17 columns are connected in series, and the separated solution enters the No. 8 and No. 10 columns through pipelines for anion exchange.
2) A feeding area: the raw material liquid is parallelly connected and enters No. 7 and No. 9 columns, and the discharged material liquid and the material liquid discharged from No. 5 columns are subjected to secondary separation together.
3) A water material ejection area: pure water enters the No. 1 column through a pipeline and is connected with the No. 3 and No. 5 columns in series, and the washed sugar liquid is secondarily separated from the sugar liquid discharged from the No. 7 and No. 9 columns.
4) A regeneration zone: hydrochloric acid enters a No. 27 column through a pipeline, and the discharged acid liquid and the acid liquid washed out from the No. 25 top are mixed, enter a No. 29 column and are connected with a No. 31 column in series.
5) Water top acid zone: pure water enters the No. 21 column through a pipeline and is connected with the No. 23 and the No. 25 column in series, and the process is repeated after the pure water is rinsed and enters the secondary feeding area.
6) A material top water area: part of the cation delivered material enters a No. 19 column through a pipeline, and water washed out from the top can be recycled.
The anion exchange system comprises 16 resin columns numbered even, divided into 6 zones, each zone consisting of:
1) a secondary separation area: the material liquid from the feeding area 8 and 10 columns and the material liquid from the 6 column are mixed and then enter the 12 and 14 columns through pipelines in parallel, the 16 and 18 columns are connected in series, and the separated solution is the product liquid and enters the subsequent treatment.
2) A feeding area: the cation material is parallelly connected through pipeline and fed into No. 8 and No. 10 columns, and the discharged material liquid and material liquid discharged from No. 6 column are separated together for secondary separation.
3) A water material ejection area: pure water enters the No. 2 column through a pipeline and is connected with the No. 4 and No. 6 columns in series, and the washed sugar liquid is secondarily separated from the sugar liquid discharged from the No. 8 and No. 10 columns.
4) A regeneration zone: the liquid caustic soda enters a No. 28 column through a pipeline, and the discharged caustic soda and the caustic soda washed out from the No. 26 top are mixed and enter a No. 30 column and are connected with a No. 32 column in series.
5) Water top acid zone: pure water enters the No. 22 column through a pipeline and is connected with the No. 24 and No. 26 columns in series, and the steps are repeated after the pure water is rinsed and enters the secondary feeding area.
6) A material top water area: part of the product liquid enters a No. 20 column through a pipeline, and water washed from the top can be recycled.
The production steps of the device are as follows:
cleaning and shredding Jerusalem artichoke/herba Cichorii, leaching crude inulin leaching liquor (refraction of 12-20%, light transmittance of less than 10%, pH value of 4-5, conductivity of 5000-.
In the first step, ultrafiltration membranes (including ceramic and organic tubular membranes, pore size < 0.1 μm) are used to remove suspended substances from the solution. The generated dialysate 1 (refraction 12-20%, light transmittance less than 10%, pH 4-5, conductivity 5000-.
And secondly, the feed liquid obtained after primary activated carbon decolorization until the light transmittance is more than 80 percent and filtered by a plate frame enters a nanofiltration membrane system 3 for monosaccharide and disaccharide removal. The treated concentrated solution 2 (refraction is more than 20%, light transmittance is more than 80%, pH value is 4-5, conductivity is 5000-.
Thirdly, the concentrated solution 2 is evaporated and concentrated once until the refraction is 30-60%, and enters a continuous chromatographic separation system 5 to be desalted, decolored and desugared at the temperature of 40-65 ℃. The treated sugar has refractive index of 20-50%, light transmittance of more than 95%, pH value of 5-6, conductivity of less than 1000us/cm, and purity of more than 90%.
Fourthly, the sugar liquid separated by the continuous chromatography enters a continuous ion exchange system 6 for further desalination treatment, the refraction of the treated sugar liquid is 15-45%, the light transmittance is more than 98%, the PH value is 5-6, the electric conductivity is less than 100us/cm, and the purity is more than 90%. The solution is decolorized by secondary active carbon until the light transmittance is more than 99 percent, then the solution is subjected to secondary evaporation and concentration until the refraction is 50 to 60 percent, and then spray drying is carried out to obtain the inulin finished product.
Adopt the utility model discloses a device and technology carry out inulin production, and area is little, can be so that the consumption of water and active carbon significantly reduces, can reduce the use amount of acid-base in a large number simultaneously, and acid-base waste water reduces in a large number, reduces sewage treatment ability, has effectively saved the quantity of water, is suitable for and uses widely.
While the invention has been particularly shown and described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes in form and detail may be made therein without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (14)
1. A device for producing inulin by utilizing jerusalem artichoke or chicory is characterized in that: the device comprises an ultrafiltration membrane system, a first decolorizing unit, a nanofiltration membrane system, a first evaporation concentration unit, a continuous chromatographic separation system, a continuous ion exchange system, a second decolorizing unit, a second evaporation concentration unit and a spray drying unit which are connected in sequence, wherein a dialysate outlet of the ultrafiltration membrane system is connected with a liquid inlet pipeline of the first decolorizing unit, a concentrate outlet is connected with a first post-treatment pipe, a concentrate outlet of the nanofiltration membrane system is connected with a liquid inlet of the first evaporation concentration unit, and a dialysate outlet is connected with a second post-treatment pipe.
2. An apparatus for inulin production from Jerusalem artichoke or chicory as claimed in claim 1, wherein: the milipore filter system including the one-level head tank, one-level valve, one-level delivery pump, milipore filter unit and the dialysate tank of connecting in order, the dialysate export of milipore filter unit links to each other with the dialysate tank, and the concentrate export links to each other with one-level head tank through the one-level back flow, is equipped with one-level heat transfer device on the one-level back flow, the dialysate tank with the inlet pipeline of first decoloration unit links to each other.
3. An apparatus for inulin production from Jerusalem artichoke or chicory as claimed in claim 2, wherein: the ultrafiltration membrane adopted by the ultrafiltration membrane unit is a ceramic membrane or an organic tubular membrane with the aperture smaller than 0.1 um.
4. An apparatus for inulin production from Jerusalem artichoke or chicory as claimed in claim 1, wherein: receive the filter membrane system including the second grade head tank, second grade valve, second grade delivery pump, receive filter membrane unit and the feed liquor jar of connecting in order, the second grade head tank with the liquid outlet of first decoloration unit links to each other, receive filter membrane separating unit's concentrate export and feed liquor jar and link to each other, the dialysate outlet passes through the second grade back flow and links to each other with the second grade head tank, is equipped with second grade heat transfer device on the second grade back flow, the feed liquor jar with the inlet pipeline of first evaporation concentration unit links to each other.
5. An apparatus for inulin production from Jerusalem artichoke or chicory as claimed in claim 4, wherein: the second grade head tank with first decoloration unit between be equipped with sheet frame filtration system, sheet frame filtration system's inlet with the liquid outlet pipeline of first decoloration unit links to each other, sheet frame filtration system's liquid outlet with the second grade head tank pipeline links to each other.
6. An apparatus for inulin production from Jerusalem artichoke or chicory as claimed in claim 4, wherein: the aperture of the nanofiltration membrane adopted by the nanofiltration membrane unit is less than 1 kDa.
7. An apparatus for inulin production from Jerusalem artichoke or chicory as claimed in claim 1, wherein: the continuous chromatographic separation system comprises a plurality of resin columns which are uniformly distributed along the circumferential direction and rotate according to a fixed period, and sodium type chromatographic separation resin or calcium type chromatographic separation resin for separating sugar solution and salt solution is respectively filled in each resin column.
8. An apparatus for inulin production from Jerusalem artichoke or chicory as claimed in claim 7, wherein: the continuous chromatographic separation system comprises 12 resin columns which are divided into 6 regions, and each region comprises the following components:
a feeding area: the device comprises 2 resin columns connected in series, feed liquid of a first evaporation concentration unit positively enters a feeding area, and the feed liquid adsorbed by the feeding area positively enters a secondary separation area for re-adsorption;
a secondary separation area: the system comprises 2 resin columns connected in series, wherein a part of salt solution re-adsorbed by a secondary separation area reversely enters a salt top water area, and the rest salt solution is discharged through a pipeline for post-treatment;
a salt washing area: the device comprises 2 resin columns connected in series, and feed liquid generated in a salt washing area and feed liquid generated in a feeding area enter a secondary separation area together for re-adsorption;
a sugar washing area: the device comprises 4 resin columns connected in series, pure water is pumped into a sugar washing area in a forward direction, a part of sugar solution washed out by the sugar washing area enters a salt washing area in the forward direction, and the rest of sugar solution enters a continuous ion exchange system for further desalination treatment;
a salt top water area: comprises 1 resin column, the feed liquid washed out from the top is recycled and reused through a pipeline;
spare area: contains 1 resin column.
9. An apparatus for inulin production from Jerusalem artichoke or chicory as claimed in claim 1, wherein: the continuous ion exchange system comprises a plurality of ion exchange columns which are uniformly distributed along the circumferential direction and rotate according to a fixed period, the ion exchange columns are sequentially arranged according to numbers, wherein cation resin is filled in odd-numbered ion exchange columns, the cation exchange system is formed by the odd-numbered ion exchange columns, anion resin is filled in even-numbered ion exchange columns, and the anion exchange system is formed by the even-numbered ion exchange columns.
10. An apparatus for inulin production from Jerusalem artichoke or chicory as claimed in claim 9, wherein: the cation exchange system comprises 16 ion exchange columns which are divided into 6 regions, and each region comprises the following components:
a feeding area: the continuous chromatographic separation system comprises 2 ion exchange columns connected in parallel, sugar liquid generated by separation of the continuous chromatographic separation system positively enters a feeding area, and the feed liquid adsorbed by the feeding area positively enters a secondary separation area for re-adsorption;
a secondary separation area: the device comprises 4 ion exchange columns, wherein the 4 ion exchange columns comprise two sets of separation mechanisms connected in series, each set of separation mechanism is formed by connecting two ion exchange columns in parallel, a part of feed liquid after being re-adsorbed by a secondary separation zone enters a material top water zone in the forward direction, and the rest feed liquid is used as feed liquid of an anion exchange system;
a water material ejection area: the device comprises 3 ion exchange columns connected in series, pure water positively enters a water material lifting area, and a feed liquid washed out by the water material lifting area and a feed liquid separated by a feed area enter a secondary separation area together for re-adsorption;
a regeneration zone: comprises 3 ion exchange columns connected in series, acidic regeneration medium positively enters a regeneration zone, and feed liquid washed out by the regeneration zone is discharged out of a cation exchange system as waste acid;
water top acid zone: the system comprises 3 ion exchange columns connected in series, pure water positively enters a water top acid area, and feed liquid washed out by the water top acid area and feed liquid generated by the ion exchange column at the front end of a regeneration area enter the ion exchange column at the rear end of the regeneration area together;
a material top water area: contains 1 ion exchange column, and the feed liquid washed out from the top is recycled and reused through a pipeline.
11. An apparatus for inulin production from Jerusalem artichoke or chicory as claimed in claim 10, wherein: the acidic regeneration medium is hydrochloric acid.
12. An apparatus for inulin production from Jerusalem artichoke or chicory as claimed in claim 9, wherein: the anion exchange system comprises 16 ion exchange columns which are divided into 6 regions, and each region comprises the following components:
a feeding area: comprises 2 ion exchange columns connected in parallel, cation exchange effluent generated by the separation of a cation exchange system positively enters a feeding area, and feed liquid adsorbed by the feeding area positively enters a secondary separation area for re-adsorption;
a secondary separation area: the device comprises 4 ion exchange columns, wherein the 4 ion exchange columns comprise two sets of separation mechanisms connected in series, each set of separation mechanism is formed by connecting two ion exchange columns in parallel, one part of feed liquid after being re-adsorbed by a secondary separation zone positively enters a material top water zone, and the rest feed liquid serving as product liquid enters a second decoloring unit for decoloring;
a water material ejection area: the device comprises 3 ion exchange columns connected in series, pure water positively enters a water material lifting area, and a feed liquid washed out by the water material lifting area and a feed liquid separated by a feed area enter a secondary separation area together for re-adsorption;
a regeneration zone: comprises 3 ion exchange columns connected in series, an alkaline regeneration medium positively enters a regeneration zone, and feed liquid washed out by the regeneration zone is discharged out of an anion exchange system as waste alkali;
a water top alkali area: the system comprises 3 ion exchange columns connected in series, pure water positively enters a water top alkali area, and feed liquid washed out by the water top alkali area and feed liquid generated by the ion exchange column at the front end of a regeneration area enter the ion exchange column at the rear end of the regeneration area together;
a material top water area: contains 1 ion exchange column, and the feed liquid washed out from the top is recycled and reused through a pipeline.
13. An apparatus for inulin production from Jerusalem artichoke or chicory as claimed in claim 12, wherein: the alkaline regeneration medium is liquid alkali.
14. An apparatus for inulin production from Jerusalem artichoke or chicory as claimed in claim 1, wherein: and the decolorizing media in the first decolorizing unit and the second decolorizing unit are both activated carbon.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022805064.2U CN214300195U (en) | 2020-11-26 | 2020-11-26 | Device for producing inulin by utilizing jerusalem artichoke or chicory |
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