Galactose solution end treatment device
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- JIHENG PHARMA HENGSHUI CITY
- Filing Date
- 2025-06-16
- Publication Date
- 2026-06-19
AI Technical Summary
In the existing technology, the final yield of lactulose synthesis process using sodium aluminate is relatively low, mainly because aluminum hydroxide flocculents carry a large amount of lactulose in the precipitate, resulting in serious lactulose loss.
Primary solid-liquid separation is performed using a curtain membrane solid-liquid separation device, which utilizes the flux of the organic membrane to intercept aluminum hydroxide flocculents while allowing lactulose molecules to pass through. The aluminum hydroxide slurry is then separated by a centrifuge device, and further salting and purification are carried out by nanofiltration, reverse osmosis, and resin adsorption desalination devices.
The final yield of lactulose was improved, and efficient separation of aluminum hydroxide and high purity of lactulose products were achieved, with conductivity reduced to <50μs/cm.
Smart Images
Figure CN224378079U_ABST
Abstract
Description
Technical Field
[0001] This utility model relates to the technical field of equipment related to lactulose production, and more specifically, to a lactulose solution end-of-line treatment device. Background Technology
[0002] Lactulose is suitable for patients with acute, chronic, or habitual constipation, and can be taken by the elderly, children, pregnant women, and breastfeeding women, making it a laxative suitable for all ages.
[0003] Through a survey of lactulose synthesis methods, and a comprehensive comparison of factors such as cost, yield, equipment requirements, and ease of separation and purification, the chemical method was determined to be the optimal synthesis method for lactulose. Among the chemical methods, there are the single-alkali method, the boric acid method, and the sodium aluminate method, with the sodium aluminate method being the primary synthesis method.
[0004] In the existing technology, the traditional end-of-pipe treatment process of sodium aluminate is described as follows: lactose and sodium aluminate are added to the reaction vessel, the pH value of the solution is adjusted after a certain reaction time and aluminum hydroxide precipitate is formed, the solution is filtered (to filter out the precipitated aluminum hydroxide), and the filtrate is desalted and evaporated to a concentration of 50% lactulose solution by anion and cation exchange resin.
[0005] Analysis revealed the following advantages of the above process: high lactose conversion rate, generally above 85%, and relatively low catalyst and resin costs. The disadvantages are: the formed precipitate is flocculent aluminum hydroxide, which carries a large amount of lactulose, inevitably leading to significant lactulose loss. This results in a final lactulose yield (approximately 60%–70%) that is far lower than the lactulose conversion rate (85%). Utility Model Content
[0006] (I) Technical Issues
[0007] In conclusion, how to improve the final yield of lactulose has become an urgent problem to be solved by those skilled in the art.
[0008] (II) Technical Solution
[0009] To achieve the above objectives, this utility model provides the following technical solution:
[0010] This invention provides an end-of-life treatment device for lactulose solution. In this invention, the end-of-life treatment device for lactulose solution includes a curtain membrane solid-liquid separation device for separating aluminum hydroxide from the raw material solution. The flow rate of the curtain membrane solid-liquid separation device is configured such that it can intercept aluminum hydroxide flocculents while allowing lactulose molecules to pass through.
[0011] Preferably, in the lactulose solution end-of-life treatment device provided by this utility model, a centrifuge device is connected to the curtain membrane solid-liquid separation device. The centrifuge device is used to receive the aluminum hydroxide slurry generated by the curtain membrane solid-liquid separation device, and the centrifuged mother liquor generated by the centrifuge device re-enters the curtain membrane solid-liquid separation device for separation.
[0012] Preferably, in the lactulose solution end-of-line treatment device provided by this utility model, a product water tank is provided downstream of the curtain membrane solid-liquid separation device. The product water tank is connected to the curtain membrane solid-liquid separation device and is used to receive and temporarily store the curtain membrane product water generated by the curtain membrane solid-liquid separation device.
[0013] Preferably, in the lactulose solution end-of-line treatment device provided by this utility model, a nanofiltration device is provided downstream of the product water tank, and the nanofiltration device performs salt separation on the product water temporarily stored in the product water tank.
[0014] Preferably, in the lactulose solution end-of-pipe treatment device provided by this utility model, the nanofiltration device includes a primary nanofiltration concentration device connected to the product water tank.
[0015] Preferably, in the lactulose solution end-of-life treatment device provided by this utility model, a secondary nanofiltration desalination device is connected to the primary nanofiltration concentration device.
[0016] Preferably, in the lactulose solution end-of-line treatment device provided by this utility model, a reverse osmosis device is connected to the primary nanofiltration concentration device and / or the secondary nanofiltration desalination device; the reverse osmosis device receives nanofiltration permeate produced by the primary nanofiltration concentration device and / or the secondary nanofiltration desalination device, the reverse osmosis device is process-connected to the centrifuge and / or the secondary nanofiltration desalination device, and the reverse osmosis permeate produced by the reverse osmosis device is used to participate in the production operation of the centrifuge and / or the secondary nanofiltration desalination device.
[0017] Preferably, in the lactulose solution end-of-pipe treatment device provided by this utility model, an ultrafiltration device is provided between the primary nanofiltration concentration device and the secondary nanofiltration desalination device for separating aluminum hydroxide from the primary nanofiltration concentrate produced by the primary nanofiltration concentration device.
[0018] Preferably, in the lactulose solution end-treatment device provided by this utility model, a resin adsorption desalination device is connected to the secondary nanofiltration desalination device.
[0019] Preferably, in the lactulose solution end-treatment device provided by this utility model, an evaporation device is connected to the resin adsorption desalination device.
[0020] (III) Beneficial Effects
[0021] As described above, this utility model provides an end-of-life treatment device for lactulose solution. In this utility model, the end-of-life treatment device for lactulose solution employs a curtain-type membrane solid-liquid separation device to achieve primary solid-liquid separation of the raw material liquid to obtain primary permeate and primary concentrate. The curtain-type membrane solid-liquid separation device is used to filter and separate aluminum hydroxide. Its advantage is that by relying on the flux of the organic membrane in the curtain-type membrane solid-liquid separation device, lactulose molecules can pass through, while aluminum hydroxide flocculent matter is intercepted. After the primary separation and filtration are completed, the aluminum hydroxide slurry enters a centrifuge for centrifugation. The centrifuge produces centrifugal mother liquor and aluminum sludge precipitate. The precipitate (aluminum sludge precipitate) is high-concentration aluminum hydroxide and is outsourced for further processing. The centrifugal mother liquor obtained by the centrifuge is returned to the raw material tank and can be re-entered into the curtain-type membrane solid-liquid separation device for separation. The end-of-life treatment device for lactulose solution provided by this utility model can achieve efficient separation of aluminum hydroxide in the raw material liquid, improving the final yield of lactulose. Attached Figure Description
[0022] The accompanying drawings, which form part of this application, are used to provide a further understanding of the present invention. The illustrative embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an undue limitation of the present invention. Wherein:
[0023] Figure 1 This is a schematic diagram of the end-of-life treatment device for lactulose solution in one embodiment of the present invention.
[0024] exist Figure 1 In the figures, the correspondence between the reference numerals and the component names is as follows:
[0025] 1. First nanofiltration concentration unit; 2. Reverse osmosis unit; 3. Second nanofiltration desalination unit; 4. Ultrafiltration unit; 5. Curtain membrane solid-liquid separation unit; 6. Centrifugation unit; 7. Resin adsorption desalination unit; 8. Evaporation unit. Detailed Implementation
[0026] The present invention will now be described in detail with reference to the accompanying drawings and embodiments. Various examples are provided by way of explanation of the present invention and not by way of limitation. In fact, those skilled in the art will recognize that modifications and variations can be made to the present invention without departing from the scope or spirit of the invention. For example, a feature shown or described as part of one embodiment may be used in another embodiment to produce yet another embodiment. Therefore, it is desirable that the present invention encompass such modifications and variations that fall within the scope of the appended claims and their equivalents.
[0027] In the description of this utility model, the terms "longitudinal," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," and "bottom," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing this utility model and do not require that this utility model be constructed and operated in a specific orientation; therefore, they should not be construed as limitations on this utility model. The terms "connected" and "linked" used in this utility model should be interpreted broadly. For example, they can refer to a fixed connection or a detachable connection; they can refer to a direct connection or an indirect connection through intermediate components. Those skilled in the art can understand the specific meaning of the above terms according to the specific circumstances.
[0028] Please refer to Figure 1 , Figure 1 This is a schematic diagram of the end-of-life treatment device for lactulose solution in one embodiment of the present invention.
[0029] This invention provides an end-of-life treatment device for lactulose solution, used to process raw material liquid to obtain lactulose product.
[0030] The raw material liquid is obtained by a chemical method (specifically, the sodium aluminate method). The raw material liquid is stored in a raw material tank, which is the starting point of the process of this utility model. The raw material liquid is supplied to downstream devices from the raw material tank.
[0031] Downstream of the feed tank, a curtain membrane solid-liquid separator 5 is installed for solid-liquid separation (aluminum hydroxide separation) of the feed liquid. The flow rate of the curtain membrane solid-liquid separator 5 is configured to intercept aluminum hydroxide flocs while allowing lactulose molecules to pass through. After passing through the curtain membrane solid-liquid separator 5, the feed liquid produces two products: primary permeate, i.e., curtain membrane permeate, which contains water, lactulose, and a large number of ions, and primary concentrate (mainly containing a small amount of water, aluminum hydroxide flocs, and lactulose). The primary permeate is supplied to the downstream unit, while the primary concentrate is sent to the centrifuge unit 6.
[0032] A centrifuge 6 is connected to the curtain membrane solid-liquid separation device 5. The centrifuge 6 is used to receive the aluminum hydroxide slurry (i.e. the primary concentrate mentioned above) produced by the curtain membrane solid-liquid separation device 5. The centrifuged mother liquor produced by the centrifuge 6 is re-entered into the curtain membrane solid-liquid separation device 5 for separation. The aluminum mud precipitate produced by the centrifuge 6 is outsourced for treatment.
[0033] The downstream device of the curtain membrane solid-liquid separator 5 is a product water tank, which is connected to the curtain membrane solid-liquid separator 5 and is used to receive and temporarily store the primary product water generated by the curtain membrane solid-liquid separator 5 for supply to the downstream device.
[0034] Downstream of the product water tank is a nanofiltration unit, which separates salts (ions in the curtain membrane product water). Please refer to [reference needed]. Figure 1 To ensure salt separation efficiency, the nanofiltration unit is vertically configured with two units: a primary nanofiltration concentration unit connected to the product water tank, and a secondary nanofiltration desalination unit connected to the primary nanofiltration concentration unit.
[0035] The primary nanofiltration concentration unit separates the permeate from the curtain membrane, producing primary nanofiltration permeate and primary nanofiltration concentrate. The primary nanofiltration concentrate enters the secondary nanofiltration desalination unit, while the primary nanofiltration permeate enters the reverse osmosis unit 2. The reverse osmosis unit 2 produces reverse osmosis permeate and reverse osmosis concentrate. The reverse osmosis concentrate is saline wastewater and has two destinations: 1. After deionization, it is mixed with the secondary nanofiltration concentrate produced by the secondary nanofiltration desalination unit to form a mixed solution that enters the resin adsorption desalination unit downstream of the secondary nanofiltration desalination unit; 2. It participates in the operation of the centrifuge unit 6, serving as washing water for the centrifugation of aluminum hydroxide slurry. The reverse osmosis concentrate is then treated as saline wastewater after leaving the system.
[0036] The downstream device of the first-stage nanofiltration concentration unit is the ultrafiltration unit 4. The ultrafiltration unit 4 is used to separate aluminum hydroxide from the first-stage nanofiltration concentrate produced by the first-stage nanofiltration concentration unit. The ultrafiltration unit 4 can produce ultrafiltration permeate and ultrafiltration concentrate. The ultrafiltration permeate enters the downstream device, while the ultrafiltration concentrate is mixed with the primary concentrate (aluminum hydroxide slurry produced by the curtain membrane solid-liquid separation unit) and enters the centrifuge unit 6 for centrifugal separation.
[0037] The downstream unit of ultrafiltration unit 4 is a secondary nanofiltration desalination unit. The secondary nanofiltration desalination unit can produce secondary nanofiltration permeate and secondary nanofiltration concentrate. The secondary nanofiltration permeate enters the reverse osmosis unit 2. The secondary nanofiltration concentrate and the reverse osmosis permeate (the reverse osmosis permeate is deionized to form deionized water, and the deionized water and the secondary nanofiltration concentrate are mixed) have two paths: 1. Enter the downstream unit to produce lactulose product; 2. Return to the secondary nanofiltration desalination unit for further desalination treatment.
[0038] The downstream unit of the secondary nanofiltration desalination unit is the resin adsorption desalination unit 7, which is used to filter the secondary nanofiltration concentrate and produce lactulose products that meet the requirements.
[0039] The original treatment route involved separating lactulose and aluminum hydroxide by filtering the reacted raw material liquid through a plate and frame filter. However, during the separation process, it was found that the aluminum hydroxide precipitate contained a large amount of lactulose, resulting in material loss.
[0040] To solve the above problems, the core technology of this utility model is as follows: A curtain-type membrane solid-liquid separation device 5 is used to achieve primary solid-liquid separation of the raw material liquid (obtaining primary permeate and primary concentrate). Its advantage lies in relying on the flux of the organic membrane (allowing lactulose molecules to pass through while aluminum hydroxide flocs are intercepted), ensuring the passage of the lactulose solution, while the aluminum hydroxide precipitate remains suspended on the membrane surface. After primary separation and filtration, the aluminum hydroxide slurry enters a centrifuge for centrifugation. During centrifugation, water and lactulose in the aluminum hydroxide flocs are separated to form a centrifugal mother liquor and aluminum sludge precipitate. The precipitate (aluminum sludge precipitate) is a high-concentration aluminum hydroxide that is then processed externally. The centrifugal mother liquor obtained through centrifugation is returned to the raw material tank and can be re-entered into the curtain-type membrane solid-liquid separation device 5 for further separation. The above operation achieves efficient separation of aluminum hydroxide, and the primary permeate obtained after separation is used in subsequent desalination operations.
[0041] In existing technologies, the conventional desalination process involves using anion and cation exchange resins for ion removal, which results in a low removal rate and poor product quality. This invention, however, employs a nanofiltration + reverse osmosis unit + resin adsorption desalination device to achieve ion removal, ultimately producing a product with a conductivity of <50 μS / cm.
[0042] In one specific embodiment of this utility model, the primary permeate obtained after the curtain membrane solid-liquid separation device 5 separates the raw material liquid is a clarified liquid, and the volume of the clarified liquid (primary permeate) is approximately 20 m³. 3 The concentration is 5%, and the conductivity is approximately 30-35 mS / cm, of which Cl - Approximately 11,000 ppm, Na + Approximately 8500 ppm, Al 3+ Approximately 120 ppm. The primary permeate, after solid-liquid separation (i.e., after passing through the curtain membrane solid-liquid separation device 5), enters the first nanofiltration concentration device 1. The first nanofiltration concentration device 1 is configured to limit the flow of monovalent ions, while water and lactulose can pass through.
[0043] To clearly describe the process of this utility model, the following definitions apply: the permeate obtained by the first nanofiltration concentration device 1 is primary nanofiltration permeate, and the concentrate obtained is primary nanofiltration concentrate; the permeate obtained by the reverse osmosis device 2 is reverse osmosis permeate, and the concentrate obtained is reverse osmosis concentrate; the permeate obtained by the second nanofiltration desalination device 3 is secondary nanofiltration permeate, and the concentrate obtained is secondary nanofiltration concentrate; the permeate obtained by the ultrafiltration device 4 is ultrafiltration permeate, and the concentrate obtained is ultrafiltration concentrate; the permeate obtained by the curtain membrane solid-liquid separation device 5 is primary permeate, and the concentrate obtained is primary concentrate.
[0044] This invention first uses a first nanofiltration concentration device 1 to remove monovalent ions. This process does not involve water dialysis. After filtration, the remaining concentrate obtained from the first-stage nanofiltration is approximately 7-8 ml.3 The conductivity is 30-35 mS / cm. Because the membrane separation performed by the first nanofiltration concentration device 1 cannot guarantee complete molecular retention, this invention also includes a second nanofiltration desalination device 3. The second nanofiltration desalination device 3 receives the primary nanofiltration concentrate produced by the primary nanofiltration concentration device. The second nanofiltration membrane device further separates the primary nanofiltration concentrate to obtain secondary nanofiltration concentrate. Both the primary nanofiltration permeate (produced by the primary nanofiltration concentration device) and the secondary nanofiltration permeate (produced by the secondary nanofiltration desalination device) are sent to a reverse osmosis unit for separation. The reverse osmosis unit produces reverse osmosis permeate, which can be deionized to form deionized water, which is then mixed with the secondary nanofiltration concentrate. The reverse osmosis concentrate produced by the reverse osmosis unit is treated as saline wastewater.
[0045] In this invention, the permeate from the primary nanofiltration concentration unit enters the reverse osmosis unit 2 for reverse osmosis treatment. The primary nanofiltration concentrate then enters the secondary nanofiltration desalination unit for further dialysis and deionization. The secondary nanofiltration desalination unit further removes ions through dialysis, and the resulting secondary permeate enters the reverse osmosis unit 2 for reverse osmosis treatment. The secondary concentrate, after being mixed with deionized water, enters the resin adsorption desalination unit 7 for further desalination, producing a lactulose product that meets the standards. Furthermore, this invention also includes an evaporation unit 8 after the resin adsorption desalination unit 7 to increase the concentration of the lactulose product.
[0046] It should be noted that the liquid treatment devices involved in this utility model, such as the first nanofiltration concentration device 1, the reverse osmosis device 2, the second nanofiltration desalination device 3, the ultrafiltration device 4, and the curtain membrane solid-liquid separation device 5, can all produce two products, namely concentrated water and permeate. Therefore, this utility model is also equipped with corresponding pipelines to export and transport the two different products to the corresponding downstream process points. Regarding the specific pipeline setup and wiring, this utility model will not elaborate on them. Based on the above accurate and clear process flow, how to set up pipelines and wiring is a conventional technical means.
[0047] The above are merely preferred embodiments of this utility model and are not intended to limit the scope of this utility model. Various modifications and variations can be made to this utility model by those skilled in the art. Any modifications, equivalent substitutions, or improvements made within the spirit and principles of this utility model should be included within the protection scope of this utility model.
Claims
1. A lactulose solution end-of-pipe treatment device, characterized in that, The device includes a curtain membrane solid-liquid separation device for separating aluminum hydroxide from a feed liquid. The flow rate of the curtain membrane solid-liquid separation device is configured to intercept aluminum hydroxide flocculents while allowing lactulose molecules to pass through.
2. The end-of-life treatment device for lactulose solution according to claim 1, characterized in that, A centrifuge is connected to the curtain membrane solid-liquid separation device. The centrifuge is used to receive the aluminum hydroxide slurry produced by the curtain membrane solid-liquid separation device, and the centrifuged mother liquor produced by the centrifuge re-enters the curtain membrane solid-liquid separation device for separation.
3. The end-of-life treatment device for lactulose solution according to claim 1, characterized in that, A product water tank is provided downstream of the curtain membrane solid-liquid separation device. The product water tank is connected to the curtain membrane solid-liquid separation device and is used to receive and temporarily store the curtain membrane product water generated by the curtain membrane solid-liquid separation device.
4. The end-of-life treatment device for lactulose solution according to claim 3, characterized in that, A nanofiltration device is installed downstream of the product water tank to separate salts from the product water temporarily stored in the product water tank.
5. The end-of-life treatment device for lactulose solution according to claim 4, characterized in that, The nanofiltration device includes a primary nanofiltration concentration unit connected to the product water tank.
6. The end-of-life treatment device for lactulose solution according to claim 5, characterized in that, A secondary nanofiltration desalination device is connected to the primary nanofiltration concentration device.
7. The end-of-life treatment device for lactulose solution according to claim 6, characterized in that, A reverse osmosis unit is connected to the primary nanofiltration concentration unit and / or the secondary nanofiltration desalination unit; The reverse osmosis unit receives nanofiltration permeate produced by the primary nanofiltration concentration unit and / or the secondary nanofiltration desalination unit. The reverse osmosis unit is connected to the centrifuge and / or the secondary nanofiltration desalination unit in a process connection. The reverse osmosis permeate produced by the reverse osmosis unit is used to participate in the production operation of the centrifuge and / or the secondary nanofiltration desalination unit.
8. The end-of-life treatment apparatus for lactulose solution according to claim 7, characterized in that, An ultrafiltration device is provided between the primary nanofiltration concentration device and the secondary nanofiltration desalination device for separating aluminum hydroxide from the primary nanofiltration concentrate produced by the primary nanofiltration concentration device.
9. The end-of-life treatment device for lactulose solution according to claim 8, characterized in that, A resin adsorption desalination device is connected to the secondary nanofiltration desalination device.
10. The end-of-life treatment apparatus for lactulose solution according to claim 9, characterized in that, An evaporation device is connected to the resin adsorption and desalination device.