CN219730619U - High-water-quantity multi-tank desalting equipment - Google Patents
High-water-quantity multi-tank desalting equipment Download PDFInfo
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- CN219730619U CN219730619U CN202320570057.XU CN202320570057U CN219730619U CN 219730619 U CN219730619 U CN 219730619U CN 202320570057 U CN202320570057 U CN 202320570057U CN 219730619 U CN219730619 U CN 219730619U
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- 238000011033 desalting Methods 0.000 title abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 155
- 239000002253 acid Substances 0.000 claims abstract description 63
- 238000000034 method Methods 0.000 claims abstract description 38
- 239000002351 wastewater Substances 0.000 claims abstract description 32
- 238000005406 washing Methods 0.000 claims abstract description 29
- 239000012267 brine Substances 0.000 claims abstract description 15
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 15
- 239000011347 resin Substances 0.000 claims description 108
- 229920005989 resin Polymers 0.000 claims description 108
- 239000003513 alkali Substances 0.000 claims description 53
- 230000008569 process Effects 0.000 claims description 30
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 23
- 239000000243 solution Substances 0.000 claims description 23
- 230000001105 regulatory effect Effects 0.000 claims description 22
- 238000010612 desalination reaction Methods 0.000 claims description 14
- 238000004519 manufacturing process Methods 0.000 claims description 13
- 238000005516 engineering process Methods 0.000 claims description 5
- 238000005262 decarbonization Methods 0.000 claims description 4
- 238000010790 dilution Methods 0.000 claims description 4
- 239000012895 dilution Substances 0.000 claims description 4
- 238000005261 decarburization Methods 0.000 claims description 3
- 238000003860 storage Methods 0.000 claims description 3
- 230000020477 pH reduction Effects 0.000 claims 2
- 230000008929 regeneration Effects 0.000 abstract description 26
- 238000011069 regeneration method Methods 0.000 abstract description 24
- 239000007788 liquid Substances 0.000 abstract description 22
- 238000005554 pickling Methods 0.000 abstract description 13
- 239000002699 waste material Substances 0.000 abstract description 13
- 238000010276 construction Methods 0.000 abstract description 9
- 238000002360 preparation method Methods 0.000 abstract description 5
- 238000005520 cutting process Methods 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 4
- 238000003795 desorption Methods 0.000 description 10
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 8
- 230000007246 mechanism Effects 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 150000001768 cations Chemical class 0.000 description 5
- 238000011010 flushing procedure Methods 0.000 description 5
- 239000011777 magnesium Substances 0.000 description 5
- 210000002381 plasma Anatomy 0.000 description 5
- 150000003839 salts Chemical class 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 5
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 4
- 239000011575 calcium Substances 0.000 description 4
- 230000001276 controlling effect Effects 0.000 description 4
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 3
- 150000001450 anions Chemical class 0.000 description 3
- 229910052791 calcium Inorganic materials 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 229910052749 magnesium Inorganic materials 0.000 description 3
- 235000011121 sodium hydroxide Nutrition 0.000 description 3
- 238000005349 anion exchange Methods 0.000 description 2
- 238000011001 backwashing Methods 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- FZUJWWOKDIGOKH-UHFFFAOYSA-N sulfuric acid hydrochloride Chemical compound Cl.OS(O)(=O)=O FZUJWWOKDIGOKH-UHFFFAOYSA-N 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 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 description 1
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 229910001424 calcium ion Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000005341 cation exchange Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 150000002500 ions Chemical group 0.000 description 1
- 229910001425 magnesium ion Inorganic materials 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Landscapes
- Treatment Of Water By Ion Exchange (AREA)
Abstract
The utility model discloses a large-water-quantity multi-tank desalting device, which belongs to the technical field of waste liquid treatment and is used for treating waste water and waste liquid in industry; the method has the advantages that a plurality of groups of serial connection are changed, each group is a three-tank serial connection regeneration pickling scheme, the activity of dilute acid is fully utilized, the time for cutting out a system from each tank is reduced to 8-12 minutes, the property of the dilute acid is fully utilized, the total pickling time is still ensured to be 24-36 minutes, but the addition amount of the dilute acid is reduced by 50%, the regeneration efficiency is effectively improved, and the wastewater yield is reduced by 50%; each group of two tanks are connected in series to form a water washing scheme, pure water is fully utilized, the adding amount of the pure water is reduced by 30%, the pure water after washing is directly conveyed to an acid washing regeneration system, enters dynamic dilute acid configuration, is directly used for acid preparation on line, does not need to be conveyed to an intermediate water tank, and reduces the construction cost of the intermediate water tank, the cost of a conveying pump and a pipeline; the waste brine is used as acid-pushing water, partial unused acid in the waste brine is fully utilized, the regeneration efficiency is effectively improved, and the waste water quantity is reduced.
Description
Technical Field
The utility model belongs to the technical field of waste liquid treatment, is used for treating waste water and waste liquid in industry, and particularly relates to a large-water-quantity multi-tank desalting device.
Background
The basic principle of resin tank desalination generally refers to that a water softener adopts strong acid cation resin to replace calcium and magnesium ions in raw water, and water flowing out from the device is softened water with extremely low hardness. Because of the exceeding of anions and cations in many industrial waste water, it is required to reduce the total soluble salt content to the salt standard of process water. Firstly, a cation resin exchange process is adopted to remove metal ions such as Na+, K+, ca2+, mg2+; then carrying out a blowing-supporting decarbonization process, blowing out CO2 in water, separating the CO2 from water, and achieving the purpose of removing CO 32-and HCO 3-; and then anion exchange technology is adopted to remove anions SO42-, cl-, NO3-, NO 2-and the like in the water. The chemical reaction of cation exchange is: 2rh+ca2+ (mg2+) =r2ca (Mg) +2h+, and the produced water contains a large amount of h+, so that the produced water is acidic. When the resin is adsorbed to a certain amount of calcium and magnesium plasmas, the resin must be regenerated, the diluted hydrochloric acid (sulfuric acid) is adopted to soak and rinse the resin to replace the calcium and magnesium plasmas in the resin, the exchange capacity of the resin is recovered, and the waste liquid is discharged; the chemical reaction of regeneration is: r2Ca (Mg) +2h+ =2rh+ca2+ (mg2+) the whole regeneration process comprises: backwashing, loosening a resin layer, absorbing acid, slowly washing, performing exchange reaction, flushing (forward washing), flushing out calcium, magnesium and other ions exchanged by the chemical reaction, and injecting water to prepare for the next regeneration; the chemical reaction of anion exchange is: 2ROH+SO42- (CI-, HCO3-, NO 3-), =R2SO4 (CI-, HCO3-, NO 3-) +2OH-, when the resin is adsorbed to a certain amount of SO42- (CI-, HCO3-, NO 3-) plasma, the resin must be regenerated, SO42- (CI-, HCO3-, NO 3-) plasma in the resin is replaced again by soaking and flushing the resin with caustic soda, the exchange capacity of the resin is recovered, and the waste liquid is discharged; the chemical reaction of regeneration is: r2 SO4 (CI-, HCO3-, NO 3-) +2oh- =2roh+so42- (CI-, HCO3-, NO 3-) the whole regeneration process comprises: backwashing, loosening a resin layer, absorbing alkali, slowly washing, carrying out exchange reaction, flushing (forward washing), flushing SO42- (CI-, HCO3-, NO 3-) plasmas exchanged by chemical reaction, and injecting water to prepare for the next regeneration. The ion exchange resin is selected, the working exchange capacity is large, the energy consumption is low, the service life is long, the control part completely adopts the inlet controller, the continuous and safe operation of equipment is ensured, the full-automatic control system is used, the water outlet is stable, the use and the operation are convenient and quick, the structure is reasonable, and the installation and the operation are convenient.
In the existing exchange resin desalting device, for a resin exchange system with large water volume (more than 1000m 3/h), pure water is directly used for ejecting water remained in a resin tank, when dilute acid (dilute alkali liquor) is used for regeneration, partial dilute acid (dilute alkali liquor) is diluted by the top water in the resin tank, the dosage of the dilute acid (dilute alkali liquor) required to be added is increased, the waste water yield of the system is increased, and the subsequent waste water treatment cost is increased; for a resin exchange system with large water volume (more than 1000m 3/h), the traditional method is to directly add dilute acid (hydrochloric acid or sulfuric acid) (alkali liquor) into a single resin tank, and to stay for 20-30 minutes in acid washing (alkali washing), then directly discharge the acid washing (alkali washing) into a wastewater tank, so that the wastewater yield of the system is high, and the problem of high treatment cost of subsequent wastewater exists; for a resin exchange system with large water volume (more than 1000m 3/h), the traditional method is to directly add purified water into a single resin tank to clean regenerated resin, the cleaned water is conveyed to an intermediate water tank to be used as water for acid (alkali) preparation, a large amount of system water production is occupied in the process, and the water consumption is large, so that the treatment cost is increased. Therefore, a large water volume multi-tank desalination system is needed to solve the problems in the prior art.
Disclosure of Invention
The utility model aims to provide a large-water-quantity multi-tank desalting device so as to solve the problem of high cost in the prior art.
In order to solve the technical problems, the utility model adopts the following technical scheme: the utility model provides a big many jar of body desalination systems of water yield, includes a plurality of resin jars, every resin jar respectively through pipeline and first equalizing basin, second equalizing basin, decarbonization ware, hydrochloric acid (sulfuric acid) jar, process pool, alkali fluid reservoir, concentrated brine pond and outer water drainage pond are connected, a plurality of resin jars divide into the multiunit, and every group is respectively through process water pipeline and dilute acid (dilute lye) pipe connection and output process water and waste water, the pipeline includes house steward and many spinal branchs pipe, the one end and the house steward of many spinal branchs pipe are connected, the other end and respectively with the resin jar is connected, be provided with control valve (pneumatic or electronic) on the branch pipe respectively.
The pipeline includes top water pipeline, washing acid (washing alkali) pipeline, water production pipeline, raw water pipeline, add sour (adding alkali) pipeline, go to equalizing basin pipeline and go to the waste water pond pipeline, top water pipeline, washing acid (washing alkali) pipeline, water production pipeline, raw water pipeline, dilute acid (dilute alkali) pipeline, technology pond pipeline, go to equalizing basin pipeline, add sour (adding alkali) pipeline and go to the waste water pond pipeline all through the branch pipe with the resin jar is connected, the control valve is installed on the branch pipe.
The top water pipeline, the water washing acid (water washing alkali) pipeline, the water production pipeline and the process water pipeline are arranged at the upper part of the resin tank, and the raw water pipeline, the pipeline to the regulating tank, the dilute acid (dilute alkali liquid) pipeline, the acid (alkali) adding pipeline and the pipeline to the wastewater tank are arranged at the lower part of the resin tank.
The concentrated brine pond is connected with a water jacking pipeline through a pipeline, a pressure transmitter, a manual butterfly valve, a pump, a check valve, an electromagnetic flowmeter, a pressure gauge and a PH detector are arranged on the pipeline, and the pipeline to the wastewater pond is communicated with the concentrated brine pond.
The process water tank is connected with a process water pipeline through a pipeline, and a pressure transmitter, a manual butterfly valve, a pump, a check valve, an electromagnetic flowmeter and a PH detector are arranged on the pipeline.
The hydrochloric acid tank is connected with an acid (alkali) adding pipeline through a pipeline, and a pressure transmitter, a manual butterfly valve, a pump, a check valve, an electromagnetic flowmeter, a pressure gauge and a PH detector are arranged on the pipeline.
The water production pipeline is connected with the decarburization device, is connected with the second regulating tank through a pipeline and is connected with the resin tank through a pipeline, and a pressure transmitter, a manual butterfly valve, a pump, a check valve, an electromagnetic flowmeter, a pressure gauge and a PH detector are arranged on the pipeline.
The outer drainage pool (water producing pool) is connected with the resin tank and the process pool through pipelines, wherein the pipelines connected with the process pool are provided with check valves.
The alkali solution tank, the first regulating tank and the second regulating tank are all connected with the resin tank through pipelines, and the pipelines are respectively provided with a pressure transmitter, a manual butterfly valve, a pump, a check valve, an electromagnetic flowmeter, a pressure gauge and a PH detector.
The desalination system is also provided with an air source, the air source comprises an air compressor, an air storage tank, a Q-level filter, a freeze dryer, a P-level filter and an S-level filter, and is connected through a pipeline, the other end of the pipeline is connected with a pneumatic (electric) control valve through a branch pipe, and a pressure gauge, electromagnetic flow and a manual ball valve are arranged on the pipeline.
Compared with the prior art, the utility model has the following advantages:
according to the utility model, a plurality of groups of series connection are changed, each group is a three-tank series connection regeneration pickling scheme, the activity of dilute acid (dilute alkali solution) is fully utilized, the time for cutting out a system from each tank is reduced to 8-12 minutes, the property of the dilute acid (dilute alkali solution) is fully utilized, the total pickling time is still ensured to be 24-36 minutes, but the addition amount of the dilute acid (dilute alkali solution) is reduced by half, the regeneration efficiency is effectively improved, and the generation amount of wastewater is reduced by half; the method has the advantages that a plurality of groups of tanks are changed into a water washing scheme, pure water is fully utilized, the adding amount of the pure water is reduced by one third, the cleaned pure water is directly conveyed to a pickling regeneration dynamic dilution configuration pipeline, the pure water is directly used for acid preparation on line, the pure water is not required to be conveyed to an intermediate water tank, and the construction and conveying pump and pipeline cost of the intermediate water tank is reduced; the waste water yield is only one third of that of the traditional resin exchange system, the consumption of dilute acid (dilute alkali solution) is only two thirds of that of the traditional resin exchange system, the construction cost is reduced by 15-20%, and the running cost is reduced by 20-25%.
Drawings
Fig. 1 is a schematic diagram of the apparatus of the present utility model.
In the figure, a second regulating tank, a decarburization device 2, a hydrochloric acid tank 3, a process water tank 4, a concentrated salt water tank 5, a pipeline 6, a first regulating tank 7, a resin tank 8, an air source 9, an alkali solution tank 10, an external drainage tank 11 and a control valve 12 are arranged.
Detailed Description
The technical solutions in the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model.
As shown in fig. 1, the large-water-quantity multi-tank desalting equipment comprises a plurality of resin tanks 8, wherein each resin tank 8 is respectively connected with a first regulating tank 7, a second regulating tank 1, a decarbonizer 2, a hydrochloric acid tank 3, a process water tank 4, an alkali liquor tank 10, a concentrated salt water tank 5 and an external drainage tank 11 through pipelines 6, the plurality of resin tanks 8 are divided into a plurality of groups, each group is respectively connected with a process water pipeline and a dilute acid (dilute alkali liquor) pipeline and outputs process water and dilute acid (dilute alkali liquor), the pipes 6 comprise a main pipe and a plurality of branch pipes, one ends of the plurality of branch pipes are connected with the main pipe, the other ends of the plurality of branch pipes are respectively connected with the resin tanks 8, and control valves 12 are respectively arranged on the branch pipes and controlled by a control mechanism; the method is characterized in that a plurality of groups of series connection are changed, each group is a three-tank series connection regeneration pickling scheme, the activity of dilute acid (dilute alkali solution) is fully utilized, the time for cutting out a system from each tank is reduced to 8-12 minutes, the property of the dilute acid (dilute alkali solution) is fully utilized, the total pickling time is still ensured to be 24-36 minutes, the addition amount of the dilute acid (dilute alkali solution) is reduced by about half, the regeneration efficiency is effectively improved, and the general wastewater amount is reduced; the method is characterized in that a plurality of groups of tanks are connected in series, each group of tanks are connected in series to form a water washing scheme, pure water is fully added, the adding amount of the pure water is reduced by about one third, the cleaned pure water is directly conveyed to a pickling regeneration dynamic dilution configuration pipeline, the pure water is directly used for acid preparation on line, the pure water is not required to be conveyed to an intermediate water tank, and the construction and conveying pump and pipeline costs of the intermediate water tank are reduced; the waste brine is used as top water, so that partial acid which is not utilized in the waste brine is fully utilized, the regeneration efficiency is effectively improved, and the waste water quantity is reduced; the waste water yield is only about one third of that of the traditional resin exchange system, the consumption of dilute acid (dilute alkali solution) is only two thirds of that of the traditional resin exchange system, and the construction cost and the running cost are low.
As shown in fig. 1: in the embodiment, the control mechanism adopts any one of a DCS and a PLC controller, the DCS and the PLC control system realize control through a computer, resin is filled in the resin tank 7, the control valve 11 adopts any one of a pneumatic (electric) ball valve or a pneumatic (electric) butterfly valve, and the control mechanism adopts automatic control through the DCS and the PLC control system, the pipeline is a stainless steel pipe, the resin tank 7 is a plurality of, three of the three are connected in series in a regenerative pickling scheme, and two of the two are connected in series in a water washing scheme; the embodiment is based on the improvement of the wastewater treatment mode in the prior art, and is characterized in that every three resin tanks 8 are connected in series to be a regenerated pickling scheme, every two resin tanks are connected in series to be a water washing scheme, and are connected with a first regulating tank 7, a second regulating tank 1, a decarbonizer 2, a hydrochloric acid tank 3, a process water tank 4, an alkali liquor tank 10, a concentrated salt water tank 5 and an external drainage tank 11 through pipelines in a combined way, so that the wastewater yield is only about one third of that of a traditional resin exchange system, the consumption of dilute acid (dilute alkali liquor) is only two thirds of that of the traditional resin exchange system, and the construction cost and the operation cost are low. In actual installation, the upper part of each resin tank 8 is respectively provided with a water jacking pipeline, an acid (alkali) washing pipeline, a water production pipeline and a process water pipeline, and three adjacently arranged resin tanks 8 and two adjacently arranged resin tanks 8 are respectively connected with each other through the process water pipeline and the dilute acid (alkaline liquor) pipeline and output the process water and the dilute acid (alkaline liquor) for convenient subsequent use; wherein, the top water pipeline, the water washing acid (water washing alkali) pipeline, the water production pipeline, the process water pipeline and the dilute acid (dilute alkali) pipeline are respectively connected with the resin tank through branch pipes, each branch pipe is respectively provided with a control valve 12 and is used for controlling the flow direction of the liquid in each pipeline through a control mechanism; the lower part of each resin tank 8 is respectively provided with a raw water pipeline, a pipeline which is connected with the regulating tank, a dilute acid (dilute alkali solution) pipeline, an acid (alkali solution) adding pipeline and a wastewater tank pipeline, wherein the raw water pipeline, the pipeline which is connected with the regulating tank, the dilute acid (alkali solution) pipeline, the acid (alkali solution) adding pipeline and the wastewater tank pipeline are respectively connected with the resin tanks through branch pipes, and each branch pipe is respectively provided with a control valve 12 and is used for controlling the flow direction of liquid in each pipeline through a control mechanism; the periphery of the resin tank 8 is respectively provided with a first regulating tank 7, a second regulating tank 1, a decarbonizer 2, a hydrochloric acid tank 3, a process water tank 4, an alkali liquor tank 10, a concentrated brine tank 5, an external drainage tank 11 and an air source 9, which are used for assisting the arrangement to finish the waste water yield which is only about one third of that of the traditional resin exchange system, and the consumption of dilute acid (dilute alkali liquor) is only two thirds of that of the traditional resin exchange system, so that the construction cost and the running cost are low; the concentrated brine pond 5 is connected with an acid jacking pipeline through a pipeline, and a pressure transmitter, a manual butterfly valve, a pump, a check valve, an electromagnetic flowmeter, a pressure gauge and a PH detector are arranged on the pipeline and communicated with the concentrated brine pond 5 through a pipeline which is connected with the wastewater pond; the process water tank is connected with a process water pipeline through a pipeline 4, and a pressure transmitter, a manual butterfly valve, a pump, a check valve, an electromagnetic flowmeter and a PH detector are arranged on the pipeline; the hydrochloric acid tank 3 is connected with an acid (alkali) adding pipeline through a pipeline, and a pressure transmitter, a manual butterfly valve, a pump, a check valve, an electromagnetic flowmeter, a pressure gauge and a PH detector are arranged on the pipeline; the water production pipeline is connected with the decarbonization device 2, is connected with the second regulating tank 1 through a pipeline, is connected with the resin tank 8 through a pipeline, and is provided with a pressure transmitter, a manual butterfly valve, a pump, a check valve, an electromagnetic flowmeter, a pressure gauge and a PH detector; the alkali solution tank 10, the first regulating tank 7 and the second regulating tank 1 are all connected with the resin tank 8 through pipelines, and the pipelines are respectively provided with a pressure transmitter, a manual butterfly valve, a pump, a check valve, an electromagnetic flowmeter, a pressure gauge and a PH detector which are connected with a control mechanism and are used for detecting and controlling the flow direction of liquid on the pipelines; the air source 9 comprises a P-level filter, an air compressor, an air storage tank, a Q-level filter, a freeze dryer and an S-level filter which are connected through pipelines, the other end of each pipeline is connected with the control valve 12 through a branch pipe, a pressure gauge, an electromagnetic flow and a manual ball valve are arranged on each pipeline, and the pressure gauge is connected with an electromagnetic flow control mechanism and is used for conveying air to the control valve 12, controlling and detecting; the method is characterized in that a plurality of groups of series connection are changed, each group is a three-tank series connection regeneration pickling scheme, the activity of dilute acid (dilute alkali solution) is fully utilized, the time for cutting out a system from each tank is reduced to 8-12 minutes, the property of the dilute acid (dilute alkali solution) is fully utilized, the total pickling time is still ensured to be 24-36 minutes, the addition amount of the dilute acid (dilute alkali solution) is reduced by about half, the regeneration efficiency is effectively improved, and the general wastewater amount is reduced; the method is characterized in that a plurality of groups of tanks are connected in series, each group of tanks are connected in series to form a water washing scheme, pure water is fully added, the adding amount of the pure water is reduced by about one third, the cleaned pure water is directly conveyed to a pickling regeneration dynamic dilution configuration pipeline, the pure water is directly used for acid preparation on line, the pure water is not required to be conveyed to an intermediate water tank, and the construction and conveying pump and pipeline costs of the intermediate water tank are reduced; the waste brine is used as top water, so that partial acid which is not utilized in the waste brine is fully utilized, the regeneration efficiency is effectively improved, and the waste water quantity is reduced; the waste water yield is only about one third of that of the traditional resin exchange system, the consumption of dilute acid (dilute alkali solution) is only two thirds of that of the traditional resin exchange system, and the construction cost and the running cost are low.
The specific implementation is as follows: in the cation removal step, when raw water (waste liquid) is pumped from the regulating tank 1 through a raw water pump, the raw water enters the resin tank 8 through a pipeline at the lower end of the resin tank 8, and after the raw water is adsorbed by the resin, the treated water enters the water production pipeline and enters the decarburizer 2. When the resin is near saturation, top water is first performed. After the top water is over, the top water enters a countercurrent regeneration program, fresh hydrochloric acid (sulfuric acid) is conveyed from a hydrochloric acid tank (sulfuric acid tank) to the lower end of a resin tank 8-1 through a pipeline by a dilute acid (dilute alkali solution) pump after being diluted on line, resin is regenerated in countercurrent, desorption liquid of the resin tank 8-1 enters an inlet pipeline at the lower end of a resin tank 8-2 from an outlet at the upper end of the resin tank 8-1, the desorption liquid enters the resin tank 8-2 in countercurrent, resin is regenerated in countercurrent, the desorption liquid of the resin tank 8-2 enters an inlet pipeline at the lower end of the resin tank 8-3 from an outlet at the upper end of the resin tank 8-2, the desorption liquid enters the resin tank 8-3 in countercurrent, and the desorption liquid of the resin tank 8-3 is discharged into a wastewater pool from the pipeline at the upper end of the resin tank 8-3. After the regeneration, the mixture was washed with water. In addition to the anion process, the cation bed produced water is discharged to remove carbon dioxide, and then enters the resin tank 13 from the regulating tank 2 through a pipeline at the lower end of the resin tank 13 by a water pump, and after being adsorbed by the resin, the treated water enters a produced water pipeline to be sent into an external drainage tank. When the resin is near saturation, top water is first performed. After the top water is over, the top water enters a countercurrent regeneration program, fresh caustic soda liquid is conveyed from an alkali liquor tank to the lower end of a resin tank 13-1 through a pipeline by an alkali liquor pump after being diluted on line, the resin is regenerated in countercurrent, desorption liquid of the resin tank 13-1 enters an inlet pipeline at the lower end of the resin tank 13-2 from an outlet at the upper end of the resin tank 13-1, the desorption liquid enters the resin tank 13-2 in countercurrent, the resin is regenerated in countercurrent, the desorption liquid of the resin tank 13-2 enters an inlet pipeline at the lower end of the resin tank 13-3 from an outlet at the upper end of the resin tank 13-2, the desorption liquid enters the resin tank 13-3 in countercurrent, the resin is regenerated in countercurrent, and the desorption liquid of the resin tank 13-3 is discharged into a wastewater pool from a pipeline at the upper end of the resin tank 13-3. After the regeneration, the mixture was washed with water. After the water washing is completed, the normal desalting operation state is shifted.
The foregoing description is only a preferred embodiment of the present utility model, and is not intended to limit the present utility model, and any simple modification, variation and equivalent structural changes made to the above embodiment according to the technical substance of the present utility model still fall within the scope of the technical solution of the present utility model.
Claims (10)
1. The utility model provides a many jar of body desalination equipment of large water yield, includes a plurality of resin jars, every resin jar respectively through pipeline and first equalizing basin, second equalizing basin, decarbonization ware, hydrochloric acid tank, technology pond, alkali liquor jar, concentrated brine pond and outer drainage tank are connected, its characterized in that, a plurality of resin jars divide into the multiunit, and every group is connected and output demineralized water and waste water through technology water pipeline and dilute acid pipeline respectively, the pipeline includes house steward and many spinal branchpipes, and the one end and the house steward of many spinal branchpipes are connected, the other end respectively with the resin jar is connected, be provided with the control valve on the branch pipe respectively.
2. A large water volume multi-tank desalination apparatus as defined in claim 1 wherein: the pipeline includes top water pipeline, washing sour pipeline, produces water pipeline, raw water pipeline, acidification pipeline, goes to the equalizing basin pipeline and goes to the waste water pond pipeline, top water pipeline, washing sour pipeline, produce water pipeline, raw water pipeline, dilute acid pipeline, technology pond pipeline, go to the equalizing basin pipeline, acidification pipeline and go to the waste water pond pipeline all through the branch pipe with the resin jar is connected, the control valve is installed on the branch pipe.
3. A large water volume multi-tank desalination apparatus as defined in claim 2 wherein: the top water pipeline, the water washing acid pipeline, the water production pipeline and the process water pipeline are arranged on the upper portion of the resin tank, and the raw water pipeline, the dilute acid pipeline, the acid adding pipeline and the wastewater tank pipeline are arranged on the lower portion of the resin tank.
4. A large water volume multi-tank desalination apparatus as claimed in claim 1 or 2, wherein: the concentrated brine pond is connected with a water jacking pipeline through a pipeline, a pressure transmitter, a manual butterfly valve, a pump, a check valve, an electromagnetic flowmeter, a pressure gauge and a PH detector are arranged on the pipeline, and the pipeline is communicated with the concentrated brine pond.
5. A large water volume multi-tank desalination apparatus as claimed in claim 1 or 2, wherein: the process water tank is connected with a process water pipeline through a pipeline, and a pressure transmitter, a manual butterfly valve, a pump, a check valve, an electromagnetic flowmeter and a PH detector are arranged on the pipeline.
6. A large water volume multi-tank desalination apparatus as claimed in claim 1 or 2, wherein: the hydrochloric acid tank is connected with an acid adding pipeline through a pipeline, and a pressure transmitter, a manual butterfly valve, a pump, a check valve, an electromagnetic flowmeter, a pressure gauge, a PH detector and hydrochloric acid dilution are arranged on the pipeline.
7. A large water volume multi-tank desalination apparatus as defined in claim 2 wherein: the water production pipeline is connected with the decarburization device, is connected with the second regulating tank through a pipeline, is connected with the resin tank through a water pump and a pipeline, and is provided with a pressure transmitter, a manual butterfly valve, a pump, a check valve, an electromagnetic flowmeter, a pressure gauge and a PH detector.
8. A large water volume multi-tank desalination apparatus as claimed in claim 1 or 2, wherein: the outer drainage tank is connected with the resin tank and the water production pipeline through pipelines, wherein the water production pipeline is provided with a check valve.
9. A large water volume multi-tank desalination apparatus as claimed in claim 1 or 2, wherein: the alkali solution tank, the first regulating tank and the second regulating tank are all connected with the resin tank through pipelines, and the pipelines are respectively provided with a pressure transmitter, a manual butterfly valve, a pump, a check valve, an electromagnetic flowmeter, a pressure gauge and a PH detector.
10. A large water volume multi-tank desalination apparatus as defined in claim 1 wherein: the air source comprises an air compressor, an air storage tank, a Q-level filter, a freeze dryer, a P-level filter and an S-level filter, and is connected through pipelines, the other end of each pipeline is connected with the control valve through a branch pipe, and a pressure gauge, electromagnetic flow and a manual ball valve are arranged on the pipeline.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320570057.XU CN219730619U (en) | 2023-03-22 | 2023-03-22 | High-water-quantity multi-tank desalting equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320570057.XU CN219730619U (en) | 2023-03-22 | 2023-03-22 | High-water-quantity multi-tank desalting equipment |
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| Publication Number | Publication Date |
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| CN219730619U true CN219730619U (en) | 2023-09-22 |
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| CN202320570057.XU Active CN219730619U (en) | 2023-03-22 | 2023-03-22 | High-water-quantity multi-tank desalting equipment |
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| Country | Link |
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| CN (1) | CN219730619U (en) |
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- 2023-03-22 CN CN202320570057.XU patent/CN219730619U/en active Active
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