Device for improving continuous separation of glucose and fructose by simulated moving bed

Abstract

The invention discloses a device for improving continuous separation of glucose and fructose by a simulated moving bed, and relates to the technical field of organic compound separation. The problem that in the prior art, glucose and fructose are separated is solved. The device specifically comprises an upstream storage tank module, an upstream rotary joint module, a separation module, a downstream rotary joint module, a downstream storage tank module and an inert gas supply module, and the upstream storage tank module, the upstream rotary joint module, the separation module, the downstream rotary joint module, the downstream storage tank module and the inert gas supply module are operated in parallel. According to the present invention, the resin mounted in the column is kept in a semi-dry state to eliminate the displacement zone of the traditional chromatography operation process, while reducing the consumption of the resin, the feed solution is separated into pure liquid glucose and pure liquid fructose at a yield of 100%, while reducing the consumption of water for washing and dewatering, thereby reducing the production cost. Therefore, the dry solid% concentration of the product and the by-product is improved.

Description

Technical Field

[0001] This invention relates to the field of organic compound separation technology, and more particularly to an apparatus for improving the continuous separation of glucose and fructose using a simulated moving bed. Background Technology

[0002] Currently, the method for separating a mixture of glucose and fructose solutions involves feeding the feed solution through a cation exchange column, followed by elution with deionized water to remove dissolved components, thus achieving separation. As taught in US patents US3044904A, US4472203A, US24807A, and Japanese patent JPH064179U, as well as many other unlisted disclosures, single-bed chromatography is invariably the mechanical basis for obtaining purification, and similar mass transfer mechanisms are used in these publications. While column chromatography has long been recognized as standard equipment due to the development of various methods and processes based on mass transfer mechanisms in chromatography, it still encompasses its inherent drawbacks. To further improve purification equipment for glucose and fructose with lower resin and eluent consumption and higher concentrations and purity, effective improvements have not yet been achieved. These fundamental mass transfer mechanism defects are multifaceted and interconnected, including: 1) Low resin utilization efficiency, with mass transfer occurring only at the very front of the mass transfer zone, leaving the resin idle in the preceding and following portions. 2) Excessive dilution due to the presence of a displacement zone in the column process increases cycle time, leading to even less efficient resin use. 3) Engineering defects that impair component purification during column processing, such as flow kinetics: axial dispersion and diffusion effects of the feed solution affect separation quality, including backmixing effects at the column inlet and outlet; column geometry: end-effector effects including dead volume; feed volume limitations: avoiding broadening, overlap, and tailing between separation peaks caused by flow kinetics. 4) Requires longer cycle times, further reducing the economical consumption of resin and eluent, exacerbating the aforementioned engineering defects. 5) High pressure drop and difficult maintenance.

[0003] With the development and application of the improved simulated moving bed (SMB) method, it has been found to be far superior to single fixed bed processes in terms of resin consumption, operating efficiency, product yield, and quality. Therefore, it has been adopted as the standard industrial process by the vast majority of manufacturers. However, this method is limited by the use of chromatography, attempting to manipulate column configuration and optimize fluid distribution, where it still inherits the aforementioned inherent drawbacks of column chromatography. In view of the aforementioned shortcomings of using chromatography to separate glucose and fructose, we propose an improved apparatus for the continuous separation of glucose and fructose using a simulated moving bed. Summary of the Invention

[0004] The purpose of this invention is to address the shortcomings of existing technologies by proposing an improved apparatus for the continuous separation of glucose and fructose in a simulated moving bed.

[0005] To achieve the above objectives, the present invention adopts the following technical solution:

[0006] An apparatus for improving the continuous separation of glucose and fructose in a simulated moving bed includes an upstream storage tank module, an upstream rotary joint module, a separation module, a downstream rotary joint module, a downstream storage tank module, and an inert gas supply module, wherein the upstream storage tank module, upstream rotary joint module, separation module, downstream rotary joint module, downstream storage tank module, and inert gas supply module operate in parallel.

[0007] The upstream storage tank module includes multiple insulating jackets and an upper storage tank disposed inside the insulating jackets;

[0008] The upstream rotary joint module includes a circular multi-valve body I driven by a servo motor I, multiple storage containers disposed on the top surface of the circular multi-valve body I, and multiple liquid outlet conduits disposed on the bottom surface of the circular multi-valve body I;

[0009] The separation module includes multiple integral units disposed inside the sandwich sleeve and multiple columns disposed inside the integral units;

[0010] The downstream rotary joint module includes a circular multi-valve body II driven by a servo motor II, multiple transfer containers disposed on the top surface of the circular multi-valve body II, and multiple output conduits disposed on the bottom surface of the circular multi-valve body II.

[0011] The downstream storage tank module includes multiple hollow sleeves and a lower storage tank disposed inside the hollow sleeves;

[0012] The inert gas supply module includes a closed vacuum environment loop, an upstream wide-range inert gas supply loop, and a downstream wide-range inert gas supply loop connected in sequence to form a closed loop; the inert gas is one or a mixture of two or more of nitrogen, carbon dioxide, and argon; the wide-range pressure level of the inert gas is 40-90 psi, the low-range pressurized inert gas pressure level is 40-55 psi, the medium-range pressurized inert gas pressure level is 55 psi and 70 psi, and the high-range pressurized inert gas pressure level is 75-90 psi;

[0013] A method for continuously separating glucose and fructose using this apparatus includes the following steps:

[0014] S1: To provide a new mass transfer method to eliminate the displacement region and further utilize it;

[0015] S2: Differential setting scheme used between resin and various types of liquid;

[0016] S3: The single-stage recirculation scheme adopted by the device uses a new mass transfer method to recover all liquid streams into the lower storage tank;

[0017] The displacement zone is the amount of resin installed in each column, where the resin is fully adsorbed to saturation by a predetermined input volume of feed solution, and the installed amount of resin is kept in a semi-dry state.

[0018] Preferably, the insulating jacket includes manifold A and manifold B;

[0019] Each of the upper storage tanks is provided with an inlet conduit penetrating the outer wall of the insulating jacket on its top surface; and each of the upper storage tanks is provided with an outlet conduit penetrating the outer wall of the insulating jacket on its bottom surface.

[0020] The bottom end of the inlet conduit is equipped with a baffle a, the top surface of the upper storage tank is equipped with a pipe one, the top end of the outlet conduit is equipped with a baffle b, and the outer circumference of the outlet conduit is fixedly connected with a pipe two.

[0021] Preferably, the sandwich sleeve includes a manifold C and a manifold D, and the interior of the sandwich sleeve is provided with two or more vertically installed partitions;

[0022] Each column has an inlet end on its top surface and an outlet end on its bottom surface, with a mesh filter installed inside the outlet end.

[0023] The column is filled with resin, which is a strong acidic cation exchange resin of alkaline earth metal base with an average particle size of 320 μm ± 10 μm.

[0024] Preferably: Each integral unit is provided with a liquid inlet conduit penetrating the outer wall of the jacket on its top surface, a nozzle is provided on the outer circumference of the liquid inlet conduit, a reservoir is connected to the top of the liquid inlet conduit, and a baffle c is provided on the top of the reservoir; a baffle d is provided between the bottom of the reservoir and the top of the nozzle; a pipe three is provided on the outer wall of the reservoir between the baffle c and the baffle d.

[0025] All the reservoirs in the same column are connected to the same manifold O at the top, and the manifold O is connected to the bottom of the outlet conduit.

[0026] Each of the integral units is provided with a pipe 4 on its top surface; each of the integral units is connected to a vacuum box on its bottom surface, and an exhaust pipe and a manifold E are respectively provided on one side of the vacuum box.

[0027] Each of the integral units is provided with a funnel-shaped liquid collecting conduit on its bottom surface, and a baffle e is provided inside the liquid collecting conduit; a liquid reservoir is provided inside the vacuum box, and a liquid conduit is provided at the bottom end of the liquid reservoir, and a baffle f is provided inside the liquid conduit, and a pipe five is provided on the outer circumference of the liquid conduit located below the baffle f.

[0028] The vacuum level of the vacuum chamber is 15-27 inches of mercury.

[0029] Preferably, the hollow sleeve includes a manifold F and a manifold G;

[0030] The water temperature inside the insulating jacket, the interlayer jacket, and the hollow jacket is 55-70℃;

[0031] Each of the lower storage tanks is provided with an infusion conduit penetrating the outer wall of the hollow sleeve on the top surface, and a baffle g is provided at the top of the infusion conduit. Each of the lower storage tanks is provided with a drainage pipe penetrating the outer wall of the hollow sleeve on the bottom surface, and the output end of the drainage pipe and the input end of the inlet conduit are connected to the same connecting pipe.

[0032] A pipe is installed on the top surface of the lower storage tank located on one side of the infusion conduit; a liquid level sensor is installed inside each lower storage tank; and an infusion pipe is installed on the top surface of each lower storage tank.

[0033] Preferably, the closed vacuum environment loop includes an aerosol separator, a central vacuum pump, a water storage tank, a liquid guide pipe fixedly connected to the bottom surface of the water storage tank, an inert gas generator, a steel tank container, and a cold water condenser. The outlet of the aerosol separator is connected to one end of the central vacuum pump and the water storage tank through a delivery conduit. The inlet and outlet ends of the inert gas generator are respectively connected to the outlet end of the central vacuum pump and the inlet end of the steel tank container.

[0034] The air inlet of the aerosol separator is connected to a manifold P, and the output end of the manifold P is connected to the input end of multiple air outlet pipes; the water inlet and outlet of the cold water condenser are respectively connected to the drain outlet of the aerosol separator and the inlet of the water storage tank.

[0035] Preferably, the upstream wide-range inert gas supply loop includes a single gas pipeline connected to the medium-pressure outlet of the steel tank container, a manifold H connected to the second input end of the pipeline and the output end of the single gas pipeline, a second gas pipeline connected to the low-pressure outlet of the steel tank container, a manifold J connected to the first input end of the pipeline and the output end of the second gas pipeline, a third gas pipeline connected to the high-pressure outlet of the steel tank container, a manifold K connected to the third input end of the pipeline and the output end of the third gas pipeline, a fourth gas pipeline, and a manifold L connected to the fourth input end of the pipeline and the output end of the fourth gas pipeline.

[0036] The upstream wide-range inert gas supply loop also includes a heater, the inlet and outlet of which are connected to the output end of the steel tank container and the input end of the four gas pipelines via conduits, respectively.

[0037] The heating temperature of the heater is 60-85℃;

[0038] The downstream wide-range inert gas supply loop includes five gas pipelines connected to another medium-pressure outlet of the steel tank container, a manifold M connected to the fifth inlet of the pipeline and the outlet of the five gas pipelines, a sixth gas pipeline connected to another high-pressure outlet of the steel tank container, and a manifold N connected to the sixth inlet of the pipeline and the outlet of the six gas pipelines.

[0039] Preferably, the new mass transfer method includes the following steps:

[0040] A1: Retain the solid resin material in a set of columns as a single unit;

[0041] A2: The mobile phase liquid material is delivered intermittently as a dose via the pulse input SI method, and is dripped into each unit cell;

[0042] A3: After each delivery of the mobile phase liquid material, a wide range of pressurized inert gas is supplied intermittently and simultaneously to each integral unit;

[0043] A4: This ensures that the solid resin material installed in the unit maintains a closed vacuum environment on the other side.

[0044] A5: The processed mobile phase liquid material is collected intermittently from the bundle outlet at the bottom of the unit;

[0045] The total time spent on steps A2-A5 is the minimum time interval Δt;

[0046] The wide range of pressurized inert gas is supplied from the top of the unit, while a vacuum is applied from the bottom of the unit.

[0047] Preferably, the specific operation of the pulse input SI method includes the following steps:

[0048] A21: Simultaneously deliver mobile phase liquid material, subdivided into several predetermined doses, to the top of each integral unit in the shortest possible time to form a partially wetted area;

[0049] A22: Simultaneously collect the liquid discharged from the bottom of each integral unit, so that the transported liquid and the resin material installed in each integral unit can instantly undergo non-uniform mass transfer contact.

[0050] The mobile phase liquid material includes an aqueous feed solution, an aqueous homogeneous mixture containing sugar components, and elution water.

[0051] Preferred: The differential setting scheme includes the following methods:

[0052] B1: Take a predetermined amount of feed solution and resin to achieve complete adsorption saturation, and fill the column with this amount of resin;

[0053] B2: Start-up tests were conducted using a new mass transfer method, in which the feed solution and elution water were sequentially and intermittently delivered to generate a stable characteristic curve;

[0054] B3: Steady-state testing is conducted by intermittently delivering various liquids arranged in sequence using a new mass transfer method;

[0055] B4: Divide the time required for each portion of the obtained characteristic curve to deliver the liquid by the minimum time interval to obtain the number of dose drops in the device as a specific range of the corresponding liquid input area;

[0056] B5: Divide the volume of the liquid by the number of doses to obtain the partial volume required for each dose;

[0057] B6: The amount and partial volume of resin obtained in step B1 ÷ the preselected number, with the volume of the droplet dose received simultaneously as the specific area range of the corresponding liquid;

[0058] B7: Assign all integral units with each corresponding liquid to a range of specific regions;

[0059] B8: All types of transported liquids are arranged in the same order in a circular circulation pattern in the device;

[0060] The preselected number corresponds to a set of columns set in a single integral unit, and the preselected number is a finite integer greater than 1.

[0061] Preferably, B2 further includes the following:

[0062] B21: Based on the decomposition characteristic curves of the collected sequential samples, and collect sequential samples as multiple recycled liquid mixtures for further testing;

[0063] B22: A characteristic curve is generated by intermittently feeding a recirculated liquid mixture in the order of collection, with the feed solution arranged after the sugar mixture in the feed solution with a glucose content slightly higher than that in the feed solution and before the sugar mixture in the feed solution with a glucose content slightly lower than that in the feed solution, followed by the remaining unused recirculated liquid, elution water, and then the liquid mixture collected from the characteristic curve in sequence.

[0064] B23: The samples collected in the previous step are recorded on the predetermined sugar mixture characteristic curve and decomposed into various recycle liquids for further testing;

[0065] B24: Repeat steps B22-B23 until a stable characteristic curve is obtained.

[0066] Preferably, B3 further includes the following:

[0067] B31: Based on the collected samples, in the order of collection for each corresponding delivery liquid, decompose and record each required portion of time and generate characteristic curves;

[0068] B32: Record the individual components and concentrations of all expanded recirculated liquid mixtures;

[0069] B33: By intermittently feeding the expanded recirculated liquid mixture in the order of collection, a characteristic curve is generated by further testing. The feed solution is arranged after the glucose content is slightly higher than that of the sugar mixture in the feed solution and before the glucose content is slightly lower than that of the sugar mixture in the feed solution. Then, the remaining unused recirculated liquid is fed in a specific order, followed by elution water, and then the liquid mixture collected first from the characteristic curve.

[0070] B34: Record the portion of the time required to deliver the corresponding liquid from the characteristic curve obtained in step B33;

[0071] B35: If the recovered raffinate and product fail to meet the predetermined purity and concentration of the raffinate and product, then repeat steps B31-B34 continuously; if the recovered raffinate and product meet the predetermined purity and concentration of the raffinate and product, then record only their respective components and concentrations as an extended range of the characteristics of the recovered liquid for subsequent use.

[0072] The characteristic curve includes a glucose-rich raffinate, multiple recycled liquid mixtures in a specific order, and an expansion of multiple recycled liquid mixtures by adding liquid mixtures with specific compositions and limited concentrations of glucose-rich raffinate and fructose-rich product solutions recovered from the previous characteristic curve.

[0073] The dry solids content of the expanded recirculated liquid mixture is 40%-60%.

[0074] Preferably, the specific content of B6 includes the following aspects:

[0075] B61: Assign all the units of each input liquid to their respective liquid regions in sequence, and assign all regions to an infinite format in sequence;

[0076] B62: Prepare the corresponding solution and store it in the corresponding tank in the tank module for distribution of this liquid;

[0077] B63: During steady-state operation, various fluids are simultaneously delivered to their respective regions by the device in a period of minimal time interval, changing the liquid flow pattern observed in conventional chromatographic separation from parallel to the mobile phase to a flow direction perpendicular to the mobile phase.

[0078] Preferably, the content of B8 further includes preparing the entire series of recycled liquids recorded in step B35 into the corresponding lower storage tanks in sequence, and connecting them together with the pressurized inert gas supply module to support liquid distribution via the upstream storage tank module as a closed loop.

[0079] Preferably, the liquid stream includes a raffinate stream rich in glucose solution, a product stream rich in fructose solution, and multiple recirculated liquid streams with stable composition and specific concentration;

[0080] The method for recovering the liquid stream includes the following:

[0081] C1: The liquid sequentially passes through the closed-loop downstream storage tank module, the upstream storage tank module, and the rotation and positioning mechanism in the upstream rotary joint module to complete the mass transfer balance of the separation module, and then returns to the downstream rotary joint module.

[0082] C2: Perform steady-state operation during each time interval spent.

[0083] Preferably, C1 further includes the following:

[0084] C11: The integral unit located in the first position in the separation module receives liquid delivery, while the other integral units do not receive liquid. The liquid is simultaneously transferred from the lower tank to the upper tank in a specific order and is associated with a wide range of pressurized inert gas supplies through the storage device.

[0085] C12: After delivery of various liquids, the liquid is intermittently delivered through a device that alternately supplies two separate, wide-range pressurized inert gas paths to force the dripping dose of liquid to be rapidly discharged through the resin, thereby completing the expected mass transfer contact equilibrium between the solid and liquid phases.

[0086] C13: Maintain a closed vacuum environment, discharge each liquid solution into the corresponding transfer container (38), and keep the resin in a semi-dry state;

[0087] C14: Intermittently collect the discharged liquid from each transfer container and transfer the collected liquid to the lower storage tank via a wide-range pressurized inert gas supply route through the downstream rotary joint module;

[0088] C15: Repeat steps C11-C14 continuously, while covering the first and second integral units of the liquid receiving module, until the storage container and the transfer container of the first liquid receiving unit are set back to their initial positions, completing one cycle, and the start-up operation is completed.

[0089] The various liquids recovered during the startup operation include water as circulating water, low-dryness solid-phase glucose solutions for other uses, various recovered liquids stored in a specific order, solutions as glucose residues, and solutions as fructose products.

[0090] Preferably, the steady-state operation includes the following steps:

[0091] C21: Various liquids are transported by a liquid transport method using a large-scale pressurized inert gas, while simultaneously transferring all available liquids from the upper storage tank and forcing them into the storage container;

[0092] C22: After delivery of various liquids, the device intermittently delivers the liquid by alternating supply between two separate, wide-range pressurized inert gas paths to force the dripping dose of liquid to be rapidly discharged through the resin, thereby completing the expected mass transfer contact equilibrium between the solid and liquid phases.

[0093] C23: Maintain a closed vacuum environment, discharge each liquid solution into the corresponding transfer container, and keep the resin in a semi-dry state;

[0094] C24: Collects various discharged liquids from each transfer container and transfers the collected liquids to the lower storage tank via a downstream rotary joint module through a wide-range pressurized inert gas supply route.

[0095] The various liquids recovered during the steady-state operation include water as circulating water, low-dryness solid-phase glucose solutions for other uses, various recovered liquids stored in a specific order, solutions as glucose residues, and solutions as fructose products.

[0096] The beneficial effects of this invention are as follows:

[0097] 1. This invention relates to an apparatus for purifying a mixed solution of glucose, fructose, and oligosaccharides from a feed solution containing glucose, fructose, and oligosaccharides. The apparatus comprises multiple sequentially connected modules integrated into a closed loop. Each module operates independently within the loop but is coordinated as a whole. It works in conjunction with a novel mass transfer method, differential settings between the solid and liquid phases, and a circulation scheme. By maintaining the resin installed in the column in a semi-dry state, the displacement zone of traditional chromatographic processes is eliminated. This reduces resin consumption while separating the feed solution into pure liquid glucose and pure liquid fructose in 100% yield. Simultaneously, by reducing the amount of water consumed in elution, the concentration of the dry solids percentage of the product and byproducts is increased.

[0098] 2. In this invention, the inert gas supply module and the separation module are integrated together, which has the purpose of rapid liquid drainage and prevention of possible microbial growth. In the process of separating glucose and fructose, the inert gas can act as a carrier to increase the concentration of various sugar solutions by removing moisture. By using recycled condensed water, the consumption of washing water is reduced, and the energy consumption in the device is also reduced.

[0099] 3. In this invention, a circular multi-valve body I driven by a servo motor I rotates forward intermittently at equal angles or stops rotating in a selected direction. During any time interval between the stopping and forward rotation of the circular multi-valve body I, liquid stored in each upper tank is simultaneously transported from the specific upper tank to the next module through the upstream rotary joint module. Under steady-state operation, each rotational step forward by the circular multi-valve body II signifies that the device has completed a complete separation cycle. During steady-state operation, all integrated units in the device repeatedly and simultaneously perform the liquid filling, liquid discharge, and collection processes through all sequentially connected modules within each minimum time interval Δt. The operation mode of this invention differs from the liquid handling methods observed in currently widely used SMB processes.

[0100] 4. In an emergency, such as when a specific module experiences a mechanical failure, the present invention allows that part of the equipment to be shut down for maintenance without affecting the operation of other parts of the equipment. This flexible setup of each independently operating module as a whole provides flexibility in terms of throughput requirements, operational stability, and reduced downtime required for maintenance.

[0101] 5. In this invention, a wide range of pressurized inert gas can be supplied simultaneously via a pipe three connecting baffles c and d on a temporary transfer storage unit, and another pipe three adjacent to the temporary transfer storage unit, so that a portion of the liquid received in the temporary transfer storage unit is intermittently dosed in a pulsed input pattern, resulting in rapid wetting of the top of each integral unit and rapid passage through the resin bed to achieve the desired mass transfer balance.

[0102] 6. The apparatus of the present invention is used to simultaneously recover mixtures of glucose and fructose solutions of various grades and to achieve separation of higher concentration grades. Compared with traditional chromatographic methods, it can effectively reduce production costs, reduce resin usage and elution water consumption, and obtain ultimate purity of higher concentration glucose and fructose components.

[0103] 7. This invention extracts a water-rich wet inert gas, which is driven by a central vacuum pump through its manifold. The water in the wet inert gas is recovered by a mist separator for water recycling. This keeps the resin installed in each unit of the separation module in a semi-dry state. At the same time, when the dripping liquid dose rapidly passes through the stationary resin particles, heterogeneous contact is generated to meet the standards of the new mass transfer method, which can convert the wet inert gas into a dry inert gas.

[0104] 8. This invention maximizes the utilization rate of resin in the overall unit. The resin content in each overall unit is equivalent to the amount of resin in the mass transfer zone of a conventional chromatography. The resin installed in the feed deployment zone is completely saturated with the feed solution. All types of solutions are used in a differential setting scheme and interact with the resin installed in the overall unit, thereby effectively reducing the cycle time compared with chromatography.

[0105] 9. This invention establishes a single-stage recirculation scheme in the apparatus to simultaneously perform continuous separation and concentration of various fractionated mixtures, reducing the consumption of eluent. The recirculation scheme simultaneously inputs the feed solution, eluent, and other recirculation streams from predetermined storage tanks into predetermined zones. Although each zone is independent of the others, they are interconnected through their respective upstream and downstream storage tank modules. Therefore, this invention continuously separates the feed stream into two streams: separating glucose and fructose in the feed solution into a pure composition with 100% recovery, and multiple recirculation streams of a glucose and fructose mixture with stable composition and concentration. Scale-up of the industrial production unit is achieved by replicating single-column test results in multiple differential setups using all modules to obtain the final purification efficiency.

[0106] 10. In use, the apparatus of the present invention comprises multiple modules connected in sequence that operate independently in a closed loop. Simultaneously, a feed liquid containing glucose and fructose, along with other reflux liquid, is input. Water is washed away to obtain glucose raffinate and fructose product, and other reflux liquids are recovered. This process simultaneously increases the concentration of the separated mixture and continuously purifies the glucose and fructose in the feed liquid to their respective 100% pure components, with a concentration exceeding 51% dry solids and achieving 100% yield. Compared to the conventional synchronous moving bed process, the apparatus of the present invention reduces resin consumption by nearly 40% under the same feed throughput. Attached Figure Description

[0107] Figure 1 This is an exploded view of the overall structure of the device proposed in this invention for improving the continuous separation of glucose and fructose in a simulated moving bed.

[0108] Figure 2 This is a schematic diagram of the single-process structure of the device proposed in this invention for improving the continuous separation of glucose and fructose in a simulated moving bed.

[0109] Figure 3 This is a schematic diagram of the inert gas supply module of the device proposed in this invention for improving the continuous separation of glucose and fructose in a simulated moving bed.

[0110] Figure 4 A schematic diagram of the elution characteristic concentration curve of a single column test, which is an example of the 24-region scheme proposed in this invention.

[0111] Figure 5 The present invention proposes to Figure 4 A schematic diagram showing the transformation of the elution characteristic curve into a single-stage cycle process;

[0112] Figure 6 This is a perspective view of the single-stage cyclic process proposed in this invention;

[0113] Figure 7 This is a schematic diagram of the elution characteristic curves of cycles 1-4 obtained by pulse input SI with a feed volume to bed volume ratio of 0.25 (25%), as proposed in this invention.

[0114] Figure 8 This is a schematic diagram of the elution characteristic curve of cycle 5 proposed in this invention;

[0115] Figure 9 This is a schematic diagram of the steady-state elution curves of six consecutive cycles constructed by adding the raffinate region and the product region to the current cycle, as proposed in this invention.

[0116] Figure 10 A schematic diagram of the steady-state elution curves of six consecutive cycles constructed by adding the raffinate region and the product region to the current cycle for the 11 distribution regions proposed in this invention.

[0117] Figure 11 A schematic diagram of the steady-state elution curves of six consecutive cycles, which are constructed by adding the raffinate region and the product region to the current cycle for the 13 distribution regions proposed in this invention.

[0118] Figure 12 A schematic diagram of the steady-state elution curves of six consecutive cycles, which are constructed by adding the raffinate region and the product region to the current cycle to the 15 distribution regions proposed in this invention.

[0119] Figure 13This is a schematic diagram of the steady-state elution curves of six consecutive cycles, which are constructed by adding the raffinate region and the product region to the current cycle to the 17 distribution regions proposed in this invention.

[0120] In the diagram: 1. Baffle a, 2. Baffle b, 3. Baffle c, 4. Baffle d, 5. Baffle f, 6. Baffle g, 7. Pipeline 1, 8. Pipeline 2, 9. Pipeline 3, 10. Pipeline 5, 11. Insulating jacket, 12. Upstream storage tank module, 13. Manifold A, 14. Manifold B, 15. Upper storage tank, 16. Inlet conduit, 17. Outlet conduit, 19. Circular multi-valve body I, 21. Storage container, 22. Liquid outlet conduit, 23. Column, 24. Inlet end, 25. Mesh filter, 26. Manifold C, 27. Manifold D, 28. Storage container, 29. Nozzle, 30. Pipeline 4, 31. Vacuum box, 32. Liquid collection conduit, 33. Liquid storage container, 34. Liquid conduit, 36. Jacket, 37. Circular multi-valve body II, 38. Transfer container, 39. Output conduit, 40. Downstream storage Tank module, 41 hollow sleeve, 42 manifold F, 43 manifold G, 44 lower storage tank, 45 infusion conduit, 46 drainage pipe, 48 gas outlet pipe, 49 manifold E, 50 aerosol separator, 51 central vacuum pump, 52 water tank, 53 liquid guide pipe, 54 inert gas generator, 55 steel tank container, 56 heater, 57 manifold L, 62 pipeline six, 63 liquid level sensor, 64 infusion pipe, 65 baffle e, 66 first gas supply line, 67 manifold H, 68 second gas supply line, 69 manifold J, 70 third gas supply line, 71 manifold K, 72 fourth gas supply line, 73 fifth gas supply line, 74 manifold M, 75 sixth gas supply line, 76 manifold N, 79 manifold O, 84 manifold P. Detailed Implementation

[0121] The technical solution of this patent will be further described in detail below with reference to specific embodiments.

[0122] The embodiments of this patent are described in detail below. Examples of these embodiments are shown in the accompanying drawings, wherein the same or similar reference numerals denote the same or similar elements or elements having the same or similar functions throughout. The embodiments described below with reference to the accompanying drawings are exemplary and are only used to explain this patent, and should not be construed as limiting this patent.

[0123] Example 1:

[0124] Devices designed to improve the continuous separation of glucose and fructose in a simulated moving bed, such as... Figure 1-3 and Figure 5-6As shown, the device includes an upstream storage tank module 12, an upstream rotary joint module, a separation module, a downstream rotary joint module, a downstream storage tank module 40, and an inert gas supply module. The upstream storage tank module 12, the upstream rotary joint module, the separation module, the downstream rotary joint module, the downstream storage tank module 40, and the inert gas supply module operate in parallel. By sequentially conveying liquid from top to bottom, the device can meet the specified throughput of multiple separation modules operating in parallel.

[0125] The upstream storage tank module 12 includes multiple insulating jackets 11 arranged in an array, and an upper storage tank 15 disposed inside the insulating jackets 11 for receiving specific liquids;

[0126] Preferably, in this embodiment, there are 24 upper storage tanks 15, which may have the same structure and different sizes.

[0127] Furthermore, each of the upper storage tanks 15 is provided with an inlet conduit 16 that penetrates the outer wall of the insulating jacket 11 and extends upward, for receiving liquid; and each of the upper storage tanks 15 is provided with an outlet conduit 17 that penetrates the outer wall of the insulating jacket 11 and extends downward, for discharging all the stored liquid.

[0128] Preferably, a baffle a1 is provided at the bottom end of the inlet conduit 16, and a pipe 7 for supplying dry, low-range pressurized inert gas is provided on the top surface of the upper storage tank 15.

[0129] Preferably, a baffle b2 is provided at the top of the outlet conduit 17, and a pipe 8 for the entry of medium-pressure dry inert gas is fixedly connected to the outer circumference of the outlet conduit 17; inert gas with a wide pressure range is supplied through corresponding gas pipes provided around the top and bottom sides of each upper storage tank 15, which is the driving force for opening or closing the baffle a1 or baffle b2. When the baffle b2 is closed, the received liquid is contained and stored, or when the baffle b2 is open and the baffle a1 is closed, the stored liquid is discharged into the next module.

[0130] In a further preferred embodiment, the second pipe 8 extends to the outer wall of the insulating jacket 11;

[0131] Furthermore, the insulating jacket 11 includes a manifold A13 for connecting the warm water inlet and a manifold B14 for connecting the warm water outlet; by placing the upper storage tanks 15 inside the warm water circulation insulating jacket 11, all upper storage tanks 15 can be kept within a selected temperature range.

[0132] The upstream rotary joint module includes a circular multi-valve body I 19 driven by a servo motor I, multiple storage containers 21 arranged in a ring array on the top surface of the circular multi-valve body I 19, and multiple liquid outlet conduits 22 arranged in a ring array on the bottom surface of the circular multi-valve body I 19. The circular multi-valve body I 19 driven by the servo motor I rotates forward intermittently at equal angles in a selected direction or stops rotating. When the circular multi-valve body I 19 stops, all predetermined volumes of specific liquid are rapidly and simultaneously transferred. The liquid transferred from a specific upper storage tank 15 of the upstream storage tank module 12 is received through the storage containers 21. The liquid outlet conduits 22 are configured to accurately transfer the liquid to the next subsequent module.

[0133] Preferably, the number of storage containers 21 and outlet conduits 17 are the same, and they are connected one-to-one via conduits. In use, after each storage container 21 has received all types of liquids, the circular multi-valve body I 19 moves forward by a rotational step, transporting the stored liquid to the next subsequent module, and waits for another round of liquid transport. During any time interval between the circular multi-valve body I 19 stopping and rotating forward, the liquid stored in each upper storage tank 15 is simultaneously transported from the specific upper storage tank 15 through the upstream rotary joint module to the next module. The operation method in this embodiment differs from the liquid handling method observed in the currently widely used SMB process.

[0134] The separation module comprises multiple integral units housed within an insulated warm water jacket 36, and multiple columns 23 arranged in a predetermined number within each integral unit to maintain the multiple integral units within a selected temperature range. The separation module can be expanded into parallel-operating modules for alternating resin regeneration without shutting down the entire unit; the upper storage tank size can be increased, and liquid can be distributed to the parallel-operating separation modules via an upstream rotary joint module and distributed back to the downstream storage tank module 40 via a downstream rotary joint module. In emergency situations, such as mechanical failure of a specific module, that section of the equipment can be shut down for maintenance without affecting the operation of other parts of the equipment. This flexible setup, operating as a single unit across each independently operating module, provides flexibility in terms of throughput requirements, operational smoothness, and reduced downtime required for maintenance.

[0135] Preferably, the interior of the jacket 36 is provided with two or more vertically mounted partitions to confine each integral unit within a predetermined compartment; so that warm water flows through all the enclosed integral unit compartments in sequence and then flows out, so that all integral units are maintained within a predetermined temperature range.

[0136] Preferably, each of the columns 23 has an inlet end 24 on its top surface and an outlet end on its bottom surface, and a mesh filter 25 is provided inside the outlet end;

[0137] Further preferably, the interior of column 23 is filled with resin, which is a strong acidic cation exchange resin of alkaline earth metal base, preferably a calcium-based strong acidic cation exchange resin, to accommodate an equal amount of resin material and prevent it from being discharged.

[0138] Preferably, the calcium-based strong acid cation exchange resin has an average particle size of 320 μm ± 10 μm; it is widely used in most industrial SMB processes.

[0139] Furthermore, the jacket 36 includes a manifold C26 for connecting the warm water inlet and a manifold D27 for connecting the warm water outlet; by arranging multiple integral units inside the warm water circulation insulating jacket 36, all integral units can be kept within a selected temperature range.

[0140] Furthermore, each of the integral units is provided with a liquid inlet conduit that penetrates the outer wall of the interlayer sleeve 36 and extends upward. The outer circumferential wall of the liquid inlet conduit is provided with a nozzle 29. The top end of the liquid inlet conduit is connected to a storage device 28 for receiving liquid in the corresponding upper storage tank 15. Each integral unit is provided with a temporary transfer storage device 28 at its top to receive specific liquid transported from the corresponding upper storage tank 15 in the upstream storage tank module 12.

[0141] Preferably, all the reservoirs 28 in the same column or row are connected to the same manifold O79 at their top ends, and the manifold O79 is connected to the bottom end of the liquid outlet conduit 22; it can receive all kinds of liquids and simultaneously and equally transfer the liquid to the top of each corresponding integral unit operating in parallel or row, so that the wetting part contains the resin in each integral unit.

[0142] Preferably, a baffle c3 is provided at the top of the storage unit 28;

[0143] Preferably, a baffle d4 is provided between the bottom end of the reservoir 28 and the top end of the nozzle 29; by controlling the entry and exit of pressurized inert gas, a portion of the stored liquid is intermittently delivered to the reservoir 28 or the liquid delivery is stopped in a pulsed manner such as pulse SI.

[0144] More preferably, the outer wall of the reservoir 28 located between baffle c3 and baffle d4 is provided with a pipe 9; the pipe 9 is used to input high-pressure dry inert gas into the corresponding reservoir 28.

[0145] Furthermore, each of the integral units is provided with a conduit 30 on its top surface for simultaneously and intermittently receiving a supply of high-pressure dry inert gas. Through a conduit 9 connecting baffles c3 and d4 on the temporary transfer reservoir 28, and another conduit 9 adjacent to the temporary transfer reservoir 28, a wide range of pressurized inert gas can be supplied simultaneously, causing a portion of the liquid received in the temporary transfer reservoir 28 to be intermittently dosed in a pulsed input pattern, resulting in rapid wetting of the top of each integral unit and rapid passage through the resin bed to achieve the desired mass transfer equilibrium.

[0146] As a supplement, the bottom surface of each integral unit is connected to a vacuum chamber 31, and one side of the vacuum chamber 31 is provided with an outlet pipe 48 for the discharge of wet inert gas; the bottom of each integral unit is exposed to a closed vacuum environment so that the resin material is in a semi-dry state.

[0147] Preferably, the vacuum level of the vacuum chamber 31 is 15-27 inches of mercury; used to keep solid resin materials in a semi-dry state.

[0148] Preferably, each of the integral units is provided with a funnel-shaped liquid collection conduit 32 on its bottom surface, and a baffle e65 is provided inside the liquid collection conduit 32; the vacuum box 31 is provided with a temporary liquid reservoir 33 for assisting in receiving the discharge of droplet-sized liquid, and preferably, the top of the liquid reservoir 33 is open; the liquid in the integral unit is discharged into the liquid reservoir 33 through the funnel-shaped liquid collection conduit 32 so as to collect liquid from various areas and redistribute it for further application.

[0149] More preferably, a liquid conduit 34 is provided at the bottom end of the liquid reservoir 33, a baffle f5 is provided inside the liquid conduit 34, and a pipe 10 is provided on the outer circumference of the liquid conduit 34 located below the baffle f5.

[0150] Preferably, both pipe 5 10 and liquid conduit 34 extend through the bottom outer wall of the jacket sleeve 36; so that the liquid in the reservoir 33 below each integral unit can be transported to the corresponding upper reservoir 15 through the downstream rotary joint module, so as to further continuously carry out the new mass transfer method, thereby separating the glucose and overheated solution mixture.

[0151] Furthermore, a manifold E49 is provided on one side of the vacuum chamber 31 for supplying low-range pressurized inert gas when the vacuum chamber 31 is closed. Preferably, the manifold E49 is located below the closed vacuum environment and extends downward through the outer wall of the jacket sleeve 36. The top of the liquid reservoir 33 is widely open, and wet inert gas is extracted through the manifold E49 via the gas outlet pipe 48 to keep the resin in a semi-dry state. The discharged liquid is received via the bottom funnel-shaped liquid collection conduit 32 and guided into the various temporary liquid reservoirs 33 below via the baffle e65. A wide-range pressurized inert gas is supplied through a gas pipe connected by the same manifold E49 adjacent to the wet inert gas outlet pipe 48 to close the baffle e65, thereby closing the vacuum environment; at the same time, all the liquid is discharged to the subsequent modules via another open baffle f5.

[0152] The downstream rotary joint module includes a circular multi-valve body II 37 driven by a servo motor II, multiple transfer containers 38 arranged in a ring array on the top surface of the circular multi-valve body II 37, and multiple output conduits 39 arranged in a ring array on the bottom surface of the circular multi-valve body II 37 and equal in number to the transfer containers 38; the circular multi-valve body II 37 rotates forward intermittently or stops rotating in a selected direction at a predetermined equal angle; the transfer containers 38 are used to receive various liquids discharged through each liquid conduit 34 of the separation module; the arrangement of the output conduits 39 enables the precise transfer of specific liquids to the subsequent downstream storage tank module 40.

[0153] When the circular multi-valve body II 37 stops, it means that all kinds of liquids collected in the liquid reservoir 33 at the bottom of each integral unit are simultaneously transported and stored in the transfer container 38. Once all kinds of liquids in the transfer container 38 have been transported through the output conduit 39, the circular multi-valve body II 37 will enter the predetermined rotation step again and repeat the above operation. Under steady-state operation, each rotation step of the circular multi-valve body II 37 means that the equipment has completed a complete separation cycle.

[0154] The downstream storage tank module 40 includes multiple hollow sleeves 41 arranged in an array, and a lower storage tank 44 disposed inside the hollow sleeves 41 for receiving specific liquids.

[0155] Preferably, the water temperature inside the insulating jacket 11, the interlayer jacket 36, and the hollow jacket 41 is 55-70℃; this can reduce the viscosity of the liquid passing through the upstream storage tank module 12, the downstream storage tank module 40, and the separation module, and prevent the growth of microorganisms.

[0156] Preferably, the number of lower storage tanks 44 and upper storage tanks 15 is the same; used to receive specific liquids from the downstream rotary joint module via the output conduit 39.

[0157] Furthermore, the hollow sleeve 41 includes a manifold F42 for connecting the warm water inlet and a manifold G43 for connecting the warm water outlet; by placing the lower storage tank 44 inside the warm water circulation hollow sleeve 41, all lower storage tanks 44 can be kept within the selected temperature range.

[0158] Preferably, each of the lower storage tanks 44 is provided with a liquid infusion conduit 45 extending upward through the outer wall of the hollow sleeve 41 on its top surface. A baffle g6 is provided at the top of the liquid infusion conduit 45. The liquid infusion conduit 45 receives liquid through the open baffle g6. A wide range of pressurized inert gas is supplied through the arranged pipe six 62 as a driving force to open or close the baffle g6.

[0159] Preferably, each of the lower storage tanks 44 is provided with a drain pipe 46 extending downward through the outer wall of the hollow sleeve 41 on its bottom surface. The drain pipe 46 can be used to discharge the stored liquid as pure glucose residue or fructose liquid sequentially through different external pipelines. It can also be used to recirculate a portion of the usable liquid in each lower storage tank 44 back to each designated upper storage tank 15 in the aforementioned upstream storage tank module 12 via external pipelines and each volumetric pump.

[0160] Preferably, the output end of the drainage tube 46 and the input end of the inlet conduit 16 are connected to the same connecting pipe to facilitate the recycling of the liquid.

[0161] More preferably, the top surface of the lower storage tank 44 located on one side of the infusion conduit 45 is provided with a pipe 62 for supplying high-range pressurized inert gas;

[0162] More preferably, each of the lower storage tanks 44 is provided with a liquid level sensor 63 inside; each of the lower storage tanks 44 is provided with a delivery pipe 64 on its top surface; the liquid level sensor 63 can control the predetermined sugar mixture delivered through the delivery pipe 64 to maintain the liquid level of the predetermined composition.

[0163] The inert gas supply module is a route for supplying pressurized inert gas over a wide range, and is applied to the upstream storage tank module 12, the upstream rotary joint module, the separation module, the downstream rotary joint module, and the downstream storage tank module 40. It includes a closed vacuum environment loop, an upstream wide-range inert gas supply loop, and a downstream wide-range inert gas supply loop connected sequentially to form a closed loop; thereby enabling continuous separation of the glucose and fructose feed solution mixture.

[0164] Preferably, the inert gas is one or a mixture of nitrogen, carbon dioxide, argon, etc., to reduce the oxidation of oxygen and resin, so as not to hinder long-term separation efficiency. The inert gas supply module is integrated with the separation module, which has the purpose of rapid liquid drainage and preventing possible microbial growth. In the process of separating glucose and fructose, the inert gas can act as a carrier to increase the concentration of various sugar solutions by removing moisture. With the use of recycled condensed water, the consumption of washing water is reduced, and the energy consumption in the device is also reduced.

[0165] During each time interval of steady-state operation, all available liquid solutions of all types from the upper tanks 15 of the upstream tank module 12 are simultaneously distributed to the integral units in the separation module via the storage containers 21 in the upstream rotary joint module for mass transfer equilibrium. The collected liquid discharged from each temporary reservoir 33 is transferred to the lower tanks 44 in the downstream tank module 40 via the transfer container 38 in the downstream rotary joint module, and then sequentially circulated back to the upstream tank module 12 through the downstream tank module 40 to achieve a new closed-loop operation mode for mass transfer equilibrium. This repeated process continuously achieves the separation of the glucose and fructose mixture. Furthermore, this organized liquid transfer operation is carried out by equipment control combined with a large-scale pressurized inert gas supply module, achieving the ultimate purification goal of the glucose and fructose mixture.

[0166] Preferably, the pressure level of the inert gas is 40-90 psi for a wide range, 40-55 psi for a low-range pressurized inert gas, 55 psi and 70 psi for a medium-range pressurized inert gas, and 75-90 psi for a high-range pressurized inert gas.

[0167] More preferably, the pressure level of the medium-range pressurized inert gas on the upstream storage tank module is 55-70 psi, which is used to provide sufficient pressure to the mechanical baffle b2 to support the weight of the entire transported liquid.

[0168] More preferably, the pressure level of the low-range pressurized inert gas on the upstream storage tank module is 40-55 psi, which is used to provide the driving force for the closing baffle a1 and provide sufficient pressure to quickly push the liquid into the next area.

[0169] More preferably, the pressure level of the high-range pressurized inert gas on the separation module is 70-90 psi, which is used to provide the driving force for alternately closing the baffle c3 and closing or opening the baffle d4 to achieve the desired mass transfer balance.

[0170] More preferably, the pressure level of the low-range pressurized inert gas on the separation module is 40-55 psi, which is used to provide the driving force for the shut-off baffle e65;

[0171] More preferably, the pressure level of the medium-range pressurized inert gas on the separation module is 55-70 psi, which is used to provide the driving pressure for the shut-off baffle f5;

[0172] More preferably, the pressure level of the high-range pressurized inert gas on the downstream storage tank module is 70-90 psi, which is used to provide the driving force for the shut-off baffle g6.

[0173] Furthermore, the closed vacuum environment loop includes an aerosol separator 50, a central vacuum pump 51 for facilitating the discharge of liquid into each temporary reservoir 33 and simultaneously extracting a wet inert gas rich in water mist, a water reservoir 52, a liquid guide pipe 53 fixedly connected to the bottom surface of the water reservoir 52, an inert gas generator 54, and a steel tank container 55. The outlet of the aerosol separator 50 is connected to one end of the central vacuum pump 51 and the water reservoir 52 through a delivery conduit. The inlet and outlet ends of the inert gas generator 54 are respectively connected to the outlet end of the central vacuum pump 51 and the inlet end of the steel tank container 55.

[0174] Preferably, the air inlet of the aerosol separator 50 is connected to a manifold P84, and the output end of the manifold P84 is connected to the input end of multiple air outlet pipes 48; the moisture-rich wet inert gas is extracted through the multiple air outlet pipes 48, collected by the manifold P84, and then enters the aerosol separator 50.

[0175] Preferably, a cold water condenser is also included, with its inlet and outlet connected to the drain port of the aerosol separator 50 and the inlet port of the water storage tank 52, respectively. Throughout the process, the inert gas rich in water mist is discharged from the outlet pipe 48, first passing through the aerosol separator 50 to remove moisture, and then condensed by the cold water condenser. The collected liquid water is stored in the water storage tank 52 through the liquid guide pipe 53 for water recycling. The dry inert gas separated from the aerosol separator 50 is mixed with pressurized dry air and passed through the inert gas generator 54 to obtain fresh dry inert gas, which is then stored in a steel tank container 55 to maintain the inert gas at a preferably wide range of pressure levels.

[0176] This structure extracts a water-rich wet inert gas, which is driven by a central vacuum pump 51 through its manifold. The moisture in the wet inert gas is recovered by a mist separator 50, keeping the resin installed in each integral unit of the separation module in a semi-dry state. At the same time, when the dripping liquid dose rapidly passes through the stationary resin particles, heterogeneous contact is generated to meet the standards of the new mass transfer method, which can convert the wet inert gas into a dry inert gas.

[0177] Furthermore, the upstream wide-range inert gas supply loop includes a single gas pipeline 66 connected to the medium-pressure outlet of the steel tank container 55, a manifold H67 connected to the input end of pipeline 2 8 and the output end of the single gas pipeline 66, a second gas pipeline 68 connected to the low-pressure outlet of the steel tank container 55, a manifold J69 connected to the input end of pipeline 1 7 and the output end of the second gas pipeline 68, a third gas pipeline 70 connected to the high-pressure outlet of the steel tank container 55, a manifold K71 connected to the input end of pipeline 3 9 and the output end of the third gas pipeline 70, a fourth gas pipeline 72, and a manifold L57 connected to the input end of pipeline 4 30 and the output end of the fourth gas pipeline 72.

[0178] Preferably, the upstream wide-range inert gas supply loop further includes a heater 56, the inlet and outlet of which are connected to the output end of the steel tank container 55 and the input end of the four gas supply lines 72 via conduits, respectively. Before the four gas supply lines 72 supply high-range pressurized inert gas to each pipeline 30 through the manifold L57, the embedded gas heater 56 is used to ensure that the fresh, dry inert gas is kept slightly above the temperature range of all types of liquid solutions to prevent microbial growth.

[0179] More preferably, the heating temperature of heater 56 is 60-85°C; the temperature range of the fresh, dry, inert gas is kept slightly higher than the temperature range of all kinds of liquid solutions, which can effectively prevent the growth of microorganisms.

[0180] A medium-pressure inert gas is supplied sequentially via manifold H67 to each pipe 8 through a gas pipeline 66 connected to the steel tank container 55. Simultaneously, the low-pressure inert gas supplied by pipe 7 is shut off, causing baffle a1 to open. This allows a predetermined amount of liquid to be output from the lower tank 44 in the downstream tank module 40 after passing through each volumetric pump, while baffle b2 is pushed upwards to prevent downward flow of liquid, temporarily storing the supplied liquid before it enters each tank 15 in the upstream tank module 12. Then, pipe 8 is shut off to stop the supply of medium-pressure gas. Inert gas is supplied via two gas lines 68 extending from the steel tank container 55, with low-range pressurized inert gas being supplied sequentially to each pipe 7 via manifold J69. At the same time, high-range pressurized inert gas is supplied to pipe 9 via three gas lines 70 and manifold K71. During the gas supply, baffles a1 and c3 are closed, while baffle b2 is opened, so that liquid can be transported from the upper storage tank 15 to the storage container 21 through the outlet conduit 17. The circular multi-valve body I19 in the upstream rotary joint module advances one rotation step.

[0181] After the circular multi-valve body I19 stops operating, the low-range pressurized inert gas supplied by pipeline 17 and the high-range pressurized inert gas supplied by pipeline 39 are quickly shut off. Meanwhile, the steel tank container 55 is supplied with medium-range pressurized inert gas via pipeline 28. At the same time, high-range pressurized inert gas is supplied to each pipeline 430 via manifold L57 through the four gas pipelines 72, causing baffles b2 and d4 to close. This allows all the liquid in the storage container 21 to be transferred to the corresponding transfer storage unit 28 located at the top of the separation module c via the open baffle c3.

[0182] After the above operations are completed, the high-range pressurized inert gas is re-supplyed through pipe 39 within a predetermined time, causing baffle c3 to close. Simultaneously, the high-range pressurized inert gas supply through pipe 430 is shut off, allowing the liquid stored in reservoir 28 to rapidly pass through baffle d4, so that the dripping liquid quickly wets the top portion of the installed solid resin over a short period. Then, pipe 430 is immediately opened to supply pressurized inert gas, while pipe 39 is closed to cut off the high-range pressurized inert gas supply, causing baffle d4 to be pushed upwards to prevent liquid dripping. Simultaneously, the dripping liquid is pushed rapidly through the resin contained in each integral unit to achieve the expected mass transfer balance between the two phases. By repeatedly operating the opening and closing of the inert gas supply between pipe 39 and pipe 430, while simultaneously introducing the liquid stored in reservoir 28 separately at predetermined liquid doses within a specific time period, the differential setting scheme used between the solid and liquid phases is completed, and the differential setting scheme and the predetermined volume delivered in the form of pulse input SI are mutually matched.

[0183] Furthermore, the downstream wide-range inert gas supply loop includes a five-way gas pipeline 73 connected to another medium-pressure gas outlet of the steel tank container 55, a manifold M74 connected to the input end of pipeline 510 and the output end of the five-way gas pipeline 73, a six-way gas pipeline 75 connected to another high-pressure gas outlet of the steel tank container 55, and a manifold N76 connected to the input end of pipeline 62 and the output end of the six-way gas pipeline 75.

[0184] Five gas pipelines 73 connected to the steel tank container 55 supply medium-pressure inert gas sequentially through manifold M74 to each of the five pipelines 10. This is used to push the baffle f5 upward when the vacuum box 31 is applied, storing the discharged liquid in the corresponding reservoir 33. After the liquid is discharged, the vacuum box 31 and the medium-pressure inert gas supplied through the pipelines 10 are closed. At the same time, the low-range pressurized inert gas supplied through manifold E49 and the high-pressure inert gas supplied sequentially from manifold N76 through the six gas pipelines 75 to the pipeline 62 are opened. This causes the baffle e65 in the funnel-shaped liquid collection conduit 32 and the baffle g6 in the liquid transfer conduit 45 to be pushed up and closed at the same time, while the baffle f5 in the liquid conduit 34 is opened, so that all the liquid in each reservoir 33 is transferred to each transfer container 38 in the downstream rotary joint module. The circular multi-valve body II 37 in the downstream rotary joint module advances one rotation step. After multiple circular multi-valve bodies II 37 stop, the supply of medium-pressure inert gas through pipeline 5 10 is immediately resumed, and the supply of high-pressure inert gas through pipeline 6 62 is shut off, causing the baffle 5 to close. The liquid in each transfer container 38 is pushed by the infusion conduit 45 to open the baffle g6 and enter the corresponding lower storage tank 44 in the downstream storage tank module 40.

[0185] In this embodiment, the present invention is an apparatus for purifying a mixed solution of glucose, fructose and oligosaccharides from a feed solution containing glucose, fructose and oligosaccharides. The apparatus consists of multiple modules connected in sequence, which are integrated into a closed loop. Each module is connected in sequence and operates independently within the loop, but can be coordinated as a whole. It is also used in conjunction with the proposed new mass transfer method, the differential setting between the solid and liquid phases, and the circulation scheme.

[0186] All predetermined amounts of liquid are intermittently and simultaneously delivered via nozzles installed inside the respective integral units through the upstream rotary joint module to spray and wet the resin retained in the top area, forming a partially wetted zone for instantaneous and heterogeneous mass transfer contact, thereby achieving an equilibrium between the collected discharged liquid and the resin material installed in the respective units. The delivered liquid is instantaneously settled and discharged by applying pressurized inert gas from the top of all integral units and simultaneously applying a vacuum from the bottom of all integral units, keeping the resin in a semi-dry state. The liquid discharged from each integral unit is collected in each transfer container 38 located below each integral unit, and the collected liquid flows through the downstream rotary joint and is delivered to the corresponding lower storage tank 44. Throughout the process, the wet inert gas discharged from the bottom of the device is condensed into water mist through the inert gas supply module.

[0187] Before the next dose of liquid is simultaneously introduced, the upstream and downstream rotary joint modules are further advanced by a predetermined rotation step via servo motor I and servo motor II. During steady-state operation, all integrated units in the device repeatedly and simultaneously perform the liquid filling, liquid discharging, and collection processes through all sequentially connected modules within each minimum time interval Δt.

[0188] A sealed vacuum environment is applied to the entire bottom of the separation module to rapidly drain the liquid. Simultaneously, a moisture-rich wet inert gas is extracted via a mist separator 50 and a cold water condenser, water is collected and recovered, and the wet inert gas is converted into dry inert gas. The dry inert gas is combined with pressurized dry air and passed through an inert gas generator 54 to obtain fresh inert gas, which is then stored in a steel tank container 55 at a preferred pressure level, ready for deployment back to the separation module.

[0189] Example 2:

[0190] Devices designed to improve the continuous separation of glucose and fructose in a simulated moving bed, such as... Figure 1-6 As shown, the continuous separation method for a homogeneous aqueous solution containing glucose, fructose, and oligosaccharides using this apparatus includes the following steps:

[0191] S1: Provides a new mass transfer method to eliminate the displacement zone and further utilize it; it is a new mass transfer method different from that observed in chromatography, which can be used for rapid mass transfer of resin void volumes.

[0192] Preferably, the displacement zone is equipped with an equal amount of resin in each column 23, the resin is fully adsorbed to saturation by a predetermined input volume of feed solution, and the amount of resin installed is kept in a semi-dry state.

[0193] Furthermore, the new mass transfer method includes the following steps:

[0194] A1: The solid resin material is retained in a predetermined number of columns 23 as a whole unit; an equal amount of solid resin material is installed and retained in each column of the whole unit, and this bundle of columns behaves as a local fluidized bed as a whole unit.

[0195] Preferably, the amount of resin installed in each column 23 is equivalent to the mass transfer zone of a single column in chromatographic separation; to maximize the utilization rate of resin in the overall unit, the amount of resin in each overall unit is equivalent to the amount of resin in the mass transfer zone (MTZ) of traditional chromatography, and the resin installed in the feed deployment zone is completely saturated with the feed solution.

[0196] Preferably, each of the columns 23 has an inlet end 24 on its top surface and an outlet end on its bottom surface, and the outlet end is provided with a mesh filter 25 to accommodate an equal amount of the material to prevent it from being discharged.

[0197] A2: A predetermined amount of mobile phase liquid material is delivered intermittently as a dose by pulse input SI method, and added dropwise to each unit cell; this promotes the adsorption of dissolved components onto the resin material, while simultaneously eluting adsorbed components from the resin material.

[0198] Preferably, the specific operation of the pulse input SI method includes the following steps:

[0199] A21: Simultaneously deliver mobile phase liquid material, subdivided into several predetermined doses, to the top of each integral unit in the shortest possible time to form a partially wetted area;

[0200] A22: Simultaneously collect the liquid discharged from the bottom of each integral unit, so that the transported liquid and the resin material installed in each integral unit can instantly undergo non-uniform mass transfer contact, so as to achieve a balance between the collected discharged liquid and the resin material.

[0201] Preferably, the mobile phase liquid material includes an aqueous feed solution, an aqueous homogeneous mixture containing sugar components, and elution water; more preferably, the elution water is deionized water free of contaminants.

[0202] A3: After each delivery of the mobile phase liquid material, a wide range of pressurized inert gas is supplied intermittently and simultaneously to each integral unit; the pressurized inert gas is added to each integral unit to force the added mobile phase liquid material to pass through the solid resin material contained in each integral unit and then be quickly discharged, thereby achieving the expected mass transfer balance between the mobile phase and solid phase materials through the difference in bonding affinity between sugar components.

[0203] A4: To maintain a closed vacuum environment on the other side of the solid resin material installed in the monolithic unit; to keep the resin material in a semi-dry state. Pressurized inert gas is supplied from the top of the monolithic unit, and a vacuum is applied from the bottom of the monolithic unit to keep the resin in a semi-dry state, so that the elution water filled in the resin can be removed in the shortest possible time.

[0204] Preferably, a wide range of pressurized inert gas is supplied from the top of the monolithic unit, while a vacuum is applied from the bottom of the monolithic unit.

[0205] A5: Most of the processed mobile phase liquid material is collected intermittently from the bundle outlet at the bottom of the unit.

[0206] Furthermore, the total time spent in steps A2-A5 is the minimum time interval Δt.

[0207] S2: Differential setup scheme used between resin and various types of liquids; preferably, a preliminary study of individual column 23 is required to obtain satisfactory separation before implementing the differential setup.

[0208] Preferably, the type of liquid includes feed solution, wash water, and various recirculated liquids for delivery into the equipment;

[0209] Furthermore, the differential setting scheme includes the following methods:

[0210] B1: Take a predetermined amount of feed solution and resin to achieve complete adsorption saturation, and install this amount of resin into column 23;

[0211] B2: Start-up tests were conducted using a new mass transfer method, which sequentially and intermittently delivers the feed solution and elution water to generate a stable characteristic curve; the new mass transfer method starts this curve from the beginning of the elution time, unlike typical chromatographic elution characteristic curves that have a displacement zone followed by elution.

[0212] Preferably, step B2 further includes the following:

[0213] B21: Based on the decomposition characteristic curves of the collected sequential samples, and collect sequential samples as multiple recycled liquid mixtures for further testing;

[0214] B22: A characteristic curve is generated by intermittently feeding a recirculated liquid mixture in the order of collection, with the feed solution arranged after the sugar mixture in the feed solution with a glucose content slightly higher than that in the feed solution and before the sugar mixture in the feed solution with a glucose content slightly lower than that in the feed solution, followed by the remaining unused recirculated liquid, elution water, and then the liquid mixture collected from the characteristic curve in sequence.

[0215] B23: The samples collected in the previous step are recorded on the predetermined sugar mixture characteristic curve and decomposed into various recycle liquids for further testing;

[0216] B24: Repeat steps B22-B23 until a stable characteristic curve is obtained; the concentration and composition of glucose and fructose in all liquid mixtures remain stable through this further test to conclude the initiation test.

[0217] B3: Steady-state tests were conducted by intermittently delivering various liquids arranged in a specific order using a novel mass transfer method; the steady state was characterized by almost no difference in the concentration and composition of the glucose and fructose mixture in each region during repeated tests.

[0218] Preferably, the various liquids include all the recovered fluids, feed solutions, and elution water from the previously initiated tests in B2.

[0219] More preferably, step B3 further includes the following:

[0220] B31: Based on the collected samples, in the order of collection for each corresponding delivery liquid, decompose and record each required portion of time and generate characteristic curves;

[0221] Preferably, the characteristic curve includes a glucose-rich raffinate, multiple recycled liquid mixtures in a specific order, and an expansion of multiple recycled liquid mixtures by adding liquid mixtures having specific compositions and limited concentrations of glucose-rich raffinate and fructose-rich product solutions recovered from the previous characteristic curve.

[0222] B32: Record the individual composition and concentration of all expanded recirculating liquid mixtures; expand multiple recirculating liquids by increasing the recovered raffinate and products with mixtures having the corresponding composition as recovered raffinate and products.

[0223] Preferably, the dry solids content of the expanded recirculated liquid mixture is 40%-60%. The recovered raffinate and product have high concentrations.

[0224] Preferably, a variety of recycle liquids with stable properties in terms of sugar composition and limited concentration are used, wherein the raffinate is pure glucose at a limited concentration and the product is pure fructose at a limited concentration.

[0225] B33: By intermittently feeding the expanded recirculated liquid mixture in the order of collection, a characteristic curve is generated by further testing. The feed solution is arranged after the glucose content is slightly higher than that of the sugar mixture in the feed solution and before the glucose content is slightly lower than that of the sugar mixture in the feed solution. Then, the remaining unused recirculated liquid is fed in sequence, followed by the elution water, and then the liquid mixture collected first from the characteristic curve.

[0226] B34: Record the portion of the time required to deliver the corresponding liquid from the characteristic curve obtained from B33;

[0227] Preferably, the curved portion includes the raffinate of a glucose-rich solution, a mixture of multiple recycled liquids in a specific order, and the product of a fructose-rich solution.

[0228] B35: If the recovered raffinate and product fail to meet the predetermined purity and concentration, then repeat steps B31-B34 continuously; if the recovered raffinate and product meet the predetermined purity and concentration, then record their respective components and concentrations as an extended range of the recovered liquid characteristics for subsequent use.

[0229] B4: Divide the time required for each portion of the liquid delivery in the obtained characteristic curve by the minimum time interval to obtain the number of dose drops in the device as a specific range for the corresponding liquid input area; the number of overall units, the number of rotations of the upstream and downstream rotary joint modules, and the predetermined minimum time interval Δt allocated to the separation module are not fixed, but depend on the total time taken to complete a characteristic curve divided by the predetermined minimum time interval Δt, thereby simplifying the procedure to the minimum complexity to obtain the best purification results.

[0230] B5: Divide the volume of the liquid by the number of doses to obtain the partial volume required for each dose;

[0231] B6: Divide the amount of resin and partial volume obtained in step B1 by the pre-selected number, and use the volume of the simultaneously received drip dose as the specific area range of the corresponding liquid.

[0232] Preferably, the preselected number corresponds to a set of columns arranged in a single integral unit for simultaneously inputting liquid into each unit.

[0233] Preferably, the number of preselected items is a finite integer greater than 1.

[0234] Further optimization, step B6 specifically includes:

[0235] B61: Assign all the units of each input liquid to their respective liquid regions in sequence, and assign all regions to an infinite format in sequence;

[0236] B62: Prepare a predetermined volume of the corresponding solution and store it in the corresponding tank in the tank module for distribution of this liquid;

[0237] B63: During steady-state operation, various fluids are simultaneously delivered to their respective regions via the device within each minimum time interval. The device has transformed the liquid flow pattern observed in conventional chromatographic separation from parallel to the mobile phase to a perpendicular flow direction; the installed resin is utilized to the maximum extent possible within each minimum time interval Δt of the duration. The differential setting scheme for all types of solutions interacts simultaneously with the resin installed in the overall unit, thereby effectively reducing cycle time compared to chromatography.

[0238] B7: Assign all integral units with each corresponding liquid to a range of specific regions;

[0239] B8: All types of transported liquids are arranged in the same order in a circular circulation pattern in the device;

[0240] Preferably, step B8 further includes preparing the predetermined volume of the series of recirculated liquids recorded in step B35 into the corresponding lower storage tank 44 in sequence, and connecting it together with the pressurized inert gas supply module to support the liquid distribution via the upstream storage tank module 12 as a closed loop, through the upstream rotary joint module, the separation module, and then the downstream rotary joint module, and finally back to the downstream storage tank module 40.

[0241] S3: The single-stage recirculation scheme adopted by the unit uses a new mass transfer method to recover all liquid streams into the lower storage tank 44; the single-stage recirculation scheme adopted by the unit uses a new mass transfer method to simultaneously feed and elute, thereby enabling the simultaneous recovery of raffinate stream, as well as one product stream and multiple recirculated mixture streams.

[0242] A single-stage recirculation scheme is established on the device to simultaneously perform continuous separation and concentration of various fractionated mixtures, reducing the consumption of eluent. The recirculation scheme simultaneously inputs the feed solution, eluent, and other recirculation streams from predetermined tanks into predetermined zones. Each zone, while independent of each other, is interconnected via its respective upstream tank module 12 and downstream tank module 40. Therefore, this invention continuously separates the feed stream into two streams: separating glucose and fructose in the feed solution into a pure composition with 100% recovery, and multiple recirculation streams of a glucose and fructose mixture with stable composition and concentration. Scale-up of the industrial production unit is achieved by replicating single-column test results across multiple differential setups using all modules to obtain the final purification efficiency.

[0243] Preferably, the liquid stream includes a glucose-rich raffinate stream, a fructose-rich product stream, and multiple recirculated liquid streams with stable compositions and specific concentrations.

[0244] The method for recovering the liquid stream includes the following:

[0245] C1: The liquid passes sequentially through the closed-loop downstream storage tank module 40, the upstream storage tank module 12, and the rotation and positioning mechanism in the upstream rotary joint module to complete the mass transfer balance of the separation module, and then returns to the downstream rotary joint module.

[0246] Preferably, step C1 further includes the following:

[0247] C11: The integral unit located in the first position in the separation module receives a predetermined volume of liquid transport, while the other integral units do not receive liquid. The liquid is sequentially and simultaneously transferred from the lower tank 44 to the upper tank 15 and associated with a wide range of pressurized inert gas supplies via the storage device 28.

[0248] Furthermore, the circular multi-valve body I19 is propelled by a servo motor I to rotate a step, and then the received liquid is transferred to the integral unit in the separation module;

[0249] Preferably, the predetermined volume of liquid comprises a plurality of recirculation streams arranged in a specific order, a feed solution, and another plurality of recirculation streams arranged in a specific order, followed by elution water and an inert gas.

[0250] C12: After delivery of various liquids, the liquid is intermittently delivered through a device that alternately supplies two separate, wide-range pressurized inert gas paths to force the dripping dose of liquid to be rapidly discharged through the resin, thereby completing the expected mass transfer contact equilibrium between the solid and liquid phases.

[0251] C13: Maintain a closed vacuum environment, discharge each liquid solution into the corresponding transfer container 38, and keep the resin in a semi-dry state;

[0252] C14: Intermittently collect the discharged liquid from each transfer container 38 and transfer the collected liquid to the lower storage tank 44 via a large-scale pressurized inert gas supply route through the downstream rotary joint module; the circular multi-valve body II 37 advances by a rotation angle along a predetermined rotation direction via the servo motor II, and then pushes all the liquid into the lower storage tank 44 simultaneously through a large-scale pressurized inert gas supply path.

[0253] C15: Repeat steps C11-C14 continuously, while covering the first and second integral units of the liquid receiving module, until the storage container 21 and the transfer container 38 of the first liquid receiving unit are set back to their initial positions, completing one cycle, and the start-up operation is completed.

[0254] Preferably, the various liquids recovered during the start-up operation include water as circulating water, low-dryness solid-phase glucose solutions for other uses, various recovered liquids stored in a specific order, solutions as glucose residues, and solutions as fructose products.

[0255] Further preferably, all types of sugar mixtures in each lower tank 44, except for the retained raffinate and product liquid, are recycled by being transferred to each upper tank 15 in the upstream tank module 12.

[0256] C2: Perform steady-state operation during each time interval of expenditure;

[0257] Furthermore, the steady-state operation includes the following steps:

[0258] C21: Various liquids of a predetermined volume are transported by a liquid transport method using a large-scale pressurized inert gas, while all available liquids from the upper storage tank 15 are transported and forced into the storage container 21; at this time, the circular multi-valve body II 37 advances by a rotation angle along the predetermined rotation direction via the servo motor II, and then transports the liquid to the liquid inlet pipes of each integral unit below by a large-scale pressurized inert gas transport method.

[0259] Preferably, the various liquids comprise multiple recirculation streams arranged in a specific order, a feed solution, and another multiple recirculation streams arranged in a specific order, followed by elution water and an inert gas.

[0260] C22: After delivery of various liquids, the device intermittently delivers the liquid by alternating supply between two separate, wide-range pressurized inert gas paths to force the dripping dose of liquid to be rapidly discharged through the resin, thereby completing the expected mass transfer contact equilibrium between the solid and liquid phases.

[0261] C23: Maintain a closed vacuum environment, discharge each liquid solution into the corresponding transfer container 38, and keep the resin in a semi-dry state;

[0262] C24: Collects various discharged liquids from each transfer container 38 and transfers the collected liquids to the lower storage tank 44 via the downstream rotary joint module through a wide-range pressurized inert gas supply route; the circular multi-valve body II 37 advances by a rotation angle along a predetermined rotation direction via the servo motor II, and then pushes all the liquids into the lower storage tank 44 simultaneously through the wide-range pressurized inert gas supply path.

[0263] Preferably, the various liquids recovered during steady-state operation include water as circulating water, low-dryness solid-phase glucose solutions for other uses, various recovered liquids stored in a specific order, solutions as glucose residues, and solutions as fructose products.

[0264] Further preferably, all types of sugar mixtures in the lower tank 44, except for the retained raffinate and product liquid, are recycled by being transferred to the upper tank 15. The liquid dosage is rapidly introduced through the resin bed installed in the single column 23, and the liquid is discharged through a pressurized inert gas introduced at the top and a vacuum environment at the bottom. As the delivered liquid is discharged through the resin, the expected mass transfer has ended, and all types of processed sugar mixtures of each concentration and composition collected from the bottom of column 23 represent a complete separation cycle.

[0265] In a further preferred embodiment, the raffinate is pure glucose of a limited concentration, the multiple recirculation streams have stable characteristics of sugar composition and limited concentration, and the product stream is pure fructose of a limited concentration.

[0266] In this embodiment, while reducing resin consumption, the feed solution is separated into pure liquid glucose and pure liquid fructose with 100% yield. Simultaneously, by reducing water consumption during elution, the concentration of the product and by-product dry solids percentage is increased. This process is achieved through integrated combination of a new mass transfer method, a differential setting scheme between the resin phase and the liquid phase, an operating scheme, and implementation equipment.

[0267] A novel mass transfer method is implemented using this device to eliminate the displacement zone in conventional chromatographic processes by maintaining the resin installed in column 23 in a semi-dry state. Multiple modules connected sequentially operate independently in a closed loop, simultaneously feeding a feed solution containing glucose and fructose, along with other reflux liquids. Water is eluted to obtain glucose extract and fructose product, and other reflux liquids are recovered. This increases the concentration of the separated mixture and continuously purifies the glucose and fructose in the feed solution to 100% purity, exceeding 51% dry solids, achieving 100% yield. Compared to conventional synchronous moving bed processes with the same feed throughput, this device reduces resin consumption by nearly 40%, while the conventional synchronous moving bed process only purifies fructose to 88% purity in the product stream, with a concentration of 30-35% dry solids and a recovery yield of only 90%.

[0268] For large-scale process design and construction to achieve target feed throughput, to obtain specific glucose and fructose separation; the sizing of specific modules and / or the parallel operation of multiple modules are generally considered as part of the disclosed apparatus and can be understood as a subset of the scalable disclosed apparatus; increasing the number of identical modules or sequentially connected modules as multiple modules operating in parallel in sequence are also within the scope of this invention.

[0269] Example 3:

[0270] Example 2 describes the apparatus for improving the simulated moving bed continuous separation of glucose and fructose, such as... Figure 4 As shown, the method for separating a homogeneous aqueous solution containing glucose, fructose, and oligosaccharides using this apparatus, the differential setting method between the solid phase material and the mobile phase, includes the following steps:

[0271] B101: Sequentially decompose the elution characteristic curves obtained by the new mass transfer method to obtain the time required for each solution, which is the time required for that region. Figure 4 The elution characteristic curve shown indicates that multiple mass transfer phenomena reach equilibrium in sequence, while a mass transfer equilibrium is achieved between a specific mixture of sugar solutions that enters from the top of column 23 rapidly through the resin bed and another combination of sugar mixtures collected from the bottom of column 23.

[0272] Preferably, each solution includes a feed solution, an eluent, and a circulating flow.

[0273] B102: Divide each partial time by the minimum time interval Δt to obtain the number of doses in that region; divide the volume of the liquid by the number of doses to obtain the partial volume required for each dose; divide the amount of resin obtained from complete saturation of the feed solution and the partial volume of this liquid by the preselected number;

[0274] Preferably, the preselected number corresponds to at least one unit in a group of units in each region, so as to simultaneously receive a portion of the volume of such liquid for liquid in each overall unit in the unit group.

[0275] B103: Assign all integral units with their respective solutions to the range of their respective regions in sequence, and assign all regions to an infinite format;

[0276] B104: Arrange all regions in sequence into an infinite loop format, representing a complete separate loop;

[0277] B105: Prepare a predetermined volume of the corresponding solution for storage in the upper tank 15 for this liquid distribution throughout the device to achieve glucose and fructose separation;

[0278] B106: During steady-state operation, this device can simultaneously deliver a mixture of multiple sugars to their respective regions, changing the traditional chromatographic separation path from parallel to the mobile phase flow direction to a perpendicular direction. This is to achieve the separation of glucose and fructose. Figure 4 The text describes how the sugar mixture in the feed stream migrates towards the left side of the elution curve, while fructose migrates towards the right side, to achieve separation. Under steady-state operation in any case, the elution results from the single-column test show that a complete separation cycle is completed after each time spent in all regions. Figure 4 The time taken for a complete separation cycle is displayed in four minutes. Glucose, fructose, and oligosaccharide concentrations are plotted as the percentage of dry solids on the Y-axis and the elution time in minutes on the X-axis. Tests are performed in increments of one minute as the minimum time interval Δt. Figure 4 The percentage of glucose, fructose, and oligosaccharides (abbreviated as oligosaccharides) in dry solids was plotted as a function of elution time in minutes, with pure glucose and pure fructose streams recovered from the feed stream.

[0279] Preferably, all minimum time intervals Δt are simplified using an "ellipse" arranged in an infinite circle in the upstream and downstream rotary joint modules.

[0280] Furthermore, for the purification of the sugar mixture, a start-up operation is required to bring the fresh, semi-dry resin installed in the separation module to an initial equilibrium with each incoming fresh sugar mixture. The start-up operation in step C15 includes the following:

[0281] C151: Through Figure 1-3 The liquid is introduced into the storage container 21 of the device and then enters each of the lower integral units for subsequent mass transfer and balancing processes. The predetermined amount of various liquids are introduced from each upper storage tank 15 starting from zone 0, and then zones 0 and 1 are covered simultaneously. Zones 0, 1 and 3 are covered simultaneously, and zone 4 is covered sequentially. Zone 5 is covered sequentially, and so on until zones 6, 7, feed liquid, zones 8-19, washing water, and inert gas are introduced. After completion, the liquid volume of all available liquids in the covered zones is added sequentially. Then, the rotating mechanism, i.e., the circular multi-valve body I 19, advances one rotation step in the predetermined rotation direction.

[0282] C152: After each delivery of a predetermined volume of various liquids, pressurized inert gas is intermittently supplied between pipe 30 and pipe 9 to force the dripping liquid to be rapidly discharged from the resin bed in order to achieve the expected mass transfer contact equilibrium between the two phases.

[0283] C153: Maintain the vacuum environment inside the vacuum chamber 31, continuously discharge each liquid solution into its respective reservoir 33 below, and keep the resin in a semi-dry state.

[0284] C154: Intermittently collect the discharged liquid in each reservoir 33 and transport it to the transfer container 38. Through the rotation mechanism, i.e., the circular multi-valve body II 37, it advances one step in the predetermined rotation direction and then enters each designated lower reservoir 44. The predetermined volume of liquid is transported from the lower reservoir 44 to the designated upper reservoir 15 through the connecting pipe.

[0285] C155: Repeat steps C151-C154 for zone 0, then “zone 0 together with zone 1”, until storage container 21 and transfer container 38 in the downstream rotary joint module return to their initial positions. After completing one rotation, the startup operation can be ended.

[0286] Preferably, the various liquids recovered during startup include water for recycling, low-dry-solids glucose solution for other uses, and the circulating flow in zones 0-19, where zone 2 collects residual glucose solution and zone 15 collects fructose product solution; such as Figure 1-2 As shown, all types of sugar mixtures, except for residual liquid and product, are distributed from the lower storage tank 44 and transported via connecting pipes to each corresponding storage tank 15 for recirculation.

[0287] After the start-up operation is completed, the operation transitions to steady state. During the time allocated to each region, multiple storage containers 21 simultaneously receive all available predetermined amounts of various liquids and simultaneously deliver them to their respective integral units for a new mass transfer method in the separation module. The specific sugar mixture discharged from the bottom of each integral unit is obtained in order to start the next steady state operation.

[0288] Furthermore, steady-state operation repeatedly includes the following identical process:

[0289] C211: Through Figure 1-3 The liquid transport method shown in the figure simultaneously transports all available liquids of a predetermined volume from each of the lower storage tanks 15 and the inert gas in the final zone to the storage container 21. Then, through a rotation mechanism, the circular multi-valve body I 19 advances one rotation step in a predetermined rotation direction and then enters each of the lower integral units for the subsequent mass transfer and balancing process.

[0290] Preferably, the liquid includes zones 0, 1, 3-7, feed liquid, zones 8-14, 16-19, and elution water.

[0291] C212: After each delivery of a predetermined volume of various liquids, pressurized inert gas is intermittently supplied between pipe 30 and pipe 9 to force the dripping liquid to be rapidly discharged from the resin bed in order to achieve the expected mass transfer contact equilibrium between the two phases.

[0292] C213: At the same time, maintain the vacuum environment inside the vacuum chamber 31, continuously discharge each liquid solution into its respective reservoir 33 below, and keep the resin in a semi-dry state.

[0293] C214: Intermittently collect various discharged liquids from each reservoir 33 and transport them to the transfer container 38. Through a rotation mechanism, the circular multi-valve body II 37 advances one rotation step in the predetermined rotation direction and then enters the lower storage tank 44.

[0294] Preferably, the recovered liquids include water for recycling, low dry solids glucose solution for other uses, and recovery streams in zones 0-19, of which zone 2 collects glucose residue solution and zone 15 collects fructose product solution.

[0295] C215: All types of sugar mixtures, excluding raffinate and product, are synchronously transferred from the lower tank 44 via connecting pipes to each corresponding upper tank 15 for recycling. All steady-state operation repetition procedures are synchronously completed during the consumption period accumulated at each minimum time interval Δt, which synchronously covers steps C211-C214. Figure 4The minimum time interval Δt specified in the figure represents the elution curve obtained from a single unit study. By implementing a new mass transfer method and a differential setting between the two phases on the device, every four minutes spent in each specific liquid zone corresponds to one separation cycle. This invention has shown that the conventional mass transfer path occurring in chromatography, typically parallel to the liquid flow direction, has been transformed to be perpendicular to the flow direction. An aqueous feed solution is introduced through a connecting pipe located between the circulating flows in zones 7 and 8, wherein the glucose content of the feed solution is slightly lower than that in zone 7 and slightly higher than that in zone 8. Therefore, through steady-state operation of various aqueous circulating flows, the sugars contained in the feed solution migrate to zone 2, are recovered as a raffinate stream of pure glucose, and migrate horizontally towards zone 15, recovering the pure fructose product stream. Furthermore, the aqueous feed solution requires additional time in conventional chromatography to exit the so-called displacement zone, where the separation of sugar components occurs with the flow of a large volume of liquid. This invention demonstrates that this displacement zone can be eliminated, thus significantly reducing the cycle time to 4 minutes. Consequently, the amount of resin loaded, elution water consumption, and other unspecified operating costs can be proportionally reduced. Figure 4 It can be seen that, compared with traditional chromatography, the reduction in cycle time in this invention means a reduction in resin consumption.

[0296] like Figure 6 As shown, Figure 6 The text emphasizes a single-stage recirculation process for sugar solution separation arranged in a ring, and further illustrates the parallel operation of multiple separation modules using three such modules as an example.

[0297] Taking three separation modules as an example, the following illustrates a steady-state operation scheme for multiple separation modules operating simultaneously in parallel, thereby enabling the simultaneous and continuous separation of a glucose and fructose mixture, as detailed below:

[0298] (1) Various circulating mixtures in zones 0-1, 3-14, and 16-19 of a predetermined volume are output from the downstream storage tank module 40 through each connecting pipe to the corresponding upper storage tank 15, except for glucose residue in zone 2 and fructose product in zone 15; the lower storage tank 44 is arranged in a ring in the hollow sleeve 41 and is equipped with manifolds F42 and G43 for water circulation to maintain the multiple lower storage tanks 44 within a selected temperature range;

[0299] (2) The recovered liquid is transported to the corresponding upper storage tank 15 through each connecting pipe. Each upper storage tank 15 is arranged in the same circulation pattern. It is installed in the insulating jacket 11 and equipped with manifold A13 and manifold B14 for water circulation.

[0300] (3) Transfer the designated circulating flow of the entire predetermined volume from each upper storage tank 15, and simultaneously transport it from zone 0-1, zone 3-7, feed solution, zone 8-14, zone 16-19, washing water and inert gas to the upstream rotary joint module.

[0301] Preferably, the circular multi-valve body I 19 includes multiple top-side liquid transfer and storage containers arranged in a ring and installed at predetermined positions to simultaneously receive a predetermined volume of liquid transferred from the specific storage tank above to the storage container 21; the circular multi-valve body I 19 is equipped with an equal number of liquid outlet conduits 22 for accurately transferring all types of liquids through manifolds O79 located above the top of the corresponding separation modules, so as to simultaneously transfer and inject the predetermined volume of liquid into the top of each corresponding integral unit of the module operating in parallel. After the top-side liquid transfer tank has received all the liquid solution, the circular multi-valve body I 19 advances one rotation step in a predetermined rotation direction by a servo motor I.

[0302] (4) The liquid enters multiple separation modules operating in parallel via the outlet conduit 22:

[0303] 4A: Each integral unit in the separation module includes multiple columns 23, each column 23 housing a top inlet end 24 and a bottom mesh filter 25. All integral units in each separation module are arranged in a ring within an insulating water circulation jacket 36. The jacket 36 is equipped with multiple vertically mounted baffles to confine each integral unit in the separation module to a single predetermined compartment. These baffles, arranged alternately as instructed, allow water to freely enter from one inlet and flow out from the next outlet into the next compartment. Warm water enters the corresponding jacket 36 through manifold C26, freely passing through the first integral unit in the separation module, then continuing into the second integral unit, the third integral unit, and so on, until the water flows through all the confined integral unit compartments before exiting from manifold D27. Figure 6 As shown, this is to maintain all the integral units installed in the mezzanine sleeve 36 within a predetermined temperature range for multiple separate modules operating in parallel.

[0304] 4B: A specific liquid [only six such pipes are shown in the figures for simplicity] is delivered via the liquid outlet conduit 22 to each manifold O79 above the top of the monolithic unit to distribute the liquid equally through the nozzle 29 of each monolithic unit to wet a portion of the resin contained in each monolithic unit, and inert gas is delivered intermittently and simultaneously via the integrated inert gas supply module to force out the delivery liquid dose through the resin to achieve the expected mass transfer contact balance between the two phases.

[0305] 4C: Maintain a closed vacuum environment at the bottom of each integral unit of the corresponding separation module operating in parallel to drain specific liquids into the corresponding transfer container 38 below and keep the resin in a semi-dry state.

[0306] 4D: Integrated inert gas supply module, each separation module operates in closed loop, and the vacuum environment is uniformly applied to the entire bottom of multiple separation modules operating in parallel by a central vacuum pump 51.

[0307] Preferably, the inert gas supply module includes a manifold P84 disposed around the bottom of each integral unit of each separation module, connected via each outlet pipe 48 to the respective separation modules operating in parallel, to extract moisture-rich wet inert gas. The wet inert gas is first converted to dry inert gas by an atomizer 50, while the water is collected in a water reservoir 52 for recycling. A vacuum is applied around the bottom of each integral unit to keep the resin in a semi-dry state to meet the standards of the new mass transfer method. Heterogeneous contact is generated when the liquid rapidly passes through the stationary resin particles to achieve mass transfer equilibrium. The dry inert gas exiting the atomizer 50 is mixed with pressurized dry air and fresh dry inert gas is obtained by deployment through an inert gas generator 54 and stored in a steel tank container 55, maintained at a wide range of pressure levels. By means of an embedded heater 56 and a manifold L57 deployed above the top of each integral unit, all kinds of liquids in the drip dose are rapidly discharged to achieve mass transfer balance through the solid phase, and the liquid collected by the resin in the transfer container 38 at the bottom of each integral unit is returned to the downstream storage tank module 40.

[0308] (5) The liquid discharged from the bottom of each integral unit in the parallel-operating separation module is collected intermittently; the liquid is transferred to the downstream rotary joint module through the liquid conduit 34 set below the bottom of each specific integral unit of the separation module. The downstream rotary joint module is equipped with a circular multi-valve body II 37. The circular multi-valve body II 37 includes multiple top-side liquid transfer containers 38 arranged in a ring shape, installed in a predetermined position, for receiving the liquid transferred from the storage 28 above the parallel-operating separation module. The bottom side of the circular multi-valve body II 37 is provided with an equal amount of output conduit 39 to accurately deliver the liquid. After the top-side storage 28 has received all the liquid solution, the circular multi-valve body II 37 moves forward one rotation step in the predetermined rotation direction by the servo motor II.

[0309] (6) Figure 6 As shown, the liquid stored in the downstream rotary joint module is transported through the output conduit 39 and enters each designated lower storage tank 44 in the downstream storage tank module 40.

[0310] The recovered liquids include water for recycling, low dry solids glucose solution for other uses, and recovery streams in zones 0-19, where zone 2 collects glucose residue solution and zone 15 collects fructose product solution. Downstream storage tank modules 40 are arranged in the same annular form and installed in hollow sleeves 41, which are equipped with manifolds F42 and G43 for water circulation to maintain the entire plurality of lower storage tanks within a selected temperature range.

[0311] In this invention, the amount of resin installed in each monolithic unit corresponds to the amount of resin in the mass transfer zone (MTZ) during chromatographic operation, which is directly related to the resin's maximum adsorption capacity under semi-dry conditions. Guided by this novel mass transfer method, the adsorption capacity is independent of the concentration (dry solids%) of the sugar mixture in the feed aqueous solution; in fact, it depends only on the absolute weight of the adsorbed sugar and the resin's adsorption capacity. Therefore, the input range of the feed solution can be from 10% to 70% dry solids. In this invention, 60% dry solids is used for predetermined conditions and demonstrations in single monolithic unit experimental testing, as 60% dry solids is most commonly used in SMB processes. Generally, a higher dry solids percentage concentration in the feed solution is better, as the volume to be processed is smaller.

[0312] The consumption of deionized water is independent of its fluid dynamics; however, conversely, fluid dynamics, including flow rate and flow pattern, are crucial in chromatographic operations. This is because the separation parameters of the target system are directly derived from the predetermined elution curve and can be well achieved by the equipment. The amount of elution water consumed directly affects the elution completion rate. The equipment can manage the rates of various fluids in the fastest and most efficient way to achieve elution in each zone in the shortest possible time. This water consumption was directly calculated through research and experiments using a new mass transfer method based on 100% resin utilization and the absolute weight of the maximum adsorbed sugar in the resin. Water recovered from the wet inert gas at the outlet of the aerosol separator 50 and... Figure 5 The water recovered in Zone 0 shown can be reused, which can be deducted from the total water consumption.

[0313] In this embodiment, the novel mass transfer method of this invention is employed, using vacuum to remove fluid between resin particles, thus keeping the resin in a semi-dry state at all times. Problems that may hinder separation efficiency in current chromatographic operations, such as the widely used SMB, and further exacerbate issues like fluid flow dynamics, resin sieve size related to pressure loss, and mass transfer resistance related to adsorption sites in porous resins, are irrelevant in this invention. This is solely because removing fluid between resin particles by vacuum maximizes the area available for mass transfer, thereby allowing ligand exchange equilibrium and elution of sugar components in the most efficient manner. This invention selects a calcium-based strong acid cation exchanger to directly compare the bottom-line economic efficiency of this invention with conventional methods in terms of resin and elution water consumption. Generally, it is preferable to use resin particles with smaller sieve sizes to have a larger usable mass transfer contact area, as pressure loss is less important in this invention. The operating temperature is preferably in the range of 60-85°C to prevent microbial growth, thereby reducing viscosity and facilitating the flow of the sugar mixture during recovery.

[0314] Figure 5 To achieve a preferred configuration of twenty-four zones on the device via a differential scheme, for the input of the feed solution, sugar mixtures, various recycled sugar mixtures, and elution water; a single-stage recovery scheme for increasing the concentration of the separated products is further described.

[0315] Figure 5 The complete liquid separation cycle process is outlined, based on a minimum time interval Δt of one minute, with each zone having a 4-minute interval or a total of 24 zones arranged sequentially to reflect... Figure 4 The elution curves were derived from the data.

[0316] Experimental Example 1:

[0317] The feed solution is high-fructose corn syrup from a domestic corn refinery, consisting of 43.05% fructose, 51.09% glucose, and the remainder oligosaccharides, with a dry solids concentration of 71.1%. This homogeneous aqueous liquid mixture is diluted with dust-free deionized water to 60% dry solids.

[0318] The resin is Dowex Monosphere 99, a calcium-based strong acidic cation exchanger with an average particle size of 320 μm x 10 μm.

[0319] Single-column tests were conducted on aqueous feed solutions from domestic corn refineries and resins of the same specifications as SMB. These tests demonstrated a significant difference in mass transfer phenomena between this invention and other chromatographic operations.

[0320] Column 23 has an inner diameter of 1.27 cm and a height of 203.2 cm, and is installed in a water-circulating environment at 65°C. The total height of the resin packed in column 23 is 190.5 cm, and the bed volume is 241 cc [the resin packed in conventional chromatography is water-saturated]. The new mass transfer method is performed with a 27-inch mercury column vacuum applied to the bottom of column 23 to continuously remove interparticle fluid.

[0321] The feed solution, recirculated flow, and elution water transfer reservoirs are equipped with a 65°C water-circulating insulating jacket 11. For a very short duration, all liquid inputs are delivered in the form of a predetermined volume of liquid, simulating a pulse input SI, via a rapid stroke of the liquid pipette. A hermetically sealed, easily detachable bottle is installed at the bottom of column 23 for collecting samples at predetermined time intervals, i.e., a minimum time interval Δt. An atomizer 50, installed between the bed and the central vacuum pump 51, recovers vapors from the circulating cooling water jacket, collecting condensate from a bottle installed below the cooling water condenser. Between each liquid delivery, pressurized inert gas is supplied from the top of column 23 to combine with the vacuum at the bottom of column 23 for rapid liquid discharge.

[0322] The above experimental features simulate a new mass transfer method, and are based on, for example... Figure 1-6 The apparatus of the present invention shown is used to simulate inputs, including feed solution and eluent and various sugar mixtures from upstream tank module 12, for precise liquid distribution via upstream rotary joint module, for separation by separation module integrated with inert gas supply module, for further liquid discharge via downstream rotary joint module, and finally for further liquid distribution via downstream tank module 40 at each time interval; for convenience, pressurized air is used instead of pressurized inert gas for subsequent single-column studies.

[0323] Figure 9-13 The composition of the pre-determined liquid flow in the region is derived from the recovered raffinate and product liquid from the previously described cycle, wherein, Figure 12 This indicates that the product stream with increased concentration was recovered from region 13. Figure 13 This indicates that the product stream with increased concentration and near-pure quality was recovered from zone 15. Figure 13 The elution characteristic curve shown was converted to... Figure 4-6 The example shown is of 24 distribution regions set in the time domain, which integrate the above-described new mass transfer method, the differential setting scheme between the resin phase and the liquid phase, and the single-stage recirculation scheme in which the device of the present invention is used.

[0324] Experimental Example 1-1:

[0325] Appendix Figure 7 The following are the characteristic curves of four cycles performed under the new mass transfer method, based on the conditions of Experimental Example 1, with steady state reached in cycle 4:

[0326] In this study, the sample from each cycle was plotted as dry solids % concentration on the Y-axis, while the cumulative sample volume was converted to bed volume % on the X-axis. For the first cycle, 60 cc (25% of bed volume) of feed solution was introduced at a dose of 2.5 cc / dose for 10 seconds per minute for 4 minutes. A total of 24.8 cc of water was collected as sample #1, containing mostly oligonucleotides, representing 2-4% of the minor components in the feed solution. This phenomenon is not typically observed in typical chromatographic operations, primarily because column 23 is already water-saturated, and introducing additional water after the MTZ further weakens the adsorbed glucose and fructose, causing them to dissolve rapidly back into the surrounding mobile phase, i.e., water. Typical SMB processes use this well-known phenomenon as the basis for separation in current corn syrup industry purification because the resin is installed in the bed of column 23, where fructose has a stronger binding affinity than glucose. In contrast, the new mass transfer method continuously removes the water component while maximizing the binding affinity between the installed resin and the sugar components originally present in the aqueous feed solution, resulting in rapid elution of oligonucleotides.

[0327] In addition, in the above Figure 1-3 The novel mass transfer method executed via pulsed input SI in the separation module further enhances the difference in binding affinity between glucose and fructose through the input circulating flow and the input homogeneous aqueous feed. The elution water in the single-stage scheme is because water is a component of this aqueous liquid stream. When various sugar solutions are introduced at the top of each unit of the separation module, the sugar components bind to the resin, and these water components rapidly pass through the resin bed, further pulling the glucose profile ahead of the fructose profile to achieve a better mass transfer equilibrium than observed in chromatographic operations. Typical chromatographic schemes, such as SMB, use elution water as the basis for separation, but to some extent produce the opposite effect, leading to a deterioration in separation efficiency.

[0328] The main difference between this invention and all other conventional chromatographic operations lies in its significant maximization of resin adsorption capacity. The apparatus of this invention is completely independent of flow kinetics, allowing the resin to better increase this binding capacity and improve separation efficiency. This advantage, benefiting from the novel mass transfer method, will be further illustrated in the following examples using a multi-zone, single-stage recirculation scheme.

[0329] The solution collected from sample #1 is in region 1. After the feed solution is input, water elution is performed through the following three forms of pulse input SI, and the sample is collected.

[0330] The first input format covers a water dose of 1.0 cc delivered every 20 seconds, which is a total of 3 doses delivered every minute. For simplicity, this pulse input SI can be represented as ((1.0 cc / 20 sec.) * 3 / min), with a total water input interval of 3 cc per minute;

[0331] The second type of pulse input SI format can be expressed as ((1.0cc / 10 seconds)*6 / minute), that is, 6cc every minute, 6 times a dose of 1cc every 10 seconds;

[0332] The third pulse input SI format can be expressed as ((1.5cc / 10 seconds)*6 / minute), that is, the interval between six doses of 1.5cc every 10 seconds is 9cc / min; for the sake of simplicity, the detailed combination of input formats is omitted below.

[0333] The main adjustment involves regulating the input rate of elution water per unit time to ensure that most of the glucose is eluted as the leading peak, while delaying the fructose peak to place it further away from the glucose peak. As shown in cycle 1, the collected sample is selectively combined into solutions in zones 1-6 and retained as the input solution for the next cycle. The cycle time is 30 min, consuming 157 cc of elution water and collecting 17 cc of condensate. The input sequence for cycle 2 is: zones 2, 3, 4, 60 cc feed solution, then zones 5, 6, 124.8 cc elution water, and finally the solution from zone 1. The feed solution is always transferred between two zones, with zone 4 having a slightly higher glucose content than the feed solution, while zone 5 has a slightly lower glucose content. The cycle time is increased to 36 min, and 21 cc of condensate is collected.

[0334] The elution curve of cycle 2 shows a very pure glucose region in the initial peak (region 2) and a very pure fructose mixture in the fructose peak (region 5). Similarly, the combined sample, such as the solutions from regions 1-6, is retained as the input solution in cycle 3. Following the same composition order as in cycle 2, the solution consists of regions 2-4, 60 cc feed solution, regions 5, regions 6, 125 cc eluent water, and the solution from region 1, with a cycle time of 36 min and a collection of 18 cc of condensate. Both sugars in the feed solution stably migrate to regions 2 (as a glucose-rich solution) and 5 (as a fructose-rich solution). Only the solution from region 2 in cycle 3 is retained as the raffinate. The remaining solutions are sequentially input into cycle 4 as region 3, 60 cc feed, 4, 5, 6, 90 cc eluent water, and the solution from region 1, with a cycle time of 36 min and a collection of 9 cc of condensate.

[0335] Table 1 lists the raffinate from region 2 as a glucose-rich solution and the product from region 5 as a fructose-rich solution. The recovery rate % for each sugar is defined as the weight percentage of the recovered sugar relative to the original pure components in the feed solution, and the percentage of each sugar is defined as the weight of that sugar in the total recovered amount.

[0336] Table 1:

[0337] area Total output g Dry solids % Recovery rate % glucose% fructose% 2 25.7318 27.58 83.79% glucose 81.14 18.86 5 17.0599 19.41 81.25% fructose 10.74 89.26

[0338] Experimental Example 1-2:

[0339] Appendix Figure 8 The elution curves shown represent the elution curves from the attached... Figure 7 The fifth cycle of the extended cycle, as shown, had the same liquid input sequence as cycle 4, except that zone 5 was retained as the product, i.e., zone 3, 60 cc feed liquid, zone 4, 6, 96 cc eluent, and zone 1 solution, with a cycle time of 37 min. Again, the solution collected from zone 2 was retained as a glucose-rich raffinate, and the solution collected from zone 5 was retained as a fructose-rich product. The results, shown in Table 2, indicate that a steady state had been reached, with constant composition and concentration.

[0340] Table 2:

[0341] area Total output Dry solids % Recovery rate % glucose% fructose% 2 24.3698g 31.40 78.80% glucose 81.12 18.82 5 16.9526g 31.20 86.06% fructose 13.8 86.20

[0342] As can be seen from the above, the elution curves remain stable after several cycles because the predetermined number of regions, composition, and concentration of the input liquids (including feed volume, eluent, and recirculation flow) remain constant. The elution curves obtained through the above single-column studies indicate that the aforementioned mass transfer equilibrium is reached sequentially between specific sugar solution mixtures passing through the resin bed, and furthermore, the sugar mixture collected from the bottom of the column represents another equilibrium composition.

[0343] The following Experiments 1-3 to 1-5 demonstrate how to create a target scheme by using only the necessary amount of resin to achieve the final purity of the raffinate and product while simultaneously increasing the product concentration. This resin usage is directly related to a specific cycle time. This scheme constructs a steady-state elution curve by adding two regions with a concentration range between 40% and 60% dry solids to the current curve. The composition of these regions is predetermined based on the composition of the recovered raffinate and product stream from the previous curve. By expanding the number of regions—meaning increasing the number of two recirculation streams in the next elution curve—the purity and concentration of the separated raffinate and product stream can be improved. Therefore, the amounts of the original glucose and fructose in the feed solution mixture continuously migrate towards opposite ends of their respective curves through the recirculation streams until their respective pure sugar components are obtained.

[0344] Experimental Examples 1-3:

[0345] like Figure 9 As shown, liquids were collected from a total of nine zones, with the liquid input sequence being: zones 3 and 4 (60 cc feed liquid), zones 5 and 6 (20 cc feed liquid), zone 7 (24 cc eluent), zone 9 (120 cc elution water), and zone 1. The predetermined sugar concentration of all liquid streams was between 5% and 60% dry solids, and the composition was... Figure 8 The results showed that the total input volume of the other unspecified recirculation stream was 30 cc, and a total of 10 cc of condensate was collected over a total circulation time of 50 minutes. Figure 8 The results shown are similar, with the raffinate recovered as a glucose-rich solution from zone 2 and the product recovered as a fructose-rich solution from zone 8. By incorporating the three added zones into the previous elution curve, the cycle time was increased from 36 min to 50 min, further promoting the migration of glucose and fructose to the ends of their respective curves through the addition of these zones. Table 3 lists the composition and concentration of the recovered raffinate and product, demonstrating better separation results than the six-zone approach.

[0346] Table 3:

[0347] area Total output Dry solids % Recovery rate % glucose% fructose% 2 22.2852g 29.20 90.40% glucose 89.61 10.39 8 19.8856g 35.80 90.30% fructose 10.58 89.42

[0348] To avoid repetition, the following describes the general conditions relevant to the following examples, from which the following can be developed. Figure 4 The separation process is shown. The test column dimensions are an inner diameter of 0.95 cm and a column height of 206 cm. Resin is filled to a column height of 195.6 cm, resulting in a total bed volume of 139.6 cc. Since the bed volume is smaller than that in the previous example, a feed volume of 36 cc is delivered in each example; however, this 36 cc corresponds to 25.8% of the resin bed volume. Other conditions remain unchanged as in the previous example.

[0349] Experimental Examples 1-4:

[0350] like Figure 10 As shown, liquids from a total of 11 zones were collected, with the liquid input order being zones 3, 4, 5, feed liquid, zones 6, 7, 8, 9, 24 cc from zone 11, 63 cc of eluent, and zone 1. The total input of other unspecified predetermined recirculation streams was 18 cc. A total of 3 cc of condensate was collected. Zones 3 and 9 were addition zones, having compositions of the two sugars specified in Table 3 as for zones 2 and 8, respectively, and each having a predetermined concentration of 53% dry solids. The other recirculation streams from zones 3-7 and 9 used in Experimental Examples 1-3 were renamed zones 4-8 and 11, respectively, with their compositions and concentrations remaining unchanged as shown in the liquid inputs, and the components were... Figure 9The results were as follows. The raffinate, rich in glucose, was recovered from region 2, and the product, rich in fructose, was recovered from region 10. By incorporating both addition regions into the previous elution curve, the cycle time was increased from 50 min to 60 min, further promoting the migration of glucose and fructose through the addition of these regions. Figure 10 The ends of the respective glucose and fructose curves are shown. Table 4 lists the composition and concentration of the recovered raffinate and products, indicating better separation results than the nine-zone scheme.

[0351] Table 4:

[0352] area Total output Dry solids % Recovery rate % glucose% fructose% 2 13.8567g 31.23 93.44% glucose 95.43 4.57 10 12.1267g 32.58 94.69% fructose 6.88 93.12

[0353] Experimental Examples 1-5:

[0354] like Figure 11 As shown, the results of liquid collection from a total of thirteen zones are as follows: the order of liquid input is zones 3-6, feed liquid, zones 7-11, 24 cc of eluent from zone 13, 63 cc of eluent from zone 1, and zone 1. The total input of other unspecified predetermined recycle streams remains 18 cc. A total of 3 cc of condensate is collected. Zones 3 and 11 are additive zones, which have the compositions of the two sugars specified in zones 2 and 10 of Table 4, and each has predetermined concentrations of 48% and 55% dry solids, respectively. The recycle streams from zones 3-7, 9, and 11 used in Experiments 1-4 are renamed zones 4-8, 10, and 13, respectively, with the same composition and concentration as shown in the liquid inputs, and the components are... Figure 10 The results showed that the raffinate, rich in glucose, was recovered from region 2, and the product, rich in fructose, was recovered from region 12. By incorporating both addition regions into the previous elution curve, the cycle time was increased from 60 min to 68 min, further promoting the migration of glucose and fructose through the addition of these regions. Figure 11 The ends of the respective glucose and fructose curves are shown. Table 5 lists the composition and concentration of the recovered raffinate and products, indicating better separation results than the Zone 11 scheme.

[0355] Table 5:

[0356] area Total output Dry solids % Recovery rate % glucose% fructose% 2 14.1856g 34.53 96.50% glucose 97.60 2.40 12 12.4183g 32.58 98.06% fructose 5.83 94.17

[0357] The following Experimental Examples 1-6 to 1-7 increase the product concentration level from the typical SMB process of 30-35% dry solids to 50-55% dry solids. The higher concentration level also improves the purity of the product. The same approach can also be applied to the region where a predetermined glucose is added in order to improve the concentration and purity of the raffinate.

[0358] Experimental Examples 1-6:

[0359] like Figure 12 As shown, the results of liquid collection from a total of 15 zones were obtained, with the liquid input order being zones 3-6, feed liquid, zones 7-12, 14, 21.6 cc of zone 15, 62 cc of eluent, and zone 1. The total input of other unspecified predetermined recirculation streams was 18 cc, and a total of 5 cc of condensate was collected. Slightly different from the previous examples, zones 12 and 14 are newly added zones. Zone 12 has the composition of two sugars as specified in Table 5, with a concentration of 55% dry solids, and zone 14 has a composition of 100% fructose with a concentration of 33% dry solids. The composition and concentration of the recirculation streams in zones 3-7, 9, and 11 used in Experimental Examples 1-5 are the same as the indicated liquid inputs, and the composition is... Figure 11 The results. Except for region 13 being renamed region 15, from... Figure 12 It can be seen from the above that... Figure 11 The diagram shows a slight difference: the raffinate, as a glucose-rich solution, is recovered from region 2, and the product, as a fructose-rich solution, is recovered from region 13, the third-to-last region. The cycle time is increased from 68 min to 76 min because the two addition regions are merged into the previous curve to enhance the improvement only for fructose, thus further migrating towards the end of the fructose curve through the addition regions. Table 6 lists the composition and concentration of the recovered raffinate and product, indicating that the increased concentration of the product results in better separation compared to the thirteen-region scheme. Figure 12 As shown, the product concentration was increased from the typical 30-35% dry solids in the SMB process to 52% dry solids.

[0360] Table 6:

[0361]

[0362]

[0363] Experimental Examples 1-7:

[0364] like Figure 13As shown, a total of 17 liquid samples were collected, with the liquid input order being zones 3-7, feed liquid, zones 8-14, 22.5 cc of zone 16, 25.2 cc of zone 17, 58.5 cc of eluent, and zone 1. The total input of other unspecified predetermined recovery streams remained 18 cc. A total of 5 cc of condensate and 10.8 cc of water from zone 1 were recovered, resulting in a net water consumption of 42.7 cc. Therefore, the volume ratio to the 36 cc feed liquid was 1.19. Again, slightly different from Experimental Examples 1-6, zone 3 was an additive zone with the composition of two sugars as specified in zone 2 of Table 6 and a predetermined concentration of 45% dry solids; zone 14 was another additive zone with a composition of 95% fructose and 5% glucose in 55% dry solids. The other recirculation flows used in regions 3-12, 14, and 15 of Experiments 1-6 were renamed regions 4-13, 16, and 17, respectively, with the composition and concentration remaining unchanged as shown in the liquid input, and the composition being... Figure 12 The results from... Figure 13 Region 2 was used to recover the raffinate as a glucose-rich solution, and Region 15 was used to recover the product as a fructose-rich solution. By incorporating both addition regions into the previous elution curve, the cycle time was increased from 76 min to 86 min, further promoting the migration of glucose and fructose towards the ends of their respective curves. Table 7 lists the composition and concentration of the recovered raffinate and product, demonstrating that final separation results were achieved with increased concentrations of both raffinate and product. Figure 13 As shown, the concentration of almost pure fructose products increased to over 51% dry solids.

[0365] Table 7:

[0366]

[0367]

[0368] from Figure 4 As can be seen from the present invention, the device can continuously recover pure glucose extract with a concentration range of 30.0-40.0% dry solids from zone 2 and pure fructose product from zone 15, thereby increasing the concentration range of the product to 50.0-58.0% dry solids.

[0369] Experimental Examples 1-8:

[0370] The SMB process can process 200 gallons of 60% dry solids feed per minute. A typical industrial SMB process unit is designed with four columns, each with an inner diameter of 14 feet and a height of 27.5 feet, each column loading 4,125 cubic feet (30,855 gallons), for a total resin stock of 123,420 gallons. SMB requires an input rate of 350 gallons of eluent per minute to recover 88% of fructose, resulting in a purity of 90% fructose and 10% glucose. A direct comparison between the SMB process and the currently disclosed process is based on resin stock and eluent consumption at the same throughput and feed composition. As mentioned above, with a water-to-feed volume ratio of 1.19, 238 gallons of eluent are required based on a 200-gallon throughput, representing 68% of the water consumption of the conventional SMB process (350 gallons).

[0371] The feed rate to bed volume ratio is 0.258. Figure 4 The cycle time in this process is 96 minutes, which is 96 minimum time intervals Δt. The resin stock required for a 96-minute cycle time is calculated by dividing 200 by 0.258 and then multiplying by 96, equivalent to 74,419 gallons to handle a feed throughput of 200 gallons per minute. Compared to the 123,420 gallons consumed in the SMB process, the resin stock calculated using 123,420 gallons represents 60.3% based on a similar feed throughput. Furthermore, the excellent separation results demonstrated in previous experimental examples are clearly directly related to this cycle time and form the basis for calculating the resin feed required for this apparatus and method.

[0372] The above description is only a preferred embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Any equivalent substitutions or modifications made by those skilled in the art within the scope of the technology disclosed in the present invention, based on the technical solution and inventive concept of the present invention, should be covered within the scope of protection of the present invention.

Claims

1. An apparatus for improving the continuous separation of glucose and fructose in a simulated moving bed, comprising an upstream storage tank module (12), an upstream rotary joint module, a separation module, a downstream rotary joint module, a downstream storage tank module (40), and an inert gas supply module, characterized in that, The upstream storage tank module (12), the upstream rotary joint module, the separation module, the downstream rotary joint module, the downstream storage tank module (40), and the inert gas supply module operate in parallel; The upstream storage tank module (12) includes multiple insulating jackets (11) and an upper storage tank (15) disposed inside the insulating jackets (11); The upstream rotary joint module includes a circular multi-valve body I (19) driven by a servo motor I, multiple storage containers (21) disposed on the top surface of the circular multi-valve body I (19), and multiple liquid outlet conduits (22) disposed on the bottom surface of the circular multi-valve body I (19). The separation module includes multiple integral units disposed inside the interlayer sleeve (36) and multiple columns (23) disposed inside the integral units; The downstream rotary joint module includes a circular multi-valve body II (37) driven by a servo motor II, multiple transfer containers (38) disposed on the top surface of the circular multi-valve body II (37), and multiple output conduits (39) disposed on the bottom surface of the circular multi-valve body II (37). The downstream storage tank module (40) includes multiple hollow sleeves (41) and a lower storage tank (44) disposed inside the hollow sleeves (41); The inert gas supply module includes a closed vacuum environment loop, an upstream wide-range inert gas supply loop, and a downstream wide-range inert gas supply loop connected in sequence to form a closed loop; the inert gas is one or a mixture of two or more of nitrogen, carbon dioxide, and argon; the wide-range pressure level of the inert gas is 40-90 psi, the low-range pressurized inert gas pressure level is 40-55 psi, the medium-range pressurized inert gas pressure level is 55 psi and 70 psi, and the high-range pressurized inert gas pressure level is 75-90 psi; A method for continuously separating glucose and fructose using this apparatus includes the following steps: S1: To provide a new mass transfer method to eliminate the displacement region and further utilize it; S2: Differential setting scheme used between resin and various types of liquid; S3: The single-stage recirculation scheme adopted by the device uses a new mass transfer method to recover all liquid flow into the lower storage tank (44); The replacement zone is the amount of resin installed in each column (23), where the resin is fully adsorbed to saturation by a predetermined input volume of feed solution, and the amount of resin installed is kept in a semi-dry state.

2. The apparatus for improving the continuous separation of glucose and fructose in a simulated moving bed according to claim 1, characterized in that, The insulating jacket (11) includes manifold A (13) and manifold B (14); Each of the upper storage tanks (15) is provided with an inlet conduit (16) that penetrates the outer wall of the insulating jacket (11) on its top surface; and each of the upper storage tanks (15) is provided with an outlet conduit (17) that penetrates the outer wall of the insulating jacket (11) on its bottom surface. The bottom end of the inlet conduit (16) is provided with a baffle a (1), the top surface of the upper storage tank (15) is provided with a pipe one (7), the top end of the outlet conduit (17) is provided with a baffle b (2), and the outer circumferential wall of the outlet conduit (17) is fixedly connected with a pipe two (8).

3. The apparatus for improving the continuous separation of glucose and fructose in a simulated moving bed according to claim 2, characterized in that, The sandwich sleeve (36) includes a manifold C (26) and a manifold D (27), and the interior of the sandwich sleeve (36) is provided with two or more vertically installed partitions; Each column (23) has an inlet end (24) on its top surface and an outlet end on its bottom surface, and the outlet end is provided with a mesh filter (25). The column (23) is filled with resin, which is a strong acidic cation exchange resin of alkaline earth metal base with an average particle size of 320μm±10μm.

4. The apparatus for improving the continuous separation of glucose and fructose in a simulated moving bed according to claim 3, characterized in that, Each integral unit is provided with a liquid inlet conduit penetrating the outer wall of the interlayer sleeve (36) on its top surface. A nozzle (29) is provided on the outer circumference of the liquid inlet conduit. A reservoir (28) is connected to the top of the liquid inlet conduit. A baffle c (3) is provided at the top of the reservoir (28). A baffle d (4) is provided between the bottom of the reservoir (28) and the top of the nozzle (29). A pipe three (9) is provided on the outer wall of the reservoir (28) between the baffle c (3) and the baffle d (4). All the reservoirs (28) in the same column are connected to the same manifold O (79) at the top, and the manifold O (79) is connected to the bottom end of the outlet conduit (22); Each of the integral units is provided with a pipe four (30) on its top surface; each of the integral units is connected to a vacuum box (31) on its bottom surface, and an exhaust pipe (48) and a manifold E (49) are provided on one side of the vacuum box (31); Each of the integral units is provided with a funnel-shaped liquid collecting conduit (32) on its bottom surface, and a baffle e (65) is provided inside the liquid collecting conduit (32); a liquid reservoir (33) is provided inside the vacuum box (31), and a liquid conduit (34) is provided at the bottom end of the liquid reservoir (33). A baffle f (5) is provided inside the liquid conduit (34), and a pipe five (10) is provided on the outer circumference of the liquid conduit (34) located below the baffle f (5); The vacuum level of the vacuum chamber (31) is 15-27 inches of mercury.

5. The apparatus for improving the continuous separation of glucose and fructose in a simulated moving bed according to claim 4, characterized in that, The hollow sleeve (41) includes a manifold F (42) and a manifold G (43); The water temperature inside the insulating jacket (11), the interlayer sleeve (36), and the hollow sleeve (41) is 55-70℃; Each of the lower storage tanks (44) is provided with an infusion conduit (45) that penetrates the outer wall of the hollow sleeve (41) on the top surface. A baffle g (6) is provided at the top of the infusion conduit (45). Each of the lower storage tanks (44) is provided with a drainage pipe (46) that penetrates the outer wall of the hollow sleeve (41) on the bottom surface. The output end of the drainage pipe (46) and the input end of the inlet conduit (16) are connected to the same connecting pipe. A pipe six (62) is provided on the top surface of the lower storage tank (44) located on one side of the infusion conduit (45); a liquid level sensor (63) is provided inside each of the lower storage tanks (44); and an infusion pipe (64) is provided on the top surface of each of the lower storage tanks (44).

6. The apparatus for improving the continuous separation of glucose and fructose in a simulated moving bed according to claim 5, characterized in that, The closed vacuum environment loop includes an aerosol separator (50), a central vacuum pump (51), a water tank (52), a liquid guide pipe (53) fixedly connected to the bottom surface of the water tank (52), an inert gas generator (54), a steel tank container (55), and a cold water condenser. The outlet of the aerosol separator (50) is connected to one end of the central vacuum pump (51) and the water tank (52) through a delivery pipe. The inlet and outlet ends of the inert gas generator (54) are respectively connected to the outlet end of the central vacuum pump (51) and the inlet end of the steel tank container (55). The air inlet of the aerosol separator (50) is connected to a manifold P (84), and the output end of the manifold P (84) is connected to the input end of a plurality of air outlet pipes (48); the inlet and outlet of the cold water condenser are respectively connected to the drain port of the aerosol separator (50) and the inlet of the water storage tank (52).

7. The apparatus for improving the continuous separation of glucose and fructose in a simulated moving bed according to claim 6, characterized in that, The upstream wide-range inert gas supply loop includes a gas pipeline (66) connected to the medium-pressure outlet of the steel tank container (55), a manifold H (67) connected to the input end of pipeline two (8) and the output end of the gas pipeline (66), a second gas pipeline (68) connected to the low-pressure outlet of the steel tank container (55), a manifold J (69) connected to the input end of pipeline one (7) and the output end of the second gas pipeline (68), a third gas pipeline (70) connected to the high-pressure outlet of the steel tank container (55), a manifold K (71) connected to the input end of pipeline three (9) and the output end of the third gas pipeline (70), a fourth gas pipeline (72), and a manifold L (57) connected to the input end of pipeline four (30) and the output end of the fourth gas pipeline (72). The upstream wide-range inert gas supply loop also includes a heater (56), the inlet and outlet of which are connected to the output end of the steel tank container (55) and the input end of the four gas pipelines (72) respectively through conduits; The heating temperature of the heater (56) is 60-85℃; The downstream wide-range inert gas supply loop includes a five-way gas pipeline (73) connected to another medium-pressure outlet of the steel tank container (55), a manifold M (74) connected to the input end of pipeline five (10) and the output end of the five-way gas pipeline (73), a six-way gas pipeline (75) connected to another high-pressure outlet of the steel tank container (55), and a manifold N (76) connected to the input end of pipeline six (62) and the output end of the six-way gas pipeline (75).

8. The apparatus for improving the continuous separation of glucose and fructose in a simulated moving bed according to claim 1, characterized in that, The new mass transfer method includes the following steps: A1: The solid resin material is retained in a set of columns (23) as a whole unit; A2: The mobile phase liquid material is delivered intermittently as a dose via the pulse input SI method, and is dripped into each unit cell; A3: After each delivery of the mobile phase liquid material, a wide range of pressurized inert gases is supplied intermittently and simultaneously to each integral unit; A4: This ensures that the solid resin material installed in the unit maintains a closed vacuum environment on the other side. A5: The processed mobile phase liquid material is collected intermittently from the bundle outlet at the bottom of the unit; The total time spent on steps A2-A5 is the minimum time interval Δt; The wide range of pressurized inert gas is supplied from the top of the unit, while a vacuum is applied from the bottom of the unit.

9. The apparatus for improving the continuous separation of glucose and fructose in a simulated moving bed according to claim 8, characterized in that, The specific operation of the pulse input SI method includes the following steps: A21: Simultaneously deliver mobile phase liquid material, subdivided into several predetermined doses, to the top of each integral unit in the shortest possible time to form a partially wetted area; A22: Simultaneously collect the liquid discharged from the bottom of each integral unit, so that the transported liquid and the resin material installed in each integral unit can instantly undergo non-uniform mass transfer contact. The mobile phase liquid material includes an aqueous feed solution, an aqueous homogeneous mixture containing sugar components, and elution water.

10. The apparatus for improving the continuous separation of glucose and fructose in a simulated moving bed according to claim 9, characterized in that, The differential setting scheme includes the following methods: B1: Take a predetermined amount of feed solution and resin to achieve complete adsorption saturation, and install this amount of resin into column (23); B2: Start-up tests were conducted using a new mass transfer method, in which the feed solution and elution water were sequentially and intermittently delivered to generate a stable characteristic curve; B3: Steady-state testing is conducted by intermittently delivering various liquids arranged in sequence using a new mass transfer method; B4: Divide the time required for each portion of the obtained characteristic curve to deliver the liquid by the minimum time interval to obtain the number of dose drops in the device as a specific range of the corresponding liquid input area; B5: Divide the volume of the liquid by the number of doses to obtain the partial volume required for each dose; B6: The amount and partial volume of resin obtained in step B1 ÷ the preselected number, with the volume of the droplet dose received simultaneously as the specific area range of the corresponding liquid; B7: Assign all integral units with each corresponding liquid to a range of specific regions; B8: All types of transported liquids are arranged in the same order in a circular circulation pattern in the device; The preselected number corresponds to a set of columns set in a single integral unit, and the preselected number is a finite integer greater than 1.

11. The apparatus for improving the continuous separation of glucose and fructose in a simulated moving bed according to claim 10, characterized in that, B2 also includes the following: B21: Based on the decomposition characteristic curves of the collected sequential samples, and collect sequential samples as multiple recycled liquid mixtures for further testing; B22: A characteristic curve is generated by intermittently feeding a recirculated liquid mixture in the order of collection, with the feed solution arranged after the sugar mixture in the feed solution with a glucose content slightly higher than that in the feed solution and before the sugar mixture in the feed solution with a glucose content slightly lower than that in the feed solution, followed by the remaining unused recirculated liquid, elution water, and then the liquid mixture collected from the characteristic curve in sequence. B23: The samples collected in the previous step are recorded on the predetermined sugar mixture characteristic curve and decomposed into various recycle liquids for further testing; B24: Repeat steps B22-B23 until a stable characteristic curve is obtained.

12. The apparatus for improving the continuous separation of glucose and fructose in a simulated moving bed according to claim 11, characterized in that, B3 also includes the following: B31: Based on the collected samples, in the order of collection for each corresponding delivery liquid, decompose and record each required portion of time and generate characteristic curves; B32: Record the individual components and concentrations of all expanded recirculated liquid mixtures; B33: By intermittently feeding the expanded recirculated liquid mixture in the order of collection, a characteristic curve is generated by further testing. The feed solution is arranged after the glucose content is slightly higher than that of the sugar mixture in the feed solution and before the glucose content is slightly lower than that of the sugar mixture in the feed solution. Then, the remaining unused recirculated liquid is fed in a specific order, followed by elution water, and then the liquid mixture collected first from the characteristic curve. B34: Record the portion of the time required to deliver the corresponding liquid from the characteristic curve obtained in step B33; B35: If the recovered raffinate and product fail to meet the predetermined purity and concentration, then repeat steps B31-B34 continuously. If the recovered raffinate and product can meet the predetermined purity and concentration of the raffinate and product, then only their respective components and concentrations are recorded as an extended range of the characteristics of the recovered liquid for subsequent use; The characteristic curve includes a glucose-rich raffinate, multiple recycled liquid mixtures in a specific order, and an expansion of multiple recycled liquid mixtures by adding liquid mixtures with specific compositions and limited concentrations of glucose-rich raffinate and fructose-rich product solutions recovered from the previous characteristic curve. The dry solids content of the expanded recirculated liquid mixture is 40%-60%.

13. The apparatus for improving the continuous separation of glucose and fructose in a simulated moving bed according to claim 12, characterized in that, The specific content of B6 includes the following aspects: B61: Assign all the units of each input liquid to their respective liquid regions in sequence, and assign all regions to an infinite format in sequence; B62: Prepare the corresponding solution and store it in the corresponding tank in the tank module for distribution of this liquid; B63: During steady-state operation, various fluids are simultaneously delivered to their respective regions by the device in a period of minimal time interval, changing the liquid flow pattern observed in conventional chromatographic separation from parallel to the mobile phase to a flow direction perpendicular to the mobile phase.

14. The apparatus for improving the continuous separation of glucose and fructose in a simulated moving bed according to claim 13, characterized in that, The content of B8 also includes preparing the entire series of recycled liquids recorded in step B35 into the corresponding lower storage tank (44) in sequence, and connecting them together with the pressurized inert gas supply module to support liquid distribution via the upstream storage tank module (12) as a closed loop.

15. The apparatus for improving the continuous separation of glucose and fructose in a simulated moving bed according to claim 1, characterized in that, The liquid stream includes a glucose-rich raffinate stream, a fructose-rich product stream, and multiple recirculated liquid streams with stable composition and specific concentrations. The method for recovering the liquid stream includes the following: C1: The liquid passes sequentially through the closed-loop downstream storage tank module (40), the upstream storage tank module (12), and the rotation and positioning mechanism in the upstream rotary joint module to complete the mass transfer balance of the separation module, and then returns to the downstream rotary joint module. C2: Perform steady-state operation during each time interval spent.

16. The apparatus for improving the continuous separation of glucose and fructose in a simulated moving bed according to claim 15, characterized in that, C1 also includes the following: C11: The integral unit located in the first position in the separation module receives liquid delivery, while the other integral units do not receive liquid. The liquid is simultaneously transferred from the lower tank (44) to the upper tank (15) in a specific order and is associated with a wide range of pressurized inert gas supply through the storage device (28). C12: After delivery of various liquids, the liquid is intermittently delivered through a device that alternately supplies two separate, wide-range pressurized inert gas paths to force the dripping dose of liquid to be rapidly discharged through the resin, thereby completing the expected mass transfer contact equilibrium between the solid and liquid phases. C13: Maintain a closed vacuum environment, discharge each liquid solution into the corresponding transfer container (38), and keep the resin in a semi-dry state; C14: Intermittently collect the discharged liquid from each transfer container (38) and transfer the collected liquid to the lower storage tank (44) via a wide-range pressurized inert gas supply route through the downstream rotary joint module; C15: Repeat steps C11-C14 continuously, while covering the first and second integral units of the liquid receiving module, until the storage container (21) and the transfer container (38) of the first liquid receiving are set back to their initial positions, completing one cycle, and the start-up operation is completed. The various liquids recovered during the startup operation include water as circulating water, low-dryness solid-phase glucose solutions for other uses, various recovered liquids stored in a specific order, solutions as glucose residues, and solutions as fructose products.

17. The apparatus for improving the continuous separation of glucose and fructose in a simulated moving bed according to claim 16, characterized in that, The steady-state operation includes the following steps: C21: Various liquids are transported by a liquid transport method using a large-scale pressurized inert gas, and all available liquids from the upper storage tank (15) are forcibly transported into the storage container (21). C22: After delivery of various liquids, the device intermittently delivers the liquid by alternating supply between two separate, wide-range pressurized inert gas paths to force the dripping dose of liquid to be rapidly discharged through the resin, thereby completing the expected mass transfer contact equilibrium between the solid and liquid phases. C23: Maintain a closed vacuum environment, discharge each liquid solution into the corresponding transfer container (38), and keep the resin in a semi-dry state; C24: Collect the various discharged liquids from each transfer container (38) and transfer the collected liquids to the lower storage tank (44) via a downstream rotary joint module through a wide-range pressurized inert gas supply route; The various liquids recovered during the steady-state operation include water as circulating water, low-dryness solid-phase glucose solutions for other uses, various recovered liquids stored in a specific order, solutions as glucose residues, and solutions as fructose products.

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