JPH0588693U - Waste liquid boric acid processor - Google Patents
Waste liquid boric acid processorInfo
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- JPH0588693U JPH0588693U JP3289392U JP3289392U JPH0588693U JP H0588693 U JPH0588693 U JP H0588693U JP 3289392 U JP3289392 U JP 3289392U JP 3289392 U JP3289392 U JP 3289392U JP H0588693 U JPH0588693 U JP H0588693U
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- reverse osmosis
- osmosis membrane
- waste liquid
- boric acid
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Abstract
(57)【要約】
【目的】 廃棄する濃縮液へのほう酸の移行量の低減を
図り、ほう酸回収率を向上させる。
【構成】 処理廃液１１Ａが供給される循環タンク１２
と、循環タンク１２に接続する循環通路に直列三段に介
装された第１〜第３段逆浸透膜モジュール１４〜１６
と、循環タンク１２から第１段逆浸透膜モジュール１４
へ処理廃液を送給する高圧供給ポンプ１７と、高圧供給
ポンプ１７と第１段逆浸透膜モジュール１４との間に介
装され処理廃液１１中の粒状不純物を除去する限外濾過
モジュール１８と、第３段逆浸透膜モジュール１６から
の濃縮廃液を固化処理する固化装置１９とを具備し、第
１段逆浸透膜モジュール１４を塩排除率の高い逆浸透膜
とし、第２、第３段逆浸透膜モジュール１５、１６の逆
浸透膜の塩排除率を第１段逆浸透膜モジュールの塩排除
率より幾分低い逆浸透膜とする。
(57) [Abstract] [Purpose] To reduce the amount of boric acid transferred to the concentrated liquid to be discarded and improve the boric acid recovery rate. [Structure] Circulation tank 12 to which processing waste liquid 11A is supplied
And the first to third stage reverse osmosis membrane modules 14 to 16 installed in three stages in series in the circulation passage connected to the circulation tank 12.
And the circulation tank 12 to the first stage reverse osmosis membrane module 14
A high-pressure supply pump 17 for supplying the treatment waste liquid to the ultra-high-pressure supply pump 17, and an ultrafiltration module 18 interposed between the high-pressure supply pump 17 and the first-stage reverse osmosis membrane module 14 for removing particulate impurities in the treatment waste liquid 11. A solidification device 19 for solidifying the concentrated waste liquid from the third-stage reverse osmosis membrane module 16, and the first-stage reverse osmosis membrane module 14 is a reverse osmosis membrane having a high salt removal rate. The reverse osmosis membranes of the osmosis membrane modules 15 and 16 have a salt rejection rate that is somewhat lower than that of the first-stage reverse osmosis membrane module.
Description
【０００１】[0001]
本考案はＰＷＲ原子力プラント等の処理設備として用いられる廃液ほう酸処理 装置に関する。 The present invention relates to a waste liquid boric acid treatment apparatus used as treatment equipment for a PWR nuclear power plant and the like.
【０００２】[0002]
加圧水型動力炉（ＰＷＲ）プラントにおける液体廃棄物処理システム又は使用 済燃料ピット水、ほう酸タンク水等の浄化システム等では処理廃液からほう酸を 回収して再使用しており、この従来技術の一例を図２に示す。 In a liquid waste treatment system or a purification system for spent fuel pit water, boric acid tank water, etc. in a pressurized water power reactor (PWR) plant, boric acid is recovered from the processing waste liquid and reused. An example of this conventional technology As shown in FIG.
【０００３】 従来の廃液ほう酸処理装置は、複数の逆浸透膜モジュールを直列に配して処理 廃液を循環させてほう酸を回収すると共に不純物を処理するものである。 すなわち、図２に示すように、従来の廃液ほう酸処理装置は処理廃液１１を循 環に供する循環タンク１２と、この循環タンク１２に接続する循環通路１３に直 列三段に介装された第１〜第３段逆浸透膜モジュール１４〜１６と、前記循環タ ンク１２から第１段逆浸透膜モジュール１４へ処理廃液を送給する高圧供給ポン プ１７と、この高圧供給ポンプ１７と第１段逆浸透膜モジュール１４との間に介 装され処理廃液１１中の粒状不純物を除去する限外濾過モジュール１８と、第３ 段逆浸透膜モジュール１６からの濃縮廃液を固化処理する固化装置１９とを具備 するものである。In the conventional waste liquid boric acid treatment apparatus, a plurality of reverse osmosis membrane modules are arranged in series to circulate the treatment waste liquid to recover boric acid and treat impurities. That is, as shown in FIG. 2, in the conventional waste liquid boric acid treatment apparatus, a circulation tank 12 for circulating the treatment waste liquid 11 and a circulation passage 13 connected to the circulation tank 12 are installed in three stages in series. First to third stage reverse osmosis membrane modules 14 to 16, a high pressure supply pump 17 for supplying the processing waste liquid from the circulation tank 12 to the first stage reverse osmosis membrane module 14, the high pressure supply pump 17 and the first An ultrafiltration module 18 which is interposed between the third-stage reverse osmosis membrane module 14 and removes particulate impurities in the treatment waste liquid 11, and a solidification device 19 which solidifies the concentrated waste liquid from the third-stage reverse osmosis membrane module 16. It is equipped with.
【０００４】 この廃液ほう酸処理装置を用いて処理廃液１１を処理するに際しては、先ず循 環タンク１２内の処理廃液１１を、高圧供給ポンプ１７により限外濾過モジュー ル１８に送り、ここで粒子状不純物を取り除いた後、第１段逆浸透膜モジュール １４へ供給する。When treating the treatment waste liquid 11 using this waste liquid boric acid treatment apparatus, first, the treatment waste liquid 11 in the circulation tank 12 is sent to the ultrafiltration module 18 by the high-pressure supply pump 17, where it is particulated. After removing impurities, it is supplied to the first-stage reverse osmosis membrane module 14.
【０００５】 この第１段逆浸透膜モジュール１４からの透過液２０Ａは回収ほう酸として再 使用する。一方、第１段逆浸透膜モジュール１４からの濃縮液２１Ａは第２段逆 浸透膜モジュール１５に供給し透過液２０Ｂと濃縮液２１Ｂとに分離する。この 内の濃縮液２１Ｂは第３段逆浸透膜モジュール１６に送られ更に濃縮され、濃縮 液２１Ｃとして濃縮液側圧力調整弁２２を介して固化装置１９に送り、ここでＳ ｉＯ2 等の不純物が固化される。The permeate 20A from the first-stage reverse osmosis membrane module 14 is reused as recovered boric acid. On the other hand, the concentrate 21A from the first-stage reverse osmosis membrane module 14 is supplied to the second-stage reverse osmosis membrane module 15 and separated into a permeate 20B and a concentrate 21B. The concentrated liquid 21B therein is sent to the third-stage reverse osmosis membrane module 16 to be further concentrated, and is sent as a concentrated liquid 21C to the solidification device 19 through the concentrated liquid side pressure adjusting valve 22 where impurities such as SiO 2 are added. Is solidified.
【０００６】 一方、第２段逆浸透膜モジュール１５及び第３段逆浸透膜モジュール１６から の各々の透過液２０Ｂ，２０Ｃは循環タンク１２に戻され、再び循環に供される 。On the other hand, the permeated liquids 20B and 20C from the second-stage reverse osmosis membrane module 15 and the third-stage reverse osmosis membrane module 16 are returned to the circulation tank 12 and again provided for circulation.
【０００７】[0007]
上述した従来の廃液ほう酸処理装置においては、直列に配した第１段〜第３段 逆浸透膜モジュールとして塩排除率がいずれも同一のモジュール、例えばＳｉＯ 2 等の不純物除去性能の向上を重視して逆浸透膜モジュールを選定した場合、必 然的にほう酸透過性能も低下し、循環タンク１２に戻される第２段、第３段逆浸 透膜モジュール１５，１６からの透過液２０Ｂ，２０Ｃに移行するほう酸量が低 下する。 この結果、廃棄される濃縮液２１Ｃへのほう酸移行量が増大し、回収装置とし てのほう酸回収率が低下するという問題がある。 In the conventional waste liquid boric acid treatment apparatus described above, the first to third stage reverse osmosis membrane modules arranged in series have the same salt removal rate, for example, SiO. 2 When a reverse osmosis membrane module is selected with an emphasis on improving the performance of removing impurities such as, the boric acid permeation performance is inevitably lowered and the second and third stage reverse osmosis membrane modules 15 are returned to the circulation tank 12. , 16 from the permeated liquids 20B and 20C is reduced. As a result, there is a problem that the amount of boric acid transferred to the concentrated liquid 21C to be discarded increases, and the boric acid recovery rate as a recovery device decreases.
【０００８】 一方、塩排除率の幾分低い逆浸透膜モジュールを選定した場合、回収装置とし てのほう酸回収率は向上するものの、ＳｉＯ2 等の不純物除去性能も低下するた め、一次系水質管理の基準値を満足する透過回収液を得ることが困難となる。On the other hand, when a reverse osmosis membrane module having a somewhat low salt removal rate is selected, the recovery rate of boric acid as a recovery device is improved, but the performance of removing impurities such as SiO 2 is also reduced, so that the primary system water quality is reduced. It becomes difficult to obtain a permeate recovery liquid that satisfies the control standard value.
【０００９】 すなわち、従来の廃液ほう酸処理装置においては、ＳｉＯ2 等の不純物の除去 性能の向上とほう酸回収率の向上とが相反する関係にあるので、これらを満足す ることができないという問題がある。That is, in the conventional waste liquid boric acid treatment apparatus, there is a contradictory relationship between the improvement of the removal performance of impurities such as SiO 2 and the improvement of the boric acid recovery rate, and therefore there is a problem that these cannot be satisfied. is there.
【００１０】[0010]
前記課題を達成する本考案に係る廃液ほう酸処理装置は、複数の逆浸透膜モジ ュールを直列に配設し、第１段逆浸透膜モジュールの透過液を回収すると共に第 ２段逆浸透膜モジュール以降の透過液を循環タンクに戻すことで廃液中のほう酸 を回収し、当該廃液中の不純物を除去する廃液ほう酸処理装置において、各段の 逆浸透膜モジュールの塩排除率が異なることを特徴とする。 In the waste liquid boric acid treatment apparatus according to the present invention, which achieves the above-mentioned object, a plurality of reverse osmosis membrane modules are arranged in series to collect the permeate of the first stage reverse osmosis membrane module and the second stage reverse osmosis membrane module. In the waste liquid boric acid treatment equipment that recovers the boric acid in the waste liquid by returning the permeated liquid to the circulation tank and removes the impurities in the waste liquid after that, the reverse osmosis membrane module at each stage is characterized by different salt removal rates. To do.
【００１１】[0011]
前記構成において、処理廃液中のほう酸を回収する第１段逆浸透膜モジュール として、塩排除率の高いモジュールを使用することで不純物除去性能を向上させ る。また第２、第３段逆浸透膜モジュールとして第１段逆浸透膜モジュールより 塩排除率の幾分低い逆浸透膜モジュールを使用することで濃縮廃液へのほう酸の 移行量を低減させる。 この結果、廃棄する濃縮液へのほう酸の移行量の低減を図ることができ、処理 システムとしてのほう酸回収率が向上する。 In the above structure, the impurity removal performance is improved by using a module having a high salt removal rate as the first-stage reverse osmosis membrane module for recovering boric acid in the treatment waste liquid. Also, by using a reverse osmosis membrane module having a slightly lower salt rejection than the first stage reverse osmosis membrane module as the second and third stage reverse osmosis membrane module, the transfer amount of boric acid to the concentrated waste liquid is reduced. As a result, the amount of boric acid transferred to the concentrated liquid to be discarded can be reduced, and the boric acid recovery rate as a processing system is improved.
【００１２】[0012]
以下、本考案に係る廃液ほう酸処理装置の好適な実施例を説明する。 図１は本実施例に係る廃液ほう酸処理装置の概略図である。 Hereinafter, preferred embodiments of the waste liquid boric acid treatment apparatus according to the present invention will be described. FIG. 1 is a schematic diagram of a waste liquid boric acid processing apparatus according to this embodiment.
【００１３】 同図に示すように、本実施例に係る廃液ほう酸処理装置は処理廃液１１Ａを循 環に供す循環タンク１２と、この循環タンク１２に接続する循環通路１３に直列 に複数段（本実施例では三段）に介装された第１〜第３段逆浸透膜モジュール１ ４〜１６と、前記循環タンク１２から第１段逆浸透膜モジュール１４へ処理廃液 を送給する高圧供給ポンプ１７と、この高圧供給ポンプ１７と第１段逆浸透膜モ ジュール１４との間に介装され処理廃液１１中の粒状不純物を除去する限外濾過 モジュール１８と、第３段逆浸透膜モジュール１６からの濃縮廃液を固化処理す る固化装置１９とを具備すると共に、前記第１段逆浸透膜モジュール１４を塩排 除率の高い逆浸透膜とし、第２、第３逆浸透膜モジュール１５、１６の逆浸透膜 の塩排除率を第１逆浸透膜モジュール１４の塩排除率より幾分低い逆浸透膜とし 、第１段逆浸透膜モジュール１４と第２及び第３段逆浸透膜モジュール１５、１ ６との塩排除率を異なるものとしている。As shown in FIG. 1, the waste liquid boric acid treatment apparatus according to the present embodiment has a plurality of stages (mains) in series in a circulation tank 12 for circulating the treatment waste liquid 11 A and a circulation passage 13 connected to the circulation tank 12. First to third stage reverse osmosis membrane modules 14 to 16 interposed in three stages in the embodiment, and a high-pressure supply pump for supplying the processing waste liquid from the circulation tank 12 to the first stage reverse osmosis membrane module 14. 17, an ultrafiltration module 18 that is interposed between the high-pressure supply pump 17 and the first-stage reverse osmosis membrane module 14 to remove particulate impurities in the treatment waste liquid 11, and a third-stage reverse osmosis membrane module 16 And a solidification device 19 for solidifying the concentrated waste liquid from the above, the first-stage reverse osmosis membrane module 14 is a reverse osmosis membrane having a high salt removal rate, and second and third reverse osmosis membrane modules 15 are provided. 16 reverse osmosis membranes A salt of the first-stage reverse osmosis membrane module 14 and the second and third-stage reverse osmosis membrane modules 15, 16 is used as a reverse osmosis membrane having a salt rejection rate somewhat lower than the salt rejection rate of the first reverse osmosis membrane module 14. Exclusion rates are different.
【００１４】 前記逆浸透膜としては、流量値（供給液流量／濃縮液流量）が2.４の場合、「 表−１」に示す塩排除率を有する逆浸透膜を使用し、塩排除率の高い第１段逆浸 透膜モジュール１４の流量比を2.２とすると共に、塩排除率の幾分低い第２、第 ３段逆浸透膜モジュール１５、１６の流量比を3.７として処理を行った。As the reverse osmosis membrane, when the flow rate value (supply liquid flow rate / concentrated liquid flow rate) is 2.4, a reverse osmosis membrane having a salt rejection rate shown in “Table-1” is used. The flow rate ratio of the first-stage reverse osmosis membrane module 14 having a high value is set to 2.2, and the flow rate ratio of the second and third-stage reverse osmosis membrane modules 15 and 16 having a slightly lower salt removal rate is set to 3.7. Processed.
【００１５】[0015]
【表１】 [Table 1]
【００１６】 前記構成の廃液ほう酸処理装置において、循環タンク１２に処理廃液１１Ａを 流入してほう酸の回収を行う場合、高圧供給ポンプ１７により限外濾過モジュー ル１８に循環タンク１２からの処理廃液１１Ｂを送り、ここで粒子状不純物を取 り除く。そして塩排除率が高い第１段逆浸透膜モジュール１４によって、ほう酸 を含有する透過液２０Ａと濃縮液２１Ａとに分離する。次いで、濃縮液２１Ａは 第２、第３段逆浸透膜モジュール１５、１６に送られて分離されるが、第２、第 ３段逆浸透膜モジュール１５、１６の塩排除率が第１段逆浸透膜モジュール１４ よりも低いので濃縮液２１Ｂ，２１Ｃ中へのほう酸の移行が低減される。In the waste liquid boric acid treatment apparatus having the above-described configuration, when the treatment waste liquid 11A is introduced into the circulation tank 12 to recover boric acid, the high-pressure supply pump 17 causes the ultrafiltration module 18 to process waste liquid 11B from the circulation tank 12. To remove particulate impurities. Then, the permeate 20A containing boric acid and the concentrate 21A are separated by the first-stage reverse osmosis membrane module 14 having a high salt removal rate. Next, the concentrated liquid 21A is sent to the second and third stage reverse osmosis membrane modules 15 and 16 and separated, but the salt removal rate of the second and third stage reverse osmosis membrane modules 15 and 16 is the first stage reverse. Since it is lower than that of the osmosis membrane module 14, the transfer of boric acid into the concentrated solutions 21B and 21C is reduced.
【００１７】 例えば、循環タンク１２に供給する処理廃液１１Ａの組成をほう素１０００ｐ ｐｍ，ＳｉＯ2 ６ｐｐｍとし、流量1.７ｍ3 ／ｈで流入した場合には、９０％の ほう素を回収した場合の回収液水質はＳｉＯ2 ：0.４６ｐｐｍとなり、一次系水 質管理の基準値（0.５ｐｐｍ以下）を満足することを確認した。For example, when the composition of the treatment waste liquid 11A supplied to the circulation tank 12 is 1000 ppm of boron and 6 ppm of SiO 2 , and the flow rate is 1.7 m 3 / h, when 90% of boron is recovered. It was confirmed that the water quality of the recovered liquid was SiO 2 : 0.46 ppm, which satisfied the standard value (0.5 ppm or less) of the primary system water quality control.
【００１８】 尚、上記処理時の各処理液（処理廃液１１Ａ，１１Ｂ，透過液２０Ａ，濃縮液 ２１Ｃ）の流量、ほう素濃度及びＳｉＯ2 濃度を下記「表２」に示す。The flow rate, boron concentration and SiO 2 concentration of each treatment liquid (treatment waste liquid 11A, 11B, permeate liquid 20A, concentrated liquid 21C) at the time of the above treatment are shown in "Table 2" below.
【００１９】[0019]
【表２】 [Table 2]
【００２０】 一方、従来技術で示した廃液ほう酸処理装置の第１〜第３段逆浸透膜モジュー ルを上記実施例の第２、第３段逆浸透膜モジュールとして使用したのと同様の塩 排除率の低いものとした場合、ほう素濃度１０００ｐｐｍ、ＳｉＯ2 濃度６ｐｐ ｍの処理廃液１１Ａを用いて９０％のほう素を回収した場合の回収液水質はＳｉ Ｏ2 ：0.８５ｐｐｍとなり、一次系水質管理の基準値を満足することができなか った。On the other hand, the same salt exclusion as the first to third stage reverse osmosis membrane modules of the waste liquid boric acid treatment apparatus shown in the prior art are used as the second and third stage reverse osmosis membrane modules of the above-mentioned embodiment. When the rate is low, when 90% of boron is recovered using the treated waste liquid 11A having a boron concentration of 1000 ppm and a SiO 2 concentration of 6 ppm, the water quality of the recovered liquid is SiO 2 : 0.85 ppm. It was not possible to meet the standard value for water quality management.
【００２１】 このように、逆浸透膜モジュールを直列に複数段組み合わせた廃液ほう酸処理 装置において、各段に塩排除率の異なる逆浸透膜モジュールを使用することによ り、透過回収液のほう酸回収率を高めることができるため、ほう素損失補填のた めＰＷＲ原子力プラント運転上補充されるべきほう酸量を低減できる。又、ほう 酸回収率の向上に伴い、濃縮廃液へのほう酸移行量を低減できるため、廃棄物発 生量を低減できる。As described above, in the waste liquid boric acid treatment apparatus in which the reverse osmosis membrane modules are combined in series in plural stages, by using the reverse osmosis membrane modules having different salt removal rates in each stage, the boric acid recovery of the permeation recovery liquid is performed. Since the rate can be increased, it is possible to reduce the amount of boric acid to be replenished during the operation of the PWR nuclear power plant to compensate for the boron loss. In addition, as the boric acid recovery rate improves, the amount of boric acid transferred to the concentrated waste liquid can be reduced, so the amount of waste generated can be reduced.
【００２２】 尚、各段の逆浸透膜モジュールの機能分担として、第１段逆浸透膜モジュール にほう酸回収率向上機能、第２、第３段逆浸透膜モジュールに不純物除性能向上 機能を受け持たせた場合もシステム全体としては同様の効果が期待できる。As functions of the reverse osmosis membrane module of each stage, the first-stage reverse osmosis membrane module has a function of improving a boric acid recovery rate, and the second and third-stage reverse osmosis membrane modules have a function of improving an impurity removal performance. Even if it is turned on, the same effect can be expected as the entire system.
【００２３】[0023]
以上、実施例と共に説明したように本考案に係る廃液ほう酸処理装置は、逆浸 透膜モジュールを直列に複数段組み合わせた廃液ほう酸処理装置において、各段 に塩排除率の異なる逆浸透膜モジュールを使用することにより、不純物除去性能 の向上とほう酸回収性能の向上を同時に満足することができ、濃縮廃液へのほう 酸移行量の低減が図られ、ＰＷＲ原子力プラント運転上補充されるべきほう酸の 低減及び廃棄物発生量低減の効果がある。 As described above with reference to the embodiments, the waste liquid boric acid treatment apparatus according to the present invention is a waste liquid boric acid treatment apparatus in which a plurality of reverse osmosis membrane modules are combined in series. By using it, the improvement of impurity removal performance and the improvement of boric acid recovery performance can be satisfied at the same time, the transfer amount of boric acid to the concentrated waste liquid can be reduced, and the boric acid to be replenished during the operation of the PWR nuclear power plant can be reduced. It also has the effect of reducing the amount of waste generated.
【図１】本実施例に係る廃液ほう酸処理装置の概略図で
ある。FIG. 1 is a schematic view of a waste liquid boric acid treatment apparatus according to this embodiment.
【図２】従来技術に係る廃液ほう酸処理装置の概略図で
ある。FIG. 2 is a schematic diagram of a waste liquid boric acid treatment apparatus according to a conventional technique.
１１Ａ，１１Ｂ 処理廃液 １２ 循環タンク １３ 循環通路 １４ 第１段逆浸透膜モジュール １５ 第２段逆浸透膜モジュール １６ 第３段逆浸透膜モジュール １７ 高圧供給ポンプ １８ 限外濾過モジュール １９ 固化装置 11A, 11B Treatment waste liquid 12 Circulation tank 13 Circulation passage 14 First stage reverse osmosis membrane module 15 Second stage reverse osmosis membrane module 16 Third stage reverse osmosis membrane module 17 High pressure supply pump 18 Ultrafiltration module 19 Solidifying device
Claims (1)
し、第１段逆浸透膜モジュールの透過液を回収すると共
に第２段逆浸透膜モジュール以降の透過液を循環タンク
に戻すことで廃液中のほう酸を回収し、当該廃液中の不
純物を除去する廃液ほう酸処理装置において、各段の逆
浸透膜モジュールの塩排除率が異なることを特徴とする
廃液ほう酸処理装置。1. A plurality of reverse osmosis membrane modules are arranged in series to collect the permeate of the first-stage reverse osmosis membrane module and return the permeate after the second-stage reverse osmosis membrane module to a circulation tank. In a waste liquid boric acid treatment device for recovering boric acid in a waste liquid and removing impurities in the waste liquid, the waste liquid boric acid treatment device is characterized in that the reverse osmosis membrane module in each stage has a different salt rejection rate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3289392U JPH0588693U (en) | 1992-05-19 | 1992-05-19 | Waste liquid boric acid processor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3289392U JPH0588693U (en) | 1992-05-19 | 1992-05-19 | Waste liquid boric acid processor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0588693U true JPH0588693U (en) | 1993-12-03 |
Family
ID=12371572
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3289392U Pending JPH0588693U (en) | 1992-05-19 | 1992-05-19 | Waste liquid boric acid processor |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0588693U (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52128888A (en) * | 1976-04-22 | 1977-10-28 | Ebara Infilco Co Ltd | Separation by membrane |
| JPS5358974A (en) * | 1976-11-10 | 1978-05-27 | Ebara Infilco Co Ltd | Separating method by use of membrane |
| JPS55109406A (en) * | 1979-02-14 | 1980-08-22 | Toray Ind Inc | Liquid separating system |
| JPS6332396A (en) * | 1986-07-25 | 1988-02-12 | 株式会社東芝 | Gas recombination facility |
| JPS6353499A (en) * | 1986-08-22 | 1988-03-07 | 科学技術庁原子力局長 | Method of processing radioactive waste liquor |
| JPH0461983A (en) * | 1990-06-25 | 1992-02-27 | Kawasaki Heavy Ind Ltd | Method and apparatus for treating salt-containing water |
-
1992
- 1992-05-19 JP JP3289392U patent/JPH0588693U/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52128888A (en) * | 1976-04-22 | 1977-10-28 | Ebara Infilco Co Ltd | Separation by membrane |
| JPS5358974A (en) * | 1976-11-10 | 1978-05-27 | Ebara Infilco Co Ltd | Separating method by use of membrane |
| JPS55109406A (en) * | 1979-02-14 | 1980-08-22 | Toray Ind Inc | Liquid separating system |
| JPS6332396A (en) * | 1986-07-25 | 1988-02-12 | 株式会社東芝 | Gas recombination facility |
| JPS6353499A (en) * | 1986-08-22 | 1988-03-07 | 科学技術庁原子力局長 | Method of processing radioactive waste liquor |
| JPH0461983A (en) * | 1990-06-25 | 1992-02-27 | Kawasaki Heavy Ind Ltd | Method and apparatus for treating salt-containing water |
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