CN202359042U - Device for utilizing liquefied gas to process and produce hydrocarbon - Google Patents
Device for utilizing liquefied gas to process and produce hydrocarbon Download PDFInfo
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- CN202359042U CN202359042U CN201120484643XU CN201120484643U CN202359042U CN 202359042 U CN202359042 U CN 202359042U CN 201120484643X U CN201120484643X U CN 201120484643XU CN 201120484643 U CN201120484643 U CN 201120484643U CN 202359042 U CN202359042 U CN 202359042U
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Abstract
The utility model discloses a device for utilizing liquefied gas to process and produce hydrocarbon. The device comprises a cracking reaction system, an absorption stabilizing system, an aromatization reaction system, a gas raw material gas stripping and concentrating system and an aromatic hydrocarbon purifying system. The device disclosed by the utility model has the advantages that the energy consumption is low; after the process disclosed by the utility model is utilized, a deisobutanizer is stopped; 90 kg of standard coal is consumed to process each ton of C4 raw materials and the energy consumption is saved by 48.5%; the content of gas propylene in a gas raw material is high, the previous mass fraction is improved to 50% from 15%, and the requirements of equipment and heat energy are low, so that the device is easy to realize; and the device disclosed by the utility model has the advantages of simple flow, easiness for manipulation and stability in operation.
Description
Technical field
The present invention relates to a kind of liquefied gas deep processing technology, specifically a kind of device 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 device that utilizes liquefied gas processing system hydrocarbon, this device simply, be easy to control, energy consumption is low, quality product is high.
Technical scheme of the present invention is:
A kind of device that utilizes liquefied gas processing system hydrocarbon comprises that scission reaction system, absorbing-stabilizing system, aromatization system, gas divide virgin gas to carry concentration systems, aromatic hydrocarbons purification system;
Described scission reaction system comprises that 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, stablizes the cat head water cooler, stablizes 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 is provided with the desorption tower reboiler at the bottom of tower; 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;
Stabilizer tower is provided with the stabilizer tower reboiler at the bottom of tower; The top of stabilizer tower, through 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;
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 to comprise 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;
Depropanizing tower reboiler to tower in the heat supply of 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;
Described stripping tower is provided with the stripping tower reboiler at the bottom of tower; 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.
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 is the connection synoptic diagram 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
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 to carry concentration systems, aromatic hydrocarbons purification system;
Described scission reaction system comprises that 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 absorption tower 14; Stage casing, absorption tower pump 15; Stage casing, absorption tower water cooler 16; Oil pump 17 at the bottom of the absorption tower; 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; 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 to comprise 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;
Depropanizing tower 42 is by depropanizing tower reboiler 43 heat supply in tower at the bottom of the tower, and thermal source adopts thermal oil;
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 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.
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%.
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 device that utilizes liquefied gas processing system hydrocarbon comprises 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.
2. the device that utilizes liquefied gas processing system hydrocarbon according to claim 1 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).
3. the device that utilizes liquefied gas processing system hydrocarbon according to claim 1 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.
4. the device that utilizes liquefied gas processing system hydrocarbon according to claim 1 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).
5. the device that utilizes liquefied gas processing system hydrocarbon according to claim 1 is characterized in that:
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.
6. the device that utilizes liquefied gas processing system hydrocarbon according to claim 1 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.
7. the device that utilizes liquefied gas processing system hydrocarbon according to claim 3, it is characterized in that: described desorption tower (18) is provided with desorption tower reboiler (21) at the bottom of tower.
8. the device that utilizes liquefied gas processing system hydrocarbon according to claim 3, it is characterized in that: described stabilizer tower (22) is provided with stabilizer tower reboiler (25) at the bottom of tower.
9. the device that utilizes liquefied gas processing system hydrocarbon according to claim 5, it is characterized in that: described depropanizing tower (42) is provided with depropanizing tower reboiler (43) at the bottom of tower.
10. the device that utilizes liquefied gas processing system hydrocarbon according to claim 6, it is characterized in that: described stripping tower is provided with stripping tower reboiler (51) at the bottom of tower.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201120484643XU CN202359042U (en) | 2011-11-29 | 2011-11-29 | Device for utilizing liquefied gas to process and produce hydrocarbon |
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| CN201120484643XU CN202359042U (en) | 2011-11-29 | 2011-11-29 | Device for utilizing liquefied gas to process and produce hydrocarbon |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102516007A (en) * | 2011-11-29 | 2012-06-27 | 山东东方宏业化工有限公司 | Process and device for processing and preparing hydrocarbon by utilizing liquefied gas |
| CN103755508A (en) * | 2011-11-29 | 2014-04-30 | 山东东方宏业化工有限公司 | Device for processing preparation of hydrocarbon by utilizing liquefied gas |
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2011
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102516007A (en) * | 2011-11-29 | 2012-06-27 | 山东东方宏业化工有限公司 | Process and device for processing and preparing hydrocarbon by utilizing liquefied gas |
| CN102516007B (en) * | 2011-11-29 | 2014-03-26 | 山东东方宏业化工有限公司 | Process and device for processing and preparing hydrocarbon by utilizing liquefied gas |
| CN103755508A (en) * | 2011-11-29 | 2014-04-30 | 山东东方宏业化工有限公司 | Device for processing preparation of hydrocarbon by utilizing liquefied gas |
| 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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