CN215517292U - Integrated process system for producing LNG (liquefied Natural gas) and LPG (liquefied Petroleum gas) from oilfield associated gas - Google Patents
Integrated process system for producing LNG (liquefied Natural gas) and LPG (liquefied Petroleum gas) from oilfield associated gas Download PDFInfo
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Abstract
The utility model provides an integrated process system for producing LNG and LPG by using oilfield associated gas. The utility model provides an integrated process technology for performing the hydrocarbon removal and the light component liquefaction on petroleum associated gas rich in heavy hydrocarbon by adopting a process combining fractionation and low-temperature separation, and aims to effectively recover the petroleum associated gas and produce Liquefied Natural Gas (LNG), Liquefied Petroleum Gas (LPG) and stable light hydrocarbon products with high added values. The mixed hydrocarbon recovery and natural gas liquefaction are combined in one system, so that the effects of fully utilizing energy and resources and reducing environmental pollution are achieved; and the cold energy at the top of the pre-separation tower and the deethanizer enters a cold box for natural gas liquefaction to participate in heat exchange, so that the cold energy is recycled.
Description
Technical Field
The utility model relates to the technical field of oilfield associated gas, in particular to an integrated process system for producing LNG and LPG by oilfield associated gas.
Background
At present, the oil field associated gas is directly burnt, most of the associated gas only recovers propane and the components thereof as products, and the methane with high content is discharged and burnt to conditionally dry the gas for generating power or producing CNG (compressed natural gas), so that the utilization rate of the oil field associated gas in remote areas is low on the whole, and the method is not energy-saving and environment-friendly.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide an integrated process system for producing LNG and LPG by using oilfield associated gas. The utility model provides an integrated process technology for performing the hydrocarbon removal and the light component liquefaction on petroleum associated gas rich in heavy hydrocarbon by adopting a process combining fractionation and low-temperature separation, and aims to effectively recover the petroleum associated gas and produce Liquefied Natural Gas (LNG), Liquefied Petroleum Gas (LPG) and stable light hydrocarbon products with high added values.
In order to achieve the purpose, the utility model adopts the following technical scheme:
an integrated process system for producing LNG and LPG by using oilfield associated gas, which comprises: the system comprises a purified natural gas pipeline, a pre-separation tower top reflux tank, an LNG pipeline, a pre-separation tower top reflux pump, a deethanizer top reflux tank, a deethanizer top reflux pump, a liquefied gas tower, an LPG pipeline, a dry gas pipeline, a stable light hydrocarbon pipeline, a cold box and a circulating refrigerant mechanism;
the cold box comprises a precooling heat exchanger, a main cold heat exchanger and a postcooling heat exchanger;
the natural gas pipeline enters from the top and is led out from the bottom of the precooling heat exchanger and then is connected with a feed inlet of the preseparation tower, the pipeline of the gas phase outlet at the top of the preseparation tower enters from the top and is led out from the bottom of the precooling heat exchanger and then is connected with the feed inlet of the reflux tank at the top of the preseparation tower, the gas phase outlet at the top of the reflux tank at the top of the preseparation tower is connected with the LNG pipeline, and the LNG pipeline sequentially enters from the top and is led out from the bottom of the main cooling heat exchanger and the back cooling heat exchanger; a liquid phase outlet of the reflux tank at the top of the pre-separation tower is connected with a reflux inlet at the top of the pre-separation tower through a reflux pump at the top of the pre-separation tower; a liquid phase outlet at the bottom of the pre-separation tower is connected with a feed inlet of the deethanizer, a pipeline of a gas phase outlet at the top of the deethanizer enters from the top of the main cooling heat exchanger, is led out from the bottom of the main cooling heat exchanger, and is then connected with a feed inlet of a reflux tank at the top of the deethanizer, a gas phase outlet of the reflux tank at the top of the deethanizer is connected with the dry gas pipeline, and a liquid phase outlet of the reflux tank at the top of the deethanizer is connected with a reflux inlet at the top of the deethanizer through a reflux pump at the top of the deethanizer; a liquid phase outlet at the bottom of the deethanizer is connected with a feed inlet of the liquefied gas tower, a cooling reflux pipeline is arranged at the top of the liquefied gas tower, and the LPG pipeline is led out of the cooling reflux pipeline; and a liquid phase outlet at the bottom of the liquefied gas tower is connected with the stable light hydrocarbon pipeline.
According to the system of the present invention, preferably, the system further comprises a raw gas-dry gas heat exchanger through which the purified natural gas line and the dry gas line pass.
According to the system of the utility model, preferably, the LNG pipeline is provided with a liquefied natural gas J-T valve after being led out from the bottom of the after-cooling heat exchanger.
According to the system of the present invention, preferably, the cooling reflux line provided at the top of the liquefied gas tower includes: the liquefied gas tower top air cooler, the liquefied gas tower top reflux tank and the liquefied gas tower top reflux pump are sequentially connected with the tower top gas phase outlet of the liquefied gas tower, the outlet of the liquefied gas tower top reflux pump is connected with the tower top reflux inlet of the liquefied gas tower, and the LPG pipeline is led out from the connecting pipeline.
According to the system of the present invention, preferably, the refrigerant circulation mechanism includes a refrigerant compressor unit, a mixed refrigerant separator, a liquid-phase refrigerant J-T valve, a gas-phase refrigerant line, and a liquid-phase refrigerant line;
an outlet of the refrigerant compressor unit is connected with a feed inlet of the mixed refrigerant separator, and a gas-phase outlet of the mixed refrigerant separator is connected with the gas-phase refrigerant pipeline; the gas-phase refrigerant pipeline sequentially enters from the top and is led out from the bottom of the precooling heat exchanger, the main cold heat exchanger and the aftercooling heat exchanger, and then the gas-phase refrigerant J-T valve is arranged; the gas-phase refrigerant pipeline enters from the bottoms and is led out from the top of the after-cooling heat exchanger, the main cooling heat exchanger and the pre-cooling heat exchanger in sequence after the gas-phase refrigerant J-T valve and circulates to a feed inlet of the refrigerant compressor unit;
a liquid phase outlet at the bottom of the mixed refrigerant separator is connected with the liquid phase refrigerant pipeline, the liquid phase refrigerant pipeline sequentially enters from the top and is led out from the bottom of the precooling heat exchanger and the main cold heat exchanger, and then the liquid phase refrigerant J-T valve is arranged; and the liquid-phase refrigerant pipeline enters from the bottoms and is led out from the top of the main cooling heat exchanger and the precooling heat exchanger in sequence after the J-T valve of the liquid-phase refrigerant and circulates to the feed inlet of the refrigerant compressor unit.
According to the system of the present invention, preferably, the refrigerant compressor set includes a compressor, an air cooler and an aftercooler arranged in this order.
According to the system of the present invention, preferably, the refrigerant cycle mechanism further includes a refrigerant first separator;
and the liquid-phase refrigerant pipeline is connected with an inlet of the first refrigerant separator after the J-T valve, pipelines of a top gas-phase outlet and a bottom liquid-phase outlet of the first refrigerant separator respectively enter from the bottom of the main cold heat exchanger, and are led out from the top after being converged in the heat exchanger.
According to the system of the present invention, preferably, the refrigerant circulation mechanism further includes a second refrigerant separator;
and the gas-phase refrigerant pipeline is connected with an inlet of the second refrigerant separator after the J-T valve, pipelines of a top gas-phase outlet and a bottom liquid-phase outlet of the second refrigerant separator respectively enter from the bottom of the after-cooling heat exchanger, and are merged in the heat exchanger and then led out from the top.
According to the system of the present invention, preferably, the refrigerant circulation mechanism further includes a mixed refrigerant line;
after passing through the second refrigerant separator, pipelines entering from the bottom and leading out from the top of the aftercooling heat exchanger, and pipelines of a top gas phase outlet and a bottom liquid phase outlet of the first refrigerant separator enter from the bottom of the main cooling heat exchanger respectively, and are converged into the mixed refrigerant pipeline and then are led out from the top; and then the mixed refrigerant pipeline enters from the bottom of the precooling heat exchanger, is led out from the top of the precooling heat exchanger, and circulates to be connected with a feed inlet of the refrigerant compressor unit.
According to the system of the utility model, a liquid level regulating valve is preferably arranged on a connecting pipeline between a liquid phase outlet at the bottom of the pre-separation tower and a feed inlet of the deethanizer.
