CN213866100U - Be applied to light hydrocarbon recovery and take off heavy hydrocarbon device of FLNG - Google Patents
Be applied to light hydrocarbon recovery and take off heavy hydrocarbon device of FLNG Download PDFInfo
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- CN213866100U CN213866100U CN202022883203.3U CN202022883203U CN213866100U CN 213866100 U CN213866100 U CN 213866100U CN 202022883203 U CN202022883203 U CN 202022883203U CN 213866100 U CN213866100 U CN 213866100U
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Abstract
The utility model discloses a be applied to FLNG's lighter hydrocarbons and retrieve and take off heavy hydrocarbon device, including cold box, separator, expander, compressor, condenser, reflux drum, deethanizer and reboiler. And (3) condensing the dried feed gas after the dried feed gas enters a cold box, and separating gas and liquid after the condensed gas enters a separator. One part of gas at the top of the separator is decompressed by an expander and then enters the middle part of the deethanizer, and the other part of gas is sent to a condenser for condensation, thereby providing reflux for the deethanizer. After the pressure of the liquid at the bottom of the separator is reduced, the liquid enters a cold box to exchange heat with feed gas and then is sent to the bottom of a deethanizer; the bottom effluent outlet is connected to a reboiler via a pipeline, and the reboiler is supplied with heat from hot oil. The liquid at the bottom of the deethanizer is an NGL product containing recovered LPG, and the gas at the top of the deethanizer is lean gas or natural gas without heavy hydrocarbon, and enters a compressor for pressurization after exchanging heat with a condenser and a cold box at the top of the tower. The utility model discloses the higher market value's such as LPG in the recovery natural gas product.
Description
Technical Field
The utility model belongs to the technical field of the chemical industry, concretely relates to be applied to FLNG's lighter hydrocarbons and retrieve and take off heavy hydrocarbon device.
Background
As the world seeks cleaner energy for reducing pollution and carbon dioxide emissions, the demand for Liquefied Natural Gas (LNG) will steadily increase for the next decades, with a wide prospect for floating liquefied natural gas units (FLNG). While the gas source for the FLNG device is typically rich, containing a significant amount of C3+ components. The significance of light hydrocarbon recovery and heavy hydrocarbon removal lies in that:
the C3+ should be separated and removed to adjust the heating value of the LNG for the worldwide LNG users' requirements on the heating value of the LNG;
propane and butane have a higher market value than pipeline gas and should be separated from the feed gas;
if the heavy hydrocarbon components of the feed gas cannot be removed effectively, the cold box will be frozen and blocked and normal production will not be possible;
disclosure of Invention
The to-be-solved technical problem of the utility model is to provide a be applied to FLNG's lighter hydrocarbons and retrieve and take off heavy hydrocarbon device, the LPG etc. in the recovery natural gas have the product of higher market value.
In order to solve the technical problem, the utility model discloses take following technical scheme: a light hydrocarbon recovery and heavy hydrocarbon removal device applied to FLNG comprises a cold box, a separator, an expander, a compressor, a condenser, a reflux tank, a deethanizer and a reboiler; the cold box is provided with a raw material gas inlet, a heat exchange gas outlet and a liquid inlet; the separator is provided with a heat exchange gas inlet, the top of the separator is provided with a gas outlet, and the bottom of the separator is provided with a liquid outlet; a heat exchange gas outlet on the cold box is connected with a heat exchange gas inlet of the separator through a pipeline; the liquid outlet of the separator is connected with the liquid inlet on the cold box through a pipeline; the gas outlet of the separator is connected with the expander and the condenser through pipelines; the middle part of the deethanizer is provided with a gas inlet, the top part of the deethanizer is provided with a gas outlet, the upper part of the deethanizer is provided with a reflux port, and the lower part of the deethanizer is provided with a tower bottom effluent outlet and a return inlet; the expansion machine is connected with a gas inlet in the middle of the deethanizer through a pipeline; the condenser is connected with the reflux tank through a pipeline; the reflux tank is connected with a reflux port at the upper part of the deethanizer through a pipeline; the bottom of the cold box is provided with a heat exchange liquid outlet which is connected with a heat exchange liquid inlet at the lower part of the deethanizer through a pipeline; the reboiler is provided with an effluent inlet and a return outlet; the bottom effluent outlet is connected with an effluent inlet on the reboiler through a pipeline, and a return outlet on the reboiler is connected with a return inlet on the deethanizer through a pipeline; the top of the deethanizer is provided with a gas outlet which is sequentially connected with a condenser and a cold box through pipelines; the cold box is connected with the compressor.
Further, the compressor is coaxial with and driven by the expander.
Further, the gas outlet of the separator is connected with a main gas pipe; the main air pipe is connected with a first branch air pipe and a second branch air pipe; the first branch air pipe is connected with an expansion machine; and the second branch gas pipe is connected with the condenser.
Furthermore, the top of the cold box is provided with a high-pressure refrigerant inlet and a low-pressure refrigerant outlet.
Further, the high-pressure refrigerant inlet is refrigerated by the mixed refrigerant to provide auxiliary cooling capacity.
The utility model has the advantages that:
1) recycling products with higher market value such as LPG in natural gas;
2) heavy hydrocarbons are removed from the feed gas upstream of the liquefaction unit, thereby increasing the single line capacity of the FLNG unit by natural gas pressurization.
Drawings
The invention is further illustrated by the following figures and examples.
Fig. 1 is a schematic structural diagram of the present invention.
Detailed Description
Referring to fig. 1, the light hydrocarbon recovery and heavy hydrocarbon removal device applied to FLNG of the present invention includes a cold box 1, a separator 2, an expander 3, a compressor 4, a condenser 5, a reflux tank 6, a deethanizer 7 and a reboiler 8; the cold box 1 is provided with a raw material gas inlet 11, a heat exchange gas outlet 12 and a liquid inlet 13; the top of the cold box 1 is provided with a high-pressure refrigerant inlet 14 and a low-pressure refrigerant outlet 15; the separator 2 is provided with a heat exchange gas inlet 21, the top of the separator 2 is provided with a gas outlet 22, and the bottom of the separator 2 is provided with a liquid outlet 23; the heat exchange gas outlet 12 on the cold box 1 is connected with the heat exchange gas inlet 21 of the separator 2 through a pipeline; the liquid outlet 23 of the separator 2 is connected with the liquid inlet 13 on the cold box through a pipeline; the gas outlet 22 of the separator is connected to the main gas pipe 9; the main air pipe 9 is connected with a first branch air pipe 91 and a second branch air pipe 92; the first branch air pipe 91 is connected with the expander 3; the second branch gas pipe 92 is connected with the condenser 5; the middle part of the deethanizer 7 is provided with a gas inlet 71, the top part is provided with a gas outlet 72, the upper part is provided with a reflux port 73, and the lower part is provided with a bottom effluent outlet 74 and a return inlet 75; the expansion machine 3 is connected with a gas inlet 71 at the middle part of the deethanizer through a pipeline; the condenser 5 is connected with the reflux tank 6 through a pipeline; the reflux tank 6 is connected with a reflux port 73 at the upper part of the deethanizer through a pipeline; the bottom of the cold box 1 is provided with a heat-exchange liquid outlet 16, and the heat-exchange liquid outlet 16 is connected with a heat-exchange liquid inlet 76 at the lower part of the deethanizer 7 through a pipeline; the reboiler 8 is provided with an effluent inlet 81 and a return outlet 82; the bottom effluent outlet 74 is connected with an effluent inlet 81 on the reboiler 8 through a pipeline, and a return outlet 82 on the reboiler 8 is connected with a return inlet 75 on the deethanizer through a pipeline; the top of the deethanizer is provided with a gas outlet 72 which is sequentially connected with the condenser 5 and the cold box 1 through pipelines; the cold box 1 is connected with a compressor 4.
The utility model discloses after the feeding gas after the drying got into cold box 1, carried out the heat transfer and was condensed with the gas after having got rid of the heavy ends, gas after the condensation got into low temperature separator 2 and carries out gas, liquid separation. Auxiliary cooling capacity is provided by mixed refrigerant refrigeration according to the intake air component and the LPG recovery requirement.
The gas at the top of the low-temperature separator 2 is divided into two parts, and one part of the gas enters the middle part of the deethanizer after being decompressed by an expander 3; another portion of the gas is sent to condenser 4 where it is condensed by the deethanizer overhead gas, thereby providing reflux to the deethanizer.
After the pressure of the liquid at the bottom of the low-temperature separator 2 is reduced, the liquid enters a cooling box 1 to exchange heat with feed gas and then is sent to the bottom of a deethanizer; the deethanizer has a low temperature of about 90 ℃, the bottom stream outlet 74 is connected to the reboiler 8 via a line, the bottom stream enters the reboiler and is heated and sent to the bottom of the secondary deethanizer, and the reboiler is supplied with heat from the hot oil.
The operating pressure of the deethanizer 7 is about 2.5Mpa, the liquid at the bottom of the deethanizer is NGL product containing recovered LPG, the gas at the top of the deethanizer is lean gas or natural gas from which heavy hydrocarbon has been removed, the gas exchanges heat with the overhead condenser 5 and the cold box 1 and then enters the compressor 4 for pressurization, and the compressor 4 is coaxial with the expander 3 and is driven by the expander.
The above description is only a preferred embodiment of the present invention, and is not intended to limit the present invention, and those skilled in the art can make various modifications or equivalent substitutions within the spirit and scope of the present invention, and such modifications or equivalent substitutions should also be considered as falling within the scope of the present invention.
Claims (5)
1. Be applied to light hydrocarbon recovery and take off heavy hydrocarbon device of FLNG, its characterized in that: comprises a cold box (1), a separator (2), an expander (3), a compressor (4), a condenser (5), a reflux tank (6), a deethanizer (7) and a reboiler (8); the cold box (1) is provided with a raw material gas inlet (11), a heat exchange gas outlet (12) and a liquid inlet (13); a heat exchange gas inlet (21) is arranged on the separator (2), a gas outlet (22) is arranged at the top of the separator (2), and a liquid outlet (23) is arranged at the bottom of the separator (2); a heat exchange gas outlet (12) on the cold box (1) is connected with a heat exchange gas inlet (21) of the separator (2) through a pipeline; the liquid outlet (23) of the separator (2) is connected with the liquid inlet (13) on the cold box through a pipeline; the gas outlet (22) of the separator is connected with the expander (3) and the condenser (5) through pipelines; the middle part of the deethanizer (7) is provided with a gas inlet (71), the top part is provided with a gas outlet (72), the upper part is provided with a reflux port (73), and the lower part is provided with a tower bottom effluent outlet (74) and a return inlet (75); the expansion machine (3) is connected with a gas inlet (71) at the middle part of the deethanizer through a pipeline; the condenser (5) is connected with the reflux tank (6) through a pipeline; the reflux tank (6) is connected with a reflux port (73) at the upper part of the deethanizer through a pipeline; the bottom of the cold box (1) is provided with a heat exchange liquid outlet (16), and the heat exchange liquid outlet (16) is connected with a heat exchange liquid inlet (76) at the lower part of the deethanizer (7) through a pipeline; the reboiler (8) is provided with an effluent inlet (81) and a return outlet (82); the bottom effluent outlet (74) is connected with an effluent inlet (81) on the reboiler (8) through a pipeline, and a return outlet (82) on the reboiler (8) is connected with a return inlet (75) on the deethanizer through a pipeline; a gas outlet (72) arranged at the top of the deethanizer is sequentially connected with the condenser (5) and the cold box (1) through pipelines; the cold box (1) is connected with the compressor (4).
2. A light hydrocarbon recovery and heavy hydrocarbon removal device as claimed in claim 1, applied to FLNG, wherein: the compressor (4) is coaxial with the expander (3) and is driven by the expander (3).
3. A light hydrocarbon recovery and heavy hydrocarbon removal device as claimed in claim 1, applied to FLNG, wherein: the gas outlet (22) of the separator (2) is connected with the main gas pipe (9); the main air pipe (9) is connected with a first branch air pipe (91) and a second branch air pipe (92); the first branch air pipe (91) is connected with the expander (3); and the second branch gas pipe (92) is connected with the condenser (5).
4. A light hydrocarbon recovery and heavy hydrocarbon removal device as claimed in claim 1, applied to FLNG, wherein: the top of the cold box (1) is provided with a high-pressure refrigerant inlet (14) and a low-pressure refrigerant outlet (15).
5. A light hydrocarbon recovery and heavy hydrocarbon removal device as claimed in claim 1, applied to FLNG, wherein: the high-pressure refrigerant inlet (14) is refrigerated by the mixed refrigerant to provide auxiliary cooling capacity.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022883203.3U CN213866100U (en) | 2020-12-03 | 2020-12-03 | Be applied to light hydrocarbon recovery and take off heavy hydrocarbon device of FLNG |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022883203.3U CN213866100U (en) | 2020-12-03 | 2020-12-03 | Be applied to light hydrocarbon recovery and take off heavy hydrocarbon device of FLNG |
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| Publication Number | Publication Date |
|---|---|
| CN213866100U true CN213866100U (en) | 2021-08-03 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202022883203.3U Active CN213866100U (en) | 2020-12-03 | 2020-12-03 | Be applied to light hydrocarbon recovery and take off heavy hydrocarbon device of FLNG |
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| CN (1) | CN213866100U (en) |
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