CN203389623U - Liquid-phase hydrogenation reaction system - Google Patents
Liquid-phase hydrogenation reaction system Download PDFInfo
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- CN203389623U CN203389623U CN201320384839.0U CN201320384839U CN203389623U CN 203389623 U CN203389623 U CN 203389623U CN 201320384839 U CN201320384839 U CN 201320384839U CN 203389623 U CN203389623 U CN 203389623U
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Abstract
The utility model discloses a liquid-phase hydrogenation reaction system. The liquid-phase hydrogenation reaction system comprises a raw oil buffering tank, a reaction feedstock heating furnace, a gas-liquid mixer, a liquid-phase hydrogenation reactor, decompression equipment and a low-pressure separator, wherein an outlet of the raw oil buffering tank is connected with an inlet of the gas-liquid mixer by the reaction feedstock heating furnace; the outlet of the gas-liquid mixer is connected with the inlet of the liquid-phase hydrogenation reactor; the outlet of the liquid-phase hydrogenation reactor is connected with the inlet of the low-pressure separator by the decompression equipment; one path of a bottom material outlet pipeline of the low-pressure separator is connected with the inlet of the raw oil buffering tank. According to the liquid-phase hydrogenation reaction system disclosed by the utility model, a lot of hydrogen sulfide and ammonia light components can be evaporated.
Description
Technical field
The utility model belongs to hydrogen addition technology field, particularly a kind of liquid-phase hydrogenatin reaction system.
Background technology
Liquid-phase hydrogenatin technology is a novel hydrogen addition technology.The reactions such as the desulfurization of conventional trickle bed hydrogenation reactor, denitrogenation are mainly with hydrogen mass transfer, and hydrogen is from gas phase diffusion and be dissolved into the control step that the speed oil is whole hydrogenation reaction.The feature of liquid-phase hydrogenatin technique is to eliminate the impact of hydrogen mass transfer, hydrogenation reaction is carried out in dynamics Controlling district, being about to hydrogen is dissolved in and in feedstock oil, meets the required hydrogen of hydrogenation reaction, it in reactor, is pure liquid phase reactor, can eliminate the mass transport affects of hydrogen from gas phase to liquid phase, by liquid-circulating, to dissolve enough hydrogen, meet the needs of hydrogenation reaction, save the investment of the equipment such as circulating hydrogen compressor and high-pressure separator.Compare with traditional trickle bed technique, hydrogen gas circulating system and Separate System of Water-jet are not set in liquid-phase hydrogenatin technological process, liquid phase circulation system and hydrogen and oily static mixer have been increased, to guarantee that hydrogen is dissolved in charging completely, and the material in reactor exists with pure liquid phase state.
But in current liquid-phase hydrogenatin technological process, because hydrogenation reaction needs a large amount of hydrogen, and only depend on the hydrogen dissolving in fresh feed oil to there is no method, satisfy the demands, therefore in technological process, be provided with product circulating pump, a large amount of product is circulated to reactor inlet by reactor outlet, provides hydrogenation reaction needed hydrogen.Yet, owing to containing the H of hydrogenation reaction generation in product after hydrogenation reaction
2s and NH
3, after being circulated to reactor inlet and fresh feed oil and mixing, will cause containing in reactor inlet logistics a large amount of H
2s and NH
3.The principle of chemical reaction equilibrium, H
2s and NH
3existence will suppress the carrying out of hydrodesulfurization reaction and denitrification reaction, the product that causes the sulfur content stipulated in the V standard of production Europe and nitrogen content to be 10 μ g/g has difficulties.
CN200910204293.4 discloses a kind of reactor and liquid-phase hydrogenation processing method, this reactor comprises at least two beds, the hydrogen sulfide and the ammonia that for removing reaction, generate, the inner member that is provided with complicated gas make-up and the impure excess air of discharge between at least one adjacent catalyst bed layer, brings difficulty to the design of equipment and processing.
CN201010001103.1 discloses a kind of circulating liquid phase hydrogenation method, and the method is by arranging the liquid phase of thermal high knockout drum and heat low knockout drum separating cycle, although can partly isolate hydrogen sulfide and ammonia, separating effect is limited.
CN200910187765.X discloses a kind of hydrotreating method of product circulation, part circulation through the liquid product of hydrotreatment is mixed into liquid phase material with raw material, liquid phase material enters reactor top, reactor top arranges at least one air lift tower tray, below air lift tower tray, pass into hydrogen, hydrogen contacts air lift and goes out hydrogen sulfide and the ammonia in liquid phase material on air lift tower tray with liquid phase material, hydrogen is further dissolved in liquid phase material simultaneously, the beds that liquid phase material after air lift enters reactor lower part carries out hydrotreatment reaction, the gas that contains hydrogen sulfide and ammonia after air lift is discharged reactor from reactor head.But under condition of high voltage, due to hydrogen sulfide and the solubility of ammonia in oil product higher, air lift removal effect not obvious, limited to improving hydrogenation reaction efficiency.
Meanwhile, above-mentioned prior art all needs to adopt circular-pump high temperature resistant, high pressure, and the cost of investment of this pump is high, and in operation process, fault rate is high, is the limiting factor that affects the steady running of liquid-phase hydrogenatin device.
Summary of the invention
One of the purpose of this utility model is to provide a kind of liquid-phase hydrogenatin reaction system.
According to Yi Ge of the present utility model aspect, a kind of liquid-phase hydrogenatin reaction system is provided, comprise feedstock oil surge tank, reaction feed heating furnace, air and liquid mixer, liquid phase hydrogenation reactor, pressure regulating equipment and low pressure separator; The outlet of described feedstock oil surge tank is connected with the entrance of described air and liquid mixer by described reaction feed heating furnace; The outlet of described air and liquid mixer is connected with the entrance of described liquid phase hydrogenation reactor; The outlet of described liquid phase hydrogenation reactor is connected with the entrance of described low pressure separator by described pressure regulating equipment; Material outlet pipeline one tunnel, bottom of described low pressure separator is connected with the entrance of described feedstock oil surge tank.
Further, described liquid-phase hydrogenatin reaction system dress also comprises that described the first supercharging equipment is arranged between described feedstock oil surge tank and described reaction feed heating furnace for improving the first supercharging equipment of hydrogenation feed pressure.
Further, described liquid-phase hydrogenatin reaction system also comprises heat exchanger, and an entrance of described heat exchanger is connected with described the first supercharging equipment, and an outlet is connected with the entrance of described reaction feed heating furnace; Another entrance of described heat exchanger is connected with another road of material outlet pipeline, bottom of described low pressure separator, and another outlet is connected with hydrogenation products recovery system.
Further, described liquid-phase hydrogenatin reaction system also comprises that the outlet of described the second supercharging equipment is connected with the entrance of described air and liquid mixer, described liquid phase hydrogenation reactor respectively for supplementing the second supercharging equipment of hydrogenation feed pressure.
Further, the first via outlet line of described the second supercharging equipment is connected with the entrance of described air and liquid mixer by described heat exchanger, reaction feed heating furnace successively; The second way outlet pipeline of the second supercharging equipment is connected with another entrance of described air and liquid mixer; The Third Road outlet line of the second supercharging equipment is connected with described liquid phase hydrogenation reactor.
Further, described low pressure separator bottom is provided with gas stripping gas entrance.
Further, described low pressure separator top arranges gas discharge outlet.
The liquid-phase hydrogenatin reaction system that the utility model provides, owing to having increased a low pressure separator on the basis in existing liquid-phase hydrogenatin flow process, cancels oil circulating pump, and the product of liquid phase hydrogenation reactor outlet enters low pressure separator after by decompression device step-down.In low pressure separator, can make most hydrogen sulfide and ammonia flash off with light component.
Accompanying drawing explanation
The structural representation of the liquid-phase hydrogenatin reaction system that Fig. 1 provides for the utility model embodiment.
The specific embodiment
Referring to Fig. 1, the liquid-phase hydrogenatin reaction system that the utility model embodiment provides comprises feedstock oil surge tank 1, reaction feed heating furnace 4, air and liquid mixer 10, liquid phase hydrogenation reactor 5, pressure regulating equipment 9 and low pressure separator 6.The outlet of feedstock oil surge tank 1 is connected with the entrance of air and liquid mixer 10 by reaction feed heating furnace 4.The outlet of air and liquid mixer 10 is connected with the entrance of liquid phase hydrogenation reactor 5.The outlet of liquid phase hydrogenation reactor 5 is connected with the entrance of low pressure separator 6 by pressure regulating equipment 9.Material outlet pipeline one tunnel, bottom of low pressure separator 6 is connected with the entrance of feedstock oil surge tank 1.Low pressure separator top arranges gas phase outlet 8, and bottom is provided with gas stripping gas entrance.The operating pressure of low pressure separator is 0～3MPa(gauge pressure), be preferably 0.1～1MPa.
When hydrogenation feed pressure is not enough, the first supercharging equipment that improves hydrogenation feed pressure can be set between feedstock oil surge tank 1 and reaction feed heating furnace 4.The first supercharging equipment specifically can adopt hydrogenation feed pump 2.
For by the 2 outlet material heat exchange of the hydrogenation feed pump of the product of the high temperature from liquid phase hydrogenation reactor 5 and low temperature, between hydrogenation feed pump 2 and low pressure separator 6, be also provided with heat exchanger 3.One entrance of heat exchanger 3 is connected with hydrogenation feed pump 2, and an outlet is connected with the entrance of described reaction feed heating furnace 4; Another entrance of heat exchanger 3 is connected with another road of material outlet pipeline, bottom of low pressure separator 6, and another outlet is connected with hydrogenation products recovery system.
When hydrogen make-up insufficient pressure, can be provided for supplementing the second supercharging equipment of hydrogenation feed pressure.The outlet of the second supercharging equipment is connected with the entrance of air and liquid mixer 10, liquid phase hydrogenation reactor 5 respectively.The first via outlet line of the second supercharging equipment is connected with the entrance of air and liquid mixer 10 by heat exchanger 3, reaction feed heating furnace 4 successively; The second way outlet pipeline of the second supercharging equipment is connected with another entrance of air and liquid mixer 10; The Third Road outlet line of the second supercharging equipment is connected with liquid phase hydrogenation reactor 5.The second supercharging equipment specifically can adopt make-up hydrogen compressor 7.
The liquid-phase hydrogenatin reaction system that the utility model embodiment provides has increased a low pressure separator on the basis of existing liquid-phase hydrogenatin flow process, cancel oil circulating pump, the product of liquid phase hydrogenation reactor outlet enters low pressure separator after by decompression device step-down.In low pressure separator, light component flashes off, and hydrogen sulfide wherein and ammonia major part flash off with light component.Owing to increasing air lift gas, make the removal effect of hydrogen sulfide and ammonia more abundant, and then reduced the high impact on reaction depth of impurity content in recycle oil in addition.The utility model is cancelled the oil circulating pump of HTHP simultaneously, recycle oil is mixed by feedstock pump and carried with fresh feed, reduced high-tension apparatus quantity, although the scale of feedstock pump needs to increase, but overall investment reduces greatly, and the stability of running improves, and is conducive to the long period steady running of device.
It should be noted last that, the above specific embodiment is only unrestricted in order to the technical solution of the utility model to be described, although the utility model is had been described in detail with reference to example, those of ordinary skill in the art is to be understood that, can modify or be equal to replacement the technical solution of the utility model, and not departing from the spirit and scope of technical solutions of the utility model, it all should be encompassed in the middle of claim scope of the present utility model.
Claims (7)
1. a liquid-phase hydrogenatin reaction system, comprises feedstock oil surge tank (1), reaction feed heating furnace (4), air and liquid mixer (10), liquid phase hydrogenation reactor (5), pressure regulating equipment (9) and low pressure separator (6); The outlet of described feedstock oil surge tank (1) is connected with the entrance of described air and liquid mixer (10) by described reaction feed heating furnace (4); The outlet of described air and liquid mixer (10) is connected with the entrance of described liquid phase hydrogenation reactor (5); The outlet of described liquid phase hydrogenation reactor (5) is connected with the entrance of described low pressure separator (6) by described pressure regulating equipment (9); Material outlet pipeline one tunnel, bottom of described low pressure separator (6) is connected with the entrance of described feedstock oil surge tank (1).
2. liquid-phase hydrogenatin reaction system according to claim 1, it is characterized in that, also comprise that described the first supercharging equipment is arranged between described feedstock oil surge tank (1) and described reaction feed heating furnace (4) for improving the first supercharging equipment of hydrogenation feed pressure.
3. liquid-phase hydrogenatin reaction system according to claim 2, is characterized in that, also comprises heat exchanger (3), and an entrance of described heat exchanger (3) is connected with described the first supercharging equipment, and an outlet is connected with the entrance of described reaction feed heating furnace (4); Another entrance of described heat exchanger (3) is connected with another road of material outlet pipeline, bottom of described low pressure separator (6), and another outlet is connected with hydrogenation products recovery system.
4. liquid-phase hydrogenatin reaction system according to claim 3, it is characterized in that, also comprise that the outlet of described the second supercharging equipment is connected with the entrance of described air and liquid mixer (10), described liquid phase hydrogenation reactor (5) respectively for supplementing the second supercharging equipment of hydrogenation feed pressure.
5. liquid-phase hydrogenatin reaction system according to claim 4, is characterized in that, the first via outlet line of described the second supercharging equipment is connected with the entrance of described air and liquid mixer (10) by described heat exchanger (3), reaction feed heating furnace (4) successively; The second way outlet pipeline of the second supercharging equipment is connected with another entrance of described air and liquid mixer (10); The Third Road outlet line of the second supercharging equipment is connected with described liquid phase hydrogenation reactor (5).
6. liquid-phase hydrogenatin reaction system according to claim 1, is characterized in that, described low pressure separator bottom is provided with gas stripping gas entrance.
7. liquid-phase hydrogenatin reaction system according to claim 1, is characterized in that, described low pressure separator top arranges gas discharge outlet.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320384839.0U CN203389623U (en) | 2013-06-28 | 2013-06-28 | Liquid-phase hydrogenation reaction system |
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| CN201320384839.0U CN203389623U (en) | 2013-06-28 | 2013-06-28 | Liquid-phase hydrogenation reaction system |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105441125A (en) * | 2015-12-25 | 2016-03-30 | 华南理工大学 | Method for enhancing mixing degree of raw oil and fresh hydrogen of oil liquid-phase hydrogenation refining device |
| CN105524657A (en) * | 2014-09-29 | 2016-04-27 | 中国石油化工股份有限公司 | Method for hydrogenation of distillate oil via fluidized bed |
| CN107141200A (en) * | 2017-06-27 | 2017-09-08 | 查都（上海）科技有限公司 | A kind of 1,4 butynediols hydrogenation reaction systems |
| CN107941047A (en) * | 2017-11-21 | 2018-04-20 | 宁波东鼎石化装备有限公司 | A kind of heat exchanger, the four Hydrogenation iso-butane device and method of mixing carbon using the heat exchanger |
| CN108620001A (en) * | 2017-03-16 | 2018-10-09 | 新疆摩珈生物科技有限公司 | Continuously hydrogen adding reduction reaction system |
| CN113877488A (en) * | 2021-11-16 | 2022-01-04 | 中国石油大学(华东) | Up-flow hydrogenation reaction device based on tubular micropore medium foaming mechanism |
| CN114437809A (en) * | 2020-11-05 | 2022-05-06 | 中国石油天然气集团有限公司 | Liquid-phase hydrogenation device and liquid-phase hydrogenation method |
-
2013
- 2013-06-28 CN CN201320384839.0U patent/CN203389623U/en not_active Expired - Fee Related
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105524657A (en) * | 2014-09-29 | 2016-04-27 | 中国石油化工股份有限公司 | Method for hydrogenation of distillate oil via fluidized bed |
| CN105524657B (en) * | 2014-09-29 | 2017-03-29 | 中国石油化工股份有限公司 | A kind of fraction oil boiling bed hydrogenation method |
| CN105441125A (en) * | 2015-12-25 | 2016-03-30 | 华南理工大学 | Method for enhancing mixing degree of raw oil and fresh hydrogen of oil liquid-phase hydrogenation refining device |
| CN108620001A (en) * | 2017-03-16 | 2018-10-09 | 新疆摩珈生物科技有限公司 | Continuously hydrogen adding reduction reaction system |
| CN108620001B (en) * | 2017-03-16 | 2021-10-01 | 新疆摩珈生物科技有限公司 | Continuous hydrogenation reduction reaction system |
| CN107141200A (en) * | 2017-06-27 | 2017-09-08 | 查都（上海）科技有限公司 | A kind of 1,4 butynediols hydrogenation reaction systems |
| CN107941047A (en) * | 2017-11-21 | 2018-04-20 | 宁波东鼎石化装备有限公司 | A kind of heat exchanger, the four Hydrogenation iso-butane device and method of mixing carbon using the heat exchanger |
| CN114437809A (en) * | 2020-11-05 | 2022-05-06 | 中国石油天然气集团有限公司 | Liquid-phase hydrogenation device and liquid-phase hydrogenation method |
| CN114437809B (en) * | 2020-11-05 | 2023-12-22 | 中国石油天然气集团有限公司 | Liquid phase hydrogenation device and liquid phase hydrogenation method |
| CN113877488A (en) * | 2021-11-16 | 2022-01-04 | 中国石油大学(华东) | Up-flow hydrogenation reaction device based on tubular micropore medium foaming mechanism |
| CN113877488B (en) * | 2021-11-16 | 2023-07-04 | 中国石油大学(华东) | Up-flow hydrogenation reaction device based on tubular microporous medium foaming mechanism |
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| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140115 Termination date: 20210628 |
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| CF01 | Termination of patent right due to non-payment of annual fee |