JPH0142722B2 - - Google Patents
Info
- Publication number
- JPH0142722B2 JPH0142722B2 JP11225085A JP11225085A JPH0142722B2 JP H0142722 B2 JPH0142722 B2 JP H0142722B2 JP 11225085 A JP11225085 A JP 11225085A JP 11225085 A JP11225085 A JP 11225085A JP H0142722 B2 JPH0142722 B2 JP H0142722B2
- Authority
- JP
- Japan
- Prior art keywords
- heat exchanger
- tube
- steam
- liquid
- aqueous solution
- 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
Links
- 239000007788 liquid Substances 0.000 claims description 40
- 238000004140 cleaning Methods 0.000 claims description 12
- 239000007864 aqueous solution Substances 0.000 claims description 9
- 238000001704 evaporation Methods 0.000 claims description 8
- 230000008020 evaporation Effects 0.000 claims description 8
- 239000012141 concentrate Substances 0.000 claims description 7
- 238000007654 immersion Methods 0.000 claims description 4
- 239000012530 fluid Substances 0.000 claims description 2
- 238000001556 precipitation Methods 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 239000000243 solution Substances 0.000 description 5
- 239000011550 stock solution Substances 0.000 description 5
- 238000000034 method Methods 0.000 description 4
- 238000005192 partition Methods 0.000 description 4
- 239000013078 crystal Substances 0.000 description 3
- 230000003670 easy-to-clean Effects 0.000 description 3
- 238000004065 wastewater treatment Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000010409 thin film Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Landscapes
- 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〕
本発明は廃水などの水溶液を蒸気再圧縮法で濃
縮処理する水溶液の蒸発濃縮装置に関するもので
ある。DETAILED DESCRIPTION OF THE INVENTION [Industrial Application Field] The present invention relates to an aqueous solution evaporation concentration device for concentrating an aqueous solution such as waste water by a vapor recompression method.
廃水を蒸気再圧縮法で濃縮し、蒸発した水蒸気
を凝縮させて清浄水として再利用する廃水処理装
置の蒸発器は通常竪型のものが使用されている。
したがつてどうしても背丈が高くなる欠点があ
る。すなわち屋内に設置する場合、通常の建屋に
は収納できず、蒸発器に合わせて、特別に建屋を
設計しなければならず、建屋の建設費が割高とな
る。そのため、最近、背丈の低い蒸発装置に対す
る要求が多くなつてきている。蒸発器の高さを低
くするためには蒸発器のチユーブを横形とする横
形シエルアンドチユーブ式蒸発装置とする必要が
ある。すなわち、通常使用されている管外蒸発型
の「液浸型」か「薄膜式」の蒸発器が採用され
る。しかしながら、スケールが生成する場合には
この方式では掃除がし難いという欠点がある。特
に晶析まで行わなければならない場合には採用困
難である。そのため、スケールが付着し難く、且
つ、スケールを除去し易い廃水処理システムとし
ては、従来からある第２図に示すようなシステム
を採用せざるを得ない。以下第２図に基いて従来
例を説明する。
A vertical type evaporator is usually used in a wastewater treatment device that condenses wastewater using a vapor recompression method, condenses the evaporated water vapor, and reuses it as clean water.
Therefore, it has the disadvantage of being taller. That is, when installed indoors, it cannot be housed in a normal building, and the building must be specially designed to fit the evaporator, making the construction cost of the building relatively high. For this reason, there has recently been an increasing demand for evaporation apparatuses that are short in height. In order to reduce the height of the evaporator, it is necessary to use a horizontal shell-and-tube type evaporator in which the tube of the evaporator is horizontal. That is, a commonly used extra-tube evaporation type "immersion type" or "thin film type" evaporator is employed. However, if scale is generated, this method has the disadvantage that it is difficult to clean. It is difficult to employ this method, especially when crystallization must be performed. Therefore, as a wastewater treatment system in which scale is difficult to adhere to and scale can be easily removed, a conventional system as shown in FIG. 2 has to be adopted. A conventional example will be explained below based on FIG.
原液はポンプ４１，４１′により配管４２、四
方弁４３を通り、顕熱熱交換器４４に送られ４４
の管５７の外側で凝縮する蒸気で加熱され温度、
圧力ともに上昇する。そして配管４５、四方弁４
３、配管４６を通り、フラツシユタンク４７内の
減圧穴４８から、フラツシユタンク内部に吐出さ
れ、一部蒸気が発生し、該配気は配管４９から蒸
気圧力上昇装置であるブロワー５０に吸込まれ圧
縮され吐出管５１を通り、前記熱交換器４４に送
られ、原液を加熱しポンプ５２により外部に排出
される。一方フラツシユタンク４７内で蒸気の発
生により濃くなつて一部結晶の析出している濃溶
液はポンプ５３，５３′により分離機５４に送り、
分離された固形分を外部に取り出す。残りの液は
バランスタンク５５を経由しポンプ４１′により
再び配管４２側に戻す。また、熱交換器４４にお
ける液の温度上昇を少なくするため、バイパス管
５６よりフラツシユタンクからの濃溶液を配管４
２に流すようにして熱交換器４４内を通る流量を
多くするようにしている。 The stock solution is sent to a sensible heat exchanger 44 by pumps 41 and 41' through a pipe 42 and a four-way valve 43.
It is heated by the steam condensing outside the tube 57, and the temperature reaches
Both pressure increases. And piping 45, four-way valve 4
3. The air passes through the pipe 46 and is discharged into the flash tank from the depressurizing hole 48 in the flash tank 47, generating some steam, which is sucked from the pipe 49 into the blower 50, which is a steam pressure increasing device. The liquid is compressed and sent to the heat exchanger 44 through the discharge pipe 51, where the raw liquid is heated and discharged to the outside by the pump 52. On the other hand, the concentrated solution which has become thick due to the generation of steam in the flash tank 47 and in which some crystals have precipitated is sent to the separator 54 by pumps 53 and 53'.
The separated solids are taken out to the outside. The remaining liquid is returned to the piping 42 side via the balance tank 55 by the pump 41'. In addition, in order to reduce the temperature rise of the liquid in the heat exchanger 44, the concentrated solution from the flash tank is transferred to the pipe 4 through the bypass pipe 56.
2 to increase the flow rate passing through the heat exchanger 44.
このシステムにおいては熱交換器４４では被加
熱液がチユーブ内を液状で流れるので、スケール
が付き難く、掃除も簡単であり且つチユーブ自動
洗浄システムを採用しやすいという長所がある。
すなわち第２図において、四方弁の仕切りの位置
が実線の位置になつているときは、熱交換器チユ
ーブ５７内の流れは左から右側に流れるようにな
つている。そして、チユーブ内には掃除用ブラシ
５８が挿入されていてチユーブ内流れの動圧によ
り、該ブラシは同じく左から右側に流れるので、
スケール付着を防止するように作用する。ブラシ
が最右端にくると、ブラシは多数の穴のあいたチ
ユーブ保持器５９に保持される。そして一定時間
後、自動または手動にて四方弁を切り替え四方弁
の仕切りの位置を点線の位置とすることにより、
チユーブ内の被加熱液の流れ方向は反対方向とな
る。従つてチユーブ保持器５９内に保持されてい
たブラシは動圧によりチユーブ内を掃除しながら
右から左方向に流れ、チユーブ保持器６０に保持
される。この四方弁の切り替えによりチユーブ内
面のスケール付着は防止できる。 In this system, since the liquid to be heated flows through the tubes in the heat exchanger 44 in a liquid state, it has the advantage that it is difficult to build up scale, is easy to clean, and is easy to adopt an automatic tube cleaning system.
That is, in FIG. 2, when the partition of the four-way valve is at the position indicated by the solid line, the flow in the heat exchanger tube 57 flows from left to right. A cleaning brush 58 is inserted into the tube, and due to the dynamic pressure of the flow inside the tube, the brush also flows from left to right.
Acts to prevent scale adhesion. When the brush is at the rightmost end, it is held in a tube holder 59 with a number of holes. After a certain period of time, the four-way valve is automatically or manually switched and the four-way valve partition is positioned as indicated by the dotted line.
The flow direction of the heated liquid in the tube is opposite. Therefore, the brush held in the tube holder 59 flows from right to left while cleaning the inside of the tube due to the dynamic pressure, and is held in the tube holder 60. By switching this four-way valve, scale adhesion on the inner surface of the tube can be prevented.
第２図に示す従来の装置においては被加熱液は
熱交換器のチユーブの内側を流れるので、掃除も
簡単であり、且つ掃除を自動化することも容易で
ある。しかしながら、この形式の装置には次のよ
うな大きな欠点があり、実用化までは至つていな
い。すなわち、熱交換器４４を通る液の流量を多
くすると循環用ポンプ５３の所要動力が大きくな
り、流量を少なくすると熱交換器出入口における
被加熱液の温度差が大きくなる。この温度差が大
きくなると当然ブロワーの動力が大きくなる。
In the conventional device shown in FIG. 2, the liquid to be heated flows inside the tube of the heat exchanger, so cleaning is easy and cleaning can be easily automated. However, this type of device has the following major drawbacks, and has not yet been put into practical use. That is, when the flow rate of the liquid passing through the heat exchanger 44 is increased, the power required for the circulation pump 53 is increased, and when the flow rate is decreased, the temperature difference of the heated liquid at the entrance and exit of the heat exchanger becomes large. Naturally, as this temperature difference increases, the power of the blower increases.
本発明の目的は上記欠点を除去したシステム、
すなわち、
(1) 循環用ポンプ動力が少ないこと
(2) ブロワー所要動力も少ないこと
(3) スケール掃除が容易であること
(4) 背丈が低いこと
の条件を同時に満足する廃水処理等における水溶
液蒸発濃縮装置を提供することである。 The object of the present invention is to provide a system which eliminates the above-mentioned drawbacks.
In other words, it is suitable for evaporation of aqueous solutions in wastewater treatment, etc., which simultaneously satisfies the following conditions: (1) low pump power for circulation, (2) low power required for blowers, (3) easy scale cleaning, and (4) short height. An object of the present invention is to provide a concentrating device.
本発明は、上記の問題点を解決するためのもの
で、第一熱交換器２４、該第一熱交換器で発生し
た蒸気を加圧する蒸気圧力上昇装置３１、第二熱
交換器４、第二熱交換器の被加熱流体下流側に設
けたフラツシユタンク７、ポンプ及びこれらの機
器を接続する経路を備え、前記第一熱交換器２４
はチユーブ３２が被蒸発液に浸される液浸形蒸発
器であり、該チユーブ内側に前記蒸気圧力上昇装
置３１からの吐出蒸気の少なくとも一部が供給さ
れ、被蒸発液を加熱すると共に凝縮するように構
成され、前記第二熱交換器４は前記第一熱交換器
２４で濃縮された中間濃縮液の一部または全部を
チユーブ内側に通すシエルアンドチユーブ式熱交
換器であり、該チユーブ外側に前記蒸気圧力上昇
装置３１からの吐出蒸気またはボイラからの蒸気
が供給され前記中間濃縮液をさらに加熱すると共
に凝縮するように構成され、前記蒸気圧力上昇装
置３１は前記第一熱交換器２４の蒸発蒸気を吸入
し加圧する如く構成されており、かつ、前記第二
熱交換器４で加熱された中間濃縮液が、フラツシ
ユタンクで更に濃縮され、濃縮液となり系外に一
部とり出され、残りの濃縮液は濃縮液循環経路を
通り、再び第二熱交換器４に送られるように構成
されている水溶液の蒸発濃縮装置である。
The present invention is intended to solve the above problems, and includes a first heat exchanger 24, a steam pressure increasing device 31 for pressurizing the steam generated in the first heat exchanger, a second heat exchanger 4, a second heat exchanger 4, The first heat exchanger 24 is equipped with a flush tank 7 provided on the downstream side of the heated fluid of the second heat exchanger, a pump, and a path connecting these devices.
is an immersion type evaporator in which a tube 32 is immersed in the liquid to be evaporated, and at least a part of the steam discharged from the steam pressure increasing device 31 is supplied to the inside of the tube to heat and condense the liquid to be evaporated. The second heat exchanger 4 is a shell-and-tube heat exchanger that passes part or all of the intermediate concentrate concentrated in the first heat exchanger 24 to the inside of the tube, and The discharge steam from the steam pressure increasing device 31 or the steam from the boiler is supplied to further heat and condense the intermediate concentrate, and the steam pressure increasing device 31 is connected to the first heat exchanger 24 The system is configured to suck in evaporated steam and pressurize it, and the intermediate concentrated liquid heated in the second heat exchanger 4 is further concentrated in the flash tank to become a concentrated liquid and a portion is taken out of the system. This is an aqueous solution evaporation concentration device configured so that the remaining concentrated liquid passes through a concentrated liquid circulation path and is sent to the second heat exchanger 4 again.
本発明の実施例を図面に基いて説明する。 Embodiments of the present invention will be described based on the drawings.
第１図は補助蒸気を全く使用しない場合のフロ
ーシートを示すものである。原液は配管２１から
ポンプ３０により供給され、熱交換器２３で予熱
された後、蒸発器２４に供給される。蒸発器２４
は水平チユーブ内に蒸気を通すシエルアンドチユ
ーブ式液浸形の蒸発器である。原液はこの蒸発器
内で、チユーブ３２内を流れる蒸気により加熱濃
縮されて濃くなつた液（以下この液を中間濃縮液
とよぶ）は配管２５を通り、いつたんタンク２６
に蓄えられる。なお、この配管２５には流量調節
弁２７が備えられており、蒸発器内の水位が一定
水位となるよう制御されている。また配管２５に
はこの配管内を流れる液の濃度を検出する濃度検
出器２８が取りつけられていて、この部分を流れ
る液の濃度が一定値となるように調節弁２９によ
り、バイパス配管２２を流れる中間濃縮液のバイ
パス流量をコントロールするようになつている。
一方蒸発器２４内で蒸発した蒸気はブロワー３１
で圧縮されてその一部は前記蒸発器の加熱チユー
ブ３２内に供給され原液を加熱すると共に凝縮す
る。凝縮した凝縮水は熱交換器２３で冷却された
後いつたん凝縮水タンク３３に蓄えられ、ポンプ
３４により、外部に排出される。 FIG. 1 shows a flow sheet when no auxiliary steam is used. The stock solution is supplied from a pipe 21 by a pump 30, preheated by a heat exchanger 23, and then supplied to an evaporator 24. Evaporator 24
is a shell-and-tube immersion type evaporator that passes steam through a horizontal tube. The stock solution is heated and concentrated in this evaporator by the steam flowing in the tube 32, and the concentrated solution (hereinafter referred to as intermediate concentrated solution) passes through the pipe 25 and is then transferred to the tank 26.
is stored in Note that this piping 25 is equipped with a flow rate control valve 27, and the water level in the evaporator is controlled to be a constant water level. Further, a concentration detector 28 is attached to the pipe 25 to detect the concentration of the liquid flowing in this pipe, and a control valve 29 is used to control the concentration of the liquid flowing in this part so that the concentration of the liquid flowing through the bypass pipe 22 is maintained at a constant value. It is designed to control the bypass flow rate of the intermediate concentrate.
On the other hand, the steam evaporated in the evaporator 24 is transferred to the blower 31.
A portion of the compressed liquid is supplied into the heating tube 32 of the evaporator to heat the raw liquid and condense it. The condensed water is cooled by the heat exchanger 23 and then stored in the condensed water tank 33 and discharged to the outside by the pump 34.
またタンク２６に蓄えられた中間濃縮液はポン
プ１，１′により配管２、四方弁３より、顕熱熱
交換器４の管内に送られ、該管外で凝縮するブロ
ワー３１からの蒸気で加熱され、温度、圧力とも
に上昇する。そして配管５、四方弁３、配管６を
通り、フラツシユタンク７内の減圧穴８からフラ
ツシユタンク内部に吐出され、一部蒸気が発生
し、該蒸気は真空装置１２により配管１１を通り
外部に放出される。一方蒸気発生により濃縮され
一部結晶の析出している濃溶液はポンプ１３，１
３′により固液分離器１４に送られ、固形分を外
部に取り出し、残液はバランスタンク５５を経由
しポンプ１′により再び配管２側に戻される。ま
た、熱交換器４における管内液の温度上昇を少な
くするため、バイパス配管１６によりフラツシユ
タンクからの濃縮液を配管２に流すようにして熱
交換器内を通る流量を多くするようにしている。
この装置では熱交換器４において被加熱液がチユ
ーブ内を液状で流れるので、スケールが付き難
く、掃除も簡単であり且つ薬洗によらないチユー
ブ自動洗浄システムを採用しやすいという長所が
ある。すなわち第１図において、四方弁３の仕切
りの位置が実線の位置にあるときは、熱交換器の
チユーブ１７内の液の流れは左から右側に流れる
ようになつている。そして、チユーブ内には掃除
用ブラシ１８が挿入されていてチユーブ内流れの
動圧により、ブラシは同じく左から右方向にチユ
ーブ内を掃除しながら流れるので、スケール付着
を防止するように作用する。ブラシが最右端にく
ると、ブラシは多数の穴のあいたチユーブ保持器
１９に保持される。そして一定時間後、自動また
は手動にて四方弁を切り替え、四方弁の仕切りの
位置を点線の位置とすることにより、チユーブ内
の被加熱液の流れ方向は前と反対方向となる。従
つて、チユーブ保持器１９内に保持されていたブ
ラシは動圧により、チユーブ内を掃除しながら右
から左方向に流れ、チユーブ保持器２０に保持さ
れる。この四方弁の切り替えによりチユーブ内面
のスケール付着は防止できる。 In addition, the intermediate concentrated liquid stored in the tank 26 is sent to the pipe of the sensible heat exchanger 4 through the pipe 2 and the four-way valve 3 by the pumps 1 and 1', and is heated by the steam from the blower 31 that condenses outside the pipe. temperature and pressure increase. Then, it passes through the piping 5, the four-way valve 3, and the piping 6, and is discharged from the depressurizing hole 8 in the flash tank 7 into the flush tank, where some steam is generated. is released. On the other hand, the concentrated solution that has been concentrated by steam generation and has some crystals precipitated is pumped by pumps 13 and 1.
3' to the solid-liquid separator 14, the solid content is taken out, and the remaining liquid is returned to the piping 2 side via the balance tank 55 by the pump 1'. Furthermore, in order to reduce the temperature rise of the liquid in the pipes in the heat exchanger 4, the concentrated liquid from the flash tank is made to flow into the pipe 2 by the bypass pipe 16, thereby increasing the flow rate through the heat exchanger. .
In this device, since the liquid to be heated flows in the tube in the heat exchanger 4 in a liquid state, it has the advantage that it is difficult to build up scale, is easy to clean, and is easy to adopt an automatic tube cleaning system that does not require chemical washing. That is, in FIG. 1, when the partition of the four-way valve 3 is at the position indicated by the solid line, the liquid in the tube 17 of the heat exchanger flows from left to right. A cleaning brush 18 is inserted into the tube, and due to the dynamic pressure of the flow inside the tube, the brush flows from left to right while cleaning the inside of the tube, thereby acting to prevent scale adhesion. When the brush is at the rightmost end, it is held in a tube holder 19 with a number of holes. After a certain period of time, the four-way valve is automatically or manually switched and the partition of the four-way valve is set to the position indicated by the dotted line, so that the flow direction of the heated liquid in the tube becomes opposite to the previous direction. Therefore, the brush held in the tube holder 19 flows from right to left while cleaning the inside of the tube due to the dynamic pressure, and is held in the tube holder 20. By switching this four-way valve, scale adhesion on the inner surface of the tube can be prevented.
また熱交換器４に供給される蒸気は前記ブロワ
ー３１の吐出管から一部分岐して供給されるよう
になつている。 Further, the steam supplied to the heat exchanger 4 is partially branched from the discharge pipe of the blower 31 and supplied.
ただし、第一の熱交換器すなわち蒸発器２４で
濃縮される濃度は、通常結晶の生じない濃度にコ
ントロールされているが、原液の種類によつては
この濃度が薄い場合がある。このような場合はブ
ロワー３１からの蒸気だけでは足りない場合があ
るがこの場合は外部のボイラからの蒸気を供給す
ればよい。 However, the concentration concentrated in the first heat exchanger, that is, the evaporator 24, is normally controlled to a concentration that does not generate crystals, but depending on the type of stock solution, this concentration may be low. In such a case, steam from the blower 31 alone may not be sufficient, but in this case steam from an external boiler may be supplied.
本発明の装置は前述の構成となつているので、
下記のような優れた効果が生ずる。
Since the device of the present invention has the above-mentioned configuration,
The following excellent effects are produced.
(1) 大部分の濃縮は第一熱交換器で行われるの
で、第二熱交換器における交換熱量は少なく、
従つて中間濃縮液の流量すなわち循環ポンプ１
３の動力は少なくてすむ。（ポンプ１を流れる
中間濃縮液の流量は原液の５％程度の場合が多
い。）
(2) また同様の理由により、第二熱交換器４に供
給すべき蒸気量は少ないので、通常の廃水処理
システムでは、補助蒸気が不要であり、かつ、
ブロワー３１の所要ヘツドが少ないので所要動
力も少なくてよい。(1) Most of the concentration is done in the first heat exchanger, so the amount of heat exchanged in the second heat exchanger is small;
Therefore, the flow rate of the intermediate concentrate, that is, the circulation pump 1
3 requires less power. (The flow rate of the intermediate concentrated liquid flowing through the pump 1 is often about 5% of the raw liquid.) (2) Also, for the same reason, the amount of steam to be supplied to the second heat exchanger 4 is small, The treatment system does not require auxiliary steam, and
Since the blower 31 requires less head, less power is required.
(3) スケールの生じやすい第二熱交換器はチユー
ブ内が水溶液側なので掃除し易く、且つスケー
ル除去のため、熱交換器チユーブ内流速を利用
した自動洗浄システムを容易に採用することが
できる。(3) The second heat exchanger, which is prone to scale, is easy to clean because the inside of the tube is on the aqueous solution side, and an automatic cleaning system that utilizes the flow rate inside the heat exchanger tube can be easily adopted to remove scale.
(4) 熱交換器の背の高さを低くすることができ
る。(4) The height of the heat exchanger can be reduced.
第１図は本発明の装置の一実施例のフロー図、
第２図は従来例を説明するためのフロー図であ
る。
３……四方弁、４……第二熱交換器、７……フ
ラツシユタンク、１４……固液分離器、１７……
チユーブ、１８……ブラシ、２１……原液導入
管、２３……熱交換器、２４……蒸発器、３１…
…ブロワー、２６……中間濃縮液タンク。
FIG. 1 is a flow diagram of an embodiment of the apparatus of the present invention;
FIG. 2 is a flow diagram for explaining a conventional example. 3... Four-way valve, 4... Second heat exchanger, 7... Flash tank, 14... Solid-liquid separator, 17...
Tube, 18... Brush, 21... Stock solution introduction tube, 23... Heat exchanger, 24... Evaporator, 31...
...Blower, 26...Intermediate concentrate tank.
Claims (1)
た蒸気を加圧する蒸気圧力上昇装置３１、第二熱
交換器４、第二熱交換器の被加熱流体下流側に設
けたフラツシユタンク７、ポンプ及びこれらの機
器を接続する経路を備え、前記第一熱交換器２４
はチユーブが被蒸発液に浸される液浸形蒸発器で
あり、該チユーブ内側に前記蒸気圧力上昇装置３
１からの吐出蒸気の少なくとも一部が供給され、
被蒸発液を加熱すると共に凝縮するように構成さ
れ、前記第二熱交換器４は前記第一熱交換器２４
で濃縮された中間濃縮液の一部または全部をチユ
ーブ内側に通すシエルアンドチユーブ式熱交換器
であり、該チユーブ外側に前記蒸気圧力上昇装置
３１からの吐出蒸気またはボイラからの蒸気が供
給され前記中間濃縮液をさらに加熱すると共に凝
縮するように構成され、前記蒸気圧力上昇装置３
１は前記第一熱交換器２４の蒸発蒸気を吸入し加
圧する如く構成されており、かつ、前記第二熱交
換器４で加熱された中間濃縮液が、フラツシユタ
ンク７で更に濃縮されて濃縮液となり、系外に一
部とり出され、残りの濃縮液は濃縮液循環経路を
通り、再び第二熱交換器４に送られるように構成
されている水溶液の蒸発濃縮装置。 ２ 前記第２熱交換器がチユーブ内流速を利用し
た洗浄装置により洗浄可能となつている特許請求
の範囲第１項記載の水溶液の蒸発濃縮装置。 ３ 前記中間濃縮液が、溶質の析出濃度以下の濃
度に制御されている前記特許請求の範囲第１項ま
たは第２項記載の水溶液の蒸発濃縮装置。[Claims] 1. A first heat exchanger 24, a steam pressure increasing device 31 that pressurizes the steam generated in the first heat exchanger, a second heat exchanger 4, and a heated fluid downstream of the second heat exchanger. The first heat exchanger 24 is equipped with a flush tank 7 provided on the side, a pump, and a path for connecting these devices.
is an immersion type evaporator in which a tube is immersed in the liquid to be evaporated, and the vapor pressure increasing device 3 is installed inside the tube.
at least a portion of the discharged steam from 1 is supplied;
The second heat exchanger 4 is configured to heat and condense the liquid to be evaporated, and the second heat exchanger 4 is connected to the first heat exchanger 24.
This is a shell-and-tube heat exchanger that passes part or all of the intermediate concentrated liquid through the inside of the tube, and the discharged steam from the steam pressure increasing device 31 or the steam from the boiler is supplied to the outside of the tube. The vapor pressure increasing device 3 is configured to further heat and condense the intermediate concentrate;
1 is configured to suck in and pressurize the evaporated vapor from the first heat exchanger 24, and the intermediate concentrated liquid heated in the second heat exchanger 4 is further concentrated in the flash tank 7. The aqueous solution evaporation concentration device is configured so that a part of the aqueous solution becomes a concentrated liquid and is taken out of the system, and the remaining concentrated liquid passes through a concentrated liquid circulation path and is sent to the second heat exchanger 4 again. 2. The aqueous solution evaporation concentration device according to claim 1, wherein the second heat exchanger can be cleaned by a cleaning device that utilizes the flow velocity within the tube. 3. The aqueous solution evaporation concentration device according to claim 1 or 2, wherein the intermediate concentrate is controlled to a concentration lower than the solute precipitation concentration.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11225085A JPS61271002A (en) | 1985-05-27 | 1985-05-27 | Device for evaporating and concentrating aqueous solution |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11225085A JPS61271002A (en) | 1985-05-27 | 1985-05-27 | Device for evaporating and concentrating aqueous solution |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS61271002A JPS61271002A (en) | 1986-12-01 |
| JPH0142722B2 true JPH0142722B2 (en) | 1989-09-14 |
Family
ID=14582002
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP11225085A Granted JPS61271002A (en) | 1985-05-27 | 1985-05-27 | Device for evaporating and concentrating aqueous solution |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS61271002A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2021159783A (en) * | 2020-03-30 | 2021-10-11 | 大阪瓦斯株式会社 | Waste liquid treatment device |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2006255503A (en) * | 2005-03-15 | 2006-09-28 | Tlv Co Ltd | Heating/cooling apparatus |
| CN104368162B (en) * | 2014-11-05 | 2016-01-20 | 象山医疗精密仪器有限公司 | Steam compression type is concentrated, solvent recovery all-in-one |
| CN104368163A (en) * | 2014-11-05 | 2015-02-25 | 象山医疗精密仪器有限公司 | Liquid medicine concentration and solvent recovery process |
-
1985
- 1985-05-27 JP JP11225085A patent/JPS61271002A/en active Granted
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2021159783A (en) * | 2020-03-30 | 2021-10-11 | 大阪瓦斯株式会社 | Waste liquid treatment device |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS61271002A (en) | 1986-12-01 |
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