JP2694427B2 - Internal heat exchange type distillation column - Google Patents
Internal heat exchange type distillation columnInfo
- Publication number
- JP2694427B2 JP2694427B2 JP30282994A JP30282994A JP2694427B2 JP 2694427 B2 JP2694427 B2 JP 2694427B2 JP 30282994 A JP30282994 A JP 30282994A JP 30282994 A JP30282994 A JP 30282994A JP 2694427 B2 JP2694427 B2 JP 2694427B2
- Authority
- JP
- Japan
- Prior art keywords
- pipe
- tube
- outside
- distillation column
- heat exchange
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Description
【発明の詳細な説明】DETAILED DESCRIPTION OF THE INVENTION
【０００１】[0001]
【産業上の利用分野】本発明は、蒸留塔に関し、詳しく
は、低圧塔と高圧塔とを備え両者の間で熱交換を行う内
部熱交換型の蒸留塔に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a distillation column, and more particularly to an internal heat exchange type distillation column comprising a low pressure column and a high pressure column for exchanging heat between them.
【０００２】[0002]
【関連技術及び発明が解決しようとする課題】従来、石
油化学その他の分野で種々の蒸留操作が行われている。
ところで、図４に示すような、従来の蒸留操作に用いら
れている蒸留塔によれば、例えばベンゼン・トルエン３
０ｔｏｎを蒸留して、トルエン１６．５ｔｏｎ、ベンゼ
ン１３．５ｔｏｎを回収しようとすると、入熱が４００
０ｋＷ、放熱が３９４０ｋＷとなる。そして、この放熱
が４３℃の温排水と系外に排出されることになるが、温
排水の温度が４３℃と低いため温排水のもつ熱を利用す
ることができず、そのまま排水されているのが現状であ
り、省資源、省エネルギーの見地からみて好ましいもの
ではない。Related Art and Problems to be Solved by the Invention Conventionally, various distillation operations have been carried out in petrochemical and other fields.
By the way, according to a distillation column used in a conventional distillation operation as shown in FIG. 4, for example, benzene / toluene 3
When 0 ton was distilled and 16.5 ton of toluene and 13.5 ton of benzene were to be recovered, the heat input was 400.
0 kW and heat dissipation is 3940 kW. Then, this heat radiation is discharged to the outside of the system with the warm wastewater of 43 ° C, but since the temperature of the warm wastewater is as low as 43 ° C, the heat of the warm wastewater cannot be used and is discharged as it is. The current situation is that it is not preferable from the viewpoint of resource saving and energy saving.
【０００３】そこで、発明者等は、多管型熱交換器のよ
うに、単管または複数管を両端管板によって本体胴と連
結させて、管内と管外が隔離された構造とし、管内側と
管外側の操作圧力に差をつけることにより、管内側と管
外側のいずれか一方を低圧塔、他方を高圧塔とし、単管
または複数管の管壁を伝熱面として、両者の間で熱交換
を行わせるようにした内部熱交換型蒸留塔を提案してい
る（平成６年８月２９日提出の特許出願（整理番号ＫＣ
６０６２Ｐ），「発明の名称」内部熱交換型蒸留塔）。Therefore, the inventors of the present invention, like a multi-tube heat exchanger, connect a single tube or a plurality of tubes to the main body by means of tube plates at both ends so that the inside of the tube and the outside of the tube are separated from each other. By making a difference in operating pressure between the inside and outside of the pipe, one of the inside and outside of the pipe is a low-pressure column, the other is a high-pressure column, and the wall of a single pipe or multiple pipes is used as a heat transfer surface. We have proposed an internal heat exchange type distillation column that allows heat exchange (Patent application filed on August 29, 1994 (reference number KC
6062P), "Title of Invention" internal heat exchange type distillation column).
【０００４】しかし、単管または複数管の管壁を伝熱面
として両者の間で熱交換を行わせるようにした構造の内
部熱交換型蒸留塔においては、確保することが可能な伝
熱面積に構造上の限界があり、取り扱う物質の物性や蒸
留分離の精度に対応して、理論的に最も効率よく省エネ
ルギー効果を発揮させるために必要な伝熱面積を確保で
きない場合がある。However, in an internal heat exchange type distillation column having a structure in which heat is exchanged between the single tube wall or the plural tube walls as a heat transfer surface, the heat transfer area that can be secured is There is a structural limit, and it may not be possible to secure the heat transfer area that is theoretically most efficient in order to exert the energy saving effect, depending on the physical properties of the substance to be handled and the accuracy of distillation separation.
【０００５】本発明は、上記問題点を解決するものであ
り、取り扱う物質の物性や蒸留分離の精度に対応した伝
熱面積を確保して、十分な省エネルギー効果を得ること
が可能な内部熱交換型蒸留塔を提供することを目的とす
る。The present invention solves the above-mentioned problems, and an internal heat exchange capable of obtaining a sufficient energy-saving effect by ensuring a heat transfer area corresponding to the physical properties of a substance to be handled and the accuracy of distillation separation. An object is to provide a type distillation column.
【０００６】[0006]
【課題を解決するための手段】上記目的を達成するため
に、本発明の内部熱交換型蒸留塔は、本体胴内に単管を
挿入するとともに、管内（単管の内側）と管外（単管の
外側）が隔離された構造とし、管内側と管外側の操作圧
力に差をつけることにより操作温度を異ならせ、高圧側
から低圧側に熱移動させることにより、高圧側を濃縮
部、低圧側を回収部として一つの蒸留塔を構成した内部
熱交換型蒸留塔において、前記単管をその軸方向に複数
に分割形成するとともに、互に隣接する単管のうちの、
一方の単管の管外を構成する領域（一方の領域）と他方
の単管の管外を構成する領域（他方の領域）の間に、前
記一方の領域と他方の領域を連通させる１以上の連通管
を配設し、前記単管の管壁及び前記連通管の管壁を、前
記高圧側から前記低圧側への伝熱面としたことを特徴と
する。In order to achieve the above object, in the internal heat exchange type distillation column of the present invention, a single tube is inserted into the body barrel, and at the same time, inside the tube (inside the single tube) and outside the tube (inside the tube). the outer single pipe) was isolated structure, with different operating temperature by attaching a difference in operating pressure in the tube side and the abluminal, by heat transfer to the low pressure side from the high pressure side, enriching section high-pressure side, In an internal heat exchange type distillation column that constitutes one distillation column with the low pressure side as a recovery part, while dividing the single tube into a plurality of parts in the axial direction, among the single tubes adjacent to each other ,
During the region constituting the extravascular between the region constituting the extravascular one-way single tube (one area) other monotube (other regions), prior to
The one or more communication pipes that connect the one region and the other region are provided, and the pipe wall of the single pipe and the pipe wall of the communication pipe are heat transfer surfaces from the high pressure side to the low pressure side. It is characterized by
【０００７】また、管内及び管外に充填物を充填したこ
とを特徴とする。Further, it is characterized in that a filling material is filled inside and outside the tube.
【０００８】また、管内に規則充填物を充填して濃縮部
とし、管外に不規則充填物を充填して回収部としたこと
を特徴とする。Further, the invention is characterized in that the tube is filled with an ordered packing to form a concentrating section and the outside of the tube is filled with an irregular packing to form a collecting section.
【０００９】また、管内及び管外に棚段を設けたことを
特徴とする。Further, it is characterized in that a shelf is provided inside and outside the pipe.
【００１０】また、管内に棚段を設け、管外に充填物を
充填したことを特徴とする。Further, the present invention is characterized in that a tray is provided inside the pipe and a filling material is filled outside the pipe.
【００１１】また、管内に充填物を充填し、管外に棚段
を設けたことを特徴とする。Further, the invention is characterized in that a filling material is filled in the pipe and a shelf is provided outside the pipe.
【００１２】[0012]
【作用】管内（単管の内側）と管外（単管の外側）を隔
離し、管内側と管外側の操作圧力に差をつけることによ
り、管内側と管外側のいずれか一方を低圧塔、他方を高
圧塔とし、単管の管壁を伝熱面として、高圧側（高温
側）から低圧側（低温側）に熱移動させることにより、
実用可能な内部熱交換型蒸留塔が構成される。[Function] By separating the inside of the pipe (inside of the single pipe) and the outside of the pipe (outside of the single pipe) and making a difference in the operating pressure between the inside of the pipe and the outside of the pipe, either the inside or outside of the pipe is a low pressure column. , The other is a high pressure column, and the wall of the single tube is a heat transfer surface, and heat is transferred from the high pressure side (high temperature side) to the low pressure side (low temperature side),
A practical internal heat exchange type distillation column is constructed.
【００１３】さらに、前記単管をその軸方向に複数に分
割形成し、互に隣接する単管のうちの、一方の単管の管
外を構成する領域（一方の領域）と他方の単管の管外を
構成する領域（他方の領域）を連通させる１以上の連通
管を配設し、単管の管壁及び連通管の管壁を、高圧側か
ら低圧側への伝熱面とすることにより、全体として必要
な伝熱面積を確保することが可能になり、取り扱う物質
の物性や蒸留分離の精度に対応した、十分な省エネルギ
ー化を図ることが可能になる。Furthermore, the single tube divided form into a plurality in the axial direction, each other of the adjacent single tube, monotube a region (one region) other constituting the extravascular of one single tube One or more communication pipes that communicate the region (the other region) that constitutes the outside of the pipe are provided, and the pipe wall of the single pipe and the pipe wall of the communication pipe are heat transfer surfaces from the high pressure side to the low pressure side. As a result, it is possible to secure the necessary heat transfer area as a whole, and it is possible to achieve sufficient energy saving corresponding to the physical properties of the substance to be handled and the accuracy of distillation separation.
【００１４】なお、蒸留操作は、主として、単管の内部
（管内）と外部（管外）で行われるが、連通管の内部及
び外部においても、連通管の管壁を上部より液が流れ、
下部より上昇する蒸気と気液接触する（いわゆる濡れ壁
塔となる）ことにより蒸留操作が行われる。The distillation operation is mainly carried out inside (inside the pipe) and outside (outside the pipe) the single pipe, but also inside and outside the communication pipe, the liquid flows from the upper part through the pipe wall of the communication pipe,
Distillation operation is performed by making vapor-liquid contact with vapor rising from the lower part (so-called wet wall column).
【００１５】また、塔頂より塔底に至る全蒸留部におい
て、内部熱交換型蒸留塔の最適設計値に合うように、各
単管の高さ（長さ）と、連通管の高さ（長さ）を決定す
ることにより、最も効率よく省エネルギー化を図ること
が可能になる。なお、各単管の高さ（長さ）は、多くの
場合、蒸留棚０．５〜５段程度に相当する高さになるも
のと考えられるが、その範囲に特別の制約はない。Further, in the entire distillation section from the top to the bottom of the tower, the height (length) of each single tube and the height of the communication tube (to meet the optimum design value of the internal heat exchange type distillation tower) By determining the length, the energy can be saved most efficiently. The height (length) of each single tube is considered to be a height corresponding to about 0.5 to 5 distillation shelves in most cases, but there is no particular restriction on the range.
【００１６】さらに、本発明の内部熱交換型蒸留塔にお
いては、管内及び管外に充填物を充填することにより、
蒸留分離の精度や省エネルギー効果を向上させることが
可能になり、特に、管内に規則充填物を充填して濃縮部
とし、管外に不規則充填物を充填して回収部とすること
により、さらに蒸留分離の精度や省エネルギー効果に優
れた内部熱交換型蒸留塔を得ることが可能になる。Further, in the internal heat exchange type distillation column of the present invention, by filling the inside and outside of the pipe with a packing,
It is possible to improve the accuracy of distillative separation and the energy saving effect. In particular, by filling the tube with a regular packing as a concentrating section and filling the outside of the tube with an irregular packing as a collecting section, It is possible to obtain an internal heat exchange type distillation column excellent in accuracy of distillation separation and energy saving effect.
【００１７】なお、管内に規則充填物を充填して濃縮部
とし、管外に不規則充填物を充填して回収部とすること
が望ましいのは、次のような理由による。The reason why it is desirable to fill the inside of the tube with the regular packing to form the concentrating section and to fill the outside of the tube with the irregular packing to form the collecting section is as follows.
【００１８】（１）濃縮部から回収部に水平方向に熱移
動があるため、濃縮部では熱交換されて冷却された蒸気
が伝熱面を液膜となって流下する。一方回収部では、伝
熱面上の液膜は、加熱され、蒸発する。そして、蒸留効
率を向上させるためには、この伝熱面上で新しく発生し
た液を蒸留部全体に均等に分散させることが重要である
が、それには、不規則充填物を充填するより規則充填物
を充填する方がはるかに有利である。また、管内に規則
充填物を充填するのはきわめて容易であるが、管外に規
則充填物を充填することは容易ではない。一方、伝熱面
上で新しく発生した蒸気の分散に関しては、規則充填、
不規則充填の差はそれほど大きいものではなく、いずれ
の場合にも、蒸気を蒸留部全体に均等に分散させること
が可能であると考えられる。(1) Since there is horizontal heat transfer from the concentrating section to the collecting section, the vapor that has been heat-exchanged and cooled in the concentrating section flows down as a liquid film on the heat transfer surface. On the other hand, in the recovery part, the liquid film on the heat transfer surface is heated and evaporated. And in order to improve the distillation efficiency, it is important to evenly disperse the newly generated liquid on the heat transfer surface throughout the distillation section, which is more regular packing than irregular packing. It is much more advantageous to fill things. Further, it is extremely easy to fill the regular packing inside the pipe, but it is not easy to fill the regular packing outside the pipe. On the other hand, regarding the dispersion of newly generated steam on the heat transfer surface, regular filling,
The difference in irregular packing is not so large, and in any case, it is considered possible to evenly disperse the vapor throughout the distillation section.
【００１９】（２）一般に、強度上は、高圧側は径の小
さいことが望ましく、保温上は、操作温度の高い方が内
部にあることが望ましい。したがって、濃縮部（高圧
（高温）側）が管内となり、それを取り囲むように回収
部（低圧（低温）側）が管外となる構造とすることが望
ましい。(2) In general, it is desirable that the diameter is small on the high pressure side in terms of strength, and it is desirable that the operating temperature is higher inside in terms of heat retention. Therefore, it is desirable to have a structure in which the concentrating part (high pressure (high temperature) side) is inside the pipe and the collecting part (low pressure (low temperature) side) is outside the pipe so as to surround it.
【００２０】なお、内部熱交換型蒸留塔は、前記（１）
において述べたように、濃縮部では蒸気が凝縮するので
気液の流量は下部ほど増加し、回収部では液が蒸発する
ので気液の流量は上部ほど増加する。したがって、濃縮
部断面積対回収部断面積の比（管内側総断面積／管外側
総断面積）は、塔頂が最も小さく、塔底になるにしたが
って増大し、塔底では最大になる構造であることが最も
望ましい。The internal heat exchange type distillation column is described in (1) above.
As described above, since the vapor is condensed in the concentrating part, the flow rate of the gas-liquid increases toward the lower part, and the liquid vaporizes in the recovery part, and the flow rate of the gas-liquid increases toward the upper part. Therefore, the ratio of the cross-sectional area of the enrichment section to the cross-section of the recovery section (total cross-sectional area inside the pipe / total cross-sectional area outside the pipe) is the smallest at the top of the column, increases as it goes to the bottom, and becomes the maximum at the bottom. Is most desirable.
【００２１】また、管内、管外を棚段構造とするとき、
その段間隔は、自由にとることが可能であるため、伝熱
面積を確保する見地から一段当りの高さを調整すること
ができる。When the inside and outside of the pipe have a shelf structure,
Since the step interval can be freely set, the height per step can be adjusted from the viewpoint of ensuring the heat transfer area.
【００２２】なお、棚段構造とした場合には、伝熱面上
で凝縮した液がその段上で、必ず分散されるというメリ
ットがある。The shelf structure has an advantage that the liquid condensed on the heat transfer surface is always dispersed on the plate.
【００２３】また、棚段構造としては、多孔板、無堰が
最も本発明の構造に適している。As the shelf structure, a perforated plate and a weirless structure are most suitable for the structure of the present invention.
【００２４】さらに、管内に棚段を設け、管外に充填物
を充填したり、あるいは、管内に充填物を充填し、管外
に棚段を設けたりすること（すなわち、充填物と棚段を
任意に組み合せること）も可能であり、これにより、設
計の自由度を向上させることが可能になる。Further, it is possible to provide a tray inside the pipe and fill the filling outside the pipe, or to fill the filling inside the pipe and provide a tray outside the pipe (that is, the filling and the tray). Can be arbitrarily combined), and thereby the degree of freedom in design can be improved.
【００２５】[0025]
【実施例】以下、この発明の実施例を図に基づいて説明
する。図１（ａ）はこの発明の一実施例にかかる内部熱
交換型蒸留塔を示す正面断面図、図１（ｂ）はそのＩｂ
−Ｉｂ線断面図である。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS An embodiment of the present invention will be described below with reference to the drawings. FIG. 1 (a) is a front sectional view showing an internal heat exchange type distillation column according to an embodiment of the present invention, and FIG. 1 (b) is its Ib.
It is a -Ib line sectional view.
【００２６】この実施例の内部熱交換型蒸留塔（を構成
する構造体）Ａは、本体胴１内に複数に分割形成された
単管２，２……を挿入するとともに、互に隣接する単管
２のうちの、一方の単管（例えば２ａ）の管外を構成す
る領域（本体胴１と単管２ａにより仕切られた空間）
（一方の領域）５（５ａ）と、隣接する他方の単管（例
えば２ｂ）の管外を構成する領域（本体胴１と単管２ｂ
により仕切られた空間）（他方の領域）５（５ｂ）を連
通させる複数（この実施例では１０本）の連通管２０を
配設することにより構成されている。そして、各単管２
の高さ（長さ）Ｈ、及び連通管２０の高さ（長さ）ｈの
値（すなわち、Ｈ及びｈの絶対値、及びＨとｈの比率）
は、コンピュータにより算出した採算性に見合う最適設
計値に合わせて定められている。なお、この実施例で
は、各単管２の高さ（長さ）Ｈは、蒸留棚１〜３段に相
当する高さとなっている。In the internal heat exchange type distillation column A of this embodiment (a structure constituting the same), the single tubes 2, 2 ... Divided into a plurality of pieces are inserted into the main body cylinder 1 and are adjacent to each other. of single pipe 2, one single tube area constituting the outer tube (e.g. 2a) (space partitioned by the body cylinder 1 and the single tube 2a)
(One area) 5 (5a) and an area that constitutes the outside of the other adjacent single tube (for example, 2b) (main body 1 and single tube 2b)
It is configured by arranging a plurality of (10 in this embodiment) communicating pipes 20 for communicating the space (the other region) 5 (5b). And each single tube 2
Height (length) H and the height (length) h of the communicating pipe 20 (that is, the absolute value of H and h, and the ratio of H and h)
Is determined in accordance with the optimum design value calculated by the computer which is suitable for profitability. In addition, in this embodiment, the height (length) H of each single tube 2 is a height corresponding to the first to third distillation shelves.
【００２７】また、この内部熱交換型蒸留塔において
は、各単管２の管内（濃縮部）４とその外側部分である
管外（回収部）５が隔離された構造を有しており、管内
（濃縮部）４には規則充填物が充填され、管外（回収
部）５には不規則充填物が充填されている。The internal heat exchange type distillation column has a structure in which the inside (concentration section) 4 of each single tube 2 and the outside (recovery section) 5 which is the outside thereof are isolated. The inside (concentration part) 4 of the pipe is filled with ordered packing, and the outside (collecting part) 5 is filled with irregular packing.
【００２８】本体胴１の上部には、最上部の単管２の管
外（回収部）５に液を供給するための回収部液入口６、
管外（回収部）５からの蒸気を抜き出す回収部蒸気出口
７、及び管内（濃縮部）４に液を供給するための濃縮部
液入口８が配設されているとともに、最上部の単管２か
ら延設された管２２ａの上部開口が管内（濃縮部）４か
らの蒸気を抜き出す濃縮部蒸気出口９となっている。At the upper part of the main body 1, a recovery part liquid inlet 6 for supplying liquid to the outside (recovery part) 5 of the uppermost single pipe 2,
A recovery part vapor outlet 7 for extracting steam from the outside of the pipe (recovery part) 5 and a concentrating part liquid inlet 8 for supplying the liquid to the inside of the pipe (concentrating part) 4 are arranged, and the uppermost single pipe The upper opening of the pipe 22 a extending from 2 serves as a vaporizing portion vapor outlet 9 for extracting vapor from the inside (concentrating portion) 4 of the pipe.
【００２９】一方、本体胴１の下部には、管外（回収
部）５に蒸気を供給するための回収部蒸気入口１０、管
外（回収部）５からの液を抜き出す回収部液出口１１が
配設されているとともに、最下部の単管２から延設され
た管２２ｂの下部開口が管内（濃縮部）４に蒸気を供給
するための濃縮部蒸気入口１２及び管内（濃縮部）４か
らの液を抜き出すための濃縮部液出口１３となってい
る。On the other hand, in the lower part of the main body 1, a recovery part vapor inlet 10 for supplying steam to the outside of the pipe (recovery part) 5 and a recovery part liquid outlet 11 for extracting the liquid from the outside of the pipe (recovery part) 5 And a lower opening of a pipe 22b extending from the lowermost single pipe 2 is provided with a vaporizing portion vapor inlet 12 for supplying vapor into the pipe (concentrating portion) 4 and the pipe (concentrating portion) 4 It is a concentration part liquid outlet 13 for extracting the liquid from the.
【００３０】また、図２は、図１に示す内部熱交換型蒸
留塔（を構成する構造体）Ａと同等の内部熱交換型蒸留
塔（構造体）を用いて構成した内部熱交換型蒸留塔（装
置）を示す図である。なお、図２において、図１と同一
符号を付した部分は、図１の各部と同一の部分又は相当
する部分を示している。Further, FIG. 2 shows an internal heat exchange type distillation column (structure) which is equivalent to the internal heat exchange type distillation column (structure which constitutes) A shown in FIG. It is a figure which shows a tower (apparatus). In addition, in FIG. 2, the parts given the same reference numerals as those in FIG. 1 indicate the same parts as or the parts corresponding to the parts in FIG.
【００３１】この内部熱交換型蒸留塔においては、原液
は構造体Ａの回収部液入口６に供給される。In this internal heat exchange type distillation column, the stock solution is supplied to the recovery section liquid inlet 6 of the structure A.
【００３２】構造体Ａの回収部蒸気出口７は、管２３に
より濃縮部蒸気入口１２に接続されており、管２３には
蒸気を圧縮するための圧縮機２４が配設されている。The recovery part vapor outlet 7 of the structure A is connected to the concentration part vapor inlet 12 by a pipe 23, and the pipe 23 is provided with a compressor 24 for compressing vapor.
【００３３】さらに、構造体Ａの濃縮部液出口１３から
抜き出された液は、絞り弁２５を備えた管２６を経て回
収部液入口６に供給される。Further, the liquid extracted from the concentration part liquid outlet 13 of the structure A is supplied to the recovery part liquid inlet 6 via a pipe 26 equipped with a throttle valve 25.
【００３４】また、構造体Ａの濃縮部蒸気出口９から抜
き出された蒸気は、管２７により冷却器２８に導かれて
凝縮し、留出液として回収されるとともに、一部が濃縮
部液入口８に戻される。Further, the vapor extracted from the vaporizing outlet 9 of the concentrating portion of the structure A is guided to a cooler 28 by a pipe 27 and condensed, and is collected as a distillate, and a part of the liquid is concentrated portion. Returned to the entrance 8.
【００３５】さらに、構造体Ａの回収部液出口１１から
抜き出された液は管２９を経て、缶出液として系外に排
出される。Further, the liquid withdrawn from the recovery portion liquid outlet 11 of the structure A is discharged to the outside of the system as a bottom liquid through the pipe 29.
【００３６】この内部熱交換型蒸留塔においては、例え
ば、図３に示すように、ベンゼン・トルエン３０ｔｏｎ
を蒸留して、トルエン１６．５ｔｏｎ、ベンゼン１３．
５ｔｏｎを回収する場合に、入熱が２０００ｋＷ、圧縮
機の動力が４５０ｋＷ、回収される熱エネルギーが１５
０℃（２２００ｋＷ）となり、前述の従来の蒸留塔を用
いる場合に較べて格段の省エネルギーを実現することが
できる。In this internal heat exchange type distillation column, for example, as shown in FIG.
Was distilled to give 16.5 ton of toluene and 13.
When recovering 5 tons, the heat input is 2000 kW, the power of the compressor is 450 kW, and the recovered heat energy is 15 kW.
The temperature is 0 ° C. (2200 kW), and much energy saving can be realized as compared with the case of using the conventional distillation column described above.
【００３７】なお、上記実施例では、各単管を連通させ
る連通管の配設数を１０本とした場合について説明した
が、連通管の配設数はこれに限られるものではなく、必
要な伝熱面積を確保すべく、その配設数を任意に調整す
ることが可能である。また、連通管の径や長さを調節す
ることによっても伝熱面積の大きさを調整することが可
能である。In the above embodiment, the case where the number of connecting pipes for connecting the individual pipes to each other was set to 10 has been described, but the number of connecting pipes is not limited to this, and is necessary. In order to secure the heat transfer area, the number of the heat transfer areas can be arbitrarily adjusted. Also, the size of the heat transfer area can be adjusted by adjusting the diameter and length of the communication pipe.
【００３８】また、上記実施例では、一つの内部熱交換
型蒸留塔（構造体Ａ）を用いた場合について説明した
が、所定の蒸留性能が実現されるように、必要に応じて
構造体Ａを、複数段積み重ねるように構成することも可
能である。Further, in the above embodiment, the case where one internal heat exchange type distillation column (structure A) is used has been described, but the structure A is used as required so that a predetermined distillation performance is realized. Can also be configured to be stacked in multiple stages.
【００３９】また、上記実施例では、管内側を濃縮部、
管外側を回収部とした場合について説明したが、場合に
よっては、管内側を低圧側として回収部とし、管外側を
高圧側として濃縮部とすることも可能である。Further, in the above embodiment, the inside of the pipe is
Although the case where the outside of the tube is used as the recovery unit has been described, in some cases, the inside of the tube may be used as the recovery unit with the low pressure side, and the outside of the tube may be used as the concentration unit with the high pressure side.
【００４０】また、上記実施例では、管内側に規則充填
物、管外側に不規則充填物を充填した場合について説明
したが、場合によっては、充填物の種類を同一にした
り、あるいは逆にしたり、さらには、棚段構造や、棚段
と充填物充填とを組み合せた構造とすることも可能であ
る。In the above embodiment, the case where the inner side of the tube is filled with the regular packing and the outer side of the tube is filled with the irregular packing is explained. However, in some cases, the types of the packing may be the same or may be reversed. Further, it is also possible to adopt a tray structure or a structure in which the tray and the filling of the packing are combined.
【００４１】本発明は、さらにその他の点においても上
記実施例に限定されるものではなく、単管の配設数（分
割数）、互に隣接する単管の間隔、連通管の形状、管内
と管外の断面積の比率などに関し、発明の要旨の範囲内
において、種々の応用、変形を加えることが可能であ
る。The present invention is not limited to the above-mentioned embodiment in other points as well, and the number of arranged single tubes (the number of divisions), the distance between adjacent single tubes, the shape of the communicating tube, the inside of the tube, and the like. With respect to the ratio of the cross-sectional area outside the tube and the like, various applications and modifications can be made within the scope of the invention.
【００４２】[0042]
【発明の効果】上述のように、本発明の内部熱交換型蒸
留塔は、単管をその軸方向に複数に分割形成し、互に隣
接する単管のうちの、一方の単管の管外を構成する領域
（一方の領域）と他方の単管の管外を構成する領域（他
方の領域）の間に、一方の領域と他方の領域を連通させ
る１以上の連通管を配設し、単管の管壁及び連通管の管
壁を、高圧側から低圧側への伝熱面としているので、必
要に応じて、連通管の管壁の面積（すなわち、連通管の
本数、径、長さなど）を調整することにより、全体とし
て必要な伝熱面積を確保することが可能になり、取り扱
う物質の物性や蒸留分離の精度に対応した、十分な省エ
ネルギー化を図ることが可能になる。According to the present invention as described above, the internal heat exchanging type distillation column of the present invention, a single pipe is divided form into a plurality in the axial direction, each other of the adjacent single tube, hand single tube Area outside the tube
(One region) and constituting the extravascular of the other single-duct region (other
(One region), one or more communication pipes for communicating one region and the other region are provided, and the pipe wall of the single pipe and the pipe wall of the communication pipe transfer heat from the high pressure side to the low pressure side. Since it is a surface, it is possible to secure the necessary heat transfer area as a whole by adjusting the area of the pipe wall of the communication pipe (that is, the number, diameter, length, etc. of the communication pipe) as necessary. Therefore, it is possible to achieve sufficient energy saving corresponding to the physical properties of substances to be handled and the accuracy of distillation separation.
【００４３】なお、管内を濃縮部、管外を回収部とし
て、管内を規則充填物充填あるいは無堰多孔板の棚段、
管外を不規則充填物充填あるいは無堰多孔板の棚段とす
ることにより、最も実用的な内部熱交換型蒸留塔を構成
することができる。The inside of the tube is used as a concentrating section and the outside of the tube is used as a recovery section, and the inside of the tube is filled with regular packings or trays without perforated plates.
The most practical internal heat exchange type distillation column can be constructed by filling the outside of the tube with irregular packing or as a tray of a perforated plate without a weir.
【図１】本発明の一実施例にかかる内部熱交換型蒸留塔
（を構成する構造体）を示す図であり、（ａ）は正面断
面図、（ｂ）は（ａ）のＩｂ−Ｉｂ線断面図である。FIG. 1 is a diagram showing (an internal heat-exchange type distillation column according to an embodiment of the present invention) (a structure constituting the same), (a) is a front sectional view, and (b) is Ib-Ib of (a). It is a line sectional view.
【図２】本発明の一実施例にかかかる内部熱交換型蒸留
塔を示す図である。FIG. 2 is a diagram showing an internal heat exchange type distillation column according to one embodiment of the present invention.
【図３】本発明の一実施例にかかる内部熱交換型蒸留塔
の運転状態の一例を示す図である。FIG. 3 is a diagram showing an example of an operating state of an internal heat exchange type distillation column according to an example of the present invention.
【図４】従来の蒸留塔の運転状態の一例を示す図であ
る。FIG. 4 is a diagram showing an example of operating conditions of a conventional distillation column.
１ 本体胴 ２ 単管 ４ 管内（濃縮部） ５ 管外（回収部）５ａ 管外を構成する一方の領域 ５ｂ 管外を構成する他方の領域 ６ 回収部液入口 ７ 回収部蒸気出口 ８ 濃縮部液入口 ９ 濃縮部蒸気出口 １０ 回収部蒸気入口 １１ 回収部液出口 １２ 濃縮部蒸気入口 １３ 濃縮部液出口 ２０ 連通管 ２２ａ 最上部の単管から延設された管 ２２ｂ 最下部の単管から延設された管 ２４ 圧縮機 ２８ 冷却機 Ｈ 各単管の高さ（長さ） ｈ 連通管の高さ（長さ）1 Main Body 2 Single Tube 4 Inside (Concentration Section) 5 Outside (Recovery Section) 5a One Area Outside the Tube 5b The Other Area Outside the Tube 6 Recovery Section Liquid Inlet 7 Recovery Section Vapor Outlet 8 Concentration Section Liquid inlet 9 Condensation part vapor outlet 10 Recovery part vapor inlet 11 Recovery part liquid outlet 12 Concentration part vapor inlet 13 Concentration part liquid outlet 20 Communication pipe 22a Pipe extended from the uppermost single pipe 22b Extending from the lowermost single pipe Installed pipe 24 Compressor 28 Cooler H Height of each single pipe (length) h Height of communicating pipe (length)
───────────────────────────────────────────────────── フロントページの続き (72)発明者 松尾 洋志 兵庫県尼崎市杭瀬寺島２丁目１番２号 木村化工機株式会社内 (72)発明者 野田 秀夫 兵庫県尼崎市南七松町２丁目９番７号 関西化学機械製作株式會社内 (72)発明者 松原 五作 東京都中央区八丁堀二丁目25番10号 丸 善石油化学株式会社内 (56)参考文献 実開 平２−95501（ＪＰ，Ｕ) Ｐｅｒｒｙ’ｓ Ｃｈｅｍｉｃａｌ Ｅｎｇｉｎｅｅｒｓ’ Ｈａｎｄｂｏｏ ｋ ｓｉｘｔｈ ｅｄｉｔｉｏｎ （1984） Ｓｅｃｔｉｏｎ 13 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Hiroshi Matsuo 2-1-2, Hirasejijima, Amagasaki City, Hyogo Prefecture Kimura Kakoki Co., Ltd. (72) Hideo Noda 2-9-7 Minaminanamatsucho, Amagasaki City, Hyogo Prefecture No. Kansai Chemical Machinery Co., Ltd. (72) Inventor Gosaku Matsubara 2-25-10 Hatchobori, Chuo-ku, Tokyo Maruzen Petrochemical Co., Ltd. (56) References Perry's Chemical Engineers' Handbook Sixth Edition (1984) Section 13
Claims (6)
内（単管の内側）と管外（単管の外側）が隔離された構
造とし、管内側と管外側の操作圧力に差をつけることに
より操作温度を異ならせ、高圧側から低圧側に熱移動さ
せることにより、高圧側を濃縮部、低圧側を回収部とし
て一つの蒸留塔を構成した内部熱交換型蒸留塔におい
て、 前記単管をその軸方向に複数に分割形成するとともに、 互に隣接する単管のうちの、一方の単管の管外を構成す
る領域（一方の領域）と他方の単管の管外を構成する領
域（他方の領域）の間に、前記一方の領域と他方の領域
を連通させる１以上の連通管を配設し、 前記単管の管壁及び前記連通管の管壁を、前記高圧側か
ら前記低圧側への伝熱面としたことを特徴とする内部熱
交換型蒸留塔。1. A structure in which a single pipe is inserted into the body barrel and the inside of the pipe (inside of the single pipe) and the outside of the pipe (outside of the single pipe) are isolated, and a difference in operating pressure between the inside and outside of the pipe is provided. with different operating temperatures by attaching, by heat transfer to the low pressure side from the high pressure side, enriching section a high-pressure side, the heat integrated distillation column which constitute one of the distillation column a low pressure side as the recovery unit, the single configured with split formed in a plurality of tubes in the axial direction, of the single tubes mutually adjacent, the region constituting the extravascular one-way single tube (one region) and extravascular the other monotube One or more communication pipes that connect the one region and the other region are provided between the regions (the other region), and the pipe wall of the single pipe and the pipe wall of the communication pipe are formed. An internal heat exchange type distillation column having a heat transfer surface from the high pressure side to the low pressure side.
特徴とする請求項１記載の内部熱交換型蒸留塔。2. The internal heat exchange type distillation column according to claim 1, wherein a packing is filled inside and outside the tube.
し、管外に不規則充填物を充填して回収部としたことを
特徴とする請求項１記載の内部熱交換型蒸留塔。3. The internal heat exchange type distillation column according to claim 1, wherein the tube is filled with an ordered packing to form a concentrating section, and the outside of the tube is packed to serve as a recovery section.
とする請求項１記載の内部熱交換型蒸留塔。4. The internal heat exchange type distillation column according to claim 1, wherein trays are provided inside and outside the pipe.
したことを特徴とする請求項１記載の内部熱交換型蒸留
塔。5. The internal heat exchange type distillation column according to claim 1, wherein a tray is provided inside the tube and a packing is filled outside the tube.
けたことを特徴とする請求項１記載の内部熱交換型蒸留
塔。6. The internal heat exchange type distillation column according to claim 1, wherein the tube is filled with a packing material, and a tray is provided outside the tube.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP30282994A JP2694427B2 (en) | 1994-11-11 | 1994-11-11 | Internal heat exchange type distillation column |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP30282994A JP2694427B2 (en) | 1994-11-11 | 1994-11-11 | Internal heat exchange type distillation column |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH08131704A JPH08131704A (en) | 1996-05-28 |
| JP2694427B2 true JP2694427B2 (en) | 1997-12-24 |
Family
ID=17913599
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP30282994A Expired - Fee Related JP2694427B2 (en) | 1994-11-11 | 1994-11-11 | Internal heat exchange type distillation column |
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| Country | Link |
|---|---|
| JP (1) | JP2694427B2 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1552870B1 (en) * | 2002-06-28 | 2012-08-15 | Kansai Chemical Engineering Co. Ltd | Internal heat exchange-type distillation column |
| JP4966655B2 (en) * | 2004-08-24 | 2012-07-04 | 関西化学機械製作株式会社 | Multi-structure internal heat exchange distillation column |
| JP6076579B2 (en) * | 2010-06-23 | 2017-02-08 | 株式会社ダイセル | Operation method of distillation tower |
| US8906141B2 (en) | 2012-08-09 | 2014-12-09 | Mitsubishi Heavy Industries, Ltd. | Carbon dioxide recovery apparatus and method |
-
1994
- 1994-11-11 JP JP30282994A patent/JP2694427B2/en not_active Expired - Fee Related
Non-Patent Citations (1)
| Title |
|---|
| Ｐｅｒｒｙ’ｓ Ｃｈｅｍｉｃａｌ Ｅｎｇｉｎｅｅｒｓ’ Ｈａｎｄｂｏｏｋ ｓｉｘｔｈ ｅｄｉｔｉｏｎ （１９８４） Ｓｅｃｔｉｏｎ １３ |
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| Publication number | Publication date |
|---|---|
| JPH08131704A (en) | 1996-05-28 |
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