JPS6328486A - Method for removing dissolved carbon dioxide in pure water producing apparatus - Google Patents
Method for removing dissolved carbon dioxide in pure water producing apparatusInfo
- Publication number
- JPS6328486A JPS6328486A JP17213586A JP17213586A JPS6328486A JP S6328486 A JPS6328486 A JP S6328486A JP 17213586 A JP17213586 A JP 17213586A JP 17213586 A JP17213586 A JP 17213586A JP S6328486 A JPS6328486 A JP S6328486A
- Authority
- JP
- Japan
- Prior art keywords
- water
- carbon dioxide
- reverse osmosis
- treatment
- stage
- 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 83
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 80
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 40
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims description 18
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 51
- 238000005342 ion exchange Methods 0.000 claims abstract description 17
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims abstract description 10
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 claims abstract description 9
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 8
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 239000002455 scale inhibitor Substances 0.000 claims description 3
- 229920000388 Polyphosphate Polymers 0.000 abstract description 3
- 239000003513 alkali Substances 0.000 abstract description 3
- 239000001205 polyphosphate Substances 0.000 abstract description 3
- 235000011176 polyphosphates Nutrition 0.000 abstract description 3
- 230000003449 preventive effect Effects 0.000 abstract description 2
- 241000976416 Isatis tinctoria subsp. canescens Species 0.000 abstract 1
- 150000001450 anions Chemical group 0.000 abstract 1
- 238000010979 pH adjustment Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 17
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 15
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 8
- 238000002347 injection Methods 0.000 description 7
- 239000007924 injection Substances 0.000 description 7
- 238000006114 decarboxylation reaction Methods 0.000 description 6
- 150000003839 salts Chemical class 0.000 description 6
- 239000012528 membrane Substances 0.000 description 5
- 235000011121 sodium hydroxide Nutrition 0.000 description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 4
- 239000002253 acid Substances 0.000 description 4
- 238000001556 precipitation Methods 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 229910019142 PO4 Inorganic materials 0.000 description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 3
- 239000010452 phosphate Substances 0.000 description 3
- 238000007664 blowing Methods 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 239000012466 permeate Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 238000005349 anion exchange Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 238000012733 comparative method Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000004065 semiconductor Substances 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 229910021642 ultra pure water Inorganic materials 0.000 description 1
- 239000012498 ultrapure water Substances 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Physical Water Treatments (AREA)
Abstract
Description
【発明の詳細な説明】
（産業上の利用分野）
本発明は、半導体工業用の超純水装置、ボイラー給水用
の純水装置等、逆浸透法とイオン交換法どを併用して純
水をつくる純水製造装置における溶存炭酸ガスの除去方
法【関する。Detailed Description of the Invention (Field of Industrial Application) The present invention is applicable to ultrapure water equipment for the semiconductor industry, pure water equipment for boiler water supply, etc., which uses reverse osmosis and ion exchange methods in combination to produce pure water. Method for removing dissolved carbon dioxide in pure water production equipment [Related].
（従来の技術）
半透膜を用いる逆浸透装置により水を処理する場合、カ
ルシウム、ナトリウム、塩素イオン等のイオン化された
水中溶存塩類、硬度成分：は８０〜９９％程度の高効率
で除去される。しかし水中に溶存する酸素、窒素、炭酸
ガス等のガス類は半透膜で殆んど除去されることなく膜
の透過水側に通り抜ける。(Prior art) When water is treated with a reverse osmosis device using a semipermeable membrane, ionized dissolved salts in water such as calcium, sodium, and chloride ions, and hardness components are removed with a high efficiency of about 80 to 99%. Ru. However, gases such as oxygen, nitrogen, and carbon dioxide dissolved in water are hardly removed by the semipermeable membrane and pass through to the permeate side of the membrane.
この透過水中の溶存炭酸ガスを減じて後続のイオン交換
装置の負担となることを少くするため、あるいは透過水
のＰＨを調整することを目的として、逆浸透装置による
処理前まだに後て空気吹込み式の充填塔すなわち脱炭酸
塔装置を併設して脱炭酸処理することが一般に行われて
いる。In order to reduce the amount of carbon dioxide dissolved in this permeated water and reduce the burden on the subsequent ion exchange equipment, or to adjust the pH of the permeated water, air is blown out before treatment with the reverse osmosis equipment. It is common practice to carry out decarboxylation treatment by installing a packed column, that is, a decarboxylation tower device.
（発明が解決しようとする問題点）
従来技術による逆浸透装置に組合わせる脱炭酸塔による
水中溶存炭酸ガスの除去方法は、空気吹込み方式のため
、空気中に通常３００ ｐｐｍ程度含まれている炭酸ガ
スの分圧により水中溶存炭酸ガスを稍々２ ｍｇ／ｌ
、普通には５ ｍｇ／／の残存濃度になる程度までしか
除去できない。この除去残の炭酸ガスはそのまま後続の
イオン交換装置に７１する負担となる。(Problems to be Solved by the Invention) The conventional method for removing carbon dioxide dissolved in water using a decarboxylation tower combined with a reverse osmosis device uses an air blowing method, so the amount of carbon dioxide gas normally contained in the air is about 300 ppm. Due to the partial pressure of carbon dioxide, dissolved carbon dioxide in water is reduced to 2 mg/l.
, which can normally only be removed to a residual concentration of 5 mg//. The remaining carbon dioxide remains as a burden on the subsequent ion exchange device.
本発明は従来技術の上記問題点を解決し、逆浸透処理後
にイオン交換処理を行う純水製造装置において、イオン
交換処理に先立って水中溶存炭酸ガスの高率除去を行う
ことを可能とする方法を提供することを目的とする。The present invention solves the above-mentioned problems of the prior art, and provides a method that makes it possible to remove carbon dioxide dissolved in water at a high rate prior to ion exchange treatment in a pure water production apparatus that performs ion exchange treatment after reverse osmosis treatment. The purpose is to provide
（問題点を解決するための手段）
前記目的は、本発明方法により、逆浸透装置を２段階に
分け、第１段階では炭酸ガスの透過を＃１容し、第２段
階でばＰＨ唇整により溶存炭酸ガスをイオン態に変換し
て逆浸透処理して除去することてより達成される。(Means for Solving the Problems) The above object is to divide the reverse osmosis device into two stages by the method of the present invention, in the first stage, the permeation of carbon dioxide gas is carried out at #1, and in the second stage, the PH lip adjustment is carried out. This is achieved by converting dissolved carbon dioxide into ionic form and removing it by reverse osmosis treatment.
すなわち、本発明の純水製造装置における溶存炭酸ガス
の除去方法は、構成としては、遊離炭酸ガスを含む原水
を逆浸透処理したのちイオン交換処理して純水を製造す
る装置において、逆浸透処理の第１段階目に原水中の硬
度成分を高率にて除去する逆浸透装置を用いて処理し、
その透過水にアルカリ剤を加えてＰＨをアルカリ側にし
、さらに必要な場合極く少量のスケール防止剤を配加し
、かくして重炭酸イオンおよび炭酸イオンに変化させた
炭酸ガス成分全２ニ２段階目の逆浸透装置を用いて除去
する処理を行うことを特徴とする。That is, the method for removing dissolved carbon dioxide in a pure water production apparatus of the present invention is configured such that raw water containing free carbon dioxide is subjected to reverse osmosis treatment and then ion exchange treatment to produce pure water. In the first stage, the raw water is treated using a reverse osmosis device that removes hard components at a high rate.
Add an alkaline agent to the permeated water to make the pH alkaline, and if necessary, add a very small amount of scale preventive agent, thus converting the carbon dioxide gas components into bicarbonate ions and carbonate ions in two steps. It is characterized by performing a removal process using a reverse osmosis device.
（作用）
本発明方法によると、遊離炭酸ガスを含む原水は少量の
硫酸、塩酸等の添加により弱酸性として先づ第１段階逆
浸透装置で、炭酸カル／ラム等のスケール析出を防止し
ながら一般塩類、硬度成分等が高率で除去される。この
透過水は硬度成分が相対的に少いものとなる。またこの
段階では溶存炭酸ガスについて第１段階逆浸透処理の前
または後で空気吹込み方式の脱炭酸塔で処理して炭酸ガ
ス成分ができるだけ除去でれるようにするのがよい。(Function) According to the method of the present invention, raw water containing free carbon dioxide is made weakly acidic by adding a small amount of sulfuric acid, hydrochloric acid, etc., and is first processed in the first stage reverse osmosis device, while preventing the precipitation of scales such as cal/rum carbonate. General salts, hard components, etc. are removed at a high rate. This permeated water has a relatively low hardness component. Further, at this stage, it is preferable that dissolved carbon dioxide gas be treated in an air-blowing decarboxylation tower before or after the first stage reverse osmosis treatment to remove as much carbon dioxide gas component as possible.
次に第１段階逆浸透装置の透過水に苛性ソーダ等のアル
カリ剤を添加しＰＨを弱アルカリ性とし、例えばＰＨを
８．５以上とすることにより、ガス類として水中に溶存
していた炭酸ガスは重炭酸イオン（ＨＣＯｘ−）または
炭酸イオン（Ｃｏ、 ）に変換されてイオン状態とな
る。これを第２段階逆浸透装置で処理すれば、前記の炭
酸ガス成分は他のイオンと同様ＶＣ９０％以上の高い除
去率で除去される。従って後工程のイオン交換処理装置
に対する炭酸ガスの負担は著しく減じられる０第２段階
逆浸透装置は、東しく株）製品番ＳＵ −４０ＯＲ、デ
ュポン社製品番ｌ３−９、Ｂ−１５等の合成膜で高いＰ
Ｈに適用でき、しかも高い塩排除率を持つものを使用す
れば有効である。この第２段階逆浸透処理においては、
入口水の第１段階逆浸透処理の透過水は硬度成分がよく
除去され１いるためＫ ＰＨを上げても炭酸力ルンウム
等の析出は起り難くなっているが、アルカリ剤を添加す
る他、必要に応じ極く少量のポリＩＪン酸塩等のスケー
ル防止剤を加えて第２段階逆浸透処理を行えば、スケー
ル析出の防止に一層有効となる。Next, an alkaline agent such as caustic soda is added to the permeated water of the first stage reverse osmosis device to make the pH slightly alkaline, for example, to 8.5 or higher, thereby removing carbon dioxide dissolved in the water as a gas. It is converted into bicarbonate ion (HCOx-) or carbonate ion (Co, ) and becomes ionic. If this is treated with a second-stage reverse osmosis device, the carbon dioxide component, like other ions, is removed at a high removal rate of VC90% or more. Therefore, the burden of carbon dioxide gas on the ion exchange treatment equipment in the subsequent process is significantly reduced.The second stage reverse osmosis equipment is manufactured by Toshiku Co., Ltd.) product number SU-40OR, DuPont Co., Ltd. product number 13-9, B-15, etc. High P in membrane
It is effective to use a material that can be applied to H and has a high salt rejection rate. In this second stage reverse osmosis treatment,
The hardness components of the permeated water from the first stage reverse osmosis treatment of the inlet water are well removed1, so even if the KPH is raised, precipitation of carbonate etc. is unlikely to occur, but in addition to adding an alkaline agent, it is necessary to If the second stage reverse osmosis treatment is performed by adding a very small amount of a scale inhibitor such as a poly-IJ phosphate, it will be more effective in preventing scale precipitation.
（実施例）
次に本発明方法を添付図を参照し実施％Ｉに即して具体
的に説明する。添は図は本発明方法を実施するフローの
１例を示す。(Example) Next, the method of the present invention will be specifically explained in accordance with the implementation %I with reference to the attached drawings. The attached figure shows an example of a flow for implementing the method of the present invention.
原水（１）は予め凝集沈澱法、濾過法等の通常水処理を
施して懸濁固形物を充分に除去した清浄水とし、固形物
が逆浸透装置の半透漠の目づまり原因となることを予防
する。The raw water (1) must be clean water that has been subjected to conventional water treatment such as coagulation sedimentation and filtration to sufficiently remove suspended solids, which can cause semi-clear clogging of reverse osmosis equipment. prevent.
この原水（１）は原水槽（２）に受入れられ、原水ポン
プ（３）により加圧送出され、カートリノンフィルター
（４）を通って精密濾過され、昇圧ポンプ（５）てより
逆浸透圧力に昇圧されて第１段階逆浸透装置（６）に向
って送られる。この送水系のカートリッジフィルター（
４）前に硫酸、塩酸等の酸を酸階逆浸透処理する。This raw water (1) is received in a raw water tank (2), pumped out under pressure by a raw water pump (3), microfiltered through a Cartolinon filter (4), and then raised to reverse osmosis pressure by a booster pump (5). It is pressurized and sent to the first stage reverse osmosis device (6). This water supply system cartridge filter (
4) Beforehand, perform reverse osmosis treatment using acids such as sulfuric acid and hydrochloric acid.
逆浸透装置（６）より一般塩類、硬！ｆｅ：分を高率に
除去でれた透過水（９）は−旦脱災酸塔α１に送られ、
また塩類が濃縮でれる側の原水は過大な濃縮を防止する
ため一部プロー水α刀として逆浸透装置（６）から放出
される。General salts, hard from reverse osmosis equipment (6)! The permeated water (9) from which fe: was removed at a high rate is sent to the acid removal tower α1,
In addition, a portion of the raw water from which salts are concentrated is discharged from the reverse osmosis device (6) as flow water to prevent excessive concentration.
脱炭酸塔ｏｃｔは充填層＠を持ち前記の透過水（９）が
充填層０内を流下する間にブロアー０３から吹込まれ上
昇する新鮮な空気と向流接触することにより炭酸ガスが
除去され脱炭酸水０Φとなって塔底に貯まる。The decarboxylation tower OCT has a packed bed @, and while the permeated water (9) flows down inside the packed bed 0, carbon dioxide gas is removed and decarbonized through countercurrent contact with the rising fresh air blown from the blower 03. Carbonated water becomes 0Φ and accumulates at the bottom of the tower.
次にこの脱炭酸水の送水系には第２段階逆浸透処理のだ
め苛性ソーダ等のアルカリ剤をアルカリ貯槽ａつから注
入ポンプＨにより注入してＰＨを８．５前後に調整して
残る溶存炭酸ガスを重炭酸イオンおよび炭酸イオンに変
化させ、またボＩＪ ＩＪン酸塩等のスケール防止剤の
少１を、その貯漕αηから注入ポンプ（ト）によシ配加
し、こうし第２段階逆浸透処理する。Next, an alkaline agent such as caustic soda is injected from the alkaline storage tank A into the water supply system of this decarbonated water for the second stage of reverse osmosis treatment, and the pH is adjusted to around 8.5, leaving behind dissolved carbon dioxide. is converted into bicarbonate ions and carbonate ions, and a small amount of a scale inhibitor such as phosphate is added from the reservoir αη to the injection pump (G), and thus the second step is carried out. Treat with reverse osmosis.
逆浸透装置（１）より重炭酸イオン、炭鼠イオンが除去
された透過水Ｑυは次のイオン交換塔（イ）に送ってイ
オン交換処理する。The permeated water Qυ from which bicarbonate ions and carbonate ions have been removed from the reverse osmosis device (1) is sent to the next ion exchange tower (a) for ion exchange treatment.
生じたイオン交換処理水＠は純水として処理水槽（財）
に貯められ、そこから目的用途に供給される。The resulting ion-exchange treated water @ is treated as pure water in the treated water tank (Foundation)
from which it is stored and supplied for its intended purpose.
逆浸透装置（イ）からも塩の濃、縮を防止するために一
定水素のブロー水（イ）が放出される。A constant amount of hydrogen blow water (A) is also discharged from the reverse osmosis device (A) to prevent salt concentration and condensation.
以下、本発明方法の実施例を数値により示す。Examples of the method of the present invention are shown below using numerical values.
図示フローの装置を使用して実施した例である。This is an example implemented using the apparatus shown in the illustrated flow.
その操作の概要は次のとおりである。The outline of the operation is as follows.
先づ原水に硫酸を注入しＰＨを下げ重炭酸イオン等を炭
酸ガスに変換するとともにスケール析出を防止しながら
第１段階逆浸透装置にて処理する。この透過水を脱炭酸
塔にて炭酸ガスをできるだけ除去する。こうして得られ
た脱炭酸水は水中に僅かの硬度成分と空気中炭酸ガス分
圧との平衡量程度の炭酸ガスを含む。First, sulfuric acid is injected into the raw water to lower the pH and convert bicarbonate ions etc. into carbon dioxide gas, and the raw water is treated in the first stage reverse osmosis device while preventing scale precipitation. This permeated water is passed through a decarbonation tower to remove as much carbon dioxide gas as possible. The decarbonated water thus obtained contains a small amount of hardness component in the water and an amount of carbon dioxide gas that is in balance with the partial pressure of carbon dioxide gas in the air.
これに苛性ソーダと少量のポリリン酸塩を注入しＰＨを
８．５程度に調整し炭酸ガスを重炭酸イオンおよび炭酸
イオンに変換し第２段階逆浸透装置にて処理する。第２
段階逆浸透装置の透過水は、この装置の入口側で炭酸ガ
スが重炭酸ガスンおよび炭酸イオンに変換されているた
めこれらがイオンとして高い除去率で除去され、後続の
イオン交換装置に対する炭酸ガス成分の負担が軽減され
る。Caustic soda and a small amount of polyphosphate are injected into this to adjust the pH to about 8.5, and carbon dioxide gas is converted into bicarbonate ions and carbonate ions, which are then treated in a second stage reverse osmosis device. Second
In the permeated water of the staged reverse osmosis device, carbon dioxide gas is converted into bicarbonate gas and carbonate ions at the inlet side of this device, so these are removed as ions at a high removal rate, and the carbon dioxide components are sent to the subsequent ion exchange device. The burden of this will be reduced.
図中、符号（４）０３１ （Ｃ）■）■）（月で指摘の
各経過点における水質分析値を次表に示す。表の水質数
値の単位はすべてｐｐｍ ＣａＣ０１である。ＰＨは２
５℃の値である。比較のため、本発明と異り第２段階逆
浸透処理前に苛性ソーダ、ポＩＪ ＩＪン酸塩の注入を
行わずに脱炭酸塔出口水を直接第２段階逆浸透装置で処
理した場合の処理水の水質数値を最終列に併記した。In the figure, code (4) 031 (C)■)■) (The following table shows the water quality analysis values at each point in the month. All water quality values in the table are in units of ppm CaC01.PH is 2
The value is at 5°C. For comparison, unlike the present invention, the decarboxylation tower outlet water was directly treated in the second stage reverse osmosis device without injecting caustic soda or polyphosphate before the second stage reverse osmosis treatment. Water quality values are also listed in the last column.
表 本発明実施例の水質（単位： ｐｐｍ ＣａＣ０
＋）１ 経過点Ａ：原水
経過点Ｂ：第１段階逆浸透装置人ロ水
径過点Ｃ：第１段階逆浸透装置出ロ透過水経過点Ｄ＝脱
炭酸塔出ロ脱炭酸水
２経過点Ｅ：第２段階逆浸透装置入ロ水経過点Ｆ：第１
段階逆浸透装置出口透過水２ 第１段階逆浸透装置（６
）での処理条件入口′側硫酸注入号： ４４．１ ｐｐ
ｍ、半透膜二乗しく株）品番ＳＵ ４０［］Ｒ、運転圧
カニ １５ ｈｉ乙層Ｇ１回収率ニア５％。Table: Water quality in Examples of the present invention (unit: ppm CaC0
+) 1 Progress point A: Raw water progress point B: 1st stage reverse osmosis equipment Water diameter passing point C: 1st stage reverse osmosis equipment exit permeate water progress point D = Decarbonation tower exit decarbonated water 2 progress Point E: 2nd stage reverse osmosis equipment water transition point F: 1st
Stage reverse osmosis device outlet permeated water 2 1st stage reverse osmosis device (6
) Treatment conditions Inlet' side sulfuric acid injection number: 44.1 pp
m, semi-permeable membrane square Shikushi Co., Ltd.) Product number SU 40[]R, operating pressure crab 15 hi layer Otsu G1 recovery rate near 5%.
６ 第２段階逆浸透装置（１）での処理条件入ロ測苛性
ソーダ注入量： ５ ｐｐｍ、入口測ボＩＪ ＩＪン酸
塩注入量： ５ｐｐｍ、半透＠二乗しく株）品番ＳＵ
４００Ｉ’ｔ 、運転圧カニ１４．５を鉤Ｇ１回収率：
８０チ。〕
（発明の効果）
本発明方法によると、遊離災酸ガスを含む原浸透装置に
より高率で除去して、後続のイオン交換塔に対する負荷
アニオン交換１を比較方法の場合の７．６ ｐｐｍ Ｃ
ａＣＯ５から２．０ ｐｐｍ Ｃａ００＋ にすなわち
２６．６係に効果的に低減することができる。6 Processing conditions in the second stage reverse osmosis device (1) Input amount of caustic soda injection: 5 ppm, Inlet measurement port IJ IJ phosphate injection amount: 5 ppm, Semi-permeable @Square Shikaku Co., Ltd.) Product number SU
400 I't, operating pressure crab 14.5 hook G1 recovery rate:
80 chi. (Effects of the Invention) According to the method of the present invention, the free acid gas is removed at a high rate by the original permeation device, and the load anion exchange 1 to the subsequent ion exchange column is reduced to 7.6 ppm C compared to the comparative method.
It can be effectively reduced from aCO5 to 2.0 ppm Ca00+, that is, by a factor of 26.6.
添付図は本発明方法を実施するフローの１例を示す図で
ある。
（１）・・原水、（２）・・厘水槽、（３）・・原水ポ
ンプ、（４）・・カートリッジフィルター、（５）・・
昇圧ポンプ、（６）・・第１段階逆浸透装置、（７）・
・酸貯槽、（８）・・注入ポンプ、（９）・・透過水、
ａ４・・脱炭酸塔、（１１）・・ブロー水、（２）・・
充填、智、ｑ３・・ブロアー、ｑ４・・脱炭酸水、αＱ
・・アルカリ貯槽、αＱ・・注入ポンプ、Ｑ７１・・貯
１り、（至）・・注入ポンプ、０１・・加圧ポンプ、・
（１）・争第２段階逆浸透装置、Ｑυ・・透過水、■・
・イオン交換塔、（１）・・イオン交換処理水、ｅ卓・
・処理水槽、曽・・ブロー水。The attached figure is a diagram showing an example of a flow for implementing the method of the present invention. (1) Raw water, (2) Water tank, (3) Raw water pump, (4) Cartridge filter, (5)
Boosting pump, (6)...1st stage reverse osmosis device, (7)...
・Acid storage tank, (8)... Injection pump, (9)... Permeated water,
a4...Decarbonation tower, (11)...Blow water, (2)...
Filling, wisdom, q3... blower, q4... decarbonated water, αQ
・・Alkali storage tank, αQ・・Injection pump, Q71・・Storage 1, (to)・・Injection pump, 01・・・Pressure pump,・
(1)・Second stage reverse osmosis equipment, Qυ・Permeated water, ■・
・Ion exchange tower, (1)...Ion exchange treated water, e-table・
・Treatment water tank, So...Blow water.
Claims (1)
換処理して純水を製造する装置において、逆浸透処理の
第１段階目に原水中の硬度成分を高率にて除去する逆浸
透装置を用いて処理し、その透過水にアルカリ剤を加え
てＰＨをアルカリ側にし、さらに必要な場合極く少量の
スケール防止剤を配加し、かくして重炭酸イオンおよび
炭酸イオンに変化させた炭酸ガス成分を第２段階目の逆
浸透装置を用いて除去する処理を行うことを特徴とする
純水製造装置における溶存炭酸ガスの除去方法。In a device that produces pure water by performing reverse osmosis treatment on raw water containing free carbon dioxide and then ion exchange treatment, the first stage of reverse osmosis treatment is a reverse osmosis device that removes hard components in the raw water at a high rate. The permeated water is treated with an alkaline agent to make the pH alkaline, and if necessary, a very small amount of scale inhibitor is added, thus converting the carbon dioxide components into bicarbonate ions and carbonate ions. A method for removing dissolved carbon dioxide in a pure water production device, the method comprising performing a process of removing carbon dioxide using a second-stage reverse osmosis device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61172135A JPH0790215B2 (en) | 1986-07-21 | 1986-07-21 | Method for removing dissolved carbon dioxide gas in pure water production equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61172135A JPH0790215B2 (en) | 1986-07-21 | 1986-07-21 | Method for removing dissolved carbon dioxide gas in pure water production equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6328486A true JPS6328486A (en) | 1988-02-06 |
| JPH0790215B2 JPH0790215B2 (en) | 1995-10-04 |
Family
ID=15936215
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61172135A Expired - Lifetime JPH0790215B2 (en) | 1986-07-21 | 1986-07-21 | Method for removing dissolved carbon dioxide gas in pure water production equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0790215B2 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6336890A (en) * | 1986-07-28 | 1988-02-17 | Kurita Water Ind Ltd | Apparatus for producing high-purity water |
| JPH01231988A (en) * | 1988-03-14 | 1989-09-18 | Japan Organo Co Ltd | Two-step treatment with reverse osmosis membrane |
| JP2007117808A (en) * | 2005-10-25 | 2007-05-17 | Kurita Water Ind Ltd | Method and apparatus for treating carbonic acid and ammonia-containing drain |
| JP2013022521A (en) * | 2011-07-21 | 2013-02-04 | Jfe Steel Corp | Pure water producing facility and method of elongating service life of ion-exchange resin |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7771599B1 (en) * | 2009-03-09 | 2010-08-10 | Doosan Hydro Technology, Inc. | System and method for using carbon dioxide sequestered from seawater in the remineralization of process water |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS614591A (en) * | 1984-06-04 | 1986-01-10 | アローヘツド、インダストリアル、ウオーター、インコーポレイテツド | Reverse osmosis system |
| JPS62110795A (en) * | 1985-11-06 | 1987-05-21 | Kurita Water Ind Ltd | Device for producing high-purity water |
-
1986
- 1986-07-21 JP JP61172135A patent/JPH0790215B2/en not_active Expired - Lifetime
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS614591A (en) * | 1984-06-04 | 1986-01-10 | アローヘツド、インダストリアル、ウオーター、インコーポレイテツド | Reverse osmosis system |
| JPS62110795A (en) * | 1985-11-06 | 1987-05-21 | Kurita Water Ind Ltd | Device for producing high-purity water |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6336890A (en) * | 1986-07-28 | 1988-02-17 | Kurita Water Ind Ltd | Apparatus for producing high-purity water |
| JPH01231988A (en) * | 1988-03-14 | 1989-09-18 | Japan Organo Co Ltd | Two-step treatment with reverse osmosis membrane |
| JP2007117808A (en) * | 2005-10-25 | 2007-05-17 | Kurita Water Ind Ltd | Method and apparatus for treating carbonic acid and ammonia-containing drain |
| JP2013022521A (en) * | 2011-07-21 | 2013-02-04 | Jfe Steel Corp | Pure water producing facility and method of elongating service life of ion-exchange resin |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0790215B2 (en) | 1995-10-04 |
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