JP7046301B1 - Oil extraction and distillation equipment using flash steam - Google Patents

Oil extraction and distillation equipment using flash steam Download PDF

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JP7046301B1
JP7046301B1 JP2021164744A JP2021164744A JP7046301B1 JP 7046301 B1 JP7046301 B1 JP 7046301B1 JP 2021164744 A JP2021164744 A JP 2021164744A JP 2021164744 A JP2021164744 A JP 2021164744A JP 7046301 B1 JP7046301 B1 JP 7046301B1
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昇 蓮池
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藤▲崎▼エンジニアリング株式会社
蓮池 ▲昇▼
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Abstract

【課題】蒸発缶におけるスチーム使用量を削減し、省エネルギーを促進することができる油脂抽出蒸留設備を提供する。【解決手段】本発明のフラッシュ蒸気を用いる油脂抽出蒸留設備１００は、ミセラを受給しその溶剤ノルマルヘキサンを蒸発させる第２蒸発缶１２２を備え、第２蒸発缶１２２は、ミセラを予熱する予熱部１２２Ａと、ミセラを加熱する加熱部１２２Ｂと、予熱部１２２Ａにおいてミセラから蒸発するノルマルヘキサンを排出する蒸気放出管１２２Ｃと、を有し、フラッシュ蒸気によって予熱部１２２Ａを予熱する。【選択図】図１PROBLEM TO BE SOLVED: To provide an oil / fat extraction distillation facility capable of reducing the amount of steam used in an evaporator and promoting energy saving. An oil / fat extraction / distillation facility 100 using flash steam of the present invention includes a second evaporation can 122 that receives a micellar and evaporates the solvent normal hexane, and the second evaporation can 122 is a preheating unit that preheats the micellar. It has 122A, a heating unit 122B for heating the misera, and a steam discharge tube 122C for discharging normal hexane evaporating from the misera in the preheating unit 122A, and preheats the preheating unit 122A with flash steam. [Selection diagram] Fig. 1

Description

本発明は、植物油の製造工程で用いられる油脂抽出蒸留設備に関し、更に詳しくは、フラッシュ蒸気を用いて省エネルギー化を図った油脂抽出蒸留設備に関する。 The present invention relates to an oil-and-fat extraction-distillation facility used in a vegetable oil manufacturing process, and more particularly to an oil-and-fat extraction-distillation facility that saves energy by using flash steam.

植物油の製造では、菜種、とうもろこし胚芽あるいは大豆等の植物油原料から菜種油、とうもろこし油あるいは大豆油などの油脂を採油する。採油方法としては、圧搾法、抽出法及び圧油法がある。菜種、とうもろこし胚芽等のように油脂成分が多い植物油原料では、原料を圧搾して油脂成分を搾り出す圧搾法が採用されている。大豆等のように油脂成分が２０％に満たない油脂成分の少ない植物油原料では、加熱などの前処理後押し潰してフレーク状にした植物油原料（以下、「フレーク」と称す。）から油脂成分を溶剤（例えば、ノルマルヘキサン）によって抽出する抽出法が採用されている。また。菜種、とうもろこし胚芽等の圧搾後の搾り粕にも油脂成分が１０数％程度残留しているため、ノルマルヘキサンを用いて搾り粕から油脂成分を抽出する、圧搾法と抽出法を組み合わせた圧抽法が採用されている。抽出法や圧抽法ではフレークや搾り粕（以下、「フレーク等」と称す。）から油脂成分を注した後、抽出液を例えば３５０～２４０ｔｏｒｒほどの減圧下で加熱してノルマルヘキサンを蒸発させて油脂を得る油脂抽出蒸発設備が用いられる。 In the production of vegetable oil, oils and fats such as rapeseed oil, corn oil or soybean oil are extracted from vegetable oil raw materials such as rapeseed, corn germ or soybean. The oil extraction method includes a pressing method, an extraction method and a pressing method. For vegetable oil raw materials having a large amount of oil and fat components such as rapeseed and corn germ, a squeezing method is adopted in which the raw materials are squeezed to squeeze out the oil and fat components. For vegetable oil raw materials such as soybeans, which have less than 20% fat and oil components and are low in fat and oil components, the oil and fat components are used as a solvent from the vegetable oil raw materials (hereinafter referred to as "flakes") that are crushed into flakes after pretreatment such as heating. An extraction method of extracting with (for example, normal hexane) is adopted. Also. Since about 10% of oil and fat components remain in the squeezed lees after squeezing rapeseed, corn germ, etc., the oil and fat components are extracted from the squeezed lees using normal hexane. The law is adopted. In the extraction method and the pressure extraction method, after pouring oil and fat components from flakes and squeezed lees (hereinafter referred to as "flakes, etc."), the extract is heated under a reduced pressure of, for example, 350 to 240 torr to evaporate normal hexane. A fat extraction and evaporation facility is used to obtain fats and oils.

上記油脂抽出蒸発設備は、例えば図６に示すように、抽出部１０及び蒸発部２０を備え、抽出部１１においてフレーク等から抽出液(以下、「ミセラ」と称す)。を得た後、ミセラを減圧下の蒸発部２０へ供給し、ここでノルマルヘキサンを蒸発させて回収すると共に大豆油等の油脂を得ている。 As shown in FIG. 6, for example, the oil / fat extraction / evaporation facility includes an extraction unit 10 and an evaporation unit 20, and an extraction liquid (hereinafter referred to as “Misera”) is extracted from flakes or the like in the extraction unit 11. After that, Misera is supplied to the evaporation unit 20 under reduced pressure, where normal hexane is evaporated and recovered, and fats and oils such as soybean oil are obtained.

抽出部１０は、コンベア式抽出機（以下、単に「抽出機」と称す。）１１、その上流側と下流側にそれぞれ付設された、抽出前後のフレーク等を搬送する第１、第２搬送機１１Ａ．１１Ｂ、抽出機１１内にノルマルヘキサンを供給する溶剤ポンプ１２、抽出機１１からのミセラ（例えば油脂２０％、ノルマルヘキサン８０％）を貯留するミセラタンク１３、後述する蒸発部２０内の溶剤セパレータから供給されるノルマルヘキサン液を加熱する溶剤加熱器１４、抽出機１１から第２搬送機１１Ｂを介して搬入されるフレーク等内に含まれるノルマルヘキサンを除去する脱溶剤器１５を備えている。以下ではノルマルヘキサンに含まれる油脂の含有率をミセラ濃度と称する。ノルマルヘキサン中の油脂含有率が２０％であれば、ミセラ濃度２０％と称する。また、脱溶剤器１５は脱溶剤されたフレーク等を焼く機能が付されている。脱溶剤器１５の上部と下部にはそれぞれ第３、第４搬送機１５Ａ、１５Ｂが付設されており、脱溶剤器１５は第２、第３搬送機１１Ｂ、１５Ａを介して抽出機１１１側からのノルマルヘキサンを含んでいるレーク等が搬入され、第４搬送機１５Ｂを介して脱溶剤されたフレーク等を搬出する。脱溶剤器１５の上部にはスクラバー１５Ｃが取り付けられ、スクラバー１５Ｃによって脱溶剤器１５から上昇するノルマルヘキサンガス内に含まれる微粉を除塵する。また、脱溶剤器１５からのノルマルヘキサンガスはスクラバー１５Ｃを介し、例えば約６０～７５℃のノルマルヘキサンガスを蒸発部２０側へ供給するように構成されている。また、ミセラタンク１３は蒸発部２０側へ抽出機１１において生成した例えば約５５℃～６５℃のミセラを供給するように構成されている。 The extraction unit 10 is a conveyor type extractor (hereinafter, simply referred to as an “extractor”) 11, and first and second conveyors attached to the upstream side and the downstream side of the conveyor type extractor (hereinafter, simply referred to as “extractor”) for transporting flakes before and after extraction. 11A. 11B, a solvent pump 12 that supplies normal hexane into the extractor 11, a miscellaneous tank 13 that stores miscella (for example, 20% fat and oil, 80% normal hexane) from the extractor 11, and a solvent separator in the evaporation section 20 described later. It is provided with a solvent heater 14 for heating the normal hexane solution, and a solvent remover 15 for removing normal hexane contained in flakes and the like carried in from the extractor 11 via the second transporter 11B. Hereinafter, the content of fats and oils contained in normal hexane is referred to as the Misera concentration. If the oil / fat content in normal hexane is 20%, it is referred to as a miscellaneous concentration of 20%. Further, the solvent remover 15 has a function of burning the desolvated flakes and the like. The third and fourth conveyors 15A and 15B are attached to the upper part and the lower part of the solvent remover 15, respectively, and the solvent remover 15 is attached to the extractor 111 side via the second and third conveyors 11B and 15A, respectively. The lake or the like containing the normal hexane is carried in, and the desolvated flakes or the like are carried out via the fourth carrier 15B. A scrubber 15C is attached to the upper part of the solvent remover 15, and the scrubber 15C removes fine powder contained in the normal hexane gas rising from the solvent remover 15. Further, the normal hexane gas from the solvent remover 15 is configured to supply the normal hexane gas at, for example, about 60 to 75 ° C. to the evaporation unit 20 side via the scrubber 15C. Further, the micellar tank 13 is configured to supply the micellar produced in the extractor 11 to the evaporation unit 20 side, for example, at about 55 ° C. to 65 ° C.

蒸発部２０は、第１、第２蒸発缶２１、２２及び油脂塔２３を備え、減圧下の第１、第２蒸発缶２１、２２においてミセラのノルマルヘキサンを順次蒸発させ、真空度が徐々に 高くなる油脂塔２３において残留ノルマルヘキサンを除去し、微量のノルマルヘキサンを含む油脂を得る。第１蒸発缶２１には脱溶剤器１５から供給される加熱ノルマルヘキサン（例えば６０～７０数℃）を用いてミセラタンク１３から第１蒸発缶２１に供給される例えば５０数℃のミセラを加熱してノルマルヘキサンを蒸発させ、第１コンデンサ２４においてノルマルヘキサンを凝縮させて溶剤セパレータ２５で回収する。第１蒸発缶２１において得られる例えばミセラ濃度６０％のミセラは第２蒸発缶２２へ供給される。第２蒸発缶２２では例えば３６０ｔｏｒｒの減圧下でミセラがスチームを用いて更に加熱されてノルマルヘキサンが蒸発してミセラ濃縮９６％のミセラが生成し、蒸発したノルマルヘキサンが第１コンデンサ２４において凝縮し溶剤セパレータ２５で回収される。このように第２蒸発缶２２では大半のノルマルヘキサンが除去される。油脂塔２３は、上下に分割され、下部が上部より高真空になっている。上下の分割部には、それぞれ複数の棚段が設けられ、濃縮されたミセラが各棚段を流下する間にスチームで加熱されてノルマルヘキサンが徐々に除去される。油脂塔２３において除去されたノルマルヘキサンは第２コンデンサ２６で凝縮され溶剤セパレータ２５で回収される。この液化した溶剤には少量の水が含まれているため、溶剤セパレータ２５において溶剤から水が分離されて、水回収部２７において水が回収される。溶剤セパレータ２５で回収された溶剤は配管を介して溶剤加熱器１４へ戻される。 The evaporation unit 20 includes first and second evaporation cans 21 and 22 and an oil and fat tower 23, and the normal hexane of Misera is sequentially evaporated in the first and second evaporation cans 21 and 22 under reduced pressure, and the degree of vacuum gradually increases. Residual normal hexane is removed in the elevated fat and oil column 23 to obtain a fat and oil containing a trace amount of normal hexane. For the first evaporation can 21, a heated normal hexane (for example, 60 to 70 ° C.) supplied from the solvent remover 15 is used to heat a miscella at, for example, 50 ° C. supplied from the miscellaneous tank 13 to the first evaporation can 21. The normal hexane is evaporated, the normal hexane is condensed in the first condenser 24, and the normal hexane is recovered by the solvent separator 25. For example, the micellar having a micellar concentration of 60% obtained in the first evaporative can 21 is supplied to the second evaporative can 22. In the second evaporation can 22, for example, under a reduced pressure of 360 torr, the micellar is further heated using steam to evaporate the normal hexane to produce a micellar with a micellar concentration of 96%, and the evaporated normal hexane is condensed in the first capacitor 24. It is recovered by the solvent separator 25. In this way, most of the normal hexane is removed in the second evaporation can 22. The oil and fat tower 23 is divided into upper and lower parts, and the lower part has a higher vacuum than the upper part. A plurality of shelves are provided in the upper and lower divisions, and the concentrated micella is heated by steam while flowing down each shelf to gradually remove normal hexane. The normal hexane removed in the oil and fat column 23 is condensed by the second capacitor 26 and recovered by the solvent separator 25. Since this liquefied solvent contains a small amount of water, the solvent separator 25 separates the water from the solvent, and the water recovery unit 27 recovers the water. The solvent recovered by the solvent separator 25 is returned to the solvent heater 14 via the pipe.

従来の油脂抽出蒸発設備は、例えば図６に示すように、抽出部１０及び蒸発部２０を備え、抽出部１１においてフレーク等からミセラを得た後、ミセラを蒸発部２０へ供給し、ここでミセラからノルマルヘキサンを回収すると共に大豆油等の油脂を得ている。 As shown in FIG. 6, for example, the conventional oil / fat extraction / evaporation equipment includes an extraction unit 10 and an evaporation unit 20, and after obtaining a micella from flakes or the like in the extraction unit 11, the micella is supplied to the evaporation unit 20 here. Normal hexane is recovered from Misera and fats and oils such as soybean oil are obtained.

しかしながら、図６に示す従来の油脂抽出蒸留設備の場合には、第１蒸発缶２１ではミセラの加熱に脱溶剤器１５から供給される加熱ノルマルヘキサンガスと水蒸気を用いるため、ミセラは加熱用熱源としては十分でなく、第２蒸発缶２２の負荷が大きくなる。また、第２蒸発缶２２では缶全長に亘ってスチーム加熱を行うため、第２蒸発缶２２の途中でノルマルヘキサンが蒸発し始め、本来加熱すべきミセラ以外にノルマルヘキサン蒸気をも余分に加熱するため、本来必要とされるスチーム使用量よりも多くのスチームが消費されるという課題があった。 However, in the case of the conventional oil / fat extraction / distillation facility shown in FIG. 6, since the first evaporative can 21 uses the heated normal hexane gas and steam supplied from the solvent remover 15 for heating the miscella, the misera is a heat source for heating. However, the load on the second evaporation can 22 becomes large. Further, since steam heating is performed over the entire length of the can in the second evaporation can 22, normal hexane begins to evaporate in the middle of the second evaporation can 22, and the normal hexane steam is excessively heated in addition to the miscella that should be originally heated. Therefore, there is a problem that more steam is consumed than originally required.

本発明は、上記課題を解決するためになされたもので、蒸発缶におけるスチーム使用量を削減し、省エネルギーを促進することができる油脂抽出蒸留設備を提供することを目的としている。 The present invention has been made to solve the above problems, and an object of the present invention is to provide an oil / fat extraction / distillation facility capable of reducing the amount of steam used in an evaporator and promoting energy saving.

本発明の請求項１に記載のフラッシュ蒸気を用いる油脂抽出蒸留設備は、油脂抽出液を受給しその溶剤を蒸発させる少なくとも一つの蒸発缶を備えた油脂抽出液蒸発設備であって、上記蒸発缶は、上記油脂抽出液を予熱する予熱部と、上記予熱部の下流側に接続されて上記油脂抽出液を加熱する加熱部と、上記予熱部の下流側に上記加熱部と併設されて上記予熱部で上記油脂抽出液から蒸発する溶剤を排出する排気部と、を有し、上記予熱部にフラッシュ蒸気を供給するフラッシュタンクを接続し、上記フラッシュ蒸気によって上記予熱部を予熱することを特徴とするものである。 The oil / fat extraction / distillation equipment using the flash steam according to claim 1 of the present invention is an oil / fat extract evaporating equipment provided with at least one evaporative can for receiving the oil / fat extract and evaporating the solvent thereof, and is the above-mentioned evaporative can. Is annexed to the preheating section for preheating the fat and oil extract, the heating section connected to the downstream side of the preheating section to heat the fat and oil extract, and the heating section on the downstream side of the preheating section. It has an exhaust part that discharges the solvent that evaporates from the oil and fat extract, and a flash tank that supplies flash steam is connected to the preheating part, and the preheating part is preheated by the flash steam. It is something to do.

また、本発明の請求項２に記載のフラッシュ蒸気を用いる油脂抽出蒸留設備は、請求項１に記載の発明において、上記少なくとも一つの蒸発缶は、上流側に配置された第１蒸発缶と、下流側に配置された第２蒸発缶と、を備え、上記第２蒸発缶は、上記予熱部、上記加熱部及び上記排気部を有し、上記第１蒸発缶及び上記予熱部それぞれに上記フラッシュタンクを接続したことを特徴とするものである。 Further, in the oil / fat extraction / distillation facility using the flash steam according to claim 2 of the present invention, in the invention according to claim 1, the at least one evaporation can is the first evaporation can arranged on the upstream side. A second evaporative can provided on the downstream side, the second evaporative can has a preheating section, a heating section, and an exhaust section, and the flash is provided in each of the first evaporative can and the preheating section. It is characterized by connecting a tank.

また、本発明の請求項３に記載のフラッシュ蒸気を用いる油脂抽出蒸留設備は、油脂抽出液を受給しその溶剤を蒸発させる少なくとも一つの蒸発缶を備えた油脂抽出液蒸発設備であって、上記蒸発缶は、上記油脂抽出液を予熱する予熱部と、上記予熱部の下流側に接続されて上記油脂抽出液を加熱する加熱部と、上記予熱部の下流側に上記加熱部と併設されて上記予熱部で上記油脂抽出液から蒸発する溶剤を排出する排気部と、を有し、上記予熱部に高温ドレン水の供給配管を接続し、上記供給配管を介して上記予熱部内に上記高温ドレン水を供給してフラッシュ蒸気及びフラッシュ後の熱水をそれぞれ生成させ、これらのフラッシュ蒸気及び熱水によって上記予熱部を予熱することを特徴とするものである。 Further, the oil / fat extraction / distillation equipment using the flash steam according to claim 3 of the present invention is an oil / fat extract evaporating equipment provided with at least one evaporative can for receiving the oil / fat extract and evaporating the solvent thereof. The evaporation can is provided with a preheating unit for preheating the oil / fat extract, a heating unit connected to the downstream side of the preheating unit to heat the oil / fat extract, and a heating unit on the downstream side of the preheating unit. The preheating section has an exhaust section for discharging a solvent evaporating from the oil / fat extract, a high temperature drain water supply pipe is connected to the preheating section, and the high temperature drain is inside the preheating section via the supply piping. It is characterized in that water is supplied to generate flash steam and hot water after flash, respectively, and the preheated portion is preheated by these flash steam and hot water.

また、本発明の請求項４に記載のフラッシュ蒸気を用いる油脂抽出蒸留設備は、請求項３に記載の発明において、上記少なくとも一つの蒸発缶は、上流側に配置された第１蒸発缶と、下流側に配置された第２蒸発缶と、を備え、上記第２蒸発缶は、上記予熱部、上記加熱部及び上記排気部を有し、上記第１蒸発缶及び上記予熱部それぞれに高温ドレン水の供給配管を接続したことを特徴とするものである。 Further, in the oil / fat extraction / distillation facility using the flash steam according to claim 4 of the present invention, in the invention according to claim 3, the at least one evaporation can is the first evaporation can arranged on the upstream side. The second evaporative can is provided with a second evaporative can arranged on the downstream side, and the second evaporative can has a preheating section, a heating section, and an exhaust section, and a high temperature drain is provided in each of the first evaporative can and the preheating section. It is characterized by connecting a water supply pipe.

また、本発明の請求項５に記載のフラッシュ蒸気を用いる油脂抽出蒸留設備は、求項１～請求項４のいずれか１項に記載の発明において、上記すくなくとも一つの蒸発缶から受給する油脂抽出液中の残留溶剤を除去する油脂塔を備え、上記油脂塔は、上記蒸発缶からの油脂抽出液を受給する塔本体と、上記塔本体内に挿入されて上記蒸発缶からの油脂抽出液中に蒸気をバブリングさせる蒸気吹き込み部を有することを特徴とするものである。 Further, the fat extraction and distillation equipment using the flash steam according to claim 5 of the present invention is the fat extraction and fat extraction received from at least one evaporation can in the invention according to any one of claims 1 to 4. The oil and fat tower is provided with an oil and fat tower for removing residual solvent in the liquid, and the oil and fat tower is contained in a tower body for receiving the oil and fat extract from the evaporation can and in the oil and fat extract from the evaporation can inserted into the tower body. It is characterized by having a steam blowing portion for bubbling steam.

本発明によれば、蒸発缶におけるスチーム使用量を削減し、省エネルギーを促進することができる油脂抽出蒸留設備を提供することができる。 According to the present invention, it is possible to provide an oil / fat extraction distillation facility capable of reducing the amount of steam used in an evaporator and promoting energy saving.

本発明の油脂抽出蒸留設備の第１の実施形態を示す構成図である。It is a block diagram which shows the 1st Embodiment of the oil-and-fat extraction distillation equipment of this invention. 本発明の第２の実施形態の油脂抽出蒸留設備を示す構成図である。It is a block diagram which shows the oil-and-fat extraction distillation equipment of the 2nd Embodiment of this invention. 本発明の第３の実施形態の油脂抽出蒸留設備を示す構成図である。It is a block diagram which shows the oil-and-fat extraction distillation equipment of the 3rd Embodiment of this invention. 本発明の第４の実施形態の油脂抽出蒸留設備を示す構成図である。It is a block diagram which shows the oil-fat extraction and distillation equipment of 4th Embodiment of this invention. 本発明の第５の実施形態の油脂抽出蒸留設備の要部を拡大して示す摸式図である。It is a schematic diagram which shows the main part of the oil-and-fat extraction and distillation equipment of 5th Embodiment of this invention in an enlarged manner. 従来の油脂抽出蒸留設備を示す構成図である。It is a block diagram which shows the conventional oil-and-fat extraction distillation equipment.

以下、図１～図５に示す実施形態に基づいて本発明の油脂抽出蒸留設備について説明する。 Hereinafter, the oil / fat extraction / distillation equipment of the present invention will be described based on the embodiments shown in FIGS. 1 to 5.

本実施形態の油脂抽出蒸留設備は、図１に示すように、大豆のフレーク等に含まれる油脂を抽出してミセラを生成する抽出部１１０と、抽出部１１０から供給されるミセラのノルマルヘキサンを蒸発させて大豆油を得る蒸発部１２０と、を備えている。 As shown in FIG. 1, the oil / fat extraction / distillation facility of the present embodiment uses an extraction unit 110 that extracts oils and fats contained in soybean flakes and the like to generate micellar, and a micellar normal hexane supplied from the extraction unit 110. It is provided with an evaporation unit 120 for evaporating to obtain soybean oil.

抽出部１１０は、フレーク等の油脂成分を抽出するコンベア式抽出機（以下、単に「抽出機」と称す。）１１１と、その上流側、下流側それぞれに付設された第１、第２搬送機１１１Ａ．１１１Ｂと、抽出機１１１内でコンベアにより搬送されるフレーク等に上方からノルマルヘキサンを配管を介して供給する溶剤ポンプ１１２と、抽出機１１１から排出されるミセラを一時的に貯留するミセラタンク１１３と、後述する蒸発部１２０内の溶剤セパレータから供給されるノルマルヘキサン及び抽出機１１１から排気されるノルマルヘキサンを加熱する溶剤加熱器１１４と、抽出機１１１から第２搬送機１１１Ｂを介して搬入されるフレーク等中に含まれるノルマルヘキサンを除去する脱溶剤器１１５と、を備えている。また、脱溶剤器１１５の上部と下部にはそれぞれ第３、第４搬送機１１５Ａ、１１５Ｂが付設されており、脱溶剤器１１５は第２、第３搬送機１１１Ｂ、１１５Ａを介して抽出機１１１から搬出されるノルマルヘキサンを含むフレーク等が搬入され、第４搬送機１１５Ｂを介して脱溶剤されたフレーク等を搬出する。脱溶剤器１１５の上部にはスクラバー１１５Ｃが取り付けられ、スクラバー１１５Ｃが脱溶剤器１１５から上昇するノルマルヘキサンガス中の微粉を除塵した後、水蒸気を含むノルマルヘキサンガスが下流側の蒸発部１２０側へ供給されるように構成されている。また、ミセラタンク１１３は蒸発部１２０側へ抽出機１１１において生成したミセラを供給するように構成されている。 The extraction unit 110 is a conveyor type extractor (hereinafter, simply referred to as “extractor”) 111 for extracting oil and fat components such as flakes, and first and second conveyors attached to the upstream side and the downstream side of the conveyor type extractor (hereinafter, simply referred to as “extractor”) 111. 111A. 111B, a solvent pump 112 that supplies normal hexane from above to flakes or the like conveyed by a conveyor in the extractor 111 via a pipe, and a misera tank 113 that temporarily stores the miscella discharged from the extractor 111. The solvent heater 114 for heating the normal hexane supplied from the solvent separator in the evaporating unit 120 and the normal hexane exhausted from the extractor 111, which will be described later, and the flakes carried in from the extractor 111 via the second carrier 111B. It is provided with a solvent remover 115 for removing normal hexane contained in the above. Further, the third and fourth conveyors 115A and 115B are attached to the upper part and the lower part of the solvent remover 115, respectively, and the solvent remover 115 is connected to the extractor 111 via the second and third conveyors 111B and 115A, respectively. The flakes containing normal hexane carried out from the above are carried in, and the desolvated flakes and the like are carried out via the fourth carrier 115B. A scrubber 115C is attached to the upper part of the solvent remover 115, and after the scrubber 115C removes fine powder in the normal hexane gas rising from the solvent remover 115, the normal hexane gas containing water vapor moves to the evaporation part 120 side on the downstream side. It is configured to be supplied. Further, the micellar tank 113 is configured to supply the micellar produced by the extractor 111 to the evaporation unit 120 side.

蒸発部１２０は、減圧下で例えばミセラ濃度２０％のミセラを従来と同様の減圧下で加熱してノルマルヘキサンを蒸発させて段階的に濃縮する第１、第２蒸発缶１２１、１２２と、第２蒸発缶１２２から供給される濃縮ミセラ中の残留ノルマルヘキサンを除去して高純度の油脂を生成する油脂塔１２３と、を備えている。第１蒸発缶１２１は、従来と同様に脱溶剤器１１５から供給される加熱ノルマルヘキサンガスを用いてミセラタンク１１３から供給されるミセラを例えばミセラ濃度６０％まで濃縮し、第２蒸発缶１２２へ供給するように構成されている。第１蒸発缶１２１から蒸発して放出されるノルマルヘキサンガスは第１コンデンサ１２４において冷却された後、溶剤セパレータ１２５で溶剤として回収する。溶剤セパレータ１２５は、配管によって抽出部１１０の溶剤加熱器１１４と配管を介して接続され、溶剤セパレータにおいて溶剤として回収されたノルマルヘキサンが溶剤加熱器１１４に戻される。ここまでは従来と同様に構成されている。 The evaporation unit 120 includes first and second evaporation cans 121 and 122 under reduced pressure, for example, heating a micellar having a micellar concentration of 20% under the same reduced pressure as before to evaporate normal hexane and gradually concentrating the normal hexane. The oil column 123 is provided with a fat column 123 for removing residual normal hexane in the concentrated miscella supplied from the evaporation can 122 to produce a high-purity fat and oil. In the first evaporation can 121, the misera supplied from the misera tank 113 is concentrated to, for example, a miscella concentration of 60% by using the heated normal hexane gas supplied from the solvent remover 115 as in the conventional case, and is supplied to the second evaporation can 122. It is configured to do. The normal hexane gas that evaporates and is released from the first evaporation can 121 is cooled in the first condenser 124 and then recovered as a solvent by the solvent separator 125. The solvent separator 125 is connected to the solvent heater 114 of the extraction unit 110 via a pipe by a pipe, and the normal hexane recovered as a solvent in the solvent separator is returned to the solvent heater 114. Up to this point, the configuration is the same as before.

而して、本実施形態では、第２蒸発缶１２２が予熱部１２２Ａと加熱部１２２Ｂとに分割され、予熱部１２２Ａがミセラの上流側に位置し、加熱部１２２Ｂが予熱部１２２Ａの下流側に位置し、互いに配管で接続されている。予熱部１２２Ａは、後述するようにフラッシュ蒸気によってミセラが予熱し、加熱部１２２Ｂの手前でミセラからノルマルヘキサンを蒸発させてミセラ内にノルマルヘキサンガスの気泡が含まれない状態にした後、加熱部１２２Ｂ内ではミセラ濃縮液のみを加熱するように工夫されている。 Thus, in the present embodiment, the second evaporation can 122 is divided into a preheating section 122A and a heating section 122B, the preheating section 122A is located on the upstream side of the miscella, and the heating section 122B is located on the downstream side of the preheating section 122A. It is located and connected to each other by piping. As will be described later, the preheating section 122A is preheated by the micellar by flash steam, and normal hexane is evaporated from the micellar in front of the heating section 122B to make the micellar free of bubbles of normal hexane gas, and then the heating section. In 122B, it is devised to heat only the miscellaneous concentrate.

また、予熱部１２２Ａと加熱部１２２Ｂの接続配管から蒸気放出管１２２Ｃが分岐し、加熱部１２２Ｂと蒸気放出管１２２Ｃの分岐点には覗き窓１２２Ｄが設けられている。この覗き窓１２２Ｄにおいて予熱部１２２Ａで発生するノルマルヘキサンガスの様子と加熱部１２２Ｂへ向かう濃縮ミセラの様子を確認することができる。予熱部１２２Ａの下端には第１蒸発缶１２１からの濃縮６０％のミセラが流入する配管が接続されている。加熱部１２２Ａの濃縮ミセラの出口には油脂塔１２３の上部のミセラの入口が配管を介して接続されている。また、加熱部１２２Ｂの上端と蒸気放出管１２２Ｃには第１コンデンサ１２４が接続され、加熱部１２２Ｂと蒸気放出管１２２Ｃから放出されるノルマルヘキサンガスが溶剤として凝縮し、溶剤セパレータ１２５へ供給されるようになっている。第２蒸発缶１２２の加熱部１２２Ｂでは大半のノルマルヘキサンが除去され、例えば濃度９６％のミセラが油脂塔１２３へ供給される。 Further, the steam discharge pipe 122C branches from the connecting pipe between the preheating unit 122A and the heating unit 122B, and a viewing window 122D is provided at the branch point between the heating unit 122B and the steam discharge pipe 122C. In this viewing window 122D, the state of the normal hexane gas generated in the preheating part 122A and the state of the concentrated miscellaneous toward the heating part 122B can be confirmed. A pipe into which a 60% concentrated miscella from the first evaporation can 121 flows is connected to the lower end of the preheating portion 122A. The inlet of the miscella in the upper part of the oil and fat tower 123 is connected to the outlet of the concentrated miscella of the heating unit 122A via a pipe. Further, a first capacitor 124 is connected to the upper end of the heating unit 122B and the steam discharge pipe 122C, and the normal hexane gas discharged from the heating unit 122B and the steam discharge pipe 122C is condensed as a solvent and supplied to the solvent separator 125. It has become like. Most of the normal hexane is removed in the heating section 122B of the second evaporation can 122, and for example, a miscella having a concentration of 96% is supplied to the oil and fat column 123.

油脂塔１２３は、図１に示すように上下に分割され、下部１２３Ａが上部１２３Ｂより高真空になっている。上下の分割部には、それぞれ複数の棚段が設けられ、濃縮ミセラが各棚段を流下する間にスチームで加熱されてノルマルヘキサンが蒸発して徐々に除去される。また、下部１２３Ａ内の棚段の下方に蒸気吹き込み部１２３Ｃが配置され、高真空下で棚段から流下する油脂内に蒸気をバブリングさせ、バブリング時の気泡表面から油脂中の微量の残留ノルマルヘキサンがガス化して完全に除去され、実質的にノルマルヘキサンを含まない高純度の油脂が得られる。油脂塔１２３において除去されたノルマルヘキサンが第２コンデンサ１２６で凝縮され溶剤セパレータ１２５で回収する。尚、１２７は溶剤セパレータ１２５に付帯する水回収部である。 As shown in FIG. 1, the oil and fat tower 123 is divided into upper and lower parts, and the lower portion 123A has a higher vacuum than the upper portion 123B. A plurality of shelves are provided in the upper and lower divisions, and the concentrated micellar is heated by steam while flowing down each shelf to evaporate normal hexane and gradually remove it. Further, the steam blowing portion 123C is arranged below the shelf stage in the lower 123A, and the steam is bubbled into the fat and oil flowing down from the shelf stage under high vacuum, and a small amount of residual normal hexane in the fat and oil is generated from the bubble surface at the time of bubbling. Is gasified and completely removed, resulting in a high-purity fat and oil that is substantially free of normal hexane. The normal hexane removed in the oil and fat column 123 is condensed by the second capacitor 126 and recovered by the solvent separator 125. Reference numeral 127 is a water recovery unit attached to the solvent separator 125.

また、第２蒸発缶１２２の予熱部１２２Ａのシェル側上部にフラッシュタンク１２８が接続されている。このフラッシュタンク１２８には高温ドレン水が供給されて、常圧下のフラッシュタンク１２８内で高温ドレン水からフラッシュ蒸気が発生するようになっている。このフラッシュ蒸気がフラッシュタンク１２８から配管を介して予熱部１２２Ａのシェル側内に供給され、第１蒸発缶１２１から供給されるミセラを予熱し、加熱部１２２Ｂへ達する前にミセラからノルマルヘキサンの一部を蒸発させるようにしてある。つまり、本実施形態では予熱部１２２Ａにおいてフラッシュ蒸気が再利用され、予熱部１２２Ａ内で予めノルマルヘキサンの一部を蒸発させ、加熱部１２２Ｂではノルマルヘキサンの気泡をなくしてミセラを効率よく加熱し、第２蒸発缶１２２Ｂ全体におけるスチームの使用量を削減するようにしている Further, the flash tank 128 is connected to the upper part of the preheating portion 122A of the second evaporation can 122 on the shell side. High-temperature drain water is supplied to the flash tank 128, and flash steam is generated from the high-temperature drain water in the flash tank 128 under normal pressure. This flush steam is supplied from the flash tank 128 to the shell side of the preheating section 122A via a pipe to preheat the miscella supplied from the first evaporation can 121, and is one of normal hexane from the miscella before reaching the heating section 122B. The part is made to evaporate. That is, in the present embodiment, the flash steam is reused in the preheating section 122A, a part of normal hexane is evaporated in advance in the preheating section 122A, and the heating section 122B eliminates bubbles of normal hexane to efficiently heat the misera. The amount of steam used in the entire second evaporation can 122B is reduced.

予熱部１２２Ａ内で蒸発したノルマルヘキサンガスは上述したように蒸気放出管１２２Ｃから放出され、加熱部１２２へは蒸気を含まないミセラ濃度８４％まで濃縮したミセラが流入するようになっている。加熱部１２２Ｂへ流入するミセラの様子は覗き窓１２２Ｄから確認することができる。加熱部１２２Ｂではノルマルヘキサンガスを含まない状態の濃縮ミセラが通過するため、予熱部１２２Ａ内と相俟ってノルマルヘキサンを効率的に蒸発させ、従来よりも少ないスチーム使用量で高濃度に濃縮された例えば濃度９６％のミセラを生成させることができる。つまり、フラッシュタンク１２８内で高温ドレン水から得られるフラッシュ蒸気を再利用することで第２蒸発缶１２２でのスチーム使用量を削減し、省エネルギーを促進することができる。また、予熱部１２２Ａと加熱部１２２Ｂは配管を介して連通し、加熱部１２２Ｂで使用されたスチームが予熱部１２２Ａで使用されたフラッシュ蒸気と一緒にドレン水として排出されるようになっている。また、フラッシュタンク１２８と予熱部１２２Ａは周方向の複数個所で等間隔を空けて接続されていても良い。これにより予熱部１２２Ａ全周面でミセラを効率よく加熱し、加熱部１２２Ｂではミセラをより効率よく加熱し、ミセラの処理能力を高めることができる。 The normal hexane gas evaporated in the preheating section 122A is discharged from the steam discharge pipe 122C as described above, and the steamer-free miscella concentrated to 84% concentration flows into the heating section 122. The state of the miscellaneous flow into the heating unit 122B can be confirmed from the viewing window 122D. Since the concentrated micellar that does not contain normal hexane gas passes through the heating section 122B, the normal hexane is efficiently evaporated together with the inside of the preheating section 122A, and the normal hexane is concentrated to a high concentration with a smaller amount of steam used than before. For example, a micera having a concentration of 96% can be produced. That is, by reusing the flash steam obtained from the high temperature drain water in the flash tank 128, the amount of steam used in the second evaporation can 122 can be reduced and energy saving can be promoted. Further, the preheating section 122A and the heating section 122B communicate with each other via a pipe, and the steam used in the heating section 122B is discharged as drain water together with the flash steam used in the preheating section 122A. Further, the flash tank 128 and the preheating unit 122A may be connected at a plurality of locations in the circumferential direction at equal intervals. As a result, the micellar is efficiently heated on the entire peripheral surface of the preheating section 122A, and the micellar is heated more efficiently in the heating section 122B, so that the processing capacity of the micellar can be increased.

以上説明したように本実施形態によれば、第２蒸発缶１２２を予熱部１２２Ａと加熱部１２２Ｂに分割し、フラッシュタンク１２８から予熱部１２２Ａにフラッシュ蒸気を供給し、フラッシュ蒸気を再使用してミセラを予熱するようにしたため、第２蒸発缶１２２で余計なノルマルヘキサンの気泡を加熱することがなく、第２蒸発缶１２２でのスチームの使用量を格段に節約することができ、省エネルギーを促進することができる。 As described above, according to the present embodiment, the second evaporation can 122 is divided into a preheating section 122A and a heating section 122B, flash steam is supplied from the flash tank 128 to the preheating section 122A, and the flash steam is reused. Since the miscella is preheated, the second evaporative can 122 does not heat extra normal hexane bubbles, and the amount of steam used in the second evaporative can 122 can be significantly saved, promoting energy saving. can do.

図２は本発明の第２の実施形態を示す構成図である。本実施形態の油脂抽出蒸留設備１００Ａは、抽出部１１０は上記実施形態と実質的に同一に構成されているため、上記実施形態と同一の符号を付してその説明を省略し、蒸発部１２０について説明する。 FIG. 2 is a block diagram showing a second embodiment of the present invention. In the oil / fat extraction / distillation equipment 100A of the present embodiment, since the extraction unit 110 is configured to be substantially the same as that of the above embodiment, the same reference numerals as those of the above embodiment are used to omit the description thereof, and the evaporation unit 120 Will be explained.

本実施形態では、図２に示すように、蒸発部１２０は、第１、第２蒸発缶１２１、１２２及び油脂塔１２３を主体に構成されている。上記実施形態との相違点は、基本的には、第１蒸発缶１２１にもフラッシュタンク１２８が接続されている点、及び油脂塔１２３が棚段を有しない点にある。 In the present embodiment, as shown in FIG. 2, the evaporation unit 120 is mainly composed of the first and second evaporation cans 121 and 122 and the oil and fat tower 123. The difference from the above embodiment is that the flash tank 128 is basically connected to the first evaporation can 121, and the oil and fat tower 123 does not have a shelf.

図２に示すように、第１蒸発缶１２１のシャル側上部にはフラッシュタンク１２８が接続され、フラッシュタンク１２８で生成するフラッシュ蒸気を第１蒸発缶１２１に供給し、フラッシュ蒸気を再利用して第１蒸発缶１２１を加熱し、内部を通るミセラを加熱する。図１に示す従来の第１蒸発缶１２１は脱溶剤器１１５から供給されるノルマルヘキサンガスの余熱を利用しているため、ノルマルヘキサンガスの温度が低く熱容量が小さく、第１蒸発缶１２１でのミセラの濃縮が十分ではなかった。これに対して、本実施形態では第１蒸発缶１２１でもフラッシュ蒸気を利用するため、フラッシュ蒸気の熱容量が脱溶剤器１１５からの加熱ノルマルヘキサンガスの熱容量より大きく、第１蒸発缶１２１を通るミセラをより強く加熱し、ミセラ中のノルマルヘキサンの蒸発量を増やしてミセラを効果的に濃縮し、延いてはミセラの処理能力を高めることができる。 As shown in FIG. 2, a flash tank 128 is connected to the upper portion of the first evaporation can 121 on the shear side, and the flash steam generated by the flash tank 128 is supplied to the first evaporation can 121, and the flash steam is reused. The first evaporation can 121 is heated, and the miscella passing through the inside is heated. Since the conventional first evaporation can 121 shown in FIG. 1 utilizes the residual heat of the normal hexane gas supplied from the solvent remover 115, the temperature of the normal hexane gas is low and the heat capacity is small, so that the first evaporation can 121 has a small heat capacity. The concentration of miscella was not sufficient. On the other hand, in the present embodiment, since the flash steam is also used in the first evaporation can 121, the heat capacity of the flash steam is larger than the heat capacity of the heated normal hexane gas from the solvent remover 115, and the miscella passes through the first evaporation can 121. Can be heated more strongly to increase the evaporation of normal hexane in the micellar to effectively concentrate the micellar, which in turn enhances the processing capacity of the micellar.

また、第２蒸発缶１２２は、図１に示すものと同様に、予熱部１２２Ａ、加熱部１２２Ｂ、蒸気放出管１２２Ｃ及び覗き窓１２２Ｄを備えて構成されているため、フラッシュ蒸気を再利用して第１蒸発缶１２１から供給されるミセラを効率よく加熱し、ミセラを効率的に濃縮することができる。本実施形態では、蒸気放出管１２２Ｃが加熱部１２２Ｂの蒸気滞留部に接続され、予熱部１２２Ａで発生したノルマルヘキサンガスが加熱部１２２Ｂで発生したルマルヘキサンガスと合流するようになっている。従って、第１、第２蒸発缶１２１、１２２からのノルマルヘキサンガスが合流して第１コンデンサ１２４へ供給され、ここでノルマルヘキサンガスが凝縮、液化し、溶剤セパレータ１２５へ供給されるように構成されている。 Further, since the second evaporation can 122 is configured to include the preheating unit 122A, the heating unit 122B, the steam discharge pipe 122C, and the viewing window 122D, as shown in FIG. 1, the flash steam is reused. The micellar supplied from the first evaporation can 121 can be efficiently heated and the micellar can be efficiently concentrated. In the present embodiment, the steam discharge pipe 122C is connected to the steam retention portion of the heating unit 122B, and the normal hexane gas generated in the preheating unit 122A merges with the lumar hexane gas generated in the heating unit 122B. Therefore, the normal hexane gas from the first and second evaporation cans 121 and 122 merges and is supplied to the first capacitor 124, where the normal hexane gas is condensed and liquefied and supplied to the solvent separator 125. Has been done.

図２に示すように、第１蒸発缶１２２から濃縮ミセラを受給する油脂塔１２３は、図２に示すように塔本体１２３Ａが下部１２３Ａ、上部１２３Ｂに分割され、下部１２３Ａと上部１２３Ｂは配管を介して連通している。下部１２３Ａ、上部１２３Ｂにはそれぞれ蒸気吹き込み管１２３Ｃが挿入され、高真空に調整された上下部１２３Ａ、１２３Ｂ内の油脂に蒸気吹き込み管１２３Ｃから水蒸気を吹き込んでバブリングさせて効率よく微量のノルマルヘキサンを除去し、実質的にノルマルヘキサンを含まない油脂を得ることができる。図１に示す油脂塔１２３は、既設の油脂塔１２３を改造して塔本体１２３Ａの下端に気吹き込み管１２３Ｃを設けたため、塔高が高いが、本実施形態では塔高が低くコンパクトに構成されているにも拘わらず、ノルマルヘキサンを確実に除去することができる。 As shown in FIG. 2, in the oil and fat tower 123 that receives the concentrated mixer from the first evaporation can 122, the tower main body 123A is divided into a lower part 123A and an upper part 123B as shown in FIG. 2, and the lower part 123A and the upper part 123B have pipes. Communicate through. A steam blowing pipe 123C is inserted into the lower portion 123A and the upper portion 123B, respectively, and steam is blown into the fats and oils in the upper and lower portions 123A and 123B adjusted to a high vacuum from the steam blowing pipe 123C to bubbling and efficiently a small amount of normal hexane. It can be removed to obtain fats and oils that are substantially free of normal hexanes. The oil and fat tower 123 shown in FIG. 1 has a high tower height because the existing oil and fat tower 123 is modified to provide an air blowing pipe 123C at the lower end of the tower main body 123A, but in the present embodiment, the tower height is low and compactly configured. Nevertheless, normal hexane can be reliably removed.

尚、本実施形態では、脱溶剤器１１５から排出される加熱後のノルマルヘキサンガスは、排熱コレクタ１２９へ供給され、排熱コレクタ１２９内で液化したノルマルヘキサンは溶剤セパレータ１２５へ供給される。また、排熱コレクタ１２９内のノルマルヘキサンガスは凝縮器１２４Ａを介して溶剤セパレータ１２５へ供給される。 In the present embodiment, the heated normal hexane gas discharged from the solvent remover 115 is supplied to the exhaust heat collector 129, and the normal hexane liquefied in the exhaust heat collector 129 is supplied to the solvent separator 125. Further, the normal hexane gas in the exhaust heat collector 129 is supplied to the solvent separator 125 via the condenser 124A.

以上説明したように本実施形態によれば、上記実施形態による効果に加えて、フラッシュ蒸気により第１蒸発缶１２１を効率的に機能させることができ、油脂抽出蒸留設備１００Ａの処理量を増やすことができる。しかも、油脂塔１２３では上下２段の蒸気吹き込み管１２３Ｃによって実質的にノルマルヘキサンを含まない高純度の油脂を得ることができる。 As described above, according to the present embodiment, in addition to the effect of the above embodiment, the first evaporation can 121 can be efficiently functioned by the flash steam, and the processing amount of the fat extraction and distillation equipment 100A can be increased. Can be done. Moreover, in the oil and fat tower 123, high-purity oil and fat that does not substantially contain normal hexane can be obtained by the steam blowing pipes 123C in the upper and lower stages.

図３は本発明の第３の実施形態を示す構成図である。本実施形態の油脂抽出蒸留設備１００Ｂは第１蒸発缶１２１を省略し。油脂塔１２３をコンパクト化したこと以外は、実質的に第２の実施形態と同様に構成されている。本実施形態の油脂抽出蒸留設備１００Ｂは植物油原料の処理量が少ない場合に好ましく適用される。 FIG. 3 is a block diagram showing a third embodiment of the present invention. In the oil / fat extraction / distillation equipment 100B of the present embodiment, the first evaporation can 121 is omitted. Except for the compactification of the oil and fat tower 123, the structure is substantially the same as that of the second embodiment. The oil / fat extraction / distillation equipment 100B of the present embodiment is preferably applied when the processing amount of the vegetable oil raw material is small.

本実施形態では、第１図、図２に示す第１蒸発缶１２１が省略されているため、ここでは第２蒸発缶１２２を単に蒸発缶１２２と称す。蒸発缶１２２は、図３に示すように、ミセラタンク１１３と蒸発缶１２２の予熱部１２２Ａが直に接続され、ミセラタンク１１３から予熱部１２２Ａへミセラが直接供給されるようになっている。蒸発缶１２２が一基だけであるため、上記各実施形態の場合より蒸発缶１２２でのミセラの滞留時間が長くなり、単位時間当たりの処理量が少なくなる。また、油脂塔１２３も第２の実施形態と比較して蒸気吹き込み管１２３Ｃが一つと少なく、処理量が少なくなっている。油脂塔１２３でも第２の実施形態と同程度の品質の油脂を得ることができる。 In the present embodiment, since the first evaporation can 121 shown in FIGS. 1 and 2 is omitted, the second evaporation can 122 is simply referred to as an evaporation can 122 here. As shown in FIG. 3, in the evaporation can 122, the misera tank 113 and the preheating portion 122A of the evaporation can 122 are directly connected, and the misera is directly supplied from the miscella tank 113 to the preheating portion 122A. Since there is only one evaporation can 122, the residence time of the miscella in the evaporation can 122 is longer and the processing amount per unit time is smaller than in the case of each of the above embodiments. Further, the oil and fat tower 123 also has a small number of steam blowing pipes 123C as compared with the second embodiment, and the processing amount is small. The oil and fat tower 123 can also obtain oil and fat of the same quality as that of the second embodiment.

以上説明したように本実施形態でも上記各実施形態と同様にフラッシュ蒸気を再利用することで省エネルギーを促進することができる。 As described above, in the present embodiment as well, energy saving can be promoted by reusing the flash steam as in each of the above embodiments.

図４は本発明の第４の実施形態を示す構成図である。本実施形態の油脂抽出蒸留設備１００Ｃは、同図に示すように、フラッシュタンクに代えて高温ドレン水の供給配管１３０を第１蒸発缶１２１及び第２蒸発缶１２２の予熱部１２２Ａに直接接続したこと以外は図２に示す油脂抽出蒸留設備１００Ａと同様に構成されている。そのため、図２と同様に部分には同一符号を付してその説明を省略し、第２の実施形態と相違する点を中心に説明する。 FIG. 4 is a block diagram showing a fourth embodiment of the present invention. In the oil / fat extraction / distillation equipment 100C of the present embodiment, as shown in the figure, the high temperature drain water supply pipe 130 is directly connected to the preheating portion 122A of the first evaporation can 121 and the second evaporation can 122 instead of the flash tank. Except for this, it is configured in the same manner as the oil / fat extraction / distillation facility 100A shown in FIG. Therefore, the same reference numerals are given to the portions as in FIG. 2, and the description thereof will be omitted, and the differences from the second embodiment will be mainly described.

本実施形態では高温ドレン水の供給配管１３０が二方向に分岐し、２つの分岐管１３０Ａ、１３０Ｂが第１蒸発缶１２１と予熱部１２２Ａそれぞれに直接接続されている。従って、高温ドレン水が２つの分岐管１３０Ａ、１３０Ｂから第１蒸発缶１２１と予熱部１２２Ａそれぞれのシェル側へ直接供給されるようになっている。この供給配管１３０の２つの分岐管１３０Ａ、１３０Ｂそれぞれの先端が第１蒸発缶１２１と予熱部１２２Ａ内に挿入され、それぞれの先端に取り付けられたノズル（図示せず）を介して第１蒸発缶１２１、予熱部１２２Ａそれぞれのシェル側に高温ドレン水を噴射させ、フラッシュ蒸気と１００℃の熱水を生成させる。従って、本実施形態ではフラッシュ蒸気と熱水を利用して第１蒸発缶１２１と予熱部１２２Ａ内を通るミセラをそれぞれ加熱するようにしてある。 In the present embodiment, the high temperature drain water supply pipe 130 branches in two directions, and the two branch pipes 130A and 130B are directly connected to the first evaporation can 121 and the preheating portion 122A, respectively. Therefore, the high-temperature drain water is directly supplied from the two branch pipes 130A and 130B to the shell side of each of the first evaporation can 121 and the preheating portion 122A. The tips of the two branch pipes 130A and 130B of the supply pipe 130 are inserted into the first evaporation can 121 and the preheating portion 122A, and the first evaporation can is passed through a nozzle (not shown) attached to each tip. High-temperature drain water is sprayed onto the shell side of each of 121 and the preheating unit 122A to generate flash steam and hot water at 100 ° C. Therefore, in the present embodiment, the flash steam and hot water are used to heat the first evaporative can 121 and the miscella passing through the preheating portion 122A, respectively.

また、第１蒸発缶１２１と予熱部１２２Ａには分岐管１３１Ａ、１３１Ｂ及びこれらが合流する排出管１３１を介してドレンタンク１３２が接続され、このドレンタンク１３２において第１蒸発缶１２１と予熱部１２２Ａのシェル側内で生成するドレン水を回収し、ドレンタック１３２から例えばボイラー（図示せず）へ戻すようにしてある。 Further, a drain tank 132 is connected to the first evaporation can 121 and the preheating section 122A via branch pipes 131A and 131B and a discharge pipe 131 in which they merge, and in this drain tank 132, the first evaporation can 121 and the preheating section 122A are connected. The drain water generated in the shell side of the above is collected and returned from the drain tack 132 to, for example, a boiler (not shown).

本実施形態によれば、高温ドレン水を第１蒸発缶１２１と第２蒸発缶１２２の予熱部１２２Ａ内へ直接供給するため、高温ドレン水の熱エネルギーをより効果的に利用し、油脂精製能力を高めることができる。 According to the present embodiment, since the high temperature drain water is directly supplied into the preheating section 122A of the first evaporative can 121 and the second evaporative can 122, the thermal energy of the high temperature drain water is used more effectively and the oil and fat refining ability is achieved. Can be enhanced.

また、供給管１３０の分岐管１３０Ａの第１蒸発缶１２１との接続部は、図５（ａ）、（ｂ）に示すように構成することができる。即ち、第１蒸発缶１２１のシェル上部に大径部１２１Ａを設け、この部分に分岐管１３０Ａを接続するようにする。この分岐管１３０Ａは、第１蒸発缶１２１の大径部１２１Ａを囲むリング部１３０Ａ１と、このリング部１３０Ａ１の３箇所に等間隔を空けて配置されたノズル１３０Ａ２と、を有し、３箇所のノズル１３０Ａ２が第１蒸発缶１２１の大径部１２１Ａ内に挿入され、３箇所のノズル１３０Ａ１からシェル内に高温ドレン水を噴射するようになっている。また、第２蒸発缶１２２の予熱部１２２Ａに高温ドレン水を供給する分岐管１３０Ｂも分岐管１３０Ａと同様に構成することができる。尚、図５において、１２１Ｂはミセラの流れるパイプである。 Further, the connection portion of the branch pipe 130A of the supply pipe 130 with the first evaporation can 121 can be configured as shown in FIGS. 5A and 5B. That is, a large diameter portion 121A is provided on the upper part of the shell of the first evaporation can 121, and the branch pipe 130A is connected to this portion. The branch pipe 130A has a ring portion 130A 1 surrounding the large diameter portion 121A of the first evaporation can 121, and nozzles 130A 2 arranged at three positions of the ring portion 130A 1 at equal intervals. Three nozzles 130A 2 are inserted into the large diameter portion 121A of the first evaporation can 121, and high-temperature drain water is sprayed into the shell from the three nozzles 130A 1 . Further, the branch pipe 130B for supplying the high temperature drain water to the preheating portion 122A of the second evaporation can 122 can be configured in the same manner as the branch pipe 130A. In FIG. 5, 121B is a pipe through which the misera flows.

このような構成により第１蒸発缶１２１及び予熱部１２２Ａ全体に高温ドレン水を満遍なく供給し、それぞれのミセラ全体を均一に加熱することができる。このような構成はフラッシュタンクからフラシュ蒸気を供給する第１、第２の実施形態にも適用することができる。 With such a configuration, high-temperature drain water can be evenly supplied to the entire first evaporation can 121 and the preheating portion 122A, and the entire micellar can be uniformly heated. Such a configuration can also be applied to the first and second embodiments in which flash steam is supplied from the flash tank.

尚、本発明は上記各実施形態に何ら制限されるものではなく、本発明の趣旨に反しない限り、各構成要素を必要に応じて適宜変更することができる。 The present invention is not limited to each of the above embodiments, and each component can be appropriately modified as necessary as long as it does not contradict the gist of the present invention.

１００、１００Ａ、１００Ｂ、１００Ｃ 油脂抽出蒸留設備
１２０ 蒸発部
１２１ 第１蒸発缶
１２２ 第２蒸発缶
１２２Ａ 予熱部
１２２Ｂ 加熱部
１２２Ｃ 蒸気放出管（排気部）
１２３ 油脂塔
１２３Ａ 塔本体
１２３Ｃ 蒸気吹き込み管
１２８ フラッシュタンク
１３０ 高温ドレン水の供給配管 100, 100A, 100B, 100C Oil extraction and distillation equipment 120 Evaporation unit 121 First evaporation can 122 Second evaporation can 122A Preheating unit 122B Heating unit 122C Steam discharge pipe (exhaust unit)
123 Oil tower 123A Tower body 123C Steam blow pipe 128 Flash tank 130 High temperature drain water supply pipe

Claims (5)

油脂抽出液を受給しその溶剤を蒸発させる少なくとも一つの蒸発缶を備えた油脂抽出液蒸発設備であって、上記蒸発缶は、上記油脂抽出液を予熱する予熱部と、上記予熱部の下流側に接続されて上記油脂抽出液を加熱する加熱部と、上記予熱部の下流側に上記加熱部と併設されて上記予熱部で上記油脂抽出液から蒸発する溶剤を排出する排気部と、を有し、上記予熱部にフラッシュ蒸気を供給するフラッシュタンクを接続し、上記フラッシュ蒸気によって上記予熱部を予熱することを特徴とするフラッシュ蒸気を用いる油脂抽出蒸留設備。 It is an oil and fat extract evaporating facility equipped with at least one evaporative can that receives the oil and fat extract and evaporates the solvent. It has a heating unit connected to the oil and fat extract to heat the oil and fat extract, and an exhaust unit connected to the heating unit on the downstream side of the preheating unit and discharging the solvent evaporating from the oil and fat extract in the preheating unit. An oil / fat extraction distillation facility using flash steam, which comprises connecting a flash tank for supplying flash steam to the preheating section and preheating the preheating section with the flash steam. 上記少なくとも一つの蒸発缶は、上流側に配置された第１蒸発缶と、下流側に配置された第２蒸発缶と、を備え、上記第２蒸発缶は、上記予熱部、上記加熱部及び上記排気部を有し、上記第１蒸発缶及び上記予熱部それぞれに上記フラッシュタンクを接続したことを特徴とする請求項１に記載のフラッシュ蒸気を用いる油脂抽出蒸留設備。 The at least one evaporation can includes a first evaporation can arranged on the upstream side and a second evaporation can arranged on the downstream side, and the second evaporation can includes the preheating section, the heating section, and the heating section. The oil / fat extraction / distillation facility using the flash steam according to claim 1, further comprising the exhaust section and connecting the flash tank to each of the first evaporation can and the preheating section. 油脂抽出液を受給しその溶剤を蒸発させる少なくとも一つの蒸発缶を備えた油脂抽出液蒸発設備であって、上記蒸発缶は、上記油脂抽出液を予熱する予熱部と、上記予熱部の下流側に接続されて上記油脂抽出液を加熱する加熱部と、上記予熱部の下流側に上記加熱部と併設されて上記予熱部で上記油脂抽出液から蒸発する溶剤を排出する排気部と、を有し、上記予熱部に高温ドレン水の供給配管を接続し、上記供給配管を介して上記予熱部内に上記高温ドレン水を供給してフラッシュ蒸気及びフラッシュ後の熱水をそれぞれ生成させ、これらのフラッシュ蒸気及び熱水によって上記予熱部を予熱することを特徴とするフラッシュ蒸気を用いる油脂抽出蒸留設備。 An oil / fat extract evaporating facility equipped with at least one evaporative can for receiving the oil / fat extract and evaporating the solvent. The evaporative can has a preheating unit for preheating the oil / fat extract and a downstream side of the preheating unit. It has a heating unit that is connected to the oil and fat extract to heat the oil and fat extract, and an exhaust unit that is installed next to the heating unit on the downstream side of the preheating unit and discharges a solvent that evaporates from the oil and fat extract in the preheating unit. Then, a high-temperature drain water supply pipe is connected to the preheating section, and the high-temperature drain water is supplied into the preheating section via the supply pipe to generate flash steam and hot water after flushing, respectively. An oil / fat extraction distillation facility using flash steam, which preheats the preheated portion with steam and hot water. 上記少なくとも一つの蒸発缶は、上流側に配置された第１蒸発缶と、下流側に配置された第２蒸発缶と、を備え、上記第２蒸発缶は、上記予熱部、上記加熱部及び上記排気部を有し、上記第１蒸発缶及び上記予熱部それぞれに高温ドレン水の供給配管を接続したことを特徴とする請求項３に記載のフラッシュ蒸気を用いる油脂抽出蒸留設備。 The at least one evaporation can includes a first evaporation can arranged on the upstream side and a second evaporation can arranged on the downstream side, and the second evaporation can includes the preheating section, the heating section, and the heating section. The oil / fat extraction / distillation facility using flash steam according to claim 3, further comprising the exhaust unit and connecting a high-temperature drain water supply pipe to each of the first evaporation can and the preheating unit. 上記すくなくとも一つの蒸発缶から受給する油脂抽出液中の残留溶剤を除去する油脂塔を備え、上記油脂塔は、上記蒸発缶からの油脂抽出液を受給する塔本体と、上記塔本体内に挿入されて上記蒸発缶からの油脂抽出液中に蒸気をバブリングさせる蒸気吹き込み部を有することを特徴とする請求項１～請求項４のいずれか１項に記載のフラッシュ蒸気を用いる油脂抽出蒸留設備。 The oil and fat tower is provided with an oil and fat tower for removing residual solvent in the oil and fat extract received from at least one evaporation can, and the oil and fat tower is inserted into the tower body for receiving the oil and fat extract from the evaporation can and the inside of the tower body. The oil / fat extraction / distillation facility using the flash steam according to any one of claims 1 to 4, further comprising a steam blowing portion for bubbling steam in the oil / fat extract from the evaporation can.
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JP7503276B1 (en) 2023-11-18 2024-06-20 株式会社宮富士工業 Oil extraction and distillation equipment

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JPS5968398A (en) * 1982-07-23 1984-04-18 ヘルマン・スタゲ Method and device of deodorization and/or phisical purifica-tion for high boiling point organic edible oil, fat and este
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JPS58147499A (en) * 1982-02-26 1983-09-02 玉川機械株式会社 Rice oil manufacturing device
JPS5968398A (en) * 1982-07-23 1984-04-18 ヘルマン・スタゲ Method and device of deodorization and/or phisical purifica-tion for high boiling point organic edible oil, fat and este
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