CN212894607U - Heavy hydrocarbon device is taken off to natural gas - Google Patents
Heavy hydrocarbon device is taken off to natural gas Download PDFInfo
- Publication number
- CN212894607U CN212894607U CN202021049318.6U CN202021049318U CN212894607U CN 212894607 U CN212894607 U CN 212894607U CN 202021049318 U CN202021049318 U CN 202021049318U CN 212894607 U CN212894607 U CN 212894607U
- Authority
- CN
- China
- Prior art keywords
- heavy hydrocarbon
- gas
- cooling
- natural gas
- hydrocarbon removal
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 190
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 172
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 166
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 130
- 239000003345 natural gas Substances 0.000 title claims abstract description 64
- 239000007789 gas Substances 0.000 claims abstract description 146
- 230000008929 regeneration Effects 0.000 claims abstract description 52
- 238000011069 regeneration method Methods 0.000 claims abstract description 52
- 238000001816 cooling Methods 0.000 claims abstract description 28
- 239000000112 cooling gas Substances 0.000 claims abstract description 23
- 239000000945 filler Substances 0.000 claims abstract description 23
- 238000001179 sorption measurement Methods 0.000 claims abstract description 13
- 239000012071 phase Substances 0.000 claims description 20
- 239000007791 liquid phase Substances 0.000 claims description 13
- 239000007788 liquid Substances 0.000 claims description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 7
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical group [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 3
- 229910052782 aluminium Inorganic materials 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 238000010926 purge Methods 0.000 claims description 3
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 238000003795 desorption Methods 0.000 abstract description 13
- 238000009434 installation Methods 0.000 abstract description 4
- 230000015572 biosynthetic process Effects 0.000 abstract 1
- 239000002994 raw material Substances 0.000 description 24
- 238000000034 method Methods 0.000 description 8
- 230000008569 process Effects 0.000 description 8
- 238000012856 packing Methods 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 238000005057 refrigeration Methods 0.000 description 5
- 239000002737 fuel gas Substances 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- 230000001172 regenerating effect Effects 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 230000002745 absorbent Effects 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 230000000274 adsorptive effect Effects 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000007792 gaseous phase Substances 0.000 description 2
- 230000010354 integration Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000009835 boiling Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000003749 cleanliness Effects 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 238000002336 sorption--desorption measurement Methods 0.000 description 1
Images
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model provides a natural gas takes off heavy hydrocarbon device, take off heavy hydrocarbon unit and adsorb and take off heavy hydrocarbon unit including integrated the cooling of arranging on same sled dress: the cooling heavy hydrocarbon removal unit comprises a heat exchanger for precooling the feed gas and a cold dryer for cooling the precooled feed gas to remove heavy hydrocarbon; the heat exchanger is provided with a feed gas channel and a cooling gas channel which exchange heat with each other; the inlet of the feed gas channel is used for receiving feed gas; the inlet of the cold dryer is connected with the outlet of the feed gas channel, and the outlet of the cold dryer is communicated with the inlet of the cooling gas channel; the adsorption heavy hydrocarbon removal unit comprises a heavy hydrocarbon removal tower and a regeneration gas heater; the heavy hydrocarbon removal tower is filled with filler for absorbing heavy hydrocarbon, the bottom of the heavy hydrocarbon removal tower is connected with an outlet of the cooling gas channel, and the top of the heavy hydrocarbon removal tower outputs purified natural gas outwards; the regeneration gas heater is communicated with the top of the heavy hydrocarbon removal tower. The utility model discloses to the desorption degree of heavy hydrocarbon high, structural formation sled dress structure, convenient transportation and on-the-spot installation.
Description
Technical Field
The utility model relates to a natural gas processing technology field, in particular to natural gas takes off heavy hydrocarbon device.
Background
Before natural gas enters the cold box to be liquefied and produced, deacidification, dehydration and heavy hydrocarbon removal treatment are needed to avoid the impurities from freezing and blocking the cold box in a low-temperature state. The heavy hydrocarbon refers to hydrocarbons having a carbon number of 5 or more in natural gas.
At present, the desorption mode to the heavy hydrocarbon often adopts and takes off the heavy hydrocarbon tower with the input of raw materials natural gas, utilizes the filler absorption heavy hydrocarbon that takes off in the heavy hydrocarbon tower. If contain a large amount of heavy hydrocarbon in the raw and natural gas, then need increase the volume of packing in order to satisfy the demand of desorption heavy hydrocarbon, correspondingly, still need more regeneration gas to be regenerated to packing, cause the increase of running cost and the reduction of LNG yield, and simultaneously, still can directly increase the height of taking off the heavy hydrocarbon tower, it causes very big difficulty to change for product sled dress, how to reduce to take off the heavy hydrocarbon tower height and can normally get rid of a large amount of heavy hydrocarbon again and not influence the cold box normal work and not freeze stifled, the biggest problem and difficulty at present have become.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a heavy hydrocarbon device is taken off to natural gas, the running cost is higher when solving the heavy hydrocarbon volume that needs the desorption among the prior art great, and is difficult to the problem of sled dress ization.
In order to solve the technical problem, the utility model adopts the following technical scheme: the utility model provides a heavy hydrocarbon device is taken off to natural gas, takes off heavy hydrocarbon unit and adsorbs taking off heavy hydrocarbon unit including the integrated cooling of arranging on same sled dress: the cooling heavy hydrocarbon removal unit comprises a heat exchanger for precooling the feed gas and a cold dryer for cooling the precooled feed gas to remove heavy hydrocarbon; the heat exchanger is provided with a feed gas channel and a cooling gas channel which exchange heat with each other; the inlet of the feed gas channel is used for receiving feed gas; the inlet of the cold dryer is connected with the outlet of the feed gas channel, and the outlet of the cold dryer is communicated with the inlet of the cooling gas channel; the adsorption heavy hydrocarbon removal unit comprises a heavy hydrocarbon removal tower and a regeneration gas heater; the heavy hydrocarbon removal tower is filled with filler for absorbing heavy hydrocarbon, the bottom of the heavy hydrocarbon removal tower is connected with the outlet of the cooling gas channel, and the top of the heavy hydrocarbon removal tower outputs purified natural gas outwards; and the regeneration gas heater is communicated with the top of the heavy hydrocarbon removal tower and used for heating part of the purified natural gas and then sending the heated natural gas back to the heavy hydrocarbon removal tower so as to regenerate the filler.
Optionally, the cooled heavy hydrocarbon removal unit further comprises a first separator for gas-liquid separation of the cooled feed gas; the inlet of the first separator is connected with the outlet of the cold dryer, and the gas-phase outlet of the first separator is connected with the inlet of the cooling gas channel; the heat exchanger also has a heavy hydrocarbon channel in heat exchange with the feed gas channel; and an inlet of the heavy hydrocarbon channel is connected with a liquid phase outlet of the first separator, and an outlet of the heavy hydrocarbon channel outputs heavy hydrocarbon outwards.
Optionally, the heat exchanger is an aluminum plate-fin heat exchanger.
Optionally, the chilled heavy hydrocarbon removal unit further comprises a feed gas filter disposed upstream of the feed gas channel.
Optionally, the heavy hydrocarbon removal towers are two, and the two heavy hydrocarbon removal towers are arranged in parallel and are respectively connected with the cooling gas channel and the regeneration gas heater.
Optionally, the filler is activated carbon.
Optionally, the adsorptive heavy hydrocarbon removal unit further comprises a purge gas filter; and the inlet of the purified gas filter is connected with the top of the heavy hydrocarbon removal tower.
Optionally, the regeneration gas heater is an electric heater.
Optionally, the adsorptive heavy hydrocarbon removal unit further comprises a regeneration gas cooler and a second separator; the inlet of the regeneration gas cooler is connected with the bottom of the heavy hydrocarbon removal tower, and the outlet of the regeneration gas cooler is connected with the inlet of the second separator; a gas phase outlet of the second separator outputs regenerated gas outwards; and the liquid phase outlet of the second separator outputs heavy hydrocarbon outwards.
According to the above technical scheme, the utility model discloses following advantage and positive effect have at least: the utility model discloses an among the natural gas takes off the heavy hydrocarbon device, through cold dry quick-witted cooling natural gas, utilize the low temperature to appear most heavy hydrocarbon, later again through taking off the heavy hydrocarbon tower, utilize remaining heavy hydrocarbon of absorbent mode desorption, high to the heavy hydrocarbon desorption degree of natural gas, satisfy the requirement of the follow-up liquefaction of natural gas. In this scheme, take off the load of heavy hydrocarbon tower low, the demand of packing is little, and then can reduce the height of taking off the heavy hydrocarbon tower, and the cold machine of doing is independent operation's equipment, and the process flow and the pipeline simple structure of a complete set of device to be convenient for arrange each equipment and pipeline integration on a sled dress, a complete set of natural gas takes off the heavy hydrocarbon device and forms sled dress structure, convenient transportation and field installation. Meanwhile, in the scheme, the heat exchanger is used for recovering the cold energy of the natural gas cooled by the cold dryer, and the recovered cold energy is used for precooling the feed gas entering the cold dryer, so that the power load of the cold dryer is reduced, and the operation cost is reduced. In addition, because the required amount of the filler is small, the consumption of the regeneration gas for regenerating the filler can be reduced, so that the amount of the natural gas conveyed to the downstream cold box can be increased, and the LNG yield is correspondingly increased.
Drawings
FIG. 1 is a process flow diagram of an embodiment of a natural gas heavy hydrocarbon removal device of the present invention.
The reference numerals are explained below:
1. cooling the heavy hydrocarbon removal unit; 11. a heat exchanger; 111. a feed gas channel; 112. a cooling gas channel; 113. A heavy hydrocarbon passageway; 12. a cold dryer; 13. a first separator; 14. a raw material gas filter;
2. an adsorption heavy hydrocarbon removal unit; 21. a heavy hydrocarbon removal tower; 22. a regeneration gas heater; 23. a purified gas filter; 24. a regeneration gas cooler; 25. a second separator;
5. a heavy hydrocarbon storage tank.
Detailed Description
Exemplary embodiments that embody features and advantages of the present invention will be described in detail in the following description. It is to be understood that the invention is capable of other and different embodiments and its several details are capable of modification without departing from the scope of the invention, and that the description and drawings are to be regarded as illustrative in nature and not as restrictive.
The utility model provides a heavy hydrocarbon device is taken off to natural gas for carry out the desorption of heavy hydrocarbon to raw and natural gas (hereinafter for short the feed gas). Wherein, the raw gas entering the natural gas heavy hydrocarbon removing device is subjected to deacidification (decarburization and desulfurization) and dehydration in advance. The natural gas treated by the natural gas heavy hydrocarbon removal device enters a cold box for liquefaction treatment.
Referring to fig. 1, according to the utility model discloses an embodiment, this natural gas takes off heavy hydrocarbon device takes off heavy hydrocarbon unit 1 and adsorbs taking off heavy hydrocarbon unit 2 including cooling. Wherein, this cooling takes off heavy hydrocarbon unit 1 and adsorbs taking off heavy hydrocarbon unit 2 structurally is the integrated arrangement on same sled dress (not shown), is convenient for transport and field installation.
According to the technological process that this natural gas takes off heavy hydrocarbon device provided, the raw gas of outside (skid-mounted promptly outside) gets into the cooling through A department and takes off heavy hydrocarbon unit 1, takes off heavy hydrocarbon unit 1 by the cooling and cools off most heavy hydrocarbon to the raw gas, gets into the absorption after that and takes off heavy hydrocarbon unit 2, takes off heavy hydrocarbon unit 2 by the absorption and adsorbs remaining heavy hydrocarbon, and the natural gas after the purification is located to the outside cold box through B.
In some embodiments, as shown in fig. 1, cold heavy hydrocarbon removal unit 1 comprises heat exchanger 11, cold dryer 12, first separator 13, and feed gas filter 14.
