CN111530293A - Continuous flow-through membrane filtration device and method - Google Patents
Continuous flow-through membrane filtration device and method Download PDFInfo
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- CN111530293A CN111530293A CN202010443535.1A CN202010443535A CN111530293A CN 111530293 A CN111530293 A CN 111530293A CN 202010443535 A CN202010443535 A CN 202010443535A CN 111530293 A CN111530293 A CN 111530293A
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Abstract
The invention discloses a continuous flow-through membrane filtration device and a method, wherein a multistage booster pump is arranged, so that multistage membrane filtration modules can be effectively pressurized in a sectional manner, a membrane element of each filtration module has proper membrane permeation pressure, a membrane retentate concentrated solution of each filtration module continuously enters a next stage of filtration module connected in series until the concentrated solution is finally discharged out of a membrane device, the membrane retentate concentrated solution does not flow back in a circulating manner, and the retentate does not pollute the membrane element in a circulating accumulation manner, so that higher membrane filtration efficiency is obtained. The invention can skip the working module through the bypass arrangement, can flexibly select according to the actual production requirement and has high practicability. The booster pump provided by the invention is matched with parameters of each section of pressure monitoring instrument and each section of flow monitoring instrument to regulate pressure and flow, and is linked with the electric regulating valve to regulate, so that the booster pump can be used for accurately boosting, and the device has high safety and strong stability, and has important values in the fields of liquid solute membrane filtration and liquid solute membrane concentration.
Description
Technical Field
The invention relates to a device and a method for concentrating or filtering liquid solute, in particular to a continuous flow-through membrane filtering device, belonging to the field of concentration and filtration of liquid solute.
Background
Membrane separation is a physical process, and its basic principle is to use a membrane with selective permeability to separate, filter and concentrate solutes, impurities, solvents, etc. in a feed liquid under the driving force of concentration difference, pressure difference, potential difference, etc. Because the membrane separation technology has the functions of filtration, fractional separation, solute concentration, solute purification and refining, and has the characteristics of high efficiency, energy conservation, environmental protection, simple molecular filtration and filtration process, easy control and the like, the membrane separation technology is widely applied to various fields of food, medicine, chemical industry, biology, environmental protection, metallurgy, energy, petroleum, water treatment, electronics, bionics and the like at present, and becomes one of the most important means in the separation science at present.
At present, the membrane filtration device technology mainly adopts a batch type full-circulation filtration technology or a forced internal circulation continuous filtration technology, the device is provided with a booster pump and a plurality of forced circulation pumps, the two membrane filtration devices have more problems, wherein the membrane retention substance of the batch type full-circulation filtration technology membrane device is always in a circulation tank and the membrane device in batch operation time, no discharge device is arranged, along with the increase of filtration times, the concentration of the membrane retention substance rises, the pollution of the membrane element is serious, the membrane flux drops fast, and the membrane filtration efficiency is low; wherein, a large part of the membrane retentate of the membrane device of the forced internal circulation continuous filtration process also exists in the forced internal circulation membrane group, which causes the membrane elements in the membrane group to be polluted by the retentate, the membrane flux is reduced quickly, and the membrane filtration efficiency is low; the existing membrane filtration device only has one booster pump, the osmotic pressure requirement of the membrane is higher along with the rising of the concentration of the intercepted matters, the membrane flux is low because the booster pump cannot provide higher osmotic pressure, and the membrane filtration efficiency cannot be exerted.
"patent 200910129343.7" proposes a multi-stage continuous reverse osmosis membrane concentration system, in which a pressure pump is installed after each stage of membrane stack, thus improving the membrane filtration efficiency, but the pressure pump is too dense, the number of membrane elements in the high-grade membrane stack is gradually reduced, and the flow rate of feed liquid is too large; and when the liquid inlet flow is small, the membrane stack can not be selectively put into operation, and the requirement of low concentration ratio can not be met.
Disclosure of Invention
The invention provides a continuous flow-through membrane filtering device, which is used for realizing more efficient and high-utilization-rate feed liquid filtering or concentration.
The purpose of the invention is realized by the following technical scheme: the utility model provides a continuous STREAMING membrane filtration device, includes feed pump, stoste buffer tank, stoste jar, concentrate jar and dialysis fluid jar, its characterized in that: the filter comprises N filter modules which are sequentially connected in series, wherein N is an integer which is more than or equal to 2 and less than or equal to 15, each filter module comprises M filter groups which are sequentially connected in series, M is an integer which is more than or equal to 1 and less than or equal to 4, each filter group comprises K membrane shells which are connected in parallel, and K is an integer which is more than or equal to 1 and less than or equal to 100; the filter groups are connected in series through the conveying pipelines, the input end of each filter module is provided with a booster pump, the filtrate output end of each filter group is connected with the dialysate tank after being converged, the concentrated liquid output end of the Nth filter module is connected with the concentrated liquid tank, the output end of the concentrated liquid tank is connected with the input end of the concentrated liquid buffer tank, and the feed pump is connected with the input end of the first concentrated module.
Pressure monitoring instruments are arranged among the input end of each filtering module, the concentrated solution output end and each filtering group; the pressure monitoring instruments at the input end and the concentrated solution output end of the filtering module monitor the pressure before the membrane and the pressure after the membrane, and are used for calculating the pressure difference of each filtering module and judging the running condition of the corresponding filtering module; the pressure monitoring instrument monitors the pressure between membranes between the filtering groups, and the pressure monitoring instrument monitors the values of the pressure monitoring instrument at the input end and the output end of the concentrated solution of the filtering module, so that the pressure difference of each filtering group is calculated, and the running condition of the corresponding filtering group is judged.
The filtrate output end of each section of filtering group is connected with a one-way valve and a flow monitoring instrument, and the input end of each filtering module and the concentrated solution output end of the Nth filtering module are connected with the flow monitoring instrument; wherein, the check valve is used for avoiding the filtrating backward flow, flow monitoring instrument is used for detecting each section filtration subgroup's filtrate flow, each filtration module's feed liquor flow and system concentrate flow.
The input end of the first filtering module and the output end of each filtering module are provided with three-way reversing valves, wherein the three-way reversing valve at the output end of each filtering module is connected with the three-way reversing valve at the input end of the first filtering module; the three-way reversing valve is matched with the filtering module to select whether to skip P filtering modules for working, and P is an integer less than or equal to N.
The concentrated liquid output end of the Nth filtering module is connected with a pneumatic ball valve and a concentration meter, and the pneumatic ball valve is connected with an electric regulating valve in parallel; the pneumatic ball valve is used for cleaning the thick liquid, the concentration meter is used for monitoring the concentration of the thick liquid, and the electric adjusting valve can be replaced by a density meter, a quality meter, a concentration meter, a turbidity meter or a refractometer and the like according to requirements.
And liquid level monitoring meters are arranged in the stock solution buffer tank, the stock solution tank, the concentrated solution tank and the dialysate tank and are used as the judgment basis for the starting and stopping conditions of automatic operation.
The continuous overflowing type membrane filtering device further comprises a cleaning system, wherein the cleaning system comprises a dosing module, the dosing module is connected to the input end of the 1 st filtering module, and the dosing module is used for matching with the raw material buffer tank and cleaning a pipeline to clean the device.
The invention relates to a continuous overflowing type membrane filtering method, which is based on the continuous overflowing type membrane filtering device and further comprises an operation desk, a signal receiving end and a control terminal, wherein an operation panel of the operation desk is connected with each controlled element in the filtering device through an internal circuit, and the method comprises the following steps:
s1: setting the liquid inlet flow, concentration ratio and alarm value of the system in an operation table, selecting the opening and closing of a three-way reversing valve on a connecting pipeline of the filtering modules according to the liquid inlet flow, thereby determining the number of the filtering modules participating in the work, and starting a liquid inlet valve and a feeding pump of the raw liquid tank;
s2: each section of pressure detection instrument transmits data to a signal receiving end, the signal receiving end uploads the calculated pressure difference of each section to a control terminal, and each section of booster pump receives an instruction of the control terminal to carry out accurate boosting;
s3: the system stock solution flow monitoring instrument, the system concentrated solution detection instrument and the concentration instrument transmit data to a signal receiving end, the signal receiving end uploads the actual concentration ratio and the concentrated solution concentration obtained through calculation to a control terminal, and the control terminal starts an electric regulating valve to automatically regulate the concentrated solution flow according to the difference value of the actual data and the set data;
s4: the equipment during operation, the concentrate flows into the concentrate jar, and the filtrating flows into the dislysate jar, sets up the automatic start that each liquid was irritated at the operation panel, stops the liquid level data, and the level detection meter in dislysate jar, stock solution buffer tank, stock solution jar, concentrate jar and the dislysate jar is all uploaded the liquid level in the jar, carries out automatic operation or shuts down by control center.
The invention achieves the following beneficial effects:
1. the multistage booster pump is arranged, so that multistage membrane filtration modules can be effectively pressurized in a sectional mode, membrane elements of each filtration module have proper membrane permeation pressure, membrane retentate concentrated solution of each filtration module continuously enters the next stage of filtration modules connected in series until the concentrated solution is finally discharged out of the membrane device, the membrane retentate concentrated solution does not flow back in a circulating mode, the membrane retentate cannot pollute the membrane elements in a circulating accumulation mode, and higher membrane filtration benefit is obtained.
2. The invention can skip the working module through the bypass arrangement, can flexibly select according to the actual production requirement and has high practicability.
3. The booster pump provided by the invention is matched with parameters of each section of pressure monitoring instrument and each section of flow monitoring instrument to regulate pressure and flow, and is linked with the electric regulating valve to regulate, so that the booster pump can be used for accurately boosting, and the device has high safety and strong stability, and has important values in the fields of liquid solute membrane filtration and liquid solute membrane concentration.
Drawings
Other features and advantages of the invention will be apparent from the following description of the preferred embodiments of the invention, taken in conjunction with the accompanying drawings and from the claims. Individual features of the different embodiments shown in the figures may be combined in any desired manner in this case without going beyond the scope of the invention. In the drawings:
FIG. 1 is a schematic block diagram of the structure of the present invention;
fig. 2 is a schematic block diagram of the structure of the embodiment.
The reference numbers illustrate: 1-feeding pump, 2-three-way reversing valve, 3-filtering group, 4-flow monitoring instrument, 5-one-way valve, 6-pressure monitoring instrument, 7-electric regulating valve, 8-pneumatic ball valve, 9-brix meter, 10-stock solution buffer tank, 11-stock solution tank, 12-concentrated solution tank, 13-dialyzing solution tank, 14-filtering module, 15-booster pump and 16-dosing module.
The implementation, functional features and advantages of the objects of the present invention will be further explained with reference to the accompanying drawings.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
Example 1
As shown in fig. 1, a continuous flow-through membrane filtration device comprises a feed pump 1, a stock solution buffer tank 10, a stock solution tank 11, a concentrate tank 12 and a dialysate tank 13, and is characterized in that: the device comprises 2 filtering modules 14 which are sequentially connected in series, wherein each filtering module 14 comprises 2 filtering groups 3 which are sequentially connected in series, and the number of membrane shells in each filtering group 3 is sequentially reduced; the filtration small groups 3 are connected in series through a material conveying pipe, the input end of each filtration module 14 is provided with a booster pump 15, the filtrate output end of each section of filtration small group 3 is converged and then connected with a dialysate tank 13, the concentrated solution output end of the 2 nd filtration module 14 is connected with a concentrated solution tank 12, the output end of a raw solution tank 11 is connected with the input end of a raw solution buffer tank 10, and a feed pump 1 is connected with the input end of a first concentrated module.
The pressure monitoring instrument 6 is arranged among the input end of each filtering module 14, the concentrated solution output end and each filtering group 3; wherein, the pressure monitoring instruments 6 at the input end and the concentrated solution output end of the filtering module 14 monitor the pressure before the membrane and the pressure after the membrane, and are used for calculating the pressure difference of each filtering module 14 and judging the running condition of the corresponding filtering module 14; the pressure monitoring instrument 6 between the filtering groups 3 monitors the pressure between membranes, and the monitoring values of the pressure monitoring instrument 6 at the input end and the concentrated liquid output end of the filtering module 14 are matched for calculating the pressure difference of each filtering group 3 and judging the running condition of the corresponding filtering group 3.
The filtrate output end of each section of filtering group 3 is connected with a one-way valve 5 and a flow monitoring instrument 4, and the input end of each filtering module 14 and the concentrated solution output end of the 2 nd filtering module 14 are connected with the flow monitoring instrument 4; wherein, the check valve 5 is used for avoiding the filtrating backward flow, flow monitor 4 is used for detecting each section filtration subgroup 3's filtrating flow, each filtration module 14's feed liquor flow and system concentrate flow.
The input end of the first filtering module 14 and the output end of each filtering module 14 are provided with three-way reversing valves 2, wherein the three-way reversing valve 2 at the output end of each filtering module 14 is connected with the three-way reversing valve 2 at the input end of the first filtering module 14; the 3 three-way reversing valves 2 are matched to select whether to skip one of the filter modules 14 to work.
The concentrated liquid output end of the 2 nd filtering module 14 is connected with a pneumatic ball valve 8 and a brix meter 9, and the pneumatic ball valve 8 is connected with an electric regulating valve 7 in parallel; the electric regulating valve 7 is used for regulating the flow of the concentrated solution, the pneumatic ball valve 8 is used for bypassing the concentrated solution during cleaning, and the brix meter 9 is used for monitoring the brix of the concentrated solution.
Liquid level monitoring meters are arranged in the stock solution buffer tank 10, the stock solution tank 11, the concentrated solution tank 12 and the dialyzate tank 13 and are used as judgment bases for automatic operation starting and stopping conditions.
The continuous overflowing type membrane filtering device further comprises a cleaning system, the cleaning system comprises a dosing module 16, the dosing module 16 is connected to the input end of the 1 st filtering module 14, and the dosing module 16 is used for being matched with a raw material buffer tank and a cleaning pipeline to clean the device.
The specific implementation method of the embodiment is as follows: setting the liquid inlet flow rate, and selecting a filter module 14 to start working according to the liquid inlet flow rate; the booster pump 15 boosts the filtration modules 14 in sections according to indication values of the membrane front and rear pressure monitoring instruments 6 and the flow monitoring instruments 4 of the filtration modules 14, and keeps a stable state of the system; the electric regulating valve 7 regulates the flow of the concentrated solution according to the indication values of the sugar degree instrument 9 and the system flow monitoring instrument 4 so as to control the filtration concentration ratio or the sugar degree of the concentrated solution; when the device works, concentrated solution flows into the concentrated solution tank 12, and filtrate flows into the dialyzate tank 13.
In order to further achieve the above object, the present invention proposes a second embodiment.
Example 2
As shown in fig. 2, a continuous membrane concentration device comprises a feed pump 1, a stock solution buffer tank 10, a stock solution tank 11, a concentrate tank and a dialysate tank 13, and is characterized in that: the device comprises 3 concentration modules which are sequentially connected in series, wherein each concentration module comprises 2 sections of filtering groups 3 which are sequentially connected in series, and the number of membrane shells in each section of filtering group 3 is sequentially reduced; the filtration small groups 3 are connected in series through a conveying pipeline, the input end of each concentration module is provided with a booster pump 15, the filtrate output end of each section of the filtration small group 3 is converged and then connected with a dialysate tank 13, the concentrated solution output end of the 3 rd concentration module is connected with a concentrated solution tank, the output end of a raw solution tank 11 is connected with the input end of a raw solution buffer tank 10, and a feeding pump 1 is connected with the input end of the first concentration module.
A pressure monitoring instrument 6 is arranged among the input end of each concentration module, the output end of the concentrated solution and each section of filtering group 3; the pressure monitoring instruments 6 at the input end and the concentrated solution output end of the concentration module monitor the pressure before the membrane and the pressure after the membrane, are used for calculating the pressure difference of each concentration module and judging the running condition of the corresponding concentration module; the pressure monitoring instrument 6 monitors the pressure between membranes between the filtering groups 3, and the monitoring values of the pressure monitoring instrument 6 are matched with the input end of the concentration module and the output end of the concentrated solution, so that the pressure difference of each filtering group 3 is calculated, and the running condition of the corresponding filtering group 3 is judged.