The beneficial effects of the utility model include:
1) the utility model combines the mixed hydrocarbon recovery and the natural gas liquefaction in one system, thereby achieving the effects of fully utilizing energy and resources and reducing environmental pollution.
2) In the utility model, the cold energy at the top of the pre-separation tower and the deethanizer enters the cold box for natural gas liquefaction to participate in heat exchange, and the cold energy is recycled. Meanwhile, for remote areas with water shortage, the cooler in the device can adopt a combined type of air cooling and water cooling.
3) The mixed refrigerant refrigeration cycle of the utility model adopts a two-stage throttling process, the quantity of J-T valves (Joule-Thomson throttling expansion valves) and separation equipment is less, and the flow is simplified.
4) The utility model realizes the high-efficiency recycling of the petroleum associated gas and produces LNG, LPG and stable light hydrocarbon products with high added values.
5) The equipment in the system belongs to conventional equipment, and for remote well regions or fast-failure oil and gas wells, skid-mounted integration, carrying, assembly and secondary utilization are facilitated.
Drawings
The drawings described herein are for illustration purposes only and are not intended to limit the scope of the present disclosure in any way. In addition, the shapes, the proportional sizes, and the like of the respective members in the drawings are merely schematic for facilitating the understanding of the present invention, and do not specifically limit the shapes, the proportional sizes, and the like of the respective members of the present invention. Those skilled in the art, having the benefit of the teachings of this invention, may choose from the various possible shapes and proportional sizes to implement the utility model as a matter of case.
Fig. 1 is an integrated process system for producing LNG and LPG from oilfield associated gas in a preferred embodiment.
Description of reference numerals:
100 clean natural gas line
T-101 pre-separation tower
V-104 pre-separation tower top reflux tank
200 LNG pipeline
P-101 pre-separation tower top reflux pump
T-102 deethanizer
V-105 deethanizer overhead reflux drum
Reflux pump at top of P-102 deethanizer
T-103 liquefied gas tower
300 LPG pipeline
400 dry gas pipeline
500 stable light hydrocarbon pipeline
LNG-101 precooling heat exchanger
LNG-102 main cooling heat exchanger
LNG-103 after-cooling heat exchanger
E101 raw gas-dry gas heat exchanger
J-T-03 liquefied natural gas J-T valve
A-102 liquefied gas tower top air cooler
V-106 liquefied gas tower top reflux tank
P-103 liquefied gas tower top reflux pump
C-101 compressor
A-101 air cooler
E-102 aftercooler
V-101 mixed refrigerant separator
J-T-01 liquid phase cryogen J-T valve
J-T-02 gas-phase refrigerant J-T valve
600 gas phase refrigerant line
700 liquid phase refrigerant line
V-102 refrigerant first separator
V-103 refrigerant second separator
800 mixed refrigerant line
LV-101 liquid level regulating valve
R material circulation
Detailed Description
In order to more clearly illustrate the utility model, the utility model is further described below with reference to preferred embodiments and the accompanying drawings. Similar parts in the figures are denoted by the same reference numerals. It is to be understood by persons skilled in the art that the following detailed description is illustrative and not restrictive, and is not to be taken as limiting the scope of the utility model.
In addition, some directional terms, such as "top," "bottom," etc., may be used in the embodiments of the present invention, and should not be construed as limiting the scope of the present invention, since such directional terms are used in conjunction with the placement of the device.
The present invention further provides a preferred embodiment, as shown in fig. 1, an integrated process system for producing LNG and LPG from oilfield associated gas, the system comprising: the system comprises a purified natural gas pipeline 100, a pre-separation tower T-101, a pre-separation tower top reflux tank V-104, an LNG pipeline 200, a pre-separation tower top reflux pump P-101, a deethanizer T-102, a deethanizer tower top reflux tank V-105, a deethanizer tower top reflux pump P-102, a liquefied gas tower T-103, an LPG pipeline 300, a dry gas pipeline 400, a stable light hydrocarbon pipeline 500, a cold box and a refrigerant circulation mechanism.
The cold box comprises a precooling heat exchanger LNG-101, a main cooling heat exchanger LNG-102 and a postcooling heat exchanger LNG-103.
The purified natural gas pipeline 100 is used for inputting a purified natural gas raw material to the system, the purified natural gas pipeline 100 enters from the top of the pre-cooling heat exchanger LNG-101, is led out from the bottom of the pre-cooling heat exchanger LNG-101 for cooling, and is then connected with a feed inlet of the pre-separation tower T-101, a pipeline of a gas phase outlet at the top of the pre-separation tower T-101 enters from the top of the pre-cooling heat exchanger LNG-101, is led out from the bottom of the pre-separation tower T-101, and is then connected with a feed inlet of a reflux tank V-104 at the top of the pre-separation tower, a gas phase outlet at the top of the reflux tank V-104 at the top of the pre-separation tower is connected with the LNG pipeline 200, and the LNG pipeline 200 sequentially enters from the top and is led out from the bottom of the main cooling heat exchanger LNG-102 and the after cooling heat exchanger LNG-103; a liquid phase outlet of the pre-separation tower top reflux tank V-104 is connected with a tower top reflux inlet of the pre-separation tower T-101 through the pre-separation tower top reflux pump P-101; a liquid phase outlet at the bottom of the pre-separation tower T-101 is connected with a feed inlet of the deethanizer T-102, a pipeline of a gas phase outlet at the top of the deethanizer T-102 enters from the top of the main cooling heat exchanger LNG-102, is led out from the bottom of the main cooling heat exchanger LNG-102, and is then connected with a feed inlet of a reflux tank V-105 at the top of the deethanizer, a gas phase outlet of the reflux tank V-105 at the top of the deethanizer is connected with the dry gas pipeline 400, and a liquid phase outlet at the bottom of the reflux tank V-105 at the top of the deethanizer is connected with a reflux inlet at the top of the deethanizer T-102 through a reflux pump P-102 at the top of the deethanizer; a liquid phase outlet at the bottom of the deethanizer T-102 is connected with a feed inlet of the liquefied gas tower T-103, a cooling return line is arranged at the top of the liquefied gas tower T-103, and the LPG line 300 is led out of the cooling return line; the liquid phase outlet at the bottom of the liquefied gas tower T-103 is connected with the stable light hydrocarbon pipeline 500.
In the preferred embodiment, the system further comprises a raw gas-dry gas heat exchanger E101, and the purified natural gas pipeline 100 and the dry gas pipeline 400 pass through the raw gas-dry gas heat exchanger E101, so that the purified natural gas recovers the cold energy of the dry gas.
In the preferred embodiment, the LNG line 200 is provided with a liquefied natural gas J-T valve J-T-03 after being led out from the bottom of the after-cooling heat exchanger LNG-103. After the material of the LNG pipeline 200 is cooled and condensed to-160 ℃ by a cold box, the throttling is reduced to 100kPa (G) and about-162 ℃ by a liquefied natural gas J-T valve J-T-03, and an LNG product is produced.
In the preferred embodiment, the cooling reflux line provided at the top of the liquefied gas column T-103 includes: the liquefied gas tower top air cooler A-102, the liquefied gas tower top reflux tank V-106 and the liquefied gas tower top reflux pump P-103 are sequentially connected with the tower top gas phase outlet of the liquefied gas tower T-103, the outlet of the liquefied gas tower top reflux pump P-103 is connected with the tower top reflux inlet of the liquefied gas tower T-103, and the LPG pipeline is led out of the connecting pipeline.
In the preferred embodiment, the refrigerant cycle mechanism includes a refrigerant compressor train, a mixed refrigerant separator V-101, a liquid refrigerant J-T valve J-T-01, a gas refrigerant J-T valve J-T-02, a gas refrigerant line 600, and a liquid refrigerant line 700.
The outlet of the refrigerant compressor unit is connected with the feed inlet of the mixed refrigerant separator V-101, and the gas-phase outlet of the mixed refrigerant separator V-101 is connected with the gas-phase refrigerant pipeline 600; the gas-phase refrigerant pipeline 600 sequentially enters from the top and is led out from the bottom of the precooling heat exchanger LNG-101, the main cooling heat exchanger LNG-102 and the after-cooling heat exchanger LNG-103, and then the gas-phase refrigerant J-T valve J-T-02 is arranged; the gas-phase refrigerant pipeline 600 enters from the bottoms and is led out from the tops of the after-cooling heat exchanger LNG-103, the main-cooling heat exchanger LNG-102 and the pre-cooling heat exchanger LNG-101 in sequence after the gas-phase refrigerant J-T valve J-T-02 and circulates to a feed inlet of the refrigerant compressor unit.
The bottom liquid phase outlet of the mixed refrigerant separator V-101 is connected to the liquid phase refrigerant pipeline 700, the liquid phase refrigerant pipeline 700 sequentially enters from the top and is led out from the bottom of the pre-cooling heat exchanger LNG-101 and the main cooling heat exchanger LNG-102, and then the liquid phase refrigerant J-T valve J-T-01 is arranged; the liquid-phase refrigerant pipeline 700 enters from the bottom and is led out from the top of the main cooling heat exchanger LNG-102 and the precooling heat exchanger LNG-101 in sequence after the liquid-phase refrigerant J-T valve J-T-01, and circulates to the feed inlet of the refrigerant compressor unit.
In the preferred embodiment, the refrigerant compressor train includes a compressor C-101, an air cooler A-101 and an aftercooler E-102 arranged in series.
In the preferred embodiment, the refrigerant cycle mechanism further includes a first refrigerant separator V-102.
The liquid-phase refrigerant pipeline 700 is connected with an inlet of the first refrigerant separator V-102 after the liquid-phase refrigerant J-T valve J-T-01, a pipeline of a top gas-phase outlet and a pipeline of a bottom liquid-phase outlet of the first refrigerant separator V-102 respectively enter from the bottom of the main cooling heat exchanger LNG-102, and are led out from the top after being converged in the heat exchanger.
In the preferred embodiment, the refrigerant cycle mechanism further includes a second refrigerant separator V-103.
The gas-phase refrigerant pipeline 600 is connected with an inlet of the second refrigerant separator V-103 after the gas-phase refrigerant J-T valve J-T-02, a pipeline of a top gas-phase outlet and a pipeline of a bottom liquid-phase outlet of the second refrigerant separator V-103 respectively enter from the bottom of the after-cooling heat exchanger LNG-103, and are merged in the heat exchanger and then led out from the top.
In the preferred embodiment, the refrigerant cycle mechanism further includes a mixed refrigerant line 800.
After passing through the refrigerant second separator V-103, a pipeline which enters from the bottom of the aftercooling heat exchanger LNG-103 and is led out from the top, and a pipeline which enters from the bottom of the main cooling heat exchanger LNG-102 together with a pipeline of a top gas phase outlet and a bottom liquid phase outlet of the refrigerant first separator V-102, are merged in a heat exchanger to form the mixed refrigerant pipeline 800 and are led out from the top; and then the mixed refrigerant pipeline 800 enters from the bottom and is led out from the top of the pre-cooling heat exchanger LNG-101, and circulates to be connected with a feed inlet of the refrigerant compressor unit.
In the preferred embodiment, a liquid level regulating valve LV-101 is arranged on a connecting pipeline between the liquid phase outlet at the bottom of the pre-separation tower T-101 and the feed inlet of the deethanizer T-102.
The integrated process for producing LNG and LPG by using the system in the preferred embodiment comprises the following processes:
purifying natural gas by about 4.5MPaG (after acid gas removal, dehydration and mercury removal treatment), recovering cold energy of dry gas by a raw gas-dry gas heat exchanger E101, then removing the cold gas to a cold box, cooling the cold gas to about-20 ℃ by a reflux mixed refrigerant by a precooling heat exchanger LNG-101 of the cold box, then entering a low-temperature gas of a pre-separation tower T-101 and tower top reflux (pumping low-temperature liquid at the bottom of a reflux tank V-104 at the top of the pre-separation tower into the top of the pre-separation tower T-101 by a reflux pump P-101 at the top of the pre-separation tower), transferring heat and mass, and then pumping most C in the reflux4H10Recovering equal weight component and returning CH in condensate4And C2H6Gasifying light components, returning the tower top natural gas with the heavy hydrocarbon separated out to a cold box, cooling the tower top natural gas by a main cooling heat exchanger LNG-102 and a post cooling heat exchanger LNG-103, condensing the tower top natural gas to-160 ℃, throttling the cooled tower top natural gas to 100kPa (G) by a liquefied natural gas J-T valve J-T-03, and producing an LNG product when the temperature is about-162 ℃.
Heavy hydrocarbon components at the bottom of the pre-separation tower T-101 are fed into a deethanizer T-102 through a liquid level regulating valve LV-101 (the pressure after the valve is about 1.8MPaG), and C is enriched3H8The top gas of the deethanizer of the components is subjected to heat and mass transfer with the low-temperature gas refluxed from the top of the deethanizer (the low-temperature liquid at the bottom of a V-105 tank of a reflux tank at the top of the deethanizer is pumped into the top of a deethanizer T-102 by a reflux pump P-102 at the top of the deethanizer), and then most of C in the gas is transferred3And partial ethane is condensed, mixed hydrocarbon at the bottom of the deethanizer T-102 is sent to a liquefied gas tower T-103, a liquefied gas tower top air cooler A-102, a liquefied gas tower top reflux tank V-106 and a liquefied gas tower top reflux pump P-103 are arranged at the top of the liquefied gas tower T-103 to form tower top reflux and control the quality of liquefied petroleum gas at the top of the tower, a reboiler is arranged at the bottom of the tower to control the quality of stable light hydrocarbon, LPG is produced at the top of the liquefied gas tower, and stable light hydrocarbon is produced at the bottom of the tower.
The mixed refrigerant is recycled in the system through a refrigerant circulating mechanism. The mixed refrigerant is separated into liquid phase refrigerant and gas phase refrigerant by a refrigerant compressor unit (comprising a compressor C-101, an air cooler A-101 and an aftercooler E-102) and respectively enters a cold box, the liquid phase refrigerant is throttled and depressurized to about 0.25MPaG by a liquid phase refrigerant J-T valve J-T-01 after being cooled by a precooling heat exchanger LNG-101 and a main cooling heat exchanger LNG-102 and is mixed with the returned gas phase refrigerant, the gas phase refrigerant is liquefied in the aftercooling heat exchanger LNG-103 and is subcooled to-160 ℃, the gas phase refrigerant is throttled and depressurized to about 0.28MPaG by a gas phase refrigerant J-T valve J-T-02 and returns to the bottom end of the cold box, the gas phase refrigerant is vaporized from bottom to top to provide cooling energy for the aftercooling heat exchanger LNG-103, the main cooling heat exchanger LNG-102 and the precooling heat exchanger LNG-101, the mixed refrigerant after being discharged from the cold box returns to an inlet of the compressor C-101, and completing a circulation process after the pressure is increased by a compressor C-101.
When the gas-phase refrigerant returns to the bottom of the cold box, in order to ensure better heat exchange effect and simultaneously reduce the vibration of the two-phase flow pipeline, the low-temperature fluid is separated into an outlet gas phase by the refrigerant second separator V-103, the outlet gas phase and the liquid phase are separately led to the bottom of the back-cooling heat exchanger LNG-103 to enter, and the convergence in the heat exchanger is led out from the top of the back-cooling heat exchanger LNG-103. Similarly, when the liquid-phase refrigerant returns to the bottom of the main cold heat exchanger LNG-102, the liquid-phase refrigerant is also subjected to gas-liquid separation by the refrigerant first separator V-102, separately introduced to the bottom of the after-main cold heat exchanger LNG-102, and merged with the refrigerant pipeline introduced from the top of the after-cold heat exchanger LNG-103 in the main cold heat exchanger LNG-102 to form the mixed refrigerant pipeline 800, and circulated to the inlet of the compressor C-101.
Associated gas liquefaction pretreatment processes such as natural gas pressurization and purification (deacidification, dehydration, demercuration and the like) belong to the conventional technology in the field, and the utility model is not described herein again.
It should be understood that the above-mentioned embodiments of the present invention are only examples for clearly illustrating the present invention, and are not intended to limit the embodiments of the present invention, and it will be obvious to those skilled in the art that other variations or modifications may be made on the basis of the above description, and all embodiments may not be exhaustive, and all obvious variations or modifications may be included within the scope of the present invention.
Claims (10)
1. An integrated process system for producing LNG and LPG by using oilfield associated gas is characterized by comprising the following steps:
the system comprises a purified natural gas pipeline (100), a pre-separation tower (T-101), a pre-separation tower top reflux tank (V-104), an LNG pipeline (200), a pre-separation tower top reflux pump (P-101), a deethanizer (T-102), a deethanizer top reflux tank (V-105), a deethanizer top reflux pump (P-102), a liquefied gas tower (T-103), an LPG pipeline (300), a dry gas pipeline (400), a stable light hydrocarbon pipeline (500), a cold box and a refrigerant circulating mechanism;
the cold box comprises a precooling heat exchanger (LNG-101), a main cold heat exchanger (LNG-102) and a postcooling heat exchanger (LNG-103);
the purified natural gas pipeline (100) enters from the top and is led out from the bottom of the precooling heat exchanger (LNG-101), and then is connected with a feed inlet of the preseparation tower (T-101), a pipeline of a gas phase outlet at the top of the precooling heat exchanger (LNG-101) enters from the top and is led out from the bottom of the precooling heat exchanger (T-101), and then is connected with a feed inlet of a reflux tank (V-104) at the top of the preseparation tower, a gas phase outlet of the reflux tank (V-104) at the top of the preseparation tower is connected with the LNG pipeline (200), and the LNG pipeline (200) sequentially enters from the top and is led out from the bottom of the main cooling heat exchanger (LNG-102) and the back cooling heat exchanger (LNG-103); a tower bottom liquid phase outlet of the tower top reflux tank (V-104) of the pre-separation tower is connected with a tower top reflux inlet of the pre-separation tower (T-101) through the tower top reflux pump (P-101) of the pre-separation tower; a liquid phase outlet at the bottom of the pre-separation tower (T-101) is connected with a feed inlet of the deethanizer (T-102), a pipeline of a gas phase outlet at the top of the deethanizer (T-102) enters from the top of the main cooling heat exchanger (LNG-102), is led out from the bottom of the main cooling heat exchanger and is then connected with a feed inlet of a reflux tank (V-105) at the top of the deethanizer, a gas phase outlet of the reflux tank (V-105) at the top of the deethanizer is connected with the dry gas pipeline (400), and a liquid phase outlet of the reflux tank (V-105) at the top of the deethanizer is connected with a reflux inlet at the top of the deethanizer (T-102) through a reflux pump (P-102) at the top of the deethanizer; a liquid phase outlet at the bottom of the deethanizer (T-102) is connected with a feed inlet of the liquefied gas tower (T-103), a cooling return line is arranged at the top of the liquefied gas tower (T-103), and the LPG line (300) is led out of the cooling return line; and the liquid phase outlet at the bottom of the liquefied gas tower (T-103) is connected with the stable light hydrocarbon pipeline (500).
2. The system of claim 1, further comprising a raw gas-to-dry gas heat exchanger (E101), the purified natural gas line (100) and the dry gas line (400) passing through the raw gas-to-dry gas heat exchanger (E101).
3. The system according to claim 1, characterized in that the LNG line (200) is provided with a liquefied natural gas J-T valve (J-T-03) after exiting from the bottom of the after-cooling heat exchanger (LNG-103).
4. The system according to claim 1, wherein the cooling reflux line provided at the top of the liquefied gas column (T-103) comprises: the liquefied gas tower top air cooler (A-102), the liquefied gas tower top reflux tank (V-106) and the liquefied gas tower top reflux pump (P-103) are sequentially connected with the tower top gas phase outlet of the liquefied gas tower (T-103), the outlet of the liquefied gas tower top reflux pump (P-103) is connected with the tower top reflux inlet of the liquefied gas tower (T-103), and the LPG pipeline is led out of the connecting pipeline.
5. The system according to claim 1, wherein the refrigerant circulation mechanism comprises a refrigerant compressor train, a mixed refrigerant separator (V-101), a liquid-phase refrigerant J-T valve (J-T-01), a gas-phase refrigerant J-T valve (J-T-02), a gas-phase refrigerant line (600), and a liquid-phase refrigerant line (700);
the outlet of the refrigerant compressor unit is connected with the feed inlet of the mixed refrigerant separator (V-101), and the gas-phase outlet of the mixed refrigerant separator (V-101) is connected with the gas-phase refrigerant pipeline (600); the gas-phase refrigerant pipeline (600) sequentially enters from the top and is led out from the bottom of the precooling heat exchanger (LNG-101), the main cooling heat exchanger (LNG-102) and the after-cooling heat exchanger (LNG-103), and then the gas-phase refrigerant J-T valve (J-T-02) is arranged; the gas-phase refrigerant pipeline (600) enters from the bottoms and is led out from the tops of the after-cooling heat exchanger (LNG-103), the main cooling heat exchanger (LNG-102) and the pre-cooling heat exchanger (LNG-101) in sequence after the gas-phase refrigerant J-T valve (J-T-02) and circulates to a feed inlet of the refrigerant compressor unit;
a liquid phase outlet of the mixed refrigerant separator (V-101) is connected with the liquid phase refrigerant pipeline (700), the liquid phase refrigerant pipeline (700) sequentially enters from the top and is led out from the bottom of the pre-cooling heat exchanger (LNG-101) and the main cooling heat exchanger (LNG-102), and then the liquid phase refrigerant J-T valve (J-T-01) is arranged; and the liquid-phase refrigerant pipeline (700) enters from the bottoms and is led out from the tops of the main cooling heat exchanger (LNG-102) and the precooling heat exchanger (LNG-101) in sequence after the liquid-phase refrigerant J-T valve (J-T-01) and circulates to a feeding hole of the refrigerant compressor unit.
6. The system according to claim 5, wherein the refrigerant compressor train comprises a compressor (C-101), an air cooler (A-101) and an aftercooler (E-102) arranged in series.
7. The system according to claim 5, wherein the refrigerant cycle mechanism further comprises a refrigerant first separator (V-102);
the liquid-phase refrigerant pipeline (700) is connected with an inlet of the first refrigerant separator (V-102) after the liquid-phase refrigerant J-T valve (J-T-01), a gas-phase outlet at the top of the first refrigerant separator (V-102) and a liquid-phase outlet pipeline respectively enter from the bottom of the main cold heat exchanger (LNG-102), and are led out from the top after being converged in the heat exchanger.
8. The system according to claim 7, wherein the refrigerant cycle mechanism further comprises a second refrigerant separator (V-103);
the gas-phase refrigerant pipeline (600) is connected with an inlet of the second refrigerant separator (V-103) after the gas-phase refrigerant J-T valve (J-T-02), pipelines of a top gas-phase outlet and a bottom liquid-phase outlet of the second refrigerant separator (V-103) respectively enter from the bottom of the after-cooling heat exchanger (LNG-103), and are led out from the top after being converged in the heat exchanger.
9. The system of claim 8, wherein the refrigerant cycle mechanism further comprises a mixed refrigerant line (800);
after passing through the refrigerant second separator (V-103), a pipeline which enters from the bottom and is led out from the top of the after-cooling heat exchanger (LNG-103) and a pipeline which is at the top gas phase outlet and the bottom liquid phase outlet of the refrigerant first separator (V-102) respectively enter from the bottom of the main cooling heat exchanger (LNG-102), and are merged in the heat exchangers to become the mixed refrigerant pipeline (800) and then are led out from the top; and then the mixed refrigerant pipeline (800) enters from the bottom of the precooling heat exchanger (LNG-101), is led out from the top of the precooling heat exchanger, and circulates to be connected with a feed inlet of the refrigerant compressor unit.
10. The system according to claim 1, characterized in that a level regulating valve (LV-101) is provided on the connection line between the liquid bottom phase outlet of the pre-separation column (T-101) and the feed inlet of the deethanizer (T-102).
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| CN117106499A (en) * | 2023-10-23 | 2023-11-24 | 陕西航天德林科技集团有限公司 | Oilfield associated gas comprehensive utilization system and process |
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| CN117106499A (en) * | 2023-10-23 | 2023-11-24 | 陕西航天德林科技集团有限公司 | Oilfield associated gas comprehensive utilization system and process |
| CN117106499B (en) * | 2023-10-23 | 2024-02-23 | 陕西航天德林科技集团有限公司 | Oilfield associated gas comprehensive utilization system and process |
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