Ion exchange device and method for desalting and deodorizing erythritol fermentation liquor

Abstract

The invention relates to an ion exchange device and method for desalting and deodorizing erythritol fermentation liquor. The ion exchange device comprises a continuous cation exchange system, a continuous anion exchange system and a mixed bed ion exchange system, the cation exchange system comprises a first-stage cation exchange bin and a second-stage cation exchange bin which are communicated with the erythritol fermentation liquor, and cation exchange columns are arranged in the first-stage cation exchange bin and the second-stage cation exchange bin; the continuous anion exchange system comprises a first-stage anion exchange bin and a second-stage anion exchange bin which are both provided with anion exchange columns; the first-stage cation exchange bin, the first-stage anion exchange bin, the second-stage cation exchange bin, the second-stage anion exchange bin and the mixed bed ion exchange system are sequentially communicated, so that the treatment effects of efficiently desalting and deodorizing the erythritol fermentation liquor are achieved, and finally, the purity of the erythritol is improved, and no peculiar smell exists.

Description

Technical Field

[0001] The invention belongs to the technical field of microbial fermentation production, and particularly relates to an ion exchange device and method for desalting and deodorizing erythritol fermentation liquid. Background Art

[0002] Erythritol, also known as 1,2,3,4-butanetetrol, is a new type of functional sugar alcohol sweetener. It is widely found in fruits, algae, fungi, and fermented foods such as soy sauce and wine. Erythritol has the characteristics of high thermal stability, low hygroscopicity, harmonious sweetness, low calories, low GI and high tolerance. Erythritol is widely used in the chemical, pharmaceutical and food fields, and has strong competitiveness in the sweetener market. Erythritol is the only sweetener that can be produced by microbial fermentation. It is a filling functional food additive. With the increase in the number of diabetics, the public's health awareness and sugar control measures in various countries are constantly increasing, and the demand for erythritol as a low-calorie sweetener is showing a continuous growth trend.

[0003] Fermentation is the main way to industrialize the production of erythritol. After obtaining the erythritol fermentation broth by microbial fermentation, separation and purification technology is needed to extract and purify it in order to obtain the erythritol product. The composition of erythritol fermentation broth is complex. The presence of organic acids, residual sugars, proteins, pigments and some ionic impurities increases the difficulty of separating and purifying erythritol. In particular, the presence of small molecule inorganic salts in the fermentation broth seriously affects the crystallization purity and extraction rate of erythritol. At the same time, the bad smell in the fermentation broth also seriously affects the quality of erythritol as a food additive. The conventional ion exchange technology is used to remove inorganic salts from the fermentation broth. Not only is the desalination efficiency low, the operation time is long, the consumption of washing water and regeneration agent is large, and the amount of waste liquid generated is large, but it cannot effectively remove the odor in the fermentation broth, which seriously affects the extraction yield and finished product quality of erythritol.

[0004] Therefore, an ion exchange device and method for desalting and deodorizing erythritol fermentation broth are designed to achieve efficient desalting and deodorizing of erythritol fermentation broth, so that the total extraction yield of pure erythritol reaches more than 94%, the purity reaches more than 99.9%, and the product has no odor, which is a technical problem that technical personnel in this field need to solve. Summary of the invention

[0005] In order to solve the above problems, the present invention provides an ion exchange device and method for desalting and deodorizing erythritol fermentation broth. A continuous cation exchange system, a continuous anion exchange system and a mixed bed ion exchange system form a comprehensive ion exchange system. The erythritol fermentation broth is sequentially processed through a primary cation exchange chamber, a primary anion exchange chamber, a secondary cation exchange chamber, a secondary anion exchange chamber and the mixed bed ion exchange system to achieve the effect of efficiently desalting and deodorizing the erythritol fermentation broth, and finally the total extraction yield of pure erythritol reaches more than 94%, the purity reaches more than 99.9%, and the product has no odor.

[0006] To achieve the above object, the present invention provides the following solutions:

[0007] An ion exchange device for desalting and deodorizing erythritol fermentation liquid, comprising a continuous cation exchange system, a continuous anion exchange system and a mixed bed ion exchange system;

[0008] The cation exchange system includes a primary cation exchange tank and a secondary cation exchange tank connected to the erythritol fermentation liquid, and the primary cation exchange tank and the secondary cation exchange tank are both provided with cation exchange columns, and the continuous anion exchange system includes a primary anion exchange tank and a secondary anion exchange tank, both of which are provided with anion exchange columns;

[0009] The primary cation exchange chamber, the primary anion exchange chamber, the secondary cation exchange chamber, the secondary anion exchange chamber and the mixed bed ion exchange system are connected in sequence.

[0010] Preferably, the continuous cation exchange system further comprises a cylindrical first supporting device, a first rotating chassis arranged at the bottom of the first supporting device, and a cation exchange primary water washing tank, a cation exchange regeneration tank, a cation exchange secondary water washing tank, the secondary cation exchange tank and the primary cation exchange tank arranged in sequence on the first rotating chassis in a cylindrical shape, wherein the cation exchange primary water washing tank, the cation exchange regeneration tank and the cation exchange secondary water washing tank are all provided with cation exchange columns, the first supporting device is provided with a first wash water inlet and a first waste water outlet connected to the cation exchange column in the cation exchange primary water washing tank at the location corresponding to the cation exchange primary water washing tank, the first supporting device is provided with a first dilute alkali inlet, a first dilute hydrochloric acid inlet and a second waste water outlet connected to the cation exchange column in the cation exchange regeneration tank at the location corresponding to the cation exchange regeneration tank, the first supporting device is provided with a first pure water inlet connected to the cation exchange column in the cation exchange secondary water washing tank at the location corresponding to the cation exchange secondary water washing tank, and the first supporting device is provided with an erythritol fermentation liquid inlet connected to the cation exchange column in the primary cation exchange tank at the location corresponding to the primary cation exchange tank.

[0011] Preferably, the continuous anion exchange system includes a cylindrical second supporting device, a second rotating chassis arranged at the bottom of the second supporting device, and an anion exchange primary water washing tank, an anion exchange regeneration tank, an anion exchange secondary water washing tank, the secondary anion exchange tank and the primary anion exchange tank arranged in sequence on the second rotating chassis in a cylindrical shape, anion exchange primary water washing tank, anion exchange regeneration tank and anion exchange secondary water washing tank are all provided with anion exchange columns, the second supporting device is provided with a second wash water inlet and a third waste water outlet connected to the anion exchange column in the anion exchange primary water washing tank corresponding to the anion exchange primary water washing tank, the second supporting device is provided with a second dilute alkali inlet, a second dilute hydrochloric acid inlet and a fourth waste water outlet connected to the anion exchange column in the anion exchange regeneration tank corresponding to the anion exchange regeneration tank, and the second supporting device is provided with a second pure water inlet connected to the anion exchange column in the anion exchange secondary water washing tank corresponding to the anion exchange secondary water washing tank.

[0012] Preferably, three cation exchange columns are evenly distributed in the cation exchange primary water washing tank, and a connecting pipeline is arranged on the first supporting device so that the three cation exchange columns are connected in sequence. Four cation exchange columns are evenly distributed in the cation exchange regeneration tank, and a connecting pipeline is arranged on the first supporting device so that the four cation exchange columns are connected in sequence. Three cation exchange columns are evenly distributed in the cation secondary water washing tank, and a connecting pipeline is arranged on the first supporting device so that the three cation exchange columns are connected in sequence, and the cation exchange column close to the cation exchange regeneration tank is connected to any one of the cation exchange columns in the cation exchange regeneration tank. Four cation exchange columns connected in parallel are evenly distributed in the secondary cation exchange tank, the first dilute alkali inlet is connected to the cation exchange column close to the cation exchange primary water washing tank, and the first dilute hydrochloric acid inlet is connected to the cation exchange column close to the cation exchange secondary water washing tank.

[0013] Preferably, three anion exchange columns are evenly distributed in the anion exchange primary water washing tank, and a connecting pipeline is arranged on the first supporting device so that the three anion exchange columns are connected in sequence. Four anion exchange columns are evenly distributed in the anion exchange regeneration tank, and a connecting pipeline is arranged on the first supporting device so that the four anion exchange columns are connected in sequence. Three anion exchange columns are evenly distributed in the anion secondary water washing tank, and a connecting pipeline is arranged on the first supporting device so that the three anion exchange columns are connected in sequence, and the anion exchange column close to the anion exchange regeneration tank is connected to any one of the anion exchange columns in the anion exchange regeneration tank. Four anion exchange columns connected in parallel are evenly distributed in the secondary anion exchange tank, the second dilute alkali inlet is connected to the anion exchange column close to the anion exchange secondary water washing tank, and the second dilute hydrochloric acid inlet is connected to the anion exchange column close to the anion exchange primary water washing tank.

[0014] Preferably, the mixed bed ion exchange system comprises a pre-bed bag filter, a mixed bed ion exchange column and a post-bed bag filter which are connected in sequence, the mixed bed ion exchange column is provided with a third wash water inlet, a third pure water inlet, a third dilute alkali inlet, a third dilute hydrochloric acid inlet and a fifth waste water outlet, the post-bed bag filter is provided with a fourth wash water inlet and a discharge port, and the discharge port is connected to the concentrating device.

[0015] Preferably, the fifth wastewater outlet is connected to the wastewater tank and the primary cation exchange tank at the same time.

[0016] Preferably, the upper half of the mixed bed ion exchange column is an anion exchange column, and the lower half of the mixed bed ion exchange column is a cation exchange column.

[0017] Preferably, the cation exchange column is an exchange resin D001FD, and the anion exchange column is an exchange resin D354FD.

[0018] The present invention also discloses an ion exchange method for desalting and deodorizing erythritol fermentation liquid, comprising the following steps:

[0019] The erythritol fermentation liquid is sequentially passed into a primary cation exchange tank, a primary anion exchange tank, a secondary cation exchange tank, a secondary anion exchange tank and a mixed bed ion exchange system for continuous ion exchange;

[0020] The cation exchange column in the cation exchange bin is rotated to the cation exchange primary water washing bin, the cation exchange regeneration bin, and the cation exchange secondary water washing bin in sequence through the rotation of the first rotating chassis for water washing and regeneration;

[0021] The anion exchange column in the anion exchange chamber is rotated to the anion exchange primary water washing chamber, the anion exchange regeneration chamber, and the anion exchange secondary water washing chamber in sequence through the rotation of the second rotating chassis for water washing and regeneration;

[0022] The mixed bed ion exchange column is washed and regenerated.

[0023] Compared with the prior art, the present invention has achieved the following technical effects:

[0024] The erythritol fermentation liquid is sequentially processed through a primary cation exchange chamber, a primary anion exchange chamber, a secondary cation exchange chamber, a secondary anion exchange chamber and a mixed bed ion exchange system, so as to achieve the effect of efficient desalination and deodorization of the erythritol fermentation liquid, and finally the total extraction yield of pure erythritol reaches more than 94%, the purity reaches more than 99.9%, and the product has no odor. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] In order to more clearly illustrate the technical solutions in the present invention or the prior art, the drawings required for use in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative labor.

[0026] Attached Figure 1 It is a schematic diagram of a continuous cation exchange process equipment flow chart of an ion exchange device and method for desalting and deodorizing erythritol fermentation broth disclosed in an embodiment of the present invention;

[0027] Attached Figure 2 It is a schematic diagram of a continuous anion exchange process equipment flow chart of an ion exchange device and method for desalting and deodorizing erythritol fermentation broth disclosed in an embodiment of the present invention;

[0028] Attached Figure 3 It is a schematic diagram of a mixed bed ion exchange process equipment flow chart of an ion exchange device and method for desalting and deodorizing erythritol fermentation broth disclosed in an embodiment of the present invention;

[0029] Among them, II, cation exchange primary water washing tank; I-II, primary cation exchange tank; I-III, secondary cation exchange tank; I-IV, cation exchange secondary water washing tank; IV, cation exchange regeneration tank; Pa~Pr, 18 pairs of cation exchange column feed and discharge ports; P1~P18, 18 cation exchange columns; PL, erythritol fermentation broth; FW1, first wash water inlet; FW2, second wash water inlet; FW3, third wash water inlet; FW4, fourth wash water inlet; DW1, first pure water inlet; DW2, second pure water inlet; DW3, third pure water inlet; DHA1, first dilute hydrochloric acid inlet; DHA2, second dilute hydrochloric acid inlet; DHA3, third dilute hydrochloric acid inlet; DL1, first dilute alkali inlet; DL2, the second dilute alkali inlet; DL3, the third dilute alkali inlet; WWT1, the first wastewater outlet; WWT2, the second wastewater outlet; WWT3, the third wastewater outlet; WWT4, the fourth wastewater outlet; WWT5, the fifth wastewater outlet; II-I, the anion exchange primary water washing tank; II-II, the primary anion exchange tank; II-III, the secondary anion exchange tank; II-IV, the anion exchange secondary water washing tank; II-V, the anion exchange regeneration tank; Na~Nr, the feed inlet and discharge outlet of 18 pairs of anion exchange columns; N1~N18, 18 anion exchange columns; III-I, the pre-bed bag filter; III-II, the mixed bed ion exchange column; III-III, the post-bed bag filter; CTS, the concentration device. DETAILED DESCRIPTION

[0030] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0031] The invention aims to provide an ion exchange device and method for desalting and deodorizing erythritol fermentation liquid. A continuous cation exchange system, a continuous anion exchange system and a mixed bed ion exchange system form a comprehensive ion exchange system. The erythritol fermentation liquid PL is sequentially processed through a primary cation exchange chamber I-II, a primary anion exchange chamber II-II, a secondary cation exchange chamber I-III, a secondary anion exchange chamber II-III and the mixed bed ion exchange system, so as to achieve the treatment effect of efficiently desalting and deodorizing the erythritol fermentation liquid PL, and finally make the total extraction yield of pure erythritol reach more than 94%, the purity reach more than 99.9%, and the product has no odor.

[0032] In order to make the above-mentioned objects, features and advantages of the present invention more obvious and easy to understand, the present invention is further described in detail below with reference to the accompanying drawings and specific embodiments.

[0033] refer to Figure 1-3 The ion exchange device for desalting and deodorizing the erythritol fermentation liquid PL disclosed in the embodiment of the present invention comprises at least a continuous cation exchange system, a continuous anion exchange system and a mixed bed ion exchange system, the cation exchange system comprises a primary cation exchange chamber I-II and a secondary cation exchange chamber I-III connected to the erythritol fermentation liquid PL, the primary cation exchange chamber I-II and the secondary cation exchange chamber I-III are both provided with cation exchange columns, the continuous anion exchange system comprises a primary anion exchange chamber II-II and a secondary anion exchange chamber II-III, both of which are provided with anion exchange columns, the primary cation exchange chamber I-II and the secondary anion exchange chamber II-III are both provided with anion exchange columns, The warehouse I-II, the primary anion exchange warehouse II-II, the secondary cation exchange warehouse I-III, the secondary anion exchange warehouse II-III and the mixed bed ion exchange system are connected in sequence, and the erythritol fermentation liquid PL is processed in sequence through the primary cation exchange warehouse I-II, the primary anion exchange warehouse II-II, the secondary cation exchange warehouse I-III, the secondary anion exchange warehouse II-III and the mixed bed ion exchange system, so as to achieve the effect of efficient desalination and deodorization of the erythritol fermentation liquid PL, and finally make the total extraction yield of pure erythritol reach more than 94%, the purity reach more than 99.9%, and the product has no odor.

[0034] refer to Figure 1As an embodiment, the cation exchange system also includes a cylindrical first supporting device, a first rotating chassis is arranged at the bottom of the first supporting device, and a cylindrical cation exchange primary water washing chamber II, a cation exchange regeneration chamber IV, a cation exchange secondary water washing chamber I-IV, a secondary cation exchange chamber I-III and a primary cation exchange chamber I-II are arranged in sequence on the first rotating chassis. When the first rotating chassis rotates, the cation exchange primary water washing chamber II, the cation exchange regeneration chamber IV, the cation exchange secondary water washing chamber I-IV, the secondary cation exchange chamber I-III and the primary cation exchange chamber I-II will be driven to change positions in sequence. The rotation direction of the first rotating chassis Towards the direction from the cation exchange primary water washing tank II to the cation exchange regeneration tank IV, the cation exchange primary water washing tank II, the cation exchange regeneration tank IV and the cation exchange secondary water washing tanks I-IV are all provided with cation exchange columns, the first supporting device is provided with a first wash water inlet FW1 and a first waste water outlet WWT1 connected to the cation exchange column in the cation exchange primary water washing tank II at the corresponding cation exchange primary water washing tank II, the first supporting device is provided with a first dilute alkali inlet DL1, a first dilute hydrochloric acid inlet DHA1 and a second waste water outlet WWT2 connected to the cation exchange column in the cation exchange regeneration tank IV at the corresponding cation exchange regeneration tank IV, the first supporting device A first pure water inlet DW1 connected to the cation exchange column in the cation exchange secondary water washing tank I-IV is provided at the corresponding cation exchange secondary water washing tank I-IV, and an erythritol fermentation liquid PL inlet connected to the cation exchange column in the primary cation exchange tank I-II is provided at the first supporting device corresponding to the primary cation exchange tank I-II. When the first rotating chassis rotates, each pipeline inlet or outlet arranged on the first supporting device does not rotate with the first rotating chassis, but drives the cation exchange column to rotate through the rotation of the first rotating chassis. When the cation exchange column rotates one position, it is automatically connected to the pipeline inlet or pipeline outlet at the corresponding position. For example, the secondary cation exchange tank I -III rotates to the cation exchange primary water washing tank II through the first rotating chassis, the cation exchange column inside the secondary cation exchange tank I-III rotates into the cation exchange primary water washing tank II, and is connected to the first washing water inlet FW1 and the first waste water outlet WWT1 at the cation exchange primary water washing tank II corresponding to the first supporting device. When the ion exchange of the ion exchange columns arranged in the primary cation exchange tank I-II and the secondary cation exchange tank I-III is completed, the automatic rotation of the cation exchange column can be realized by setting the first rotating chassis to realize automatic water washing and regeneration of the cation exchange column, so that the cation exchange column can be reused and the water washing and regeneration efficiency is improved;

[0035] It should be noted that the connecting pipeline on the cation exchange column and the connecting pipeline on the first supporting device can be set to be magnetically attracted, and when the cation exchange column rotates to a corresponding position, it can be automatically connected to the pipeline at the corresponding position.

[0036] refer to Figure 2As an embodiment, the anion exchange system further comprises a cylindrical second supporting device, a second rotating chassis is arranged at the bottom of the second supporting device, and a cylindrical anion exchange primary water washing chamber II-I, anion exchange regeneration chamber II-V, anion exchange secondary water washing chamber II-IV, secondary anion exchange chamber II-III and primary anion exchange chamber II-II are arranged on the second rotating chassis in sequence. When the second rotating chassis rotates, the anion exchange primary water washing chamber II-I, anion exchange regeneration chamber II-V, anion exchange secondary water washing chamber II-IV, secondary anion exchange chamber II-III and primary anion exchange chamber II-II are driven to rotate in sequence. The position changes for the second time, and the rotation direction of the second rotating chassis is toward the direction from the anion exchange primary water washing tank II-I to the anion exchange regeneration tank II-V. Anion exchange columns are arranged inside the anion exchange primary water washing tank II-I, the anion exchange regeneration tank II-V and the anion exchange secondary water washing tank II-IV. The second supporting device is provided with a second wash water inlet FW2 and a third waste water outlet WWT3 connected to the anion exchange column in the anion exchange primary water washing tank II-I at the anion exchange primary water washing tank II-I, and a third waste water outlet WWT3 connected to the anion exchange column in the anion exchange regeneration tank II-V at the second supporting device. The second dilute alkali inlet DL2, the second dilute hydrochloric acid inlet DHA2 and the fourth wastewater outlet WWT4 are provided at the second supporting device corresponding to the anion exchange secondary water washing tank II-IV, and the second pure water inlet DW2 connected with the anion exchange column in the anion exchange secondary water washing tank II-IV is provided. When the second rotating chassis rotates, the various pipeline inlets or outlets arranged on the second supporting device do not rotate with the second rotating chassis, but the anion exchange column is driven to rotate by the rotation of the second rotating chassis. When the anion exchange column rotates one position, it is automatically connected to the pipeline inlet or pipeline outlet at the corresponding position. For example, the secondary anion exchange tank II-III is connected to the anion exchange column by the second rotating chassis. When rotating to the anion exchange primary water washing warehouse II-I, the anion exchange column inside the secondary anion exchange warehouse II-III rotates into the anion exchange primary water washing warehouse II-I, and is connected to the second washing water inlet FW2 and the third waste water outlet WWT3 at the anion exchange primary water washing warehouse II-I corresponding to the second supporting device. When the ion exchange of the ion exchange columns arranged in the primary anion exchange warehouse II-II and the secondary anion exchange warehouse II-III is completed, the automatic rotation of the anion exchange column can be realized by setting two rotating chassis to realize automatic water washing and regeneration of the anion exchange column, so that the anion exchange column can be reused and the water washing and regeneration efficiency is improved;

[0037] It should be noted that the connecting pipeline on the anion exchange column and the connecting pipeline on the second supporting device can be set to a magnetic type. When the anion exchange column rotates to the corresponding position, it can be automatically connected to the pipeline at the corresponding position. The first rotating base and the second rotating base are driven by a driving device.

[0038] refer to Figure 1 As an embodiment, three cation exchange columns are evenly distributed in the cation exchange primary water washing warehouse II, and a connecting pipeline is arranged on the first supporting device so that the three cation exchange columns are connected in sequence. Four cation exchange columns are evenly distributed in the cation exchange regeneration warehouse IV, and a connecting pipeline is arranged on the first supporting device so that the four cation exchange columns are connected in sequence. Three cation exchange columns are evenly distributed in the cation exchange secondary water washing warehouses I-IV, and a connecting pipeline is arranged on the first supporting device so that the three cation exchange columns are connected in sequence, and the cation exchange column close to the cation exchange regeneration warehouse IV is connected to any cation exchange column in the cation exchange regeneration warehouse IV. Four cation exchange columns connected in parallel are evenly distributed in the secondary cation exchange warehouses I-III, and the first dilute alkali inlet DL1 is connected to the cation exchange column close to the cation exchange primary water washing warehouse II, and the first dilute hydrochloric acid inlet DHA1 is connected to the cation exchange column close to the cation exchange secondary water washing warehouse I-IV. By arranging multiple cation exchange columns in each chamber, it can be ensured that multiple cation exchange columns are simultaneously subjected to ion exchange, water washing and regeneration, thereby improving the extraction efficiency of erythritol.

[0039] During operation, each cation exchange column regularly passes through the cation exchange primary water washing tank II, the cation exchange regeneration tank IV, the cation exchange secondary water washing tank I-IV, the secondary cation exchange tank I-III, the primary cation exchange tank I-II, the cation exchange primary water washing tank II, etc. and performs corresponding work, and the cycle continues.

[0040] When continuous cation exchange is performed, when the conductivity of the effluent from the last cation exchange column (P4 position) of the primary cation exchange chamber I-II reaches 50-55 μs / cm, the first rotating chassis rotates, and the cation exchange column enters the cation exchange primary water washing chamber II (P3 position), and the other ion exchange columns move to the next position accordingly (in the direction of Pr to Pa). During the primary water washing, when the concentration of the effluent from the ion exchange column is higher than 0.5-1%, it flows back to the primary cation exchange chamber I-II, and when the concentration of the effluent is lower than 0.5-1%, it is discharged to the first wastewater outlet WWT1, and the water washing is stopped until the outlet water is clear;

[0041] When continuous cation exchange is performed, the cation exchange column needs to be regenerated. The ion exchange column (P18 position) that has been washed once and enters the cation exchange regeneration tank IV is first cleaned with 4-6% dilute alkali solution through the first dilute alkali inlet DL1, and then enters the next position (P17 position), and is regenerated by soaking in 4-6% dilute hydrochloric acid. Then, it enters the cation exchange secondary water washing tank I-IV, and is rinsed with pure water entering from the first pure water inlet DW1 until the outlet water is clear and the washing is stopped. The effluent from the cation exchange regeneration tank IV and the cation exchange secondary water washing tank I-IV are discharged through the second wastewater outlet WWT2.

[0042] refer to Figure 2 As an embodiment, three anion exchange columns are evenly distributed in the anion exchange primary washing chamber II-I, and a connecting pipeline is set on the first supporting device to connect the three anion exchange columns in sequence. Four anion exchange columns are evenly distributed in the anion exchange regeneration chamber II-V, and a connecting pipeline is set on the first supporting device to connect the four anion exchange columns in sequence. Three anion exchange columns are evenly distributed in the anion exchange secondary washing chamber II-IV, and a connecting pipeline is set on the first supporting device to connect the three anion exchange columns in sequence, and the anion exchange column close to the anion exchange regeneration chamber II-V is connected to the anion exchange column. Any anion exchange column in the anion exchange regeneration chamber II-V is connected, four anion exchange columns connected in parallel are evenly distributed in the secondary anion exchange chamber II-III, the second dilute alkali inlet DL2 is connected to the anion exchange column in the anion exchange secondary water washing chamber II-IV, and the second dilute hydrochloric acid inlet DHA2 is connected to the anion exchange column in the anion exchange primary water washing chamber II-I. By arranging multiple anion exchange columns in each chamber, it can be ensured that multiple anion exchange columns are ion exchanged, washed and regenerated at the same time, thereby improving the extraction efficiency of erythritol;

[0043] refer to Figure 1-2 As an implementation method, during operation, each anion exchange column regularly passes through the anion exchange primary water washing chamber II-I, the anion exchange regeneration chamber II-V, the anion exchange secondary water washing chamber II-IV, the secondary anion exchange chamber II-III, the primary anion exchange chamber II-II, the anion exchange primary water washing chamber II-I, etc. and performs corresponding work, and the cycle continues.

[0044] When continuous anion exchange is performed, when the conductivity of the effluent from the last anion exchange column (N4 position) of the primary anion exchange chamber II-II reaches 35-40 μs / cm, the second rotating chassis rotates, and the anion exchange column enters the anion exchange primary water washing chamber II-I (N3 position), and the other ion exchange columns move to the next position accordingly (according to the direction from Nr to Na). During the primary water washing, when the concentration of the effluent from the ion exchange column is higher than 0.5-1%, it flows back to the primary anion exchange chamber II-II, and when the concentration of the effluent is lower than 0.5-1%, it is discharged to the third wastewater outlet WWT3 until the outlet water is clear and the water washing is stopped;

[0045] When continuous anion exchange is performed, the anion exchange column needs to be regenerated. The ion exchange column (N18 position) that enters the anion exchange regeneration warehouse II-V after a water wash is firstly used to enter the cathode ion exchange column through the second dilute hydrochloric acid inlet DHA2 with 4-6% dilute hydrochloric acid, and the cathode ion exchange column is rinsed. Then the cathode ion exchange column enters the next position (N17 position), and 4-6% dilute alkali is used to enter the cathode ion exchange column through the second dilute alkali inlet DL2 for soaking and regeneration. The cathode ion exchange column then enters the anion exchange secondary water washing warehouse II-IV, and is rinsed with pure water entering through the second pure water inlet DW2 until the outlet water is clear and the water washing is stopped. The effluents of the anion exchange regeneration warehouse II-V and the anion exchange secondary water washing warehouse II-IV are discharged through the fourth wastewater outlet WWT4;

[0046] It should be noted that the first wastewater outlet WWT1, the second wastewater outlet WWT2, the third wastewater outlet WWT3, the fourth wastewater outlet WWT4 and the fifth wastewater outlet WWT5 are all connected to the wastewater tank.

[0047] refer to Figure 3 In one embodiment, the mixed bed ion exchange system includes a pre-bed bag filter III-I, a mixed bed ion exchange column III-II and a post-bed bag filter III-III which are connected in sequence. The mixed bed ion exchange column III-II is provided with a third wash water inlet FW3, a third pure water inlet DW3, a third dilute alkali inlet DL3, a third dilute hydrochloric acid inlet DHA3 and a fifth wastewater outlet WWT5. The post-bed bag filter III-III is provided with a fourth wash water inlet FW4 and a discharge port, and the discharge port is connected to the concentrator CTS. By sequentially arranging the pre-bed bag filter III-I, the mixed bed ion exchange column III-II and the post-bed bag filter III-III in the mixed field ion exchange system, the extraction effect of erythritol can be improved.

[0048] refer to Figure 3In one embodiment, the fifth wastewater outlet WWT5 is connected to the wastewater tank and the primary cation exchange tank I-II at the same time. By connecting the fifth wastewater outlet WWT5 to the primary cation exchange tank I-II, when the concentration of the flushing effluent is higher than 0.5-1%, the effluent is refluxed to the primary cation exchange tank I-II to avoid waste of raw materials.

[0049] refer to Figure 3 In one embodiment, the upper half of the mixed bed ion exchange column III-II is an anion exchange column, and the lower half of the mixed bed ion exchange column III-II is a cation exchange column;

[0050] When the mixed bed ion exchange is carried out, when the conductivity of the discharge port reaches 10-15 μs / cm, the ion exchange is terminated, and the resin in the mixed bed ion exchange column III-II is rinsed with water from the third washing water inlet FW3. When the concentration of the rinsing effluent is higher than 0.5-1%, the effluent is refluxed to the primary cation exchange tank I-II. When the concentration of the effluent is lower than 0.5-1%, it is discharged to the wastewater tank through the fifth wastewater outlet WWT5. After the water washing is completed, the cations in the mixed bed ion exchange column III-II are first washed with 4-6% dilute alkali through the third dilute alkali inlet DL3, and then regenerated with 4-6% dilute hydrochloric acid through the third dilute hydrochloric acid inlet DHA3, and finally washed with pure water entering through the third pure water inlet DW3. The anions are first washed with 4-6% dilute hydrochloric acid, and then regenerated with 4-6% dilute alkali, and finally washed with pure water until the outlet water is clear and the water washing is stopped. The regenerated and washed effluents are discharged through the fifth wastewater outlet WWT5.

[0051] refer to Figure 3 As an embodiment, the cation exchange column in the continuous cation system is exchange resin D001FD, the anion exchange column in the continuous anion exchange system is exchange resin D354FD, the anion exchange column in the mixed bed ion exchange system is exchange resin ZGA352, and the cation exchange column is exchange resin ZGA151.

[0052] refer to Figure 1-3 This embodiment also discloses an ion exchange method for desalting and deodorizing erythritol fermentation broth, comprising the following steps:

[0053] The erythritol fermentation liquid PL is sequentially passed into the primary cation exchange chamber I-II, the primary anion exchange chamber II-II, the secondary cation exchange chamber I-III, the secondary anion exchange chamber II-III and the mixed bed ion exchange system for continuous ion exchange;

[0054] The cation exchange column in the cation exchange bin is rotated to the cation exchange primary water washing bin II, the cation exchange regeneration bin IV, and the cation exchange secondary water washing bins I-IV in sequence for water washing and regeneration by rotating the first rotating chassis;

[0055] The anion exchange column in the anion exchange chamber is rotated to the anion exchange primary water washing chamber II-I, the anion exchange regeneration chamber II-V, and the anion exchange secondary water washing chamber II-IV in sequence through the rotation of the second rotating chassis for water washing and regeneration;

[0056] Washing and regenerating the mixed bed ion exchange column III-II;

[0057] The following is the treatment object: the erythritol fermentation liquid PL after preliminary filtration and decolorization, the concentration before treatment is 19.78%, the conductivity is 1273μs / cm, and the pH is 3.86. The specific operation steps are as follows:

[0058] The filtered and decolorized erythritol fermentation liquid PL transported from the ion exchange feed tank enters the four cation exchange columns of the primary cation exchange chambers I-II at a flow rate of 3 column volumes / h for primary cation exchange;

[0059] The effluent from the primary cation exchange chamber I-II is transported to the primary anion exchange chamber II-II for anion exchange, the effluent from the primary anion exchange chamber II-II is transported to the secondary cation exchange chamber I-III for cation exchange, the effluent from the secondary cation exchange chamber I-III is transported to the secondary anion exchange chamber II-III for anion exchange, the effluent from the secondary anion exchange chamber II-III is transported to the mixed bed ion exchange column III-II for mixed bed ion exchange, the effluent from the mixed bed ion exchange column III-II enters the post-bed bag filter III-III and enters the concentration device CTS for further treatment.

[0060] When continuous cation exchange is performed, when the conductivity of the effluent of the last cation exchange column of the primary cation exchange chamber I-II reaches 55 μs / cm, the ion exchange column group rotates, and the cation exchange column enters the cation exchange primary water washing chamber II, and the other ion exchange columns move to the next position accordingly. During the primary water washing, when the concentration of the effluent of the ion exchange column is higher than 1%, it flows back to the primary cation exchange chamber I-II, and when the concentration of the effluent is lower than 1%, it is discharged to the waste water tank. The ion exchange column entering the cation exchange regeneration chamber IV is first rinsed with 4% dilute alkali solution, and then enters the next position, is regenerated by soaking in 4% dilute hydrochloric acid, and then enters the cation exchange secondary water washing chamber I-IV, and is rinsed with pure water;

[0061] When continuous anion exchange is performed, when the conductivity of the effluent of the last anion exchange column of the primary anion exchange chamber II-II reaches 40 μs / cm, the anion exchange column group rotates, and this anion exchange column enters the anion exchange primary water washing chamber II-I, and other anion exchange columns move to the next position accordingly. During the primary water washing, when the concentration of the effluent of the ion exchange column is higher than 1%, it flows back to the primary cation exchange chamber I-II, and when the concentration of the effluent is lower than 1%, it is discharged to the waste water tank. The ion exchange column entering the anion exchange regeneration chamber II-V is first rinsed with 4% dilute hydrochloric acid, and then enters the next position, is regenerated by soaking in 4% dilute alkali, and then enters the anion exchange secondary water washing chamber II-IV, and is rinsed with pure water.

[0062] When continuous ion exchange is performed, the cation exchange column and the anion exchange column enter the secondary cation exchange tank I-III from the cation exchange secondary water washing tank I-IV and the secondary anion exchange tank II-III from the anion exchange secondary water washing tank II-IV respectively. The feed liquid first pushes out the water in the system. When the concentration of the effluent from the discharge port of the cation exchange column and the anion exchange column is lower than 10%, the effluent is refluxed to the primary cation exchange tank I-II. When the concentration of the effluent reaches 10%, the effluent runs according to the normal process.

[0063] When the mixed bed ion exchange is carried out, when the conductivity of the effluent reaches 15μs / cm, the ion exchange is terminated, and the resin is rinsed with water. When the concentration of the effluent is higher than 1%, the effluent is refluxed to the primary cation exchange tank I-II. When the concentration of the effluent is lower than 1%, it is discharged to the waste water tank. After the water washing is completed, the cation is firstly rinsed with 4% dilute alkali, then regenerated with 4% dilute hydrochloric acid, and finally rinsed with pure water. The anion is firstly rinsed with 4% dilute hydrochloric acid, then regenerated with 4% dilute alkali, and finally rinsed with pure water.

[0064] In this embodiment, after the erythritol fermentation liquid PL was treated with continuous cation exchange and continuous anion exchange, the conductivity dropped to 15.31μs / cm, the erythritol concentration was 19.10%, and the pH was 4.24. After mixed bed ion exchange, the conductivity of the fermentation liquid dropped to 7.32μs / cm, the erythritol concentration was 18.21%, and the pH was 5.02. In this example, the ion exchange operation time was saved by about 40% compared with the conventional method, the amount of washing water was saved by about 35%, the consumption of regeneration agent was reduced by 30%, the amount of waste liquid generated was reduced by about 33%, and the final total extraction yield of pure erythritol reached more than 93%, the purity reached more than 99.9%, and the product had no odor.

[0065] The following is the treatment object: the erythritol fermentation liquid PL after preliminary filtration and decolorization, the concentration before treatment is 15.63%, the conductivity is 1089μs / cm, and the pH is 3.97. The specific operation steps are as follows:

[0066] The filtered and decolorized erythritol fermentation liquid PL transported from the ion exchange feed tank enters the four cation exchange columns of the primary cation exchange chambers I-II at a flow rate of 2 column volumes / h for primary cation exchange.

[0067] The effluent discharged from the primary cation exchange warehouse I-II is transported to the primary anion exchange warehouse II-II for anion exchange, the effluent discharged from the primary anion exchange warehouse II-II is transported to the secondary cation exchange warehouse I-III for cation exchange, the effluent discharged from the secondary cation exchange warehouse I-III is transported to the secondary anion exchange warehouse II-III for anion exchange, the effluent discharged from the secondary anion exchange warehouse II-III is transported to the mixed bed ion exchange column III-II for mixed bed ion exchange, and the effluent discharged from the mixed bed ion exchange column III-II enters the next warehouse for further treatment;

[0068] When cation exchange is performed, when the conductivity of the effluent of the last cation exchange column of the primary cation exchange chamber I-II reaches 50 μs / cm, the ion exchange column group rotates, and this exchange column enters the cation exchange primary water washing chamber II, and the other ion exchange columns move to the next position accordingly. During the primary water washing, when the concentration of the effluent of the ion exchange column is higher than 0.5%, it is refluxed to the primary cation exchange chamber I-II, and when the concentration of the effluent is lower than 0.5%, it is discharged to the waste water tank;

[0069] When anion exchange is performed, when the conductivity of the effluent of the last anion exchange column of the primary anion exchange chamber II-II reaches 35μs / cm, the ion exchange column group rotates, and this exchange column enters the anion exchange primary water washing chamber II-I, and the other ion exchange columns move to the next position accordingly. During the primary water washing, when the concentration of the effluent of the ion exchange column is higher than 0.5%, it flows back to the primary cation exchange chamber I-II, and when the concentration of the effluent is lower than 0.5%, it is discharged to the wastewater tank.

[0070] When continuous cation exchange is performed, the cation exchange column needs to be regenerated. The ion exchange column entering the cation exchange regeneration bin IV is first rinsed with a 6% dilute alkali solution, and then enters the next position and is regenerated by soaking in 6% dilute hydrochloric acid, and then enters the cation exchange secondary water washing bin I-IV and is rinsed with pure water. The effluent from the cation exchange regeneration bin IV and the cation exchange secondary water washing bin I-IV are discharged to the wastewater tank.

[0071] When continuous anion exchange is performed, the anion exchange column needs to be regenerated. The ion exchange column entering the anion exchange regeneration chamber II-V is first rinsed with 6% dilute hydrochloric acid, then enters the next position, and is regenerated by soaking with 6% dilute alkali, and then enters the anion exchange secondary water washing chamber II-IV and is rinsed with pure water;

[0072] When continuous ion exchange is performed, the cation exchange column and the anion exchange column enter the secondary cation exchange tank I-III from the cation exchange secondary water washing tank I-IV and the secondary anion exchange tank II-III from the anion exchange secondary water washing tank II-IV respectively, and the feed liquid first pushes out the water in the system. When the concentration of the effluent from the discharge port of the cation exchange column and the anion exchange column is lower than 8%, the effluent is refluxed to the primary cation exchange tank I-II. When the concentration of the effluent reaches 8%, the effluent runs according to the normal process;

[0073] When the ion exchange of mixed bed is carried out, when the conductivity of the effluent reaches 10μs / cm, the ion exchange is terminated and the resin is rinsed with water. When the concentration of the effluent is higher than 0.5%, the effluent is refluxed to the primary cation exchange tank I-II, and the effluent concentration is lower than 0.5% and discharged to the waste water tank. After the water washing is completed, the cation is first rinsed with 6% dilute alkali, then regenerated with 6% dilute hydrochloric acid, and finally rinsed with pure water; the anion is first rinsed with 6% dilute hydrochloric acid, then regenerated with 6% dilute alkali, and finally rinsed with pure water;

[0074] In this example, after the erythritol fermentation broth PL was treated with continuous cation exchange and continuous anion exchange, the conductivity dropped to 13.69 μs / cm, the erythritol concentration was 15.05%, and the pH was 4.58. After mixed bed ion exchange, the conductivity of the fermentation broth dropped to 3.80 μs / cm, the erythritol concentration was 14.31%, and the pH was 5.32. In this example, the ion exchange operation time was saved by about 42% compared with the conventional method, the amount of washing water was saved by about 35%, the consumption of regeneration agent was reduced by 32%, and the amount of waste liquid generated was reduced by about 34%. Finally, the total extraction yield of pure erythritol reached more than 94%, the purity reached more than 99.9%, and the product had no odor.

[0075] Adaptive changes made according to actual needs are all within the protection scope of the present invention.

[0076] It should be noted that it is obvious to those skilled in the art that the present invention is not limited to the details of the exemplary embodiments described above, and that the present invention can be implemented in other specific forms without departing from the spirit or essential features of the present invention. Therefore, the embodiments should be regarded as exemplary and non-restrictive from any point of view, and the scope of the present invention is defined by the appended claims rather than the above description, and it is intended that all changes falling within the meaning and scope of the equivalent elements of the claims are included in the invention. Any reference numeral in a claim should not be regarded as limiting the claim to which it relates.

Claims

1. An ion exchange device for desalting and deodorizing erythritol fermentation liquid, characterized in that: Including continuous cation exchange system, continuous anion exchange system and mixed bed ion exchange system; The cation exchange system includes a primary cation exchange tank and a secondary cation exchange tank connected to the erythritol fermentation liquid, and the primary cation exchange tank and the secondary cation exchange tank are both provided with cation exchange columns, and the continuous anion exchange system includes a primary anion exchange tank and a secondary anion exchange tank, both of which are provided with anion exchange columns; The primary cation exchange chamber, the primary anion exchange chamber, the secondary cation exchange chamber, the secondary anion exchange chamber and the mixed bed ion exchange system are connected in sequence.

