CN202853258U - Gas separation device for liquefied petroleum gas aromatization tail gas - Google Patents
Gas separation device for liquefied petroleum gas aromatization tail gas Download PDFInfo
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- CN202853258U CN202853258U CN201220436481.7U CN201220436481U CN202853258U CN 202853258 U CN202853258 U CN 202853258U CN 201220436481 U CN201220436481 U CN 201220436481U CN 202853258 U CN202853258 U CN 202853258U
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Abstract
The utility model discloses a gas separation device for liquefied petroleum gas aromatization tail gas. The gas separation device comprises a liquefied petroleum gas aromatization tail gas supplying device, a fine desulfurization device, a compressor, a hydrocarbon mixed rectifying tower, a drying device, a first heat exchanger and a liquefied petroleum gas rectifying tower, wherein the inlet of the fine desulfurization device is connected with the liquefied petroleum gas aromatization tail gas supplying device through a pipeline, the compressor is connected with the outlet of the fine desulfurization device through a pipeline provided with a cooling device, the inlet of the hydrocarbon mixed rectifying tower is connected with the compressor through a pipeline, the inlet of the drying device is connected with the outlet of the tower top of the hydrocarbon mixed rectifying tower through a pipeline, the first heat exchanger comprises a plurality of hot fluid flow channels and a plurality of cold fluid flow channels, wherein the inlet of a first hot fluid flow channel is connected with the outlet of the drying device through a pipeline, and the inlet of the liquefied petroleum gas rectifying tower is connected with the outlet of the first hot fluid flow channel of the first heat exchanger through a pipeline. According to the gas separation device for the liquefied petroleum gas aromatization tail gas, higher extraction efficiency and purity of products can be obtained by utilizing less energy consumption and investment.
Description
Technical field
The utility model belongs to the gas separating technology field, is specifically related to a kind of gas separating technology and device thereof of liquefied petroleum gas aromatisation tail gas.
Background technology
Benzene in the aromatic hydrocarbons, toluene and dimethylbenzene (BTX) are widely used in synthetic fibers, resin, rubber and various fine chemicals.Add up according to World PetrochemicalsSRI Consulting, between 2005-2010, the average demand growth rate of whole world benzene, toluene and dimethylbenzene reaches respectively 4.4%, 3 ~ 4% and 5.4%, and the same period China to the growth rate of demand of benzene, toluene and dimethylbenzene up to 16%, 8.2% and 19.1%.In recent years, because the development of aromatic hydrocarbons downstream product rapidly, the domestic and international market is for the demand sustainable growth of aromatic hydrocarbons, and China has been the net importer of triphen.BTX is mainly derived from platforming technique and preparing ethylene by steam cracking technique.Platforming process using precious metals pt series catalysts take naphtha (direct steaming gasoline) as raw material, is produced aromatic hydrocarbons by courses of reaction such as dehydrogenations.The drippolene of by-product can be used for extracting aromatic hydrocarbons through behind the hydrogenation in the preparing ethylene by steam cracking technique.Because the naphtha resource of the high aromatic hydrocarbons of China is few, therefore provide BTX to be very limited in China with platforming technique.Therefore, the volume increase new way of exploring aromatic hydrocarbons actively in China is significant for supporting national sustained economic development.Take the abundant liquefied petroleum gas of originating as raw material, produce industrial chemicals-triphen of many uses and that added value is higher by aromatisation, can satisfy the demand of domestic market, create obvious economic benefit.
The main component of aromatisation tail gas has hydrogen, methane, ethane, ethene, propane, butane, butylene, pentane, the above alkane of pentane, benzene, methane etc.From aromatisation tail gas, reclaim the hydrocarbon that C5+(contains 5 above carbon atoms), the LPG(liquefied gas) (carbon three, carbon four components) product and dry gas ((carbon two following components, comprise hydrogen, methane and carbon two components)) can realize taking full advantage of of resource, minimizing is created considerable economic benefit simultaneously to the pollution of environment.At present, the gas separating technology of the aromatisation tail gas of prior art, and immature exists that separative efficiency is low, energy utilization rate is low, equipment is complicated, the high in cost of production shortcoming, therefore demand developing a kind of gas separating technology of new aromatisation tail gas urgently, so that each gas is fully recycled.
The utility model content
In order to solve the problems of the technologies described above, the utility model provides a kind of gas fractionation unit of liquefied petroleum gas aromatisation tail gas, comprising:
Liquefied petroleum gas aromatisation tail gas feeding mechanism;
Smart desulfurizer, its entrance is connected with above-mentioned liquefied petroleum gas aromatisation tail gas feeding mechanism by pipeline;
Compressor is connected with the outlet of above-mentioned smart desulfurizer by the pipeline that is provided with cooler;
Mixed hydrocarbon rectifying column, its entrance is connected with above-mentioned compressor by pipeline, and the cat head of above-mentioned mixed hydrocarbon rectifying column is provided with overhead condenser, is provided with tower bottom reboiler at the bottom of the tower;
Drying device, its entrance is connected by the tower top outlet of pipeline with above-mentioned mixed hydrocarbon rectifying column;
First Heat Exchanger, it comprises multiply zone of heat liberation and multiply cold fluid pass, wherein the first zone of heat liberation entrance is connected with above-mentioned drying device outlet by pipeline;
The liquefied gas rectifying column, its entrance is connected with the first zone of heat liberation outlet of above-mentioned First Heat Exchanger by pipeline, and the cat head of above-mentioned liquefied gas rectifying column is provided with overhead condenser, is provided with tower bottom reboiler at the bottom of the tower.
Preferably, the gas fractionation unit of above-mentioned liquefied petroleum gas aromatisation tail gas also comprises: the second heat exchanger, it comprises gas passage and heat exchange media channel, be located on the pipeline between above-mentioned liquefied petroleum gas aromatisation tail gas feeding mechanism and the above-mentioned smart desulfurizer entrance, wherein, the gas passage entrance of the second heat exchanger is connected with above-mentioned liquefied petroleum gas aromatisation tail gas feeding mechanism by pipeline, and the gas passage outlet of the second heat exchanger is connected with the entrance of above-mentioned smart desulfurizer by pipeline; The heat exchange media channel entrance of the second heat exchanger is connected with the tower bottom outlet of above-mentioned mixed hydrocarbon rectifying column by pipeline.
The tower bottom reboiler of preferably, the outlet of above-mentioned smart desulfurizer, above-mentioned liquefied gas rectifying column, above-mentioned cooler are connected pipeline with above-mentioned compressor and sequentially connect.
Preferably, the gas fractionation unit of above-mentioned liquefied petroleum gas aromatisation tail gas also comprises the cryogen compressor, and the cryogen entrance of the second zone of heat liberation of the outlet of cryogen compressor, above-mentioned First Heat Exchanger, choke valve and liquefied gas rectifying column cat head condenser sequentially is communicated with by pipeline; The cryogen outlet of liquefied gas rectifying column cat head condenser, the first cold fluid pass of above-mentioned First Heat Exchanger and the entrance of cryogen compressor sequentially are communicated with by pipeline.
Preferably, the tower top outlet of above-mentioned liquefied gas rectifying column is communicated with the second cold fluid pass of above-mentioned First Heat Exchanger by pipeline.
More preferably, the regeneration gas entrance of the second cold fluid pass of the tower top outlet of described liquefied gas rectifying column, described First Heat Exchanger and described drying device sequentially is communicated with by pipeline.
Preferably, the gas fractionation unit of above-mentioned liquefied petroleum gas aromatisation tail gas, also comprise decompressor, the 3rd cold fluid pass of the expanding end of the second cold fluid pass of the tower top outlet of above-mentioned liquefied gas rectifying column, above-mentioned First Heat Exchanger, above-mentioned decompressor, above-mentioned First Heat Exchanger and above-mentioned decompressor pressurized end sequentially be communicated with by pipeline.
More preferably, the 3rd cryogen passage of the tower top outlet of described liquefied gas rectifying column, described First Heat Exchanger, the expanding end of described decompressor, the 3rd cold fluid pass of described First Heat Exchanger, described decompressor pressurized end and the regeneration gas entrance of described drying device sequentially be communicated with by pipeline.
Preferably, above-mentioned First Heat Exchanger is plate-fin heat exchanger.
Adopt technique of the present utility model and device, can realize obtaining larger product recovery rate and purity with lower energy consumption and investment.Target level of product quality can reach:
1) in the dry gas product carbon three above components less than the 0.2%(mass fraction);
2) in liquefied gas (carbon three, carbon four components) the LPG product carbon two following components less than the 0.1%(mass fraction), carbon five above components are less than the 0.3%(mass fraction);
3) in the C5+ product carbon four following components (hydrocarbon of carbon atom quantity below 4) less than the 0.2%(mass fraction).
Description of drawings
Fig. 1 is the device schematic diagram of the utility model embodiment 1.
Fig. 2 is the device schematic diagram of the utility model embodiment 2.
1, liquefied petroleum gas aromatisation tail gas feeding mechanism; 2, the second heat exchanger; 3, smart desulfurizer; 4, cooler; 5, compressor; 6, mixed hydrocarbon rectifying column; 601 overhead condensers; 602, tower bottom reboiler; 7, drying device; 8, First Heat Exchanger; 9, cryogen compressor; 10 choke valves; 11, liquefied gas rectifying column; 1101, overhead condenser; 1102, tower bottom reboiler; 12, decompressor; 1201, expanding end; 1202, pressurized end.
The specific embodiment
The utility model is described in further detail below in conjunction with the drawings and specific embodiments, so that those skilled in the art can better understand the utility model and being implemented, but illustrated embodiment is not as to restriction of the present utility model.
As shown in Figure 1, the gas fractionation unit of liquefied petroleum gas aromatisation tail gas of the present utility model comprises:
Liquefied petroleum gas aromatisation tail gas feeding mechanism 1;
Smart desulfurizer 3, its entrance is connected with liquefied petroleum gas aromatisation tail gas feeding mechanism 1 by pipeline;
Compressor 5 is connected with the outlet of smart desulfurizer 3 by the pipeline that is provided with cooler 4;
Mixed hydrocarbon rectifying column 6, its entrance is connected with compressor 5 by pipeline, and the cat head of mixed hydrocarbon rectifying column 6 is provided with overhead condenser 601, is provided with tower bottom reboiler 602 at the bottom of the tower;
Drying device 7, its entrance is connected by the tower top outlet of pipeline with mixed hydrocarbon rectifying column 6;
First Heat Exchanger 8(is preferably plate-fin heat exchanger), it comprises multiply zone of heat liberation and multiply cold fluid pass, wherein the first zone of heat liberation is communicated with drying device 7 outlets by pipeline;
Liquefied gas rectifying column 11, its entrance is connected with the first zone of heat liberation outlet of First Heat Exchanger 8 by pipeline, and the cat head of liquefied gas rectifying column 11 is provided with overhead condenser 1101, is provided with tower bottom reboiler 1102 at the bottom of the tower.
Be fully used for the heat that makes the C5+ product (molecular formula contains the hydrocarbon of 5 above carbon atoms) that obtains at the bottom of mixed hydrocarbon rectifying column 6 towers, the gas fractionation unit of liquefied petroleum gas aromatisation tail gas of the present utility model also comprises the second heat exchanger 2.This second heat exchanger 2 comprises that (when the second heat exchanger 2 was lamella heat exchanger, two passages referred to respectively shell side and plate journey for gas passage and heat exchange media channel; When the second heat exchanger 2 was shell-and-tube heat exchanger, two passages referred to respectively shell side and tube side).This second heat exchanger 2 is located on the pipeline between liquefied petroleum gas aromatisation tail gas feeding mechanism 1 and the smart desulfurizer 2, namely, the gas passage entrance of the second heat exchanger 2 is connected with liquefied petroleum gas aromatisation tail gas feeding mechanism 1 by pipeline, and the gas passage outlet of the second heat exchanger 2 is connected by the entrance of pipeline with smart desulfurizer 3; The heat exchange media channel entrance of the second heat exchanger 2 is connected with the tower bottom outlet of mixed hydrocarbon rectifying column 6 by pipeline.
For the heat that makes smart desulfurizer 3 exit gas is fully used, the outlet of smart desulfurizer 3, the tower bottom reboiler 1102 of liquefied gas rectifying column, cooler 4 are connected with compressor and are sequentially connected by pipeline, so that the gas of smart desulfurizer 3 outlets is by the tower bottom reboiler 1102 of liquefied gas rectifying column 11, after heat being provided for tower bottom reboiler 1102, by cooler 4, then enter compressor 5 again.
In the gas fractionation unit of liquefied petroleum gas aromatisation tail gas of the present utility model, the cold source device of First Heat Exchanger 8 is circularly cooling.Gas fractionation unit of the present utility model also comprises cryogen compressor 9, and the cryogen entrance of the second zone of heat liberation of the outlet of cryogen compressor 9, First Heat Exchanger 8, choke valve 10 and liquefied gas rectifying column 11 overhead condensers 1101 sequentially is communicated with by pipeline; The cryogen outlet of liquefied gas rectifying column 11 overhead condensers 1101, the first cold fluid pass of First Heat Exchanger 8 and the entrance of cryogen compressor 9 sequentially are communicated with by pipeline.
For giving from liquefied gas rectifying column 11 cats head dry gas rewarming out, the tower top outlet of liquefied gas rectifying column 11 is communicated with the second cold fluid pass of First Heat Exchanger 8 by pipeline.
Dry gas behind the rewarming can be used for the regeneration of drying device 7, and the second cold fluid pass of the tower top outlet of liquefied gas rectifying column 11, First Heat Exchanger 8 and the regeneration gas entrance of drying device 7 sequentially are communicated with (not shown) by pipeline.
As shown in Figure 2, in another embodiment of the present utility model, the gas fractionation unit of liquefied petroleum gas aromatisation tail gas also comprises decompressor 12, and the 3rd cold fluid pass of the second cold fluid pass of the tower top outlet of liquefied gas rectifying column 11, First Heat Exchanger 8, the expanding end 1201 of decompressor 12, First Heat Exchanger 8 and the pressurized end of decompressor 1202 sequentially are communicated with by pipeline.Dry gas behind the rewarming can be used for the regeneration of drying device, therefore preferably, the 3rd cold fluid pass of the second cold fluid pass of the tower top outlet of liquefied gas rectifying column, First Heat Exchanger, the expanding end of decompressor, First Heat Exchanger, decompressor pressurized end and the regeneration gas entrance of drying device sequentially be communicated with (not shown) by pipeline.
In conjunction with Fig. 1, the gas separating technology of liquefied petroleum gas aromatisation tail gas of the present utility model comprises the steps:
1) desulfurization: liquefied petroleum gas aromatisation tail gas enters smart desulfurizer more than 3,150 ℃ under the temperature after the desulfurization, and gas is cooled to 30 ~ 50 ℃ by cooler 4;
2) contain the separation of the hydrocarbon of 5 above carbon atoms: after the compressed machine 5 of the cooled gas of step 1) is forced into 2 ~ 3MPa, pass into mixed hydrocarbon rectifying column 6, tower bottom reboiler 602 temperature of described mixed hydrocarbon rectifying column 6 are more than 200 ℃, the temperature of the overhead condenser 601 of mixed hydrocarbon rectifying column 6 is 30 ~ 60 ℃, after the rectifying, 6 hydrocarbon that obtain containing 5 above carbon atoms are discharged at the bottom of the mixed hydrocarbon rectifying column, collect, and all the other compositions are discharged from the cat head of mixed hydrocarbon rectifying column 6;
3) separating of liquefied gas and dry gas: after gas drying device 7 dryings of discharging from the cat head of mixed hydrocarbon rectifying column 6 step 2), be cooled to-40 ~-60 ℃ through First Heat Exchanger 8, then enter liquefied gas rectifying column 11, tower bottom reboiler 1102 temperature of liquefied gas rectifying column 11 are made as 70 ~ 90 ℃, the temperature of the overhead condenser 1101 of liquefied gas rectifying column 11 is made as-50 ~-75 ℃, after the rectifying, obtaining liquefied gas at the bottom of the liquefied gas rectifying column discharges, collect, the cat head of liquefied gas rectifying column 11 is discharged dry gas.
The aromatisation of liquefied petroleum gas described in step 1) tail gas enters smart desulfurizer 3 after 2 heating of the second heat exchanger, because the temperature of the hydrocarbon that contains 5 above carbon atoms of discharging at the bottom of mixed hydrocarbon rectifying column 6 towers is very high, for taking full advantage of its heat, the heat exchange medium of the second heat exchanger 2 is step 2) in the hydrocarbon that contains 5 above carbon atoms of discharging at the bottom of mixed hydrocarbon rectifying column 6 towers.
For taking full advantage of the heat of smart desulfurizer 3 exit gas, liquefied petroleum gas aromatisation tail gas enters smart desulfurizer 3 in the step 1), more than 150 ℃ under the temperature after the desulfurization, pass into the tower bottom reboiler 1102 of liquefied gas rectifying column 11, for liquefied gas rectifying column 11 provides boiling hot amount again, self also obtain simultaneously cooling, and then by cooler 4 coolings.
The 8(of First Heat Exchanger described in the step 3) can be plate-fin heat exchanger), comprise multiply zone of heat liberation and multiply cold fluid pass, drying device 7 dried gases are cooled to-40 ~-60 ℃ by the first zone of heat liberation of First Heat Exchanger 8, the cold of this First Heat Exchanger 8 is mainly from the azeotrope kind of refrigeration cycle: azeotrope is compressed to 1.2MPag ~ 5.0MPag through cryogen compressor 9, and after the coolers by cryogen compressor 9 itself are cooled to room temperature, the second zone of heat liberation by First Heat Exchanger 8, temperature reduces liquefy, through choke valve 10 expenditure and pressures, temperature is reduced to-60 ℃ ~-120 ℃, becomes simultaneously gas-liquid two-phase; The overhead condenser 1101 that azeotrope behind the expenditure and pressure is introduced into liquefied gas rectifying column 11 as cold medium to liquefied gas rectifying column 11 cats head give vent to anger freeze after, return again the first cold fluid pass re-heat of this First Heat Exchanger 8, and be that the hot fluid fluid of zone of heat liberation (that is, by) provides cold; Azeotrope becomes the low pressure gaseous fluid after going out this First Heat Exchanger, returns cryogen compressor 9 entrances, so circulation,
Wherein, described azeotrope is the two or more components mixing compositions in methane, ethane or ethene, propane or propylene, butane and the pentane.
The dry gas that the cat head of liquefied gas rectifying column 11 is discharged in the step 3) is by the second cold fluid pass of described First Heat Exchanger 8, carries out heat exchange with the multiply hot fluid of First Heat Exchanger 8, reclaims cold, and rewarming is to room temperature.
Rewarming to the dry gas of room temperature can pass into drying device 7, to remove the moisture that adsorbs in the drying device etc., after drying device 7 is regenerated, discharges and collects dry gas.
As another technical scheme, the dry gas that the cat head of liquefied gas rectifying column 11 is discharged in the step 3) is by the second cold fluid pass of described First Heat Exchanger 8, carry out heat exchange with the multiply hot fluid of First Heat Exchanger 8, reclaim cold, rewarming is to-50 ~ 0 ℃, and rewarming to-50 ~ 0 ℃ dry gas enters expanding end 1201 swell refrigerations of decompressor 12, and then the 3rd cold fluid pass that returns First Heat Exchanger provides cold, after going out First Heat Exchanger, enter 1202 superchargings of decompressor pressurized end.Dry gas after the supercharging passes into drying device 7, to remove the moisture that adsorbs in the drying device etc., after drying device 7 is regenerated, discharges and collects dry gas.
For further the utility model being described, below enumerate two preferred embodiments so that the utility model is described.
As shown in Figure 1, liquefied petroleum gas aromatisation tail gas enters behind the battery limit (BL) first by First Heat Exchanger 2 and out C5+ product (hydrocarbon that contains 5 the above carbon atoms) heat exchange of mixed hydrocarbon rectifying column 6 tower bottom reboilers 601, temperature enters smart desulfurizer 3 after raising, the temperature of smart desulfurizer is made as more than 150 ℃, behind the tower bottom reboiler 1101 and its heat exchange by liquefied gas (LPG) rectifying column 11 behind the gas of desulfurization, by cooler 4(water cooler or air cooler) cooling after enter compressor 5, compressed being forced into enters mixed hydrocarbon rectifying column 6 behind 2 ~ 3MPa, mixed hydrocarbon rectifying column 6 tower bottom reboilers 602 temperature are made as more than 200 ℃, overhead condenser 601 temperature are made as 30 ~ 60 ℃, after the rectifying, obtain the C5+ product at the bottom of mixed hydrocarbon rectifying column 6 towers, through with the heat exchange of liquefied petroleum gas aromatisation tail gas after deliver to out-of-bounds.The gas that mixed hydrocarbon rectifying column 6 cats head are discharged enters the second heat exchanger 8(plate-fin heat exchanger take carbon 4 following components and hydrogen as main behind the drying device 7) the first zone of heat liberation, enter liquefied gas rectifying column 11 when being cooled to-45 ℃.Liquefied gas rectifying column 11 tower bottom reboilers 1102 temperature are made as 70 ~ 90 ℃, and overhead condenser 1101 temperature are made as-50 ~-75 ℃, obtain liquefied gas after the rectifying at the bottom of the tower.Liquefied gas rectifying column 11 cats head obtain take carbon 1, carbon 2 and hydrogen as main dry gas ,-65 ℃ approximately of tower top outlet gas temperatures, and after First Heat Exchanger 8 reclaimed cold, rewarming to 38 ℃ output was as the regeneration gas of drying process, and going out at last the battery limit (BL) becomes the dry gas product.
The azeotrope kind of refrigeration cycle is comprised of cryogen compressor 9, First Heat Exchanger 8, choke valve 10 etc. in the present embodiment, and azeotrope is mixed by the two or more components in methane, ethane (or ethene), propane (or propylene), butane, the pentane and forms.
Cyclic process is as follows: the compressed machine 9 of azeotrope is compressed to 1.2MPag ~ 5.0MPag, and be cooled to (water-cooled or air-cooled) after the room temperature, the second zone of heat liberation by First Heat Exchanger 8, temperature reduces liquefy, through choke valve 10 expenditure and pressures, temperature is reduced to-60 ℃ ~-120 ℃, becomes simultaneously gas-liquid two-phase; The overhead condenser 1101 that azeotrope behind the expenditure and pressure is introduced into liquefied gas rectifying column 11 as cold medium to liquefied gas rectifying column 11 cats head give vent to anger freeze after, return again the first cold fluid pass re-heat of this First Heat Exchanger 8, and be that the hot fluid fluid of zone of heat liberation (that is, by) provides cold; Azeotrope becomes the low pressure gaseous fluid after going out this First Heat Exchanger, returns cryogen compressor 9 entrances, so circulation,
After measured, separate the gas that obtains according to the described method of present embodiment, quality is as follows:
1) in dry gas ((carbon two following components comprise hydrogen, methane and carbon two the components)) product carbon three above components less than the 0.2%(mass fraction);
2) in liquefied gas (carbon three, carbon four components) the LPG product carbon two following components less than the 0.1%(mass fraction), carbon five above components are less than the 0.3%(mass fraction);
3) the middle carbon four following components of C5+ product (hydrocarbon that contains 5 above carbon atoms) are less than the 0.2%(mass fraction).
As shown in Figure 2, embodiment 2 is with the difference of embodiment 1:
The dry gas that liquefied gas rectifying 11 cats head obtain is after First Heat Exchanger 8 heat exchange, temperature does not directly go out system after rising to-50 ~ 0 ℃ by-65 ℃, expand into 1.4MPa but enter decompressor 12, after the temperature-41 ℃, return again First Heat Exchanger cold be provided, go out First Heat Exchanger 8 after being warming up to 38 ℃ after, enter decompressor 12 pressurized end superchargings, then go the drying and dehydrating operation to make regeneration gas, going out at last the battery limit (BL) becomes the dry gas product.
The above embodiment is the preferred embodiment that proves absolutely that the utility model is lifted, and protection domain of the present utility model is not limited to this.Being equal to that those skilled in the art do on the utility model basis substitutes or conversion, all within protection domain of the present utility model.Protection domain of the present utility model is as the criterion with claims.
Claims (9)
1. the gas fractionation unit of a liquefied petroleum gas aromatisation tail gas is characterized in that, comprising:
Liquefied petroleum gas aromatisation tail gas feeding mechanism;
Smart desulfurizer, its entrance is connected with described liquefied petroleum gas aromatisation tail gas feeding mechanism by pipeline;
Compressor is connected with the outlet of described smart desulfurizer by the pipeline that is provided with cooler;
Mixed hydrocarbon rectifying column, its entrance is connected with described compressor by pipeline, and the cat head of described mixed hydrocarbon rectifying column is provided with overhead condenser, is provided with tower bottom reboiler at the bottom of the tower;
Drying device, its entrance is connected by the tower top outlet of pipeline with described mixed hydrocarbon rectifying column;
First Heat Exchanger, it comprises multiply zone of heat liberation and multiply cold fluid pass, wherein the first zone of heat liberation entrance is connected with described drying device outlet by pipeline;
The liquefied gas rectifying column, its entrance is connected with the first zone of heat liberation outlet of described First Heat Exchanger by pipeline, and the cat head of described liquefied gas rectifying column is provided with overhead condenser, is provided with tower bottom reboiler at the bottom of the tower.
2. the gas fractionation unit of liquefied petroleum gas aromatisation tail gas according to claim 1, it is characterized in that, also comprise: the second heat exchanger, it comprises gas passage and heat exchange media channel, be located on the pipeline between described liquefied petroleum gas aromatisation tail gas feeding mechanism and the described smart desulfurizer entrance, wherein, the gas passage entrance of the second heat exchanger is connected with described liquefied petroleum gas aromatisation tail gas feeding mechanism by pipeline, and the gas passage outlet of the second heat exchanger is connected with the entrance of described smart desulfurizer by pipeline; The heat exchange media channel entrance of the second heat exchanger is connected with the tower bottom outlet of described mixed hydrocarbon rectifying column by pipeline.
3. the gas fractionation unit of liquefied petroleum gas aromatisation tail gas according to claim 1 is characterized in that, the tower bottom reboiler of the outlet of described smart desulfurizer, described liquefied gas rectifying column, described cooler and the compressor of being connected sequentially connect by pipeline.
4. the gas fractionation unit of liquefied petroleum gas aromatisation tail gas according to claim 1, it is characterized in that, also comprise the cryogen compressor, the cryogen entrance of the second zone of heat liberation of the outlet of cryogen compressor, described First Heat Exchanger, choke valve and liquefied gas rectifying column cat head condenser sequentially is communicated with by pipeline; The cryogen outlet of liquefied gas rectifying column cat head condenser, the first cold fluid pass of described First Heat Exchanger and the entrance of cryogen compressor sequentially are communicated with by pipeline.
5. the gas fractionation unit of liquefied petroleum gas aromatisation tail gas according to claim 4 is characterized in that, the tower top outlet of described liquefied gas rectifying column is communicated with the second cold fluid pass of described First Heat Exchanger by pipeline.
6. the gas fractionation unit of liquefied petroleum gas aromatisation tail gas according to claim 5, it is characterized in that the second cold fluid pass of the tower top outlet of described liquefied gas rectifying column, described First Heat Exchanger and the regeneration gas entrance of described drying device sequentially are communicated with by pipeline.
7. the gas fractionation unit of liquefied petroleum gas aromatisation tail gas according to claim 5, it is characterized in that, also comprise decompressor, the 3rd cold fluid pass of the expanding end of the second cold fluid pass of the tower top outlet of described liquefied gas rectifying column, described First Heat Exchanger, described decompressor, described First Heat Exchanger and described decompressor pressurized end sequentially be communicated with by pipeline.
8. the gas fractionation unit of liquefied petroleum gas aromatisation tail gas according to claim 7, it is characterized in that, the 3rd cryogen passage of the tower top outlet of described liquefied gas rectifying column, described First Heat Exchanger, the expanding end of described decompressor, the 3rd cold fluid pass of described First Heat Exchanger, described decompressor pressurized end and the regeneration gas entrance of described drying device sequentially be communicated with by pipeline.
9. the gas fractionation unit of liquefied petroleum gas aromatisation tail gas according to claim 1 is characterized in that, described First Heat Exchanger is plate-fin heat exchanger.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201220436481.7U CN202853258U (en) | 2012-08-30 | 2012-08-30 | Gas separation device for liquefied petroleum gas aromatization tail gas |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201220436481.7U CN202853258U (en) | 2012-08-30 | 2012-08-30 | Gas separation device for liquefied petroleum gas aromatization tail gas |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102840737A (en) * | 2012-08-30 | 2012-12-26 | 北京科瑞赛斯气体液化技术有限公司 | Process and device for separating aromatized exhaust from liquefied petroleum gas |
| CN106947563A (en) * | 2017-05-09 | 2017-07-14 | 天津亿利科能源科技发展股份有限公司 | A kind of production method of low-corrosiveness liquefied petroleum gas |
-
2012
- 2012-08-30 CN CN201220436481.7U patent/CN202853258U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102840737A (en) * | 2012-08-30 | 2012-12-26 | 北京科瑞赛斯气体液化技术有限公司 | Process and device for separating aromatized exhaust from liquefied petroleum gas |
| CN106947563A (en) * | 2017-05-09 | 2017-07-14 | 天津亿利科能源科技发展股份有限公司 | A kind of production method of low-corrosiveness liquefied petroleum gas |
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