JPH0134084B2 - - Google Patents
Info
- Publication number
- JPH0134084B2 JPH0134084B2 JP12056185A JP12056185A JPH0134084B2 JP H0134084 B2 JPH0134084 B2 JP H0134084B2 JP 12056185 A JP12056185 A JP 12056185A JP 12056185 A JP12056185 A JP 12056185A JP H0134084 B2 JPH0134084 B2 JP H0134084B2
- Authority
- JP
- Japan
- Prior art keywords
- evaporator
- steam
- heating
- turbine
- pressure
- 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
- 238000010438 heat treatment Methods 0.000 claims description 27
- 238000009835 boiling Methods 0.000 claims description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 8
- 238000001704 evaporation Methods 0.000 description 8
- 230000008020 evaporation Effects 0.000 description 6
- 239000007788 liquid Substances 0.000 description 6
- 238000000034 method Methods 0.000 description 4
- 235000011121 sodium hydroxide Nutrition 0.000 description 3
- 239000011550 stock solution Substances 0.000 description 3
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000012086 standard solution Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002351 wastewater Substances 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
本発明は蒸発濃縮装置に関し、詳しくは硫酸、
苛性ソーダのように沸点上昇の高い水溶液の蒸発
濃縮に適するようにした蒸発装置内のスチームの
利用手段に関するものであつて、装置操業のエネ
ルギー節減に資するものである。DETAILED DESCRIPTION OF THE INVENTION Field of Industrial Application The present invention relates to an evaporative concentrator, in particular sulfuric acid,
The present invention relates to a means for utilizing steam in an evaporator that is suitable for evaporating and concentrating an aqueous solution with a high boiling point such as caustic soda, and contributes to energy savings in operating the apparatus.
従来の技術
従来から硫酸、苛性ソーダ等を蒸発濃縮するに
当たつては、それら濃縮液の沸点上昇が高いため
単効用あるいは２重、３重効用蒸発装置が用いら
れて来た。そのような装置においては、１効用加
熱缶の加熱源として、0.5〜5.0Kg／cm2Ｇの比較的
低圧のスチームを使用する必要があり、通常はこ
の加熱用のスチームを得るために６〜14Kg／cm2Ｇ
の中圧のスチームを減圧して使用して来た。この
ことはとりもなおさずスチームの持つエネルギー
に関する限りエンタルピーの労費であつてこの圧
力の落差について調和をはかることは行われてい
なかつた。BACKGROUND ART Conventionally, single-effect, double-effect, or triple-effect evaporators have been used to evaporate and concentrate sulfuric acid, caustic soda, etc., since the boiling point of these concentrates is high. In such equipment, it is necessary to use relatively low-pressure steam of 0.5 to 5.0 Kg/cm 2 G as the heating source for the single-effect heating can, and usually 6 to 5 kg/cm 2 G of steam is required to obtain this heating steam. 14Kg/ cm2G
I have been using reduced pressure steam at medium pressure. As far as the energy of steam is concerned, this is an enthalpy labor cost, and no effort has been made to balance this pressure difference.
一方、スチームの持つエンタルピーを有効に利
用し、化学プラント内の省エネルギーをはかるこ
とについては本出願人の出願にかかる「蒸発濃縮
法」（特願昭59−151168号）の発明があり、その
要旨は機械圧縮式蒸発濃縮法において機械圧縮機
の駆動機に蒸発タービンの補機を併設し、これに
供給したスチームの排気を他の工程に供給して低
圧スチームによる加熱、駆動源とするものであつ
た。この発明が対象とするスチームは２−４Kg／
cm2Ｇのスチームをさらに低圧の２Kg／cm2Ｇ以下ま
たは１〜２Kg／cm2Ｇのスチームに減圧するもので
ある。 On the other hand, regarding the effective use of the enthalpy of steam to save energy in chemical plants, there is an invention of the "evaporation concentration method" (Japanese Patent Application No. 151168/1982) filed by the present applicant. In the mechanical compression evaporation concentration method, an auxiliary equipment for the evaporation turbine is attached to the drive machine of the mechanical compressor, and the exhaust steam supplied to this is supplied to other processes to use the low-pressure steam as a heating and driving source. It was hot. The steam targeted by this invention is 2-4 kg/
The steam pressure of cm 2 G is further reduced to a lower pressure of 2 kg/cm 2 G or less or 1 to 2 kg/cm 2 G.
発明が解決しようとする問題点
上記したような蒸発装置において蒸発器には各
種の型式のものが採用できるが、その加熱缶への
加熱源として供給されるスチームにあつては、そ
の目的に沿うものとして２〜４Kg／cm2Ｇのものを
必要とする。このスームは直接供給源があれば問
題はないが、先願発明のようにして得るとすれば
さらに前段ともいうべき蒸気条件によらねばなら
ず、この点に着目して開示はなされておらず、中
圧のスチームを無為に減圧する欠点は残されたま
まである。Problems to be Solved by the Invention Various types of evaporators can be used in the evaporator as described above, but the steam supplied as a heating source to the heating can must be selected according to its purpose. A material with a weight of 2 to 4 kg/cm 2 G is required. There is no problem with this steam if there is a direct supply source, but if it were to be obtained as in the prior invention, it would have to be based on the steam conditions that can be called the first step, and there is no disclosure focusing on this point. However, the disadvantage of unnecessarily reducing the pressure of medium-pressure steam remains.
問題点を解決するための手段
本発明は中圧スチームを減圧し、加熱スチーム
として使用している蒸発装置において、スチーム
の持つエンタルピーを有効に利用し、蒸発装置の
省エネルギーをはかることを目的とするものであ
つて、蒸発器における処理対象液の循環ポンプの
駆動機に蒸気タービンを採用し、これに中圧スチ
ームを供給して駆動するとともに、その排気スチ
ームを蒸発装置内の構成要素系で活用することを
要旨とし、蒸発装置内の蒸発器の加熱缶、熱圧縮
機、またはそれらの組合わせに供給するように構
成した蒸発装置を特徴とするものである。Means for Solving the Problems The present invention aims to reduce the pressure of medium-pressure steam and effectively utilize the enthalpy of the steam in an evaporator that is used as heating steam, thereby saving energy in the evaporator. A steam turbine is used as the drive device for the circulation pump for the liquid to be treated in the evaporator, and medium-pressure steam is supplied to drive the pump, and the exhaust steam is utilized in the component system within the evaporator. The invention features an evaporator configured to feed an evaporator heating can, a thermal compressor, or a combination thereof within the evaporator.
実施例
以下に本発明の蒸発装置をフロー図で示す実施
例によつて詳細に説明する。EXAMPLES The evaporator of the present invention will be explained in detail below using examples shown in flowcharts.
第１図において、１０は蒸発器であつて、気液
分離室に構成された蒸発缶２０と熱交換器として
構成された加熱缶３０とからなり、蒸発缶２０と
加熱缶３０とは強制循環ポンプ４０を有する管路
によつて接続され循環管路Ｃを構成している。循
環管路Ｃには濃縮処理をすべき硫酸または苛性ソ
ーダ等の処理原点Ａの注入管が接続され、ポンプ
４０から加熱缶３０の底部３１、頂部３２と蒸発
缶の下部２１、その底部２２とポンプ４０が配管
接続されている。加熱缶３０は熱交換部３３を有
し、循環する原液を加熱し、繰返し循環したのち
蒸発缶底部２３から回収液Ｐとして取出され、一
方、蒸発器２０の上部２４から真空発生装置５０
に接続する管は冷却水Ｗを供給される凝縮器５１
を有して蒸発器１０は全体として公知の構成とな
つている。以下においては管路とそこを通過する
流体とは同一符号で示すこととする。 In FIG. 1, 10 is an evaporator, which consists of an evaporator 20 configured as a gas-liquid separation chamber and a heating can 30 configured as a heat exchanger. A circulation pipe C is configured by being connected by a pipe having a pump 40. The circulation pipe C is connected to the injection pipe of the processing origin A for sulfuric acid, caustic soda, etc. to be concentrated, and from the pump 40 to the bottom 31 and top 32 of the heating can 30, to the lower part 21 of the evaporating can, to the bottom 22 and the pump. 40 is connected by piping. The heating can 30 has a heat exchange section 33, which heats the circulating stock solution, and after repeated circulation, it is taken out as a recovered liquid P from the bottom 23 of the evaporator 20, while a vacuum generator 50 is removed from the top 24 of the evaporator 20.
The pipe connected to the condenser 51 is supplied with cooling water W.
The evaporator 10 has a generally known construction. In the following, the pipe line and the fluid passing therethrough will be indicated by the same reference numerals.
本発明の蒸発装置は上記の循環ポンプ４０の駆
動機として中圧スチームで駆動されるタービン４
１を設置してあり、タービン４１には中圧のスチ
ームＳが供給されて回転し連結結合したポンプ４
０を駆動する。タービン４１を駆動したタービン
排気は管４２によつて熱交換器３３の上部３４に
導かれ、前記循環液Ｃと熱交換しドレンは下部３
５から排出される。 The evaporator of the present invention has a turbine 4 driven by intermediate pressure steam as a driving machine for the above-mentioned circulation pump 40.
1 is installed, and a pump 4 connected to the turbine 41 is supplied with intermediate pressure steam S and rotates.
Drive 0. The turbine exhaust gas that has driven the turbine 41 is led to the upper part 34 of the heat exchanger 33 through a pipe 42, where it exchanges heat with the circulating fluid C, and the drain is sent to the lower part 34.
It is discharged from 5.
次に第２図に示す第２の実施態様について説明
する。第２図は自己蒸気圧縮式の蒸発装置の例を
フロー図で示し、熱圧縮機６０を有している。熱
圧縮機６０はスチーム・エジエクターとして構成
され、蒸発缶２０から発生する蒸気の一部を、駆
動系として供給される蒸気S1によつて昇温・昇圧
したのち加熱源として加熱缶３０に戻す方式とし
て知られている。本発明ではこの熱圧縮機の駆動
源S1（点線図示）に代えてタービン４１の排気を
使用する。即ちタービン排気は管４３によつて熱
圧縮機６０に導かれ、蒸発缶２０の頂部６１から
の蒸発蒸気を昇温、昇圧させ、加熱缶３０の熱交
換器３３の上部６２に供給する。なお、蒸発缶２
０、加熱缶３０、その両者間の循環管路Ｃ及び管
路Ｃの循環ポンプ４０からなる蒸発装置１０の構
成は前例と同様である。 Next, a second embodiment shown in FIG. 2 will be described. FIG. 2 shows a flow diagram of an example of a self-vapor compression type evaporator, which includes a thermal compressor 60. The thermal compressor 60 is configured as a steam effluent, and after raising the temperature and pressure of a portion of the steam generated from the evaporator 20 by the steam S1 supplied as a drive system, it is returned to the heating can 30 as a heating source. known as the method. In the present invention, the exhaust gas of the turbine 41 is used in place of the drive source S 1 (shown in dotted line) for the thermal compressor. That is, the turbine exhaust gas is led to the thermal compressor 60 by the pipe 43, and the evaporated steam from the top 61 of the evaporator 20 is raised in temperature and pressure, and is supplied to the upper part 62 of the heat exchanger 33 of the heating can 30. In addition, evaporator 2
The configuration of the evaporator 10 is the same as that of the previous example, and includes a heating can 30, a circulation pipe C between the two, and a circulation pump 40 for the pipe C.
上記の２例におけるタービン排気の活用は蒸発
装置の構成と操業条件の範囲において組合わせて
採用することができる。 The utilization of the turbine exhaust gas in the above two examples can be combined and adopted depending on the configuration of the evaporator and the range of operating conditions.
作 用
上記のように構成された蒸発装置の運転につい
て述べ本発明の作用を説明する。Operation The operation of the evaporator configured as described above will be described to explain the operation of the present invention.
硫酸などの原液Ａは循環管路Ｃに流入させら
れ、循環ポンプ４０を駆動源として循環させら
れ、その間に加熱缶３０の熱交換器３３中で加熱
され一部は蒸発してその頂部３２から蒸発缶２０
に送られる。蒸発缶２０の気密分離室内では濃縮
されつつある原液は循環管路Ｃの循環を繰返して
順次濃縮されるとともに溶液中の水は室上部２４
から真空発生装置５０に引かれてフラツシユ蒸発
し、蒸発缶２０の頂部２４から凝縮器５１に至つ
て冷却されて排水となる。 A stock solution A such as sulfuric acid is made to flow into the circulation pipe C and is circulated using the circulation pump 40 as a driving source. During this time, it is heated in the heat exchanger 33 of the heating can 30, and a part of it evaporates and is discharged from the top 32. Evaporator 20
sent to. The stock solution that is being concentrated in the airtight separation chamber of the evaporator 20 is successively concentrated by repeating the circulation through the circulation pipe C, and the water in the solution is transferred to the upper part 24 of the chamber.
The water is drawn into the vacuum generator 50 and evaporated into flash, and then flows from the top 24 of the evaporator 20 to the condenser 51 where it is cooled and becomes waste water.
以上の蒸発濃度は繰返し循環によつて順次濃縮
され、随時蒸発缶底部２３から回収液Ｐとして取
出されるから公知の蒸発濃縮が行われる。 The above evaporation concentration is sequentially concentrated through repeated circulation, and is taken out from the bottom 23 of the evaporator as a recovered liquid P at any time, so that known evaporation concentration is performed.
本発明の装置では循環ポンプ４０の駆動機とし
て採用された蒸気タービン４１に特徴がある。即
ちタービンを駆動するスチームＳは６〜14Kg／cm2
Ｇの中圧のものを用い、このエネルギーは循環ポ
ンプ４０に結合されたタービン４１を十分に駆動
したのち、その排気が加熱缶３０の熱交換器３３
に加熱源として送られ処理液を熱交換によつて昇
温させている。これによつて供給スチームＳは単
なる減圧操作を加えるのではなく、駆動エネルギ
ーとしてスチームの持つエンタルピーを有効に利
用してのち、加熱缶３０への適圧である２〜４
Kg／cm2Ｇのスチームとして供給している。 The apparatus of the present invention is characterized by the steam turbine 41 employed as a driving machine for the circulation pump 40. In other words, the steam S that drives the turbine is 6 to 14 kg/cm 2
This energy sufficiently drives the turbine 41 connected to the circulation pump 40, and then the exhaust gas is sent to the heat exchanger 33 of the heating can 30.
The processing liquid is sent as a heating source and heated through heat exchange. As a result, the supplied steam S is not simply subjected to a pressure reduction operation, but after effectively utilizing the enthalpy of the steam as driving energy, the supply steam S is supplied to the heating can 30 at an appropriate pressure of 2 to 4.
It is supplied as steam of Kg/cm 2 G.
次に本発明の第２の態様では、タービン排気４
３は熱圧縮機６０を有する形式の蒸発装置におい
てスチーム・エジエクタの駆動源として供給さ
れ、２〜４Kg／cm2Ｇの低圧スチームは適圧として
働く。 Next, in a second aspect of the present invention, the turbine exhaust 4
3 is supplied as a driving source for a steam ejector in an evaporator having a heat compressor 60, and low-pressure steam of 2 to 4 kg/cm 2 G acts as an appropriate pressure.
発明の効果
本発明は上述のように構成されているので、蒸
発装置の蒸発器に設けられる循環ポンプの駆動機
として中圧用のタービンを採用することによつ
て、中圧スチームをそのまま利用することがで
き、装置内の加熱源、駆動源で要求される低圧ス
チームがタービン排気として得られるからエネル
ギー源の中圧スチームの減圧操作が極めて合理的
に行われ、省エネルギーの効果はまことに顕著で
あり、業界にもたらす寄与が極めて大きいもので
ある。Effects of the Invention Since the present invention is configured as described above, by employing an intermediate pressure turbine as a driving machine for the circulation pump provided in the evaporator of the evaporator, intermediate pressure steam can be used as is. Since the low-pressure steam required by the heating source and drive source in the equipment can be obtained as turbine exhaust, the depressurization of the medium-pressure steam as an energy source can be carried out extremely rationally, and the energy saving effect is truly remarkable. The contribution it makes to the industry is extremely large.
図面は本発明の蒸発装置をフロー図で示すもの
であつて第１図は低圧スチームを加熱源として使
用する実施例、第２図は低圧スチームを駆動源と
して使用する第２の実施例である。
１０……蒸発器、２０……蒸発缶、３０……加
熱缶、３３……熱交換器、４０……循環ポンプ、
４１……中圧タービン、４２，４３……タービン
排気管路、タービン排気、６０……熱圧縮機、Ａ
……処理対象原液、Ｐ……回収液、Ｓ……中圧ス
チーム、S1……低圧スチーム。
The drawings are flowcharts showing the evaporation apparatus of the present invention, in which Fig. 1 shows an embodiment in which low pressure steam is used as a heating source, and Fig. 2 shows a second embodiment in which low pressure steam is used as a driving source. . 10... Evaporator, 20... Evaporator, 30... Heating can, 33... Heat exchanger, 40... Circulation pump,
41... Intermediate pressure turbine, 42, 43... Turbine exhaust pipe, turbine exhaust, 60... Heat compressor, A
...Standard solution to be treated, P...Recovered liquid, S...Medium pressure steam, S1 ...Low pressure steam.
Claims (1)
る蒸発器によつて濃縮するように構成した蒸発装
置であつて、蒸発器の蒸発缶と加熱缶との間に循
環管路を形成したものにおいて、 循環用のポンプの駆動機として蒸気タービンを
連動させて設置し、そのタービンを中圧スチーム
の供給源に接続するとともに、タービン排気を蒸
発装置の加熱系または／及び駆動系に接続してな
ることを特徴とする蒸発装置。 ２ 加熱系は蒸発器の加熱缶である特許請求の範
囲第１項に記載の蒸発装置。 ３ 駆動系は蒸発装置を構成する熱圧縮機である
特許請求の範囲第１項に記載の蒸発装置。[Scope of Claims] 1. An evaporator configured to condense a solution with a high boiling point increase using an evaporator using low-pressure steam as a heating source, the evaporator having a structure in which a solution is circulated between an evaporator and a heating can of the evaporator. In the case where a pipe is formed, a steam turbine is installed in conjunction with the driving machine for the circulation pump, and the turbine is connected to a medium pressure steam supply source, and the turbine exhaust is sent to the heating system of the evaporator or/and An evaporator characterized by being connected to a drive system. 2. The evaporator according to claim 1, wherein the heating system is a heating can of an evaporator. 3. The evaporator according to claim 1, wherein the drive system is a thermal compressor that constitutes the evaporator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP12056185A JPS61283302A (en) | 1985-06-05 | 1985-06-05 | Evaporating apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP12056185A JPS61283302A (en) | 1985-06-05 | 1985-06-05 | Evaporating apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS61283302A JPS61283302A (en) | 1986-12-13 |
| JPH0134084B2 true JPH0134084B2 (en) | 1989-07-18 |
Family
ID=14789354
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP12056185A Granted JPS61283302A (en) | 1985-06-05 | 1985-06-05 | Evaporating apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS61283302A (en) |
-
1985
- 1985-06-05 JP JP12056185A patent/JPS61283302A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS61283302A (en) | 1986-12-13 |
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