CN210481411U - Separation system for preparing xylose - Google Patents
Separation system for preparing xylose Download PDFInfo
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- CN210481411U CN210481411U CN201921261501.XU CN201921261501U CN210481411U CN 210481411 U CN210481411 U CN 210481411U CN 201921261501 U CN201921261501 U CN 201921261501U CN 210481411 U CN210481411 U CN 210481411U
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Abstract
The utility model relates to a piece-rate system for preparing xylose belongs to xylose production technical field. Including the demineralized water storage tank, the electrodialysis device, ion exchange column and alkali lye storage tank, the electrodialysis device is three, be first order electrodialysis device respectively, second electrodialysis device and third level electrodialysis device, first order electrodialysis device is connected with second order electrodialysis device, second order electrodialysis device is connected with the demineralized water storage tank, second order electrodialysis device is connected with third level electrodialysis device, third level electrodialysis device is connected with the demineralized water storage tank, the ion exchange column is connected with third level electrodialysis system, and the ion exchange column is connected with the alkali lye storage tank, the ion exchange column even has dealkalization device. The separation and purification of xylose are completed, and the reduction of the sugar leakage amount is realized; and the third pole high salt solution and the regenerated solution are recycled, so that the economic value is improved, the COD content in the wastewater is reduced, and the environmental pollution is reduced.
Description
Technical Field
The utility model relates to a piece-rate system for preparing xylose especially relates to a piece-rate system for preparing xylose with hemicellulose hydrolysate, belongs to xylose production technical field.
Background
The hemicellulose is a main raw material for producing xylose, wherein the main procedures comprise hydrolysis, decoloration, desalting, deacidification, evaporation, centrifugation, drying and the like in the process of preparing the xylose by taking the hemicellulose as the raw material. The specific process for producing xylose comprises the following steps: taking hemicellulose as a raw material, adding sulfuric acid into the hemicellulose under a heating condition, hydrolyzing the hemicellulose into xylose and other miscellaneous sugars by the sulfuric acid, and simultaneously, impurities such as sodium sulfate, sulfuric acid and the like exist in a hydrolysate; since the xylose produced before the centrifugation step is present in a solution state, impurities such as sodium sulfate and sulfuric acid in the hemicellulose hydrolysate need to be removed efficiently in order to improve the quality of the xylose.
At present, in the existing separation method, salt (such as calcium oxide and barium carbonate) and acid (such as sulfuric acid) are generally added into hemicellulose hydrolysate to generate precipitate (calcium sulfate or barium sulfate) so as to remove impurities such as sodium sulfate, sulfuric acid and the like in the hemicellulose hydrolysate, but the related separation system is complex, large in regulation and control difficulty, low in efficiency and high in cost, and electrolyte in the hydrolysate still has more residues and cannot meet the actual process requirements.
Disclosure of Invention
The utility model aims at overcoming the defects of the prior art and provides a separation system for preparing xylose. According to the technical scheme, a desalted water storage tank, an electrodialysis device, an ion exchange column, an alkali liquor storage tank and the like are arranged, three-stage electrodialysis is carried out on pretreated hemicellulose hydrolysate to obtain a first-stage high-salt solution, a third-stage high-salt solution and a third-stage high-sugar solution, the third-stage high-salt solution (comprising reducing sugar with the concentration of 13-15 g/L and the conductance of 20-30 ms/cm) is concentrated and desalted, and then the third-stage high-salt solution and the third-stage high-sugar solution are injected into the ion exchange column together to carry out a chromatography process; in the chromatography process, based on the exchange capacity of the resin in the ion exchange column, switching the ion exchange column meeting the requirement (the discharge conductance is less than or equal to 0.5ms/cm or the pH is more than or equal to 3); when the adsorption capacity of the ion exchange column is saturated, introducing alkali liquor to regenerate the ion exchange column to obtain regenerated liquid containing alkali and sugar, dealkalizing the regenerated liquid to obtain regenerated alkali liquor and regenerated alkaline sugar liquid, reusing the regenerated alkali liquor in the regeneration of the ion exchange column, concentrating the regenerated alkaline sugar liquid and the third-stage high-salt liquid, desalting, introducing into the ion exchange column, and performing chromatography again.
In the separation system, on one hand, the removal rate of impurities in the xylose solution is increased, and the product quality is improved; on the other hand, the third-level high-salt solution and the regenerated solution are recycled, the sugar leakage amount is reduced (80-90%), the economic benefit is improved, and meanwhile, on the premise of improving the quality of the xylose solution and the production efficiency, the COD content in sewage is reduced, and the environmental protection pressure is reduced.
In order to achieve the technical purpose, the following technical scheme is proposed:
the separation system for preparing xylose comprises a desalted water storage tank, three electrodialysis devices, an ion exchange column and an alkali liquor storage tank, wherein the three electrodialysis devices are respectively a first electrodialysis device, a second electrodialysis device and a third electrodialysis device; the second-stage electrodialysis device is connected with the desalted water storage tank, and a second-stage electrodialysis system is formed between the desalted water storage tank and the second-stage electrodialysis device; the second electrodialysis device is connected with the third electrodialysis device, the third electrodialysis device is connected with the desalted water storage tank, and a third electrodialysis system is formed between the desalted water storage tank and the third electrodialysis device;
the ion exchange column is connected with the third-stage electrodialysis system and is connected with the alkali liquor storage tank, and an ion exchange column regeneration system is formed between the ion exchange column and the alkali liquor storage tank; the ion exchange column is connected with a dealkalizing device.
Furthermore, a feed inlet of the first-stage electrodialysis device is connected with a conveying pipe for conveying hemicellulose hydrolysate, a high-sugar liquid outlet of the first-stage electrodialysis device is connected with a feed inlet of the second-stage electrodialysis device through the conveying pipe, a high-salt liquid outlet of the second-stage electrodialysis device is connected with the first-stage electrodialysis device through the conveying pipe, and a high-sugar liquid outlet of the second-stage electrodialysis device is connected with a feed inlet of the third-stage electrodialysis device through the conveying pipe; the high-sugar liquid outlet of the third electrodialysis device is connected with a temporary storage tank through a conveying pipe, and the high-salt liquid outlet of the third electrodialysis device is connected with the temporary storage tank through the conveying pipe; the temporary storage tank is connected with the feed inlet of the ion exchange column.
Further, still be equipped with enrichment facility and desalination device between third level electrodialysis device high salt liquid export and the jar of keeping in, third level electrodialysis device high salt liquid export is connected with enrichment facility, and enrichment facility is connected with desalination device, and desalination device is connected with the jar of keeping in.
Further, an alkali outlet of the dealkalization device is connected with an alkali inlet of the ion exchange column through a conveying pipe, or the alkali outlet of the dealkalization device is connected with an alkali liquor storage tank through a conveying pipe; the sugar outlet of the dealkalization device is connected with the concentration device through a conveying pipe.
Furthermore, the number of the ion exchange columns is at least two, and the ion exchange columns are connected with each other through a conveying pipe.
Furthermore, the electrodialysis separation system also comprises a dilution tank and a neutralization tank, wherein a high-salt solution outlet of the first-stage electrodialysis device is connected with the dilution tank through a conveying pipe, and the dilution tank is connected with the neutralization tank; the neutralization tank is connected with a waste water discharge pipe, or the neutralization tank is connected with a recycling device through a conveying pipe.
Furthermore, the first electrodialysis device, the second electrodialysis device and the third electrodialysis device respectively comprise electrodialysis membranes, and the electrodialysis membranes are alloy membranes.
Further, the dealkalization device comprises an electrodialysis membrane, and the electrodialysis membrane is an alloy membrane.
Furthermore, the concentration device and the desalination device both comprise electrodialysis membranes, and the electrodialysis membranes are homogeneous electrodialysis membranes or alloy membranes.
Further, the ion exchange column comprises a cation exchange column and an anion exchange column, wherein the cation exchange column adopts 001 × 7 type of cation resin, and the anion exchange column adopts D301 type of anion resin.
By adopting the technical scheme, the beneficial technical effects brought are as follows:
1) the utility model forms a separation system for preparing xylose by setting a demineralized water storage tank, an electrodialysis device, an ion exchange column, an alkali liquor storage tank and the like, completes the separation and purification of xylose, and realizes the reduction of the sugar leakage amount (80-90%); and the third pole high salt solution and the regenerated solution are recycled, so that the economic value is improved. Meanwhile, the discharge of sewage which is difficult to treat is reduced, the environmental protection benefit is greatly improved, and the environmental protection pressure is reduced (for example, the discharge of organic matters is reduced by about 5.5 tons/day, the sewage treatment cost is saved by about 15 yuan/ton, the sewage treatment capacity is reduced by 400 cubic meters/day, and the like);
2) in the utility model, because most of the run sugar is recovered by the separation system, the service life of the electrodialysis device is greatly prolonged (the service life of the diaphragm is prolonged by more than 30 percent), which not only increases the stability of the xylose preparation process, but also improves the usability of the equipment and reduces the cost of equipment consumption;
3) in the utility model, through the arrangement of the three-stage electrodialysis device, the electrodialysis method is adopted to remove the electrolyte, thereby improving the operation efficiency and the effectiveness of removing the electrolyte, leading the controllability to be higher, effectively avoiding introducing new impurities, reducing the cost and increasing the profit by about 2.5 ten thousand yuan/day;
4) in the utility model, through the arrangement of the concentration device and the desalination device, the third-level high-salt liquid is concentrated and desalted, and then enters the next process as the final feed liquid meeting the index together with the third-level high-sugar liquid, the sugar leakage amount is reduced to 2-3% from 10%, and the xylose yield is improved by about 2.8 tons/day;
5) the utility model is suitable for industrial mass production, can be directly arranged in the xylose production process to prepare xylose, realizes high yield, high quality and high efficiency, saves production cost and improves the integrity of equipment installation; the system can be independently arranged and is specially used for treating high-salt liquid after electrodialysis, regenerating an ion exchange column and treating regenerated liquid after chromatography, so that the equipment integration level is improved.
Drawings
FIG. 1 is a logic diagram of the present invention;
FIG. 2 is a block diagram of the operation of the present invention;
fig. 3 is a schematic view of the working principle of the electrodialysis device in the present invention;
wherein, in the figure: 1. desalting water storage tank, 2, first-stage electrodialysis device, 3, second-stage electrodialysis device, 4, third-stage electrodialysis device, 5, alkali liquor storage tank, 6, dealkalization device, 7, conveying pipe, 8, temporary storage tank, 9, concentration device, 10, desalination device, 11, dilution tank, 12, neutralization tank, 13, ion exchange column.
Detailed Description
In the following, the technical solutions in the embodiments of the present invention are clearly and completely described, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.
Example 1
As shown in fig. 1: the separation system for preparing xylose comprises a desalted water storage tank 1, electrodialysis devices, an ion exchange column 13 and an alkali liquor storage tank 5, wherein the number of the electrodialysis devices is three, namely a first-stage electrodialysis device 2, a second-stage electrodialysis device 3 and a third-stage electrodialysis device 4, the first-stage electrodialysis device 2 is connected with the second-stage electrodialysis device 3, and a first-stage electrodialysis system is formed between the first-stage electrodialysis device 2 and the second-stage electrodialysis device 3; the second-stage electrodialysis device 3 is connected with the desalted water storage tank 1, and a second-stage electrodialysis system is formed between the desalted water storage tank 1 and the second-stage electrodialysis device 3; the second electrodialysis device 3 is connected with the third electrodialysis device 4, the third electrodialysis device 4 is connected with the desalted water storage tank 1, and a third electrodialysis system is formed between the desalted water storage tank 1 and the third electrodialysis device 4;
the ion exchange column 13 is connected with the third-stage electrodialysis system, the ion exchange column 13 is connected with the alkali liquor storage tank 5, an ion exchange column regeneration system is formed between the ion exchange column 13 and the alkali liquor storage tank 5, and the ion exchange column 13 is connected with the dealkalization device 6.
Example 2
On the basis of example 1, further,
a feed port of the first-stage electrodialysis device 2 is connected with a conveying pipe 7 for conveying hemicellulose hydrolysate, a high-sugar liquid outlet of the first-stage electrodialysis device 2 is connected with a feed port of the second-stage electrodialysis device 3 through the conveying pipe 7, a high-salt liquid outlet of the second-stage electrodialysis device 3 is connected with the first-stage electrodialysis device 2 through the conveying pipe 7, and a high-sugar liquid outlet of the second-stage electrodialysis device 3 is connected with a feed port of the third-stage electrodialysis device 4 through the conveying pipe 7; a high-sugar liquid outlet of the third electrodialysis device 4 is connected with a temporary storage tank 8 through a conveying pipe 7, and a high-salt liquid outlet of the third electrodialysis device 4 is connected with the temporary storage tank 8 through the conveying pipe 7; the temporary storage tank 8 is connected with the feed inlet of the ion exchange column 13.
Still be equipped with enrichment facility 9 and desalination device 10 between third electrodialysis device 4 high salt liquid export and the jar 8 of keeping in, third electrodialysis device 4 high salt liquid export is connected with enrichment facility 9, and enrichment facility 9 is connected with desalination device 10, and desalination device 10 is connected with jar 8 of keeping in.
Example 3
On the basis of example 2, further,
the alkali outlet of the dealkalization device 6 is connected with the alkali inlet of the ion exchange column 13 through a conveying pipe 7, and the sugar outlet of the dealkalization device 6 is connected with the concentration device 9 through the conveying pipe 7.
Example 4
On the basis of embodiment 3, the present embodiment is different in that:
an alkali outlet of the dealkalization device 6 is connected with the alkali liquor storage tank 5 through a conveying pipe 7; the sugar outlet of the dealkalization device 6 is connected with a concentration device 9 through a conveying pipe 7.
Example 5
On the basis of examples 3 to 4, further,
the number of the ion exchange columns 13 is two, and the ion exchange columns 13 are connected with the ion exchange columns 13 through the conveying pipe 7.
Example 6
On the basis of example 5, further,
the electrodialysis separation system also comprises a dilution tank 11 and a neutralization tank 12, wherein a high-salt solution outlet of the first-stage electrodialysis device 2 is connected with the dilution tank 11 through a conveying pipe 7, and the dilution tank 11 is connected with the neutralization tank 12; the neutralization tank 12 is connected to a waste water discharge pipe, or the neutralization tank 12 is connected to a recycling device through a delivery pipe 7, such as: the treated wastewater is used for flushing equipment.
Example 7
On the basis of example 6, further,
the first-stage electrodialysis device 2, the second-stage electrodialysis device 3, the third-stage electrodialysis device 4 and the dealkalization device 6 respectively comprise electrodialysis membranes, and the electrodialysis membranes are alloy membranes; the concentration device 9 and the desalination device 10 both comprise electrodialysis membranes, and the electrodialysis membranes are homogeneous electrodialysis membranes or alloy membranes.
The ion exchange column 13 comprises a cation exchange column and an anion exchange column, wherein the cation exchange column adopts 001 × 7 type cation resin, and the anion exchange column adopts D301 type anion resin; the anion exchange column is connected with the alkali liquor storage tank 5, and an ion exchange column regeneration system is formed between the anion exchange column and the alkali liquor storage tank 5.
Example 7
Based on the separation system, the electrodialysis and chromatography combined process for preparing xylose (shown in figures 2-3) comprises the following steps:
1) first-stage electrodialysis: introducing the hemicellulose hydrolysate into a first-stage electrodialysis system, and introducing a second-stage high-salt solution (when the electrodialysis system is used for the first time, introducing desalted water, and when the electrodialysis system is in normal operation, namely the second-stage electrodialysis systemThe generated discharge flow is 17m3Stopping introducing desalted water into the second-stage high-salt solution,/h, and converting into a second-stage high-salt solution), and obtaining a first-stage high-sugar solution and a first-stage high-salt solution under the action of an electrodialysis membrane;
the feed flow of the hemicellulose hydrolysate is 40m3The feed flow of the second-stage high-salt liquid is 17m3H; the voltage is 150V, the current is 100A, and the temperature is 45 ℃; the discharge flow of the first-stage high-salt solution is 17m3The discharge flow of the first-stage high-sugar liquid is 40m3/h；
2) Second-stage electrodialysis: introducing the first-stage high-sugar solution obtained in the step 1) into a second-stage electrodialysis system, introducing desalted water, and performing the action of an electrodialysis membrane to obtain a second-stage high-sugar solution and a second-stage high-salt solution;
the feeding flow of the first-stage high-sugar liquid is 40m3Feed flow rate of desalted water is 17m3H; the voltage is 150V, the current is 100A, and the temperature is 45 ℃; the discharge flow of the second-stage high-salt solution is 17m3The discharge flow of the second-stage high-sugar liquid is 40m3/h；
3) Third-stage electrodialysis: introducing the second-stage high-sugar solution obtained in the step 2) into a third-stage electrodialysis system, introducing desalted water, and performing the action of an electrodialysis membrane to obtain a third-stage high-sugar solution and a third-stage high-salt solution;
the feeding flow of the second stage high sugar liquid is 40m3Feed flow rate of desalted water is 17m3H; the voltage is 150V, the current is 85A, and the temperature is 45 ℃; the discharge flow of the third-stage high-salt solution is 17m3The third-stage high sugar liquid discharge flow is 40m3/h。
4) Temporary storage: concentrating and desalting the third-stage high-salt solution obtained in the step 3), and storing the concentrated and desalted third-stage high-salt solution and the third-stage high-sugar solution obtained in the step 3) in a temporary storage tank for later use;
5) chromatography: injecting the temporary storage solution obtained in the step 4) into an ion exchange column, and carrying out chromatography to obtain a xylose solution; the feed flow of the temporary storage solution is 50m3H, the temperature is 35 ℃, and the pressure is 0.1 MPa; the discharge flow of the xylose solution is 50m3/h；
6) Regeneration: step of going to the channelsIntroducing alkali liquor into the used ion exchange column, and regenerating to obtain regenerated liquid containing sugar and alkali; the alkali liquor feed flow is 15m3H, the temperature is 45 ℃, and the pressure is 0.1 MPa;
7) recycling: carrying out electrodialysis dealkalization on the regenerated solution obtained in the step 6) to obtain regenerated alkali liquor and alkaline regenerated sugar liquor, and introducing the regenerated alkali liquor into the ion exchange column used in the step 5) for recycling; concentrating and desalting the alkaline regenerated sugar solution and the third-stage high-salt solution obtained in the step 3) for recycling;
the discharge flow of the regenerated alkali liquor is 15m3H, the discharge flow of the alkaline regenerated sugar solution is 15m3/h。
The hemicellulose hydrolysate is prepared by the following steps: after hemicellulose raw material is hydrolyzed by sulfuric acid, the hemicellulose hydrolysate is pretreated by adopting the prior mature technology such as filtration, decoloration, ultrafiltration and the like. Wherein, in the hemicellulose hydrolysate, the xylose content is 85g/L, the sodium sulfate content is 21g/L, and the sulfuric acid content is 23 g/L.
In steps 6) and 7), the ion exchange column used in step 5) comprises an ion exchange column with a discharge conductance of more than 500 us/cm or a discharge pH of less than 3.
In the steps 1), 2) and 3), the electrodialysis membrane is an alloy membrane.
In the concentration process of the step 4), an alloy membrane is adopted for concentration, and the conductance of the concentrated third-stage high-salt solution is 220 ms/cm.
In the desalting step of the step 4), an alloy membrane is adopted for desalting, and the conductivity of the desalted third-stage high-salt solution is 4 ms/cm.
In the step 1), the first-stage high-salt solution comprises reducing sugar with the concentration of 20g/L, sulfuric acid with the concentration of 35g/L and sodium sulfate with the concentration of 18 g/L; the first-stage high-sugar liquid comprises reducing sugar with the concentration of 75g/L, sulfuric acid with the concentration of 14g/L and sodium sulfate with the concentration of 5 g/L;
in the step 2), the second-stage high-salt solution comprises reducing sugar with the concentration of 15g/L, sulfuric acid with the concentration of 20g/L and sodium sulfate with the concentration of 18 g/L; the second-stage high-sugar solution comprises reducing sugar with the concentration of 75g/L, sulfuric acid with the concentration of 10g/L and sodium sulfate with the concentration of 5 g/L;
in the step 3), the third-stage high-salt solution comprises reducing sugar with the concentration of 15g/L, sulfuric acid with the concentration of 8g/L and sodium sulfate with the concentration of 5 g/L; the third-level high-sugar solution comprises reducing sugar with the concentration of 75g/L, sulfuric acid with the concentration of 2g/L and sodium sulfate with the concentration of 1 g/L;
in step 5), the xylose solution comprises 75g/L of xylose;
in the step 6), the regeneration liquid comprises 30g/L of reducing sugar and 30/L of sodium hydroxide;
in the step 7), the regenerated alkali solution comprises 70g/L of sodium hydroxide, and the alkaline regenerated sugar solution comprises 30g/L of reducing sugar, 10g/L of sodium sulfate and 0.2g/L of sodium hydroxide.
According to the GB/T23532-2009 xylose standard, through detection, after the hemicellulose hydrolysate is subjected to electrodialysis separation: the conductivity is less than or equal to 4000us/cm, the light transmittance is more than or equal to 98.0 percent, the refraction is more than or equal to 7.0, the specific rotation is 18.5-19.5 degrees, and the pH value is 2.2-2.8; the content of reducing sugar is more than or equal to 70g/L, the content of xylose is more than or equal to 55g/L, and the purity of xylose is more than or equal to 80 percent; less than or equal to 0.3 percent of inorganic acid, less than or equal to 0.4 percent of total acid, less than or equal to 0.005 percent of sulfate, less than or equal to 0.05 percent of ash, less than or equal to 0.3 percent of water and less than or equal to 0.005 percent of chloride;
after ion exchange column chromatography, the conductivity of the xylose solution is 0.05-0.5 ms/cm, the pH is 2.5-3.5, and the refraction is 8-9.
Claims (10)
1. A separation system for the production of xylose characterized by: the desalting device comprises a desalted water storage tank (1), three electrodialysis devices, an ion exchange column (13) and an alkali liquor storage tank (5), wherein the three electrodialysis devices are respectively a first electrodialysis device (2), a second electrodialysis device (3) and a third electrodialysis device (4), the first electrodialysis device (2) is connected with the second electrodialysis device (3), and a first electrodialysis system is formed between the first electrodialysis device (2) and the second electrodialysis device (3); the second-stage electrodialysis device (3) is connected with the desalted water storage tank (1), and a second-stage electrodialysis system is formed between the desalted water storage tank (1) and the second-stage electrodialysis device (3); the second electrodialysis device (3) is connected with the third electrodialysis device (4), the third electrodialysis device (4) is connected with the desalted water storage tank (1), and a third electrodialysis system is formed between the desalted water storage tank (1) and the third electrodialysis device (4);
the ion exchange column (13) is connected with the third-stage electrodialysis system, the ion exchange column (13) is connected with the alkali liquor storage tank (5), an ion exchange column regeneration system is formed between the ion exchange column (13) and the alkali liquor storage tank (5), and the ion exchange column (13) is connected with the dealkalization device (6).
2. The separation system for the production of xylose according to claim 1, characterized by the fact that: the feed inlet of the first-stage electrodialysis device (2) is connected with a conveying pipe (7) for conveying hemicellulose hydrolysate, a high-sugar liquid outlet of the first-stage electrodialysis device (2) is connected with the feed inlet of the second-stage electrodialysis device (3) through the conveying pipe (7), a high-salt liquid outlet of the second-stage electrodialysis device (3) is connected with the first-stage electrodialysis device (2) through the conveying pipe (7), and a high-sugar liquid outlet of the second-stage electrodialysis device (3) is connected with the feed inlet of the third-stage electrodialysis device (4) through the conveying pipe (7); a high-sugar liquid outlet of the third electrodialysis device (4) is connected with a temporary storage tank (8) through a conveying pipe (7), and a high-salt liquid outlet of the third electrodialysis device (4) is connected with the temporary storage tank (8) through the conveying pipe (7); the temporary storage tank (8) is connected with a feed inlet of the ion exchange column (13).
3. The separation system for the production of xylose according to claim 2, characterized by the fact that: still be equipped with between third electrodialysis device (4) high salt liquid export and the jar (8) of keeping in concentration device (9) and desalination device (10), third electrodialysis device (4) high salt liquid export is connected with concentration device (9), and concentration device (9) are connected with desalination device (10), and desalination device (10) are connected with jar (8) of keeping in.
4. The separation system for the production of xylose according to claim 3, characterized by the fact that: the alkali outlet of the dealkalization device (6) is connected with the alkali inlet of the ion exchange column (13) through a conveying pipe (7), or the alkali outlet of the dealkalization device (6) is connected with the alkali liquor storage tank (5) through the conveying pipe (7); the sugar outlet of the dealkalization device (6) is connected with a concentration device (9) through a conveying pipe (7).
5. The separation system for the production of xylose according to claim 1, characterized by the fact that: the number of the ion exchange columns (13) is at least two, and the ion exchange columns (13) are connected with the ion exchange columns (13) through conveying pipes (7).
6. The separation system for the production of xylose according to claim 1, characterized by the fact that: the separation system also comprises a dilution tank (11) and a neutralization tank (12), wherein a high-salt liquid outlet of the first-stage electrodialysis device (2) is connected with the dilution tank (11) through a conveying pipe (7), and the dilution tank (11) is connected with the neutralization tank (12); the neutralization tank (12) is connected with a waste water discharge pipe or a waste water recycling pipe.
7. The separation system for the production of xylose according to claim 1, characterized by the fact that: the first-stage electrodialysis device (2), the second-stage electrodialysis device (3), the third-stage electrodialysis device (4) and the dealkalization device (6) comprise electrodialysis membranes, and the electrodialysis membranes are alloy membranes.
8. The separation system for the production of xylose according to claim 3, characterized by the fact that: the concentration device (9) and the desalination device (10) both comprise membrane mechanisms, and the membrane mechanisms are homogeneous electrodialysis membranes or alloy membranes.
9. The separation system for the production of xylose according to claim 1, characterized by the fact that: the ion exchange column (13) comprises a cation exchange column and an anion exchange column, wherein the cation exchange column is provided with 001 x 7 type of cation resin, and the anion exchange column is provided with D301 type of anion resin.
10. The separation system for the production of xylose according to claim 9, characterized by the fact that: the anion exchange column (13) is connected with the alkali liquor storage tank (5), and an ion exchange column regeneration system is formed between the anion exchange column (13) and the alkali liquor storage tank (5).
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113976186A (en) * | 2021-11-25 | 2022-01-28 | 浙江华康药业股份有限公司 | Xylose mother liquor ion exchange system and method |
| CN115198038A (en) * | 2021-04-08 | 2022-10-18 | 四川雅华生物有限公司 | Process for recovering electrodialysis sugar-containing wastewater from semi-fiber xylose production |
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2019
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115198038A (en) * | 2021-04-08 | 2022-10-18 | 四川雅华生物有限公司 | Process for recovering electrodialysis sugar-containing wastewater from semi-fiber xylose production |
| CN115198038B (en) * | 2021-04-08 | 2023-09-19 | 四川雅华生物有限公司 | Process for recycling semi-fiber xylose-making electrodialysis sugar-containing wastewater |
| CN113976186A (en) * | 2021-11-25 | 2022-01-28 | 浙江华康药业股份有限公司 | Xylose mother liquor ion exchange system and method |
| CN113976186B (en) * | 2021-11-25 | 2023-08-15 | 浙江华康药业股份有限公司 | Xylose mother liquor ion exchange system and method |
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