JP2010036059A - Separation process module - Google Patents

Separation process module Download PDF

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JP2010036059A
JP2010036059A JP2008198442A JP2008198442A JP2010036059A JP 2010036059 A JP2010036059 A JP 2010036059A JP 2008198442 A JP2008198442 A JP 2008198442A JP 2008198442 A JP2008198442 A JP 2008198442A JP 2010036059 A JP2010036059 A JP 2010036059A
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output
fluid
separator
output fluid
input
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JP5392699B2 (en
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Kazuo Matsuda
一夫 松田
Yoshiichi Hirochi
芳一 広地
Kenichi Kaeruishi
健一 蛙石
Rei Sato
玲維 佐藤
Kenichi Mimura
健一 味村
Kaoru Shimokawara
薫 下河原
Yutaka Shikatani
裕 鹿谷
Koji Kunikiyo
浩志 國清
Takaaki Takeshita
隆顯 竹下
Atsushi Tsutsumi
敦司 堤
Chihiro Fushimi
千尋 伏見
Naoki Tsuru
直樹 鶴
Yasuki Kansha
寂樹 甘蔗
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Chiyoda Corp
University of Tokyo NUC
Chiyoda Chemical Engineering and Construction Co Ltd
Eneos Corp
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Chiyoda Corp
University of Tokyo NUC
Chiyoda Chemical Engineering and Construction Co Ltd
Nippon Oil Corp
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Abstract

<P>PROBLEM TO BE SOLVED: To provide a separation process module having high energy saving effect. <P>SOLUTION: The separation process module 100 is provided with a separator S separating input fluid into a first output fluid and a second output fluid; a first branched part J1 branching the first output fluid output from the separator S; a compressor C to raise the temperature of the first output fluid output from the first branched part J1 by compressing it; a second branched part j2 branching the second output fluid output from the separator S; and a heat exchanger H heat-exchanging between the second output fluid output from the second branched part j2 and the first fluid compressed by the compressor C. The first output fluid having passed through the heat exchanger H and second output fluid having passed through the heat exchanger H are input into the separator S. <P>COPYRIGHT: (C)2010,JPO&INPIT

Description

本発明は、分離プロセスモジュールに関する。   The present invention relates to a separation process module.

蒸留塔の塔頂蒸気を全て圧縮機で昇圧した後、リボイラに供給することによって熱回収を行う蒸留装置が知られている（例えば特許文献１，２参照）。
特開昭６０−１９７３１号公報 特許第３１２８８０９号公報 2. Description of the Related Art There is known a distillation apparatus that recovers heat by boosting all the vapor at the top of a distillation column with a compressor and then supplying it to a reboiler (see, for example, Patent Documents 1 and 2).
JP 60-19731 A Japanese Patent No. 3128809

しかしながら、上記蒸留装置では、塔頂蒸気を全て圧縮機で昇圧してリボイラに供給しているので、系外に出力される塔頂蒸気までも無駄に圧縮してしまっている。そのため、省エネルギー効果はいずれも不十分である。   However, in the distillation apparatus, since all the tower top steam is pressurized by the compressor and supplied to the reboiler, the tower top steam output to the outside of the system is also compressed wastefully. Therefore, any energy saving effect is insufficient.

本発明は、上記事情に鑑みて為されたものであり、省エネルギー効果の高い分離プロセスモジュールを提供することを目的とする。   The present invention has been made in view of the above circumstances, and an object thereof is to provide a separation process module having a high energy saving effect.

上述の課題を解決するため、本発明の分離プロセスモジュールは、第１成分及び前記第１成分とは異なる第２成分を含む入力流体が入力される入力端と、前記入力端に入力された前記入力流体を、気体の前記第１成分を含む第１出力流体と、前記第２成分を含む第２出力流体とに分離する分離器と、前記分離器から出力された前記第１出力流体を分岐する第１分岐部と、前記第１分岐部から出力され、気体の前記第１成分を含む前記第１出力流体を圧縮することによって昇温させる圧縮機と、前記分離器から出力された前記第２出力流体を分岐する第２分岐部と、前記第２分岐部から出力された前記第２出力流体と、前記圧縮機によって圧縮された前記第１出力流体との間で熱交換を行う熱交換器と、前記第１分岐部から出力された前記第１出力流体を出力する第１出力端と、前記第２分岐部から出力された前記第２出力流体を出力する第２出力端と、を備え、前記熱交換器を通過した前記第１出力流体と、前記熱交換器を通過した前記第２出力流体とが、前記分離器に入力される。   In order to solve the above-described problems, the separation process module of the present invention includes an input end to which an input fluid including a first component and a second component different from the first component is input, and the input to the input end. A separator that separates an input fluid into a first output fluid that includes the first component of gas and a second output fluid that includes the second component, and the first output fluid output from the separator is branched A first branching section, a compressor that is output from the first branching section and that raises the temperature by compressing the first output fluid containing the first component of gas, and the first output from the separator Heat exchange for exchanging heat between the second branch part that branches the two output fluids, the second output fluid output from the second branch part, and the first output fluid compressed by the compressor And the first output from the first branching unit A first output end that outputs a force fluid; and a second output end that outputs the second output fluid output from the second branch portion; and the first output fluid that has passed through the heat exchanger; The second output fluid that has passed through the heat exchanger is input to the separator.

本発明の分離プロセスモジュールでは、第１出力流体及び第２出力流体をそれぞれ第１出力端及び第２出力端から系外に出力すると共に、分離器から出力された第１出力流体及び第２出力流体を分離器に還流させることができる。その際、熱交換器において、第２出力流体が、圧縮機によって圧縮された第１出力流体によって昇温される。   In the separation process module of the present invention, the first output fluid and the second output fluid are output from the first output end and the second output end to the outside of the system, respectively, and the first output fluid and the second output output from the separator are output. The fluid can be refluxed to the separator. At that time, in the heat exchanger, the temperature of the second output fluid is increased by the first output fluid compressed by the compressor.

この場合、圧縮機によって第１出力流体を圧縮する際に所定エネルギーの仕事が必要になるが、第２出力流体を別途ボイラー等の加熱炉で加熱する必要は殆どなくなる。   In this case, when the first output fluid is compressed by the compressor, work of a predetermined energy is required, but there is almost no need to separately heat the second output fluid in a heating furnace such as a boiler.

また、分離器から出力された第１出力流体を、圧縮機によって圧縮する前に第１分岐部によって分岐して第１出力端から出力することができる。このため、第１出力端から系外に出力される第１出力流体を無駄に圧縮する必要がない。よって、圧縮に必要なエネルギーを低減することができる。   In addition, the first output fluid output from the separator can be branched by the first branching section and output from the first output end before being compressed by the compressor. For this reason, it is not necessary to wastefully compress the first output fluid output from the first output end to the outside of the system. Therefore, energy required for compression can be reduced.

さらに、分離器から出力された第２出力流体を、熱交換器において昇温する前に第２分岐部によって分岐して第２出力端から出力することができる。このため、第２出力端から系外に出力される第２出力流体を無駄に昇温する必要がない。よって、昇温に必要なエネルギーを低減することができる。   Furthermore, the second output fluid output from the separator can be branched by the second branching section before being heated in the heat exchanger and output from the second output end. For this reason, it is not necessary to unnecessarily raise the temperature of the second output fluid output from the second output end to the outside of the system. Therefore, energy required for temperature rise can be reduced.

したがって、本発明の分離プロセスモジュールでは、省エネルギー効果が大幅に高くなる。   Therefore, in the separation process module of the present invention, the energy saving effect is greatly increased.

また、前記第１出力端から出力される前記第１出力流体のエンタルピーと、前記第２出力端から出力される前記第２出力流体のエンタルピーとの和が、前記入力端に入力される前記入力流体のエンタルピーと同じであることが好ましい。これにより、分離プロセスモジュールを標準化されたモジュールとすることができる。   In addition, a sum of an enthalpy of the first output fluid output from the first output end and an enthalpy of the second output fluid output from the second output end is input to the input end. It is preferably the same as the enthalpy of the fluid. As a result, the separation process module can be a standardized module.

前記熱交換器を通過した前記第１出力流体は、液体の前記第１成分を含んでいることが好ましい。   The first output fluid that has passed through the heat exchanger preferably includes the liquid first component.

この場合、熱交換器において、圧縮機によって圧縮された第１出力流体が液化する際の潜熱を、分離器から出力された第２出力流体によって回収することができる。よって、省エネルギー効果が更に高くなる。   In this case, in the heat exchanger, the latent heat when the first output fluid compressed by the compressor is liquefied can be recovered by the second output fluid output from the separator. Therefore, the energy saving effect is further enhanced.

なお、上記構成要素を任意に組み合わせてもよいし、本発明の表現を方法、コンピュータプログラム、当該コンピュータプログラムが記録された記録媒体としてもよい。   Note that the above-described components may be arbitrarily combined, and the expression of the present invention may be a method, a computer program, or a recording medium on which the computer program is recorded.

本発明によれば、省エネルギー効果の高い分離プロセスモジュールが提供される。   According to the present invention, a separation process module having a high energy saving effect is provided.

以下、添付図面を参照しながら本発明の実施形態を詳細に説明する。なお、図面の説明において、同一又は同等の要素には同一符号を用い、重複する説明を省略する。   Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings. In the description of the drawings, the same reference numerals are used for the same or equivalent elements, and duplicate descriptions are omitted.

図１は、実施形態に係る分離プロセスモジュールを模式的に示す図である。図２は、本実施形態に係る分離プロセスモジュールにおける熱量Ｑと温度Ｔとの関係を示すグラフである。図１に示される分離プロセスモジュール１００は、入力端Ｉ、分離器Ｓ、第１分岐部Ｊ１、圧縮機Ｃ、第２分岐部Ｊ２、熱交換器Ｈ、第１出力端Ｅ１及び第２出力端Ｅ２を備える。   FIG. 1 is a diagram schematically illustrating a separation process module according to the embodiment. FIG. 2 is a graph showing the relationship between the heat quantity Q and the temperature T in the separation process module according to this embodiment. The separation process module 100 shown in FIG. 1 includes an input end I, a separator S, a first branch J1, a compressor C, a second branch J2, a heat exchanger H, a first output E1, and a second output. E2 is provided.

入力端Ｉには、第１成分及び第１成分とは異なる第２成分を含む入力流体が入力される。入力流体は、例えば気体の第１成分と液体の第２成分を含む。第１成分と第２成分とは、例えば沸点が異なる。一実施例において、入力流体は、第１成分としてベンゼン、第２成分としてトルエンを含む混合液である。入力端Ｉに入力された入力流体は、配管１を通って分離器Ｓに到達する。   An input fluid including a first component and a second component different from the first component is input to the input terminal I. The input fluid includes, for example, a gas first component and a liquid second component. The first component and the second component have different boiling points, for example. In one embodiment, the input fluid is a liquid mixture containing benzene as the first component and toluene as the second component. The input fluid input to the input end I reaches the separator S through the pipe 1.

分離器Ｓは、入力端Ｉに入力される入力流体を、気体の第１成分を含む第１出力流体と、第２成分を含む第２出力流体とに分離する。第１出力流体は例えば留出蒸気等であり、第２出力流体は例えば缶出液である。分離器Ｓは、気液分離器であることが好ましく、例えば蒸留塔、膜分離器、吸着分離器、フラッシュドラム等である。また、分離器Ｓは例えばフラッシュドラム等の単段の分離器であってもよいし、多段の分離器であってもよい。   The separator S separates the input fluid input to the input end I into a first output fluid that includes a gas first component and a second output fluid that includes a second component. The first output fluid is, for example, distillate vapor, and the second output fluid is, for example, bottom liquid. The separator S is preferably a gas-liquid separator, such as a distillation column, a membrane separator, an adsorption separator, or a flash drum. The separator S may be a single-stage separator such as a flash drum, or may be a multi-stage separator.

分離器Ｓから出力される第１出力流体は、例えば気体の第１成分を含み、配管２を通って第１分岐部Ｊ１に到達する。第１分岐部Ｊ１に到達した第１出力流体は、配管３を通って第１出力端Ｅ１に到達すると共に、配管４を通って圧縮機Ｃに到達する。第１分岐部Ｊ１は、分離器Ｓと第１出力端Ｅ１との間に配置され、分離器Ｓから出力された第１出力流体を分岐する。圧縮機Ｃは、第１分岐部Ｊ１から出力され、気体の第１成分を含む第１出力流体を圧縮することによって昇温させる。圧縮機Ｃは、例えばターボ圧縮機である。圧縮機Ｃの圧縮比は１．５〜５であることが好ましい。圧縮機Ｃは、第１出力流体の温度を１０〜５０℃上昇させることが好ましい。圧縮機Ｃによって圧縮された第１出力流体は、配管５を通って熱交換器Ｈに到達する。   The first output fluid output from the separator S includes, for example, a gas first component, and reaches the first branch portion J1 through the pipe 2. The first output fluid that has reached the first branch portion J1 reaches the first output end E1 through the pipe 3, and reaches the compressor C through the pipe 4. The first branch portion J1 is disposed between the separator S and the first output end E1, and branches the first output fluid output from the separator S. The compressor C raises the temperature by compressing the first output fluid that is output from the first branch portion J1 and that includes the first component of gas. The compressor C is a turbo compressor, for example. The compression ratio of the compressor C is preferably 1.5 to 5. The compressor C preferably increases the temperature of the first output fluid by 10 to 50 ° C. The first output fluid compressed by the compressor C reaches the heat exchanger H through the pipe 5.

一方、分離器Ｓから出力される第２出力流体は、例えば液体の第２成分を含み、配管９を通って第２分岐部Ｊ２に到達する。第２分岐部Ｊ２に到達した第２出力流体は、配管１０を通って第２出力端Ｅ２に到達すると共に、配管１１を通って熱交換器Ｈに到達する。第２分岐部Ｊ２は、分離器Ｓと第２出力端Ｅ２との間に配置され、分離器Ｓから出力された第２出力流体を分岐する。   On the other hand, the second output fluid output from the separator S includes, for example, a liquid second component, and reaches the second branch portion J2 through the pipe 9. The second output fluid that has reached the second branch portion J2 reaches the second output end E2 through the pipe 10, and reaches the heat exchanger H through the pipe 11. The second branch portion J2 is disposed between the separator S and the second output end E2, and branches the second output fluid output from the separator S.

熱交換器Ｈは、第２分岐部Ｊ２から出力された第２出力流体と、圧縮機Ｃによって圧縮された第１出力流体との間で熱交換を行う。熱交換器Ｈを通過した第１出力流体は、例えば液体の第１成分を含む。熱交換器Ｈを通過した第２出力流体は、例えば気体の第２成分を含む。   The heat exchanger H performs heat exchange between the second output fluid output from the second branch portion J2 and the first output fluid compressed by the compressor C. The first output fluid that has passed through the heat exchanger H includes, for example, a liquid first component. The second output fluid that has passed through the heat exchanger H includes, for example, a gaseous second component.

熱交換器Ｈでは、圧縮機Ｃによって圧縮された第１出力流体の温度と熱交換器Ｈを通過した第２出力流体との差（温度差Ａ）が、熱交換器Ｈを通過した第１出力流体の温度と熱交換器Ｈに入力される第２出力流体の温度との差（温度差Ｄ）と略同じであることが好ましい（図２参照）。この場合、熱交換器Ｈにおいて、効率よく熱交換することができる。   In the heat exchanger H, the difference (temperature difference A) between the temperature of the first output fluid compressed by the compressor C and the second output fluid that has passed through the heat exchanger H is the first that has passed through the heat exchanger H. It is preferable that the difference (temperature difference D) between the temperature of the output fluid and the temperature of the second output fluid input to the heat exchanger H is substantially the same (see FIG. 2). In this case, the heat exchanger H can efficiently exchange heat.

熱交換器Ｈを通過した第１出力流体は、配管６を通ってバルブＶに到達する。バルブＶは、熱交換器Ｈを通過した第１出力流体の圧力を、配管２を通る第１出力流体の圧力と同程度まで低下させる。バルブＶを通過した第１出力流体は、配管７を通って冷却器Ｌに到達する。冷却器Ｌによって冷却された第１出力流体は、配管８を通って分離器Ｓに戻る。一方、熱交換器Ｈを通過した第２出力流体は、配管１２を通って分離器Ｓに戻る。   The first output fluid that has passed through the heat exchanger H reaches the valve V through the pipe 6. The valve V reduces the pressure of the first output fluid that has passed through the heat exchanger H to the same level as the pressure of the first output fluid that passes through the pipe 2. The first output fluid that has passed through the valve V reaches the cooler L through the pipe 7. The first output fluid cooled by the cooler L returns to the separator S through the pipe 8. On the other hand, the second output fluid that has passed through the heat exchanger H returns to the separator S through the pipe 12.

ここで、第１出力端Ｅ１から出力される第１出力流体のエンタルピーと第２出力端Ｅ２から出力される第２出力流体のエンタルピーとの和が、入力端Ｉに入力される入力流体のエンタルピーと同じであることが好ましい。これにより、分離プロセスモジュール１００を標準化されたモジュールとすることができる。   Here, the sum of the enthalpy of the first output fluid output from the first output end E1 and the enthalpy of the second output fluid output from the second output end E2 is the enthalpy of the input fluid input to the input end I. Is preferably the same. As a result, the separation process module 100 can be a standardized module.

分離プロセスモジュール１００では、第１出力流体及び第２出力流体をそれぞれ第１出力端Ｅ１及び第２出力端Ｅ２から系外に出力すると共に、分離器Ｓから出力された第１出力流体及び第２出力流体を分離器Ｓに還流させることができる。   The separation process module 100 outputs the first output fluid and the second output fluid from the first output end E1 and the second output end E2 to the outside of the system, and the first output fluid and the second output fluid output from the separator S, respectively. The output fluid can be refluxed to the separator S.

また、図２に示されるように、熱交換器Ｈにおいて熱量Ｑ１と熱量Ｑ２とが熱交換されるので、第２出力流体が第１出力流体によって昇温される。圧縮機Ｃによって第１出力流体を圧縮する際に所定エネルギーの仕事Ｗｃが必要になるが、第２出力流体を別途ボイラー等の加熱炉で加熱する必要は殆どなくなる。一方、第１出力流体を圧縮しない場合、第２出力流体を別途ボイラー等の加熱炉で加熱する必要がある。別途ボイラー等の加熱炉で加熱する際に必要なエネルギーは、第１出力流体を圧縮する際に必要な所定エネルギーに比べて非常に大きい。 Further, as shown in FIG. 2, since the amount of heat Q 2 are exchange heat with heat Q 1 in the heat exchanger H, the second output fluid is heated by the first output fluid. Although it is necessary to work W c of a predetermined energy in compressing the first output fluid by the compressor C, is necessary to heat a heating furnace separately such boilers the second output fluid almost eliminated. On the other hand, when the first output fluid is not compressed, the second output fluid needs to be separately heated in a heating furnace such as a boiler. Separately, the energy required for heating in a heating furnace such as a boiler is much larger than the predetermined energy required for compressing the first output fluid.

分離器Ｓから出力された第１出力流体を、圧縮機Ｃによって圧縮する前に第１分岐部Ｊ１によって分岐して第１出力端Ｅ１から出力することができる。このため、第１出力端Ｅ１から系外に出力される第１出力流体を無駄に圧縮する必要がない。よって、圧縮に必要なエネルギーを低減することができる。   The first output fluid output from the separator S can be branched by the first branch portion J1 before being compressed by the compressor C and output from the first output end E1. For this reason, it is not necessary to wastefully compress the first output fluid output from the first output end E1 to the outside of the system. Therefore, energy required for compression can be reduced.

さらに、分離器Ｓから出力された第２出力流体を、熱交換器Ｈにおいて昇温する前に第２分岐部Ｊ２によって分岐して第２出力端Ｅ２から出力することができる。このため、第２出力端Ｅ２から系外に出力される第２出力流体を無駄に昇温する必要がない。よって、昇温に必要なエネルギーを低減することができる。   Further, the second output fluid output from the separator S can be branched by the second branch portion J2 before being heated in the heat exchanger H and output from the second output end E2. For this reason, it is not necessary to unnecessarily raise the temperature of the second output fluid output from the second output end E2 to the outside of the system. Therefore, energy required for temperature rise can be reduced.

以上説明したように、分離プロセスモジュール１００では、省エネルギー効果が大幅に高くなる。   As described above, in the separation process module 100, the energy saving effect is significantly increased.

また、熱交換器Ｈを通過した第１出力流体が、液体の第１成分を含む場合、熱交換器Ｈにおいて、圧縮機Ｃによって圧縮された第１出力流体が液化する際の潜熱を、第２出力流体によって回収することができる。よって、省エネルギー効果が更に高くなる。   Further, when the first output fluid that has passed through the heat exchanger H contains the first component of the liquid, in the heat exchanger H, the latent heat when the first output fluid compressed by the compressor C is liquefied is It can be recovered by two output fluids. Therefore, the energy saving effect is further enhanced.

さらに、現状の分離器をそのまま使用して、分離器の周辺を改良するだけで高い省エネルギー効果が低コストかつ短時間で得られる。   Furthermore, a high energy saving effect can be obtained in a low cost and in a short time by simply using the current separator as it is and improving the periphery of the separator.

図３は、比較例に係る分離プロセスモジュールを模式的に示す図である。図４は、比較例に係る分離プロセスモジュールにおける熱量Ｑと温度Ｔとの関係を示すグラフである。図３に示される分離プロセスモジュール１００ａは、加熱炉Ｂ、分離器Ｓ、冷却器Ｌを備えている。入力端Ｉに入力された入力流体は、配管１を通って分離器Ｓに到達する。   FIG. 3 is a diagram schematically illustrating a separation process module according to a comparative example. FIG. 4 is a graph showing the relationship between the heat quantity Q and the temperature T in the separation process module according to the comparative example. The separation process module 100a shown in FIG. 3 includes a heating furnace B, a separator S, and a cooler L. The input fluid input to the input end I reaches the separator S through the pipe 1.

分離器Ｓから出力される第１出力流体は、配管２を通ってコンデンサ等の冷却器Ｌに到達する。冷却器Ｌによって冷却された第１出力流体は、配管１３を通って分岐部Ｊ３に到達する。分岐部Ｊ３に到達した第１出力流体は、配管１４を通って分離器Ｓに戻ると共に、配管１５を通って第１出力端Ｅ１に到達する。   The first output fluid output from the separator S reaches the cooler L such as a condenser through the pipe 2. The first output fluid cooled by the cooler L reaches the branch portion J3 through the pipe 13. The first output fluid that has reached the branch portion J3 returns to the separator S through the pipe 14, and reaches the first output end E1 through the pipe 15.

分離器Ｓから出力される第２出力流体は、配管９を通ってリボイラ等の加熱炉Ｂに到達する。加熱炉Ｂによって加熱された第２出力流体は、配管１６を通って分離器Ｓに戻ると共に、配管１７を通って第２出力端Ｅ２に到達する。   The second output fluid output from the separator S reaches the heating furnace B such as a reboiler through the pipe 9. The second output fluid heated by the heating furnace B returns to the separator S through the pipe 16 and reaches the second output end E2 through the pipe 17.

分離プロセスモジュール１００ａでは、図４に示されるように、加熱炉Ｂでは熱量Ｑ１が必要となり、冷却器Ｌでは熱量Ｑ１と同等の熱量Ｑ２が排熱される。 In the separation process modules 100a, as shown in FIG. 4, the furnace heat Q 1 is required in B, cooler heat Q 1, equivalent to the amount of heat Q 2 at L is waste heat.

したがって、本実施形態に係る分離プロセスモジュール１００では、分離プロセスモジュール１００ａに比べて、省エネルギー効果が高くなる。   Therefore, the separation process module 100 according to the present embodiment has a higher energy saving effect than the separation process module 100a.

以上、本発明の好適な実施形態について詳細に説明したが、本発明は上記実施形態に限定されない。   As mentioned above, although preferred embodiment of this invention was described in detail, this invention is not limited to the said embodiment.

実施形態に係る分離プロセスモジュールを模式的に示す図である。It is a figure which shows typically the separation process module which concerns on embodiment. 本実施形態に係る分離プロセスモジュールにおける熱量Ｑと温度Ｔとの関係を示すグラフである。It is a graph which shows the relationship between the calorie | heat amount Q and temperature T in the separation process module which concerns on this embodiment. 比較例に係る分離プロセスモジュールを模式的に示す図である。It is a figure which shows typically the separation process module which concerns on a comparative example. 比較例に係る分離プロセスモジュールにおける熱量Ｑと温度Ｔとの関係を示すグラフである。It is a graph which shows the relationship between the calorie | heat amount Q and temperature T in the separation process module which concerns on a comparative example.

符号の説明Explanation of symbols

Ｉ…入力端、Ｓ…分離器、Ｊ１…第１分岐部、Ｃ…圧縮機、Ｊ２…第２分岐部、Ｈ…熱交換器、Ｅ１…第１出力端、Ｅ２…第２出力端、１００…分離プロセスモジュール。   I ... Input end, S ... Separator, J1 ... First branch, C ... Compressor, J2 ... Second branch, H ... Heat exchanger, E1 ... First output end, E2 ... Second output end, 100 … Separate process module.

Claims (3)

第１成分及び前記第１成分とは異なる第２成分を含む入力流体が入力される入力端と、
前記入力端に入力された前記入力流体を、気体の前記第１成分を含む第１出力流体と、前記第２成分を含む第２出力流体とに分離する分離器と、
前記分離器から出力された前記第１出力流体を分岐する第１分岐部と、
前記第１分岐部から出力され、気体の前記第１成分を含む前記第１出力流体を圧縮することによって昇温させる圧縮機と、
前記分離器から出力された前記第２出力流体を分岐する第２分岐部と、
前記第２分岐部から出力された前記第２出力流体と、前記圧縮機によって圧縮された前記第１出力流体との間で熱交換を行う熱交換器と、
前記第１分岐部から出力された前記第１出力流体を出力する第１出力端と、
前記第２分岐部から出力された前記第２出力流体を出力する第２出力端と、
を備え、
前記熱交換器を通過した前記第１出力流体と、前記熱交換器を通過した前記第２出力流体とが、前記分離器に入力される、分離プロセスモジュール。 An input end to which an input fluid including a first component and a second component different from the first component is input;
A separator that separates the input fluid input to the input end into a first output fluid containing the first component of gas and a second output fluid containing the second component;
A first branching section for branching the first output fluid output from the separator;
A compressor that raises the temperature by compressing the first output fluid that is output from the first branch part and includes the first component of gas;
A second branching section for branching the second output fluid output from the separator;
A heat exchanger for exchanging heat between the second output fluid output from the second branch and the first output fluid compressed by the compressor;
A first output terminal for outputting the first output fluid output from the first branch part;
A second output terminal for outputting the second output fluid output from the second branch part;
With
The separation process module, wherein the first output fluid that has passed through the heat exchanger and the second output fluid that has passed through the heat exchanger are input to the separator. 前記第１出力端から出力される前記第１出力流体のエンタルピーと、前記第２出力端から出力される前記第２出力流体のエンタルピーとの和が、前記入力端に入力される前記入力流体のエンタルピーと同じである、請求項１に記載の分離プロセスモジュール。   The sum of the enthalpy of the first output fluid output from the first output end and the enthalpy of the second output fluid output from the second output end is the sum of the input fluid input to the input end. The separation process module of claim 1, which is the same as enthalpy. 前記熱交換器を通過した前記第１出力流体は、液体の前記第１成分を含んでいる、請求項１又は２に記載の分離プロセスモジュール。   The separation process module according to claim 1 or 2, wherein the first output fluid that has passed through the heat exchanger includes the first component of liquid.
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2012045449A (en) * 2010-08-24 2012-03-08 Jx Nippon Oil & Energy Corp Separation process module
JP2012110832A (en) * 2010-11-24 2012-06-14 Chiyoda Kako Kensetsu Kk Device for separating azeotropic mixture and method for separating azeotropic mixture

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GB1452377A (en) * 1974-04-10 1976-10-13 British Petroleum Co Distillation
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DE1114168B (en) * 1960-08-03 1961-09-28 Bayer Ag Distillation device with heat pump
US3592015A (en) * 1967-12-21 1971-07-13 Messer Griesheim Gmbh Rectification column with two component closed heat exchange cycle
GB1452377A (en) * 1974-04-10 1976-10-13 British Petroleum Co Distillation
JPS62502587A (en) * 1985-04-09 1987-10-08 フオエスト−アルピネ　アクチエンゲゼルシヤフト Equipment that continuously collects ethanol from saccharification starting materials

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2012045449A (en) * 2010-08-24 2012-03-08 Jx Nippon Oil & Energy Corp Separation process module
JP2012110832A (en) * 2010-11-24 2012-06-14 Chiyoda Kako Kensetsu Kk Device for separating azeotropic mixture and method for separating azeotropic mixture

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