CN108635889B - Light benzene evaporation tower in benzene hydrogenation system and working method thereof - Google Patents
Light benzene evaporation tower in benzene hydrogenation system and working method thereof Download PDFInfo
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- CN108635889B CN108635889B CN201810732081.2A CN201810732081A CN108635889B CN 108635889 B CN108635889 B CN 108635889B CN 201810732081 A CN201810732081 A CN 201810732081A CN 108635889 B CN108635889 B CN 108635889B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/0011—Heating features
- B01D1/0041—Use of fluids
- B01D1/0047—Use of fluids in a closed circuit
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/30—Accessories for evaporators ; Constructional details thereof
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
- C07C7/163—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation
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Abstract
The invention relates to a light benzene evaporation tower in a benzene hydrogenation system and a working method thereof, wherein the light benzene evaporation tower comprises a tower body, and the tower body is divided into an upper gas-fog separation section and a lower evaporation section by a baffle plate; the top of the tower body is provided with a light benzene gas outlet, and the bottom of the tower body is provided with a tower bottom liquid extraction device; the aerosol separation section is provided with a central pipeline and a spiral channel; the bottom liquid extraction device adopts an inner and outer sleeve structure, wherein the top of the inner tube extends upwards to the central part of the tower kettle liquid, and the bottom of the inner tube is provided with a light benzene liquid outlet; the top of the outer tube is communicated with the bottom of the tower body, and the lower part of the outer tube is provided with a light benzene residual oil outlet; the outer side of the inner pipe extension section close to the bottom of the tower body is provided with a horizontal baffle. The tower body of the light benzene evaporation tower is divided into the upper aerosol separation section and the lower evaporation section, so that the blockage of a reboiler is effectively avoided or the blockage frequency of the reboiler is reduced; the gas and fog drops are completely separated by adopting a cyclone separation principle in the gas-fog separation section.
Description
Technical Field
The invention relates to the technical field of crude benzene hydrofining, in particular to a light benzene evaporation tower in a benzene hydrogenation system and a working method thereof.
Background
The main components of crude benzene produced in the coking process are benzene, toluene and xylene, and in addition, 5% -10% of unsaturated compounds are cyclic hydrocarbons and linear olefins with one or two double bonds, so that polymerization reaction is easy to occur, and the boiling points of some unsaturated compounds, sulfides and nitrogenous compounds are similar to the boiling point temperature between corresponding benzene products, so that they cannot be separated by a rectification method. The hydrofining process is to remove all impurities including thiophene in crude benzene by hydrogenation process, wherein sulfide is converted into H 2 S, conversion of nitride to NH 3 Conversion of oxides to H 2 O, unsaturated hydrocarbon is hydrogenated and saturated, and H is removed by separation 2 S、NH 3 And H 2 The hydrogenated oil left after O can easily produce high-quality benzene, toluene and xylene by means of extractive distillation.
The crude benzene hydrofining process has little pollution and the product quality can be compared with petroleum benzene, so the crude benzene hydrofining process in the coking industry is basically based on crude benzene hydrofining. Crude benzene hydrorefining is divided into two basic modes of liquid phase hydrogenation, gas phase hydrogenation and two-stage gas phase hydrogenation, and mainly adopts gas phase hydrogenation.
The gasification process mainly comprises the following two steps before gas-phase hydrogenation of crude benzene, wherein the first step is that the crude benzene is de-heavy, namely, the fraction with high boiling point in the crude benzene is removed by a distillation method to obtain liquid light benzene; the second step is light benzene gasification, as shown in fig. 1, circulating hydrogen gas forms negative pressure through a pre-evaporator jet mixer 4 at high speed, so that external light benzene liquid flows circularly in the pre-evaporator 1 at high speed, the external light benzene liquid is preheated and mostly gasified through the pre-evaporator 1 by utilizing the heat of the light benzene gas after hydrogenation reaction, a light benzene gas-liquid mixture is formed, the negative pressure is formed as power through a light benzene evaporation tower jet mixer 5 at high speed, the bottom of a light benzene evaporation tower 3 and a reboiler 2 form a closed cycle, the heat of the light benzene gas after hydrogenation reaction is utilized, and the rest light benzene is completely gasified in the light benzene evaporation tower 3 by keeping the liquid level balance at the bottom of the tower by utilizing the heat of the light benzene gas after hydrogenation reaction and the heat of the reboiler 2. The core equipment of the light benzene gasification process is a light benzene evaporation tower 3.
The conventional light benzene evaporation tower 3 belongs to an empty tower, the upper part of the tower body is provided with only one mist catcher, and two main problems exist in the actual operation of the light benzene evaporation tower: firstly, the reboiler 2 of the light benzene evaporation tower 3 is frequently blocked (blocked once in 3 months), and the whole equipment is stopped when serious, and is not easy to clean, so that great economic loss is caused for enterprises; the reason for this phenomenon is that, due to the presence of unsaturated compounds, polymerization occurs during the heating and gasification to produce a certain amount of polymer, most of which is accumulated at the bottom of the evaporation tower, suspended in the liquid at the bottom of the tower, and blocks the reboiler 2 while circulating with the liquid; currently, in order to reduce the frequency of reboiler blockage, only a method of extracting a large amount of light benzene raffinate at the bottom of the light benzene evaporation tower to reduce the concentration of polymer at the bottom can be adopted. The second problem is that the mist catcher at the top of the tower cannot catch mist, and because the gas flow rate is too fast, a large amount of mist drops are carried into the following pre-reactor by the light benzene gas passing through at high speed and attached to the surface of the catalyst, so that the efficiency of the pre-reactor is reduced.
Disclosure of Invention
The invention provides a light benzene evaporation tower in a benzene hydrogenation system and a working method thereof, wherein a tower body is divided into an upper aerosol separation section and a lower evaporation section, so that the blockage of a reboiler is effectively avoided or the blockage frequency of the reboiler is reduced; the gas and fog drops are completely separated by adopting a cyclone separation principle in the gas-fog separation section.
In order to achieve the above purpose, the invention is realized by adopting the following technical scheme:
a light benzene evaporation tower in a benzene hydrogenation system comprises a tower body, wherein the tower body is divided into an upper aerosol separation section and a lower evaporation section by a partition plate; the top of the tower body is provided with a light benzene gas outlet, and the bottom of the tower body is provided with a tower bottom liquid extraction device; the aerosol separation section is provided with a central pipeline and a spiral channel, the central pipeline is suspended in the middle of the tower body through a horizontal supporting plate, and the upper part of the central pipeline penetrates through the horizontal supporting plate and stretches into an upper tower body space, namely the tower body space above the horizontal supporting plate is communicated with a lower tower body space through the central pipeline; a spiral channel is arranged in an annular space formed by the tower body below the horizontal supporting plate and the central pipeline; a light benzene separation liquid outlet is arranged on one side of the tower body of the aerosol separation section close to the partition plate, a light benzene separation liquid inlet is arranged on the lower tower body of the evaporation section on the same side, and the light benzene separation liquid inlet is connected with the light benzene separation liquid outlet through a light benzene separation liquid pipeline; a gasified light benzene gas outlet is arranged at the other side of the tower body close to the evaporation section of the partition plate, a light benzene gas inlet is arranged on the tower body at the same side below the horizontal support plate, and the light benzene gas inlet is connected with the gasified light benzene gas outlet through a light benzene gas pipeline; a light benzene gas-liquid mixture inlet is arranged at one side of the middle part of the tower body of the evaporation section and at a position lower than the liquid level of the tower kettle liquid, and the light benzene gas mixture inlet is tangentially connected with the tower body; the bottom liquid extraction device adopts an inner and outer sleeve structure, wherein the top of the inner tube extends upwards to the central part of the tower kettle liquid, and the bottom of the inner tube is provided with a light benzene liquid outlet; the top of the outer tube is communicated with the bottom of the tower body, and the lower part of the outer tube is provided with a light benzene residual oil outlet; the outer side of the inner pipe extension section close to the bottom of the tower body is provided with a horizontal baffle.
The light benzene gas outlet is connected with the light benzene gas inlet of the hydrogenation pre-reactor.
The light benzene gas-liquid mixture inlet is connected with a mixed medium outlet of the light benzene evaporation tower jet mixer, one mixed medium inlet of the light benzene evaporation tower jet mixer is connected with a light benzene liquid outlet through a reboiler, and the other mixed medium inlet is connected with a light benzene liquid outlet of the pre-evaporator; the pre-evaporator is provided with a light benzene liquid inlet, a circulating hydrogen inlet and a circulating hydrogen outlet, the circulating hydrogen inlet and the circulating hydrogen outlet are connected through a circulating hydrogen pipeline, and the circulating hydrogen pipeline is provided with a pre-evaporator jet mixer; the heat exchange medium inlet of the reboiler is connected with the light benzene gas pipeline after hydrogenation reaction, the heat exchange medium outlet of the reboiler is connected with the heat exchange medium inlet of the pre-evaporator, and the heat exchange medium outlet of the pre-evaporator is connected with the light benzene gas-liquid mixture pipeline after hydrogenation.
The tower body above the horizontal support plate adopts a split structure and is connected through a flange.
A horn-shaped drainage port is arranged at the top of the inner tube; the area of the horizontal baffle is not smaller than 2/3 of the sectional area of the tower body at the corresponding position.
The working method of the light benzene evaporation tower comprises the following steps:
1) Circulating hydrogen is sprayed into a mixer at a high speed through a pre-evaporator to form negative pressure, so that the heavy crude benzene is removed to obtain liquid light benzene which flows circularly at a high speed in the pre-evaporator, and the liquid light benzene is subjected to heat exchange and temperature rise with the light benzene gas after hydrogenation reaction, so that the liquid light benzene is preheated and mostly gasified to form a light benzene gas-liquid mixture;
2) The light benzene gas-liquid mixture is sprayed by a light benzene evaporation tower spray mixer to form negative pressure as power, so that the bottom of the light benzene evaporation tower and a reboiler form a closed cycle, the reboiler exchanges heat with the light benzene gas after hydrogenation reaction, and the reboiler supplies heat to fully gasify the rest liquid light benzene in the light benzene evaporation tower, so that the liquid level of tower bottom liquid is kept unchanged in the process;
3) Evaporating light benzene gas in an evaporation section at the lower part of the tower body, leading out the evaporated light benzene gas from a gasified light benzene gas outlet, entering an aerosol separation section at the upper part of the tower body through a light benzene gas inlet, and then descending along a spiral channel; in the process, gas-liquid separation is realized, a large amount of fog drops carried in evaporated light benzene gas are attached to the wall of the tower through the action of centrifugal force, are collected above the partition plate under the action of dead weight and air flow along the spiral channel, are led out from the light benzene separation liquid outlet, enter the evaporation section at the lower part of the tower body through the light benzene separation liquid inlet, turn back 180 degrees to flow upwards along the central pipeline, and finally are sent into the subsequent hydrogenation pre-reactor through the light benzene gas outlet for hydrogenation reaction;
4) In the evaporation section, the light benzene gas-liquid mixture inlet adopts a tangential feeding mode, and meanwhile, as the light benzene gas-liquid mixture inlet is positioned below the liquid level of the tower kettle liquid, the tower kettle liquid can be kept in a high-speed rotation state, so that polymers suspended in the tower kettle liquid are gathered on the tower wall; the top of the inner pipe connected with the light benzene liquid outlet is directly extended to the central part of the tower kettle liquid, so that the content of the extracted light benzene liquid polymer is ensured to be minimum, and the blockage phenomenon of a reboiler can be avoided or reduced; the light benzene residual oil outlet is directly connected with the outer tube, the light benzene residual oil containing high-concentration polymer is continuously extracted at a low flow rate at the lowest point in the tower through the outer tube, the horizontal baffle arranged on the inner tube plays a role in blocking flow, and only peripheral suspended polymer can be ensured to be extracted through the light benzene residual oil outlet, and light benzene liquid with low polymer content in the center of tower bottom liquid can not be extracted.
Compared with the prior art, the invention has the beneficial effects that:
1) The tower body is divided into an upper aerosol separation section and a lower evaporation section, in the evaporation section, the state of light benzene evaporation tower bottom liquid is changed from a static state to a rotary flow state, so that polymers suspended in the liquid are gathered around the tower wall and are gathered to the tower bottom along the tower wall, the light benzene liquid which is sent to a reboiler is extracted by an outer pipe of a tower bottom liquid extraction device in a continuous low-flow mode, and the light benzene liquid which is extracted from the center of the tower bottom liquid with very little polymer content by an inner pipe of the tower bottom liquid extraction device, thereby effectively avoiding the blockage of the reboiler or reducing the blockage frequency of the reboiler;
2) The gas and fog drops are completely separated by adopting a cyclone separation principle in the gas-fog separation section.
Drawings
Fig. 1 is a schematic diagram of the structure of a conventional light benzene vaporization tower.
Fig. 2 is a schematic structural diagram of the light benzene evaporation tower according to the present invention.
FIG. 3 is a schematic diagram showing the connection of the light benzene gas-liquid mixture inlet and the tower body.
In the figure: 1. pre-evaporator 2, reboiler 3, conventional light benzene evaporation tower 4, pre-evaporator jet mixer 5, light benzene evaporation tower jet mixer 6, mist catcher 7, tower body 8, partition 9, central pipe 10, spiral channel 11, tower bottom 12, horizontal baffle 13, flange 14 and horizontal support plate
A1. Light benzene gas-liquid mixture inlet a2, light benzene gas inlet a3, light benzene separating liquid inlet b1, light benzene gas outlet b2, light benzene liquid outlet b3, light benzene residue outlet B4. gasified light benzene gas outlet B5., light benzene separating liquid outlet
Detailed Description
The following is a further description of embodiments of the invention, taken in conjunction with the accompanying drawings:
as shown in fig. 2, the light benzene evaporation tower in the benzene hydrogenation system comprises a tower body 7, wherein the tower body 7 is divided into an upper gas-fog separation section and a lower evaporation section by a partition plate 8; the top of the tower body 7 is provided with a light benzene gas outlet B1, and the bottom of the tower body 7 is provided with a tower bottom liquid extraction device; the aerosol separation section is provided with a central pipeline 9 and a spiral channel 10, the central pipeline 9 is suspended in the middle of the tower body 7 through a horizontal supporting plate 14, and the upper part of the central pipeline 9 penetrates through the horizontal supporting plate 14 and stretches into an upper tower body space, namely the tower body space above the horizontal supporting plate 14 is communicated with a lower tower body space through the central pipeline 9; a spiral channel 10 is arranged in an annular space formed by the tower body 7 below the horizontal supporting plate 14 and the central pipeline 9; a light benzene separating liquid outlet B5 is arranged on one side of the tower body of the aerosol separating section close to the partition plate 8, a light benzene separating liquid inlet A3 is arranged on the lower tower body of the evaporating section on the same side, and the light benzene separating liquid inlet A3 is connected with the light benzene separating liquid outlet B5 through a light benzene separating liquid pipeline; a gasified light benzene gas outlet B4 is arranged on the other side of the tower body of the evaporation section close to the partition plate 8, a light benzene gas inlet A2 is arranged on the tower body 7 on the same side below the horizontal support plate 14, and the light benzene gas inlet A2 is connected with the gasified light benzene gas outlet B4 through a light benzene gas pipeline; a light benzene gas-liquid mixture inlet A1 is arranged at one side of the middle part of the tower body 7 of the evaporation section and at a position lower than the liquid level of the tower bottom liquid 11, and the light benzene gas mixture inlet A1 is tangentially connected with the tower body 7 (shown in figure 3); the bottom liquid extraction device adopts an inner and outer sleeve structure, wherein the top of the inner tube extends upwards to the central part of the tower bottom liquid 11, and the bottom of the inner tube is provided with a light benzene liquid outlet B2; the top of the outer pipe is communicated with the bottom of the tower body 7, and the lower part of the outer pipe is provided with a light benzene residual oil B3 outlet; the outside of the extension section of the inner pipe near the bottom of the tower body 7 is provided with a horizontal baffle 12.
And the light benzene gas outlet B1 is connected with a light benzene gas inlet of the hydrogenation pre-reactor.
The light benzene gas-liquid mixture inlet A1 is connected with a mixed medium outlet of the light benzene evaporation tower jet mixer 5, one mixed medium inlet of the light benzene evaporation tower jet mixer 5 is connected with a light benzene liquid outlet B2 through a reboiler 2, and the other mixed medium inlet is connected with a light benzene liquid outlet of the pre-evaporator 1; the pre-evaporator 1 is provided with a light benzene liquid inlet, a circulating hydrogen inlet and a circulating hydrogen outlet, the circulating hydrogen inlet and the circulating hydrogen outlet are connected through a circulating hydrogen pipeline, and the circulating hydrogen pipeline is provided with a pre-evaporator jet mixer 4; the heat exchange medium inlet of the reboiler 2 is connected with a light benzene gas pipeline after hydrogenation reaction, the heat exchange medium outlet of the reboiler 2 is connected with the heat exchange medium inlet of the pre-evaporator 1, and the heat exchange medium outlet of the pre-evaporator 1 is connected with a light benzene gas-liquid mixture pipeline after hydrogenation reaction.
The tower body 7 above the horizontal supporting plate 14 adopts a split structure and is connected through a flange 13.
A horn-shaped drainage port is arranged at the top of the inner tube; the area of the horizontal baffle 12 is not less than 2/3 of the sectional area of the tower body 7 at the corresponding position.
The working method of the light benzene evaporation tower comprises the following steps:
1) The circulating hydrogen passes through a pre-evaporator jet mixer 4 at a high speed to form negative pressure, so that the liquid light benzene obtained after the heavy benzol is removed flows in the pre-evaporator 1 at a high speed in a circulating way, and exchanges heat with the light benzene gas after hydrogenation reaction to raise the temperature, so that the liquid light benzene is preheated and mostly gasified to form a light benzene gas-liquid mixture;
2) The light benzene gas-liquid mixture is sprayed by a light benzene evaporation tower spraying mixer 5 at high speed to form negative pressure as power, so that the bottom of the light benzene evaporation tower and a reboiler 2 form a closed cycle, the reboiler 2 exchanges heat with the light benzene gas after hydrogenation reaction, the reboiler 2 supplies heat to fully gasify the rest liquid light benzene in the light benzene evaporation tower, and the liquid level of tower bottom liquid 11 is kept unchanged in the process;
3) Evaporating light benzene gas in an evaporation section at the lower part of the tower body 7, leading out the evaporated light benzene gas from a gasified light benzene gas outlet B4, entering an aerosol separation section at the upper part of the tower body 7 through a light benzene gas inlet A2, and then descending along a spiral channel 10; in the process, gas-liquid separation is realized, a large amount of mist drops carried in evaporated light benzene gas are attached to the wall of a tower through the action of centrifugal force, are collected above a baffle plate 8 under the action of dead weight and air flow along a spiral channel 10, are led out from a light benzene separation liquid outlet B5, enter an evaporation section at the lower part of a tower body 7 through a light benzene separation liquid inlet A3, turn back 180 degrees to flow upwards along a central pipeline 9, and are finally sent into a subsequent hydrogenation pre-reactor through a light benzene gas outlet B1 for hydrogenation reaction;
4) In the evaporation section, the light benzene gas-liquid mixture inlet A1 adopts a tangential feeding mode, and meanwhile, as the light benzene gas-liquid mixture inlet A is positioned below the liquid level of the tower kettle liquid 11, the tower kettle liquid 11 can be kept in a high-speed rotation state, so that polymers suspended in the tower kettle liquid 11 are gathered on the tower wall; the top of the inner pipe connected with the light benzene liquid outlet B2 directly extends to the central part of the tower kettle liquid 11, so that the content of the extracted light benzene liquid polymer is ensured to be minimum, and the blocking phenomenon of the reboiler 2 can be avoided or reduced; the light benzene residual oil outlet B3 is directly connected with the outer pipe, the light benzene residual oil containing high-concentration polymer is continuously extracted at the lowest point in the tower through the outer pipe, the horizontal baffle 14 arranged on the inner pipe plays a role in blocking flow, and only peripheral suspended polymer can be ensured to be extracted through the light benzene residual oil outlet B3, and light benzene liquid with low polymer content in the center of the tower bottom liquid can not be extracted.
The foregoing is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art, who is within the scope of the present invention, should make equivalent substitutions or modifications according to the technical scheme of the present invention and the inventive concept thereof, and should be covered by the scope of the present invention.
Claims (6)
1. The light benzene evaporation tower in the benzene hydrogenation system is characterized by comprising a tower body, wherein the tower body is divided into an upper aerosol separation section and a lower evaporation section by a partition plate; the top of the tower body is provided with a light benzene gas outlet, and the bottom of the tower body is provided with a tower bottom liquid extraction device; the aerosol separation section is provided with a central pipeline and a spiral channel, the central pipeline is suspended in the middle of the tower body through a horizontal supporting plate, and the upper part of the central pipeline penetrates through the horizontal supporting plate and stretches into an upper tower body space, namely the tower body space above the horizontal supporting plate is communicated with a lower tower body space through the central pipeline; a spiral channel is arranged in an annular space formed by the tower body below the horizontal supporting plate and the central pipeline; a light benzene separation liquid outlet is arranged on one side of the tower body of the aerosol separation section close to the partition plate, a light benzene separation liquid inlet is arranged on the lower tower body of the evaporation section on the same side, and the light benzene separation liquid inlet is connected with the light benzene separation liquid outlet through a light benzene separation liquid pipeline; a gasified light benzene gas outlet is arranged at the other side of the tower body close to the evaporation section of the partition plate, a light benzene gas inlet is arranged on the tower body at the same side below the horizontal support plate, and the light benzene gas inlet is connected with the gasified light benzene gas outlet through a light benzene gas pipeline; a light benzene gas-liquid mixture inlet is arranged at one side of the middle part of the tower body of the evaporation section and at a position lower than the liquid level of the tower kettle liquid, and the light benzene gas mixture inlet is tangentially connected with the tower body; the bottom liquid extraction device adopts an inner and outer sleeve structure, wherein the top of the inner tube extends upwards to the central part of the tower kettle liquid, and the bottom of the inner tube is provided with a light benzene liquid outlet; the top of the outer tube is communicated with the bottom of the tower body, and the lower part of the outer tube is provided with a light benzene residual oil outlet; the outer side of the inner pipe extension section close to the bottom of the tower body is provided with a horizontal baffle.
2. The light benzene vaporization tower in a benzene hydrogenation system according to claim 1, wherein said light benzene gas outlet is connected to a light benzene gas inlet of a hydrogenation pre-reactor.
3. The light benzene evaporation tower in benzene hydrogenation system according to claim 1, wherein the light benzene gas-liquid mixture inlet is connected with a mixed medium outlet of a light benzene evaporation tower jet mixer, one mixed medium inlet of the light benzene evaporation tower jet mixer is connected with the light benzene liquid outlet through a reboiler, and the other mixed medium inlet is connected with the light benzene liquid outlet of the pre-evaporator; the pre-evaporator is provided with a light benzene liquid inlet, a circulating hydrogen inlet and a circulating hydrogen outlet, the circulating hydrogen inlet and the circulating hydrogen outlet are connected through a circulating hydrogen pipeline, and the circulating hydrogen pipeline is provided with a pre-evaporator jet mixer; the heat exchange medium inlet of the reboiler is connected with the light benzene gas pipeline after hydrogenation reaction, the heat exchange medium outlet of the reboiler is connected with the heat exchange medium inlet of the pre-evaporator, and the heat exchange medium outlet of the pre-evaporator is connected with the light benzene gas-liquid mixture pipeline after hydrogenation.
4. The light benzene evaporation tower in benzene hydrogenation system according to claim 1, wherein the tower body above the horizontal support plate adopts a split structure and is connected through a flange.
5. The light benzene evaporation tower in benzene hydrogenation system according to claim 1, wherein a horn-shaped drainage port is arranged at the top of the inner pipe; the area of the horizontal baffle is not smaller than 2/3 of the sectional area of the tower body at the corresponding position.
6. The method of operating a light benzene vaporization tower as claimed in claim 1, including the steps of:
1) Circulating hydrogen is sprayed into a mixer at a high speed through a pre-evaporator to form negative pressure, so that the heavy crude benzene is removed to obtain liquid light benzene which flows circularly at a high speed in the pre-evaporator, and the liquid light benzene is subjected to heat exchange and temperature rise with the light benzene gas after hydrogenation reaction, so that the liquid light benzene is preheated and mostly gasified to form a light benzene gas-liquid mixture;
2) The light benzene gas-liquid mixture is sprayed by a light benzene evaporation tower spray mixer to form negative pressure as power, so that the bottom of the light benzene evaporation tower and a reboiler form a closed cycle, the reboiler exchanges heat with the light benzene gas after hydrogenation reaction, and the reboiler supplies heat to fully gasify the rest liquid light benzene in the light benzene evaporation tower, so that the liquid level of tower bottom liquid is kept unchanged in the process;
3) Evaporating light benzene gas in an evaporation section at the lower part of the tower body, leading out the evaporated light benzene gas from a gasified light benzene gas outlet, entering an aerosol separation section at the upper part of the tower body through a light benzene gas inlet, and then descending along a spiral channel; in the process, gas-liquid separation is realized, a large amount of fog drops carried in evaporated light benzene gas are attached to the wall of the tower through the action of centrifugal force, are collected above the partition plate under the action of dead weight and air flow along the spiral channel, are led out from the light benzene separation liquid outlet, enter the evaporation section at the lower part of the tower body through the light benzene separation liquid inlet, turn back 180 degrees to flow upwards along the central pipeline, and finally are sent into the subsequent hydrogenation pre-reactor through the light benzene gas outlet for hydrogenation reaction;
4) In the evaporation section, the light benzene gas-liquid mixture inlet adopts a tangential feeding mode, and meanwhile, as the light benzene gas-liquid mixture inlet is positioned below the liquid level of the tower kettle liquid, the tower kettle liquid can be kept in a high-speed rotation state, so that polymers suspended in the tower kettle liquid are gathered on the tower wall; the top of the inner pipe connected with the light benzene liquid outlet is directly extended to the central part of the tower kettle liquid, so that the content of the extracted light benzene liquid polymer is ensured to be minimum, and the blockage phenomenon of a reboiler can be avoided or reduced; the light benzene residual oil outlet is directly connected with the outer tube, the light benzene residual oil containing high-concentration polymer is continuously extracted at a low flow rate at the lowest point in the tower through the outer tube, the horizontal baffle arranged on the inner tube plays a role in blocking flow, and only peripheral suspended polymer can be ensured to be extracted through the light benzene residual oil outlet, and light benzene liquid with low polymer content in the center of tower bottom liquid can not be extracted.
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| CN111939584B (en) * | 2020-09-04 | 2023-09-15 | 中冶焦耐(大连)工程技术有限公司 | Crude benzene evaporation process and system in benzene hydrogenation reaction system |
| CN114713000A (en) * | 2022-04-21 | 2022-07-08 | 中冶焦耐(大连)工程技术有限公司 | Exhaust cleaning tower, asphalt smoke tail gas incineration system and process |
| WO2024112714A1 (en) * | 2022-11-22 | 2024-05-30 | Cameron International Corporation | Direct contact vaporizer |
| CN116899249B (en) * | 2023-09-13 | 2024-01-02 | 山西诚宏福得一化工有限公司 | Light benzene separation processing device and processing technology thereof |
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