CN215560715U - Control device for zero-pole distance electronic membrane electrolytic cell temperature - Google Patents
Control device for zero-pole distance electronic membrane electrolytic cell temperature Download PDFInfo
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- CN215560715U CN215560715U CN202122324891.4U CN202122324891U CN215560715U CN 215560715 U CN215560715 U CN 215560715U CN 202122324891 U CN202122324891 U CN 202122324891U CN 215560715 U CN215560715 U CN 215560715U
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- 239000012528 membrane Substances 0.000 title claims abstract description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 79
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 60
- 239000001257 hydrogen Substances 0.000 claims abstract description 60
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 60
- 230000001105 regulatory effect Effects 0.000 claims abstract description 15
- 230000001276 controlling effect Effects 0.000 claims description 15
- 238000005868 electrolysis reaction Methods 0.000 claims description 8
- 239000003513 alkali Substances 0.000 abstract description 58
- 239000003014 ion exchange membrane Substances 0.000 abstract description 3
- 238000000034 method Methods 0.000 description 20
- 239000007788 liquid Substances 0.000 description 5
- 238000001816 cooling Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 230000001932 seasonal effect Effects 0.000 description 1
- 230000001131 transforming effect Effects 0.000 description 1
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Abstract
The utility model discloses a control device for the temperature of a zero-pole distance electronic membrane electrolytic cell, which comprises a spiral wound heat exchanger, a tubular heat exchanger and a control system, wherein the spiral wound heat exchanger is connected with the tubular heat exchanger through a pipeline; the front end of the spiral wound heat exchanger is connected with a pure water control system, and the rear end of the spiral wound heat exchanger is connected with the tube type heat exchanger; the spiral wound heat exchanger is provided with a first temperature transmitter and is connected with a steam system through a regulating valve; and the shell and tube heat exchanger is provided with a second temperature transmitter and is arranged on the hydrogen main pipe. The utility model can stably control the temperature of the alkali liquor discharged from the zero-polar distance ion-exchange membrane electrolytic cell, reduce the steam consumption and effectively solve the problems of large steam consumption, unstable temperature control of the electrolytic cell and the like in the prior art.
Description
Technical Field
The utility model belongs to the technical field of ion membrane electrolytic cells, and particularly relates to a control device for the temperature of a zero-polar-distance ion membrane electrolytic cell.
Background
The chlor-alkali industry adopts the production process of polar distance ion membrane electrolytic cell and zero polar distance electron membrane electrolytic cell, and the zero polar distance ion membrane electrolytic cell has the advantages of high yield and low power consumption compared with the polar distance ion membrane electrolytic cell, thereby being more and more widely applied.
Among the numerous process control parameters of ionic membrane electrolyzers, the electrolyzer temperature has always been one of the key control points. In the chlor-alkali industry, the temperature of the cathode alkali liquor of the electrolytic cell is regarded as the temperature of the electrolytic cell, and the temperature of the electrolytic cell is indirectly controlled by controlling the temperature of the inlet alkali liquor high-level cell.
Hydrogen and alkali liquor (finished product alkali concentration) from the cathode side of the ion membrane electrolytic cell are preliminarily separated by a gas-liquid separator, the alkali liquor (the temperature T234 of the alkali discharged from the electrolytic cell is dependent on the temperature of the electrolytic cell) enters an alkali liquor circulating tank, most of the liquid alkali (about 94.5%) enters a plate heat exchanger by a circulating pump, and enters an alkali liquor head tank after the temperature (T237) is controlled by steam or circulating water; a small part of alkali liquor (controlling the liquid level of the circulating tank) enters a finished product alkali tank. Adding pure water to the alkali liquor in the alkali liquor head tank to dilute the concentration (the pure water amount is the multiplication factor of the running current of the electrolytic cell), returning to the ionic membrane electrolytic cell, and feeding to a gas-liquid separator after the concentration is improved by electrolysis. Hydrogen (a gas-liquid separator, an alkali liquor circulating tank and an alkali liquor elevated tank) is collected to a hydrogen main pipe and enters a hydrogen treatment process.
In the starting process, heating the circulating alkali liquor passing through the plate heat exchanger by using steam to reach the starting temperature of the electrolytic cell; in the parking process, circulating alkali liquor passing through the plate heat exchanger is cooled by circulating water to achieve the purpose of cooling the electrolytic cell.
In the normal operation process, the polar distance ion membrane electrolytic cell has high electrolytic cell temperature due to high voltage of the electrolytic cell, high heat productivity and large electrolytic cell temperature, and circulating water is required to cool the circulating alkali liquor all the time to stabilize the temperature of the electrolytic cell; and the zero-pole distance electronic membrane electrolytic cell has low electrolytic cell temperature due to low electrolytic cell voltage (low power consumption) and small calorific value, and the temperature of the electrolytic cell can be stabilized only by heating circulating alkali liquor with steam.
In the process of transforming the ionic membrane electrolytic cell with the polar distance into the ionic membrane electrolytic cell with the zero-polar distance (or building a new zero-polar distance ionic membrane electrolytic cell), the control mode of the temperature of the electrolytic cell still uses the original control process of the temperature of the ionic membrane electrolytic cell with the polar distance. The process has the following defects in the normal operation process of the zero-pole distance ion membrane electrolytic cell (except for driving and stopping, the temperature of the membrane pole distance ion membrane electrolytic cell is controlled between 83 ℃ and 85 ℃):
1. the temperature difference of the plate heat exchanger is small, the temperature of the discharged condensed water is high, and a large amount of steam is wasted.
The circulating alkali liquor (T234, about 83 ℃) discharged from the zero-polar distance electronic membrane electrolytic cell is heated by steam through a plate heat exchanger (T237, about 85 ℃) and then is mixed with pure water added at normal temperature (about 25 ℃), and then the temperature is reduced (about 80 ℃) and the mixture enters the electrolytic cell.
The temperature of the circulating alkali liquor is about 83 ℃ before entering the plate heat exchanger, the temperature is raised to 85 ℃ after being heated by steam, the temperature difference is only 2 ℃, the circulating amount is large, the temperature of the discharged steam condensate is higher than 85 ℃, the condensate carries a large amount of steam, and the steam consumption is large.
2. The circulating alkali liquor with large flow rate is heated firstly by the plate heat exchanger, and has no practical significance.
The process is designed for the ionic membrane electrolytic cell with the polar distance, the temperature of the alkaline liquor discharged from the electrolytic cell with the polar distance is high (T234, the temperature is about 89 ℃), the temperature is cooled to a certain degree by a heat exchanger, and then the temperature is further reduced to 80 ℃ of the temperature of the electrolytic cell entering the electrolytic cell by adding 25 ℃ pure water. Because the addition amount of pure water is only 5.5% of the circulating alkali liquor flow of the tank temporarily, the cooling alkali temperature is relatively limited.
In the zero-polar distance ion membrane electrolytic cell process, the process has no practical significance because the temperature (T234, the temperature is about 83 ℃) of the alkali liquor discharged from the cell is higher than the temperature (about 80 ℃) of the alkali liquor entering the cell; the reheating is performed to compensate for the temperature drop caused by the addition of pure water at normal temperature (25 ℃). Then can the post-mixing temperature be achieved by raising the temperature of pure water by only 5.5% of the circulating amount (83 ℃ down to 80 ℃), without raising the temperature of circulating alkali by 94.5%?
3. Because the temperature difference of the plate heat exchanger is small, the circulation volume is large, the temperature of the alkali liquor discharged from the heat exchanger is difficult to control stably, so that the temperature fluctuation of the electrolytic cell is large, the cell voltage of the electrolytic cell is correspondingly fluctuated, and the stable production is not facilitated.
SUMMERY OF THE UTILITY MODEL
Aiming at the defects, the utility model provides a device for controlling the temperature of a zero-pole distance electronic membrane electrolytic cell, which can stably control the temperature of the alkaline liquor discharged from the zero-pole distance electronic membrane electrolytic cell, reduce the steam consumption and effectively solve the problems of large steam consumption, unstable temperature control of the electrolytic cell and the like in the prior art.
In order to achieve the purpose, the technical scheme adopted by the utility model for solving the technical problems is as follows: the purpose of controlling the temperature of the electrolytic bath is achieved by controlling the temperature of pure water added to the electrolytic circulating alkali system; the preheating of the pure water mainly adopts the waste heat of the recovered hydrogen main pipe.
The utility model provides a device for controlling the temperature of a zero-pole distance electronic membrane electrolytic cell, which comprises a spiral wound heat exchanger, a tubular heat exchanger and a control system. The front end of the spiral wound heat exchanger is connected with the pure water control system, and the rear end of the spiral wound heat exchanger is connected with the tube type heat exchanger; the spiral wound heat exchanger is provided with a first temperature transmitter and is connected with a steam system through a regulating valve. And the shell and tube heat exchanger is provided with a second temperature transmitter and is arranged on the hydrogen main pipe.
Furthermore, in the tube-type heat exchanger, the sum of the inner sectional areas of tube-side tubes is larger than the inner sectional area of the hydrogen main pipe, the hydrogen inlet end is an elliptical seal head, and the outlet end is an eccentric seal head. The hydrogen tube type heat exchanger is installed with 1-2% gradient.
Further, the spiral wound heat exchanger and the shell and tube heat exchanger are both made of 316L stainless steel.
And further, the control system for the temperature of the zero-pole distance electronic membrane electrolytic cell also comprises a control system, a first temperature transmitter comprising a spiral wound heat exchanger, a steam regulating valve and a second temperature transmitter comprising a tubular heat exchanger. The first temperature transmitter is used for controlling the opening of a steam regulating valve of the spiral wound heat exchanger, and the second temperature transmitter is used for detecting the pure water temperature of the tube type heat exchanger.
Further, the method is characterized in that the pure water is preheated by steam through the spiral wound heat exchanger and then is preheated by hydrogen of the electrolysis main pipe through the hydrogen tube type heat exchanger. The temperature of pure water of the spiral wound heat exchanger is controlled to control the temperature of the zero-pole distance electronic membrane electrolytic cell.
When the device is used, the added normal-temperature pure water firstly passes through the spiral wound heat exchanger, the temperature is raised by steam, and then the heat of the hydrogen in the tank is recovered through the tube type heat exchanger arranged on the electrolysis hydrogen header pipe, and the temperature is further raised and then enters the electrolysis circulating alkali system to be used as make-up water. The electrolytic bath is discharged from the bath, the circulating alkali enters the circulating alkali bath, the circulating pump is used for pumping the circulating alkali into the elevated tank (the plate heat exchanger bypasses), and after the alkali liquor in the alkali liquor elevated tank is mixed with the preheated pure water, the temperature is reduced to the temperature of the alkali liquor entering the bath and the alkali liquor enters the electrolytic bath.
A shell and tube heat exchanger: the pure water passes through the shell side and the hydrogen passes through the tube side, and the sum of the inner sectional areas of the tube side tubes is larger than the inner sectional area of the hydrogen main tube (about 30%). The hydrogen inlet end is an elliptical end socket, so that hydrogen can be uniformly distributed conveniently; the outlet end is an eccentric seal head, and the tubular heat exchanger is provided with 1-2% of gradient, so that hydrogen condensate water can be automatically discharged to a hydrogen main pipe conveniently. Spiral wound heat exchanger: the steam passes through the tube pass, the pure water passes through the shell pass, and the regulating valve is used for controlling the steam amount entering the spiral wound heat exchanger.
In summary, the utility model has the following advantages:
1. the preheating of the pure water mainly adopts the waste heat of the recovered hydrogen main pipe, so that the steam consumption can be saved. The circulating alkali liquor of the steam heating plate type heat exchanger for the original polar distance ion-exchange membrane electrolytic cell is large in circulating amount of the alkali liquor, the temperature difference between an inlet and an outlet of the plate type heat exchanger is small, the outlet temperature is high, condensate water carries a large amount of steam, and the steam consumption is large. The pure water passes through the spiral wound heat exchanger, the temperature of the pure water is raised from 25 ℃ to about 30 ℃, and then the pure water is preheated by recovering waste heat through the hydrogen shell and tube heat exchanger, and the temperature is raised from 30 ℃ to 62 ℃. Only using a small amount of steam in the spiral wound heat exchanger or using steam in the condition of low temperature in winter; the spiral wound heat exchanger has the characteristic of saving steam on occasions with small temperature difference. Therefore, the steam consumption is greatly reduced.
2. The temperature of the zero-polar distance ion-exchange membrane electrolyzer is easy to control and is stable. In the production control of the ion membrane electrolytic cell, the running current of the electrolytic cell is not frequently increased or decreased, and the running load is stable. Therefore, the total amount of the hydrogen out of the ion membrane electrolytic cell and the amount of pure water added by the circulating alkali system (the pure water amount is the coefficient multiplied by the running current of the electrolytic cell) are stable. The flow and the temperature of the hydrogen (heat source) passing through the hydrogen tube type heat exchanger are stable. Enterprises in various places have large temperature difference (or seasonal temperature) and pure water temperature difference, but the difference can be reduced by controlling the outlet temperature of the spiral wound heat exchanger; therefore, the flow and the temperature of the pure water (cold source) passing through the hydrogen tube type heat exchanger are stable, and the temperature of the preheated pure water is stable. Moreover, the flow rate of the pure water only accounts for 5.5 percent of the amount of the circulating alkali liquor in the electrolytic bath, and the temperature of the circulating alkali liquor in the electrolytic bath is less fluctuated (less than 0.5 ℃) even if the temperature of the pure water fluctuates a small amount (such as 2-3 ℃). Therefore, the temperature of the zero-pole distance electronic membrane electrolytic cell is easy to control and is stable.
3. The load of the subsequent hydrogen treatment process of the electrolytic cell is reduced. In the prior method, the hydrogen treatment process needs to cool the electrolyzed high-temperature hydrogen to below 40 ℃, and the temperature of the hydrogen in the tubular heat exchanger is reduced to about 65 ℃ at 83 ℃, so that the load of the hydrogen treatment process is greatly reduced (the amount of circulating water is reduced).
4. The original pipeline is convenient to transform, the use is safer, the circulating alkali system of the electrolytic bath is not changed, the electrolytic pure water adding regulating valve is not changed, and only the preheating system branch is added to the source pure water pipeline. The spiral wound heat exchanger has compact structure, tubular shape and small floor area, and can be installed on a pure water pipeline. Therefore, the project is convenient to modify. The hydrogen heat exchanger adopts a tube type heat exchanger, pure water passes through a shell pass, hydrogen passes through a tube pass, and the sum of the inner sectional areas of tube pass tubes is larger than the inner sectional area (about 30%) of a hydrogen main pipe. The hydrogen inlet end is an elliptical end socket, so that hydrogen can be uniformly distributed conveniently; the outlet end is an eccentric seal head, and the tubular heat exchanger is provided with 1-2% of gradient, so that hydrogen condensate water can be automatically discharged to a hydrogen main pipe conveniently. Therefore, the hydrogen tube type heat exchanger can ensure complete nitrogen replacement in the starting and stopping process and automatic discharge of hydrogen condensate in the running process, and is safer to use.
Drawings
FIG. 1 is a schematic diagram of a control device for the cell temperature of a zero-pole distance electromembrane electrolyzer;
FIG. 2 is a schematic diagram of the operation principle of the zero-pole distance electromembrane cell temperature;
wherein, 1, inlet valve I; 2. a second inlet valve; 3. a blowoff valve; 4. a third inlet valve; 5. adjusting a valve; 6. a spiral wound heat exchanger; 7. a first temperature transmitter; 8. a shell and tube heat exchanger; 9. and a second temperature transmitter.
Detailed Description
The following detailed description of embodiments of the utility model refers to the accompanying drawings.
In an embodiment of the utility model, as shown in fig. 1, a control device for the temperature of a zero-pole distance electronic membrane electrolytic cell is provided, which comprises a spiral wound heat exchanger 6, wherein one end of the spiral wound heat exchanger 6 is connected with a pure water control system, a third inlet valve 4 is arranged between the spiral wound heat exchanger 6 and the pure water control system, the spiral wound heat exchanger 6 is further connected with a steam system through a regulating valve 5, the other end of the spiral wound heat exchanger 6 is connected with a tubular heat exchanger 8, a first temperature transmitter 7 is arranged on the spiral wound heat exchanger 6, one end of the tubular heat exchanger 8 is connected with a second inlet valve 2 and a first inlet valve 1, and the tubular heat exchanger 8 is further connected with a blowdown valve 3 and a second temperature transmitter 9 respectively.
In the tubular heat exchanger 8, the sum of the inner sectional areas of the tube passes is larger than the inner sectional area of the hydrogen main pipe (about 30 percent), the hydrogen inlet end is an elliptical seal head, and the hydrogen outlet end is an eccentric seal head. The hydrogen tube type heat exchanger is installed with 1-2% gradient. The spiral wound heat exchanger 6 and the tubular heat exchanger 8 are both made of 316L stainless steel.
The control system of the zero polar distance ion membrane electrolytic cell temperature comprises a first temperature transmitter 7 of a spiral wound heat exchanger 6, a steam regulating valve 5 and a second temperature transmitter 9 of a shell and tube heat exchanger 8. The first temperature transmitter 7 is used for controlling the opening of the steam regulating valve 5 entering the spiral wound heat exchanger 6, and the second temperature transmitter 9 is used for detecting the pure water temperature of the shell and tube heat exchanger 8.
Before the first inlet valve 1, a pure water preheating system bypass is connected, pure water enters the spiral wound heat exchanger 6 through the third inlet valve 4, goes out of the first temperature transmitter 7 on the spiral wound heat exchanger 6 and is used for controlling the opening degree of the steam regulating valve 5 entering the spiral wound heat exchanger 6, the preheated pure water enters the tubular heat exchanger 8, goes out of the second temperature transmitter 9 of the tubular heat exchanger 8 and enters the original pure water flow regulating valve 5 through the second inlet valve 2 to enter the alkali liquor of the electrolytic tank below the head tank, and unqualified pure water is discharged by the front blow-down valve 3 after each opening.
The shell and tube heat exchanger 8: the pure water passes through the shell side and the hydrogen passes through the tube side, and the sum of the inner sectional areas of the tube side tubes is larger than the inner sectional area of the hydrogen main tube (about 30%). The hydrogen inlet end is an elliptical end socket, so that hydrogen can be uniformly distributed conveniently; the outlet end is an eccentric seal head, and the tubular heat exchanger 8 is provided with 1-2% gradient, so that hydrogen condensate water can be automatically discharged to a hydrogen main pipe conveniently. Spiral wound heat exchanger 6: the steam passes through the tube pass, and the pure water passes through the shell pass.
The added normal temperature pure water firstly passes through the spiral wound heat exchanger 6, the temperature is raised by steam, and then the added normal temperature pure water passes through the tube type heat exchanger 8 arranged on the electrolysis hydrogen header pipe to recover the hydrogen heat of the tank, and the temperature is further raised and then enters the electrolysis circulating alkali system to be used as make-up water. The electrolytic bath is discharged from the bath, the circulating alkali enters the circulating alkali bath, the circulating pump is used for pumping the circulating alkali into the elevated tank (the plate heat exchanger bypasses), and after the alkali liquor in the alkali liquor elevated tank is mixed with the preheated pure water, the temperature is reduced to the temperature of the alkali liquor entering the bath and the alkali liquor enters the electrolytic bath.
Before the current of the ionic membrane rises: the circulating lye passing through the plate heat exchanger is gradually heated by steam 1 (temperature T273), thereby slowly raising the bath temperature of the electrolyzer (temperature T234) to the specified start-up temperature (T234 about 65 ℃).
In the process of increasing current of the ionic membrane: pure water does not flow in the tube type heat exchanger, and the pure water is always preheated along with the rise of the temperature of hydrogen in the current rise process. Therefore, when the pure water is discharged 5 to 10 minutes before the addition, the pure water that has not flowed through the heat exchanger for a long time is replaced (possibly corroded), and the high-temperature pure water can be discharged. The operation is as follows: and (3) closing the original pure water adding valve 1 and the pure water adding and preheating inlet valve 2, opening the pure water inlet valve 4 of the preheater, properly opening the drain valve 3, and discharging the pure water after passing through the spiral wound heat exchanger 6 and the tubular heat exchanger 8.
Adding pure water: when the required pure water is added when the specified current and alkali concentration are reached, the drain valve 3 is closed, the adding preheating pure water inlet valve 2 is opened, and the preheated pure water enters the circulating alkali system. The steam 2 of the spiral wound heat exchanger 6 is properly opened, and the pure water temperature 7(T271) of the spiral wound heat exchanger is controlled at 30 ℃ through a steam regulating valve.
Current rise to specified load: along with the increase of the current, the temperature of the electrolytic cell gradually rises, and the steam 1 of the plate heat exchanger is gradually turned down until the electrolytic cell is completely closed.
During normal operation, the outlet temperature T271 of the spiral wound heat exchanger is properly adjusted according to the temperature T234 of the electrolytic cell, and the temperature T234 of the electrolytic cell is ensured to be about 83 ℃. The temperature T273 (about 83 ℃) of the original plate heat exchanger and the temperature T272 (about 62 ℃) of pure water of the tube heat exchanger were monitored only.
When the electrolysis is stopped: at the moment, the pure water addition is automatically stopped, the steam 2 of the spiral wound heat exchanger 6 is closed, the circulating water of the original plate heat exchanger is opened, and the circulating alkali liquor passing through the plate heat exchanger is cooled by the circulating water, so that the purpose of cooling the electrolytic bath is achieved.
While the present invention has been described in detail with reference to the illustrated embodiments, it should not be construed as limited to the scope of the present patent. Various modifications and changes may be made by those skilled in the art without inventive step within the scope of the appended claims.
Claims (4)
1. A control device for the temperature of a zero-pole distance electronic membrane electrolytic cell is characterized by comprising a spiral wound heat exchanger, a tubular heat exchanger and a control system; the front end of the spiral wound heat exchanger is connected with the pure water control system, and the rear end of the spiral wound heat exchanger is connected with the tube type heat exchanger; the spiral wound heat exchanger is provided with a first temperature transmitter and is connected with a steam system through a regulating valve; and the shell and tube heat exchanger is provided with a second temperature transmitter and is arranged on the hydrogen main pipe.
2. The apparatus for controlling the cell temperature of the zero-polar distance PEM electrolyzer of claim 1 wherein in said shell and tube heat exchanger, the sum of the internal cross-sectional areas of the tube side shell and tube is greater than the internal cross-sectional area of the hydrogen manifold, the hydrogen inlet port is an elliptical head and the hydrogen outlet port is an eccentric head; the hydrogen tube type heat exchanger is installed with 1-2% gradient.
3. The apparatus for controlling the temperature of the zero-pole-distance PEM electrolyzer of claim 1 wherein the control system comprises a first temperature transmitter of a spiral wound heat exchanger, a steam regulating valve, and a second temperature transmitter of a tubular heat exchanger; the first temperature transmitter is used for controlling the opening of a steam regulating valve of the spiral wound heat exchanger, and the second temperature transmitter is used for detecting the pure water temperature of the tube type heat exchanger.
4. The apparatus for controlling the cell temperature of a zero-pole-distance PEM electrolyzer of claim 1 wherein the pure water is preheated by steam through the spiral wound heat exchanger and by hydrogen from the electrolysis header through the hydrogen shell and tube heat exchanger; the temperature of pure water of the spiral wound heat exchanger is controlled to control the temperature of the zero-pole distance electronic membrane electrolytic cell.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202122324891.4U CN215560715U (en) | 2021-09-24 | 2021-09-24 | Control device for zero-pole distance electronic membrane electrolytic cell temperature |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122324891.4U CN215560715U (en) | 2021-09-24 | 2021-09-24 | Control device for zero-pole distance electronic membrane electrolytic cell temperature |
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