CN111484870A - Heat exchange method for fractionating tower - Google Patents
Heat exchange method for fractionating tower Download PDFInfo
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- CN111484870A CN111484870A CN201910085131.7A CN201910085131A CN111484870A CN 111484870 A CN111484870 A CN 111484870A CN 201910085131 A CN201910085131 A CN 201910085131A CN 111484870 A CN111484870 A CN 111484870A
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- fractionating tower
- reboiler
- bottom reboiler
- tower bottom
- oil
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/146—Multiple effect distillation
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
- C10G7/12—Controlling or regulating
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a heat exchange method of a fractionating tower. The first method is that the first fractionating tower bottom reboiler oil (8) from the first fractionating tower (1) is boosted by a reboiler pump (2) and then enters a second fractionating tower bottom reboiler (5) as a heat source, the second fractionating tower bottom reboiler exchanges heat and then enters a third fractionating tower bottom reboiler (7) as a heat source, the third fractionating tower bottom reboiler exchanges heat and then enters a reboiler (3) for reboiling, and the reboiled oil returns to the first fractionating tower (1). The second method is mainly different from the first method in that the reboiling oil at the bottom of the first fractionating tower from the first fractionating tower is boosted by a reboiling furnace pump and then divided into two paths, one path of the reboiling oil enters a reboiler at the bottom of the second fractionating tower to be used as a heat source, and the other path of the reboiling oil enters a reboiler at the bottom of the third fractionating tower to be used as a heat source. The invention is mainly used for heat exchange of the fractionating tower in devices such as diesel hydrocracking or diesel hydro-upgrading in petrochemical industry.
Description
Technical Field
The invention relates to a heat exchange method of a fractionating tower in petrochemical industry.
Background
The petroleum fraction is a multi-component hydrocarbon mixture mainly composed of alkane, alkene, cyclane, aromatic hydrocarbon and the like, and products obtained after separation comprise dry gas (mainly carbon 1 and carbon 2), liquefied gas (mainly carbon 3 and carbon 4), light naphtha (with the boiling point range of carbon 5-75 ℃), heavy naphtha (with the boiling point range of 75-175 ℃), kerosene (with the boiling point range of 175-230 ℃), diesel oil (with the boiling point range of 230-350 ℃), fuel oil (with the boiling point range of more than 350 ℃) and the like.
In the petrochemical industry, various fractionation systems are required to separate the petroleum fraction products, and the fractionation systems specifically include a stripping tower, a main fractionation tower, a diesel stripping tower, a aviation kerosene stripping tower, a naphtha fractionation tower, a deethanizer, a debutanizer, a light hydrocarbon absorption tower, and the like. In order to separate various fraction products, a large amount of heating heat needs to be provided for the fractionation system. In the prior art, a main fractionating tower generally adopts a heating furnace as a heat source and obtains heat through combustion of fuel gas; steam is generally used as a heat source in a aviation kerosene stripping tower, a naphtha fractionating tower, a deethanizer, a debutanizer and the like. For a diesel hydrocracking unit or a diesel upgrading unit, low or medium pressure steam is typically used as the heat source for the bottoms reboiler when the heat available in the unit for the hot process stream is depleted. However, when the fractionation system uses too much steam as the heat source for the bottom reboiler, it results in a high energy consumption of the fractionation system.
Disclosure of Invention
The invention aims to provide a heat exchange method of a fractionating tower, which aims to solve the problem that the energy consumption of a fractionating system is higher when steam is excessively used as a heat source of a tower bottom reboiler in the existing heat exchange method of the fractionating tower.
In order to solve the problems, the invention adopts the technical scheme that two fractionating tower heat exchange methods are used. The first heat exchange method for the fractionating tower is characterized by comprising the following steps: the method comprises the steps that reboiled oil at the bottom of a first fractionating tower from a first fractionating tower enters a second fractionating tower bottom reboiler of a second fractionating tower as a heat source after being boosted by a reboiling furnace pump, enters a third fractionating tower bottom reboiler of a third fractionating tower as a heat source after heat exchange in the second fractionating tower bottom reboiler, enters a reboiling furnace for reboiling after heat exchange in the third fractionating tower bottom reboiler, and returns to the first fractionating tower after reboiling in the reboiling furnace.
The second heat exchange method of the fractionating tower is characterized by comprising the following steps: the method comprises the steps that the reboiled oil at the bottom of a first fractionating tower from a first fractionating tower is boosted by a reboiling furnace pump and then divided into two paths, one path of the reboiled oil enters a reboiler at the bottom of a second fractionating tower to be used as a heat source, the reboiling furnace enters the reboiling furnace to reboil after heat exchange in the reboiler at the bottom of the second fractionating tower, the other path of the reboiling oil enters a reboiler at the bottom of a third fractionating tower to be used as a heat source, the reboiling furnace enters the reboiling furnace to reboil after heat exchange in the reboiler at the bottom of the third fractionating tower, and the reboiled oil at the bottom of the first fractionating tower returns to the first fractionating tower after reboiling.
The invention has the following beneficial effects: the reboiler at the bottom of the first fractionating tower is used as the heat source of the reboiler at the bottom of the second fractionating tower and the reboiler at the bottom of the third fractionating tower, and the two reboilers do not use steam any more
The present invention will be described in further detail with reference to the drawings, embodiments and examples. The drawings, detailed description, and examples do not limit the scope of the invention as claimed.
Drawings
FIG. 1 is a flow diagram of a first fractionation column heat exchange process of the present invention.
FIG. 2 is a flow diagram of a second fractionation column heat exchange process according to the present invention.
In fig. 1 and 2, the same reference numerals denote the same technical features.
Detailed Description
Referring to fig. 1, a first fractionation column heat exchange process of the present invention comprises the steps of: the first fractionating tower bottom reboiler 8 from the first fractionating tower 1 is boosted by the reboiler pump 2 and then enters the second fractionating tower bottom reboiler 5 of the second fractionating tower 4 as a heat source, the second fractionating tower bottom reboiler 5 exchanges heat and then enters the third fractionating tower bottom reboiler 7 of the third fractionating tower 6 as a heat source, the third fractionating tower bottom reboiler 7 exchanges heat and then enters the reboiler 3 for reboiling, and the reboiler 3 returns to the first fractionating tower 1.
Referring to fig. 2, a second fractionation column heat exchange process of the present invention comprises the steps of: the first fractionating tower bottom reboiler oil 8 from the first fractionating tower 1 is boosted by the reboiler pump 2 and then divided into two paths, one path enters the second fractionating tower bottom reboiler 5 of the second fractionating tower 4 to be used as a heat source, and enters the reboiler 3 after heat exchange in the second fractionating tower bottom reboiler 5 to be reboiled. The other path of the heat exchange liquid enters a third fractionating tower bottom reboiler 7 of the third fractionating tower 6 to be used as a heat source, and the heat exchange liquid enters the reboiling furnace 3 to be reboiled after exchanging heat in the third fractionating tower bottom reboiler 7. The reboiled first fractionator bottom reboiled oil 8 in the reboiling furnace 3 is returned to the first fractionator 1.
The bottom oil in the first fractionator 1 is divided into two parts after flowing out from the bottom of the first fractionator 1, one part is used as a first fractionator reaction product 9, and the other part is used as a first fractionator bottom reboiled oil 8. In the second fractionating tower bottom reboiler 5 and the third fractionating tower bottom reboiler 7, the first fractionating tower bottom reboiler 8 exchanges heat with the second fractionating tower bottom reboiler and the third fractionating tower bottom reboiler respectively, and the second fractionating tower bottom reboiler and the third fractionating tower bottom reboiler after heat exchange return to the second fractionating tower 4 and the third fractionating tower 6 respectively. The difference between the flow shown in fig. 1 and the flow shown in fig. 2 is that in the flow shown in fig. 1, the first fractionating tower bottom reboiler oil 8 after the pressure of the reboiler pump 2 is raised enters the second fractionating tower bottom reboiler 5, flows out from the second fractionating tower bottom reboiler 5, enters the third fractionating tower bottom reboiler 7, flows out from the third fractionating tower bottom reboiler 7, and enters the reboiler 3. In the flow shown in fig. 2, the first fractionating tower bottom reboiler 8 after the pressure of the reboiling furnace pump 2 is raised simultaneously enters the second fractionating tower bottom reboiler 5 and the third fractionating tower bottom reboiler 7, and simultaneously flows out of the two bottom reboilers and enters the reboiling furnace 3.
The temperature of the first fractionator bottom reboiled oil 8 flowing out from the first fractionator 1 is generally 170 to 350 ℃. The temperature of the first fractionating tower bottom reboiler 8 entering the second fractionating tower bottom reboiler 5 is generally reduced by 40-100 ℃ after heat exchange in the second fractionating tower bottom reboiler 5, and the temperature of the first fractionating tower bottom reboiler 8 entering the third fractionating tower bottom reboiler 7 is generally reduced by 40-100 ℃ after heat exchange in the third fractionating tower bottom reboiler 7.
The temperature of the first fractionation tower bottom reboiler oil flowing out from the bottom of the first fractionation tower 1 is higher than the temperature of the second fractionation tower bottom reboiler oil flowing out from the bottom of the second fractionation tower 4 and the temperature of the third fractionation tower bottom reboiler oil flowing out from the bottom of the third fractionation tower 6. The first fractionation column heat exchange method of the present invention (shown in fig. 1) is considered to be used when the temperature of the second fractionation column bottom reboiler oil flowing from the bottom of the second fractionation column 4 is higher than the temperature of the third fractionation column bottom reboiler oil flowing from the bottom of the third fractionation column 6 by 20 ℃ or more, otherwise the second fractionation column heat exchange method of the present invention (shown in fig. 2) is used.
The invention is mainly used for heat exchange of the fractionating tower in devices such as diesel hydrocracking or diesel hydro-upgrading in petrochemical industry. The application is not limited by the heat load of the tower bottom reboiler, and is particularly suitable for the occasions with large heat load of the tower bottom reboiler (the single heat load is more than five megawatts). The first fractionating tower 1 is a main fractionating tower, the second fractionating tower 4 is a naphtha fractionating tower, a aviation kerosene stripping tower or a debutanizer, and the third fractionating tower 6 is a naphtha fractionating tower, a debutanizer or a deethanizer.
For example, ① the invention is used in a diesel hydrocracking unit to produce only light and heavy naphtha products, a first fractionator 1 is a main fractionator, a second fractionator 4 is a naphtha fractionator, a third fractionator 6 is a debutanizer, ② the invention is used in a diesel hydrocracking unit to produce light and heavy naphtha products and also to produce aviation kerosene products, a first fractionator 1 is a main fractionator, a second fractionator 4 is a aviation kerosene stripper, a third fractionator 6 is a naphtha fractionator, ③ the invention is used in a diesel hydro-upgrading unit to produce upgraded diesel and also to produce aviation kerosene products, a first fractionator 1 is a main fractionator, a second fractionator 4 is a aviation kerosene stripper, and a third fractionator 6 is a debutanizer.
The reboiling furnace 3 is generally a cylindrical furnace, a vertical furnace or a box furnace. In the flow shown in fig. 1, the reboiled oil 8 at the bottom of the first fractionating tower enters the reboiling furnace 3 after heat exchange in the reboiler 7 at the bottom of the third fractionating tower, and sequentially passes through the convection section and the radiation section of the reboiling furnace 3. In the flow shown in fig. 2, the reboiled oil 8 at the bottom of the first fractionating tower, which has undergone heat exchange in the reboiler 5 at the bottom of the second fractionating tower and the reboiler 7 at the bottom of the third fractionating tower, enters the reboiling furnace 3 and sequentially passes through the convection section and the radiation section of the reboiling furnace 3.
The second fractionating tower bottom reboiler 5 and the third fractionating tower bottom reboiler 7 are generally a kettle-type reboiler, a horizontal thermosiphon-type reboiler or a vertical thermosiphon-type reboiler, and the horizontal thermosiphon-type reboiler or the vertical thermosiphon-type reboiler is a once-through type or a forced circulation type. The first fractionator bottom reboiler 8 entering the second fractionator bottom reboiler 5 and the third fractionator bottom reboiler 7 may be taken from the shell side or the tube side of the two bottom reboilers, respectively.
In fig. 1 and 2, the connections between the first fractionating tower 1, the second fractionating tower 4, the third fractionating tower 6, the reboiling furnace pump 2, the reboiling furnace 3, the second fractionating tower bottom reboiler 5, and the third fractionating tower bottom reboiler 7 are connected by pipes, and the detailed description thereof will be omitted.
Examples
In a certain diesel oil hydrocracking device, the feed is the mixed feed of straight-run diesel oil, catalytic diesel oil and suspension bed diesel oil, and only light and heavy naphtha products are produced. After the hydrocracking reaction, the hydrogenation product firstly enters a stripping tower to remove hydrogen sulfide and partial light hydrocarbon, and then enters a fractionating system to fractionate, and the heat exchange of the fractionating tower adopts the flow shown in the figure 2. Naphtha and diesel oil are separated in a first fractionator 1 (main fractionator), light and heavy naphtha separation is performed in a second fractionator 4 (naphtha fractionator), and naphtha stabilization is performed in a third fractionator 6 (debutanizer).
The heat load, fuel gas consumption and steam consumption of the process using the present invention as shown in FIG. 2 and the conventional steam heating process are compared in Table 1, and the specific energy consumption is compared in Table 2. The conventional steam heating scheme differs from the scheme of the present invention shown in fig. 2 in that the second fractionator bottom reboiler uses medium pressure steam (3.5MPaG) as a heat source and the third fractionator bottom reboiler uses low pressure steam (1.0MPaG) as a heat source.
From the data in tables 1 and 2, it can be seen that the specific energy consumption can be reduced by 6.12 kg of standard oil per ton of feedstock with the same separation task using the process of the invention as shown in figure 2 compared to the process using conventional steam heating.
TABLE 1
TABLE 2
Claims (10)
1. A heat exchange method for a fractionating tower is characterized by comprising the following steps: the method comprises the steps that reboiled oil (8) at the bottom of a first fractionating tower from a first fractionating tower (1) enters a second fractionating tower bottom reboiler (5) of a second fractionating tower (4) as a heat source after being boosted by a reboiling furnace pump (2), enters a third fractionating tower bottom reboiler (7) of a third fractionating tower (6) as the heat source after heat exchange in the second fractionating tower bottom reboiler (5), enters a reboiling furnace (3) for reboiling after heat exchange in the third fractionating tower bottom reboiler (7), and returns to the first fractionating tower (1) after reboiling in the reboiling furnace (3).
2. The method of claim 1, wherein: the temperature of the first fractionating tower bottom reboiler oil (8) flowing out of the first fractionating tower (1) is 170-350 ℃, the temperature of the first fractionating tower bottom reboiler oil (8) is reduced by 40-100 ℃ after heat exchange in the second fractionating tower bottom reboiler (5), and the temperature of the first fractionating tower bottom reboiler oil (8) is reduced by 40-100 ℃ after heat exchange in the third fractionating tower bottom reboiler (7).
3. The method according to claim 1 or 2, characterized in that: the method is used for a diesel hydrocracking device or a diesel hydro-upgrading device, the first fractionating tower (1) is a main fractionating tower, the second fractionating tower (4) is a naphtha fractionating tower, a aviation kerosene stripping tower or a debutanizer, and the third fractionating tower (6) is a naphtha fractionating tower, a debutanizer or a deethanizer.
4. The method of claim 3, wherein: the reboiling furnace (3) is a cylinder furnace, a vertical furnace or a box furnace, and reboiling oil (8) at the bottom of the first fractionating tower enters the reboiling furnace (3) after heat exchange in a reboiler (7) at the bottom of the third fractionating tower and sequentially passes through a convection section and a radiation section of the reboiling furnace (3).
5. The method of claim 4, wherein: the second fractionating tower bottom reboiler (5) and the third fractionating tower bottom reboiler (7) are kettle type reboilers, horizontal thermosiphon type reboilers or vertical thermosiphon type reboilers, the horizontal thermosiphon type reboilers or vertical thermosiphon type reboilers are in once-through type or forced circulation type, and the first fractionating tower bottom reboilers (8) entering the second fractionating tower bottom reboiler (5) and the third fractionating tower bottom reboiler (7) can respectively go through the shell pass or the tube pass of the two tower bottom reboilers.
6. A heat exchange method for a fractionating tower is characterized by comprising the following steps: the method comprises the steps that the first fractionating tower bottom reboiler oil (8) from a first fractionating tower (1) is boosted by a reboiler pump (2) and then divided into two paths, one path of the first fractionating tower bottom reboiler oil enters a second fractionating tower bottom reboiler (5) of a second fractionating tower (4) to be used as a heat source, the second fractionating tower bottom reboiler oil (5) exchanges heat and then enters a reboiler furnace (3) to be reboiled, the other path of the first fractionating tower bottom reboiler oil enters a third fractionating tower bottom reboiler (7) of a third fractionating tower (6) to be used as a heat source, the third fractionating tower bottom reboiler oil (7) exchanges heat and then enters the reboiler furnace (3) to be reboiled, and the reboiled first fractionating tower bottom reboiler oil (8) returns to the first fractionating tower (1).
7. The method of claim 6, wherein: the temperature of the first fractionating tower bottom reboiler oil (8) flowing out of the first fractionating tower (1) is 170-350 ℃, the temperature of the first fractionating tower bottom reboiler oil (8) is reduced by 40-100 ℃ after heat exchange in the second fractionating tower bottom reboiler (5), and the temperature of the first fractionating tower bottom reboiler oil (8) is reduced by 40-100 ℃ after heat exchange in the third fractionating tower bottom reboiler (7).
8. The method according to claim 6 or 7, characterized in that: the method is used for a diesel hydrocracking device or a diesel hydro-upgrading device, the first fractionating tower (1) is a main fractionating tower, the second fractionating tower (4) is a naphtha fractionating tower, a aviation kerosene stripping tower or a debutanizer, and the third fractionating tower (6) is a naphtha fractionating tower, a debutanizer or a deethanizer.
9. The method of claim 8, wherein: the reboiling furnace (3) is a cylinder furnace, a vertical furnace or a box furnace, reboiling oil (8) at the bottom of the first fractionating tower enters the reboiling furnace (3) after heat exchange in a reboiler (5) at the bottom of the second fractionating tower and a reboiler (7) at the bottom of the third fractionating tower, and sequentially passes through a convection section and a radiation section of the reboiling furnace (3).
10. The method of claim 9, wherein: the second fractionating tower bottom reboiler (5) and the third fractionating tower bottom reboiler 7 are a kettle type reboiler, a horizontal thermosiphon type reboiler or a vertical thermosiphon type reboiler. The horizontal type thermosyphon reboiler or the vertical type thermosyphon reboiler is a once-through type or a forced circulation type, and the first fractionating tower bottom reboiler (8) entering the second fractionating tower bottom reboiler (5) and the third fractionating tower bottom reboiler (7) can respectively leave the shell pass or the tube pass of the two tower bottom reboilers.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1160748A (en) * | 1996-03-21 | 1997-10-01 | 中国石油化工总公司石油化工科学研究院 | Separation method of catalytically converted hydrocarbon product |
| CN105214329A (en) * | 2015-09-06 | 2016-01-06 | 上海优华系统集成技术股份有限公司 | Distillation system and rectification process |
| CN105617706A (en) * | 2016-03-02 | 2016-06-01 | 上海优华系统集成技术股份有限公司 | Waste heat recovery technology for chemical engineering device and chemical engineering device |
| CN106715370A (en) * | 2014-09-04 | 2017-05-24 | 环球油品公司 | Heat recovery from a naphtha fractionation column |
| CN106987264A (en) * | 2017-05-25 | 2017-07-28 | 北京石油化工工程有限公司 | A kind of condensation oil separating device and process |
| WO2018226056A1 (en) * | 2017-06-08 | 2018-12-13 | 주식회사 엘지화학 | Distillation device and distillation method |
-
2019
- 2019-01-29 CN CN201910085131.7A patent/CN111484870A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1160748A (en) * | 1996-03-21 | 1997-10-01 | 中国石油化工总公司石油化工科学研究院 | Separation method of catalytically converted hydrocarbon product |
| CN106715370A (en) * | 2014-09-04 | 2017-05-24 | 环球油品公司 | Heat recovery from a naphtha fractionation column |
| CN105214329A (en) * | 2015-09-06 | 2016-01-06 | 上海优华系统集成技术股份有限公司 | Distillation system and rectification process |
| CN105617706A (en) * | 2016-03-02 | 2016-06-01 | 上海优华系统集成技术股份有限公司 | Waste heat recovery technology for chemical engineering device and chemical engineering device |
| CN106987264A (en) * | 2017-05-25 | 2017-07-28 | 北京石油化工工程有限公司 | A kind of condensation oil separating device and process |
| WO2018226056A1 (en) * | 2017-06-08 | 2018-12-13 | 주식회사 엘지화학 | Distillation device and distillation method |
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Application publication date: 20200804 |