CN102516007A - Process and device for processing and preparing hydrocarbon by utilizing liquefied gas - Google Patents
Process and device for processing and preparing hydrocarbon by utilizing liquefied gas Download PDFInfo
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- CN102516007A CN102516007A CN201110387102XA CN201110387102A CN102516007A CN 102516007 A CN102516007 A CN 102516007A CN 201110387102X A CN201110387102X A CN 201110387102XA CN 201110387102 A CN201110387102 A CN 201110387102A CN 102516007 A CN102516007 A CN 102516007A
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Abstract
The invention discloses a process and a device for processing and preparing hydrocarbon by utilizing liquefied gas. The process comprises the processes of cracking reaction, absorption and stabilization, aromatization reaction, gas separation raw material gas stripping concentration and aromatic hydrocarbon purification. The device comprises a cracking reaction system, an absorption and stabilization system, an aromatization reaction system, a gas separation raw material gas stripping concentration system and an aromatic hydrocarbon purification system. The process and the device have the advantages that the energy consumption is low, and after the process is adopted, a deisobutanizer stops running, 90 kilograms of standard coals consumed by a carton-4 raw material per ton are treated, and 48.5 percent of energy is saved; gas separation raw material gas propylene is high in content and is improved from 15 percent to 50 percent in mass fraction; the requirements on equipment and heat energy are low and are easily realized; and the device is simple in process, is easy in operation and control and stable in running.
Description
Technical field
The present invention relates to a kind of liquefied gas deep processing technology, specifically a kind of technology and device thereof that utilizes liquefied gas processing system hydrocarbon belongs to liquefied gas processing system hydrocarbon field.
Background technology
Used liquefied gas is processed isolating method in the Chemical Manufacture has multiple.At present; Mainly containing of generally adopting in the industry is a kind of: carry out raw materials pretreatment earlier; From the extraction of depropanizing cat head, the mixed c 4 component gets into deisobutanizer at the bottom of the tower, and Trimethylmethane autospasy Trimethylmethane cat head is separated with two carbon of the carbon in the LPG liquefied petroleum gas, three components; Get into the scission reaction system more than or equal to the component of carbon four at the bottom of the tower and carry out scission reaction, the lower carbon number hydrocarbons that contains propylene etc. that obtains gets into absorbing-stabilizing system; Absorption tower, desorption tower, stabilizer tower three towers circulation the carrying out separation of material in the absorbing-stabilizing system; At last divide the aromatic hydrocarbons that virgin gas, stabilizer tower bottom divide and the dry gas of absorption cat head by stablize gas that cat head obtains containing propylene massfraction 15%; Dry gas carries out obtaining aromatic hydrocarbons and fuel gas behind the aromatization; Gas divides virgin gas extraction behind the stabilizer tower reflux pump, sends to gas separation unit or gas and divides head tank to store.
This method is had relatively high expectations to equipment and heat energy, especially when deisobutanizer carries out the separation of Trimethylmethane, needs 200 layers of tower tray; Full tower height degree reaches 160 meters, and tower top temperature requires to be not less than 50 ℃, thereby the heat supply condition is harsh; Energy consumption is high; Account for 50% of total energy consumption, the device operation is inharmonious, and the Trimethylmethane quality product does not reach requirement; The gas of producing simultaneously divides the virgin gas propylene content low, is merely 15%, causes downstream gas separation unit fluctuation of service.Simultaneously, the aromatic hydrocarbon impurities content behind the aromatization is high, and a little less than the product market competitiveness, price is low.
Summary of the invention
In order to address the above problem, the present invention has designed a kind of technology and device thereof that utilizes liquefied gas processing system hydrocarbon, and this technology is simple, be easy to control, energy consumption is low, quality product is high.
Technical scheme of the present invention is:
A kind of technology of utilizing liquefied gas processing system hydrocarbon comprises the scission reaction operation, absorbs stabilizing process, aromatization operation, comprises that also gas divides virgin gas to carry dense operation and aromatic hydrocarbons purification process.
Wherein:
(1) scission reaction operation:
The carbon four liquid stock gasifications of cracking stock jar are delivered to the device district through feedstock pump; Carry out heat exchange through first interchanger, second interchanger and cleavage reaction product; Carbon four raw materials after the heat exchange get into process furnace again; Further temperature raising to 500 ℃, the gas after the temperature raising gets into from the top of cracking reactor, carries out scission reaction;
Cleavage reaction product is from the bottom of cracking reactor, carries out the heat exchange cooling through second interchanger, first interchanger, hot water heat exchanger, split product water cooler successively, reduce to 40 ℃ to temperature after, get into knockout drum and separate; Separate the lime set that obtains and be pumped into the absorption tower, be used for the rich gas that compressor is sent here is further absorbed with reaction liquid; The gas that separation obtains is delivered to the absorption tower and is further absorbed after rich gas compressor compresses, cools off.
(2) absorb stabilizing process:
Gas from above-mentioned operation (1) after the rich gas compressor compression; With exporting water cooler through pneumatic press outlet air cooler, pneumatic press successively from the absorption oil of bottom, absorption tower and the stripping gas of desorb top of tower; Get into the pneumatic press outlet after being cooled to 40 ℃ and divide flow container, oil, gas are separated;
Divide the top of flow container to separate out rich gas and be delivered to the bottom, absorption tower from the pneumatic press outlet; In the absorption tower with the absorption agent counter current contact that gets into from top, absorption tower; Lean gas after absorbing gets into dry gas and divides flow container from the top, absorption tower; Carry out gas-liquid separation, liquid imports stabilizer tower and refluxes, and delivers to aromatization reactor from the dry gas that comes out in dry gas separatory tank top;
In order to take liberated heat in the absorption tower away, extract the gasoline of mid-pumparound at the middle part, absorption tower out with stage casing, absorption tower pump, water cooler is cooled to 20 ℃ through the stage casing, absorption tower, returns the absorption tower again;
From the lime set that pneumatic press outlet separatory pot bottom comes out, be divided into two-way through the desorption tower fresh feed pump: the one tunnel directly gets into the desorption tower top, and another road is through desorption tower feed exchanger heat exchange to 70 ℃ entering desorption tower top;
Stripping gas is overflowed from cat head, converges with the compression rich gas of rich gas compressor to get into pneumatic press outlet air cooler; Desorb gasoline gets in the middle part of the stabilizer tower from extracting out with the stabilizer tower fresh feed pump at the bottom of the desorption tower after the stable gasoline heat exchange to 125 at the bottom of stabilizer tower feed exchanger and the stabilizer tower ℃;
Carbon four and the component of carbon below four distillate from stablizing cat head; Pass through stabilizer tower head space cooler, stablize overhead condenser entering stablizing return tank of top of the tower; Gas is divided into two-way after dividing virgin gas to extract out through the stabilizer tower reflux pump from the jar end of stablizing return tank of top of the tower: the one tunnel does to reflux returns the stabilizer tower top, and another road gets into the depropanizing tower feed preheater;
The stable gasoline of stabilizer tower comes out at the bottom of tower; Successively after stabilizer tower feed exchanger, desorption tower feed exchanger, lighter hydrocarbons water cooler are cooled to 30 ℃; Separated into two parts: the light aromatic hydrocarbons that a part gets into stripping tower feed exchanger and the backflow extraction of stripping tower top is to get into stripping tower after the product gasoline heat exchange, and another part is cooled to 20 ℃ and delivers to the top, absorption tower and make absorption agent through absorbing oil pump pressurization, absorption oil cooler.
Further, desorption tower reboiler to tower in the heat supply of desorption tower at the bottom of by tower.
Further, stabilizer tower reboiler to tower in the heat supply of stabilizer tower at the bottom of by tower.
(3) aromatization operation:
The dry gas that come out in dry gas separatory tank top from above-mentioned operation (2) and the fuel gas of dry gas circulator converge the back separated into two parts: a part at first gets into the dry gas feed exchanger as main line; Carry out heat exchange with the gas behind the aromatization; After further being heated to 300 ℃ to the dry gas electric heater again; Get into from the aromatization reactor top, contact with aromatized catalyst and carry out aromatization; Another part, directly gets into aromatization reactor and carries out aromatization without the heat exchange temperature raising for control aromatization reactor internal temperature from the middle part;
Gas behind the aromatization gets into the dry gas feed exchanger after coming out from the aromatization reactor bottom; After the heat exchange of raw material dry gas; After process aromizing product water cooler and aromizing product deep freezer are reduced to 20 ℃; Carry out gas-liquid separation to aromizing product knockout drum, gas phase is divided into two portions: a part gets into the process furnace gas that acts as a fuel, and another part returns aromatization reactor after the compression of dry gas circulator; Liquid phase aromatic hydrocarbons is that raw gasline relies on the pressure reduction of aromatization system and stripping tower system directly to get into the stripping tower feed exchanger.
(4) gas divides virgin gas to put forward dense operation
Gas from above-mentioned operation (2) divides virgin gas after the pressure reduction that a stabilizer tower reflux pump part relies on stabilizer tower to connect depropanizing tower directly gets into the temperature raising of depropanizing tower feed preheater, to get into depropanizing tower from the jar end of stablizing return tank of top of the tower, carries out the separation of carbon three, carbon four components;
C3 fraction i.e. gas divides virgin gas to steam from the depropanizing tower top; After depropanizing tower head space cooler and condensing surface cooling; Get into depropanizing cat head return tank; Be divided into two portions after phlegma is extracted out by the depropanizing tower reflux pump: a part is used as depropanizing tower and refluxes, and another part divides raw material to send into gas separation unit or deliver to gas and divide head tank to store as gas;
Carbon four components of coming out at the bottom of the depropanizing tower rely on pressure reduction directly to get into the MTBE device and participate in reaction or send into the storage of carbon four head tanks as raw material.
Further, depropanizing tower reboiler to tower in the heat supply of depropanizing tower at the bottom of by tower, thermal source adopts thermal oil.
(5) aromatic hydrocarbons purification process
After the aromatic hydrocarbons that from the aromizing product knockout drum of the lighter hydrocarbons water cooler of above-mentioned operation (2) stabilizer tower and (3), comes out through feed exchanger is the gas phase heat exchange at product water cooler and stripping tower top of cat head, the entering stripping tower from the stripping tower stage casing;
Original light aromatic hydrocarbons is that product gasoline is carried out mass-and heat-transfer in the aromatic hydrocarbons of entering stripping tower and the tower, is divided into heavy constituent and light constituent;
Heavy constituent are displaced downwardly at the bottom of the tower, further heat through the stripping tower reboiler, and the extraction behind the forced circulation pump pressure-raising of part heavy constituent is simultaneously delivered to heavy oil tank and stored;
The light constituent evaporation is risen; And fully vaporization; After the light constituent that rises escapes into feed exchanger from cat head, further be cooled to 30 ℃ through overhead condenser, the back gets into return tank; Behind the reflux pump pressure-raising, be divided into two portions: a part as aromatic hydrocarbon product extraction deliver to gasoline tank and store, another part gets into stripping tower as refluxing from cat head.
Raw material directly gets into the scission reaction system and reacts, and the lower carbon number hydrocarbons that obtains after the scission reaction gets into depropanizing tower after absorbing-stabilizing system is handled, and the gas of former propylene content 15% divides virgin gas by the extraction of depropanizing tower cat head; Stripping tower to aromizing and stabilizer tower at the bottom of resulting aromatic hydrocarbons carry out the weight component and separate, obtain the more purified light aromatic hydrocarbons of component.Lower carbon number hydrocarbons liquefied gas through obtaining behind the absorbing-stabilizing system gets into depropanizing tower, and gas divides virgin gas to separate from cat head, and propylene content reaches 50%.
A kind ofly realize the above-mentioned device that utilizes liquefied gas processing process for producing hydrocarbons, comprise that scission reaction system, absorbing-stabilizing system, aromatization system, gas divide virgin gas upgrading system, aromatic hydrocarbons purification system.
Wherein,
Described scission reaction system comprises: feedstock pump, first interchanger, second interchanger, process furnace, cracking reactor, reaction product water cooler, hot water heat exchanger, knockout drum, reaction liquid pump, rich gas compressor, pneumatic press outlet air cooler, pneumatic press outlet water cooler, pneumatic press outlet divide a flow container;
The feedstock pump outlet links to each other with first heat exchanger shell pass bottom mouth of pipe, and the first heat exchanger shell pass top mouth of pipe links to each other with second heat exchanger shell pass bottom mouth of pipe, and the second heat exchanger shell pass top mouth of pipe links to each other with the middle part of process furnace inlet, cracking reactor respectively; Furnace outlet links to each other with the cracking reactor top;
The bottom of cracking reactor links to each other with the second interchanger tube side head tube mouth; The second interchanger tube side lower tube mouth links to each other with the first interchanger tube side head tube mouth; The first interchanger tube side lower tube mouth links to each other with the hot water heat exchanger tube side top mouth of pipe; The hot water heat exchanger tube side bottom mouth of pipe links to each other with split product water cooler shell side head tube mouth, and split product water cooler shell side lower tube mouth links to each other with gas-liquid separation tank top inlet, and the knockout drum outlet at bottom links to each other with the reaction liquid pump intake; The reaction liquid pump discharge links to each other with top, absorption tower; Gas-liquid separation tank top gaseous phase outlet links to each other with rich gas compressor; Rich gas compressor, pneumatic press outlet air cooler, pneumatic press outlet water cooler, pneumatic press outlet divide flow container to link to each other successively; Pneumatic press outlet separatory tank top gaseous phase outlet links to each other with the bottom, absorption tower; The outlet of pneumatic press outlet separatory pot bottom links to each other with the desorption tower fresh feed pump.
Described absorbing-stabilizing system comprises: oil pump, desorption tower, desorption tower fresh feed pump, desorption tower feed exchanger, desorption tower reboiler, stabilizer tower, stabilizer tower fresh feed pump, stabilizer tower feed exchanger, stabilizer tower reboiler, stabilizer tower head space cooler at the bottom of absorption tower, stage casing, absorption tower pump, stage casing, absorption tower water cooler, the absorption tower, stablize the cat head water cooler, stablize return tank of top of the tower, stabilizer tower reflux pump, lighter hydrocarbons water cooler, absorb oil pump, absorb oil cooler, dry gas divides flow container;
The bottom on absorption tower oil pump at the bottom of the absorption tower links to each other with pneumatic press outlet air cooler inlet, and the top on absorption tower divides flow container to link to each other with dry gas; Dry gas divides the top of flow container to link to each other with the dry gas feed exchanger shell side bottom mouth of pipe; Dry gas divides the bottom of flow container to link to each other with stabilizer tower reflux pump inlet; Stabilizer tower backflow pump outlet links to each other with the stabilizer tower top and the depropanizing tower feed preheater tube side bottom mouth of pipe respectively;
Middle part parallelly connected successively absorption tower stage casing pump and stage casing, absorption tower water cooler on the absorption tower;
The desorption tower fresh feed pump links to each other with the top of desorption tower, and the desorption tower fresh feed pump also links to each other with the top of desorption tower through the desorption tower feed exchanger;
Desorption tower all links to each other with pneumatic press outlet air cooler with rich gas compressor; The bottom of desorption tower links to each other with the middle part of stabilizer tower through stabilizer tower fresh feed pump, stabilizer tower feed exchanger successively;
The top of stabilizer tower, stabilizer tower head space cooler, stabilizer tower condensing surface, stablize return tank of top of the tower and link to each other successively; The jar end of stablizing return tank of top of the tower, link to each other with the top and the depropanizing tower feed preheater of stabilizer tower respectively through stablizing the cat head reflux pump;
At the bottom of the tower of stabilizer tower, stabilizer tower feed exchanger, desorption tower feed exchanger, lighter hydrocarbons water cooler link to each other successively; The lighter hydrocarbons water cooler links to each other with the stripping tower feed exchanger, and the lighter hydrocarbons water cooler also links to each other with the top on absorption tower through absorption oil pump, absorption oil cooler successively.
Further, described desorption tower is provided with the desorption tower reboiler at the bottom of tower.
Further, described stabilizer tower is provided with the stabilizer tower reboiler at the bottom of tower.
Described aromatization system comprises: dry gas feed exchanger, dry gas electric heater, aromatization reactor, aromizing product water cooler, aromizing product deep freezer, aromizing product knockout drum, dry gas circulator;
The dry gas feed exchanger shell side top mouth of pipe links to each other with the top of aromatization reactor through the dry gas electric heater successively; The dry gas feed exchanger tube side top mouth of pipe also links to each other with the bottom of aromatization reactor; Dry gas feed exchanger tube side bottom, aromizing product water cooler aromizing product deep freezer, aromizing product knockout drum link to each other successively; Dry gas divides the top of flow container to link to each other with the middle part of dry gas circulator and aromatization reactor respectively;
Aromizing product gas-liquid separation tank top links to each other with process furnace, and aromizing product knockout drum also links to each other with aromatization reactor through dry gas circulator, dry gas feed exchanger, dry gas electric heater successively successively.
Described gas divides the virgin gas upgrading system, comprising: depropanizing tower feed preheater, depropanizing tower, depropanizing tower reboiler, depropanizing tower head space cooler, depropanizing cat head condensing surface, depropanizing tower item return tank, depropanizing tower reflux pump;
The jar end of stablizing return tank of top of the tower, link to each other with depropanizing tower feed preheater, depropanizing tower through the stabilizer tower reflux pump successively;
The top of depropanizing tower links to each other with depropanizing tower head space cooler, depropanizing cat head condensing surface, depropanizing cat head return tank, depropanizing cat head reflux pump successively, and forms the loop; Depropanizing cat head reflux pump also links to each other with gas separation unit.
Further, depropanizing tower reboiler to tower in the heat supply of described depropanizing tower at the bottom of by tower, thermal source adopts thermal oil.
Described lighter hydrocarbons purification system comprises: feed exchanger, electric heater, stripping tower, stripping tower reboiler, stripping overhead condenser, stripping return tank of top of the tower, stripping tower reflux pump, forced circulation pump;
The stripping tower feed exchanger links to each other with stripping tower; Forced circulation pump links to each other with heavy oil tank;
The stripping tower cat head links to each other successively with stripping tower feed exchanger, stripping overhead condenser, stripping return tank of top of the tower, stripping tower reflux pump and forms the loop; The stripping tower reflux pump also links to each other with gasoline tank.
Further, described stripping tower is provided with the stripping tower reboiler at the bottom of tower.
Compare with existing process for producing hydrocarbons; The present invention has removed deisobutanizer and attached support equipment thereof; Raw material is no longer carried out pre-treatment, directly get into the scission reaction system and react, reacted lower carbon number hydrocarbons gets into depropanizing tower after absorbing-stabilizing system is handled; Carrying out gas, to divide virgin gas to carry dense, makes the propylene gas of weight content >=15% divide virgin gas by the extraction of depropanizing tower cat head; Through the stripping tower in the aromatic hydrocarbons purification process to aromizing and stabilizer tower at the bottom of resulting aromatic hydrocarbons carry out the weight component and separate, further carry dense, thereby obtain the more purified light aromatic hydrocarbons of component, it is 50% that propylene content reaches weight fraction.
The invention has the advantages that:
(1) energy consumption is low: when adopting existing deisobutanizer technology, handle material carbon four per ton and consume mark coal 175kg, adopt technology of the present invention after, deisobutanizer is out of service, handles carbon four raw materials consumption mark coal 90kg per ton, energy efficient 48.5%;
(2) gas divides the virgin gas propylene content high, and massfraction content brings up to 50% by original 15%;
(3) low to equipment and heat energy requirement, realize that easily the device flow process is simple, is easy to control, and operates steadily.
Below in conjunction with accompanying drawing and embodiment the present invention is described further.
Description of drawings
Fig. 1 connects synoptic diagram for the equipment of embodiment of the invention liquefied gas processing system hydrocarbon device;
Among the figure: the 1-feedstock pump; 2-first interchanger; 3-second interchanger; The 4-process furnace; The 5-cracking reactor; 6-reaction product water cooler; The 7-hot water heat exchanger; The 8-knockout drum; 9-reaction liquid pump; The 10-rich gas compressor; 11-pneumatic press outlet air cooler; 12-pneumatic press outlet water cooler; The outlet of 13-pneumatic press divides flow container; The 14-absorption tower; Stage casing, 15-absorption tower pump; Stage casing, 16-absorption tower water cooler; Oil pump at the bottom of the 17-absorption tower; The 18-desorption tower; 19-desorption tower fresh feed pump; 20-desorption tower feed exchanger; 21-desorption tower reboiler; The 22-stabilizer tower; 23-stabilizer tower fresh feed pump; 24-stabilizer tower feed exchanger; 25-stabilizer tower reboiler; 26-stabilizer tower head space cooler; 27-stablizes overhead condenser; 28-stablizes return tank of top of the tower; 29-stabilizer tower reflux pump; 30-lighter hydrocarbons water cooler; 31-absorbs oil pump; 32-absorbs oil cooler; The 33-dry gas divides flow container; 34-dry gas feed exchanger; 35-dry gas electric heater; The 36-aromatization reactor; 37-aromizing product water cooler; 38-aromizing product deep freezer; 39-aromizing product knockout drum; 40-dry gas circulator; 41-depropanizing tower feed preheater; The 42-depropanizing tower; 43-depropanizing tower reboiler; 44-depropanizing tower head space cooler; 45-depropanizing cat head condensing surface; 46-depropanizing tower item return tank; 47-depropanizing tower reflux pump; 48-stripping tower feed exchanger; The 49-electric heater; The 50-stripping tower; 51-stripping tower reboiler; 52-stripping overhead condenser; 53-stripping return tank of top of the tower; 54-stripping tower reflux pump; The 55-forced circulation pump.
Embodiment
Embodiment 1
A kind of technology of utilizing liquefied gas processing system hydrocarbon comprises following operation:
(1) scission reaction operation:
Carbon four raw materials of cracking stock jar are delivered to the device district through feedstock pump; Carry out heat exchange through first interchanger, second interchanger and cleavage reaction product; Carbon four raw materials after the heat exchange get into process furnace again; Further temperature raising to 500 ℃, the gas after the temperature raising gets into from the top of cracking reactor, carries out scission reaction;
Cleavage reaction product is from the bottom of cracking reactor; Carry out the heat exchange cooling through second interchanger, first interchanger, hot water heat exchanger, split product water cooler (promptly reacting condensing surface) successively; After reducing to 40 ℃ to temperature, get into knockout drum and separate that (cleavage reaction product carries out heat exchange at second interchanger and first interchanger and carbon four raw materials; Carry out heat exchange at hot water heat exchanger and split product water cooler respectively with hot water and recirculated water); Separate the lime set that obtains and be pumped into the absorption tower, be used for the rich gas that compressor is sent here is further absorbed with reaction liquid; The gas that separation obtains is delivered to the absorption tower and is further absorbed after rich gas compressor compresses, cools off;
(2) absorb stabilizing process:
Gas from above-mentioned operation (1) after the rich gas compressor compression; With exporting water cooler through pneumatic press outlet air cooler, pneumatic press successively from the absorption oil of bottom, absorption tower and the stripping gas of desorb top of tower; Get into the pneumatic press outlet after being cooled to 40 ℃ and divide flow container, oil, gas are separated;
Divide the top of flow container to separate out rich gas and be delivered to the bottom, absorption tower from the pneumatic press outlet; In the absorption tower with absorption agent (like the stable gasoline) counter current contact that gets into from top, absorption tower; Lean gas after absorbing gets into dry gas and divides flow container from the top, absorption tower; Carry out gas-liquid separation, liquid imports stabilizer tower and refluxes, and delivers to aromatization reactor from the dry gas that comes out in dry gas separatory tank top;
In order to take liberated heat in the absorption tower away, extract the gasoline of mid-pumparound at the middle part, absorption tower out with stage casing, absorption tower pump, water cooler is cooled to 20 ℃ through the stage casing, absorption tower, returns the absorption tower again;
From the lime set that pneumatic press outlet separatory pot bottom comes out, be divided into two-way through the desorption tower fresh feed pump: the one tunnel directly gets into the desorption tower top, and another road is through desorption tower feed exchanger heat exchange to 70 ℃ entering desorption tower top;
Desorption tower reboiler to tower in the heat supply of desorption tower at the bottom of by tower; Stripping gas is overflowed from cat head, converges with the compression rich gas of rich gas compressor to get into pneumatic press outlet air cooler; Desorb gasoline gets in the middle part of the stabilizer tower from extracting out with the stabilizer tower fresh feed pump at the bottom of the desorption tower after the stable gasoline heat exchange to 125 at the bottom of stabilizer tower feed exchanger and the stabilizer tower ℃;
Stabilizer tower reboiler to tower in the heat supply of stabilizer tower at the bottom of by tower; Carbon four and the component of carbon below four distillate from stablizing cat head; Pass through stabilizer tower head space cooler, stablize overhead condenser entering stablizing return tank of top of the tower; Gas is divided into two-way after dividing virgin gas to extract out through the stabilizer tower reflux pump from the jar end of stablizing return tank of top of the tower: the one tunnel does to reflux returns the stabilizer tower top, and another road gets into the depropanizing tower feed preheater;
The stable gasoline of stabilizer tower comes out at the bottom of tower; Successively after stabilizer tower feed exchanger, desorption tower feed exchanger, lighter hydrocarbons water cooler are cooled to 30 ℃; Separated into two parts: the light aromatic hydrocarbons that a part gets into stripping tower feed exchanger (being the overhead product water cooler) and the backflow extraction of stripping tower top is to get into stripping tower after the product gasoline heat exchange, and another part is through absorbing the oil pump pressurization, absorbing oil cooler and be cooled to 20 ℃ and deliver to the top, absorption tower and make absorption agent;
(3) aromatization operation:
The fuel gas of dry gas that come out in dry gas separatory tank top from above-mentioned operation (2) and dry gas circulator (spiral-lobe compressor) converges the back separated into two parts: a part at first gets into the dry gas feed exchanger as main line; Carry out heat exchange with the gas behind the aromatization; After further being heated to 300 ℃ to the dry gas electric heater again; Get into from the aromatization reactor top, contact with aromatized catalyst and carry out aromatization; Another part, directly gets into aromatization reactor and carries out aromatization without the heat exchange temperature raising for control aromatization reactor internal temperature from the middle part;
Gas behind the aromatization gets into the dry gas feed exchanger after coming out from the aromatization reactor bottom; After the heat exchange of raw material dry gas; After process aromizing product water cooler and aromizing product deep freezer are reduced to 20 ℃; Carry out gas-liquid separation to aromizing product knockout drum, gas phase is divided into two portions: a part gets into the process furnace gas that acts as a fuel, and another part returns aromatization reactor after the compression of dry gas circulator; Liquid phase aromatic hydrocarbons is that raw gasline relies on the pressure reduction of aromatization system and stripping tower system directly to get into the stripping tower feed exchanger;
(4) gas divides virgin gas to put forward dense operation
Gas from above-mentioned operation (2) divides virgin gas after the pressure reduction that a stabilizer tower reflux pump part relies on stabilizer tower to connect depropanizing tower directly gets into the temperature raising of depropanizing tower feed preheater, to get into depropanizing tower from the jar end of stablizing return tank of top of the tower, carries out the separation of carbon three, carbon four components;
C3 fraction i.e. gas divides virgin gas to steam from the depropanizing tower top; After depropanizing tower head space cooler and condensing surface cooling; Get into depropanizing cat head return tank; Be divided into two portions after phlegma is extracted out by the depropanizing tower reflux pump: a part is used as depropanizing tower and refluxes, and another part divides raw material to send into gas separation unit or deliver to gas and divide head tank to store as gas;
Carbon four components of coming out at the bottom of the depropanizing tower rely on pressure reduction directly to get into MTBE (MTBE) device and participate in reaction or send into the storage of carbon four head tanks as raw material;
Depropanizing tower reboiler to tower in the heat supply of depropanizing tower at the bottom of by tower, thermal source adopts thermal oil
(5) aromatic hydrocarbons purification process
After the aromatic hydrocarbons that from the aromizing product knockout drum of the lighter hydrocarbons water cooler of above-mentioned operation (2) stabilizer tower and (3), comes out through feed exchanger is the gas phase heat exchange at product water cooler and stripping tower top of cat head, the entering stripping tower from the stripping tower stage casing;
Original light aromatic hydrocarbons is that product gasoline is carried out mass-and heat-transfer in the aromatic hydrocarbons of entering stripping tower and the tower, is divided into heavy constituent and light constituent;
Heavy constituent are displaced downwardly at the bottom of the tower, further heat through the stripping tower reboiler, and the extraction behind the forced circulation pump pressure-raising of part heavy constituent is simultaneously delivered to heavy oil tank and stored;
The light constituent evaporation is risen; And fully vaporization; After the light constituent that rises escapes into feed exchanger from cat head, further be cooled to 30 ℃ through overhead condenser, the back gets into return tank; Behind the reflux pump pressure-raising, be divided into two portions: a part as aromatic hydrocarbon product extraction deliver to gasoline tank and store, another part gets into stripping tower as refluxing from cat head.
Result: handle carbon four raw materials consumption mark coal 90kg per ton, energy efficient 48.5%; Gas divides the virgin gas propylene content to bring up to massfraction 50%.
Embodiment 2
As shown in Figure 1, a kind of embodiment of realization 1 described device that utilizes liquefied gas processing process for producing hydrocarbons comprises that scission reaction system, absorbing-stabilizing system, aromatization system, gas divide virgin gas upgrading system, aromatic hydrocarbons purification system.
Described scission reaction system comprises: feedstock pump 1, first interchanger 2, second interchanger 3, process furnace 4, cracking reactor 5, reaction product water cooler 6, hot water heat exchanger 7, knockout drum 8, reaction liquid pump 9, rich gas compressor 10, pneumatic press outlet air cooler 11, pneumatic press outlet water cooler 12, pneumatic press outlet divide a flow container 13;
Feedstock pump 1 outlet links to each other with first interchanger, the 2 shell sides bottom mouth of pipe, and first interchanger, the 2 shell side top mouths of pipe link to each other with second interchanger, the 3 shell sides bottom mouth of pipe, and second interchanger, the 3 shell side top mouths of pipe link to each other with the middle part of process furnace 4 inlets, cracking reactor 5 respectively; Process furnace 4 outlets link to each other with cracking reactor 5 tops;
The bottom of cracking reactor 5 links to each other with second interchanger, the 3 tube side top mouths of pipe; Second interchanger, the 3 tube sides bottom mouth of pipe links to each other with first interchanger, the 2 tube side top mouths of pipe; First interchanger, the 2 tube sides bottom mouth of pipe links to each other with the hot water heat exchanger 7 tube side top mouths of pipe; The hot water heat exchanger 7 tube sides bottom mouth of pipe links to each other with the split product water cooler 6 shell side top mouths of pipe; The split product water cooler 6 shell sides bottom mouth of pipe links to each other with knockout drum 8 tops inlet, and knockout drum 8 outlet at bottoms link to each other with reaction liquid pump 9 inlets; 9 outlets of reaction liquid pump link to each other with 14 tops, absorption tower; Knockout drum 8 top gaseous phase outlets link to each other with rich gas compressor 10; Rich gas compressor 10, pneumatic press outlet air cooler 11, pneumatic press outlet water cooler 12, pneumatic press outlet divide flow container 13 to link to each other successively; The pneumatic press outlet divides flow container 13 top gaseous phase outlets to link to each other with 14 bottoms, absorption tower; The pneumatic press outlet divides flow container 13 outlet at bottoms to link to each other with desorption tower fresh feed pump 19.
Described absorbing-stabilizing system comprises: oil pump 17, desorption tower 18, desorption tower fresh feed pump 19, desorption tower feed exchanger 20, desorption tower reboiler 21, stabilizer tower 22, stabilizer tower fresh feed pump 23, stabilizer tower feed exchanger 24, stabilizer tower reboiler 25, stabilizer tower head space cooler 26 at the bottom of absorption tower 14, stage casing, absorption tower pump 15, stage casing, absorption tower water cooler 16, the absorption tower, stablize cat head water cooler 27, stablize return tank of top of the tower 28, stabilizer tower reflux pump 29, lighter hydrocarbons water cooler 30, absorb oil pump 31, absorb oil cooler 32, dry gas divides flow container 33;
The bottom on absorption tower 14 oil pump 17 at the bottom of the absorption tower links to each other with pneumatic press outlet air cooler 11 inlets, and the top on absorption tower 14 divides flow container 33 to link to each other with dry gas; Dry gas divides the top of flow container 33 to link to each other with the dry gas feed exchanger 34 shell sides bottom mouth of pipe; Dry gas divides the bottom of flow container 33 to link to each other with stabilizer tower reflux pump 29 inlets; The outlet of stabilizer tower reflux pump 29 links to each other with stabilizer tower 22 tops and the depropanizing tower feed preheater 41 tube sides bottom mouth of pipe respectively;
Stage casing, parallelly connected successively absorption tower, 14 middle parts pump 15 and stage casing, absorption tower water cooler 16 on the absorption tower;
Desorption tower fresh feed pump 19 links to each other with the top of desorption tower 18, and desorption tower fresh feed pump 19 also links to each other through the top of desorption tower feed exchanger 20 with desorption tower 18;
Desorption tower 18 is provided with desorption tower reboiler 21 at the bottom of tower; Desorption tower 18 all links to each other with pneumatic press outlet air cooler 11 with rich gas compressor 10; The bottom of desorption tower 18 links to each other with the middle part of stabilizer tower 22 through stabilizer tower fresh feed pump 23, stabilizer tower feed exchanger 24 successively;
Stabilizer tower 22 is provided with stabilizer tower reboiler 25 at the bottom of tower; The top of stabilizer tower 22 according to, inferior through stabilizer tower head space cooler 26, stabilizer tower condensing surface 27, stablize return tank of top of the tower 28 continuous successively; The jar end of stablizing return tank of top of the tower 28, link to each other with the top and the depropanizing tower feed preheater 41 of stabilizer tower 22 respectively through stablizing cat head reflux pump 29;
At the bottom of the tower of stabilizer tower 22, stabilizer tower feed exchanger 24, desorption tower feed exchanger 20, lighter hydrocarbons water cooler 30 link to each other successively; Lighter hydrocarbons water cooler 30 links to each other with stripping tower feed exchanger 48, and lighter hydrocarbons water cooler 30 also links to each other with the top on absorption tower 14 through absorption oil pump 31, absorption oil cooler 32 successively.
Described aromatization system comprises: dry gas feed exchanger 34, dry gas electric heater 35, aromatization reactor 36, aromizing product water cooler 37, aromizing product deep freezer 38, aromizing product knockout drum 39, dry gas circulator 40;
The dry gas feed exchanger 34 shell side top mouths of pipe link to each other through the top of dry gas electric heater 35 with aromatization reactor 36 successively; The dry gas feed exchanger 34 tube side top mouths of pipe also link to each other with the bottom of aromatization reactor 36; Dry gas feed exchanger 34 tube sides bottom, aromizing product water cooler 37, aromizing product deep freezer 38, aromizing product knockout drum 39 link to each other successively; Dry gas divides the top of flow container 33 to link to each other with the middle part of dry gas circulator 40 with aromatization reactor 36 respectively;
Aromizing product knockout drum 39 links to each other with process furnace 4, and aromizing product knockout drum 39 also links to each other with aromatization reactor 36 through dry gas circulator 40, dry gas feed exchanger 34, dry gas electric heater 35 successively.
Described gas divides the virgin gas upgrading system, comprising: depropanizing tower feed preheater 41, depropanizing tower 42, depropanizing tower reboiler 43, depropanizing tower head space cooler 44, depropanizing cat head condensing surface 45, depropanizing tower item return tank 46, depropanizing tower reflux pump 47;
The jar end of stablizing return tank of top of the tower 28, link to each other with depropanizing tower feed preheater 41, depropanizing tower 42 through stabilizer tower reflux pump 29 successively;
The top of depropanizing tower 42 links to each other with depropanizing tower head space cooler 44, depropanizing cat head condensing surface 45, depropanizing cat head return tank 46, depropanizing cat head reflux pump 47 successively, and forms the loop; Depropanizing cat head reflux pump 47 also links to each other with gas separation unit;
Described lighter hydrocarbons purification system comprises: feed exchanger 48, electric heater 49, stripping tower 50, stripping tower reboiler 51, stripping overhead condenser 52, stripping return tank of top of the tower 53, stripping tower reflux pump 54, forced circulation pump 55;
Stripping tower feed exchanger 48 links to each other with stripping tower 50; Forced circulation pump 55 links to each other with heavy oil tank;
Stripping tower 50 is provided with stripping tower reboiler 51 at the bottom of tower.Stripping tower 50 cats head link to each other with stripping tower feed exchanger 48, stripping overhead condenser 52, stripping return tank of top of the tower 53, stripping tower reflux pump 54 successively, and form the loop; Stripping tower reflux pump 54 also links to each other with gasoline tank.
Need to prove: the various device that is adopted among the present invention, be the conventional equipment that uses in the production technique of this area, and each operation of equipment, parameter etc. carry out according to routine operation all, do not have special feature.
Claims (10)
1. a technology of utilizing liquefied gas processing system hydrocarbon comprises the scission reaction operation, absorbs stabilizing process, aromatization operation, it is characterized in that: comprise that also gas divides virgin gas to carry dense operation and aromatic hydrocarbons purification process;
Wherein, described gas divides virgin gas to put forward dense operation to be:
Gas from absorb stabilizing process divides virgin gas after a stabilizer tower reflux pump part gets into the temperature raising of depropanizing tower feed preheater, to get into depropanizing tower from the jar end of stablizing return tank of top of the tower, carries out the separation of carbon three, carbon four components;
C3 fraction steams from the depropanizing tower top; After depropanizing tower head space cooler and condensing surface cooling; Get into depropanizing cat head return tank; Be divided into two portions after phlegma is extracted out by the depropanizing tower reflux pump: a part is used as depropanizing tower and refluxes, and another part divides raw material to send into gas separation unit or deliver to gas and divide head tank to store as gas;
Carbon four components of coming out at the bottom of the depropanizing tower get into the MTBE device and participate in reaction or send into the storage of carbon four head tanks as raw material.
2. the technology of utilizing liquefied gas processing system hydrocarbon according to claim 1 is characterized in that described aromatic hydrocarbons purification process is:
The aromatic hydrocarbons that from absorb stabilizing process, comes out in the lighter hydrocarbons water cooler of stabilizer tower and the aromizing product knockout drum in the aromatization operation gets into stripping tower from the stripping tower stage casing after the gas phase heat exchange at feed exchanger and stripping tower top;
The light aromatic hydrocarbons of original gasoline carries out mass-and heat-transfer in the aromatic hydrocarbons of entering stripping tower and the tower, is divided into heavy constituent and light constituent;
Heavy constituent are displaced downwardly at the bottom of the tower, and through further heating, the extraction behind the forced circulation pump pressure-raising of part heavy constituent is simultaneously delivered to heavy oil tank and stored;
The light constituent evaporation is risen; And fully vaporization; After the light constituent that rises escapes into feed exchanger from cat head, after overhead condenser further is cooled to 30 ℃, get into return tank; Behind the reflux pump pressure-raising, be divided into two portions: a part as aromatic hydrocarbon product extraction deliver to gasoline tank and store, another part gets into stripping tower as refluxing from cat head.
3. the technology of utilizing liquefied gas processing system hydrocarbon according to claim 1 is characterized in that described scission reaction operation is:
The carbon 4 liquid gas raw material of cracking stock jar passes through feedstock pump; Carry out heat exchange through first interchanger, second interchanger and cleavage reaction product successively; Carbon four raw materials after the heat exchange get into process furnace again; Further temperature raising to 500 ℃, the gas after the temperature raising gets into cracking reactor from the top of cracking reactor, carries out scission reaction;
Cleavage reaction product is from the bottom of cracking reactor, carries out the heat exchange cooling through second interchanger, first interchanger, hot water heat exchanger, split product water cooler successively, reduce to 40 ℃ to temperature after, get into knockout drum and separate; Separate the lime set that obtains and be pumped into the absorption tower with reaction liquid; Separating the gas that obtains compresses, cools off through rich gas compressor.
4. the technology of utilizing liquefied gas processing system hydrocarbon according to claim 1 is characterized in that described absorption stabilizing process is:
Gas from the scission reaction operation after the rich gas compressor compression; With exporting water cooler through pneumatic press outlet air cooler, pneumatic press successively from the absorption oil of bottom, absorption tower and the stripping gas of desorb top of tower; Get into the pneumatic press outlet after being cooled to 40 ℃ and divide flow container, oil, gas are separated;
Divide the top of flow container to separate out rich gas and be delivered to the bottom, absorption tower from the pneumatic press outlet; In the absorption tower with the absorption agent counter current contact that gets into from top, absorption tower; Lean gas after absorbing gets into dry gas and divides flow container from the top, absorption tower; Carry out gas-liquid separation, liquid imports stabilizer tower and refluxes, and delivers to aromatization reactor from the dry gas that comes out in dry gas separatory tank top;
Extract the gasoline of mid-pumparound at the middle part, absorption tower out with stage casing, absorption tower pump, water cooler is cooled to 20 ℃ through the stage casing, absorption tower, returns the absorption tower again;
From the lime set that pneumatic press outlet separatory pot bottom comes out, be divided into two-way through the desorption tower fresh feed pump: the one tunnel directly gets into the desorption tower top, and another road is through desorption tower feed exchanger heat exchange to 70 ℃ entering desorption tower top;
Stripping gas is overflowed from cat head, converges with the compression rich gas of rich gas compressor to get into pneumatic press outlet air cooler; Desorb gasoline gets in the middle part of the stabilizer tower from extracting out with the stabilizer tower fresh feed pump at the bottom of the desorption tower after the stable gasoline heat exchange to 125 at the bottom of stabilizer tower feed exchanger and the stabilizer tower ℃;
Carbon four and the component of carbon below four distillate from stablizing cat head; Pass through stabilizer tower head space cooler, stablize overhead condenser entering stablizing return tank of top of the tower; Gas is divided into two-way after dividing virgin gas to extract out through the stabilizer tower reflux pump from the jar end of stablizing return tank of top of the tower: the one tunnel does to reflux returns the stabilizer tower top, and another road gets into the depropanizing tower feed preheater;
The stable gasoline of stabilizer tower comes out at the bottom of tower; Successively after stabilizer tower feed exchanger, desorption tower feed exchanger, lighter hydrocarbons water cooler are cooled to 30 ℃; Separated into two parts: a part gets into stripping tower after getting into the light aromatic hydrocarbons heat exchange of product gasoline of stripping tower feed exchanger and the backflow extraction of stripping tower top, and another part is cooled to 20 ℃ and delivers to the top, absorption tower and make absorption agent through absorbing oil pump pressurization, absorption oil cooler.
5. the technology of utilizing liquefied gas processing system hydrocarbon according to claim 1 is characterized in that described aromatization operation is:
The dry gas that come out in dry gas separatory tank top from absorb stabilizing process and the fuel gas of dry gas circulator converge the back separated into two parts: a part at first gets into the dry gas feed exchanger as main line; Carry out heat exchange with the gas behind the aromatization; After further being heated to 300 ℃ to the dry gas electric heater again; Get into from the aromatization reactor top, contact with aromatized catalyst and carry out aromatization; Another part directly gets into aromatization reactor and carries out aromatization;
Gas behind the aromatization gets into the dry gas feed exchanger after coming out from the aromatization reactor bottom; After the heat exchange of raw material dry gas; After process aromizing product water cooler and aromizing product deep freezer are reduced to 20 ℃; Carry out gas-liquid separation to aromizing product knockout drum, gas phase is divided into two portions: a part gets into the process furnace gas that acts as a fuel, and another part returns aromatization reactor after the compression of dry gas circulator; Liquid phase gets into the stripping tower feed exchanger.
6. realize the device that utilizes liquefied gas processing process for producing hydrocarbons as claimed in claim 1 for one kind, comprise that the scission reaction system, absorbing-stabilizing system, aromatization system, the gas that are communicated with successively divide virgin gas upgrading system, aromatic hydrocarbons purification system;
Wherein, Described gas divides the virgin gas upgrading system, comprising: depropanizing tower feed preheater (41), depropanizing tower (42), depropanizing tower head space cooler (44), depropanizing cat head condensing surface (45), depropanizing tower item return tank (46), depropanizing tower reflux pump (47);
The jar end of stablizing return tank of top of the tower (28), link to each other with depropanizing tower feed preheater (41), depropanizing tower (42) through stabilizer tower reflux pump (29) successively;
The top of depropanizing tower (42) links to each other with depropanizing tower head space cooler (44), depropanizing cat head condensing surface (45), depropanizing cat head return tank (46), depropanizing cat head reflux pump (47) successively, and forms the loop; Depropanizing cat head reflux pump (47) also links to each other with gas separation unit.
7. the device that utilizes liquefied gas processing system hydrocarbon according to claim 6 is characterized in that:
Described lighter hydrocarbons purification system comprises: feed exchanger (48), electric heater (49), stripping tower (50), stripping overhead condenser (52), stripping return tank of top of the tower (53), stripping tower reflux pump (54), forced circulation pump (55);
Stripping tower feed exchanger (48) links to each other with stripping tower (50); Forced circulation pump (55) links to each other with heavy oil tank;
Stripping tower (50) cat head links to each other with stripping tower feed exchanger (48), stripping overhead condenser (52), stripping return tank of top of the tower (53), stripping tower reflux pump (54) successively, and forms the loop; Stripping tower reflux pump (54) also links to each other with gasoline tank.
8. the device that utilizes liquefied gas processing system hydrocarbon according to claim 6 is characterized in that:
Described scission reaction system comprises: feedstock pump (1), first interchanger (2), second interchanger (3), process furnace (4), cracking reactor (5), reaction product water cooler (6), hot water heat exchanger (7), knockout drum (8), reaction liquid pump (9), rich gas compressor (10), pneumatic press outlet air cooler (11), pneumatic press outlet water cooler (12), pneumatic press outlet divide a flow container (13);
Feedstock pump (1) outlet links to each other with first interchanger (2) the shell side bottom mouth of pipe; First interchanger (2) the shell side top mouth of pipe links to each other with second interchanger (3) the shell side bottom mouth of pipe, and second interchanger (3) the shell side top mouth of pipe links to each other with the middle part of process furnace (4) inlet, cracking reactor (5) respectively; Process furnace (4) outlet links to each other with cracking reactor (5) top;
The bottom of cracking reactor (5) links to each other with second interchanger (3) the tube side top mouth of pipe; Second interchanger (3) the tube side bottom mouth of pipe links to each other with first interchanger (2) the tube side top mouth of pipe; First interchanger (2) the tube side bottom mouth of pipe links to each other with hot water heat exchanger (7) the tube side top mouth of pipe; Hot water heat exchanger (7) the tube side bottom mouth of pipe links to each other with split product water cooler (6) the shell side top mouth of pipe; Split product water cooler (6) the shell side bottom mouth of pipe links to each other with knockout drum (8) top inlet, and knockout drum (8) outlet at bottom links to each other with reaction liquid pump (9) inlet; Reaction liquid pump (9) outlet links to each other with top, absorption tower (14); Knockout drum (8) top gaseous phase outlet links to each other with rich gas compressor (10); Rich gas compressor (10), pneumatic press outlet air cooler (11), pneumatic press outlet water cooler (12), pneumatic press outlet divide flow container (13) to link to each other successively; The pneumatic press outlet divides flow container (13) top gaseous phase outlet to link to each other with bottom, absorption tower (14); The pneumatic press outlet divides flow container (13) outlet at bottom to link to each other with desorption tower fresh feed pump (19).
9. the device that utilizes liquefied gas processing system hydrocarbon according to claim 6 is characterized in that:
Described absorbing-stabilizing system comprises: oil pump (17), desorption tower (18), desorption tower fresh feed pump (19), desorption tower feed exchanger (20), stabilizer tower (22), stabilizer tower fresh feed pump (23), stabilizer tower feed exchanger (24), stabilizer tower head space cooler (26) at the bottom of absorption tower (14), stage casing, absorption tower pump (15), stage casing, absorption tower water cooler (16), the absorption tower, stablize cat head water cooler (27), stablize return tank of top of the tower (28), stabilizer tower reflux pump (29), lighter hydrocarbons water cooler (30), absorb oil pump (31), absorb oil cooler (32), dry gas divides flow container (33);
The bottom on absorption tower (14) oil pump (17) at the bottom of the absorption tower links to each other with pneumatic press outlet air cooler (11) inlet, and the top of absorption tower (14) divides flow container (33) to link to each other with dry gas; Dry gas divides the top of flow container (33) to link to each other with dry gas feed exchanger (34) the shell side bottom mouth of pipe; Dry gas divides the bottom of flow container (33) to link to each other with stabilizer tower reflux pump (29) inlet; The outlet of stabilizer tower reflux pump (29) links to each other with stabilizer tower (22) top and depropanizing tower feed preheater (41) the tube side bottom mouth of pipe;
(14) middle part stage casing, parallelly connected successively absorption tower pump (15) and stage casing, absorption tower water cooler (16) on the absorption tower;
Desorption tower fresh feed pump (19) links to each other with the top of desorption tower (18), and desorption tower fresh feed pump (19) also links to each other through the top of desorption tower feed exchanger (20) with desorption tower (18);
Desorption tower (18) all links to each other with pneumatic press outlet air cooler (11) with rich gas compressor (10); The bottom of desorption tower (18) links to each other with the middle part of stabilizer tower (22) through stabilizer tower fresh feed pump (23), stabilizer tower feed exchanger (24) successively;
The top of stabilizer tower (22) links to each other with stable return tank of top of the tower (28) through stabilizer tower head space cooler (26), stabilizer tower condensing surface (27) successively; The jar end of stablizing return tank of top of the tower (28), link to each other with the top and the depropanizing tower feed preheater (41) of stabilizer tower (22) respectively through stablizing cat head reflux pump (29);
Link to each other successively with stabilizer tower feed exchanger (24), desorption tower feed exchanger (20), lighter hydrocarbons water cooler (30) at the bottom of the tower of stabilizer tower (22): lighter hydrocarbons water cooler (30) links to each other with stripping tower feed exchanger (48), and lighter hydrocarbons water cooler (30) also links to each other with the top of absorption tower (14) through absorption oil pump (31), absorption oil cooler (32) successively.
10. the device that utilizes liquefied gas processing system hydrocarbon according to claim 6; It is characterized in that: described aromatization system comprises: dry gas feed exchanger (34), dry gas electric heater (35), aromatization reactor (36), aromizing product water cooler (37), aromizing product deep freezer (38), aromizing product knockout drum (39), dry gas circulator (40);
Dry gas feed exchanger (34) the shell side top mouth of pipe links to each other with the top of aromatization reactor (36); Dry gas feed exchanger (34) the tube side top mouth of pipe links to each other with the bottom of aromatization reactor (36); Dry gas feed exchanger (34) tube side bottom links to each other with aromizing product water cooler (37), aromizing product deep freezer (38), aromizing product knockout drum (39) successively; Dry gas divides the top of flow container (33) to link to each other with the middle part of dry gas circulator (40) with aromatization reactor (36) respectively;
Aromizing product knockout drum (39) links to each other with process furnace (4), and aromizing product knockout drum (39) also links to each other with aromatization reactor (36) through dry gas circulator (40).
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| CN201110387102.XA CN102516007B (en) | 2011-11-29 | 2011-11-29 | Process and device for processing and preparing hydrocarbon by utilizing liquefied gas |
| CN201310485574.8A CN103755508B (en) | 2011-11-29 | 2011-11-29 | A kind of technique utilizing liquefied gas processing and preparing hydrocarbon |
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| CN201110387102.XA CN102516007B (en) | 2011-11-29 | 2011-11-29 | Process and device for processing and preparing hydrocarbon by utilizing liquefied gas |
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| CN107603669A (en) * | 2017-10-26 | 2018-01-19 | 中国石油化工股份有限公司 | The ethylene recovery system of catalytic cracked dry gas |
| CN108865212A (en) * | 2018-07-13 | 2018-11-23 | 佛山市三水区精联自动化设备有限公司 | A kind of crude flashing device |
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| CN103755508B (en) * | 2011-11-29 | 2016-08-17 | 山东东方宏业化工有限公司 | A kind of technique utilizing liquefied gas processing and preparing hydrocarbon |
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