JP2005288283A - Condensing apparatus of volatilized vapor and recovering method of volatilized vapor in the apparatus - Google Patents
Condensing apparatus of volatilized vapor and recovering method of volatilized vapor in the apparatus Download PDFInfo
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- 239000000498 cooling water Substances 0.000 abstract 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 38
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 15
- 230000006837 decompression Effects 0.000 description 14
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- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 1
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- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
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Abstract
Description
本発明は、真空で揮発蒸気が発生する真空系に、真空を維持させる真空ポンプと発生した揮発蒸気を真空下で凝縮する凝縮手段とを備えた揮発蒸気の凝縮装置とその装置において凝縮されなかった揮発蒸気を回収する方法とに関する。 The present invention relates to a volatile vapor condensing apparatus comprising a vacuum pump for generating volatile vapor in a vacuum, a vacuum pump for maintaining the vacuum, and a condensing means for condensing the generated volatile vapor under vacuum, and the apparatus is not condensed. And a method for recovering volatile vapor.
従来、主に化学工業分野において発生する揮発蒸気、例えばアルコール含水蒸気の凝縮装置では、真空ポンプの前、即ち真空系内に凝縮手段を配置して揮発蒸気を凝縮させる構成が一般であった。 2. Description of the Related Art Conventionally, a condensing apparatus for volatile vapor generated mainly in the chemical industry, for example, alcohol-containing steam, generally has a configuration in which condensing means is disposed before a vacuum pump, that is, in a vacuum system to condense volatile vapor.
しかし、このような従来の装置では、飽和蒸気圧の関係から揮発蒸気の凝縮温度が低くなるため、凝縮手段に供給される冷媒は、比較的低温の特殊な冷媒（例えばチラー）を用いる必要があり、しかも大量に必要とするため、コストが嵩むという問題があった。
又、揮発蒸気中に比較的高温で凝固する例えば水のような物質が含まれたりすると、冷媒温度が低すぎるために凝縮手段の槽内や配管内で凝固してしまうという問題があった。水等の物質が凝縮手段の内部に凝固してしまうと、蒸気の流通が阻害され真空状態が維持できなくなるため凝縮装置を一旦停止させ、温度が自然に上昇するのを待ち、凝固を自然解凍によって除去せざるを得ず、凝固の解凍に長時間を要し、生産性向上の重大な障害となっていた。
However, in such a conventional apparatus, since the condensation temperature of the volatile vapor is lowered due to the saturation vapor pressure, it is necessary to use a relatively low temperature special refrigerant (for example, a chiller) as the refrigerant supplied to the condensing means. In addition, since a large amount is required, there is a problem that costs increase.
In addition, when a substance such as water that solidifies at a relatively high temperature is contained in the volatile vapor, the refrigerant temperature is too low, causing solidification in the tank of the condensing means or in the piping. If water or other substances solidify inside the condensing means, the flow of steam is hindered and the vacuum state cannot be maintained, so the condensing device is temporarily stopped, waiting for the temperature to rise naturally, and solidification is naturally thawed. Therefore, it took a long time to thaw the coagulation, which was a serious obstacle to improving productivity.
又、従来のように、真空ポンプと当該真空ポンプの前に配置された凝縮手段とを備えた構成の装置では、凝縮手段によって凝縮されなかった揮発蒸気が有する熱（潜熱等）及び／又は揮発蒸気に含有される製品成分について効率的な回収方法が確立されていない。 In addition, in a conventional apparatus having a vacuum pump and a condensing means arranged in front of the vacuum pump, heat (latent heat, etc.) and / or volatilization of volatile vapor not condensed by the condensing means is provided. An efficient recovery method has not been established for product components contained in steam.
例えば、真空ポンプ出口でのアルコール濃度は約３３ｗｔ％であるが、スチームエジェクタの駆動蒸気としては少なくとも約１００ｋｇ／ｈ程度必要であるため、スチームエジェクタ吐出側では約７ｗｔ％程度以下となってしまい、アルコールの回収（製品化）としては好ましくなかった。 For example, although the alcohol concentration at the outlet of the vacuum pump is about 33 wt%, the driving steam for the steam ejector requires at least about 100 kg / h, so the steam ejector discharge side has about 7 wt% or less. It was not preferable for alcohol recovery (commercialization).
本発明は、真空で揮発蒸気が発生する系に、真空を維持させる真空ポンプと揮発蒸気を凝縮する第１の凝縮手段（凝縮装置）とを備えた揮発蒸気の凝縮装置において、前記真空ポンプの出口側に第２の凝縮手段を配設して二段分縮としたり、第１の凝縮手段により凝縮されなかった揮発蒸気を、全体装置（即ち当該第１の凝縮手段や後述の製品化手段等を含む装置の全体）の熱給配システムの熱源として回収したり、回収した前記揮発蒸気を、更に第２の凝縮手段や減圧塔等の製品化手段によって、凝縮されなかった揮発蒸気中の目的物を更に回収するための装置及びその方法の提供を目的とするもので、次の特徴を持つ。 The present invention relates to a condensing apparatus for volatile vapor comprising a vacuum pump for maintaining a vacuum and a first condensing device (condensing apparatus) for condensing the volatile vapor in a system in which volatile vapor is generated in a vacuum. The second condensing means is disposed on the outlet side to reduce the pressure into two stages, or the volatile vapor that has not been condensed by the first condensing means is removed from the entire apparatus (that is, the first condensing means and the commercializing means described later). Or the like, the recovered volatile vapor in the volatile vapor not condensed by the second condensing means or the commercialization means such as the decompression tower. An object of the present invention is to provide an apparatus and a method for further recovering an object, and has the following characteristics.
即ち、本発明の揮発蒸気の凝縮装置は、真空で揮発蒸気が発生する真空系に、真空を維持させる真空ポンプと揮発蒸気を凝縮して回収する第１の凝縮手段とを備えた揮発蒸気の凝縮装置において、前記真空ポンプの出口側に第２の凝縮手段を設けたことを特徴とする。 That is, the condensing apparatus for volatile vapor according to the present invention is a volatile vapor condensing device comprising a vacuum system for generating volatile vapor in a vacuum and a vacuum pump for maintaining the vacuum and a first condensing means for condensing and recovering the volatile vapor. In the condensing device, the second condensing means is provided on the outlet side of the vacuum pump.
又、本発明の揮発蒸気の凝縮装置は、真空で揮発蒸気を発生する真空系を有する揮発蒸気の凝縮装置において、第１の凝縮手段と第２の凝縮手段との二段で前記揮発蒸気を分縮するために、前記真空系の真空を維持させる真空ポンプの入口側に第１の凝縮手段を配設すると共に前記真空ポンプの出口側に第２の凝縮手段を設けたことを特徴とする。 The volatile vapor condensing device of the present invention is a volatile vapor condensing device having a vacuum system for generating volatile vapor in a vacuum, wherein the volatile vapor is two-staged by a first condensing means and a second condensing means. In order to reduce the pressure, a first condensing means is provided on the inlet side of the vacuum pump that maintains the vacuum of the vacuum system, and a second condensing means is provided on the outlet side of the vacuum pump. .
又、本発明の揮発蒸気の凝縮装置は、真空ポンプと第２の凝縮手段との間に前記真空ポンプからの揮発蒸気を回収する揮発蒸気の回収流路分岐手段を設けたことを特徴とする。 The volatile vapor condensing apparatus of the present invention is characterized in that a volatile vapor recovery flow path branching means for recovering volatile vapor from the vacuum pump is provided between the vacuum pump and the second condensing means. .
又、本発明の揮発蒸気の凝縮装置は、揮発蒸気の回収流路分岐手段により回収された揮発蒸気を揮発蒸気の凝縮装置を含む装置全体の熱給配システムの熱源として送り込む揮発蒸気供給手段を設けたことを特徴とする。 Further, the volatile vapor condensing apparatus of the present invention comprises volatile vapor supply means for sending the volatile vapor recovered by the volatile vapor recovery flow path branching means as a heat source of the heat distribution system of the entire apparatus including the volatile vapor condensing apparatus. It is provided.
又、本発明の揮発蒸気の凝縮装置は、揮発蒸気の回収流路分岐手段により回収された揮発蒸気を製品化する製品化処理手段を設けたことを特徴とする。 Further, the volatile vapor condensing apparatus of the present invention is characterized in that a commercialization processing means for commercializing the volatile vapor recovered by the volatile vapor recovery flow path branching means is provided.
又、本発明の揮発蒸気の凝縮装置は、揮発蒸気の回収流路分岐手段により回収された揮発蒸気を製品化する製品化処理手段と前記揮発蒸気の回収流路分岐手段により回収された揮発蒸気を揮発蒸気の凝縮装置を含む装置全体の熱給配システムに熱源として送り込む揮発蒸気供給手段とを設け、前記揮発蒸気の回収流路分岐手段により回収された揮発蒸気を前記製品化処理手段と前記揮発蒸気供給手段との何れか又は双方に供給する揮発蒸気分配手段を設けたことを特徴とする。 The volatile vapor condensing apparatus according to the present invention includes a commercialization processing means for commercializing the volatile vapor recovered by the volatile vapor recovery flow path branching means and the volatile vapor recovered by the volatile vapor recovery flow path branching means. Volatile vapor supply means for sending the volatile vapor as a heat source to a heat distribution system of the entire apparatus including the volatile vapor condensation device, and the volatile vapor recovered by the recovery flow path branching means for the volatile vapor Volatile vapor distribution means for supplying either or both of the volatile vapor supply means and the volatile vapor supply means is provided.
又、本発明の揮発蒸気の凝縮装置は、第２の凝縮手段が大気圧下で作動するよう設けたことを特徴とする。 The volatile vapor condensing apparatus of the present invention is characterized in that the second condensing means is provided to operate under atmospheric pressure.
又、本発明の揮発蒸気の凝縮装置は、第２の凝縮手段の冷却液が常温の水であることを特徴とする。 The volatile vapor condensing apparatus of the present invention is characterized in that the cooling liquid of the second condensing means is water at room temperature.
又、本発明の揮発蒸気の凝縮装置は、真空ポンプがドライ真空ポンプであることを特徴とする。 In the volatile vapor condensing apparatus of the present invention, the vacuum pump is a dry vacuum pump.
又、本発明の揮発蒸気の凝縮装置における揮発蒸気の回収方法は、真空で揮発蒸気が発生する真空系に真空を維持させる真空ポンプと揮発蒸気を凝縮して回収する第１の凝縮手段とを備えた揮発蒸気の凝縮装置において、前記真空ポンプの出口側に第２の凝縮手段を設けて、前記第１の凝縮手段にて凝縮処理されなかった揮発蒸気を前記真空ポンプを介して取り込み更に凝縮処理して回収することを特徴とする。 The volatile vapor recovery method in the volatile vapor condensing apparatus of the present invention includes a vacuum pump that maintains a vacuum in a vacuum system that generates volatile vapor in a vacuum, and a first condensing means that condenses and recovers the volatile vapor. In the volatile vapor condensing apparatus, a second condensing unit is provided on the outlet side of the vacuum pump, and the volatile vapor not condensed by the first condensing unit is taken in through the vacuum pump and further condensed. It is characterized by processing and collecting.
又、本発明の揮発蒸気の凝縮装置における揮発蒸気の回収方法は、真空で揮発蒸気が発生する真空系に、真空を維持させる真空ポンプと揮発蒸気を凝縮して回収する第１の凝縮手段とを備えると共に、前記真空ポンプの出口側に第２の凝縮手段を設けた揮発蒸気の凝縮装置において、前記真空系の圧力が所定の圧力より低下すると第１の復圧用圧力制御弁により外気を取り入れ、真空系Ａの圧力が所定の圧力より上昇すると第２の復圧用圧力制御弁により真空ポンプへの流量を増加させて、真空系の圧力を一定に維持させながら凝縮処理して回収することを特徴とする。 The volatile vapor recovery method in the volatile vapor condensing apparatus of the present invention includes a vacuum system for generating volatile vapor in a vacuum, a vacuum pump for maintaining the vacuum, and a first condensing means for condensing and recovering the volatile vapor. A volatile vapor condensing device provided with a second condensing means on the outlet side of the vacuum pump, and when the pressure in the vacuum system falls below a predetermined pressure, outside air is taken in by the first pressure-reducing pressure control valve. When the pressure in the vacuum system A rises above a predetermined pressure, the flow rate to the vacuum pump is increased by the second pressure-reducing pressure control valve, and the condensation is recovered while maintaining the vacuum system pressure constant. Features.
又、本発明の揮発蒸気の凝縮装置は、真空で揮発蒸気が発生する真空系に、真空を維持させる真空ポンプと揮発蒸気を凝縮して回収する第１の凝縮手段とを備えた揮発蒸気の凝縮装置において、前記真空ポンプの出口側に、当該真空ポンプからの揮発蒸気の一部又は全部を回収する揮発蒸気の回収流路分岐手段を設け、前記揮発蒸気の回収流路分岐手段により回収された揮発蒸気を揮発蒸気の凝縮装置を含む装置全体の熱給配システムに熱源として送り込む揮発蒸気供給手段を設けたことを特徴とする。 Further, the volatile vapor condensing apparatus of the present invention is a volatile vapor condensing device provided with a vacuum pump for maintaining the vacuum and a first condensing means for condensing and recovering the volatile vapor in a vacuum system in which the volatile vapor is generated in a vacuum. In the condensing device, a volatile vapor recovery channel branching means for recovering part or all of the volatile vapor from the vacuum pump is provided on the outlet side of the vacuum pump, and the volatile vapor recovery channel branching means collects the volatile vapor. Volatile vapor supply means for sending the volatile vapor as a heat source to the heat distribution system of the entire apparatus including the volatile vapor condensing device is provided.
又、本発明の揮発蒸気の凝縮装置は、真空で揮発蒸気が発生する真空系に、真空を維持させる真空ポンプと揮発蒸気を凝縮して回収する第１の凝縮手段とを備えた揮発蒸気の凝縮装置において、前記真空ポンプの出口側に、当該真空ポンプからの揮発蒸気の一部又は全部を回収する揮発蒸気の回収流路分岐手段を設け、前記揮発蒸気の回収流路分岐手段により回収された揮発蒸気を製品化する製品化処理手段を設けたことを特徴とする。 Further, the volatile vapor condensing apparatus of the present invention is a volatile vapor condensing device provided with a vacuum pump for maintaining the vacuum and a first condensing means for condensing and recovering the volatile vapor in a vacuum system in which the volatile vapor is generated in a vacuum. In the condensing device, a volatile vapor recovery channel branching means for recovering part or all of the volatile vapor from the vacuum pump is provided on the outlet side of the vacuum pump, and the volatile vapor recovery channel branching means collects the volatile vapor. The present invention is characterized by providing a commercialization processing means for commercializing the volatile vapor.
又、本発明の揮発蒸気の凝縮装置は、真空で揮発蒸気が発生する真空系に、真空を維持させる真空ポンプと揮発蒸気を凝縮して回収する第１の凝縮手段とを備えた揮発蒸気の凝縮装置において、前記真空ポンプの出口側に、当該真空ポンプからの揮発蒸気の一部又は全部を回収する揮発蒸気の回収流路分岐手段を設け、前記揮発蒸気の回収流路分岐手段により回収された揮発蒸気を揮発蒸気の凝縮装置を含む装置全体の熱給配システムに熱源として送り込む揮発蒸気供給手段と前記揮発蒸気の回収流路分岐手段により回収された揮発蒸気を製品化する製品化処理手段とを設けたことを特徴とする。 Further, the volatile vapor condensing apparatus of the present invention is a volatile vapor condensing device provided with a vacuum pump for maintaining the vacuum and a first condensing means for condensing and recovering the volatile vapor in a vacuum system in which the volatile vapor is generated in a vacuum. In the condensing device, a volatile vapor recovery channel branching means for recovering part or all of the volatile vapor from the vacuum pump is provided on the outlet side of the vacuum pump, and the volatile vapor recovery channel branching means collects the volatile vapor. Volatile vapor supply means for sending the volatile vapor as a heat source to the heat distribution system of the entire apparatus including the volatile vapor condensing device, and a commercialization processing means for commercializing the volatile vapor recovered by the recovery flow path branching means for the volatile vapor And is provided.
又、本発明の揮発蒸気の凝縮装置は、揮発蒸気の回収流路分岐手段により回収された揮発蒸気の一部又は全部を製品化処理手段と揮発蒸気供給手段との何れか又は双方に供給する揮発蒸気分配手段を設けたことを特徴とする。 The volatile vapor condensing apparatus of the present invention supplies a part or all of the volatile vapor recovered by the volatile vapor recovery flow path branching means to either or both of the commercialization processing means and the volatile vapor supply means. Volatile vapor distribution means is provided.
又、本発明の揮発蒸気の凝縮装置における揮発蒸気の回収方法は、真空で揮発蒸気が発生する真空系に、真空を維持させる真空ポンプと揮発蒸気を凝縮して回収する第１の凝縮手段とを備えた揮発蒸気の凝縮装置において、前記真空ポンプの出口側に、当該真空ポンプからの揮発蒸気の一部又は全部を回収する揮発蒸気の回収流路分岐手段を設けて、前記揮発蒸気の回収流路分岐手段により回収された揮発蒸気の一部又は全部を揮発蒸気の凝縮装置を含む装置全体の熱給配システムの熱源として利用することを特徴とする。 The volatile vapor recovery method in the volatile vapor condensing apparatus of the present invention includes a vacuum system for generating volatile vapor in a vacuum, a vacuum pump for maintaining the vacuum, and a first condensing means for condensing and recovering the volatile vapor. In the volatile vapor condensing apparatus, the volatile vapor recovery channel branching means for recovering part or all of the volatile vapor from the vacuum pump is provided on the outlet side of the vacuum pump, and the volatile vapor is recovered. A part or all of the volatile vapor recovered by the flow path branching means is used as a heat source of a heat distribution system of the entire apparatus including a volatile vapor condensing device.
又、本発明の揮発蒸気の凝縮装置における揮発蒸気の回収方法は、真空で揮発蒸気が発生する真空系に、真空を維持させる真空ポンプと揮発蒸気を凝縮して回収する第１の凝縮手段とを備えた揮発蒸気の凝縮装置において、前記真空ポンプの出口側に、当該真空ポンプからの揮発蒸気の一部又は全部を回収する揮発蒸気の回収流路分岐手段を設けて、前記揮発蒸気の回収流路分岐手段により回収された揮発蒸気を製品化処理手段により製品化することを特徴とする。 The volatile vapor recovery method in the volatile vapor condensing apparatus of the present invention includes a vacuum system for generating volatile vapor in a vacuum, a vacuum pump for maintaining the vacuum, and a first condensing means for condensing and recovering the volatile vapor. In the volatile vapor condensing apparatus, the volatile vapor recovery channel branching means for recovering part or all of the volatile vapor from the vacuum pump is provided on the outlet side of the vacuum pump, and the volatile vapor is recovered. The volatile vapor recovered by the flow path branching unit is commercialized by the commercialization processing unit.
又、本発明の揮発蒸気の凝縮装置における揮発蒸気の回収方法は、真空で揮発蒸気が発生する真空系に、真空を維持させる真空ポンプと揮発蒸気を凝縮して回収する第１の凝縮手段とを備えた揮発蒸気の凝縮装置において、前記真空ポンプの出口側に、当該真空ポンプからの揮発蒸気の一部又は全部を回収する揮発蒸気の回収流路分岐手段を設けて、前記揮発蒸気の回収流路分岐手段により回収された揮発蒸気を揮発蒸気の凝縮装置を含む装置全体の熱給配システムに送り込む揮発蒸気供給手段により熱源として利用したり、前記揮発蒸気の回収流路分岐手段により回収された揮発蒸気を製品化処理手段により製品化したりすることを特徴とする。 The volatile vapor recovery method in the volatile vapor condensing apparatus of the present invention includes a vacuum system for generating volatile vapor in a vacuum, a vacuum pump for maintaining the vacuum, and a first condensing means for condensing and recovering the volatile vapor. In the volatile vapor condensing apparatus, the volatile vapor recovery channel branching means for recovering part or all of the volatile vapor from the vacuum pump is provided on the outlet side of the vacuum pump, and the volatile vapor is recovered. The volatile vapor recovered by the flow path branching means is used as a heat source by the volatile vapor supply means that sends the volatile vapor to the heat distribution system of the entire apparatus including the volatile vapor condensing device, or is recovered by the recovery flow path branching means of the volatile vapor. The volatile vapor is commercialized by a commercialization processing means.
本発明によれば、大気圧下で作動するよう配設された第２の凝縮手段が、真空下で作動する第１の凝縮手段によって凝縮処理（第一段凝縮処理）されなかった揮発蒸気を取り込んで、更に凝縮処理（第二段凝縮処理）するので、従来のように第１の凝縮手段だけによって凝縮処理する場合に比べて、第１の凝縮手段の処理能力を低目に設定することができる。 According to the present invention, the second condensing means arranged to operate under atmospheric pressure can remove volatile vapor that has not been condensed (first-stage condensing process) by the first condensing means operating under vacuum. Since it is taken in and further condensed (second stage condensation), the processing capacity of the first condensing means should be set lower than in the conventional case where the condensing process is performed only by the first condensing means. Can do.
又、従来の、真空系を有する揮発蒸気の凝縮装置では揮発蒸気が、通常、全回収又は全排水となっていたが、本発明によれば、二段の凝縮手段を有する分縮作用によって製品成分多い留分と製品成分の少ない留分とに分離でき、いわゆる分縮処理ができるため、装置全体として製品成分（凝縮液）の回収率を上昇させることができると共に、製品高濃度留分と製品低濃度留分を各々その濃度成分及びその他の不純物の割合を勘案して装置の最適位置に導入できるため、結果的に品質の向上及び省エネルギー化を図ることができる。 Further, in the conventional volatile vapor condensing apparatus having a vacuum system, the volatile vapor is usually totally recovered or drained, but according to the present invention, the product is produced by the partial reduction action having the two-stage condensing means. Since it can be separated into fractions with a large amount of components and fractions with a small amount of product components, so-called fractionalization can be performed, the recovery rate of product components (condensate) as a whole can be increased, Since the low concentration fraction of the product can be introduced into the optimum position of the apparatus in consideration of the concentration component and the ratio of other impurities, the quality can be improved and energy can be saved as a result.
又、本発明によれば、圧力制御手段によって真空系の圧力を一定に維持することができる。 According to the present invention, the pressure of the vacuum system can be kept constant by the pressure control means.
又、本発明によれば、第１の凝縮装置（コンデンサー）を小型化することができると共に、チラーを製造するための冷凍装置をも小型化することができる。 Further, according to the present invention, the first condensing device (condenser) can be reduced in size, and the refrigeration device for producing the chiller can also be reduced in size.
又、本発明によれば、比較的高温のチラーを用いることができるため、一般産業用の冷凍装置を利用することができる。 Further, according to the present invention, since a relatively high temperature chiller can be used, a general industrial refrigeration apparatus can be used.
又、本発明によれば、真空配管内の凍結防止のために必要だった、複雑なチラーの温度制御装置が不要になる。 Further, according to the present invention, a complicated chiller temperature control device, which is necessary for preventing freezing in the vacuum pipe, is not required.
又、本発明によれば、従来技術では有効な回収方法が確立されていない凝縮されなかった揮発蒸気を、全体装置の熱供給システムの熱源として利用することができるので、省エネルギー化を実現でき、製品コストを下げることができる。 In addition, according to the present invention, the volatile vapor that has not been condensed with an effective recovery method that has not been established in the prior art can be used as a heat source of the heat supply system of the entire apparatus, so energy saving can be realized, Product cost can be reduced.
又、本発明によれば、凝縮装置で凝縮されなかった揮発蒸気中の目的物を、更に第２の凝縮手段や減圧塔等のような製品化手段によって、製品として回収することができるので、製品回収率を著しく高めることができ、製品コストを下げることができる。 In addition, according to the present invention, the object in the volatile vapor that has not been condensed by the condensing device can be further recovered as a product by a productizing means such as a second condensing means or a vacuum tower. Product recovery can be significantly increased and product costs can be reduced.
本発明の揮発蒸気の凝縮装置及びその装置における揮発蒸気の回収方法は、あらゆる揮発蒸気の凝縮装置に適用できるものであるが、アルコール蒸気回収の凝縮装置に適用した形態を実施例として以下説明する。 The volatile vapor condensing apparatus and the volatile vapor recovery method in the apparatus of the present invention can be applied to any volatile vapor condensing apparatus, but the embodiment applied to the alcohol vapor recovering condensing apparatus will be described below as an example. .
本発明の実施例１は、真空で揮発蒸気が発生する系に、真空を維持させる真空ポンプと揮発蒸気を凝縮する第１の凝縮手段（凝縮装置）とを備えた揮発蒸気の凝縮装置において、前記真空ポンプの出口側に第２の凝縮手段を配設して二段分縮とした例である。 Embodiment 1 of the present invention is a volatile vapor condensing apparatus comprising a vacuum pump for maintaining a vacuum and a first condensing means (condensing apparatus) for condensing the volatile vapor in a system in which volatile vapor is generated in a vacuum. This is an example in which the second condensing means is disposed on the outlet side of the vacuum pump to reduce the pressure to two stages.
先ず、本発明の揮発蒸気の凝縮装置及び凝縮方法を図１に基づいて説明する。図１は実施例１の凝縮装置及び制御システムのフロー図である。
図中において二点鎖線で囲む領域Ａが真空系即ち真空で揮発蒸気が発生する系であり、この真空系Ａ内には、真空系Ａ内に導入された揮発蒸気を真空下で凝縮して回収する第１の凝縮手段１０が前記真空系Ａの真空を維持する真空ポンプ１１の入口側に配設されている。この真空ポンプとしては高真空下で作動するドライ真空ポンプが好適である。
第１の凝縮手段１０で凝縮された凝縮液（濃縮液ともいう）は、当該凝縮手段１０に付設された受液槽１２に一旦回収され、取出ポンプ１３を介して系外の製品化手段へその全部又は一部が導入されることとなる。
First, the condensing apparatus and condensing method of the volatile vapor of this invention are demonstrated based on FIG. FIG. 1 is a flowchart of the condensing device and the control system of the first embodiment.
In the figure, a region A surrounded by a two-dot chain line is a vacuum system, that is, a system in which volatile vapor is generated in vacuum. In this vacuum system A, volatile vapor introduced into the vacuum system A is condensed under vacuum. The first condensing means 10 to be recovered is disposed on the inlet side of the
The condensate condensed by the first condensing means 10 (also referred to as a concentrated liquid) is once recovered in a
真空ポンプ１１の出口側、即ち、揮発蒸気を発生させる真空系Ａ外にて、大気圧下で作動するよう第２の凝縮手段２０が配設されている。この第２の凝縮手段２０は、第１の凝縮手段１０によって一旦凝縮処理（第一段凝縮処理）されても凝縮されなかった揮発蒸気を、真空ポンプ１１を介して取り込み、更に凝縮処理（第二段凝縮処理）して揮発蒸気中の目的物（エタノール）を回収する。
第２の凝縮手段２０で凝縮された凝縮液（第二段凝縮液）は、当該凝縮手段２０に付設された受液槽２２に一旦回収された後、最終取出ポンプ２３を介して、本装置外に取り出され、製品化手段へその全部又は一部が導入されることとなる。
A second condensing means 20 is arranged to operate under atmospheric pressure on the outlet side of the
The condensate condensed by the second condensing means 20 (second-stage condensate) is once recovered in the
この実施例では、第１の凝縮手段１０の受液槽１２に回収された凝縮液（第一段凝縮液）は、取出ポンプ１３を介して、第２の凝縮手段２０の受液槽２２に送出されているため、第一段凝縮液と共に最終取出ポンプ２３を介して取り出され、製品化手段へその全部又は一部が導入されることとなる。
In this embodiment, the condensate (first stage condensate) collected in the
第１の凝縮手段１０に冷媒供給手段を介して供給される冷媒としては真空下において用いられるチラーが好適であるが、第２の凝縮手段２０については、揮発蒸気の凝縮をほぼ大気圧で行うことができるので、凝縮温度が比較的高く、冷媒液として常温或いは常温付近の水を使用することができる。 As the refrigerant supplied to the first condensing means 10 via the refrigerant supplying means, a chiller used under vacuum is suitable, but for the second condensing means 20, the volatile vapor is condensed at substantially atmospheric pressure. Therefore, the condensation temperature is relatively high, and water at or near room temperature can be used as the refrigerant liquid.
次に、真空系Ａを一定の圧力に保つ圧力制御手段を説明する。
圧力制御手段３０は、真空系Ａの圧力を測定する圧力検出器３１と、真空系Ａへの外気の流入を制御する第１の復圧用圧力制御弁３２と、真空ポンプ１１への流量を制御する第２の復圧用圧力制御弁３３とを備えている。
図１において、第１の復圧用圧力制御弁３２は第１の凝縮手段１０と真空ポンプ１１との間の揮発蒸気流路３４の途中に接続された外気導入流路３５に介在し、第２の復圧用圧力制御弁３３は前記揮発蒸気流路３４と外気導入流路３５との接続部と真空ポンプ１１との間の揮発蒸気流路３４の途中に介在している。
Next, pressure control means for maintaining the vacuum system A at a constant pressure will be described.
The pressure control means 30 controls the
In FIG. 1, the first pressure-reducing
この圧力制御手段３０は、圧力検出器３１で真空系Ａの圧力を測定し、真空系Ａの圧力が所定の圧力より低下した場合には第１の復圧用圧力制御弁３２を用いて外気を取り入れ、真空系Ａの圧力が所定の圧力より上昇した場合には第２の復圧用圧力制御弁３３を用いて真空ポンプ１１への流量を増加させることにより、真空系Ａの圧力を一定に維持させている。
This pressure control means 30 measures the pressure of the vacuum system A with the
実施例２は、上記実施例１において、第１の凝縮手段１０により凝縮されなかった揮発蒸気を、製品化手段の熱給配システムの熱源として回収する装置や方法、及び減圧塔のような製品化手段によって製品化する装置や方法の例である。以下、これを図２及び図３に基づいて説明する。図２はこの実施例２の制御システムのフロー図、図３は蒸留工程図である。
尚、図２及び図３中において図１と同じ符号は同じ内容であるのでその説明を省略する。又、図２中において点線で示す蒸気供給管路４５の部分は間接加熱を行う管路である。
Example 2 is an apparatus and method for recovering the volatile vapor that has not been condensed by the first condensing means 10 in Example 1 as a heat source of the heat distribution system of the productizing means, and a product such as a decompression tower. It is an example of the apparatus and method which commercialize by a production | generation means. Hereinafter, this will be described with reference to FIGS. FIG. 2 is a flowchart of the control system of the second embodiment, and FIG. 3 is a distillation process diagram.
In FIG. 2 and FIG. 3, the same reference numerals as those in FIG. Further, the portion of the
先ず、図３において製品化手段を簡単に説明する。
製品化手段としては、第１及び第２の凝縮手段１０、２０の外に図示されていない濃縮塔Ａ２や図２に図示されている第１抽出塔Ｄ、精留塔Ｂ、精製塔Ｆや不純物処理塔Ｇ、第２抽出塔Ｄ２、減圧塔Ｖ等がある。
First, the product production means will be briefly described with reference to FIG.
As the commercialization means, the first and second condensing means 10 and 20, the concentration tower A2 not shown, the first extraction tower D, the rectification tower B, the purification tower F shown in FIG. There are an impurity treatment tower G, a second extraction tower D2, a decompression tower V, and the like.
図示されていない濃縮塔Ａ２は、もろみ濃縮装置から留出した低濃度アルコールを共沸組成近くまでの濃縮して後述の抽出塔Ｄへ送入すると共に、当該塔頂付近から低沸点不純物を、又、当該塔央部から高沸点不純物を除去する。 The concentration tower A2 (not shown) concentrates the low-concentration alcohol distilled from the mash concentration apparatus to near the azeotropic composition and sends it to the extraction tower D described later, and low-boiling impurities from the vicinity of the top of the tower. Further, high boiling point impurities are removed from the central portion of the column.
濃縮塔Ａ２で濃縮されたアルコール、原料の粗留アルコールを温水で希釈し、抽出蒸留を行うことによりメタノール以外の不純物を当該塔頂部から分離すると共に、希薄アルコール（アルコール分１３〜１５％）を塔底部から次の蒸留工程の精留塔Ｂへ送入する。 The alcohol concentrated in the concentration tower A2 and the crude crude alcohol as a raw material are diluted with warm water and subjected to extractive distillation to separate impurities other than methanol from the top of the tower and dilute alcohol (alcohol content: 13 to 15%). It sends into the rectification tower B of the next distillation process from a tower bottom part.
精留塔Ｂでは、抽出塔Ｄで希釈されたアルコールを再び共沸組成近くまで濃縮し、当該塔央部から高沸点不純物を除去しながら塔頂から次の蒸留工程の精製塔Ｆへ送入する。 In the rectification column B, the alcohol diluted in the extraction column D is concentrated again to near the azeotropic composition, and sent to the purification column F in the next distillation step from the top of the column while removing high boiling impurities from the center of the column. To do.
精製塔Ｆでは、特に分離が困難なメタノールについて、アルコール濃度が高いと比揮発度が高くなることを利用し、当該塔底から製品としてのアルコールを留出させ、当該塔頂からメタノールを除去する。 In the purification column F, particularly for methanol that is difficult to separate, the alcohol as a product is distilled from the bottom of the column and the methanol is removed from the top of the column by utilizing the fact that the relative volatility increases when the alcohol concentration is high. .
不純物処理塔Ｇでは、精留塔Ｂ及び精製塔Ｆの塔頂部の留出液を更にメタノールを濃縮・分離し、メタノールを塔頂に集積すると共に、当該塔底から回収されたアルコールを後述の第２抽出塔Ｄに送入する。こうして回収されるアルコールはその品質をチェックの上一部が製品化される。 In the impurity treatment tower G, methanol is further concentrated and separated from the distillate at the top of the rectification tower B and the purification tower F, and methanol is collected at the top of the tower, and alcohol recovered from the bottom of the tower is described later. It feeds into the 2nd extraction tower D. The alcohol recovered in this way is partly commercialized after checking its quality.
第２抽出塔Ｄ２では、第１抽出塔Ｄと同様に、温水を加えることによる抽出効果を利用して、当該塔頂部に不純物を濃縮させて不順アルコールとして系外に除去する。 In the second extraction column D2, as in the first extraction column D, using the extraction effect by adding warm water, impurities are concentrated at the top of the column and removed out of the system as irregular alcohol.
減圧塔Ｖでは、濃縮塔Ａ２、第１抽出塔Ｄ、精留塔Ｂの中間部からカットされたノルマルプロピルアルコール等の高沸点不純物を当該塔央部で濃縮・分離する。この減圧塔Ｖの圧力はアルコール水の共沸が外れる７０ｍｍＨｇ付近で操作される。 In the vacuum column V, high-boiling impurities such as normal propyl alcohol cut from the middle part of the concentration column A2, the first extraction column D, and the rectification column B are concentrated and separated at the center of the column. The pressure in the decompression tower V is operated in the vicinity of 70 mmHg from which the azeotropy of alcohol water is removed.
脱水塔Ｃでは、当該脱水塔Ｃに供給された含水アルコールの水分を、脱水剤（例えばシクロヘキサン）を用いて３成分共沸化合物として系外に除去することによって、含水アルコールを無水アルコールとして、当該塔底部から留出させる。 In the dehydration tower C, the water-containing alcohol supplied to the dehydration tower C is removed from the system as a three-component azeotrope using a dehydrating agent (for example, cyclohexane). Distill from the bottom of the tower.
図２及び図３において、図中の符号４１は第１の凝縮手段１０で凝縮されなかった揮発蒸気（以下、単に揮発蒸気ともいう）の一部又は全部を回収するための回収流路分岐手段である。この回収流路分岐手段４１は、真空ポンプ１１の出口側、この実施例では真空ポンプ１１と第２の凝縮手段２０との間の揮発蒸気の回収流路４２の途中に配設されており、真空ポンプ１１から送り出される揮発蒸気を回収する。回収流路分岐手段４１としては適当な切換弁を用いればよい。
2 and 3, reference numeral 41 in the drawing denotes a recovery flow path branching unit for recovering a part or all of the volatile vapor (hereinafter also simply referred to as volatile vapor) that has not been condensed by the
次に、回収流路分岐手段４１によって回収された揮発蒸気を抽出塔４４に供給する例（以下、抽出塔供給手段ともいう）を説明する。
回収流路分岐手段４１によって回収された揮発蒸気は、揮発蒸気の凝縮装（この実施例では第１及び第２の凝縮手段１０、２０）を含む揮発蒸気を製品化するに必要な装置の全体即ち全体装置の熱給配システム４０の熱源として揮発蒸気供給手段４３に送り込まれる。揮発蒸気供給手段４３としてこの実施例ではスチームエジェクタ（以下、エジェクタともいう）を用いている。
このエジェクタは、７〜８気圧程度の水蒸気（第１流体）を発生させる熱給配システム４０のボイラと製品化手段としての抽出塔４４（図３における抽出塔Ｄや抽出塔Ｄ２）との間に配設され、第１流体としての前記水蒸気に第２流体としての揮発蒸気を吸引させる。こうしてボイラからの水蒸気と共に揮発蒸気が熱源として抽出塔４４の底部の加熱部から供給される。
Next, an example in which the volatile vapor recovered by the recovery flow path branching means 41 is supplied to the extraction tower 44 (hereinafter also referred to as extraction tower supply means) will be described.
The volatile vapor recovered by the recovery flow path branching means 41 is the entire apparatus necessary for commercializing the volatile vapor including the volatile vapor condensing device (first and second condensing means 10 and 20 in this embodiment). That is, it is sent to the volatile vapor supply means 43 as a heat source of the
This ejector is provided between the boiler of the
抽出塔４４（Ｄ、Ｄ２）は、塔内に水蒸気が直接導入されるいわゆる直接加熱構造となっているため、割合として低率の揮発蒸気を含んだ水蒸気が直接塔底部に導入されても、蒸留運転上に支障が無い。
こうして抽出塔４４（Ｄ、Ｄ２）に直接送り込まれた揮発蒸気に含まれる微量のエタノールを当該抽出塔４４（Ｄ、Ｄ２）から結果的に濃縮エタノール液として回収することもできる。
これにより、エタノール（製品）の回収率が一段と向上し、大幅なコストダウンを実現させる。即ち、この例によれば、直接加熱される製品化手段に、凝縮されなかった揮発蒸気を熱源として供給することにより、その潜熱を有効に活用できるため省エネルギー化と共に製品回収率をも向上させることができるのである。
Since the extraction tower 44 (D, D2) has a so-called direct heating structure in which water vapor is directly introduced into the tower, even if water vapor containing a low rate of volatile vapor is introduced directly into the tower bottom, There is no problem in distillation operation.
In this way, a trace amount of ethanol contained in the volatile vapor sent directly to the extraction tower 44 (D, D2) can also be recovered from the extraction tower 44 (D, D2) as a concentrated ethanol solution.
As a result, the recovery rate of ethanol (product) is further improved and a significant cost reduction is realized. In other words, according to this example, by supplying volatile vapor that has not been condensed as a heat source to the productization means that is directly heated, the latent heat can be used effectively, so energy saving and product recovery can be improved. Can do it.
次に、上述の例と異なり、回収流路分岐手段４１によって回収された揮発蒸気を、直接、減圧塔Ｖに供給する例（以下、減圧塔供給手段ともいう）を説明する。
図２に示すようにこの減圧塔供給手段では、エジェクタ４３及び抽出塔４４（Ｄ、Ｄ２）を経ずして、揮発蒸気を減圧塔Ｖに直接供給する。この場合、供給される揮発蒸気は、当該揮発蒸気に含まれるエタノール濃度に相応する濃度の当該減圧塔Ｖの棚段に送り込むことが望ましい。
こうして減圧塔Ｖに供給された揮発蒸気は、当該減圧塔Ｖにおいて、凝縮されなかった揮発蒸気中から結果的に製品としてのエタノールが回収されるので、製品化回収率が向上することとなる。
Next, unlike the above example, an example in which the volatile vapor recovered by the recovery flow path branching means 41 is directly supplied to the decompression tower V (hereinafter also referred to as decompression tower supply means) will be described.
As shown in FIG. 2, this decompression tower supply means directly supplies the volatile vapor to the decompression tower V without passing through the
The volatile vapor thus supplied to the decompression tower V results in an improvement in the product recovery rate because ethanol as a product is recovered from the volatile vapor that has not been condensed in the decompression tower V.
この減圧塔供給手段を用いるか上述の抽出塔供給手段を用いるか、或いは双方を用いるかは、運転状況に応じて適宜選択する。
図２に示す実施例２では、回収流路分岐手段４１によって回収された揮発蒸気を熱源及び当該揮発蒸気中の目的物たるエタノールを製品として回収（製品化）する製品化処理手段としての抽出塔Ｄ、Ｄ２へ供給する流路と、全体装置の熱給配システム４０の流路に乗せて、熱源及び製品化のために利用すべく熱給配システム４０の揮発蒸気供給手段４３（エジェクタ）へと供給する流路との分岐点に、この揮発蒸気分配手段４６を設けている。
この揮発蒸気分配手段４６によって、凝縮されなかった揮発蒸気を何れか又は双方の流路に適当に分配する。
従って、何れか一方の流路のみが設けられて用いられている全体装置の場合には揮発蒸気分配手段４６は必要でない。
Whether to use this decompression tower supply means, the above-mentioned extraction tower supply means, or both, is appropriately selected according to the operating conditions.
In the second embodiment shown in FIG. 2, an extraction tower as a commercialization processing means for recovering (productizing) the volatile vapor recovered by the recovery flow path branching means 41 as a heat source and ethanol as a target product in the volatile vapor. D and D2 are mounted on the flow path of the
The volatile vapor distribution means 46 appropriately distributes the volatile vapor that has not been condensed to one or both of the flow paths.
Accordingly, the volatile vapor distribution means 46 is not necessary in the case of the entire apparatus in which only one of the flow paths is provided.
この実施例２によれば、回収流路分岐手段４１によって回収された揮発蒸気の一部又は全部を、上述のように全体装置の熱源として再利用できると共に、所要の製品化処理手段によって当該揮発蒸気中の目的物（エタノール）を更に製品として回収できるので、全体装置としての省エネルギー化と目的物たるエタノール成分の製品化回収率の向上によって大幅なコストダウンを図ることができる。 According to the second embodiment, a part or all of the volatile vapor recovered by the recovery flow path branching means 41 can be reused as a heat source for the entire apparatus as described above, and the volatileization can be performed by a required product processing means. Since the target product (ethanol) in the steam can be further recovered as a product, the cost can be greatly reduced by saving energy as an entire device and improving the product recovery rate of the ethanol component as the target product.
更に、図２及び図３に示す実施例２では、第１の凝縮手段１０で凝縮されなかった揮発蒸気は、装置全体の立ち上げを実施している間、熱給配システム４０のエジェクタ４３の駆動状態も不安定であるため、ここに送り込むことは熱給配システム４０に対し外乱要素を与える要因となり得るため、装置全体の立ち上げを実施している間は、凝縮液を直接導入した方が安定的に立ち上げることが可能となる。
Furthermore, in the second embodiment shown in FIGS. 2 and 3, the volatile vapor that has not been condensed by the first condensing means 10 is discharged from the
これは、装置全体の立ち上げをしている間、全体装置の熱給配システムに設置されているエジェクタ４３の駆動源である蒸気の量も装置全体が安定するまでその量が変動するため、エジェクタ４３で回収される第１の凝縮手段１０で凝縮されなかった揮発時容器の量も変動をきたし、結果的に装置全体を不安定な状態に陥れる恐れがあるためである。
従って、この実施例２における目的物たるエタノール製品の回収効率や省エネルギー効果としては、定常状態になるまでの間は、第１の凝縮手段１０で凝縮されなかった揮発蒸気を全体装置の熱給配システムの熱源として揮発蒸気供給手段４３のエジェクタを介して抽出塔供給手段に送り込むように、回収流路分岐手段４１の切換弁を操作するとよい。
This is because the amount of steam that is the drive source of the
Therefore, the recovery efficiency and energy saving effect of the ethanol product as the object in Example 2 are as follows. The switching valve of the recovery flow path branching means 41 may be operated so as to be sent to the extraction tower supply means via the ejector of the volatile vapor supply means 43 as a heat source of the system.
実施例３は、上記実施例２（図２）において、第２の凝縮手段２０以下の構成を無くし、真空ポンプ１１から取り出される凝縮されなかった揮発蒸気を、抽出塔供給手段及び又は減圧塔供給手段に送り込む構造としたものである。この構造は図２において容易に理解されるものであるから図示を省略する。尚、この構成では回収流路分岐手段４１は無用となり、揮発蒸気は揮発蒸気分配手段４６に直接送り込まれる。
全体装置をこのような構造とした場合におけるよる作用効果は、抽出塔供給手段及び減圧塔供給手段において記述した通りである。
The third embodiment eliminates the configuration below the second condensing means 20 in the second embodiment (FIG. 2), and converts the uncondensed volatile vapor extracted from the
The operational effects of the overall apparatus having such a structure are as described in the extraction tower supply means and the decompression tower supply means.
本発明の揮発蒸気の凝縮装置を、アルコール蒸気回収凝縮装置に適用した実施例で説明したが、これに限らず、従来の化学工業で発生する揮発蒸気の凝縮装置の代替として、コスト削減や安定運転が可能となるため広く適用できる。 The volatile vapor condensing device of the present invention has been described in the embodiment applied to the alcohol vapor recovery condensing device. However, the present invention is not limited to this, and as an alternative to the conventional volatile vapor condensing device generated in the chemical industry, cost reduction and stability can be achieved. Since it becomes possible to drive, it is widely applicable.
１０ 第１の凝縮手段、
１１ 真空ポンプ、
１２ 受液槽（第１の凝縮手段）、
１３ 取出ポンプ、
２０ 第２の凝縮手段、
２２ 受液槽（第２の凝縮手段）、
２３ 取出ポンプ、
３０ 圧力調整装置
３１ 圧力検出装置
３２ 第１の復圧用圧力制御弁
３３ 第２の復圧用圧力制御弁
３４ 揮発蒸気流路
３５ 外気導入流路
４０ ボイラ
４１ 回収流路分岐手段
４３ 揮発蒸気供給手段（エジェクタ）
４６ 揮発蒸気分配手段
10 first condensing means,
11 Vacuum pump,
12 liquid receiving tank (first condensing means),
13 Extraction pump,
20 second condensing means,
22 liquid receiving tank (second condensing means),
23 Extraction pump,
DESCRIPTION OF
46 Volatile vapor distribution means
Claims (18)
A volatile vapor condensing apparatus comprising a vacuum system for generating volatile vapor in a vacuum, a vacuum pump for maintaining the vacuum, and first condensing means for condensing and recovering the volatile vapor, wherein the first is disposed on the outlet side of the vacuum pump. A condensing apparatus for volatile vapor, comprising two condensing means.
In a volatile vapor condensing apparatus having a vacuum system for generating volatile vapor in a vacuum, in order to depressurize the volatile vapor in two stages of a first condensing means and a second condensing means, the vacuum in the vacuum system is reduced. A volatile vapor condensing apparatus, wherein a first condensing means is disposed on the inlet side of the vacuum pump to be maintained and a second condensing means is provided on the outlet side of the vacuum pump.
The volatile vapor condensing unit according to claim 1 or 2, further comprising a volatile vapor recovery flow path branching unit for recovering the volatile vapor from the vacuum pump between the vacuum pump and the second condensing unit. apparatus.
The volatile vapor supply means for sending the volatile vapor recovered by the volatile vapor recovery flow path branching means as a heat source of the heat distribution system of the entire apparatus including the volatile vapor condensing device is provided. Steam condensing device.
4. A volatile vapor condensing apparatus according to claim 3, further comprising a commercialization processing means for commercializing the volatile vapor recovered by the recovery flow path branching means.
The heat of the entire apparatus including the commercialization processing means for commercializing the volatile vapor recovered by the volatile vapor recovery flow path branching means and the volatile vapor recovered by the volatile vapor recovery flow path branching means. Volatile vapor supply means to be sent as a heat source to the distribution system is provided, and the volatile vapor recovered by the recovery flow path branching means for supplying the volatile vapor is supplied to one or both of the commercialization processing means and the volatile vapor supply means 4. The volatile vapor condensing device according to claim 3, further comprising a volatile vapor distribution means for performing the above operation.
The volatile vapor condensing device according to any one of claims 1 to 7, wherein the vacuum pump is a dry vacuum pump.
前記真空ポンプの出口側に第２の凝縮手段を設けて、前記第１の凝縮手段にて凝縮処理されなかった揮発蒸気を前記真空ポンプを介して取り込み更に凝縮処理して回収することを特徴とする揮発蒸気の凝縮装置における揮発蒸気の回収方法。
In a volatile vapor condensing apparatus comprising a vacuum pump for maintaining a vacuum in a vacuum system in which volatile vapor is generated in vacuum and a first condensing means for condensing and recovering the volatile vapor,
A second condensing means is provided on the outlet side of the vacuum pump, and volatile vapor that has not been condensed by the first condensing means is taken in via the vacuum pump, further condensed and recovered. A method for recovering volatile vapor in a volatile vapor condensing device.
前記真空系の圧力が所定の圧力より低下すると第１の復圧用圧力制御弁により外気を取り入れ、真空系Ａの圧力が所定の圧力より上昇すると第２の復圧用圧力制御弁により真空ポンプへの流量を増加させて、真空系の圧力を一定に維持させながら凝縮処理して回収することを特徴とする揮発蒸気の凝縮装置における揮発蒸気の回収方法。
A vacuum system that generates volatile vapor in a vacuum includes a vacuum pump that maintains the vacuum and a first condensing unit that condenses and recovers the volatile vapor, and a second condensing unit is provided on the outlet side of the vacuum pump. In the volatile vapor condensing device,
When the pressure in the vacuum system drops below a predetermined pressure, outside air is taken in by the first pressure-reducing pressure control valve, and when the pressure in the vacuum system A rises above the predetermined pressure, the second pressure-reducing pressure control valve controls the vacuum pump. A method for recovering volatile vapor in a volatile vapor condensing apparatus, characterized by increasing the flow rate and condensing and recovering while maintaining a constant vacuum system pressure.
前記真空ポンプの出口側に、当該真空ポンプからの揮発蒸気の一部又は全部を回収する揮発蒸気の回収流路分岐手段を設け、前記揮発蒸気の回収流路分岐手段により回収された揮発蒸気を揮発蒸気の凝縮装置を含む装置全体の熱給配システムに熱源として送り込む揮発蒸気供給手段を設けたことを特徴とする揮発蒸気の凝縮装置。
In a volatile vapor condensing apparatus comprising: a vacuum pump that generates volatile vapor in a vacuum; and a vacuum pump that maintains the vacuum and a first condensing unit that condenses and recovers the volatile vapor.
Volatile vapor recovery flow path branching means for recovering part or all of the volatile vapor from the vacuum pump is provided on the outlet side of the vacuum pump, and the volatile vapor recovered by the volatile vapor recovery flow path branching means is provided. A volatile vapor condensing apparatus comprising a volatile vapor supplying means for supplying a heat source to a heat distribution system of the entire apparatus including a volatile vapor condensing apparatus.
前記真空ポンプの出口側に、当該真空ポンプからの揮発蒸気の一部又は全部を回収する揮発蒸気の回収流路分岐手段を設け、前記揮発蒸気の回収流路分岐手段により回収された揮発蒸気を製品化する製品化処理手段を設けたことを特徴とする揮発蒸気の凝縮装置。
In a volatile vapor condensing apparatus comprising: a vacuum pump that generates volatile vapor in a vacuum; and a vacuum pump that maintains the vacuum and a first condensing unit that condenses and recovers the volatile vapor.
Volatile vapor recovery flow path branching means for recovering part or all of the volatile vapor from the vacuum pump is provided on the outlet side of the vacuum pump, and the volatile vapor recovered by the volatile vapor recovery flow path branching means is provided. A volatile vapor condensing apparatus, characterized in that a commercializing means for commercialization is provided.
前記真空ポンプの出口側に、当該真空ポンプからの揮発蒸気の一部又は全部を回収する揮発蒸気の回収流路分岐手段を設け、前記揮発蒸気の回収流路分岐手段により回収された揮発蒸気を揮発蒸気の凝縮装置を含む装置全体の熱給配システムに熱源として送り込む揮発蒸気供給手段と前記揮発蒸気の回収流路分岐手段により回収された揮発蒸気を製品化する製品化処理手段とを設けたことを特徴とする揮発蒸気の凝縮装置。
In a volatile vapor condensing apparatus comprising: a vacuum pump that generates volatile vapor in a vacuum; and a vacuum pump that maintains the vacuum and a first condensing unit that condenses and recovers the volatile vapor.
Volatile vapor recovery flow path branching means for recovering part or all of the volatile vapor from the vacuum pump is provided on the outlet side of the vacuum pump, and the volatile vapor recovered by the volatile vapor recovery flow path branching means is provided. Volatile vapor supply means for supplying heat as a heat source to a heat distribution system of the entire apparatus including a condensing device for volatile vapor, and productization processing means for commercializing the volatile vapor recovered by the recovery flow path branching means for the volatile vapor are provided. A volatile vapor condensing device characterized in that.
Volatile vapor distribution means for supplying a part or all of the volatile vapor recovered by the volatile vapor recovery flow path branching means to one or both of the productization processing means and the volatile vapor supply means is provided. The volatile vapor condensing apparatus according to claim 13.
前記真空ポンプの出口側に、当該真空ポンプからの揮発蒸気の一部又は全部を回収する揮発蒸気の回収流路分岐手段を設けて、前記揮発蒸気の回収流路分岐手段により回収された揮発蒸気の一部又は全部を揮発蒸気の凝縮装置を含む装置全体の熱給配システムの熱源として利用することを特徴とする揮発蒸気の凝縮装置における揮発蒸気の回収方法。
In a volatile vapor condensing apparatus comprising: a vacuum pump that generates volatile vapor in a vacuum; and a vacuum pump that maintains the vacuum and a first condensing unit that condenses and recovers the volatile vapor.
Volatile vapor recovery channel branching means for recovering part or all of the volatile vapor from the vacuum pump is provided on the outlet side of the vacuum pump, and the volatile vapor recovered by the volatile vapor recovery channel branching means A method for recovering volatile vapor in a volatile vapor condensing device, wherein a part or all of the above is used as a heat source of a heat distribution system of the entire apparatus including the volatile vapor condensing device.
In a volatile vapor condensing apparatus comprising a vacuum pump that generates volatile vapor in a vacuum, and a first condensing device that condenses and recovers the volatile vapor, the volatile vapor condensing apparatus includes: Volatile vapor recovery channel branching means for recovering part or all of the volatile vapor from the vacuum pump is provided, and the volatile vapor recovered by the volatile vapor recovery channel branching means is commercialized by the commercialization processing means. A method for recovering volatile vapor in a volatile vapor condensing apparatus.
前記真空ポンプの出口側に、当該真空ポンプからの揮発蒸気の一部又は全部を回収する揮発蒸気の回収流路分岐手段を設けて、前記揮発蒸気の回収流路分岐手段により回収された揮発蒸気を揮発蒸気の凝縮装置を含む装置全体の熱給配システムに送り込む揮発蒸気供給手段により熱源として利用したり、前記揮発蒸気の回収流路分岐手段により回収された揮発蒸気を製品化処理手段により製品化したりすることを特徴とする揮発蒸気の凝縮装置における揮発蒸気の回収方法。
In a volatile vapor condensing apparatus comprising: a vacuum pump that generates volatile vapor in a vacuum; and a vacuum pump that maintains the vacuum and a first condensing unit that condenses and recovers the volatile vapor.
Volatile vapor recovery channel branching means for recovering part or all of the volatile vapor from the vacuum pump is provided on the outlet side of the vacuum pump, and the volatile vapor recovered by the volatile vapor recovery channel branching means Is used as a heat source by the volatile vapor supply means that sends it to the heat distribution system of the entire apparatus including the volatile vapor condensing device, or the volatile vapor recovered by the recovery flow path branching means of the volatile vapor is converted into a product by the commercialization processing means. A method for recovering volatile vapor in a volatile vapor condensing device.
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|---|---|---|---|---|
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0346413U (en) * | 1989-09-12 | 1991-04-30 | ||
| JPH06502584A (en) * | 1990-11-15 | 1994-03-24 | ポール・コーポレーション | Fluid purification equipment and method for removing chlorofluorocarbons from contaminated fluids |
| JPH0863304A (en) * | 1994-08-19 | 1996-03-08 | Toshiba Corp | Printer controller |
| JPH08266803A (en) * | 1995-04-03 | 1996-10-15 | Nippon Soda Co Ltd | Vacuum concentrator using diaphragm vacuum pump |
| JPH1128301A (en) * | 1997-07-10 | 1999-02-02 | Nippon Refine Kk | Apparatus and method for separating and recovering volatile component |
| JPH11128603A (en) * | 1997-08-29 | 1999-05-18 | Knf Neuberger Gmbh | Rotary evaporator |
| JP2000084303A (en) * | 1998-09-10 | 2000-03-28 | Gl Sciences Inc | Organic solvent recovery device |
| JP2002143601A (en) * | 2000-11-13 | 2002-05-21 | Gl Sciences Inc | Method and apparatus for concentrating solvent |
-
2004
- 2004-03-31 JP JP2004105623A patent/JP2005288283A/en not_active Ceased
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0346413U (en) * | 1989-09-12 | 1991-04-30 | ||
| JPH06502584A (en) * | 1990-11-15 | 1994-03-24 | ポール・コーポレーション | Fluid purification equipment and method for removing chlorofluorocarbons from contaminated fluids |
| JPH0863304A (en) * | 1994-08-19 | 1996-03-08 | Toshiba Corp | Printer controller |
| JPH08266803A (en) * | 1995-04-03 | 1996-10-15 | Nippon Soda Co Ltd | Vacuum concentrator using diaphragm vacuum pump |
| JPH1128301A (en) * | 1997-07-10 | 1999-02-02 | Nippon Refine Kk | Apparatus and method for separating and recovering volatile component |
| JPH11128603A (en) * | 1997-08-29 | 1999-05-18 | Knf Neuberger Gmbh | Rotary evaporator |
| JP2000084303A (en) * | 1998-09-10 | 2000-03-28 | Gl Sciences Inc | Organic solvent recovery device |
| JP2002143601A (en) * | 2000-11-13 | 2002-05-21 | Gl Sciences Inc | Method and apparatus for concentrating solvent |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| JP2020172873A (en) * | 2019-04-09 | 2020-10-22 | 伏虎金属工業株式会社 | Fluid conveyance system |
| JP7291935B2 (en) | 2019-04-09 | 2023-06-16 | 伏虎金属工業株式会社 | Fluid transfer system |
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