CN203728776U - Naphtha and aromatization device for naphtha and liquefied gas - Google Patents
Naphtha and aromatization device for naphtha and liquefied gas Download PDFInfo
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- CN203728776U CN203728776U CN201420061185.2U CN201420061185U CN203728776U CN 203728776 U CN203728776 U CN 203728776U CN 201420061185 U CN201420061185 U CN 201420061185U CN 203728776 U CN203728776 U CN 203728776U
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Abstract
The utility model provides naphtha and an aromatization device for naphtha and liquefied gas. The aromatization device comprises a feed buffer tank and a reactor, wherein the feed buffer tank is connected with a heat exchanger A through a pipeline, a feed pump is arranged on the pipeline between the feed buffer tank and the heat exchanger A, a discharge port of the heat exchanger A is sequentially connected with a heat exchanger B and a reaction heating furnace, the discharge port of the reaction heating furnace is connected with a feed port at the tower top of the reactor through the pipeline, the discharge port of the heat exchanger A is further connected with the feed port of a tower kettle of the reactor through the pipeline, and the discharge port at the tower bottom of the reactor is sequentially connected with a heat exchanger C and a separation system through the pipeline. The aromatization device has the advantages of saving the equipment investment, saving the area occupied by equipment, simplifying the structure of the aromatization device, reducing the cooling at an outlet of the reactor and the heating before the separation system, greatly reducing the energy consumption and saving the cost; the production can be performed by only utilizing the heat exchangers to perform heat exchange, and the energy is fully utilized.
Description
Technical field
The utility model relates to the aromizing device of a kind of petroleum naphtha and petroleum naphtha and liquefied gas.
Background technology
Petroleum naphtha is a kind of light-end products, is cut corresponding cut and is obtained by crude distillation or oil secondary processing, can improve octane value by aromizing.Oil refinery liquefied gas is mainly derived from catalytic cracking and delayed coking unit, in liquefied gas, C3 and C4 olefin hydrocarbon molecules are on an acidic catalyst, react that by carbonium ion olefin hydrocarbon molecules is superimposed, generate macromole alkene, gained alkene can be reacted and be continued the larger olefin hydrocarbon molecules of superimposed generation by carbonium ion again, forms gasoline fraction, simultaneously under the effect of shape-selective molecular sieve, there is aromatization, generate aromatic hydrocarbons.
At present, petroleum naphtha, liquefied gas through aromatization device are that petroleum naphtha, liquefied gas are undertaken after aromatization by reactor, by interchanger heat exchange, carry out cooling through air cooling or water cooling plant again, then compress by gas compressor, finally by crossing heater heats, send into separation system and separate.This apparatus structure complexity, enters before gas compressor compresses and needs elder generation cooling in air cooling or water cooling plant, after compression, also needs through heater heats, and use equipment is many, and floor space is large, and energy expenditure is large, wastes energy.
Summary of the invention
The technical problems to be solved in the utility model is to provide petroleum naphtha that a kind of simple in structure, consuming little energy, floor space are little and the aromizing device of petroleum naphtha and liquefied gas.
Technical solution of the present utility model is:
The aromizing device of a kind of petroleum naphtha and petroleum naphtha and liquefied gas, there is charging surge tank and reactor, its special character is: described charging surge tank is connected by pipeline with interchanger A, pipeline between described charging surge tank and interchanger A is provided with fresh feed pump, the discharge port of described interchanger A is connected with interchanger B in turn, reaction heating furnace, the discharge port of described reaction heating furnace is connected with the tower top opening for feed of reactor by pipeline, the discharge port of described interchanger A is also connected by pipeline with the tower reactor opening for feed of reactor, at the bottom of the tower of described reactor discharge port successively with interchanger C, separation system is connected by pipeline.
Described separation system has stabilizer tower, the stabilizer tower return tank being connected by pipeline with the tower top discharge port of stabilizer tower, the absorption Analytic Tower being connected by pipeline with the pneumatic outlet of stabilizer tower return tank, the separation column being connected by pipeline with discharge port at the bottom of the tower of stabilizer tower; The opening for feed of described stabilizer tower is connected by pipeline with the discharge port of interchanger C, the liquid exit of described stabilizer tower return tank is connected by pipeline with the phegma entrance of stabilizer tower, pipeline between described stabilizer tower return tank and stabilizer tower is provided with stabilizer tower reflux pump, at the bottom of the tower of described absorption Analytic Tower, discharge port is connected by pipeline with the opening for feed of stabilizer tower, the tower top of described absorption Analytic Tower has dry gas outlet, and the tower top of described separation column has diesel oil outlet at the bottom of having fuel dispensing outlet, tower.
Described reactor is reactor A and reactor B parallel connection, with the aromatization that hockets.
In described reactor A, be provided with beds A, in described reactor B, be provided with beds B.
The pipeline at the tower reactor opening for feed place of described reactor A is provided with control valve a, and the pipeline at the tower top opening for feed place of reactor A is provided with control valve c, and at the bottom of the tower of reactor A, the pipeline at discharge port place is provided with control valve e.
The pipeline at the tower reactor opening for feed place of described reactor B is provided with control valve b, and the pipeline at the tower top opening for feed place of reactor B is provided with control valve d, and at the bottom of the tower of reactor B, the pipeline at discharge port place is provided with control valve f.
The beneficial effects of the utility model:
Fresh feed pump is set before reactor feed, directly by fresh feed pump, raw material is pressurizeed, without at reactor, water cooling plant and gas compressor being installed, before the separation system at rear portion, saved heating system.Aromizing device has been saved facility investment like this, save occupation area of equipment, simplify the structure of aromizing device, and reduce the heating before the cooling and separation system of reactor outlet, greatly reduce energy consumption cost-saving, only need utilize interchanger to carry out heat exchange just can produce, utilize fully energy, make the tooling cost of raw material reduce by 50 yuan/ton.
Brief description of the drawings
Fig. 1 is structural representation of the present utility model.
In figure: 1-charging surge tank, 2-fresh feed pump, 3-interchanger A, 4-interchanger B, 5-reaction heating furnace, 6-reactor, 601-reactor A, 6001-beds A, 602-reactor B, 6002-beds B, 7-interchanger C, I-separation system, 8-stabilizer tower, 9-stabilizer tower return tank, 10-stabilizer tower reflux pump, 11-separation column, 12-absorbs Analytic Tower.
Embodiment
As shown in the figure, the aromizing device of this petroleum naphtha and petroleum naphtha and liquefied gas, has charging surge tank 1 and reactor 6, and described reactor 6 is reactor A 601 and reactor B 602 parallel connections, with the aromatization that hockets, in described reactor A 601, be provided with beds A6001, in described reactor B 602, be provided with beds B6002, described charging surge tank 1 is connected by pipeline with interchanger A3, pipeline between described charging surge tank 1 and interchanger A3 is provided with fresh feed pump 2, the discharge port of described interchanger A3 is connected with interchanger B4 in turn, reaction heating furnace 5, the discharge port of described reaction heating furnace 5 by pipeline respectively with reactor A 601, the tower top opening for feed of reactor B 602 is connected, the discharge port of described interchanger A3 also respectively with reactor A 601, the tower reactor opening for feed of reactor B 602 is connected by pipeline, described reactor A 601, at the bottom of the tower of reactor B 602 discharge port respectively successively with interchanger C7, separation system I is connected by pipeline, the pipeline at the tower reactor opening for feed place of described reactor A 601 is provided with control valve a, the pipeline at the tower top opening for feed place of reactor A 601 is provided with control valve c, at the bottom of the tower of reactor A 601, the pipeline at discharge port place is provided with control valve e, the pipeline at the tower reactor opening for feed place of described reactor B 602 is provided with control valve b, and the pipeline at the tower top opening for feed place of reactor B 602 is provided with control valve d, and at the bottom of the tower of reactor B 602, the pipeline at discharge port place is provided with control valve f,
Described separation system I has stabilizer tower 8, the stabilizer tower return tank 9 being connected by pipeline with the tower top discharge port of stabilizer tower 8, the absorption Analytic Tower 12 being connected by pipeline with the pneumatic outlet of stabilizer tower return tank 9, the separation column 11 being connected by pipeline with discharge port at the bottom of the tower of stabilizer tower 8; The opening for feed of described stabilizer tower 8 is connected by pipeline with the discharge port of interchanger C7, the liquid exit of described stabilizer tower return tank 9 is connected by pipeline with the phegma entrance of stabilizer tower 8, pipeline between described stabilizer tower return tank 9 and stabilizer tower 8 is provided with stabilizer tower reflux pump 10, at the bottom of the tower of described absorption Analytic Tower 12, discharge port is connected by pipeline with the opening for feed of stabilizer tower 8, the tower top of described absorption Analytic Tower 12 has dry gas outlet, and the tower top of described separation column 11 has diesel oil outlet at the bottom of having fuel dispensing outlet, tower.
When production, control valve f at the bottom of control valve d on control valve b on the tower reactor opening for feed place pipeline of off-response device B602, the tower top opening for feed place pipeline of reactor B 602, the tower of reactor B 602 on discharge port place pipeline, open the control valve a on the tower reactor opening for feed place pipeline of reactor A 601, control valve c on the pipeline at reactor A 601 tower top opening for feed places, the control valve e at the bottom of reactor A 601 towers on the pipeline at discharge port place;
Petroleum naphtha and liquefied gas unstripped gas are delivered to charging surge tank 1, being forced into 0.8 Mpa～1.6Mpa (gauge pressure) by fresh feed pump 2 sends, after interchanger A3 heat exchange, be divided into two-way, the first via is after the further heat exchange of interchanger B4, be heated to required temperature of reaction (350 DEG C) through reaction heating furnace 5, send into reactor A 601 tower top throat-fed, the second tunnel in the mode of cold feed (being about 158 DEG C) in reactor A 601 tower reactor throat-fed, carry out aromatization through beds 6001, reaction product is gasoline, diesel oil, the mixture of poor alkene liquefied gas, simultaneously with a small amount of dry gas.Mixture by reactor A 601 towers at the bottom of discharge port deliver to interchanger C7, lower the temperature through interchanger C7, deliver to stabilizer tower 8, the overhead product of stabilizer tower 8 is poor alkene liquefied gas and a small amount of dry gas, entering stabilizer tower return tank 9 through the tower top discharge port of stabilizer tower 8 separates, the mixture of gasoline and diesel oil is delivered to separation column 11 by the bottom of stabilizer tower 8 and is separated, and the bottom product of separation column 11 is diesel oil, collects through diesel oil outlet; The overhead product of separation column 11 is gasoline, collects through fuel dispensing outlet; Dry gas in stabilizer tower return tank 9 is delivered to and is absorbed Analytic Tower 12 by the pneumatic outlet of stabilizer tower return tank 9, absorbs the interior institute of Analytic Tower 12 rich absorbent oil by the throat-fed that absorbs discharge port at the bottom of the tower of Analytic Tower 12 and deliver to stabilizer tower 8; The dry gas (C1 and C2 component) that absorbs the tower top of Analytic Tower 12 is collected through dry gas outlet.
Claims (6)
1. the aromizing device of a petroleum naphtha and petroleum naphtha and liquefied gas, there is charging surge tank and reactor, it is characterized in that: described charging surge tank is connected by pipeline with interchanger A, pipeline between described charging surge tank and interchanger A is provided with fresh feed pump, the discharge port of described interchanger A is connected with interchanger B in turn, reaction heating furnace, the discharge port of described reaction heating furnace is connected with the tower top opening for feed of reactor by pipeline, the discharge port of described interchanger A is also connected by pipeline with the tower reactor opening for feed of reactor, at the bottom of the tower of described reactor discharge port successively with interchanger C, separation system is connected by pipeline.
2. the aromizing device of petroleum naphtha according to claim 1 and petroleum naphtha and liquefied gas, it is characterized in that: described separation system has stabilizer tower, the stabilizer tower return tank being connected by pipeline with the tower top discharge port of stabilizer tower, the absorption Analytic Tower being connected by pipeline with the pneumatic outlet of stabilizer tower return tank, the separation column being connected by pipeline with discharge port at the bottom of the tower of stabilizer tower; The opening for feed of described stabilizer tower is connected by pipeline with the discharge port of interchanger C, the liquid exit of described stabilizer tower return tank is connected by pipeline with the phegma entrance of stabilizer tower, pipeline between described stabilizer tower return tank and stabilizer tower is provided with stabilizer tower reflux pump, at the bottom of the tower of described absorption Analytic Tower, discharge port is connected by pipeline with the opening for feed of stabilizer tower, the tower top of described absorption Analytic Tower has dry gas outlet, and the tower top of described separation column has diesel oil outlet at the bottom of having fuel dispensing outlet, tower.
3. the aromizing device of petroleum naphtha according to claim 1 and petroleum naphtha and liquefied gas, is characterized in that: described reactor is reactor A and reactor B parallel connection, with the aromatization that hockets.
4. the aromizing device of petroleum naphtha according to claim 1 and petroleum naphtha and liquefied gas, is characterized in that: in described reactor A, be provided with beds A, be provided with beds B in described reactor B.
5. the aromizing device of petroleum naphtha according to claim 1 and petroleum naphtha and liquefied gas, it is characterized in that: the pipeline at the tower reactor opening for feed place of described reactor A is provided with control valve a, the pipeline at the tower top opening for feed place of reactor A is provided with control valve c, and at the bottom of the tower of reactor A, the pipeline at discharge port place is provided with control valve e.
6. the aromizing device of petroleum naphtha according to claim 1 and petroleum naphtha and liquefied gas, it is characterized in that: the pipeline at the tower reactor opening for feed place of described reactor B is provided with control valve b, the pipeline at the tower top opening for feed place of reactor B is provided with control valve d, and at the bottom of the tower of reactor B, the pipeline at discharge port place is provided with control valve f.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420061185.2U CN203728776U (en) | 2014-02-11 | 2014-02-11 | Naphtha and aromatization device for naphtha and liquefied gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420061185.2U CN203728776U (en) | 2014-02-11 | 2014-02-11 | Naphtha and aromatization device for naphtha and liquefied gas |
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| CN203728776U true CN203728776U (en) | 2014-07-23 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201420061185.2U Expired - Fee Related CN203728776U (en) | 2014-02-11 | 2014-02-11 | Naphtha and aromatization device for naphtha and liquefied gas |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105861039A (en) * | 2015-01-23 | 2016-08-17 | 上海优华系统集成技术有限公司 | liquefied gas aromatization apparatus |
| CN106520190A (en) * | 2016-12-14 | 2017-03-22 | 四川中腾能源科技有限公司 | Light hydrocarbon production method |
| CN107523327A (en) * | 2017-09-15 | 2017-12-29 | 武汉凯顺石化科技有限公司 | The reuse means and method of C4 accessory substances obtained by a kind of gasoline production |
| CN109749774A (en) * | 2019-01-31 | 2019-05-14 | 东方傲立石化有限公司 | A kind of naphtha aromtization process |
-
2014
- 2014-02-11 CN CN201420061185.2U patent/CN203728776U/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105861039A (en) * | 2015-01-23 | 2016-08-17 | 上海优华系统集成技术有限公司 | liquefied gas aromatization apparatus |
| CN106520190A (en) * | 2016-12-14 | 2017-03-22 | 四川中腾能源科技有限公司 | Light hydrocarbon production method |
| CN107523327A (en) * | 2017-09-15 | 2017-12-29 | 武汉凯顺石化科技有限公司 | The reuse means and method of C4 accessory substances obtained by a kind of gasoline production |
| CN109749774A (en) * | 2019-01-31 | 2019-05-14 | 东方傲立石化有限公司 | A kind of naphtha aromtization process |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140723 Termination date: 20220211 |
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| CF01 | Termination of patent right due to non-payment of annual fee |