CN1782645A - Low temperature separating process for natural gas - Google Patents
Low temperature separating process for natural gas Download PDFInfo
- Publication number
- CN1782645A CN1782645A CN 200410096434 CN200410096434A CN1782645A CN 1782645 A CN1782645 A CN 1782645A CN 200410096434 CN200410096434 CN 200410096434 CN 200410096434 A CN200410096434 A CN 200410096434A CN 1782645 A CN1782645 A CN 1782645A
- Authority
- CN
- China
- Prior art keywords
- gas
- natural gas
- low temperature
- temperature
- throttling
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to low temperature natural gas separating process for treating natural gas produced in oil-gas field containing micro amount of condensate oil, and features that the technological process consists of three parts, including injecting alcohol, heating/pre-cooling and low temperature separating. The present invention has methanol injecting amount of 4.0-5.5 liters each kilo cubic meter of natural gas and low temperature separating temperature of -8~-15 deg C, and the separation process includes the first gas-liquid separation in a gravitational separator, the second ary filtering separation in a Pole pre-filter and the third agglomerating condensate oil and water in a Pole gas-liquid coalescer. The low temperature separated natural gas has 9.33 MPa lowered critical condensing pressure, 59.1 deg C lowered critical condensing temperature, reduced retrograde condensation area and obvious low temperature oil eliminating effect.
Description
Technical field
The present invention relates to a kind of little low temperature separating process for natural gas that contains the natural gas processing of condensate gas field production that is used for, specifically, is condensate removal dehydration process for purifying.
Background technology
When long celebrating 141 wellblocks, Shan, gas field, Yulin adopt normal temperature to separate (10～30 ℃ of separation temperatures), triethylene glycol dehydration purification process technique, can not effectively remove the condensate in the natural gas, natural gas is in the defeated process of collection and under the operating pressure and temperature conditions of foreign trade metering interface point, there is liquid hydrocarbon to separate out, not only influenced the conveying capacity of pipeline, bring many potential safety hazards also for overhaul of the equipments and pipe-line maintenance, also foreign trade metering handing-over has been produced adverse influence.According to stipulating in the national second category of commodities makings standard, under natural gas interface point pressure and temperature condition, should not have lime set, must adopt corresponding technology reaching the purpose of de-oiling and dehydration, therefore carried out the trial and the test of cryogenic separation de-oiling, dehydration in long celebrating gas field, Yulin.
1998, the low temperature dewatering test was carried out in long celebrating gas field at the Shan17Jing station, adopt throttling refrigeration, low temperature one-level separating technology, and the natural gas makings water dew point after the low temperature one-level is separated does not reach the requirement of second category of commodities makings, and test is not succeedd.
A kind of gas wave refrigeration dehydration skid-mounted device that is used for the natural gas cold condensation for removing water, by air wave refrigerating device, methyl alcohol mist jet pump or micro-throttling alchol injector, do-the moisture cool exchanger, equipment such as gas-liquid separator formed.The operation principle of capital equipment and design feature in the device make this device can realize not having electricity operation and deep dehydration, the gas dew point temperature is reduced to below-30 ℃ and is convenient to long-distance pipeline and carries.The air wave refrigerating device that this device adopts is the pressure work done with natural gas self, high velocity air is injected around the swivel nozzle of particular design in the equally distributed receiving tube, produce dilatational wave and make the gas cooling, can obtain-40 ~-10 ℃ low temperature, present stage, the gas wave refrigeration technology also was mainly used in gas dehydration, only be a spot of light hydrocarbon component of attached product, can not effectively remove the condensate in natural.The low temperature steel must be adopted in technology running temperature-20～-40 of existing gas wave refrigeration dewater unit ℃.
Summary of the invention
The objective of the invention is:
1. in order to remove the condensate in the natural gas, reduce the influence that condensate causes production.
2. after well head natural gas via low temperature separating process was handled, natural gas can reach the purpose of gas dehydration in de-oiling, so that outer gas transmission makings reaches second category of commodities gas makings standard (GB17820-1999).
3. innovation natural gas purification treatment process is simplified condensate removal, dehydration purification process technique flow process, reaches the purpose that reduces investment.
Technological process of the present invention:
This technological process is made up of three parts such as annotating pure unit, heating/precooling unit, cryogenic separation unit.
Annotate pure unit and comprise that well head is annotated in the pure and mild station and annotate alcohol, be mainly used to suppress the formation of hydrate.
Heating/precooling unit is the enter the station difference of pressure of gas according to individual well, utilizes heating furnace to heat, and the pressure＞14MPa that enters the station does not heat yet not precooling, the pressure≤14MPa that enters the station, and heat exchanger carries out precooling, and pressure pact≤14MPa generally enters the station.
The cryogenic separation unit is the core cell of low temperature separating process technology, comprises choke valve and three grades of gas-liquid separators.Choke valve is general Throttle needle valve, and the scene is a KL44Y-250DN50 type needle-valve; Primary separator is common horizontal type gas and liquid gravity separator, and the scene is made up of many PN6.8/DN600 metering separators and 1 PN6.8/DN1000 production separator; Secondary, three grades of separators are your gas-liquid separation device quite, i.e. quite your prefilter and quite your gas-liquid coalescer are your company's shaped article quite, gas field, Yulin use at present 700,000 side/skies and 1,000,000 sides/two kinds of models in sky are arranged.Apparatus casing is by quite that company production of Beijing, and the equipment filter core is the quite product of your company of the import U.S..
Complete technological process is: individual well comes gas earlier to inject methyl alcohol by annotating pure unit in air-flow, to prevent after heat exchanger or the throttling that hydrate generates in the cryogenic separation, annotates the alcohol amount and determines ten thousand side's gas at 40-55L/; Enter heating/precooling unit then, carry out adjustment through heating furnace or heat exchanger, if individual well comes insufficient pressure, be lower than 14Ma, advance throttling after the heat exchanger precooling, if hypertonia, for temperature after preventing throttling low excessively, be lower than-20 ℃, must advance the heating furnace heating, with cryogenic separation temperature requirement after the assurance throttling; Freeze through the choke valve throttling expansion again, make pressure by 7～25MPa throttling to 4.0-6.2MPa, make the individual well throttling after temperature be reduced to-8～-18 ℃, making many implications well mix the back natural gas temperature is-8～-15 ℃, reach the cryogenic separation operating temperature, enter the cryogenic separation unit; In the cryogenic separation unit, after natural gas via one-level gas-liquid gravity separator carries out gas-liquid separation, isolate a large amount of condensates, water and solid particle, enter secondary quite your prefilter filter to isolate most solid particle and a small amount of condensate and water, enter again three grades quite your gas-liquid coalescer coalesces go out condensate and water, export the qualified back of hydrocarbon dew point, water dew point after testing directly metering is outer and transport to main line and (satisfy national two class makings standards, water dew point≤-5 ℃ do not have liquid hydrocarbon under the pressure and temp condition of natural gas interface point).
In the present invention, used prefilter and your gas-liquid coalescer quite, the prefilter filtering accuracy can reach 0.3 μ m, remove efficient 99.98%, the gas-liquid coalescer can be removed the following drop of 0.01ppmw, even can reach 0.003ppmw, promptly removes particle diameter 0.1 μ m drop.Compare with the present invention, long in the past celebrating gas field carry out at Shan17Jing station main cause that the low temperature dewatering test do not achieve success be the back generation of natural gas via throttling expansion refrigeration mainly be the drop of sub-micro level particle diameter, and general gravity separator can not effectively separate the drop of sub-micro level particle diameter.
Compare with the gas wave refrigeration dewatering process, technology of the present invention belongs to shallow cold low temperature separating process, and the steel of using in the flow process, pipe fitting, valve etc. are the normal temperature steel.And main purpose of the present invention is water and the condensate that effectively removes in the natural gas.
The effect of invention
From Fig. 1, Fig. 2 as can be seen: unstripped gas and gas-liquid coalescer exported product gas all are in the retrograde condensation district in the phasor; 108.45 ℃ of unstripped gas cricondenbar 21.52MPa, cricondentherms, and 49.35 ℃ of gas-liquid coalescer exported product gas cricondenbar 12.19MPa, cricondentherm, promptly after cryogenic separation, the natural gas cricondenbar has reduced 9.33MPa, cricondentherm has reduced by 59.1 ℃, very intuitively from phasor find out that the retrograde condensation zone diminishes, illustrate that cryogenic separation de-oiling effect is obvious.
Description of drawings
Gas area, Fig. 1 south unstripped gas fluid phasor
Fig. 2 gas-liquid coalescer export gas fluid phasor
Fig. 3 gas-liquid separating technological process schematic diagram.
The specific embodiment
This low temperature separating process has all been adopted in long celebrating South Area, Oilfield Company second gas production factory Yulin since calendar year 2001 is dropped into exploitation, by to the end of the year in 2003, had 5 of low temperature gas gathering stations, builds production capacity 8.15 * 10
8m
3/ a.
Production instance:
Whole process of production contrast low temperature separating process flowchart text: it is 18.2MPa that elm 43-3 well individual well comes gas, tolerance 70,000 side/skies, and 8 ℃ of inlet temperatures, temperature is 24 ℃ before the individual well throttling after the heating furnace heating; Pressure is 4.68MPa after the throttling, and temperature is-18 ℃ after the throttling; Come gas to mix back gas separation temperature with other individual wells and be-13--15 ℃, gaseous mixture is earlier through gravity separator (existing equipment, specification PN6.8 DN1000 * 500,000 side/skies), through removing supersaturation free water and a part of solid impurity in the natural gas behind the gravity separator; Gas enters the secondary separation behind gravity separator, this equipment of filter plant prefilter (existing equipment Beijing quite your company produces) mainly acts on is that the protection next stage filters, separation equipment, removes granulometric impurity and the big drop (greater than 10um) of a part in the gas; Gaseous mixture enters three-stage filtration, separation equipment after prefilter, and gas-liquid coalescer (existing equipment, Beijing quite your company are produced) this equipment (13--15 ℃, pressure 4.68MPa) under the separation operating mode can be removed the drop of particle diameter 0.01um; The defeated outside at last water dew point of measuring can reach national two class makings standards (water dew point≤-5 ℃, do not have liquid hydrocarbon under the pressure and temp condition of natural gas interface point) fully.
Stop up for ordinary production prevents the gas gathering line hydrate, must annotate alcohol.Annotate pure technology and be divided into interior, the two kinds of pure modes of notes of well head of standing, under the above production status, well head was annotated pure 170L/ days, annotated pure 114L/ days in standing, and added up to 40.5L/ days/all places gas.
Claims (1)
1. low temperature separating process for natural gas is characterized in that: inject methyl alcohol earlier in individual well comes the air-flow of gas, the methyl alcohol injection rate is 40-55L/ ten thousand side's gas; Enter heating/precooling then, carry out adjustment through heating furnace or heat exchanger, individual well forces down in 14Ma, advances throttling after the heat exchanger precooling, and pressure is greater than or equal to 14Ma, and temperature is lower than-20 ℃ after the throttling, advances the heating furnace heating; Again through choke valve throttling expansion refrigeration, make pressure by 7～25MPa throttling to 4.0-6.2MPa, make the individual well throttling after temperature be reduced to-8～-18 ℃, making many implications well mix the back natural gas temperature is-8～-15 ℃; Enter cryogenic separation, after natural gas via one-level gas-liquid gravity separator carries out gas-liquid separation, isolate a large amount of condensates, water and solid particle, enter secondary quite your prefilter filter to isolate remaining solid particle and part condensate and water, enter again three grades quite your gas-liquid coalescer coalesces go out condensate and water.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410096434 CN1782645A (en) | 2004-12-01 | 2004-12-01 | Low temperature separating process for natural gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410096434 CN1782645A (en) | 2004-12-01 | 2004-12-01 | Low temperature separating process for natural gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1782645A true CN1782645A (en) | 2006-06-07 |
Family
ID=36773104
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200410096434 Pending CN1782645A (en) | 2004-12-01 | 2004-12-01 | Low temperature separating process for natural gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1782645A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102322568A (en) * | 2011-05-17 | 2012-01-18 | 西安长庆科技工程有限责任公司 | Natural gas and gas condensate metering and distribution method |
| CN110617049A (en) * | 2019-09-30 | 2019-12-27 | 中国石油集团川庆钻探工程有限公司 | A dehydration cooling system for well head natural gas |
-
2004
- 2004-12-01 CN CN 200410096434 patent/CN1782645A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102322568A (en) * | 2011-05-17 | 2012-01-18 | 西安长庆科技工程有限责任公司 | Natural gas and gas condensate metering and distribution method |
| CN102322568B (en) * | 2011-05-17 | 2013-04-10 | 西安长庆科技工程有限责任公司 | Natural gas and gas condensate metering and distribution method |
| CN110617049A (en) * | 2019-09-30 | 2019-12-27 | 中国石油集团川庆钻探工程有限公司 | A dehydration cooling system for well head natural gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108913252B (en) | Hydrocarbon injection dewaxing device and process suitable for dehydrating and dealkylating wax-containing natural gas | |
| US6085545A (en) | Liquid natural gas system with an integrated engine, compressor and expander assembly | |
| CN105038882A (en) | Comprehensive fine dewatering technique for recovering LNG/LPG/NGL (liquefied natural gas/liquefied petroleum gas/natural gas liquid) product from saturated hydrous petroleum associated gas | |
| CN112648536A (en) | Fluid infusion type oil-gas mixed transportation device | |
| CN1782645A (en) | Low temperature separating process for natural gas | |
| CN205011721U (en) | Smart dewatering system of synthesis of LNGLPGNGL product is retrieved to saturation wet oil associated gas | |
| CN1515651A (en) | Small type skid-mounted natural gas light hydrocarbon recovering method | |
| CN116481261A (en) | Method for recovering benzene-containing natural gas medium-pressure cryogenic light hydrocarbon | |
| CN214919173U (en) | Multiphase extraction system for in-situ thermal desorption repair device of polluted site | |
| CN203048901U (en) | Low-cost and low-energy natural gas recovering and processing device | |
| CN213177697U (en) | Short-flow natural gas gathering and transportation system | |
| CN207195147U (en) | Gas-pressed equipment | |
| CN204987651U (en) | Explosion -proof liquefying plant of making an uproar falls in sleeve pipe gas | |
| CN101100292A (en) | Composite film separation nitrogen-preparing system and method for well drilling technique | |
| CN212205328U (en) | Carbon dioxide-rich oil-gas well natural gas decarbonization and carbon dioxide recovery and liquefaction device | |
| CN210030602U (en) | Skid-mounted natural gas deoiling and dehydrating integrated device | |
| CN2666916Y (en) | Low differential pressure throttling natural gas condensate oil removing device | |
| CN203144363U (en) | System for recycling gas below standard in LNG (liquefied natural gas) production | |
| CN203248411U (en) | Three-section reverse-flow system used for anti-surge of supercharger | |
| CN114440549B (en) | Computer control method for natural gas deep-cooling denitrification process | |
| CN204958819U (en) | Liquefied gas recovery unit in intensive natural gas | |
| RU2285212C2 (en) | Method and device for liquefying natural gas | |
| CN205398565U (en) | Natural gas takes off hydrocarbon device | |
| CN109439375A (en) | A kind of method of heat exchange type purification and liquefaction coalbed or coal mine gas | |
| CN112524487B (en) | System and method for controlling accumulated liquid of large-caliber flash vapor pipeline of oil field |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |