CN211056995U

CN211056995U - Styrene production equipment

Info

Publication number: CN211056995U
Application number: CN201922234729.6U
Authority: CN
Inventors: 吕鸿博
Original assignee: Individual
Current assignee: Individual
Priority date: 2019-12-13
Filing date: 2019-12-13
Publication date: 2020-07-21
Anticipated expiration: 2029-12-13

Abstract

The utility model discloses a styrene production facility, including reaction unit, rectification separator and material recovery unit, behind the reaction unit was located to the rectification separator, material recovery unit locates behind the reaction unit and parallel with the rectification separator, reaction unit is including consecutive tar delivery pump, exhaust-heat boiler, ethylbenzene heater, material blender, negative pressure adiabatic reactor, ethylbenzene preheater, reactant condenser and phase splitter. The utility model belongs to the technical field of styrene production, specifically indicate a styrene production facility of energy consumption and material consumption in the reduction production process.

Description

Styrene production equipment

Technical Field

The utility model belongs to the technical field of styrene production, specifically indicate a styrene production facility.

Background

Styrene is an important monomer of polymer synthetic materials, and is widely applied to the industrial fields of pharmacy, coating, prevention and the like. In the prior art, the production method of styrene mainly uses ethylbenzene as a raw material, styrene is finally obtained through dehydrogenation, benzene and toluene recovery, ethylbenzene recovery and styrene rectification, and excessive energy consumption and material loss exist in the production process. Therefore, there is a need for an energy efficient styrene production facility.

Application number 201820077939.1's patent application discloses a styrene production facility, including consecutive heating furnace, dehydrogenation adiabatic reactor, exhaust-heat boiler, condensation splitter group, ethylbenzene evaporation tower, benzene and toluene recovery tower, benzene and toluene knockout tower and the styrene rectifying column that links to each other with ethylbenzene evaporation tower delivery outlet, the ethylbenzene intake pipe of dehydrogenation adiabatic reactor, the styrene output tube of styrene rectifying column, the ethylbenzene output tube of benzene and toluene recovery tower pass through the three-way valve and link to each other, styrene rectifying column tar delivery outlet even has the flash tank, and this patent application does not relate to the relevant equipment that energy consumption and hydrogen smuggle secretly and cause material loss, has too big energy consumption and material loss in the production process.

Disclosure of Invention

In order to solve the existing problems, the invention provides styrene production equipment capable of reducing energy consumption and material consumption in the production process.

The utility model discloses the technical scheme who takes as follows: a styrene production device comprises a reaction device, a rectification separation device and a material recovery device, wherein the rectification separation device is arranged behind the reaction device, the material recovery device is arranged behind the reaction device and is parallel to the rectification separation device, the reaction device comprises a tar delivery pump, a waste heat boiler, an ethylbenzene heater, a material mixer, a negative pressure adiabatic reactor, an ethylbenzene preheater, a reactant condenser and a phase splitter which are sequentially connected, the phase splitter is provided with a hydrogen discharge pipe, an oil phase discharge pipe and a water phase discharge pipe, the rectification separation device comprises an ethylbenzene recovery tower and a styrene refining tower which are sequentially connected, the ethylbenzene recovery tower is connected with the oil phase discharge pipe, the ethylbenzene recovery tower is provided with a benzene and toluene discharge pipe, an ethylbenzene discharge pipe and a styrene and tar discharge pipe, the ethylbenzene discharge pipe is provided with an ethylbenzene mixer, and fresh ethylbenzene is gathered through the ethylbenzene mixer, the ethylbenzene mixer is connected with an ethylbenzene preheater, the styrene refining tower is connected with styrene and a tar discharging pipe, the styrene refining tower is provided with the styrene discharging pipe, the tar discharging pipe and a tar conveying pipe, one end of the tar conveying pipe is connected to the tar discharging pipe, the other end of the tar conveying pipe is connected to a tar conveying pump, the material recovery device comprises a hydrogen compressor, a hydrogen deep cooler and an adsorption tower which are sequentially connected, the hydrogen compressor is connected with the hydrogen discharging pipe, and a condensate down sliding pipe is arranged at the bottom of the hydrogen deep cooler.

Furthermore, the ethylbenzene recovery tower is a clapboard rectifying tower, so that heat coupling in the tower is realized, and the reduction of steam consumption is facilitated.

Furthermore, polymerization inhibitor injection pipes are arranged at the tops of the ethylbenzene recovery tower and the styrene refining tower.

Furthermore, the vacuum degrees of the negative pressure adiabatic reactor, the phase separator, the ethylbenzene recovery tower and the styrene refining tower are sequentially increased, and materials can be automatically conveyed among the devices under the action of pressure difference.

Furthermore, the number of the adsorption towers is more than one, so that the switching is convenient when the device runs.

Furthermore, the tar conveying pipe is a jacketed pipe and is heated by hot steam to prevent tar from cooling and blocking the pipeline.

Adopt the utility model discloses the beneficial effect who gains as follows: the utility model provides a styrene production facility retrieves the reactant heat through the ethylbenzene preheater to and the ethylbenzene recovery tower realizes that the in-tower thermal coupling reduces steam consumption, thereby realizes reducing the energy consumption in the production process, through injecting the catalyst at ethylbenzene recovery tower and styrene refining tower top, reduce in the tower styrene auto-polymerization and carry the recovery of material and reduce the material consumption in the production process to hydrogen.

Drawings

FIG. 1 is a flow chart of the styrene production equipment of the present invention.

The system comprises a reaction device 1, a rectification separation device 2, a material recovery device 3, a material recovery device 4, a tar delivery pump 5, a waste heat boiler 6, an ethylbenzene heater 7, a material mixer 8, a negative pressure adiabatic reactor 9, an ethylbenzene preheater 10, a reactant condenser 11, a phase separator 12, a hydrogen discharge pipe 13, an oil phase discharge pipe 14, a water phase discharge pipe 15, an ethylbenzene recovery tower 16, a styrene refining tower 17, a benzene and toluene discharge pipe 18, an ethylbenzene discharge pipe 19, a styrene and tar discharge pipe 20, an ethylbenzene mixer 21, a styrene discharge pipe 22, a tar discharge pipe 23, a tar delivery pipe 24, a hydrogen compressor 25, a hydrogen deep cooler 26, an adsorption tower 27, a condensate slip pipe 28 and a polymerization inhibitor injection pipe.

In FIG. 1, a, process water, b, fresh ethylbenzene, c, superheated steam, d, polymerization inhibitor, e, benzene, f, ethylbenzene, g, styrene, h, hydrogen, i, toluene, j, tar.

Detailed Description

The technical solutions of the present invention will be further described in detail with reference to specific implementations, and all the portions of the present invention not described in detail are the prior art.

The present invention will be described in further detail with reference to the accompanying drawings.

As shown in figure 1, the utility model relates to a styrene production facility, including reaction unit 1, rectification separator 2 and material recovery unit 3, rectification separator 2 locates behind the reaction unit 1, material recovery unit 3 locates behind the reaction unit 1 and parallel with rectification separator 2, reaction unit 1 is including consecutive tar delivery pump 4, exhaust-heat boiler 5, ethylbenzene heater 6, material blender 7, negative pressure adiabatic reactor 8, ethylbenzene preheater 9, reactant condenser 10 and phase splitter 11, phase splitter 11 is equipped with hydrogen discharging pipe 12, oil phase discharging pipe 13 and water phase discharging pipe 14, separation unit 2 is including consecutive ethylbenzene recovery tower 15 and styrene refining tower 16, ethylbenzene recovery tower 15 is connected in oil phase discharging pipe 13, ethylbenzene recovery tower 15 is equipped with benzene and toluene discharging pipe 17, benzene discharging pipe 14, Ethylbenzene discharging pipe 18 and styrene and tar discharging pipe 19, ethylbenzene discharging pipe 18 is equipped with ethylbenzene mixer 20, ethylbenzene mixer 20 links to each other with ethylbenzene preheater 9, styrene refining tower 16 is connected in styrene and tar discharging pipe 19, styrene refining tower 16 is equipped with styrene discharging pipe 21, tar discharging pipe 22 and tar conveyer pipe 23, tar conveyer pipe 23 one end links to each other with tar discharging pipe 22, the tar conveyer pipe 23 other end links to each other with tar delivery pump 4, material recovery unit 3 is including consecutive hydrogen compressor 24, hydrogen deep cooler 25 and adsorption tower 26, hydrogen compressor 24 links to each other with hydrogen discharging pipe 12, hydrogen deep cooler 25 bottom is equipped with slip pipe 27 under the condensate.

The ethylbenzene recovery column 15 is a baffle distillation column.

And polymerization inhibitor injection pipes 28 are arranged at the tops of the ethylbenzene recovery tower 15 and the styrene refining tower 16.

The vacuum degrees of the negative pressure adiabatic reactor 8, the phase separator 11, the ethylbenzene recovery tower 15 and the styrene refining tower 16 are increased in sequence.

The number of the adsorption columns 26 is more than one.

The tar conveying pipe 23 is a jacketed pipe.

When the process water is used specifically, the process water is heated by a waste heat boiler 5 to generate steam, in an ethylbenzene heater 6, the ethylbenzene is heated by the steam, a certain amount of steam and the ethylbenzene are mixed in a material mixer 7 and enter a negative pressure adiabatic reactor 8 to react, the surplus steam is supplied to a rectification system, the reacted material preheats the mixed ethylbenzene by an ethylbenzene preheater 9 to recover energy, the heat-exchanged material is further cooled by a reactant condenser 10 and subjected to oil-water separation by a phase separator 11, hydrogen generated in the system flows out of a hydrogen discharge pipe 12 and enters a material recovery device 3, a water phase is discharged from a water phase discharge pipe 14 to be treated, an oil phase flows out of an oil phase discharge pipe 13 and enters an ethylbenzene recovery tower 15, a polymerization inhibitor is injected from a polymerization inhibitor injection pipe 28 to inhibit styrene from self polymerization, benzene and toluene are extracted from a benzene and toluene discharge pipe 17, the recovered ethylbenzene is extracted from an ethylbenzene discharge pipe 18, the recovered ethylbenzene is mixed with fresh ethylbenzene in an ethylbenzene mixer 20 and then enters an ethylbenzene preheater 9, styrene and tar enter a styrene refining tower 16 through a styrene and tar discharge pipe 19, a styrene product obtained through separation is extracted from a styrene discharge pipe 21, tar is sent into a waste heat boiler 5 through a tar discharge pipe 22 along a tar delivery pipe 23 through a tar delivery pump 4 to generate steam, in order to prevent tar from being cooled and coked in the delivery process, the tar delivery pipe 23 adopts a jacket pipe, steam is introduced into the jacket for heat preservation, hydrogen flowing out from a hydrogen discharge pipe 12 is pressurized by a compressor and then enters a hydrogen deep cooler 25 for deep cooling, and benzene carried by the hydrogen is condensed and recovered, toluene and styrene material, the lime set flows into ethylbenzene recovery tower 15 along the lime set pipe and separates, and the noncondensable hydrogen that flows out from hydrogen deep cooler 25 gets into hydrogen adsorption tower 26, adsorbs the trace organic matter that the hydrogen was smugglied secretly.

The present invention and its embodiments have been described above, and the description is not intended to be limiting, and the drawings are only one embodiment of the present invention, and the actual structure is not limited thereto. In summary, those skilled in the art should appreciate that they can readily use the disclosed conception and specific embodiments as a basis for designing or modifying other structures for carrying out the same purposes of the present invention without departing from the spirit and scope of the invention as defined by the appended claims.

Claims

1. A styrene production equipment is characterized in that: the device comprises a reaction device, a rectification separation device and a material recovery device, wherein the rectification separation device is arranged behind the reaction device, the material recovery device is arranged behind the reaction device and is parallel to the rectification separation device, the reaction device comprises a tar delivery pump, a waste heat boiler, an ethylbenzene heater, a material mixer, a negative pressure adiabatic reactor, an ethylbenzene preheater, a reactant condenser and a phase splitter which are sequentially connected, the phase splitter is provided with a hydrogen discharge pipe, an oil phase discharge pipe and a water phase discharge pipe, the rectification separation device comprises an ethylbenzene recovery tower and a styrene refining tower which are sequentially connected, the ethylbenzene recovery tower is connected with the oil phase discharge pipe, the ethylbenzene recovery tower is provided with a benzene and toluene discharge pipe, an ethylbenzene discharge pipe and a styrene and tar discharge pipe, the ethylbenzene discharge pipe is provided with an ethylbenzene mixer, and the ethylbenzene mixer is connected to the ethylbenzene preheater, the styrene refining tower is connected in styrene and tar discharging pipe, the styrene refining tower is equipped with styrene discharging pipe, tar discharging pipe and tar conveyer pipe, tar conveyer pipe one end links to each other with the tar discharging pipe, the tar conveyer pipe other end links to each other with the tar delivery pump, material recovery unit is including consecutive hydrogen compressor, hydrogen deep cooler and adsorption tower, the hydrogen compressor links to each other with the hydrogen discharging pipe, hydrogen deep cooler bottom is equipped with the slip pipe under the condensate.

2. The styrene production apparatus according to claim 1, wherein: the ethylbenzene recovery tower is a clapboard rectifying tower.

3. The styrene production apparatus according to claim 1, wherein: and polymerization inhibitor injection pipes are arranged at the tops of the ethylbenzene recovery tower and the styrene refining tower.

4. The styrene production apparatus according to claim 1, wherein: the vacuum degrees of the negative pressure adiabatic reactor, the phase separator, the ethylbenzene recovery tower and the styrene refining tower are increased in sequence.

5. The styrene production apparatus according to claim 1, wherein: the number of the adsorption columns is more than one.

6. The styrene production apparatus according to claim 1, wherein: the tar conveying pipe is a jacketed pipe.