CN208541823U - A variable load system for benzene distillation unit - Google Patents

Abstract

A kind of varying duty system for benzene distillation device, including pressurization tower reboiler, pressurizing tower condenser, pressurizing tower, atmospheric tower, benzene vapour pipe, benzene condensate line；The pressurization tower reboiler is located at pressurizing tower bottom outside, pressurizing tower condenser is located on the outside of atmospheric tower bottoms, benzene vapour pipe both ends connect pressurization tower top and connect pressurizing tower condenser and pressurizing tower benzene condensate drum with pressurizing tower condenser inlet end, benzene vapour pipe both ends.

Description

A kind of varying duty system for benzene distillation device

Technical field

The utility model relates to mixture rectifying separation fields, and in particular to contain light component benzene and other heavy constituent impurity Benzene distillation system.

Background technique

In chemical field, rectifying is a kind of well known chemical industry operation technology, different for separating two or more boiling points Substance.Such as the rectifying separation during caprolactam refining containing benzol mixture, although single tower distillation can isolate benzene at present, But the quantity of steam of consumption is larger, while also needing using a large amount of circulating water gaseous phase materials, unfavorable the mount of using heat makes full use of, Energy consumption cost is higher.Although traditional double-effect rectification can reduce steam consumption, but influenced by two tower heat balances, it is necessary to double Tower is run simultaneously, and integral load is restricted by the load of atmospheric tower, can not improve pressurizing tower load, to constrain economic benefits and social benefits steaming Evaporate the controllability and flexibility of operation.

Summary of the invention

The purpose of this utility model is will be while meeting normal rectifying separation requirement, under the conditions of realization different load Production.

The purpose of utility model is achieved in that

A kind of varying duty system for benzene distillation device, including pressurization tower reboiler, pressurizing tower condenser, pressurizing tower, Atmospheric tower, the first benzene vapour pipe, benzene the first benzene condensate line；The pressurization tower reboiler is located at pressurizing tower bottom outside, pressurization Tower condenser is located on the outside of atmospheric tower bottoms, the first benzene vapour pipe both ends connection is pressurizeed tower top and pressurizing tower condenser air inlet End, the first benzene vapour pipe both ends connection pressurizing tower condenser and pressurizing tower benzene condensate drum.

Slot is pumped including benzene distillation cooler and benzene, it is cooling that benzene distillation feed exchanger shell bottom discharge connects benzene distillation Device, benzene distillation cooler bottom discharge connect benzene and pump groove top portion.

Including product primary heater and product secondary heater, benzene distillation feed exchanger feed end connects crude benzol charging Pipe, benzene distillation feed exchanger discharge end connects product primary heater feed end, the connection of product primary heater discharge end produces Product secondary heater feed end.

Including pressurizing tower feed pipe, pressurizing tower feed pipe both ends connect product secondary heater and pressurizing tower.

Further include pressurizing tower benzene condensate drum, pressurizing tower benzene condensate drum bottom discharge pipe connect product primary heater into Expect end, product primary heater discharge end is connect with benzene distillation cooler bottom discharge pipe.

Blow-down pipe is equipped on benzene distillation feed exchanger.

Including atmospheric tower feed pipe, atmospheric tower feed pipe both ends connect product primary heater and atmospheric tower.

Including steam pipe, steam condensate pipe, steam condensate tank, steam pipe connects the connection of the first benzene vapour pipe, steam Condensate line both ends connect steam condensate tank and the first benzene vapour pipe；

Including the second benzene vapour pipe, the second benzene condensate line, second benzene vapour pipe one end connects product secondary heater, the Hexichol condensate line both ends connection connection product secondary heater and pressurizing tower benzene condensate drum.

By adopting the above technical scheme, following technical effect can be brought:

1) it by pressurizing tower series connection atmospheric tower operation, is heated using pressurizing tower reboiler steam, steams benzene in pressurizing tower Gas partial rectification, benzene vapor continue to heat benzene in atmospheric tower by pressurizing tower condenser, itself cooling recycling condenses liquid bath with benzene, Atmospheric tower benzene vapour is cooling after being exchanged heat by feed exchanger and charging, after the refining benzene heat exchange of pressurizing tower and atmospheric tower stationary stream All it is recovered to benzene pump slot；

2) by benzene pipeline, the cooperation of steam pipe line, steam condensate (SC) pipeline, steam condensate slot can close and add It presses the charging of tower to close the door, is opened to the benzene pipeline of atmospheric tower, is heated using steam pipe line, in underload, only open normal pressure Tower rectifying；

3) cooperation for passing through benzene vapour pipeline, benzene condensate liquid pipeline, product secondary heater, by opening benzene vapour pipe Line, benzene condensate line, can be improved pressurizing tower load, increase the rectifying amount of benzene, improve refining benzene yield.

Generally speaking, compared with prior art, benzene distillation system provided by the utility model can be in excess load and low negative Lotus benzin evaporates, and meets different duty requirements.It is effectively saved the energy.

Detailed description of the invention

The utility model is described in further detail with reference to the accompanying drawings and examples:

Fig. 1 is the structural schematic diagram of the embodiments of the present invention 1.

Specific embodiment

As shown in Figure 1, a kind of varying duty system for benzene distillation device, including pressurization tower reboiler 1, pressurizing tower condensation Device 2, pressurizing tower 3, atmospheric tower 4, the first benzene vapour pipe 19, the first benzene condensate line 20；The pressurization tower reboiler 1 is located at pressurization 3 bottom outside of tower, pressurizing tower condenser 2 are located at 4 bottom outside of atmospheric tower, 19 both ends of the first benzene vapour pipe connection pressurizing tower 3 top with 2 inlet end of pressurizing tower condenser, 19 both ends of the first benzene vapour pipe connect pressurizing tower condenser 2 and pressurizing tower benzene is cold Lime set tank 9.

It further include benzene distillation cooler 8 and benzene pump slot 13,7 shell bottom discharge of benzene distillation feed exchanger connects benzene distillation Cooler 8,8 bottom discharge of benzene distillation cooler connect 13 top of benzene pump slot.

Including product primary heater 6 and product secondary heater 5,7 feed end of benzene distillation feed exchanger connects crude benzol Feed pipe, 7 discharge end of benzene distillation feed exchanger connect 6 feed end of product primary heater, 6 discharge end of product primary heater Connect 5 feed end of product secondary heater.

Including pressurizing tower feed pipe 15,15 both ends of pressurizing tower feed pipe connect product secondary heater 5 and pressurizing tower 3.

It further include pressurizing tower benzene condensate drum 9,9 bottom discharge pipe of pressurizing tower benzene condensate drum connects product primary heater 6 feed ends, 6 discharge end of product primary heater are connect with 8 bottom discharge pipe of benzene distillation cooler.

Blow-down pipe 18 is equipped on benzene distillation feed exchanger 7, the blow-down pipe 18 is diameter DN80, long 1.5 meters of pipe Road.

Including atmospheric tower feed pipe 14,14 both ends of atmospheric tower feed pipe connect product primary heater 6 and atmospheric tower 4.

Including steam pipe 11, steam condensate pipe 12, steam condensate tank 10, steam pipe 11 connects the first benzene vapour pipe 19 Connection, 12 both ends of steam condensate pipe connect steam condensate tank 10 and the first benzene vapour pipe 19；

Including the second benzene vapour pipe 16, the second benzene condensate line 17,16 one end of the second benzene vapour pipe connects product second and adds Hot device 5,17 both ends of the second benzene condensate line connect product secondary heater 5 and pressurizing tower benzene condensate drum 9.

Application method one: crude benzol is pumped into pressurizing tower, pressurizing tower is heated to 120-150 DEG C with steam, pressurizing tower The voltage-controlled system of tower waits until part refining benzene in 0.2-0.35MPa, and bottom crude benzol is pressed into atmospheric tower by pressurization pressure tower, is passed through The heating of pressurizing tower benzene vapour, atmospheric tower crude benzol is distilled, and is controlled 85-90 DEG C of bottom temperature, 81 DEG C of tower top temperature, is obtained refining benzene.

Application method two: crude benzol is pumped into atmospheric tower, crude benzol without pressurizing tower, product primary heater, Steam is passed through the heating of pressurizing tower condenser, using atmospheric tower rectifying, controls 85-90 DEG C of bottom temperature by product secondary heater, 81 DEG C of tower top temperature, obtain refining benzene.

Application method three: crude benzol is pumped into pressurizing tower, pressurizing tower is heated to 120-150 DEG C with steam, pressurizing tower The voltage-controlled system of tower is divided into two-way, it is cold with pressurizing tower to respectively enter product secondary heater in 0.2-0.35MPa, the tower top benzene vapour that pressurizes In condenser, into the benzene vapour heating charging crude benzol of product secondary heater, heated by the benzene vapour of pressurizing tower condenser normal Tower crude benzol is pressed, pressurization tower bottom crude benzol is pressed into atmospheric tower using pressurizing tower and atmospheric tower pressure difference, atmospheric tower crude benzol steams It evaporates, control 85-90 DEG C of bottom temperature, 81 DEG C of tower top temperature.Obtain refining benzene.

It is obvious to a person skilled in the art that the present invention is not limited to the details of the above exemplary embodiments, and And without departing substantially from the spirit or essential attributes of the utility model, it can realize that this is practical new in other specific forms Type.Therefore, in all respects, the present embodiments are to be considered as illustrative and not restrictive, this is practical new The range of type is indicated by the appended claims rather than the foregoing description, it is intended that containing for the equivalent requirements of the claims will be fallen in All changes in justice and range are embraced therein.It should not treat any reference in the claims as limiting Related claim.

Claims (9)

1. A variable load system for a benzene distillation plant, characterized in that: comprising a pressurized tower reboiler (1), a pressurized tower condenser (2), a pressurized tower (3), an atmospheric tower (4) ), the first benzene vapor pipe (19), the first benzene condensate pipe (20); the pressurized tower reboiler (1) is located outside the bottom of the pressurized tower (3), and the pressurized tower condenser (2) Located on the outside of the bottom of the atmospheric tower (4), both ends of the first benzene vapor pipe (19) are connected to the top of the pressurized tower (3) and the inlet end of the pressurized tower condenser (2), and the first benzene vapor pipe (19) Both ends are connected to the pressurized tower condenser (2) and the pressurized tower benzene condensate tank (9). 2. The variable load system for a benzene distillation plant according to claim 1, characterized in that: further comprising a benzene distillation cooler (8) and a benzene pump tank (13), a benzene distillation feed heat exchanger (7) The bottom discharge of the shell layer is connected to the benzene distillation cooler (8), and the bottom discharge of the benzene distillation cooler (8) is connected to the top of the benzene pump tank (13). 3. The variable load system for a benzene distillation plant according to claim 1 or 2, characterized in that: it comprises a first product heater (6) and a second product heater (5), and the benzene distillation feed is heat-exchanged The feed end of the device (7) is connected to the crude benzene feed pipe, and the discharge end of the benzene distillation feed heat exchanger (7) is connected to the feed end of the first product heater (6) and the discharge end of the first product heater (6). The end is connected to the feed end of the product second heater (5). 4. The variable load system for a benzene distillation device according to claim 1 or 2, characterized in that it comprises a feed pipe (15) of a pressurizing tower, and both ends of the feed pipe (15) of the pressurizing tower are connected to the product No. Two heaters (5) and pressurizing towers (3). 5. The variable load system for a benzene distillation device according to claim 1 or 2, characterized in that: it also comprises a pressurized tower benzene condensate tank (9), and the bottom of the pressurized tower benzene condensate tank (9) exits The feed pipe is connected to the feed end of the first product heater (6), and the discharge end of the first product heater (6) is connected to the bottom discharge pipe of the benzene distillation cooler (8). 6 . The variable load system for a benzene distillation unit according to claim 2 , wherein a vent pipe ( 18 ) is provided on the benzene distillation feed heat exchanger ( 7 ). 7 . 7. The variable load system for a benzene distillation unit according to claim 3, characterized in that it comprises an atmospheric tower feed pipe (14), and both ends of the atmospheric tower feed pipe (14) are connected to the first heating product of the product device (6) and atmospheric tower (4). 8. The variable load system for a benzene distillation plant according to claim 1 or 2, characterized in that it comprises a steam pipe (11), a steam condensate pipe (12), a steam condensate tank (10), a steam pipe (11) The first benzene steam pipe (19) is connected, and both ends of the steam condensate pipe (12) are connected to the steam condensate tank (10) and the first benzene steam pipe (19). 9. The variable load system for a benzene distillation plant according to claim 3, characterized in that it comprises a second benzene steam pipe (16), a second benzene condensate pipe (17), a second benzene steam pipe (16) ) is connected to the second product heater (5) at one end, and both ends of the second benzene condensate pipe (17) are connected to the product second heater (5) and the pressurized tower benzene condensate tank (9).