CN102206504A - Equipment and method for separating reformed oil - Google Patents
Equipment and method for separating reformed oil Download PDFInfo
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- CN102206504A CN102206504A CN2011101386439A CN201110138643A CN102206504A CN 102206504 A CN102206504 A CN 102206504A CN 2011101386439 A CN2011101386439 A CN 2011101386439A CN 201110138643 A CN201110138643 A CN 201110138643A CN 102206504 A CN102206504 A CN 102206504A
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Abstract
The invention relates to equipment and a method for separating reformed oil. The method comprises the following steps of: separating three components, namely C5, C6-C7 and C8<+> in the reformed oil by using a bulkhead rectification column; adding the reformed oil prepared in a reforming device from a rectifying section of a feeding part and the middle part of a stripping section of the feeding part into the bulkhead rectification column; cooling the C5 component on the top of the column by using a condenser, and adding the cooled C5 component into a reflux tank, wherein a liquid phase at the bottom of the reflux tank is partially used as a C5 component product, and the rest liquid phase is used as back flow and flows back to a shared rectifying section on the upper part of the bulkhead rectification column; performing gas-phase side-line extraction on the C6-C7 component from a rectifying section of an extraction part of a side line product and the middle plate of a stripping section on the extraction part of the side line product; and performing condensation cooling and then feeding to an aromatics extraction device, wherein the C8<+> component is arranged at the bottom of the column. The feeding pressure is 0.5MPa (g), the operation pressure of the bulkhead rectification column is 0.4MPa (g), the energy consumption is low, the purity of the C6-C7 component can reach 99.7 percent, floor space is reduced by 40 percent, and the total investment on the equipment is saved by 20 percent.
Description
Technical field
The present invention relates to a kind of equipment and method of separating reformed oil, adopt the bulkhead rectifying tower to separate reformed oil, in single bulkhead rectifying tower, reformed oil is separated into C
5, C
6-C
7And C
8 +Three kinds of components.
Background technology
One of important device of catalytic reforming unit refinery, the reformed oil of its production is rich in aromatic hydrocarbons, has the octane value height, olefin(e) centent is low, substantially characteristics such as sulfur-bearing not can also can be used for producing aromatic hydrocarbon products such as benzene, toluene and dimethylbenzene directly as the high-octane rating blending component of motor spirit.Reformed oil mainly consists of C
5 +Distillation gasoline approximately contains more than 40 kind of detailed hydrocarbon component, when producing high-purity benzene, toluene and dimethylbenzene (being called for short B, T, X) product, reformed oil need be separated into different components.Because arene extracting process generally can only be handled narrow boiling point charging (C
6～C
7), and to C in the charging
5Components contents has restriction, otherwise C
5Can in circulation loop, accumulate and final polluted product.Therefore, reformed oil need be cut into C
5, C
6-C
7And C
8 +Component, C
6-C
7Produce benzene and toluene product, C through the aromatic hydrocarbons extracting
8 +Produce xylol through fractionation again.Traditional separation method is that two towers series connection is set, at first in depentanizer with C
5 -Component is in removed overhead, and oil enters and takes off C at the bottom of the depentanizer
7Tower, cat head cuts out C
6-C
7, be C at the bottom of the tower
8 +Component.This kind separation method long flow path, equipment is many, and energy consumption is big, and process cost is higher.Its technical process as shown in Figure 1.
Divided wall column (Dividing Wall Column is called for short DWC) is a kind of rectifying tower of complete thermal coupling, can realize three or more product separation in single tower.U.S. Pat 6927314B1 adopt divided wall column with full cut petroleum naphtha be divided into gently, neutralize weighs three kinds of cuts, lighting end and last running admission oil sump carry out blended gasoline, middle cut passes through behind the isomerization processing boosting of octane rating as gasoline blending component.U.S. Pat 7169267B2 adopts divided wall column with the separating of oil one-tenth lower boiling of cracking of ethylene, mid-boiling point and three kinds of cuts of high boiling point.Separate reformed oil with divided wall column, there is no report at home and abroad.
Summary of the invention
The purpose of this invention is to provide a kind of equipment and method of separating reformed oil.The raw material of handling is the stable reformed oil that catalytic reforming unit is produced.Adopt the bulkhead rectifying tower, make depentanize and take off C
7Operate in the tower and finish.Have flow process weak point, reduced investment, energy consumption is low, floor space is few characteristics.
Distillation operation of the present invention is to carry out in the bulkhead rectifying tower, and the bulkhead rectifying tower is the rectifying device that a kind of medium position at the conventional rectification tower is provided with a dividing plate, and central dividing plate is vertically installed, and prevents that the liquid and gas of both sides from taking place laterally to mix.The internal structure of bulkhead rectifying tower is divided into public rectifying section, charging rectifying section, charging stripping section, sideline product extraction rectifying section, sideline product extraction stripping section and public stripping section.The shared dividing plate in charging rectifying section and charging stripping section district is called charging prefractionation part at interval, rough segmentation is carried out in charging heated up in a steamer; The shared dividing plate of sideline product extraction rectifying section and sideline product extraction stripping section is called king-tower with public rectifying section, public stripping section at interval, carry out light, in the separating of heavy constituent.Top of tower is provided with condenser, is provided with reboiler at the bottom of the tower.
The mode that divided wall column sideline product of the present invention adopts gas phase to extract out is to improve product purity.
The present invention has the following advantages:
1. energy consumption is low
Divided wall column is the ideal system structure on thermodynamics, avoided between charging and feed tray the formation that mixes because of entropy that difference that component is formed causes, also avoided simultaneously the back-mixing effect of intermediate component, has higher separation efficiency, and the conventional two tower flow process gas phase total amounts of gas phase throughput ratio are little in the tower, for given material, finish same separation task, divided wall column is than littler reboiling heat amount and the condensation number of conventional two tower requirementss of process, and general facilities consumption reduces more than 25%.
2. middle component product purity height
Adopt the side line of rectifying tower to extract product out, be difficult to reach high purity.Charging and product extraction are separated after the employing divided wall column, have stoped the remix of separated portion, and sideline product adopts gas phase to extract out simultaneously, has reduced heavy constituent and has carried, and extraction product (C6-C7 component) purity can reach 99.7%.
3. flow process is short, takes up an area of few
The divided wall column flow process only adopts a tower, compares with traditional two tower serial flows, reduces 1 tower and attached auxiliary facility thereof, has simplified flow process, has saved the occupation of land usable floor area, and occupation of land can reduce about 40%.
4. reduced investment
The present invention compares with traditional two tower serial flows, adopts the divided wall column flow process, and major equipment quantity reduces half, and the divided wall column diameter is less than the tower diameter of diameter maximum in the two tower serial flows, so can reduce cost of investment significantly, the equipment gross investment can save about 20%.
Description of drawings
Fig. 1 divided wall column process flow diagram.
Wherein, 1, divided wall column, 2, condenser, 3, return tank, 4, reboiler, I, public rectifying section, the rectifying section of II, feeding part, the stripping section of III, feeding part, the rectifying section of IV, sideline product extraction part, the stripping section of V, sideline product extraction part, VI, public stripping section.
Embodiment
The method of separation reformed oil provided by the invention is so concrete enforcement:
The equipment that the method for separation reformed oil of the present invention adopts is divided wall column 1, be that medium position at the conventional rectification tower is provided with a vertical partition plate, tower be separated into from top to bottom the rectifying section II, the stripping section III of feeding part, the rectifying section IV of sideline product extraction part, stripping section V, six zones of public stripping section VI (as shown in Figure 1) of sideline product extraction part of public rectifying section I, feeding part.Public rectifying section I is positioned at the upper space of divided wall column 1 vertical partition plate, is the disengaging zone of light constituent; The rectifying section and the stripping section of the feeding part that is separated by dividing plate in the middle part of the rectifying section II of feeding part, the stripping section III of feeding part are respectively, the rectifying section II of feeding part, the stripping section III of feeding part are formed charging prefractionation part; The stripping section V of the rectifying section IV of sideline product extraction part, sideline product extraction part is respectively the rectifying section and the stripping section of sideline product extraction part; Public stripping section VI is positioned at the lower space of divided wall column 1 vertical partition plate; Forms king-tower by the rectifying section IV of public rectifying section I, sideline product extraction part, stripping section V, the public stripping section VI of sideline product extraction part, for gently, in and the disengaging zone of heavy constituent; Be provided with condenser 2 at top of tower, condenser 2 is connected with return tank 3; Be provided with reboiler 4 at the bottom of the tower.
The reformed oil that comes from reformer enters divided wall column 1, cat head C from the rectifying section II of feeding part, the stripping section III middle part of feeding part
5Component enters return tank 3 after condenser 2 coolings, 3 end of return tank, a liquid phase part was as C
5The component product, all the other return divided wall column 1 top common rectification section area I, C as backflow
6-C
7Component is carried out the extraction of gas phase side line from the rectifying section IV of sideline product extraction part, the stripping section V middle part of sideline product extraction part, delivers to aromatic extraction unit after the condensation cooling, is C at the bottom of the tower
8 +Component.Reboiler 4 adopts middle pressure steam as the heating thermal source.Feed pressure is 0.5MPa (g), and the divided wall column working pressure is 0.4MPa (g).
Adopt the divided wall column flow process to separate reformed oil.Processing condition are: treatment capacity is 2,000,000 tons/year, and the typical feedstock composition sees Table 1, and feed pressure is 0.5MPa (g), the bubble point charging.Separation requirement: C
5Component purity is 99% (mol), C
6-C
7Component purity is 99.7% (mol), C
8 +Component purity is 99% (mol).The divided wall column working pressure is 0.4MPa (g), needs 82 tower trays altogether.Technical process as shown in Figure 2, processing parameter sees Table 2.Adopting divided wall column to can save energy energy as can be seen from Table 2 is 26.1%.
Comparative Examples 1
Adopt two tower serial flows to separate reformed oil.Processing condition are: treatment capacity is 2,000,000 tons/year, and the typical feedstock composition sees Table 1, and feed pressure is 0.5MPa (g), the bubble point charging.Separation requirement: C
5 -Component purity is 99% (mol), C
6-C
7Component purity is 99.7% (mol), C
8 +Component purity is 99% (mol).The depentanizer working pressure is 0.6MPa (g), needs 40 tower trays altogether, takes off C
7The tower working pressure is 0.05MPa (g), needs 60 tower trays altogether.Technical process as shown in Figure 1, processing parameter sees Table 2.
Table 1 reformed oil is formed
| Component | mol％ |
| i-Butane | 0.0001 |
| n-Butane | 0.0081 |
| i-Pentane | 0.0341 |
| n-Pentane | 0.0220 |
| 2-Mpentane | 0.0905 |
| n-Hexane | 0.0407 |
| Benzene | 0.1462 |
| n-Heptane | 0.0186 |
| Toluene | 0.3124 |
| 2-Mheptane | 0.0009 |
| E-Benzene | 0.0481 |
| p-Xylene | 0.0508 |
| m-Xylene | 0.1079 |
| o-Xylene | 0.0672 |
| 124-MBenzene | 0.0456 |
| n-Pentyl-BZ | 0.0068 |
| Amount to | 1.0000 |
Table 2 divided wall column and two tower flow process parameter lists
Claims (2)
1. the separation method of a reformed oil is characterized in that: adopt the bulkhead rectifying tower, with the C in the reformed oil
5, C
6-C
7And C
8 +Three kinds of components are separated; The reformed oil that comes from reformer enters bulkhead rectifying tower, cat head C from the rectifying section of feeding part, the stripping section middle part of feeding part
5Component enters return tank after the condenser cooling, a liquid phase part is as C at the bottom of the return tank
5The component product, all the other return bulkhead rectifier common rectification section, C as backflow
6-C
7Component is carried out the extraction of gas phase side line from the rectifying section of sideline product extraction part, the stripping section middle part of sideline product extraction part, delivers to aromatic extraction unit after the condensation cooling, is C at the bottom of the tower
8 +Component; Feed pressure is 0.5MPa (g), and bulkhead rectifying tower working pressure is 0.4MPa (g).
2. the separating device of a reformed oil, it is characterized in that: the bulkhead rectifying tower (1) of employing, be that medium position at the conventional rectification tower is provided with a vertical partition plate, tower is separated into the rectifying section (II) of public rectifying section (I), feeding part, the stripping section (III) of feeding part, the rectifying section (IV) of sideline product extraction part, stripping section (V), six zones of public stripping section (VI) of sideline product extraction part from top to bottom; Public rectifying section is positioned at the upper space of divided wall column vertical partition plate, is the disengaging zone of light constituent; The rectifying section of feeding part, the stripping section of feeding part are positioned at the middle part, are the rectifying section of the feeding part that separated by dividing plate and the stripping section of feeding part, and the rectifying section of feeding part, the stripping section of feeding part are formed charging prefractionation part; The stripping section of the rectifying section of sideline product extraction part, sideline product extraction part is respectively the rectifying section of sideline product extraction part and the stripping section of sideline product extraction part; Public stripping section is positioned at the lower space of bulkhead rectifying tower vertical partition plate; Forms king-tower by the rectifying section of public rectifying section, sideline product extraction part, stripping section, the public stripping section of sideline product extraction part, for gently, in and the disengaging zone of heavy constituent; Be provided with condenser (2) at top of tower, condenser is connected with return tank (3), and return tank is connected with divided wall column top common rectification section; Be provided with reboiler (4) at the bottom of the tower.
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|---|---|---|---|
| CN2011101386439A CN102206504B (en) | 2011-05-26 | 2011-05-26 | Method for separating reformed oil |
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|---|---|---|---|
| CN2011101386439A CN102206504B (en) | 2011-05-26 | 2011-05-26 | Method for separating reformed oil |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107699278A (en) * | 2016-08-08 | 2018-02-16 | 中国石化工程建设有限公司 | A kind of product separation method of hydro carbons CONTINUOUS REFORMER |
| CN108239553A (en) * | 2016-12-23 | 2018-07-03 | 中国石油天然气集团公司 | A kind of reforming reaction product separation system and method |
| CN111484868A (en) * | 2019-08-22 | 2020-08-04 | 中国石油天然气集团有限公司 | Naphtha fraction device |
| CN112403013A (en) * | 2020-10-28 | 2021-02-26 | 洛阳金达石化有限责任公司 | Fine processing method of crude hexane |
| RU2809322C2 (en) * | 2019-05-15 | 2023-12-11 | Зульцер Менеджмент Аг | Hexane as by-product of isomerization plant using dividing wall column |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US10118878B2 (en) | 2016-09-20 | 2018-11-06 | Uop Llc | Process for increasing xylene isomer to benzene ratio |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1469765A (en) * | 2000-09-20 | 2004-01-21 | �����ɷ� | Method and device for carrying out the distillative separation of C5+ cuts |
| CN101348412A (en) * | 2007-07-18 | 2009-01-21 | 中国石油化工股份有限公司 | Energy-saving method for phenyl ethylene rectification |
-
2011
- 2011-05-26 CN CN2011101386439A patent/CN102206504B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1469765A (en) * | 2000-09-20 | 2004-01-21 | �����ɷ� | Method and device for carrying out the distillative separation of C5+ cuts |
| CN101348412A (en) * | 2007-07-18 | 2009-01-21 | 中国石油化工股份有限公司 | Energy-saving method for phenyl ethylene rectification |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107699278A (en) * | 2016-08-08 | 2018-02-16 | 中国石化工程建设有限公司 | A kind of product separation method of hydro carbons CONTINUOUS REFORMER |
| CN107699278B (en) * | 2016-08-08 | 2019-10-29 | 中国石化工程建设有限公司 | A kind of product separation method of hydro carbons CONTINUOUS REFORMER |
| CN108239553A (en) * | 2016-12-23 | 2018-07-03 | 中国石油天然气集团公司 | A kind of reforming reaction product separation system and method |
| CN108239553B (en) * | 2016-12-23 | 2020-06-09 | 中国石油天然气集团有限公司 | Reforming reaction product separation system and method |
| RU2809322C2 (en) * | 2019-05-15 | 2023-12-11 | Зульцер Менеджмент Аг | Hexane as by-product of isomerization plant using dividing wall column |
| CN111484868A (en) * | 2019-08-22 | 2020-08-04 | 中国石油天然气集团有限公司 | Naphtha fraction device |
| CN112403013A (en) * | 2020-10-28 | 2021-02-26 | 洛阳金达石化有限责任公司 | Fine processing method of crude hexane |
| CN112403013B (en) * | 2020-10-28 | 2023-01-10 | 洛阳金达石化有限责任公司 | Fine processing method of crude hexane |
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| CN102206504B (en) | 2013-12-04 |
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Owner name: CNPC EAST CHINA PROSPECTING DESIGN + RESEARCH INST Owner name: CHINA PETROLEUM +. NATURAL GAS CO., LTD. Free format text: FORMER OWNER: CNPC EAST CHINA PROSPECTING DESIGN + RESEARCH INSTITUTE Effective date: 20111021 |
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Inventor after: Shao Wen Inventor after: Liu Chuanqiang Inventor after: Zhao Xingwu Inventor after: Li Xiaona Inventor after: Zhu Daliang Inventor after: Gong Haifeng Inventor before: Shao Wen Inventor before: Liu Chuanqiang Inventor before: Zhao Xingwu Inventor before: Li Xiaona |
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Free format text: CORRECT: ADDRESS; FROM: 266071 QINGDAO, SHANDONG PROVINCE TO: 100007 DONGCHENG, BEIJING Free format text: CORRECT: INVENTOR; FROM: SHAO WEN LIU ZHUANQIANG ZHAO XINGWU LI XIAONUO TO: SHAO WEN LIU ZHUANQIANGZHAO XINGWU LI XIAONUO ZHU DALIANG GONG HAIFENG |
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Effective date of registration: 20111021 Address after: 100007 Dongcheng District, Dongzhimen, China, North Street, No. 9 Oil Mansion, No. Applicant after: China Petroleum & Natural Gas Co., Ltd. Co-applicant after: CNPC East China Prospecting Design & Research Institute Address before: 266071 Shandong province Qingdao City Hua Road No. 2 Applicant before: CNPC East China Prospecting Design & Research Institute |
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