JP2016195972A - Evaporative concentration apparatus - Google Patents
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- JP2016195972A JP2016195972A JP2015076811A JP2015076811A JP2016195972A JP 2016195972 A JP2016195972 A JP 2016195972A JP 2015076811 A JP2015076811 A JP 2015076811A JP 2015076811 A JP2015076811 A JP 2015076811A JP 2016195972 A JP2016195972 A JP 2016195972A
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- condensed water
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- neutralizing agent
- evaporator
- monitor
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 154
- 238000005507 spraying Methods 0.000 claims abstract description 18
- 230000003472 neutralizing effect Effects 0.000 claims description 67
- 239000003795 chemical substances by application Substances 0.000 claims description 65
- 239000007788 liquid Substances 0.000 claims description 45
- 239000011550 stock solution Substances 0.000 claims description 34
- 238000010438 heat treatment Methods 0.000 claims description 17
- 238000007599 discharging Methods 0.000 claims description 2
- 239000007921 spray Substances 0.000 abstract description 10
- 239000000460 chlorine Substances 0.000 description 20
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 19
- 229910052801 chlorine Inorganic materials 0.000 description 19
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 18
- 239000007864 aqueous solution Substances 0.000 description 16
- 238000005260 corrosion Methods 0.000 description 11
- 230000007797 corrosion Effects 0.000 description 11
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 10
- 239000000243 solution Substances 0.000 description 10
- 239000002699 waste material Substances 0.000 description 10
- GVPFVAHMJGGAJG-UHFFFAOYSA-L cobalt dichloride Chemical compound [Cl-].[Cl-].[Co+2] GVPFVAHMJGGAJG-UHFFFAOYSA-L 0.000 description 9
- 238000001704 evaporation Methods 0.000 description 9
- 229910052751 metal Inorganic materials 0.000 description 8
- 239000002184 metal Substances 0.000 description 8
- 229910001220 stainless steel Inorganic materials 0.000 description 8
- 239000010935 stainless steel Substances 0.000 description 8
- 239000010941 cobalt Substances 0.000 description 7
- 229910017052 cobalt Inorganic materials 0.000 description 7
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 7
- 230000008020 evaporation Effects 0.000 description 7
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 6
- 238000005363 electrowinning Methods 0.000 description 5
- QWPPOHNGKGFGJK-UHFFFAOYSA-N hypochlorous acid Chemical compound ClO QWPPOHNGKGFGJK-UHFFFAOYSA-N 0.000 description 5
- 229910052742 iron Inorganic materials 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- 238000005070 sampling Methods 0.000 description 5
- 229910021586 Nickel(II) chloride Inorganic materials 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 238000005868 electrolysis reaction Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 229910052759 nickel Inorganic materials 0.000 description 3
- QMMRZOWCJAIUJA-UHFFFAOYSA-L nickel dichloride Chemical compound Cl[Ni]Cl QMMRZOWCJAIUJA-UHFFFAOYSA-L 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 239000005708 Sodium hypochlorite Substances 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000009854 hydrometallurgy Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 238000003911 water pollution Methods 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
Description
本発明は、蒸発濃縮装置に関する。さらに詳しくは、原液中の水分を蒸発させて濃縮液を得る蒸発濃縮装置に関する。 The present invention relates to an evaporative concentration apparatus. More specifically, the present invention relates to an evaporating and concentrating apparatus that obtains a concentrated liquid by evaporating water in a stock solution.
ニッケル・コバルト湿式製錬の電解工程では、電解採取により、例えば塩化コバルト水溶液に含まれるコバルトを電気コバルトとして回収する。電解採取は、電解槽に電解始液として塩化コバルト水溶液を供給し、電解槽に挿入されたアノードとカソードとの間に電流を流すことにより行われる。電解槽から排出された電解廃液はコバルト濃度が低下した塩化コバルト水溶液である。この電解廃液は蒸発濃縮装置により所定のコバルト濃度まで濃縮された後、再び電解始液として電解槽に供給される。このプロセスはニッケルの電解採取においても同様である。 In the electrolysis process of nickel / cobalt hydrometallurgy, for example, cobalt contained in an aqueous cobalt chloride solution is recovered as electric cobalt by electrowinning. Electrolytic extraction is performed by supplying a cobalt chloride aqueous solution as an electrolytic start solution to the electrolytic cell and passing a current between the anode and the cathode inserted in the electrolytic cell. The electrolytic waste liquid discharged from the electrolytic cell is a cobalt chloride aqueous solution having a reduced cobalt concentration. This electrolytic waste liquid is concentrated to a predetermined cobalt concentration by an evaporation concentrator, and then supplied again to the electrolytic cell as an electrolytic start liquid. The process is similar for nickel electrowinning.
蒸発濃縮装置では、原液として電解廃液を蒸発器に供給し、低圧下で加熱することで水分を蒸発させ、所定の濃度まで濃縮した濃縮液を排出する。蒸発器内では塩化コバルト水溶液の水分が蒸発するとともに、原液に含まれる塩素の一部も気化される。塩素を含有する水蒸気は金属腐食性を有するため、蒸発器から排出された水蒸気が通るステンレス製の部材が腐食されるという問題がある。 In the evaporative concentration apparatus, electrolytic waste liquid is supplied to the evaporator as a stock solution, heated under low pressure to evaporate water, and the concentrated liquid concentrated to a predetermined concentration is discharged. In the evaporator, the water of the cobalt chloride aqueous solution evaporates and a part of chlorine contained in the stock solution is also vaporized. Since water vapor containing chlorine has metal corrosivity, there is a problem that a stainless steel member through which water vapor discharged from the evaporator passes is corroded.
特許文献１には、蒸発器において水蒸気とともに生成された酸性ガスを蒸気ダクト内においてアルカリ液散布装置から散布されるアルカリ液と接触させることにより中和し、除去することが開示されている。これにより、蒸気ダクトの腐食を防止している。また、アルカリ液散布装置から散布されるアルカリ液の流量は、凝縮水のｐＨ値が水汚濁防止法に規定されている排水規制値の範囲内となるように、揮発性酸液を含む水溶液の酸濃度に基づいて計算により求められることが開示されている。 Patent Document 1 discloses that acid gas generated together with water vapor in an evaporator is neutralized and removed by contacting with an alkaline liquid sprayed from an alkaline liquid spraying device in a steam duct. This prevents the corrosion of the steam duct. In addition, the flow rate of the alkaline liquid sprayed from the alkaline liquid spraying device is such that the pH value of the condensed water is within the range of the drainage regulation value stipulated in the Water Pollution Control Law. It is disclosed that it is obtained by calculation based on the acid concentration.
ｐＨ計は大気圧下で用いないと正確にｐＨを測定できない。また、ｐＨ計は測定対象液の液位が安定していないと測定値にバラつきが生じる。ところが、蒸発器内は低圧に維持されている。また、凝縮水は間欠的に排出されるため液位が安定しない。そのため、正確にｐＨを測定できず、中和剤の流量を適切に調整できないという問題がある。 A pH meter cannot accurately measure pH unless it is used under atmospheric pressure. Moreover, when the pH level of the measurement target liquid is not stable, the measured value varies. However, the inside of the evaporator is maintained at a low pressure. Moreover, since the condensed water is discharged intermittently, the liquid level is not stable. Therefore, there is a problem that the pH cannot be measured accurately and the flow rate of the neutralizing agent cannot be adjusted appropriately.
本発明は上記事情に鑑み、凝縮水のｐＨに基づき中和剤の流量を適切に調整できる蒸発濃縮装置を提供することを目的とする。 In view of the above circumstances, an object of the present invention is to provide an evaporation concentrator capable of appropriately adjusting the flow rate of a neutralizing agent based on the pH of condensed water.
第１発明の蒸発濃縮装置は、原液が供給される蒸発器と、前記蒸発器に設けられ、前記原液を加熱する間接式加熱器と、前記蒸発器内において発生した水蒸気を前記間接式加熱器の入口ヘッダに導く水蒸気ダクトと、前記水蒸気ダクト内を流れる前記水蒸気に中和剤を散布する中和剤散布装置と、前記間接式加熱器の出口ヘッダから排出された凝縮水を一時貯留する凝縮水タンクと、前記凝縮水タンクから排出された前記凝縮水を大気圧下で貯留するモニタタンクと、前記モニタタンクに設けられ、前記凝縮水のｐＨを測定するｐＨ計と、を備えることを特徴とする。
第２発明の蒸発濃縮装置は、第１発明において、前記モニタタンクの液位を測定する液位計と、前記モニタタンクから前記凝縮水を排出する排出配管と、前記排出配管に設けられた制御弁と、前記液位計の測定値が目標値を維持するように前記制御弁を制御する制御器と、を備えることを特徴とする。
第３発明の蒸発濃縮装置は、第１または第２発明において、前記モニタタンクから排出された前記凝縮水を前記出口ヘッダに導く排出配管を備えることを特徴とする。
An evaporative concentration apparatus according to a first aspect of the present invention includes an evaporator to which a stock solution is supplied, an indirect heater that is provided in the evaporator and heats the stock solution, and water vapor generated in the evaporator is the indirect heater. A water vapor duct that leads to the inlet header, a neutralizer spray device that sprays a neutralizing agent to the water vapor flowing in the water vapor duct, and a condensate that temporarily stores condensed water discharged from the outlet header of the indirect heater A water tank, a monitor tank that stores the condensed water discharged from the condensed water tank under atmospheric pressure, and a pH meter that is provided in the monitor tank and measures the pH of the condensed water. And
The evaporative concentration apparatus according to a second invention is the first aspect of the invention, wherein a liquid level meter for measuring the liquid level in the monitor tank, a discharge pipe for discharging the condensed water from the monitor tank, and a control provided in the discharge pipe And a controller for controlling the control valve so that a measured value of the liquid level meter maintains a target value.
The evaporative concentration apparatus according to a third aspect of the invention is characterized in that, in the first or second aspect of the invention, the evaporative concentration apparatus includes a discharge pipe for guiding the condensed water discharged from the monitor tank to the outlet header.
第１発明によれば、凝縮水を大気圧下で貯留するモニタタンクにｐＨ計が設けられているので、凝縮水のｐＨを正確に測定できる。そのため、凝縮水のｐＨに基づき中和剤の流量を適切に調整できる。
第２発明によれば、モニタタンクの液位が安定するので、凝縮水のｐＨをバラつきなく測定できる。
第３発明によれば、凝縮水が凝縮水タンクとモニタタンクとの間を循環するので、凝縮水のｐＨを均一にでき、凝縮水のｐＨを正確に測定できる。
According to the first aspect, since the pH meter is provided in the monitor tank that stores the condensed water under atmospheric pressure, the pH of the condensed water can be accurately measured. Therefore, the flow rate of the neutralizing agent can be appropriately adjusted based on the pH of the condensed water.
According to the second invention, since the liquid level of the monitor tank is stabilized, the pH of the condensed water can be measured without variation.
According to the third aspect, since the condensed water circulates between the condensed water tank and the monitor tank, the pH of the condensed water can be made uniform and the pH of the condensed water can be accurately measured.
つぎに、本発明の実施形態を図面に基づき説明する。
図１に示すように、本発明の一実施形態に係る蒸発濃縮装置１は蒸発器１０を備えている。蒸発器１０は気密性を有する容器であり、図示しない真空ポンプによりその内部は低圧（例えば、15〜20kPa）に維持されている。また、蒸発器１０には間接式加熱器２０が設けられており、その内部の温度は例えば58〜63℃に維持されている。蒸発器１０内に供給された原液を低圧下で加熱することにより、原液中の水分を蒸発させて濃縮液を得る。
Next, an embodiment of the present invention will be described with reference to the drawings.
As shown in FIG. 1, an evaporative concentration apparatus 1 according to an embodiment of the present invention includes an evaporator 10. The evaporator 10 is an airtight container, and the inside thereof is maintained at a low pressure (for example, 15 to 20 kPa) by a vacuum pump (not shown). Further, the evaporator 10 is provided with an indirect heater 20, and the internal temperature is maintained at 58 to 63 ° C., for example. By heating the stock solution supplied into the evaporator 10 under a low pressure, water in the stock solution is evaporated to obtain a concentrated solution.
蒸発濃縮装置１により電解廃液を濃縮する場合、原液は電解廃液である。例えば、塩化浴のコバルト電解採取工程から排出された電解廃液は塩化コバルト水溶液である。塩化浴のニッケル電解採取工程から排出された電解廃液は塩化ニッケル水溶液である。塩化コバルト水溶液や塩化ニッケル水溶液を濃縮する場合、金属濃度40〜70g/Lの原液（電解廃液）を濃縮して、金属濃度50〜80g/Lの濃縮液（電解始液）を得る。 When the electrolytic waste liquid is concentrated by the evaporative concentration apparatus 1, the stock solution is the electrolytic waste liquid. For example, the electrolytic waste liquid discharged from the cobalt electrowinning process of the chloride bath is a cobalt chloride aqueous solution. The electrolytic waste liquid discharged from the nickel electrowinning process of the chloride bath is an aqueous nickel chloride solution. When a cobalt chloride aqueous solution or a nickel chloride aqueous solution is concentrated, a stock solution (electrolytic waste solution) having a metal concentration of 40 to 70 g / L is concentrated to obtain a concentrated solution (electrolysis start solution) having a metal concentration of 50 to 80 g / L.
蒸発器１０の上部には原液散布ノズル１１が設けられている。蒸発器１０の底部と原液散布ノズル１１とは、ポンプ１２を有する原液循環配管１３で接続されている。原液循環配管１３の途中には原液供給配管１４が接続されている。 A stock solution spray nozzle 11 is provided at the upper part of the evaporator 10. The bottom of the evaporator 10 and the stock solution spray nozzle 11 are connected by a stock solution circulation pipe 13 having a pump 12. In the middle of the stock solution circulation pipe 13, a stock solution supply pipe 14 is connected.
原液供給配管１４から供給された新規の原液は原液散布ノズル１１により間接式加熱器２０に向かって散布される。原液が間接式加熱器２０により加熱されることで、原液中の水分が蒸発する。蒸発器１０内を流下した原液は蒸発器１０の底部に貯留される。蒸発器１０の底部に貯留された原液は、ポンプ１２の駆動により原液循環配管１３を流れ、再び原液散布ノズル１１に導かれる。このように原液は蒸発器１０内を循環し、その過程で水分が蒸発して濃縮液となる。 The new stock solution supplied from the stock solution supply pipe 14 is sprayed toward the indirect heater 20 by the stock solution spray nozzle 11. When the stock solution is heated by the indirect heater 20, the water in the stock solution evaporates. The stock solution flowing down in the evaporator 10 is stored at the bottom of the evaporator 10. The stock solution stored at the bottom of the evaporator 10 flows through the stock solution circulation pipe 13 by driving the pump 12 and is guided to the stock solution spray nozzle 11 again. In this way, the stock solution circulates in the evaporator 10, and in the process, water evaporates to become a concentrated solution.
原液循環配管１３は途中で濃縮液排出配管１５に分岐している。濃縮液排出配管１５にはポンプ１６が設けられている。蒸発器１０において所定の濃度まで濃縮された濃縮液は、ポンプ１６の駆動により濃縮液排出配管１５から排出される。 The stock solution circulation pipe 13 branches to a concentrate discharge pipe 15 on the way. The concentrate discharge pipe 15 is provided with a pump 16. The concentrated liquid concentrated to a predetermined concentration in the evaporator 10 is discharged from the concentrated liquid discharge pipe 15 by driving the pump 16.
間接式加熱器２０は、蒸発器１０の内部に設けられた複数の加熱管２１と、加熱管２１の入口端に接続された入口ヘッダ２２と、加熱管２１の出口端に接続された出口ヘッダ２３とからなる。入口ヘッダ２２に供給された熱媒体は加熱管２１を通った後、出口ヘッダ２３から排出される。 The indirect heater 20 includes a plurality of heating tubes 21 provided inside the evaporator 10, an inlet header 22 connected to the inlet end of the heating tube 21, and an outlet header connected to the outlet end of the heating tube 21. 23. The heat medium supplied to the inlet header 22 passes through the heating pipe 21 and is then discharged from the outlet header 23.
蒸発器１０の上部には水蒸気ダクト２４の一端が接続されている。この水蒸気ダクト２４の他端は間接式加熱器２０の入口ヘッダ２２に接続されている。また、水蒸気ダクト２４の途中にはヒートポンプ２５が設けられている。蒸発器１０内において原液中の水分が蒸発して発生した水蒸気は水蒸気ダクト２４を介して入口ヘッダ２２に導かれる。その途中で水蒸気はヒートポンプ２５により圧縮され温度が上昇する（例えば5℃上昇する）。このように、蒸発器１０内において発生した水蒸気は間接式加熱器２０の熱媒体として利用される。 One end of a water vapor duct 24 is connected to the upper part of the evaporator 10. The other end of the water vapor duct 24 is connected to the inlet header 22 of the indirect heater 20. A heat pump 25 is provided in the middle of the water vapor duct 24. The water vapor generated by the evaporation of the water in the stock solution in the evaporator 10 is guided to the inlet header 22 through the water vapor duct 24. On the way, the water vapor is compressed by the heat pump 25 and the temperature rises (for example, rises by 5 ° C.). Thus, the water vapor generated in the evaporator 10 is used as a heat medium for the indirect heater 20.
また、入口ヘッダ２２には水蒸気供給配管２６が接続されている。水蒸気供給配管２６からは新規の水蒸気が供給される。この水蒸気も間接式加熱器２０の熱媒体として利用される。 In addition, a steam supply pipe 26 is connected to the inlet header 22. New steam is supplied from the steam supply pipe 26. This water vapor is also used as a heat medium for the indirect heater 20.
なお、ヒートポンプ２５に代えて蒸気エジェクタを用いてもよい。この場合、水蒸気供給配管２６から供給される高圧の水蒸気により、蒸発器１０内において発生した水蒸気を吸引し、蒸気エジェクタから吐出される水蒸気を入口ヘッダ２２に供給するよう構成すればよい。 Note that a steam ejector may be used instead of the heat pump 25. In this case, the high-pressure steam supplied from the steam supply pipe 26 may be configured to suck the steam generated in the evaporator 10 and supply the steam discharged from the steam ejector to the inlet header 22.
出口ヘッダ２３には水蒸気排出配管２７および凝縮水排出配管２８が接続されている。入口ヘッダ２２に供給された水蒸気は加熱管２１を介して出口ヘッダ２３に導かれる。その後、水蒸気は水蒸気排出配管２７に設けられたポンプ２９により吸引され、系外に排出される。また、水蒸気は加熱管２１において原液と熱交換することにより一部が凝縮水となる。その凝縮水は出口ヘッダ２３に導かれた後、凝縮水排出配管２８から排出される。 A steam discharge pipe 27 and a condensed water discharge pipe 28 are connected to the outlet header 23. The water vapor supplied to the inlet header 22 is guided to the outlet header 23 via the heating pipe 21. Thereafter, the water vapor is sucked by a pump 29 provided in the water vapor discharge pipe 27 and discharged out of the system. Moreover, a part of the steam becomes condensed water by exchanging heat with the stock solution in the heating tube 21. The condensed water is guided to the outlet header 23 and then discharged from the condensed water discharge pipe 28.
ところで、塩化コバルト水溶液や塩化ニッケル水溶液など塩素を含有する水溶液を原液として用いる場合、蒸発器１０内では原液中の水分が蒸発するとともに、原液に含まれる塩素も気化される。そのため、蒸発器１０から排出される水蒸気には塩素が含まれる。 When an aqueous solution containing chlorine, such as a cobalt chloride aqueous solution or a nickel chloride aqueous solution, is used as a stock solution, moisture in the stock solution evaporates in the evaporator 10 and chlorine contained in the stock solution is also vaporized. Therefore, the steam discharged from the evaporator 10 contains chlorine.
塩素を含有する水蒸気は金属腐食性を有する。この水蒸気から生じた凝縮水には塩素が次亜塩素酸の形態で含まれているため、凝縮水も金属腐食性を有する。ヒートポンプ２５や加熱管２１などのステンレス製の部材は塩素を含有する水蒸気や凝縮水により腐食される。特に、加熱管２１に孔食が生じると、蒸発器１０内の気圧が上昇して、蒸発器１０の効率が低下してしまう。 Water vapor containing chlorine has metal corrosivity. Since the condensed water generated from the water vapor contains chlorine in the form of hypochlorous acid, the condensed water also has metal corrosiveness. Stainless steel members such as the heat pump 25 and the heating tube 21 are corroded by water vapor or condensed water containing chlorine. In particular, when pitting corrosion occurs in the heating tube 21, the atmospheric pressure in the evaporator 10 increases and the efficiency of the evaporator 10 decreases.
また、ステンレス製の部材が腐食されると凝縮水に鉄が溶出する。さらに、加熱管２１に孔食が生じると、鉄を含有する凝縮水が加熱管２１に形成された孔を介して蒸発器１０の内部に浸入する。そうすると、濃縮液に鉄が混入してしまう。 Further, when the stainless steel member is corroded, iron is eluted in the condensed water. Further, when pitting corrosion occurs in the heating tube 21, condensed water containing iron enters the inside of the evaporator 10 through the holes formed in the heating tube 21. If it does so, iron will mix in a concentrate.
塩化コバルト水溶液を用いた電解採取においては、電解槽から排出された電解廃液を蒸発濃縮装置１により濃縮した後、再び電解始液として電解槽に供給することが行われる。上記のごとく濃縮液（電解始液）に鉄が混入すると、不純物である鉄が製品（電気コバルト）に電着するため、製品の品位が低下してしまう。 In electrowinning using an aqueous solution of cobalt chloride, the electrolytic waste liquid discharged from the electrolytic cell is concentrated by the evaporation concentrator 1 and then supplied again to the electrolytic cell as an electrolytic start solution. As described above, when iron is mixed into the concentrated liquid (electrolysis start liquid), the impurity iron is electrodeposited on the product (electrical cobalt), so that the quality of the product is lowered.
そこで、水蒸気ダクト２４には中和剤散布装置３０が設けられている。中和剤散布装置３０は例えば水蒸気ダクト２４の内部に設けられた噴霧器である。中和剤散布装置３０により、水蒸気ダクト２４内を流れる水蒸気に中和剤を散布することで、水蒸気を中和する。これによりヒートポンプ２５や加熱管２１などのステンレス製の部材の腐食を防止できる。これにより、蒸発濃縮装置１の寿命を長くすることができる。ヒートポンプ２５や加熱管２１の素材として耐腐食性を有するチタンなどの高価な素材を採用する必要がなく、ステンレスなどの安価な素材を採用することができるので、設備コストを削減できる。 Accordingly, the water vapor duct 24 is provided with a neutralizing agent spraying device 30. The neutralizer spraying device 30 is a sprayer provided inside the water vapor duct 24, for example. Water vapor is neutralized by spraying the neutralizing agent onto the water vapor flowing in the water vapor duct 24 by the neutralizer spraying device 30. Thereby, corrosion of stainless steel members such as the heat pump 25 and the heating tube 21 can be prevented. Thereby, the lifetime of the evaporative concentration apparatus 1 can be lengthened. It is not necessary to use an expensive material such as titanium having corrosion resistance as a material for the heat pump 25 and the heating tube 21, and an inexpensive material such as stainless steel can be used, so that the equipment cost can be reduced.
なお、中和剤散布装置３０の取り付け場所は水蒸気ダクト２４であれば特に限定されないが、ヒートポンプ２５の吸気口付近が好ましい。このような位置に中和剤散布装置３０を取り付ければ、稼働中のヒートポンプ２５に直接中和剤を散布でき、ヒートポンプ２５の腐食を十分に防止できるからである。 The installation location of the neutralizing agent spray device 30 is not particularly limited as long as it is the water vapor duct 24, but is preferably near the intake port of the heat pump 25. If the neutralizing agent spraying device 30 is attached at such a position, the neutralizing agent can be sprayed directly on the heat pump 25 in operation, and corrosion of the heat pump 25 can be sufficiently prevented.
また、中和剤は水蒸気ダクト２４を流れる水蒸気の流れに沿って散布することが好ましい。中和剤を水蒸気の流れに逆らって散布すると、中和剤が蒸発器１０まで逆流して原液に混入する恐れがあるからである。 The neutralizing agent is preferably sprayed along the flow of water vapor flowing through the water vapor duct 24. This is because if the neutralizing agent is sprayed against the flow of water vapor, the neutralizing agent may flow backward to the evaporator 10 and be mixed into the stock solution.
中和剤散布装置３０には中和剤を供給する中和剤供給部４０が接続されている。中和剤供給部４０は、中和剤を貯留する中和剤タンク４１と、中和剤タンク４１に接続された中和剤供給配管４２と、中和剤供給配管４２に設けられた中和剤ポンプ４３とからなる。中和剤供給配管４２は後述の凝縮水循環配管５１を介して中和剤散布装置３０に接続されている。中和剤ポンプ４３の駆動により中和剤が中和剤散布装置３０に供給され、中和剤が水蒸気ダクト２４内を流れる水蒸気に散布される。また、中和剤ポンプ４３の吐出量を調整することで、水蒸気に散布される中和剤の流量を調整できる。 A neutralizer supply unit 40 for supplying a neutralizer is connected to the neutralizer spray device 30. The neutralizing agent supply unit 40 includes a neutralizing agent tank 41 for storing the neutralizing agent, a neutralizing agent supply pipe 42 connected to the neutralizing agent tank 41, and a neutralizing agent provided in the neutralizing agent supply pipe 42. The agent pump 43. The neutralizing agent supply pipe 42 is connected to the neutralizing agent spraying apparatus 30 through a condensed water circulation pipe 51 described later. The neutralizer is supplied to the neutralizer spraying device 30 by driving the neutralizer pump 43, and the neutralizer is sprayed on the water vapor flowing in the water vapor duct 24. Further, by adjusting the discharge amount of the neutralizing agent pump 43, the flow rate of the neutralizing agent dispersed in the water vapor can be adjusted.
中和剤としては特に限定されないが、塩素を中和する場合にはアルカリ液、特に水酸化ナトリウム水溶液が好適に用いられる。塩素を含有する水蒸気に散布される水酸化ナトリウム水溶液の濃度は0.2〜1.0%が好ましい。濃度が1.0%より高い場合、水蒸気中の塩素と水酸化ナトリウムとが反応して塩化ナトリウムや次亜塩素ナトリウムが生成される。これらが装置の内壁に付着すると孔食発生の起点となる。また、これらがヒートポンプ２５のファンに付着すると、動バランスが崩れてしまう。濃度が0.2%未満の場合、中和剤としての効果が不十分となる。 Although it does not specifically limit as a neutralizing agent, When neutralizing chlorine, an alkali liquid, especially sodium hydroxide aqueous solution is used suitably. The concentration of the aqueous sodium hydroxide solution dispersed in the water vapor containing chlorine is preferably 0.2 to 1.0%. When the concentration is higher than 1.0%, chlorine in the water vapor reacts with sodium hydroxide to produce sodium chloride or sodium hypochlorite. If these adhere to the inner wall of the device, they become the starting point for pitting corrosion. Moreover, if these adhere to the fan of the heat pump 25, the dynamic balance will be lost. When the concentration is less than 0.2%, the effect as a neutralizing agent is insufficient.
中和剤タンク４１に貯留された中和剤の濃度が前記濃度よりも高い場合には、中和剤を希釈してから中和剤散布装置３０に供給すればよい。本実施形態では、間接式加熱器２０から排出された凝縮水で中和剤を希釈する構成としている。 If the concentration of the neutralizing agent stored in the neutralizing agent tank 41 is higher than the above concentration, the neutralizing agent may be diluted before being supplied to the neutralizing agent spraying device 30. In the present embodiment, the neutralizing agent is diluted with the condensed water discharged from the indirect heater 20.
間接式加熱器２０の出口ヘッダ２３は凝縮水排出配管２８により凝縮水タンク５０に接続されている。したがって、出口ヘッダ２３から排出された凝縮水は凝縮水タンク５０に一時貯留される。凝縮水タンク５０は気密性を有する容器である。また、出口ヘッダ２３内の水蒸気はポンプ２９により吸引されているため、出口ヘッダ２３内および凝縮水タンク５０は負圧となっている。 The outlet header 23 of the indirect heater 20 is connected to a condensed water tank 50 by a condensed water discharge pipe 28. Therefore, the condensed water discharged from the outlet header 23 is temporarily stored in the condensed water tank 50. The condensed water tank 50 is an airtight container. Further, since the water vapor in the outlet header 23 is sucked by the pump 29, the pressure in the outlet header 23 and the condensed water tank 50 is negative.
凝縮水タンク５０には凝縮水循環配管５１の一端が接続されている。凝縮水循環配管５１の他端は中和剤散布装置３０に接続されている。凝縮水循環配管５１には凝縮水ポンプ５２が設けられている。凝縮水ポンプ５２の駆動により、凝縮水タンク５０に貯留された凝縮水が中和剤散布装置３０に導かれる。その途中で中和剤タンク４１から供給された中和剤と凝縮水とが混合され、希釈された中和剤が中和剤散布装置３０に供給される。また、凝縮水ポンプ５２の吐出量を調整することで、中和剤に対する凝縮水の混合比率を調整できる。 One end of a condensed water circulation pipe 51 is connected to the condensed water tank 50. The other end of the condensed water circulation pipe 51 is connected to the neutralizer spray device 30. A condensed water pump 52 is provided in the condensed water circulation pipe 51. By driving the condensed water pump 52, the condensed water stored in the condensed water tank 50 is guided to the neutralizing agent spraying device 30. On the way, the neutralizing agent supplied from the neutralizing agent tank 41 and the condensed water are mixed, and the diluted neutralizing agent is supplied to the neutralizing agent spraying device 30. Moreover, the mixing ratio of the condensed water with respect to the neutralizing agent can be adjusted by adjusting the discharge amount of the condensed water pump 52.
凝縮水タンク５０から排出された凝縮水のうち余剰分は凝縮水排出配管５４を介して系外に排出される。 A surplus portion of the condensed water discharged from the condensed water tank 50 is discharged outside the system through the condensed water discharge pipe 54.
中和剤散布装置３０から散布する中和剤の流量は凝縮水のｐＨに基づき調整される。塩素を中和する場合には、凝縮水がｐＨ１０以上となるように中和剤の流量を調整することが好ましい。図２に示すように、塩素を含む水溶液はｐＨに依存してCl2、HClO、ClO-の各形態が所定の比率で存在する。ｐＨ５から７の領域では次亜塩素酸態濃度が高い。ｐＨ７以上では有効塩素存在率が低下し、特にｐＨ１０以上の領域では次亜塩素酸がなくなるため、金属腐食性が著しく低下する。そのため、凝縮水がｐＨ１０以上であれば、ヒートポンプ２５や加熱管２１などのステンレス製の部材の腐食を十分に防止できる。 The flow rate of the neutralizing agent sprayed from the neutralizing agent spraying device 30 is adjusted based on the pH of the condensed water. When neutralizing chlorine, it is preferable to adjust the flow rate of the neutralizing agent so that the condensed water has a pH of 10 or more. As shown in FIG. 2, the aqueous solution containing chlorine has Cl 2 , HClO, and ClO − forms in a predetermined ratio depending on the pH. In the range of pH 5 to 7, the hypochlorous acid concentration is high. When the pH is 7 or more, the effective chlorine abundance decreases, and particularly when the pH is 10 or more, hypochlorous acid disappears, so that the metal corrosiveness is remarkably reduced. Therefore, if the condensed water has a pH of 10 or more, corrosion of stainless steel members such as the heat pump 25 and the heating pipe 21 can be sufficiently prevented.
本実施形態は凝縮水のｐＨを測定するためにモニタタンク６０を設けたところに特徴を有する。
前記凝縮水循環配管５１には凝縮水ポンプ５２の下流に採取配管６１の一端が接続されている。採取配管６１の他端はモニタタンク６０に接続されている。凝縮水タンク５０から排出された凝縮水の一部が採取配管６１を介してモニタタンク６０に供給される。モニタタンク６０は上部が開放されたタンクである。そのため、モニタタンク６０では凝縮水が大気圧下で貯留される。
The present embodiment is characterized in that a monitor tank 60 is provided to measure the pH of the condensed water.
One end of a sampling pipe 61 is connected to the condensed water circulation pipe 51 downstream of the condensed water pump 52. The other end of the sampling pipe 61 is connected to the monitor tank 60. A part of the condensed water discharged from the condensed water tank 50 is supplied to the monitor tank 60 through the sampling pipe 61. The monitor tank 60 is a tank with an open top. Therefore, condensed water is stored in the monitor tank 60 under atmospheric pressure.
モニタタンク６０には凝縮水のｐＨを測定するｐＨ計６２が設けられている。このｐＨ計６２の測定値に基づき中和剤の流量を調整できる。 The monitor tank 60 is provided with a pH meter 62 for measuring the pH of the condensed water. Based on the measured value of the pH meter 62, the flow rate of the neutralizing agent can be adjusted.
モニタタンク６０には排出配管６３の一端が接続されている。排出配管６３の他端は間接式加熱器２０の出口ヘッダ２３に接続されている。モニタタンク６０に貯留された凝縮水は排出配管６３を介して排出される。排出された凝縮水は排出配管６３により出口ヘッダ２３に導かれ、再び凝縮水タンク５０に排出される。 One end of a discharge pipe 63 is connected to the monitor tank 60. The other end of the discharge pipe 63 is connected to the outlet header 23 of the indirect heater 20. The condensed water stored in the monitor tank 60 is discharged through the discharge pipe 63. The discharged condensed water is guided to the outlet header 23 by the discharge pipe 63 and discharged again to the condensed water tank 50.
排出配管６３には制御弁６４が設けられている。制御弁６４には制御弁６４の開閉を制御する制御部６５が接続されている。制御部６５はＣＰＵやメモリなどで構成されたコンピュータで構成されてもよいし、単純な電子回路で構成されてもよい。前述のごとく、出口ヘッダ２３内は負圧となっている。そのため、制御弁６４を開にすると、モニタタンク６０内の凝縮水はその負圧により出口ヘッダ２３に吸引される。 The discharge pipe 63 is provided with a control valve 64. A control unit 65 that controls opening and closing of the control valve 64 is connected to the control valve 64. The control unit 65 may be configured by a computer configured by a CPU, a memory, or the like, or may be configured by a simple electronic circuit. As described above, the inside of the outlet header 23 has a negative pressure. Therefore, when the control valve 64 is opened, the condensed water in the monitor tank 60 is sucked into the outlet header 23 by the negative pressure.
モニタタンク６０には凝縮水の液位を測定する液位計６６が設けられている。液位計６６の測定値は制御部６５に入力されている。制御部６５は液位計６６の測定値が目標値を維持するように制御弁６４の開閉を制御する。 The monitor tank 60 is provided with a liquid level meter 66 for measuring the level of condensed water. The measured value of the liquid level meter 66 is input to the control unit 65. The controller 65 controls the opening and closing of the control valve 64 so that the measured value of the liquid level meter 66 maintains the target value.
制御部６５は例えば以下のように制御弁６４を制御する。液位計６６の測定値が上限値に達すると制御部６５は制御弁６４を開とする。そうすると、モニタタンク６０から凝縮水が排出され、液位が下がる。液位計６６の測定値が下限値に達すると、制御部６５は制御弁６４を閉とする。そうすると、採取配管６１から供給される凝縮水によりモニタタンク６０の液位が上がる。このようにして、モニタタンク６０の液位が一定に維持される。なお、上記例のように液位の目標値を上限値と下限値とからなる幅で設定してもよいし、ただ１つの値として定めてもよい。 The control unit 65 controls the control valve 64 as follows, for example. When the measured value of the liquid level meter 66 reaches the upper limit value, the control unit 65 opens the control valve 64. If it does so, condensed water will be discharged | emitted from the monitor tank 60, and a liquid level will fall. When the measured value of the liquid level meter 66 reaches the lower limit value, the control unit 65 closes the control valve 64. Then, the liquid level in the monitor tank 60 is raised by the condensed water supplied from the sampling pipe 61. In this way, the liquid level in the monitor tank 60 is kept constant. Note that, as in the above example, the target value of the liquid level may be set within a range consisting of an upper limit value and a lower limit value, or may be determined as a single value.
ｐＨ計６２はその構造上負圧下では正確にｐＨを測定できない。これに対して、本実施形態では凝縮水を大気圧下で貯留するモニタタンク６０にｐＨ計６２が設けられているので、凝縮水のｐＨを正確に測定できる。 The pH meter 62 cannot accurately measure pH under a negative pressure due to its structure. On the other hand, in this embodiment, since the pH meter 62 is provided in the monitor tank 60 which stores condensed water under atmospheric pressure, the pH of condensed water can be measured accurately.
また、ｐＨ計６２は測定対象液の液位が安定しないと測定値にバラつきが生じる。出口ヘッダ２３からは凝縮水が間欠的に排出されるため、この凝縮水のｐＨをそのまま測定しようとすると測定値にバラつきが生じる。これに対して、本実施形態では出口ヘッダ２３から排出された凝縮水を一度凝縮水タンク５０に貯留した後、モニタタンク６０に供給している。凝縮水タンク５０とモニタタンク６０の二段構成とすることで、モニタタンク６０には凝縮水が連続的に静かに供給される。また、モニタタンク６０の液位は、制御弁６４、制御部６５および液位計６６が協働することで一定に維持される。そのため、モニタタンク６０の液位が安定するので、凝縮水のｐＨをバラつきなく測定できる。 Further, the pH value of the pH meter 62 varies when the liquid level of the liquid to be measured is not stable. Since the condensed water is intermittently discharged from the outlet header 23, the measured value varies when the pH of the condensed water is measured as it is. In contrast, in this embodiment, the condensed water discharged from the outlet header 23 is once stored in the condensed water tank 50 and then supplied to the monitor tank 60. By adopting a two-stage configuration of the condensed water tank 50 and the monitor tank 60, the condensed water is continuously and quietly supplied to the monitor tank 60. Further, the liquid level in the monitor tank 60 is maintained constant by the cooperation of the control valve 64, the control unit 65, and the liquid level meter 66. Therefore, since the liquid level of the monitor tank 60 is stabilized, the pH of the condensed water can be measured without variation.
さらに、モニタタンク６０から排出された凝縮水は出口ヘッダ２３に戻される。これにより、凝縮水が凝縮水タンク５０とモニタタンク６０との間を循環するので、凝縮水の局所的な濃淡が少なくなり凝縮水のｐＨを均一にできる。その結果、凝縮水のｐＨを正確に測定できる。 Further, the condensed water discharged from the monitor tank 60 is returned to the outlet header 23. Thereby, since condensed water circulates between the condensed water tank 50 and the monitor tank 60, the local density of condensed water decreases and the pH of condensed water can be made uniform. As a result, the pH of the condensed water can be accurately measured.
以上のように、凝縮水のｐＨを正確に測定できるため、凝縮水のｐＨに基づき中和剤の流量を適切に調整できる。また、凝縮水のｐＨに基づき中和剤の流量を調整することで、原液の溶存塩素負荷が変動する場合にも、その変動に追従して中和剤の流量を適切に増減できる。 As described above, since the pH of the condensed water can be accurately measured, the flow rate of the neutralizing agent can be appropriately adjusted based on the pH of the condensed water. Further, by adjusting the flow rate of the neutralizing agent based on the pH of the condensed water, even when the dissolved chlorine load of the stock solution fluctuates, the flow rate of the neutralizing agent can be appropriately increased or decreased following the fluctuation.
中和剤の流量調整は、ｐＨ計６２の測定値を監視し、測定値の上下動に合わせて中和剤ポンプ４３の吐出量を増減させることにより行われる。塩素を中和する場合、ｐＨ計６２の測定値がｐＨ１０以上となるように中和剤の流量を調整すれば、ヒートポンプ２５や加熱管２１などのステンレス製の部材の腐食を十分に防止できる。 The flow rate of the neutralizing agent is adjusted by monitoring the measured value of the pH meter 62 and increasing or decreasing the discharge amount of the neutralizing agent pump 43 in accordance with the vertical movement of the measured value. In the case of neutralizing chlorine, corrosion of stainless steel members such as the heat pump 25 and the heating tube 21 can be sufficiently prevented by adjusting the flow rate of the neutralizing agent so that the measured value of the pH meter 62 becomes pH 10 or more.
中和剤の流量調整は作業員が手動で行ってもよい。この場合、作業員がｐＨ計６２の測定値を監視し、その測定値に基づいて中和剤ポンプ４３の吐出量を調整する。これに代えて、制御装置により自動で中和剤の流量調整を行ってもよい。この場合、制御装置はｐＨ計６２の測定値に基づいて中和剤ポンプ４３の吐出量を制御するよう構成される。このような構成とすれば人員コストを削減できる。 The flow rate of the neutralizing agent may be manually adjusted by an operator. In this case, the operator monitors the measured value of the pH meter 62 and adjusts the discharge amount of the neutralizer pump 43 based on the measured value. Instead of this, the flow rate of the neutralizing agent may be automatically adjusted by the control device. In this case, the control device is configured to control the discharge amount of the neutralizer pump 43 based on the measured value of the pH meter 62. With such a configuration, personnel costs can be reduced.
また、中和剤の濃度を調整することもできる。例えば、凝縮水ポンプ５２の吐出量を一定として凝縮水の流量を一定とする。一方で中和剤ポンプ４３の吐出量を調整することで中和剤の流量を調整する。これにより中和剤と凝縮水との混合比率を調整することで中和剤の濃度を調整できる。中和剤ポンプ４３の吐出量を一定として凝縮水ポンプ５２の吐出量を調整してもよいし、中和剤ポンプ４３と凝縮水ポンプ５２の両方の吐出量を調整してもよい。中和剤として水酸化ナトリウム水溶液を用いる場合、希釈した後の水酸化ナトリウム水溶液の濃度が0.2〜1.0%となるように、中和剤と凝縮水との混合比率を調整すればよい。 In addition, the concentration of the neutralizing agent can be adjusted. For example, the discharge amount of the condensed water pump 52 is constant, and the flow rate of the condensed water is constant. On the other hand, the flow rate of the neutralizing agent is adjusted by adjusting the discharge amount of the neutralizing agent pump 43. Thereby, the density | concentration of a neutralizing agent can be adjusted by adjusting the mixing ratio of a neutralizing agent and condensed water. The discharge amount of the condensed water pump 52 may be adjusted with the discharge amount of the neutralizing agent pump 43 being constant, or the discharge amounts of both the neutralizing agent pump 43 and the condensed water pump 52 may be adjusted. When using a sodium hydroxide aqueous solution as the neutralizing agent, the mixing ratio of the neutralizing agent and the condensed water may be adjusted so that the concentration of the diluted sodium hydroxide aqueous solution is 0.2 to 1.0%.
つぎに、実施例を説明する。
（実施例）
上記実施形態の蒸発濃縮装置１を用いて、電解廃液（塩化コバルト水溶液）の濃縮を行った。中和剤としては水酸化ナトリウム水溶液を用いた。ｐＨ計６２の測定値に基づき、凝縮液のｐＨが１０となるように中和剤の流量を調整した。
Next, examples will be described.
(Example)
The electrolytic waste liquid (cobalt chloride aqueous solution) was concentrated using the evaporation concentration apparatus 1 of the said embodiment. A sodium hydroxide aqueous solution was used as the neutralizing agent. Based on the measured value of the pH meter 62, the flow rate of the neutralizing agent was adjusted so that the pH of the condensate was 10.
実施例における運転状況は表１に示す通りである。
凝縮水のｐＨが１０以上であることから、凝縮水の金属腐食性は低くなっていることが分かる。６ヶ月ごとに装置の点検を行ったが、孔食の発生は確認されなかった。 Since the pH of condensed water is 10 or more, it turns out that the metal corrosivity of condensed water is low. The device was inspected every 6 months, but no pitting corrosion was confirmed.
（比較例）
上記実施形態の蒸発濃縮装置１において、中和剤の散布を行わずに運転を行った。比較例における運転状況は表２に示す通りである。
In the evaporative concentration apparatus 1 of the above embodiment, the operation was performed without spraying the neutralizing agent. The operation status in the comparative example is as shown in Table 2.
凝縮水のｐＨが上記の領域では、凝縮水中の塩素は遊離塩素を含む次亜塩素酸であり金属腐食性を有する。そのため、装置を長期間運転した場合にはステンレス製の部材は凝縮水により腐食される。発生した孔食を溶接して補修する作業が２ヶ月ごとに必要であった。 When the pH of the condensed water is in the above range, chlorine in the condensed water is hypochlorous acid containing free chlorine and has metal corrosiveness. Therefore, when the apparatus is operated for a long time, the stainless steel member is corroded by the condensed water. Work to repair the generated pitting corrosion by welding was necessary every two months.
１ 蒸発濃縮装置
１０ 蒸発器
２０ 間接式加熱器
２１ 加熱管
２２ 入口ヘッダ
２３ 出口ヘッダ
２４ 水蒸気ダクト
２５ ヒートポンプ
３０ 中和剤散布装置
４０ 中和剤供給部
５０ 凝縮水タンク
６０ モニタタンク
６１ 採取配管
６２ ｐＨ計
６３ 排出配管
６４ 制御弁
６５ 制御部
６６ 液位計
DESCRIPTION OF SYMBOLS 1 Evaporation concentration apparatus 10 Evaporator 20 Indirect heater 21 Heating pipe 22 Inlet header 23 Outlet header 24 Water vapor duct 25 Heat pump 30 Neutralizing agent spraying apparatus 40 Neutralizing agent supply part 50 Condensed water tank 60 Monitor tank 61 Sampling piping 62 pH Total 63 Discharge piping 64 Control valve 65 Control unit 66 Liquid level meter
Claims (3)
前記蒸発器に設けられ、前記原液を加熱する間接式加熱器と、
前記蒸発器内において発生した水蒸気を前記間接式加熱器の入口ヘッダに導く水蒸気ダクトと、
前記水蒸気ダクト内を流れる前記水蒸気に中和剤を散布する中和剤散布装置と、
前記間接式加熱器の出口ヘッダから排出された凝縮水を一時貯留する凝縮水タンクと、
前記凝縮水タンクから排出された前記凝縮水を大気圧下で貯留するモニタタンクと、
前記モニタタンクに設けられ、前記凝縮水のｐＨを測定するｐＨ計と、を備える
ことを特徴とする蒸発濃縮装置。 An evaporator to which the stock solution is supplied;
An indirect heater provided in the evaporator for heating the stock solution;
A steam duct for guiding steam generated in the evaporator to an inlet header of the indirect heater;
A neutralizing agent spraying device for spraying a neutralizing agent to the steam flowing in the steam duct;
A condensed water tank for temporarily storing condensed water discharged from the outlet header of the indirect heater;
A monitor tank for storing the condensed water discharged from the condensed water tank under atmospheric pressure;
An evaporative concentration apparatus comprising: a pH meter provided in the monitor tank and measuring the pH of the condensed water.
前記モニタタンクから前記凝縮水を排出する排出配管と、
前記排出配管に設けられた制御弁と、
前記液位計の測定値が目標値を維持するように前記制御弁を制御する制御器と、を備える
ことを特徴とする請求項１記載の蒸発濃縮装置。 A liquid level meter for measuring the liquid level of the monitor tank;
A discharge pipe for discharging the condensed water from the monitor tank;
A control valve provided in the discharge pipe;
The evaporative concentration apparatus according to claim 1, further comprising a controller that controls the control valve so that a measured value of the liquid level meter maintains a target value.
ことを特徴とする請求項１または２記載の蒸発濃縮装置。 The evaporative concentration apparatus according to claim 1, further comprising a discharge pipe that guides the condensed water discharged from the monitor tank to the outlet header.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110947191A (en) * | 2018-09-27 | 2020-04-03 | 韩林辰 | Contact evaporation system |
| CN111389801A (en) * | 2020-04-16 | 2020-07-10 | 生态环境部华南环境科学研究所 | Automatic cleaning water-saving device and cleaning method for electroplating production |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0724202A (en) * | 1993-07-12 | 1995-01-27 | Sasakura Eng Co Ltd | Vapor-compression vacuum-evaporation concentrator |
| JP2007098320A (en) * | 2005-10-06 | 2007-04-19 | Sasakura Engineering Co Ltd | Enrichment apparatus and neutralizing method |
| JP2007136374A (en) * | 2005-11-21 | 2007-06-07 | Sasakura Engineering Co Ltd | Evaporating/concentrating device |
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2015
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0724202A (en) * | 1993-07-12 | 1995-01-27 | Sasakura Eng Co Ltd | Vapor-compression vacuum-evaporation concentrator |
| JP2007098320A (en) * | 2005-10-06 | 2007-04-19 | Sasakura Engineering Co Ltd | Enrichment apparatus and neutralizing method |
| JP2007136374A (en) * | 2005-11-21 | 2007-06-07 | Sasakura Engineering Co Ltd | Evaporating/concentrating device |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110947191A (en) * | 2018-09-27 | 2020-04-03 | 韩林辰 | Contact evaporation system |
| CN111389801A (en) * | 2020-04-16 | 2020-07-10 | 生态环境部华南环境科学研究所 | Automatic cleaning water-saving device and cleaning method for electroplating production |
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