CN105566051B - A kind of disproportionated reaction product separation and heat-exchange system and its processing method - Google Patents
A kind of disproportionated reaction product separation and heat-exchange system and its processing method Download PDFInfo
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- CN105566051B CN105566051B CN201610100141.XA CN201610100141A CN105566051B CN 105566051 B CN105566051 B CN 105566051B CN 201610100141 A CN201610100141 A CN 201610100141A CN 105566051 B CN105566051 B CN 105566051B
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Abstract
The invention provides a kind of separation of disproportionated reaction product and heat-exchange system, the system to include disproportionated reaction system, heat separation device, cooling system, heat exchanger and piece-rate system；Wherein, the discharging of disproportionated reaction system is connected with the charging aperture of heat separation device, the gas phase discharging opening of heat separation device is connected with the gas phase entrance of cooling system, the liquid-phase outlet of cooling system is connected through heat exchanger with the charging aperture of piece-rate system, and the liquid-phase outlet of heat separation device is connected with the charging aperture of piece-rate system.The present invention is thermally integrated heat-exchange network by using heat separation device and change, the heat of disproportionated reaction product can effectively be utilized, reaction product cooling load can not only be greatly reduced, while can also significantly save stabilizer reboiler furnace and the consumption of clay tower feed heater thermal source.
Description
Technical field
The invention belongs to paraxylene disproportionated reaction product separation field, is related to a kind of separation of disproportionated reaction product and heat exchange
System and its processing method, more particularly to a kind of separation of disproportionated reaction product and heat-exchange system and its place based on thermal separation process
Reason method.
Background technology
Paraxylene (PX) device is one of core material device of chemical fibre industry, and it is with the C7-C9 virtues in Reformed Gasoline
Hydrocarbon is raw material, the product such as production benzene, paraxylene and ortho-xylene.Complete PX devices include disproportionation and transalkylation, absorption
Separation, isomerization and disproportionation products fractionation unit.Wherein disproportionation products fractionating system is with the C6-C8 aromatic hydrocarbons in disproportionated reaction product
The C6-C7 aromatic hydrocarbons come with Aromatics Extractive Project unit is raw material, passes through rectificating method, generation benzene, toluene and C8 aromatic hydrocarbons；Adsorbing separation list
Member, according to adsorbing separation principle, isolates poor paraxylene and to diformazan using the Mixed XYLENE of xylene fractionation unit as raw material
Benzaldehyde product；Isomerization unit, by isomerization reaction, obtains being rich in two using the poor paraxylene of adsorption separation unit as raw material
The reaction product of toluene；Xylene fractionation unit is to reform the C8 aromatic hydrocarbons and different of C8 aromatic hydrocarbons, disproportionation and transalkylation reaction generation
Structure metaplasia into C8 aromatic hydrocarbons be raw material, according to principles of rectification, isolate Mixed XYLENE and ortho-xylene product.
In existing disproportionation products fractionating system, the separation of disproportionated reaction product mainly uses cold separation process, that is, is disproportionated
Reaction product could enter subsequent fractionation operation with being needed after reaction feed heat exchange after all cooling down, can so cause the cold of system
But load is larger, meanwhile, the thermic load that also result in stabilizer reboiler furnace and clay tower feed heater is larger.
Therefore, a kind of cooling load that can reduce disproportionated reaction air cooler of research and the heating of subsequent fractionation system are needed badly
Load, and the method for saving energy consumption.
The content of the invention
Using cold separation process the cooling load of system can be caused larger for existing disproportionation products fractionating system, meanwhile,
Also result in stabilizer reboiler furnace and clay tower feed heater thermic load it is larger the problem of, the invention provides one kind disproportionation is anti-
Product separation and heat-exchange system are answered, the system is thermally integrated heat-exchange network, Ke Yiyou by using heat separation device and change
Using the heat of disproportionated reaction product reaction product cooling load can be not only greatly reduced, while can also greatly improve in effect
Stabilizer feeding temperature and clay tower feed heater entrance stream temperature, so as to significantly save stabilizer reboiler furnace and clay tower
Feed heater thermal source consumes.
To use following technical scheme up to this purpose, the present invention：
In a first aspect, the invention provides a kind of separation of disproportionated reaction product and heat-exchange system, the system includes disproportionation
Reaction system, heat separation device, cooling system, heat exchanger and piece-rate system；Wherein, the discharging and thermal release of disproportionated reaction system
The charging aperture of device is connected, and the gas phase discharging opening of heat separation device is connected with the gas phase entrance of cooling system, the liquid of cooling system
Mutually outlet is connected through heat exchanger with the charging aperture of piece-rate system, the liquid-phase outlet of heat separation device and the charging aperture phase of piece-rate system
Even.
The present invention is separated using the high division technique of heat to disproportionated reaction product, and the liquid phase that hot high score handles to obtain is need not be cold
But material, it is directly entered follow-up piece-rate system；The gas phase that hot high score handles to obtain is cooled to 30 to need the material cooled down
Gas phase and liquid phase are again split into cold knockout drum after~50 DEG C, its liquid phase exchanges heat with stabilizer top gaseous phase in piece-rate system
The liquid phase for handling to obtain with hot high score afterwards mixes, and is further separated subsequently into piece-rate system.
Currently preferred technical scheme is used as below, but not as the limitation of technical scheme provided by the invention, is passed through
Following technical scheme, it can preferably reach and realize the technical purpose and beneficial effect of the present invention.
As the preferred scheme of the present invention, the heat separation device is hot high score tank.
As the preferred scheme of the present invention, the disproportionated reaction system includes material liquid surge tank, the raw material being sequentially connected
Heat exchanger, reaction feed heating furnace and disproportionation reactor, the product discharge mouth of disproportionation reactor are connected with raw material heat exchanger, i.e. discrimination
The discharging and disproportionation raw material for changing reactor are exchanged heat.
Wherein, disproportionated reaction system is the disproportionated reaction system in existing disproportionation products fractionating system.
Preferably, the material liquid surge tank discharging pipeline is provided with product pump.
Preferably, the product discharge mouth of disproportionation reactor is connected through raw material heat exchanger with the charging aperture of heat separation device.
As the preferred scheme of the present invention, the cooling system includes reaction product air cooler, the reaction production being sequentially connected
Thing cooler and cold knockout drum, the gaseous phase outlet of cold knockout drum and circulating hydrogen compressor entrance liquid separation tank and hydrogen compressor phase successively
Even, the gaseous phase outlet of hydrogen compressor is connected with the raw material heat exchanger in disproportionated reaction system, and the liquid-phase outlet of cold knockout drum is through heat exchange
Device is connected with the charging aperture of piece-rate system.
Wherein, the gas phase of hydrogen compressor returns to the discharging with disproportionation reactor again after disproportionated reaction system mixes with disproportionation raw material
Exchanged heat.The cooling system is the cooling system of existing disproportionation products fractionating system.
As the preferred scheme of the present invention, the piece-rate system includes stabilizer, stabilizer reboiler furnace, stabilizer bottom of towe and changed
Hot device, stable column overhead air cooler, stabilizer tower top Gas Cooler, stabilizer return tank, clay tower, clay tower feed exchanger
With clay tower feed heater；Wherein, the outlet of stabilizer top gaseous phase through heat exchanger successively with stablizing column overhead air cooler, stably
Column overhead Gas Cooler is connected with stabilizer return tank, and liquid-phase outlet and the stabilizer overhead reflux liquid phase of stabilizer return tank enter
Mouth is connected, and stabilizer bottom of towe liquid-phase outlet is connected with stabilizer reboiler furnace, and stabilizer bottom of towe liquid-phase outlet is successively through stabilizer tower
Bottom heat exchanger, clay tower feed exchanger and clay tower feed heater are connected with the charging aperture of clay tower, clay tower discharging opening
It is connected with clay tower feed exchanger.
Wherein, stabilizer top gaseous phase is through heat exchanger and condensing reflux after the liquid phase heat exchange from cooling system, stabilizer
The part backflow of tower top liquid phase, a part mixes with the crude benzol from stabilizer lateral line withdrawal function sends out the present apparatus as product；Surely
Determine tower base stream, first exchanged heat with the mixed material of heat separation device and cooling system, then with the benzene from clay tower head tank
Mixed with toluene, then successively with entering clay tower after clay tower discharging and clay tower feed exchanger.
Preferably, charging aperture phase of the liquid-phase outlet of cooling system through heat exchanger, stabilizer bottom of towe heat exchanger and stabilizer
Even, the liquid-phase outlet of heat separation device is connected through stabilizer bottom of towe heat exchanger with the charging aperture of stabilizer.
Preferably, it is equipped with product pump on the discharging pipeline of the stabilizer bottom of towe discharging pipeline and stabilizer return tank.
Second aspect, the invention provides the separation of above-mentioned disproportionated reaction product and the processing method of heat-exchange system, the side
Method is：
Disproportionated reaction product after reaction feed heat exchange with carrying out hot high score gas-liquid separation, the isolated gas of hot high score gas-liquid
Cold separation is mutually carried out after cooling is again split into gas phase and liquid phase, the liquid isolated with hot high score gas-liquid after the heat exchange of its liquid phase
Mix, mixed material carries out subsequent fractionation operation.
Wherein, disproportionated reaction product and temperature after reaction feed heat exchange are about 150~160 DEG C；Hot high score gas-liquid separation obtains
Temperature is 40 DEG C or so after the reacted product air cooler of gas phase and reaction product the cooler cooling arrived.
As the preferred scheme of the present invention, the isolated gas phase of hot high score gas-liquid carries out cold separation and divided again after cooling
From into gas phase and liquid phase, the temperature after the heat exchange of its liquid phase is 80~100 DEG C, for example, 80 DEG C, 83 DEG C, 85 DEG C, 87 DEG C, 90 DEG C, 93
DEG C, 95 DEG C, 97 DEG C or 100 DEG C etc., more preferably 90~95 DEG C, it is not limited to cited numerical value, listed scope
Other interior numerical value are feasible.
As the preferred scheme of the present invention, the isolated gas phase of hot high score gas-liquid carries out cold separation and divided again after cooling
It is isolated with hot high score gas-liquid after being exchanged heat with stabilizer top gaseous phase in disproportionated reaction system from into gas phase and liquid phase, its liquid phase
Liquid phase mixing.
As the preferred scheme of the present invention, the isolated gas phase of hot high score gas-liquid carries out cold separation and divided again after cooling
From into gas phase and liquid phase, the liquid phase isolated with hot high score gas-liquid mixes after the heat exchange of its liquid phase, mixed material and disproportionation
Enter stabilizer after the heat exchange of stabilizer bottom of towe liquid phase in reaction system.
Preferably, it is 180~200 DEG C to be exchanged heat after mixing with stabilizer bottom of towe liquid phase in disproportionated reaction system to temperature, example
Such as 180 DEG C, 183 DEG C, 185 DEG C, 187 DEG C, 190 DEG C, 193 DEG C, 195 DEG C, 197 DEG C or 200 DEG C, more preferably 190~
195 DEG C, it is not limited to cited numerical value, other interior numerical value of listed scope are feasible.
Preferably, in subsequent fractionation operation, after stabilizer (12) bottom of towe liquid phase and mixed material-heat-exchanging again with from dress
The temperature for putting outer introducing mixes for 30~50 DEG C of material, then with clay tower discharging heat exchange to 160~170 DEG C, most afterwards through adding
Heat enters clay tower.Wherein, the temperature after heat exchange can be 160 DEG C, 162 DEG C, 164 DEG C, 166 DEG C, 168 DEG C or 170 DEG C etc., but simultaneously
Cited numerical value is not limited only to, other numerical value are feasible in listed scope.
As the preferred scheme of the present invention, disproportionated reaction product carries out heat with entering heat separation device after reaction feed heat exchange
High score gas-liquid separation, the isolated gas phase of hot high score gas-liquid carry out cold separation after cooling system cools down and are again split into gas phase
And liquid phase, its liquid phase are exchanged heat in heat exchanger with stabilizer top gaseous phase in disproportionated reaction system, exchanged heat to 80~100 again
The liquid phase isolated with hot high score gas-liquid mixes after DEG C, mixed material and stabilizer bottom of towe liquid phase in disproportionated reaction system
Heat exchange to entering stabilizer after 180~200 DEG C, stabilizer bottom of towe liquid phase with after mixed material-heat-exchanging again with introducing outside device
Temperature be 30~50 DEG C material mix, then with clay tower discharging heat exchange to 160~170 DEG C, then it is heated enter it is white
Tu Ta processing.
To being thermally integrated the optimization of heat-exchange network in the present invention, in addition to stabilizer bottom of towe heat exchanger, clay tower charging are changed
The optimization of hot device and clay tower feed heater, by increasing the heat exchange area of heat exchanger and heater, enter to strengthen stabilizer
Material exchanges heat with the heat exchange of stabilizer tower base stream and the charging of reinforcement clay tower and clay tower discharging.
Compared with prior art, the invention has the advantages that：
The present invention is thermally integrated heat-exchange network by using heat separation device and change, effectively can be produced using disproportionated reaction
The heat of thing, reaction product cooling load is greatly reduced compared with prior art, while stabilizer charging can also be greatly improved
Temperature and clay tower feed heater entrance stream temperature, make stabilizer feeding temperature improve to 180~200 DEG C, clay tower enters
Material calorifier inlets stream temperature is improved to 160~170 DEG C, so as to significantly save stabilizer reboiler furnace and clay tower charging heating
Device thermal source consumes.
Brief description of the drawings
Fig. 1 is the structural representation of the separation of disproportionated reaction product and heat-exchange system described in the embodiment of the present invention 1；
Fig. 2 is the structural representation of the separation of disproportionated reaction product and heat-exchange system described in comparative example 1 of the present invention；
Wherein, 1- material liquids surge tank, 2- raw material heat exchangers, 3- reaction feed heating furnaces, 4- disproportionation reactors, 5- heat point
From device, 6- reaction product air coolers, 7- reaction product coolers, the cold knockout drums of 8-, 9- circulating hydrogen compressor entrance liquid separation tanks,
10- hydrogen compressors, 11- heat exchangers, 12- stabilizers, 13- stabilizer reboiler furnaces, 14- stabilizer bottom of towe heat exchangers, 15- stabilizer towers
Head space cooler, 16- stabilizer tower top Gas Coolers, 17- stabilizer return tanks, 18- clay towers, 19- clay tower feed exchangers,
20- clay tower feed heaters.
Embodiment
For the present invention is better described, technical scheme is readily appreciated, below to the present invention further specifically
It is bright.But following embodiments is only the simple example of the present invention, the scope of the present invention is not represented or limits, this
Invention protection domain is defined by claims.
Embodiment 1：
As shown in figure 1, present embodiments provide a kind of disproportionated reaction product separation and heat-exchange system, it is characterised in that institute
Stating system includes disproportionated reaction system, heat separation device 5, cooling system, heat exchanger 11 and piece-rate system.
The disproportionated reaction system includes material liquid surge tank 1, raw material heat exchanger 2, the reaction feed heating being sequentially connected
Stove 3 and disproportionation reactor 4, charging aperture phase of the product discharge mouth through raw material heat exchanger 2 with heat separation device 5 of disproportionation reactor 4
Even, the discharging of material liquid surge tank 1 pipeline is provided with product pump.
The heat separation device 5 is hot high score tank, the gas phase discharging opening of heat separation device 5 and the gas phase entrance of cooling system
It is connected, the liquid-phase outlet of heat separation device 5 is connected with the charging aperture of piece-rate system.
The cooling system includes reaction product air cooler 6, reaction product cooler 7 and the cold knockout drum 8 being sequentially connected,
The gaseous phase outlet of cold knockout drum 8 is sequentially connected with circulating hydrogen compressor entrance liquid separation tank 9 and hydrogen compressor 10, the gas phase of hydrogen compressor 10
Outlet is connected with the raw material heat exchanger 2 in disproportionated reaction system, and the liquid-phase outlet of cold knockout drum 8 is through heat exchanger 11 and piece-rate system
Charging aperture be connected.
The piece-rate system includes stabilizer 12, stabilizer reboiler furnace 13, stabilizer bottom of towe heat exchanger 14, stable column overhead
Air cooler 15, stabilizer tower top Gas Cooler 16, stabilizer return tank 17, clay tower 18, clay tower feed exchanger 19 and white
Native tower feed heater 20；Wherein, the top gaseous phase of stabilizer 12 outlet through heat exchanger 11 successively with stablize column overhead air cooler 15,
Stabilizer tower top Gas Cooler 16 is connected with stabilizer return tank 17, liquid-phase outlet and the tower of stabilizer 12 of stabilizer return tank 17
Top backflow liquid phase entrance be connected, while be also connected with stabilizer reboiler furnace 13, the bottom of towe liquid-phase outlet of stabilizer 12 successively through surely
Determine the charging aperture phase of tower bottom of towe heat exchanger 14, clay tower feed exchanger 19 and clay tower feed heater 20 and clay tower 18
Even, the discharging opening of clay tower 18 is connected with clay tower feed exchanger 19.
In the cooling system liquid-phase outlet of cold knockout drum 8 through heat exchanger 11, stabilizer bottom of towe heat exchanger 14 with stably
The charging aperture of tower 12 is connected, charging aperture of the liquid-phase outlet through stabilizer bottom of towe heat exchanger 14 Yu stabilizer 12 of heat separation device 5
It is connected.
Product pump is equipped with the discharging pipeline of stabilizer (12) the bottom of towe discharging pipeline and stabilizer return tank (17).
Embodiment 2：
The present embodiment carries out disproportionated reaction product using the disproportionated reaction product separation described in embodiment 1 and heat-exchange system
Separation and heat exchange processing, processing procedure is as follows：
Disproportionated reaction raw material enters material liquid surge tank 1 from the external world, it is pressurized after successively through raw material heat exchanger 2 with react into
Expect that heating furnace 3 enters disproportionation reactor 4 and disproportionated reaction occurs after heating, disproportionated reaction product exchanges heat to about through raw material heat exchanger 2
Enter heat separation device 5 after 155 DEG C, gas-liquid separation is carried out in heat separation device 5, the reacted production of gas phase that gas-liquid separation obtains
Thing air cooler 6 and reaction product cooler 7 are cooled to 40 DEG C or so the cold knockout drums 8 of rear entrance, and the gas phase of cold knockout drum 8 is through circulation
Hydrogen compressor entrance liquid separation tank 9 is sent into hydrogen compressor 10, is then back to after being mixed with disproportionated reaction and enters raw material heat exchanger 2, cold point
Liquid phase from tank 8 mixes after heat exchanger 11 exchanges heat to 90 DEG C with the tower bottom liquid of heat separation device 5, and mixed material is through stable
The bottom of towe discharging of tower bottom of towe heat exchanger 14 and stabilizer 12 is exchanged heat, and is exchanged heat to entering stabilizer 12, stabilizer 12 after 190 DEG C
Top gaseous phase enter successively after heat exchanger 11, stable column overhead air cooler 15 and stabilizer tower top Gas Cooler 16 cool down it is steady
Determine tower return tank 17 to be separated, the top gaseous phase incoming fuel gas pipe network of stabilizer return tank 17, the tank bottom of stabilizer return tank 17
The pressurized rear portion backflow of liquid phase, another part return to tank field together with the crude benzol of the lateral line withdrawal function of stabilizer 12；Stabilizer 12
Bottom of towe liquid phase it is pressurized after enter stabilizer bottom of towe heat exchanger 14 and the mixed material from heat separation device 5 and cooling system
Exchanged heat, then enter after being mixed with 40 DEG C of the benzene from clay tower head tank and toluene clay tower feed exchanger 19 with it is white
The bottom of towe discharging of native tower 18 is exchanged heat, and is exchanged heat to being heated to 180 DEG C or so through clay tower feed heater 20 after 165 DEG C, is entered
Enter clay tower 18 to be handled.
In the separation and heat exchange processing procedure of disproportionated reaction product described in the present embodiment, reaction product cooling load is
19800kW, stable tower overhead gas cooling load are 7500kW, and the feeding temperature of stabilizer 12 is up to 190 DEG C, clay tower feed heater
20 entrance stream temperatures up to 165 DEG C, stabilizer reboiler furnace and clay tower feed heater thermic load be respectively 11000kW and
3100kW。
Comparative example 1：
As shown in Fig. 2 this comparative example provides separation and the heat-exchange system of a kind of disproportionated reaction product, the system is main
It is that cold separating treatment is used to disproportionated reaction product, the system includes disproportionated reaction system, cooling system and piece-rate system.
In the disproportionated reaction system and cooling system the structure of device with annexation structure with being described in embodiment 1
The structure of system is identical, the product discharge mouth of disproportionation reactor 4 and reaction product air cooler 6 in cooling system in disproportionated reaction system
Charging aperture be connected, the tank bottom liquid-phase outlet of cold knockout drum 8 is through the stabilizer bottom of towe heat exchanger in piece-rate system in cooling system
14 are connected with the charging aperture of stabilizer 12, and the top gaseous phase outlet of stabilizer 12 is with stablizing column overhead air cooler 15 in piece-rate system
Entrance is connected, and the structure of other devices is identical with system described in embodiment 1 with annexation in the piece-rate system.
The separation of disproportionated reaction product described in the present embodiment and the handling process of heat-exchange system are as follows：
Disproportionated reaction raw material enters material liquid surge tank 1 from the external world, it is pressurized after successively through raw material heat exchanger 2 with react into
Expect that heating furnace 3 enters disproportionation reactor 4 and disproportionated reaction occurs after heating, disproportionated reaction product exchanges heat to about through raw material heat exchanger 2
Enter cold knockout drum 8, cold separation after 155 DEG C after reaction product air cooler 6 and reaction product cooler 7 are cooled to 40 DEG C or so
The gas phase of tank 8 is sent into hydrogen compressor 10 through circulating hydrogen compressor entrance liquid separation tank 9, is then back to after being mixed with disproportionated reaction and enters original
Expect heat exchanger 2, bottom of towe discharging of the liquid phase of cold knockout drum 8 through stabilizer bottom of towe heat exchanger 14 and stabilizer 12 is exchanged heat, changed
Enter stabilizer 12 after hot to 170 DEG C, the top gaseous phase of stabilizer 12 stablizes column overhead air cooler 15 and stablizes column overhead successively
Gas Cooler 16 is separated after cooling down into stabilizer return tank 17, the top gaseous phase incoming fuel tracheae of stabilizer return tank 17
Net, the pressurized rear portion backflow of the bottom of towe liquid phase of stabilizer return tank 17, the crude benzol of another part and the lateral line withdrawal function of stabilizer 12
Tank field is returned to together；The bottom of towe liquid phase of stabilizer 12 is pressurized rear into stabilizer bottom of towe heat exchanger 14 and from cooling system
Material is exchanged heat, then enters clay tower feed exchanger 19 after being mixed with 40 DEG C of the benzene from clay tower head tank and toluene
Exchanged heat, exchanged heat to being heated to 180 DEG C of left sides through clay tower feed heater 20 after 140 DEG C with the discharging of the bottom of towe of clay tower 18
The right side, handled into clay tower 18.
In the separation and heat exchange processing procedure of disproportionated reaction product described in this comparative example, reaction product cooling load is
29500kW, stable tower overhead gas cooling load are 9500kW, and the feeding temperature of stabilizer 12 is 170 DEG C, clay tower feed heater 20
Entrance stream temperature is 140 DEG C, stabilizer reboiler furnace and clay tower feed heater thermic load be respectively 15400kW and
6540kW。
Comparative example 1-2 and the result of comparative example 1 can be seen that the processing side of system and system described in embodiment 1-2
Reaction product cooling load, which is compared, in method reduces 9700kW in comparative example 1, stable tower overhead gas cooling load reduction 2000kW, and
And stabilizer feeding temperature is compared comparative example 1 with clay tower feed heater entrance stream temperature and improved a lot, and significantly saves
Stabilizer reboiler furnace and the consumption of clay tower feed heater thermal source, stabilizer reboiler furnace and clay tower feed heater thermic load point
Jiang Di not 4400kW and 3440kW.
The result of integrated embodiment 1-2 and comparative example 1 can be seen that the present invention by using heat separation device and change
Heat-exchange network is thermally integrated, can effectively utilize the heat of disproportionated reaction product, makes reaction product cooling load and stablizes tower overhead gas
Cooling load is greatly reduced compared with prior art, while can also greatly improve stabilizer feeding temperature and clay tower charging heating
Device entrance stream temperature, making stabilizer feeding temperature, clay tower feed heater entrance stream temperature can up to 180~200 DEG C
Up to 160~170 DEG C, so as to significantly save stabilizer reboiler furnace and the consumption of clay tower feed heater thermal source.
Applicant states that the present invention illustrates the method detailed of the present invention, but not office of the invention by above-described embodiment
It is limited to above-mentioned method detailed, that is, does not mean that the present invention has to rely on above-mentioned method detailed and could implemented.Art
Technical staff it will be clearly understood that any improvement in the present invention, equivalence replacement and auxiliary element to each raw material of product of the present invention
Addition, selection of concrete mode etc., within the scope of all falling within protection scope of the present invention and disclosing.
Claims (3)
1. a kind of disproportionated reaction product separation and heat-exchange system, it is characterised in that the system includes disproportionated reaction system, heat point
From device (5), cooling system, heat exchanger (11) and piece-rate system；Wherein, the discharging of disproportionated reaction system and heat separation device
(5) charging aperture is connected, and the gas phase discharging opening of heat separation device (5) is connected with the gas phase entrance of cooling system, cooling system
Liquid-phase outlet is connected through heat exchanger (11) with the charging aperture of piece-rate system, the liquid-phase outlet and piece-rate system of heat separation device (5)
Charging aperture be connected；
The disproportionated reaction system includes material liquid surge tank (1), raw material heat exchanger (2), the reaction feed heating being sequentially connected
Stove (3) and disproportionation reactor (4), the product discharge mouth of disproportionation reactor (4) are connected with raw material heat exchanger (2)；Disproportionation reactor
(4) product discharge mouth is connected through raw material heat exchanger (2) with the charging aperture of heat separation device (5)；
The heat separation device (5) is hot high score tank；
The cooling system includes reaction product air cooler (6), reaction product cooler (7) and the cold knockout drum being sequentially connected
(8), the gaseous phase outlet of cold knockout drum (8) is sequentially connected with circulating hydrogen compressor entrance liquid separation tank (9) and hydrogen compressor (10), hydrogen pressure
The gaseous phase outlet of machine (10) is connected with the raw material heat exchanger (2) in disproportionated reaction system, and the liquid-phase outlet of cold knockout drum (8) is through changing
Hot device (11) is connected with the charging aperture of piece-rate system；
The piece-rate system includes stabilizer (12), stabilizer reboiler furnace (13), stabilizer bottom of towe heat exchanger (14), stabilizer tower
Head space cooler (15), stabilizer tower top Gas Cooler (16), stabilizer return tank (17), clay tower (18), clay tower charging are changed
Hot device (19) and clay tower feed heater (20)；Wherein, stabilizer (12) top gaseous phase outlet through heat exchanger (11) successively with
Stable column overhead air cooler (15), stabilizer tower top Gas Cooler (16) are connected with stabilizer return tank (17), stabilizer backflow
The liquid-phase outlet of tank (17) is connected with stabilizer (12) overhead reflux liquid phase entrance, stabilizer (12) bottom of towe liquid-phase outlet with stably
Tower reboiler furnace (13) is connected, and stabilizer (12) bottom of towe liquid-phase outlet is fed through stabilizer bottom of towe heat exchanger (14), clay tower successively
Heat exchanger (19) and clay tower feed heater (20) are connected with the charging aperture of clay tower (18), clay tower (18) discharging opening with it is white
Native tower feed exchanger (19) is connected；
Charging aperture phase of the liquid-phase outlet of cooling system through heat exchanger (11), stabilizer bottom of towe heat exchanger (14) and stabilizer (12)
Even, the liquid-phase outlet of heat separation device (5) is connected through stabilizer bottom of towe heat exchanger (14) with the charging aperture of stabilizer (12).
2. disproportionated reaction product separation according to claim 1 and the processing method of heat-exchange system, it is characterised in that described
Method is：
Disproportionated reaction product is with carrying out hot high score gas-liquid separation, the isolated gas phase warp of hot high score gas-liquid after reaction feed heat exchange
Cold separation is carried out after cooling and is separated again into gas phase and liquid phase, its liquid phase liquid phase isolated with hot high score gas-liquid after heat exchange
Mixing, mixed material carry out subsequent fractionation operation.
3. processing method according to claim 2, it is characterised in that disproportionated reaction product enters after being exchanged heat with reaction feed
Heat separation device (5) carries out hot high score gas-liquid separation, and the isolated gas phase of hot high score gas-liquid is carried out through cooling system after cooling
Cold separation is again split into gas phase and liquid phase, and its liquid phase is again with stabilizer (12) top gaseous phase in disproportionated reaction system in heat exchanger
(11) exchanged heat in, exchange heat to isolated with hot high score gas-liquid liquid phase after 80~100 DEG C and mix, mixed material with
Stabilizer (12) bottom of towe liquid phase exchanges heat to entering stabilizer (12), stabilizer (12) tower after 180~200 DEG C in disproportionated reaction system
Bottom liquid phase with the temperature introduced outside device being again that 30~50 DEG C of material mixes after mixed material-heat-exchanging, then with carclazyte
Tower discharging heat exchange is last heated into clay tower (18) to 160~170 DEG C.
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|---|---|---|---|---|
| CN108795494B (en) * | 2017-05-04 | 2023-07-28 | 中国石油化工股份有限公司 | Coupling system of hydrogenation device and light component removing tower for reforming generated oil |
| CN110937972B (en) * | 2018-09-25 | 2022-02-08 | 中国石油化工股份有限公司 | Production device and process of p-xylene |
| CN110849193A (en) * | 2019-12-20 | 2020-02-28 | 大连福佳·大化石油化工有限公司 | Air cooling waste heat utilization system |
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| CN204162631U (en) * | 2014-10-30 | 2015-02-18 | 中国石油化工股份有限公司 | A kind of xylene production system |
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