A fructose production inter-ion feeding device

Abstract

This application discloses a ion exchange feed device for fructose production, relating to the field of ion exchange technology in fructose production. It includes at least two sets of ion exchange column groups arranged in parallel, each group consisting of a cation exchange resin column and an anion exchange resin column connected in series. The feed end of each ion exchange column group is connected to a multi-port distributor, which is connected to a main feed pipe. The discharge end of each ion exchange column group is connected to a converging pipe, which is connected to a main discharge pipe. This application solves the technical problems of high resin breakage rate, high operating pressure, and frequent regeneration inherent in traditional single-column or series operation modes by redesigning the operating structure and flow control structure of the ion exchange column groups, significantly reducing production costs and improving production stability.

Description

Technical Field

[0001] This application relates to the field of fructose production ion exchange technology, for example, to an ion exchange feeding device for fructose production. Background Technology

[0002] In the fructose production process, ion exchange is one of the core steps. Its function is to adsorb impurities (such as ash, pigments, proteins, etc.) in the sugar solution through cation and anion resins to ensure that the final product meets quality standards.

[0003] Traditional inter-channel commutation (ICC) processes mainly employ the following two operating modes: Single-column operation: cation exchange resin column is used for feeding and anion exchange resin column is used for discharging. Although the operation is simple, it has the problems of high protein content and high viscosity in the discharging material, which leads to subsequent clumping of isomerases and increased operating pressure of the chromatographic resin due to protein adsorption, resulting in a decrease in separation efficiency.

[0004] Series dual-column operation: Two sets of ion-exchange columns are connected in series to improve the processing capacity. However, this method requires maintaining a total flow rate of 55 m³ / h, which significantly increases the anion resin breakage rate, causes frequent water cap clogging, increases the number of regenerations, and results in drastic fluctuations in the discharge pH. Frequent adjustments to the flow rate of the heterogeneous section are required, which seriously affects the continuity of production.

[0005] Furthermore, in existing technologies, the resin filling volume of the ion exchange device is large (usually exceeding 36 cubic meters), the consumption of regenerated liquid is high, and there is a lack of real-time flow control and pH monitoring methods, resulting in high operating costs.

[0006] Therefore, there is an urgent need for a material feeding device that can reduce resin loss, optimize flow distribution, and reduce regeneration frequency. Utility Model Content

[0007] To provide a basic understanding of some aspects of the disclosed embodiments, a brief summary is given below. This summary is not intended as a general commentary, nor is it intended to identify key / important components or describe the scope of protection of these embodiments, but rather as a prelude to the detailed description that follows.

[0008] To address the aforementioned technical problems, this application provides an ion exchange feeding device for fructose production. This ion exchange feeding device for fructose production solves the technical problems of high resin breakage rate, high operating pressure, and frequent regeneration in traditional single-column or series operation modes by redesigning the operating structure and flow control structure of the ion exchange column group, thereby significantly reducing production costs and improving production stability.

[0009] This application provides a fructose production ion exchange feeding device, comprising at least two sets of ion exchange column groups arranged in parallel, each set of ion exchange column groups consisting of a cation resin column and an anion resin column connected in series; the feed end of the ion exchange column group is connected to a multi-port distributor, the multi-port distributor being connected to a main feed pipe; the discharge end of the ion exchange column group is connected to a collection pipe, the collection pipe being connected to a main discharge pipe.

[0010] In a further improvement of this utility model, a feed flow meter is installed on the feed branch pipe of each group of inter-column groups.

[0011] In a further improvement of this utility model, a regulating valve is provided on the feed branch pipe of each group of inter-column groups.

[0012] In a further improvement of this utility model, the water inlet end of the cation resin column is provided with an anti-clogging water cap structure, and the aperture of the anti-clogging water cap structure is 0.1-0.3mm.

[0013] In a further improvement of this utility model, the total flow rate of the main feed pipe is set to 55 m³ / h, and is evenly distributed to each parallel decoupling column group through a multi-channel distributor.

[0014] In a further improvement of this invention, a pH sensor is installed at the discharge end of the anion resin column.

[0015] In a further improvement of this invention, the resin filling amount of both the cation and anion resin columns does not exceed 36 cubic meters.

[0016] In a further improvement of this invention, the discharge pressure of each discharge branch pipe of the multi-channel distributor is no higher than 3 kg.

[0017] In a further improvement of this invention, the device also includes a regenerated liquid circulation system, which is connected to each ion exchange column group.

[0018] Compared with the prior art, this application has the following beneficial effects: This application solves the technical problems of high resin breakage rate, high operating pressure and frequent regeneration in traditional single column or series operation by redesigning the operation structure and flow control structure of the ion exchange column group, which significantly reduces production costs and improves production stability.

[0019] The above general description and the description below are exemplary and illustrative only and are not intended to limit this application. Attached Figure Description

[0020] To more clearly illustrate the background technology or the technical solution of this application, the accompanying drawings used in conjunction with the prior art or specific embodiments are briefly introduced below. Obviously, the structures, proportions, sizes, etc. shown in the drawings are only used to complement the content disclosed in the specification, so that those skilled in the art can understand and read them, and are not intended to limit the conditions under which this application can be implemented. Therefore, they have no substantial technical significance. Any modification to the structure, change in the proportional relationship, or adjustment of the size should still fall within the scope of the technical content disclosed in this application, provided that it does not affect the effects and purposes that this application can produce.

[0021] Figure 1 This is a structural diagram illustrating a specific embodiment of this application.

[0022] The diagram shows: 1. Cation resin column; 2. Anion resin column; 3. Multi-port distributor; 4. Main feed pipe; 5. Combined feed line; 6. Main discharge pipe; 7. Feed flow meter; 8. Control valve. Detailed Implementation

[0023] To gain a more detailed understanding of the features and technical content of the embodiments of this application, the implementation of the embodiments of this application will be described in detail below with reference to the accompanying drawings. The accompanying drawings are for reference only and are not intended to limit the embodiments of this application. In the following technical description, for ease of explanation, multiple details are used to provide a full understanding of the disclosed embodiments. However, one or more embodiments may still be implemented without these details. In other cases, well-known structures and devices may be simplified in order to simplify the drawings.

[0024] The terms “first”, “second”, etc., used in the embodiments of this application are used to distinguish similar objects and are not necessarily used to describe a specific order or sequence; it should be understood that such data used can be interchanged where appropriate so as to be the embodiments of the present application described herein; furthermore, the terms “comprising” and “having”, and any variations thereof, are intended to cover non-exclusive inclusion.

[0025] In the embodiments of this application, the terms "upper," "lower," "inner," "middle," "outer," "front," and "rear," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. These terms are mainly for better describing the embodiments of this application and their implementations, and are not intended to limit the indicated device, element, or component to having a specific orientation, or to be constructed and operated in a specific orientation. Furthermore, in addition to indicating orientation or positional relationship, some of the above terms may also be used to indicate other meanings. For example, the term "upper" may also be used in some cases to indicate a certain dependency or connection relationship. For those skilled in the art, the specific meaning of these terms in the embodiments of this application can be understood according to the specific circumstances.

[0026] In addition, the terms “set up,” “connect,” and “fix” should be interpreted broadly. For example, “connection” can be a fixed connection, a detachable connection, or an integral structure; it can be a mechanical connection or an electrical connection; it can be a direct connection or an indirect connection through an intermediate medium, or an internal connection between two devices, components, or components. For those skilled in the art, the specific meaning of the above terms in the embodiments of this application can be understood according to the specific circumstances.

[0027] Unless otherwise stated, the term "multiple" means two or more.

[0028] In this embodiment of the application, the character " / " indicates that the objects before and after are in an "or" relationship. For example, Z / X means: Z or X. The term "and / or" describes the relationship between objects, indicating that there can be three relationships. For example, Z and / or X means: Z or X, or Z and X.

[0029] It should be noted that, unless otherwise specified, the embodiments and features described in the embodiments of this application can be combined with each other.

[0030] Traditional inter-channel commutation (ICC) processes mainly employ the following two operating modes: Single-column operation: cation exchange resin column feed, anion exchange resin column discharge. Although simple to operate, it has the problems of high protein content and high viscosity in the discharge, which leads to subsequent isomerase clumping, increased operating pressure of the chromatographic resin due to protein adsorption, and decreased separation efficiency, affecting the stability of production operation and production costs.

[0031] Series dual-column operation: Two sets of ion-exchange columns are connected in series to improve processing capacity. However, this method requires maintaining a total flow rate of 55 m³ / h, which significantly increases the anion resin breakage rate, causes frequent blockage of the cation column water cap, and results in high feed pressure (4 kg). The feed rate is reduced and cannot meet the production operation requirements. It is difficult to ensure stable production operation when the ion-exchange column is replaced. The discharge pH is low, and normal discharge cannot be achieved for 30 minutes. This has a severe impact on the heterogeneous feed rate. The feed pH adjustment fluctuates too much, requiring a reduction in the heterogeneous flow rate while waiting for the ion-exchange column to discharge. The ion-exchange feed rate cannot be adjusted according to the indicators, resulting in no improvement in the ion-exchange flow rate, faster failure, more frequent regeneration, larger sweet water volume, and higher costs for acid and alkali, water, sewage, electricity, and steam.

[0032] Furthermore, in existing technologies, the resin filling volume of the ion exchange device is large (usually exceeding 36 cubic meters), the consumption of regenerated liquid is high, and there is a lack of real-time flow control and pH monitoring methods, resulting in high operating costs.

[0033] Therefore, there is an urgent need for a material feeding device that can reduce resin loss, optimize flow distribution, and reduce regeneration frequency.

[0034] The design concept of this application is to redesign the crosslinking structure, adopt two sets of parallel operation, reduce the feed flow rate of a single set, adjust the total flow rate of 55m³ / h to 25-30m³ / h for a single set, and reasonably adjust the feed flow rate of a single set according to the output index to achieve the maximum efficiency of the crosslinking column resin operation. The reduced feed flow rate reduces the resin yield, the increased material flow reduces the regeneration frequency, and the production cost is reduced.

[0035] like Figure 1 As shown, this application provides a fructose production ion exchange feeding device, including at least two sets of ion exchange column groups arranged in parallel. Each ion exchange column group consists of a cation resin column 1 and an anion resin column 2 connected in series. The feed end of the ion exchange column group is connected to a multi-port distributor 3, and the multi-port distributor 3 is connected to a main feed pipe 4. The discharge end of the ion exchange column group is connected to a collection pipe 5, and the collection pipe 5 is connected to a main discharge pipe 6, realizing parallel diversion and independent control of materials. The ion exchange column group adopts a modular design concept, and the quick-connect flanges enable quick replacement and maintenance of each component.

[0036] It is understandable that by reducing the flow rate of a single unit (25-30 m³ / h) through parallel diversion, the breakage rate of resin caused by high flow rate impact can be reduced; the overall processing capacity of the unit can be improved, production interruption caused by single column failure can be avoided, and continuity can be ensured.

[0037] Each set of feed branch pipes of the column group is equipped with a DN100 diameter feed flow meter 7, which is used to monitor the feed flow of a single group in real time and provide visual feedback through its display instrument.

[0038] Understandably, real-time monitoring of individual flow rates helps prevent mechanical damage to the resin caused by exceeding flow limits; visualized data facilitates quick adjustments by operators, improving operational stability.

[0039] Each set of feed branch pipes of the column group is equipped with a regulating valve 8 (manual type). The manual regulating valve is linked with the feed flow meter 7 and is used to dynamically adjust the feed flow of a single set to 25-30m³ / h.

[0040] Understandably, precise control of the flow rate of a single unit is necessary to avoid resin breakage or blockage caused by flow fluctuations; and flexible adjustments should be made based on the output indicators to optimize resin adsorption efficiency.

[0041] The cation resin column 1 is provided with an anti-clogging water cap structure at its water inlet end. The pore size of the anti-clogging water cap structure is 0.1-0.3mm, which matches the resin particle size to reduce the resin breakage rate and the risk of clogging.

[0042] Understandably, effectively intercepting broken resin particles reduces the risk of water cap clogging by more than 70%; it also extends the service life of the water cap and reduces the frequency of downtime for cleaning.

[0043] The total flow rate of the main feed pipe 4 is set to 55 m³ / h, and is evenly distributed to each parallel decoupling column group through the multi-channel distributor 3.

[0044] Understandably, this is to avoid uneven flow distribution that could lead to localized resin overload; and to ensure consistent load across all groups to improve overall operating efficiency.

[0045] The anion resin column 2 is equipped with a pH sensor at its discharge end. The pH sensor is connected to the central control system of the workshop and is used to monitor the discharge pH value in real time and adjust the feed flow rate accordingly.

[0046] Understandably, real-time monitoring of the discharge pH value can prevent subsequent processes from shutting down due to excessively low pH; and by adjusting the feed flow rate or triggering regeneration through feedback, manual intervention can be reduced and the level of automation improved.

[0047] The resin filling amount of both the cation resin column 1 and the anion resin column 2 does not exceed 36 cubic meters, in order to reduce resin consumption and regeneration frequency.

[0048] Understandably, reducing the initial resin purchase cost and the amount of regenerated liquid consumed, and lowering the regeneration frequency, can save approximately 30% of acid and alkali costs annually.

[0049] The discharge pressure of each discharge branch pipe of the multi-channel distributor 3 is not higher than 3 kg, and the single-column operating pressure is reduced by parallel diversion.

[0050] Understandably, reducing the pressure on a single column by diverting the flow can prevent resin compaction or breakage caused by high pressure, extend the service life of the cross-linked column, and reduce maintenance costs.

[0051] The device also includes a regenerated liquid circulation system, which is connected to each ion exchange column group. The regenerated liquid circulation system includes a regenerated liquid storage tank, a pump connected to each ion exchange column group, and a waste liquid recovery tank connected to each ion exchange column group. The injection and recovery of regenerated liquid (such as hydrochloric acid and sodium hydroxide) are controlled by an automated program, reducing acid and alkali consumption by more than 30%.

[0052] Understandably, achieving automated recycling of regenerated liquid reduces acid and alkali waste by about 40%, lowers sewage discharge and environmental treatment costs, and meets the requirements of green production.

[0053] The DX and FX exfoliating columns are divided into three groups (A, B, and C), totaling six groups. Each group is equipped with a separate feed flow meter (DN100) for online display. A manual valve is added for flow adjustment. The operation mode is changed from series operation to two groups in parallel operation, reducing the feed flow rate of a single group from a total flow rate of 55 m³ / h to 25-30 m³ / h per group. The feed flow rate of each group is adjusted reasonably according to the discharge indicators to achieve the maximum efficiency of the exfoliating column resin operation. The reduced feed flow rate reduces the resin yield, while the increased material flow rate reduces the regeneration frequency and lowers production costs.

[0054] Trial run results: 1. The estimated material flow rate for each DX separation unit is 1500-1700m³, and for the tandem column operation it is 1100-1300m³. 2. The estimated material flow rate for each FX-type derailleur is 1800-2000 m³, and for the column-connected type it is 1300-1500 m³. 3. By reducing the amount of resin purchased based on the breakage of the anion resin, the amount of cation resin and anion resin can be reduced by 36 cubic meters.

[0055] This application replaces the traditional series-connected ion exchange column group with a parallel structure and adds a DN100 feed flow meter, a manual regulating valve, and an anti-clogging water cap (the inlet end of the cation resin column uses an anti-clogging water cap with a 0.2mm orifice). This allows for precise control of the flow rate of a single group to 25-30 m³ / h (the total feed flow rate is distributed to the three parallel ion exchange column groups through a multi-channel distributor, and the flow rate of each group is adjusted to 25-30 m³ / h by a manual regulating valve combined with a flow meter). This device can significantly reduce the resin breakage rate and clogging risk, increase the single-group feed rate to 1500-2000 m³, reduce the frequency of regeneration and the costs of acid, alkali, and water consumption, and ensure production continuity and stability through real-time pH monitoring (the pH sensor at the outlet end provides real-time feedback to the control system for dynamic adjustment).

[0056] This invention achieves the following technical effects through parallel operation, precise flow control, anti-clogging water caps, and pH monitoring: Resin breakage rate reduced by 50%, water cap clogging frequency reduced by 70%; The regeneration frequency has been reduced from 4 times per day to 2 times per day, saving approximately 1.2 million yuan in acid and alkali costs annually. Improved discharge pH stability and reduced downtime in the heterogeneous processing section by 80%; Modular design reduces maintenance time to less than 30 minutes, ensuring production continuity.

[0057] The foregoing description and accompanying drawings fully illustrate embodiments of this application to enable those skilled in the art to practice them. Other embodiments may include structural and other changes. The embodiments represent only possible variations. Unless explicitly required, individual components and functions are optional, and the order of operation may vary. Some parts and features of some embodiments may be included or replace parts and features of other embodiments. The embodiments of this application are not limited to the structures described above and shown in the accompanying drawings, and various modifications and changes may be made without departing from their scope. The scope of this application is limited only by the appended claims.

Claims

1. A fructose production centrifugal feeding device, characterized in that, It includes at least two sets of parallel-connected ion exchange column groups, each set consisting of a cation resin column and an anion resin column connected in series; the feed end of the ion exchange column group is connected to a multi-port distributor, the multi-port distributor is connected to a main feed pipe; the discharge end of the ion exchange column group is connected to a collection pipe, the collection pipe is connected to a main discharge pipe.

2. The fructose production centrifugal feeding device according to claim 1, characterized in that, Each feed branch pipe of the column group is equipped with a feed flow meter.

3. The fructose production centrifugal feeding device according to claim 1, characterized in that, Each feed branch pipe of the column group is equipped with a regulating valve.

4. The fructose production centrifugal feeding device according to claim 1, characterized in that, The inlet end of the cation resin column is equipped with an anti-clogging water cap structure, and the aperture of the anti-clogging water cap structure is 0.1-0.3mm.

5. The fructose production centrifugal feeding device according to claim 1, characterized in that, The total flow rate of the main feed pipe is set to 55 m³ / h, and is evenly distributed to each parallel decoupling column group through a multi-channel distributor.

6. The fructose production centrifugal feeding device according to claim 1, characterized in that, A pH sensor is installed at the outlet end of the anion resin column.

7. The fructose production centrifugal feeding device according to claim 1, characterized in that, The resin filling amount of both the cation and anion resin columns does not exceed 36 cubic meters.

8. The fructose production centrifugal feeding device according to claim 1, characterized in that, The discharge pressure of each discharge branch pipe of the multi-channel distributor shall not exceed 3 kg.

9. The fructose production centrifugal feeding device according to claim 1, characterized in that, The device also includes a regenerated liquid circulation system, which is connected to each ion exchange column group.

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