CN215963001U - Fine quality heparin sodium desalination system - Google Patents
Fine quality heparin sodium desalination system Download PDFInfo
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- CN215963001U CN215963001U CN202122429633.2U CN202122429633U CN215963001U CN 215963001 U CN215963001 U CN 215963001U CN 202122429633 U CN202122429633 U CN 202122429633U CN 215963001 U CN215963001 U CN 215963001U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
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- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
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Abstract
The utility model discloses a fine heparin sodium desalting system which comprises a primary ultrafiltration membrane system, a secondary nanofiltration membrane system and a tertiary nanofiltration membrane system, wherein the maximum pressure values of the primary ultrafiltration membrane system, the secondary nanofiltration membrane system and the tertiary nanofiltration membrane system are 6bar, 16bar and 16bar in sequence, the primary ultrafiltration membrane system comprises a primary Y-shaped filter and a primary membrane assembly, the secondary nanofiltration membrane system comprises a secondary Y-shaped filter and a secondary membrane assembly, and the tertiary nanofiltration membrane system comprises a tertiary Y-shaped filter and a tertiary membrane assembly. According to the utility model, after the heparin sodium product is purified, filtered, concentrated and recovered by the primary ultrafiltration membrane system, the secondary nanofiltration membrane system and the tertiary nanofiltration membrane system, except the primary ultrafiltration membrane system, a small amount of product loss exists, the product loss does not exist in other parts, the recovery rate of the heparin sodium is obviously improved, the damage to the molecular structure of the heparin sodium is reduced to the maximum extent, meanwhile, the whole process is operated at normal temperature, and the energy consumption is low.
Description
Technical Field
The utility model relates to the technical field of heparin sodium extraction, in particular to a fine heparin sodium desalting system.
Background
Heparin sodium is a raw material medicine with anticoagulant and antithrombotic characteristics, and is formed by combining heparin molecules with sodium salt in the extraction process, wherein the heparin sodium is firstly extracted from small intestinal mucosa of a fresh healthy live pig and prepared into a heparin sodium crude product, however, the crude product also contains viruses, residual protein impurities, nucleic acid substances and mucopolysaccharide substances, has low titer, contains more impurities and cannot be directly applied to clinic, the heparin sodium crude product needs to be further purified to remove impurities and remove part of residual impurities, and the process is called as the refining of the heparin sodium.
At present, the protein connected with heparin sodium is degraded by utilizing the efficient and specific characteristics of protease in the market to remove foreign protein, the structure of the heparin sodium is not damaged, the purity and the titer of the heparin sodium can be improved simultaneously, and then separation, purification, alcohol precipitation and drying are carried out to finally obtain a refined heparin sodium product.
SUMMERY OF THE UTILITY MODEL
The utility model aims to: in order to solve the technical problems mentioned in the background art, a system for desalting refined heparin sodium is provided.
In order to achieve the purpose, the utility model adopts the following technical scheme:
a fine heparin sodium desalting system comprises a primary ultrafiltration membrane system, a secondary nanofiltration membrane system and a tertiary nanofiltration membrane system, wherein the maximum pressure values of the primary ultrafiltration membrane system, the secondary nanofiltration membrane system and the tertiary nanofiltration membrane system are 6bar, 16bar and 16bar in sequence, the primary ultrafiltration membrane system comprises a primary Y-shaped filter and a primary membrane assembly, the secondary nanofiltration membrane system comprises a secondary Y-shaped filter and a secondary membrane assembly, the tertiary nanofiltration membrane system comprises a tertiary Y-shaped filter and a tertiary membrane assembly, a stock solution is filtered by the primary Y-shaped filter and the primary membrane assembly to obtain a primary permeate, the primary permeate is filtered by the secondary Y-shaped filter and the secondary membrane assembly to obtain a secondary permeate and a secondary concentrate, the secondary concentrate is a finished solution, the secondary permeate is filtered by the tertiary Y-shaped filter and the tertiary membrane assembly to obtain a tertiary permeate and a tertiary concentrate, and the tertiary concentrate flows back to the secondary nanofiltration membrane system, and concentrating the filtrate by a secondary membrane system, and conveying the concentrated filtrate to a finished liquid box to be discharged as a finished liquid.
As a further description of the above technical solution:
the primary ultrafiltration membrane system also comprises a primary stock solution tank, a primary feed pump and a primary high-pressure pump, wherein the input ends and the output ends of the primary stock solution tank, the primary feed pump, the primary Y-shaped filter, the primary high-pressure pump and the primary membrane component are sequentially connected end to end so as to realize the conveying or the backflow of the stock solution, the deionized water and the primary concentrated solution.
As a further description of the above technical solution:
the input end and the output end of the first-stage high-pressure pump and the first-stage membrane module are sequentially connected end to realize the backflow of the first-stage concentrated solution.
As a further description of the above technical solution:
the second grade receives filter membrane system still includes second grade stoste case, second grade feed pump and second grade high-pressure pump, the input and the output end of second grade stoste case, second grade feed pump, second grade Y type filter, second grade high-pressure pump and second grade membrane module connect gradually end to realize the transport, the backward flow and the collection of one-level permeate liquid, deionized water, second grade concentrate and tertiary concentrate.
As a further description of the above technical solution:
and the input end and the output end of the second-stage high-pressure pump and the second-stage membrane component are sequentially connected end to end so as to realize the backflow of the second-stage concentrated solution.
As a further description of the above technical solution:
the tertiary nanofiltration membrane system also comprises a tertiary stock solution tank, a tertiary feed pump and a tertiary high-pressure pump, wherein the input ends and the output ends of the tertiary stock solution tank, the tertiary feed pump, the tertiary Y-shaped filter, the tertiary high-pressure pump and the tertiary membrane assembly are sequentially connected end to end so as to realize the conveying and the backflow of secondary permeate liquid, deionized water and tertiary concentrate.
As a further description of the above technical solution:
the first-stage feed pump, the second-stage feed pump and the third-stage feed pump are all horizontal stainless steel sanitary centrifugal pumps, the first-stage high pump, the second-stage high pump and the third-stage high pump are all vertical stainless steel centrifugal pumps, and the horizontal stainless steel sanitary centrifugal pumps and the vertical stainless steel centrifugal pumps are only mechanically sealed and do not have oil seals.
In summary, due to the adoption of the technical scheme, the utility model has the beneficial effects that:
1. according to the utility model, after a heparin sodium product is purified, filtered, concentrated and recovered by a primary ultrafiltration membrane system, a secondary nanofiltration membrane system and a tertiary nanofiltration membrane system, except for the primary ultrafiltration membrane system, a small amount of product loss is caused, and no product loss is caused in other parts, the recovery rate of the heparin sodium is remarkably improved, the damage to the molecular structure of the heparin sodium is reduced to the maximum extent, meanwhile, the whole process is operated at normal temperature, the energy consumption is low, and in the whole filtering process, the required water consumption is low, so that deionized water can be used, materials are also in a closed equipment environment, the contact with the outside is less, the quality of the heparin sodium product is improved, the alcohol precipitation process is omitted, and the generation and treatment work of ethanol wastewater is avoided.
3. In the utility model, all liquid receiving parts of the equipment involved in the whole process flow are made of 2205 duplex stainless steel materials, so that the corrosion of sodium chloride in the feed liquid to the equipment is prevented.
Drawings
Fig. 1 is a schematic structural diagram illustrating a primary ultrafiltration membrane system of a competitive heparin sodium desalination system according to an embodiment of the present invention;
fig. 2 is a schematic structural diagram illustrating a two-stage nanofiltration membrane system of a competitive heparin sodium desalination system according to an embodiment of the present invention;
fig. 3 is a schematic structural diagram illustrating a three-stage nanofiltration membrane system of a competitive heparin sodium desalination system according to an embodiment of the present invention;
FIG. 4 is a schematic diagram illustrating the delivery and reflux of the raw liquid and the primary concentrated liquid of a refined heparin sodium desalination system according to an embodiment of the present invention;
FIG. 5 is a schematic diagram illustrating partial reflux of a primary concentrate of a refined heparin sodium desalination system according to an embodiment of the present invention;
FIG. 6 is a schematic diagram illustrating the transportation and reflux of deionized water in a primary ultrafiltration system of a refined heparin sodium desalination system according to an embodiment of the present invention;
FIG. 7 is a schematic diagram illustrating the primary permeate and secondary concentrate volumetric delivery and reflux of a refined heparin sodium desalination system according to an embodiment of the present invention;
FIG. 8 is a schematic diagram of partial reflux of the secondary concentrate of a refined heparin sodium desalination system according to an embodiment of the present invention;
fig. 9 is a schematic diagram illustrating the transportation and backflow of deionized water in a two-stage nanofiltration membrane system of a competitive heparin sodium desalination system provided according to an embodiment of the present invention;
FIG. 10 is a schematic diagram illustrating the delivery and reflux of the secondary permeate and the tertiary concentrate of a refined heparin sodium desalination system according to an embodiment of the present invention;
fig. 11 shows a schematic backflow diagram of deionized water of a competitive heparin sodium desalination system in a three-stage nanofiltration membrane system according to an embodiment of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Referring to fig. 1-11, the present invention provides a technical solution: a fine heparin sodium desalination system comprises a primary ultrafiltration membrane system, a secondary nanofiltration membrane system and a tertiary nanofiltration membrane system, wherein the maximum pressure values of the primary ultrafiltration membrane system, the secondary nanofiltration membrane system and the tertiary nanofiltration membrane system are 6bar, 16bar and 16bar in sequence, the primary ultrafiltration membrane system comprises a primary Y-shaped filter and a primary membrane assembly, the primary ultrafiltration membrane assembly is provided with two or more ultrafiltration membranes with retention rates, such as ultrafiltration membranes with retention molecular weights of 50000Dal and 80000Dal, different macromolecular impurities are removed according to different raw materials and processes in actual production, the primary ultrafiltration membrane system further comprises a primary stock solution tank, a primary feed pump and a primary high-pressure pump, the primary stock solution tank, the primary feed pump, the primary Y-shaped filter, the primary high-pressure pump and the input end and the output end of the primary membrane assembly are connected in sequence, so that the raw solution, deionized water and the primary concentrated solution are conveyed or refluxed;
the secondary nanofiltration membrane system comprises a secondary Y-shaped filter and a secondary membrane component, and further comprises a secondary stock solution tank, a secondary feed pump and a secondary high-pressure pump, wherein the input ends and the output ends of the secondary stock solution tank, the secondary feed pump, the secondary Y-shaped filter, the secondary high-pressure pump and the secondary membrane component are sequentially connected end to end so as to realize the conveying, the backflow and the collection of primary permeate, deionized water, secondary concentrate and tertiary concentrate;
the three-stage nanofiltration membrane system comprises a three-stage Y-shaped filter and a three-stage membrane assembly, and further comprises a three-stage stock solution tank, a three-stage feed pump and a three-stage high-pressure pump, wherein the input ends and the output ends of the three-stage stock solution tank, the three-stage feed pump, the three-stage Y-shaped filter, the three-stage high-pressure pump and the three-stage membrane assembly are sequentially connected end to end so as to realize the conveying and the backflow of second-stage permeate liquid, deionized water and third-stage concentrated liquid;
firstly, under the action of a primary feed pump, pumping a stock solution into a primary Y-shaped filter from a primary stock tank, filtering large-particle substances by the primary Y-shaped filter, pumping the filtered stock solution into a primary membrane component under the action of a primary high-pressure pump, filtering macromolecular proteins, polysaccharides and some insoluble substances by the primary membrane component to obtain a primary permeate and a primary concentrate, refluxing the primary concentrate into the primary stock tank, and flowing the primary permeate into a secondary stock tank;
secondly, pumping the primary permeate liquid into a secondary Y-shaped filter from a secondary raw material tank under the action of a secondary feed pump, continuously filtering large-particle substances through the secondary Y-shaped filter, pumping the filtered primary permeate liquid into a secondary membrane module under the action of a secondary high-pressure pump, treating the secondary permeate liquid through the secondary membrane module to obtain secondary permeate liquid and secondary concentrate liquid, refluxing the secondary concentrate liquid back to the secondary raw material tank, outputting the secondary concentrate liquid as a finished product liquid under the action of the secondary feed pump, and allowing the secondary permeate liquid to flow into a tertiary raw material tank;
the secondary nanofiltration membrane system can be added with a proper amount of deionized water to elute the salt content in the secondary concentrated solution according to the product requirements in the operation process, for example, the mass fraction of sodium chloride contained in the original product is 5%, while the mass fraction of sodium chloride in the secondary finished product solution needs to be controlled within 0.5%, so that constant volume desalination needs to be carried out in a secondary original solution tank, and the process mainly utilizes the characteristic that the sodium chloride is not intercepted while the nanofiltration membrane intercepts the product;
finally, pumping the secondary permeate from the tertiary raw material tank into a tertiary Y-shaped filter under the action of a tertiary feed pump, filtering the secondary permeate by the secondary Y-shaped filter, pumping the filtered secondary permeate into a tertiary membrane module under the action of a secondary high-pressure pump, treating the secondary permeate by the tertiary membrane module to obtain tertiary permeate and tertiary concentrate, and refluxing the tertiary concentrate back to the secondary raw material tank for secondary recovery of a product, and collecting or discharging the tertiary permeate;
under the action of the feed pump and the high-pressure pump, the deionized water passes through the stock solution tank and the membrane module and then flows back to the stock solution tank, and the feed pump, the Y-shaped filter, the high-pressure pump and the membrane module are cleaned;
after purifying the heparin sodium solution by a 50000Dal or 80000Dal ultrafiltration membrane, detecting the protein, the content of P-containing substances and the titer of heparin sodium in filtrate, and calculating to obtain the following table 1:
TABLE 150000Dal or 80000Dal Ultrafiltration membranes data for the detection of the filtrate after filtration of the sodium heparin solution
Specifically, (1) the primary ultrafiltration membrane system mainly has the main functions of purifying a heparin sodium product and removing some macromolecular impurities in the heparin sodium solution, and because the molecular weight of the heparin sodium is 12000Dal, in order to ensure the recovery rate of the heparin sodium, an ultrafiltration membrane with the molecular weight of 50000Dal or 80000Dal is selected for purification, the recovery rate of the heparin sodium in the purification process of the primary ultrafiltration membrane system can reach more than 95%, the impurity removal rate reaches more than 70%, and the lost product is discharged along with the impurities;
(2) the secondary nanofiltration membrane system is mainly used for concentrating and desalting the heparin sodium solution purified by the primary ultrafiltration membrane system, the concentration of the heparin sodium solution can directly meet the concentration requirement of a subsequent working section after being concentrated by the secondary nanofiltration membrane system, the content of sodium chloride can be adjusted according to the requirement of a product, and the lowest concentration of the sodium chloride can be controlled within 200 ppm;
(3) the three-stage nanofiltration membrane system mainly has the advantages that the secondary recovery of heparin sodium is carried out on the permeate of the secondary nanofiltration membrane system, so that the overall product recovery rate is improved;
in conclusion, after a heparin sodium product is purified, filtered, concentrated and recovered by a primary ultrafiltration membrane system, a secondary nanofiltration membrane system and a tertiary nanofiltration membrane system, except for the primary ultrafiltration membrane system, a small amount of product loss is caused, no product loss is caused in other parts, the recovery rate of the heparin sodium is remarkably improved, the damage to the molecular structure of the heparin sodium is reduced to the maximum extent, meanwhile, the whole process is operated at normal temperature, the energy consumption is low, in addition, the required water consumption is low in the whole filtering process, therefore, deionized water can be used, materials are also in a closed equipment environment, the contact with the outside is less, the product quality of the heparin sodium is improved, the alcohol precipitation process is omitted, and the generation and treatment work of ethanol wastewater is avoided.
Specifically, as shown in fig. 5, the input end and the output end of the first-stage high-pressure pump and the first-stage membrane module are sequentially connected end to realize the backflow of the first-stage concentrated solution, and the input end and the output end of the second-stage high-pressure pump and the second-stage membrane module are sequentially connected end to realize the backflow of the second-stage concentrated solution.
The device comprises a first-stage feed pump, a second-stage feed pump and a third-stage feed pump, wherein the first-stage feed pump, the second-stage feed pump and the third-stage feed pump are horizontal stainless steel sanitary centrifugal pumps, the first-stage feed pump, the second-stage feed pump and the third-stage feed pump are used for pumping feed liquid from a first-stage stock solution tank, a second-stage stock solution tank and a third-stage stock solution tank and conveying the feed liquid to a corresponding first-stage Y-type filter, a second-stage Y-type filter and a third-stage Y-type filter, the first-stage high pump, the second-stage high pump and the third-stage high pump are vertical stainless steel centrifugal pumps, the first-stage high pump, the second-stage high pump and the third-stage high pump are respectively used for providing certain flow and pressure for corresponding first-stage membrane assemblies, and only have mechanical seals, no oil seal is used, the material pollution cannot be caused by seal abrasion, and the two pumps of the feed pump and the high-pressure pump are used for: the backflow flow is reduced, the problem that the pressure of an ultrafiltration membrane or nanofiltration membrane system is unstable due to the generation of vortex in a stock solution box and the generation of air caused by large conveying quantity and backflow quantity is prevented, and the transfer pump can be used as a transfer pump after the purification and concentration of feed liquid are finished.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and equivalent alternatives or modifications according to the technical solution of the present invention and the inventive concept thereof should be covered by the scope of the present invention.
Claims (7)
1. A fine heparin sodium desalting system is characterized by comprising a primary ultrafiltration membrane system, a secondary nanofiltration membrane system and a tertiary nanofiltration membrane system, wherein the maximum pressure values of the primary ultrafiltration membrane system, the secondary nanofiltration membrane system and the tertiary nanofiltration membrane system are 6bar, 16bar and 16bar in sequence, the primary ultrafiltration membrane system comprises a primary Y-shaped filter and a primary membrane assembly, the secondary nanofiltration membrane system comprises a secondary Y-shaped filter and a secondary membrane assembly, the tertiary nanofiltration membrane system comprises a tertiary Y-shaped filter and a tertiary membrane assembly, a primary permeate is obtained after a stock solution is filtered by the primary Y-shaped filter and the primary membrane assembly, a secondary permeate and a secondary concentrate are obtained after the primary permeate is filtered by the secondary Y-shaped filter and the secondary membrane assembly, the secondary concentrate is a finished product solution, the secondary permeate is filtered by the tertiary Y-shaped filter and the tertiary membrane assembly to obtain a tertiary permeate and a tertiary concentrate, and the tertiary concentrate flows back to the secondary nanofiltration membrane system, and concentrating the filtrate by a secondary membrane system, and conveying the concentrated filtrate to a finished liquid box to be discharged as a finished liquid.
2. The system for desalinating heparin sodium competitive products according to claim 1, wherein the primary ultrafiltration membrane system further comprises a primary raw liquid tank, a primary feed pump and a primary high-pressure pump, and the input end and the output end of the primary raw liquid tank, the primary feed pump, the primary Y-shaped filter, the primary high-pressure pump and the primary membrane module are sequentially connected end to end so as to realize the conveying or the backflow of the raw liquid, the deionized water and the primary concentrated liquid.
3. The system for desalting of refined heparin sodium according to claim 2, wherein the input end and the output end of the primary high-pressure pump and the primary membrane module are sequentially connected end to realize the backflow of the primary concentrated solution.
4. The fine heparin sodium desalting system according to claim 3, wherein the secondary nanofiltration membrane system further comprises a secondary stock solution tank, a secondary feed pump and a secondary high-pressure pump, and the input end and the output end of the secondary stock solution tank, the secondary feed pump, the secondary Y-shaped filter, the secondary high-pressure pump and the secondary membrane module are sequentially connected end to end so as to realize the conveying, the backflow and the collection of the primary permeate, the deionized water, the secondary concentrate and the tertiary concentrate.
5. The system for desalting of refined heparin sodium according to claim 4, wherein the input end and the output end of the second-stage high-pressure pump and the second-stage membrane module are sequentially connected end to realize the backflow of the second-stage concentrated solution.
6. The fine heparin sodium desalting system according to claim 5, wherein the three-stage nanofiltration membrane system further comprises a three-stage stock solution tank, a three-stage feed pump and a three-stage high-pressure pump, and the input end and the output end of the three-stage stock solution tank, the three-stage feed pump, the three-stage Y-shaped filter, the three-stage high-pressure pump and the three-stage membrane module are sequentially connected end to end so as to realize the conveying and the backflow of the second-stage permeate liquid, the deionized water and the third-stage concentrate liquid.
7. The system for desalinating heparin sodium competitive products according to claim 6, wherein the first-stage feed pump, the second-stage feed pump and the third-stage feed pump are all horizontal stainless steel sanitary centrifugal pumps, the first-stage high pump, the second-stage high pump and the third-stage high pump are all vertical stainless steel centrifugal pumps, and the horizontal stainless steel sanitary centrifugal pumps and the vertical stainless steel centrifugal pumps are only mechanically sealed and have no oil seal.
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| CN202122429633.2U CN215963001U (en) | 2021-10-09 | 2021-10-09 | Fine quality heparin sodium desalination system |
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| CN202122429633.2U CN215963001U (en) | 2021-10-09 | 2021-10-09 | Fine quality heparin sodium desalination system |
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