CN114345423A - Continuous ion-exchange resin resuscitation method and system - Google Patents
Continuous ion-exchange resin resuscitation method and system Download PDFInfo
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- CN114345423A CN114345423A CN202210069353.1A CN202210069353A CN114345423A CN 114345423 A CN114345423 A CN 114345423A CN 202210069353 A CN202210069353 A CN 202210069353A CN 114345423 A CN114345423 A CN 114345423A
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- ion exchange
- exchange resin
- valve
- resin
- resin column
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- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 title claims abstract description 127
- 239000003456 ion exchange resin Substances 0.000 title claims abstract description 127
- 229920003303 ion-exchange polymer Polymers 0.000 title claims abstract description 127
- 238000000034 method Methods 0.000 title claims abstract description 64
- 239000011347 resin Substances 0.000 claims abstract description 109
- 229920005989 resin Polymers 0.000 claims abstract description 108
- 238000011084 recovery Methods 0.000 claims abstract description 101
- 230000008929 regeneration Effects 0.000 claims abstract description 43
- 238000011069 regeneration method Methods 0.000 claims abstract description 43
- 238000005086 pumping Methods 0.000 claims abstract description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 71
- 238000011001 backwashing Methods 0.000 claims description 40
- 239000007788 liquid Substances 0.000 claims description 39
- 230000001186 cumulative effect Effects 0.000 claims description 36
- 230000008569 process Effects 0.000 claims description 36
- 230000001105 regulatory effect Effects 0.000 claims description 25
- 239000003513 alkali Substances 0.000 claims description 17
- 239000000463 material Substances 0.000 claims description 14
- 238000002386 leaching Methods 0.000 claims description 12
- 238000002791 soaking Methods 0.000 claims description 8
- 238000004519 manufacturing process Methods 0.000 claims description 6
- 238000011010 flushing procedure Methods 0.000 claims description 4
- 238000007664 blowing Methods 0.000 claims description 2
- 230000001960 triggered effect Effects 0.000 claims description 2
- 230000000694 effects Effects 0.000 abstract description 6
- 238000005342 ion exchange Methods 0.000 description 14
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 239000002253 acid Substances 0.000 description 4
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 3
- 238000004891 communication Methods 0.000 description 3
- 230000006870 function Effects 0.000 description 3
- 230000009191 jumping Effects 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000012492 regenerant Substances 0.000 description 2
- 239000011780 sodium chloride Substances 0.000 description 2
- 238000010408 sweeping Methods 0.000 description 2
- 244000261422 Lysimachia clethroides Species 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 150000001450 anions Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000003745 diagnosis Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 238000000338 in vitro Methods 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- XZPVPNZTYPUODG-UHFFFAOYSA-M sodium;chloride;dihydrate Chemical compound O.O.[Na+].[Cl-] XZPVPNZTYPUODG-UHFFFAOYSA-M 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J49/00—Regeneration or reactivation of ion-exchangers; Apparatus therefor
- B01J49/60—Cleaning or rinsing ion-exchange beds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J49/00—Regeneration or reactivation of ion-exchangers; Apparatus therefor
- B01J49/80—Automatic regeneration
- B01J49/85—Controlling or regulating devices therefor
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treatment Of Water By Ion Exchange (AREA)
Abstract
The invention discloses a method and a system for recovering continuous ion-exchange resin, wherein the method comprises the following steps: and positioning the excessively ineffective ion exchange resin column, starting a recovery program to automatically pump the resin in the excessively ineffective ion exchange resin column into a recovery tank for resin recovery, and automatically pumping the resin back into the ion exchange resin column after the resin recovery is finished. The system comprises a DCS control unit, a data acquisition unit, a pneumatic valve bank and a resuscitation tank. The resin leading-in and leading-out and resin recovery processes are carried out automatically, manual operation is not needed, the operation is simple and convenient, the period is short, the recovery effect is uniform, standardization can be realized, and the like, so that the problem of frequent resin recovery and regeneration is solved.
Description
Technical Field
The invention relates to the field of ion exchange of starch sugar and biological fermentation, in particular to a continuous ion exchange resin recovery method and a system.
Background
In the related field of application ion exchange, ion exchange resin is widely applied to purification and treatment processes in various fields such as medicine health, different devices are involved, the occupied area is large, the ion exchange resin cannot be moved, the ion exchange resin needs to be designed and installed according to actual conditions in engineering application, the construction period is long, the operation cost is high, especially in the engineering transformation process, when original devices need to be replaced by new devices, a factory needs to be shut down to implement, the resin recovery treatment is carried out, the process is more complex, and the production continuity can be affected even.
In the operation process of the ion exchange resin, the resin is influenced by materials and water quality, so that the operation period is short, the resin is frequently regenerated, and the resin needs to be frequently regenerated. The existing resin recovery tank is not connected with an acid and alkali conveying system of a workshop, a regenerant cannot be directly pumped into the resin recovery tank for recovery, the prepared acid and alkali agent can be led into the resin recovery tank from a manhole, the operation is inconvenient, safety risks exist, the resuscitation depends on long-time continuous regeneration, and the resuscitation cannot be uniformly mixed.
Chinese patent CN 111533216A discloses a method for recovering anion and cation resin. The regeneration dosage needing to be allocated is large, the operation period is long, the artificial factors are many, and the recovery effect is uneven.
Disclosure of Invention
In view of the purpose of solving the defects of the prior art, the invention provides a method and a system for recovering resin by continuous ion exchange, so as to solve the problem of frequent regeneration of resin recovery. The resuscitation process is automatic, the operation is simple and convenient, the period is short, the resuscitation effect is uniform, and the standardization can be realized.
The invention provides a method for recovering continuous ion-exchange resin, which comprises the following steps: and positioning the excessively ineffective ion exchange resin column, starting a recovery program to automatically pump the resin in the excessively ineffective ion exchange resin column into a recovery tank for resin recovery, and automatically pumping the resin back into the ion exchange resin column after the resin recovery is finished. An excessively spent ion exchange resin column is a resin column that cannot recover the ion exchange function even after a regeneration process in a continuous ion exchange resin valve array system.
The method for positioning the excessively failed ion exchange resin column comprises the following steps: acquiring parameters of all ion exchange resin columns in the continuous ion exchange resin valve array system, and determining that the ith ion exchange resin column is excessively ineffective when the ith ion exchange resin column simultaneously meets the following conditions:
d.SUM[i]>＝SUMmax
e.Lmn[i]>Lmnmaxand the duration is longer than the set time
f. The pH value and the conductivity value of the discharged material exceed the set values,
wherein SUM [ i]Means the total flow rate of the material flowing through the i ion exchange resin column, SUMmaxFor a set total flow of material through a single ion exchange resin column;
Lmn[i]is the opening of the automatic regulating valve on the ith ion exchange resin column, LmnmaxThe maximum opening size of the automatic regulating valve is set. In condition b, the duration, i.e., the self-regulating valve continues Lmn [ i [ ]]>LmnmaxThe time of the state.
When the ion exchange resin columns are positioned to be excessively failed, the recovery is carried out according to the sequence of the process positions of the ion exchange resin columns.
When the order of the positioned excessively spent ion exchange resin columns is i column, i + j column, i + k column, the i + j column can be subjected to the recovery procedure only after the i column is recovered.
The recovery procedure is initiated when the ion exchange resin column positioned for excessive failure is run to the sugar top water process level.
The resuscitation procedure was as follows:
opening a resin outlet valve and a backwashing water inlet valve at the bottom of the ion exchange resin column, opening a resin inlet valve of a recovery tank, pumping resin into the recovery tank, and closing all valves of the ion exchange resin column after the resin is discharged;
adjusting the height of the liquid level in the recovery tank to keep the liquid level in the recovery tank at a middle liquid level switch;
opening a saline-alkali water solution inlet valve, and injecting the saline-alkali water solution into the recovery tank to a set accumulated flow volume; the saline-alkali water is a mixed solution of sodium chloride and sodium hydroxide;
step four, closing all valves of the recovery tank, and soaking the resin until the corresponding ion exchange resin column is switched to a set process position of the production procedure;
opening an exhaust valve and an air inlet valve of the recovery tank, and introducing air into the recovery tank to perform back blowing on the resin until the set time;
opening a water inlet valve and a regeneration blow-down valve of the recovery tank, leaching the resin by using desalted water, and finishing leaching when the cumulative flow volume of the desalted water reaches a set value;
opening a lower water inlet valve and a backwashing upper discharge valve of the recovery tank, backwashing the resin by using desalted water, and finishing backwashing when the cumulative flow volume of the desalted water reaches a set value;
step eight, adjusting the liquid level height of the resuscitation tank to a middle liquid level switch;
opening an exhaust valve of the resuscitation tank, and releasing the pressure of the resuscitation tank;
step ten, opening a recovery tank cross regeneration valve and a regeneration blow-down valve, performing cross regeneration on the resin by using the regeneration liquid, and stopping adding the regeneration liquid when the accumulated flow volume of the regeneration liquid reaches a set value;
step eleven, closing all valves of the recovery tank, and soaking the resin until the corresponding ion exchange resin column is switched to a water-top sugar setting process position;
step twelve, opening a water inlet valve and a regeneration blow-down valve of the recovery tank, leaching the resin by using desalted water, and closing the water inlet valve and the regeneration blow-down valve after leaching is finished when the cumulative flow volume of the desalted water reaches a set value;
step thirteen, opening a lower water inlet valve and a backwashing upper discharge valve of the recovery tank, backwashing the resin by using desalted water, and finishing backwashing when the cumulative flow volume of the desalted water reaches a set value;
step fourteen, opening a backwashing outlet valve and a bottom resin outlet valve on a recovery tank, connecting the recovery tank with a resin flushing valve on a pipeline connecting the recovery tank with an ion exchange resin column, and driving the resin back to the ion exchange resin column by a resin inlet valve, a backwashing outlet valve and a blowdown valve of the corresponding ion exchange resin column, wherein when a liquid level switch at the bottom of the recovery tank is triggered, the resin is completely driven;
and step fifteen, switching the ion exchange resin column to a backwashing procedure, and finishing recovery.
And step fourteen, the ion exchange resin column is finished when being positioned at a set process position of the water sugar-ejecting process, and if the ion exchange resin column is not finished, the continuous ion exchange resin valve array system needs to wait for the step fourteen to be finished and then carries out switching.
Step one, the execution time exceeds the set time T1setAnd finally, executing the step two.
The adjusting method of the second step comprises the following steps: when the liquid level of the recovery tank is higher than the medium liquid level switch, opening an air inlet valve and a regeneration blow-down valve of the recovery tank to remove part of liquid; when the liquid level of the resuscitation tank is lower than the middle liquid level switch, the exhaust valve is opened to remove certain gas so as to increase the liquid level.
Step two execution time exceeds the set time T2setAnd finally, executing the third step.
The invention also provides a continuous ion exchange resin resuscitation system, which comprises a DCS control unit, a data acquisition unit, a pneumatic valve bank and a resuscitation tank, wherein the resuscitation tank is communicated with the ion exchange resin column in the continuous ion exchange resin valve array system through a pipeline; the DCS control unit comprises a CPU, an IO module and a pneumatic valve set control module, the IO module receives parameter data transmitted by the data acquisition unit and transmits the parameter data to the CPU, the CPU positions the excessively failed ion exchange resin column according to the parameters of the ion exchange resin column obtained by the data acquisition unit, the pneumatic valve set control module controls the pneumatic valves between the excessively failed ion exchange resin column and the recovery tank and the pneumatic valves on the recovery tank to be opened and closed through the IO module, and a recovery program is started.
The data acquisition unit comprises a flowmeter, a regulating valve, a pressure sensor, a pH value measuring instrument and a conductivity measuring instrument which are arranged on each ion exchange resin column, and the flowmeter, the regulating valve and a liquid level switch which are arranged on the resuscitation tank.
The resin inlet of the ion exchange resin column is connected to the resin outlet of the recovery tank through a three-way valve, and the resin outlet of the ion exchange resin column is connected to the resin inlet of the recovery tank through a three-way valve.
The ion exchange resin column satisfying the following three conditions at the same time is an excessively spent ion exchange resin column:
d.SUM[i]>＝SUMmax
e.Lmn[i]>Lmnmaxand the duration is longer than the set time
f. The pH value and the conductivity value of the discharged material exceed the set values,
wherein SUM [ i]Means the total flow rate of the material flowing through the i ion exchange resin column, SUMmaxFor a set total flow of material through a single ion exchange resin column;
Lmn[i]is the opening of the automatic regulating valve on the ith ion exchange resin column, LmnmaxThe maximum opening size of the automatic regulating valve is set. In condition b, the duration, i.e., the self-regulating valve continues Lmn [ i [ ]]>LmnmaxThe time of the state.
Compared with the prior art, the technical scheme of the invention has the following beneficial effects: the resin leading-in and leading-out and resin recovery processes are carried out automatically, manual operation is not needed, the operation is simple and convenient, the period is short, the recovery effect is uniform, standardization can be realized, and the like, so that the problem of frequent resin recovery and regeneration is solved.
Drawings
Figure 1 shows a diagram of a continuous ion exchange resin valve array system.
Figure 2 shows a schematic diagram of the connection of the continuous ion exchange resin valve array system to the resuscitation canister.
Figure 3 shows a schematic of resuscitation canister and pneumatic valve set connections.
Fig. 4 shows a schematic of a resuscitation canister resin resuscitation flow.
Detailed Description
The present invention will be described in detail with reference to the following embodiments in order to fully understand the objects, means, and effects of the present invention. Unless otherwise defined, technical terms referred to in the present invention have meanings commonly understood by those skilled in the art.
Example 1
This example serves to illustrate the implementation of the present invention to combine the DCS system with a conventional improvement of the ion-exchange resuscitation apparatus.
The invention also provides a continuous ion exchange resin resuscitation system, which comprises a DCS control unit, a data acquisition unit, a pneumatic valve bank and a resuscitation tank, wherein the resuscitation tank is communicated with the ion exchange resin column in the continuous ion exchange resin valve array system through a pipeline; the DCS control unit comprises a CPU, an IO module and a pneumatic valve set control module, the IO module receives parameter data transmitted by the data acquisition unit and transmits the parameter data to the CPU, the CPU commands positions the excessively failed ion exchange resin column according to parameters of the ion exchange resin column obtained by the data acquisition unit, the pneumatic valve set control module controls the pneumatic valves between the excessively failed ion exchange resin column and the recovery tank and the pneumatic valves on the recovery tank to be opened and closed through the IO module, and a recovery program is started.
The data acquisition unit comprises a flowmeter, a regulating valve, a pressure sensor, a pH value measuring instrument and a conductivity measuring instrument which are arranged on each ion exchange resin column, and the flowmeter, the regulating valve and a liquid level switch which are arranged on the resuscitation tank.
The IO module is arranged in the valve island cabinet, and the flowmeter, the regulating valve, the pressure sensor, the pH value measuring instrument and the conductivity measuring instrument on each ion exchange resin column are connected to the IO module of the valve island cabinet through signal lines.
The pneumatic valve is a double-acting valve and is connected to an electromagnetic valve group in the valve island cabinet through an air pipe. Pneumatic valves control module among the DCS control unit passes through profinet bus, connects the IO module, through digital output module drive solenoid valve, and pneumatic valve A hole admits air, and the pneumatic valve is opened, closes the solenoid valve, and pneumatic valve B hole admits air, and the pneumatic valve is closed.
The DCS control unit also comprises a communication interface module and an MRP (media redundancy) ring network, the CPU and the IO module slave station are connected into the MRP ring network through a PROFINET bus, the MRP obviously improves the availability of equipment, and the fault of single equipment has no influence on communication. The DCS control unit also includes a SCADA system connected to the CPU via PROFINET bus to monitor and control the operating equipment in the field. The recovery tank is connected with the continuous ion exchange valve array system through pipelines of a resin inlet and a resin outlet of the ion exchange resin column. And the DCS is electrically connected with the recovery tank and the running mechanism in the continuous ion-exchange valve array system. The invention has the advantages of automatic resuscitation process, simple operation, short period, uniform resuscitation effect, realization of standardization and the like, and solves the problem of frequent resin resuscitation and regeneration.
The manual valve and the manual device in the traditional ion exchange are changed into the automatic valve, and the field instrument is improved into the intelligent instrument. The recovery steps summarized by the traditional operating rules of the ion exchange are compiled into a PLC program, and a DCS system acquires signals of a field flowmeter, a liquid level and a pressure, controls a field switch valve, a regulating valve and a pump to realize the automatic recovery of the ion exchange program.
When the resin is revived in vitro, the normal material feeding of the continuous ion-exchange system can not be influenced, and the reviving program needs to interlock the main program of the continuous ion-exchange.
Example 2
This example is for explaining the continuous ion exchange resin valve array system according to the present invention, and as shown in fig. 1, the continuous ion exchange resin valve array system includes a production process, a sugar water top process, a backwashing process, a regeneration process, and a sugar top water process.
The inlet of each ion exchange resin column is provided with a flowmeter and a regulating valve, the feeding flow rate is set, the PLC circulation sweeping period is set to be n (unit: ms), and the maximum feeding volume k (unit: m) of the ith ion exchange resin column is set3) The resin loading is v (unit: m is3)，flowfeed[i](unit: m)3H) is the current flow rate of the ith ion exchange resin column, the cumulative volume SUM [ i]The following were used:
SUM[i]＝SUM[i]+flowfeed[i]/3600000*n；
SUM [ i ] > k v, the PLC program marks the column as potentially resuscitable
Meanwhile, a pH value measuring instrument and a conductivity measuring instrument are installed on a discharge pipe of the ion exchange resin column, and whether the resin exchange capacity of the ith ion exchange resin column is reduced or not and whether the ion exchange resin column needs to be recovered or not are judged through comprehensive analysis of data of the instruments.
The resin inlet of each ion exchange resin column is connected to the resin outlet of the resuscitation tank through a three-way valve, the three-way valve is opened, the resin inlet is communicated with the resin outlet of the resuscitation tank, the three-way valve is closed, the resin inlet is closed, as shown in fig. 2, the resin outlet of the ion exchange resin column is connected to the resin inlet of the resuscitation tank through the three-way valve, the three-way valve is opened, and the ion exchange resin column outlet is communicated with the resin inlet pipeline of the resin resuscitation tank.
Example 3
This example illustrates the resuscitation canister configuration, as shown in FIG. 3
The lining rubber in the recovery tank can prevent the corrosion of acid and alkali;
the top of the recovery tank is connected with pure water, acid, alkali, saline-alkali water and a water inlet pipeline, the pipeline is provided with a regulating valve and a flowmeter, the upper regulating valve is used for controlling the flow of the water inlet, the acid-alkali water and the saline-alkali water,
an air inlet switch valve, an exhaust switch valve and a liquid level switch in the linkage of the air inlet and exhaust valves are arranged on the top of the recovery tank.
The upper part of the secondary tank body is connected with a back washing pipeline.
The bottom of the resuscitation tank body is connected with an air inlet pipe, a backwashing water inlet pipe, a blow-off pipe and a regeneration blow-off pipe, wherein the downstream of the regeneration blow-off pipe is connected with a gooseneck pipe.
An upper liquid level switch 113, a middle liquid level switch 114 and a bottom liquid level switch 115 are arranged on the resuscitation tank body.
Example 4
This example illustrates the operation of the present continuous ion-exchange resin resuscitation system.
The DCS control unit of the continuous ion-exchange resin recovery system selects a Siemens 1500 series CPU, is provided with an et200sp module, supports the functions of hot plug, online diagnosis, state display and the like, an upper computer selects winc, all pneumatic valves and motors can be operated on the winc picture, an automatic mode is set, and a DCS system can automatically execute programs according to a parameter table. The communication mode of the main control system is Profinet, and the programming language adopts SCL language.
Example 5
This example is used in the flow of the present continuous ion-exchange resin resuscitation method, as shown in fig. 2, 3, and 4.
Firstly, running a positioned column to be resuscitated to a sugar top water process position to start to execute a resuscitation program, wherein sugar top water of a main program is not executed any more at the moment, and the steps 1 and 2 (comprising backwashing, regeneration and sugar top water) of the main program (a continuous ion exchange program) are continuously executed, and the step 3 (water top sugar) is not executed; the continuous ion exchange valve array system opens the resin outlet valve and resin backwash inlet valve at the bottom of the column, opens the resin inlet valve 108 of the resuscitation tank, injects resin into the resuscitation tank, and the column is resuscitated at T1 (or Time)t1) After the resin discharge is completed, all valves are in a closed state (including when the column is operated to the refining and production process position). The parameter of the step is Time which is larger than the set Timet1setJumping to the next step, setting the PLC cycle sweeping period as n (unit: ms)
Timet1＝Timet1+n；
Timet1>Timet1setThe program executes the next step
Step two, discharging the part of the recovery tank, opening a switch higher than the middle liquid level, and opening an air inlet valve 106 and a regeneration blow-down valve 109; below the mid-level switch, vent valve 107 is opened, the primary function of this step is to maintain the liquid level at mid-level. The parameter of the step is time which is larger than the set time, and the next step is skipped.
Timet2＝Timet2+n；
Timet2>Timet2setThe program executes the next step
Step three, opening a saline-alkali water inlet device, pumping saline-alkali water into the resuscitation tank, and opening a saline-alkali water inlet valve105, a regeneration blow-down valve 109, and an upper regulating valve 101 for feeding the saline-alkali water. The flow meter 102 measures the flow rate of the saline-alkali water, the parameter is volume control, and the accumulated flow volume reaches a set value and jumps to the next step. SUMv3FT102 is the count value of flowmeter 102, SUM, for the cumulative flow volume of saltwater to third stepv3setCumulative flow volume for the set saline water:
SUMv3＝SUMv3+FT102/3600000*n；
SUMv3set>SUMv3the program executes the next step
And step four, closing all valves of the resuscitation tank, switching to a soaking state, and entering a dormant state. At this time, the resuscitation program needs to interlock with the main program in operation, namely when the resuscitation column is cut to the production set process position, such as the 3 rd process position, and the accumulated time is greater than the set time, the soaking is judged to be finished. Timet4For the cumulative running Time of the fourth step, Timet4setFor a set cumulative time:
Timet4＝Timet4+n；
Timet4>Timet4setthe program executes the next step
Step five, opening the exhaust valve 107 of the resuscitation tank, wherein the parameter of the step is Time which is larger than the set Time, jumping to the next step, and the Timet5For the cumulative running Time of the fifth step, Timet5setFor a set cumulative time:
Timet5＝Timet5+n；
Timet5>Timet5setthe program executes the next step
And step six, opening the resin scrubbing valve 120 of the recovery tank, backwashing the upper discharge valve 121, and performing back flushing to loosen resin. The parameter of the step is Time which is larger than the set Time, the next step is skipped to, and the Time ist6Is the cumulative running Time of the sixth step, Timet6setFor a set cumulative time:
Timet6＝Timet6+n；
Timet6>Timet6setthe program executes the next step
And step seven, leaching, namely opening the water inlet valve 103, the regeneration blow-down valve 109 and the upper inlet regulating valve 101 of the recovery tank to perform leaching, and interlocking with the liquid level switch to maintain the medium liquid level. This step was performed to dilute the brine water and to avoid resin running during backwashing up to step eight. The parameters are volume control, cumulative flow volume arrives, jump to next step, SUMv7FT102 is the counter value, SUM, of flowmeter 102 for the cumulative flow volume of the seventh step desalinated waterv7setCumulative flow volume for the set desalted water:
SUMv7＝SUMv7+FT102/3600000*n；
SUMv7set>SUMv7the program executes the next step
And step eight, opening the recovery tank backwashing switch valve 116, the backwashing valve 121 and the descending regulating valve 111 to perform backwashing operation. This step is based on a clean resin backwash. The parameters are volume control, cumulative flow volume arrives, jump to next step, SUMv8FT111 is the count value of the flow meter 111, SUM, for the cumulative flow volume of the desalted water of the eighth stepv8setCumulative flow volume for the set desalted water:
SUMv8＝SUMv8+FT111/3600000*n；
SUMv8set>SUMv8the program executes the next step
Opening a regeneration blowdown valve 109 of the recovery tank, opening a switch higher than the medium liquid level, and opening an air inlet valve 106; below the mid level switch, vent valve 107 is opened, lowering the resin tank level. The parameter of the step is Time which is larger than the set Time, the next step is skipped to, and the Time ist9For the cumulative running Time of the ninth step, Timet9setFor a set cumulative time:
Timet9＝Timet9+n；
Timet9>Timet9setthe program executes the next step
Step ten, opening the exhaust valve 107 of the resuscitation tank to release the pressure of the resuscitation tank, accumulating the pressure of the resuscitation tank by using Time, jumping to the next step, Time, wherein the Time is the parameter of the step, and is more than the set Timet10Is as followsTen step cumulative run Time, Timet10setFor a set cumulative time:
Timet10＝Timet10+n；
Timet10>Timet10setthe program executes the next step
Step eleven, performing cross regeneration, opening a cross regeneration valve 104, a regeneration blow-off valve 109 and an upper adjusting valve 101, performing cross regeneration on the resin, and performing volume accumulation, SUM (surface energy management) on the resinv11For the cumulative flow volume of the regeneration liquid (the regeneration liquid may be hydrochloric acid or sodium hydroxide solution, determined according to the type of resin) of the eleventh step, FT102 is the count value of the flow meter 102, SUMv11setFor a set cumulative flow volume of regeneration fluid:
SUMv11＝SUMv11+FT102/3600000*n；
SUMv11set>SUMv11the program executes the next step
And step twelve, closing all valves of the recovery tank, switching to a soaking state, and entering a dormant state. At this Time, the resuscitation program needs to interlock with the main program in operation, namely when the resuscitation column is cut to the water top sugar setting process level (such as the 3 rd process level), the soaking is judged to be finished, and the Time ist12Is the accumulated running Time of the twelfth step, Timet12setFor a set cumulative time:
Timet12＝Timet12+n；
Timet12>Timet12setthe program executes the next step
And step thirteen, rinsing, namely opening the water inlet valve 103 of the recovery tank, the regeneration blow-down valve 109 and the upper inlet regulating valve 101 for rinsing. This step is performed to dilute the regenerant and prevent resin slip during backwashing. The parameters are volume control, cumulative flow volume arrives, jump to next step, SUMv13FT102 is the count value of flowmeter 102, SUM, for the cumulative flow volume of the thirteenth step desalinated waterv13setCumulative flow volume for the set desalted water:
SUMv13＝SUMv13+FT102/3600000*n；
SUMv13set>SUMv13the program executes the next step
Step fourteen, opening the exhaust valve 107 of the resuscitation tank, wherein the parameter of the step is Time which is larger than the set Time, jumping to the next step, and the Timet14For the cumulative running Time of the fourteenth step, Timet14setFor a set cumulative time:
Timet14＝Timet14+n；
Timet14>Timet14setthe program executes the next step
And step fifteen, backwashing 2, opening a backwashing switch valve 116 of the recovery tank, a backwashing valve 121 and a descending regulating valve 111 to perform backwashing operation. The parameters are volume control, cumulative flow volume arrives, jump to next step, SUMv15FT110 is the count value, SUM, of flow meter 110 for the cumulative flow volume of the fifteenth step desalinated waterv15setCumulative flow volume for the set desalted water:
SUMv15＝SUMv15+FT110/3600000*n；
SUMv15set>SUMv15the program executes the next step
Sixthly, after the recovery is finished, the resin needs to be pumped back to the ion exchange column, the back washing valve 121, the resin outlet valve 119 and the resin flushing water valve 118 are opened, and the descending regulating valve 111 is opened; opening a resin inlet valve, a backwashing outlet valve and a blow-down valve on an ion exchange column (resin column), pumping resin back to the resin column through a disc pump 121, triggering a liquid level switch 115 at the bottom of a recovery tank, namely judging that the resin is pumped up, wherein the step needs to be finished in a process position (such as a 3 rd process position) set by water top sugar, if the step is not finished, a main program needs to wait for the step, and the Time ist16For the cumulative running Time of the sixteenth step, Timet16setFor a set cumulative time:
Timet16＝Timet16+n；
Timet16>Timet16setthe program executes the next step
Seventhly, opening a recovery tank exhaust valve 107, wherein the Time is the parameter of the step, the Time is larger than the set Time, the next step is skipped, and the Time ist17Is the accumulation of the seventeenth stepCounting the running Time, Timet17setFor a set cumulative time:
Timet17＝Timet17+n；
Timet17>Timet17setthe program executes the next step
Eighteen, when the main program of the to-be-recovered column is switched to the backwashing process position, judging that the recovery period is finished.
Timet18＝Timet18+n；
Timet18>Timet18setThe program executes the next step
In the recovery process, leaching, backwashing and exhausting are required to be completed in the process period that the recovery column is in the water-top sugar process position, and if the leaching, backwashing and exhausting are not completed, the main process needs to wait, and the steps cannot be cut. And after the recovery program is finished, switching the recovery column to a backwashing process position, and judging that the recovery period is finished. The automatic and intelligent resuscitation process is realized.
The above embodiments are only preferred embodiments of the present invention, but the present invention is not limited to the above embodiments, and it should be understood that any modifications, equivalent substitutions, improvements and the like within the spirit and principle of the present invention by those skilled in the art are included in the protection scope of the present invention.
Claims (10)
1. A method for recovering continuous ion-exchange resin is characterized by comprising the following steps: and positioning the excessively ineffective ion exchange resin column, starting a recovery program to automatically pump the resin in the excessively ineffective ion exchange resin column into a recovery tank for resin recovery, and automatically pumping the resin back into the ion exchange resin column after the resin recovery is finished.
2. The method for continuous ion exchange resin resuscitation according to claim 1, wherein the method for locating an excessively spent ion exchange resin column is: acquiring parameters of all ion exchange resin columns in the continuous ion exchange resin valve array system, and determining that the ith ion exchange resin column is excessively ineffective when the ith ion exchange resin column simultaneously meets the following conditions:
a.SUM[i]>＝SUMmax
b.Lmn[i]>Lmnmaxand the duration is longer than the set time
c. The pH value and the conductivity value of the discharged material exceed the set values,
wherein SUM [ i]Means the total flow rate of the material flowing through the i ion exchange resin column, SUMmaxFor a set total flow of material through a single ion exchange resin column;
Lmn[i]is the opening of the automatic regulating valve on the ith ion exchange resin column, LmnmaxThe maximum opening size of the automatic regulating valve is set.
3. The continuous ion exchange resin resuscitation method according to any one of claims 1 or 2, wherein when the plurality of ion exchange resin columns are positioned to be excessively spent, the resuscitation is performed in order of the process sites in which the ion exchange resin columns are located.
4. The continuous ion exchange resin resuscitation method of any one of claims 1 or 2, wherein the resuscitation procedure is initiated when an ion exchange resin column positioned for excessive failure is run to a sugar top water process site.
5. The continuous ion-exchange resin resuscitation method according to any one of claims 1 or 2, wherein the resuscitation procedure is as follows:
opening a resin outlet valve and a backwashing water inlet valve at the bottom of the ion exchange resin column, opening a resin inlet valve of a recovery tank, pumping resin into the recovery tank, and closing all valves of the ion exchange resin column after the resin is discharged;
adjusting the height of the liquid level in the recovery tank to keep the liquid level in the recovery tank at a middle liquid level switch;
opening a saline-alkali water solution inlet valve, and injecting the saline-alkali water solution into the recovery tank to a set accumulated flow volume;
step four, closing all valves of the recovery tank, and soaking the resin until the corresponding ion exchange resin column is switched to a set process position of the production procedure;
opening an exhaust valve and an air inlet valve of the recovery tank, and introducing air into the recovery tank to perform back blowing on the resin until the set time;
opening a water inlet valve and a regeneration blow-down valve of the recovery tank, leaching the resin by using desalted water, and closing the water inlet valve and the regeneration blow-down valve after leaching is finished when the cumulative flow volume of the desalted water reaches a set value;
opening a lower water inlet valve and a backwashing upper discharge valve of the recovery tank, backwashing the resin by using desalted water, and closing the lower water inlet valve and the backwashing upper discharge valve when the cumulative flow volume of the desalted water reaches a set value;
step eight, adjusting the liquid level height of the resuscitation tank to a middle liquid level switch;
opening an exhaust valve of the resuscitation tank, and releasing the pressure of the resuscitation tank;
step ten, opening a recovery tank cross regeneration valve and a regeneration blow-down valve, performing cross regeneration on the resin by using the regeneration liquid, and stopping adding the regeneration liquid when the accumulated flow volume of the regeneration liquid reaches a set value;
step eleven, closing all valves of the recovery tank, and soaking the resin until the corresponding ion exchange resin column is switched to a set process position of the water-top sugar procedure;
step twelve, opening a water inlet valve and a regeneration blow-down valve of the recovery tank, leaching the resin by using desalted water, and closing the water inlet valve and the regeneration blow-down valve after leaching is finished when the cumulative flow volume of the desalted water reaches a set value;
step thirteen, opening a lower water inlet valve and a backwashing upper discharge valve of the recovery tank, backwashing the resin by using desalted water, and finishing backwashing when the cumulative flow volume of the desalted water reaches a set value;
step fourteen, opening a backwashing outlet valve and a bottom resin outlet valve on a recovery tank, connecting the recovery tank with a resin flushing valve on a pipeline connecting the recovery tank with an ion exchange resin column, and driving the resin back to the ion exchange resin column by a resin inlet valve, a backwashing outlet valve and a blowdown valve of the corresponding ion exchange resin column, wherein when a liquid level switch at the bottom of the recovery tank is triggered, the resin is completely driven;
and step fifteen, switching the ion exchange resin column to a backwashing procedure, and finishing recovery.
6. The method for recovering continuous ion exchange resin according to claim 5, wherein the fourteen steps are completed when the ion exchange resin column is at the set process position of the water-top-sugar process, and if the ion exchange resin column is not completed, the continuous ion exchange resin valve array system waits for the fourteen steps to be completed and then performs switching.
7. A continuous ion exchange resin recovery system is characterized by comprising a DCS control unit, a data acquisition unit, a pneumatic valve bank and a recovery tank, wherein the recovery tank is communicated with an ion exchange resin column in a continuous ion exchange resin valve array system through a pipeline; the DCS control unit comprises a CPU, an IO module and a pneumatic valve set control module, the IO module receives parameter data transmitted by the data acquisition unit and transmits the parameter data to the CPU, the CPU positions the excessively failed ion exchange resin column according to the parameters of the ion exchange resin column obtained by the data acquisition unit, the pneumatic valve set control module controls the pneumatic valves between the excessively failed ion exchange resin column and the recovery tank and the pneumatic valves on the recovery tank to be opened and closed through the IO module, and a recovery program is started.
8. The continuous ion exchange resin resuscitation system of claim 7, wherein the data acquisition unit comprises a flow meter, a regulating valve, a pressure sensor, a pH meter, a conductivity meter disposed on each ion exchange resin column, and a flow meter, a regulating valve and a level switch disposed on the resuscitation tank.
9. The continuous ion exchange resin resuscitation system according to claim 7, wherein the resin inlet of the ion exchange resin column is connected to the resin outlet of the resuscitation tank by a three-way valve, and the resin outlet of the ion exchange resin column is connected to the resin inlet of the resuscitation tank by a three-way valve.
10. The continuous ion exchange resin resuscitation system according to claim 7, wherein the ion exchange resin column satisfying the following three conditions simultaneously is an excessively spent ion exchange resin column:
a.SUM[i]>＝SUMmax
b.Lmn[i]>Lmnmaxand the duration is longer than the set time
c. The pH value and the conductivity value of the discharged material exceed the set values,
wherein SUM [ i]Means the total flow rate of the material flowing through the i ion exchange resin column, SUMmaxFor a set total flow of material through a single ion exchange resin column;
Lmn[i]is the opening of the automatic regulating valve on the ith ion exchange resin column, LmnmaxThe maximum opening size of the automatic regulating valve is set.
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| CN115504541A (en) * | 2022-09-14 | 2022-12-23 | 西安热工研究院有限公司 | Method and device for positioning ion exchange resin of condensate polishing system |
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