CN212425914U - Device for controlling condensation rate of gaseous ethane at top of deethanizer - Google Patents
Device for controlling condensation rate of gaseous ethane at top of deethanizer Download PDFInfo
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- CN212425914U CN212425914U CN202021323694.XU CN202021323694U CN212425914U CN 212425914 U CN212425914 U CN 212425914U CN 202021323694 U CN202021323694 U CN 202021323694U CN 212425914 U CN212425914 U CN 212425914U
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Abstract
The utility model provides a device for controlling the condensation rate of gaseous ethane at the top of a deethanizer, which at least comprises a deethanizer, a propane evaporator, a gas-liquid separator and an ethane reflux pump, wherein a tower bottom reboiler is externally connected to the middle-lower part of the deethanizer; the utility model adopts the mode of controlling the reflux quantity to indirectly control the temperature of the gaseous ethane discharged from the tower; the liquid level of the separator and the suction pressure cascade regulation mode of the propane compressor are adopted to control the condensation rate of the gaseous ethane at the tower top, the principle that the refrigeration pressure and the temperature of propane correspond to each other one by one is utilized, and the heat exchange load is regulated in a way of changing the evaporation pressure and adjusting the heat exchange temperature difference; an immersed evaporation condenser is arranged, the heat exchange tubes are totally immersed in liquid propane, and the gaseous ethane at the top of the tower is cooled by virtue of the evaporation of the propane; and a separator is arranged to separate ethane at the top of the gas-liquid two-phase tower, the liquid phase of the ethane separator is pressurized by a reflux pump and then returns to the top of the deethanizer, and the gas phase of the ethane separator is used as an ethane product for outward transportation.
Description
Technical Field
The utility model belongs to natural gas processing field, concretely relates to device of deethanizer tower top gaseous state ethane condensation rate control.
Background
Ethane is a high-quality raw material of ethylene, the production cost of ethylene prepared by cracking ethane is two thirds of that of naphtha, the ethylene raw material C2-C4 accounts for about 48% internationally, and China is restricted by the raw materials and mainly uses naphtha. The ethane product is recovered from the natural gas and is used as the raw material for preparing the ethylene by the steam thermal cracking, so that the method has positive significance for improving the yield of the ethylene product, reducing the energy consumption of an ethylene device, improving the quality and increasing the efficiency.
Ethane is a high-quality ethylene raw material, the comprehensive production cost is about two thirds of that of naphtha raw material, a plurality of domestic enterprises begin to adopt imported ethane as a construction project of the 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 of the country.
The deethanizer is one of the key equipments in natural gas ethane recovery engineering, and its main function is to complete ethane and C3 +Separation of light hydrocarbon components, the feed to the apparatus being C2 +Mixing hydrocarbon, heating and reboiling the heat-conducting oil of the reboiler at the bottom of the tower and cooling and refluxing the propane evaporator at the top of the tower to control the quality index of the ethane product at the top of the tower and the C at the bottom of the tower3 +The ethane content in the light hydrocarbon component and the cooling of the gaseous ethane at the top of the deethanizer are in a semi-condensation mode, the reflux quantity is the condensation quantity, the reflux quantity influences the temperature of the gaseous ethane at the top of the deethanizer, and the uncondensed gaseous ethane is taken as a product to be output; the temperature of the gaseous ethane at the tower top influences the quality index of an ethane product, the conventional control mode is to control the condensation temperature, the condensation temperature is related to the condensation amount, but the gaseous ethane at the tower top has higher ethane content, small temperature change can cause large change of the condensation amount, and the temperature detection is lagged, so that the temperature of the gaseous ethane at the tower top is difficult to stabilize.
SUMMERY OF THE UTILITY MODEL
The above-mentioned defect to prior art exists, the utility model provides a device of deethanizer tower top gaseous state ethane condensation rate control, the condensation rate of control natural gas ethane recovery engineering deethanizer tower top gaseous state ethane that can be stable, accurate to control deethanizer tower top of the tower reflux volume and top of the tower temperature, reach the purpose of control ethane product quality index.
The utility model discloses the technical scheme who adopts as follows:
a device for controlling the condensation rate of gaseous ethane at the top of a deethanizer tower at least comprises a deethanizer, a propane evaporator and a gas-liquid separatorAnd an ethane reflux pump, wherein the side wall of the middle upper part of the deethanizer is provided with a raw material inlet, the tower top of the deethanizer is provided with a tower top gas phase outlet, and the tower bottom is provided with a tower bottom C3 +A hydrocarbon mixing outlet, wherein the middle lower part of the deethanizer is externally connected with a tower bottom reboiler;
C2 +the mixed hydrocarbon enters the deethanizer through a raw material inlet at the middle upper part of the deethanizer, and a tower top gas phase outlet at the tower top of the deethanizer is sequentially connected with a propane evaporator and a gas-liquid separator 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 deethanizer3 +The mixed hydrocarbon outlet is connected with the C through a pipeline3 +A hydrocarbon mixing spherical tank.
Furthermore, an oil inlet and a reboiled hydrocarbon mixing outlet are arranged at the top of the tower bottom reboiler, an oil outlet and a reboiled hydrocarbon mixing inlet are arranged at the bottom of the tower bottom reboiler, the oil inlet of the tower bottom reboiler is connected with high-temperature heat conducting oil through an oil inlet pipeline, the oil outlet of the tower bottom reboiler is connected with low-temperature heat conducting oil through an oil outlet pipeline, and the reboiled hydrocarbon mixing inlet and the reboiled hydrocarbon mixing outlet of the tower bottom reboiler are respectively connected with a hydrocarbon mixing outlet and a hydrocarbon mixing return port of the deethanizer;
further, dispose conduction oil temperature regulation valve and tower cauldron temperature-detecting appearance on the oil inlet line, the one end of tower cauldron temperature-detecting appearance is connected on the deethanizer, and the other end and the conduction oil temperature regulation valve of tower cauldron temperature-detecting appearance are connected.
Further, a gas-phase outlet is formed in the top of the propane evaporator, a liquid-phase inlet is formed in the bottom of the propane evaporator, the liquid-phase inlet in the bottom of the propane evaporator is connected with a liquid propane storage tank through a pipeline, the gas-phase outlet in the top of the propane evaporator discharges gaseous propane through an exhaust pipeline, and a propane screw compressor is mounted on the exhaust pipeline.
Furthermore, a connecting pipeline between the liquid propane storage tank and a liquid phase inlet of the propane evaporator is provided with a propane liquid level meter and a propane liquid level regulating valve, 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 a slide valve of the propane screw compressor form a pressure regulating loop.
Furthermore, an ethane liquid level meter is installed on the gas-liquid separator, 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, the gas-liquid separator is also connected with a vent pipeline, and the vent pipeline is provided with a constant pressure vent valve.
Furthermore, an ethane gas pressure detector is further installed on the gas-liquid separator, a pressure regulating valve is installed 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 blow-down valve form a pressure regulating and protecting loop.
Furthermore, a reflux liquid flow meter, a reflux liquid 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 liquid flow regulating valve and the reflux liquid flow meter.
The tower bottom C of the deethanizer tower bottom3 +Outlet for mixed hydrocarbons with C3 +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.
Adopt above-mentioned technical scheme, the utility model discloses following beneficial effect has:
(1) the utility model adopts a combined control mode, and adopts a mode of controlling reflux quantity to indirectly control the temperature of the gaseous ethane discharged from the tower; the liquid level of the separator and the suction pressure cascade regulation mode of the propane screw compressor are adopted to control the condensation rate of the gaseous ethane at the tower top, the principle that the refrigeration pressure and the temperature of propane correspond to each other one by one is utilized, and the heat exchange load is regulated in a way of changing the evaporation pressure and adjusting the heat exchange temperature difference; an immersed evaporation condenser is arranged, the heat exchange tubes are totally immersed in liquid propane, and the gaseous ethane at the top of the tower is cooled by virtue of the evaporation of the propane; and a separator is arranged to separate ethane at the top of the gas-liquid two-phase tower, the liquid phase of the ethane separator is pressurized by a reflux pump and then returns to the top of the deethanizer, and the gas phase of the ethane separator is used as an ethane product for outward transportation.
(2) The device of deethanizer top of the tower gaseous state ethane condensation rate control can be accurate, quick, the temperature of stable control top of the tower gaseous state ethane to ensure the quality index of ethane product, avoided conventional control condensation temperature mode in the past to cause the unstability of condensation volume, make out the fluctuation of tower gaseous state ethane temperature and influence the steady operation of deethanizer.
The above description is only an overview of the technical solution of the present invention, and in order to clearly understand the technical means of the present invention and to implement the technical solution according to the content of the description, the following detailed description is made with reference to the preferred embodiments of the present invention and 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 required to be used 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 for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
Fig. 1 is a schematic view of the process of the present invention.
Description of reference numerals:
1、C2 +mixing hydrocarbons; 2. a deethanizer; 3. a gas phase outlet at the top of the tower; 4. a tower top temperature detector; 5. return fluidA flow regulating valve; 6. a reflux flow meter; 7. a return line; 8. a propane vaporizer; 9. a propane level gauge; 10. a propane liquid level regulating valve; 11. a constant pressure blow-down 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. the mixed hydrocarbon is discharged from the tower mouth; 19. returning the mixed hydrocarbon to the tower mouth; 20. a tower kettle liquid level meter; 21. a propane pressure detector; 22. column bottom C3 +A hydrocarbon mixture outlet; 23. a liquid level regulating valve; 24. a column bottom reboiler; 25. a heat conducting oil temperature regulating valve; 26. c3 +A hydrocarbon mixing spherical tank; 27. low-temperature heat conducting oil; 28. high-temperature heat conducting oil; 29. an ethane storage tank; 30. an emptying pipeline; 31. a liquid propane tank; 32. gaseous propane; 33. a propane screw compressor; 34. propane screw compressor slide valve.
Detailed Description
The following description is provided for illustrative embodiments of the present invention, and other advantages and effects of the present invention will be readily apparent to those skilled in the art from the disclosure herein.
The exemplary embodiments of the present invention will now be described with reference to the accompanying drawings, which, however, may be embodied in many different forms and are not limited to the embodiments described herein, which are provided for complete and complete disclosure of the present invention and to fully convey the scope of the invention to those skilled in the art. The terminology used in the exemplary embodiments presented in the accompanying drawings is not intended to be limiting of the invention. In the drawings, the same units/elements are denoted by the same reference numerals.
Unless otherwise defined, terms (including technical and scientific terms) used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. Further, it will be understood that terms, such as those 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.
The 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 a deethanizer 2, a propane evaporator 8, a gas-liquid separator 14 and an ethane reflux pump 16, wherein the sidewall of the middle upper 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 is provided with a bottom C3 +A hydrocarbon mixture outlet 22, the middle lower part of the deethanizer 2 is externally connected with a tower bottom reboiler 24;
C2 +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 a reflux pipeline 7; bottom C of deethanizer 2 tower3 +The mixed hydrocarbon outlet 22 is connected with the C through a pipeline3 +A hydrocarbon mixture spherical tank 26.
The utility model adopts a combined control mode, and adopts a mode of controlling reflux quantity to indirectly control the temperature of the gaseous ethane discharged from the tower; the liquid level of the separator and the suction pressure cascade regulation mode of the propane compressor are adopted to control the condensation rate of the gaseous ethane at the tower top, the principle that the refrigeration pressure and the temperature of propane correspond to each other one by one is utilized, and the heat exchange load is regulated in a way of changing the evaporation pressure and adjusting the heat exchange temperature difference; an immersed evaporation condenser is arranged, the heat exchange tubes are totally immersed in liquid propane, and the gaseous ethane at the top of the tower is cooled by virtue of the evaporation of the propane; and a separator is arranged to separate ethane at the top of the gas-liquid two-phase tower, the liquid phase of the ethane separator is pressurized by a reflux pump and then returns to the top of the deethanizer, and the gas phase of the ethane separator is used as an ethane product for outward transportation.
Second embodiment:
on the basis of the first embodiment, further, an oil inlet and a reboiled hydrocarbon mixed outlet are arranged at the top of the tower bottom reboiler 24, an oil outlet and a reboiled hydrocarbon mixed inlet are arranged at the bottom of the tower bottom reboiler 24, the oil inlet of the tower bottom reboiler 24 is connected with high-temperature heat conduction oil 28 through an oil inlet pipeline, the oil outlet of the tower bottom reboiler 24 is connected with low-temperature heat conduction oil 27 through an oil outlet pipeline, and the reboiled hydrocarbon mixed inlet and the reboiled hydrocarbon mixed outlet of the tower bottom reboiler 24 are respectively connected with the hydrocarbon mixed outlet 18 and the hydrocarbon mixed return outlet 19 of the deethanizer 2;
dispose heat conduction oil temperature control valve 25 and tower cauldron temperature-detecting appearance 17 on advancing the oil pipe, the one end of tower cauldron temperature-detecting appearance 17 is connected on deethanization tower 2, and the other end and the heat conduction oil temperature control valve 25 of tower cauldron temperature-detecting appearance 17 are connected, tower cauldron temperature-detecting appearance 17 constitutes the temperature regulation return circuit with heat conduction oil temperature control valve 25.
Further, a gas phase outlet is formed in the top of the propane evaporator 8, a liquid phase inlet is formed in the bottom of the propane evaporator 8, the liquid phase inlet in the bottom of the propane evaporator 8 is connected with a liquid propane storage tank 31 through a pipeline, the gas phase outlet in the top of the propane evaporator 8 discharges gaseous propane 32 through an exhaust pipeline, and a propane screw compressor 33 is installed on the exhaust pipeline.
A connecting pipeline between the liquid propane storage tank 31 and a liquid phase inlet of the propane evaporator 8 is provided with a propane liquid level meter 9 and a propane liquid level regulating valve 10, 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 form a pressure regulating circuit.
Further, an ethane level meter 15 is mounted on the gas-liquid separator 14.
Further, the gas-liquid separator 14 is also connected with a vent pipeline 30, and the vent pipeline 30 is provided with a constant pressure vent valve 11. An ethane gas pressure detector 13 is further mounted on the gas-liquid separator 14, a pressure regulating valve 12 is mounted 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 relief valve 11 form a pressure regulating and protecting loop.
Furthermore, a reflux liquid flow meter 6, a reflux liquid flow regulating valve 5 and a tower top temperature detector 4 are arranged on a reflux pipeline 7 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 7, and the other end of the tower top temperature detector 4 is respectively connected with the reflux liquid flow regulating valve 5 and the reflux liquid flow meter 6; specifically, the deethanizer 2, the tower top gas phase outlet 3, the tower bottom temperature detector 4, the propane evaporator 8, the gas-liquid separator 14, the ethane reflux pump 16, the reflux liquid flow meter 6 and the reflux liquid flow regulating valve 5 are connected with the deethanizer 2 end to end through pipelines; the tower bottom temperature detector 4, the reflux liquid flow regulating valve 5 and the reflux liquid flowmeter 6 form a cascade regulating loop.
The tower bottom C at the tower bottom of the deethanizer 23 +Hydrocarbon mixture outlet 22 and C3 +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.
A method of deethanization tower top gaseous state ethane condensation rate control can be accurate, quick, the temperature of stable control top gaseous state ethane to ensure the quality index of ethane product, avoided conventional control condensation temperature mode in the past to cause the unstability of condensation volume, make out the fluctuation of tower gaseous state ethane temperature and influence the steady operation of deethanization tower.
The third 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 coming from outside the boundary area2 +The mixed hydrocarbon 1 is introduced into the middle upper part and C of the deethanizer 2 after the metering adjustment2 +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 and heat transfer, and the gas phase ascends and reversely contacts with the descending liquid phase to carry out mass and heat transfer;
s2, detecting the temperature of the gas phase material flow discharged from the top of the deethanizer 2 in the step S1, introducing the gas phase material flow into a propane evaporator 8 for cooling, and changing the gas state into gas-liquid two-phase ethane; specifically, a gas-phase material flow discharged from the top of the deethanizer 2 is cooled by liquid propane introduced from a boundary region in the propane evaporator 8, the temperature of the gas-phase material flow is reduced from 10-15 ℃ to 7-9 ℃ to form a gas-liquid two-phase, the temperature of the liquid propane is increased from 0 ℃ to 55-60 ℃ to form 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 obtained in the step S2 into a gas-liquid separator 14 for separation, and separating the ethane into gaseous ethane and liquid ethane;
s4, introducing the liquid ethane obtained 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 after metering and adjusting;
s5, discharging the gaseous ethane in the step S3 from the top of the gas-liquid separator 14, adjusting the pressure of the gaseous ethane, and outputting the gaseous ethane to an ethane storage tank 29;
s6, the liquid phase discharged from the bottom of the deethanizer 2 in the step S1 is adjusted by a liquid level adjusting valve 23 and then is output to the tower C3 +A hydrocarbon mixture spherical tank 26. Worth mentioning is C at the bottom of the deethanizer 23 +Before the mixed hydrocarbon is discharged, the mixed hydrocarbon is heated by a tower bottom reboiler 24 externally connected to the middle lower part of the debutanizer 2, and the temperature of the mixed hydrocarbon at the tower bottom is controlled to be 100-105 ℃.
In addition, C is2 +The mixed hydrocarbon is composed of ethane, propane and C4 +Methane and CO2The composition comprises 69.62% by volume of ethane, 12.5% by volume of propane and C4 +6.25% by volume, 0.09% by volume of methane and CO2The volume content is 10.71 percent, the pressure is 3.05MPa, and the temperature is 32 ℃.
The gaseous ethane is exported from ethane, propane and C4 +Methane and CO2Composition comprising 83.45% by volume of ethane, 2.56% by volume of propane and C4 +0.0021% by volume, 1.08% by volume methane and CO2The volume content is 12.88 percent, the pressure is 3.00MPa, and the temperature is 8.5 ℃.
C3 +The mixed hydrocarbon is composed of propane, ethane and C4 +Composition comprising 61.45% by volume of propane, 1.53% by volume of ethane and C4 +37.03 percent of mass content, 3.05MPa of pressure and 105 ℃.
The pressure of the high-temperature heat-conducting oil from outside is 0.4 MPa, the temperature is 230 ℃, and the temperature of the low-temperature heat-conducting oil discharged from the device is not lower than 180 ℃.
The pressure of the liquid propane from outside is 1.3MPa, and the temperature is 0 ℃; the pressure of the gaseous propane discharged from the device is 1.3MPa, and the temperature is 60 ℃.
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 coming from outside the boundary area2 +The mixed hydrocarbon 1 is introduced into the middle upper part and C of the deethanizer 2 after the metering adjustment2 +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 and heat transfer, and the gas phase ascends and reversely contacts with the descending liquid phase to carry out mass and heat transfer;
s2, detecting the temperature of the gas phase material flow discharged from the top of the deethanizer 2 in the step S1, introducing the gas phase material flow into a propane evaporator 8 for cooling, wherein the temperature is cooled from 12.15 ℃ to 8.5 ℃, the gas phase is changed into a gas phase and a liquid phase, and the liquefaction rate is 49%;
s3, introducing the gas-liquid two-phase ethane obtained in the step S2 into a gas-liquid separator 14 for separation, and separating the ethane into gaseous ethane and liquid ethane;
s4, introducing the liquid ethane obtained 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 after metering and adjusting;
s5, discharging the gaseous ethane in the step S3 from the top of the gas-liquid separator 14, adjusting the pressure of the gaseous ethane, and outputting the gaseous ethane to an ethane storage tank 29;
s6, the liquid phase discharged from the bottom of the deethanizer 2 in the step S1 is adjusted by a liquid level adjusting valve 23 and then is output to the tower C3 +A hydrocarbon mixture spherical tank 26;
s7, introducing liquid propane from the outside of the boundary zone 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 inlet gaseous propane is controlled by a propane screw compressor slide valve 34;
s9, high-temperature heat conducting oil 28 from the outside of the boundary region enters the reboiler 24 at the bottom of the deethanizer 2, a temperature regulating valve is arranged to heat the mixed hydrocarbon at the bottom of the deethanizer, and the temperature of the mixed hydrocarbon at the bottom of the deethanizer is controlled to be 105 ℃.
The application of the embodiment in actual production is as follows:
the raw material natural gas treatment capacity of the ancient natural gas treatment main plant in the Changqing oil field is 6000 multiplied by 104m3(d) 4 sets of liquid hydrocarbon recovery processing devices with the same scale are arranged at the pressure of 4.1MPa of the incoming gas and the temperature of 7-26 ℃, and the processing scale of a single set of device reaches 1500 multiplied by 104m3/d。
In summary, the utility model indirectly controls the temperature of the gaseous ethane discharged from the tower by controlling the reflux quantity; the liquid level of the separator and the suction pressure cascade regulation mode of the propane screw compressor are adopted to control the condensation rate of the gaseous ethane at the tower top, the principle that the refrigeration pressure and the temperature of propane correspond to each other one by one is utilized, and the heat exchange load is regulated in a way of changing the evaporation pressure and adjusting the heat exchange temperature difference; an immersed evaporation condenser is arranged, the heat exchange tubes are totally immersed in liquid propane, and the gaseous ethane at the top of the tower is cooled by virtue of the evaporation of the propane; and a separator is arranged to separate ethane at the top of the gas-liquid two-phase tower, the liquid phase of the ethane separator is pressurized by a reflux pump and then returns to the top of the deethanizer, and the gas phase of the ethane separator is used as an ethane product for outward transportation.
The device of deethanizer top of the tower gaseous state ethane condensation rate control can be accurate, quick, the temperature of stable control top of the tower gaseous state ethane to ensure the quality index of ethane product, avoided conventional control condensation temperature mode in the past to cause the unstability of condensation volume, make out the fluctuation of tower gaseous state ethane temperature and influence the steady operation of deethanizer.
The foregoing is illustrative of the preferred embodiments of the present invention and is not to be construed as 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 changes and modifications made to the above embodiments according to the technical spirit of the present invention all fall within the scope of the technical solution of the present invention.
Claims (10)
1. A 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 formed in the side wall of the middle upper part of the deethanizer (2), a tower top gas phase outlet (3) is formed in the tower top of the deethanizer (2), and a tower bottom C is formed in the tower bottom3 +A hydrocarbon mixing outlet (22), wherein the middle lower part of the deethanizer (2) is externally connected with a tower bottom reboiler (24);
C2 +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 the propane evaporator (8) and the 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 a reflux pipeline (7); bottom C of the deethanizer (2) column3 +The hydrocarbon mixture outlet (22) is connected with the C through a pipeline3 +A hydrocarbon mixing spherical tank (26).
2. The apparatus according to claim 1, wherein the apparatus comprises: the top of the tower bottom reboiler (24) is provided with an oil inlet and a reboiled hydrocarbon mixing outlet, the bottom of the tower bottom reboiler (24) is provided with an oil outlet and a reboiled hydrocarbon mixing 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 reboiled hydrocarbon mixing inlet and the reboiled hydrocarbon mixing outlet of the tower bottom reboiler (24) are respectively connected with a hydrocarbon mixing outlet (18) and a hydrocarbon mixing return outlet (19) of the deethanizer (2).
3. The apparatus according to claim 2, wherein the apparatus further comprises: dispose conduction oil temperature regulation valve (25) and tower cauldron temperature-detecting appearance (17) on the oil inlet pipeline, the one end of tower cauldron temperature-detecting appearance (17) is connected on deethanizer (2), and the other end and the conduction oil temperature regulation valve (25) of tower cauldron temperature-detecting appearance (17) are connected.
4. The apparatus according to claim 1, wherein the apparatus comprises: the top of propane evaporimeter (8) is provided with the gaseous phase export, and the bottom is provided with the liquid phase import, and the liquid phase import of propane evaporimeter (8) bottom passes through pipe connection liquid propane storage tank (31), and the gaseous phase export at propane evaporimeter (8) top is through the outer gaseous propane (32) of arranging of exhaust pipe line, install propane screw compressor (33) on the exhaust pipe line.
5. The apparatus according to claim 4, wherein the apparatus further comprises: a connecting pipeline between a liquid propane storage tank (31) and a liquid phase inlet of the propane evaporator (8) is provided with a propane liquid level meter (9) and a propane liquid level regulating valve (10), 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).
6. The apparatus according to claim 5, wherein the apparatus further comprises: 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);
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 a slide valve (34) of the propane screw compressor form a pressure regulating circuit.
7. The apparatus according to claim 1, wherein the apparatus comprises: the gas-liquid separator (14) is also connected with an emptying pipeline (30), and the emptying pipeline (30) is provided with a constant pressure emptying valve (11).
8. The apparatus according to claim 5, wherein the apparatus further comprises: the ethane gas pressure detection device is characterized in that an ethane gas pressure detector (13) is further mounted on the gas-liquid separator (14), a pressure regulating valve (12) is mounted on a connecting pipeline between a gas phase outlet of the gas-liquid separator (14) and an ethane storage tank (29), and the ethane gas pressure detector (13), the pressure regulating valve (12) and the constant pressure blow-down valve (11) form a pressure regulating and protecting loop.
9. The apparatus according to claim 1, wherein the apparatus comprises: dispose reflux flow meter (6), reflux flow control valve (5) and top of the tower temperature detector (4) on reflux line (7) between ethane reflux pump (16) export and deethanizer (2), the one end of top of the tower temperature detector (4) is connected on reflux line (7), and the other end of top of the tower temperature detector (4) is connected with reflux flow control valve (5), reflux flow meter (6) respectively.
10. The apparatus according to claim 1, wherein the apparatus comprises: the tower bottom C at the tower bottom of the deethanizer (2)3 +A hydrocarbon mixture outlet (22) and C3 +A connecting pipeline between the hydrocarbon mixing spherical tanks (26) is provided with a tower kettle liquid level meter (20) and a liquid level regulating valve (23), 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).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021323694.XU CN212425914U (en) | 2020-07-08 | 2020-07-08 | Device for controlling condensation rate of gaseous ethane at top of deethanizer |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021323694.XU CN212425914U (en) | 2020-07-08 | 2020-07-08 | Device for controlling condensation rate of gaseous ethane at top of deethanizer |
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| CN212425914U true CN212425914U (en) | 2021-01-29 |
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| CN202021323694.XU Active CN212425914U (en) | 2020-07-08 | 2020-07-08 | Device for controlling condensation rate of gaseous ethane at top of deethanizer |
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