CN105566051A - Disproportionated reaction product separation and heat exchange system and processing method thereof - Google Patents
Disproportionated reaction product separation and heat exchange system and processing method thereof Download PDFInfo
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- CN105566051A CN105566051A CN201610100141.XA CN201610100141A CN105566051A CN 105566051 A CN105566051 A CN 105566051A CN 201610100141 A CN201610100141 A CN 201610100141A CN 105566051 A CN105566051 A CN 105566051A
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Abstract
The invention provides a disproportionated reaction product separation and heat exchange system. The system comprises a disproportionated reaction system, a heat separation device, a cooling system, a heat exchanger and a separation system, wherein a discharging port of the disproportionated reaction system is connected with a feeding port of the heat separation device; a gas-phase discharging port of the heat separation device is connected with a gas-phase inlet of the cooling system; a liquid-phase outlet of the cooling system is connected with a discharging port of the separation system through the heat exchanger; a liquid-phase outlet of the heat separation device is connected with a feeding port of the separation system. The heat separation device is adopted, a heat integration heat exchange network is changed, heat of disproportionated reaction products can be effectively utilized, reaction product cooling loads can be substantially reduced, and meanwhile heat resource consumption of a stabilizer reboiler furnace and a carclazyte tower feeding heater can be substantially reduced.
Description
Technical field
The invention belongs to p-Xylol disproportionation reaction product separation field, relate to a kind of disproportionation reaction product separation and heat-exchange system and treatment process thereof, particularly relate to a kind of disproportionation reaction product separation based on thermal separation process and heat-exchange system and treatment process thereof.
Background technology
P-Xylol (PX) device is one of core material device of chemical fibre industry, and it for raw material, produces the products such as benzene, p-Xylol and o-Xylol with the C7-C9 aromatic hydrocarbons in reformed gasoline.Complete PX device comprises disproportionation and transalkylation, fractionation by adsorption, isomerization and disproportionation products fractionation unit.Wherein disproportionation products fractionating system is with the C6-C7 aromatic hydrocarbons of the C6-C8 aromatic hydrocarbons in disproportionation reaction product and Aromatics Extractive Project unit for raw material, by rectificating method, generates benzene, toluene and C8 aromatic hydrocarbons; Adsorption separation unit for raw material, according to fractionation by adsorption principle, isolates poor p-Xylol and para-xylene product with the Mixed XYLENE of xylene fractionation unit; Isomerization unit for raw material, by isomerization reaction, obtains the reaction product being rich in p-Xylol with the poor p-Xylol of adsorption separation unit; The C8 aromatic hydrocarbons that xylene fractionation unit generates with reformation C8 aromatic hydrocarbons, disproportionation and transalkylation reaction and the C8 aromatic hydrocarbons that isomerization generates, for raw material, according to principles of rectification, isolate Mixed XYLENE and o-Xylol product.
In existing disproportionation products fractionating system, the separation of disproportionation reaction product mainly adopts cold separation process, namely just can enter subsequent fractionation after needing after disproportionation reaction product and reaction feed heat exchange all to cool to operate, the cooling load of system can be caused so larger, meanwhile, the thermal load that also result in stabilizer tower reboiler furnace and clay tower feed heater is larger.
Therefore, need research badly and a kind ofly can reduce the cooling load of disproportionation reaction air cooler and the heating load of subsequent fractionation system, and the method for energy efficient.
Summary of the invention
Adopt cold separation process that the cooling load of system can be caused larger for existing disproportionation products fractionating system, simultaneously, also the problem that the thermal load of stabilizer tower reboiler furnace and clay tower feed heater is larger is caused, the invention provides a kind of disproportionation reaction product separation and heat-exchange system, described system is by adopting heat separation device and changing hot integrated heat exchange network, effectively can utilize the heat of disproportionation reaction product, not only can significantly reduce reaction product cooling load, significantly can also improve stabilizer tower feeding temperature and clay tower feed heater inlet streams temperature simultaneously, thus significantly save stabilizer tower reboiler furnace and the consumption of clay tower feed heater thermal source.
For reaching this object, the present invention by the following technical solutions:
First aspect, the invention provides a kind of disproportionation reaction product separation and heat-exchange system, described system comprises disproportionation reaction system, heat separation device, cooling system, interchanger and separation system; Wherein, the discharging of disproportionation reaction system is connected with the opening for feed of heat separation device, the gas phase discharge port of heat separation device is connected with the gas phase entrance of cooling system, the liquid-phase outlet of cooling system is connected with the opening for feed of separation system through interchanger, and the liquid-phase outlet of heat separation device is connected with the opening for feed of separation system.
The present invention adopts hot high division technique to disproportionation reaction product separation, and the liquid phase that hot high divisional processing obtains cools material for not needing, and it directly enters follow-up separation system; The gas phase that the high divisional processing of heat obtains is the material needing cooling, enter cold separating tank after being cooled to 30 ~ 50 DEG C and be again separated into gas phase and liquid phase, the liquid-phase mixing obtained with the high divisional processing of heat after the heat exchange of stabilizer tower top gaseous phase in its liquid phase and separation system, then enters separation system and is further separated.
Following as the preferred technical scheme of the present invention, but not as the restriction of technical scheme provided by the invention, by the following technical programs, better can reach and realize technical purpose of the present invention and beneficial effect.
As preferred version of the present invention, described heat separation device is hot high score tank.
As preferred version of the present invention, described disproportionation reaction system comprises the stock liquid surge tank, raw material interchanger, reaction feed process furnace and the disproportionation reactor that are connected successively, the product discharge mouth of disproportionation reactor is connected with raw material interchanger, and namely the discharging of disproportionation reactor and disproportionation raw material carry out heat exchange.
Wherein, disproportionation reaction system is the disproportionation reaction system in existing disproportionation products fractionating system.
Preferably, described stock liquid surge tank discharging pipeline is provided with product pump.
Preferably, the product discharge mouth of disproportionation reactor is connected with the opening for feed of heat separation device through raw material interchanger.
As preferred version of the present invention, described cooling system comprises the reaction product air cooler, reaction product water cooler and the cold separating tank that are connected successively, the gaseous phase outlet of cold separating tank divides flow container to be connected successively with hydrogen compressor with circulating hydrogen compressor entrance, the gaseous phase outlet of hydrogen compressor is connected with the raw material interchanger in disproportionation reaction system, and the liquid-phase outlet of cold separating tank is connected with the opening for feed of separation system through interchanger.
Wherein, the gas phase of hydrogen compressor returns after disproportionation reaction system mixes with disproportionation raw material and carries out heat exchange with the discharging of disproportionation reactor again.Described cooling system is the cooling system of existing disproportionation products fractionating system.
As preferred version of the present invention, described separation system comprises interchanger at the bottom of stabilizer tower, stabilizer tower reboiler furnace, stabilizer tower tower, stabilizer tower tower top air cooler, stabilizer tower overhead gas water cooler, stabilizer tower return tank, clay tower, clay tower feed exchanger and clay tower feed heater; Wherein, the outlet of stabilizer tower top gaseous phase is connected with stabilizer tower return tank with stabilizer tower tower top air cooler, stabilizer tower overhead gas water cooler successively through interchanger, the liquid-phase outlet of stabilizer tower return tank is connected with stabilizer tower trim the top of column liquid phase entrance, at the bottom of stabilizer tower tower, liquid-phase outlet is connected with stabilizer tower reboiler furnace, liquid-phase outlet at the bottom of stabilizer tower tower successively at the bottom of stabilizer tower tower interchanger, clay tower feed exchanger be connected with the opening for feed of clay tower with clay tower feed heater, clay tower discharge port is connected with clay tower feed exchanger.
Wherein, stabilizer tower top gaseous phase is through interchanger and from condensing reflux after the liquid phase heat exchange of cooling system, and a stabilizer tower tower top liquid phase part refluxes, and a part mixes with the crude benzol from stabilizer tower lateral line withdrawal function sends this device as product; Stabilizer tower bottoms stream, the mixture heat exchange of elder generation and heat separation device and cooling system, then mixes with the Benzene and Toluene from clay tower charging stock tank, then enters clay tower successively with after clay tower discharging and clay tower feed exchanger.
Preferably, liquid-phase outlet interchanger at the bottom of interchanger, stabilizer tower tower of cooling system is connected with the opening for feed of stabilizer tower, and liquid-phase outlet interchanger at the bottom of stabilizer tower tower of heat separation device is connected with the opening for feed of stabilizer tower.
Preferably, the discharging pipeline of discharging pipeline and stabilizer tower return tank at the bottom of described stabilizer tower tower is equipped with product pump.
Second aspect, the invention provides the treatment process of above-mentioned disproportionation reaction product separation and heat-exchange system, described method is:
Hot high score gas-liquid separation is carried out after disproportionation reaction product and reaction feed heat exchange, the gas phase that hot high score gas-liquid separation obtains is carried out cold separation and is again separated into gas phase and liquid phase after cooling, the liquid-phase mixing obtained with hot high score gas-liquid separation after its liquid phase heat exchange, mixed material carries out subsequent fractionation operation.
Wherein, after disproportionation reaction product and reaction feed heat exchange, temperature is about 150 ~ 160 DEG C; The gas phase that hot high score gas-liquid separation obtains temperature after reaction product air cooler and the cooling of reaction product water cooler is about 40 DEG C.
As preferred version of the present invention, the gas phase that hot high score gas-liquid separation obtains is carried out cold separation and is again separated into gas phase and liquid phase after cooling, temperature after its liquid phase heat exchange is 80 ~ 100 DEG C, such as 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, but be not limited in cited numerical value, in listed scope, other numerical value are all feasible.
As preferred version of the present invention, the gas phase that hot high score gas-liquid separation obtains is carried out cold separation and is again separated into gas phase and liquid phase after cooling, the liquid-phase mixing obtained with hot high score gas-liquid separation after the heat exchange of stabilizer tower top gaseous phase in its liquid phase and disproportionation reaction system.
As preferred version of the present invention, the gas phase that hot high score gas-liquid separation obtains is carried out cold separation and is again separated into gas phase and liquid phase after cooling, the liquid-phase mixing obtained with hot high score gas-liquid separation after its liquid phase heat exchange, enters stabilizer tower after liquid phase heat exchange at the bottom of stabilizer tower tower in mixed material and disproportionation reaction system.
Preferably, mixing liquid phase heat exchange to temperature at the bottom of stabilizer tower tower in rear and disproportionation reaction system is 180 ~ 200 DEG C, 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 etc., more preferably 190 ~ 195 DEG C, but be not limited in cited numerical value, in listed scope, other numerical value are all feasible.
Preferably, in subsequent fractionation operation, after liquid phase at the bottom of stabilizer tower (12) tower and mixed material-heat-exchanging again with the mixing of materials that the temperature introduced outward from device is 30 ~ 50 DEG C, then with clay tower discharging heat exchange to 160 ~ 170 DEG C, enter clay tower finally by heating.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 is not limited in cited numerical value, and in listed scope, other numerical value are all feasible.
As preferred version of the present invention, enter heat separation device after disproportionation reaction product and reaction feed heat exchange and carry out hot high score gas-liquid separation, the gas phase that hot high score gas-liquid separation obtains is carried out cold separation and is again separated into gas phase and liquid phase after cooling system cooling, its liquid phase carries out heat exchange with stabilizer tower top gaseous phase in disproportionation reaction system again in interchanger, the liquid-phase mixing obtained with hot high score gas-liquid separation behind heat exchange to 80 ~ 100 DEG C, stabilizer tower is entered behind liquid phase heat exchange to 180 ~ 200 at the bottom of stabilizer tower tower DEG C in mixed material and disproportionation reaction system, the temperature introduced outward with device again after liquid phase at the bottom of stabilizer tower tower and mixed material-heat-exchanging is the mixing of materials of 30 ~ 50 DEG C, then with clay tower discharging heat exchange to 160 ~ 170 DEG C, then enter clay tower through heating to process.
To the optimization of hot integrated heat exchange network in the present invention, also comprise the optimization to interchanger, clay tower feed exchanger and clay tower feed heater at the bottom of stabilizer tower tower, by increasing the heat interchanging area of interchanger and well heater, strengthening stabilizer tower charging and the heat exchange of stabilizer tower tower base stream and strengthening clay tower charging and clay tower discharging heat exchange.
Compared with prior art, the present invention has following beneficial effect:
The present invention is by adopting heat separation device and changing hot integrated heat exchange network, effectively can utilize the heat of disproportionation reaction product, reaction product cooling load is significantly reduced compared to existing technology, significantly can also improve stabilizer tower feeding temperature and clay tower feed heater inlet streams temperature simultaneously, stabilizer tower feeding temperature is made to be increased to 180 ~ 200 DEG C, clay tower feed heater inlet streams temperature is increased to 160 ~ 170 DEG C, thus significantly saves stabilizer tower reboiler furnace and the consumption of clay tower feed heater thermal source.
Accompanying drawing explanation
Fig. 1 is the structural representation of disproportionation reaction product separation described in the embodiment of the present invention 1 and heat-exchange system;
Fig. 2 is the structural representation of disproportionation reaction product separation described in comparative example 1 of the present invention and heat-exchange system;
Wherein, 1-stock liquid surge tank, 2-raw material interchanger, 3-reaction feed process furnace, 4-disproportionation reactor, 5-heat separation device, 6-reaction product air cooler, 7-reaction product water cooler, the cold separating tank of 8-, 9-circulating hydrogen compressor entrance divides flow container, 10-hydrogen compressor, 11-interchanger, 12-stabilizer tower, 13-stabilizer tower reboiler furnace, interchanger at the bottom of 14-stabilizer tower tower, 15-stabilizer tower tower top air cooler, 16-stabilizer tower overhead gas water cooler, 17-stabilizer tower return tank, 18-clay tower, 19-clay tower feed exchanger, 20-clay tower feed heater.
Embodiment
For better the present invention being described, be convenient to understand technical scheme of the present invention, below the present invention is described in more detail.But following embodiment is only simple and easy example of the present invention, and do not represent or limit the scope of the present invention, scope is as the criterion with claims.
Embodiment 1:
As shown in Figure 1, present embodiments provide a kind of disproportionation reaction product separation and heat-exchange system, it is characterized in that, described system comprises disproportionation reaction system, heat separation device 5, cooling system, interchanger 11 and separation system.
Described disproportionation reaction system comprises the stock liquid surge tank 1, raw material interchanger 2, reaction feed process furnace 3 and the disproportionation reactor 4 that are connected successively, the product discharge mouth of disproportionation reactor 4 is connected through the opening for feed of raw material interchanger 2 with heat separation device 5, and stock liquid surge tank 1 discharging pipeline is provided with product pump.
Described heat separation device 5 is hot high score tank, and the gas phase discharge port of heat separation device 5 is connected with the gas phase entrance of cooling system, and the liquid-phase outlet of heat separation device 5 is connected with the opening for feed of separation system.
Described cooling system comprises the reaction product air cooler 6, reaction product water cooler 7 and the cold separating tank 8 that are connected successively, gaseous phase outlet and the circulating hydrogen compressor entrance of cold separating tank 8 divide flow container 9 to be connected successively with hydrogen compressor 10, the gaseous phase outlet of hydrogen compressor 10 is connected with the raw material interchanger 2 in disproportionation reaction system, and the liquid-phase outlet of cold separating tank 8 is connected with the opening for feed of separation system through interchanger 11.
Described separation system comprises interchanger 14 at the bottom of stabilizer tower 12, stabilizer tower reboiler furnace 13, stabilizer tower tower, stabilizer tower tower top air cooler 15, stabilizer tower overhead gas water cooler 16, stabilizer tower return tank 17, clay tower 18, clay tower feed exchanger 19 and clay tower feed heater 20; Wherein, the outlet of stabilizer tower 12 top gaseous phase is connected with stabilizer tower return tank 17 with stabilizer tower tower top air cooler 15, stabilizer tower overhead gas water cooler 16 successively through interchanger 11, the liquid-phase outlet of stabilizer tower return tank 17 is connected with stabilizer tower 12 trim the top of column liquid phase entrance, while be also connected with stabilizer tower reboiler furnace 13, liquid-phase outlet at the bottom of stabilizer tower 12 tower successively at the bottom of stabilizer tower tower interchanger 14, clay tower feed exchanger 19 be connected with the opening for feed of clay tower feed heater 20 with clay tower 18, clay tower 18 discharge port is connected with clay tower feed exchanger 19.
In described cooling system, the liquid-phase outlet of cold separating tank 8 interchanger 14 at the bottom of interchanger 11, stabilizer tower tower is connected with the opening for feed of stabilizer tower 12, and liquid-phase outlet interchanger 14 at the bottom of stabilizer tower tower of heat separation device 5 is connected with the opening for feed of stabilizer tower 12.
The discharging pipeline of discharging pipeline and stabilizer tower return tank (17) at the bottom of described stabilizer tower (12) tower is equipped with product pump.
Embodiment 2:
The present embodiment adopts the disproportionation reaction product separation described in embodiment 1 to carry out being separated of disproportionation reaction product and heat exchange process with heat-exchange system, and treating processes is as follows:
Disproportionation reaction raw material is incoming stock liquid surge tank 1 from the external world, after pressurization, after raw material interchanger 2 and reaction feed process furnace 3 heat, enter disproportionation reactor 4 successively disproportionation reaction occurs, disproportionation reaction product enters heat separation device 5 after raw material interchanger 2 heat exchange is to about 155 DEG C, gas-liquid separation is carried out in heat separation device 5, the gas phase that gas-liquid separation obtains enters cold separating tank 8 after reaction product air cooler 6 and reaction product water cooler 7 are cooled to about 40 DEG C, the gas phase of cold separating tank 8 divides flow container 9 to send into hydrogen compressor 10 through circulating hydrogen compressor entrance, then incoming stock interchanger 2 after mixing with disproportionation reaction is returned, the liquid phase of cold separating tank 8 after interchanger 11 heat exchange to 90 DEG C with liquid-phase mixing at the bottom of heat separation device 5 tower, mixed material interchanger 14 at the bottom of stabilizer tower tower carries out heat exchange with discharging at the bottom of the tower of stabilizer tower 12, stabilizer tower 12 is entered after heat exchange to 190 DEG C, the top gaseous phase of stabilizer tower 12 is successively through interchanger 11, stabilizer tower tower top air cooler 15 enters stabilizer tower return tank 17 after cooling with stabilizer tower overhead gas water cooler 16 and is separated, stabilizer tower return tank 17 top gaseous phase enters fuel gas pipe network, liquid phase at the bottom of stabilizer tower return tank 17 tank is through the backflow of pressurization rear portion, another part returns to tank field together with the crude benzol of stabilizer tower 12 lateral line withdrawal function, liquid phase at the bottom of the tower of stabilizer tower 12 enters interchanger 14 at the bottom of stabilizer tower tower and carries out heat exchange with the mixture from heat separation device 5 and cooling system after pressurization, enter clay tower feed exchanger 19 after mixing with the Benzene and Toluene of 40 DEG C from clay tower charging stock tank again and carry out heat exchange with discharging at the bottom of the tower of clay tower 18, be heated to about 180 DEG C through clay tower feed heater 20 after heat exchange to 165 DEG C, enter clay tower 18 and process.
In the separation of disproportionation reaction product described in the present embodiment and heat exchange treating processes, reaction product cooling load is 19800kW, stabilizer tower top gas cooling load is 7500kW, stabilizer tower 12 feeding temperature can reach 190 DEG C, clay tower feed heater 20 inlet streams temperature can reach 165 DEG C, and stabilizer tower reboiler furnace and clay tower feed heater thermal load are respectively 11000kW and 3100kW.
Comparative example 1:
As shown in Figure 2, this comparative example provides a kind of separation and heat-exchange system of disproportionation reaction product, and described system mainly adopts cold separating treatment to disproportionation reaction product, and described system comprises disproportionation reaction system, cooling system and separation system.
Described disproportionation reaction system is identical with the structure of system described in annexation structure and embodiment 1 with the structure of device in cooling system, in disproportionation reaction system, the product discharge mouth of disproportionation reactor 4 is connected with the opening for feed of reaction product air cooler 6 in cooling system, in cooling system cold separating tank 8 tank at the bottom of interchanger 14 at the bottom of the stabilizer tower tower of liquid-phase outlet in separation system be connected with the opening for feed of stabilizer tower 12, in separation system, the top gaseous phase outlet of stabilizer tower 12 is connected with stabilizer tower tower top air cooler 15 entrance, in described separation system, the structure of other devices is identical with system described in annexation and embodiment 1.
The separation of disproportionation reaction product described in the present embodiment and the treatment scheme of heat-exchange system as follows:
Disproportionation reaction raw material is incoming stock liquid surge tank 1 from the external world, after pressurization, after raw material interchanger 2 and reaction feed process furnace 3 heat, enter disproportionation reactor 4 successively disproportionation reaction occurs, disproportionation reaction product enters cold separating tank 8 after raw material interchanger 2 heat exchange is to about 155 DEG C after reaction product air cooler 6 and reaction product water cooler 7 are cooled to about 40 DEG C, the gas phase of cold separating tank 8 divides flow container 9 to send into hydrogen compressor 10 through circulating hydrogen compressor entrance, then incoming stock interchanger 2 after mixing with disproportionation reaction is returned, liquid phase interchanger 14 at the bottom of stabilizer tower tower of cold separating tank 8 carries out heat exchange with discharging at the bottom of the tower of stabilizer tower 12, stabilizer tower 12 is entered after heat exchange to 170 DEG C, the top gaseous phase of stabilizer tower 12 successively stabilizer tower tower top air cooler 15 with enter stabilizer tower return tank 17 after the cooling of stabilizer tower overhead gas water cooler 16 and be separated, stabilizer tower return tank 17 top gaseous phase enters fuel gas pipe network, liquid phase at the bottom of stabilizer tower return tank 17 tower is through the backflow of pressurization rear portion, another part returns to tank field together with the crude benzol of stabilizer tower 12 lateral line withdrawal function, liquid phase at the bottom of the tower of stabilizer tower 12 enters interchanger 14 at the bottom of stabilizer tower tower and carries out heat exchange with the material from cooling system after pressurization, enter clay tower feed exchanger 19 after mixing with the Benzene and Toluene of 40 DEG C from clay tower charging stock tank again and carry out heat exchange with discharging at the bottom of the tower of clay tower 18, be heated to about 180 DEG C through clay tower feed heater 20 after heat exchange to 140 DEG C, enter clay tower 18 and process.
In the separation of disproportionation reaction product described in this comparative example and heat exchange treating processes, reaction product cooling load is 29500kW, stabilizer tower top gas cooling load is 9500kW, stabilizer tower 12 feeding temperature is 170 DEG C, clay tower feed heater 20 inlet streams temperature is 140 DEG C, and stabilizer tower reboiler furnace and clay tower feed heater thermal load are respectively 15400kW and 6540kW.
The result of comparative example 1-2 and comparative example 1 can be found out, in the treatment process of system described in embodiment 1-2 and system, reaction product cooling load compares in ratio 1 and reduces 9700kW, stabilizer tower top gas cooling load reduces 2000kW, and stabilizer tower feeding temperature and clay tower feed heater inlet streams temperature compare ratio 1 and improve a lot, significantly save stabilizer tower reboiler furnace and the consumption of clay tower feed heater thermal source, stabilizer tower reboiler furnace and clay tower feed heater thermal load reduce 4400kW and 3440kW respectively.
The result of integrated embodiment 1-2 and comparative example 1 can be found out, the present invention is by adopting heat separation device and changing hot integrated heat exchange network, effectively can utilize the heat of disproportionation reaction product, reaction product cooling load and stabilizer tower top gas cooling load are significantly reduced compared to existing technology, significantly can also improve stabilizer tower feeding temperature and clay tower feed heater inlet streams temperature simultaneously, make stabilizer tower feeding temperature can reach 180 ~ 200 DEG C, clay tower feed heater inlet streams temperature can reach 160 ~ 170 DEG C, thus significantly save stabilizer tower reboiler furnace and the consumption of clay tower feed heater thermal source.
Applicant states, the present invention illustrates method detailed of the present invention by above-described embodiment, but the present invention is not limited to above-mentioned method detailed, does not namely mean that the present invention must rely on above-mentioned method detailed and could implement.Person of ordinary skill in the field should understand, any improvement in the present invention, to equivalence replacement and the interpolation of ancillary component, the concrete way choice etc. of each raw material of product of the present invention, all drops within protection scope of the present invention and open scope.
Claims (10)
1. disproportionation reaction product separation and a heat-exchange system, is characterized in that, described system comprises disproportionation reaction system, heat separation device (5), cooling system, interchanger (11) and separation system; Wherein, the discharging of disproportionation reaction system is connected with the opening for feed of heat separation device (5), the gas phase discharge port of heat separation device (5) is connected with the gas phase entrance of cooling system, the liquid-phase outlet of cooling system is connected with the opening for feed of separation system through interchanger (11), and the liquid-phase outlet of heat separation device (5) is connected with the opening for feed of separation system.
2. disproportionation reaction product separation according to claim 1 and heat-exchange system, is characterized in that, described heat separation device (5) is hot high score tank.
3. disproportionation reaction product separation according to claim 1 and 2 and heat-exchange system, it is characterized in that, described disproportionation reaction system comprises the stock liquid surge tank (1), raw material interchanger (2), reaction feed process furnace (3) and the disproportionation reactor (4) that are connected successively, and the product discharge mouth of disproportionation reactor (4) is connected with raw material interchanger (2);
Preferably, the discharging pipeline of described stock liquid surge tank (1) is provided with product pump;
Preferably, the product discharge mouth of disproportionation reactor (4) is connected through the opening for feed of raw material interchanger (2) with heat separation device (5).
4. the disproportionation reaction product separation according to any one of claim 1-3 and heat-exchange system, it is characterized in that, described cooling system comprises the reaction product air cooler (6) be connected successively, reaction product water cooler (7) and cold separating tank (8), gaseous phase outlet and the circulating hydrogen compressor entrance of cold separating tank (8) divide flow container (9) to be connected successively with hydrogen compressor (10), the gaseous phase outlet of hydrogen compressor (10) is connected with the raw material interchanger (2) in disproportionation reaction system, the liquid-phase outlet of cold separating tank (8) is connected with the opening for feed of separation system through interchanger (11).
5. the disproportionation reaction product separation according to any one of claim 1-4 and heat-exchange system, it is characterized in that, described separation system comprises interchanger (14), stabilizer tower tower top air cooler (15), stabilizer tower overhead gas water cooler (16), stabilizer tower return tank (17), clay tower (18), clay tower feed exchanger (19) and clay tower feed heater (20) at the bottom of stabilizer tower (12), stabilizer tower reboiler furnace (13), stabilizer tower tower, wherein, stabilizer tower (12) top gaseous phase outlet through interchanger (11) successively with stabilizer tower tower top air cooler (15), stabilizer tower overhead gas water cooler (16) is connected with stabilizer tower return tank (17), the liquid-phase outlet of stabilizer tower return tank (17) is connected with stabilizer tower (12) trim the top of column liquid phase entrance, at the bottom of stabilizer tower (12) tower, liquid-phase outlet is connected with stabilizer tower reboiler furnace (13), liquid-phase outlet at the bottom of stabilizer tower (12) tower is interchanger (14) at the bottom of stabilizer tower tower successively, clay tower feed exchanger (19) is connected with the opening for feed of clay tower feed heater (20) with clay tower (18), clay tower (18) discharge port is connected with clay tower feed exchanger (19),
Preferably, liquid-phase outlet interchanger (14) at the bottom of interchanger (11), stabilizer tower tower of cooling system is connected with the opening for feed of stabilizer tower (12), and liquid-phase outlet interchanger (14) at the bottom of stabilizer tower tower of heat separation device (5) is connected with the opening for feed of stabilizer tower (12);
Preferably, the discharging pipeline of discharging pipeline and stabilizer tower return tank (17) at the bottom of described stabilizer tower (12) tower is equipped with product pump.
6. the disproportionation reaction product separation according to any one of claim 1-5 and the treatment process of heat-exchange system, it is characterized in that, described method is:
Hot high score gas-liquid separation is carried out after disproportionation reaction product and reaction feed heat exchange, the gas phase that hot high score gas-liquid separation obtains is carried out cold separation and is again separated into gas phase and liquid phase after cooling, the liquid-phase mixing that its liquid phase obtains with hot high score gas-liquid separation after heat exchange, mixed material carries out subsequent fractionation operation.
7. treatment process according to claim 6, is characterized in that, the gas phase that hot high score gas-liquid separation obtains is carried out cold separation and is again separated into gas phase and liquid phase after cooling, and the temperature after its liquid phase heat exchange is 80 ~ 100 DEG C, more preferably 90 ~ 95 DEG C.
8. the treatment process according to claim 6 or 7, it is characterized in that, the gas phase that hot high score gas-liquid separation obtains is carried out cold separation and is again separated into gas phase and liquid phase after cooling, the liquid-phase mixing obtained with hot high score gas-liquid separation after stabilizer tower (12) top gaseous phase heat exchange in its liquid phase and disproportionation reaction system.
9. the treatment process according to any one of claim 6-8, it is characterized in that, the gas phase that hot high score gas-liquid separation obtains is carried out cold separation and is again separated into gas phase and liquid phase after cooling, the liquid-phase mixing obtained with hot high score gas-liquid separation after its liquid phase heat exchange, enters stabilizer tower (12) after liquid phase heat exchange at the bottom of stabilizer tower (12) tower in mixed material and disproportionation reaction system;
Preferably, mixing liquid phase heat exchange to temperature at the bottom of stabilizer tower (12) tower in rear and disproportionation reaction system is 180 ~ 200 DEG C, more preferably 190 ~ 195 DEG C;
Preferably, in subsequent fractionation operation, after liquid phase at the bottom of stabilizer tower (12) tower and mixed material-heat-exchanging again with the mixing of materials that the temperature introduced outward from device is 30 ~ 50 DEG C, then with clay tower discharging heat exchange to 160 ~ 170 DEG C, clay tower (18) is entered finally by heating.
10. the treatment process according to any one of claim 6-9, it is characterized in that, enter heat separation device (5) after disproportionation reaction product and reaction feed heat exchange and carry out hot high score gas-liquid separation, the gas phase that hot high score gas-liquid separation obtains is through cooling system, carry out cold separation after cooling and be again separated into gas phase and liquid phase, its liquid phase carries out heat exchange with stabilizer tower (12) top gaseous phase in disproportionation reaction system again in interchanger (11), the liquid-phase mixing obtained with hot high score gas-liquid separation behind heat exchange to 80 ~ 100 DEG C, stabilizer tower (12) is entered behind liquid phase heat exchange to 180 ~ 200 at the bottom of stabilizer tower (12) tower DEG C in mixed material and disproportionation reaction system, the temperature introduced outward with device again after liquid phase at the bottom of stabilizer tower (12) tower and mixed material-heat-exchanging is the mixing of materials of 30 ~ 50 DEG C, then with clay tower discharging heat exchange to 160 ~ 170 DEG C, clay tower (18) is entered finally by heating.
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| CN201610100141.XA CN105566051B (en) | 2016-02-24 | 2016-02-24 | A kind of disproportionated reaction product separation and heat-exchange system and its processing method |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108795494A (en) * | 2017-05-04 | 2018-11-13 | 中国石油化工股份有限公司 | Recapitalization generating oil hydrogenation device and cut light tower coupled system |
| 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 |
| CN110937972A (en) * | 2018-09-25 | 2020-03-31 | 中国石油化工股份有限公司 | Production device and process of p-xylene |
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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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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108795494A (en) * | 2017-05-04 | 2018-11-13 | 中国石油化工股份有限公司 | Recapitalization generating oil hydrogenation device and cut light tower coupled system |
| 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 |
| CN110937972A (en) * | 2018-09-25 | 2020-03-31 | 中国石油化工股份有限公司 | Production device and process of p-xylene |
| 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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| CN105566051B (en) | 2018-02-27 |
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