CN112111297A - Device and method for recycling light hydrocarbon through small offshore FPSO - Google Patents
Device and method for recycling light hydrocarbon through small offshore FPSO Download PDFInfo
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- CN112111297A CN112111297A CN202011039801.0A CN202011039801A CN112111297A CN 112111297 A CN112111297 A CN 112111297A CN 202011039801 A CN202011039801 A CN 202011039801A CN 112111297 A CN112111297 A CN 112111297A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
- C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/12—Liquefied petroleum gas
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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention discloses a device and a method for recycling light hydrocarbon by a small offshore FPSO. The device comprises a compressor, a condensate separator, a deethanizer and an LPG tower; a gas phase outlet of the compressor inlet separator is communicated with an inlet of the condensate separator through a gas phase pipeline, a liquid phase outlet of the compressor inlet separator is communicated with an inlet of the condensate separator through a liquid phase pipeline, the gas phase pipeline is sequentially provided with a compressor and a compressor outlet cooler, and a condensate booster pump I is arranged on the liquid phase pipeline; the condensate separator is filled with oil-water separation filler; a water phase outlet of the condensate separator is connected with the water treatment system, a gas phase outlet of the condensate separator is connected with an FPSO fuel gas user, and a condensate outlet is connected with the deethanizer; the non-condensable gas at the tower top of the deethanizer enters an FPSO fuel gas user, and the tower bottom is connected with a deethanizer reboiler; the tower bottom of the deethanizer is connected with an LPG tower; the tower bottom of the LPG tower is connected with the LPG tower reboiler, and the tower top is provided with a cold reflux device. The equipment for recovering light hydrocarbon has compact structure and can better meet the production requirement of an offshore device.
Description
Technical Field
The invention relates to a device and a method for recycling light hydrocarbon by a small offshore FPSO (Floating production storage and offloading), belonging to the technical field of marine oil and gas development.
Background
China has proved that offshore oil and gas resources are rich, and offshore oil and gas gathering and transportation are various, wherein FPSO (Floating Production Storage Offloading System) is a core facility applied to a full-sea type development mode. In the existing offshore oil and gas field development project, because of the limitation of factors such as area, light hydrocarbon recovery processing procedures are mostly not arranged or are only arranged in a simpler light hydrocarbon recovery processing procedure.
At present, the recovery process of the light hydrocarbon of the associated gas of the land oilfield mainly focuses on the yield of the natural gas condensate, and the main process facilities comprise facilities such as an expansion compressor, a heavy contact tower, propane refrigeration and the like, so that the process flow is complex, the occupied area is large, the installation is difficult, and the applicability on the sea is poor. Therefore, the existing light hydrocarbon recovery process used on land can not be directly used in FPSO, and a new process suitable for marine environment needs to be researched.
The light hydrocarbon process needs to meet the following requirements: (1) the process is stable in operation and small in fluctuation; (2) the adaptability to different gas sources is strong; (3) heavy hydrocarbon is recycled as much as possible so as to improve the economy of the device; (4) the process is simple, the equipment is as few as possible, and the occupied area is small; (5) is safe and reliable.
Disclosure of Invention
The invention aims to provide a light hydrocarbon recovery device and a method which are suitable for marine environment, simple and have higher propane recovery rate.
The invention provides a small offshore FPSO light hydrocarbon recovery device, which comprises a compressor, a condensate separator, a deethanizer and an LPG tower;
a gas phase outlet of the compressor inlet separator is communicated with an inlet of the condensate separator through a gas phase pipeline, a liquid phase outlet of the compressor inlet separator is communicated with an inlet of the condensate separator through a liquid phase pipeline, the compressor and a compressor outlet cooler are sequentially arranged on the gas phase pipeline, and a condensate booster pump I is arranged on the liquid phase pipeline;
the condensate separator is filled with an oil-water separation filler; a water phase outlet of the condensate separator is connected with a water treatment system, a gas phase outlet of the condensate separator is connected with an FPSO fuel gas user, and a condensate outlet is connected with a deethanizer;
the non-condensable gas at the tower top of the deethanizer enters an FPSO fuel gas user, and the tower bottom of the deethanizer is connected with a reboiler;
the tower bottom of the deethanizer is connected with an LPG tower;
the tower bottom of the LPG tower is connected with the LPG tower reboiler, and the tower top is provided with a cold reflux device.
Specifically, the inlet of the compressor inlet separator is connected with a cooler in front of the inlet of the compressor inlet separator, so as to cool the associated gas.
Specifically, a condensate booster pump II is arranged on a pipeline connecting the condensate separator and the deethanizer so as to carry out booster conveying on the dehydrated condensate.
Specifically, the cold reflux device comprises an LPG tower condenser, an LPG tower reflux tank and an LPG tower reflux pump which are sequentially connected.
Specifically, an LPG emergency emptying pipeline is arranged at the top of the LPG tower, namely only C5+ components at the bottom of the LPG tower are recovered in a light hydrocarbon recovery process, the cold reflux flow of the LPG tower top is ensured, meanwhile, redundant tower top gas is emptied to a flare system through the emergency discharge pipeline, and in order to ensure the stability of the process, the emergency discharge flow is regulated and controlled by a liquid level signal of an LPG tower top reflux tank.
Further, the invention also provides a method for recovering light hydrocarbon by the offshore FPSO, which comprises the following steps:
1) inputting associated gas from a crude oil dehydration stabilization unit into the compressor inlet separator in an offshore FPSO light hydrocarbon recovery unit;
2) the gas phase separated by the compressor inlet separator is compressed and cooled in sequence and then enters the condensate separator, the liquid phase separated by the compressor inlet separator is pressurized and then enters the condensate separator, the gas phase enters an FPSO fuel gas user, and the water phase enters a water treatment system; the water content in the condensate is less than 50 ppmv;
3) conveying the condensate dehydrated by the condensate separator to the deethanizer, feeding the top noncondensable gas of the deethanizer into an FPSO fuel gas user, and returning the bottom product of the deethanizer to the bottom of the deethanizer after passing through a reboiler of the deethanizer in a gas phase manner;
the bottom stream of the deethanizer enters the middle part of the LPG tower by virtue of the self pressure;
4) and obtaining a collecting tower top product at the tower top of the LPG tower, and obtaining a collecting tower bottom product at the tower bottom of the LPG tower.
In the method, in the step 1), the associated gas is cooled to 35-45 ℃ before being input into the compressor inlet separator.
In the method, in the step 2), the gas phase separated by the compressor inlet separator is pressurized to 2400-2600 kPaA and then cooled to 35-45 ℃.
In the method, in the step 3), the operation pressure of the deethanizer is 2300-2500 kPaA;
the operation temperature of the deethanizer reboiler is 135-145 ℃.
In the method, in the step 4), the operation temperature of the LPG tower is 50-145 ℃.
The method comprises the steps of pressurizing and cooling the associated gas generated by the multistage separation of crude oil, and treating the condensate generated in the pressurizing and cooling process as a raw material; in order to improve the recovery rate of light hydrocarbon, a double-tower flow of a deethanizer and an LPG tower is adopted to produce qualified LPG and stable light oil, the qualified LPG is stored independently, and the stable light oil is mixed back into the qualified crude oil.
The pressurization pressure of associated gas is determined by combining the multistage separation operation pressure of crude oil and the selection type of a compressor, and in order to improve the yield of liquid products, the outlet pressure of the compressor is recommended to be properly improved to be at least 2.5 MPaA.
In order to simplify the process, the condensed liquid separator is provided with a condensed liquid dehydration function, so that the deethanizer is not provided with a dehydration tower tray, the tower is fed from the top and only has a stripping section.
In order to adapt to different component conditions, the tower pressure of the LPG tower is designed according to the high C3 component so as to adapt to the fluctuation of the components of the oilfield associated gas.
Because FPSO product exports and is influenced by the environment great, when because the outer defeated restriction of LPG product, the LPG storage tank can't continue to store because of full jar, and in order to guarantee oil field stable production under this operating mode, the top of LPG tower sets up emergent discharge flow, discharges the LPG that partly can't get into the storage tank to torch system.
Due to the adoption of the technical scheme, the invention has the following advantages:
1. the invention recovers the condensate generated in the pressurizing and cooling of the compressor, adopts the double-tower flow of the associated gas pressurizing, the deethanizing tower and the LPG tower, has the propane yield over 95 percent, increases the liquefied petroleum gas product, increases the crude oil yield and improves the project benefit.
2. The method has great adaptability to associated gas component changes by improving the design and the operating pressure of the LPG tower, and increases the stability of flow use and severe weather by arranging the LPG tower emergency discharge flow.
3. The equipment and the process for recovering the light hydrocarbon are simple, the equipment is less, the structure is compact, and the production requirements of offshore devices can be better met.
Drawings
FIG. 1 is a schematic diagram of an apparatus for light hydrocarbon recovery from an offshore FPSO according to the present invention.
The equipment and logistics names corresponding to the reference numbers in the figure are as follows:
the system comprises an associated gas 1, a cooler 2, a compressor inlet separator 3, a condensate booster pump I4, a compressor 5, a compressor outlet cooler 6, a condensate separator 7, a water phase separated by the condensate separator 8, a condensate booster pump II 9, a gas phase separated by the condensate separator 10, a deethanizer 11, a deethanizer 12, a deethanizer overhead noncondensable gas 13, a deethanizer reboiler 14, an LPG tower 15, an LPG tower condenser 16, an LPG tower reflux tank 17, an LPG tower reflux pump 18, an LPG tower reboiler 19, an LPG tower top product 20, an LPG tower bottom product 20 and an LPG tower excess tower top gas 21.
Detailed Description
The present invention will be further described with reference to the accompanying drawings, but the present invention is not limited to the following embodiments.
As shown in figure 1, the device for recovering light hydrocarbon by the small-scale offshore FPSO provided by the invention comprises a condensate separator 7, a deethanizer 11 and an LPG tower 14. The inlet of the compressor inlet separator 3 is connected with the cooler 2, the gas-phase outlet of the compressor inlet separator is communicated with the inlet of the condensate separator 7 through a gas-phase pipeline, the liquid-phase outlet of the compressor inlet separator is communicated with the inlet of the condensate separator 7 through a liquid-phase pipeline, the gas-phase pipeline is sequentially provided with a compressor 5 and a compressor outlet cooler 6, and the liquid-phase pipeline is provided with a condensate booster pump I4. The condensate separator 7 is filled with oil-water separation filler, a water phase 8 separated by the condensate separator at a water phase outlet of the condensate separator 7 enters a water treatment system, a gas phase 10 separated by the condensate separator at a gas phase outlet enters an FPSO fuel gas user, and condensate is conveyed to the top of a deethanizer 11 under pressure through a condensate increasing pump II 9 after being dehydrated. The top noncondensable gas 12 of the deethanizer 11 enters an FPSO fuel gas user, and the bottom of the deethanizer is connected with a reboiler 13. The tower bottom of the deethanizer 11 is connected with an LPG tower 14, the tower bottom of the LPG tower 14 is connected with an LPG tower reboiler 18, and the tower top is provided with a cold reflux device: the device comprises an LPG tower condenser 15, an LPG tower reflux tank 16 and an LPG tower reflux pump 17 which are connected in sequence. An LPG emergency emptying pipeline is arranged at the top of the LPG tower 14 and used for discharging surplus tower top gas 21 of the LPG tower under emergency working conditions.
The steps of recovering the light hydrocarbon in the associated gas by the device are as follows:
1) associated gas 1(150kPa, 66 ℃) from a crude oil dehydration stabilizing unit is cooled to 40 ℃ by a cooler 2, enters a compressor inlet separator 3, a separated gas phase enters a compressor 5 to be pressurized to 2500kPaA, and a liquid phase is pressurized by a condensate booster pump I4 and then is merged into an inlet pipeline of a condensate separator 7;
2) the material flow at the outlet of the compressor 5 is cooled to 40 ℃ by a cooler 6 and then enters a condensate separator 7, an oil-water separation filler (the water content in condensate is controlled to be less than 50ppm) is arranged in the condensate separator 7, the condensate is conveyed to the top of a deethanizer 11 under pressure by a condensate increasing pump II 9 after being dehydrated, a gas phase 10 separated by the condensate separator 7 enters an FPSO fuel gas user, and a separated water phase 8 enters a water treatment system;
3) the deethanizer 11 is a half-tower only provided with a stripping section, a deethanizer reboiler 13 is arranged at the bottom of the tower, noncondensable gas 12 at the top of the deethanizer is used for removing FPSO fuel gas, water in condensate is removed by the condensate-liquid separator 7, the deethanizer 11 is not provided with a drainage tray, the operating temperature of the deethanizer reboiler 13 is 142 ℃, and the operating pressure of the deethanizer 11 is 2.5 MPaA; the gas phase of the tower bottom product of the deethanizer 11 returns to the bottom of the deethanizer 11 after passing through the deethanizer reboiler 13;
4) the bottom material flow of the deethanizer 11 enters the middle part of an LPG tower 14 by self pressure, the LPG tower 14 is a whole tower, the top of the tower is provided with cold reflux, the bottom of the tower is provided with an LPG tower reboiler 18, the pressure control of the top of the tower adopts a hot bypass flow, the gas phase at the top of the LPG tower 14 enters a top reflux tank 16 after being cooled to 40 ℃ by a condenser 15, the operating temperature of the LPG tower reboiler 18 is 124 ℃, and the material flow is merged in front of a crude oil cooler of a crude oil processing system.
5) In order to ensure that LPG can not be exported for a long time under the severe weather condition, the normal production of an oil field is not influenced by the full LPG storage tank, an LPG emergency emptying pipeline is arranged at the top of the LPG tower 14, namely, only C5+ components at the bottom of the LPG tower 14 are recovered in a light hydrocarbon recovery process, the cold reflux flow at the top of the LPG tower 14 is ensured, meanwhile, redundant top gas 21 of the LPG tower under the emergency working condition is emptied to a torch system through the emergency unloading pipeline, and in order to ensure the stability of the process, the adjustment of the emergency unloading flow is controlled by a liquid level signal of the reflux tank at the top of the LPG tower 14.
Through simulation, the molar compositions of the inlet component of the compressor (material flow 1), the top product of the deethanizer (material flow 12), the top product of the LPG tower (material flow 19) and the bottom product of the LPG tower (material flow 20) are shown in Table 1, the overall propane yield of the process is 72%, and the propane yield of the double-tower light hydrocarbon recovery part is 95%.
Table 1 key stream molar composition for light hydrocarbon recovery process
| Logistics 1 | Stream 12 | Stream 19 | Stream 20 | |
| Temperature, C | 40.00 | 52.80 | 39.50 | 124.40 |
| Pressure, MPaA | 0.13 | 2.50 | 0.80 | 0.85 |
| Methane (mol%) | 14.22 | 37.02 | 0.00 | 0.00 |
| Ethane (mol%) | 5.99 | 25.88 | 2.24 | 0.00 |
| Propane (mol%) | 11.60 | 12.27 | 33.00 | 0.01 |
| Butane (mol%) | 19.87 | 9.06 | 62.75 | 4.99 |
| Nitrogen gas (mol%) | 0.56 | 0.71 | 0.00 | 0.00 |
| Carbon dioxide (mol%) | 2.72 | 10.24 | 0.00 | 0.00 |
Claims (10)
1. A small-sized offshore FPSO light hydrocarbon recovery device comprises a compressor, a condensate separator, a deethanizer and an LPG tower;
a gas phase outlet of the compressor inlet separator is communicated with an inlet of the condensate separator through a gas phase pipeline, a liquid phase outlet of the compressor inlet separator is communicated with an inlet of the condensate separator through a liquid phase pipeline, the compressor and a compressor outlet cooler are sequentially arranged on the gas phase pipeline, and a condensate booster pump I is arranged on the liquid phase pipeline;
the condensate separator is filled with an oil-water separation filler; a water phase outlet of the condensate separator is connected with a water treatment system, a gas phase outlet of the condensate separator is connected with an FPSO fuel gas user, and a condensate outlet is connected with a deethanizer;
the non-condensable gas at the tower top of the deethanizer enters an FPSO fuel gas user, and the tower bottom of the deethanizer is connected with a reboiler;
the tower bottom of the deethanizer is connected with an LPG tower;
the tower bottom of the LPG tower is connected with the LPG tower reboiler, and the tower top is provided with a cold reflux device.
