CN201648315U - Skid-mounted natural gas condensate stabilizer - Google Patents
Skid-mounted natural gas condensate stabilizer Download PDFInfo
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- CN201648315U CN201648315U CN 201020302554 CN201020302554U CN201648315U CN 201648315 U CN201648315 U CN 201648315U CN 201020302554 CN201020302554 CN 201020302554 CN 201020302554 U CN201020302554 U CN 201020302554U CN 201648315 U CN201648315 U CN 201648315U
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Abstract
The utility model provides a skid-mounted natural gas condensate stabilizer, which belongs to a recovery plant of natural gas and casing-head gas. The utility model is characterized in that it comprises at least a first condensateoil heat exchanger, a second condensateoil heat exchanger, a condensateoil aftercooler, and a condensateoil stabilization tower. The first condensateoil heat exchanger is connected to a system condensateoil outlet through a pipeline valve gate, and the heat exchange outlet of the first condensateoil heat exchanger is communicated to the inlet of a condensate buffer tank through a pipeline valve gate. The inlet of a condensate buffer tank is communicated to the heat exchange inlet of the second condensateoil heat exchanger, and the heat exchange outlet of the second condensateoil heat exchanger is communicated to the inlet of the condensateoil stabilization tower. The skid-mounted natural gas condensate stabilizer has advantages of simplifying process, saving investment, reducing land occupation and operation cost, and eliminating safety potential of the storage and transportation of natural gas condensateoil.
Description
Technical field
The utility model belongs to recovery system in the Sweet natural gas in gas field and the associated gas, and particularly a kind of sledge dressization natural gas condensate stabilizing deyice is a kind of skid-mounted unit of byproduct condensate stabilization in the oil-gas field production process.
Background technology
At present, China Petroleum is paid attention to gradually reclaiming from the Sweet natural gas of gas condensate field and associated gas and is obtained lighter hydrocarbons-ethane, propane, butane and the carbon component more than five, is commonly called as condensate oil or natural gas liquids, lime set, lighter hydrocarbons (oil).Condensate oil is big with gas yield, light oil yield is high is characteristics.Oil-gas field separates in separator after condensate gas is determined ground, except obtaining a considerable amount of condensate oils, also isolates Sweet natural gas usually and delivers to source mill.
Adopt the method for low temperature separation process can obtain more condensate oil, condensate oil generally all contains the C of some amount
4, C
3, even C
2Etc. rudimentary hydro carbons, this rudimentary hydro carbons stores has problems such as serious potential safety hazard and environmental pollution, thereby also needs stabilizing treatment, removes wherein rudimentary hydro carbons to obtain stable condensate oil.Present stabilising method are employing separation methods, and condensate oil is delivered to fractionation plant, through three grades of separation, obtain stabilized condensate by stabilizer tower is stable at last, exist but have shortcomings such as flow process complexity, the big occupation of land of investment and working cost height.
Summary of the invention
The purpose of this utility model is to provide a kind of simplifies flow process, reduce investment outlay, reduce and take up an area of and the sledge dressization natural gas condensate stabilizing deyice of working cost, eliminates the potential safety hazard that the natural gas condensate storage is transported.
The purpose of this utility model is to realize like this, a kind of sledge dressization natural gas condensate stabilizing deyice, it is characterized in that: which comprises at least the first condensate oil interchanger, the second condensate oil interchanger, condensate oil aftercooler, condensate stabilization tower, the first condensate oil interchanger is by pipeline valve connected system condensate oil delivery port, and the heat exchange delivery port of the first condensate oil interchanger is communicated with lime set surge tank input aperture through pipeline valve; Lime set surge tank delivery port is communicated with the heat exchange input aperture of the second condensate oil interchanger; The heat exchange delivery port of the second condensate oil interchanger is communicated with condensate stabilization tower input aperture, and the upper end of condensate stabilization tower is connected with fuel gas system by pipeline valve; The lower end of condensate stabilization tower connects the second condensate oil interchanger and the first condensate oil interchanger by pipeline valve; The first condensate oil interchanger is connected with the storage of condensate oil storage tank through the condensate oil aftercooler by pipeline valve with the second condensate oil interchanger.
Described condensate stabilization tower is connected with high temperature heat conductive oil, low temperature thermal oil by pipeline valve.
Described lime set surge tank input aperture is connected the bypass duct valve with lime set surge tank delivery port.
Working process of the present utility model and advantage are: the condensate oil of producing device certainly be depressurized to behind the 600kPa with stabilized condensate heat exchange to 20～30 ℃ after enter lime set surge tank (sledge external equipment), isolate noncondensable gas.The sewage containing methanol that lime set surge tank (sledge external equipment) bottom liquid storage bag stockpiles enters Sewage treatment systems automatically by the profit liquidometer, and the isolated a small amount of gas of tank deck enters full factory fuel gas system after mixing by pressure controlled valve and stable overhead gas.Stabilized condensate is regulated back and stabilized condensate by level control valve and is entered stabilizer tower (4) after the heat exchange to 60 ℃ once more, is heated to 140 ℃ at the bottom of the tower, and pressure tower is controlled at 0.4～0.45MPa.Condensate oil at the bottom of the tower after stable is cooled to through the first condensate oil interchanger, the second condensate oil interchanger and condensate oil aftercooler and goes stabilized condensate tank stores (saturation vapour pressure of stabilized condensate during at 40 ℃ is less than 60kPa) after 40 ℃.Because being cooled to through the first condensate oil interchanger, the second condensate oil interchanger and condensate oil aftercooler, the condensate oil at the bottom of the tower after stable go stabilized condensate tank stores (saturation vapour pressure of stabilized condensate during at 40 ℃ is less than 60kPa) to simplify flow process after 40 ℃, therefore reduce investment outlay, the sledge dressization natural gas condensate stabilizing deyice of occupation of land and working cost, eliminate the potential safety hazard that the natural gas condensate storage is transported.
Description of drawings:
Below in conjunction with accompanying drawing the utility model is described further.
Fig. 1 the utility model example structure synoptic diagram.
Among the figure: 1, the first condensate oil interchanger; 2, the second condensate oil interchanger; 3, condensate oil aftercooler; 4, condensate stabilization tower; 5, fuel gas system; 6, lime set surge tank input aperture; 7, system's condensate oil delivery port; 8, lime set surge tank delivery port; 9, condensate oil storage tank storage; 10, low temperature thermal oil; 11, high temperature heat conductive oil.
Embodiment
As shown in Figure 1, a kind of sledge dressization natural gas condensate stabilizing deyice, comprise the first condensate oil interchanger 1, the second condensate oil interchanger 2, condensate oil aftercooler 3, condensate stabilization tower 4, the first condensate oil interchanger 1 is communicated with lime set surge tank input aperture 6 through pipeline valve by the heat exchange delivery port of pipeline valve connected system condensate oil delivery port 7, the first condensate oil interchanger 1; Lime set surge tank delivery port 8 is communicated with the heat exchange input aperture of the second condensate oil interchanger 2; The heat exchange delivery port of the second condensate oil interchanger 2 is communicated with condensate stabilization tower 4 input apertures, and the upper end of condensate stabilization tower 4 is connected with fuel gas system 5 by pipeline valve; The lower end of condensate stabilization tower 4 connects the second condensate oil interchanger 2 and the first condensate oil interchanger 1 by pipeline valve; The first condensate oil interchanger 1 is connected with condensate oil storage tank storage 9 through condensate oil aftercooler 3 by pipeline valve with the second condensate oil interchanger 2.Condensate stabilization tower 4 is connected with high temperature heat conductive oil 11, low temperature thermal oil 10 by pipeline valve.Be connected the bypass duct valve in lime set surge tank input aperture 6 with lime set surge tank delivery port 8.
During work, system's condensate oil delivery port 7 enters lime set surge tank input aperture 6 in the first condensate oil interchanger 1 with behind stabilized condensate heat exchange to 20～30 ℃ after being depressurized to 600kPa, isolate noncondensable gas.The sewage containing methanol that lime set surge tank (sledge external equipment) bottom liquid storage bag stockpiles enters Sewage treatment systems automatically by the profit liquidometer, and the isolated a small amount of gas of tank deck enters full factory fuel gas system 5 after mixing by pressure controlled valve and stable overhead gas.Stabilized condensate by level control valve regulate the back in the second condensate oil interchanger 2 and stabilized condensate enter condensate stabilization tower 4 after the heat exchange to 60 ℃ once more, be connected with high temperature heat conductive oil 11 through pipeline valve at the bottom of the tower, be heated to 140 ℃ by high temperature heat conductive oil 11, pressure tower is controlled at 0.4～0.45MPa.Condensate oil at the bottom of the tower after stable is cooled to through the first condensate oil interchanger 1, the second condensate oil interchanger 2 and condensate oil aftercooler 3 and goes condensate oil storage tank stores (saturation vapour pressure of stabilized condensate during at 40 ℃ is less than 60kPa) after 40 ℃.Consider that the interior no thermal source of device can be used when device had just been driven, (sledge external equipment) is provided with heating system in the lime set surge tank, and lime set is heated to 20～30 ℃.
