JPH0380991A - Method and apparatus for treating supplied water to boiler - Google Patents
Method and apparatus for treating supplied water to boilerInfo
- Publication number
- JPH0380991A JPH0380991A JP1219369A JP21936989A JPH0380991A JP H0380991 A JPH0380991 A JP H0380991A JP 1219369 A JP1219369 A JP 1219369A JP 21936989 A JP21936989 A JP 21936989A JP H0380991 A JPH0380991 A JP H0380991A
- Authority
- JP
- Japan
- Prior art keywords
- water
- reverse osmosis
- osmosis membrane
- raw water
- alkalinity
- 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.)
- Granted
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 105
- 238000000034 method Methods 0.000 title claims abstract description 20
- 239000012528 membrane Substances 0.000 claims abstract description 42
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 41
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 16
- 238000010612 desalination reaction Methods 0.000 claims description 8
- 238000011144 upstream manufacturing Methods 0.000 claims description 5
- 238000004887 air purification Methods 0.000 claims 1
- 230000003204 osmotic effect Effects 0.000 claims 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 20
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 10
- 239000001569 carbon dioxide Substances 0.000 abstract description 10
- -1 ion compound Chemical class 0.000 abstract description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 4
- 238000011033 desalting Methods 0.000 abstract description 4
- 229910052760 oxygen Inorganic materials 0.000 abstract description 4
- 239000001301 oxygen Substances 0.000 abstract description 4
- 238000005260 corrosion Methods 0.000 abstract description 3
- 230000007797 corrosion Effects 0.000 abstract description 3
- 230000000694 effects Effects 0.000 abstract description 3
- 230000002411 adverse Effects 0.000 abstract description 2
- 230000007717 exclusion Effects 0.000 abstract 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 12
- 239000007789 gas Substances 0.000 description 7
- 238000005342 ion exchange Methods 0.000 description 5
- 238000002347 injection Methods 0.000 description 3
- 239000007924 injection Substances 0.000 description 3
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 229910052925 anhydrite Inorganic materials 0.000 description 1
- 150000001450 anions Chemical class 0.000 description 1
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000001802 infusion Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
Abstract
Description
【発明の詳細な説明】 〔産業上の利用分野〕 本発明は、ボイラ給水の処理技術に関する。[Detailed description of the invention] [Industrial application field] The present invention relates to a technology for treating boiler feed water.
詳しくは、逆浸透膜装置により原水を脱塩してボイラに
供給するボイラ給水処理方法と、ボイラへの給水路に原
水脱塩用の逆浸透膜装置を介装してあるボイラ給水処理
装置とに関する。In detail, there is a boiler feed water treatment method in which raw water is desalinated using a reverse osmosis membrane device and supplied to the boiler, and a boiler feed water treatment device in which a reverse osmosis membrane device for raw water desalination is interposed in the water supply channel to the boiler. Regarding.
ボイラでは、缶水のＭアルカリ度と、Ｍアルカリ度が分
解生成するＰアルカリ度と、ＰＨとを設定範囲内に維持
するように管理することが肝要である。また、Ｍアルカ
リ度が高いことは、ボイラ内により分解生成する炭酸ガ
スが復水配管の腐蝕原因であるため望ましいことではな
い。In a boiler, it is important to manage the M alkalinity of canned water, the P alkalinity generated by decomposition of the M alkalinity, and the pH to maintain them within set ranges. Furthermore, a high M alkalinity is not desirable because carbon dioxide gas decomposed and produced within the boiler causes corrosion of the condensate piping.
そのような缶水管理をボイラ給水処理により行う場合に
は、ボイラ圧力、つまり、ボイラ内でのＭアルカリ度の
濃縮状況・ボイラ内でのＰアルカリ度成分の生成状況に
基づいて、缶水のＰＨを設定範囲内の値にさせるボイラ
給水のＭアルカリ度を求め、その求めたＭアルカリ度と
なるように原水を処理することが理想的である。When such canned water management is performed by boiler feed water treatment, the canned water is Ideally, the M alkalinity of the boiler feed water that brings the PH to a value within a set range is determined, and the raw water is treated to achieve the determined M alkalinity.
そのように缶水ＰＨを適正とさせる設定範囲のＭアルカ
リ度のボイラ給水に原水を処理するに、従来では、逆浸
透膜装置による脱塩により、Ｍアルカリ度が設定範囲と
なるようにＭアルカリ度成分を同時に排除していた。こ
の従来手段によるときは、例えばイオン交換塔に原水を
供給してＭアルカリ度成分を排除するイオン交換手段に
比べて構成および操作が簡単となる。つまり、イオン交
換手段によるときは、酸、アルカリを含む再生排水を中
和処理するための後処理が必要であるのに対して、それ
が不要である。In order to treat raw water to boiler feed water with M alkalinity within the set range that makes the PH of canned water appropriate, conventional methods have been to reduce M alkalinity to the set range by desalting using a reverse osmosis membrane device. At the same time, the chemical components were eliminated. When this conventional means is used, the structure and operation are simpler than, for example, an ion exchange means that supplies raw water to an ion exchange column and removes the M alkalinity component. In other words, when using ion exchange means, post-treatment for neutralizing recycled wastewater containing acids and alkalis is required, but this is not necessary.
〔発明が解決しようとする課題〕
しかし、前記従来技術によるときは、逆浸透膜装置によ
り排除すべきＭアルカリ度成分が、その逆浸透膜装置に
よる排除率が低い一価の陰イオン〔例えばＣａ（ＨＣＯ
ｓ）２）であるため、特にＭアルカリ度が高くて設定範
囲のＭアルカリ度にするには多くのＭアルカリ度成分を
除去する必要がある原水の場合、逆浸透膜装置として高
性能なものが必要で、エネルギーコストが高く付いてい
た。[Problems to be Solved by the Invention] However, when using the above-mentioned prior art, the M alkalinity component to be removed by the reverse osmosis membrane device is monovalent anions [e.g. Ca (H.C.O.
s) Because of 2), especially in the case of raw water with high M alkalinity and it is necessary to remove many M alkalinity components to bring the M alkalinity within the set range, a high-performance reverse osmosis membrane device is recommended. was required, resulting in high energy costs.
本発明の目的は、設定範囲のＭアルカリ度に原水を安価
に処理できるボイラ給水処理の方法と装置とを提供する
点にある。An object of the present invention is to provide a boiler feed water treatment method and apparatus that can inexpensively treat raw water to a set range of M alkalinity.
本発明によるボイラ給水の処理方法の特徴は、前記逆浸
透膜装置により原水を脱塩する前に、ボイラ圧力に応じ
て原水中のＭアルカリ度成分を分解し、前記逆浸透膜装
置による原水の脱塩後に、透過水から脱気する点にある
。The feature of the method for treating boiler feed water according to the present invention is that before the raw water is desalinated by the reverse osmosis membrane device, the M alkalinity component in the raw water is decomposed according to the boiler pressure, and the raw water is treated by the reverse osmosis membrane device. After desalination, the permeate is degassed.
上記方法において、前記脱気処理の前に水を軟化処理す
ることが好ましい。In the above method, it is preferable that the water is subjected to a softening treatment before the deaeration treatment.
本発明によるボイラ給水の処理装置の特徴構成は、前記
給水路のうち前記逆浸透膜装置の上流部に、原水中のＭ
アルカリ度成分を分解するための分解装置を設け、前記
給水路のうち前記逆浸透膜装置の下流部に、透過水から
脱気するための脱気装置を設けてある点にある。The characteristic configuration of the boiler feed water treatment device according to the present invention is such that M in the raw water is placed in the upstream portion of the reverse osmosis membrane device in the water supply channel.
A decomposition device for decomposing alkalinity components is provided, and a deaeration device for deaeration from the permeated water is provided downstream of the reverse osmosis membrane device in the water supply channel.
上記装置において、前記給水路のうち脱気装置の上流部
に、水を軟化処理するための軟化器を設けてあることが
好ましい。In the above device, it is preferable that a softener for softening the water is provided in an upstream portion of the deaerator in the water supply channel.
逆浸透膜装置により原水を脱塩する前に、原水中のＭア
ルカリ度成分を分解して、Ｍアルカリ度成分を逆浸透膜
による排除率の高い２価イオンの化合物に変化させるこ
とができるので、逆浸透膜装置による脱塩によりＭアル
カリ度が設定範囲内となるようにＭアルカリ度成分を排
除できながらも、逆浸透膜装置として性能の低いもので
済む。しかも、前記のＭアルカリ度成分の分解によって
、復水配管に悪影響を及ぼす炭酸ガスが生じるものの、
逆浸透膜装置からの透過水を脱気するようにしてあるか
ら、ボイラ給水から炭酸ガスはもちろん、ボイラ腐蝕の
主因である溶存酸素も脱気できる。Before desalinating raw water using a reverse osmosis membrane device, it is possible to decompose the M alkalinity component in the raw water and change the M alkalinity component into a divalent ion compound that has a high rejection rate by the reverse osmosis membrane. Although the M alkalinity component can be removed by desalination using a reverse osmosis membrane device so that the M alkalinity falls within the set range, a reverse osmosis membrane device with low performance is sufficient. Moreover, although the decomposition of the M alkalinity component described above produces carbon dioxide gas that has an adverse effect on condensate piping,
Since the permeated water from the reverse osmosis membrane device is degassed, not only carbon dioxide gas but also dissolved oxygen, which is the main cause of boiler corrosion, can be degassed from the boiler feed water.
従って、本発明は、構成、操作が簡単なもので済む逆浸
透膜法による処理形態を採用しながらも、かつ、Ｍアル
カリ度が高くて設定範囲のＭアルカリ度とするには多く
のＭアルカリ度成分を排除する必要がある原水であって
も、逆浸透膜装置として安価なものを用いて、設定範囲
のＭアルカリ度のボイラ給水に処理することができるよ
うになった。また、これにより、復水配管内におけるＰ
Ｈ値の低下の原因となる炭酸ガスの中和に要する揮発性
アミンの注入が皆無又は極めて僅かで済むのである。Therefore, the present invention adopts a treatment method using a reverse osmosis membrane method that is simple in configuration and operation, yet has a high M alkalinity, and requires a large amount of M alkalinity to reach the M alkalinity within the set range. Even raw water that requires the removal of alkalinity components can now be treated to boiler feed water with an alkalinity within the set range using an inexpensive reverse osmosis membrane device. In addition, this also results in P in the condensate piping.
There is no or very little injection of volatile amine required to neutralize carbon dioxide gas, which causes a decrease in H value.
〔実施例〕 次に本発明の実施例を示す。〔Example〕 Next, examples of the present invention will be shown.
ボイラ給水処理装置は、図示するように、ボイラ（１）
への給水路（２）に、前処理用の保安フィルタ（３）と
、原水脱塩用の逆浸透膜装置（４）と、軟化器（５）と
、給水タンク（６）と、脱気装置（７）とをその記載順
で上流側から下流側に並ぶ配置で介装し、分解装置（８
〉を設けたものである。As shown in the figure, the boiler feed water treatment device includes a boiler (1)
A safety filter (3) for pretreatment, a reverse osmosis membrane device (4) for desalination of raw water, a softener (5), a water supply tank (6), and a deaerator are installed in the water supply channel (2) to the The decomposition device (8) is interposed in such a manner that the decomposition device (7) and
> has been established.
前記逆浸透膜装置（４）は、逆浸透膜モジュール（４Ａ
）と駆動が発生用の高圧ポンプ（４Ｂ）とから成る。The reverse osmosis membrane device (4) includes a reverse osmosis membrane module (4A
) and a high-pressure pump for generation (4B).
前記軟化器（５〉は、前記逆浸透膜装置（４）からの透
過水を軟化処理するものである。The softener (5>) softens the permeated water from the reverse osmosis membrane device (4).
前記脱気装置（７）は、前記給水タンク（６）から軟化
処理水を取出す脱気ポンプ（７Ａ）と、取出した軟化処
理水から脱気する真空脱気塔（７Ｂ）とから成る。The deaerator (7) includes a deaerator pump (7A) that takes out the softened water from the water supply tank (6), and a vacuum deaerator (7B) that deaerates the softened water that has been taken out.
前記分解装置（８）は、前記給水路（２）のうち保安フ
ィルタ（３）の上流部で原水に硫酸を注入することによ
り、原水中のＭアルカリ度成分を分解して２価イオンの
化合物に変化させる装置であって、硫酸溶解槽（８Ａ）
と注入ポンプ（８Ｂ）とから成る。因みに、前記硫酸の
注入に伴う化学反応は、
Ｃａ（ＨＣＯｚ ）ｚ＋Ｈ！ｓＯ＊→ＣａＳＯ４＋ＣＯ
２＋Ｈ１０Ｍｇ（ＨＣＯ３）ｚ＋ＨｚｓＯ４→Ｍｇ５Ｏ
ｔ＋ＣＯｚ＋ＨｚＯである。The decomposition device (8) decomposes the M alkalinity component in the raw water into divalent ion compounds by injecting sulfuric acid into the raw water at the upstream portion of the safety filter (3) in the water supply channel (2). It is a device for changing into a sulfuric acid dissolving tank (8A).
and an infusion pump (8B). Incidentally, the chemical reaction accompanying the injection of sulfuric acid is Ca(HCOz)z+H! sO*→CaSO4+CO
2+H10Mg(HCO3)z+HzsO4→Mg5O
t+COz+HzO.
前記分解装置（８）による分解、つまり、硫酸の注入の
要領は次の通りである。The decomposition by the decomposition device (8), that is, the injection of sulfuric acid, is as follows.
保安フィルタ（３）の入口側での原水のＭアルカリ度お
よびボイラ圧力に基づいて、ボイラ（１）内でのＭアル
カリ度成分の分解量を計算し、その結果と、缶水の所定
ＰＨと、原水のＭアルカリ度とに基づいて、缶水のＰＨ
を所定ＰＨとさせる上で原水中から排除するＭアルカリ
度成分の量を算出し、その算出された排除量のＭアルカ
リ度成分を分解するための硫酸の量を算出する。Based on the M alkalinity of the raw water on the inlet side of the safety filter (3) and the boiler pressure, calculate the amount of decomposition of the M alkalinity component in the boiler (1), and calculate the decomposition amount of the M alkalinity component in the boiler (1) and the predetermined pH of the canned water. , the PH of canned water based on the M alkalinity of raw water.
The amount of M alkalinity component to be removed from the raw water to bring the water to a predetermined pH is calculated, and the amount of sulfuric acid for decomposing the calculated amount of M alkalinity component to be removed is calculated.
以上の予備作業を行ったのち、原水を定量供給する一方
、硫酸を前記算出量をもって定量注入し、排除すべきＭ
アルカリ度成分の全部を２価イオンの化合物（ＣａＳＯ
＜、 Ｍｇ５Ｏｉ ）に変える。After performing the above preliminary work, while supplying raw water in a fixed amount, sulfuric acid is injected in the calculated amount above, and M
All alkalinity components are replaced by divalent ion compounds (CaSO
<, Mg5Oi).
（９）は原水ポンプであり、（１０）はボイラ（１）の
給水ポンプである。(9) is a raw water pump, and (10) is a water supply pump for the boiler (1).
そして、上記構成のボイラ給水処理装置の運転によって
、
原水中のＭアルカリ度成分を、ボイラ給水のＭアルカリ
度が設定範囲内になるように分解する処理と、
逆浸透膜装置（４〉により、原水を脱塩し、同時に、分
解で２価イオンの化合物に変わったＭアルカリ度成分を
排除する処理と、逆浸透膜装置（４）からの透過水を軟
化する処理と、
前記の分解で発生した炭酸ガス、原水中の溶解炭酸ガス
、溶存酸素を脱気する処理とがその記載順に行われるこ
とになる。Then, by operating the boiler feed water treatment device with the above configuration, the M alkalinity component in the raw water is decomposed so that the M alkalinity of the boiler feed water falls within the set range, and by the reverse osmosis membrane device (4), A process that desalinates raw water and simultaneously eliminates the M alkalinity component that has been converted into divalent ion compounds due to decomposition, a process that softens the permeated water from the reverse osmosis membrane device (4), and a process that softens the permeated water from the reverse osmosis membrane device (4). The processes of degassing the carbon dioxide gas, dissolved carbon dioxide gas in the raw water, and dissolved oxygen are performed in the order listed.
従って、上記構成によれば、逆浸透膜装置（４）により
原水を脱塩する前に、原水中のＭアルカリ度成分のうち
不要なものを分解して２価イオンの化合物に変えるため
、原水のＭアルカリ度が高くても、性能の低い逆浸透膜
装置（４）による脱塩によって、原水中の不要なＭアル
カリ度成分を排除して、ボイラ給水を設定範囲内のＭア
ルカリ度のものにすることができ、しかも、前記の分解
によって発生した炭酸ガス、溶存酸素、溶解炭酸ガスを
脱気して、それらのないボイラ給水とすることができる
。Therefore, according to the above configuration, before the raw water is desalinated by the reverse osmosis membrane device (4), unnecessary M alkalinity components in the raw water are decomposed and converted into divalent ion compounds. Even if the M alkalinity of the raw water is high, the unnecessary M alkalinity components in the raw water are removed by desalination using the low-performance reverse osmosis membrane device (4), and the boiler feed water has an M alkalinity within the set range. Furthermore, carbon dioxide, dissolved oxygen, and dissolved carbon dioxide generated by the decomposition can be degassed to provide boiler feed water free of them.
次に、本発明者が行ったボイラ給水の水質比較実験を示
す。実験は、ルーズ型、高リジェクション型の逆浸透膜
装置（４）を用いた本発明方法による処理と、比較対象
としてのイオン交換法による処理とを行い、水質を調べ
た。ルーズ型の逆浸透膜装置（４）を用いた本発明方法
による処理の条件は、圧カフｋｇ、入口温度２０℃、回
収率８０％であり、高リジェクション型の逆浸透膜装置
（４）を用いた本発明方法による処理の条件は、圧力１
２ｋｇ、入口温度２０℃、回収率７０％である。また、
イオン交換法による処理の条件は、Ｎａｃ ｌ １００
ｇ／ １、再生濃度２０％、５Ｖ２０である。Next, a water quality comparison experiment of boiler feed water conducted by the present inventor will be shown. In the experiment, water quality was investigated using the method of the present invention using a loose-type, high-rejection type reverse osmosis membrane device (4) and the treatment using an ion exchange method for comparison. The conditions for the treatment according to the method of the present invention using a loose-type reverse osmosis membrane device (4) are a pressure cuff kg, an inlet temperature of 20°C, and a recovery rate of 80%. The conditions for the treatment according to the method of the present invention using
2 kg, inlet temperature 20°C, recovery rate 70%. Also,
The conditions for treatment by ion exchange method are NaCl 100
g/1, regeneration density 20%, 5V20.
結果は表１の通りである。The results are shown in Table 1.
表−１処理水水質の比較 〔別実施例〕 以下に本発明の別実施例を示す。Table-1 Comparison of treated water quality [Another example] Another example of the present invention will be shown below.
〔１〕上記実施例において、軟化器（５）を図中二点鎖
線で示すように保安フィルタ（３）と逆浸透膜装置（４
）との間の給水路部分に設ける。[1] In the above embodiment, the softener (5) is connected to the safety filter (3) and the reverse osmosis membrane device (4) as shown by the two-dot chain line in the figure.
) is installed in the water supply channel between the
〔２〕上記実施例では、脱気装置（７〉として真空脱気
装置を示したが、加熱脱気装置やガス透過式のものであ
っても良い。[2] In the above embodiments, a vacuum deaerator is shown as the deaerator (7), but a heating deaerator or a gas permeation type may be used.