2. The apparatus of claim 1, wherein: the inlet of the compressor inlet separator is connected with a cooler in front.
3. The apparatus of claim 1 or 2, wherein: and a condensate booster pump II is arranged on a pipeline connecting the condensate separator and the deethanizer.
4. The apparatus of any one of claims 1-3, wherein: the cold reflux device comprises an LPG tower condenser, an LPG tower reflux tank and an LPG tower reflux pump which are sequentially connected.
5. The apparatus of any one of claims 1-4, wherein: an LPG emergency emptying pipeline is arranged at the top of the LPG tower.
6. A method for recovering light hydrocarbon by an offshore FPSO comprises the following steps:
1) inputting associated gas from a crude oil dehydration stabilization unit into the compressor inlet separator in the apparatus of any of claims 1-5;
2) the gas phase separated by the compressor inlet separator is compressed and cooled in sequence and then enters the condensate separator, the liquid phase separated by the compressor inlet separator is pressurized and then enters the condensate separator, the gas phase enters an FPSO fuel gas user, and the water phase enters a water treatment system; the water content in the condensate is less than 50 ppmv;
3) conveying the condensate dehydrated by the condensate separator into the deethanizer, feeding the top noncondensable gas of the deethanizer into an FPSO fuel gas user, and feeding the bottom material flow of the deethanizer into the middle part of the LPG tower by means of the pressure of the bottom material flow;
4) and obtaining a collecting tower top product at the tower top of the LPG tower, and obtaining a collecting tower bottom product at the tower bottom of the LPG tower.
7. The method of claim 6, wherein: in the step 1), the associated gas is cooled to 35-45 ℃ before being input into the compressor inlet separator.
8. The method according to claim 6 or 7, characterized in that: in the step 2), the gas phase separated by the compressor inlet separator is pressurized to 2400-2600 kPaA and then cooled to 35-45 ℃.
9. The method according to any one of claims 6-8, wherein: in the step 3), the operation pressure of the deethanization is 2300-2500 kPaA;
the operation temperature of the deethanizer reboiler is 135-145 ℃.
10. The method according to any one of claims 6-9, wherein: in the step 4), the operation temperature of the LPG tower is 50-145 ℃.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011039801.0A CN112111297A (en) | 2020-09-28 | 2020-09-28 | Device and method for recycling light hydrocarbon through small offshore FPSO |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202011039801.0A CN112111297A (en) | 2020-09-28 | 2020-09-28 | Device and method for recycling light hydrocarbon through small offshore FPSO |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103822438A (en) * | 2012-11-16 | 2014-05-28 | 中国石油天然气股份有限公司 | Shallow-cooling light hydrocarbon recovery process method |
| CN107163975A (en) * | 2017-05-27 | 2017-09-15 | 中国石油集团工程设计有限责任公司 | The device and method that a kind of lighter hydrocarbons depth is reclaimed |
| CN110538476A (en) * | 2019-09-11 | 2019-12-06 | 杭州宏盛中弘新能源有限公司 | Low-temperature flash light hydrocarbon recovery system and method for oilfield associated gas |
-
2020
- 2020-09-28 CN CN202011039801.0A patent/CN112111297A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103822438A (en) * | 2012-11-16 | 2014-05-28 | 中国石油天然气股份有限公司 | Shallow-cooling light hydrocarbon recovery process method |
| CN107163975A (en) * | 2017-05-27 | 2017-09-15 | 中国石油集团工程设计有限责任公司 | The device and method that a kind of lighter hydrocarbons depth is reclaimed |
| CN110538476A (en) * | 2019-09-11 | 2019-12-06 | 杭州宏盛中弘新能源有限公司 | Low-temperature flash light hydrocarbon recovery system and method for oilfield associated gas |
Non-Patent Citations (1)
| Title |
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| 陈宾等: "海上油气田压缩机系统凝析液回收工艺", 《盐科学与化工》 * |
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