JPH0557037B2 - - Google Patents
Info
- Publication number
- JPH0557037B2 JPH0557037B2 JP15096885A JP15096885A JPH0557037B2 JP H0557037 B2 JPH0557037 B2 JP H0557037B2 JP 15096885 A JP15096885 A JP 15096885A JP 15096885 A JP15096885 A JP 15096885A JP H0557037 B2 JPH0557037 B2 JP H0557037B2
- Authority
- JP
- Japan
- Prior art keywords
- brine
- amount
- produced water
- water
- pipe
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 75
- 239000012267 brine Substances 0.000 claims description 55
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 55
- 238000010438 heat treatment Methods 0.000 claims description 12
- 238000001704 evaporation Methods 0.000 description 18
- 230000008020 evaporation Effects 0.000 description 18
- 239000013535 sea water Substances 0.000 description 10
- 230000010354 integration Effects 0.000 description 8
- 239000007788 liquid Substances 0.000 description 7
- 230000033228 biological regulation Effects 0.000 description 4
- 230000007423 decrease Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 230000001276 controlling effect Effects 0.000 description 2
- 238000005192 partition Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000011109 contamination Methods 0.000 description 1
- 230000001186 cumulative effect Effects 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 235000020188 drinking water Nutrition 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 230000001932 seasonal effect Effects 0.000 description 1
- 239000008400 supply water Substances 0.000 description 1
- 238000003809 water extraction Methods 0.000 description 1
Landscapes
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Description
【発明の詳細な説明】
（産業上の利用分野）
本発明は海水淡水化に用いる多段フラツシユ蒸
発装置における製造水量を供給海水の温度変化、
装置の汚れなどにもかかわらず常に一定量を確保
するための自動制御装置に関するものである。DETAILED DESCRIPTION OF THE INVENTION (Industrial Application Field) The present invention aims to reduce the amount of produced water in a multi-stage flash evaporator used for seawater desalination by changing the temperature of the seawater,
This relates to an automatic control device that always maintains a constant amount of water regardless of whether the device is dirty or the like.
（従来の技術）
ブライン再循環式多段フラツシユ蒸発装置は、
安定した作動を維持するためには、熱入力とブラ
イン循環量とを一定のバランスに保ちながら操業
しなければならず、そのため最高温の第１段蒸発
室内のブライン液位、もしくはブラインヒータ出
口のブライン温度、または両者を検出し、この検
出値を演算器で設定ブライン流量入力として、ブ
ライン流量調節計へ入力して、この調節計の出力
に応答して循環ブライン流量を調節しブライン液
位を一定に保つ制御手段が一般に採用されてい
る。このような調節は貫流式多段フラツシユ蒸発
装置にも適用できる。(Prior art) Brine recirculation multi-stage flash evaporator is
In order to maintain stable operation, it is necessary to maintain a constant balance between heat input and brine circulation. Therefore, the brine liquid level in the first stage evaporation chamber, which is at the highest temperature, or at the outlet of the brine heater must be maintained at a constant balance. Detect the brine temperature, or both, and input this detected value to the brine flow rate controller as the brine flow rate input set by the calculator, and adjust the circulating brine flow rate in response to the output of this controller to adjust the brine liquid level. Control means to keep it constant are generally employed. Such adjustment can also be applied to once-through multi-stage flash evaporators.
しかしながら製造水量変更のためのブライン温
度設定値の大巾な変更は制御系を擾乱し、ブライ
ン温度は大きくハンチングする恐れがある。これ
を抑え制御遅れを可及的に短縮する目的で、緩衝
器を用い、かつブライン流量調節とブライン温度
調節とを同時並行的に行う制御方法が、先行技術
として特開昭57−140691号公報に記載されてい
る。 However, a large change in the brine temperature setting value to change the amount of produced water may disturb the control system and cause the brine temperature to greatly hunt. In order to suppress this and shorten the control delay as much as possible, a control method using a buffer and simultaneously controlling the brine flow rate and brine temperature is disclosed in Japanese Patent Application Laid-Open No. 57-140691 as a prior art. It is described in.
この先行技術は添付した第５図で明らかなよう
に、ある運転状態から製造水量の需要に応じた値
だけ設定器Ａの設定値を変えたとすると、この設
定値の変化分は大小を問わず緩衝器Ｂによつて緩
慢な変化に変えられ、第１の演算器Ｃによつて設
定ブライン量に変換されてブライン流量調節器Ｄ
へ供給され、この調節器Ｄからは徐々に変化する
開弁または閉弁のための制御信号がブライン流量
調節弁Ｅへ供給されると同時に、第２の演算器Ｆ
を経てブラインヒータ出口ブライン温度調節器Ｇ
へも供給されて、該調節器Ｇからブラインヒータ
加熱量調節手段Ｈへ、そのための制御信号が供給
される。このようにして調節弁Ｅ及び調節手段Ｈ
の調節は同時並行的に行われるので、従来のよう
に制御遅れは生ぜず、需要量の変化に即応し得
る、と述べている。 As is clear from the attached Fig. 5, in this prior art, if the setting value of the setting device A is changed by a value corresponding to the demand for the amount of produced water from a certain operating state, the change in this setting value will change regardless of the size. It is changed into a slow change by the buffer B, and converted into a set brine amount by the first computing unit C, and then the brine flow rate controller D
A gradually changing control signal for opening or closing the valve is supplied from the regulator D to the brine flow rate regulating valve E.
Brine heater outlet brine temperature regulator G
A control signal therefor is also supplied from the regulator G to the brine heater heating amount regulating means H. In this way, the control valve E and the control means H
Since the adjustments are made in parallel, there is no control delay like in the past, and it is possible to respond immediately to changes in demand.
（発明が解決しようとする問題点）
しかしながら、多段フラツシユ蒸発装置におけ
る製造水量は潮流の変動、供給海水の季節的な温
度変化に左右されるから、海水温度により製造水
量設定をカスケード制御する場合は、上記先行技
術ではフイードバツクする手段がないため、或る
変数が変わると製造水量は設定値に追従できず、
その都度製造水量設定器Ａをセツトし直さねばな
らず、面倒であつた。このような問題は貫流式多
段フラツシユ蒸発装置でも同様である。(Problem to be Solved by the Invention) However, the amount of water produced in a multi-stage flash evaporator is affected by fluctuations in tidal currents and seasonal temperature changes in the supplied seawater. In the above prior art, there is no means for feedback, so if a certain variable changes, the amount of produced water cannot follow the set value,
The produced water amount setting device A had to be reset each time, which was troublesome. Such problems also occur in once-through type multi-stage flash evaporators.
（問題を解決するための手段）
上記に鑑み本発明では、多段フラツシユ蒸発装
置において、製造水量積算値がフイードバツクさ
れて、製造水量設定値とその製造水積算値とを比
較演算する製造水量調節系統と、この比較値の差
が小さくなるよう加熱蒸気量修正系統及び給水量
修正系統とを備えて、蒸発装置における製造水量
自動制御を行う手段を採用して上記の問題を解決
し、これにより供給海水の温度変化や伝熱量の汚
れ等によつて伝熱量が変化しても、わざわざ設定
器を操作せずに年間を通じて自動的に一定量の製
造水を確保できる。(Means for Solving the Problem) In view of the above, in the present invention, in a multi-stage flash evaporator, an integrated value of produced water is fed back, and a produced water amount adjustment system that compares and calculates a set value of produced water amount and the integrated produced water value is provided. The above problem is solved by adopting means for automatically controlling the amount of water produced in the evaporator, which is equipped with a heating steam amount correction system and a water supply amount correction system so that the difference between the comparison values becomes smaller. Even if the amount of heat transfer changes due to changes in seawater temperature or contamination of the heat transfer amount, it is possible to automatically secure a constant amount of manufactured water throughout the year without having to go through the trouble of operating a setting device.
（実施例）
第１図に示すブライン再循環式多段フラツシユ
蒸発装置１は、通常のように複数の蒸発室２が隔
壁３を介して並設された熱回収部４と、熱放出部
５及びブラインヒータ６を有し、各蒸発室２は隔
壁３の下端に設けられて開口面積が調整されたオ
リフイス７によつて連通し、上方には凝縮管束８
が配置されていて、その下方に蒸留水溜があつ
て、製造水取出管９によつて製造水がポンプ１０
を経て外部に取出され、最終段蒸発室２ｎに連絡
する真空装置１１によつて各蒸発室２は真空に保
たれている。(Example) The brine recirculation type multi-stage flash evaporator 1 shown in FIG. It has a brine heater 6, and each evaporation chamber 2 communicates through an orifice 7 provided at the lower end of the partition wall 3 and whose opening area is adjusted.
is arranged, there is a distilled water reservoir below it, and the produced water is supplied to the pump 10 through the produced water take-out pipe 9.
Each evaporation chamber 2 is kept in a vacuum by a vacuum device 11 which is taken out to the outside through the evaporation chamber 2n and communicates with the final stage evaporation chamber 2n.
最終段蒸発室２ｎには、液面計１２と濃縮ブラ
イン排出管に設けた調節弁１３からなる液面調節
装置１４が設けられている。ブラインヒータ６は
蒸気管１５によつて外部より加熱用蒸気が導入さ
れて、管内を流れるブラインを加熱する。 The final stage evaporation chamber 2n is provided with a liquid level adjustment device 14 consisting of a liquid level gauge 12 and a control valve 13 provided on the concentrated brine discharge pipe. Heating steam is introduced into the brine heater 6 from the outside through a steam pipe 15, and heats the brine flowing inside the pipe.
前述の製造水取出管９には製造水検出器１６
と、設定器１７を附属した製造水量調節系統１８
が設けられて、この調節系統１８には積算演算器
１９から製造水量積算値がフイードバツク回路２
０を経てフイードバツクされていて、更に比較開
始装置２１が附属している。また製造水量調節系
統１８は第１演算器２２と第２演算器２３に連絡
し、それぞれ加熱蒸気量修正系統２４及びブライ
ン循環量修正系統２５に連絡している。各調節弁
の開閉を緩やかにするため緩衝器３６を設けても
よい。 A manufactured water detector 16 is installed in the aforementioned manufactured water take-out pipe 9.
and a production water flow control system 18 with a setter 17 attached.
The adjustment system 18 receives an integrated value of produced water amount from an integration calculator 19 and sends it to the feedback circuit 2.
0, and a comparison start device 21 is also attached. Further, the produced water amount adjustment system 18 is connected to a first computing unit 22 and a second computing unit 23, and is also connected to a heating steam amount correction system 24 and a brine circulation amount correction system 25, respectively. A buffer 36 may be provided to ease the opening and closing of each control valve.
上記の装置において、給水管２６から導入され
た海水は熱放出部５の凝縮管束を通り、大部分の
海水は管２７から排出され、一部が分岐して管２
８より最終段蒸発室２ｎに入る。この海水は濃縮
ブラインと混合したのち、ブライン循環管路２９
を経て熱回収部４の凝縮管束８を流れ、ブライン
ヒータ６で外部蒸気と熱交換して加熱されたのち
出口管３０から第１段蒸発室２ａに入り、オリフ
イス７を通過して流れ、その間フラツシユ蒸発す
る。各蒸発室の発生蒸気は凝縮して製造水取出管
９を流れ、ポンプ１０によつて外部に取出され
る。残存濃縮ブラインは最終段蒸発室２ｎで液面
調節装置１４によつて一定水位が保たれ、管３５
より排出される。 In the above device, the seawater introduced from the water supply pipe 26 passes through the condensing pipe bundle of the heat release section 5, and most of the seawater is discharged from the pipe 27, and a part branches off to the pipe 2.
8 into the final stage evaporation chamber 2n. After this seawater is mixed with concentrated brine, the brine circulation pipe 29
It flows through the condensing tube bundle 8 of the heat recovery section 4, is heated by exchanging heat with external steam in the brine heater 6, enters the first stage evaporation chamber 2a from the outlet tube 30, flows through the orifice 7, and during that time The flash evaporates. The steam generated in each evaporation chamber is condensed, flows through the produced water take-out pipe 9, and is taken out to the outside by a pump 10. The remaining concentrated brine is kept at a constant water level in the final stage evaporation chamber 2n by the liquid level control device 14, and then passed through the pipe 35.
more excreted.
製造水は上記のようにして生成し取出管９から
取出されるが、ここで製造水検出器１６から積算
演算器１９を経た信号が調節系統１８にフイード
バツクされ、この調節系統１８からの出力信号は
必要に応じて設けられる緩衝器３６を介して第１
演算器２２、第２演算器２３に入力され、第１演
算器２２からの信号は、ブラインヒータ出口管３
０のブライン温度を検出器３１により検出して加
熱蒸気調節弁３２によつて加熱蒸気量を製造水の
設定量に合うように修正する加熱蒸気量修正系統
２４に送信されると同時に、第２演算器２３から
の信号がブライン循環管路２９の循環ブライン流
量を検出器３３で検出して、調節弁３４により、
循環ブライン流量を製造水の設定値に合うよう循
環ブライン量修正系統２５に送信される。 Manufactured water is generated as described above and taken out from the take-out pipe 9. Here, the signal from the manufactured water detector 16 via the integration calculator 19 is fed back to the regulation system 18, and the output signal from this regulation system 18 is is the first via a buffer provided as necessary.
The signal is input to the computing unit 22 and the second computing unit 23, and the signal from the first computing unit 22 is sent to the brine heater outlet pipe 3.
The brine temperature of 0 is detected by the detector 31 and transmitted to the heating steam amount correction system 24 which corrects the heating steam amount by the heating steam control valve 32 to match the set amount of manufactured water. A signal from the calculator 23 detects the circulating brine flow rate in the brine circulation pipe 29 by the detector 33, and the control valve 34 detects the circulating brine flow rate in the brine circulation pipe 29.
The circulating brine flow rate is sent to the circulating brine amount correction system 25 so as to match the set value of manufactured water.
このようにしてある一定時間毎に製造水量設定
値SVと製造水積算値K2∫Xdtを比較演算し、その
比較値の差が小さくなるまで前記両修正系統２
４，２５が作動し、一致したときはそれ以降は安
定状態を保つ。このようにして外乱によつて作動
條件が変つても製造水量は常時一定量が確保でき
る。この関係を式で示せば
Ｙ＝Ｙ＋K1（SV−K2∫Xdt）
SV：製造水量設定値
Ｘ：積算演算入力
Ｙ：設定器出力
K1；K2；可変定数
となる。 In this way, the produced water amount setting value SV and the produced water integrated value K 2 ∫
4 and 25 are activated, and when they match, a stable state is maintained from then on. In this way, even if the operating conditions change due to disturbances, a constant amount of produced water can be ensured at all times. This relationship can be expressed as a formula: Y=Y+K 1 (SV-K 2 ∫Xdt) SV: Production water volume setting value X: Integration calculation input Y: Setter output K 1 ; K 2 ; Variable constant.
ここで出力Ｙが所定の値に到達後、例えば１時
間経過してから入力Ｘの積算開始、30分後に出力
Ｙを修正、さらに１時間後に入力Ｘの積算開始、
30分後に出力Ｙを修正、かかる作動とSVと
K2∫Xdtが一致するまで繰返す。 After the output Y reaches a predetermined value, for example, start integrating the input X after one hour, modify the output Y after 30 minutes, and start integrating the input X after another hour.
After 30 minutes, output Y is corrected, and this operation and SV
Repeat until K 2 ∫Xdt matches.
上記作動を更に具体的に説明すれば、例えば或
る値の製造水量を冬季の低温時に設定したと仮定
すれば、夏期では供給海水温度が上昇するため蒸
発量が減じ、設定値と製造水積算値の差は大とな
るが、積算演算器１９を介してフイードバツク信
号を受け、製造水量積算値を設定器１７の設定値
と比較演算する調節系統１８の出力信号により、
第１、第２演算器２２，２３によつて加熱蒸気調
節弁３２を開いてブラインヒータ出口管３０のブ
ライン温度を上昇させるとともに、ブライン循環
量調節弁３４を開いて流量を増加し、この両調節
によつて蒸発量は増大でき、この増大した製造水
量が調節系統１８にフイードバツクされ、ブライ
ン温度、ブライン循環量を再度調節し、かかる作
動は製造水設定値と製造水量積算値の比較値の差
が小さくなるまで自動的に作動し、一致したとき
安定した製造大量が確保できる。ただしブライン
温度はスケール防止の関係で上限値がありまたブ
ライン流量もその温度に応じた上限界があるた
め、実際上は上限値に限定する機構が必要である
ことは言うまでもない。 To explain the above operation more specifically, for example, if we assume that a certain value of produced water volume is set during low temperatures in winter, the evaporation amount will decrease in summer due to the rise in the temperature of the supplied seawater, and the set value and the total volume of produced water will decrease. Although the difference in values is large, the output signal of the regulation system 18 receives a feedback signal via the integration calculator 19 and compares and calculates the integrated value of the produced water amount with the setting value of the setting device 17.
The first and second computing units 22 and 23 open the heated steam control valve 32 to increase the brine temperature in the brine heater outlet pipe 30, and open the brine circulation amount control valve 34 to increase the flow rate. The amount of evaporation can be increased by adjustment, and this increased amount of produced water is fed back to the regulation system 18, and the brine temperature and brine circulation amount are adjusted again. It operates automatically until the difference becomes small, and when it matches, stable production volume can be ensured. However, since the brine temperature has an upper limit for scale prevention and the brine flow rate also has an upper limit depending on the temperature, it goes without saying that in practice a mechanism is required to limit the brine to the upper limit.
なおスタート時は製造水量は無いため、或る時
間までは比較演算はできないので、その間設定器
１７によつて製造水量は指定の値に設定し、製造
水量が安定したのち比較開始装置２１により比較
開始させる。 Since there is no produced water amount at the start, comparison calculations cannot be performed until a certain time. During this time, the produced water amount is set to a specified value using the setter 17, and after the produced water amount stabilizes, the comparison start device 21 performs comparison. Let it start.
第２図は他の実施例である貫流式多段フラツシ
ユ蒸発装置１′の場合であり、原料海水は給水管
２６より導入され、各蒸発室の凝縮管束８を通過
したのちブラインヒータ６で外部蒸気と熱交換し
て加熱され、出口管を経て蒸発装置に入り、順次
フフラツシユ蒸発を繰返し、製造水は取出管９か
ら取出され、濃縮ブラインは管３５から外部へ排
出される。 FIG. 2 shows the case of another embodiment of a once-through type multi-stage flash evaporator 1', in which raw seawater is introduced from a water supply pipe 26, passes through a condensing pipe bundle 8 in each evaporation chamber, and then is heated to external steam by a brine heater 6. The brine is heated by exchanging heat with the water, enters the evaporator via the outlet pipe, and undergoes repeated flash evaporation in sequence. The produced water is taken out from the take-out pipe 9, and the concentrated brine is discharged to the outside from the pipe 35.
ここで、製造水検出器１６から積算演算器１９
を経た信号が調節系統１８にフイードバツクさ
れ、この調節系統１８からの出力信号は必要に応
じて設けられる緩衝器３６を介して第１演算器２
２第２演算器２３に入力され、第１図の場合と同
様、第１演算器２２からの信号が加熱蒸気調節弁
３２を調節して加熱蒸気量を製造水の設定量と合
致するように修正する加熱蒸気量修正系統２４に
送信されると同時に、第２演算器２３からの信号
が給水入口管２６の流量を給水量検出器３３′で
検出して調節弁３４′により供給海水量を製造水
の設定値に合うように修正する給水量修正系統２
５′に送信され、製造水量設定値と製造水積算値
を比較演算し、その差が小さくなるまで作動し一
致したときは安定状態を保つ。 Here, from the manufactured water detector 16 to the integration calculator 19
The signal passed through is fed back to the adjustment system 18, and the output signal from this adjustment system 18 is sent to the first arithmetic unit 2 via a buffer 36 provided as necessary.
2 The signal from the first computing unit 22 is inputted to the second computing unit 23, and as in the case of FIG. At the same time as the signal from the second computing unit 23 is transmitted to the heating steam amount correction system 24 to be corrected, the flow rate of the water supply inlet pipe 26 is detected by the water supply amount detector 33', and the flow rate of the supplied seawater is detected by the control valve 34'. Water supply amount correction system 2 that corrects to match the set value of manufactured water
5', it compares and calculates the produced water amount setting value and the produced water integrated value, operates until the difference becomes small, and when they match, maintains a stable state.
なお製造水量積算値がフイードバツクされて製
造水量設定値とその製造水量積算値とを比較する
製造水調節系統は、第１図第２図に示したように
各々の計器を別個に設ける以外、第３図のように
積算演算器１９を調節系統１８内に内蔵させた計
器を用いてもよく、あるいは第４図のように設定
器１７、積算演算器１９を調節系統１８内に組込
んだコンパクトな計器として使用することもでき
る。 The produced water control system, which feeds back the integrated value of produced water and compares the set value of produced water with the integrated produced water, does not require separate meters as shown in Figures 1 and 2. As shown in Fig. 3, a meter in which the integration calculator 19 is built into the adjustment system 18 may be used, or as shown in Fig. 4, a compact instrument in which the setting device 17 and integration calculator 19 are built into the adjustment system 18 may be used. It can also be used as a measuring instrument.
（作用効果）
本発明においては、多段フラツシユ蒸発装置に
おいて、製造水量積算がフイードバツクされて、
製造水量設定値とその製造水量積算値とを比較演
算する製造水量調節系統と、この比較値の差が小
さくなるよう加熱蒸気量修正系統及びブライン循
環量もしくは給水量修正系統とを備えてなる多段
フラツシユ蒸発装置における製造水量自動制御装
置であるから、たとえ給水温度が潮流によつて変
動したり、また春夏秋冬にわたり季節によつて変
化し、或いは伝熱管の汚れによつて蒸発量が減少
するなどの種々な要因によつて制御系が擾乱して
も、製造水量積算値は製造水量調節系統にフイー
ドバツクされ、製造水量と積算値と設定値との差
が小さくなるように給水量及び加熱蒸気量が修正
され、製造水量が年間を通じて設定値どおりに確
保でき、先行技術のように温度ハンチングの問題
が解決してもなお設定値を変更するたびに設定器
をセツトし直すと云つた煩雑な手数は不要とな
り、製造水を飲料水として使用する場合、都市水
道の配水計画の立案が容易となるなどその効果は
大である。(Effects) In the present invention, in the multi-stage flash evaporator, the cumulative amount of produced water is fed back,
A multi-stage system comprising a produced water quantity adjustment system that compares and calculates the produced water quantity set value and its produced water quantity integrated value, a heating steam quantity correction system, and a brine circulation quantity or water supply quantity correction system so as to reduce the difference between the comparison values. Since this is an automatic control device for the amount of produced water in a flash evaporator, even if the supply water temperature fluctuates with the tide, changes depending on the season (spring, summer, fall, winter), or the amount of evaporation decreases due to dirt on the heat transfer tubes. Even if the control system is disturbed due to various factors such as Even if the amount of water produced is corrected and the amount of produced water can be maintained at the set value throughout the year, and the problem of temperature hunting as in the prior art is solved, there is still no need to reset the setting device every time the set value is changed. This eliminates the need for labor, and when using manufactured water as drinking water, the benefits are great, such as making it easier to formulate a water distribution plan for urban water supplies.
第１図第２図はそれぞれ本発明の異なる実施例
のフローシート、第３図、第４図はその要部の他
の実施例であり、第５図は従来例のフローシート
である。
１……ブライン再循環式多段フラツシユ蒸発装
置、１′……貫流式多段フラツシユ蒸発装置、２
……蒸発室、２ａ……第１段蒸発室、２ｎ……最
終段蒸発室、３……隔壁、４……熱回収部、５…
…熱放出部、６……ブラインヒータ、７……オリ
フイス、８……凝縮管束、９……製造水取出管、
１０……ポンプ、１１……真空装置、１２……液
面計、１３……調節弁、１４……液面調節装置、
１５……蒸気管、１６……製造水検出器、１７…
…設定器、１８……製造水量調節計、１９……積
算演算器、２０……フイードバツクする回路、２
１……比較開始装置、２２……第１演算器、２３
……第２演算器、２４……加熱蒸気量修正装置、
２５……ブライン循環量修正装置、２５′……給
水量修正装置、２６……給水管、２７……管、２
８……管、２９……ブライン循環管路、３０……
出口管、３１……温度検出器、３２……加熱蒸気
調節弁、３３……ブライン流量検出器、３３′…
…給水量検出器、３４，３４′……調節弁、３５
……濃縮ブライン排出管、３６……緩衝器。
FIG. 1, FIG. 2 are flow sheets of different embodiments of the present invention, FIGS. 3 and 4 are other embodiments of the essential parts thereof, and FIG. 5 is a flow sheet of a conventional example. 1... Brine recirculation type multi-stage flash evaporator, 1'... Once-through type multi-stage flash evaporator, 2
...Evaporation chamber, 2a...First stage evaporation chamber, 2n...Final stage evaporation chamber, 3...Partition wall, 4...Heat recovery section, 5...
...Heat release section, 6...Brine heater, 7...Orifice, 8...Condensing tube bundle, 9...Produced water extraction pipe,
10...Pump, 11...Vacuum device, 12...Liquid level gauge, 13...Control valve, 14...Liquid level adjustment device,
15...Steam pipe, 16...Produced water detector, 17...
... Setting device, 18 ... Produced water amount controller, 19 ... Integration calculator, 20 ... Feedback circuit, 2
1... Comparison start device, 22... First computing unit, 23
...Second computing unit, 24...Heating steam amount correction device,
25... Brine circulation amount correction device, 25'... Water supply amount correction device, 26... Water supply pipe, 27... Pipe, 2
8...Pipe, 29...Brine circulation pipe, 30...
Outlet pipe, 31...Temperature detector, 32...Heating steam control valve, 33...Brine flow rate detector, 33'...
...Water supply amount detector, 34, 34'...Control valve, 35
...Concentrated brine discharge pipe, 36...Buffer.
Claims (1)
積算値がフイードバツクされて製造水量設定値と
その製造水量積算値とを比較演算する製造水量調
節系統と、この比較値の差が小さくなるよう加熱
蒸気量修正系統及びブライン循環量もしくは給水
量修正系統とを備えてなる多段フラツシユ蒸発装
置における製造水量自動制御装置。1. In a multi-stage flash evaporator, there is a produced water quantity adjustment system that receives feedback from the produced water quantity integrated value and compares and calculates the produced water quantity set value and the produced water quantity integrated value, and a heating steam quantity correction system that reduces the difference between the comparison values. and a system for adjusting the amount of brine circulation or water supply.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15096885A JPS6211590A (en) | 1985-07-08 | 1985-07-08 | Automatic controller for controlling production of water in multi-flash evaporator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15096885A JPS6211590A (en) | 1985-07-08 | 1985-07-08 | Automatic controller for controlling production of water in multi-flash evaporator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6211590A JPS6211590A (en) | 1987-01-20 |
| JPH0557037B2 true JPH0557037B2 (en) | 1993-08-23 |
Family
ID=15508372
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP15096885A Granted JPS6211590A (en) | 1985-07-08 | 1985-07-08 | Automatic controller for controlling production of water in multi-flash evaporator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6211590A (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5641601B2 (en) * | 2010-01-27 | 2014-12-17 | 株式会社ササクラ | Ammonia recovery device and recovery method |
-
1985
- 1985-07-08 JP JP15096885A patent/JPS6211590A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6211590A (en) | 1987-01-20 |
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