JPH0545281B2 - - Google Patents
Info
- Publication number
- JPH0545281B2 JPH0545281B2 JP59169900A JP16990084A JPH0545281B2 JP H0545281 B2 JPH0545281 B2 JP H0545281B2 JP 59169900 A JP59169900 A JP 59169900A JP 16990084 A JP16990084 A JP 16990084A JP H0545281 B2 JPH0545281 B2 JP H0545281B2
- Authority
- JP
- Japan
- Prior art keywords
- heat
- distillation column
- distillation
- column
- heat pump
- 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 - Lifetime
Links
Classifications
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Description
【発明の詳細な説明】
〔発明の技術分野〕
本発明は蒸溜塔、特に精留塔における熱エネル
ギーをヒートポンプにより回収し、蒸溜熱源とし
て利用する方法に関する。DETAILED DESCRIPTION OF THE INVENTION [Technical Field of the Invention] The present invention relates to a method for recovering thermal energy in a distillation column, particularly in a rectification column, using a heat pump and utilizing it as a heat source for distillation.
従来、蒸溜塔における熱エネルギーをヒートポ
ンプを利用して回収するにあたつては、蒸溜塔塔
頂部において被蒸溜物が有する熱エネルギーを媒
体により回収し、この回収した熱エネルギーをヒ
ートポンプによつて蒸溜熱源として利用する方法
が提案されている。
Conventionally, when recovering thermal energy in a distillation column using a heat pump, the thermal energy possessed by the material to be distilled is recovered by a medium at the top of the distillation column, and this recovered thermal energy is used to perform distillation using a heat pump. A method of using it as a heat source has been proposed.
しかしながら、この方法は蒸溜塔塔頂と塔底の
温度差が大きく、例えば原油の常圧蒸溜塔の一例
によると、蒸溜塔に供給される原油温度は340℃
であるのに対して塔頂における溜出油温度に110
℃であり、塔頂と供給原油の温度差が230℃に達
し、即ち塔頂温度が低いので、ヒートポンプ駆動
動力が大きくなり、回収した熱量とポンプ駆動動
力との差が小さくなるので、エネルギー回収によ
り省エネルギー効果が期待できない欠点があつ
た。 However, in this method, there is a large temperature difference between the top and the bottom of the distillation column.For example, in an example of an atmospheric distillation column for crude oil, the temperature of the crude oil supplied to the distillation column is 340℃.
, whereas the distillate oil temperature at the top of the column is 110
℃, and the temperature difference between the top of the column and the supplied crude oil reaches 230℃, that is, the temperature at the top of the column is low, so the heat pump driving power increases, and the difference between the recovered heat and the pump driving power becomes small, so energy recovery is possible. Therefore, there was a drawback that no energy saving effect could be expected.
現在、ヒートポンプで可能な昇温巾は150℃程
度が限界と考えられる。 Currently, the temperature range that can be raised by heat pumps is thought to be limited to about 150°C.
本発明の目的は、上記従来の欠点を解消せんと
するものであり、蒸溜塔のサイドフラツクスから
熱エネルギーをヒートポンプにより回収して蒸溜
熱源として利用し、エネルギー回収効率を高める
ことにある。
An object of the present invention is to solve the above-mentioned conventional drawbacks, and to improve energy recovery efficiency by recovering thermal energy from the side flux of a distillation column using a heat pump and using it as a heat source for distillation.
上記目的を達成する本発明は、石油精製蒸溜塔
の中間段より蒸溜中の液の一部をとりだし冷却し
たのち蒸溜塔の次段に還流させるサイドリフラツ
クスにおいて、とりだし液をヒートポンプの蒸発
器に導き熱交換した後に還流させるとともに、蒸
発器より蒸発したヒートポンプの熱媒体蒸気を圧
縮機により圧縮し高圧蒸気をヒートポンプの凝縮
器に導き、高圧蒸気の凝縮時に発生する熱を蒸溜
塔の原料の予熱のため加熱炉前の最高温部の予熱
熱源として利用することを特徴とするものであ
る。
The present invention achieves the above-mentioned object by taking out a part of the liquid being distilled from an intermediate stage of a petroleum refining distillation tower, cooling it, and then refluxing it to the next stage of the distillation tower. At the same time, the heat medium vapor of the heat pump evaporated from the evaporator is compressed by the compressor, and the high-pressure vapor is guided to the condenser of the heat pump, and the heat generated when the high-pressure vapor is condensed is used to preheat the raw material of the distillation column. Therefore, it is characterized by being used as a preheating heat source for the hottest part in front of the heating furnace.
以下、本発明を図面に示した実施例にもとずき
説明する。 The present invention will be explained below based on embodiments shown in the drawings.
図は原油の常圧蒸溜に本発明を適用した場合を
例示し、精留塔１からサイドリフラツクス２が取
り出されている。 The figure illustrates a case where the present invention is applied to atmospheric distillation of crude oil, and a side reflux 2 is taken out from a rectification column 1.
サイドリフラツクス２の取り出し位置は限定さ
れるものではなく、精留塔１の塔頂リフラツクス
を除き、任意のサイドリフラツクスを利用するこ
とができる。 The extraction position of the side reflux 2 is not limited, and any side reflux can be used except for the top reflux of the rectification column 1.
図において、サイドリフラツクス２の取り出し
温度は185℃、取り出し量は137000Kg／hrである。 In the figure, the temperature at which the side reflux 2 is taken out is 185°C, and the amount taken out is 137,000 Kg/hr.
取り出されたサイドリフラツクス２は蒸発器３
に導かれ、蒸発器３中の熱媒体４（本実施例では
水）によつて、107×10Kcal／hrの熱量が回収さ
れた後に、サイドリフラツクス２の全量が塔側部
に戻される。熱媒体４はコンプレツサー５に供給
され、モーター６の駆動によつて、600℃、88気
圧に圧縮され、圧縮熱媒体は管路７を経て凝縮器
８に送られる。 The side reflux 2 taken out is sent to the evaporator 3.
After 107×10 Kcal/hr of heat is recovered by the heat medium 4 (water in this example) in the evaporator 3, the entire amount of the side reflux 2 is returned to the side of the column. The heat medium 4 is supplied to a compressor 5 and compressed to 600° C. and 88 atmospheres by driving a motor 6, and the compressed heat medium is sent to a condenser 8 via a pipe 7.
コンプレツサー５からの圧縮熱媒体の排出量は
3300Kg／hrである。 The amount of compressed heating medium discharged from compressor 5 is
It is 3300Kg/hr.
凝縮器８においては、圧縮熱媒体と、管路９に
より供給される、270℃に予備加熱された原油と
の熱交換が行われ、原油は298℃に加熱され、一
方、圧縮熱媒体は熱エネルギーを失つて300℃と
なる。 In the condenser 8, heat exchange is performed between the compressed heat medium and the crude oil preheated to 270°C, which is supplied through the pipe 9, and the crude oil is heated to 298°C. It loses energy and becomes 300℃.
凝縮器８に送られる原油量は、100000Kg／hrで
あり、凝縮器８における熱交換量は182×
104Kcal／hrである。 The amount of crude oil sent to condenser 8 is 100000Kg/hr, and the amount of heat exchange in condenser 8 is 182×
10 4 Kcal/hr.
凝縮器８で熱交換により加熱された原油は、管
路１０を経て加熱炉１１に送られ、340℃に加熱
されて精留塔１に供給される。 The crude oil heated by heat exchange in the condenser 8 is sent to a heating furnace 11 via a pipe 10, heated to 340° C., and supplied to the rectification column 1.
一方、凝縮器８において熱交換した後の圧縮熱
媒体は、減圧弁１２により減圧され、158℃、６
気圧の媒体として管路１３を経て再び蒸発器３に
循環される。 On the other hand, the compressed heat medium after heat exchange in the condenser 8 is reduced in pressure by the pressure reducing valve 12, and is heated to 158°C and 6°C.
It is circulated again to the evaporator 3 via the line 13 as an atmospheric medium.
なお、精留塔１の塔頂からは、110℃、1.35気
圧の塔頂溜分１４が取り出され、一方、塔底から
は320℃の残油が管路１５から50000Kg／hrで抜き
出される。 In addition, from the top of the rectification column 1, a top fraction 14 at 110°C and 1.35 atm is taken out, while from the bottom of the tower, residual oil at 320°C is taken out from pipe 15 at a rate of 50,000 kg/hr. .
このように、原油の常圧蒸溜に本発明を適用し
た場合、本発明における省エネルギー量は、凝縮
器８における放熱量―（モーター６の駆動エネル
ギー量）であるから、
182×104Kcal／hr−820Kw×860Kcal／hr／Kw
＝111.5×104Kcal／hrとなる。 As described above, when the present invention is applied to the atmospheric distillation of crude oil, the amount of energy saved in the present invention is the amount of heat dissipated in the condenser 8 - (the amount of driving energy of the motor 6), so 182 × 10 4 Kcal/hr −820Kw×860Kcal/hr/Kw
= 111.5×10 4 Kcal/hr.
一方、本発明によるヒートポンプを利用せず
に、原油を加熱炉１１のみで加熱する場合の所用
エネルギー量は、270℃の原油を340℃に加熱する
に要するエネルギーであるから、原油供給量×
（340−270）、即ち
100000×（340−270）×0.65＝455×104Kcal／hrと
なる。 On the other hand, the amount of energy required when crude oil is heated only in the heating furnace 11 without using the heat pump according to the present invention is the energy required to heat crude oil at 270°C to 340°C, so the amount of crude oil supplied ×
(340−270), that is, 100000×(340−270)×0.65=455×10 4 Kcal/hr.
従つて省エネルギー率は、 111.5／455＝0.245、即ち24.5％となる。 Therefore, the energy saving rate is 111.5/455=0.245, or 24.5%.
以上述べたように、本発明によれば蒸溜塔のサ
イドリフラツクスからヒートポンプによつて熱エ
ネルギーを回収し、この回収した熱エネルギーを
蒸溜熱源として利用する。塔頂部と塔底の温度差
が大きい場合にヒートポンプで連結すると熱エネ
ルギー回収効果は低下してしまう（塔頂100℃、
塔底350℃で成績係数は1.2程度となる）。これに
対して本発明のように、サイドリフラツクスをた
とえば185℃の段でとり、蒸溜熱源として利用す
ることにより、ヒートポンプ出力温度を、たとえ
ば300℃とすれば昇温巾115℃に低下させれば、成
績係数を増大（約2.6）させることができ、蒸溜
塔加熱に要する熱エネルギーを低減することがで
き、省エネルギー効率を高めることができる。
As described above, according to the present invention, thermal energy is recovered from the side reflux of a distillation column by a heat pump, and the recovered thermal energy is used as a distillation heat source. If the temperature difference between the top and the bottom of the tower is large, the thermal energy recovery effect will be reduced if the heat pump is used.
The coefficient of performance is approximately 1.2 at 350℃ at the bottom of the tower). On the other hand, as in the present invention, by taking side reflux at a stage of, for example, 185°C and using it as a distillation heat source, if the heat pump output temperature is set to, for example, 300°C, the temperature increase range can be reduced to 115°C. For example, the coefficient of performance can be increased (approximately 2.6), the thermal energy required to heat the distillation column can be reduced, and energy saving efficiency can be increased.
また、本発明は蒸溜塔からサイドリフラツクス
を取り出す位置にかかわらず適用することが可能
であり、利用範囲が極めて広範である。 Further, the present invention can be applied regardless of the location where the side reflux is taken out from the distillation column, and has an extremely wide range of applications.
更に本発明は、蒸溜塔の種類にかかわらず適用
することができ、特に塔頂と塔底との温度差が大
きい蒸溜塔に効果的に適用することができる。 Furthermore, the present invention can be applied regardless of the type of distillation column, and can be particularly effectively applied to a distillation column in which there is a large temperature difference between the top and the bottom of the column.
従つて本発明によれば、蒸溜塔内の熱エネルギ
ーをサイドリフラツクスにより回収するので塔頂
の排エネルギーを相対的に減少させることができ
る。 Therefore, according to the present invention, since the thermal energy within the distillation column is recovered by side reflux, the waste energy at the top of the column can be relatively reduced.
図は本発明の実施例を示す説明図である。
１…精留塔、２…サイドリフラツクス、３…蒸
発器、５…コンプレツサー、８…凝縮器。
The figure is an explanatory diagram showing an embodiment of the present invention. 1... Rectification column, 2... Side reflux, 3... Evaporator, 5... Compressor, 8... Condenser.
Claims (1)
とりだし冷却したのち蒸溜塔の次段に還流させる
サイドリフラツクスにおいて、とりだした液をヒ
ートポンプの蒸発器に導き熱交換した後に還流さ
せるとともに、蒸発器より蒸発したヒートポンプ
の熱媒体蒸気を圧縮機により圧縮し高圧蒸気をヒ
ートポンプの凝縮器に導き、凝縮高圧蒸気の時に
発生する熱を蒸溜塔の原料の予熱のため加熱炉前
の最高温部の予熱熱源として利用することを特徴
とする蒸溜塔における熱エネルギーの回収方法。1. In side reflux, a part of the distilled liquid is taken out from the intermediate stage of the petroleum refining distillation tower, cooled, and then refluxed to the next stage of the distillation tower. The heat medium vapor of the heat pump evaporated from the evaporator is compressed by the compressor, and the high-pressure vapor is guided to the condenser of the heat pump.The heat generated when the high-pressure vapor is condensed is used to preheat the raw material of the distillation column at the highest temperature part in front of the heating furnace. A method for recovering thermal energy in a distillation column, characterized in that it is used as a preheating heat source for a distillation column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59169900A JPS6150602A (en) | 1984-08-16 | 1984-08-16 | Recovery of heat energy in distillation tower |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59169900A JPS6150602A (en) | 1984-08-16 | 1984-08-16 | Recovery of heat energy in distillation tower |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6150602A JPS6150602A (en) | 1986-03-12 |
| JPH0545281B2 true JPH0545281B2 (en) | 1993-07-08 |
Family
ID=15895048
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP59169900A Granted JPS6150602A (en) | 1984-08-16 | 1984-08-16 | Recovery of heat energy in distillation tower |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6150602A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE112009004737B4 (en) * | 2009-05-01 | 2016-12-08 | Toyota Jidosha Kabushiki Kaisha | FUEL PROPERTY DETERMINATION UNIT |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7172686B1 (en) | 2002-11-14 | 2007-02-06 | The Board Of Regents Of The University Of Oklahoma | Method of increasing distillates yield in crude oil distillation |
| JP4604028B2 (en) * | 2003-07-04 | 2010-12-22 | イネオス フェノール ゲゼルシャフト ミット ベシュレンクテル ハフツング ウント コンパニー コマンディートゲゼルシャフト | Method for producing phenolic compound, method for separating phenol from cleavage product mixture, and apparatus |
| US7626060B2 (en) | 2003-07-11 | 2009-12-01 | INEOS Phenol GmbH & Co., KG | Process for the preparation of phenolic compounds, for separating phenol from cleavage product mixtures, and an apparatus |
| CN103017411B (en) * | 2012-11-28 | 2014-11-05 | 西安交通大学 | High temperature heat pump system for distillation |
| JP7551361B2 (en) * | 2020-06-30 | 2024-09-17 | 木村化工機株式会社 | Distillation Apparatus |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS588281A (en) * | 1981-07-07 | 1983-01-18 | Mitsubishi Electric Corp | Enclosed-type motor compressor |
| JPS5815161A (en) * | 1981-07-21 | 1983-01-28 | Nippon Denso Co Ltd | Connecting method of electric meter |
-
1984
- 1984-08-16 JP JP59169900A patent/JPS6150602A/en active Granted
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE112009004737B4 (en) * | 2009-05-01 | 2016-12-08 | Toyota Jidosha Kabushiki Kaisha | FUEL PROPERTY DETERMINATION UNIT |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6150602A (en) | 1986-03-12 |
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