CN210030602U - Skid-mounted natural gas deoiling and dehydrating integrated device - Google Patents
Skid-mounted natural gas deoiling and dehydrating integrated device Download PDFInfo
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- CN210030602U CN210030602U CN201920059688.9U CN201920059688U CN210030602U CN 210030602 U CN210030602 U CN 210030602U CN 201920059688 U CN201920059688 U CN 201920059688U CN 210030602 U CN210030602 U CN 210030602U
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Abstract
The utility model provides a based on skid-mounted formula natural gas deoiling dehydration integration device, including filtering separator, winding pipe heat exchanger, low temperature three-phase separator, flash distillation branch fluid reservoir, notes mellow wine system, unloading system, defeated system outward, the blowdown system, go fuel gas system and natural gas system of coming, filtering separator import and natural gas system of coming be connected, natural gas system of coming be connected with unloading system and defeated system outward respectively; an outlet at the upper end of the filtering separator is connected with an inlet at the upper part of the wound tube type heat exchanger, and an inlet at the upper part of the wound tube type heat exchanger is also connected with an alcohol injection system; the lower outlet of the filtering separator is connected with a sewage ball valve arranged on a sewage system; the outlet at the lower part of the coiled heat exchanger is connected with the inlet at the upper end of the low-temperature three-phase separator, and the device enables the natural gas to generate a small temperature drop through small pressure difference throttling, so that the feed gas generates a large enough temperature drop through heat exchange under the small cold end temperature difference, and the requirements of natural gas low-temperature deoiling and dehydration are met.
Description
Technical Field
The utility model relates to a skid-mounted formula natural gas deoiling dehydration integration device, specifically speaking are applied to the integration device of ancient natural gas (the non-sulfur-containing natural gas) station on gas field, adopt "little pressure differential throttling refrigeration, large tracts of land heat transfer low temperature separation" technology, condensate oil and saturated water in the desorption natural gas reach national standard "natural gas" GB17820-2012 two kinds of gas matter index.
Background
The natural gas in the Changqing gas field is divided into two types of ancient natural gas and ancient natural gas according to different properties. Wherein the ancient natural gas contains a certain amount of condensate oil and water, and does not contain H2S and CO2Mainly distributed in the gas fields of Su Li Ge gas field, Yulin gas field and Shenmu, Zizhou, etc., and the centralized construction of natural gas treatment plant and propane refrigeration low-temperature condensation deoiling and dewatering process are adopted at present; the ancient natural gas is basically free of condensate oil and contains a certain amount of H2S and CO2Mainly distributed in the Jing Ke gas field and Su Li Ge gas field, and the current technology adopts the centralized construction of natural gas purification plants, alcohol amine method desulfurization and decarbonization and triethylene glycol dehydration.
Along with the extension of gas field development time, ancient gas reservoir in ancient gas reservoir region begins to develop gradually under Jingbian gas field etc. at present, as ancient gas reservoir's remedy degressive productivity down, because ancient gas reservoir well position is distributed very dispersedly year by year on this part, ancient system does not fit actual conditions on the overall construction, if directly get into ancient system down, then can produce great influence to the operation of ancient natural gas pipeline and natural gas purification plant down, saturated water gets into the gas collection pipeline, make the pipeline become the moisture environment by the dry gas environment, arouse the H of pipeline easily2S is corroded, and the natural gas containing more condensate oil easily causes MDEA solution foaming, so a skid-mounted natural gas deoiling and dehydrating integrated device needs to be independently built, and the treated natural gas is connected into a lower ancient purified gas export system.
SUMMERY OF THE UTILITY MODEL
In order to overcome the defects that the well positions of the ancient gas reservoir are distributed in a dispersed manner in years and the ancient system is not fit for the actual situation in the whole construction, if the ancient system is directly entered, the ancient gas reservoir can generate larger shadow on the operation of the ancient natural gas pipeline and the natural gas purification plantSaturated water enters the gas collecting pipeline to change the pipeline from a dry gas environment to a wet gas environment, which easily causes H of the pipeline2S corrodes, and the natural gas that contains more condensate leads to the problem of MDEA solution foaming easily, the utility model provides a skid-mounted formula natural gas deoiling dehydration integration device, the utility model discloses ancient natural gas (non-sulfur-containing natural gas) station natural gas' S to the development of Changqing Jingbian gas field gas matter characteristics (contain condensate a little, C3 +The content is usually 1-2%, and the product contains saturated water and no H2S and CO2) The natural gas deoiling and dehydrating integrated device adopts a process of small-pressure-difference throttling refrigeration and large-area heat exchange low-temperature separation to remove condensate oil and saturated water in the natural gas, and reaches the gas quality indexes of GB17820-2012 in the national standard.
The utility model adopts the technical proposal that:
an integrated device based on skid-mounted natural gas deoiling and dehydrating comprises a filtering separator, a coiled heat exchanger, a low-temperature three-phase separator, a flash evaporation liquid separation tank, an alcohol injection system, a venting system, an output system, a blowdown system, a fuel gas removing system and a natural gas incoming system, wherein an inlet of the filtering separator is connected with the natural gas incoming system, and the natural gas incoming system is respectively connected with the venting system and the output system;
an outlet at the upper end of the filtering separator is connected with an inlet at the upper part of the wound tube type heat exchanger, and an inlet at the upper part of the wound tube type heat exchanger is also connected with an alcohol injection system; the lower outlet of the filtering separator is connected with a sewage ball valve arranged on a sewage system;
an outlet at the lower part of the coiled heat exchanger is connected with an inlet at the upper end of the low-temperature three-phase separator, an outlet at the upper end of the coiled heat exchanger is connected with an external conveying system, and a sewage discharge outlet at the upper end of the coiled heat exchanger is connected with a sewage discharge ball valve arranged on a sewage discharge system;
a natural gas outlet, an alcohol-containing sewage outlet and a condensate-containing outlet of the low-temperature three-phase separator are respectively connected with an inlet at the lower end of the coiled tube heat exchanger; an outlet at the upper end of the low-temperature three-phase separator is connected with an emptying system;
the inlet of the flash evaporation liquid separator is connected with the liquid outlet of the coiled tube heat exchanger; the lower outlet of the flash separator is connected with a blowdown ball valve of a blowdown system, and the upper outlet of the flash separator is respectively connected with a fuel gas removing system and an emptying system.
The inlet of the filtering separator is connected with a natural gas inlet system through a pipeline, and an air inlet switch ball valve is arranged on the pipeline; a ball valve I is arranged between the natural gas incoming system and the external transportation system; the natural gas incoming system is connected with the emptying system through a pipeline, an emptying safety valve is arranged on the pipeline, and the air inlet switch ball valve is connected with the emptying safety valve in parallel; and a first emptying ball valve and a second emptying ball valve are respectively arranged at two ends of the emptying safety valve.
An alcohol injection atomizer, a first temperature transmitter and a first thermometer are sequentially arranged between an upper outlet of the filtering separator and an upper inlet of the coiled tube heat exchanger; the device comprises an alcohol injection atomizer, an alcohol injection system, a filter, a first check valve, a first sealed sampling stop valve and a filter, wherein the first check valve, the first sealed sampling stop valve and the filter are sequentially arranged between the alcohol injection atomizer and the alcohol injection system, the first filter end is provided with a first alcohol injection control valve and a second alcohol injection control valve, and the first sealed sampling stop valve is provided with a first pressure gauge.
A second sealed sampling stop valve is arranged at the upper part of the filtering separator, and a second pressure gauge is arranged on the second sealed sampling stop valve; the lower part of the filtering separator is provided with a liquid level meter I and a liquid level meter II, an outlet at the lower part of the filtering separator is connected with a sewage system through two parallel pipelines, one pipeline is provided with a liquid discharge electric ball valve, a low-point liquid discharge valve, a dynamic regulating valve and a ball valve II, and the other pipeline is provided with a ball valve III and a throttle valve I.
A ball valve IV is arranged between the outlet at the upper end of the coiled tube heat exchanger and the output system; a second temperature transmitter and a second temperature gauge are arranged between the outlet at the lower part of the coiled heat exchanger and the inlet of the low-temperature three-phase separator; and a ball valve V is arranged between the coiled heat exchanger and the coiled heat exchanger, a ball valve VI is arranged between the coiled heat exchanger and the sewage system, and the ball valve V and the ball valve VI are arranged in parallel.
A three-phase separation emptying safety valve is arranged between an outlet at the upper end of the low-temperature three-phase separator and an emptying system, and a three-phase separation emptying ball valve I and a three-phase separation emptying ball valve II are respectively arranged at two ends of the three-phase separation emptying safety valve; one end of the low-temperature three-phase separator is provided with a first three-phase separation liquid level meter, and the middle part of the low-temperature three-phase separator is provided with a second three-phase separation liquid level meter; a three-phase separation temperature transmitter is arranged in the middle of the upper end of the low-temperature three-phase separator; and a first three-phase separation sealing sampling stop valve is arranged on one side of the three-phase separation temperature transmitter, and a first three-phase separation pressure gauge is arranged on the first three-phase separation sealing sampling stop valve.
A three-phase separation sealing sampling stop valve II, a three-phase separation sealing sampling stop valve III and a three-phase separation sealing sampling stop valve IV are sequentially arranged between the natural gas outlet of the low-temperature three-phase separator and the inlet at the lower end of the coiled heat exchanger, and a three-phase separation pressure gauge II, a three-phase separation pressure gauge III and a three-phase separation pressure gauge IV are respectively arranged on the three-phase separation sealing sampling stop valve II, the three-phase separation sealing sampling stop valve III and the three-phase separation sealing sampling stop valve IV; the three-phase separation sealing sampling stop valve II and the three-phase separation sealing sampling stop valve III are connected through three parallel pipelines, a first three-phase separation ball valve I, a first three-phase separation low-point liquid discharge valve, a first three-phase separation electric regulating valve and a second three-phase separation ball valve are arranged on the first pipeline, a first three-phase separation throttle valve is arranged on the second pipeline, and a first three-phase separation gate valve and a second three-phase separation gate valve are arranged on the third pipeline; a three-phase separation electric regulating valve II and a three-phase separation throttling valve II are arranged between an alcohol-containing sewage outlet of the low-temperature three-phase separator and an inlet at the lower end of the coiled pipe type heat exchanger, the three-phase separation electric regulating valve II and the three-phase separation throttling valve II are arranged in parallel, a three-phase separation ball valve III and a three-phase separation ball valve IV are respectively arranged at two ends of the three-phase separation electric regulating valve II, and a three-phase separation low-point liquid discharge valve II is arranged between the three-phase separation ball valve III and the three-; a three-phase separation electric regulating valve III and a three-phase separation throttling valve III are arranged between a condensate oil containing outlet of the low-temperature three-phase separator and a lower end inlet of the coiled heat exchanger, the three-phase separation electric regulating valve III and the three-phase separation throttling valve III are arranged in parallel, two ends of the three-phase separation electric regulating valve III are respectively provided with a three-phase separation ball valve V and a three-phase separation ball valve VI, and a three-phase separation low-point liquid discharge valve III is arranged between the three-phase separation ball valve V and the three-phase separation electric regulating valve III; the three-phase separation electric regulating valve III is electrically connected with the three-phase separation liquid level meter I of the low-temperature three-phase separator, and the three-phase separation electric regulating valve II is electrically connected with the three-phase separation liquid level meter II of the low-temperature three-phase separator.
The flash evaporation liquid separation tank is provided with a flash evaporation liquid level meter I and a flash evaporation liquid level meter II on two sides, the flash evaporation liquid separation tank is also provided with a flash evaporation temperature transmitter, a flash evaporation thermometer, a flash evaporation sealing sampling stop valve II and a flash evaporation sealing sampling stop valve I, the flash evaporation temperature transmitter is positioned above the flash evaporation liquid level meter I, the flash evaporation thermometer is positioned above the flash evaporation liquid level meter II, the flash evaporation sealing sampling stop valve I and the flash evaporation sealing sampling stop valve II are both positioned above the flash evaporation thermometer, and the flash evaporation sealing sampling stop valve I is provided with a flash evaporation pressure gauge I; a flash pressure gauge II is arranged on the flash sealing sampling stop valve II; a flash evaporation emptying safety valve is arranged between the upper outlet of the flash evaporation liquid separator and the emptying system, and a flash evaporation emptying ball valve I and a flash evaporation emptying ball valve II are respectively arranged at two ends of the flash evaporation emptying safety valve; a first flash electric regulation valve and a first flash electric throttle valve are arranged between the lower end outlet of the flash liquid separator and a blowdown ball valve of a blowdown system in parallel, a first flash ball valve and a second flash ball valve are respectively arranged at two ends of the first flash electric regulation valve, and a first flash low-point liquid discharge valve is arranged between the first flash ball valve and the first flash electric regulation valve; the first flash evaporation electric regulation device is electrically connected with the second flash evaporation liquid level meter; a flash evaporation electric regulating valve II and a flash evaporation electric throttling valve I are arranged between the outlet at the upper end of the flash evaporation liquid separation tank and the fuel gas removing system in parallel, a flash evaporation ball valve V and a flash evaporation ball valve VI are respectively arranged at two ends of the flash evaporation electric regulating valve II, and a flash evaporation low-point liquid discharge valve II is arranged between the flash evaporation ball valve V and the flash evaporation electric regulating valve II; the flash evaporation electric regulation II and the flash evaporation electric throttling valve I are connected in parallel and then are connected with a fuel gas removing system through a flash evaporation ball valve III, and the flash evaporation electric regulation II and the flash evaporation electric throttling valve I are connected in parallel and then are connected with an emptying system through a flash evaporation ball valve IV; and the second flash evaporation electric regulation unit is electrically connected with a second flash evaporation pressure gauge on the flash evaporation liquid separation tank.
The low-temperature three-phase separator is a horizontal low-temperature three-phase separator, and the flash evaporation liquid separation tank is a vertical flash evaporation liquid separation tank.
The utility model has the advantages that:
the device provided by the utility model adopt the deoiling dehydration technology and the device of "little pressure differential throttle refrigeration, large tracts of land heat transfer low temperature separation", be applicable to condensate oil and saturated water among the middle-size and small-size gas collecting station desorption natural gas, reach national standard "natural gas" GB17820-2012 second class gas matter index.
The utility model provides a little pressure differential throttling of device accessible (0.6-0.8 MPa) makes the natural gas produce a little temperature drop to this temperature drop selects enough big heat exchanger area as the heat exchanger cold junction difference in temperature, makes the feed gas produce enough big temperature drop (45 ~ 35 ℃) through the heat transfer under this little cold junction difference in temperature, in order to satisfy the requirement of natural gas low temperature deoiling dehydration.
The following will be further described with reference to the accompanying drawings.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Fig. 2 is a schematic diagram of the system connection of the present invention.
In the figures, the reference numbers are: 1. a filtration separator; 101. an air inlet switch ball valve; 102. a first emptying ball valve; 103. an air relief valve; 104. a second emptying ball valve; 105. sealing the sampling stop valve II; 106. a second pressure gauge; 107. a first temperature transmitter; 108. a first thermometer; 109. a first alcohol injection control valve; 110. a filter; 111. a second alcohol injection control valve; 112. sealing the sampling stop valve I; 113. a first pressure gauge; 114. a first check valve; 115. an alcohol injection atomizer; 116. a first liquid level meter; 117. a second liquid level meter; 118. draining the liquid electric ball; a low point drain valve 119; 120. an electric control valve; 121. a ball valve II; 122. a ball valve III; 123. a first throttling valve; 2. a coiled heat exchanger; 201. a second temperature transmitter; 202. a second thermometer; 203. a ball valve IV; 204. a ball valve V; 205. a ball valve six; 3. a cryogenic three-phase separator; 301. a three-phase separation sealing sampling stop valve I; 302. a three-phase separation pressure gauge I; 303. a three-phase separation temperature transmitter; 304. a second three-phase separation liquid level meter; 305. a second three-phase separation sealing sampling stop valve; 306. a second three-phase separation pressure gauge; 307. a first three-phase separation gate valve; 308. a three-phase separation ball valve I; 309. a first three-phase separation low-point liquid discharge valve; 310. a three-phase separation electric regulating valve I; 311. a three-phase separation ball valve II; 312. a three-phase separation throttle valve I; 313. a second three-phase separation gate valve; 314. a three-phase separation sealing sampling stop valve III; 315. separating the three phases to obtain a third pressure gauge; 316. a three-phase separation sealing sampling stop valve IV; 317. a three-phase separation pressure gauge IV; 318. a three-phase separation ball valve III; 319. a three-phase separation low-point liquid discharge valve II; 320. a second three-phase separation electric regulating valve; 321. a three-phase separation ball valve IV; 322. a three-phase separation throttle valve II; 323. a three-phase separation ball valve V; 324. a three-phase separation low-point liquid discharge valve III; 325. a three-phase separation electric regulating valve III; 326. a three-phase separation ball valve six; 327. a three-phase separation throttle valve III; 328. a first three-phase separation liquid level meter; 329. a first three-phase separation emptying ball valve; 330. a three-phase separation emptying safety valve; 331. a three-phase separation emptying ball valve II; 4. a flash evaporation liquid separation tank; 401. a flash evaporation temperature transmitter; 402. a first flash evaporation liquid level meter; 403. a second flash evaporation liquid level meter; 404. a flash thermometer; 405. a flash evaporation sealing sampling stop valve I; 406. a first flash evaporation pressure gauge; 407. a second flash sealed sampling stop valve; 408. a second flash evaporation pressure gauge; 409. a flash evaporation emptying ball valve I; 410. a flash evaporation relief valve; 411. a second flash evaporation emptying ball valve; 412. a flash evaporation ball valve V; 413. a second flash evaporation low-point liquid discharge valve; 414. performing flash evaporation electric regulation; 415. a flash evaporation ball valve six; 416. a flash evaporation electric throttle valve I; 417. a flash evaporation ball valve III; 418. a flash evaporation ball valve IV; 419. a first flash evaporation ball valve; 420. a first flash evaporation low-point liquid discharge valve; 421. performing electric flash regulation; 422. a second flash evaporation ball valve; 423. a flash evaporation electric throttle valve I; 424. a blowdown ball valve; 5. an alcohol injection system; 6. an emptying system; 7. an export system; 8. a blowdown system; 9. a de-fuel gas system; 10. natural gas comes the gas system.
Detailed Description
Example 1:
in order to overcome the defect that the well positions of the ancient gas reservoir are distributed very dispersedly in years and the whole ancient system is not in accordance with the actual situation if the ancient system is directly put intoAncient system, then can produce great influence to the operation of ancient natural gas pipeline and natural gas purification plant down, saturated water gets into the gas collecting pipe way, makes the pipeline become the moisture environment by the dry gas environment, arouses the H of pipeline easily2S corrodes, and the natural gas that contains more condensate leads to the problem of MDEA solution foaming easily, the utility model provides a skid-mounted formula natural gas deoiling dehydration integration device as shown in fig. 1 and 2, the utility model discloses ancient natural gas (the non-sulfur natural gas) station natural gas' S to the development of Changqing Jing border gas field gas matter characteristics (contain condensate a little, C natural gas) station natural gas3 +The content is usually 1-2%, and the product contains saturated water and no H2S and CO2) The natural gas deoiling and dehydrating integrated device adopts a process of small-pressure-difference throttling refrigeration and large-area heat exchange low-temperature separation to remove condensate oil and saturated water in the natural gas, and reaches the gas quality indexes of GB17820-2012 in the national standard.
An integrated device based on skid-mounted natural gas deoiling and dewatering comprises a filtering separator 1, a coiled heat exchanger 2, a low-temperature three-phase separator 3, a flash evaporation liquid separation tank 4, an alcohol injection system 5, a venting system 6, an external transportation system 7, a pollution discharge system 8, a fuel gas removal system 9 and a natural gas incoming system 10, wherein an inlet of the filtering separator 1 is connected with the natural gas incoming system 10, and the natural gas incoming system 10 is respectively connected with the venting system 6 and the external transportation system 7;
an outlet at the upper end of the filtering separator 1 is connected with an inlet at the upper part of the wound tube type heat exchanger 2, and an inlet at the upper part of the wound tube type heat exchanger 2 is also connected with an alcohol injection system 5; the lower outlet of the filtering separator 1 is connected with a blowdown ball valve 424 arranged on a blowdown system 8;
an outlet at the lower part of the coiled heat exchanger 2 is connected with an inlet at the upper end of the low-temperature three-phase separator 3, an outlet at the upper end of the coiled heat exchanger 2 is connected with an output system 7, and a blowdown outlet at the upper end of the coiled heat exchanger 2 is connected with a blowdown ball valve 424 arranged on a blowdown system 8;
a natural gas outlet, an alcohol-containing sewage outlet and a condensate-containing outlet of the low-temperature three-phase separator 3 are respectively connected with an inlet at the lower end of the coiled tube heat exchanger 2; the upper end outlet of the low-temperature three-phase separator 3 is connected with an emptying system 6;
an inlet of the flash evaporation liquid separator 4 is connected with a liquid outlet of the wound pipe type heat exchanger 2; the lower outlet of the flash separator 4 is connected with a blowdown ball valve 424 of a blowdown system 8, and the upper outlet of the flash separator 4 is respectively connected with a fuel gas removing system 9 and a blowdown system 6.
The utility model discloses design pressure is 6.3MPa, also can set up corresponding pressure system grade according to the actual operating pressure in different stations.
The utility model discloses in, wet natural gas comes gas system 10 to get into filtering separator 1 through the natural gas, filtering separator 1 can detach the solid particle diameter in the natural gas and be less than or equal to 10 mu m, separation efficiency > 99.9%, filtering separator 1 import is equipped with safe unloading system 6, can realize the automatic safety when coming the atmospheric pressure and surpassing the setting value and release, filtering separator 1 is equipped with level gauge one 116 and level gauge two 117, both all have the liquid level and show on the spot and the teletransmission function, be the alternative relation among the concrete implementation, as long as one of them shows at first and reach low liquid level or high liquid level promptly, the system will carry out corresponding warning. And the remote liquid level is interlocked with the sewage discharge valve, so that the liquid discharge electric ball valve can be closed urgently at a low liquid level, and liquid discharge is controlled through the electric regulating valve during normal liquid discharge. After removing solid particles in the natural gas, the gas enters a winding pipe type heat exchanger 2 for heat exchange, the temperature of the natural gas discharged from the winding pipe type heat exchanger 2 is reduced to-15 to-5 ℃, then the natural gas enters a low-temperature three-phase separator 3 for further oil-gas-water separation, liquid discharge control of alcohol-containing sewage and condensate of the low-temperature three-phase separator 3 is realized through an electric regulating valve, the regulating valve is regulated to be linked with a remote liquid level system of the alcohol-containing sewage and the condensate of the low-temperature three-phase separator 3, the cold energy of the low-temperature alcohol-containing sewage and the condensate is fully utilized, and the alcohol-containing sewage is reheated by the winding pipe type heat exchanger and then is sent to a sewage tank of a gas collecting. A J-T valve pressure regulating system is arranged at an outlet of the low-temperature three-phase separator 3, the J-T valve pressure regulating system at least comprises a three-phase separation throttle valve I312, the temperature of the natural gas is reduced to-19 to-9 ℃ through the pressure loss of the natural gas of 0.6 to 0.8MPa, the cooled natural gas enters the winding pipe type heat exchanger 2, and the temperature of the fed natural gas is reduced by fully utilizing the cold energy of the low-temperature natural gas; the natural gas outlet of the cryogenic three-phase separator 3 leads to an export system 7. The incoming gas is cooled by the coiled heat exchanger 2 and then enters the flash evaporation liquid separation tank 4 for separation, and finally the obtained gas is output from the outlet of the flash evaporation liquid separation tank 4 and enters the emptying system 6 and the fuel gas removing system 9. The gas discharged from the top of the flash evaporation liquid separation tank 4 is used as fuel gas in the gas gathering station, and can also be connected with a venting torch through a venting system 6, and the condensate oil discharged from the bottom is discharged from a water tank for decontamination.
The filtering separator 1 is a vertical separator, an inlet of the filtering separator 1 is provided with a baffle, the upper part of the filtering separator is provided with a mist supplementing wire net, the inside of the filtering separator 1 is formed by combining a plurality of cyclone pipes, gas enters a first-stage distribution cavity from a gas inlet pipeline, the gas is forced to do centrifugal motion in the cyclone pipes through inlets (double tangential inlets) in the symmetrical tangential directions of the upper parts of the two cyclone pipes of each cyclone pipe, the centrifugal force is different due to the difference of gas, liquid and solid density, the liquid and the solid density are far greater than the gas, so that the gas is thrown to the outer walls of the cyclone pipes, the gas enters a container lower part collection cavity through a cyclone pipe lower part outlet, the reverse flow direction of clean gas at the lower part vortex of the cyclone pipes is realized, and. The filtering separator 1 can remove solid particles in natural gas with the particle size less than or equal to 10 microns, the separation efficiency is more than 99.9 percent, the inlet of the filtering separator 1 is connected with the emptying system 6, automatic and safe discharge when the pressure of the incoming gas exceeds a set value can be realized, the filtering separator 1 is provided with two liquid level systems of liquid level on-site display and remote transmission, the remote transmission liquid level is interlocked with a valve for discharging sewage, the low-liquid-level emergency closing of the liquid discharging electric ball valve can be realized, and liquid discharging is controlled through an electric regulating valve during normal liquid discharging.
The coiled pipe type heat exchanger 2 has high heat transfer efficiency, can meet the requirement of multi-strand feeding and discharging, has good adaptability to the process of the deoiling and dehydrating device, and reduces the temperature of the natural gas discharged from the heat exchanger to-15 to-5 ℃.
The low-temperature three-phase separator 3 is of a horizontal structure and can meet the requirements of oil-gas-water three-phase separation, an oil-gas-water mixture enters a pre-degassing chamber at a high speed, a large amount of crude oil associated gas is separated by cyclone separation and gravity action, the pre-degassed oil-water mixture enters a distributor and a water washing chamber through a guide pipe at a high speed, washing and demulsifying are carried out in an active water layer containing a demulsifier, steady flow is carried out, the Reynolds coefficient of incoming liquid is reduced, the incoming liquid flows into a settling separation chamber for further settling separation after coalescence rectification, the degassed crude oil turns over a partition plate to enter an oil chamber and is metered by a flow meter, the outgoing separator is controlled, and a water phase enters a water chamber through a guide pipe by means.
The low-temperature three-phase separator 3 is provided with a two-phase separation liquid level meter 304 and a one-phase separation liquid level meter 328, both of which have the functions of liquid level local display and remote transmission, and the specific implementation is an alternative relation, namely, as long as one of the liquid level meters firstly displays that the low liquid level or the high liquid level is reached, the system can give corresponding alarm). The alcohol-containing sewage and the condensate drainage of the low-temperature three-phase separator 3 are controlled through electric control valves, the electric control valves are all linked with the second three-phase separation liquid level meter 304 and the first three-phase separation liquid level meter 328 of the low-temperature three-phase separator 3, the cold energy of the low-temperature alcohol-containing sewage and the condensate is fully utilized, and the alcohol-containing sewage is reheated by a coiled heat exchanger and then flows to a sewage tank of a gas collecting station. The outlet of the low-temperature three-phase separator 3 is provided with a J-T valve pressure regulating system, namely a three-phase separation throttle valve I312, the temperature of the natural gas is reduced to minus 19 to minus 9 ℃ through the pressure loss of the natural gas of 0.6 to 0.8MPa, the cooled natural gas enters a winding pipe type for heat exchange, and the cold energy of the low-temperature natural gas is fully utilized to reduce the temperature of the fed natural gas.
Flash distillation liquid separation jar 4 is vertical structure, is equipped with flash distillation level gauge 402 and flash distillation level gauge two 403, and the liquid level of both all has and shows on the spot and teletransmission function, and flash distillation temperature transmitter 401 and flash distillation thermometer 404 both's temperature all has and shows on the spot and teletransmission function, and the gas of flash distillation liquid separation jar 4 top play is passed through fuel gas system and is regarded as fuel gas in the gas gathering station, also can be connected with the blow-down torch through blow-down system 6, and the condensate oil that the bottom was come out goes sewage tank of drainage 8. The device is generally provided with a bypass line. The utility model discloses the scientific research project that relies on 5000 ten thousand tons in Changqing oil field and last high-efficient steady production key technology research and application, combination Jingbian gas field actual natural gas component and station yard construction are actual, can with the utility model provides a device is applied to unable concentrated large-scale natural gas treatment factory of construction, and the middle-size and small-size gas collecting station of air supply dispersion can reach better effect.
Example 2:
based on embodiment 1, in this embodiment, an inlet of the filtering separator 1 is connected to a natural gas supply system 10 through a pipeline, and an air inlet switch ball valve 101 is arranged on the pipeline; a first ball valve 124 is arranged between the natural gas incoming system 10 and the external transportation system 7; the natural gas supply system 10 is connected with the emptying system 6 through a pipeline, an emptying safety valve 103 is arranged on the pipeline, and an air inlet switch ball valve 101 is arranged in parallel with the emptying safety valve 103; two ends of the vent safety valve 103 are respectively provided with a vent ball valve I102 and a vent ball valve II 104.
An alcohol injection atomizer 115, a first temperature transmitter 107 and a first thermometer 108 are sequentially arranged between the upper outlet of the filtering separator 1 and the upper inlet of the coiled heat exchanger 2; a first check valve 114, a first sealed sampling stop valve 112 and a filter 110 are sequentially arranged between the alcohol injection atomizer 115 and the alcohol injection system 5, a first alcohol injection control valve 109 and a second alcohol injection control valve 111 are respectively arranged at two ends of the filter 110, and a first pressure gauge 113 is arranged on the first sealed sampling stop valve 112.
A second sealed sampling stop valve 105 is arranged at the upper part of the filtering separator 1, and a second pressure gauge 106 is arranged on the second sealed sampling stop valve 105; the lower part of the filtering separator 1 is provided with a first liquid level meter 116 and a second liquid level meter 117, the lower part outlet of the filtering separator 1 is connected with the sewage system 8 through two parallel pipelines, one pipeline is provided with a liquid discharge electric ball valve 118, a low-point liquid discharge valve 119, an electric regulating valve 120 and a second ball valve 121, and the other pipeline is provided with a third ball valve 122 and a first throttle valve 123.
A ball valve IV 203 is arranged between the outlet at the upper end of the coiled heat exchanger 2 and the output system 7; a second temperature transmitter 201 and a second temperature gauge 202 are arranged between the outlet at the lower part of the coiled heat exchanger 2 and the inlet of the low-temperature three-phase separator 3; a ball valve five 204 is arranged between the coiled heat exchangers 2 and 4, a ball valve six 205 is arranged between the coiled heat exchanger 2 and the sewage system 8, and the ball valve five 204 and the ball valve six 205 are arranged in parallel.
A three-phase separation emptying safety valve 330 is arranged between the upper end outlet of the low-temperature three-phase separator 3 and the emptying system 6, and a three-phase separation emptying ball valve I329 and a three-phase separation emptying ball valve II 331 are respectively arranged at two ends of the three-phase separation emptying safety valve 330; one end of the low-temperature three-phase separator 3 is provided with a first three-phase separation liquid level meter 328, and the middle part of the low-temperature three-phase separator 3 is provided with a second three-phase separation liquid level meter 304; a three-phase separation temperature transmitter 303 is arranged in the middle of the upper end of the low-temperature three-phase separator 3; one side of the three-phase separation temperature transmitter 303 is provided with a first three-phase separation sealing sampling stop valve 301, and the first three-phase separation sealing sampling stop valve 301 is provided with a first three-phase separation pressure gauge 302.
A three-phase separation sealing sampling stop valve II 305, a three-phase separation sealing sampling stop valve III 314 and a three-phase separation sealing sampling stop valve IV 316 are sequentially arranged between the natural gas outlet of the low-temperature three-phase separator 3 and the inlet at the lower end of the coiled heat exchanger 2, and a three-phase separation pressure gauge II 306, a three-phase separation pressure gauge III 315 and a three-phase separation pressure gauge IV 317 are respectively arranged on the three-phase separation sealing sampling stop valve II 305, the three-phase separation sealing sampling stop valve III 314 and the three-phase separation sealing sampling stop valve IV 316; the three-phase separation sealing sampling stop valve II 305 and the three-phase separation sealing sampling stop valve III 314 are connected through three parallel pipelines, a three-phase separation ball valve I308, a three-phase separation low-point liquid discharge valve I309, a three-phase separation electric regulating valve I310 and a three-phase separation ball valve II 311 are arranged on the first pipeline, a three-phase separation throttle valve I312 is arranged on the second pipeline, and a three-phase separation gate valve I307 and a three-phase separation gate valve II 313 are arranged on the third pipeline.
A three-phase separation electric regulating valve II 320 and a three-phase separation throttle valve II 322 are arranged between the alcohol-containing sewage outlet of the low-temperature three-phase separator 3 and the inlet at the lower end of the coiled heat exchanger 2, the three-phase separation electric regulating valve II 320 and the three-phase separation throttle valve II 322 are arranged in parallel, two ends of the three-phase separation electric regulating valve II 320 are respectively provided with a three-phase separation ball valve III 318 and a three-phase separation ball valve IV 321, and a three-phase separation low-point liquid discharge valve II 319 is arranged between the three-phase separation ball valve III 318 and the three-phase separation electric; a three-phase separation electric regulating valve III 325 and a three-phase separation throttling valve III 327 are arranged between the condensate-containing outlet of the low-temperature three-phase separator 3 and the inlet at the lower end of the coiled heat exchanger 2, the three-phase separation electric regulating valve III 325 and the three-phase separation throttling valve III 327 are arranged in parallel, two ends of the three-phase separation electric regulating valve III 325 are respectively provided with a three-phase separation ball valve V323 and a three-phase separation ball valve V326, and a three-phase separation low-point liquid discharge valve III 324 is arranged between the three-phase separation ball valve V323 and the three-phase separation electric regulating valve III; the three-phase separation electric regulating valve three 325 is electrically connected with the three-phase separation liquid level meter one 328 of the low-temperature three-phase separator 3, and the three-phase separation electric regulating valve two 320 is electrically connected with the three-phase separation liquid level meter two 304 of the low-temperature three-phase separator 3.
A first flash liquid level meter 402 and a second flash liquid level meter 403 are respectively arranged on two sides of the flash liquid separation tank 4, a first flash temperature transmitter 401, a flash thermometer 404, a second flash sealed sampling stop valve 407 and a first flash sealed sampling stop valve 405 are further arranged on the flash liquid separation tank 4, the first flash temperature transmitter 401 is positioned above the first flash liquid level meter 402, the flash thermometer 404 is positioned above the second flash liquid level meter 403, the first flash sealed sampling stop valve 405 and the second flash sealed sampling stop valve 407 are both positioned above the flash thermometer 404, and a first flash pressure gauge 406 is arranged on the first flash sealed sampling stop valve 405; a second flash pressure gauge 408 is arranged on the second flash sealing sampling stop valve 407; a flash evaporation emptying safety valve 410 is arranged between the upper outlet of the flash evaporation liquid separator 4 and the emptying system 6, and a flash evaporation emptying ball valve I409 and a flash evaporation emptying ball valve II 411 are respectively arranged at two ends of the flash evaporation emptying safety valve 410; a first flash electric regulating valve 421 and a first flash electric throttling valve 423 are arranged between the lower end outlet of the flash liquid separator 4 and a blowdown ball valve 424 of the blowdown system 8 in parallel, a first flash ball valve 419 and a second flash ball valve 422 are respectively arranged at two ends of the first flash electric regulating valve 421, and a first flash low-point liquid discharge valve 420 is arranged between the first flash ball valve 419 and the first flash electric regulating valve 421; the first flash evaporation electric regulation 421 is electrically connected with the second flash evaporation liquid level meter 403; a flash electric regulating valve II 414 and a flash electric throttling valve I416 are arranged between the outlet at the upper end of the flash liquid separating tank 4 and the fuel gas removing system 9 in parallel, a flash ball valve V412 and a flash ball valve VI 415 are respectively arranged at two ends of the flash electric regulating valve II 414, and a flash low-point liquid discharge valve II 413 is arranged between the flash ball valve V412 and the flash electric regulating valve II 414; the flash evaporation electric regulating valve II 414 and the flash evaporation electric throttling valve I416 are connected in parallel and then are connected with the fuel gas removing system 9 through a flash evaporation ball valve III 417, and the flash evaporation electric regulating valve II 414 and the flash evaporation electric throttling valve I416 are connected in parallel and then are connected with the emptying system 6 through a flash evaporation ball valve IV 418; the second flash evaporation electric regulation 414 is electrically connected with a second flash evaporation pressure gauge 408 on the flash evaporation liquid separation tank 4.
The low-temperature three-phase separator 3 is a horizontal low-temperature three-phase separator, and the flash evaporation liquid separation tank 4 is a vertical flash evaporation liquid separation tank.
The utility model provides an integration method based on skid-mounted formula natural gas deoiling dehydration, concrete step is: the natural gas enters a filtering separator 1 for separation, the separated natural gas enters a coiled tube type heat exchanger 2, exchanging heat with the low-temperature dry gas output, the low-temperature alcohol-containing sewage and the low-temperature condensate oil, then entering a low-temperature three-phase separator 3, further throttling and cooling the separated low-temperature natural gas to-19 to-9 ℃, entering a coiled tube heat exchanger 2, the raw material natural gas with higher temperature exchanges heat and enters an outward transportation system, the low-temperature alcohol-containing sewage and the low-temperature condensate oil separated by the low-temperature three-phase separator 3 enter a coiled tube type heat exchanger 2, the raw material natural gas with higher temperature exchanges heat and enters a flash evaporation liquid separation tank 4, the sewage containing alcohol and condensate oil after flash evaporation in the flash evaporation liquid separation tank 4 is discharged into a sewage tank through a sewage discharge pipeline, and the natural gas after flash evaporation can enter a fuel gas system in a station to be used as fuel gas and can also be accessed to an emptying system in the station to enter a torch to be combusted; meanwhile, the methanol injection system 5 injects methanol into the natural gas pipeline before the inlet of the pipe-wound heat exchanger 2 through the methanol atomizer, the specific injection amount can be calculated according to the temperature of the natural gas after passing through the pipe-wound heat exchanger 2, and natural gas hydrate is not formed in the natural gas at the temperature.
The device can make the natural gas generate a small temperature drop through a small pressure difference throttling (0.6-0.8 MPa), the temperature drop is used as the cold end temperature difference of the heat exchanger, the area of the heat exchanger is large enough, and the raw gas generates a large enough temperature drop (45-35 ℃) through heat exchange under the small cold end temperature difference, so that the requirement of natural gas low-temperature deoiling and dehydrating is met.
The above-mentioned, only be the concrete implementation of the preferred embodiment of the present invention, but the protection scope of the present invention is not limited thereto, and any person skilled in the art is in the technical scope of the present invention, according to the technical solution of the present invention and the utility model, the concept of which is equivalent to replace or change, should be covered within the protection scope of the present invention. The system components and the device structures thereof, which are not described in detail in the present invention, are prior art, and detailed description thereof will not be provided.
Claims (9)
1. The utility model provides a based on skid-mounted formula natural gas deoiling dehydration integration device which characterized in that: the device comprises a filtering separator (1), a coiled heat exchanger (2), a low-temperature three-phase separator (3), a flash evaporation liquid separation tank (4), an alcohol injection system (5), a venting system (6), an output system (7), a blowdown system (8), a fuel gas removal system (9) and a natural gas incoming system (10), wherein an inlet of the filtering separator (1) is connected with the natural gas incoming system (10), and the natural gas incoming system (10) is respectively connected with the venting system (6) and the output system (7);
an outlet at the upper end of the filtering separator (1) is connected with an inlet at the upper part of the wound tube type heat exchanger (2), and an inlet at the upper part of the wound tube type heat exchanger (2) is also connected with an alcohol injection system (5); the lower outlet of the filtering separator (1) is connected with a sewage ball valve (424) arranged on a sewage system (8);
an outlet at the lower part of the coiled heat exchanger (2) is connected with an inlet at the upper end of the low-temperature three-phase separator (3), an outlet at the upper end of the coiled heat exchanger (2) is connected with an external conveying system (7), and a blowdown outlet at the upper end of the coiled heat exchanger (2) is connected with a blowdown ball valve (424) arranged on a blowdown system (8);
a natural gas outlet, an alcohol-containing sewage outlet and a condensate-containing outlet of the low-temperature three-phase separator (3) are respectively connected with an inlet at the lower end of the coiled tube heat exchanger (2); an outlet at the upper end of the low-temperature three-phase separator (3) is connected with a venting system (6);
an inlet of the flash evaporation liquid separation tank (4) is connected with a liquid outlet of the wound tube type heat exchanger (2); the lower outlet of the flash evaporation liquid separation tank (4) is connected with a sewage discharge ball valve (424) of a sewage discharge system (8), and the upper outlet of the flash evaporation liquid separation tank (4) is respectively connected with a fuel gas removing system (9) and a venting system (6).
2. The natural gas deoiling and dewatering integrated device based on the skid-mounted type according to claim 1, characterized in that: the inlet of the filtering separator (1) is connected with a natural gas inlet system (10) through a pipeline, and an air inlet switch ball valve (101) is arranged on the pipeline; a ball valve I (124) is arranged between the natural gas incoming system (10) and the external transmission system (7); the natural gas supply system (10) is connected with the emptying system (6) through a pipeline, an emptying safety valve (103) is arranged on the pipeline, and the air inlet switch ball valve (101) is connected with the emptying safety valve (103) in parallel; two ends of the emptying safety valve (103) are respectively provided with an emptying ball valve I (102) and an emptying ball valve II (104).
3. The natural gas deoiling and dewatering integrated device based on the skid-mounted type according to claim 1, characterized in that: an alcohol injection atomizer (115), a first temperature transmitter (107) and a first thermometer (108) are sequentially arranged between an upper outlet of the filtering separator (1) and an upper inlet of the coiled heat exchanger (2); annotate and be equipped with check valve (114), sealed sample stop valve (112) and filter (110) between mellow wine atomizer (115) and notes mellow wine system (5) in proper order, filter (110) both ends be provided with respectively and annotate mellow wine control valve (109) and annotate mellow wine control valve two (111), be equipped with manometer (113) on the sealed sample stop valve (112).
4. The natural gas deoiling and dewatering integrated device based on the skid-mounted type according to claim 1, characterized in that: a second sealed sampling stop valve (105) is arranged at the upper part of the filtering separator (1), and a second pressure gauge (106) is arranged on the second sealed sampling stop valve (105); the lower part of the filtering separator (1) is provided with a first liquid level meter (116) and a second liquid level meter (117), the lower outlet of the filtering separator (1) is connected with the sewage system (8) through two parallel pipelines, one pipeline is provided with a liquid discharge electric ball valve (118), a low-point liquid discharge valve (119), an electric regulating valve (120) and a second ball valve (121), and the other pipeline is provided with a third ball valve (122) and a first throttle valve (123).
5. The natural gas deoiling and dewatering integrated device based on the skid-mounted type according to claim 1, characterized in that: a ball valve IV (203) is arranged between the outlet at the upper end of the coiled heat exchanger (2) and the output system (7); a second temperature transmitter (201) and a second thermometer (202) are arranged between the outlet at the lower part of the coiled tube type heat exchanger (2) and the inlet of the low-temperature three-phase separator (3); a ball valve five (204) is arranged between the coiled heat exchanger (2) and the flash evaporation liquid separation tank (4), a ball valve six (205) is arranged between the coiled heat exchanger (2) and the sewage system (8), and the ball valve five (204) and the ball valve six (205) are arranged in parallel.
6. The natural gas deoiling and dewatering integrated device based on the skid-mounted type according to claim 1, characterized in that: a three-phase separation emptying safety valve (330) is arranged between an outlet at the upper end of the low-temperature three-phase separator (3) and the emptying system (6), and a three-phase separation emptying ball valve I (329) and a three-phase separation emptying ball valve II (331) are respectively arranged at two ends of the three-phase separation emptying safety valve (330); one end of the low-temperature three-phase separator (3) is provided with a first three-phase separation liquid level meter (328), and the middle part of the low-temperature three-phase separator (3) is provided with a second three-phase separation liquid level meter (304); a three-phase separation temperature transmitter (303) is arranged in the middle of the upper end of the low-temperature three-phase separator (3); one side of the three-phase separation temperature transmitter (303) is provided with a first three-phase separation sealing sampling stop valve (301), and a first three-phase separation pressure gauge (302) is arranged on the first three-phase separation sealing sampling stop valve (301).
7. The natural gas deoiling and dewatering integrated device based on the skid-mounted type according to claim 1, characterized in that: a three-phase separation sealing sampling stop valve II (305), a three-phase separation sealing sampling stop valve III (314) and a three-phase separation sealing sampling stop valve IV (316) are sequentially arranged between the natural gas outlet of the low-temperature three-phase separator (3) and the inlet at the lower end of the coiled heat exchanger (2), and a three-phase separation pressure gauge II (306), a three-phase separation pressure gauge III (315) and a three-phase separation pressure gauge IV (317) are respectively arranged on the three-phase separation sealing sampling stop valve II (305), the three-phase separation sealing sampling stop valve III (314) and the three-phase separation sealing sampling stop valve IV (316); the three-phase separation sealing sampling stop valve II (305) is connected with the three-phase separation sealing sampling stop valve III (314) through three parallel pipelines, a three-phase separation ball valve I (308), a three-phase separation low-point liquid discharge valve I (309), a three-phase separation electric regulating valve I (310) and a three-phase separation ball valve II (311) are arranged on the first pipeline, a three-phase separation throttle valve I (312) is arranged on the second pipeline, and a three-phase separation gate valve I (307) and a three-phase separation gate valve II (313) are arranged on the third pipeline; a three-phase separation electric regulating valve II (320) and a three-phase separation throttle valve II (322) are arranged between an alcohol-containing sewage outlet of the low-temperature three-phase separator (3) and an inlet at the lower end of the coiled pipe type heat exchanger (2), the three-phase separation electric regulating valve II (320) and the three-phase separation throttle valve II (322) are arranged in parallel, a three-phase separation ball valve III (318) and a three-phase separation ball valve IV (321) are respectively arranged at two ends of the three-phase separation electric regulating valve II (320), and a three-phase separation low-point liquid discharge valve II (319) is arranged between the three-phase separation ball valve III (318) and the three-phase separation; a three-phase separation electric regulating valve III (325) and a three-phase separation throttling valve III (327) are arranged between a condensate-containing outlet of the low-temperature three-phase separator (3) and a lower end inlet of the coiled heat exchanger (2), the three-phase separation electric regulating valve III (325) and the three-phase separation throttling valve III (327) are arranged in parallel, two ends of the three-phase separation electric regulating valve III (325) are respectively provided with a three-phase separation ball valve V (323) and a three-phase separation ball valve VI and a three-phase separation ball valve 326, and a three-phase separation low-point liquid discharge valve III (324) is arranged between the three-phase separation ball valve V (323) and the three-phase separation; the three-phase separation electric regulating valve III (325) is electrically connected with the three-phase separation liquid level meter I (328) of the low-temperature three-phase separator (3), and the three-phase separation electric regulating valve II (320) is electrically connected with the three-phase separation liquid level meter II (304) of the low-temperature three-phase separator (3).
8. The natural gas deoiling and dewatering integrated device based on the skid-mounted type according to claim 1, characterized in that: a first flash liquid level meter (402) and a second flash liquid level meter (403) are respectively arranged on two sides of the flash liquid separating tank (4), a flash temperature transmitter (401), a flash thermometer (404), a second flash sealing sampling stop valve (407) and a first flash sealing sampling stop valve (405) are further arranged on the flash liquid separating tank (4), the flash temperature transmitter (401) is positioned above the first flash liquid level meter (402), the flash thermometer (404) is positioned above the second flash liquid level meter (403), the first flash sealing sampling stop valve (405) and the second flash sealing sampling stop valve (407) are both positioned above the flash thermometer (404), and a first flash pressure gauge (406) is arranged on the first flash sealing sampling stop valve (405); a second flash pressure gauge (408) is arranged on the second flash sealing sampling stop valve (407); a flash evaporation emptying safety valve (410) is arranged between the upper outlet of the flash evaporation liquid separation tank (4) and the emptying system (6), and a flash evaporation emptying ball valve I (409) and a flash evaporation emptying ball valve II (411) are respectively arranged at two ends of the flash evaporation emptying safety valve (410); a first flash electric adjusting valve (421) and a first flash electric throttling valve (423) are arranged between the lower end outlet of the flash separation tank (4) and a blowdown ball valve (424) of the blowdown system (8) in parallel, a first flash ball valve (419) and a second flash ball valve (422) are respectively arranged at two ends of the first flash electric adjusting valve (421), and a first flash low-point liquid discharge valve (420) is arranged between the first flash ball valve (419) and the first flash electric adjusting valve (421); the first flash evaporation electric regulation device (421) is electrically connected with the second flash evaporation liquid level meter (403); a flash evaporation electric regulating valve II (414) and a flash evaporation electric throttling valve II (416) are arranged between the outlet at the upper end of the flash evaporation liquid separation tank (4) and the fuel gas removal system (9) in parallel, a flash evaporation ball valve V (412) and a flash evaporation ball valve VI (415) are respectively arranged at two ends of the flash evaporation electric regulating valve II (414), and a flash evaporation low-point liquid discharge valve II (413) is arranged between the flash evaporation ball valve V (412) and the flash evaporation electric regulating valve II (414); the second flash evaporation electric regulation valve (414) and the second flash evaporation electric throttle valve (416) are connected in parallel and then are connected with the fuel gas removal system (9) through a third flash evaporation ball valve (417), and the second flash evaporation electric regulation valve (414) and the second flash evaporation electric throttle valve (416) are connected in parallel and then are connected with the emptying system (6) through a fourth flash evaporation ball valve (418); and the second flash evaporation electric regulation device (414) is electrically connected with a second flash evaporation pressure gauge (408) on the flash evaporation liquid separation tank (4).
9. The natural gas deoiling and dewatering integrated device based on the skid-mounted type according to claim 1, characterized in that: the low-temperature three-phase separator (3) is a horizontal low-temperature three-phase separator, and the flash evaporation liquid separation tank (4) is a vertical flash evaporation liquid separation tank.
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| CN201920059688.9U CN210030602U (en) | 2019-01-15 | 2019-01-15 | Skid-mounted natural gas deoiling and dehydrating integrated device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920059688.9U CN210030602U (en) | 2019-01-15 | 2019-01-15 | Skid-mounted natural gas deoiling and dehydrating integrated device |
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| CN210030602U true CN210030602U (en) | 2020-02-07 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109652154A (en) * | 2019-01-15 | 2019-04-19 | 西安长庆科技工程有限责任公司 | A kind of prying gas deoiling, dewatering integrated device and method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109652154A (en) * | 2019-01-15 | 2019-04-19 | 西安长庆科技工程有限责任公司 | A kind of prying gas deoiling, dewatering integrated device and method |
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Effective date of registration: 20201110 Address after: 710018 Shaanxi province Xi'an Weiyang road Fengcheng four Changqing building Patentee after: XI'AN CHANGQING TECHNOLOGY ENGINEERING Co.,Ltd. Patentee after: CHINA NATIONAL PETROLEUM Corp. Address before: 710018 Shaanxi city of Xi'an province Fengcheng Weiyang District four building 1809 Changqing Road Patentee before: XI'AN CHANGQING TECHNOLOGY ENGINEERING Co.,Ltd. |