Claims (3)
1. sledge dressization natural gas condensate stabilizing deyice, it is characterized in that: which comprises at least the first condensate oil interchanger (1), the second condensate oil interchanger (2), condensate oil aftercooler (3), condensate stabilization tower (4), the first condensate oil interchanger (1) is by pipeline valve connected system condensate oil delivery port (7), and the heat exchange delivery port of the first condensate oil interchanger (1) is communicated with lime set surge tank input aperture (6) through pipeline valve; Lime set surge tank delivery port (8) is communicated with the heat exchange input aperture of the second condensate oil interchanger (2); The heat exchange delivery port of the second condensate oil interchanger (2) is communicated with condensate stabilization tower (4) input aperture, and the upper end of condensate stabilization tower (4) is connected with fuel gas system (5) by pipeline valve; The lower end of condensate stabilization tower (4) connects the second condensate oil interchanger (2) and the first condensate oil interchanger (1) by pipeline valve; The first condensate oil interchanger (1) is connected with condensate oil storage tank storage (9) through condensate oil aftercooler (3) by pipeline valve with the second condensate oil interchanger (2).
2. a kind of sledge dressization natural gas condensate stabilizing deyice according to claim 1, it is characterized in that: described condensate stabilization tower (4) is connected with high temperature heat conductive oil (11), low temperature thermal oil (10) by pipeline valve.
3. a kind of sledge dressization natural gas condensate stabilizing deyice according to claim 1, it is characterized in that: described lime set surge tank input aperture (6) is connected the bypass duct valve with lime set surge tank delivery port (8).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201020302554 CN201648315U (en) | 2010-02-08 | 2010-02-08 | Skid-mounted natural gas condensate stabilizer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201020302554 CN201648315U (en) | 2010-02-08 | 2010-02-08 | Skid-mounted natural gas condensate stabilizer |
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| CN201648315U true CN201648315U (en) | 2010-11-24 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN 201020302554 Expired - Fee Related CN201648315U (en) | 2010-02-08 | 2010-02-08 | Skid-mounted natural gas condensate stabilizer |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102288007A (en) * | 2011-07-20 | 2011-12-21 | 西安长庆科技工程有限责任公司 | Natural-gas condensed-liquid recovery device and method using mixed light hydrocarbon as refrigerant |
| CN104632137A (en) * | 2013-11-08 | 2015-05-20 | 中国石油天然气股份有限公司 | Self-pressure remote-control gas condensate closed recycling process method and device |
| CN105969439A (en) * | 2016-06-07 | 2016-09-28 | 西安长庆科技工程有限责任公司 | Low-temperature condensate treatment process and device for natural gas treatment plant deoiling and dewatering device |
| CN113700456A (en) * | 2021-08-26 | 2021-11-26 | 北京大漠石油工程技术有限公司 | Natural gas modularization pilot production device |
-
2010
- 2010-02-08 CN CN 201020302554 patent/CN201648315U/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102288007A (en) * | 2011-07-20 | 2011-12-21 | 西安长庆科技工程有限责任公司 | Natural-gas condensed-liquid recovery device and method using mixed light hydrocarbon as refrigerant |
| CN102288007B (en) * | 2011-07-20 | 2013-06-19 | 西安长庆科技工程有限责任公司 | Natural-gas condensed-liquid recovery device and method using mixed light hydrocarbon as refrigerant |
| CN104632137A (en) * | 2013-11-08 | 2015-05-20 | 中国石油天然气股份有限公司 | Self-pressure remote-control gas condensate closed recycling process method and device |
| CN105969439A (en) * | 2016-06-07 | 2016-09-28 | 西安长庆科技工程有限责任公司 | Low-temperature condensate treatment process and device for natural gas treatment plant deoiling and dewatering device |
| CN105969439B (en) * | 2016-06-07 | 2019-06-04 | 西安长庆科技工程有限责任公司 | A kind of natural gas processing plant's deoiling, dewatering device low temperature lime set treatment process and device |
| CN113700456A (en) * | 2021-08-26 | 2021-11-26 | 北京大漠石油工程技术有限公司 | Natural gas modularization pilot production device |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20101124 Termination date: 20170208 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |