CN211471311U - Fine fractionation device for hydrogenation process - Google Patents
Fine fractionation device for hydrogenation process Download PDFInfo
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- CN211471311U CN211471311U CN201922372144.0U CN201922372144U CN211471311U CN 211471311 U CN211471311 U CN 211471311U CN 201922372144 U CN201922372144 U CN 201922372144U CN 211471311 U CN211471311 U CN 211471311U
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Abstract
The utility model discloses a fine fractionation device for hydrogenation process, which comprises a primary fractionation unit, a secondary fractionation unit, a heating furnace and a heat exchanger; the primary fractionation unit comprises a first fractionation tower and reflux established at the top of the first fractionation tower; the secondary fractionation unit comprises a second fractionation tower and reflux established at the top of the second fractionation tower; the cold medium inlet of the heat exchanger is communicated with a raw material pipeline, the cold medium outlet of the heat exchanger is communicated with the feed inlet of the first fractionating tower, the discharge outlet of the first fractionating tower is communicated with the inlet of the heating furnace, the outlet of the heating furnace is communicated with the discharge outlet of the second fractionating tower, the discharge outlet of the second fractionating tower is communicated with the hot medium inlet of the heat exchanger, and the hot medium outlet of the heat exchanger is communicated with a diesel oil pipeline. The utility model discloses rational utilization essential diesel's waste heat carries out the heat transfer as the heat medium to the low minute oil of once fractionating to reduce the quantity of steam in once fractionating, greatly reduced manufacturing cost, the naphtha and the essential diesel quality that obtain through twice fractionation simultaneously are higher.
Description
Technical Field
The utility model relates to a chemical industry equipment technical field, concretely relates to meticulous fractionation device for hydrogenation technology.
Background
With the increase of the national emission standard, the quality requirement of the diesel oil is correspondingly increased, which makes the refining process of the diesel oil become the key point of the improvement of each refining enterprise.
At present, the problems of low product yield and poor product quality of diesel oil and naphtha produced by a hydrogenation fractionation process are difficult to overcome, particularly the diesel oil is difficult to meet the national standard, and naphtha and diesel oil products which do not meet the national standard are usually mixed into raw materials for carrying out new hydrogenation fractionation treatment, so that the productivity is reduced, and the production cost is greatly increased.
Disclosure of Invention
The utility model aims at providing a meticulous fractionation device for hydrogenation process to the defect that prior art exists, it has rational in infrastructure, production input cost is low and the characteristics of product percent of pass height.
The technical scheme of the utility model is that:
a fine fractionation device for a hydrogenation process comprises a primary fractionation unit, a secondary fractionation unit, a heating furnace and a heat exchanger;
the primary fractionation unit comprises a first fractionation tower, a first cooler and a first reflux tank, wherein the first fractionation tower is provided with a first stripping inlet, a first feeding hole, a first discharging hole, a first reflux outlet and a first reflux inlet, the first reflux outlet passes through the first cooler and the first reflux tank through pipelines and then establishes reflux with the first reflux inlet, and the first reflux tank is provided with a low-fraction gas outlet;
the secondary fractionation unit comprises a second fractionation tower, a second cooler and a second reflux tank, a second stripping inlet, a second feeding hole, a second discharging hole, a second reflux outlet and a second reflux inlet are arranged on the second fractionation tower, the second reflux outlet passes through the second cooler and the second reflux tank through a pipeline and then establishes reflux with the second reflux inlet, a low-fraction gas outlet is arranged on the second reflux tank, and a naphtha branch is arranged on the pipeline part between the second reflux tank and the second fractionation tower;
the cold medium inlet of the heat exchanger is communicated with the raw material pipeline, the cold medium outlet of the heat exchanger is connected with the first feed inlet pipeline, the first discharge outlet is connected with the inlet pipeline of the heating furnace, the outlet of the heating furnace is connected with the second feed inlet pipeline, the second discharge outlet is connected with the hot medium inlet pipeline of the heat exchanger, and the hot medium outlet of the heat exchanger is communicated with the diesel oil pipeline.
Preferably, the first cooler and the second cooler are both water coolers.
Preferably, a first power pump is further arranged on the pipeline part between the first reflux tank and the first fractionating tower, and a second power pump is further arranged on the pipeline part between the second reflux tank and the second fractionating tower.
Preferably, a third power pump is arranged on a pipeline between the first discharge hole and the heating furnace.
Preferably, a fourth power pump is arranged on a pipeline between the second discharge hole and the heat exchanger.
Compared with the prior art, the utility model, have following advantage:
the utility model utilizes the refined diesel oil after the secondary fractionation as the heat medium to heat the low oil-separating raw material in the primary fractionation, thereby not only reasonably utilizing the waste heat of the refined diesel oil, but also reducing the using amount of steam stripping used in the primary fractionation to the minimum, and greatly reducing the production cost;
the naphtha and the refined diesel oil produced by twice fractionation have high product percent of pass and the quality far exceeds the national standard, so that huge production capacity value is obtained in low-cost investment and transformation.
Drawings
Fig. 1 is a schematic structural view of the present invention;
in the figure: 1. the system comprises a first fractionating tower, 2, a second fractionating tower, 3, a heating furnace, 4, a heat exchanger, 5, a first cooler, 6, a first reflux tank, 7, a second cooler, 8, a second reflux tank, 9, a naphtha branch, 10, a raw material pipeline, 11, a first reflux outlet, 12, a first reflux inlet, 13, a first feeding hole, 14, a first stripping inlet, 15, a first discharging hole, 16, a first power pump, 17, a second power pump, 18, a third power pump, 19, a fourth power pump, 20, a diesel pipeline, 21, a second reflux outlet, 22, a second reflux inlet, 23, a second feeding hole, 24, a second stripping inlet, 25 and a second discharging hole.
Detailed Description
The present invention will be further explained with reference to the drawings and examples.
Referring to fig. 1, a fine fractionation apparatus for a hydrogenation process includes a primary fractionation unit, a secondary fractionation unit, a heating furnace 3, and a heat exchanger 4.
The primary fractionation unit includes a first fractionation column 1, a first cooler 5, and a first reflux drum 6.
Wherein the first fractionating tower 1 is provided with a first stripping inlet 14, a first feed inlet 13, a first discharge outlet 15, a first reflux outlet 11 and a first reflux inlet 12, the first reflux outlet 11 passes through the first cooler 5 and the first reflux tank 6 through a pipeline and then establishes reflux with the first reflux inlet 12, and a first power pump 16 can be installed on the pipeline part between the first reflux tank 6 and the first fractionating tower 1 to increase the reflux speed.
The first reflux drum 6 is provided with a low-gas-fraction outlet, and the first cooler 5 is preferably a water cooler.
The secondary fractionation unit comprises a second fractionation column 2, a second cooler 7 and a second reflux drum 8.
Wherein the second fractionating tower 2 is provided with a second stripping inlet 24, a second feeding hole 23, a second discharging hole 25, a second reflux outlet 21 and a second reflux inlet 22, the second reflux outlet 21 establishes reflux with the second reflux inlet 22 through a second cooler 7 and a second reflux tank 8 by pipelines, and a second power pump 17 can be installed on the pipeline part between the second reflux tank 8 and the second fractionating tower 2 to increase reflux speed.
The second reflux drum 8 is provided with a low-split gas outlet, a naphtha branch 9 is provided on a pipe portion between the second reflux drum 8 and the second fractionator 2, and the second cooler 7 is preferably a water cooler.
The cold medium inlet of the heat exchanger 4 is communicated with the raw material pipeline 10, the cold medium outlet of the heat exchanger 4 is in pipeline connection with the first feeding hole 13, the first discharging hole 15 is in pipeline connection with the inlet of the heating furnace 3, and a third power pump 18 is installed on a pipeline between the first discharging hole 15 and the heating furnace 3.
The outlet of the heating furnace 3 is connected with the second feeding hole 23 through a pipeline, the second discharging hole 25 is connected with the heat medium inlet of the heat exchanger 4 through a pipeline, a fourth power pump 19 is installed on the pipeline between the second discharging hole 25 and the heat exchanger 4, and the heat medium outlet of the heat exchanger 4 is communicated with a diesel pipeline 20.
The working process is as follows:
the low-fraction oil raw material flows through a heat exchanger 4 from a raw material pipeline 10 and then enters a first fractionating tower 1, primary fractionation is carried out in the first fractionating tower 1 under the action of stripping steam, excessive heat in the first fractionating tower 1 is taken away by reflux established at the top of the first fractionating tower 1 in the primary fractionation process, so that heat balance in the first fractionating tower 1 is maintained, and meanwhile, most of low-fraction gas in the primary fractionation process is discharged from a low-fraction gas outlet on a first reflux tank 6;
the raw materials after the primary fractionation enter the second fractionating tower 2 after flowing through the heating furnace 3 from the first fractionating tower 1 and being heated, and are subjected to secondary fractionation in the second fractionating tower 2 under the action of stripping steam, and the excessive heat in the second fractionating tower 2 is taken away by the reflux established at the top of the second fractionating tower 2 in the secondary fractionation process, so that the heat balance in the second fractionating tower 2 is maintained, and simultaneously, a small amount of residual low-fraction gas is discharged from a low-fraction gas outlet on the second reflux tank 8 in the secondary fractionation process.
Naphtha fractionated by the secondary fractionation flows out from a naphtha branch 9 and is collected, and fractionated refined diesel oil flows through a heat exchanger 4 from a second discharge port 25 of the second fractionating tower 2 and then is converged into a diesel oil pipeline 20.
At the moment, the consumption of stripping steam in the primary fractionation can be reduced, and the refined diesel oil after the secondary fractionation is used as a heat medium to heat the low fraction oil of the primary fractionation, wherein the temperature of the refined diesel oil after the secondary fractionation is generally above 250 ℃, which is enough to meet the heating requirement of the low fraction oil in the primary fractionation.
The utility model utilizes the refined diesel oil after the secondary fractionation as the heat medium to heat the low oil-separating raw material in the primary fractionation, thereby not only reasonably utilizing the waste heat of the refined diesel oil, but also reducing the using amount of steam stripping used in the primary fractionation to the minimum, and greatly reducing the production cost;
meanwhile, the naphtha and the refined diesel oil produced by twice fractionation have high product percent of pass and the quality far exceeds the national standard, so that huge production capacity value is obtained in low-cost investment and transformation.
The present invention is not limited to the above-described embodiments, and various changes can be made within the knowledge range of those skilled in the art without departing from the spirit of the present invention, and the changed contents still belong to the protection scope of the present invention.
Claims (5)
1. A fine fractionation apparatus for a hydrogenation process, characterized by: the system comprises a primary fractionation unit, a secondary fractionation unit, a heating furnace and a heat exchanger;
the primary fractionation unit comprises a first fractionation tower, a first cooler and a first reflux tank, wherein the first fractionation tower is provided with a first stripping inlet, a first feeding hole, a first discharging hole, a first reflux outlet and a first reflux inlet, the first reflux outlet passes through the first cooler and the first reflux tank through pipelines and then establishes reflux with the first reflux inlet, and the first reflux tank is provided with a low-fraction gas outlet;
the secondary fractionation unit comprises a second fractionation tower, a second cooler and a second reflux tank, a second stripping inlet, a second feeding hole, a second discharging hole, a second reflux outlet and a second reflux inlet are arranged on the second fractionation tower, the second reflux outlet passes through the second cooler and the second reflux tank through a pipeline and then establishes reflux with the second reflux inlet, a low-fraction gas outlet is arranged on the second reflux tank, and a naphtha branch is arranged on the pipeline part between the second reflux tank and the second fractionation tower;
the cold medium inlet of the heat exchanger is communicated with the raw material pipeline, the cold medium outlet of the heat exchanger is connected with the first feed inlet pipeline, the first discharge outlet is connected with the inlet pipeline of the heating furnace, the outlet of the heating furnace is connected with the second feed inlet pipeline, the second discharge outlet is connected with the hot medium inlet pipeline of the heat exchanger, and the hot medium outlet of the heat exchanger is communicated with the diesel oil pipeline.
2. The fine fractionation apparatus for a hydrogenation process according to claim 1, wherein: the first cooler and the second cooler are both water coolers.
3. The fine fractionation apparatus for a hydrogenation process according to claim 1, wherein: and a first power pump is also arranged on the pipeline part between the first reflux tank and the first fractionating tower, and a second power pump is also arranged on the pipeline part between the second reflux tank and the second fractionating tower.
4. The fine fractionation apparatus for a hydrogenation process according to claim 1, wherein: and a third power pump is arranged on a pipeline between the first discharge hole and the heating furnace.
5. The fine fractionation apparatus for a hydrogenation process according to claim 1, wherein: and a fourth power pump is arranged on the pipeline between the second discharge hole and the heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201922372144.0U CN211471311U (en) | 2019-12-26 | 2019-12-26 | Fine fractionation device for hydrogenation process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201922372144.0U CN211471311U (en) | 2019-12-26 | 2019-12-26 | Fine fractionation device for hydrogenation process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN211471311U true CN211471311U (en) | 2020-09-11 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201922372144.0U Active CN211471311U (en) | 2019-12-26 | 2019-12-26 | Fine fractionation device for hydrogenation process |
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|---|---|
| CN (1) | CN211471311U (en) |
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2019
- 2019-12-26 CN CN201922372144.0U patent/CN211471311U/en active Active
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Haixing Chemical Co.,Ltd. Dongying City Assignor: Shandong Dongfang Hualong Industrial and Trade Group Co.,Ltd. Contract record no.: X2021980014437 Denomination of utility model: A fine fractionation device for hydrogenation process Granted publication date: 20200911 License type: Common License Record date: 20211209 |
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| EE01 | Entry into force of recordation of patent licensing contract |