〔３〕尚、特許請求の範囲の項に図面との対照を便利に
する為に符号を記すが、該記入により本発明は添付図面
の構造に限定されるものではない。[3] Note that although reference numerals are written in the claims section for convenient comparison with the drawings, the present invention is not limited to the structure shown in the accompanying drawings.
図面は本発明に係るボイラ給水処理方法とボイラ給水処
理装置の実施例を示す処理系統図である。
（４）・・・・・・逆浸透膜装置、（１）・・・・・・
ボイラ、（２）・・・・・・給水路、（８）・・・・・
・分解装置、（７）・・・・・・脱気装置。The drawing is a processing system diagram showing an embodiment of the boiler feed water treatment method and boiler feed water treatment apparatus according to the present invention. (4)・・・Reverse osmosis membrane device, (1)・・・・・・
Boiler, (2)... Water supply channel, (8)...
- Decomposition device, (7)...deaeration device.
Claims (1)
１）に供給するボイラ給水処理方法であって、前記逆浸
透膜装置（４）により原水を脱塩する前に、ボイラ圧力
に応じて原水中のＭアルカリ度成分を分解し、前記逆浸
透膜装置（４）による原水の脱塩後に、透過水から脱気
するボイラ給水処理方法。 ２、前記脱気処理の前に水を軟化処理する請求項１記載
のボイラ給水処理方法。 ３、ボイラ（１）への給水路（２）に原水脱塩用の逆浸
透膜装置（４）を介装してあるボイラ給水処理装置であ
って、前記給水路（２）のうち前記逆浸透膜装置（４）
の上流部に、原水中のＭアルカリ度成分を分解するため
の分解装置（８）を設け、前記給水路（２）のうち前記
逆浸透膜装置（４）の下流部に、透過水から脱気するた
めの脱気装置（７）を設けてあるボイラ給水処理装置。 ４、前記給水路（２）のうち脱気装置（７）の上流部に
、水を軟化処理するための軟化器（５）を設けてある請
求項３記載のボイラ給水処理装置。[Claims] 1. Desalinate the raw water using the reverse osmosis membrane device (4) and send it to the boiler (
1), in which the M alkalinity component in the raw water is decomposed according to the boiler pressure before the raw water is desalinated by the reverse osmosis membrane device (4), and the reverse osmosis membrane A boiler feedwater treatment method in which permeated water is degassed after desalination of raw water by the device (4). 2. The boiler feedwater treatment method according to claim 1, wherein the water is subjected to a softening treatment before the deaeration treatment. 3. A boiler feed water treatment device in which a reverse osmosis membrane device (4) for raw water desalination is interposed in a water supply channel (2) to a boiler (1), wherein the reverse osmosis membrane device (4) for desalination of raw water Osmotic membrane device (4)
A decomposition device (8) for decomposing the M alkalinity component in the raw water is provided upstream of the water supply channel (2), and a decomposition device (8) for decomposing the M alkalinity component in the raw water is installed downstream of the reverse osmosis membrane device (4) in the water supply channel (2). Boiler feedwater treatment equipment equipped with a deaerator (7) for air purification. 4. The boiler feed water treatment device according to claim 3, further comprising a softener (5) for softening water in the upstream portion of the deaerator (7) in the feed water channel (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1219369A JPH0790220B2 (en) | 1989-08-25 | 1989-08-25 | Boiler feedwater treatment method and boiler feedwater treatment device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1219369A JPH0790220B2 (en) | 1989-08-25 | 1989-08-25 | Boiler feedwater treatment method and boiler feedwater treatment device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0380991A true JPH0380991A (en) | 1991-04-05 |
| JPH0790220B2 JPH0790220B2 (en) | 1995-10-04 |
Family
ID=16734338
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1219369A Expired - Fee Related JPH0790220B2 (en) | 1989-08-25 | 1989-08-25 | Boiler feedwater treatment method and boiler feedwater treatment device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0790220B2 (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2004507340A (en) * | 2000-06-02 | 2004-03-11 | ビバンデイ・ユニベルサル | Nanofiltration module or reverse osmosis module, or method of checking the system integrity of such a module |
| JP2005288220A (en) * | 2004-03-31 | 2005-10-20 | Miura Co Ltd | Water quality modifying system |
| JP2005288218A (en) * | 2004-03-31 | 2005-10-20 | Miura Co Ltd | Water quality modifying system |
| JP2005296944A (en) * | 2004-03-19 | 2005-10-27 | Miura Co Ltd | Water quality improving system |
| JP2006239649A (en) * | 2005-03-07 | 2006-09-14 | Miura Co Ltd | Water supply device for boiler |
| JP2008080309A (en) * | 2006-09-29 | 2008-04-10 | Miura Co Ltd | Water treating system |
| JP2011147893A (en) * | 2010-01-22 | 2011-08-04 | Kurita Water Ind Ltd | Method for treating water of boiler water system |
-
1989
- 1989-08-25 JP JP1219369A patent/JPH0790220B2/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2004507340A (en) * | 2000-06-02 | 2004-03-11 | ビバンデイ・ユニベルサル | Nanofiltration module or reverse osmosis module, or method of checking the system integrity of such a module |
| JP2005296944A (en) * | 2004-03-19 | 2005-10-27 | Miura Co Ltd | Water quality improving system |
| JP2005288220A (en) * | 2004-03-31 | 2005-10-20 | Miura Co Ltd | Water quality modifying system |
| JP2005288218A (en) * | 2004-03-31 | 2005-10-20 | Miura Co Ltd | Water quality modifying system |
| JP2006239649A (en) * | 2005-03-07 | 2006-09-14 | Miura Co Ltd | Water supply device for boiler |
| JP2008080309A (en) * | 2006-09-29 | 2008-04-10 | Miura Co Ltd | Water treating system |
| JP2011147893A (en) * | 2010-01-22 | 2011-08-04 | Kurita Water Ind Ltd | Method for treating water of boiler water system |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0790220B2 (en) | 1995-10-04 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US10723643B2 (en) | Method of recovering oil or gas and treating the resulting produced water | |
| AU2008366066B2 (en) | Methods and systems for processing waste water | |
| TWI616404B (en) | Method and device for processing boron-containing water | |
| JPH11510432A (en) | Production of high-purity water using reverse osmosis | |
| JP4045658B2 (en) | Pure water production method | |
| JP2007307561A (en) | High-purity water producing apparatus and method | |
| JPH0380991A (en) | Method and apparatus for treating supplied water to boiler | |
| JP2007125519A (en) | Method and apparatus for producing ultrapure water | |
| JPH0252088A (en) | Apparatus for making desalted water | |
| WO2017213050A1 (en) | Water treatment method and device, water treatment device modification method, and kit for water treatment device modification | |
| JP2009160500A (en) | Ultrapure water production method and apparatus | |
| JPH11267645A (en) | Production of pure water | |
| JP6629383B2 (en) | Ultrapure water production method | |
| CN112794472A (en) | Concentration system and concentration method for high-salinity wastewater | |
| CN115485245A (en) | Method for treating wastewater, method for producing ultrapure water, and wastewater treatment apparatus | |
| JPS586297A (en) | Treatment of raw water of high content of silica | |
| JPH09294974A (en) | Water treatment apparatus | |
| JPH11169852A (en) | Pure water producing device | |
| JP7261711B2 (en) | Ultrapure water production system and ultrapure water production method | |
| JP2000271569A (en) | Production of pure water | |
| CN113698025B (en) | System and method for recycling acid and alkali from high-salt deacidification wastewater | |
| CN116639769B (en) | Method and system for recycling polished waste acid | |
| JPH09155344A (en) | Method for desalination of brackish water and apparatus therefor | |
| KR20060009128A (en) | Process for treatment of industrial water using reverse osmosis filtration and nanofiltration | |
| JPS6242787A (en) | Apparatus for producing high-purity water |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |
|
| LAPS | Cancellation because of no payment of annual fees |