CN111748387A - Device and method for purifying butane by using column pressure stable debutanizer - Google Patents
Device and method for purifying butane by using column pressure stable debutanizer Download PDFInfo
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- CN111748387A CN111748387A CN202010651183.9A CN202010651183A CN111748387A CN 111748387 A CN111748387 A CN 111748387A CN 202010651183 A CN202010651183 A CN 202010651183A CN 111748387 A CN111748387 A CN 111748387A
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/08—Production of synthetic natural gas
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
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- C07C7/005—Processes comprising at least two steps in series
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Abstract
The invention provides a device and a method for purifying butane by a column pressure stable debutanizer, wherein the device at least comprises a debutanizer, an inclined top air cooler, a reflux tank, a reflux pump, a reboiler and a tower bottom cooler; the method is based on a thermal bypass mode, and the regulating valve is additionally arranged at a liquefied gas inlet from the air cooler to the bottom of the reflux tank to control the liquid level of the liquid level air cooler, so that the influence of the pressure difference of the thermal bypass regulating valve can be counteracted, the strict requirement on the installation height difference of the tower top air cooler and the reflux tank is reduced, and the limitation on the too small amount of thermal bypass gas is reduced. The invention can ensure that the installation height of the tower top air cooler and the installation height of the reflux tank are randomly determined according to the installation conditions and are not limited, and in the operation process, the liquid level submerging height of the air cooler is controlled according to the installation positions of the tower top air cooler and the reflux tank and the actual pressure difference of the bypass regulating valve and the combination of the cooling load of the air cooler and the opening degree of the liquid level regulating valve manually regulated to meet the requirement of tower pressure regulation.
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 purifying butane by using a column pressure stable debutanizer.
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.
The debutanizer is one of the key equipments in natural gas ethane recovery engineering, its main function is to complete the separation of liquefied gas and stable light hydrocarbon component, the equipment is fed with C4 +Mixed hydrocarbons, C from debutanizer4 +Mixed hydrocarbon enters the middle part of the debutanizer, and the quality index of a tower top product liquefied gas and the tower bottom stable light hydrocarbon are controlled by heating and reboiling heat-conducting oil of a tower bottom reboiler and cooling reflux of an inclined top air cooler at the tower topThe content of butane in the components and the cooling of the gaseous liquefied gas at the top of the debutanizer are in a full condensation mode, the reflux quantity determines the temperature of the gaseous liquefied gas at the top of the debutanizer, and the quality index of the liquefied gas product is influenced by the temperature of the gaseous liquefied gas at the top of the debutanizer.
The basic condition for the stable operation of the debutanizer is that the operation pressure of the debutanizer is stable, but due to the influence of the change of installation size or raw material quantity, the debutanizer has the biggest problem in the actual production that the operation pressure of the debutanizer is easy to fluctuate and the product quality is unqualified. The control method of the tower pressure of the conventional debutanizer is divided into two control modes, wherein the first mode is a thermal bypass adjusting mode, namely the installation height of an air cooler at the top of the tower is lower than that of a reflux tank at the top of the tower, the height difference of the air cooler at the top of the tower and the reflux tank at the top of the tower is about 12m, and the pressure difference of the reflux tank and the debutanizer is adjusted by utilizing a thermal bypass, so that the heat exchange area of the air cooler is influenced; the second is to adjust the pressure of the debutanizer by adjusting the liquid level with an air cooler outlet adjusting valve, and the air cooler is required to be installed higher than the top reflux tank and ensure that the liquid inlet is not concave. In order to ensure that the liquefied gas reflux pump is not cavitated, the installation height of the reflux tank is generally not lower than 5m, so in order to be beneficial to the reliable operation of the reflux pump, a first tower pressure adjusting mode is commonly used, but the pressure difference of a bypass adjusting valve and the type selection and installation of an air cooler have higher requirements.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a device and a method for purifying butane by using a column pressure stable debutanizer.
The technical scheme adopted by the invention is as follows:
a method for purifying butane by a column pressure stabilization type debutanizer comprises the following steps:
s1, C coming from outside the boundary area4 +After the metering adjustment of the mixed hydrocarbon, introducing the mixed hydrocarbon into the middle upper part of the debutanizer;
s2, C introducing the step S1 into a debutanizer4 +The mixed hydrocarbon is divided into gas phase and liquid phase in the tower, the liquid phase descends and contacts with the ascending gas phase in a reverse direction for mass transfer and heat transfer, the gas phase material flow is discharged from the tower top of the debutanizer, and the liquid phase material flow is discharged from the tower bottom;
s3, detecting the temperature of a gas phase material flow discharged from the top of the debutanizer, dividing the gas phase material flow into a main material flow and a secondary material flow, introducing the main material flow into an inclined top air cooler for condensation, cooling the main material flow from 60-70 ℃ to 43-48 ℃, and completely condensing the gas phase into liquefied gas;
s4, conveying the liquefied gas in the step S3 to a return tank for buffer storage;
s5, introducing the liquefied gas in the step S4 into a reflux pump from a reflux tank for pressurization, dividing the pressurized liquefied gas into two paths, introducing one path of the pressurized liquefied gas into the top of a debutanizer as reflux liquid after metering and flow regulation, and introducing the other path of the pressurized liquefied gas into a liquefied gas spherical tank of a storage tank area for storage through a liquefied gas liquid level regulating valve;
s6, introducing the secondary stream obtained in the step S3 into a bypass regulating valve, and conveying the secondary stream to the gas phase space of a reflux tank after pressure regulation;
s7, cooling the liquid phase material flow and the stable light hydrocarbon discharged from the debutanizer at the bottom of the tower in the step S2, adjusting by a stable light hydrocarbon liquid level adjusting valve, and storing in a stable light hydrocarbon ball tank in a storage tank area;
s8, leading the gas phase of the reflux tank in the step 6 to a fuel gas system or a flare through a reflux tank pressure regulating valve or a constant pressure emptying valve.
Further, before the mixed hydrocarbon at the bottom of the debutanizer is discharged, a reboiler externally connected to the middle lower part of the debutanizer heats the mixed hydrocarbon, and the temperature of the mixed hydrocarbon at the bottom of the debutanizer is controlled to be 160-170 ℃.
A tower pressure stable type device for purifying butane by a debutanizer tower at least comprises the debutanizer tower, an inclined top air cooler, a reflux tank, a reflux pump, a reboiler and a tower bottom cooler, wherein a raw material inlet is arranged on the side wall of the middle upper part of the debutanizer tower, a gas phase outlet is arranged at the tower top of the debutanizer tower, and a liquid phase inlet and a liquid phase outlet are arranged at the tower bottom;
C4 +the mixed hydrocarbon enters the debutanizer through a raw material inlet at the middle upper part of the debutanizer, a gas phase outlet at the top of the debutanizer is connected with an inlet of an inclined top air cooler through a pipeline I, an outlet of the inclined top air cooler is communicated with a liquid inlet of a reflux tank through a pipeline II, a gas phase outlet is arranged at the top of the reflux tank, and liquid is arranged at the bottom of the reflux tankA phase outlet, namely a gas phase outlet at the top of the reflux tank discharges noncondensable gas of the product through a pipeline III; a liquid phase outlet at the bottom of the reflux tank is connected with an inlet of a reflux pump, an outlet of the reflux pump is divided into two paths, one path is connected with the debutanizer through a reflux pipeline, and the other path is connected with a liquefied gas spherical tank through a pipeline IV;
the liquid phase inlet at the bottom of the debutanizer is externally connected with a reboiler, the liquid phase outlet at the bottom of the debutanizer is connected with a tower bottom cooler, and the tower bottom cooler is connected with a stable light hydrocarbon spherical tank through a pipeline five.
Furthermore, a reboiling liquid inlet, a reboiling liquid outlet, a heat conduction oil inlet and a heat conduction oil outlet are formed in the reboiling device, the heat conduction oil inlet of the reboiling device is connected with high-temperature heat conduction oil through an oil inlet pipeline, the heat conduction oil outlet of the reboiling device is connected with low-temperature heat conduction oil through an oil outlet pipeline, the reboiling liquid inlet and the reboiling liquid outlet of the reboiling device are respectively communicated with the debutanizer, and the reboiling liquid inlet is positioned above the reboiling liquid outlet.
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 debutanizer, and the other end of the tower kettle temperature detector is connected with the heat-conducting oil temperature regulating valve.
Furthermore, a first connecting pipeline between a gas phase outlet at the top of the debutanizer and an inlet of the inclined top air cooler is provided with a top temperature detector, a top pressure detector and a bypass regulating valve;
a liquid level manual adjusting valve and an air cooler temperature detector are arranged on a pipeline II between the outlet of the inclined top air cooler and the liquid inlet of the reflux tank;
a return tank pressure detector and a return tank pressure regulating valve are arranged on a pipeline III connected with a gas phase outlet at the top of the return tank;
a reflux liquid flow meter and a reflux liquid flow regulating valve are arranged on a reflux pipeline between the reflux pump and the debutanizer;
a liquefied gas level regulating valve and a liquefied gas level detector are arranged on a pipeline IV connected with the outlet of the return pump;
and a fifth connecting pipeline between the tower bottom cooler and the stable light hydrocarbon spherical tank is provided with a tower kettle liquid level detector and a stable light hydrocarbon liquid level regulating valve.
Specifically, one end of the bypass regulating valve is connected to a first connecting pipeline between the tower top pressure detector and an inlet of the inclined top air cooler, and the other end of the bypass regulating valve is connected to the reflux tank;
one end of the air cooler temperature detector is connected to the inclined-roof air cooler, and the other end of the air cooler temperature detector is connected to a second pipeline connected between the liquid level manual regulating valve and the liquid inlet of the reflux tank;
one end of the liquefied gas liquid level detector is connected to the reflux tank, and the other end of the liquefied gas liquid level detector is connected with the liquefied gas liquid level regulating valve;
one end of the tower kettle liquid level detector is connected to the bottom side wall of the debutanizer, and the other end of the tower kettle liquid level detector is connected with the stable light hydrocarbon liquid level regulating valve.