2. The ion exchange device for desalting and deodorizing erythritol fermentation liquid according to claim 1, characterized in that: The continuous cation exchange system also includes a cylindrical first supporting device, a first rotating chassis arranged at the bottom of the first supporting device, and a cation exchange primary water washing tank, a cation exchange regeneration tank, a cation exchange secondary water washing tank, the secondary cation exchange tank and the primary cation exchange tank arranged in sequence on the first rotating chassis in a cylindrical shape, wherein the cation exchange primary water washing tank, the cation exchange regeneration tank and the cation exchange secondary water washing tank are all provided with cation exchange columns, the first supporting device is provided with a first wash water inlet and a first waste water outlet communicating with the cation exchange column in the cation exchange primary water washing tank at the location corresponding to the cation exchange primary water washing tank, the first supporting device is provided with a first dilute alkali inlet, a first dilute hydrochloric acid inlet and a second waste water outlet communicating with the cation exchange column in the cation exchange regeneration tank at the location corresponding to the cation exchange regeneration tank, the first supporting device is provided with a first pure water inlet communicating with the cation exchange column in the cation exchange secondary water washing tank at the location corresponding to the cation exchange secondary water washing tank, and the first supporting device is provided with an erythritol fermentation liquid inlet communicating with the cation exchange column in the primary cation exchange tank at the location corresponding to the primary cation exchange tank.

3. The ion exchange device for desalting and deodorizing erythritol fermentation liquid according to claim 1, characterized in that: The continuous anion exchange system includes a cylindrical second supporting device, a second rotating chassis arranged at the bottom of the second supporting device, and an anion exchange primary water washing tank, an anion exchange regeneration tank, an anion exchange secondary water washing tank, the secondary anion exchange tank and the primary anion exchange tank arranged in sequence on the second rotating chassis in a cylindrical shape, anion exchange primary water washing tank, anion exchange regeneration tank and anion exchange secondary water washing tank are all provided with anion exchange columns, the second supporting device is provided with a second wash water inlet and a third waste water outlet connected to the anion exchange column in the anion exchange primary water washing tank corresponding to the anion exchange primary water washing tank, the second supporting device is provided with a second dilute alkali inlet, a second dilute hydrochloric acid inlet and a fourth waste water outlet connected to the anion exchange column in the anion exchange regeneration tank corresponding to the anion exchange regeneration tank, and the second supporting device is provided with a second pure water inlet connected to the anion exchange column in the anion exchange secondary water washing tank corresponding to the anion exchange secondary water washing tank.

4. The ion exchange device for desalting and deodorizing erythritol fermentation liquid according to claim 2, characterized in that: Three cation exchange columns are evenly distributed in the cation exchange primary water washing bin, and a connecting pipeline is arranged on the first supporting device so that the three cation exchange columns are connected in sequence. Four cation exchange columns are evenly distributed in the cation exchange regeneration bin, and a connecting pipeline is arranged on the first supporting device so that the four cation exchange columns are connected in sequence. Three cation exchange columns are evenly distributed in the cation secondary water washing bin, and a connecting pipeline is arranged on the first supporting device so that the three cation exchange columns are connected in sequence, and the cation exchange column close to the cation exchange regeneration bin is connected to any one of the cation exchange columns in the cation exchange regeneration bin. Four cation exchange columns connected in parallel are evenly distributed in the secondary cation exchange bin, and the first dilute alkali inlet is connected to the cation exchange column close to the cation exchange primary water washing bin, and the first dilute hydrochloric acid inlet is connected to the cation exchange column close to the cation exchange secondary water washing bin.

5. The ion exchange device for desalting and deodorizing erythritol fermentation liquid according to claim 3, characterized in that: Three anion exchange columns are evenly distributed in the anion exchange primary water washing tank, and a connecting pipeline is arranged on the first supporting device so that the three anion exchange columns are connected in sequence. Four anion exchange columns are evenly distributed in the anion exchange regeneration tank, and a connecting pipeline is arranged on the first supporting device so that the four anion exchange columns are connected in sequence. Three anion exchange columns are evenly distributed in the anion secondary water washing tank, and a connecting pipeline is arranged on the first supporting device so that the three anion exchange columns are connected in sequence, and the anion exchange column close to the anion exchange regeneration tank is connected to any one of the anion exchange columns in the anion exchange regeneration tank. Four anion exchange columns connected in parallel are evenly distributed in the secondary anion exchange tank, and the second dilute alkali inlet is connected to the anion exchange column close to the anion exchange secondary water washing tank, and the second dilute hydrochloric acid inlet is connected to the anion exchange column close to the anion exchange primary water washing tank.

6. The ion exchange device for desalting and deodorizing erythritol fermentation liquid according to claim 1, characterized in that: The mixed bed ion exchange system comprises a pre-bed bag filter, a mixed bed ion exchange column and a post-bed bag filter which are connected in sequence. The mixed bed ion exchange column is provided with a third wash water inlet, a third pure water inlet, a third dilute alkali inlet, a third dilute hydrochloric acid inlet and a fifth waste water outlet. The post-bed bag filter is provided with a fourth wash water inlet and a discharge port, and the discharge port is connected to a concentration device.

7. The ion exchange device for desalting and deodorizing erythritol fermentation liquid according to claim 6, characterized in that: The fifth wastewater outlet is connected to the wastewater tank and the primary cation exchange tank at the same time.

8. The ion exchange device for desalting and deodorizing erythritol fermentation liquid according to claim 6, characterized in that: The upper part of the mixed bed ion exchange column is an anion exchange column, and the lower part of the mixed bed ion exchange column is a cation exchange column.

9. The ion exchange device for desalting and deodorizing erythritol fermentation liquid according to claim 1, characterized in that: The cation exchange column is an exchange resin D001FD, and the anion exchange column is an exchange resin D354FD.

10. An ion exchange method for desalting and deodorizing erythritol fermentation broth, characterized in that: The following steps are involved: The erythritol fermentation liquid is sequentially passed into a primary cation exchange tank, a primary anion exchange tank, a secondary cation exchange tank, a secondary anion exchange tank and a mixed bed ion exchange system for continuous ion exchange; The cation exchange column in the cation exchange bin is rotated to the cation exchange primary water washing bin, the cation exchange regeneration bin, and the cation exchange secondary water washing bin in sequence through the rotation of the first rotating chassis for water washing and regeneration; The anion exchange column in the anion exchange chamber is rotated to the anion exchange primary water washing chamber, the anion exchange regeneration chamber, and the anion exchange secondary water washing chamber in sequence through the rotation of the second rotating chassis for water washing and regeneration; The mixed bed ion exchange column is washed and regenerated.

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