The filtrate output end of each section of the filtering group 3 is connected with a one-way valve 5 and a flow monitoring instrument 4, and the input end of each concentration module and the concentrated solution output end of the 2 nd concentration module are connected with the flow monitoring instrument 4; wherein, check valve 5 is used for avoiding the filtrating backward flow, flow monitor 4 is used for detecting each section filtration subgroup 3's filtrate flow, each concentrated module's inlet flow and system's dense solution flow.
The input end of the first concentration module and the output end of each concentration module are provided with three-way reversing valves 2, wherein the three-way reversing valve 2 at the output end of each concentration module is connected with the three-way reversing valve 2 at the input end of the first concentration module; the 4 three-way reversing valves 2 are matched to select whether to skip one of the concentration modules to work.
The concentrated liquid output end of the 3 rd concentration module is connected with a pneumatic ball valve 8 and a brix meter 9, and the pneumatic ball valve 8 is connected with an electric regulating valve 7 in parallel; the electric regulating valve 7 is used for regulating the flow of the concentrated solution, the pneumatic ball valve 8 is used for bypassing the concentrated solution during cleaning, and the brix meter 9 is used for monitoring the density of the concentrated solution.
Liquid level monitoring meters are arranged in the stock solution buffer tank 10, the stock solution tank 11, the concentrated solution tank and the dialyzate tank 13 and are used as judgment bases for automatic operation starting and stopping conditions.
Continuous membrane enrichment facility still includes cleaning system, cleaning system includes medicine module 16, and medicine module 16 is connected at the input of 1 st concentration module, and medicine module 16 is used for cooperating the raw materials buffer tank and washs the pipeline and washs the device.
The specific implementation method of the embodiment is as follows: setting the liquid inlet flow rate, and selecting a plurality of concentration modules to start working according to the liquid inlet flow rate; the booster pump 15 carries out sectional boosting on each section of concentration module according to indicating values of the pressure monitoring instrument 6 in front of and behind each concentration module membrane and the flow monitoring instrument 4 in each section, and the stable state of the system is kept; the electric regulating valve 7 regulates the flow of the concentrated solution according to the indication values of the sugar degree instrument 9 and the system flow monitoring instrument 4 so as to control the filtration concentration ratio or the sugar degree of the concentrated solution; when the device works, the concentrated solution flows into the concentrated solution tank, and the filtrate flows into the dialysis solution tank 13.
The above description is only a preferred embodiment of the present invention, and not intended to limit the scope of the present invention, and all modifications of equivalent structures and equivalent processes, which are made by using the contents of the present specification and the accompanying drawings, or directly or indirectly applied to other related technical fields, are included in the scope of the present invention.
Claims (8)
1. A continuous flow-through membrane filtration device, comprising a feed pump (1), a stock solution buffer tank (10), a stock solution tank (11), a concentrate solution tank (12) and a dialysate solution tank (13), characterized in that: the membrane filtration device comprises N filtration modules (14) which are sequentially connected in series, wherein N is an integer greater than or equal to 2, each filtration module (14) comprises M sections of filtration subgroups (3) which are sequentially connected in series, M is an integer greater than or equal to 1, each section of filtration subgroup (3) comprises K membrane shells which are connected in parallel, and K is an integer greater than or equal to 1;
wherein, filter small group (3) and establish ties through the conveying pipeline, each filter module (14) input is provided with booster pump (15), the filtrating output of every section filter small group (3) joins the back and connects dialysis fluid jar (13), and concentrate fluid jar (12) are connected to the concentrate output of the nth filter module (14), the output of concentrate fluid jar (11) is connected the input of concentrate buffer tank (10), and feed pump (1) is connected to the output of concentrate buffer tank (10), and the input at first concentrated module is connected in feed pump (1).
2. A continuous flow-through membrane filtration device according to claim 1, wherein a pressure monitoring instrument (6) is arranged between the input end of each filtration module (14), the concentrate output end and each section of filtration group (3);
the pressure monitoring instruments (6) at the input end and the concentrated liquid output end of the filtering module (14) monitor the pressure before the membrane and the pressure after the membrane, and are used for calculating the pressure difference of each filtering module (14) and judging the running condition of the corresponding filtering module (14); the pressure monitoring instrument (6) between the filtering groups (3) monitors the pressure between membranes, and the monitoring values of the pressure monitoring instrument (6) at the input end and the concentrated liquid output end of the filtering module (14) are matched for calculating the pressure difference of each filtering group (3) and judging the running condition of the corresponding filtering group (3).
3. The continuous flow-through membrane filtration device according to claim 1, wherein the filtrate output end of each section of filtration group (3) is connected with a one-way valve (5) and a flow monitoring instrument (4), and the input end of each filtration module (14) and the concentrate output end of the Nth filtration module (14) are connected with the flow monitoring instrument (4);
wherein, check valve (5) are used for avoiding the filtrating backward flow, flow monitor (4) are used for detecting the filtrate flow of each section filtration subgroup (3), the feed liquor flow and the system concentrate flow of each filter module (14).
4. A continuous flow-through membrane filtration device according to claim 1, wherein the input of the first filtration module (14) and the output of each filtration module (14) are provided with three-way directional valves (2), wherein the three-way directional valve (2) at the output of each filtration module (14) is connected to the three-way directional valve (2) at the input of the first filtration module (14); the three-way reversing valve (2) is matched with one another to select whether to skip P filtering modules (14) to work, wherein P is an integer less than or equal to N.
5. A continuous flow-through membrane filtration device according to claim 1, wherein a pneumatic ball valve (8) and a concentration meter (9) are connected to the concentrate output end of the nth filtration module (14), and the pneumatic ball valve (8) is connected with an electric regulating valve (7) in parallel; the electric regulating valve (7) is used for regulating the flow of the concentrated solution, the pneumatic ball valve (8) is used for bypassing the concentrated solution during cleaning, and the concentration meter (9) is used for monitoring the concentration of the concentrated solution.
6. The continuous flow-through membrane filtration device according to claim 1, wherein liquid level monitoring meters are arranged in the stock solution buffer tank (10), the stock solution tank (11), the concentrate tank (12) and the dialysate tank (13) as the judgment basis for the starting and stopping conditions of automatic operation.
7. The continuous flow-through membrane filtration device according to claim 1, further comprising a cleaning system, wherein the cleaning system comprises a dosing module (16), the dosing module (16) is connected to the input end of the 1 st filtration module (14), and the dosing module (16) is used for matching with the raw material buffer tank (10) and the cleaning pipeline to clean the device.
8. A continuous flow membrane filtration process comprising a continuous flow membrane filtration device according to any one of claims 1 to 7, comprising the steps of:
s1: setting liquid inlet flow, selecting a filtering module (14) to start working according to the liquid inlet flow, enabling the filtering modules not participating in the working to be in a standby state, and connecting the concentrated liquid output end of each filtering module in series from the 1 st filtering module participating in the working to the input end of the next filtering module until the concentrated liquid output end of the last filtering module participating in the working;
s2: the booster pump (15) boosts each section of the filtering module (14) in a sectional manner according to the indicating values of the membrane front and rear pressure monitoring instrument (6) and each section of the flow monitoring instrument (4) of each filtering module (14) to keep the stable state of the system;
s3: the electric regulating valve (7) regulates the flow of the concentrated solution according to the indicating values of the concentration meter (9) and the system flow monitoring meter (4) so as to control the filtration concentration ratio or the concentration of the concentrated solution;
s4: when the device works, concentrated solution flows into a concentrated solution tank (12), and filtrate flows into a dialysis solution tank (13).
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| CN112370971A (en) * | 2020-09-22 | 2021-02-19 | 山东大溪环保科技发展有限公司 | Separation and concentration method and separation and concentration device for food materials |
| CN113441011A (en) * | 2021-07-20 | 2021-09-28 | 合肥科锐特环保工程有限公司 | Gelatin film treatment facility |
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| CN113441011A (en) * | 2021-07-20 | 2021-09-28 | 合肥科锐特环保工程有限公司 | Gelatin film treatment facility |
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