Further, the reflux tank is also connected with a vent pipeline, and the vent pipeline is used for venting the non-condensable gas.
Specifically, a constant pressure air release valve is installed on the air release pipeline.
Furthermore, one end of the backflow tank pressure detector is connected to the backflow tank, and the other end of the backflow tank pressure detector is connected with the backflow tank pressure regulating valve and the constant pressure emptying valve respectively.
The invention has the following beneficial effects:
1) aiming at the advantages and disadvantages of the existing tower pressure adjusting mode, the invention adopts a combined control mode, namely, a regulating valve is added at a liquefied gas inlet from an air cooler to the bottom of a reflux tank to control the liquid level of a liquid level air cooler on the basis of a thermal bypass mode, the effect of the combined control mode can counteract the influence of the pressure difference of the thermal bypass regulating valve so as to reduce the strict requirement on the installation height difference of the tower top air cooler and the reflux tank, and simultaneously can reduce the limitation on too small thermal bypass gas quantity, and the supercooling temperature of the air cooler is lower due to too large thermal bypass gas quantity so as to avoid the discharge of non-condensable gas in the reflux tank.
2) The invention adopts a combined regulation mode of the thermal bypass, can randomly determine the installation height of the tower top air cooler and the installation height of the reflux tank according to the installation conditions, the beauty and the installation requirements of a reflux pump and the like without being limited, and manually regulate the opening degree of the liquid level regulating valve according to the installation positions of the tower top air cooler and the reflux tank and the actual pressure difference of the bypass regulating valve and the cooling load of the air cooler in the running process to control the liquid level submerging height of the air cooler so as to adapt to the tower pressure regulation requirement.
3) The method for purifying butane by using the tower pressure stabilization type debutanizer can stably, accurately and quickly control the operation pressure of the debutanizer in the natural gas ethane recovery project, thereby controlling the operation stability of the debutanizer and ensuring that the quality indexes of liquefied gas products at the tower top and stable light hydrocarbons at the tower bottom are achieved.
The foregoing description is only an overview of the technical solutions of the present invention, and in order to clearly understand the technical solutions of the present invention and to implement the technical solutions according to the contents of the description, the following detailed description is given with reference to the preferred embodiments of the present invention and 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 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 it is obvious for those skilled in the art to obtain other drawings without creative efforts.
FIG. 1 is a schematic process flow diagram of the present invention.
Description of reference numerals:
1、C4 +mixing hydrocarbons; 2. a debutanizer column; 3. a reboiler; 4. a tower top temperature detector; 5. a tower top pressure detector; 6. a bypass regulating valve; 7. an inclined top air cooler; 8. a liquid level manual adjusting valve; 9. an air cooler temperature detector; 10. a reflux tank; 11. a reflux tank pressure detector; 12. a reflux drum pressure regulating valve; 13. a reflux pump; 14. a reflux flow meter; 15. a reflux liquid flow regulating valve; 16. a constant pressure blow-down valve; 17. a tower kettle temperature detector; 18. a reboiling liquid inlet; 19. a reboiled liquid outlet; 20. tower kettleA liquid level detector; 21. stabilizing light hydrocarbons; 22. high-temperature heat conducting oil; 23. low-temperature heat conducting oil; 24. a tower bottom cooler; 25. stabilizing a light hydrocarbon liquid level regulating valve; 26. a stable light hydrocarbon spherical tank; 27. a heat conducting oil temperature regulating valve; 28. a liquefied gas spherical tank; 29. a liquefied gas level regulating valve; 30. a liquefied gas level detector; 31. the product is non-condensable gas; 32. non-condensable gas.
Detailed Description
The following description of the embodiments of the present invention is provided for illustrative purposes, and other advantages and effects of the present invention will become apparent to those skilled in the art from the present disclosure.
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 embodiments described herein, which are provided for complete and complete disclosure of the present invention and to fully convey the scope of the present 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, 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 first embodiment of the present invention relates to a method for purifying butane by a column pressure stabilization type debutanizer, referring to fig. 1, comprising the following steps:
s1, C coming from outside the boundary area4 +After the metering adjustment of the mixed hydrocarbon 1, introducing the mixed hydrocarbon into the middle upper part of a debutanizer 2;
s2, C of introducing the step S1 into a debutanizer 24 +The mixed hydrocarbon 1 is divided into gas phase and liquid phase in the tower, the liquid phase descends and contacts with the ascending gas phase in a reverse direction to transfer mass and heat, and the tower of the debutanizer 2A gas phase material flow is discharged from the top, and a liquid phase material flow is discharged from the bottom of the tower;
s3, detecting the temperature of the gas phase material flow discharged from the top of the debutanizer 2, dividing the gas phase material flow into a main material flow and a secondary material flow, introducing the main material flow into an inclined top air cooler 7 for condensation, cooling the main material flow from 60-70 ℃ to 43-48 ℃, and completely condensing the gas phase into liquefied gas;
s4, delivering the liquefied gas in the step S3 to a reflux tank 10 for buffer storage;
s5, introducing the liquefied gas in the step S4 from the reflux tank 10 into a reflux pump 13 for pressurization, dividing the pressurized liquefied gas into two paths, introducing one path of the pressurized liquefied gas into the top of the debutanizer 2 as reflux liquid after metering and flow regulation, and introducing the other path of the pressurized liquefied gas into a liquefied gas ball tank 28 in a storage tank area for storage through a liquefied gas level regulating valve 29;
s6, introducing the secondary stream obtained in the step S3 into a bypass regulating valve 6, and conveying the secondary stream to the gas phase space of a reflux tank 10 after pressure regulation;
s7, cooling the liquid phase material flow discharged from the debutanizer 2 tower at the lower part in the step S2 and the stable light hydrocarbon 21 by a tower bottom cooler 24, adjusting by a stable light hydrocarbon liquid level adjusting valve 25, and then sending to a stable light hydrocarbon ball tank 26 in a storage tank area for storage;
s8, the gas phase of the step 6 reflux drum 10 is directed to a fuel gas system or flare through reflux drum pressure regulating valve 12 or a constant pressure blow down valve 16.
The debutanizer is one of the key equipments in natural gas ethane recovery engineering, its main function is to complete the separation of liquefied gas and stable light hydrocarbon component, the equipment is fed with C3 +Mixed hydrocarbons, C from debutanizer3 +The mixed hydrocarbon enters the middle part of the debutanizer, the quality index of the tower top product liquefied gas and the content of butane in the tower bottom stable light hydrocarbon component are controlled by heating and reboiling of the reboiler heat conducting oil at the tower bottom and cooling and refluxing of the air cooler at the inclined top of the tower top, the cooling of the gaseous liquefied gas at the tower top of the debutanizer is in a full condensation mode, the temperature of the gaseous liquefied gas at the tower top is determined by the reflux amount, and the quality index of the liquefied gas product is influenced by the temperature of the gaseous liquefied gas at the tower top.
The basic condition for the stable operation of the debutanizer is that the operation pressure of the debutanizer is stable, but due to the influence of the change of installation size or raw material quantity, the debutanizer has the biggest problem in the actual production that the operation pressure of the debutanizer is easy to fluctuate and the product quality is unqualified. The control method of the tower pressure of the conventional debutanizer is divided into two control modes, wherein the first mode is a thermal bypass adjusting mode, namely the installation height of an air cooler at the top of the tower is lower than that of a reflux tank at the top of the tower, the height difference of the air cooler at the top of the tower and the reflux tank at the top of the tower is about 12m, and the pressure difference of the reflux tank and the debutanizer is adjusted by utilizing a thermal bypass, so that the heat exchange area of the air cooler is influenced; the second is to adjust the pressure of the debutanizer by adjusting the liquid level with an air cooler outlet adjusting valve, and the air cooler is required to be installed higher than the top reflux tank and ensure that the liquid inlet is not concave. In order to ensure that the liquefied gas reflux pump is not cavitated, the installation height of the reflux tank is generally not lower than 5m, so in order to be beneficial to the reliable operation of the reflux pump, a first tower pressure adjusting mode is commonly used, but the pressure difference of a bypass adjusting valve and the type selection and installation of an air cooler have higher requirements.
Aiming at the advantages and disadvantages of the two tower pressure adjusting modes, the invention adopts a combined control mode, namely, a regulating valve is added at a liquefied gas inlet from the air cooler to the bottom of the reflux tank to control the liquid level of the liquid level air cooler on the basis of a thermal bypass mode, the effect of the combined control mode can counteract the influence of the pressure difference of the thermal bypass regulating valve so as to reduce the strict requirement on the installation height difference of the tower top air cooler and the reflux tank, and simultaneously can reduce the limitation on too small thermal bypass gas quantity, and the supercooling temperature of the air cooler is lower due to too large thermal bypass gas quantity so as to avoid the discharge of non-condensable gas in the reflux tank. By using the heat bypass+The combined adjusting mode can be used for randomly determining the installation height of the tower top air cooler and the installation height of the reflux tank according to the installation conditions, attractiveness and orderliness and installation requirements such as reflux pumps and the like without limitation, and in the operation process, the liquid level submerging height of the air cooler is controlled by manually adjusting the opening degree of the liquid level adjusting valve by combining the cooling load of the air cooler according to the installation positions of the tower top air cooler and the reflux tank and the actual pressure difference of the bypass adjusting valve so as to adapt to the tower pressure adjusting requirement.
Second embodiment:
the embodiment relates to a device for purifying butane by using a column pressure stable debutanizer, which at least comprises a debutanizer 2, an inclined top air cooler 7, a reflux tank 10, a reflux pump 16, a reboiler 3 and a tower bottom cooler 24, wherein the side wall of the middle upper part of the debutanizer 2 is provided with a raw material inlet, the tower top of the debutanizer 2 is provided with a gas phase outlet, and the tower bottom is provided with a liquid phase inlet and a liquid phase outlet;
C4 +the mixed hydrocarbon 1 enters the debutanizer 2 through a raw material inlet at the middle upper part of the debutanizer 2, a gas phase outlet at the top of the debutanizer 2 is connected with an inlet of an inclined top air cooler 7 through a pipeline I, an outlet of the inclined top air cooler 7 is communicated with a liquid inlet of a reflux tank 10 through a pipeline II, and a gas phase outlet at the top of the reflux tank 10 discharges a product noncondensable gas 31 through a pipeline III; a liquid phase outlet at the bottom of the reflux tank 10 is connected with an inlet of a reflux pump 13, an outlet of the reflux pump 13 is divided into two paths, one path is connected with the debutanizer 2 through a reflux pipeline, and the other path is connected with a liquefied gas ball tank 28 through a pipeline IV; a liquid phase inlet at the bottom of the debutanizer 2 is externally connected with a reboiler 3, a liquid phase outlet at the bottom of the debutanizer 2 is connected with a tower bottom cooler 24, and the tower bottom cooler 24 is connected with a stable light hydrocarbon ball tank 26 through a pipeline five.
The column pressure stabilization type debutanizer butane purification device can stably, accurately and quickly control the operation pressure of the debutanizer in the natural gas ethane recovery project, thereby controlling the operation stability of the debutanizer and ensuring that the quality indexes of liquefied gas products at the top of the tower and stable light hydrocarbons at the bottom of the tower are achieved.
The third embodiment:
on the basis of the second embodiment, further, the reboiler 3 is provided with a reboiler inlet 18, a reboiler outlet 19, a heat transfer oil inlet and a heat transfer oil outlet, the heat transfer oil inlet of the reboiler 3 is connected with high-temperature heat transfer oil 22 through an oil inlet pipeline, the heat transfer oil outlet of the reboiler 3 is connected with low-temperature heat transfer oil 23 through an oil outlet pipeline, the reboiler inlet 18 and the reboiler outlet 19 of the reboiler 3 are respectively communicated with the debutanizer 2, and the reboiler inlet 18 is located above the reboiler outlet 19. Dispose heat conduction oil temperature control valve 27 and tower cauldron temperature-detecting appearance 17 on the oil inlet line, specifically, the one end of tower cauldron temperature-detecting appearance 17 is connected on debutanizer 2, and the other end and the heat conduction oil temperature control valve 27 of tower cauldron temperature-detecting appearance 17 are connected. The tower bottom temperature detector 17 and the heat-conducting oil temperature regulating valve 27 form a temperature regulating loop.
Further, a first connecting pipeline between a gas phase outlet at the top of the debutanizer 2 and an inlet of the inclined top air cooler 7 is provided with a top temperature detector 4, a top pressure detector 5 and a bypass regulating valve 6; specifically, one end of the bypass regulating valve 6 is connected to a first connecting pipeline between the tower top pressure detector 5 and an inlet of the inclined top air cooler 7, and the other end of the bypass regulating valve 6 is connected to the reflux tank 10. The tower top pressure detector 5 and the bypass regulating valve 6 form a tower pressure regulating loop.
A liquid level manual adjusting valve 8 and an air cooler temperature detector 9 are arranged on a pipeline II between the outlet of the inclined top air cooler 7 and the liquid inlet of the reflux tank 10; specifically, one end of the air cooler temperature detector 9 is connected to the inclined-roof air cooler 7, and the other end of the air cooler temperature detector 9 is connected to a second pipeline connected between the liquid level manual valve 8 and a liquid inlet of the reflux tank 10.
And a third pipeline connected with a gas phase outlet at the top of the reflux tank 10 is provided with a reflux tank pressure detector 11 and a reflux tank pressure regulating valve 12. It should be noted that a vent line for venting the non-condensable gas 32 is connected to the reflux tank 10, and further, a constant pressure vent valve 16 is installed on the vent line. It is worth mentioning that one end of the reflux tank pressure detector 11 is connected to the reflux tank 10, and the other end of the reflux tank pressure detector 11 is respectively connected with the reflux tank pressure regulating valve 12 and the constant pressure blow-down valve 16; the reflux tank pressure detector 11, the reflux tank pressure regulating valve 12 and the constant pressure emptying valve 16 form a pressure regulating and protecting loop.
Furthermore, a reflux liquid flow meter 14 and a reflux liquid flow regulating valve 15 are arranged on a reflux pipeline between the reflux pump 13 and the debutanizer 2; the reflux liquid flow meter 14 and the reflux liquid flow control valve 15 constitute a flow control circuit.
Further, a liquefied gas level regulating valve 29 and a liquefied gas level detector 30 are arranged on a pipeline IV connected with the outlet of the return pump 13; specifically, one end of the liquefied gas level detector 30 is connected to the reflux tank 10, and the other end of the liquefied gas level detector 30 is connected to the liquefied gas level regulating valve 29. The liquefied gas level regulating valve 29 and the liquefied gas level detecting instrument 30 constitute a liquid level regulating circuit.
Further, a fifth connecting pipeline between the tower bottom cooler 24 and the stable light hydrocarbon ball tank 26 is provided with a tower kettle liquid level detector 20 and a stable light hydrocarbon liquid level regulating valve 25. Specifically, one end of the tower kettle liquid level detector 20 is connected to the bottom side wall of the debutanizer 2, and the other end of the tower kettle liquid level detector 20 is connected to the stable light hydrocarbon liquid level regulating valve 25. The tower kettle liquid level detector 20 and the stable light hydrocarbon liquid level regulating valve 25 form a liquid level regulating loop.
Fourth embodiment:
the embodiment relates to a method for purifying butane by a column pressure stable debutanizer, which comprises the following steps with reference to fig. 1:
s1, C coming from outside the boundary area4 +After the metering adjustment of the mixed hydrocarbon 1, introducing the mixed hydrocarbon into the middle upper part of a debutanizer 2;
s2, C of introducing the step S1 into a debutanizer 24 +The mixed hydrocarbon 1 is divided into a gas phase and a liquid phase in the tower, the liquid phase descends and reversely contacts with the ascending gas phase for mass transfer and heat transfer, the gas phase material flow is discharged from the top of the debutanizer 2, and the liquid phase material flow is discharged from the bottom of the debutanizer;
s3, detecting the temperature of the gas phase material flow discharged from the top of the debutanizer 2, dividing the gas phase material flow into a main material flow and a secondary material flow, introducing the main material flow into an inclined top air cooler 7 for condensation, cooling the temperature from 66 ℃ to 46 ℃, and completely condensing the gas phase into liquefied gas;
s4, delivering the liquefied gas in the step S3 to a reflux tank 10 for buffer storage;
s5, introducing the liquefied gas in the step S4 from the reflux tank 10 into a reflux pump 13 for pressurization, dividing the pressurized liquefied gas into two paths, introducing one path of the pressurized liquefied gas into the top of the debutanizer 2 as reflux liquid after metering and flow regulation, and introducing the other path of the pressurized liquefied gas into a liquefied gas ball tank 28 in a storage tank area for storage through a liquefied gas level regulating valve 29;
s6, introducing the secondary stream obtained in the step S3 into a bypass regulating valve 6, and conveying the secondary stream to the gas phase space of a reflux tank 10 after pressure regulation;
s7, cooling the liquid phase material flow discharged from the debutanizer 2 tower at the lower part in the step S2 and the stable light hydrocarbon 21 by a tower bottom cooler 24, adjusting by a stable light hydrocarbon liquid level adjusting valve 25, and then sending to a stable light hydrocarbon ball tank 26 in a storage tank area for storage;
s8, introducing the gas phase in the reflux tank 10 of the step 6 to a fuel gas system or a torch through a reflux tank pressure regulating valve 12 or a constant pressure emptying valve 16;
s9, high-temperature heat conducting oil from the outside of the boundary region enters a reboiler at the bottom of the debutanizer 2, a temperature regulating valve is arranged to heat hydrocarbon mixture at the bottom of the debutanizer, and the temperature of the hydrocarbon mixture at the bottom of the debutanizer is controlled to be 165 ℃.
In addition, the above-mentioned C3 +The mixed hydrocarbon is composed of propane, butane and C5 + hydrocarbonsAnd ethane, wherein the volume content of propane is 61.45%, the volume content of butane is 23.47%, C5 +13.56 percent by volume of ethane and 1.53 percent by volume of ethane, the pressure is 1.55MPa, and the temperature is 74 ℃.
The liquefied gas is composed of propane, butane and C5 +And ethane, wherein the volume content of propane is 71.93%, the volume content of butane is 25.24%, C5 +Volume content of 1.04%, volume content of ethane of 1.79%, pressure of 1.53MPa, and temperature of 65.28 deg.C.
Stabilized light hydrocarbons consisting of propane, butane and C5 +Composition of 0.32% by volume propane, 13.14% by volume butane and C5 +The volume content is 86.54 percent, the pressure is 1.55MPa, and the temperature is 165 ℃.
The pressure of high-temperature heat-conducting oil from outside is 0.4MPa, the temperature is 230 ℃, and the temperature of heat-conducting oil discharged from the device is not lower than 180 ℃.
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 × 104m3D, setting a total of 4 sets of liquid hydrocarbon recovery processing devices with the same scale, wherein the processing scale of a single set of device reaches 1500 × 104m3D, feeding unit feedstock C3 +The mixed hydrocarbon is composed of propane, butane and C5 +And ethane, wherein the volume content of propane is 61.45 percent and the volume of butane isContent 23.47%, C5 +13.56 percent by volume of ethane and 1.53 percent by volume of ethane, the pressure is 1.55MPa, and the temperature is 74 ℃.
In summary, the present invention adopts a combined control mode, that is, a regulating valve is added at the liquefied gas inlet from the air cooler to the bottom of the reflux tank to control the liquid level of the liquid level air cooler based on a thermal bypass mode, and the function of the present invention can counteract the effect of the pressure difference of the thermal bypass regulating valve to reduce the strict requirement on the installation height difference between the tower top air cooler and the reflux tank, and reduce the limitation on the too small amount of the thermal bypass gas, and the too large amount of the thermal bypass gas will cause the supercooling temperature of the air cooler to be lower to avoid the discharge of the noncondensable gas in the reflux tank. In the operation process, the liquid level submerging height of the air cooler is controlled by manually adjusting the opening of the liquid level adjusting valve according to the installation positions of the tower top air cooler and the reflux tank and the actual pressure difference of the bypass adjusting valve and combining the cooling load of the air cooler so as to meet the requirement of tower pressure adjustment.
The device and the method for purifying butane by using the tower pressure stable debutanizer can stably, accurately and quickly control the operating pressure of the debutanizer in the natural gas ethane recovery project, thereby controlling the operating stability of the debutanizer and ensuring that the liquefied gas product at the tower top and the stable light hydrocarbon quality index at the tower bottom are achieved.
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 change and modification of the above embodiments according to the technical spirit of the present invention still fall within the scope of the technical solution of the present invention.
Claims (10)
1. A method for purifying butane by a column pressure stable debutanizer is characterized by comprising the following steps:
s1, C coming from outside the boundary area4 +After the metering adjustment of the mixed hydrocarbon (1), introducing the mixed hydrocarbon into the middle upper part of the debutanizer (2);
s2, C of introducing the step S1 into the debutanizer (2)4 +Mixed hydrocarbons (1)) The gas phase and the liquid phase are separated in the tower, the liquid phase descends and contacts with the ascending gas phase in a reverse direction for mass transfer and heat transfer, the gas phase material flow is discharged from the top of the debutanizer (2), and the liquid phase material flow is discharged from the bottom of the debutanizer;
s3, detecting the temperature of the gas phase material flow discharged from the top of the debutanizer (2), dividing the gas phase material flow into a main material flow and a secondary material flow, introducing the main material flow into an inclined top air cooler (7) for condensation, cooling the main material flow from 60-70 ℃ to 43-48 ℃, and completely condensing the gas phase into liquefied gas;
s4, conveying the liquefied gas in the step S3 to a return tank (10) for buffer storage;
s5, introducing the liquefied gas in the step S4 from a reflux tank (10) into a reflux pump (13) for pressurization, dividing the pressurized liquefied gas into two paths, introducing one path of the pressurized liquefied gas into the top of a debutanizer (2) as reflux liquid after metering and flow regulation, and introducing the other path of the pressurized liquefied gas into a liquefied gas spherical tank (28) in a storage tank area for storage through a liquefied gas liquid level regulating valve (29);
s6, introducing the secondary stream obtained in the step S3 into a bypass regulating valve (6), and conveying the secondary stream to the gas phase space of a reflux tank (10) after pressure regulation;
s7, cooling the liquid phase material flow discharged from the bottom of the debutanizer (2) in the step S2 and the stable light hydrocarbon (21) by a tower bottom cooler (24), adjusting by a stable light hydrocarbon liquid level adjusting valve (25), and then storing in a stable light hydrocarbon ball tank (26) of a storage tank area;
s8, introducing the gas phase of the step 6 reflux tank (10) to a fuel gas system or a flare through a reflux tank pressure regulating valve (12) or a constant pressure emptying valve (16).
2. The method for purifying butane by using the column pressure stabilization type debutanizer as claimed in claim 1, wherein: before the mixed hydrocarbon at the bottom of the debutanizer (2) is discharged, a reboiler (3) externally connected to the middle lower part of the debutanizer (2) heats the mixed hydrocarbon, and the temperature of the mixed hydrocarbon at the bottom of the debutanizer is controlled to be 160-170 ℃.
3. A column pressure stable type debutanizer butane purification device is characterized in that: the device at least comprises a debutanizer (2), an inclined top air cooler (7), a reflux tank (10), a reflux pump (16), a reboiler (3) and a tower bottom cooler (24), wherein a raw material inlet is formed in the side wall of the middle upper part of the debutanizer (2), a gas phase outlet is formed in the tower top of the debutanizer (2), and a liquid phase inlet and a liquid phase outlet are formed in the tower bottom;
C4 +the mixed hydrocarbon (1) enters a debutanizer (2) through a raw material inlet at the middle upper part of the debutanizer (2), a gas phase outlet at the top of the debutanizer (2) is connected with an inlet of an inclined-top air cooler (7) through a first pipeline, an outlet of the inclined-top air cooler (7) is communicated with a liquid inlet of a reflux tank (10) through a second pipeline, a gas phase outlet is arranged at the top of the reflux tank (10), a liquid phase outlet is arranged at the bottom of the reflux tank (10), and a gas phase outlet at the top of the reflux tank (10) discharges noncondensable gas (31) of a product through a third pipeline; a liquid phase outlet at the bottom of the reflux tank (10) is connected with an inlet of a reflux pump (13), an outlet of the reflux pump (13) is divided into two paths, one path is connected with the debutanizer (2) through a reflux pipeline, and the other path is connected with a liquefied gas spherical tank (28) through a pipeline IV;
a liquid phase inlet at the bottom of the debutanizer (2) is externally connected with a reboiler (3), a liquid phase outlet at the bottom of the debutanizer (2) is connected with a tower bottom cooler (24), and the tower bottom cooler (24) is connected with a stable light hydrocarbon spherical tank (26) through a pipeline five.
4. The apparatus for purifying butane in the column pressure stabilization type debutanizer according to claim 3, wherein: be provided with reboiling liquid import (18), reboiling liquid export (19), conduction oil import and conduction oil export on reboiler (3), the conduction oil import of reboiling ware (3) is through advancing oil pipe connection high temperature conduction oil (22), and the conduction oil export of reboiling ware (3) is through going out oil pipe connection low temperature conduction oil (23), reboiling liquid import (18), the reboiling liquid export (19) of reboiling ware (3) communicate with debutanizer (2) respectively, and reboiling liquid import (18) are located the top of reboiling liquid export (19).
5. The apparatus for purifying butane in the column pressure stabilization type debutanizer as claimed in claim 4, wherein: a heat conduction oil temperature regulating valve (27) and a tower kettle temperature detector (17) are arranged on the oil inlet pipeline; one end of the tower kettle temperature detector (17) is connected to the debutanizer (2), and the other end of the tower kettle temperature detector (17) is connected with the heat-conducting oil temperature regulating valve (27).
6. The apparatus for purifying butane in the column pressure stabilization type debutanizer according to claim 3, wherein: a first connecting pipeline between a gas phase outlet at the top of the debutanizer (2) and an inlet of the inclined top air cooler (7) is provided with a top temperature detector (4), a top pressure detector (5) and a bypass regulating valve (6);
a liquid level manual adjusting valve (8) and an air cooler temperature detector (9) are arranged on a pipeline II between the outlet of the inclined top air cooler (7) and the liquid inlet of the reflux tank (10);
a return tank pressure detector (11) and a return tank pressure regulating valve (12) are arranged on a pipeline III connected with a gas phase outlet at the top of the return tank (10);
a reflux liquid flow meter (14) and a reflux liquid flow regulating valve (15) are arranged on a reflux pipeline between the reflux pump (13) and the debutanizer (2);
a liquefied gas level regulating valve (29) and a liquefied gas level detector (30) are arranged on a pipeline IV connected with the outlet of the reflux pump (13);
and a tower kettle liquid level detector (20) and a stable light hydrocarbon liquid level regulating valve (25) are arranged on a fifth connecting pipeline between the tower bottom cooler (24) and the stable light hydrocarbon spherical tank (26).
7. The apparatus for purifying butane in the column pressure stabilization type debutanizer as claimed in claim 6, wherein: one end of the bypass regulating valve (6) is connected to a first connecting pipeline between the tower top pressure detector (5) and an inlet of the inclined top air cooler (7), and the other end of the bypass regulating valve (6) is connected to the reflux tank (10);
one end of the air cooler temperature detector (9) is connected to the inclined-roof air cooler (7), and the other end of the air cooler temperature detector (9) is connected to a second pipeline connected between the liquid level manual regulating valve (8) and the liquid inlet of the reflux tank (10);
one end of the liquefied gas liquid level detector (30) is connected to the reflux tank (10), and the other end of the liquefied gas liquid level detector (30) is connected with the liquefied gas liquid level regulating valve (29);
one end of the tower kettle liquid level detector (20) is connected to the side wall of the tower bottom of the debutanizer (2), and the other end of the tower kettle liquid level detector (20) is connected with the stable light hydrocarbon liquid level regulating valve (25).
8. The apparatus for purifying butane in the column pressure stabilization type debutanizer as claimed in claim 6, wherein: and the backflow tank (10) is also connected with a vent pipeline, and the vent pipeline is used for venting the non-condensable gas (32).
9. The apparatus for purifying butane in the column pressure stabilization type debutanizer as claimed in claim 8, wherein: and a constant-pressure air release valve (16) is installed on the air release pipeline.
10. The apparatus for purifying butane in a column pressure stabilized debutanizer according to claim 9, wherein: one end of the reflux tank pressure detector (11) is connected to the reflux tank (10), and the other end of the reflux tank pressure detector (11) is respectively connected with the reflux tank pressure regulating valve (12) and the constant-pressure air release valve (16).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010651183.9A CN111748387A (en) | 2020-07-08 | 2020-07-08 | Device and method for purifying butane by using column pressure stable debutanizer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010651183.9A CN111748387A (en) | 2020-07-08 | 2020-07-08 | Device and method for purifying butane by using column pressure stable debutanizer |
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| CN111748387A true CN111748387A (en) | 2020-10-09 |
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| CN202010651183.9A Pending CN111748387A (en) | 2020-07-08 | 2020-07-08 | Device and method for purifying butane by using column pressure stable debutanizer |
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| Country | Link |
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| CN (1) | CN111748387A (en) |
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2020
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