CN214612345U - Dense gas takes off heavy hydrocarbon purification treatment's device - Google Patents
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- CN214612345U CN214612345U CN202120756738.6U CN202120756738U CN214612345U CN 214612345 U CN214612345 U CN 214612345U CN 202120756738 U CN202120756738 U CN 202120756738U CN 214612345 U CN214612345 U CN 214612345U
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Abstract
The utility model provides a dense gas takes off heavy hydrocarbon purification treatment's device, a serial communication port, include the cryocondensation unit and the active carbon adsorption unit that connect gradually through the pipeline, the feed gas is earlier through cryocondensation unit precooling separation part heavy hydrocarbon component, through the surplus heavy hydrocarbon component of active carbon adsorption unit desorption again, realizes the purification of feed gas, the cryocondensation unit includes precooler, precooling separator, heavy hydrocarbon heater, refrigeration compressor unit, heavy hydrocarbon flash tank and precooler pipe connection in proper order, precooling separator and precooler pipe connection, the active carbon adsorption unit is including adsorption tower, regenerative heater, regenerative cooler and the regeneration gas separator of pipe connection in proper order. The scheme solves the problems that refrigeration equipment needs to be added and the energy consumption is high in the prior art, and overcomes the defects of poor adaptability and small operation elasticity of an adsorption process.
Description
Technical Field
The utility model relates to a natural gas trade purifies technical field, especially relates to a dense gas takes off heavy hydrocarbon purification treatment's device.
Background
Dense sandstone gas (dense gas for short) generates a certain amount of condensate oil in the production process, and the gas phase contains more heavy hydrocarbon components. According to the results of wellhead sampling detection, most samples show that the components with high melting points, such as C3-C5, C6 and C6+ are low, and the components with high melting points, such as neopentane, cyclohexane and benzene, are contained.
If the natural gas component is used as a raw material gas and is prepared into LNG by cryogenic liquefaction for recovery, C6 and C6+ components, particularly components with higher melting points such as neopentane, cyclohexane and benzene, need to be effectively removed to avoid that the components are solidified and separated out at a lower temperature after being brought into a cold box, so that the channel of a plate-fin heat exchanger in the cold box is blocked, and the normal and stable operation of the cold box is influenced.
The conventional heavy hydrocarbon removal method for natural gas mainly comprises the following steps:
The isopentane washing process is to wash natural gas by using isopentane and achieve the purposes of heavy hydrocarbon condensation and removal by changing the gas-liquid balance of a system. However, the process consumes a certain amount of isopentane, which results in higher operation cost.
The washing process of the self condensate is to cool natural gas to between-50 ℃ and-55 ℃, the heavy hydrocarbon in the natural gas is condensed, and the heavy hydrocarbon liquid is utilized to wash the natural gas, so that the purposes of condensing and removing the heavy hydrocarbon are achieved. The process requires a certain amount of heavy hydrocarbon condensate to ensure adequate scrubbing of the natural gas and is therefore suitable for natural gas containing higher amounts of C3-C5 components.
The low-temperature condensation process is to condense heavy hydrocarbon in natural gas when the natural gas is cooled to a temperature between 40 ℃ below zero and 50 ℃ below zero, so as to achieve the purposes of condensing and removing the heavy hydrocarbon. The method can not completely condense the aromatic hydrocarbon when the heavy hydrocarbon content is less and the aromatic hydrocarbon content is higher, and the cold end of the liquefaction heat exchanger is frozen and blocked when the temperature is between-140 ℃ and-160 ℃.
The activated carbon adsorption process is characterized in that aromatic hydrocarbons are removed by utilizing the characteristics of normal-temperature adsorption and high-temperature desorption of activated carbon, after the design of a general adsorber is completed, when the content of heavy hydrocarbon in feed gas becomes more, the situation that the heavy hydrocarbon is unqualified can possibly occur, the adaptability is poor, the investment is higher, and the operation elasticity range is small
SUMMERY OF THE UTILITY MODEL
For overcoming prior art's not enough, the utility model provides a dense gas takes off heavy hydrocarbon purification treatment's device compares with traditional scheme, and this scheme has solved prior art and has need increase refrigeration plant, and the higher problem of energy consumption has overcome the shortcoming that adsorption process adaptability is poor, operation elasticity is little.
The utility model provides a technical scheme that above-mentioned problem adopted is:
the utility model provides a device that dense gas takes off heavy hydrocarbon purification treatment, includes cryocondensation unit and the active carbon adsorption unit that connects gradually through the pipeline, and the feed gas is earlier through cryocondensation unit precooling separation part heavy hydrocarbon component, and the purification of feed gas is realized to the remaining heavy hydrocarbon component of active carbon adsorption unit desorption again. Dense gas heavy hydrocarbon purification treatment's device in through setting up cryocondensation unit and active carbon adsorption unit, when letting natural gas cooling to between-40 ℃ to-50 ℃ through cryocondensation unit B, the heavy hydrocarbon condensation in the natural gas gets off, reaches the purpose of heavy hydrocarbon condensation and desorption. The aromatic hydrocarbons are removed by the activated carbon adsorption unit C by utilizing the characteristics of normal-temperature adsorption and high-temperature desorption of the activated carbon.
Preferably, the low-temperature condensation unit comprises a precooler, a precooling separator, a heavy hydrocarbon heater, a refrigeration compressor unit and a heavy hydrocarbon flash tank, the heavy hydrocarbon heater, the refrigeration compressor unit and the heavy hydrocarbon flash tank are sequentially connected with the precooler through pipelines, the precooling separator is connected with the precooler through a pipeline, and the activated carbon adsorption unit comprises an adsorption tower, a regenerative heater, a regenerative cooler and a regenerative gas separator which are sequentially connected through pipelines.
Preferably, the refrigeration compressor unit adopts a single-refrigerant refrigeration cycle or an LNG device applied to a mixed refrigerant refrigeration cycle process or a refrigeration cycle of a liquid-phase refrigerant of the mixed refrigerant refrigeration cycle, and the independent refrigerant component is propane, ammonia or R22.
Preferably, the precooler adopts a multi-channel plate-fin heat exchanger and a refrigeration cycle of a liquid-phase refrigerant of a mixed refrigerant refrigeration cycle, the precooler is provided with four channels, wherein the four channels comprise two hot fluid channels and two cold fluid channels, the two hot fluid channels are respectively a feed gas channel and a refrigerant positive flow channel, the two cold fluid channels are respectively a purified gas return channel and a refrigerant return channel, the feed gas is cooled to-20 to-30 ℃ through heat exchange of the feed gas channel of the precooler and then enters the precooling separator, purified gas after gas-liquid separation is discharged from the top of the precooler and returns to the precooler, and the purified gas is discharged from the precooler through the purified gas return channel to release cold energy and is heated to normal temperature and then enters the activated carbon adsorption unit; after the liquid-phase refrigerant from the refrigerating compressor unit is subjected to heat exchange and temperature reduction through the refrigerant forward flow channel of the precooler, the liquid-phase refrigerant is subjected to throttling refrigeration through the throttle valve and returns to the precooler, and the liquid-phase refrigerant is discharged from the precooler and returns to the inlet of the refrigerating compressor unit after the cold energy is released through the refrigerant return flow channel and the temperature is raised to the normal temperature.
Preferably, the precooler adopts single-component refrigerant refrigeration cycle, the precooler is provided with three channels, wherein one hot fluid channel is a raw material gas channel, two cold fluid channels are respectively a purified gas return channel and a refrigerant return channel, the raw material gas enters the precooling separator after being subjected to heat exchange and temperature reduction to-20 to-30 ℃ through the raw material gas channel of the precooler, purified gas subjected to gas-liquid separation is discharged from the top of the precooling separator and returns to the precooler, and the purified gas is discharged from the precooler and enters the active carbon adsorption unit after being heated to normal temperature through the purified gas return channel to release cold energy; liquid-phase refrigerant from the refrigerating compressor unit enters the precooler after being throttled, decompressed and cooled by the throttle valve, releases cold energy through the refrigerant return channel, is heated to normal temperature, then exits the precooler and returns to the inlet of the refrigerating compressor unit.
Preferably, precooling separator bottom discharge low temperature liquid phase heavy hydrocarbon heats up to the normal atmospheric temperature after through the heavy hydrocarbon heater heat transfer, gets into the heavy hydrocarbon flash tank, and the flash distillation gas is discharged from heavy hydrocarbon flash tank top, delivers to the fuel gas system, and heavy hydrocarbon flash tank bottom discharge normal atmospheric temperature liquid phase heavy hydrocarbon delivers to mixing the hydrocarbon storage tank.
Preferably, the activated carbon adsorption unit adopts a temperature swing adsorption process, the adsorbent adopts a special activated carbon adsorbent for removing heavy hydrocarbon, the adsorption tower adopts a three-tower or double-tower process, the temperature swing and pressure swing regeneration is carried out, and each adsorption tower alternately finishes the adsorption and regeneration processes through the sequential switching of the program control valves.
Preferably, the regenerated gas of the activated carbon adsorption unit is taken from purified gas at the outlet of the adsorption tower in an adsorption state, the regenerated gas is heated to 240 ℃ by a regeneration heater after being decompressed by a regenerated gas regulating valve, the heating medium of the regeneration heater can adopt electric heating or steam or heat conducting oil as a heating medium, the adsorbent bed layer in the adsorption tower in the regeneration state is blown, heated and regenerated, and after the heating regeneration is finished, the adsorbent bed layer is continuously blown by cold regenerated gas to be cooled to normal temperature, so that the cold blowing process is finished.
Preferably, the regenerated gas after purging the adsorbent bed is cooled to normal temperature through heat exchange of a regeneration cooler, then enters a regeneration gas separator for gas-liquid separation, gas phase is discharged from the top and sent to a fuel gas system, and normal temperature liquid phase heavy hydrocarbon discharged from the bottom is sent to a hydrocarbon mixing storage tank.
Preferably, the regenerative cooler is an air-cooled air type or a shell-and-tube heat exchanger using circulating cooling water as a refrigerant.
Compared with the prior art, the utility model, following beneficial effect has:
the utility model provides a dense gas takes off heavy hydrocarbon purification treatment's device, compare in conventional natural gas and take off the heavy hydrocarbon method, this scheme is through setting up cryocondensation unit and active carbon adsorption unit, when letting natural gas cool to between-40 ℃ to-50 ℃ through the cryocondensation unit, the heavy hydrocarbon condensation in the natural gas gets off, reach the purpose of heavy hydrocarbon condensation and desorption, utilize active carbon normal atmospheric temperature to adsorb through the active carbon adsorption unit, aromatic hydrocarbons are come the desorption to the characteristic of high temperature desorption, the cold source can be got from back end cryrogenic liquefaction unit, need not to increase refrigeration plant alone, than washing, the scheme of condensation, the demand cold volume is lower, the energy consumption still less, with shallow cold + absorbent combination, operation elasticity is big, avoid adsorbing technology adaptability poor, the shortcoming that operation elasticity is little.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required to be used in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
Fig. 1 is a schematic structural diagram of the present invention;
FIG. 2 is a schematic diagram of a cryocondensation unit of the present invention (single refrigerant refrigeration cycle);
FIG. 3 is a schematic view of the cryocondensation unit of the present invention (mixed refrigerant refrigeration cycle)
FIG. 4 is a schematic view of an activated carbon adsorption unit of the present invention;
reference numerals: 1-a precooler; 2-precooling a separator; a 3-heavy hydrocarbon heater; 4-a refrigeration compressor unit; 5-a heavy hydrocarbon flash tank; 6-an adsorption tower; 7-a regenerative heater; 8-a regenerative cooler; 9-regeneration of the gas separator; 10-purifying the regenerative electric heater; a-raw material gas; b-a cryocondensation unit; a C-activated carbon adsorption unit; d-a fuel gas system; e-a cryogenic liquefaction unit; f-hydrocarbon mixture storage tank.
Detailed Description
The technical solution in the embodiment of the present invention will be described clearly and completely with reference to the drawings in the embodiment of the present invention, and it is obvious that the described embodiment is only a part of the embodiments of the present invention, rather than all embodiments, and all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention based on the embodiments of the present invention.
In the description of the present invention, it is to be understood that the terms "upper", "lower", "front", "rear", "left", "right", "top", "bottom", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, and do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, should not be construed as limiting the present invention.
Example 1
As shown in figures 1-4, a dense gas takes off heavy hydrocarbon purification unit's device, includes cryocondensation unit and the active carbon adsorption unit who connects gradually through the pipeline, and the feed gas is earlier through cryocondensation unit precooling separation part heavy hydrocarbon component, and the purification of feed gas is realized to remaining heavy hydrocarbon component of desorption through the active carbon adsorption unit again. Dense gas take off heavy hydrocarbon purification unit in through setting up cryocondensation unit and active carbon adsorption unit, when letting natural gas cool to between-40 ℃ to-50 ℃ through the cryocondensation unit, the heavy hydrocarbon condensation in the natural gas gets off, reaches the purpose of heavy hydrocarbon condensation and desorption. The aromatic hydrocarbons are removed by the activated carbon adsorption unit C by utilizing the characteristics of normal-temperature adsorption and high-temperature desorption of the activated carbon.
The low temperature condensation unit includes precooler 1, precooling separator 2, heavy hydrocarbon heater 3, refrigeration compressor unit 4, heavy hydrocarbon flash tank 5 and 1 tube coupling in proper order of precooler, precooling separator 2 and 1 tube coupling of precooler, 2 bottom discharge low temperature liquid phase heavy hydrocarbon of precooling separator get into heavy hydrocarbon flash tank 5 after 3 heat transfer warms up to the normal atmospheric temperature of heavy hydrocarbon heater, and flash distillation gas is discharged from 5 tops of heavy hydrocarbon flash tank, delivers to fuel gas system, and 5 bottom discharge normal atmospheric temperature liquid phase heavy hydrocarbon of heavy hydrocarbon flash tank deliver to and mix the hydrocarbon storage tank. The activated carbon adsorption unit comprises an adsorption tower 6, a regenerative heater 7, a regenerative cooler 8 and a regenerative gas separator 9 which are sequentially connected through pipelines. The activated carbon adsorption unit adopts a temperature swing adsorption process, the adsorbent adopts a special activated carbon adsorbent for removing heavy hydrocarbon, the adsorption tower 6 adopts a three-tower or double-tower process, the adsorption towers 6 adopt a side-by-side mode for temperature swing and pressure swing regeneration, and the adsorption and regeneration processes are alternately completed by the adsorption towers 6 through the sequential switching of the program control valves.
The refrigeration compressor unit 4 adopts single-component refrigerant refrigeration cycle or LNG device applied to mixed refrigerant refrigeration cycle process or refrigeration cycle of liquid-phase refrigerant of mixed refrigerant refrigeration cycle, and independent refrigerant components are propane, ammonia or R22.
Example 2
As shown in fig. 3, the precooler 1 adopts a multi-channel plate-fin heat exchanger and a refrigeration cycle of a liquid-phase refrigerant of a mixed refrigerant refrigeration cycle, the precooler 1 is provided with four channels, the device comprises two hot fluid channels and two cold fluid channels, wherein the two hot fluid channels are respectively a feed gas channel and a refrigerant positive flow channel, the two cold fluid channels are respectively a purified gas return channel and a refrigerant return channel, the distribution of each channel on the precooler is sequentially the refrigerant positive flow channel, the refrigerant return channel, the purification return channel and the feed gas channel from top to bottom, the feed gas is cooled to-20 to-30 ℃ through heat exchange by the feed gas channel of the precooler 1, the purified gas after gas-liquid separation is discharged from the top of the precooling separator 2 and returns to the precooler 1, and the purified gas after being discharged from the precooler 1 enters an active carbon adsorption unit after being released with cold energy through a purified gas return channel and heated to normal temperature; liquid-phase refrigerant from the refrigerating compressor unit 4 is subjected to heat exchange and cooling through a refrigerant forward flow channel of the precooler 1, is subjected to throttling refrigeration through a throttle valve, returns to the precooler 1, is discharged from the precooler 1 after being released with cold through a refrigerant return flow channel and heated to normal temperature, and returns to an inlet of the refrigerating compressor unit 4.
Example 3
As shown in fig. 2, the precooler 1 adopts a single-component refrigerant refrigeration cycle, the precooler 1 is provided with three channels, wherein one hot fluid channel is a raw material gas channel, and two cold fluid channels are respectively a purified gas return channel and a refrigerant return channel, the raw material gas is subjected to heat exchange and temperature reduction to-20 to-30 ℃ through the raw material gas channel of the precooler 1, then enters the precooler separator 2, purified gas after gas-liquid separation is discharged from the top of the precooler separator 2 and returns to the precooler 1, and then is discharged from the precooler 1 and enters an active carbon adsorption unit after being heated to normal temperature through the purified gas return channel to release cold energy; liquid-phase refrigerant from the refrigerating compressor unit 4 enters the precooler 1 after being throttled, decompressed and cooled by the throttle valve, releases cold energy through the refrigerant return channel, is heated to normal temperature, then exits the precooler 1 and returns to the inlet of the refrigerating compressor unit 4.
Example 4
As shown in fig. 4, the regeneration gas of the activated carbon adsorption unit is taken from the purified gas at the outlet of the adsorption tower 6 in the adsorption state, after the pressure of the regeneration gas regulating valve is reduced, the purified gas is heated to 240 ℃ by the regeneration heater 7, the heating medium of the regeneration heater 7 can be electrically heated or steam or heat conducting oil is used as the heating medium, the adsorbent bed layer in the adsorption tower 6 in the regeneration state is swept, heated and regenerated, and after the heating regeneration is finished, the adsorbent bed layer is continuously swept by the cold regeneration gas to be cooled to normal temperature, so that the cold blowing process is completed.
And the regenerated gas after purging the adsorbent bed layer is subjected to heat exchange and cooling to normal temperature through a regeneration cooler 8, enters a regeneration gas separator 9 for gas-liquid separation, gas phase is discharged from the top and is conveyed to a fuel gas system, and normal-temperature liquid phase heavy hydrocarbon discharged from the bottom is conveyed to a hydrocarbon mixing storage tank.
The regenerative cooler 8 adopts an air cooling mode or a shell-and-tube heat exchanger taking circulating cooling water as a refrigerant.
The utility model discloses a theory of operation:
the low-temperature condensation unit consists of a precooler 1, a precooling separator 2, a heavy hydrocarbon heater 3 and a refrigeration compressor unit 4: the raw gas after separation, deacidification, dehydration and demercuration enters a precooler 1, exchanges heat with a refrigerant from a propane refrigeration compressor unit 4, is cooled to-40 ℃ and then enters a precooling separator 2 for separation, and the gas phase of the precooling separator 2 returns to the precooler 1 for rewarming and then enters an active carbon adsorption unit. The liquid phase of the precooling separator 2 is reheated to 40 ℃ by a hydrocarbon mixture heater to form a stable hydrocarbon mixture product, and the flash evaporated gas phase is sent to a fuel gas system.
The activated carbon adsorption unit consists of three adsorption towers 6, a regenerative heater 7, a regenerative cooler 8 and a regenerative gas separator 9: the raw material gas from the low-temperature condensation unit enters the bottom of a first adsorption tower 6 and passes through an activated carbon bed layer from bottom to top, at the moment, the first adsorption tower 6 is in an adsorption state and adsorbs most of C5+ components in the raw material gas, and then the raw material gas enters a cryogenic liquefaction unit; at the moment, the second adsorption tower 6 is in a cooling state, cold blowing gas comes from the qualified product gas after adsorption, and the cold blowing gas passes through the second adsorption tower 6 from top to bottom to cool the bed layer to 40 ℃; and then, heating the cold blowing gas to 220 ℃ through a heater, feeding the cold blowing gas into the top of the third absorption tower 6, heating the molecular sieve bed layer from top to bottom, and keeping the third absorption tower 6 in a regeneration state. Thereafter, the regeneration gas passes through a regeneration cooler 8, and then through a regeneration gas separator 9 to the fuel gas system.
To sum up, can be better realize the utility model discloses.
The above is only the preferred embodiment of the present invention, and not intended to limit the present invention in any way, and according to the technical essence of the present invention, within the spirit and principle of the present invention, any simple modification, equivalent replacement, and improvement made to the above embodiments all still belong to the protection scope of the technical solution of the present invention.
Claims (10)
1. The utility model provides a dense gas takes off heavy hydrocarbon purification treatment's device, its characterized in that includes cryocondensation unit and the active carbon adsorption unit who connects gradually through the pipeline, and the feed gas is earlier through cryocondensation unit precooling separation part heavy hydrocarbon component, and the purification of feed gas is realized to the remaining heavy hydrocarbon component of active carbon adsorption unit desorption again.
2. The device for purifying and processing dense hydrocarbon in gas according to claim 1, wherein the low-temperature condensation unit comprises a precooler (1), a precooling separator (2), a heavy hydrocarbon heater (3), a refrigeration compressor unit (4) and a heavy hydrocarbon flash tank (5), the heavy hydrocarbon heater (3), the refrigeration compressor unit (4) and the heavy hydrocarbon flash tank (5) are sequentially connected with the precooler (1) through pipelines, the precooling separator (2) is connected with the precooler (1) through pipelines, and the activated carbon adsorption unit comprises an adsorption tower (6), a regenerative heater (7), a regenerative cooler (8) and a regenerative gas separator (9) which are sequentially connected through pipelines.
3. The device for carrying out dense gas heavy hydrocarbon removal purification treatment according to claim 2, wherein the refrigeration compressor unit (4) adopts a single-refrigerant refrigeration cycle or a refrigeration cycle of a liquid-phase refrigerant of an LNG device or a mixed-refrigerant refrigeration cycle applied to a mixed-refrigerant refrigeration cycle process, and the independent refrigerant component is propane, ammonia or R22.
4. An apparatus for dense gas heavy hydrocarbon removal purification treatment according to claim 2, the precooler (1) adopts a multi-channel plate-fin heat exchanger and a refrigeration cycle of liquid-phase refrigerant of a mixed refrigerant refrigeration cycle, the precooler (1) is provided with four channels, the device comprises two hot fluid channels and two cold fluid channels, wherein the two hot fluid channels are respectively a feed gas channel and a cold medium positive flow channel, the two cold fluid channels are respectively a purified gas return channel and a cold medium return channel, the feed gas is cooled to minus 20 to minus 30 ℃ through heat exchange of the feed gas channel of the precooler (1), the purified gas after gas-liquid separation is discharged from the top of the precooling separator (2) and returns to the precooler (1), and the purified gas after gas-liquid separation is discharged from the precooler (1) and enters an active carbon adsorption unit after the cold energy is released by a purified gas return channel and the temperature is raised to the normal temperature; liquid-phase refrigerant from the refrigerating compressor unit (4) is subjected to heat exchange and cooling through a refrigerant forward flow channel of the precooler (1), is throttled and refrigerated through a throttle valve, returns to the precooler (1), is released cold through a refrigerant return flow channel, is heated to normal temperature, then is discharged from the precooler (1), and returns to an inlet of the refrigerating compressor unit (4).
5. The device for dense gas heavy hydrocarbon removal purification treatment according to claim 2, wherein the precooler (1) adopts a single-component refrigerant refrigeration cycle, the precooler (1) is provided with three channels, one hot fluid channel is a raw gas channel, and two cold fluid channels are a purified gas return channel and a refrigerant return channel, the raw gas is cooled to-20 to-30 ℃ through heat exchange of the raw gas channel of the precooler (1), then enters the precooler (2), purified gas after gas-liquid separation is discharged from the top of the precooler (2) and returns to the precooler (1), and the purified gas is discharged from the precooler (1) and enters the activated carbon adsorption unit after being released cold energy through the purified gas return channel and heated to normal temperature; liquid-phase refrigerant from the refrigerating compressor unit (4) enters the precooler (1) after being throttled, decompressed and cooled by the throttle valve, releases cold energy through the refrigerant return channel, is heated to normal temperature, then is discharged from the precooler (1), and returns to the inlet of the refrigerating compressor unit (4).
6. The device for purifying and processing heavy hydrocarbon removed from dense gas as claimed in claim 2, wherein said precooling separator (2) discharges heavy hydrocarbon liquid phase at bottom through heavy hydrocarbon heater (3) after heat exchange and temperature rise to normal temperature, enters into heavy hydrocarbon flash drum (5), and the flash gas is discharged from top of heavy hydrocarbon flash drum (5) and sent to fuel gas system, and the heavy hydrocarbon flash drum (5) discharges heavy hydrocarbon liquid phase at bottom and sends to hydrocarbon mixing storage tank.
7. The device for purifying and treating dense gas heavy hydrocarbon removal according to claim 2, wherein the activated carbon adsorption unit adopts a temperature swing adsorption process, the adsorbent adopts a special activated carbon adsorbent for heavy hydrocarbon removal, the adsorption tower (6) adopts a three-tower or two-tower process, the temperature swing and pressure swing regeneration is carried out, and the adsorption and regeneration processes are alternately completed by the adsorption towers (6) through sequential switching of program control valves.
8. The device for dense gas heavy hydrocarbon removal purification treatment according to claim 2, wherein the regeneration gas of the activated carbon adsorption unit is taken from the purified gas at the outlet of the adsorption tower (6) in the adsorption state, the regeneration gas is heated to 240 ℃ by the regeneration heater (7) after being depressurized by a regeneration gas regulating valve, the heating medium of the regeneration heater (7) can be electrically heated or steam or heat conducting oil is used as the heating medium, the adsorbent bed layer in the adsorption tower (6) in the regeneration state is purged, heated and regenerated, and after the heating regeneration is finished, the cold regeneration gas is continuously used for purging the adsorbent bed layer to cool the adsorbent bed layer to normal temperature, thereby completing the cold blowing process.
9. The device for heavy hydrocarbon removal purification treatment of dense gas as claimed in claim 8, wherein the regenerated gas after purging the adsorbent bed layer enters the regeneration gas separator (9) for gas-liquid separation after being cooled to normal temperature through heat exchange of the regeneration cooler (8), the gas phase is discharged from the top and sent to the fuel gas system, and the normal temperature liquid phase heavy hydrocarbon discharged from the bottom is sent to the hydrocarbon mixing storage tank.
10. An apparatus for dense gas heavy hydrocarbon removal purification treatment according to claim 9, wherein the regenerative cooler (8) is in the form of air cooling or a shell-and-tube heat exchanger using circulating cooling water as a refrigerant.
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