The heat exchanger 11 is used for pre-cooling the feed gas. In this embodiment, the heat exchanger 11 has a raw gas passage 111, a cooling gas passage 112, and a heavy hydrocarbon passage 113 that exchange heat with each other. Wherein, the inlet of the raw material gas channel 111 is used for receiving raw material gas. The cold energy of the cooling gas channel 112 and the heavy hydrocarbon channel 113 is absorbed by the feed gas in the process that the feed gas flows through the feed gas channel 111, the feed gas is pre-cooled, and the temperature is reduced.
Preferably, the heat exchanger 11 is an aluminum plate-fin heat exchanger, which has high heat exchange efficiency and is convenient for cold recycling, and has high structural concentration and is convenient for skid-mounted arrangement.
The raw material gas filter 14 is provided upstream of the raw material gas passage 111 of the heat exchanger 11. The inlet of the raw material gas filter 14 is connected to the position A, and the outlet of the raw material gas filter 14 is connected to the inlet of the raw material gas channel 111.
The raw material gas filter 14 filters the raw material gas inputted from the position a to make the raw material gas entering the heat exchanger 11 cleaner and prevent impurities possibly existing in the raw material gas from entering the heat exchanger 11. Especially for the heat exchanger 11 with a plate-fin structure, the feed gas filter 14 is additionally arranged, so that the micro-channel of the heat exchanger 11 can be effectively prevented from being blocked by impurities, and the heat exchange effect of the heat exchanger 11 is guaranteed.
The structure type and the filtration form of the raw material gas filter 14 are not limited, and can be flexibly selected according to actual needs.
The cold dryer 12 is used for cooling the precooled feed gas to remove heavy hydrocarbons. The freeze dryer 12, also known as a freeze dryer, generally utilizes a refrigerant cycle to provide refrigeration. The cooling dryer 12 is a device which is operated independently, and can automatically control the supplied cold quantity according to the set temperature, so as to cool the raw material gas to the set temperature. The air dryer 12 can select equipment with appropriate cooling capacity according to actual load requirements.
The cold energy provided by the cold dryer 12 cools the raw material gas, and most of heavy hydrocarbon is liquefied according to different boiling points of different hydrocarbon components in the natural gas, while the effective component methane of the natural gas is still kept in a gas phase. Thus, the outlet of the cold dryer 12 outputs gas-liquid two-phase raw gas, the liquid phase component is heavy hydrocarbon, and the gas phase component is natural gas that also contains part of heavy hydrocarbon that cannot be liquefied.
For example, in some alternative embodiments, cooling the feed gas to around-30 ℃ using the chiller dryer 12 may liquefy heavy hydrocarbons above C5.
The inlet of the cold dryer 12 is connected with the outlet of the raw material gas channel 111, and the outlet of the cold dryer 12 is communicated with the cooling gas channel 112 and the heavy hydrocarbon channel 113 of the heat exchanger 11 through the first separator 13.
The first separator 13 performs gas-liquid separation on the raw material gas cooled by the cooling dryer 12. The inlet of the first separator 13 is connected to the outlet of the freeze dryer 12.
The gas phase outlet of the first separator 13 is connected to the inlet of the cooling gas channel 112 of the heat exchanger 11, and the gas phase components in the cooled raw material gas are sent into the cooling gas channel 112, so that on one hand, the cold energy of the recovered gas phase components precools the raw material gas in the raw material gas channel 111, and on the other hand, the temperature of the gas phase components is increased so as to facilitate the subsequent heavy hydrocarbon adsorption and removal process.
The import of the heavy hydrocarbon passageway 113 of first separator 13's liquid phase exit linkage heat exchanger 11, liquid phase composition in the feed gas after will cooling is heavy hydrocarbon and sends into heavy hydrocarbon passageway 113, and the cold volume of retrieving heavy hydrocarbon carries out the precooling to the feed gas in feed gas passageway 111, promotes cold volume recycle rate.
In this embodiment, the refrigeration capacity of the gas-phase component and the liquid-phase component formed after the cooling of the refrigeration dryer 12 is recovered, and the utilization rate of the refrigeration capacity is high. In other embodiments, partial cold recovery is also possible, for example, only the gas phase cost of cold recovery, and accordingly, the structure of the heat exchanger 11 can be simplified.
Still referring to fig. 1, in some embodiments, the adsorption heavy hydrocarbon removal unit 2 includes a heavy hydrocarbon removal column 21 and a regeneration gas heater 22, and further includes a purge gas filter 23, a regeneration gas cooler 24, and a second separator 25.
Take off inside packing of heavy hydrocarbon tower 21 and have the filler that is used for adsorbing the heavy hydrocarbon, through the heavy hydrocarbon in the adsorption desorption natural gas. In some embodiments, the filler may be activated carbon.
In this embodiment, the number of the heavy hydrocarbon removal columns 21 is two. Two heavy hydrocarbon removal columns 21 are arranged in parallel. The two heavy hydrocarbon removal towers 21 are alternately in an adsorption state and a regeneration state. Wherein, the adsorption state refers to the removal of heavy hydrocarbon by utilizing the adsorption effect of the filler; the regeneration state refers to heating regeneration of the packing material adsorbed with heavy hydrocarbon.
The bottom parts of the two heavy hydrocarbon removing towers 21 are respectively connected with the outlet of the cooling gas channel 112 through a pipeline (not numbered in the figure) on which a valve member (not numbered in the figure) is arranged to control the connection and disconnection of the pipeline, so that the cooling gas channel 112 is selectively communicated with one heavy hydrocarbon removing tower 21.
The tops of the two heavy hydrocarbon removal towers 21 are connected with the position B through a purified gas filter 23 so as to output purified natural gas outwards.
Wherein, the purified gas filter 23 can filter the activated carbon possibly carried in the natural gas, so as to improve the cleanliness of the natural gas and prevent impurities from blocking the downstream cold box.
The inlet of the regeneration gas heater 22 is communicated with the top of the heavy hydrocarbon removal tower 21 through a purified gas filter 23, and the outlet of the regeneration gas heater 22 is connected with the top of the heavy hydrocarbon removal tower 21 through a pipeline and a valve. The regeneration gas heater 22 extracts a part of the purified natural gas as regeneration gas, and the regeneration gas is heated and then sent back to the heavy hydrocarbon removal tower 21 to regenerate the filler. The amount of natural gas entering the regeneration gas heater 22 may be controlled by a valve element.
In some embodiments, the regeneration gas heater 22 may be an electric heater, and is simple in structure and control.
The inlet of regeneration gas cooler 24 is connected with the bottom of heavy hydrocarbon removal tower 21, and is used for cooling the regeneration gas flowing through heavy hydrocarbon removal tower 21 after regenerating the filler, and the outlet of regeneration gas cooler 24 outputs the regeneration gas with gas-liquid two-phase. The heavy hydrocarbon adsorbed in the filler is absorbed when the regeneration gas regenerates the filler, and the heavy hydrocarbon absorbed by the regeneration gas is liquefied through the cooling of the regeneration gas cooler 24. The regeneration gas cooler 24 may take the form of a suitable cooler, such as an air cooler or the like.
The inlet of the second separator 25 is connected to the outlet of the regeneration gas cooler 24. The gas phase outlet of the second separator 25 outputs the regeneration gas outwards through C, which may be directed to a fuel gas pipe, for example, and the regeneration gas is used as fuel gas. The liquid phase outlet of the second separator 25 outputs heavy hydrocarbons outwardly.
In this embodiment, the regenerated gas is used as fuel gas after regenerating the filler and being treated by the regenerated gas cooler 24 and the second separator 25, and can satisfy other functional requirements of the plant, such as power generation. The purified natural gas is always used as the regeneration gas in the regeneration process of the filler, and the regeneration efficiency is high.
The heavy hydrocarbon removed in the cooling heavy hydrocarbon removal unit 1 and the adsorption heavy hydrocarbon removal unit 2 can also be sold as products. For example, in the above solution, the outlet of the heavy hydrocarbon passage 113 of the heat exchanger 11 and the liquid phase outlet of the second separator 25 may be respectively connected to an external heavy hydrocarbon storage tank 5, and the heavy hydrocarbon storage tank 5 collects heavy hydrocarbons, and if necessary, the heavy hydrocarbon storage tank 5 goes to a truck for transportation through the position D.
Based on the technical scheme, the process flow of the natural gas heavy hydrocarbon removal device is approximately as follows:
the raw material gas is input into the device from a position A, filtered by a raw material gas filter 14, and then enters a raw material gas channel 111 of a heat exchanger 11 for precooling, and then enters a cold dryer 12. The raw gas is cooled in the cold dryer 12 to separate out most heavy hydrocarbon, the raw gas is changed into a gas-liquid two-phase medium, the gas-liquid two-phase medium enters the first separator 13 to be subjected to gas-liquid separation, a gas-phase component enters the cooling gas channel 112 of the heat exchanger 11, and a liquid-phase component enters the heavy hydrocarbon channel 113 of the heat exchanger 11. The refrigeration of the gas-phase component and the liquid-phase component is recovered for use in precooling the feed gas in the feed gas channel 111. Then, the liquid phase component, i.e., the heavy hydrocarbon, is outputted from the outlet of the heavy hydrocarbon passage 113 to the heavy hydrocarbon storage tank 5.
Gaseous phase composition gets into the heavy hydrocarbon tower 21 that takes off of adsorption state from the export of cooling gas passageway 112, takes off the heavy hydrocarbon in the filler absorption gaseous phase composition in the heavy hydrocarbon tower 21, and the natural gas after the purification is exported from the top of taking off heavy hydrocarbon tower 21, filters through purifying gas filter 23, and then, most purification natural gas exports from B, goes to the low reaches cold box.
The natural gas of purification of another part is as the regeneration gas, send to regeneration state's heavy hydrocarbon tower 21 that takes off after regeneration gas heater 22 heats, the filler that attaches heavy hydrocarbon is regenerated, with the heavy hydrocarbon desorption back, the regeneration gas that has mixed with heavy hydrocarbon gets into regeneration gas cooler 24 from the bottom of taking off heavy hydrocarbon tower 21 and cools off, the gas-liquid two-phase regeneration gas after the cooling gets into second separator 25 and carries out gas-liquid separation, the gaseous composition of separation is used as the fuel gas for the regeneration gas from the export of C department outward, the liquid composition of separation is heavy hydrocarbon exports to heavy hydrocarbon storage tank 5 outward promptly.
According to the above description, the solution of the present invention has at least the following advantages: this natural gas takes off heavy hydrocarbon device adopts the heavy hydrocarbon in the mode desorption feed gas that cooling desorption and absorption desorption combined together, at first cools off the natural gas through cold dry machine 12, utilizes low temperature to separate out most heavy hydrocarbon, later again through taking off heavy hydrocarbon tower 21, utilizes remaining heavy hydrocarbon of absorbent mode desorption, and the heavy hydrocarbon desorption degree to the natural gas is high, satisfies the requirement of the follow-up liquefaction of natural gas.
Adopt this kind of mode, the load that takes off heavy hydrocarbon tower 21 is low, and the demand of packing is little, and then can reduce the height that takes off heavy hydrocarbon tower 21, and cold machine 12 that does is independent operation's equipment, and the process flow and the pipeline simple structure of a complete set of device to be convenient for arrange each equipment and pipeline integration on a sled dress, a complete set of natural gas takes off heavy hydrocarbon device and forms sled dress structure, convenient transportation and field installation.
Meanwhile, in the scheme, the heat exchanger 11 is used for recovering the cold energy of the natural gas cooled by the cold dryer 12, the recovered cold energy is used for precooling the feed gas entering the cold dryer 12, the power load of the cold dryer 12 is reduced, and the operation cost is reduced.
In addition, because the required amount of the filler in the heavy hydrocarbon removal tower 21 is small, the consumption of the regenerated gas for regenerating the filler can be reduced, so that the amount of the natural gas conveyed to the downstream cold box can be increased, and the LNG yield is correspondingly increased.
While the present invention has been described with reference to several exemplary embodiments, it is understood that the terminology used is intended to be in the nature of words of description and illustration, rather than of limitation. As the present invention may be embodied in several forms without departing from the spirit or essential characteristics thereof, it should also be understood that the above-described embodiments are not limited by any of the details of the foregoing description, but rather should be construed broadly within its spirit and scope as defined in the appended claims, and therefore all changes and modifications that fall within the meets and bounds of the claims, or equivalences of such meets and bounds are therefore intended to be embraced by the appended claims.
Claims (9)
1. The utility model provides a heavy hydrocarbon device is taken off to natural gas which characterized in that takes off heavy hydrocarbon unit and adsorbs taking off heavy hydrocarbon unit including the integrated cooling of arranging on same sled dress:
the cooling heavy hydrocarbon removal unit comprises:
the heat exchanger is used for precooling the feed gas and is provided with a feed gas channel and a cooling gas channel which exchange heat with each other; the inlet of the feed gas channel is used for receiving feed gas; and
the cold dryer is used for cooling the precooled feed gas to remove heavy hydrocarbons, an inlet of the cold dryer is connected with an outlet of the feed gas channel, and an outlet of the cold dryer is communicated with an inlet of the cooling gas channel;
the adsorption heavy hydrocarbon removal unit comprises:
the heavy hydrocarbon removal tower is filled with filler for absorbing heavy hydrocarbon, the bottom of the heavy hydrocarbon removal tower is connected with the outlet of the cooling gas channel, and the top of the heavy hydrocarbon removal tower outputs purified natural gas outwards; and
and the regeneration gas heater is communicated with the top of the heavy hydrocarbon removal tower and used for heating part of the purified natural gas and then sending the heated natural gas back to the heavy hydrocarbon removal tower so as to regenerate the filler.
2. The natural gas de-heavy hydrocarbon plant of claim 1, wherein the chilled de-heavy hydrocarbon unit further comprises a first separator for gas-liquid separation of the chilled feed gas; the inlet of the first separator is connected with the outlet of the cold dryer, and the gas-phase outlet of the first separator is connected with the inlet of the cooling gas channel;
the heat exchanger also has a heavy hydrocarbon channel in heat exchange with the feed gas channel; and an inlet of the heavy hydrocarbon channel is connected with a liquid phase outlet of the first separator, and an outlet of the heavy hydrocarbon channel outputs heavy hydrocarbon outwards.
3. The natural gas heavy hydrocarbon removal device of claim 1 or 2, wherein the heat exchanger is an aluminum plate-fin heat exchanger.
4. The natural gas heavy hydrocarbon removal plant of claim 3, wherein the chilled heavy hydrocarbon removal unit further comprises a feed gas filter disposed upstream of the feed gas channel.
5. The natural gas heavy hydrocarbon removal device as claimed in claim 1, wherein the number of the heavy hydrocarbon removal towers is two, and the two heavy hydrocarbon removal towers are arranged in parallel and are respectively connected with the cooling gas channel and the regeneration gas heater.
6. The natural gas heavy hydrocarbon removal plant of claim 1, wherein the filler is activated carbon.
7. The natural gas de-heavy hydrocarbon unit of claim 6, wherein the adsorption de-heavy hydrocarbon unit further comprises a purge gas filter; and the inlet of the purified gas filter is connected with the top of the heavy hydrocarbon removal tower.
8. The natural gas heavy hydrocarbon removal plant of any one of claims 1, 2, 5-7, wherein the regeneration gas heater is an electric heater.
9. The natural gas de-heavy hydrocarbon plant of any one of claims 1, 2, 5-7, wherein the adsorption de-heavy hydrocarbon unit further comprises a regeneration gas cooler and a second separator; the inlet of the regeneration gas cooler is connected with the bottom of the heavy hydrocarbon removal tower, and the outlet of the regeneration gas cooler is connected with the inlet of the second separator; a gas phase outlet of the second separator outputs regenerated gas outwards; and the liquid phase outlet of the second separator outputs heavy hydrocarbon outwards.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021049318.6U CN212894607U (en) | 2020-06-08 | 2020-06-08 | Heavy hydrocarbon device is taken off to natural gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021049318.6U CN212894607U (en) | 2020-06-08 | 2020-06-08 | Heavy hydrocarbon device is taken off to natural gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN212894607U true CN212894607U (en) | 2021-04-06 |
Family
ID=75276803
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202021049318.6U Active CN212894607U (en) | 2020-06-08 | 2020-06-08 | Heavy hydrocarbon device is taken off to natural gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN212894607U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114621798A (en) * | 2022-04-15 | 2022-06-14 | 合肥万豪能源设备有限责任公司 | Combined natural gas heavy hydrocarbon removal device and using method thereof |
| CN114856528A (en) * | 2022-05-11 | 2022-08-05 | 大庆市中瑞燃气有限公司 | Method for recovering waste heat of heavy hydrocarbon removal of wellhead gas |
-
2020
- 2020-06-08 CN CN202021049318.6U patent/CN212894607U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114621798A (en) * | 2022-04-15 | 2022-06-14 | 合肥万豪能源设备有限责任公司 | Combined natural gas heavy hydrocarbon removal device and using method thereof |
| CN114856528A (en) * | 2022-05-11 | 2022-08-05 | 大庆市中瑞燃气有限公司 | Method for recovering waste heat of heavy hydrocarbon removal of wellhead gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| AU2005249880B2 (en) | Method and apparatus for cooling in hydrogen plants | |
| CN100595263C (en) | Front end combination purification technique for producing liquefied natural gas from mixture gas rich-containing methane | |
| CN205461098U (en) | Oil -gas recovery processing device | |
| RU2597081C2 (en) | Method for complex extraction of valuable admixtures from natural helium-containing hydrocarbon gas with high nitrogen content | |
| CN110420536A (en) | Tank deck VOCs recycling and nitrogen reutilization system and method | |
| CN212894607U (en) | Heavy hydrocarbon device is taken off to natural gas | |
| AU2019295623B2 (en) | Adsorption process for treating natural gas | |
| CN102538398A (en) | Process and system for purifying, separating and liquefying nitrogen-and-oxygen-containing coal mine methane (CMM) | |
| CN106085528B (en) | High-adaptability heavy hydrocarbon removal process | |
| CN202595072U (en) | Device for partially liquefying natural gas by using pressure energy of natural gas | |
| CN113184850B (en) | High-purity carbon dioxide gas purification method and device thereof | |
| CN114621798A (en) | Combined natural gas heavy hydrocarbon removal device and using method thereof | |
| CN104673417B (en) | The system and method for precooling and dry decontamination for natural gas from coal | |
| CN105865145B (en) | A kind of coal gas gasification technique | |
| CN206244740U (en) | Pipe natural gas heavy hydrocarbon removal unit | |
| CN103589550A (en) | Carbon dioxide balanced system for beer brewing technology | |
| CN104893773B (en) | Pipe natural gas heavy hydrocarbon removal unit and heavy hydrocarbon removal methods | |
| CN114688828A (en) | Air separation device and system based on LNG cold energy utilization | |
| CN114440551B (en) | Device and method for recycling mixed hydrocarbon of associated gas of oil field rich in nitrogen and liquefying dry gas at low temperature | |
| CN211595550U (en) | Natural gas decarbonization system | |
| CN203904299U (en) | Pipeline natural gas heavy hydrocarbon removal unit | |
| CN209836108U (en) | Natural gas purification system | |
| CN213631179U (en) | Normal-temperature feeding purification ammonia synthesis gas liquid nitrogen washing device with precooling function | |
| CN211595551U (en) | Natural gas decarbonization system | |
| CN208907712U (en) | The integrated sled block co 2 liquefaction purifying plant of one kind |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |