CN111704518B - Device and method for controlling gaseous ethane condensation rate at top of deethanizer - Google Patents
Device and method for controlling gaseous ethane condensation rate at top of deethanizer Download PDFInfo
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- CN111704518B CN111704518B CN202010651165.0A CN202010651165A CN111704518B CN 111704518 B CN111704518 B CN 111704518B CN 202010651165 A CN202010651165 A CN 202010651165A CN 111704518 B CN111704518 B CN 111704518B
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- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 title claims abstract description 179
- 238000009833 condensation Methods 0.000 title claims abstract description 37
- 230000005494 condensation Effects 0.000 title claims abstract description 36
- 238000000034 method Methods 0.000 title claims abstract description 17
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims abstract description 322
- 239000007788 liquid Substances 0.000 claims abstract description 171
- 239000001294 propane Substances 0.000 claims abstract description 160
- 239000012071 phase Substances 0.000 claims abstract description 84
- 230000001105 regulatory effect Effects 0.000 claims abstract description 73
- 238000010992 reflux Methods 0.000 claims abstract description 62
- 239000007791 liquid phase Substances 0.000 claims abstract description 42
- 230000001276 controlling effect Effects 0.000 claims abstract description 26
- 238000001704 evaporation Methods 0.000 claims abstract description 11
- 230000008020 evaporation Effects 0.000 claims abstract description 10
- 150000002430 hydrocarbons Chemical class 0.000 claims description 78
- 239000004215 Carbon black (E152) Substances 0.000 claims description 76
- 229930195733 hydrocarbon Natural products 0.000 claims description 76
- 238000003860 storage Methods 0.000 claims description 20
- 238000002156 mixing Methods 0.000 claims description 15
- 239000002994 raw material Substances 0.000 claims description 14
- 239000000463 material Substances 0.000 claims description 9
- 238000012546 transfer Methods 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 230000001174 ascending effect Effects 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 5
- 238000005057 refrigeration Methods 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 49
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 22
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 9
- 239000005977 Ethylene Substances 0.000 description 9
- 239000003345 natural gas Substances 0.000 description 7
- 238000011084 recovery Methods 0.000 description 4
- 230000008859 change Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- -1 c4+ Chemical compound 0.000 description 1
- 239000009096 changqing Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- 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
-
- 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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4006—Temperature
-
- 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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4012—Pressure
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides a device and a method for controlling the condensation rate of gaseous ethane at the top of a deethanizer, wherein the device at least comprises the deethanizer, a propane evaporator, a gas-liquid separator and an ethane reflux pump, and the middle lower part of the deethanizer is externally connected with a bottom reboiler; the invention adopts a mode of controlling reflux quantity to indirectly control the temperature of gaseous ethane discharged from the tower; the condensation rate of gaseous ethane at the top of the tower is controlled by adopting a cascade regulation mode of the liquid level of the separator and the suction pressure of the propane compressor, and the heat exchange load is regulated by changing the evaporation pressure to regulate the heat exchange temperature difference by utilizing the principle that the refrigeration pressure of propane corresponds to the temperature one by one; the immersed evaporative condenser is arranged, the heat exchange tube array is totally submerged in liquid propane, and gaseous ethane at the top of the tower is cooled by virtue of evaporation of the propane; and (3) arranging a separator to separate the ethane at the top of the gas-liquid two-phase tower, pressurizing the liquid phase of the ethane separator by a reflux pump, and then completely returning the liquid phase of the ethane separator to the top of the deethanizer, wherein the gas phase of the ethane separator is completely used as ethane product for output.
Description
Technical Field
The invention belongs to the field of natural gas processing and treatment, and particularly relates to a device and a method for controlling the condensation rate of gaseous ethane at the top of a deethanizer.
Background
Ethane is a high-quality raw material of ethylene, the production cost of ethylene prepared by ethane pyrolysis is three molecules two of naphtha, the C2-C4 ratio of the international raw material of ethylene is about 48%, and the naphtha is the main material limited by the raw material in China. The ethane product is recovered from natural gas and used as a raw material for preparing ethylene by thermal cracking by a steam method, and has positive significance for improving the yield of ethylene products, reducing the energy consumption of ethylene devices and improving quality and efficiency.
In China, a plurality of enterprises begin to adopt construction projects with imported ethane as an ethylene raw material, the light weight of the ethylene raw material becomes a development trend, and ethylene is one of the most basic chemical raw materials in one country.
The deethanizer is one of key equipment in natural gas ethane recovery engineering, and has the main functions of completing ethane and C 3 + Separation of light hydrocarbon components, the equipment feed being C 2 + Mixed hydrocarbon, heated reboiling of heat conducting oil in the bottom reboiler and cooled reflux of propane evaporator in the top of tower to control the quality index of ethane in the top of tower and C in the bottom of tower 3 + The method is characterized in that the cooling of gaseous ethane at the top of a deethanizer is in a semi-condensation mode, the reflux quantity is condensation quantity, the reflux quantity influences the temperature of gaseous ethane at the top of the deethanizer, and uncondensed gaseous ethane is used as a product for output; the temperature of gaseous ethane at the top of the tower influences the quality index of ethane products, the conventional control mode is to control the condensing temperature which is related to the condensing amount, but the small temperature change of gaseous ethane at the top of the tower can cause larger change of the condensing amount due to higher ethane content, and the temperature detection is more stagnateThe resulting off-column temperature of gaseous ethane at the top of the column is difficult to stabilize.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a device and a method for controlling the gaseous ethane condensation rate at the top of a deethanizer, which can stably and accurately control the gaseous ethane condensation rate at the top of the deethanizer in natural gas ethane recovery engineering, thereby controlling the reflux quantity at the top of the deethanizer and the temperature at the top of the deethanizer and achieving the aim of controlling the quality index of ethane products.
The technical scheme adopted by the invention is as follows:
the device at least comprises a deethanizer, a propane evaporator, a gas-liquid separator and an ethane reflux pump, wherein a raw material inlet is arranged on the side wall of the middle upper part of the deethanizer, a tower top gas phase outlet is arranged at the tower top of the deethanizer, and a tower bottom C is arranged at the tower bottom 3 + The middle lower part of the deethanizer is externally connected with a tower bottom reboiler;
C 2 + the mixed hydrocarbon enters the deethanizer through a raw material inlet at the middle upper part of the deethanizer, and a gas phase outlet at the top of the deethanizer is connected with a propane evaporator and a gas-liquid separator in sequence through pipelines; the top of the gas-liquid separator is provided with a gas phase outlet, the bottom of the gas-liquid separator is provided with a liquid phase outlet, the gas phase outlet at the top of the gas-liquid separator is connected with an ethane storage tank through a pipeline, and the liquid phase outlet at the bottom of the gas-liquid separator is sequentially connected with an ethane reflux pump and a deethanizer through reflux pipelines; bottom C of deethanizer bottom 3 + The hydrocarbon mixture outlet is connected with C through a pipeline 3 + A hydrocarbon mixing spherical tank.
Further, the top of the tower bottom reboiler is provided with an oil inlet and a reboiling mixed hydrocarbon outlet, the bottom of the tower bottom reboiler is provided with an oil outlet and a reboiling mixed hydrocarbon inlet, the oil inlet of the tower bottom reboiler is connected with high-temperature heat conduction oil through an oil inlet pipeline, the oil outlet of the tower bottom reboiler is connected with low-temperature heat conduction oil through an oil outlet pipeline, and the reboiling mixed hydrocarbon inlet and the reboiling mixed hydrocarbon outlet of the tower bottom reboiler are respectively connected with a mixed hydrocarbon outlet and a mixed hydrocarbon return tower of the deethanizer;
further, a heat conduction oil temperature regulating valve and a tower kettle temperature detector are arranged on the oil inlet pipeline, one end of the tower kettle temperature detector is connected to the deethanizer, and the other end of the tower kettle temperature detector is connected with the heat conduction oil temperature regulating valve.
Further, a gas phase outlet is arranged at the top of the propane evaporator, a liquid phase inlet is arranged at the bottom of the propane evaporator, the liquid phase inlet at the bottom of the propane evaporator is connected with a liquid propane storage tank through a pipeline, the gas phase outlet at the top of the propane evaporator discharges gaseous propane through an exhaust pipeline, and a propane screw compressor is arranged on the exhaust pipeline.
Further, a propane liquid level meter and a propane liquid level regulating valve are arranged on a connecting pipeline between the liquid propane storage tank and the liquid phase inlet of the propane evaporator, one end of the propane liquid level meter is connected with the propane liquid level regulating valve, and one end of the propane liquid level meter is connected with the propane evaporator; a propane screw compressor slide valve is arranged on the propane screw compressor, and a propane pressure detector is connected between the propane evaporator and the propane screw compressor slide valve; the propane liquid level meter and the propane liquid level regulating valve form a liquid level regulating loop; the propane pressure detector and the propane screw compressor slide valve form a pressure regulating loop.
Further, an ethane liquid level meter and a propane pressure detector are arranged on the gas-liquid separator, and respectively form a control loop with a propane screw compressor slide valve.
Further, the gas-liquid separator is also connected with a vent line, and a constant-pressure vent valve is arranged on the vent line.
Further, an ethane gas pressure detector is also arranged on the gas-liquid separator, a pressure regulating valve is arranged on a connecting pipeline between a gas phase outlet of the gas-liquid separator and the ethane storage tank, and the ethane gas pressure detector, the pressure regulating valve and the constant pressure vent valve form a pressure regulating and protecting loop.
Further, a reflux flowmeter, a reflux flow regulating valve and a tower top temperature detector are arranged on a reflux pipeline between the outlet of the ethane reflux pump and the deethanizer, one end of the tower top temperature detector is connected to the reflux pipeline, and the other end of the tower top temperature detector is respectively connected with the reflux flow regulating valve and the reflux flowmeter;
bottom C of the deethanizer bottom 3 + Mixed hydrocarbon outlet and C 3 + A tower kettle liquid level meter and a liquid level regulating valve are arranged on a connecting pipeline between the hydrocarbon mixing spherical tanks, one end of the tower kettle liquid level meter is connected to the side wall of the bottom of the deethanizer, and the other end of the tower kettle liquid level meter is connected with the liquid level regulating valve.
A method for controlling the condensation rate of gaseous ethane at the top of a deethanizer, comprising the steps of:
s1, C is to be removed from the boundary region 2 + After the metering and adjustment of the mixed hydrocarbon, the mixed hydrocarbon is introduced into the upper middle part and the upper part of the deethanizer, C 2 + The mixed hydrocarbon is divided into gas-liquid two phases in the tower, the liquid phase descends and reversely contacts with the ascending gas phase to carry out mass transfer and heat transfer, the gas phase material flow is discharged from the top of the deethanizer, and the liquid phase material flow is discharged from the bottom of the deethanizer;
s2, detecting the temperature of a gas phase stream discharged from the top of the deethanizer tower in the step S1, introducing the gas phase stream into a propane evaporator for cooling, and changing the gas phase into gas-liquid two-phase ethane;
s3, introducing the gas-liquid two-phase ethane in the step S2 into a gas-liquid separator for separation, and separating into gaseous ethane and liquid ethane;
s4, introducing the liquid ethane in the step S3 into an ethane reflux pump for pressurization, and introducing the liquid ethane into the top of a deethanizer as reflux liquid after metering and adjusting;
s5, discharging the gaseous ethane in the step S3 from the top of the gas-liquid separator, and outputting the gaseous ethane to an ethane storage tank after pressure regulation;
s6, regulating the liquid phase flow discharged from the bottom of the deethanizer tower in the step S1 through a liquid level regulating valve, and then outputting the liquid phase flow to C 3 + A hydrocarbon mixing spherical tank.
Specifically, in the step S2, the gas phase stream discharged from the top of the deethanizer is cooled by liquid propane outside the boundary zone introduced into the propane evaporator, the temperature of the gas phase stream is reduced from 10 ℃ to 15 ℃ to 7 ℃ to 9 ℃ to become gas-liquid two phases, the temperature of the liquid propane is increased from 0 ℃ to 55 ℃ to 60 ℃ to become gaseous propane, and the gaseous propane is discharged after being pressurized by a propane screw compressor.
Further, C at the bottom of the deethanizer in the step S6 3 + Before the mixed hydrocarbon is discharged, a bottom reboiler externally connected to the middle and lower part of the debutanizer is used for heating the mixed hydrocarbon, and the temperature of the mixed hydrocarbon at the bottom is controlled to be 100-105 ℃.
By adopting the technical scheme, the invention has the following beneficial effects:
(1) The invention adopts a combined control mode, and adopts a mode of controlling reflux quantity to indirectly control the temperature of gaseous ethane discharged from the tower; the condensation rate of gaseous ethane at the top of the tower is controlled by adopting a cascade adjustment mode of the liquid level of the separator and the suction pressure of the propane screw compressor, and the heat exchange load is adjusted by changing the evaporation pressure to adjust the heat exchange temperature difference by utilizing the principle that the refrigeration pressure of propane corresponds to the temperature one by one; the immersed evaporative condenser is arranged, the heat exchange tube array is totally submerged in liquid propane, and gaseous ethane at the top of the tower is cooled by virtue of evaporation of the propane; and (3) arranging a separator to separate the ethane at the top of the gas-liquid two-phase tower, pressurizing the liquid phase of the ethane separator by a reflux pump, and then completely returning the liquid phase of the ethane separator to the top of the deethanizer, wherein the gas phase of the ethane separator is completely used as ethane product for output.
(2) The method for controlling the condensation rate of the gaseous ethane at the top of the deethanizer can accurately, rapidly and stably control the temperature of the gaseous ethane at the top of the deethanizer, thereby ensuring the quality index of ethane products and avoiding unstable condensation amount caused by the conventional condensation temperature control mode, and ensuring that the fluctuation of the gaseous ethane at the top of the deethanizer affects the stable operation of the deethanizer.
The foregoing description is only an overview of the technical solution of the present invention, and in order to make the technical means of the present invention more clearly understood, it can be implemented according to the content of the specification, and the following detailed description of the preferred embodiments of the present invention will be given with reference to the accompanying drawings.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings that are needed in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic illustration of the process flow of the present invention.
Reference numerals illustrate:
1、C 2 + mixing hydrocarbon; 2. a deethanizer; 3. a gaseous phase outlet at the top of the column; 4. a tower top temperature detector; 5. a reflux flow regulating valve; 6. a reflux flowmeter; 7. an exhaust line; 8. a propane evaporator; 9. a propane level gauge; 10. a propane level regulating valve; 11. a constant pressure vent valve; 12. a pressure regulating valve; 13. an ethane gas pressure detector; 14. a gas-liquid separator; 15. an ethane level gauge; 16. an ethane reflux pump; 17. a tower kettle temperature detector; 18. a mixed hydrocarbon outlet; 19. a mixed hydrocarbon return tower port; 20. a tower kettle liquid level gauge; 21. a propane pressure detector; 22. bottom C of tower 3 + A hydrocarbon mixing outlet; 23. a liquid level regulating valve; 24. a bottom reboiler; 25. a heat conducting oil temperature regulating valve; 26. c (C) 3 + A hydrocarbon mixing spherical tank; 27. low temperature heat conducting oil; 28. high-temperature heat conducting oil; 29. an ethane storage tank; 30. a vent line; 31. a liquid propane storage tank; 32. gaseous propane; 33. propane screw compressor; 34. propane screw compressor slide valve.
Detailed Description
Further advantages and effects of the present invention will become apparent to those skilled in the art from the disclosure of the present specification, by describing the embodiments of the present invention with specific examples.
The exemplary embodiments of the present invention will now be described with reference to the accompanying drawings, however, the present invention may be embodied in many different forms and is not limited to the examples described herein, which are provided to fully and completely disclose the present invention and fully convey the scope of the invention to those skilled in the art. The terminology used in the exemplary embodiments illustrated in the accompanying drawings is not intended to be limiting of the invention. In the drawings, like elements/components are referred to by like reference numerals.
Unless otherwise indicated, terms (including technical and scientific terms) used herein have the same meaning as commonly understood by one of ordinary skill in the art. In addition, it will be understood that terms defined in commonly used dictionaries should be interpreted as having a meaning that is consistent with their meaning in the context of the relevant art and will not be interpreted in an idealized or overly formal sense.
First embodiment:
the embodiment relates to a device for controlling the condensation rate of gaseous ethane at the top of a deethanizer, which at least comprises the deethanizer 2, a propane evaporator 8, a gas-liquid separator 14 and an ethane reflux pump 16, wherein the side wall of the upper middle part of the deethanizer 2 is provided with a raw material inlet, the top of the deethanizer 2 is provided with a top gas phase outlet 3, and the bottom of the deethanizer 2 is provided with a bottom C 3 + A mixed hydrocarbon outlet 22, and a bottom reboiler 24 is externally connected with the middle lower part of the deethanizer 2;
C 2 + the mixed hydrocarbon 1 enters the deethanizer 2 through a raw material inlet at the middle upper part of the deethanizer 2, and a tower top gas phase outlet 3 at the tower top of the deethanizer 2 is connected with a propane evaporator 8 and a gas-liquid separator 14 in sequence through pipelines; the top of the gas-liquid separator 14 is provided with a gas phase outlet, the bottom of the gas-liquid separator 14 is provided with a liquid phase outlet, the gas phase outlet at the top of the gas-liquid separator 14 is connected with an ethane storage tank 29 through a pipeline, and the liquid phase outlet at the bottom of the gas-liquid separator 14 is sequentially connected with an ethane reflux pump 16 and a deethanizer 2 through reflux pipelines; bottom C of deethanizer 2 bottom 3 + The hydrocarbon mixture outlet 22 is connected with C through a pipeline 3 + A hydrocarbon mixing spherical tank 26.
The invention adopts a combined control mode, and adopts a mode of controlling reflux quantity to indirectly control the temperature of gaseous ethane discharged from the tower; the condensation rate of gaseous ethane at the top of the tower is controlled by adopting a cascade regulation mode of the liquid level of the separator and the suction pressure of the propane compressor, and the heat exchange load is regulated by changing the evaporation pressure to regulate the heat exchange temperature difference by utilizing the principle that the refrigeration pressure of propane corresponds to the temperature one by one; the immersed evaporative condenser is arranged, the heat exchange tube array is totally submerged in liquid propane, and gaseous ethane at the top of the tower is cooled by virtue of evaporation of the propane; and (3) arranging a separator to separate the ethane at the top of the gas-liquid two-phase tower, pressurizing the liquid phase of the ethane separator by a reflux pump, and then completely returning the liquid phase of the ethane separator to the top of the deethanizer, wherein the gas phase of the ethane separator is completely used as ethane product for output.
Second embodiment:
the embodiment relates to a method for controlling the condensation rate of gaseous ethane at the top of a deethanizer, referring to fig. 1, comprising the following steps:
s1, C is to be removed from the boundary region 2 + After the mixed hydrocarbon 1 is metered and regulated, the mixed hydrocarbon is introduced into the upper middle part and the upper part of the deethanizer 2, C 2 + The mixed hydrocarbon 1 is divided into gas-liquid two phases in the tower, the liquid phase descends and contacts with ascending gas phase reversely to transfer mass and heat, the gas phase material flow is discharged from the top of the deethanizer 2, and the liquid phase material flow is discharged from the bottom of the deethanizer;
s2, detecting the temperature of a gas phase stream discharged from the top of the deethanizer 2 in the step S1, introducing the gas phase stream into a propane evaporator 8 for cooling, and changing the gas phase into gas-liquid two-phase ethane;
s3, introducing the gas-liquid two-phase ethane in the step S2 into a gas-liquid separator 14 for separation, and separating the gas-liquid two-phase ethane into gaseous ethane and liquid ethane;
s4, introducing the liquid ethane in the step S3 into an ethane reflux pump 16 for pressurization, and introducing the liquid ethane into the top of the deethanizer 2 as reflux liquid after metering and adjusting;
s5, discharging the gaseous ethane in the step S3 from the top of the gas-liquid separator 14, and outputting the gaseous ethane to an ethane storage tank 29 after pressure adjustment;
s6, regulating the liquid phase flow discharged from the bottom of the deethanizer 2 in the step S1 through a liquid level regulating valve 23, and then outputting the liquid phase flow to C 3 + A hydrocarbon mixing spherical tank 26.
The method for controlling the condensation rate of the gaseous ethane at the top of the deethanizer can accurately, rapidly and stably control the temperature of the gaseous ethane at the top of the deethanizer, thereby ensuring the quality index of ethane products, avoiding unstable condensation amount caused by the conventional condensing temperature control mode, and ensuring that the fluctuation of the gaseous ethane at the top of the deethanizer affects the stable operation of the deethanizer.
Third embodiment:
on the basis of the first embodiment, further, an oil inlet and a reboiling mixed hydrocarbon outlet are formed in the top of the bottom reboiler 24, an oil outlet and a reboiling mixed hydrocarbon inlet are formed in the bottom of the bottom reboiler 24, the oil inlet of the bottom reboiler 24 is connected with high-temperature heat-conducting oil 28 through an oil inlet pipeline, the oil outlet of the bottom reboiler 24 is connected with low-temperature heat-conducting oil 27 through an oil outlet pipeline, and the reboiling mixed hydrocarbon inlet and the reboiling mixed hydrocarbon outlet of the bottom reboiler 24 are respectively connected with the mixed hydrocarbon outlet 18 and the mixed hydrocarbon return port 19 of the deethanizer 2;
the oil inlet pipeline is provided with a heat-conducting oil temperature regulating valve 25 and a tower kettle temperature detector 17, one end of the tower kettle temperature detector 17 is connected to the deethanizer 2, the other end of the tower kettle temperature detector 17 is connected with the heat-conducting oil temperature regulating valve 25, and the tower kettle temperature detector 17 and the heat-conducting oil temperature regulating valve 25 form a temperature regulating loop.
Further, a gas phase outlet is arranged at the top of the propane evaporator 8, a liquid phase inlet is arranged at the bottom of the propane evaporator 8, the liquid phase inlet at the bottom of the propane evaporator 8 is connected with a liquid propane storage tank 31 through a pipeline, the gas phase outlet at the top of the propane evaporator 8 is used for exhausting gaseous propane 32 through an exhaust pipeline 7, and a propane screw compressor 33 is arranged on the exhaust pipeline 7.
A propane liquid level meter 9 and a propane liquid level regulating valve 10 are arranged on a connecting pipeline between the liquid propane storage tank 31 and a liquid phase inlet of the propane evaporator 8, and the propane liquid level meter 9 is arranged between the propane evaporator 8 and the propane liquid level regulating valve 10; a propane screw compressor slide valve 34 is arranged on the propane screw compressor 33, and a propane pressure detector 21 is connected between the propane evaporator 8 and the propane screw compressor slide valve 34; specifically, the liquid propane storage tank 31, the propane liquid level regulating valve 10, the propane evaporator 8, the propane screw compressor slide valve 34, the propane screw compressor 33 and the high-pressure gaseous propane 32 are connected end to end through pipelines; the propane liquid level meter 9 and the propane liquid level regulating valve 10 form a liquid level regulating loop; the propane pressure detector 21 and the propane screw compressor slide valve 34 constitute a pressure regulating circuit.
Further, an ethane liquid level meter 15 is installed on the gas-liquid separator 14, and the ethane liquid level meter and the propane pressure detector respectively form a control loop with a slide valve of the propane screw compressor.
Further, a vent line 30 is further connected to the gas-liquid separator 14, and a constant pressure vent valve 11 is installed on the vent line 30. The gas-liquid separator 14 is also provided with an ethane gas pressure detector 13, a pressure regulating valve 12 is arranged on a connecting pipeline between a gas phase outlet of the gas-liquid separator 14 and the ethane storage tank 29, and the ethane gas pressure detector 13, the pressure regulating valve 12 and the constant pressure emptying valve 11 form a pressure regulating and protecting loop.
Further, a reflux flowmeter 6, a reflux flowmeter regulating valve 5 and a tower top temperature detector 4 are arranged on a reflux pipeline between the outlet of the ethane reflux pump 16 and the deethanizer 2, one end of the tower top temperature detector 4 is connected to the reflux pipeline, and the other end of the tower top temperature detector 4 is respectively connected with the reflux flowmeter 6 and the reflux flowmeter 5; specifically, the deethanizer 2, the overhead gas phase outlet 3, the overhead temperature detector 4, the propane evaporator 8, the gas-liquid separator 14, the ethane reflux pump 16, the reflux flowmeter 6 and the reflux flow regulating valve 5 are connected with the deethanizer 2 end to end through pipelines; the tower top temperature detector 4, the reflux flow rate regulating valve 5 and the reflux flow rate meter 6 form a cascade regulating loop.
Bottom C of the deethanizer 2 bottom 3 + Mixing hydrocarbon outlet 22 with C 3 + A tower kettle liquid level meter 20 and a liquid level regulating valve 23 are arranged on a connecting pipeline between the hydrocarbon mixing spherical tanks 26, one end of the tower kettle liquid level meter 20 is connected to the side wall of the bottom of the deethanizer 2, the other end of the tower kettle liquid level meter 20 is connected with the liquid level regulating valve 23, and the tower kettle liquid level meter 20 and the liquid level regulating valve 23 form a liquid level regulating loop.
The device for controlling the condensation rate of the gaseous ethane at the top of the deethanizer in the natural gas ethane recovery engineering provided by the invention can accurately, rapidly and stably control the temperature of the gaseous ethane at the top of the deethanizer, thereby ensuring the quality index of ethane products, avoiding the instability of condensation amount caused by the conventional condensation temperature control mode, and influencing the stable operation of the deethanizer due to the fluctuation of the temperature of the gaseous ethane at the outlet of the deethanizer.
Fourth embodiment:
the embodiment relates to a method for controlling the condensation rate of gaseous ethane at the top of a deethanizer, which comprises the following steps:
s1, C is to be removed from the boundary region 2 + After the mixed hydrocarbon 1 is metered and regulated, the mixed hydrocarbon is introduced into the upper middle part and the upper part of the deethanizer 2, C 2 + The mixed hydrocarbon 1 is divided into gas-liquid two phases in the tower, the liquid phase descends and reversely contacts with ascending gas phase to transfer mass and heat, and the gas phase ascends and reversely contacts with descending liquid phase to transfer mass and heat;
s2, detecting the temperature of a gas phase stream discharged from the top of the deethanizer 2 in the step S1, introducing the gas phase stream into a propane evaporator 8 for cooling, and changing the gas phase into gas-liquid two-phase ethane; specifically, the gas phase stream discharged from the top of the deethanizer 2 is cooled by liquid propane outside the boundary zone introduced into the propane evaporator 8, the temperature of the gas phase stream is reduced from 10-15 ℃ to 7-9 ℃ to become gas-liquid two phases, the temperature of the liquid propane is increased from 0 ℃ to 55-60 ℃ to become gaseous propane 32, and the gaseous propane 32 is discharged after being pressurized by a propane screw compressor 33;
s3, introducing the gas-liquid two-phase ethane in the step S2 into a gas-liquid separator 14 for separation, and separating the gas-liquid two-phase ethane into gaseous ethane and liquid ethane;
s4, introducing the liquid ethane in the step S3 into an ethane reflux pump 16 for pressurization, and introducing the liquid ethane into the top of the deethanizer 2 as reflux liquid after metering and adjusting;
s5, discharging the gaseous ethane in the step S3 from the top of the gas-liquid separator 14, and outputting the gaseous ethane to an ethane storage tank 29 after pressure adjustment;
s6, regulating the liquid phase flow discharged from the bottom of the deethanizer 2 in the step S1 through a liquid level regulating valve 23, and then outputting the liquid phase flow to C 3 + A hydrocarbon mixing spherical tank 26. It is worth mentioning C at the bottom of deethanizer 2 3 + Before the mixed hydrocarbon is discharged, the mixed hydrocarbon is heated by a bottom reboiler 24 externally connected to the middle and lower part of the debutanizer 2, and the temperature of the mixed hydrocarbon at the bottom is controlled to be 100-105 ℃.
C is the same as 2 + The mixed hydrocarbon is composed of ethane, propane and the likeAlkane, c4+, methane and CO2, wherein the ethane volume content is 69.62%, the propane volume content is 12.5%, the c4+ volume content is 6.25%, the methane volume content is 0.09% and the CO2 volume content is 10.71%, the pressure is 3.05MPa, and the temperature is 32 ℃.
The export gaseous ethane consisted of ethane, propane, c4+, methane and CO2, wherein the ethane volume content 83.45%, propane volume content 2.56%, c4+ volume content 0.0021%, methane volume content 1.08% and CO2 volume content 12.88%, the pressure was 3.00MPa and the temperature was 8.5 ℃.
C 3 + The hydrocarbon mixture consisted of propane, ethane and C4+, which had a propane volume content of 61.45%, an ethane volume content of 1.53% and a C4+ mass content of 37.03%, and a pressure of 3.05MPa, at a temperature of 105 ℃.
The pressure of the high-temperature heat conduction oil from outside the boundary is 0.4 MPa, the temperature is 230 ℃, and the temperature of the low-temperature heat conduction oil discharged from the device is not lower than 180 ℃.
Liquid propane from outside the boundary, the pressure is 1.3MPa, and the temperature is 0 ℃; the gaseous propane pressure of the outlet device is 1.3MPa, and the temperature is 60 ℃.
Fifth embodiment:
the embodiment relates to a method for controlling the condensation rate of gaseous ethane at the top of a deethanizer, which comprises the following steps:
s1, C is to be removed from the boundary region 2 + After the mixed hydrocarbon 1 is metered and regulated, the mixed hydrocarbon is introduced into the upper middle part and the upper part of the deethanizer 2, C 2 + The mixed hydrocarbon 1 is divided into gas-liquid two phases in the tower, the liquid phase descends and reversely contacts with ascending gas phase to transfer mass and heat, and the gas phase ascends and reversely contacts with descending liquid phase to transfer mass and heat;
s2, detecting the temperature of a gas phase stream discharged from the top of the deethanizer 2 in the step S1, introducing the gas phase stream into a propane evaporator 8 for cooling, and cooling the gas phase stream from 12.15 ℃ to 8.5 ℃, wherein the gas phase stream is changed into gas-liquid two phases, and the liquefaction rate is 49%;
s3, introducing the gas-liquid two-phase ethane in the step S2 into a gas-liquid separator 14 for separation, and separating the gas-liquid two-phase ethane into gaseous ethane and liquid ethane;
s4, introducing the liquid ethane in the step S3 into an ethane reflux pump 16 for pressurization, and introducing the liquid ethane into the top of the deethanizer 2 as reflux liquid after metering and adjusting;
s5, discharging the gaseous ethane in the step S3 from the top of the gas-liquid separator 14, and outputting the gaseous ethane to an ethane storage tank 29 after pressure adjustment;
s6, regulating the liquid phase flow discharged from the bottom of the deethanizer 2 in the step S1 through a liquid level regulating valve 23, and then outputting the liquid phase flow to C 3 + A hydrocarbon mixing spherical tank 26;
s7, introducing liquid propane outside the boundary area into a propane evaporator after passing through a liquid level regulating valve, evaporating the liquid propane into gaseous propane, and discharging the gaseous propane out of the propane evaporator;
s8, introducing the gaseous propane discharged in the step S7 into a propane screw compressor 33 for pressurization, wherein the pressure is increased from 300kPa to 1.3MPa, and the pressure of the inlet gaseous propane is controlled by a propane screw compressor slide valve 34;
s9, high-temperature heat conduction oil 28 outside the boundary area enters a reboiler 24 at the bottom of the deethanizer 2, a temperature regulating valve is arranged to heat mixed hydrocarbon at the bottom of the deethanizer, and the temperature of the mixed hydrocarbon at the bottom is controlled to be 105 ℃.
Application of the embodiment in actual production:
the natural gas treatment capacity of raw material of ancient natural gas treatment general factories in Changqing oilfield is 6000 multiplied by 104m3/d, the incoming gas pressure is 4.1MPa, the temperature is 7 ℃ to 26 ℃, 4 sets of liquid hydrocarbon recovery treatment devices with the same scale are arranged, and the treatment scale of a single set reaches 1500 multiplied by 104m3/d.
In summary, the invention adopts a mode of controlling reflux quantity to indirectly control the temperature of gaseous ethane discharged from the tower; the condensation rate of gaseous ethane at the top of the tower is controlled by adopting a cascade adjustment mode of the liquid level of the separator and the suction pressure of the propane screw compressor, and the heat exchange load is adjusted by changing the evaporation pressure to adjust the heat exchange temperature difference by utilizing the principle that the refrigeration pressure of propane corresponds to the temperature one by one; the immersed evaporative condenser is arranged, the heat exchange tube array is totally submerged in liquid propane, and gaseous ethane at the top of the tower is cooled by virtue of evaporation of the propane; and (3) arranging a separator to separate the ethane at the top of the gas-liquid two-phase tower, pressurizing the liquid phase of the ethane separator by a reflux pump, and then completely returning the liquid phase of the ethane separator to the top of the deethanizer, wherein the gas phase of the ethane separator is completely used as ethane product for output.
The device for controlling the condensation rate of the gaseous ethane at the top of the deethanizer can accurately, rapidly and stably control the temperature of the gaseous ethane at the top of the deethanizer, thereby ensuring the quality index of ethane products and avoiding unstable condensation amount caused by the conventional condensation temperature control mode, and ensuring that the fluctuation of the gaseous ethane at the top of the deethanizer affects the stable operation of the deethanizer.
The foregoing description is of the preferred embodiments of the invention and the invention is not to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein. Any simple modification, equivalent variation and modification of the above embodiments according to the technical substance of the present invention still fall within the scope of the technical solution of the present invention.
Claims (8)
1. The device for controlling the condensation rate of gaseous ethane at the top of a deethanizer is characterized in that: the device at least comprises a deethanizer (2), a propane evaporator (8), a gas-liquid separator (14) and an ethane reflux pump (16), wherein a raw material inlet is arranged on the side wall of the middle upper part of the deethanizer (2), a tower top gas phase outlet (3) is arranged at the tower top of the deethanizer (2), and a tower bottom C is arranged at the tower bottom 3 + A mixed hydrocarbon outlet (22), and a bottom reboiler (24) is externally connected with the middle lower part of the deethanizer (2);
C 2 + the mixed hydrocarbon (1) enters the deethanizer (2) through a raw material inlet at the middle upper part of the deethanizer (2), and a tower top gas phase outlet (3) at the tower top of the deethanizer (2) is sequentially connected with a propane evaporator (8) and a gas-liquid separator (14) through pipelines; the top of the gas-liquid separator (14) is provided with a gas phase outlet, the bottom of the gas-liquid separator (14) is provided with a liquid phase outlet, the gas phase outlet at the top of the gas-liquid separator (14) is connected with an ethane storage tank (29) through a pipeline, and the liquid phase outlet at the bottom of the gas-liquid separator (14) is sequentially connected with an ethane reflux pump (16) and a deethanizer (2) through reflux pipelines; bottom C of deethanizer (2) 3 + The hydrocarbon mixture outlet (22) is connected with C through a pipeline 3 + A hydrocarbon mixing spherical tank (26);
the propane evaporator (8) is an immersed evaporation condenser, the heat exchange tubes are all submerged in liquid propane, and gaseous ethane at the top of the tower is cooled by means of evaporation of propane; the top of the propane evaporator (8) is provided with a gas phase outlet, the gas phase outlet at the top of the propane evaporator (8) is used for exhausting gaseous propane (32) through an exhaust pipeline (7), a propane screw compressor (33) is installed on the exhaust pipeline (7), a propane screw compressor slide valve (34) is arranged on the propane screw compressor (33), a propane pressure detector (21) is connected between the propane evaporator (8) and the propane screw compressor slide valve (34), and the propane pressure detector (21) and the propane screw compressor slide valve (34) form a pressure regulating loop;
the bottom of the propane evaporator (8) is provided with a liquid phase inlet, the liquid phase inlet at the bottom of the propane evaporator (8) is connected with a liquid propane storage tank (31) through a pipeline, a propane liquid level meter (9) and a propane liquid level regulating valve (10) are arranged on a connecting pipeline between the liquid propane storage tank (31) and the liquid phase inlet of the propane evaporator (8), one end of the propane liquid level meter (9) is connected with the propane liquid level regulating valve (10), and one end of the propane liquid level meter (9) is connected with the propane evaporator (8); the propane liquid level meter (9) and the propane liquid level regulating valve (10) form a liquid level regulating loop;
an ethane liquid level meter (15) is arranged on the gas-liquid separator (14), and the ethane liquid level meter (15) and a propane pressure detector (21) and a propane screw compressor slide valve (34) respectively form a control loop;
and a reflux flowmeter (6), a reflux flow regulating valve (5) and a tower top temperature detector (4) are arranged on a reflux pipeline between the outlet of the ethane reflux pump (16) and the deethanizer (2), and the tower top temperature detector (4), the reflux flow regulating valve (5) and the reflux flowmeter (6) form a cascade regulating loop.
2. The apparatus for controlling the condensation rate of gaseous ethane at the top of a deethanizer as claimed in claim 1, wherein: the top of the tower bottom reboiler (24) is provided with an oil inlet and a reboiling mixed hydrocarbon outlet, the bottom of the tower bottom reboiler (24) is provided with an oil outlet and a reboiling mixed hydrocarbon inlet, the oil inlet of the tower bottom reboiler (24) is connected with high-temperature heat-conducting oil (28) through an oil inlet pipeline, the oil outlet of the tower bottom reboiler (24) is connected with low-temperature heat-conducting oil (27) through an oil outlet pipeline, and the reboiling mixed hydrocarbon inlet and the reboiling mixed hydrocarbon outlet of the tower bottom reboiler (24) are respectively connected with a mixed hydrocarbon outlet (18) and a mixed hydrocarbon return opening (19) of the deethanizer (2);
the oil inlet pipeline is provided with a heat conduction oil temperature regulating valve (25) and a tower kettle temperature detector (17), one end of the tower kettle temperature detector (17) is connected to the deethanizer (2), and the other end of the tower kettle temperature detector (17) is connected with the heat conduction oil temperature regulating valve (25).
3. The apparatus for controlling the condensation rate of gaseous ethane at the top of a deethanizer as claimed in claim 1, wherein: the gas-liquid separator (14) is also connected with a vent pipeline (30), and a constant-pressure vent valve (11) is arranged on the vent pipeline (30).
4. A deethanizer overhead gaseous ethane condensation rate control apparatus according to claim 3, wherein: an ethane gas pressure detector (13) is further arranged on the gas-liquid separator (14), a pressure regulating valve (12) is arranged on a connecting pipeline between a gas phase outlet of the gas-liquid separator (14) and the ethane storage tank (29), and the ethane gas pressure detector (13), the pressure regulating valve (12) and the constant pressure emptying valve (11) form a pressure regulating and protecting loop.
5. The apparatus for controlling the condensation rate of gaseous ethane at the top of a deethanizer as claimed in claim 1, wherein: one end of the tower top temperature detector (4) is connected to the return pipeline, and the other end of the tower top temperature detector (4) is respectively connected with the reflux flow regulating valve (5) and the reflux flow meter (6); the deethanizer column(2) Bottom C of the bottom 3 + A hydrocarbon mixture outlet (22) and C 3 + A tower kettle liquid level meter (20) and a liquid level regulating valve (23) are arranged on a connecting pipeline between the hydrocarbon mixing spherical tanks (26), one end of the tower kettle liquid level meter (20) is connected to the side wall of the bottom of the deethanizer (2), and the other end of the tower kettle liquid level meter (20) is connected with the liquid level regulating valve (23).
6. A method of controlling the gaseous ethane condensation rate at the top of a deethanizer using the gaseous ethane condensation rate control device at the top of the deethanizer according to any one of claims 1 to 5, characterized by comprising the steps of:
s1, C is to be removed from the boundary region 2 + After the metering and adjustment of the mixed hydrocarbon (1), the mixed hydrocarbon is introduced into the middle upper part of the deethanizer (2), C 2 + The mixed hydrocarbon (1) is divided into gas-liquid two phases in the tower, the liquid phase descends and reversely contacts with the ascending gas phase to carry out mass transfer and heat transfer, the gas phase material flow is discharged from the top of the deethanizer (2), and the liquid phase material flow is discharged from the bottom of the deethanizer;
s2, detecting the temperature of a gas phase stream discharged from the top of the deethanizer (2) in the step S1, introducing the gas phase stream into a propane evaporator (8) for cooling, and changing the gas phase into gas-liquid two-phase ethane;
s3, introducing the gas-liquid two-phase ethane in the step S2 into a gas-liquid separator (14) for separation, and separating the gas-liquid two-phase ethane into gaseous ethane and liquid ethane;
s4, introducing the liquid ethane in the step S3 into an ethane reflux pump (16) for pressurization, and introducing the liquid ethane into the top of a deethanizer (2) as reflux liquid after metering and adjustment;
s5, discharging the gaseous ethane in the step S3 from the top of the gas-liquid separator (14) and outputting the gaseous ethane to an ethane storage tank (29) after pressure regulation;
s6, the liquid phase flow discharged from the bottom of the deethanizer (2) in the step S1 is regulated by a liquid level regulating valve (23) and then is externally conveyed to C 3 + A hydrocarbon mixing spherical tank (26).
7. The method for controlling the condensation rate of gaseous ethane at the top of a deethanizer according to claim 6, wherein: in the step S2, the gas phase material flow discharged from the top of the deethanizer (2) is cooled by liquid propane outside the boundary zone introduced into the propane evaporator (8), the temperature of the gas phase material flow is reduced from 10-15 ℃ to 7-9 ℃ to become gas-liquid two phases, the temperature of the liquid propane is increased from 0 ℃ to 55-60 ℃ to become gaseous propane (32), and the gaseous propane (32) is discharged after being pressurized by a propane screw compressor (33).
8. The method for controlling the condensation rate of gaseous ethane at the top of a deethanizer according to claim 6, wherein: c at the bottom of the deethanizer (2) in the step S6 3 + Before the mixed hydrocarbon is discharged, a bottom reboiler (24) externally connected to the middle and lower parts of the deethanizer (2) heats the mixed hydrocarbon, and the temperature of the mixed hydrocarbon at the bottom is controlled to be 100-105 ℃.
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| CN207299714U (en) * | 2017-10-12 | 2018-05-01 | 中国石油工程建设有限公司 | A kind of natural gas ethane recovery device using cascade refrigeration |
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| RU2217668C2 (en) * | 2001-12-19 | 2003-11-27 | Общество с ограниченной ответственностью "Оренбурггазпром" | Method of processing hydrocarbon raw material |
| CN101205484A (en) * | 2007-11-27 | 2008-06-25 | 中国海洋石油总公司 | Three-in-one stable treatment technique for crude oil |
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| CN107560319A (en) * | 2017-10-12 | 2018-01-09 | 中国石油工程建设有限公司 | A kind of natural gas ethane recovery device and method using cascade refrigeration |
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