CN112300827A - Light hydrocarbon extraction system and extraction method - Google Patents
Light hydrocarbon extraction system and extraction method Download PDFInfo
- Publication number
- CN112300827A CN112300827A CN201910713202.3A CN201910713202A CN112300827A CN 112300827 A CN112300827 A CN 112300827A CN 201910713202 A CN201910713202 A CN 201910713202A CN 112300827 A CN112300827 A CN 112300827A
- Authority
- CN
- China
- Prior art keywords
- outlet end
- light hydrocarbon
- gas
- inlet end
- deethanizer
- 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
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 225
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 225
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 210
- 238000000605 extraction Methods 0.000 title claims abstract description 93
- 239000012071 phase Substances 0.000 claims abstract description 159
- 239000000126 substance Substances 0.000 claims abstract description 143
- 238000000926 separation method Methods 0.000 claims abstract description 133
- 239000007791 liquid phase Substances 0.000 claims abstract description 90
- 238000001816 cooling Methods 0.000 claims abstract description 76
- 230000006835 compression Effects 0.000 claims abstract description 66
- 238000007906 compression Methods 0.000 claims abstract description 66
- 239000002994 raw material Substances 0.000 claims abstract description 45
- 230000018044 dehydration Effects 0.000 claims abstract description 26
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 26
- 238000004064 recycling Methods 0.000 claims abstract description 3
- 238000011084 recovery Methods 0.000 claims description 23
- 239000012808 vapor phase Substances 0.000 claims description 10
- 239000007789 gas Substances 0.000 description 203
- 238000005265 energy consumption Methods 0.000 description 29
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 26
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 14
- 238000000034 method Methods 0.000 description 10
- 238000005057 refrigeration Methods 0.000 description 9
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 8
- 230000000694 effects Effects 0.000 description 8
- 239000003345 natural gas Substances 0.000 description 7
- 239000001294 propane Substances 0.000 description 7
- 230000008901 benefit Effects 0.000 description 6
- 238000010586 diagram Methods 0.000 description 6
- 239000000463 material Substances 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 5
- 239000007792 gaseous phase Substances 0.000 description 4
- 239000001273 butane Substances 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 230000008092 positive effect Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- HOWJQLVNDUGZBI-UHFFFAOYSA-N butane;propane Chemical compound CCC.CCCC HOWJQLVNDUGZBI-UHFFFAOYSA-N 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 239000002274 desiccant Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
- C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1025—Natural gas
Abstract
The invention provides a light hydrocarbon extraction system and an extraction method. The light hydrocarbon extraction system comprises a dehydration device, a precooling device, a light hydrocarbon separation device, a dry gas compression device, a first heat exchange device and a throttling device. The first heat exchange device is provided with a first cold source channel and a first medium channel which can exchange heat; the raw material gas inlet end of the light hydrocarbon separation device is connected with the outlet end of the precooling device, the liquid phase outlet end outputs light hydrocarbon, and the gas phase outlet end outputs gas phase substances; the inlet end of the first cold source channel is connected with the gas phase outlet end to receive the gas phase substance; the outlet end of the first cold source channel is communicated with the inlet end of a dry gas compression device, the outlet end of the dry gas compression device is connected with the inlet end of the first medium channel, and the dry gas compression device pressurizes gas-phase substances to form CNG; the inlet end of the throttling device is connected with the outlet end of the first medium channel, and the outlet end of the throttling device is connected with the recycling inlet end of the light hydrocarbon separation device, so that cooling capacity is provided for the light hydrocarbon separation device after CNG is throttled and cooled.
Description
Technical Field
The invention relates to the technical field of natural gas treatment, in particular to a light hydrocarbon extraction system and an extraction method.
Background
Natural gas, which contains ethane, propane, butane, etc. in addition to methane, is widely used in the human life and industry as a valuable resource. Light hydrocarbons are a generic term for hydrocarbon mixtures in a liquid state extracted from natural gas by cold separation or the like, and the main components thereof are propane and heavier hydrocarbons. The light hydrocarbon has great economic value, can be directly used as fuel or further separated into ethane, propane, butane, or propane-butane mixture, light oil and the like, and can also be used as chemical raw materials.
At present, the following three methods are generally adopted for extracting light hydrocarbon from natural gas: 1. and (5) external cold source refrigeration. When the external cold source is used for refrigerating and extracting light dydrocarbon, the extraction rate of the light dydrocarbon is lower when the refrigerating temperature of the external cold source is insufficient. And the energy consumption is higher when the refrigeration temperature of the external cold source is reduced to improve the extraction rate of light hydrocarbon. 2. The expander refrigerates. The method is only suitable for occasions requiring low dry gas pressure, and has high energy consumption if the dry gas pressure is high or CNG is co-produced. 3. And the refrigeration of the external cold source and the refrigeration of the expander are mixed. The method has high extraction rate of light hydrocarbon, but has complex flow, large investment and difficult system operation.
Disclosure of Invention
The invention aims to provide a light hydrocarbon extraction system and a light hydrocarbon extraction method with high light hydrocarbon extraction rate and low energy consumption, and aims to solve the problems in the prior art.
In order to solve the technical problems, the invention provides a light hydrocarbon extraction system, which comprises a dehydration device, a precooling device, a light hydrocarbon separation device, a dry gas compression device, a first heat exchange device and a throttling device, wherein the dehydration device is connected with the precooling device; the light hydrocarbon separation device is provided with a raw material gas inlet end, a recovery inlet end, a gas phase outlet end and a liquid phase outlet end; the first heat exchange device is provided with a first cold source channel and a first medium channel which can exchange heat; the inlet end of the dehydration device is used for connecting a raw material gas source, and the outlet end of the dehydration device is communicated with the inlet end of the precooling device; the raw material gas inlet end of the light hydrocarbon separation device is connected with the outlet end of the precooling device, the liquid phase outlet end outputs light hydrocarbons outwards, and the gas phase outlet end outputs gas-phase substances; the inlet end of the first cold source channel is connected with the gas phase outlet end to receive the gas phase substance; the outlet end of the first cold source channel is communicated with the inlet end of the dry gas compression device, the outlet end of the dry gas compression device is connected with the inlet end of the first medium channel, and the dry gas compression device pressurizes the gas-phase substances to form CNG and conveys the CNG to the first medium channel; the inlet end of the throttling device is connected with the outlet end of the first medium channel, and the outlet end of the throttling device is connected with the recycling inlet end of the light hydrocarbon separation device, so that the cooling capacity is provided for the light hydrocarbon separation device after the CNG is throttled and cooled.
In one embodiment, the heat exchanger further comprises a second heat exchange device; the second heat exchange device is provided with a second cold source channel and a second medium channel which can exchange heat; the inlet end of the second cold source channel is connected with the outlet end of the first cold source channel, and the outlet end of the second cold source channel is connected with the inlet end of the dry gas compression device, so that the outlet end of the first cold source channel is communicated with the inlet end of the dry gas compression device; the inlet end of the second medium channel is connected with the outlet end of the dewatering device, and the outlet end of the second medium channel is connected with the inlet end of the precooling device, so that the outlet end of the dewatering device is communicated with the inlet end of the precooling device.
In one embodiment, the light hydrocarbon separation device comprises a deethanizer, and the throttling device is a throttling expansion valve.
In one embodiment, the light hydrocarbon separation unit further comprises a separator disposed between the deethanizer and the throttling device; the separator is provided with an inlet end, a gas phase outlet end and a liquid phase outlet end, and the inlet end of the separator is connected with the outlet end of the throttling device to receive the throttled and cooled liquid phase substances; and the liquid phase outlet end of the separator is connected with the recovery inlet end of the deethanizer so as to send the liquid phase substances separated by the separator to the deethanizer and provide cold energy for the deethanizer.
In one embodiment, the light hydrocarbon separation device comprises a demethanizer, a deethanizer and a heat exchange device, and the throttling device is a throttling expansion valve; the raw material gas inlet end, the gas phase outlet end and the recovery inlet end of the light hydrocarbon separation device are arranged on the demethanizer, and the liquid phase outlet end of the light hydrocarbon separation device is arranged on the deethanizer; the demethanizer also has a liquid phase outlet end;
the deethanizer further has a first inlet end and a vapor phase outlet end; the heat exchange equipment is provided with a third cold source channel and a third medium channel which can exchange heat; the inlet end of the third cold source channel is connected with the liquid phase outlet end of the demethanizer so as to receive the liquid phase substance separated by the demethanizer; the outlet end of the third cold source channel is connected with the first inlet end of the deethanizer; the inlet end of the third medium channel is connected with the gas-phase outlet end of the deethanizer so as to receive the gas-phase substances separated by the deethanizer; and the outlet end of the third medium channel is connected with the inlet end of the second cold source channel.
In one embodiment, the light hydrocarbon separation unit further comprises a separator coupled between the third heat exchanger and the deethanizer, the deethanizer further having a second inlet end; the separator is provided with an inlet end, a gas-phase outlet end and a liquid-phase outlet end, the inlet end of the separator is connected with the outlet end of the third medium channel, the liquid-phase outlet end of the separator is connected with the second inlet end of the deethanizer, and the gas-phase outlet end of the separator is connected with the inlet end of the second cold source channel.
In one embodiment, the light hydrocarbon separation device comprises a deethanizer and a separator, and the throttling device is an ejector; the feed gas inlet end, the recovery inlet end, the gas phase outlet end and the liquid phase outlet end of the light hydrocarbon separation device are arranged on the deethanizer; the separator has a gas phase outlet end, a liquid phase outlet end and an inlet end; the throttling device is provided with an inlet end, a suction end and an outlet end; the gas-phase outlet end of the deethanizer is connected with the suction end of the throttling device, and gas-phase substances are conveyed to the throttling device for depressurization; the inlet end of the separator is connected with the outlet end of the throttling device so as to receive the liquid-phase substance which is throttled and cooled by the throttling device; the gas phase outlet end of the separator is connected with the inlet end of the first cold source channel so as to provide the gas phase substances separated by the separator for the first cold source channel; the liquid phase outlet end of the separator is connected with the recovery inlet end of the deethanizer so as to provide the deethanizer with the liquid phase substances separated by the separator.
In one embodiment, the light hydrocarbon separation unit comprises a demethanizer, a deethanizer, a separator, and a heat exchange device; the raw gas inlet end, the gas phase outlet end and the recovery inlet end of the light hydrocarbon separation device are arranged on the demethanizer, and the liquid phase outlet end of the light hydrocarbon separation device is arranged on the deethanizer; the demethanizer has a liquid phase outlet end; the deethanizer has a first inlet end, a second inlet end, and a gas phase outlet end; the separator has an inlet end, a gas phase outlet end, and a liquid phase outlet end; the heat exchange equipment is provided with a third cold source channel and a third medium channel which can exchange heat; the inlet end of the third cold source channel is connected with the liquid phase outlet end of the demethanizer so as to receive the liquid phase substance separated by the demethanizer; the outlet end of the third cold source channel is connected with the first inlet end of the deethanizer; the inlet end of the third medium channel is connected with the gas-phase outlet end of the deethanizer so as to receive the gas-phase substances separated by the deethanizer; the outlet end of the third medium channel is connected with the inlet end of the separator; the throttling device is an ejector and is provided with a suction end, an inlet end and an outlet end, the inlet end of the throttling device is connected with the outlet end of the first medium channel, the suction end of the throttling device is connected with the gas phase outlet end of the separator, and the outlet end of the throttling device is connected with the recovery inlet end of the demethanizer.
In one embodiment, the outlet end of the dry gas compression device is further connected with a CNG extraction pipeline to output CNG outwards; the CNG extraction pipeline is connected with the first medium channel of the first heat exchange device in parallel.
The invention also provides a light hydrocarbon extraction method, which comprises the following steps:
and (3) dehydrating: dehydrating the raw material gas;
pre-cooling: pre-cooling the dehydrated feed gas;
light hydrocarbon separation: carrying out light hydrocarbon separation on the precooled feed gas to obtain a gas-phase substance and light hydrocarbon;
the gas phase substances are subjected to heat exchange and pressurization to obtain CNG, and the CNG is subjected to heat exchange cooling and throttling cooling to provide cooling capacity for a light hydrocarbon separation process.
In one embodiment, in the pre-cooling step, the gas-phase substance exchanges heat with the dehydrated raw material gas to provide part of cold energy for pre-cooling the dehydrated raw material gas.
In one embodiment, the method further comprises the following steps: and (3) carrying out heat exchange and pressurization on the gas-phase substance to obtain CNG, outputting the CNG outwards and finishing the extraction of the CNG.
According to the technical scheme, the invention has the advantages and positive effects that:
the light hydrocarbon extraction system comprises a dehydration device, a precooling device, a light hydrocarbon separation device, a dry gas compression device, a first heat exchange device and a throttling device. The liquid phase outlet end of the light hydrocarbon separation device outputs light hydrocarbon, and the gas phase outlet end of the light hydrocarbon separation device outputs gas phase substances. The gas phase substance is compressed by the dry gas compression device to obtain CNG, and the gas phase substance enters the first cold source channel to serve as a cold source to cool the CNG, so that the cold energy of the gas phase substance is utilized, the energy is saved, and the energy consumption is reduced. The cooled CNG enters the light hydrocarbon separation device after the throttling and cooling effects of the throttling device, thereby providing cold for the light hydrocarbon separation device, saving energy and reducing energy consumption. And the more the cold energy in the light hydrocarbon separation device is, the lower the temperature in the light hydrocarbon separation device is, and the higher the extraction rate of the light hydrocarbon is.
The light hydrocarbon extraction method has the advantages of simple process, low energy consumption and high light hydrocarbon extraction rate.
Drawings
FIG. 1 is a schematic diagram of a first embodiment of the light hydrocarbon extraction system of the present invention;
FIG. 2 is a schematic diagram of the second embodiment of the light hydrocarbon extraction system of the present invention;
FIG. 3 is a schematic diagram of a third embodiment of the light hydrocarbon extraction system of the present invention;
FIG. 4 is a schematic diagram of a fourth embodiment of the light hydrocarbon extraction system of the present invention;
FIG. 5 is a schematic diagram of a fifth embodiment of the light hydrocarbon extraction system of the present invention;
fig. 6 is a schematic structural diagram of a sixth embodiment of the light hydrocarbon extraction system of the present invention.
The reference numerals are explained below:
1. a light hydrocarbon extraction system; 11. a dewatering device; 12. a pre-cooling device; 13. a light hydrocarbon separation unit; 14. a first heat exchange means; 16. a dry gas compression device; 17. a throttling device.
2. A light hydrocarbon extraction system; 21. a dewatering device; 22. a pre-cooling device; 23. a light hydrocarbon separation unit; 24. a first heat exchange means; 25. a second heat exchange means; 26. a dry gas compression device; 27. a throttling device.
3. A light hydrocarbon extraction system; 31. a dewatering device; 32. a pre-cooling device; 33. a light hydrocarbon separation unit; 331. a deethanizer; 332. a separator; 34. a first heat exchange means; 35. a second heat exchange means; 36. a dry gas compression device; 37. a throttling device.
4. A light hydrocarbon extraction system; 41. a dewatering device; 42. a pre-cooling device; 43. a light hydrocarbon separation unit; 431. a deethanizer; 432. a separator; 433. a pressure reducing valve; 44. a first heat exchange means; 45. a second heat exchange means; 46. a dry gas compression device; 47. a throttling device.
5. A light hydrocarbon extraction system; 51. a dewatering device; 52. a pre-cooling device; 531. a demethanizer; 532. a deethanizer; 533. heat exchange equipment; 534. a separator; 54. a first heat exchange means; 55. a second heat exchange means; 56. a dry gas compression device; 57. a throttling device.
6. A light hydrocarbon extraction system; 61. a dewatering device; 62. a pre-cooling device; 631. a demethanizer; 632. a deethanizer; 633. heat exchange equipment; 634. a separator; 64. a first heat exchange means; 65. a second heat exchange means; 66. a dry gas compression device; 67. a throttling device.
Detailed Description
Exemplary embodiments that embody features and advantages of the invention are described in detail below in the specification. It is to be understood that the invention is capable of other embodiments and that various changes in form and details may be made therein without departing from the scope of the invention and the description and drawings are to be regarded as illustrative in nature and not as restrictive.
For further explanation of the principles and construction of the present invention, reference will now be made in detail to the preferred embodiments of the present invention, which are illustrated in the accompanying drawings.
The invention provides a light hydrocarbon extraction system which is used for extracting light hydrocarbon (NGL) in raw material gas. The raw material gas can be conventional natural gas, unconventional natural gas, refined tail gas, hydrocarbon-containing chemical tail gas and the like. By extracting light hydrocarbon from the natural gas and utilizing the light hydrocarbon, the environmental pollution can be reduced, and good economic benefit can be obtained.
The invention also provides a light hydrocarbon extraction method, which comprises the following steps:
and (3) dehydrating: dehydrating the raw material gas;
pre-cooling: pre-cooling the dehydrated feed gas;
light hydrocarbon separation: carrying out light hydrocarbon separation on the precooled feed gas to obtain a gas-phase substance and light hydrocarbon;
the gas phase substances are subjected to heat exchange and pressurization to obtain CNG, and the CNG is subjected to heat exchange cooling and throttling cooling to provide cooling capacity for the light hydrocarbon separation process.
The light hydrocarbon extraction system is described in detail below by way of examples.
First embodiment
Referring to fig. 1, the light hydrocarbon extraction system 1 of the present embodiment includes a dehydration device 11, a pre-cooling device 12, a light hydrocarbon separation device 13, a first heat exchange device 14, a dry gas compression device 16, and a throttling device 17.
The dehydration device 11 is used for dehydrating the feed gas, so that the phenomenon that the pipeline is blocked due to the condensation of water in the pipeline, the phenomenon that water and other components in the feed gas form solid compounds to block valves, equipment and the like, and the phenomenon that water and CO are mixed is avoided2、H2The combined action of S causes corrosion, and the normal operation of the light hydrocarbon extraction system 1 is ensured.
Specifically, the dehydration device 11 has an inlet end for connecting to a raw material gas source to receive the raw material gas, and an outlet end for connecting to the pre-cooling device 12 to deliver the dehydrated raw material gas.
The dehydration device 11 may be a glycol absorption dehydration device 11, a solid desiccant absorption dehydration device 11, a condensation dehydration device 11, or a membrane separation dehydration device 11 which is being developed at home and abroad, and may be selected according to actual conditions.
The pre-cooling device 12 is disposed downstream of the dehydration device 11, and is configured to cool the dehydrated raw material gas. And cooling by a precooling device 12 to obtain pretreated feed gas. In this embodiment, the pre-cooling device 12 is a pre-cooling unit, which can reduce the temperature of the material reaching the pre-cooling device 12 to about-30 ℃.
The light hydrocarbon separation device 13 is disposed downstream of the pre-cooling device 12, and is configured to perform component separation on the pretreated raw gas to obtain light hydrocarbons. The light hydrocarbon separation device 13 separates gas phase substances and liquid phase substances according to different properties of each component. Wherein, the gas phase substance mainly comprises methane and ethane, and the liquid phase substance is light hydrocarbon, and mainly comprises propane.
Specifically, the light hydrocarbon separation device 13 has a feed gas inlet end, a recovery inlet end, a gas phase outlet end, and a liquid phase outlet end. The raw material gas inlet end is connected with the outlet end of the precooling device 12, the gas phase outlet end is used for outputting gas phase substances, and the liquid phase outlet end is used for outputting light hydrocarbons.
In this embodiment, the light hydrocarbon separation device 13 is a deethanizer, and the components are separated as a gas phase and a liquid phase according to different condensation temperatures of the components in the pretreated raw material gas. Specifically, after the pretreated raw gas is subjected to the separation action of the deethanizer, all the methane, ethane and the remaining small amount of propane are in a gas phase and output from a gas phase outlet end, and most of the propane, butane and pentane are in a liquid phase and output from a liquid phase output end, namely light hydrocarbon. And storing the light hydrocarbon output by the liquid phase output end for later use.
The first heat exchanging device 14 has a first cold source channel and a first medium channel, which can perform heat exchange, that is, the cold source in the first cold source channel performs heat exchange with the medium in the first medium channel, so that the cold source in the first cold source channel cools the medium in the first medium channel.
The inlet end of the first cold source channel is connected with the gas-phase outlet end of the light hydrocarbon separation device 13, so that the gas-phase substances separated by the light hydrocarbon separation device 13 are used as cold sources. The temperature of the gas phase substances separated by the light hydrocarbon separation device 13 is low, the gas phase substances are used as cold sources, the cold energy is fully utilized, and the energy consumption is saved.
The inlet end of the first medium channel is connected with the outlet end of the dry gas compression device 16, and the outlet end of the first medium channel is connected with the inlet end of the throttling device 17.
A dry gas compression device 16 is provided downstream of the first heat exchange device 14 for compressing the medium entering the dry gas compression device 16 to obtain CNG. Specifically, the inlet end of the dry gas compression device 16 is connected to the outlet end of the first cold source channel, that is, the dry gas compression device 16 receives and compresses the gas-phase substance of the first cold source channel, and the outlet end of the dry gas compression device 16 is connected to the inlet end of the first medium channel to convey the gas-phase substance to the first medium channel.
In this embodiment, the dry gas compression device 16 is a CNG compressor, and the compressed dry gas is mainly used to output CNG, which mainly contains methane and ethane.
The CNG output from the dry gas compression device 16 is delivered to the first medium channel to perform energy exchange with the gas phase substance in the first cold source channel, and at this time, the gas phase substance is output from the gas phase outlet end of the light hydrocarbon separation device 13, so that the temperature of the gas phase substance is lower than that of the CNG, that is, the gas phase substance cools the CNG, the refrigeration capacity of the gas phase substance is fully utilized, and the energy consumption is saved. And the gas phase substance output by the light hydrocarbon separation device 13 enters the dry gas compression device 16 after heat exchange with the CNG output by the dry gas compression device 16.
Further, in this embodiment, a CNG extraction pipeline is further connected to an outlet end of the dry gas compression device 16 for outputting CNG to the outside, and the CNG extraction pipeline is connected in parallel to the first medium subsystem.
In other embodiments, a branch line may be provided upstream of the dry gas compression device 16. The branch line is arranged in parallel with the dry gas compression device 16. Specifically, the inlet end of the branch pipeline is connected with the outlet end of the first cold source channel, and the outlet end of the branch pipeline is used for being connected with a pipe network for users to use, so that the energy consumption of the dry gas compression device 16 is reduced. Alternatively, the outlet end of the branch pipe may be directly connected to the air to directly discharge the gas-phase substance into the air.
The throttling device 17 is arranged at the downstream of the first heat exchange device 14 and used for throttling and cooling the cooled CNG. Specifically, in this embodiment, the throttle device 17 is a throttle expansion valve (J-T valve), and its inlet end is connected to the outlet end of the first medium passage, and its outlet end is connected to the recovery inlet end of the light hydrocarbon separation device 13. The throttle expansion valve expands the CNG by throttling and lowering the temperature to generate a low temperature. In this embodiment, after being cooled by the throttling device 17, the temperature can be reduced to-80 ℃ to-90 ℃, that is, the liquid phase substance is cooled and then enters the light hydrocarbon separation device 13 to provide cold for the light hydrocarbon separation device 13. And the more the cooling capacity in the light hydrocarbon separation device 13 is, the lower the temperature in the light hydrocarbon separation device 13 is, and the higher the extraction rate of light hydrocarbon is.
The light hydrocarbon extraction system 1 in this embodiment makes full use of the cold energy of the gas-phase substances separated by the light hydrocarbon separation device 13 through the first heat exchange device 14 to cool down, thereby saving energy and reducing energy consumption. The multiple dry gas compression devices 16 pressurize gas-phase substances to obtain CNG, the CNG is cooled and then sent to the throttling device 17, and the CNG is throttled and depressurized by the throttling device 17 and then sent to the light hydrocarbon separation device 13 to provide cold energy for the light hydrocarbon separation device 13, so that energy is saved. And the more the cooling capacity in the light hydrocarbon separation device 13 is, the lower the temperature in the light hydrocarbon separation device 13 is, and the higher the extraction rate of light hydrocarbon is.
The method for extracting light hydrocarbons by the light hydrocarbon extraction system 1 in this embodiment is as follows:
and (3) dehydrating: the raw material gas is dehydrated by a dehydrating device 11.
Specifically, after entering the light hydrocarbon extraction system 1, the raw material gas is first dehydrated by a dehydration device 11.
Pre-cooling: precooling is performed by using a precooling device 12.
Light hydrocarbon separation: light dydrocarbon separation is carried out by adopting a light dydrocarbon separation device 13 to obtain gas-phase substances and light dydrocarbon.
The gas phase substance enters the first cold source channel of the first heat exchange device 14, and at this time, the first medium channel of the first heat exchange device 14 has no medium yet, so that the gas phase substance directly enters the dry gas compression device 16, and the dry gas compression device 16 pressurizes the gas phase substance to obtain CNG.
The CNG enters the first medium channel of the first heat exchanging device 14, and the gas phase substance in the first cold source channel exchanges heat with the CNG to cool the CNG.
The cooled CNG is subjected to the throttling and cooling effects of the throttling device 17 to reduce the temperature to-80 ℃ to-90 ℃, and then enters the light hydrocarbon separation device 13 to provide cold for the separation of the light hydrocarbon separation device 13.
The gas phase substances separated by the light hydrocarbon separation device 13 continuously enter the first heat exchange device 14 and the dry gas compression devices 16 and … … to be circulated in sequence, so that the cold energy is fully utilized, and the energy consumption is saved.
Extracting CNG: and outputting the compressed CNG obtained by the dry gas compression device 16 to the outside to finish the extraction of the CNG.
The light hydrocarbon extraction method of the embodiment utilizes the dry gas compression device 16 to compress the gas-phase substances separated by the light hydrocarbon separation device 13 to obtain the CNG, utilizes the cold energy of the gas-phase substances to cool the CNG, throttles and cools the CNG after heat exchange through the first throttling device 17, and transmits the CNG to the light hydrocarbon separation device 13 to provide the cold energy for the light hydrocarbon separation device 13, thereby fully utilizing the cold energy, saving energy and reducing energy consumption.
Second embodiment
Referring to fig. 2, the light hydrocarbon extraction system 2 of the present embodiment is different from the first embodiment in that: light hydrocarbon extraction system 2 of this embodiment also includes second heat exchange device 25.
The second heat exchanging device 25 has a second cold source channel and a second medium channel, which can perform heat exchange, that is, the cold source in the second cold source channel performs heat exchange with the medium in the second medium channel, so that the cold source in the second cold source channel cools the medium in the second medium channel.
The inlet end of the second cold source channel is connected with the outlet end of the first cold source channel, and the outlet end of the second cold source channel is connected with the inlet end of the dry gas compression device 26, so that the outlet end of the first cold source channel is communicated with the inlet end of the dry gas compression device 26.
The inlet end of the second medium channel is connected with the outlet end of the dewatering device 21, and the outlet end of the second medium channel is connected with the inlet end of the precooling device 22, so that the outlet end of the dewatering device 21 is communicated with the inlet end of the precooling device 22.
Namely, after the gaseous phase substance generated after separation by the light hydrocarbon separation device 23 is used as the cold source of the first heat exchange device 24 to exchange heat, the temperature of the gaseous phase substance is still lower than the temperature of the dehydrated raw material gas, so that the gaseous phase substance can be continuously used as the cold source of the second heat exchange device, the dehydrated raw material gas is cooled, the cold quantity of the gaseous phase substance is fully utilized, the energy consumption is saved, and the dehydrated raw material gas is cooled to a certain extent, so that the dehydrated raw material gas entering the pre-cooling device 22 is pre-cooled to a certain extent, and the energy consumption of the pre-cooling device 22 is reduced.
Other features of the light hydrocarbon extraction system 2 in this embodiment can be found in the first embodiment and will not be described in detail.
The method for extracting light hydrocarbons by the light hydrocarbon extraction system 2 in this embodiment is as follows:
and (3) dehydrating: the raw material gas is dehydrated by a dehydration device 21.
Specifically, the raw material gas enters the light hydrocarbon extraction system 2 and is first dehydrated by the dehydration device 21.
Pre-cooling: and pre-cooling by using a second heat exchange device 25 and a pre-cooling device 22.
Specifically, the raw material gas dehydrated by the dehydrating device 21 enters the second medium channel of the second heat exchange device 25, and at this time, the second cold source channel has no cold source temporarily, so that the dehydrated raw material gas enters the pre-cooling device 22 and is pre-cooled by the pre-cooling device 22.
Light hydrocarbon separation: and separating by using a light hydrocarbon separation device 23 to obtain a gas-phase substance and light hydrocarbon.
The gas-phase substance enters the first cold source channel of the first heat exchanger 24, and at this time, the first medium channel of the first heat exchanger 24 has no medium, so that the gas-phase substance enters the second cold source channel of the second heat exchanger 25 and exchanges heat with the dehydrated raw material gas in the second medium channel, so that the temperature of the dehydrated raw material gas entering the pre-cooling device 22 is reduced, and the energy consumption of the pre-cooling device 22 is reduced.
The gas phase substance passes through the second heat exchange device 25 and then enters the dry gas compression device 26, and the dry gas compression device 26 pressurizes the gas phase substance to obtain CNG.
The CNG enters the first medium channel of the first heat exchanging device 24, and the gas phase substance in the first cold source channel exchanges heat with the CNG to cool the CNG.
The cooled CNG is subjected to throttling and cooling effects of the throttling device 27 to reduce the temperature to-80 ℃ to-90 ℃, and then enters the light hydrocarbon separation device 23 to provide cooling capacity for separation of the light hydrocarbon separation device 23.
The gas phase substances separated by the light hydrocarbon separation device 23 continuously enter the first heat exchange device 24, the second heat exchange device 25 and the dry gas compression devices 26 and … … to be circulated in sequence, so that the cold energy is fully utilized, and the energy consumption is saved.
Extracting CNG: and outputting the compressed CNG obtained by the dry gas compression device 26 to the outside, namely finishing the extraction of the CNG.
The light hydrocarbon extraction method of the embodiment utilizes the dry gas compression device 26 to compress the gas-phase substances separated by the light hydrocarbon separation device 23 to obtain the CNG, utilizes the cold energy of the gas-phase substances to cool the CNG, throttles and cools the CNG after heat exchange through the throttling device 27, and transmits the CNG to the light hydrocarbon separation device 23 to provide the cold energy for the light hydrocarbon separation device 23, thereby fully utilizing the cold energy, saving energy and reducing energy consumption. And the gas phase substance after passing through the first heat exchange device 24 continuously enters the second heat exchange device 25 to cool the dehydrated raw material gas, so that the temperature of the dehydrated raw material gas entering the pre-cooling device 22 is reduced, and the energy consumption of the pre-cooling device 22 is reduced.
Third embodiment
Referring to fig. 3, the light hydrocarbon extraction system 3 of the present embodiment is different from the second embodiment in that: light hydrocarbon separation unit 33 includes deethanizer 331 and separator 332.
The inlet end of the separator 332 is connected to the outlet end of the throttling device 37 to receive the liquid phase substance after being throttled and cooled by the throttling device 37, i.e. to receive the cooling energy.
The liquid phase outlet end of the separator 332 is connected with the recovery inlet end of the deethanizer 331, and the liquid phase substance separated by the separator 332 is delivered to the deethanizer 331, i.e., the liquid phase substance provides cold for the deethanizer 331.
The gas phase outlet end of the separator 332 is connected to the inlet end of the first cool source passage to supply the gas phase substance separated by the separator 332 to the first cool source passage.
The separator 332 separates the liquid entering the separator 332 to obtain a gas phase substance and a liquid phase substance. Wherein the gas phase material is mainly methane and a small amount of ethane, and the liquid phase material is mainly ethane. The gas phase substance is output from the gas phase outlet end and enters the first cold source channel, and cold energy is provided for the first cold source channel. The liquid phase material is output from the liquid phase outlet port into deethanizer 331.
This embodiment adds the separator 332 to the light hydrocarbon separation system relative to the second embodiment, further improving the separation efficiency.
The specific method for extracting light hydrocarbons by the light hydrocarbon extraction system 3 in this embodiment is as follows:
after entering the light hydrocarbon extraction system 3, the raw material gas is firstly dehydrated by the dehydration device 31, and then passes through the second medium channel of the second heat exchange device 35, and at this time, the second cold source channel has no cold source temporarily, so that the dehydrated raw material gas enters the pre-cooling device 32, and is pre-cooled by the pre-cooling device 32.
Then, the mixture enters a deethanizer 331 of a light hydrocarbon separation device 33, and the deethanizer 331 generates gas-phase substances and light hydrocarbons through separation. The gas phase substance enters the second cold source channel of the second heat exchanging device 35, and exchanges heat with the medium in the second medium channel, so that the temperature of the substance entering the pre-cooling device 32 is reduced, and the energy consumption of the pre-cooling device 32 is reduced.
The gas phase substance passes through the second heat exchange device 35 and then enters the dry gas compression device 36, and the dry gas compression device 36 pressurizes the gas phase substance to obtain CNG.
The CNG enters the first medium channel of the first heat exchanging device 34, and the gas phase substance in the first cool source channel exchanges heat with the CNG to cool the CNG.
The cooled CNG is throttled and cooled by the throttling device 37 to reduce the temperature to-80 ℃ to-90 ℃, and then enters the separator 332 of the light hydrocarbon separation device 33 to provide cold energy for the separation of the separator 332.
The separator 332 separates the gas-phase substance and the liquid-phase substance, and the gas-phase substance is conveyed to the first cold source channel of the first heat exchanging device to provide a cold source for the first cold source channel. The liquid phase substance separated by the separator 332 is transferred to the deethanizer 331 to provide refrigeration for the separation of the deethanizer 331.
The gas phase substances after the deethanization separation continuously enter the second heat exchange device 35 and the dry gas compression devices 36 and … … to be circulated in sequence, so that the cold energy is fully utilized, and the energy consumption is saved.
Namely, the medium cooled by the throttling device 37 is further separated by the separator 332 and then enters the deethanizer 331, so that the separation effect is improved.
Other features of the light hydrocarbon extraction system 3 in this embodiment can be referred to the second embodiment and will not be described in detail.
Fourth embodiment
Referring to fig. 4, the light hydrocarbon extraction system 4 of the present embodiment is different from the third embodiment in that: light hydrocarbon separation unit 43 includes a deethanizer 431 and a separator 432. The throttling means 47 is an ejector.
Further, a pressure reducing valve 433 is provided between the liquid phase outlet end of the separator 432 and the recovery inlet end of the deethanizer 431.
The throttling device 47 has an inlet end, a suction end and an outlet end. The inlet end of the throttling device 47 is connected with the outlet end of the first medium channel, the suction end of the throttling device 47 is connected with the gas phase outlet end of the deethanizer 431, and the outlet end of the throttling device 47 is connected with the inlet end of the separator 432 to provide cooling capacity for the separator 432. Compared to the third embodiment, the throttle device 47 of this embodiment has a suction port and can absorb the gas phase substances in the deethanizer 431, thereby reducing the pressure in the deethanizer 431 and improving the separation effect of the deethanizer 431.
In this implementation, the specific flow of extracting light hydrocarbons by the light hydrocarbon extraction system 4 is as follows:
after entering the light hydrocarbon extraction system 4, the raw material gas is firstly dehydrated by the dehydration device 41, and then passes through the second medium channel of the second heat exchange device 45, and at this time, the second cold source channel has no cold source temporarily, so that the dehydrated raw material gas enters the pre-cooling device 42, and is pre-cooled by the pre-cooling device 42.
Then, the mixture enters a deethanizer 431 of the light hydrocarbon separation device 43, and the deethanizer 431 is separated to generate gas-phase substances and light hydrocarbons. The vapor phase material enters the suction side of the throttling device 47, reducing the pressure within the deethanizer 431.
The separator 432 separates the substances entering the separator 432 to obtain gas-phase substances and liquid-phase substances, and the liquid-phase substances separated by the separator 432 enter the deethanizer 431 through the recovery inlet end of the deethanizer 431 to provide refrigeration for the deethanizer 431.
The gas phase substance separated by the separator 432 enters the first cold source channel of the first heat exchanging device 44, and at this time, the first medium channel of the first heat exchanging device 44 has no medium, so that the gas phase substance enters the second cold source channel of the second heat exchanging device 45 and exchanges heat with the medium in the second medium channel, so that the temperature of the substance entering the pre-cooling device 42 is reduced, and the energy consumption of the pre-cooling device 42 is reduced.
The gas phase substance passes through the second heat exchange device 45 and then enters the dry gas compression device 46, and the dry gas compression device 46 pressurizes the gas phase substance to obtain CNG.
The CNG output from the dry gas compression device 46 enters the first medium channel of the first heat exchange device 44, and the gas phase substance in the first cold source channel exchanges heat with the CNG to cool the CNG.
The cooled CNG is subjected to throttling and cooling effects of the throttling device 47 to reduce the temperature to-80 ℃ to-90 ℃, and then enters the separator 432 of the light hydrocarbon separation device 43 to provide cold for the separation of the light hydrocarbon separation system.
The gas phase substances separated by the deethanizer 431 continuously enter the throttling device 47, the separator 432, the first heat exchange device 44, the second heat exchange device 45 and the dry gas compression devices 46 and … …, and are circulated in sequence, so that the cold energy is fully utilized, and the energy consumption is saved.
Other features of the light hydrocarbon extraction system in this embodiment can be found in the third embodiment and will not be described in detail.
Fifth embodiment
Referring to fig. 5, the light hydrocarbon extraction system 5 of the present embodiment is different from the third embodiment in that: the light hydrocarbon separation device comprises a demethanizer 531, a deethanizer 532, a heat exchange device 533 and a separator 534.
The heat exchanging device 533 has a third cool source passage and a third medium passage capable of exchanging heat. The inlet end of the third cold source channel is connected to the liquid phase outlet end of the demethanizer 531, and the outlet end of the third cold source channel is connected to the first inlet end of the deethanizer 532. The inlet end of the third media path is connected to the gas phase outlet end of deethanizer 532, and the outlet end of the third media path is connected to the inlet end of de-separator 534. Namely, the liquid phase substance output from the liquid phase outlet end of the demethanizer 531 cools the gas phase substance at the gas phase outlet end of the deethanizer 532, thereby fully utilizing the cold energy and saving the energy consumption.
The specific flow of extracting light hydrocarbons by the light hydrocarbon extraction system 5 in this embodiment is as follows:
after entering the light hydrocarbon extraction system 5, the raw material gas is firstly dehydrated by the dehydration device 51, and then passes through the second medium channel of the second heat exchange device 55, and at this time, the second cold source channel has no cold source temporarily, so that the dehydrated raw material gas enters the pre-cooling device 52, and is pre-cooled by the pre-cooling device 52.
Then, the mixture enters a demethanizer 531 of the light hydrocarbon separation device, and the demethanizer 531 performs separation to generate a gas phase substance and a liquid phase substance. The gas phase substance separated by the demethanizer 531 enters the first cold source channel of the first heat exchanger 54, and at this time, the first medium channel of the first heat exchanger 54 has no medium, so that the gas phase substance enters the second cold source channel of the second heat exchanger 55 and exchanges heat with the medium in the second medium channel, so that the temperature of the substance entering the pre-cooling device 52 is reduced, and the energy consumption of the pre-cooling device 52 is reduced.
The liquid phase substance of the demethanizer 531 enters the third cold source channel of the heat exchange device 533, and at this time, the third medium channel of the third heat exchange device has no medium yet, so that the liquid phase substance of the demethanizer 531 directly enters the deethanizer 532.
The deethanizer 532 is separated to obtain a gas phase substance and a light hydrocarbon, the gas phase substance of the deethanizer 532 enters a third medium channel of the third heat exchange device, exchanges heat with the liquid phase substance output from the demethanizer 531, and then enters the separator 534.
The separator 534 separates to obtain a gas-phase substance and a liquid-phase substance, and the gas-phase substance output from the separator 534 enters the second cold source channel of the second heat exchanging device 55 to provide cold. The liquid phase output from separator 534 enters deethanizer 532.
The gas phase substance output from the demethanizer 531 passes through the first heat exchanger 54 and the second heat exchanger 55 and then enters the dry gas compressor 56, and the dry gas compressor 56 pressurizes the gas phase substance to obtain CNG.
The CNG output from the dry gas compression device 56 enters the first medium channel of the first heat exchange device 54, and the gas-phase substance in the first cold source channel exchanges heat with the CNG to cool the CNG. Then further cooling the CNG to-80-90 ℃ by the throttling and cooling effects of the throttling device 57, and then entering the demethanizer 531 of the light hydrocarbon separation device to provide cooling capacity for the separation of the light hydrocarbon separation device
The gas phase substances separated by the demethanizer 531 continuously enter the first heat exchange device 54, the second heat exchange device 55 and the dry gas compression devices 56 and … … to be circulated in sequence, so that the cold energy is fully utilized, and the energy consumption is saved.
Other features of the light hydrocarbon extraction system 5 in this embodiment can be found in the third embodiment and will not be described in detail.
Sixth embodiment
Referring to fig. 6, the light hydrocarbon extraction system 6 of the present embodiment includes a dehydration device 61, a pre-cooling device 62, a light hydrocarbon separation device, a first heat exchange device 64, a second heat exchange device 65, a dry gas compression device 66, and a throttling device 67.
The difference from the fifth embodiment is: the throttling means 67 is an injector.
The throttle device 67 in this embodiment has an inlet end, a suction end and an outlet end. The inlet end of the throttling device 67 is connected to the outlet end of the first medium passage, and the outlet end of the throttling device 67 is connected to the recovery inlet end of the demethanizer 631.
The light hydrocarbon separation unit comprises a demethanizer 631, a deethanizer 632, a heat exchange device 633 and a separator 634. The light hydrocarbon separation device differs from the fourth embodiment in that the vapor phase outlet end of separator 634 is connected to the suction end of throttling device 67.
The specific method for extracting light hydrocarbons by the light hydrocarbon extraction system 6 in this embodiment is the same as that in the fourth embodiment, except that:
the vapor outlet of separator 634 is connected to the suction of throttling device 67 so that the vapor phase from separator 634 enters throttling device 67 and then to demethanizer 631.
Other features of the light hydrocarbon extraction system 6 in this embodiment can be found in the fifth embodiment and will not be described in detail.
In the light hydrocarbon extraction systems in the above embodiments, for the same amount of raw material gas, the energy consumption for extracting light hydrocarbon is from high to low in the order of the first embodiment > the second embodiment > the third embodiment > the fourth embodiment > the fifth embodiment > the sixth embodiment.
According to the technical scheme, the invention has the advantages and positive effects that:
the light hydrocarbon extraction system comprises a dehydration device, a precooling device, a light hydrocarbon separation device, a dry gas compression device, a first heat exchange device and a throttling device. The liquid phase outlet end of the light hydrocarbon separation device outputs light hydrocarbon, and the gas phase outlet end of the light hydrocarbon separation device outputs gas phase substances. The gas phase substance is compressed by the dry gas compression device to obtain CNG, and the gas phase substance enters the first cold source channel to serve as a cold source to cool the CNG, so that the cold energy of the gas phase substance is utilized, the energy is saved, and the energy consumption is reduced. The cooled CNG enters the light hydrocarbon separation device after the throttling and cooling effects of the throttling device, thereby providing cold for the light hydrocarbon separation device, saving energy and reducing energy consumption. And the more the cold energy in the light hydrocarbon separation device is, the lower the temperature in the light hydrocarbon separation device is, and the higher the extraction rate of the hydrocarbon is.
The light hydrocarbon extraction method has the advantages of simple process, low energy consumption and high light hydrocarbon extraction rate.
While the present invention has been described with reference to several exemplary embodiments, it is understood that the terminology used is intended to be in the nature of words of description and illustration, rather than of limitation. As the present invention may be embodied in several forms without departing from the spirit or essential characteristics thereof, it should also be understood that the above-described embodiments are not limited by any of the details of the foregoing description, but rather should be construed broadly within its spirit and scope as defined in the appended claims, and therefore all changes and modifications that fall within the meets and bounds of the claims, or equivalences of such meets and bounds are therefore intended to be embraced by the appended claims.
Claims (12)
1. A light hydrocarbon extraction system is characterized by comprising a dehydration device, a precooling device, a light hydrocarbon separation device, a dry gas compression device, a first heat exchange device and a throttling device;
the light hydrocarbon separation device is provided with a raw material gas inlet end, a recovery inlet end, a gas phase outlet end and a liquid phase outlet end;
the first heat exchange device is provided with a first cold source channel and a first medium channel which can exchange heat;
the inlet end of the dehydration device is used for connecting a raw material gas source, and the outlet end of the dehydration device is communicated with the inlet end of the precooling device;
the raw material gas inlet end of the light hydrocarbon separation device is connected with the outlet end of the precooling device, the liquid phase outlet end outputs light hydrocarbons outwards, and the gas phase outlet end outputs gas-phase substances;
the inlet end of the first cold source channel is connected with the gas phase outlet end to receive the gas phase substance; the outlet end of the first cold source channel is communicated with the inlet end of the dry gas compression device, the outlet end of the dry gas compression device is connected with the inlet end of the first medium channel, and the dry gas compression device pressurizes the gas-phase substances to form CNG and conveys the CNG to the first medium channel;
the inlet end of the throttling device is connected with the outlet end of the first medium channel, and the outlet end of the throttling device is connected with the recycling inlet end of the light hydrocarbon separation device, so that the cooling capacity is provided for the light hydrocarbon separation device after the CNG is throttled and cooled.
2. The light hydrocarbon extraction system of claim 1, further comprising a second heat exchange device; the second heat exchange device is provided with a second cold source channel and a second medium channel which can exchange heat;
the inlet end of the second cold source channel is connected with the outlet end of the first cold source channel, and the outlet end of the second cold source channel is connected with the inlet end of the dry gas compression device, so that the outlet end of the first cold source channel is communicated with the inlet end of the dry gas compression device;
the inlet end of the second medium channel is connected with the outlet end of the dewatering device, and the outlet end of the second medium channel is connected with the inlet end of the precooling device, so that the outlet end of the dewatering device is communicated with the inlet end of the precooling device.
3. The light hydrocarbon extraction system of claim 1, wherein the light hydrocarbon separation device comprises a deethanizer and the throttling device is a throttling expansion valve.
4. The light hydrocarbon extraction system of claim 3, wherein the light hydrocarbon separation unit further comprises a separator disposed between the deethanizer and the throttling device;
the separator is provided with an inlet end, a gas phase outlet end and a liquid phase outlet end, and the inlet end of the separator is connected with the outlet end of the throttling device to receive the throttled and cooled liquid phase substances; and the liquid phase outlet end of the separator is connected with the recovery inlet end of the deethanizer so as to send the liquid phase substances separated by the separator to the deethanizer and provide cold energy for the deethanizer.
5. The light hydrocarbon extraction system of claim 1, wherein the light hydrocarbon separation device comprises a demethanizer, a deethanizer, and a heat exchange unit, and the throttling device is a throttling expansion valve; the raw material gas inlet end, the gas phase outlet end and the recovery inlet end of the light hydrocarbon separation device are arranged on the demethanizer, and the liquid phase outlet end of the light hydrocarbon separation device is arranged on the deethanizer;
the demethanizer also has a liquid phase outlet end;
the deethanizer further has a first inlet end and a vapor phase outlet end;
the heat exchange equipment is provided with a third cold source channel and a third medium channel which can exchange heat;
the inlet end of the third cold source channel is connected with the liquid phase outlet end of the demethanizer so as to receive the liquid phase substance separated by the demethanizer; the outlet end of the third cold source channel is connected with the first inlet end of the deethanizer;
the inlet end of the third medium channel is connected with the gas-phase outlet end of the deethanizer so as to receive the gas-phase substances separated by the deethanizer; and the outlet end of the third medium channel is connected with the inlet end of the second cold source channel.
6. The light hydrocarbon extraction system of claim 5, wherein the light hydrocarbon separation unit further comprises a separator connected between the third heat exchanger and the deethanizer, the deethanizer further having a second inlet end;
the separator is provided with an inlet end, a gas-phase outlet end and a liquid-phase outlet end, the inlet end of the separator is connected with the outlet end of the third medium channel, the liquid-phase outlet end of the separator is connected with the second inlet end of the deethanizer, and the gas-phase outlet end of the separator is connected with the inlet end of the second cold source channel.
7. The light hydrocarbon extraction system of claim 1, wherein the light hydrocarbon separation unit comprises a deethanizer and a separator, and the throttling device is an ejector; the feed gas inlet end, the recovery inlet end, the gas phase outlet end and the liquid phase outlet end of the light hydrocarbon separation device are arranged on the deethanizer; the separator has a gas phase outlet end, a liquid phase outlet end and an inlet end; the throttling device is provided with an inlet end, a suction end and an outlet end;
the gas-phase outlet end of the deethanizer is connected with the suction end of the throttling device, and gas-phase substances are conveyed to the throttling device for depressurization;
the inlet end of the separator is connected with the outlet end of the throttling device so as to receive the liquid-phase substance which is throttled and cooled by the throttling device;
the gas phase outlet end of the separator is connected with the inlet end of the first cold source channel so as to provide the gas phase substances separated by the separator for the first cold source channel;
the liquid phase outlet end of the separator is connected with the recovery inlet end of the deethanizer so as to provide the deethanizer with the liquid phase substances separated by the separator.
8. The light hydrocarbon extraction system of claim 1, wherein the light hydrocarbon separation unit comprises a demethanizer, a deethanizer, a separator, and a heat exchange device; the raw gas inlet end, the gas phase outlet end and the recovery inlet end of the light hydrocarbon separation device are arranged on the demethanizer, and the liquid phase outlet end of the light hydrocarbon separation device is arranged on the deethanizer;
the demethanizer has a liquid phase outlet end;
the deethanizer has a first inlet end, a second inlet end, and a gas phase outlet end;
the separator has an inlet end, a gas phase outlet end, and a liquid phase outlet end;
the heat exchange equipment is provided with a third cold source channel and a third medium channel which can exchange heat;
the inlet end of the third cold source channel is connected with the liquid phase outlet end of the demethanizer so as to receive the liquid phase substance separated by the demethanizer; the outlet end of the third cold source channel is connected with the first inlet end of the deethanizer;
the inlet end of the third medium channel is connected with the gas-phase outlet end of the deethanizer so as to receive the gas-phase substances separated by the deethanizer; the outlet end of the third medium channel is connected with the inlet end of the separator;
the throttling device is an ejector and is provided with a suction end, an inlet end and an outlet end, the inlet end of the throttling device is connected with the outlet end of the first medium channel, the suction end of the throttling device is connected with the gas phase outlet end of the separator, and the outlet end of the throttling device is connected with the recovery inlet end of the demethanizer.
9. The light hydrocarbon extraction system of claim 1, wherein the outlet end of the dry gas compression device is further connected to a CNG extraction line for outputting CNG outwards; the CNG extraction pipeline is connected with the first medium channel of the first heat exchange device in parallel.
10. A light hydrocarbon extraction method is characterized by comprising the following steps:
and (3) dehydrating: dehydrating the raw material gas;
pre-cooling: pre-cooling the dehydrated feed gas;
light hydrocarbon separation: carrying out light hydrocarbon separation on the precooled feed gas to obtain a gas-phase substance and light hydrocarbon;
the gas phase substances are subjected to heat exchange and pressurization to obtain CNG, and the CNG is subjected to heat exchange cooling and throttling cooling to provide cooling capacity for a light hydrocarbon separation process.
11. The light hydrocarbon extraction process of claim 10, wherein,
in the pre-cooling step, the gas-phase substance and the dehydrated feed gas are subjected to heat exchange to provide part of cold energy for pre-cooling the dehydrated feed gas.
12. The light extraction method of claim 10, further comprising extraction of CNG: and (3) carrying out heat exchange and pressurization on the gas-phase substance to obtain CNG, and outputting the CNG outwards to finish the extraction of the CNG.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910713202.3A CN112300827A (en) | 2019-08-02 | 2019-08-02 | Light hydrocarbon extraction system and extraction method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910713202.3A CN112300827A (en) | 2019-08-02 | 2019-08-02 | Light hydrocarbon extraction system and extraction method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112300827A true CN112300827A (en) | 2021-02-02 |
Family
ID=74486554
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910713202.3A Pending CN112300827A (en) | 2019-08-02 | 2019-08-02 | Light hydrocarbon extraction system and extraction method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112300827A (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1169772A (en) * | 1994-11-10 | 1998-01-07 | 埃尔考公司 | Hydrocarbon gas processing method |
| US6604380B1 (en) * | 2002-04-03 | 2003-08-12 | Howe-Baker Engineers, Ltd. | Liquid natural gas processing |
| CN104792116A (en) * | 2014-11-25 | 2015-07-22 | 中国寰球工程公司 | System and technology for recycling ethane and light dydrocarbon above ethane from natural gas |
| CN210560264U (en) * | 2019-08-02 | 2020-05-19 | 中集安瑞科能源装备（苏州）有限公司 | Light hydrocarbon extraction system |
-
2019
- 2019-08-02 CN CN201910713202.3A patent/CN112300827A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1169772A (en) * | 1994-11-10 | 1998-01-07 | 埃尔考公司 | Hydrocarbon gas processing method |
| US6604380B1 (en) * | 2002-04-03 | 2003-08-12 | Howe-Baker Engineers, Ltd. | Liquid natural gas processing |
| CN104792116A (en) * | 2014-11-25 | 2015-07-22 | 中国寰球工程公司 | System and technology for recycling ethane and light dydrocarbon above ethane from natural gas |
| CN210560264U (en) * | 2019-08-02 | 2020-05-19 | 中集安瑞科能源装备（苏州）有限公司 | Light hydrocarbon extraction system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US6553784B2 (en) | Comprehensive natural gas processor | |
| CN103940199B (en) | Method and device for extracting ethane-mixed hydrocarbon from natural gas | |
| RU2671665C1 (en) | Installation for natural gas liquefaction and method for operation thereof (options) | |
| RU2562980C2 (en) | Device and method for gas condensate separation | |
| EP1565247A1 (en) | High pressure gas processing configurations and methods | |
| CN101625190A (en) | Mixed refrigerant re-circulated liquefaction process for precooling coalbed methane (CBM) by residual pressure of pressure swing adsorption (PSA) | |
| WO2015069138A2 (en) | Natural gas liquefaction method and unit | |
| EA009166B1 (en) | Method for transporting natural gas via main pipeline | |
| CN104513680A (en) | Technology and device for removing hydrogen and nitrogen from methane-rich gas through rectification and producing liquefied natural gas | |
| CN102288007B (en) | Natural-gas condensed-liquid recovery device and method using mixed light hydrocarbon as refrigerant | |
| CN210560264U (en) | Light hydrocarbon extraction system | |
| CN101126041B (en) | Cascade connection method for preparing liquefied natural gas | |
| US11946355B2 (en) | Method to recover and process methane and condensates from flare gas systems | |
| CN202924980U (en) | Natural gas liquefaction and heavy hydrocarbon treatment device | |
| EP3479037A1 (en) | System and method for producing liquefied natural gas | |
| CN205011721U (en) | Smart dewatering system of synthesis of LNGLPGNGL product is retrieved to saturation wet oil associated gas | |
| US11927391B2 (en) | Liquefaction of production gas | |
| CN112300827A (en) | Light hydrocarbon extraction system and extraction method | |
| AU2016324362A1 (en) | A method of preparing natural gas to produce liquid natural gas (lng) | |
| CA2935708C (en) | A method to recover and process methane and condensates from flare gas systems | |
| CN211847817U (en) | Associated gas light hydrocarbon recovery system for dry gas low-pressure expansion oil field | |
| CN211771091U (en) | Open refrigeration oil field associated gas light hydrocarbon recovery system | |
| CN112980489B (en) | Process method for recycling light hydrocarbons of associated gas of open refrigeration oilfield | |
| CN101290184A (en) | Chemical industry tail gas liquefied separation method and equipment | |
| RU2730773C1 (en) | Natural gas liquefaction device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |