CN220502971U - System for separating stable gasoline by three components of partition tower - Google Patents
System for separating stable gasoline by three components of partition tower Download PDFInfo
- Publication number
- CN220502971U CN220502971U CN202322029293.3U CN202322029293U CN220502971U CN 220502971 U CN220502971 U CN 220502971U CN 202322029293 U CN202322029293 U CN 202322029293U CN 220502971 U CN220502971 U CN 220502971U
- Authority
- CN
- China
- Prior art keywords
- tower
- pipeline
- gasoline
- partition wall
- partition
- 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.)
- Active
Links
- 238000005192 partition Methods 0.000 title claims abstract description 41
- 230000003197 catalytic effect Effects 0.000 claims abstract description 14
- 238000010438 heat treatment Methods 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 3
- 238000005984 hydrogenation reaction Methods 0.000 description 13
- 238000000926 separation method Methods 0.000 description 8
- 238000004821 distillation Methods 0.000 description 5
- 238000009835 boiling Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000007795 chemical reaction product Substances 0.000 description 2
- 150000001993 dienes Chemical class 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000006266 etherification reaction Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model discloses a system for separating stable gasoline by three components of a partition wall tower, which comprises a feeding tank for conveying catalytic gasoline, and also comprises a partition wall tower, wherein the feeding tank is connected to the upper end of a preheating reactor through a pipeline, three upper parts, middle parts and lower parts which are formed by tower plates are arranged in the partition wall tower from top to bottom, the upper parts, the middle parts and the lower parts are arranged at intervals, a partition plate is vertically arranged in the middle part, the bottom of the preheating reactor is connected to the left side of the middle part of the partition wall tower through a ten-way pipeline, the upper part of the partition wall tower is connected with a first pipeline for conveying light gasoline, the right side of the middle part of the partition wall tower is connected with a second pipeline for conveying middle gasoline, and the bottom of the partition wall tower is connected with a third pipeline for conveying heavy gasoline.
Description
Technical Field
The utility model relates to a component separation system, in particular to a system for separating stable gasoline by three components of a partition tower, belonging to the field of petrochemical industry.
Background
The raw material of the gasoline hydrogenation device is the stable gasoline of the catalytic cracking device, and the upstream catalytic device carries out diene saturation through a gasoline hydrogenation pre-hydrogenation reactor after the final distillation point of the stable gasoline is reduced to 175 ℃, and then enters a gasoline fractionating tower to carry out light and heavy gasoline separation. The light gasoline is processed by the light gasoline etherification device, one part of the heavy gasoline is processed by the S-zorb device, and the other part of the heavy gasoline is processed by the naphtha hydrogenation device, so that the aim of reducing the yield of gasoline is fulfilled. However, the long-time reduction of the final distillation point of the stable gasoline by the catalytic device can cause the circulating salt at the top of the fractionating tower of the catalytic device, which affects the long-period stable operation of the catalytic device.
Disclosure of Invention
The utility model aims to realize the three-component separation of the stable gasoline without reducing the final distillation point of the stable gasoline, and can stably operate for a long period under the large background of realizing the yield reduction, realize the three-component separation of one tower, save the investment and reduce the operation energy consumption of the device.
In order to achieve the above purpose, the present utility model is realized by the following technical scheme:
the utility model provides an adopt three components of bulkhead tower to separate stable petrol system, includes the feed tank who carries catalytic gasoline, the feed tank passes through the pipe connection in the upper end of preheating the reactor, still includes the bulkhead tower, top-down be equipped with three upper portion, middle part, the lower part of constituteing by the column plate in the bulkhead tower, and upper portion, middle part, lower part interval arrangement, the vertical baffle that is equipped with in the middle part, the bottom of preheating the reactor is through ten pipeline connections in the left side at bulkhead tower middle part, the upper portion of bulkhead tower is connected with first pipeline in order to be used for carrying light petrol, the right side at bulkhead tower middle part is connected with No. two pipelines in order to be used for carrying middle petrol, the bottom of bulkhead tower is connected with No. three pipelines that are used for carrying heavy petrol.
Preferably, the top of the dividing wall tower is connected with a fourth pipeline, the fourth pipeline is connected with the inlet end of the tank body, the outlet end of the tank body is connected to the dividing wall tower through a fifth pipeline with a pump and is positioned between the upper part of the dividing wall tower and the top of the dividing wall tower, and the upper end of the tank body is connected with a sixth pipeline for discharging noncondensable gas.
Preferably, a circulating pipeline is connected to the dividing wall tower between the lower part of the dividing wall tower and the bottom of the dividing wall tower, and a heat exchanger is connected to the circulating pipeline.
Preferably, the heat exchanger is located in the heating furnace.
Preferably, a seventh pipeline with a pump is connected to the partition tower between the upper part and the middle part, the seventh pipeline is provided with a eighth pipeline and a ninth pipeline, and the eighth pipeline and the ninth pipeline are connected to the partition tower and are respectively positioned on the right side and the left side of the partition tower between the upper part and the middle part.
Preferably, a pump is connected between the feed tank and the pre-heating reactor.
Preferably, the third pipeline is connected with a pump.
The beneficial effects are that: the three-component separation of the stable gasoline (catalytic gasoline) can be realized without reducing the final distillation point of the stable gasoline, and the stable operation can be realized for a long period under the large background of realizing yield reduction; realizes the separation of three components by one tower, saves investment and reduces the operation energy consumption of the device.
Drawings
Fig. 1 is a schematic diagram of the overall structure of the present utility model.
Fig. 2 is a partial schematic view of the present utility model.
Detailed Description
The present utility model will be further described with reference to the accompanying drawings, but the present utility model is not limited to the following examples.
The system for separating the stable gasoline by adopting the three components of the partition wall tower comprises a feeding tank 1 for conveying the catalytic gasoline, wherein the feeding tank 1 is connected to the upper end of a preheating reactor 2 through a pipeline, the system further comprises the partition wall tower 3, three upper parts, middle parts and lower parts which are formed by tower plates are arranged in the partition wall tower 3 from top to bottom, the upper parts, the middle parts and the lower parts are arranged at intervals, a partition plate 4 is vertically arranged in the middle part, the bottom of the preheating reactor 2 is connected to the left side of the middle part of the partition wall tower 3 through a ten-way pipeline, the upper part of the partition wall tower 3 is connected with a first pipeline for conveying the light gasoline, the right side of the middle part of the partition wall tower 3 is connected with a second pipeline for conveying the middle gasoline, and the bottom of the partition wall tower 3 is connected with a third pipeline for conveying the heavy gasoline. And a pump is connected between the feeding tank 1 and the preheating reactor 2, and a third pipeline is connected with the pump, so that the conveying is accelerated through the pump.
1. Process flow
1. The catalytic gasoline enters a pre-hydrogenation reactor 2 (model R0101) after heat exchange and temperature rise;
2. heating the pre-hydrogenation reaction product, and then entering a dividing wall column 3;
3. the separation of light, medium and heavy components is realized by adopting a partition tower 3. The light petrol at the top of the partition tower 3 is continuously processed by a light petrol etherification device, the petrol in the middle part is pumped out and then is processed by a naphtha hydrogenation device or a aviation kerosene hydrogenation device, and the heavy petrol at the bottom of the partition tower is processed by an S-zorb device or a diesel hydrogenation device;
4. and the flow of medium gasoline and heavy gasoline is increased, so that the working condition is flexibly switched.
2. Description of the Process
1. After heat exchange and temperature rising, the stable gasoline raw material enters a pre-hydrogenation reactor 2, the pressure is controlled to be 2.4-2.6 MPa, the temperature is controlled to be 90-180 ℃, and the stable gasoline raw material enters the pre-hydrogenation reactor 2 for diene removal;
2. heating the pre-hydrogenation reaction product to 175 ℃ and then entering a dividing wall column 3;
3. the separation of light, medium and heavy components is realized by adopting a partition tower 3. The pressure at the top of the tower is controlled to be 0.68MPa, the bottom temperature is controlled to be 289 ℃, the final boiling point of the light gasoline is controlled to be less than or equal to 70 ℃, the initial boiling point of the medium gasoline is controlled to be more than or equal to 87 ℃, the final boiling point of the medium gasoline is controlled to be less than or equal to 175 ℃, and the initial boiling point of the medium gasoline is controlled to be more than or equal to 80 ℃.
4. The data of each stream of the divided wall column 3 are as follows: medium gasoline is pumped out by 147t/h, light gasoline is pumped out by 92t/h, and heavy gasoline is pumped out by 45.7t/h, so that the highest catalytic gasoline with 147t/h yield reduction can be achieved.
See the following table, wherein stream numbers are shown in fig. 2: stream number 101 is located on the tenth pipeline; stream number 102 is located on line number four; stream number 103 is on line six; stream number 104 is located on line five; stream number 105 is on line number one; stream number 106 is located on line number seven;
stream number 107 is located on line eight; stream number 108 is located on line nine; stream number 109 is on line number two; stream number 110 is located on line number three; stream number 111 is on the recycle line; stream number 112 is located on the circulation line.
Therefore, the technical scheme of the application not only realizes the purpose of reducing the yield of gasoline, but also does not need a catalytic device to reduce the final distillation point of stable gasoline, realizes long-period stable operation of the catalytic device, and improves the flexibility of the whole-plant processing flow.
The technical scheme is suitable for a catalytic gasoline hydrogenation device of 200 ten thousand tons per year for Zhejiang petrochemical industry, and after application, the method has great influence on oil reduction and increase of the whole plant, can greatly reduce the gasoline yield, and has wide application prospect.
In a preferred embodiment, the top of the dividing wall tower 3 is connected with a fourth pipeline, the fourth pipeline is connected with the inlet end of the tank 5, the outlet end of the tank 5 is connected to the dividing wall tower 3 through a fifth pipeline with a pump, the tank is positioned on the right side between the upper part of the dividing wall tower 3 and the top of the dividing wall tower 3, and the upper end of the tank 5 is connected with a sixth pipeline for discharging noncondensable gas.
In a preferred embodiment, a circulation pipeline is connected to the dividing wall tower 3 between the lower part of the dividing wall tower 3 and the bottom of the dividing wall tower 3, and the circulation pipeline is connected to a heat exchanger 6, and the heat exchanger 6 is positioned in the heating furnace 7.
In a preferred embodiment, a seventh pipeline with a pump is connected to the upper and middle partition tower 3, the seventh pipeline is connected to the right side of the partition tower 3, the seventh pipeline is provided with an eighth pipeline and a ninth pipeline, and the eighth pipeline and the ninth pipeline are connected to the partition tower 3 and are respectively positioned on the right side and the left side of the upper and middle partition tower 3.
Finally, it should be noted that the utility model is not limited to the above embodiments, but that many variants are possible. All modifications directly derived or suggested to one skilled in the art from the present disclosure should be considered as being within the scope of the present utility model.
Claims (7)
1. A system for separating stable gasoline by adopting three components of a partition tower is characterized in that: including carrying feeding jar (1) that has catalytic gasoline, feeding jar (1) is through the upper end of pipe connection in preheating reactor (2), still includes bulkhead tower (3), top-down be equipped with three upper portion, middle part, the lower part of constituteing by the column plate in bulkhead tower (3), and upper portion, middle part, lower part interval arrangement, the vertical baffle (4) that are equipped with in the middle part, the left side at bulkhead tower (3) middle part is connected through ten pipeline in the bottom of preheating reactor (2), the upper portion of bulkhead tower (3) is connected with a pipeline in order to be used for carrying light petrol, the right side at bulkhead tower (3) middle part is connected with No. two pipelines and is used for carrying middle gasoline, the bottom of bulkhead tower (3) is connected with No. three pipelines that are used for carrying heavy petrol.
2. A system for separating stabilized gasoline using a dividing wall column as defined in claim 1, wherein: the top of the partition wall tower (3) is connected with a fourth pipeline, the fourth pipeline is connected with the inlet end of the tank body (5), the outlet end of the tank body (5) is connected to the partition wall tower (3) through a fifth pipeline with a pump and is positioned between the upper portion of the partition wall tower (3) and the top of the partition wall tower (3), and the upper end of the tank body (5) is connected with a sixth pipeline for discharging noncondensable gas.
3. A system for separating stabilized gasoline using a dividing wall column as claimed in claim 1 or 2, wherein: the circulating pipeline is connected to the partition tower (3) between the lower part of the partition tower (3) and the bottom of the partition tower (3), and the heat exchanger (6) is connected to the circulating pipeline.
4. A system for separating stabilized gasoline using a dividing wall column as defined in claim 3, wherein: the heat exchanger (6) is positioned in the heating furnace (7).
5. A system for separating stabilized gasoline using a dividing wall column as defined in claim 1, wherein: the upper part, be connected with the pipeline No. seven with the pump on the middle part partition wall tower (3), no. seven pipelines divide to be equipped with No. eight pipelines and No. nine pipelines, no. eight pipelines and No. nine pipelines all connect on partition wall tower (3), and are located the right side and the left side of upper part, middle part partition wall tower (3) respectively.
6. A system for separating stabilized gasoline using a dividing wall column as defined in claim 1, wherein: a pump is connected between the feeding tank (1) and the preheating reactor (2).
7. A system for separating stabilized gasoline using a dividing wall column as defined in claim 1, wherein: and the third pipeline is connected with a pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322029293.3U CN220502971U (en) | 2023-07-31 | 2023-07-31 | System for separating stable gasoline by three components of partition tower |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322029293.3U CN220502971U (en) | 2023-07-31 | 2023-07-31 | System for separating stable gasoline by three components of partition tower |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220502971U true CN220502971U (en) | 2024-02-20 |
Family
ID=89871829
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322029293.3U Active CN220502971U (en) | 2023-07-31 | 2023-07-31 | System for separating stable gasoline by three components of partition tower |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220502971U (en) |
-
2023
- 2023-07-31 CN CN202322029293.3U patent/CN220502971U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN202898341U (en) | Heavy oil catalytic cracking subarea conversion device | |
| CN220502971U (en) | System for separating stable gasoline by three components of partition tower | |
| CN212051256U (en) | Fractionating system of gasoline and diesel hydrogenation device | |
| CN210560278U (en) | Hydrocracking and hydrodesulfurization integrated unit | |
| CN202808525U (en) | System for stilling ammonia by decompressing and adding alkali | |
| CN204676039U (en) | The deoxidation bio-oil hydrogenation unit that the cycle of operation is long | |
| CN201686667U (en) | Cracking gasoline full-fraction hydrogenation device | |
| CN213623926U (en) | Device for producing normal hexane and isohexane | |
| CN104845667A (en) | Deoxidization bio-oil hydrogenation device with long operation cycle | |
| CN216808706U (en) | Catalytic diesel oil hydrogenation modification system | |
| CN211199132U (en) | Liquid phase hydrogenation treatment device for cracked gasoline | |
| CN210595940U (en) | Heat conduction oil processing device | |
| CN221051802U (en) | Diesel oil separation device of wax oil hydrogenation system | |
| CN209872345U (en) | Hydrogen production low-temperature heat recycling system | |
| CN209854079U (en) | Optimization device of hydrocracking heat exchange technology | |
| CN106701160B (en) | The setting method of circulating pump in boiling bed hydrogenation device | |
| CN107267202B (en) | Method and device for stripping fractionation and negative pressure desorption of hydrogenated diesel refinery gas | |
| CN109135809A (en) | A kind of naphtha deaerating type of cycles and deoxidation method | |
| CN110511784B (en) | Hydrocracking fractionating tower tail oil heat utilization system and method | |
| CN105087065A (en) | Pyrolysis gasoline central fraction hydrogenation device and method thereof | |
| CN221192081U (en) | System for degree of depth improves vacuum tower side line product quality | |
| CN112403013B (en) | Fine processing method of crude hexane | |
| CN218130037U (en) | DMMn separation equipment | |
| CN214142208U (en) | Combined hydrogenation reactor and reactor system | |
| CN216192099U (en) | Heavy oil lightening hydrogenation reaction system with controllable reaction degree |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |