CN111007041B - Method for reducing misinformation of turbidity meter in brine refined ceramic membrane filter - Google Patents
Method for reducing misinformation of turbidity meter in brine refined ceramic membrane filter Download PDFInfo
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- CN111007041B CN111007041B CN201911301884.3A CN201911301884A CN111007041B CN 111007041 B CN111007041 B CN 111007041B CN 201911301884 A CN201911301884 A CN 201911301884A CN 111007041 B CN111007041 B CN 111007041B
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Abstract
The invention discloses a method for reducing misinformation of a turbidimeter in a brine refined ceramic membrane filter, belongs to the technical field of brine refining of ceramic membranes, and provides a method capable of reducing misinformation of the turbidimeter in the brine refined ceramic membrane filter. According to the invention, through carrying out process control of the first liquid supplementing control process in the close vicinity after the backwashing stage is finished and additionally arranging the blank breaking device on the refined brine collecting pipe, two main reasons causing misinformation of the turbidity meter can be respectively solved, so that the problem of misinformation of the turbidity meter in the brine refining ceramic membrane filter can be effectively solved, and the stable operation of equipment and the effective operation of the online monitoring and chain shutdown functions of the turbidity meter are ensured.
Description
Technical Field
The invention relates to the technical field of ceramic membrane brine refining, in particular to a method for reducing misinformation of a turbidimeter in a brine refining ceramic membrane filter.
Background
The ceramic membrane brine refining process has the advantages of high filtration precision, short process flow, less equipment and the like, and is widely applied to the chlor-alkali industry in recent years.
The ceramic membrane belongs to an ultrafiltration membrane, and flux is reduced due to pollution on the surface of the membrane along with the extension of filtration time, so that physical backwashing is required at regular time. The physical back flushing is to press back flushing liquid (refined brine) into the membrane from the permeation side through a corresponding automatic quick-opening valve after the refined brine is pressurized by compressed air in a back flushing tank, so as to carry out back flushing on the surface of the membrane. After the ceramic membrane filter is self-started, a circulation process of filtering → backflushing → filtering … … is carried out, time is taken as control, the corresponding backwashing process of the ceramic membrane is divided into a backwashing stage and a filtering timing stage, namely, the filtering enters the backwashing stage after the filtering is carried out for a set time, and the filtering timing of the next circulation is started after the backwashing stage is finished. The existing backwashing stage is that the liquid level condition of the backwashing liquid in the backwashing tank is judged before each backwashing stage, if the liquid level is met, the backwashing operation is directly carried out, and the filtration timing of the next cycle is started after the backwashing operation is finished; if the liquid level is not satisfied, the liquid is replenished to the specified liquid level in the backflushing tank and is pressurized, and then the backflushing operation is carried out.
The ceramic membrane filter adopts a cross flow filtration process, and the filtration pressure is about 0.3 Mpa; an on-line turbidity meter is arranged on a refined brine header on the refined brine side of the penetrating fluid and is used for monitoring the quality of the refined brine obtained by filtering and interlocking shutdown; when the membrane tube is damaged and the sealing surface leaks, the penetrating fluid refined salt water becomes turbid, and the turbidity value monitored by the turbidity meter becomes high, so that the chain shutdown can be realized.
In the actual operation of the original ceramic membrane filter equipment, the condition of alarm chain shutdown of the turbidity meter frequently occurs, particularly when the ceramic membrane is subjected to a physical backwashing stage. However, the examination confirmed that the indicator of the refined brine and the ceramic membrane were normal, which actually belongs to the case of "misinformation" of the brine quality by a turbidity meter. The problem of misinformation of the turbidity meter is consistent and no root cause is found, so the problem is not effectively solved all the time; some units have to remove the chain shutdown function of turbidity appearance for the steady operation of equipment under such circumstances, rely on the manual work to patrol and examine the observation sight glass and monitor the refined salt water quality, and its actual up to the purpose of on-line monitoring refined salt water quality, the manual work is patrolled and examined moreover and is accomplished timely efficient monitoring effect, still can increase workman work load simultaneously.
Disclosure of Invention
The invention aims to provide a method capable of reducing the false alarm condition of a turbidity meter in a ceramic membrane filter for brine refining.
The technical scheme adopted by the invention for solving the technical problems is as follows: the method for reducing the misinformation of the turbidity meter in the brine refined ceramic membrane filter comprises a ceramic membrane backwashing process, wherein the ceramic membrane backwashing process comprises a backwashing stage and a filtering timing stage which are carried out in a circulating manner, and a first fluid supplementing control process is carried out adjacently after the backwashing stage in each circulating manner is finished; the first liquid supplementing control process can supplement the backflushing liquid into the backflushing tank; and after the liquid supplementing operation is carried out in the first liquid supplementing control process, keeping the backflushing liquid in the backflushing tank to stand until the filtration timing stage of the secondary cycle is finished, so as to release the micro bubbles in the backflushing liquid through standing.
Further, the method comprises the following steps: the first liquid supplementing control process comprises the steps of detecting and judging whether the actual liquid level L in the backflushing tank is higher than a liquid level lower limit set value L0 or not, when the detected actual liquid level L is higher than a liquid level lower limit set value L0, liquid supplementing operation is not carried out, and otherwise, liquid supplementing operation is carried out.
Further, the method comprises the following steps: the replenishing liquid in the first liquid replenishing control process is penetrating liquid or refined salt water; when the penetrating fluid is selected as the supplementary fluid, the filtration timing of the current circulation is started after the fluid is supplemented; when the refined brine is selected as the make-up fluid, the make-up fluid is adopted and the filtration timing of the current cycle is synchronized.
Further, the method comprises the following steps: and keeping standing until the standing time T when the filtration timing phase of the secondary cycle is finished is not less than 25 minutes after the completion of the liquid supplementing operation in the first liquid supplementing control process of each cycle.
Further, the method comprises the following steps: and immediately before the start of the back flushing stage of each cycle, performing a second liquid supplementing control process, wherein the second liquid supplementing control process is consistent with the first liquid supplementing control process.
Further, the method comprises the following steps: the device comprises a tee joint and a blank breaking pipe which are connected to the refined brine collecting pipe, one end of the blank breaking pipe is connected with the tee joint, the other end of the blank breaking pipe extends upwards and is an open end, and the height of the blank breaking pipe extending upwards meets the following requirements: so that the refined salt water flowing through the refined salt water collecting pipe can not overflow from the open end of the refined salt water collecting pipe.
Further, the method comprises the following steps: the height of the upward extension of the hollow breaking pipe is not less than 2 m.
Further, the method comprises the following steps: the water-saving water dispenser is characterized in that a pure water dropping pipe is further arranged at the open end of the hollow breaking pipe, a dropping switch is arranged on the pure water dropping pipe, and the pure water dropping pipe can drop pure water into the hollow breaking pipe in a dropping mode.
Further, the method comprises the following steps: the tee joint is a reducing tee joint, the refined brine collecting pipe is a DN200 pipe, and the broken hollow pipe is a DN50 pipe.
The invention has the beneficial effects that: by adopting the method, the first liquid supplementing control process is performed closely after the backwashing phase is finished, so that whether the liquid level height in the backwashing tank meets the solution amount required by the next cycle can be detected and judged at the first time after the backwashing phase is finished to judge whether the liquid supplementing is required, the backwashing liquid in the backwashing tank after the liquid supplementing can be sufficiently kept still within the time of the filtration timing phase in each cycle after the corresponding liquid supplementing operation is performed, and the micro bubbles introduced into the backwashing liquid by the liquid supplementing operation in the first liquid supplementing control process can be effectively released through the keeping still treatment, so that the misreporting condition of the turbidity meter caused by the micro bubbles contained in the backwashing liquid can be reduced to a certain extent. In addition, the invention also further arranges a blank breaking device on the refined brine collecting pipe at the downstream of the turbidity meter, and the blank breaking device can reduce or even avoid the pipeline negative pressure condition caused by the reduction of the refined brine flow in the refined brine collecting pipe in the backwashing operation process, thereby reducing the turbidity meter false alarm condition caused by the cut-off of the refined brine at the detection part of the turbidity meter due to the negative pressure. The invention combines the process control of the first liquid supplementing control process carried out next to the main pipe of the refined brine gathering pipe after the backwashing stage is finished with the structure of the vacuum breaking device, and can respectively solve the two main reasons causing the misinformation of the turbidity meter, thereby effectively solving the problem of the misinformation of the turbidity meter in the brine refining ceramic membrane filter, and ensuring the stable operation of the equipment and the effective operation of the online monitoring and the interlocking shutdown functions of the turbidity meter.
Drawings
FIG. 1 is a schematic process flow diagram of an exemplary ceramic membrane filter having three filtration stages;
FIG. 2 is a schematic view of an installation structure of the vacuum breaking device;
FIG. 3 is an exemplary flow chart of a main process for the ceramic membrane filter of FIG. 1 when the existing control process is used;
FIG. 4 is an exemplary flow chart of a main process for an exemplary ceramic membrane filter of FIG. 1 utilizing the control process of the present invention;
FIG. 5 is an example of a flow chart of a first fluid replacement control process in the ceramic membrane filter of FIG. 1;
FIG. 6 is an example of a flow chart of a second fluid replacement control process in the ceramic membrane filter of FIG. 1;
FIG. 7 is an exemplary flow diagram of a process for backwashing the modules in the ceramic membrane filter of FIG. 1;
labeled in the figure as: the device comprises a backflushing tank 7, a refined salt water collecting pipe 2, an air breaking device 3, a turbidity meter 1, a tee joint 5, an air breaking pipe 4, a pure water dropping pipe 6, a dropping switch 8, a backflushing liquid pipe 9, a first-level permeate liquid pipe 10, a second-level permeate liquid pipe 11 and a self-flowing section 12.
Detailed Description
The invention is further described with reference to the following figures and detailed description.
The method for reducing the misinformation of the turbidity meter in the saline water refined ceramic membrane filter is characterized in that the ceramic membrane filter for saline water refining is used as an equipment base, and the conditions of misinformation of the turbidity meter 1 in the ceramic membrane filter during the ceramic membrane backwashing operation are reduced by means of technological process optimization, structure improvement optimization and the like.
After theoretical analysis of the problem causing the false alarm of the turbidity meter 1, the inventors of the present application considered that the following two main causes are responsible for the false alarm of the turbidity meter 1: firstly, in the process control process of the original ceramic membrane filter, backwashing is carried out immediately after the liquid is replenished into a backwashing tank 7, micro bubbles are carried in the backwashing liquid in the liquid replenishing process of the backwashing tank 7, if the micro bubbles are not released in time, the micro bubbles enter the side of refined brine through the backwashing liquid, and when the refined brine containing the micro bubbles flows through the position of a turbidity meter 1, the turbidity meter 1 adopts an optical principle for detection, the micro bubbles in the liquid influence the light transmittance, so that the turbidity meter 1 is triggered to generate a false alarm condition; second, because of the equipment fixing needs, ceramic membrane main part equipment generally all installs in relatively higher position, follow-up pipeline is provided with downwardly extending's gravity flow section 12 usually in its refined salt water collection pipe 2, when carrying out the ceramic membrane back flush operation in-process, the negative pressure condition often can appear because of the reduction of the flow in refined salt water collection pipe 2, and then cause the situation of cutting off the flow at 1 sample site of turbidity meter easily, because of turbidity meter 1 adopts optical principle, the light that sees through when cutting off the flow will change, and then trigger the condition that turbidity meter 1 took place the false positive.
Based on the above analysis, it is found that the problem of the occurrence of the erroneous alarm of the turbidity meter 1 in the ceramic membrane filter for brine purification can be solved by taking corresponding measures for two main reasons. For the first reason, the problem can be solved in a direction of reducing the amount of fine bubbles introduced into the solution on the refined brine side during the ceramic membrane backwash; the second reason is that the negative pressure condition caused by the reduction of the flow rate in the refined brine collecting pipe 2 in the ceramic membrane backwashing operation process can be reduced or even avoided.
Based on the above analysis, the technical solution of the present application is optimized and improved in the process flow of the ceramic membrane filter for brine purification as follows, in order to solve the problem of the occurrence of the false alarm of the turbidity meter 1 caused by the first reason: the ceramic membrane backwashing process comprises a backwashing stage and a filtering timing stage which are carried out circularly, so that in the backwashing stage and the filtering timing stage which are carried out circularly, a first liquid supplementing control process is carried out adjacently after the backwashing stage in each cycle is finished; the backflushing liquid can be replenished into the backflushing tank 7 through the first liquid replenishing control process; and after the liquid supplementing operation is carried out in the first liquid supplementing control process, keeping the backflushing liquid in the backflushing tank 7 standing until the filtration timing stage of the current cycle is finished, so as to release the micro bubbles in the backflushing liquid through standing. After the optimization and improvement, the ceramic membrane backwashing operation can be performed after backwashing liquid is replenished into the backwashing tank 7 every time and then can be performed for a period of time instead of performing the ceramic membrane backwashing operation after the backwashing liquid is replenished every time; in this way, the fine bubbles introduced into the backwash liquid by the backwash liquid replenishment can be effectively released by the standing treatment, and the amount of the fine bubbles introduced into the refined brine in the backwash operation of the subsequent backwash liquid can be greatly reduced, whereby the occurrence of the false alarm of the turbidity meter 1 due to the first cause can be reduced. The optimization and improvement of the specific process flow can be seen with reference to the difference between fig. 3 and fig. 4, wherein fig. 3 is a flow chart of a main process of the ceramic membrane filter shown in fig. 1 when the original control process flow is adopted, and the part in the double-dotted line is a flow chart of the back washing process of the original ceramic membrane; and FIG. 4 is a flow chart of a main process for an example of the ceramic membrane filter of FIG. 1, the main optimization of which is illustrated by the two-dot chain line, when the process is controlled according to the present invention.
Without loss of generality, referring to fig. 4, the first fluid replacement control process in the present application includes detecting and determining whether the actual liquid level L in the backflushing tank 7 is higher than a lower liquid level limit set value L0, and performing no fluid replacement operation when the detected actual liquid level L is higher than a lower liquid level limit set value L0, otherwise performing fluid replacement operation. This is because, in a normal situation, the backflushing tank 7 can meet the requirement of performing backflushing operation for two or more cycles after each liquid replenishing according to the liquid storage capacity; in this case, therefore, it is possible to allow no liquid replenishment to be performed in the case where the amount of backflushing liquid in the backflushing tank 7 satisfies the amount of backflushing liquid required for the backflushing operation during the next cycle; after each liquid replenishing, two or more cycles can be continuously operated, and then the next liquid replenishing is carried out, so that the quantity of micro bubbles introduced into the backflushing liquid due to frequent liquid replenishing can be further reduced. Without loss of generality, the lower liquid level limit set value L0 should at least satisfy the amount of backflushing liquid required for backflushing operation in one cycle; meanwhile, the upper limit of the allowable liquid storage amount of the backflushing tank 7 from the liquid replenishing to the liquid replenishing can be set every time the liquid is replenished.
The backwashing operation is actually to perform backwashing on each stage of components in the ceramic membrane filter, and for the ceramic membrane filter comprising the three stages of components shown in the attached drawing 1, the backwashing operation of the first stage of components can be performed first, and then the backwashing operation of the second and third stage of components can be performed. The whole backwashing operation process can be carried out as shown in the attached figure 6.
According to the invention, by setting the first liquid supplementing control process, liquid can be supplemented in time according to the liquid level condition in the backflushing tank 7 when each backflushing stage is finished, and then the backflushing liquid in the backflushing tank 7 after liquid supplementing can be subjected to standing treatment by fully utilizing the time of the filtering timing stage in each cycle operation, so that micro bubbles introduced into the backflushing liquid due to liquid supplementing are released. In order to ensure that the backflushing tank 7 has enough standing time after liquid replenishing every time to ensure the release of micro bubbles introduced by liquid replenishing, the method further comprises the step of keeping standing until the standing time T after the filtering timing phase of the secondary cycle is finished is not less than 25 minutes after liquid replenishing operation is finished in the first liquid replenishing control process of each cycle, for example, the standing time T can be set to be 30 minutes according to actual operation conditions. Of course, in order to meet the requirement of the standing time T, the time length of a reasonable filtering timing stage can be set for control; meanwhile, the standing time T is close to the time length of the filtration timing stage as much as possible so as to prolong the standing time to the maximum extent.
Without loss of generality, the invention can further set the supplementary liquid in the first liquid supplementing control process to be penetrating liquid or refined salt water; the selection of the permeate or the refined brine as the supplementary liquid belongs to the prior art in the field, and the technology of the selection of the kind of the supplementary liquid is not improved in the invention. Specifically, the penetrating fluid in the invention refers to a liquid filtered by penetrating through the ceramic membrane tube, and the liquid is directly replenished into the backflushing tank 7 after penetrating through the ceramic membrane tube; and the refined brine refers to the brine after the permeate has been stored in a refined brine storage tank by adjusting the pH and removing free chlorine; strictly speaking, the composition of these two types of liquids is essentially the same, both being "refined brine"; the invention adopts different reference modes, and aims to distinguish different sources of the two liquids so as to correspond to different control processes in the liquid supplementing operation process.
In addition, according to different types of the selected supplementary liquid, different time points are adopted as the starting points of the filtration timing, and the method specifically comprises the following steps: when the penetrating fluid is selected as the supplementary fluid, the filtration timing of the current circulation is started after the fluid is supplemented; when the refined brine is selected as the make-up fluid, the make-up fluid is taken in synchronization with the filtration timing of the current cycle. Referring specifically to fig. 5, for the control of the selection of permeate or concentrate as make-up fluid, corresponding buttons may be provided on the control system interface of the ceramic membrane filter for selection, and the timing start point of the filtration timing stage is controlled individually according to the type of make-up fluid selected. The above arrangement is adopted because when permeate liquid replenishing is selected, the back flushing tank is replenished with the two-stage and three-stage permeate liquid directly, and at this time, the two-stage and three-stage permeate liquid is cut off to the concentrate water collecting pipe, such as FV102 is closed firstly in the attached figure 1; therefore, the filtration flow rate of the entire ceramic membrane is not considered to reach the operation flow rate, and the time is not generally counted. When the refined brine is selected for liquid supplement, the refined brine of the refined brine storage tank is used, and the integral filtering flow of the ceramic membrane is not influenced, so that liquid supplement and filtering can be carried out synchronously, and timing can be carried out firstly. Different modes are selected for timing, so that the filtering time of the ceramic membrane is prolonged as much as possible, and the back flushing times are reduced.
In addition, in the traditional original control process flow, the liquid level condition of the back flushing liquid in the back flushing tank is judged before each back flushing stage, and liquid is replenished according to the detection condition; the main reason for this is because the ceramic membrane is strictly prohibited from being backflushed without backflushing liquid during operation, because if a large amount of compressed air is backflushed, it can lead to breakage of the ceramic membrane tubes.
Without loss of generality, the invention can further reserve the second liquid supplementing control process which is performed immediately before the start of the backwashing phase of each cycle in the original control process flow, and can further ensure that enough backwashing liquid is contained in the backwashing tank 7 during the next backwashing operation by reserving the second liquid supplementing control process; the situation that backwashing operation is performed under the condition that backwashing liquid is insufficient due to the fact that backwashing liquid is leaked between the first liquid supplementing control process and the second liquid supplementing control process can be avoided; thereby ensuring that enough backflushing liquid is available during each backflushing operation.
Without loss of generality, the second liquid supplementing control process is consistent with the first liquid supplementing control process, and specifically comprises the steps of detecting and judging whether the actual liquid level L in the backflushing tank 7 is higher than a liquid level lower limit set value L0, when the detected actual liquid level L is higher than a liquid level lower limit set value L0, liquid supplementing operation is not carried out, and otherwise, liquid supplementing operation is carried out; and in the second liquid supplementing control process, penetrating liquid or refined salt water can be selected as supplementing liquid according to the requirement. Referring to fig. 5 and fig. 6, the flow chart shown in fig. 5 has a plurality of timing points corresponding to "start filtering timing" because different filtering timing starting points are required according to the selection types of the replenishment liquids, but the timing points are only related to the time of the filtering timing stage and do not substantially affect the replenishment operation itself, so that the second replenishment control process is considered to be consistent with the first replenishment control process.
Aiming at the condition that the turbidity meter 1 is mistakenly reported due to the second point, the method is additionally provided with a blank breaking device on the basis of the original equipment. Referring to the attached drawings 1 and 2, an air breaking device 3 is arranged on a concentrate water collecting pipe 2 in a ceramic membrane filter, the air breaking device 3 is arranged immediately downstream of a turbidity meter 1 along the flow direction of the concentrate water collecting pipe 2, the air breaking device 3 comprises a tee joint 5 and an air breaking pipe 4 which are connected to the concentrate water collecting pipe 2, one end of the air breaking pipe 4 is connected with the tee joint 5, the other end of the air breaking pipe 4 extends upwards and is an open end, and the height of the upward extending of the air breaking pipe 4 meets the following requirements: so that the refined brine flowing through the refined brine collecting pipe 2 cannot overflow from the open end thereof. Like this, can realize salt solution collection pipe 2 and outside air UNICOM through the open end of broken hollow tube 4, can inhale the air in order to avoid the negative pressure to influence the detection accuracy of turbidity appearance 1 through broken hollow tube 4 when the negative pressure condition appears in salt solution collection pipe 2. Wherein, broken hollow tube 4 upwards extends and can be the ascending extension of slope, also can be vertical upwards extension, as long as its height after extending can satisfy and avoid the salt solution overflow condition.
Without loss of generality, the refined salt water collecting pipe 2 collects filtered refined salt water solution corresponding to each stage of component, and then conveys the solution to a refined salt water storage tank for storage or conveys the solution to downstream equipment for use; as shown in fig. 1, the refined brine collecting pipe 2 is a refined brine solution in which respective first-stage permeate pipe 10 and second-stage permeate pipe 11 are collected. Of course, the corresponding turbidity meter 1 should be installed on the concentrate water collecting pipe 2 after the first stage permeate pipe 10 and the second stage permeate pipe 11 are collected, so as to ensure that the turbidity meter 1 can simultaneously detect the concentrate water collected by the first stage permeate pipe 10 and the second stage permeate pipe 11.
More preferably, it is considered that after the vacuum breaker 3 is installed, ambient air is introduced through the vacuum breaker 4, and the temperature of the refined brine solution in the refined brine header pipe 2 is lowered, and the refined brine solution is usually a saturated brine solution, so that the solubility is lowered after the temperature is lowered, salt crystals are easily precipitated, and the pipeline is easily clogged. For this purpose, in the present invention, a pure water dropping pipe 6 is further provided at the open end of the blank pipe 4, a dropping switch 8 is provided on the pure water dropping pipe 6, and the pure water dropping pipe 6 can drop pure water into the blank pipe 4 in a dropping manner. Without loss of generality, the speed of adding pure water into the blank pipe 4 through the pure water dropping pipe 6 can be reasonably adjusted according to actual needs, and the adjustment can be realized by controlling the opening of the dropping switch 8.
In addition, in order to ensure that the refined salt water solution flowing through the refined salt water collecting pipe 2 does not overflow from the open end at the upper end of the blank-breaking pipe 4, in the invention, in combination with the normal solution pressure condition in the refined salt water collecting pipe 2, the upward extending height of the blank-breaking pipe 4 is preferably set to be not less than 2 meters, for example, the upward extending height of the blank-breaking pipe 4 can be specifically set to be 2 meters; wherein, the height refers to a height value corresponding to the projection of the broken hollow pipe 4 in the vertical direction.
In addition, considering that the refined brine collecting pipe 2 is a pipeline adopting DN200 in a normal condition, and the main function of the blank breaking pipe is used for communicating with the outside air, the requirement on the pipe diameter of the blank breaking pipe 4 is not high. Referring to fig. 2, it is further preferable in the present invention that the tee 5 is a reducer tee, the refined brine collecting pipe 2 is a DN200 pipe, and the blank breaking pipe 4 is a DN50 pipe. Like this, the pipe diameter of broken blank pipe 4 can be little for the pipe diameter of salt solution collecting main 2, can reduce as far as possible because of setting up the temperature reduction circumstances of the salt solution of flowing through in salt solution collecting main 2 behind broken blank pipe 4 under the circumstances of guaranteeing to break the blank effect.
Claims (8)
1. The method for reducing the misinformation of the turbidity meter in the brine refined ceramic membrane filter comprises a ceramic membrane backwashing process, wherein the ceramic membrane backwashing process comprises a backwashing stage and a filtering timing stage which are carried out in a circulating mode, and is characterized in that: carrying out a first fluid infusion control process immediately after the end of the backwashing phase in each cycle; the first liquid supplementing control process can supplement the backflushing liquid into the backflushing tank (7); after the liquid supplementing operation is carried out in the first liquid supplementing control process, keeping the backflushing liquid in the backflushing tank (7) standing until the filtration timing stage of the current cycle is finished, and releasing micro bubbles in the backflushing liquid through standing; be provided with on smart salt solution header pipe (2) in ceramic membrane filter and break empty device (3), break empty device (3) and set up the low reaches in turbidity meter (1) along the flow direction of smart salt solution header pipe (2) next door, break empty device (3) including connecting tee bend (5) and broken empty pipe (4) on smart salt solution header pipe (2), the one end and the tee bend (5) of broken empty pipe (4) link to each other, the other end of broken empty pipe (4) upwards extends and is the opening end, and the height that broken empty pipe (4) upwards extended satisfies following requirements: so that the refined salt water flowing through the refined salt water collecting pipe (2) can not overflow from the open end.
2. The method of reducing turbidimeter false alarms in brine finishing ceramic membrane filters of claim 1, wherein: the first liquid supplementing control process comprises the steps of detecting and judging whether the actual liquid level L in the backflushing tank (7) is higher than a liquid level lower limit set value L0 or not, and when the detected actual liquid level L is higher than a liquid level lower limit set value L0, liquid supplementing operation is not carried out, otherwise, liquid supplementing operation is carried out.
3. The method of reducing turbidimeter false alarms in brine finishing ceramic membrane filters of claim 1, wherein: the replenishing liquid in the first liquid replenishing control process is penetrating liquid or refined salt water; when the penetrating fluid is selected as the supplementary fluid, the filtration timing of the current circulation is started after the fluid is supplemented; when the refined brine is selected as the make-up fluid, the make-up fluid is taken in synchronization with the filtration timing of the current cycle.
4. The method of reducing turbidimeter false alarms in brine finishing ceramic membrane filters of claim 1, wherein: and keeping standing until the standing time T when the filtration timing phase of the secondary cycle is finished is not less than 25 minutes after the completion of the liquid supplementing operation in the first liquid supplementing control process of each cycle.
5. The method of reducing turbidimeter false alarms in brine finishing ceramic membrane filters of claim 1, wherein: and immediately before the start of the back flushing stage of each cycle, performing a second liquid supplementing control process, wherein the second liquid supplementing control process is consistent with the first liquid supplementing control process.
6. The method of reducing turbidimeter false alarms in brine finishing ceramic membrane filters of claim 1, wherein: the height of the upward extension of the hollow breaking pipe (4) is not less than 2 m.
7. The method of reducing turbidimeter false alarms in brine finishing ceramic membrane filters of claim 1, wherein: and a pure water dropping pipe (6) is further arranged at the open end of the broken hollow pipe (4), a dropping switch (8) is arranged on the pure water dropping pipe (6), and the pure water dropping pipe (6) can drop pure water into the broken hollow pipe (4) in a dropping mode.
8. The method of reducing turbidimeter false alarms in brine finishing ceramic membrane filters of claim 1, wherein: the tee joint (5) is a reducing tee joint, the refined brine collecting pipe (2) is a DN200 pipe, and the blank breaking pipe (4) is a DN50 pipe.
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