JP6368179B2 - Distillation equipment and distillation method - Google Patents

Distillation equipment and distillation method Download PDF

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JP6368179B2
JP6368179B2 JP2014141700A JP2014141700A JP6368179B2 JP 6368179 B2 JP6368179 B2 JP 6368179B2 JP 2014141700 A JP2014141700 A JP 2014141700A JP 2014141700 A JP2014141700 A JP 2014141700A JP 6368179 B2 JP6368179 B2 JP 6368179B2
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distillation
cooled cooler
air
water
pressure steam
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JP2016016379A (en
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松田　一夫
一夫 松田
田中　茂樹
茂樹 田中
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Chiyoda Corp
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B27/00—Machines, plants or systems, using particular sources of energy
    • F25B27/02—Machines, plants or systems, using particular sources of energy using waste heat, e.g. from internal-combustion engines
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A30/00—Adapting or protecting infrastructure or their operation
    • Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
    • Y02A30/274—Relating to heating, ventilation or air conditioning [HVAC] technologies using waste energy, e.g. from internal combustion engine

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  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
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  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Description

本発明は、プラントにおいて原料を蒸留する蒸留設備および蒸留方法並びに蒸留設備の改造方法に関する。   The present invention relates to a distillation facility and distillation method for distilling raw materials in a plant, and a method for remodeling the distillation facility.

石油・石油化学等の産業プラントの蒸留設備では、蒸留塔の塔頂から流出する塔頂蒸気の凝縮方法として、空気を用いた空冷、冷却水を用いた水冷、それらを組み合わせた方法等が採用されている。蒸留塔の運転圧力を低下させる省エネルギーは広く知られており、省エネルギー実現のための課題の一つとなっている。   In the distillation equipment of industrial plants such as petroleum and petrochemicals, methods such as air cooling using air, water cooling using cooling water, or a combination of these methods are used as condensation methods for the top vapor flowing out from the top of the distillation column. Has been. Energy saving that lowers the operating pressure of the distillation tower is widely known and has become one of the challenges for realizing energy saving.

蒸留塔の運転圧力は、塔頂蒸気の凝縮温度で一様に決まり、凝縮温度が下がれば運転圧力も下がる。蒸留塔の運転圧力を下げると原料中の成分の比揮発度が大きくなり成分の分離が容易になる。従って、塔頂及び塔底の留出物（製品）の純度を所定の値に維持するための蒸留塔の内部還流が少なくできる。内部還流量は測定が困難であるが、外部還流量（以降、還流と呼ぶ）と相関があるので、一般的には還流比（＝還流量/塔頂留出量）を塔頂及び塔底の留出物の純度の管理に用いている。塔頂留出量（製品）を一定とすると内部還流が少なくできれば、それを気化（再蒸発）するリボイラーの負荷も下げられる。従って、リボイラーに供給するエネルギーが減って省エネルギーを図ることができる。   The operation pressure of the distillation column is uniformly determined by the condensation temperature of the top vapor, and the operation pressure decreases as the condensation temperature decreases. When the operating pressure of the distillation column is lowered, the relative volatility of the components in the raw material increases and the components can be easily separated. Therefore, the internal reflux of the distillation column for maintaining the purity of the distillate (product) at the top and bottom of the column at a predetermined value can be reduced. Although the internal reflux amount is difficult to measure, it generally correlates with the external reflux amount (hereinafter referred to as reflux), so generally the reflux ratio (= reflux amount / column top distillate) is set at the top and bottom of the column. It is used to control the purity of the distillate. If the amount of product at the top of the column is kept constant, if the internal reflux can be reduced, the load on the reboiler that vaporizes (re-evaporates) it can be reduced. Accordingly, the energy supplied to the reboiler can be reduced to save energy.

特開２００５−７９６号公報JP 2005-796 A

塔頂蒸気の凝縮温度をより下げるためにはより高い冷却能力が必要となる。しかしながら、従来の空気や冷却水を用いた塔頂蒸気の凝縮方法の場合、冷却媒体である空気や冷却水の温度は自然条件に依存するため、常に設定した冷却能力を期待するのは難しく、従って塔頂蒸気の凝縮温度の維持には限界がある。特に夏期の気温上昇に伴い空気や冷却水の温度が高くなって冷却能力が著しく低下するため、塔頂蒸気の凝縮温度は高く設定せざるを得ない。従って、従来の空気や冷却水を用いた塔頂蒸気の凝縮方法では、蒸留塔の運転圧力を下げて省エネルギーを図ることは難しい。   In order to lower the condensation temperature of the top vapor, a higher cooling capacity is required. However, in the case of the conventional method of condensing the top steam using air or cooling water, the temperature of the cooling medium, air or cooling water, depends on the natural conditions, so it is difficult to always expect the set cooling capacity. Therefore, there is a limit in maintaining the condensation temperature of the top vapor. In particular, as the temperature rises in summer, the temperature of air and cooling water increases and the cooling capacity decreases significantly. Therefore, the condensation temperature of the top steam must be set high. Therefore, it is difficult to save energy by lowering the operation pressure of the distillation column in the conventional method for condensing the top vapor using air or cooling water.

本発明は、こうした状況を鑑みてなされたものであり、その目的は、省エネルギーを図ることのできる蒸留設備、蒸留方法および蒸留設備の改造方法を提供することにある。   This invention is made | formed in view of such a condition, The objective is to provide the distillation equipment which can aim at energy saving, the distillation method, and the remodeling method of distillation equipment.

上記課題を解決するために、本発明のある態様の蒸留設備は、プラント内に設けられる蒸留設備であって、供給された原料を蒸留する蒸留塔と、プラント内で発生した熱を用いて冷水を製造する冷凍機と、蒸留塔から流出する塔頂蒸気を製造された冷水を用いて凝縮させる水冷冷却器と、水冷冷却器で凝縮した液体の一部を蒸留塔に還流させる還流装置と、を備える。   In order to solve the above-mentioned problems, a distillation facility according to an aspect of the present invention is a distillation facility provided in a plant, which is a distillation column for distilling a supplied raw material, and cold water using heat generated in the plant. A water-cooled condenser that condenses the top vapor flowing out from the distillation tower using the produced cold water, a reflux device that recirculates a part of the liquid condensed by the water-cooled condenser to the distillation tower, Is provided.

プラント内で発生した熱を用いて低圧蒸気を発生させる低圧蒸気発生装置をさらに備え、冷凍機は、低圧蒸気発生装置で発生した低圧蒸気を用いて冷水を製造してもよい。   The apparatus may further include a low-pressure steam generator that generates low-pressure steam using heat generated in the plant, and the refrigerator may produce cold water using the low-pressure steam generated by the low-pressure steam generator.

低圧蒸気発生装置で用いる熱は、プラント内で発生したプロセス流体から得られてもよい。   The heat used in the low pressure steam generator may be derived from process fluid generated in the plant.

蒸留塔から流出する塔頂蒸気を空冷する空冷冷却器をさらに備えてもよい。   You may further provide the air-cooling cooler which air-cools the top vapor | steam which flows out from a distillation column.

空冷冷却器は、水冷冷却器の上流に設けられてもよい。空冷冷却器と還流装置とを直接接続するためのバイパスラインをさらに備えてもよい。   The air-cooled cooler may be provided upstream of the water-cooled cooler. A bypass line for directly connecting the air-cooled cooler and the reflux device may be further provided.

冷凍機により製造される冷水は、７℃〜１２℃であってもよい。   The cold water produced by the refrigerator may be 7 ° C to 12 ° C.

本発明の別の態様は、プラント内での蒸留方法である。この方法は、蒸留塔を用いて供給された原料を蒸留する工程と、プラント内で発生した熱を用いて冷水を製造する工程と、蒸留塔から流出する塔頂蒸気を製造された冷水を用いて凝縮させる工程と、還流装置を用いて凝縮した液体の一部を蒸留塔に還流させる工程と、を備える。   Another aspect of the present invention is a distillation method in a plant. This method uses a step of distilling a raw material supplied using a distillation tower, a step of producing cold water using heat generated in the plant, and a cold water produced from the top vapor flowing out of the distillation tower. And a step of condensing the liquid condensed using the reflux device to the distillation column.

冷水を用いて凝縮させる工程で用いる水冷冷却器の上流に、蒸留塔から流出する塔頂蒸気を空冷する空冷冷却器が設けられてもよい。空冷冷却器と還流装置とがバイパスラインを介して直接接続されてもよい。プラントの環境条件に基づいて、空冷冷却器を通過した塔頂蒸気および／またはその凝縮液が水冷冷却器を介して還流装置に入る第１動作状態と、空冷冷却器を通過した塔頂蒸気および／またはその凝縮液がバイパスラインを介して直接還流装置に入る第２動作状態とを切り替える工程をさらに備えてもよい。   An air-cooled cooler for air-cooling the top vapor flowing out from the distillation tower may be provided upstream of the water-cooled cooler used in the step of condensing with cold water. The air-cooled cooler and the reflux device may be directly connected via a bypass line. Based on the environmental conditions of the plant, a first operating state in which the overhead vapor passing through the air-cooled cooler and / or its condensate enters the reflux device via the water-cooled cooler, and the overhead steam passed through the air-cooled cooler and A step of switching the second operation state in which the condensed liquid enters the reflux device directly via the bypass line may be further provided.

本発明のさらに別の態様は、プラント内に設けられた蒸留塔から流出する塔頂蒸気を空冷冷却器で凝縮させる蒸留設備の改造方法である。この方法は、プラント内で発生した熱を用いて冷水を製造する冷凍機を設ける工程と、蒸留塔から流出する塔頂蒸気を冷凍機で製造された冷水を用いて凝縮させる水冷冷却器を設ける工程と、を備える。   Yet another embodiment of the present invention is a method for remodeling a distillation facility for condensing an overhead vapor flowing out from a distillation column provided in a plant with an air-cooled cooler. This method includes a step of providing a refrigerator for producing cold water using heat generated in the plant, and a water-cooled cooler for condensing the top vapor flowing out from the distillation tower using the cold water produced by the refrigerator. A process.

蒸留設備は、凝縮した液体の一部を蒸留塔に還流させる還流装置を備え、水冷冷却器は、改造前の空冷冷却器と還流装置とを直接接続するラインを残したまま、空冷冷却器の下流にラインと並列に設けられてもよい。   The distillation equipment is equipped with a reflux device for refluxing a part of the condensed liquid to the distillation tower, and the water-cooled cooler is the air-cooled cooler while leaving a line directly connecting the air-cooled cooler and the reflux device before the modification. It may be provided downstream in parallel with the line.

なお、以上の構成要素の任意の組合せ、本発明の表現を方法、装置、システム、記録媒体、コンピュータプログラムなどの間で変換したものもまた、本発明の態様として有効である。   It should be noted that any combination of the above-described constituent elements and a conversion of the expression of the present invention between a method, an apparatus, a system, a recording medium, a computer program, etc. are also effective as an aspect of the present invention.

本発明によれば、省エネルギーを図ることのできる蒸留設備、蒸留方法および蒸留設備の改造方法を提供できる。   ADVANTAGE OF THE INVENTION According to this invention, the distillation installation which can aim at energy saving, the distillation method, and the remodeling method of a distillation installation can be provided.

本発明の実施形態に係る蒸留設備を説明するための図である。It is a figure for demonstrating the distillation installation which concerns on embodiment of this invention. 図２（ａ）および（ｂ）は、本発明の実施形態に係る蒸留設備の改造方法を説明するための図である。FIGS. 2A and 2B are views for explaining a method for remodeling a distillation facility according to an embodiment of the present invention. 改造前と改造後の蒸留設備による蒸留のシミュレーション結果を示す図である。It is a figure which shows the simulation result of distillation by the distillation installation before remodeling and after remodeling. シミュレーション計算に用いた吸収式冷凍機および吸収式冷凍機まわりの設定条件を示す図である。It is a figure which shows the setting conditions around the absorption refrigerator used for the simulation calculation, and an absorption refrigerator.

図１は、本発明の実施形態に係る蒸留設備１０を説明するための図である。図１に示す蒸留設備１０は、例えば石油精製プラントや石油化学プラント等の産業プラント内に設けられる。   FIG. 1 is a diagram for explaining a distillation facility 10 according to an embodiment of the present invention. The distillation facility 10 shown in FIG. 1 is provided in an industrial plant such as an oil refinery plant or a petrochemical plant.

図１に示すように、蒸留設備１０は、蒸留塔１２と、リボイラー１４と、空冷冷却器１６と、水冷冷却器１８と、還流装置２０と、吸収式冷凍機２２と、低圧蒸気発生装置２４とを備える。   As shown in FIG. 1, the distillation facility 10 includes a distillation column 12, a reboiler 14, an air-cooled cooler 16, a water-cooled cooler 18, a reflux device 20, an absorption refrigerator 22, and a low-pressure steam generator 24. With.

蒸留塔１２は、内部にトレイ等の構造物が設置されていて塔頂部１２ｃから流下してくる液と塔底部１２ｂから上昇してくる蒸気が熱交換と物質移動を繰り返して目的の純度の製品を得る機能を持つ。蒸留塔１２の塔頂からは揮発性の高い成分に富む、塔底からは揮発性の低い成分に富む留出液が抜き出される。蒸留塔１２は、その中段部に設けられた原料供給口１２ａから供給された原料を蒸留する。蒸留塔１２内に供給された原料は、気液の２相からなり、液は蒸留塔１２内を流下してきた液と合流して塔底部１２ｂにおいてリボイラー１４により加熱される。リボイラー１４の加熱により、塔底部１２ｂの塔底液の一部は蒸気とされ、塔頂部１２ｃに向かって上昇する。蒸気とならない塔底液は塔底留出液となる。原料供給口１２ａで蒸気となった原料はリボイラー１４からの蒸気と合流して蒸留塔１２内を上昇する。また、蒸留塔１２からの塔頂蒸気は凝縮されて還流装置を経て一部は塔頂留出液として抜き出され、残りは蒸留塔１２の塔頂部１２ｃに設けられた還流液供給口１２ｄから還流液として供給される。   The distillation column 12 is provided with a structure such as a tray. The liquid flowing down from the column top 12c and the vapor rising from the column bottom 12b repeat the heat exchange and mass transfer to obtain a product of the desired purity. With the ability to get A distillate rich in highly volatile components is extracted from the top of the distillation column 12 and a low volatile component is extracted from the bottom of the column. The distillation column 12 distills the raw material supplied from the raw material supply port 12a provided in the middle stage. The raw material supplied into the distillation column 12 consists of two phases of gas and liquid. The liquid joins with the liquid flowing down in the distillation column 12 and is heated by the reboiler 14 at the tower bottom 12b. Due to the heating of the reboiler 14, a part of the column bottom liquid at the column bottom 12b is converted to steam and rises toward the column top 12c. The bottom liquid that does not become steam becomes the bottom distillate. The raw material that has become steam at the raw material supply port 12 a joins with the steam from the reboiler 14 and rises in the distillation column 12. Further, the top vapor from the distillation column 12 is condensed and partly extracted as a column top distillate through a reflux device, and the rest from a reflux liquid supply port 12d provided at the top 12c of the distillation column 12. Supplied as reflux.

蒸気取出口１２ｅから流出した塔頂蒸気は、ライン１７を介して水冷冷却器１８に入る。水冷冷却器１８は、吸収式冷凍機２２からの冷水を用いて塔頂蒸気を凝縮させる。水冷冷却器１８により凝縮された液体は、還流装置２０に送られる。   The tower top steam flowing out from the steam outlet 12 e enters the water-cooled cooler 18 through the line 17. The water-cooled cooler 18 condenses the top vapor using the cold water from the absorption refrigerator 22. The liquid condensed by the water cooling cooler 18 is sent to the reflux device 20.

蒸留塔１２と水冷冷却器１８とを接続するライン１７上に空冷冷却器１６が設けられてもよい。すなわち、水冷冷却器１８の上流に空冷冷却器１６が設けられてもよい。空冷冷却器１６は、蒸留塔１２からの塔頂蒸気の少なくとも一部を凝縮するよう構成されてよい。この構成の場合、蒸留塔１２からの塔頂蒸気およびその凝縮液は、空冷冷却器１６、水冷冷却器１８を順に通過した後、留出液タンク２１に入る。   An air-cooled cooler 16 may be provided on a line 17 that connects the distillation column 12 and the water-cooled cooler 18. That is, the air cooling cooler 16 may be provided upstream of the water cooling cooler 18. The air-cooled cooler 16 may be configured to condense at least a portion of the top vapor from the distillation column 12. In this configuration, the top vapor from the distillation column 12 and the condensate thereof pass through the air-cooled cooler 16 and the water-cooled cooler 18 in this order, and then enter the distillate tank 21.

還流装置２０は、水冷冷却器１８で凝縮した液体の一部を蒸留塔１２に還流させる。還流装置２０は、留出液タンク２１と、ポンプ２３とを含む。水冷冷却器１８で凝縮した液体は留出液タンク２１に貯留される。留出液タンク２１に貯留された液体は、ポンプ２３により昇圧された後、その一部が留出液として取り出され、残りが還流液として還流液供給口１２ｄを介して蒸留塔１２内に還流される。   The reflux device 20 refluxes part of the liquid condensed by the water-cooled cooler 18 to the distillation column 12. The reflux device 20 includes a distillate tank 21 and a pump 23. The liquid condensed by the water cooling cooler 18 is stored in the distillate tank 21. The liquid stored in the distillate tank 21 is pressurized by the pump 23, and then a part of the liquid is taken out as a distillate, and the remainder is refluxed as a reflux liquid into the distillation column 12 through the reflux liquid supply port 12d. Is done.

低圧蒸気発生装置２４は、プラント内で発生したプロセス流体を用いて低圧蒸気を発生させる。低圧蒸気発生装置２４は、ケトル型熱交換器２５と、ポンプ２６とを備える。ケトル型熱交換器２５は、ボイラー給水（ＢＦＷ：Boiler Feed Water）が供給される。ケトル型熱交換器２５は、プロセス流体との熱交換によりこのＢＦＷを加熱蒸発し、例えば０．１５ＭＰａＧから０．２０ＭＰａＧの低圧蒸気を発生させる。プロセス流体とは、プラント内で所定の生産を行うためのプロセス設備（例えば、反応器や熱交換器など）で生じた流体である。例えば石油プラントであれば、石油からガソリンを生成するためのプロセス設備、ガソリンからナフサを生成するためのプロセス設備、石油から灯油を生成するためのプロセス設備などである。   The low-pressure steam generator 24 generates low-pressure steam using a process fluid generated in the plant. The low pressure steam generator 24 includes a kettle heat exchanger 25 and a pump 26. The kettle heat exchanger 25 is supplied with boiler feed water (BFW). The kettle heat exchanger 25 heats and evaporates the BFW by heat exchange with the process fluid, and generates low-pressure steam of, for example, 0.15 MPaG to 0.20 MPaG. The process fluid is a fluid generated in a process facility (for example, a reactor or a heat exchanger) for performing predetermined production in the plant. For example, in the case of an oil plant, there are a process facility for generating gasoline from petroleum, a process facility for generating naphtha from gasoline, a process facility for generating kerosene from petroleum, and the like.

吸収式冷凍機２２は、低圧蒸気発生装置２４で発生した低圧蒸気を用いて冷水を製造する。本実施形態では、吸収式冷凍機２２として水・臭化リチウム系のものを用いるが、吸収式冷凍機２２はこれに限定されない。吸収式冷凍機２２で製造される冷水の温度は、７℃〜１２℃であってよい。吸収式冷凍機２２から排出された凝縮水は、ポンプ２６を介して再びＢＦＷとしてケトル型熱交換器２５に供給される。   The absorption refrigerator 22 produces cold water using the low-pressure steam generated by the low-pressure steam generator 24. In this embodiment, a water / lithium bromide type is used as the absorption refrigerator 22, but the absorption refrigerator 22 is not limited to this. The temperature of the cold water produced by the absorption refrigerator 22 may be 7 ° C to 12 ° C. The condensed water discharged from the absorption refrigerator 22 is supplied again to the kettle heat exchanger 25 as BFW via the pump 26.

吸収式冷凍機２２で製造された冷水は、水冷冷却器１８に供給され、上述したように蒸留塔１２からの塔頂蒸気を凝縮させるために用いられる。吸収式冷凍機２２で製造された冷水は、自然条件に影響されない安定した高い冷却能力を提供できるため、塔頂蒸気の凝縮温度を下げて蒸留塔１２の運転圧力を低下させることができる。蒸留塔１２の運転圧力を下げることは、リボイラー１４の負荷を下げることにつながる。すなわち、リボイラー１４へ供給するエネルギーを低減できるため、省エネルギーを図ることができる。   The cold water produced by the absorption refrigerator 22 is supplied to the water-cooled cooler 18 and used to condense the top vapor from the distillation tower 12 as described above. The chilled water produced by the absorption chiller 22 can provide a stable and high cooling capacity that is not affected by natural conditions. Therefore, the operating temperature of the distillation column 12 can be lowered by lowering the condensation temperature of the top vapor. Lowering the operating pressure of the distillation column 12 leads to lowering the load on the reboiler 14. That is, since the energy supplied to the reboiler 14 can be reduced, energy saving can be achieved.

また、本実施形態に係る蒸留設備１０では、自然条件に影響されない安定した冷却能力を提供できるため、蒸留塔１２に安定的に原料を供給することができる。すなわち、本実施形態に係る蒸留設備１０によれば、収率の向上を図ることができる。   In addition, since the distillation facility 10 according to the present embodiment can provide a stable cooling capacity that is not affected by natural conditions, the raw material can be stably supplied to the distillation column 12. That is, according to the distillation facility 10 according to the present embodiment, the yield can be improved.

また、本実施形態に係る蒸留設備１０では、吸収式冷凍機２２に供給される低圧蒸気は、プラント内で発生したプロセス流体を用いて生成されている。低圧蒸気を発生させるために別途燃料を投入する必要がないため、プラント全体としてエネルギー効率を高めることができる。また、プロセス流体との熱交換で低圧蒸気を発生させているため、プロセス流体の温度を低下させることができる。これは、プロセス設備に使用するためにプロセス流体を冷却する必要がある場合には、プラント内でプロセス流体を冷却するための設備および負荷を軽減できることを意味するため、この観点からもプラント全体としてエネルギー効率を高めることができる。   Further, in the distillation facility 10 according to the present embodiment, the low-pressure steam supplied to the absorption refrigerator 22 is generated using a process fluid generated in the plant. Since it is not necessary to add fuel separately to generate low-pressure steam, the energy efficiency of the entire plant can be improved. Moreover, since the low pressure steam is generated by heat exchange with the process fluid, the temperature of the process fluid can be lowered. This means that if the process fluid needs to be cooled for use in the process equipment, the equipment and load for cooling the process fluid within the plant can be reduced. Energy efficiency can be increased.

また、蒸留塔の最高温度における運転圧力が１０ｋｇ／ｃｍ２以上の場合は「高圧ガス」の適用を受け、その結果、保守・点検に多くの工数が必要となる。その点、本実施形態に係る蒸留設備１０では、蒸留塔１２の運転圧力を低下できることから、運転圧力が１０ｋｇ／ｃｍ２未満に下がれば「高圧ガス」適用から外れ、その結果蒸留塔１２の保守・点検が容易となる。また、新設の場合、蒸留塔１２の運転圧力が低くなることにより、蒸留塔１２の建設コスト（機器費）を下げることができる。 Further, when the operating pressure at the maximum temperature of the distillation column is 10 kg / cm 2 or more, “high pressure gas” is applied, and as a result, a lot of man-hours are required for maintenance and inspection. In that respect, in the distillation facility 10 according to the present embodiment, since the operating pressure of the distillation column 12 can be reduced, if the operating pressure falls below 10 kg / cm 2 , it is removed from the application of “high pressure gas”, and as a result, maintenance of the distillation column 12 is performed.・ Inspection is easy. In the case of a new installation, the construction pressure (equipment cost) of the distillation column 12 can be reduced by lowering the operating pressure of the distillation column 12.

図２（ａ）および（ｂ）は、本発明の実施形態に係る蒸留設備の改造方法を説明するための図である。図２（ａ）および（ｂ）において、図１に示す蒸留設備１０と同一又は対応する構成要素には同一の符号を付すとともに、重複する説明は適宜省略する。   FIGS. 2A and 2B are views for explaining a method for remodeling a distillation facility according to an embodiment of the present invention. 2 (a) and 2 (b), the same or corresponding components as those in the distillation facility 10 shown in FIG.

図２（ａ）は、改造前の蒸留設備３０を示す。図２（ａ）に示す蒸留設備３０は、蒸留塔１２と留出液タンク２１を接続するライン１７上に設けられた空冷冷却器１６のみが塔頂蒸気の冷却を行うよう構成されている。従って、この改造前の蒸留設備３０では、塔頂蒸気の冷却能力が自然条件に影響される。特に夏場には冷却能力が著しく低下するため、塔頂蒸気の凝縮温度が高くなるので蒸留塔１２の運転圧力を上げなくてはならない。その結果、還流比を大きくしなければならないのでリボイラー１４に多くのエネルギーを供給する必要が生じて、改造前の蒸留設備３０は省エネルギーの観点から課題がある。   FIG. 2A shows the distillation facility 30 before remodeling. The distillation equipment 30 shown in FIG. 2A is configured such that only the air-cooled cooler 16 provided on the line 17 connecting the distillation column 12 and the distillate tank 21 cools the top vapor. Therefore, in the distillation facility 30 before remodeling, the cooling capacity of the top vapor is affected by natural conditions. Especially in the summer, the cooling capacity is remarkably reduced, so that the condensation temperature of the top vapor of the tower rises, so that the operating pressure of the distillation tower 12 must be increased. As a result, since the reflux ratio must be increased, it is necessary to supply a large amount of energy to the reboiler 14, and the distillation facility 30 before the modification has a problem from the viewpoint of energy saving.

図２（ｂ）は、改造後の蒸留設備４０を示す。この蒸留設備４０は、水冷冷却器１８と、水冷冷却器１８に冷水を供給する吸収式冷凍機２２と、プロセス流体を用いて低圧蒸気を発生させ、吸収式冷凍機２２に供給する低圧蒸気発生装置２４と、を含む追加構成要素４２を蒸留設備３０に追加する改造がなされている。追加構成要素４２は、空冷冷却器１６の出力と水冷冷却器１８の入力がライン４６で接続され、水冷冷却器１８の出力と留出液タンク２１の入力がライン４８で接続されるように追加される。すなわち、追加構成要素４２は、空冷冷却器１６の下流に水冷冷却器１８が位置するように追加される。ライン４６上には第１バルブ４７が設けられる。図２（ｂ）に示すように、空冷冷却器１６と留出液タンク２１とを直接接続するライン（バイパスライン４４と呼ぶ）は残されている。バイパスライン４４上には第２バルブ４９が設けられる。図２（ｂ）に示すように、水冷冷却器１８は、ライン４６，４８を介して、空冷冷却器１６の下流にバイパスライン４４と並列に設けられる。   FIG. 2B shows the distillation equipment 40 after modification. The distillation facility 40 includes a water-cooled cooler 18, an absorption chiller 22 that supplies chilled water to the water-cooled cooler 18, and low-pressure steam that generates low-pressure steam using a process fluid and that is supplied to the absorption chiller 22. Modifications have been made to add additional components 42, including the device 24, to the distillation facility 30. An additional component 42 is added so that the output of the air-cooled cooler 16 and the input of the water-cooled cooler 18 are connected by a line 46, and the output of the water-cooled cooler 18 and the input of the distillate tank 21 are connected by a line 48. Is done. That is, the additional component 42 is added so that the water-cooled cooler 18 is located downstream of the air-cooled cooler 16. A first valve 47 is provided on the line 46. As shown in FIG. 2B, a line (referred to as a bypass line 44) that directly connects the air-cooled cooler 16 and the distillate tank 21 remains. A second valve 49 is provided on the bypass line 44. As shown in FIG. 2B, the water-cooled cooler 18 is provided in parallel with the bypass line 44 downstream of the air-cooled cooler 16 via lines 46 and 48.

図２（ｂ）のように改造された蒸留設備４０においては、第１バルブ４７と第２バルブ４９の開閉状態を制御することで、空冷冷却器１６を通過した塔頂蒸気および／またはその凝縮液が水冷冷却器１８を介して留出液タンク２１に入る第１動作状態と、空冷冷却器１６を通過した塔頂蒸気および／またはその凝縮液がバイパスライン４４を介して直接（すなわち水冷冷却器１８を通らずに）留出液タンク２１に入る第２動作状態とを切り替えることができる。   In the distillation equipment 40 modified as shown in FIG. 2 (b), by controlling the open / close state of the first valve 47 and the second valve 49, the top vapor passing through the air-cooled cooler 16 and / or the condensation thereof. The first operating state in which the liquid enters the distillate tank 21 via the water-cooled cooler 18 and the overhead vapor and / or its condensate that has passed through the air-cooled cooler 16 are directly (ie, water-cooled cooled) via the bypass line 44. The second operating state entering the distillate tank 21 can be switched (without going through the vessel 18).

第１バルブ４７を開状態且つ第２バルブ４９を閉状態とした場合、蒸留塔１２からの塔頂蒸気は、空冷冷却器１６、ライン４６、水冷冷却器１８、ライン４８を順に通過した後、留出液タンク２１に入る（第１動作状態）。この場合、図１に示す蒸留設備１０と同様に、空冷冷却器１６に加えて、吸収式冷凍機２２で製造された冷水を用いて塔頂蒸気の凝縮が行われる。その結果、塔頂蒸気の凝縮温度を下げて蒸留塔１２の運転圧力を低下させることが可能となる。   When the first valve 47 is opened and the second valve 49 is closed, the top vapor from the distillation tower 12 passes through the air-cooled cooler 16, the line 46, the water-cooled cooler 18, and the line 48 in this order, It enters the distillate tank 21 (first operation state). In this case, similarly to the distillation facility 10 shown in FIG. 1, in addition to the air-cooled cooler 16, the top steam is condensed using the cold water produced by the absorption refrigerator 22. As a result, it is possible to lower the operation temperature of the distillation column 12 by lowering the condensation temperature of the top vapor.

一方、第１バルブ４７を閉状態且つ第２バルブ４９を開状態とした場合、蒸留塔１２からの塔頂蒸気は、空冷冷却器１６を通過した後、バイパスライン４４を介して直接（すなわち水冷冷却器１８を通らずに）留出液タンク２１に入る（第２動作状態）。この場合、空冷冷却器１６のみで塔頂蒸気の凝縮が行われる。   On the other hand, when the first valve 47 is closed and the second valve 49 is opened, the top vapor from the distillation column 12 passes through the air-cooled cooler 16 and then directly (that is, water-cooled) via the bypass line 44. It enters the distillate tank 21 (without passing through the cooler 18) (second operation state). In this case, only the air-cooled cooler 16 condenses the tower top vapor.

第１動作状態と第２動作状態の切替は、蒸留設備が用いられるプラントの環境条件（例えば環境温度等）に基づいて行われてもよい。例えば、夏場や昼間で環境温度が高い（例えばプラントの環境温度が所定の閾値以上である）場合、空冷冷却器１６だけでは十分な冷却能力が期待できないため、第１動作状態に設定する。一方、例えば冬場等で環境温度が低い（例えばプラントの環境温度が所定の閾値未満である）場合、空冷冷却器１６だけでも十分な冷却能力が期待できるため、第２動作状態に設定する。このような構成をとることにより、必要なときだけ水冷冷却器１８や吸収式冷凍機２２等の追加構成要素４２を動作さればよくなるため、エネルギー効率を高めることができる。   The switching between the first operating state and the second operating state may be performed based on environmental conditions (for example, environmental temperature) of the plant in which the distillation facility is used. For example, when the environmental temperature is high in summer or in the daytime (for example, the environmental temperature of the plant is equal to or higher than a predetermined threshold), the air cooling cooler 16 alone cannot be expected to provide sufficient cooling capacity, so the first operation state is set. On the other hand, when the environmental temperature is low (for example, the environmental temperature of the plant is lower than a predetermined threshold value) in winter, for example, the air cooling cooler 16 alone can be expected to provide sufficient cooling capacity, so the second operation state is set. By adopting such a configuration, it is only necessary to operate the additional components 42 such as the water-cooled cooler 18 and the absorption chiller 22 only when necessary, so that energy efficiency can be improved.

さらに、第１バルブ４７および第２バルブ４９を共に開状態として、空冷冷却器１６を通過した塔頂蒸気および／またはその凝縮液が、水冷冷却器１８を介して留出液タンク２１に入るとともに、バイパスライン４４を介して直接留出液タンク２１に入る第３動作状態を設定してもよい。この場合、複数の凝縮手段（すなわち空冷冷却器１６および水冷冷却器１８）を用意されるので、仮に一つの凝縮手段に故障が発生した場合でも、蒸留設備の運転を継続することができる。   Further, both the first valve 47 and the second valve 49 are opened, and the top vapor and / or its condensate that has passed through the air-cooled cooler 16 enter the distillate tank 21 via the water-cooled cooler 18. Alternatively, a third operating state that enters the distillate tank 21 directly via the bypass line 44 may be set. In this case, since a plurality of condensing means (that is, the air-cooled cooler 16 and the water-cooled cooler 18) are prepared, even if a failure occurs in one condensing means, the operation of the distillation facility can be continued.

蒸留設備４０は、上記の動作状態の切り替え、すなわち第１バルブ４７および第２バルブ４９の開閉状態の制御を自動的に行うための制御装置を備えてもよい。この制御装置は、例えば環境温度を測定するための温度センサと、該温度センサの出力に基づいて第１バルブ４７および第２バルブ４９の開閉を制御する制御部を備えてもよい。   The distillation facility 40 may include a control device for automatically switching the operation state, that is, controlling the open / close state of the first valve 47 and the second valve 49. This control device may include, for example, a temperature sensor for measuring the environmental temperature and a control unit that controls opening and closing of the first valve 47 and the second valve 49 based on the output of the temperature sensor.

制御部は、温度センサの出力に加えてまたは代えて、蒸留設備が稼働する日時に基づいて第１バルブ４７および第２バルブ４９の開閉を制御してもよい。すなわち、環境温度が高くなることが想定される日や時間帯に応じて第１バルブ４７および第２バルブ４９の開閉を制御してもよい。   The control unit may control opening and closing of the first valve 47 and the second valve 49 based on the date and time when the distillation facility operates in addition to or instead of the output of the temperature sensor. That is, the opening and closing of the first valve 47 and the second valve 49 may be controlled according to the day or time zone in which the environmental temperature is expected to rise.

あるいは、上記動作状態の切り替えは、蒸留設備４０の操作者によりなされてもよい。   Alternatively, the operation state may be switched by an operator of the distillation facility 40.

本実施形態に係る改造方法によれば、既存の蒸留設備３０に追加構成要素４２を追加することで、図１に示す蒸留設備１０と同様に、省エネルギー、収率の向上、プラント全体としてのエネルギー効率の向上、蒸留塔１２の保守・点検の容易化などを図ることができる。また、バイパスライン４４を用いて空冷冷却器１６と留出液タンク２１を直接接続することが可能なため、改造後に元々の蒸留設備３０の形態で運用することも容易である。   According to the remodeling method according to the present embodiment, by adding an additional component 42 to the existing distillation facility 30, as in the distillation facility 10 shown in FIG. It is possible to improve efficiency and facilitate maintenance / inspection of the distillation column 12. Further, since the air-cooled cooler 16 and the distillate tank 21 can be directly connected using the bypass line 44, it is easy to operate in the form of the original distillation equipment 30 after the modification.

図３は、改造前と改造後の蒸留設備による蒸留のシミュレーション結果を示す。ここでは、運転圧力が１．０ＭＰａＧから２．０ＭＰａＧの複数の蒸留塔の中から、省エネルギー効果が高く、充填物の大幅な改造を必要としないナフサスプリッターを選択し、改造前と改造後の蒸留設備による蒸留をシミュレーションした。吸収式冷凍機としては、水・臭化リチウム系のものを選択した。   FIG. 3 shows a simulation result of distillation by the distillation equipment before and after the modification. Here, a naphtha splitter is selected from a plurality of distillation columns with an operating pressure of 1.0 MPaG to 2.0 MPaG, which has a high energy-saving effect and does not require any significant remodeling of the packing. The equipment distillation was simulated. As the absorption refrigerator, a water / lithium bromide type was selected.

図４は、シミュレーション計算に用いた吸収式冷凍機および吸収式冷凍機まわりの設定条件を示す。本シミュレーションでは、吸収式冷凍機の性能係数（ＣＯＰ：Coefficient Of Performance）を０．７５とした。また、吸収式冷凍機に供給される低圧蒸気の圧力を０．１５ＭＰａＧ、温度を１２７．６℃とした。また、吸収式冷凍機２２から排出される戻り凝縮水の温度を１３４℃とした。また、吸収式冷凍機２２から水冷冷却器１８に供給される冷水の温度を１０℃とし、水冷冷却器１８から吸収式冷凍機２２に戻る冷水の温度を２２℃とした。この冷水を製造するのに必要な熱負荷を１４．９ＧＪ／ｈとした。吸収式冷凍機のＣＯＰ＝０．７５であるため、吸収式冷凍機２２が必要とする熱負荷は（１４．９ＧＪ／ｈ）／０．７５＝１９．９ＧＪ／ｈとなる。   FIG. 4 shows the setting conditions around the absorption refrigerator and the absorption refrigerator used in the simulation calculation. In this simulation, the coefficient of performance (COP) of the absorption chiller was set to 0.75. The pressure of the low-pressure steam supplied to the absorption refrigerator was set to 0.15 MPaG and the temperature was 127.6 ° C. Moreover, the temperature of the return condensed water discharged | emitted from the absorption refrigerator 22 was set to 134 degreeC. The temperature of the cold water supplied from the absorption chiller 22 to the water-cooled cooler 18 was 10 ° C., and the temperature of the cold water returning from the water-cooled cooler 18 to the absorption chiller 22 was 22 ° C. The heat load necessary to produce this cold water was 14.9 GJ / h. Since COP = 0.75 of the absorption refrigerator, the heat load required by the absorption refrigerator 22 is (14.9 GJ / h) /0.75=19.9 GJ / h.

図３のシミュレーション結果から、改造前と比較して改造後は凝縮温度を３５℃から２５℃に低下でき、蒸留塔の運転圧力を１．１０ＭＰａＧから０．７０ＭＰａＧまで低下できていることが分かる。改造前に対する改造後の低圧化率は、（１．１ＭＰａＧ−０．７ＭＰａＧ）／１．１ＭＰａＧ×１００＝３６．４％である。その結果、リボイラーの熱負荷が２０．１ＧＪ／ｈから１４．７ＧＪ／ｈまで低下し、省エネルギー率＝２０．１ＧＪ／ｈ−１４．７ＧＪ／ｈ）２０．１ＧＪ／ｈ×１００＝２６．９％を達成できている。   From the simulation results of FIG. 3, it can be seen that the condensation temperature can be lowered from 35 ° C. to 25 ° C. and the operation pressure of the distillation column can be lowered from 1.10 MPaG to 0.70 MPaG after the modification, compared to before the modification. The pressure reduction ratio after remodeling with respect to before remodeling is (1.1 MPaG−0.7 MPaG) /1.1 MPaG × 100 = 36.4%. As a result, the heat load of the reboiler is reduced from 20.1 GJ / h to 14.7 GJ / h, and the energy saving rate = 20.1 GJ / h-14.7 GJ / h) 20.1 GJ / h × 100 = 26.9% Has been achieved.

上述の実施形態では、低圧蒸気発生装置２４は、プラント内で発生したプロセス流体から得られる熱を用いて低圧蒸気を発生させている。しかしながら、低圧蒸気発生装置２４で低圧蒸気を発生させるために用いる熱は、プロセス流体から得られる熱に限定されず、従来プラント内で有効利用されていなかった排熱から得てもよい。低圧蒸気発生装置２４は、例えば、蒸留設備１０の構成要素（例えば蒸留塔１２等）の冷却の際に生じる排熱等を利用して低圧蒸気を発生させてもよい。あるいは、既存の蒸留設備を改造する場合には、低圧蒸気発生装置２４は、プラント内の既設のクーラー及びエアフィンクーラーからの排熱を用いて低圧蒸気を発生させてもよい。これらにより、蒸留設備１０のエネルギー効率を高めることができる。   In the above-described embodiment, the low-pressure steam generator 24 generates low-pressure steam using heat obtained from the process fluid generated in the plant. However, the heat used for generating the low-pressure steam by the low-pressure steam generator 24 is not limited to the heat obtained from the process fluid, and may be obtained from exhaust heat that has not been effectively used in the conventional plant. The low-pressure steam generator 24 may generate low-pressure steam using, for example, exhaust heat generated when cooling the components of the distillation facility 10 (for example, the distillation column 12 or the like). Or when remodeling the existing distillation equipment, the low pressure steam generator 24 may generate low pressure steam using the exhaust heat from the existing cooler and air fin cooler in the plant. By these, the energy efficiency of the distillation installation 10 can be improved.

上述の実施形態では、吸収式冷凍機２２は、プラント内で発生した熱を用いて発生された低圧蒸気を用いて冷水を製造している。しかしながら、吸収式冷凍機２２は、プラント内で発生した熱を用いて発生された熱水を用いて冷水を製造してもよい。熱水の温度は、８０℃以上であってよく、好ましくは９０℃以上であってよい。例えば、吸収式冷凍機２２は、８８℃の熱水を用いて７℃の冷水を製造することができる。低圧蒸気を用いる場合と熱水を用いる場合ともに、吸収式冷凍機２２はプラント内で発生した熱を用いて冷水を製造しているということができる。   In the above-described embodiment, the absorption refrigerator 22 produces cold water using low-pressure steam generated using heat generated in the plant. However, the absorption refrigerator 22 may manufacture cold water using hot water generated using heat generated in the plant. The temperature of the hot water may be 80 ° C. or higher, and preferably 90 ° C. or higher. For example, the absorption refrigerator 22 can produce 7 ° C. cold water using 88 ° C. hot water. In both cases of using low-pressure steam and hot water, it can be said that the absorption refrigerator 22 is producing cold water using heat generated in the plant.

以上、本発明を実施例をもとに説明した。この実施例は例示であり、それらの各構成要素や各処理プロセスの組合せにいろいろな変形例が可能なこと、またそうした変形例も本発明の範囲にあることは当業者に理解されるところである。   In the above, this invention was demonstrated based on the Example. This embodiment is an exemplification, and it will be understood by those skilled in the art that various modifications can be made to the combination of each component and each processing process, and such modifications are also within the scope of the present invention. .

１０、３０、４０ 蒸留設備、 １２ 蒸留塔、 １４ リボイラー、 １６ 空冷冷却器、 １８ 水冷冷却器、 ２０ 還流装置、 ２１ 留出液タンク、 ２２ 吸収式冷凍機、 ２３ ポンプ、 ２４ 低圧蒸気発生装置、 ２５ ケトル型熱交換器、 ２６ ポンプ、 ４２ 追加構成要素、 ４４ バイパスライン、 ４７ 第１バルブ、 ４９ 第２バルブ。   10, 30, 40 Distillation equipment, 12 Distillation tower, 14 Reboiler, 16 Air-cooled cooler, 18 Water-cooled cooler, 20 Reflux device, 21 Distillate tank, 22 Absorption refrigeration machine, 23 Pump, 24 Low-pressure steam generator, 25 kettle heat exchanger, 26 pump, 42 additional components, 44 bypass line, 47 first valve, 49 second valve.

Claims (6)

プラント内に設けられる蒸留設備であって、
供給された原料を蒸留する蒸留塔と、
前記プラント内で発生した熱を用いて低圧蒸気を発生させる低圧蒸気発生装置と、
前記低圧蒸気発生装置で発生した低圧蒸気を用いて冷水を製造する冷凍機と、
前記蒸留塔から流出する塔頂蒸気を製造された冷水を用いて凝縮させる水冷冷却器と、
前記水冷冷却器で凝縮した液体の一部を前記蒸留塔に還流させる還流装置と、
を備え、
前記低圧蒸気発生装置は、前記プラント内で発生したプロセス流体との熱交換により、前記冷凍機から排出された凝縮水を加熱蒸発して低圧蒸気を発生させる熱交換器を備えることを特徴とする蒸留設備。 A distillation facility provided in the plant,
A distillation column for distilling the supplied raw material;
A low-pressure steam generator that generates low-pressure steam using heat generated in the plant ;
A refrigerator that produces cold water using low-pressure steam generated by the low-pressure steam generator ;
A water-cooled cooler for condensing the top vapor flowing out of the distillation tower using the produced cold water;
A reflux device for refluxing a part of the liquid condensed by the water-cooled cooler to the distillation column;
Equipped with a,
The low-pressure steam generator includes a heat exchanger that generates low-pressure steam by heat-evaporating condensed water discharged from the refrigerator by heat exchange with a process fluid generated in the plant. Distillation equipment. 前記蒸留塔から流出する塔頂蒸気を空冷する空冷冷却器をさらに備えることを特徴とする請求項１に記載の蒸留設備。 The distillation equipment according to claim 1, further comprising an air-cooled cooler that air-cools the top vapor flowing out of the distillation tower. 前記空冷冷却器は、前記水冷冷却器の上流に設けられており、
前記空冷冷却器と前記還流装置とを直接接続するためのバイパスラインをさらに備えることを特徴とする請求項２に記載の蒸留設備。 The air-cooled cooler is provided upstream of the water-cooled cooler,
The distillation equipment according to claim 2 , further comprising a bypass line for directly connecting the air-cooled cooler and the reflux device. 前記冷凍機により製造される冷水は、７℃〜１２℃であることを特徴とする請求項１から３のいずれかに記載の蒸留設備。 The cold water produced by the refrigerator, distillation equipment according to any one of claims 1 to 3, characterized in that the 7 ° C. to 12 ° C.. プラント内での蒸留方法であって、
蒸留塔を用いて供給された原料を蒸留する工程と、
前記プラント内で発生した熱を用いて低圧蒸気を発生させる工程と、
発生させた低圧蒸気を用いて冷水を製造する工程と、
前記蒸留塔から流出する塔頂蒸気を製造された冷水を用いて凝縮させる工程と、
還流装置を用いて凝縮した液体の一部を前記蒸留塔に還流させる工程と、
を備え、
前記低圧蒸気を発生させる工程は、前記プラント内で発生したプロセス流体との熱交換により、前記冷水を製造する工程で排出された凝縮水を加熱蒸発して低圧蒸気を発生させる工程を有することを特徴とする蒸留方法。 A distillation method in a plant,
A step of distilling the raw material supplied using a distillation tower;
Generating low pressure steam using heat generated in the plant ;
Producing cold water using the generated low-pressure steam ;
Condensing the top vapor flowing out of the distillation column using the produced cold water;
A step of refluxing a part of the liquid condensed using a reflux apparatus to the distillation column;
Equipped with a,
The step of generating the low-pressure steam has a step of generating low-pressure steam by heating and evaporating the condensed water discharged in the step of producing the cold water by heat exchange with the process fluid generated in the plant. A characteristic distillation method. 前記冷水を用いて凝縮させる工程で用いる水冷冷却器の上流に、前記蒸留塔から流出する塔頂蒸気を空冷する空冷冷却器が設けられており、
前記空冷冷却器と前記還流装置とがバイパスラインを介して直接接続されており、
前記プラントの環境条件に基づいて、前記空冷冷却器を通過した塔頂蒸気および／またはその凝縮液が前記水冷冷却器を介して前記還流装置に入る第１動作状態と、前記空冷冷却器を通過した塔頂蒸気および／またはその凝縮液が前記バイパスラインを介して直接前記還流装置に入る第２動作状態とを切り替える工程をさらに備えることを特徴とする請求項５に記載の蒸留方法。 An air-cooled cooler for air-cooling the top vapor flowing out from the distillation tower is provided upstream of the water-cooled cooler used in the step of condensing with the cold water,
The air-cooled cooler and the reflux device are directly connected via a bypass line,
Based on the environmental conditions of the plant, a first operating state in which the top vapor and / or its condensate that has passed through the air-cooled cooler enters the reflux device via the water-cooled cooler, and passes through the air-cooled cooler The distillation method according to claim 5 , further comprising a step of switching between the second operation state in which the overhead vapor and / or the condensate thereof directly enters the reflux device via the bypass line.
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