CN106083512A - A kind of apparatus and method being prepared benzene and dimethylbenzene by toluene and heavy aromatics - Google Patents
A kind of apparatus and method being prepared benzene and dimethylbenzene by toluene and heavy aromatics Download PDFInfo
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- CN106083512A CN106083512A CN201610625325.8A CN201610625325A CN106083512A CN 106083512 A CN106083512 A CN 106083512A CN 201610625325 A CN201610625325 A CN 201610625325A CN 106083512 A CN106083512 A CN 106083512A
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C6/00—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions
- C07C6/08—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond
- C07C6/12—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond of exclusively hydrocarbons containing a six-membered aromatic ring
- C07C6/126—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond of exclusively hydrocarbons containing a six-membered aromatic ring of more than one hydrocarbon
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Abstract
The invention discloses a kind of apparatus and method being prepared benzene and dimethylbenzene by toluene and heavy aromatics.Reactor is sent into after toluene, heavy aromatics and hydrogen being preheated, product is after cooling, gas phase and liquid phase two streams it is divided in knockout drum, gaseous stream is after low-temperature reformate oil heat exchanger and refrigerator freeze, enter freezing contact tank, the impurity carried in hydrogen after removing reaction, hydrogen uses through compressor boosting Posterior circle.Knockout drum liquid phase stream enters stripper after heat exchange, and stripping tower bottom liquid fraction enters benzene column rectification and obtains benzene, enters back into toluene tower rectification and reclaims toluene and lay equal stress on raw feed；Toluene tower bottom liquid enters benzenol hydrorefining rectification and obtains dimethylbenzene, and heavy aromatics at the bottom of benzenol hydrorefining is delivered to feed(raw material)inlet and again fed.The present invention, on the premise of the concentration maintaining reaction hydrogen and dividing potential drop, decreases the new hydrogen amount of filling into and the impact on subsequent technique, on the basis of obtaining high-purity benzene and dimethylbenzene, it is achieved that toluene and whole recyclings of heavy aromatics.
Description
Technical field
The invention belongs to petrochemical industry production field, more particularly to a kind of by toluene and heavy aromatics prepare benzene and
The apparatus and method of dimethylbenzene.
Background technology
Along with expanding economy, the consumption of benzene and dimethylbenzene chemical products is increased by China year by year.Domestic enterprise many with
Reformed Gasoline is raw material, produce the products such as benzene, xylol and o-Dimethylbenzene, but by-product toluene and C9/C10 and above
Heavy aromatics.Alkyl migrating technology utilizes cheap toluene and heavy aromatics for raw material, and shape selective catalysis generates benzene and dimethylbenzene, then leads to
Cross simple benzene and the dimethylbenzene separating and can be obtained by high added value.Therefore remarkable in economical benefits.Existing toluene and weight virtue
Hydrocarbon alkyl migrating technology, by filling into new hydrogen continuously, the useless hydrogen of discharge low-purity, maintain the concentration of hydrogen and divide
Pressure, hydrogen content 70% in useless hydrogen, cause the serious waste of hydrogen；Some enterprises pass through supporting PSA pressure swing adsorption system pair
This part hydrogen that gives up reclaims, but due in useless hydrogen containing a small amount of C5 component, especially alkyl migrate technique produce fluctuation time,
C5 content is higher, and this part C5 can cause PSA pressure-variable adsorption agent to inactivate.Therefore, need a kind of method of research badly, both can reduce first
Benzene and heavy aromatics alkyl migrate hydrogen gas consumption, reduce cost, can eliminate again the impact on PSA or subsequent technique.
Summary of the invention
The deficiency existed for prior art, it is an object of the invention to provide a kind of by toluene and heavy aromatics prepare benzene and
The apparatus and method of dimethylbenzene, are utilized toluene and heavy aromatics alkyl migration to prepare benzene and dimethylbenzene, are contacted by freezing and aromatic hydrocarbons
Fractional distillation realizes the circulation of toluene and heavy aromatics, it is achieved the high concentration circulation of recycle hydrogen, reduces the amount of filling into of new hydrogen, it is ensured that reaction
The degree of depth and the selectivity of target product.
For achieving the above object, the technical scheme is that one is prepared benzene and two by toluene and heavy aromatics
The device of toluene, including feed exchanger, charging heating furnace, reactor, air cooler, knockout drum, low-temperature reformate oil heat exchange
Effluent exchanger, stripping at the bottom of device, refrigerator, freezing contact tank, circulating hydrogen compressor, stripper overhead heat exchanger, stripper tower
Tower, benzene column, toluene tower and benzenol hydrorefining；Feedstock pipeline is connected with the first charging aperture of feed exchanger, and described charging is changed
First discharging opening of hot device is connected with the charging aperture of charging heating furnace, the discharging opening of described charging heating furnace and the charging of reactor
Mouth is connected, and the discharging opening of described reactor is connected with the second charging aperture of feed exchanger, and the second of described feed exchanger goes out
Material mouth is connected with the charging aperture of air cooler, and the discharging opening of described air cooler is connected with the charging aperture of knockout drum, described gas-liquid
The gas phase discharging opening of knockout drum is connected with the first charging aperture of low-temperature reformate oil heat exchanger, going out of described low-temperature reformate oil heat exchanger
Material mouth is connected with the charging aperture of refrigerator, and the discharging opening of described refrigerator is connected with the charging aperture of freezing contact tank, described freezing
The gas phase discharging opening of contact tank is connected with circulating hydrogen compressor, and liquid phase discharging opening and the low-temperature reformate oil of described freezing contact tank change
Second charging aperture of hot device is connected, and described low-temperature reformate oil heat exchanger is provided with the second discharging opening, described circulating hydrogen compressor
Discharging opening fill into pipeline with new hydrogen and be connected, the liquid phase discharging opening of described knockout drum and the first of stripper overhead heat exchanger
Charging aperture is connected, the first charging aperture of effluent exchanger at the bottom of the first discharging opening of described stripper overhead heat exchanger and stripper tower
Being connected, at the bottom of described stripper tower, the first discharging opening of effluent exchanger is connected with the first charging aperture of stripper；Described stripper
The first discharging opening and the first pump entry be connected, effluent exchanger second at the bottom of described first circulating-pump outlet and stripper tower
Charging aperture is connected, and the second discharging opening of described stripper is connected with the second charging aperture of stripper overhead heat exchanger, described stripping
Second discharging opening of column overhead heat exchanger is connected with the charging aperture of fluid reservoir, the discharging opening of described fluid reservoir and the second circulating pump
Entrance is connected, and the discharging opening of described second circulating pump is connected with the second charging aperture of stripper, described second circulating pump and stripping
It is provided with light component blowing pipeline on connection pipeline between tower, described light component blowing pipeline is provided with electromagnetic valve, described
Second discharging opening of effluent exchanger at the bottom of stripper tower is connected with the charging aperture of benzene column；Discharging opening and toluene tower at the bottom of described benzene column tower
Charging aperture be connected, described benzene column is provided with tower top discharging opening, entering of discharging opening at the bottom of the tower of described toluene tower and benzenol hydrorefining
Material mouth is connected, and described toluene tower tower top discharging opening is connected with feedstock pipeline, discharging opening at the bottom of the tower of described benzenol hydrorefining and former
Material feeding line is connected, and described benzenol hydrorefining is provided with tower top discharging opening.
As a further improvement on the present invention, the conveyance conduit between described freezing contact tank and circulating hydrogen compressor connects
Being connected to tee T, three branch roads of tee T are provided with electromagnetic valve, tee T one end is connected with conveyance conduit, and another two ends are divided
Not Lian Jie a metal hydride hydrogen storage unit, described metal hydride hydrogen storage unit is provided with first exhaust pipeline and second
Electromagnetic valve, described first exhaust pipeline and circulation it is respectively arranged with on discharge duct, first exhaust pipeline and second exhaust pipeline
Hydrogen compressor charging aperture is connected.
As a further improvement on the present invention, the conveyance conduit that described freezing contact tank discharging opening is connected is provided with dry
Device.
As a further improvement on the present invention, on described first exhaust pipeline, connection has hydrogen purification apparatus.
A kind of method being prepared benzene and dimethylbenzene by toluene and heavy aromatics, comprises the following steps:
A, by toluene, heavy aromatics and hydrogen mix after, through feed exchanger heat exchange to 350～400 DEG C, pressure
3.2MPa, subsequently into charging heating furnace heating, is warming up to 390～410 DEG C, pressure 3.1MPa；
B, entrance reactor reaction, reaction pressure is 1～3MPa, and reaction temperature is 350～450 DEG C；Hydrogen oil molecule mole
Ratio 3.0～4.5；Reaction velocity 3.0～3.5h-1；
C, product from reactor out after, be cooled to 110～130 DEG C through feed exchanger, pressure to 2.6～
2.8MPa, then it is cooled to 40～60 DEG C through air cooler, pressure to 2.0～2.6MPa, subsequently into knockout drum；
Product is divided into gas phase and liquid phase two streams by d, knockout drum, and gaseous stream is mainly impure hydrogen
Gas, liquid phase stream is mainly aromatic hydrocarbons mixture；
After e, gaseous stream mix with reformate, freeze through low-temperature reformate oil heat exchanger and refrigerator successively, subsequently into
Freezing contact tank, removes the light component materials carried in gaseous stream, and remaining gas part is directly entered circulating hydrogen compressor,
Additionally being partially into drying device, by controlling the switch of each electromagnetic valve, gas enters a metal the most afterwards from drying device
Hydride hydrogen storage device, hydrogen is absorbed by hydrogen storage material in metal hydride hydrogen storage unit, and residual impurity gas is from second exhaust
Bank of tubes goes out, and meanwhile, the hydrogen release of absorption is put by another metal hydride hydrogen storage unit, enters circulation hydrogen pressure by downtake pipe
Contracting machine, rises to 3.2～3.5Mpa from circulating hydrogen compressor out rear Hydrogen Vapor Pressure, is allowed to reenter with supplementing after new hydrogen mixes
Reaction system；
F, knockout drum liquid phase stream, after effluent exchanger at the bottom of stripper overhead heat exchange and stripper tower, enter stripping
Tower；
After g, stripper overhead fraction enter stripper overhead heat exchange cooling, entering fluid reservoir, part is at the second circulating pump
Effect under reenter stripper, remainder is discharged from light component blowing pipeline；
H, stripper tower bottom distillate are introduced into benzene column rectification, the tower top temperature of described benzene column 90 DEG C, column bottom temperature 145 DEG C,
Obtain benzene, reclaim unreacted toluene, the tower top temperature of described toluene tower 177 DEG C, column bottom temperature subsequently into toluene tower rectification
225 DEG C, the toluene that recovery obtains is delivered to feed(raw material)inlet and is again fed, and toluene tower bottom liquid finally enters benzenol hydrorefining, described diformazan
Benzene column tower top temperature 235 DEG C, pressure 0.634MPa, in benzenol hydrorefining, rectification obtains dimethylbenzene, heavy aromatics at the bottom of benzenol hydrorefining tower
Deliver to feed(raw material)inlet again feed.
As a further improvement on the present invention, the operating condition of described freezing contact tank is: temperature-15～-5 DEG C, pressure
1.5～2.5MPa.
As a further improvement on the present invention, the operating condition of described knockout drum is: temperature 40～60 DEG C, pressure
2.5～3.0MPa.
As a further improvement on the present invention, the operating condition of described stripper: feeding temperature 135～160 DEG C, tower top temperature
Spend 120～130 DEG C, tower top pressure 0.5～0.6MPa.
Recycle hydrogen is purified by the present invention, and partial impurities gas is got rid of response system, it is achieved recycle hydrogen highly concentrated
Degree circulation, reduces the amount of filling into of new hydrogen, it is ensured that the reaction depth of alkyl migration and the selectivity of target product, is maintaining reaction
On the premise of the concentration of hydrogen and dividing potential drop, greatly reduce the new hydrogen amount of filling into and the impact on subsequent technique.Alkyl is migrated
Product realizes the circulation of toluene and heavy aromatics by freezing contact and aromatic hydrocarbons fractional distillation, is obtaining high-purity benzene and dimethylbenzene
On the basis of, it is achieved that toluene and whole recyclings of heavy aromatics.System is decreased by the Optimum utilization of heat and cold
Energy consumption, further increases economic benefit.
Accompanying drawing explanation
Fig. 1 is the structural representation of apparatus of the present invention.
Detailed description of the invention
Below in conjunction with the embodiment given by accompanying drawing, the present invention is described in further detail.
With reference to shown in Fig. 1, a kind of device being prepared benzene and dimethylbenzene by toluene and heavy aromatics of the present embodiment, including charging
Heat exchanger 1, charging heating furnace 2, reactor 3, air cooler 4, knockout drum 5, low-temperature reformate oil heat exchanger 6, refrigerator 7, cold
Freeze effluent exchanger 11, stripper 12, benzene at the bottom of contact tank 8, circulating hydrogen compressor 9, stripper overhead heat exchanger 10, stripper tower
Tower 13, toluene tower 14 and benzenol hydrorefining 15；Feedstock pipeline is connected with the first charging aperture of feed exchanger 1, feeds heat exchange
First discharging opening of device 1 is connected with the charging aperture of charging heating furnace 2, the discharging opening of charging heating furnace 2 and the charging aperture of reactor 3
Being connected, raw material preheating given by feed exchanger 1 and charging heating furnace 2, and the discharging opening of reactor 3 and the second of feed exchanger 1 enter
Material mouth is connected, higher from reactor 3 product temperature out, carries out heat exchange by entering feed exchanger 1, fills heat
Dividing and utilize, reduce energy consumption, increase economic efficiency, the second discharging opening of feed exchanger 1 is connected with the charging aperture of air cooler 4, empty
Cooler 4 makes product lower the temperature further, and the discharging opening of air cooler 4 is connected with the charging aperture of knockout drum 5, knockout drum
Product is divided into gaseous stream and liquid phase stream, gaseous stream to be mainly impure hydrogen by 5, and impurity therein has carbon containing
Gas, nitrogenous gas, C5 and other light component materials, liquid phase stream is mainly aromatic hydrocarbons mixture, the virtue of mainly more than C6
Hydrocarbon, the gas phase discharging opening of knockout drum 5 is connected with the first charging aperture of low-temperature reformate oil heat exchanger 6, low-temperature reformate oil heat exchange
The discharging opening of device 6 is connected with the charging aperture of refrigerator 7, and the discharging opening of refrigerator 7 is connected with the charging aperture of freezing contact tank 8, cold
Freeze contact tank 8 and the C5 in hydrogen and other light component materials are cooled down condensation thus and Hydrogen Separation, the gas of freezing contact tank 8
Phase discharging opening is connected with circulating hydrogen compressor 9, and the conveyance conduit that freezing contact tank 8 discharging opening is connected is provided with drying device
19, the water in hydrogen is removed by drying device 19, and the conveyance conduit between freezing contact tank 8 and circulating hydrogen compressor 9 connects
Having tee T, three branch roads of tee T are provided with electromagnetic valve, tee T one end is connected with conveyance conduit, and another two ends are respectively
Connect a metal hydride hydrogen storage unit 18, metal hydride hydrogen storage unit 18 is provided with first exhaust pipeline and second row
Electromagnetic valve, first exhaust pipeline and recycle hydrogen compression it is respectively arranged with on feed channel, first exhaust pipeline and second exhaust pipeline
Machine 9 charging aperture is connected, and first exhaust pipeline connects to be had hydrogen purification apparatus 20, hydrogen purification apparatus 20 to remove in hydrogen to contain
Carbon gas or nitrogenous gas, if two metal hydride hydrogen storage unit 18 are respectively A hydrogen-storing device and B hydrogen-storing device, in work
Time, the tee T side electromagnetic valve that is connected with conveyance conduit is open mode, and the electromagnetic valve A between tee T and A hydrogen-storing device is for beat
Electromagnetic valve B between open state, and B hydrogen-storing device is closed mode, the second exhaust pipeline B solenoid on B hydrogen-storing device
For closed mode, first exhaust pipeline B solenoid is open mode, enters from freezing contact tank 8 gaseous stream part out
Entering circulating hydrogen compressor 9, be partially into A hydrogen-storing device, in A hydrogen-storing device, the hydrogen in gaseous stream is stored up by metal hydride
Hydrogen material adsorbs, and second exhaust pipeline A solenoid is open mode, and first exhaust pipeline A solenoid is closed mode, surplus
Remaining carbon containing or nitrogen-containing impurity gas are got rid of from second exhaust pipeline A, after arriving the PLC setting time, and tee T and A storage
Electromagnetic valve A between hydrogen production device transfers closedown to, and the electromagnetic valve A between tee T and B hydrogen-storing device transfers to and opening, meanwhile, and A
The first exhaust pipeline A solenoid of hydrogen-storing device transfers open mode to, and second exhaust pipeline A solenoid position transfers closedown shape to
State, the first exhaust pipeline B solenoid of B hydrogen-storing device transfers closed mode to, and second exhaust pipeline B solenoid position transfers to be beaten
Open state, is now partially into B hydrogen-storing device from freezing contact tank 8 gaseous stream out, has inhaled the A storage that hydrogen is saturated
Hydrogen production device transfers to puts hydrogen condition, starts to put hydrogen, and the hydrogen of releasing enters circulating hydrogen compressor 9, same mistake from first exhaust pipeline A
PLC, to the control of electromagnetic valve and the control of metal hydride hydrogen storage unit 18, makes two hydride hydrogen-storings
While device 18 is in suction hydrogen, another two metal hydride hydrogen storage unit 18 are in hydrogen state of putting, after suction hydrogen is saturated, and two
Transition switching between individual metal hydride hydrogen storage unit 18, and is released the reversible absorption of hydrogen by hydride hydrogen-storing material
Put, hydrogen is purified, partial impurities gas is discharged reaction system；The liquid phase discharging opening of freezing contact tank 8 and low temperature weight
Second charging aperture of whole oil heat exchanger 6 is connected, and low-temperature reformate oil heat exchanger 6 is provided with the second discharging opening, circulating hydrogen compressor 9
Discharging opening fill into pipeline with new hydrogen and be connected, the hydrogen of recovery reenters reaction system, the liquid phase discharging opening of knockout drum 5
It is connected with the first charging aperture of stripper overhead heat exchanger 10, the first discharging opening of stripper overhead heat exchanger 10 and stripper tower
First charging aperture of end effluent exchanger 11 is connected, the first discharging opening of effluent exchanger 11 at the bottom of stripper tower and stripper 12
First charging aperture is connected；First discharging opening of stripper 12 and the first pump entry are connected, the first circulating-pump outlet and stripping
Effluent exchanger 11 second charging aperture at the bottom of tower tower is connected, the of the second discharging opening of stripper 12 and stripper overhead heat exchanger 10
Two charging apertures are connected, and the second discharging opening of stripper overhead heat exchanger 10 is connected with the charging aperture of fluid reservoir 16, fluid reservoir 16
The entrance of discharging opening and the second circulating pump is connected, and the discharging opening of the second circulating pump is connected with the second charging aperture of stripper 12, the
It is provided with light component blowing pipeline 17 on connection pipeline between two circulating pumps and stripper 12, light component blowing pipeline 17 sets
Being equipped with electromagnetic valve, light component is discharged from stripper 12 out rear section, and part reenters stripper 12, thus improves productivity,
Second discharging opening of effluent exchanger 11 at the bottom of stripper tower is connected with the charging aperture of benzene column 13；Discharging opening and toluene at the bottom of benzene column 13 tower
The charging aperture of tower 14 is connected, and benzene column 13 is provided with tower top discharging opening, and products benzene is discharged from benzene column 13 tower top, the tower of toluene tower 14
End discharging opening is connected with the charging aperture of benzenol hydrorefining 15, and toluene tower 14 tower top discharging opening is connected with feedstock pipeline, from toluene
Tower 14 tower top toluene out can reenter reaction system, discharging opening at the bottom of the tower of benzenol hydrorefining 15 and feedstock pipeline phase
Even, benzenol hydrorefining 15 being provided with tower top discharging opening, product dimethylbenzene is discharged from benzenol hydrorefining 15 tower top, the tower of benzenol hydrorefining 15
End heavy aromatics out reenters reaction system.
Embodiment 2
A kind of method being prepared benzene and dimethylbenzene by toluene and heavy aromatics, it comprises the following steps:
A, by toluene, heavy aromatics and hydrogen mix after, through feed exchanger 1 heat exchange to 350 DEG C, pressure 3.2MPa,
Heat subsequently into charging heating furnace 2, be warming up to 390 DEG C, pressure 3.1MPa；
B, entrance reactor 3 react, and reaction pressure is 1MPa, and reaction temperature is 350 DEG C；Hydrogen oil molecule mol ratio 3.0；Instead
Answer air speed 3.0h-1；
C, product from reactor 3 out after, be cooled to 110 DEG C through feed exchanger 1, pressure is to 2.6MPa, then warp
Air cooler 4 is cooled to 40 DEG C, pressure to 2.0MPa, subsequently into knockout drum 5；
Product is divided into gas phase and liquid phase two streams by d, knockout drum 5, and gaseous stream is mainly impure
Hydrogen, liquid phase stream is mainly aromatic hydrocarbons mixture, and the operating condition of knockout drum 5 is: temperature 40 DEG C, pressure 2.5MPa.
After e, gaseous stream mix with reformate, freeze through low-temperature reformate oil heat exchanger 6 and refrigerator 7 successively, then enter
Enter freezing contact tank 8, cool the temperature to-10 DEG C, pressure to 1.5MPa, remove the light component materials carried in gaseous stream, surplus
Remaining gas part is directly entered circulating hydrogen compressor 9, is additionally partially into drying device 19, by controlling opening of each electromagnetic valve
Closing, gas enters a metal hydride hydrogen storage unit 18 the most afterwards from drying device 19, and hydrogen is filled by hydride hydrogen-storing
Putting hydrogen storage material in 18 to absorb, residual impurity gas is discharged from second exhaust pipe, meanwhile, and another metal hydride hydrogen storage unit
The hydrogen release of absorption is put by 18, enters circulating hydrogen compressor 9 by downtake pipe, from circulating hydrogen compressor 9 out rear hydrogen pressure
Power rises to 3.2Mpa, is allowed to reenter reaction system with supplementing after new hydrogen mixes；
F, knockout drum 5 liquid phase stream, after effluent exchanger 11 at the bottom of stripper overhead heat exchange 10 and stripper tower, enter
Entering stripper 12, the condition of stripper 12 is: feeding temperature 135 DEG C, tower top temperature 120 DEG C, tower top pressure 0.5MPa；
After g, stripper 12 overhead fraction enter stripper overhead heat exchange 10 cooling, entering fluid reservoir 16, part is second
Circulating pump effect under reenter stripper 12, remainder is discharged from light component blowing pipeline 17；
H, stripper 12 tower bottom distillate are introduced into benzene column 13 rectification, the tower top temperature of described benzene column 13 90 DEG C, column bottom temperature
145 DEG C, obtain benzene, reclaim unreacted toluene, the tower top temperature 177 of described toluene tower 14 subsequently into toluene tower 14 rectification
DEG C, column bottom temperature 225 DEG C, reclaim the toluene that obtains and deliver to feed(raw material)inlet and again feed, toluene tower 14 end liquid finally enters diformazan
Benzene column 15, described benzenol hydrorefining 15 tower top temperature 235 DEG C, pressure 0.634MPa, in benzenol hydrorefining 15, rectification obtains dimethylbenzene,
Heavy aromatics at the bottom of benzenol hydrorefining 15 tower is delivered to feed(raw material)inlet and is again fed.
Embodiment 3:
A kind of method being prepared benzene and dimethylbenzene by toluene and heavy aromatics, it comprises the following steps:
A, by toluene, heavy aromatics and hydrogen mix after, through feed exchanger 1 heat exchange to 400 DEG C, pressure 3.2MPa,
Heat subsequently into charging heating furnace 2, be warming up to 400 DEG C, pressure 3.1MPa；
B, entrance reactor 3 react, and reaction pressure is 3MPa, and reaction temperature is 450 DEG C；Hydrogen oil molecule mol ratio 4.5；Instead
Answer air speed 3.5h-1；
C, product from reactor 3 out after, be cooled to 130 DEG C through feed exchanger 1, pressure is to 2.8MPa, then warp
Air cooler 4 is cooled to 60 DEG C, pressure to 2.6MPa, subsequently into knockout drum 5；
Product is divided into gas phase and liquid phase two streams by d, knockout drum 5, and gaseous stream is mainly impure
Hydrogen, liquid phase stream is mainly aromatic hydrocarbons mixture, and the operating condition of knockout drum 5 is: temperature 60 C, pressure 3.0MPa；
After e, gaseous stream mix with reformate, freeze through low-temperature reformate oil heat exchanger 6 and refrigerator 7 successively, then enter
Enter freezing contact tank 8, cool the temperature to-5 DEG C, pressure to 2.5MPa, remove the light component materials carried in gaseous stream, residue
Gas part be directly entered circulating hydrogen compressor 9, be additionally partially into drying device 19, by controlling the opening of each electromagnetic valve
Closing, gas enters a metal hydride hydrogen storage unit 18 the most afterwards from drying device 19, and hydrogen is filled by hydride hydrogen-storing
Putting hydrogen storage material in 18 to absorb, residual impurity gas is discharged from second exhaust pipe, meanwhile, and another metal hydride hydrogen storage unit
The hydrogen release of absorption is put by 18, enters circulating hydrogen compressor 9 by downtake pipe, from circulating hydrogen compressor 9 out rear hydrogen pressure
Power rises to 3.5Mpa, is allowed to reenter reaction system with supplementing after new hydrogen mixes；
F, knockout drum 5 liquid phase stream, after effluent exchanger 11 at the bottom of stripper overhead heat exchange 10 and stripper tower, enter
Enter stripper 12, the operating condition of stripper 12: feeding temperature 160 DEG C, tower top temperature 130 DEG C, tower top pressure 0.6MPa；
After g, stripper 12 overhead fraction enter stripper overhead heat exchange 10 cooling, entering fluid reservoir 16, part is second
Circulating pump effect under reenter stripper 12, remainder is discharged from light component blowing pipeline 17；
H, stripper 12 tower bottom distillate are introduced into benzene column 13 rectification, the tower top temperature of described benzene column 13 90 DEG C, column bottom temperature
145 DEG C, obtain benzene, reclaim unreacted toluene, the tower top temperature 177 of described toluene tower 14 subsequently into toluene tower 14 rectification
DEG C, column bottom temperature 225 DEG C, reclaim the toluene that obtains and deliver to feed(raw material)inlet and again feed, toluene tower 14 end liquid finally enters diformazan
Benzene column 15, described benzenol hydrorefining 15 tower top temperature 235 DEG C, pressure 0.634MPa, in benzenol hydrorefining 15, rectification obtains dimethylbenzene,
Heavy aromatics at the bottom of benzenol hydrorefining 15 tower is delivered to feed(raw material)inlet and is again fed.
Embodiment 4
A kind of method being prepared benzene and dimethylbenzene by toluene and heavy aromatics, it comprises the following steps:
A, by toluene, heavy aromatics and hydrogen mix after, through feed exchanger 1 heat exchange to 380 DEG C, pressure 3.2MPa,
Heat subsequently into charging heating furnace 2, be warming up to 410 DEG C, pressure 3.1MPa；
B, entrance reactor 3 react, and reaction pressure is 2MPa, and reaction temperature is 380 DEG C；Hydrogen oil molecule mol ratio 3.5；Instead
Answer air speed 3.2h-1；
C, product from reactor 3 out after, be cooled to 120 DEG C through feed exchanger 1, pressure is to 2.7MPa, then warp
Air cooler 4 is cooled to 50 DEG C, pressure to 2.5MPa, subsequently into knockout drum 5；
Product is divided into gas phase and liquid phase two streams by d, knockout drum 5, and gaseous stream is mainly impure
Hydrogen, liquid phase stream is mainly aromatic hydrocarbons mixture, and the operating condition of knockout drum 5 is: temperature 50 C, pressure 2.8MPa；
After e, gaseous stream mix with reformate, freeze through low-temperature reformate oil heat exchanger 6 and refrigerator 7 successively, then enter
Enter freezing contact tank 8, cool the temperature to-10 DEG C, pressure to 2MPa, remove the light component materials carried in gaseous stream, residue
Gas part be directly entered circulating hydrogen compressor 9, be additionally partially into drying device 19, by controlling the opening of each electromagnetic valve
Closing, gas enters a metal hydride hydrogen storage unit 18 the most afterwards from drying device 19, and hydrogen is filled by hydride hydrogen-storing
Putting hydrogen storage material in 18 to absorb, residual impurity gas is discharged from second exhaust pipe, meanwhile, and another metal hydride hydrogen storage unit
The hydrogen release of absorption is put by 18, enters circulating hydrogen compressor 9 by downtake pipe, from circulating hydrogen compressor 9 out rear hydrogen pressure
Power rises to 3.3Mpa, is allowed to reenter reaction system with supplementing after new hydrogen mixes；
F, knockout drum 5 liquid phase stream, after effluent exchanger 11 at the bottom of stripper overhead heat exchange 10 and stripper tower, enter
Enter stripper 12, the operating condition of stripper 12: feeding temperature 150 DEG C, tower top temperature 125 DEG C, tower top pressure 0.6MPa.
After g, stripper 12 overhead fraction enter stripper overhead heat exchange 10 cooling, entering fluid reservoir 16, part is second
Circulating pump effect under reenter stripper 12, remainder is discharged from light component blowing pipeline 17；
H, stripper 12 tower bottom distillate are introduced into benzene column 13 rectification, the tower top temperature of described benzene column 13 90 DEG C, column bottom temperature
145 DEG C, obtain benzene, reclaim unreacted toluene, the tower top temperature 177 of described toluene tower 14 subsequently into toluene tower 14 rectification
DEG C, column bottom temperature 225 DEG C, reclaim the toluene that obtains and deliver to feed(raw material)inlet and again feed, toluene tower 14 end liquid finally enters diformazan
Benzene column 15, described benzenol hydrorefining 15 tower top temperature 235 DEG C, pressure 0.634MPa, in benzenol hydrorefining 15, rectification obtains dimethylbenzene,
Heavy aromatics at the bottom of benzenol hydrorefining 15 tower is delivered to feed(raw material)inlet and is again fed.
Knockout drum 5 gaseous stream is mainly composed of impure useless hydrogen, and purity is relatively low, can only portion in prior art
Dividing and recycle, major part hydrogen sends into fuel gas system burning as low value-added fuel.When alkyl migrates technique richness material
During charging, the most about 40,000 tons useless hydrogen are burnt as fuel gas.
Migrate as a example by technique by the alkyl of 3,200,000 tons/year, it is assumed that in useless hydrogen, hydrogen content is 60%, then 1 year recyclable
Utilizing hydrogen 2.4 ten thousand tons, the liquefied gas content in useless hydrogen is about 40%, 1 year recyclable liquefied gas 1.6 ten thousand tons, economic benefit
Significantly.
The above is only the preferred embodiment of the present invention, and protection scope of the present invention is not limited merely to above-mentioned enforcement
Example, all technical schemes belonged under thinking of the present invention belong to protection scope of the present invention.It should be pointed out that, for the art
Those of ordinary skill for, some improvements and modifications without departing from the principles of the present invention, these improvements and modifications are also
Should be regarded as protection scope of the present invention.
Claims (8)
1. the device being prepared benzene and dimethylbenzene by toluene and heavy aromatics, it is characterised in that: include feed exchanger (1), enter
Material heating furnace (2), reactor (3), air cooler (4), knockout drum (5), low-temperature reformate oil heat exchanger (6), refrigerator (7),
Effluent exchanger (11) at the bottom of freezing contact tank (8), circulating hydrogen compressor (9), stripper overhead heat exchanger (10), stripper tower,
Stripper (12), benzene column (13), toluene tower (14) and benzenol hydrorefining (15)；First charging aperture of described feed exchanger (1) and
Feedstock pipeline is connected, and the first discharging opening of described feed exchanger (1) is connected with the charging aperture of charging heating furnace (2), institute
The discharging opening stating charging heating furnace (2) is connected with the charging aperture of reactor (3), and discharging opening and the charging of described reactor (3) are changed
Second charging aperture of hot device (1) is connected, and the second discharging opening of described feed exchanger (1) is connected with the charging aperture of air cooler (4),
The discharging opening of described air cooler (4) is connected with the charging aperture of knockout drum (5), the gas phase discharging of described knockout drum (5)
Mouth is connected with the first charging aperture of low-temperature reformate oil heat exchanger (6), the discharging opening of described low-temperature reformate oil heat exchanger (6) and refrigeration
The charging aperture of device (7) is connected, and the discharging opening of described refrigerator (7) is connected with the charging aperture of freezing contact tank (8), and described freezing connects
The gas phase discharging opening touching tank (8) is connected with circulating hydrogen compressor (9), the liquid phase discharging opening of described freezing contact tank (8) and low temperature
Second charging aperture of reformate heat exchanger (6) is connected, and described low-temperature reformate oil heat exchanger (6) is provided with the second discharging opening, institute
State the discharging opening of circulating hydrogen compressor (9) to fill into pipeline with new hydrogen and be connected, the liquid phase discharging opening of described knockout drum (5) and vapour
First charging aperture of stripper overhead heat exchanger (10) is connected, the first discharging opening of described stripper overhead heat exchanger (10) and stripping
First charging aperture of effluent exchanger (11) at the bottom of tower tower is connected, the first discharging opening of effluent exchanger (11) at the bottom of described stripper tower
It is connected with the first charging aperture of stripper (12)；First discharging opening of described stripper (12) and the first pump entry are connected,
Described first circulating-pump outlet is connected with effluent exchanger at the bottom of stripper tower (11) second charging aperture, the of described stripper (12)
Two discharging openings are connected with the second charging aperture of stripper overhead heat exchanger (10), the second of described stripper overhead heat exchanger (10)
Discharging opening is connected with the charging aperture of fluid reservoir (16), and the discharging opening of described fluid reservoir (16) and the entrance of the second circulating pump are connected,
The discharging opening of described second circulating pump is connected with the second charging aperture of stripper (12), described second circulating pump and stripper (12)
Between connection pipeline on be provided with light component blowing pipeline (17), described light component blowing pipeline (17) is provided with electromagnetism
Valve, at the bottom of described stripper tower, the second discharging opening of effluent exchanger (11) is connected with the charging aperture of benzene column (13)；Described benzene column
(13) discharging opening at the bottom of tower is connected with the charging aperture of toluene tower (14), and described benzene column (13) is provided with tower top discharging opening, described first
At the bottom of the tower of benzene column (14), discharging opening is connected with the charging aperture of benzenol hydrorefining (15), described toluene tower (14) tower top discharging opening and raw material
Feeding line is connected, and discharging opening at the bottom of the tower of described benzenol hydrorefining (15) is connected with feedstock pipeline, described benzenol hydrorefining (15)
On be provided with tower top discharging opening.
A kind of device being prepared benzene and dimethylbenzene by toluene and heavy aromatics the most according to claim 1, it is characterised in that: institute
State to connect on the conveyance conduit between freezing contact tank (8) and circulating hydrogen compressor (9) and have tee T, three branch roads of tee T
On be provided with electromagnetic valve, tee T one end is connected with conveyance conduit, and another two ends connect hydride hydrogen-storing dress respectively
Put (18), described metal hydride hydrogen storage unit (18) is provided with first exhaust pipeline and second exhaust pipeline, first exhaust
Electromagnetic valve, described first exhaust pipeline and circulating hydrogen compressor (9) charging aperture it is respectively arranged with on pipeline and second exhaust pipeline
It is connected.
A kind of device being prepared benzene and dimethylbenzene by toluene and heavy aromatics the most according to claim 2, it is characterised in that: institute
State and be provided with drying device (19) on the conveyance conduit that freezing contact tank (8) discharging opening is connected.
4., according to a kind of device being prepared benzene and dimethylbenzene by toluene and heavy aromatics described in any one of claim 1-3, it is special
Levy and be: connecting on described first exhaust pipeline has hydrogen purification apparatus (20).
5. the method being prepared benzene and dimethylbenzene by toluene and heavy aromatics, it is characterised in that it comprises the following steps:
A, by toluene, heavy aromatics and hydrogen mix after, through feed exchanger (1) heat exchange to 350～400 DEG C, pressure
3.2MPa, subsequently into charging heating furnace (2) heating, is warming up to 390～410 DEG C, pressure 3.1MPa；
B, entrance reactor (3) reaction, reaction pressure is 1～3MPa, and reaction temperature is 350～450 DEG C；Hydrogen oil molecule mol ratio
3.0～4.5；Reaction velocity 3.0～3.5h-1；
C, product from reactor (3) out after, be cooled to 110～130 DEG C through feed exchanger (1), pressure to 2.6～
2.8MPa, then it is cooled to 40～60 DEG C through air cooler (4), pressure to 2.0～2.6MPa, subsequently into knockout drum (5)；
Product is divided into gas phase and liquid phase two streams by d, knockout drum (5), and gaseous stream is mainly impure hydrogen
Gas, liquid phase stream is mainly aromatic hydrocarbons mixture；
After e, gaseous stream mix with reformate, freeze through low-temperature reformate oil heat exchanger (6) and refrigerator (7) successively, then enter
Entering freezing contact tank (8), remove the light component materials carried in gaseous stream, remaining gas part is directly entered circulation hydrogen pressure
Contracting machine (9), is additionally partially into drying device (19), and by controlling the switch of each electromagnetic valve, gas goes out from drying device (19)
Entering a metal hydride hydrogen storage unit (18) after Laiing, hydrogen is inhaled by hydrogen storage material in metal hydride hydrogen storage unit (18)
Receiving, residual impurity gas is discharged from second exhaust pipe, meanwhile, and the hydrogen release that another metal hydride hydrogen storage unit (18) will absorb
Put, enter circulating hydrogen compressor (9) by downtake pipe, rise to 3.2-from circulating hydrogen compressor (9) out rear Hydrogen Vapor Pressure
3.5Mpa, is allowed to reenter reaction system with supplementing after new hydrogen mixes；
F, knockout drum (5) liquid phase stream after effluent exchanger (11) at the bottom of stripper overhead heat exchange (10) and stripper tower,
Enter stripper (12)；
After g, stripper (12) overhead fraction enter stripper overhead heat exchange (10) cooling, entering fluid reservoir (16), part is the
Two circulating pumps effect under reenter stripper (12), remainder is discharged from light component blowing pipeline (17)；
H, stripper (12) tower bottom distillate are introduced into benzene column (13) rectification, the tower top temperature of described benzene column (13) 90 DEG C, temperature at the bottom of tower
Spend 145 DEG C, obtain benzene, reclaim unreacted toluene, the tower top temperature of described toluene tower (14) subsequently into toluene tower (14) rectification
Spend 177 DEG C, column bottom temperature 225 DEG C, reclaim the toluene that obtains and deliver to feed(raw material)inlet and again feed, toluene tower (14) end liquid is the most laggard
Enter benzenol hydrorefining (15), described benzenol hydrorefining (15) tower top temperature 235 DEG C, pressure 0.634MPa, essence in benzenol hydrorefining (15)
Evaporating and obtain dimethylbenzene, heavy aromatics at the bottom of benzenol hydrorefining (15) tower is delivered to feed(raw material)inlet and is again fed.
A kind of method being prepared benzene and dimethylbenzene by toluene and heavy aromatics the most according to claim 5, it is characterised in that: institute
The operating condition stating freezing contact tank (8) is: temperature-15～-5 DEG C, pressure 1.5～2.5MPa.
A kind of method being prepared benzene and dimethylbenzene by toluene and heavy aromatics the most according to claim 6, it is characterised in that: institute
The operating condition stating knockout drum (5) is: temperature 40～60 DEG C, pressure 2.5～3.0MPa.
8., according to a kind of method being prepared benzene and dimethylbenzene by toluene and heavy aromatics described in any one of claim 5-7, it is special
Levy and be: the operating condition of described stripper (12): feeding temperature 135～160 DEG C, tower top temperature 120～130 DEG C, tower top pressure
Power 0.5～0.6MPa.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20070049780A1 (en) * | 2005-08-30 | 2007-03-01 | Schwartz Hilary E | Methods of making xylene isomers |
| WO2013151710A1 (en) * | 2012-04-05 | 2013-10-10 | Gtc Technology Us Llc | Process for production of xylenes through integration of methylation and transalkylation |
| CN105130728A (en) * | 2015-08-21 | 2015-12-09 | 中石化炼化工程（集团）股份有限公司 | Method for preparing xylene from methanol, and apparatus thereof |
| CN205838877U (en) * | 2016-07-31 | 2016-12-28 | 宁波中金石化有限公司 | A kind of device being prepared benzene and dimethylbenzene by toluene and heavy aromatics |
-
2016
- 2016-07-31 CN CN201610625325.8A patent/CN106083512B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20070049780A1 (en) * | 2005-08-30 | 2007-03-01 | Schwartz Hilary E | Methods of making xylene isomers |
| CN101253137A (en) * | 2005-08-30 | 2008-08-27 | Bp北美公司 | Methods of making xylene isomers |
| WO2013151710A1 (en) * | 2012-04-05 | 2013-10-10 | Gtc Technology Us Llc | Process for production of xylenes through integration of methylation and transalkylation |
| CN105130728A (en) * | 2015-08-21 | 2015-12-09 | 中石化炼化工程（集团）股份有限公司 | Method for preparing xylene from methanol, and apparatus thereof |
| CN205838877U (en) * | 2016-07-31 | 2016-12-28 | 宁波中金石化有限公司 | A kind of device being prepared benzene and dimethylbenzene by toluene and heavy aromatics |
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