JPS6359756B2 - - Google Patents
Info
- Publication number
- JPS6359756B2 JPS6359756B2 JP13248083A JP13248083A JPS6359756B2 JP S6359756 B2 JPS6359756 B2 JP S6359756B2 JP 13248083 A JP13248083 A JP 13248083A JP 13248083 A JP13248083 A JP 13248083A JP S6359756 B2 JPS6359756 B2 JP S6359756B2
- Authority
- JP
- Japan
- Prior art keywords
- water
- distilled water
- carbon dioxide
- dioxide gas
- post
- 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
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 93
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 90
- 238000001704 evaporation Methods 0.000 claims description 52
- 239000001569 carbon dioxide Substances 0.000 claims description 45
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 45
- 239000012153 distilled water Substances 0.000 claims description 37
- 238000010612 desalination reaction Methods 0.000 claims description 34
- 150000003839 salts Chemical class 0.000 claims description 26
- 238000000034 method Methods 0.000 claims description 13
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 6
- 239000011575 calcium Substances 0.000 claims description 6
- 229910052791 calcium Inorganic materials 0.000 claims description 6
- 239000007800 oxidant agent Substances 0.000 claims description 5
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 4
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 3
- 239000000460 chlorine Substances 0.000 claims description 3
- 229910052801 chlorine Inorganic materials 0.000 claims description 3
- 238000007789 sealing Methods 0.000 claims description 2
- 239000007789 gas Substances 0.000 description 49
- 230000008020 evaporation Effects 0.000 description 34
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 14
- 239000012267 brine Substances 0.000 description 14
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 14
- 230000000694 effects Effects 0.000 description 10
- 229910000019 calcium carbonate Inorganic materials 0.000 description 7
- 238000002347 injection Methods 0.000 description 7
- 239000007924 injection Substances 0.000 description 7
- 239000002455 scale inhibitor Substances 0.000 description 7
- 238000006114 decarboxylation reaction Methods 0.000 description 5
- OAKJQQAXSVQMHS-UHFFFAOYSA-N Hydrazine Chemical compound NN OAKJQQAXSVQMHS-UHFFFAOYSA-N 0.000 description 4
- 239000013505 freshwater Substances 0.000 description 4
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 3
- 239000000920 calcium hydroxide Substances 0.000 description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 3
- 235000011116 calcium hydroxide Nutrition 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000000740 bleeding effect Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000001784 detoxification Methods 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 235000020188 drinking water Nutrition 0.000 description 1
- 239000000796 flavoring agent Substances 0.000 description 1
- 235000019634 flavors Nutrition 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 230000009931 harmful effect Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 235000010755 mineral Nutrition 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
Description
【発明の詳細な説明】
本発明は、蒸発法による塩水淡水化装置で得ら
れた蒸溜水を、水道水に適した水質に転換するた
めの、後処理方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a post-treatment method for converting distilled water obtained in a desalination apparatus using an evaporation method to a water quality suitable for tap water.
塩水から蒸発法によつて得られた蒸溜水は、ミ
ネラル成分を殆ど含んでいないことから、以後の
給水系統の配管材料を腐食させ、また、飲料水と
しては味覚に乏しいのであつた。このため、塩水
から蒸発法によつて製造された蒸溜水には、炭酸
カルシウムや消石灰と、炭酸ガスとを添加する方
法が採用されている。そして、この場合の炭酸ガ
スとしては、石油や燃料ガスを燃焼させて製造し
た炭酸ガスを用いていたが、炭酸ガスの製造に多
大の設備と運転経費とが必要である欠点があつ
た。 Distilled water obtained from salt water by evaporation contains almost no minerals, corrodes piping materials in water supply systems, and has a poor taste as drinking water. For this reason, a method is adopted in which calcium carbonate, slaked lime, and carbon dioxide gas are added to distilled water produced from salt water by the evaporation method. In this case, carbon dioxide gas produced by burning petroleum or fuel gas was used, but it had the disadvantage that a large amount of equipment and operating costs were required to produce carbon dioxide gas.
そこで、先行技術としての特開昭55−35971号
公報は、塩水から蒸発法の淡水化装置によつて蒸
溜水を製造するに際して、この蒸発法の淡水化装
置における腐食、スケール生成の防止の目的のた
めに、淡水化装置に供給する以前の塩水に塩酸又
は硫酸等の酸を添加した場合に炭酸ガスが発生す
ることを利用し、酸を添加した塩水を淡水化装置
に供給する前に、脱炭酸塔に導きここで減圧下で
炭酸ガスを発生させ、これをボイラーからの高圧
蒸気で作動する抽気エゼクターで抽気し、凝縮器
で先の高圧蒸気の水分を凝縮除去したのち、前記
淡水化装置からの蒸溜水に混合することを提案し
ている。 Therefore, Japanese Patent Application Laid-open No. 55-35971 as a prior art aims to prevent corrosion and scale formation in the evaporation method desalination equipment when producing distilled water from salt water using the evaporation method desalination equipment. To do this, we take advantage of the fact that carbon dioxide gas is generated when an acid such as hydrochloric acid or sulfuric acid is added to the salt water before it is supplied to the desalination equipment. The carbon dioxide gas is generated under reduced pressure in the decarboxylation tower, which is extracted by a bleed ejector operated by high pressure steam from a boiler, and the water in the high pressure steam is condensed and removed by a condenser. It is suggested that it be mixed with distilled water from the device.
このようにすれば、炭酸ガスを別の工程で製造
しないため運転経費がそれだけ安価になり、且つ
前記従来法に比べて設備を小型化できるが、この
方法に於いて十分な量の炭酸ガスを得るには、そ
の明細書に記載してあるように脱炭酸塔内を前記
エゼクターにて0.2気圧、つまり−600mmHg程度
の高真空にしなければならないから、その抽気エ
ゼクターの駆動に要する高圧蒸気の消費量が多く
なることに加えて、この抽気に用いた蒸気の凝縮
に多量の冷却水を必要として、運転経費が嵩むの
であり、しかも、抽気エゼクターが大型になると
共に、これに対する配管も相当太くしなければな
らないから、設備の小型化が十分に達成できず、
且つ、脱炭酸塔を密閉型にしなければならないの
で、設備費用が嵩むのであつた。 In this way, since carbon dioxide gas is not produced in a separate process, operating costs can be reduced accordingly, and the equipment can be made smaller compared to the conventional method, but in this method, a sufficient amount of carbon dioxide gas cannot be As stated in the specification, the inside of the decarboxylation tower must be brought to a high vacuum of 0.2 atmospheres, that is, approximately -600 mmHg, using the ejector, so the high pressure steam required to drive the extraction ejector is consumed. In addition to the increased volume, a large amount of cooling water is required to condense the steam used for this bleed air, which increases operating costs.Furthermore, the bleed ejector becomes large and the piping for it also becomes considerably thick. Because of this, it is not possible to achieve sufficient downsizing of equipment.
Moreover, since the decarboxylation tower must be of a closed type, the equipment cost increases.
本発明は、蒸発法による塩水淡水化装置におけ
るスケール生成は重合燐酸塩等のスケール防止剤
の使用によつて防止できる一方、塩水には炭酸成
分が重炭酸イオン（HCO- 3）として約140ppm程
度含まれており、これが蒸発法による塩水淡化に
際しての加熱によつて、
2HCO- 3→CO-- 3＋H2O＋CO2↑
CO- 3＋H2O→2OH-＋CO2↑
のように熱分解して、炭酸ガス（CO2）が発生
し、この炭酸ガスが空気等の他の不凝縮性ガスと
共に、蒸発法による塩水淡水化装置における真空
発生装置から大気中に抽気放出されることに鑑
み、大気中に放出されているこの炭酸ガスを、前
記淡水化装置で製造した蒸溜水に溶解させるよう
にすることにより、装置の小型化と、運転経費の
低減とを図つたものである。 According to the present invention, scale formation in saltwater desalination equipment using the evaporation method can be prevented by using a scale inhibitor such as polymerized phosphate, while the carbonate component in saltwater is approximately 140ppm as bicarbonate ion (HCO - 3 ). This is thermally decomposed as 2HCO - 3 →CO -- 3 +H 2 O＋CO 2 ↑ CO - 3 +H 2 O→2OH - +CO 2 ↑ by heating during brine desalination by evaporation method. , carbon dioxide (CO 2 ) is generated, and this carbon dioxide is extracted into the atmosphere from the vacuum generator in the desalination equipment using the evaporation method, along with other non-condensable gases such as air. By dissolving this carbon dioxide gas released into the desalination apparatus into the distilled water produced by the desalination apparatus, it is possible to downsize the apparatus and reduce operating costs.
以下本発明を図面について説明するに、本発明
における蒸発法の塩水淡水化装置には、多段フラ
ツシユ型塩水淡水化装置と、多重効用型塩水淡水
化装置、蒸気圧縮式塩水淡水化装置等のすべての
塩水淡水化装置を含み、第１図は従来より良く知
られているブライン循環式多段フラツシユ型塩水
淡水化装置に本発明を適用した場合の実施の一例
を示すフローシートである。 To explain the present invention with reference to the drawings below, the evaporation method brine desalination apparatus of the present invention includes all types of desalination apparatus such as a multi-stage flash type brine desalination apparatus, a multi-effect brine desalination apparatus, a vapor compression type brine desalination apparatus, etc. FIG. 1 is a flow sheet showing an example of the implementation of the present invention when the present invention is applied to a conventionally well-known brine circulation multi-stage flash type desalination apparatus.
この装置は、ブライン加熱器１、多段の蒸発室
２、及びスケール防止剤注入装置３を有し、前記
各蒸発室２には、蒸発段４と凝縮器５とを各々備
えている。 This apparatus has a brine heater 1, a multistage evaporation chamber 2, and a scale inhibitor injection device 3, and each evaporation chamber 2 is equipped with an evaporation stage 4 and a condenser 5, respectively.
原水である塩水は、管６より系に供給され、熱
放出部凝縮器５′を通過した後、一部は排出され、
残りの塩水はスケール防止剤注入装置３によりス
ケール防止剤を添加された後蒸発室に導入され
る。最終段蒸発室に至つた濃縮塩水（ブライン）
は前記塩水と混合された後、各蒸発室２の凝縮器
５の管内を低温段より高温段へと順次流れ、その
蒸発段から発生する蒸気により順次高温に加熱さ
れ、次いで、ブライン加熱器１で、例えばボイラ
ーから管７で送られてくる高温蒸気によりさらに
加熱され、そして、塩水は蒸発室２の高温蒸発段
に供給され、以下フラツシユ蒸発を繰り返し、最
終の低温蒸発段よりポンプ４５によつて一部は再
循環一部は管８を経て系外に排出される一方、各
蒸発段で発生した蒸気は凝縮器５の管外で凝縮
し、蒸溜水となつて送出管９からポンプ１０にて
炭酸カルシウム溶解装置１１を経て系外に送出さ
れるのであり、各蒸発室２内は、低温の蒸発室に
接続した抽気エゼクター１２，１３と凝縮器１
４，１５とからなる真空発生装置１６にて、不凝
縮性ガスを抽気することにより、低温の蒸発室ほ
ど高真空度になるように構成されている。なお、
多段フラツシユ型塩水淡水装置は貫流式その他で
あつても差支えない。 Salt water, which is raw water, is supplied to the system through a pipe 6, and after passing through a heat release condenser 5', a portion is discharged.
The remaining salt water is introduced into the evaporation chamber after being added with a scale inhibitor by the scale inhibitor injection device 3. Concentrated salt water (brine) reaching the final stage evaporation chamber
After being mixed with the brine, it sequentially flows through the tubes of the condenser 5 of each evaporation chamber 2 from the low temperature stage to the high temperature stage, and is sequentially heated to a high temperature by the steam generated from the evaporation stage. For example, the brine is further heated by high-temperature steam sent from the boiler through the pipe 7, and then supplied to the high-temperature evaporation stage of the evaporation chamber 2, whereupon flash evaporation is repeated, and then from the final low-temperature evaporation stage to the pump 45. A portion is recirculated and a portion is discharged to the outside of the system via pipe 8. On the other hand, the steam generated in each evaporation stage is condensed outside the pipe of condenser 5 and becomes distilled water from delivery pipe 9 to pump 10. The calcium carbonate is sent out of the system through a calcium carbonate dissolving device 11, and inside each evaporation chamber 2 there are extracted air ejectors 12, 13 connected to the low-temperature evaporation chamber and a condenser 1.
By extracting non-condensable gas using a vacuum generator 16 consisting of 4 and 15, the lower the temperature of the evaporation chamber, the higher the degree of vacuum. In addition,
The multi-stage flash saltwater freshwater equipment may be of the once-through type or other types.
そして、前記真空発生装置１６の末端から最終
的に放出されるガスには、空気等の不凝縮性ガス
を含むと共に、各蒸発室で塩水から発生する炭酸
ガスを含んでいるから、これを管１７にて水封式
圧縮機１８に送つて圧縮したのち、セパレータ１
９に送り、該セパレータ１９内で、前記圧縮機１
８の水封に用いることで炭酸ガスが溶解した水封
水と、炭酸ガスを含むガスとに分離し、炭酸ガス
が溶解した水封水及び炭酸ガスを含むガスを管２
０，２１を介して、前記蒸溜水の送出管９に供給
するのである。 The gas finally released from the end of the vacuum generator 16 contains non-condensable gas such as air, and also contains carbon dioxide gas generated from salt water in each evaporation chamber. After being sent to a water ring compressor 18 and compressed at step 17, the separator 1
9, and within the separator 19, the compressor 1
By using the water seal in step 8, the water seal in which carbon dioxide gas is dissolved is separated into a gas containing carbon dioxide gas, and the water seal in which carbon dioxide gas is dissolved and the gas containing carbon dioxide gas are transferred to pipe 2.
0 and 21, the distilled water is supplied to the distilled water delivery pipe 9.
なお、前記水封式圧縮機１８の水封水として、
管２０，２１からの炭酸ガスを溶解する前の蒸溜
水の一部を管２２及びポンプ２３にて導出して、
これを用いるようにしたから、清水の使用量を節
減できるのであり、勿論清水を水封水として管２
４より切換え供給するようにしても良い。 In addition, as the water seal of the water ring compressor 18,
A portion of the distilled water from the pipes 20 and 21 before dissolving the carbon dioxide gas is led out through the pipe 22 and the pump 23,
By using this, the amount of fresh water used can be reduced, and of course the fresh water can be used as water sealing water for the pipes.
4 may be switched and supplied.
前記セパレータ１９からの水封水と炭酸ガスを
含むガスとを蒸溜水の送出管９に供給するには、
セパレータ１９の管２０からの水封水を、管２１
からの炭酸ガスを含むガスの供給個所より下流側
にするのが好ましい、なぜならば、これが逆であ
ると、換言すると炭酸ガスが溶解している水封水
と混合した蒸溜水に炭酸ガスを溶解させると、炭
酸ガスの溶解量が、前記水封水に溶解している炭
酸ガスのために低下するからである。（勿論配置
等の都合により注入の順序がやむをえず逆となる
場合もありうる。）また、カルシウムを主成分と
する塩を溶解するに際して、消石灰を用いる場合
には、該消石灰を蒸溜水送出管９に注入すれば良
いが、一方炭酸カルシウム溶解装置１１を用いた
場合には、前記セパレータ１９からの水封水及び
炭酸ガスの供給個所の下流側に炭酸カルシウム溶
解装置１１を設けることにより、炭酸カルシウム
の溶解量を向上できる利点がある。 In order to supply the sealed water and gas containing carbon dioxide from the separator 19 to the distilled water delivery pipe 9,
The water sealed from the pipe 20 of the separator 19 is transferred to the pipe 21.
It is preferable to place the gas containing carbon dioxide gas downstream from the point where the gas containing carbon dioxide gas is supplied from. This is because the amount of carbon dioxide gas dissolved will decrease due to the carbon dioxide gas dissolved in the sealed water. (Of course, there may be cases where the injection order is unavoidably reversed due to arrangement etc.) Also, when slaked lime is used to dissolve salts whose main component is calcium, the slaked lime is poured into the distilled water delivery pipe. However, if the calcium carbonate dissolving device 11 is used, the calcium carbonate dissolving device 11 is installed downstream of the water seal and carbon dioxide gas supply point from the separator 19. It has the advantage of increasing the amount of calcium dissolved.
なお、上記実施例は、真空発生装置１６が抽気
エゼクター１２，１３と凝縮器１４，１５より構
成された場合であるが、本発明における真空発生
装置としては、前記実施例に限らず、第３図に示
すように抽気エゼクター１２、凝縮器１４および
真空ポンプ２５から構成される場合、または第４
図のように真空発生装置が空気を駆動源とする抽
気エゼクター２６と、真空ポンプ２５との組み合
せからなる場合、あるいは凝縮器と真空ポンプと
の組合わせからなる場合、さらに真空ポンプ２５
のみで構成される場合も含むことはいうまでもな
い。 The above embodiment is a case in which the vacuum generation device 16 is composed of the bleed ejectors 12, 13 and the condensers 14, 15, but the vacuum generation device in the present invention is not limited to the above embodiment. As shown in the figure, if it is composed of a bleed ejector 12, a condenser 14 and a vacuum pump 25, or a fourth
As shown in the figure, when the vacuum generating device consists of a combination of a bleed ejector 26 whose driving source is air and a vacuum pump 25, or when it consists of a combination of a condenser and a vacuum pump, a vacuum pump 25 is also provided.
It goes without saying that this also includes the case where it is composed of only one.
第２図は、従来から良く知られている多重効用
型塩水淡水化装置に適用した場合の実施の一例を
示し、塩水は管２８より系に供給され最終コンデ
ンサを通過したのち、所定量の給水はまずスケー
ル防止剤注入装置３によりスケール防止剤を添加
された後、蒸発室２９の予熱器３０の管内を低温
部より、高温部へと順次流れて加熱され、この加
熱された塩水は第一効用蒸発室３１の伝熱管３２
の外面に散布され、その伝熱管３２内に管３３よ
り供給されている加熱蒸気によつて蒸発し、未蒸
発の塩水は第二効用蒸発室３４の伝熱管３５の外
面に散布され、以下順次下段の効用蒸発室に供給
され、最終の効用蒸発室３６から管３７より系外
に排出される一方、第一効用蒸発室３１で発生し
た蒸気は第二効用蒸発室３４の伝熱管３５内に供
給されて凝縮すると同時にその外面に散布された
塩水を蒸発させ、以下前記作用を順次各効用蒸発
室について繰り返し、最終効用蒸発室３６で発生
した蒸気は凝縮器３８で、該凝縮器３８内の伝熱
管３９内を流れる塩水により冷却されて凝縮し、
前記各効用蒸発室における伝熱管からの凝縮水と
一緒になり、目的の蒸溜水として送出管４０から
炭酸カルシウム溶解装置１１を経て系外に送り出
されるのである。 Figure 2 shows an example of implementation when applied to a conventionally well-known multi-effect desalination system, in which brine is supplied to the system through pipe 28, passes through a final condenser, and then a predetermined amount of water is supplied. After the scale inhibitor is added to the salt water by the scale inhibitor injection device 3, it is heated by flowing sequentially from the low temperature part to the high temperature part in the pipe of the preheater 30 of the evaporation chamber 29, and this heated salt water is heated in the first stage. Heat exchanger tube 32 of effective evaporation chamber 31
The unevaporated salt water is sprayed on the outer surface of the heat transfer tube 35 of the second effect evaporation chamber 34, and is evaporated by the heated steam supplied from the tube 33 into the heat transfer tube 32. The steam generated in the first effect evaporation chamber 31 is supplied to the lower effect evaporation chamber and discharged from the final effect evaporation chamber 36 to the outside of the system through a pipe 37. At the same time as it is supplied and condensed, the salt water sprinkled on its outer surface is evaporated, and the above operation is repeated for each effect evaporation chamber 36 in turn, and the steam generated in the final effect evaporation chamber 36 is sent to the condenser 38. It is cooled and condensed by the salt water flowing inside the heat transfer tube 39,
Together with the condensed water from the heat transfer tubes in each of the effect evaporation chambers, it is sent out of the system from the delivery pipe 40 through the calcium carbonate dissolving device 11 as the target distilled water.
各蒸発室は真空発生装置１６にて不凝縮ガスを
抽気することにより、低温の蒸発室ほど高真空度
になるように構成されている。そして該真空発生
装置の末端から最終的に放出されるガスは水封式
圧縮機１８に送られて圧縮された後セパレータ１
９にて水封水と炭酸ガスを含むガスとに分離さ
れ、これらの水とガスは管２０，２１を介して前
記蒸溜水の送出管４０に供給されるのである。 Each evaporation chamber is configured such that the lower the temperature of the evaporation chamber, the higher the degree of vacuum by extracting non-condensable gas using the vacuum generator 16. The gas finally released from the end of the vacuum generator is sent to the water ring compressor 18 and compressed, and then the separator 1
At step 9, sealed water and gas containing carbon dioxide are separated, and these water and gas are supplied to the distilled water delivery pipe 40 via pipes 20 and 21.
ここに用いられる真空発生装置としては、第２
図に示すものに限らず、多段フラツシユ型塩水淡
水化装置の実施例で説明したと同様に、第３図、
第４図などの抽気エゼクター、凝縮器および真空
ポンプの組合せによる各種の構成の場合をも含む
ことは言うまでもない。 The vacuum generator used here is the second one.
Not limited to what is shown in the figure, similar to that described in the embodiment of the multi-stage flash type desalination apparatus,
It goes without saying that the present invention includes various configurations in which a bleed ejector, a condenser, and a vacuum pump are combined as shown in FIG. 4.
さて、上記の多段フラツシユ型および多重効用
型のいずれの塩水淡水化装置の実施例において
も、炭酸ガスを含む不凝縮性ガスとしては高温か
ら低温までのそれぞれの蒸発室で塩水から分離抽
出されたものを用いるが高温部分から取り出され
たものについて、第１図、第２図に二点鎖線にて
示すとおり圧力によつては真空発生装置内の一部
またはすべての抽気エゼクターを通らず、管４２
によつて直接真空発生装置内の凝縮器１４及び／
又は１５に導入したり、第４図のように別の凝縮
器２７を介して取出して利用する場合もある。 Now, in both the above-mentioned embodiments of the multi-stage flash type and multi-effect type brine desalination equipment, non-condensable gases including carbon dioxide are separated and extracted from the brine in each evaporation chamber from high temperature to low temperature. However, as shown by the two-dot chain line in Figures 1 and 2, when the gas is taken out from the high-temperature part, depending on the pressure, it may not pass through some or all of the bleed ejectors in the vacuum generator and may be removed from the pipe. 42
condenser 14 and/or directly in the vacuum generator by
Alternatively, it may be introduced into 15 or taken out through another condenser 27 as shown in FIG. 4 for use.
また破線にて示すごとく最高温蒸発室に導入さ
れる前の塩水から気水分離器４３にて分離抽出さ
れた不凝縮性ガスを用いる場合も同様であり、こ
れらは設計条件に応じて適宜、設計者が定めると
ころである。 The same applies to the case where non-condensable gas separated and extracted in the steam-water separator 43 from the salt water before being introduced into the highest temperature evaporation chamber is used as shown by the broken line. This is determined by the designer.
この真空発生装置に蒸気駆動の抽気エゼクター
が用いられる場合、その駆動源であるボイラーの
蒸気に脱酸剤としてのヒドラジン（N2H4）が含
まれていて、これが蒸溜水中に前記炭酸ガスの供
給と共に混入して人体に悪影響を及ぼす恐れがあ
る場合には、蒸溜水ラインに酸化剤注入装置４４
を設けて塩素またはオゾン等の酸化剤を注入する
ことにより
N2H4＋2Cl2→N2↑＋4HCl
の反応が行われ、無害化を達成できる。 When a steam-driven extraction ejector is used in this vacuum generator, the steam from the boiler that is the driving source contains hydrazine (N 2 H 4 ) as a deoxidizing agent, and this removes the carbon dioxide from the distilled water. If there is a risk of contamination with the supply and adversely affecting the human body, install an oxidizer injection device 44 in the distilled water line.
By injecting an oxidizing agent such as chlorine or ozone into the reactor, a reaction of N 2 H 4 +2Cl 2 →N 2 ↑+4HCl takes place and detoxification can be achieved.
以上要するに本発明は、蒸発法による塩水淡水
化装置で得られた蒸溜水に、カルシウムを主成分
とする塩と、炭酸ガスとを溶解させる蒸溜水の後
処理方法において、前記蒸溜水に溶解する炭酸ガ
スとして、前記蒸発法による塩水淡水化装置にお
いて真空発生装置の末端から最終的に放出された
炭酸ガスを利用することを特徴とする蒸溜水の後
処理方法であつて、従来何等利用されずに大気へ
放出されていた炭酸ガスを利用して蒸溜水の味付
けと配管の腐食防止を行うもので経済的に頗る有
利である。このように蒸発法による塩水淡水化装
置において真空発生装置によつて不凝縮性ガスと
共に抽気した炭酸ガスを利用したことにより、前
記したように炭酸ガス発生用の密閉型脱炭酸塔及
び該脱炭酸塔内を高真空にするための抽気エゼク
ターを必要としないから、設備を安価に且つ小型
化できると共に、炭酸ガスの抽気のための多量の
高圧蒸気が不必要であるから、運転経費を低減で
きるのである。また、炭酸ガスは真空発生装置の
末端から最終的に放出されたものを使用するか
ら、炭酸ガスの取出しに際しては最終ガス放出管
の端部に単に管を接続するだけで十分であり、塩
水淡水化装置の設計を大きく変更する必要もな
く、また既設の塩水淡水化装置に容易に併設する
ことができるので、むだがなくかつ経済的にも有
利である。 In summary, the present invention provides a method for post-treatment of distilled water in which a salt containing calcium as a main component and carbon dioxide gas are dissolved in distilled water obtained by a salt water desalination apparatus using an evaporation method. A method for post-treatment of distilled water characterized by using, as carbon dioxide gas, the carbon dioxide gas finally released from the end of the vacuum generator in the desalination equipment using the evaporation method, which has not been used in the past. It uses carbon dioxide gas, which was previously released into the atmosphere, to flavor distilled water and prevent corrosion of pipes, making it extremely economically advantageous. In this way, by using the carbon dioxide gas extracted together with non-condensable gas by the vacuum generator in the desalination equipment using the evaporation method, a closed decarboxylation tower for generating carbon dioxide gas and the decarboxylation tower were developed as described above. Since there is no need for a bleed ejector to create a high vacuum inside the tower, the equipment can be made cheaper and smaller, and since a large amount of high pressure steam is not required to bleed the carbon dioxide gas, operating costs can be reduced. It is. In addition, since the carbon dioxide gas that is finally released from the end of the vacuum generator is used, it is sufficient to simply connect the pipe to the end of the final gas release pipe when taking out the carbon dioxide gas, and it is sufficient to extract the carbon dioxide gas from salt water and fresh water. There is no need to make any major changes to the design of the desalination device, and it can be easily installed alongside an existing desalination device, so it is efficient and economically advantageous.
また、他の発明は、前記発明に加えて、淡水化
装置から抽気した炭酸ガスを、水封式の圧縮機で
圧縮して、その水封水と共に蒸溜水に供給するも
ので、水封式の圧縮機における圧縮時に、炭酸ガ
スを当該圧縮機における水封水に十分に溶解させ
ることができる効果がある。 In addition to the above invention, another invention is to compress carbon dioxide gas extracted from a desalination apparatus using a water ring type compressor and supply it to distilled water together with the water ring type water ring type compressor. During compression in the compressor, carbon dioxide gas can be sufficiently dissolved in the water sealed in the compressor.
更に他の発明は、蒸溜水に塩素またはオゾン等
の酸化剤を注入したから、ボイラ給水にヒドラジ
ンが使用されて万一それが真空発生装置を経て蒸
溜水に混入してもオゾン等により酸化されて無害
化され、人体への悪影響は排除できると共にボイ
ラへの脱酸剤の使用につき何等の制限をも必要な
く、効率的にボイラーの腐食を防止し寿命を長く
できる効果がある。 Still another invention is that since oxidizing agents such as chlorine or ozone are injected into distilled water, even if hydrazine is used in boiler feed water and is mixed into distilled water through a vacuum generator, it will not be oxidized by ozone, etc. The deoxidizing agent is rendered harmless, eliminating any harmful effects on the human body, and there is no need to place any restrictions on the use of deoxidizers in boilers, which effectively prevents boiler corrosion and extends its lifespan.
第１図及び第２図は本発明をそれぞれ多段フラ
ツシユ型塩水淡水化装置及び多重効用型塩水淡水
化装置に適用した場合の一実施例を示すフローシ
ートであり、第３図および第４図は他の形式の真
空発生装置を用いた場合を示す要部のフローシー
トである。
１……ブライン加熱器、２……多段の蒸発室、
３……スケール防止剤注入装置、４……蒸発段、
５……凝縮器、６……管、７……管、８……管、
９……送出管、１０……ポンプ、１１……炭酸カ
ルシウム溶解装置、１２，１３……抽気エゼクタ
ー、１４，１５……凝縮器、１６……真空発生装
置、１７……管、１８……水封式圧縮機、１９…
…セパレータ、２０，２１……管、２２……管、
２３……ポンプ、２４……管、２５……真空ポン
プ、２６……抽気エゼクター、２７……凝縮器、
２８……管、２９……蒸発室、３０……予熱器、
３１……第１効用蒸発室、３２……伝熱管、３３
……管、３４……第２効用室、３５……伝熱管、
３６……最終効用室、３７……管、３８……凝縮
器、３９……伝熱管、４０……送出管、４２……
管、４３……気水分離器、４４……酸化剤注入装
置、４５……ポンプ。
FIG. 1 and FIG. 2 are flow sheets showing an example of applying the present invention to a multi-stage flash type salt water desalination device and a multi-effect salt water desalination device, respectively, and FIG. 3 and FIG. It is a flow sheet of the main part showing the case where another type of vacuum generator is used. 1...Brine heater, 2...Multi-stage evaporation chamber,
3... Scale inhibitor injection device, 4... Evaporation stage,
5...Condenser, 6...Tube, 7...Tube, 8...Tube,
9... Delivery pipe, 10... Pump, 11... Calcium carbonate dissolving device, 12, 13... Bleeding ejector, 14, 15... Condenser, 16... Vacuum generator, 17... Tube, 18... Water ring compressor, 19...
...Separator, 20, 21...Pipe, 22...Pipe,
23... pump, 24... pipe, 25... vacuum pump, 26... bleed ejector, 27... condenser,
28... tube, 29... evaporation chamber, 30... preheater,
31...First effect evaporation chamber, 32...Heat transfer tube, 33
... tube, 34 ... second effect chamber, 35 ... heat exchanger tube,
36...Final effect chamber, 37...Pipe, 38...Condenser, 39...Heat transfer tube, 40...Delivery pipe, 42...
Pipe, 43... Steam water separator, 44... Oxidizing agent injection device, 45... Pump.
Claims (1)
水に、カルシウムを主成分とする塩と、炭酸ガス
とを溶解させる蒸溜水の後処理方法において、前
記蒸溜水に溶解する炭酸ガスとして、前記蒸発法
による塩水淡水化装置の真空発生装置の末端から
最終的に放出された炭酸ガスを利用することを特
徴とする蒸溜水の後処理方法。 ２ 蒸発法による塩水淡水化装置で得られた蒸溜
水に、カルシウムを主成分とする塩と、炭酸ガス
とを溶解させる蒸溜水の後処理方法において、前
記蒸発法による塩水淡水化装置において真空発生
装置にて抽気した炭酸ガスを、水封式圧縮機で圧
縮し、該圧縮機の水封水と共に前記多段蒸発法に
よる塩水淡水化装置からの蒸溜水に供給するよう
にしたことを特徴とする蒸溜水の後処理方法。 ３ 水封式の圧縮機の水封水として、前記塩水淡
水化装置からの蒸溜水を使用することを特徴とす
る特許請求の範囲第２項記載の蒸溜水の後処理方
法。 ４ 蒸発法による塩水淡水化装置で得られた蒸溜
水に、カルシウムを主成分とする塩と、炭酸ガス
とを溶解させる蒸溜水の後処理方法において、前
記蒸溜水に溶解する炭酸ガスとして、前記蒸発法
による塩水淡水化装置の真空発生装置の末端から
最終的に放出された炭酸ガスを利用し、且つ蒸溜
水に塩素又はオゾン等の酸化剤を注入することを
特徴とする蒸溜水の後処理方法。[Scope of Claims] 1. A method for post-treatment of distilled water in which a salt containing calcium as a main component and carbon dioxide gas are dissolved in distilled water obtained by a salt water desalination apparatus using an evaporation method. A method for post-treatment of distilled water, characterized in that the carbon dioxide gas finally released from the end of the vacuum generator of the desalination apparatus using the evaporation method is used as the carbon dioxide gas. 2. A method for post-treatment of distilled water in which a salt containing calcium as a main component and carbon dioxide gas is dissolved in distilled water obtained by a desalination apparatus using an evaporation method, wherein a vacuum is generated in the desalination apparatus using an evaporation method. The carbon dioxide gas extracted by the device is compressed by a water ring compressor, and is supplied together with the water ring water from the compressor to the distilled water from the desalination equipment using the multi-stage evaporation method. Post-treatment method for distilled water. 3. The method for post-treatment of distilled water according to claim 2, characterized in that distilled water from the desalination apparatus is used as water sealing water for a water ring compressor. 4. In a method for post-treatment of distilled water in which salt containing calcium as a main component and carbon dioxide gas are dissolved in distilled water obtained by a salt water desalination apparatus using an evaporation method, the carbon dioxide gas dissolved in the distilled water is Post-treatment of distilled water characterized by using carbon dioxide gas finally released from the end of the vacuum generator of a salt water desalination device using the evaporation method and injecting an oxidizing agent such as chlorine or ozone into the distilled water. Method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP13248083A JPS6025586A (en) | 1983-07-20 | 1983-07-20 | Post-treatment of distilled water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP13248083A JPS6025586A (en) | 1983-07-20 | 1983-07-20 | Post-treatment of distilled water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6025586A JPS6025586A (en) | 1985-02-08 |
| JPS6359756B2 true JPS6359756B2 (en) | 1988-11-21 |
Family
ID=15082355
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP13248083A Granted JPS6025586A (en) | 1983-07-20 | 1983-07-20 | Post-treatment of distilled water |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6025586A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4673443A (en) * | 1985-03-18 | 1987-06-16 | Motorola, Inc. | Continuous ionizer for semiconductor manufacturing processes |
| CN114081122A (en) * | 2021-12-03 | 2022-02-25 | 金杰食品(漳州)有限公司 | Method for removing salt of pickled product made from sugared ginger raw material |
-
1983
- 1983-07-20 JP JP13248083A patent/JPS6025586A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6025586A (en) | 1985-02-08 |
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