CN210855897U - For high content of CO2Ethane gas deep purification device - Google Patents
For high content of CO2Ethane gas deep purification device Download PDFInfo
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- CN210855897U CN210855897U CN201921110402.1U CN201921110402U CN210855897U CN 210855897 U CN210855897 U CN 210855897U CN 201921110402 U CN201921110402 U CN 201921110402U CN 210855897 U CN210855897 U CN 210855897U
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Abstract
The utility model provides a pair of high CO content2The device for deeply purifying ethane gas, the utility model discloses a two-cycle absorption desorption CO of amine liquid as absorption liquid, half barren solution and barren solution combination2、H2S and other impurities ensure CO in ethane2The content is reduced from 18.7 percent by mass to less than 100ppm, H2The S content is reduced to below 1ppm from 0.02 percent by mass, and the high CO content is deeply removed at one time2CO in ethane gas of2、H2S and the like, improves the purity of ethane products, greatly reduces the consumption of NaOH alkali liquor in downstream ethylene plants, and has higher economic benefit and environmental protection benefit.
Description
Technical Field
The utility model belongs to natural gas processing field, concretely relates to high CO that contains2Can carry out deep purification on the ethane gas, and can carry out deep purification on the high CO content2The ethane gas is deeply purified to remove most of CO2、H2S and other impurities, so that the ethane gas meets the quality requirement of a raw material for preparing ethylene by cracking, and the process is a process for recovering ethane from natural gas and an auxiliary device for implementing the process.
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, and the ethylene raw material C is internationally2-C4The proportion is about 48 percent, and China is restricted by raw materials, and naphtha is mainly used. 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.
Due to CO2The existence of the catalyst can cause adverse effect on the cracking of ethane, and the ethane gas is easy to generate dry ice in the low-temperature liquefaction process to freeze and block equipment such as a cold box, so that CO in the ethane product must be treated2Deep removal is carried out, but due to ethane and CO2Has low relative volatility, and condensed CO is generated when ethane and above light hydrocarbon are recovered from natural gas2All of the ethane gas is introduced into the ethane product, and the proportion of the ethane gas in the ethane product can be changedTo above 30%, and in the subsequent ethane cracking and cryogenic separation of ethylene, CO2As a poison for alkyne hydrogenation reaction, NaOH alkali liquor is required to be adopted for CO2Deep removal of 1 kg of CO227.6 kg of waste lye is generated and faces huge environmental protection pressure, so in the recovered ethane gas product, the quality index of the ethane gas product requires CO2The lower the content, the better, the CO content in the ethane gas product is generally required2Is less than 100 ppm.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide an it contains CO to high2The ethane gas deep purification device overcomes the technical defects.
In order to solve the technical problem, the utility model provides a pair of high CO content2The apparatus for deep purification of ethane gas of (1): comprises a decarburization absorption tower, the top of the decarburization absorption tower is connected with a gas-gas heat exchanger through a pipeline, and the inlet of the gas-gas heat exchanger is connected with a high CO content conveyor2The device comprises a pipeline of ethane raw gas, a gas-gas heat exchanger and a liquid-phase circulating pump, wherein one outlet of the gas-gas heat exchanger is connected to a decarburization absorption tower, the other outlet of the gas-gas heat exchanger is connected to a wet ethane purification-gas separator, the outlet of the wet ethane purification-gas separator and the outlet at the bottom of the decarburization absorption tower are respectively connected to a flash tank through pipelines, flash steam is discharged from a gas-phase discharge port of the flash tank, a liquid-phase discharge port of the flash tank is connected to the upper half section of an amine liquid regeneration tower through a pipeline, the outlet of the upper half section of the amine liquid regeneration tower is connected with a semi-lean amine liquid feed pump and a semi-lean amine liquid circulating pump which are connected in parallel through pipelines, the semi-lean amine liquid circulating pump is connected to the decarburization absorption tower through a semi-lean amine liquid air cooler, the semi-lean amine liquid feed pump is connected to, the other outlet of the lean-rich liquid heat exchanger is connected to the lower half section of the amine liquid regeneration tower through a pipeline, the lower half section of the amine liquid regeneration tower and a reboiler form a closed circulation pipeline through pipelines, and the reboiler is respectively connected with a heat conduction oil pipeline and a heat return oil pipeline;
the top outlet of the amine liquid regeneration tower is connected with a reflux tank through an overhead air cooler and an overhead water cooler, the reflux tank is provided with two outlets, one outlet is used for discharging regeneration tail gas, the other outlet is connected to the upper half section of the amine liquid regeneration tower through a reflux pump, and the inlet of the reflux tank is also connected with a pipeline for conveying desalted water.
The utility model also provides a high CO content2The process method for deeply purifying the ethane gas comprises the following steps:
s1, high CO content2The ethane raw gas is heated by a gas-gas heat exchanger and then enters the lower part of a decarburization absorption tower to reversely contact with semi-lean amine liquid and lean amine liquid in the decarburization absorption tower and carry out mass transfer to remove high CO content2CO in the ethane feed gas2And H2S, the treated ethane gas is generated, and CO is remained and absorbed2And H2The rich amine liquid of S is at the bottom of the decarburization absorption tower;
s2, pumping out ethane gas from the top of the decarbonization absorption tower, enabling the ethane gas to enter a gas-gas heat exchanger, cooling, enabling the ethane gas to enter a wet ethane purification gas separator for gas-liquid separation, separating wet ethane purified gas and liquid phase-amine-rich liquid, and enabling the wet ethane purified gas to enter a downstream processing device;
s3, respectively feeding the amine-rich liquid in the step S1 and the liquid phase-amine-rich liquid in the step S2 into a flash tank, after flash evaporation, feeding the gas phase in the flash tank into a downstream processing device, and feeding the amine-rich liquid into an amine liquid regeneration tower;
s4, the amine-rich liquid is contacted with the regenerated gas rising in the amine liquid regeneration tower in a countercurrent mode to carry out mass transfer, and CO in the amine-rich liquid is extracted and distilled2Pumping out the regeneration tail gas from the top of the amine liquid regeneration tower, cooling the regeneration tail gas by an overhead air cooler and an overhead water cooler, entering a reflux tank, allowing the gas phase in the reflux tank to enter a subsequent tail gas treatment device, and pressurizing the liquid phase by a reflux pump and then entering the amine liquid regeneration tower;
s5, extracting semi-lean amine liquid from the middle part of the amine liquid regeneration tower, wherein the semi-lean amine liquid is divided into two paths, and one path of the semi-lean amine liquid is pressurized by a circulating pump, cooled by a semi-lean amine liquid air cooler and then enters a decarburization absorption tower to serve as absorption liquid; the other path of semi-lean amine liquid enters the upper part of a stripping section of an amine liquid regeneration tower after being pressurized by a semi-lean amine liquid feeding pump and heated by a lean-rich liquid heat exchanger;
s6, allowing the semi-lean amine liquid entering the upper part of the stripping section of the amine liquid regeneration tower to descend in the amine liquid regeneration tower, carrying out mass transfer by countercurrent contact with ascending regeneration gas, and rectifying CO remained in the semi-lean amine liquid2And H2S；
S7, pumping out the bottom tower plate of the amine liquid regeneration tower, conveying the amine liquid on the tower plate to a reboiler, heating and heating through heat conduction oil, refluxing the gas to a gas phase space at the bottom of the amine liquid regeneration tower, and allowing the liquid to enter a product buffer section at the bottom of the amine liquid regeneration tower;
and S8, pumping the liquid in the tower bottom product buffer section, sending the liquid to a lean and rich liquid heat exchanger for cooling, then entering a lean liquid booster pump for boosting, entering a lean liquid water cooler for cooling, and then entering the upper half part of the decarburization absorption tower through boosting of a lean liquid circulating pump.
In the case of high CO content2The inlet of the lean liquid water cooler and the inlet of the tower top water cooler are respectively connected with a pipeline for conveying circulating water, and the outlet of the lean liquid water cooler and the outlet of the tower top water cooler are respectively connected with a pipeline for conveying the circulating water.
Further, the step S1 contains high content of CO2The temperature of ethane feed gas is 9.5 ℃, and is 30 ℃ after being heated by a gas-gas heat exchanger; the temperature of the ethane gas in the step S2 is 50 ℃, and the temperature is reduced to 26 ℃ through a gas-gas heat exchanger; and the pressure of the amine-rich liquid in the step S1 and the pressure of the liquid phase-amine-rich liquid in the step S2 before entering the flash tank are 3.0MPa, and the pressure is reduced to 0.6MPa after flash evaporation through the flash tank.
Further, the regeneration gas rising in the amine liquid regeneration tower in the step S4 is CO2And water; the temperature of the regeneration tail gas extracted from the top of the amine liquid regeneration tower is 62.6 ℃, and the temperature is reduced to 40 ℃ by cooling through an overhead air cooler and an overhead water cooler.
Further, the pressure of one path of the semi-lean amine liquid in the step S5 is increased from 0.06mpa.g to 3.0mpa.g by a circulating pump, and the temperature is reduced from 70 ℃ to 55 ℃ by cooling with a semi-lean amine liquid air cooler, and then the semi-lean amine liquid enters a decarburization absorption tower as an absorption liquid; the pressure of the other path of semi-lean amine liquid is increased from 0.06MPa.g to 0.08MPa.g by a semi-lean amine liquid feeding pump, and the temperature is increased from 70 ℃ to 93 ℃ by a lean rich liquid heat exchanger and then enters the upper part of a stripping section of an amine liquid regeneration tower.
Further, the regeneration gas rising in the amine liquid regeneration column in the step S6 is CO2、H2S and water.
Further, the temperature of the amine liquid sent to the reboiler in the step S7 is 117 ℃, and the amine liquid is heated to 118 ℃ through heat conduction oil;
further, in the step S8, the liquid in the buffer section of the tower bottom product is pumped out, the liquid level temperature is 118 ℃, the pressure is 0.08MPa, the liquid is sent to a lean and rich liquid heat exchanger to be cooled to 73 ℃, then the liquid enters a lean liquid booster pump to be pressurized to 0.1MPa, then the liquid is cooled to 50 ℃ by a lean liquid water cooler, and then the liquid is pressurized to 3.0MPa by a lean liquid circulating pump to enter the upper half part of the decarburization absorption tower.
Further, the step S1 contains high content of CO2The ethane content of the ethane feed gas is 76.43%, and CO2The mass content of the liquefied gas and the heavy hydrocarbon is 18.71 percent, the mass content of the methane is 0.48 percent, the mass content of the liquefied gas and the heavy hydrocarbon is 4.36 percent, and the mass content of the hydrogen sulfide is 0.02 percent;
the ethane content of the ethane gas decarbonized in the steps S1 and S2 was 93.58% by mass, and CO was contained in the ethane gas2The mass content of the liquefied gas and the heavy hydrocarbon is 0.000085%, the mass content of the methane is 0.59%, the mass content of the liquefied gas and the heavy hydrocarbon is 5.75%, the mass content of the saturated water is 0.0799%, and the balance is hydrogen sulfide;
in the step S3, the mass content of methane, the mass content of ethane and the mass content of CO in the gas phase in the flash tank are respectively 0.24%, 61.16%, and233.20% by mass, 3.27% by mass of liquefied gas, 2.09% by mass of saturated water and 0.04% by mass of hydrogen sulfide;
the ethane content of the regeneration tail gas in the step S4 is 0.33%, and CO is297.28% by mass, 0.02% by mass of liquefied gas, 2.26% by mass of saturated water and 0.11% by mass of hydrogen sulfide.
Furthermore, a liquid level meter and a liquid level regulating valve are arranged on the upper half section and the lower half section of the decarburization absorption tower, the wet ethane purification-gas separator, the flash tank, the amine liquid regeneration tower and the reflux tank;
a pressure gauge and a pressure regulating valve are arranged on a pipeline for discharging a gas phase from the flash tank and a pipeline for discharging regeneration tail gas from the reflux tank;
the inlet of the reflux tank is also connected with a pipeline for conveying demineralized water, a flow meter and a flow regulating valve are connected on the pipeline in series, and a connecting pipeline between the outlet of the semi-lean amine liquid air cooler and the decarburization absorption tower is also connected on the pipeline in series with the flow meter and the flow regulating valve;
the reboiler is respectively connected with an incoming heat conduction oil pipeline and a return heat conduction oil pipeline, the temperature of the incoming heat conduction oil is 225 ℃, the temperature of the return heat conduction oil is 185 ℃, and a thermometer and a temperature regulating valve are connected in series on a connecting pipeline between the incoming heat conduction oil pipeline and the amine liquid regeneration tower.
The utility model has the advantages as follows: the utility model provides a pair of high CO2The device for deeply purifying ethane gas can realize the purpose of purifying the ethane gas with high CO content2CO in ethane gas of2The average mass content is reduced from 18.7 percent to 85ppm, the mass content of hydrogen sulfide is reduced from 0.02 percent to 1ppm, the requirements of ethane raw materials of an ethylene plant and the requirements of low-temperature liquefaction and storage of ethane gas are completely met, and the energy consumption index reaches the international advanced level of 65.4kw for processing the heat load of 1 standard cubic meter of ethane raw material gas.
In order to make the above-mentioned aspects of the present invention more comprehensible, preferred embodiments are described in detail below with reference to the accompanying drawings.
Drawings
FIG. 1 shows the high CO content2A process flow diagram for deep purification of ethane gas.
Description of reference numerals:
1. high content of CO2An ethane feed gas; 2. a gas-gas heat exchanger; 3. a decarburization absorption tower; 4. a wet ethane purification gas separator; 5. wet ethane purification gas; 6. a flash tank; 7. an amine liquid regeneration tower; 8. a lean-rich liquid heat exchanger; 9. a semi-lean amine liquid feed pump; 10. a semi-lean amine liquid circulating pump; 11. a barren liquor booster pump; 12. a semi-lean amine liquid air cooler; 13. a barren liquor water cooler; 14. a barren liquor circulating pump; 15. an overhead air cooler; 16. a tower top water cooler; 17. a reflux tank;18. a reflux pump; 19. a reboiler; 20. a liquid level regulating valve; 21. a liquid level meter; 22. a pressure regulating valve; 23. a pressure gauge; 24. a flow regulating valve; 25. a flow meter; 26. a temperature regulating valve; 27. a thermometer; 28. to circulate water; 29. circulating water; 30. regenerating tail gas; 31. desalting water; 32. heat conducting oil; 33. returning the heat conducting oil; 34. gas phase in the flash tank.
Detailed Description
The embodiments of the present invention are described below in terms of specific embodiments, and other advantages and effects of the present invention will be readily apparent to those skilled in the art from the disclosure herein.
In the present invention, the upper, lower, left and right sides in the drawings are regarded as the high CO content in the present specification2The upper part, the lower part, the left part and the right part of the device for deeply purifying ethane gas.
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 an exhaustive and complete disclosure of the 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:
referring to fig. 1, a first embodiment of the present invention provides a method for controlling CO content2The apparatus for deep purification of ethane gas of (1): comprises a decarburization absorption tower 3, the top of the decarburization absorption tower 3 is connected with a gas-gas heat exchanger 2 through a pipeline, and gas are supplied to the decarburization absorption towerThe inlet of the heat exchanger 2 is connected with and conveys high CO content2The pipeline of ethane raw material gas 1, the gas-gas heat exchanger 2 is provided with two outlets, one outlet is connected to the decarburization absorption tower 3, the other outlet is connected to the wet ethane purification gas separator 4, the outlet of the wet ethane purification gas separator 4 and the outlet at the bottom of the decarburization absorption tower 3 are respectively connected to a flash tank 6 through pipelines, flash steam is discharged from a gas-phase discharge port of the flash tank 6, a liquid-phase discharge port of the flash tank 6 is connected to the upper half section of an amine liquid regeneration tower 7 through a pipeline, the outlet of the upper half section of the amine liquid regeneration tower 7 is connected with a semi-lean amine liquid feed pump 9 and a semi-lean amine liquid circulating pump 10 which are connected in parallel through pipelines, the semi-lean amine liquid circulating pump 10 is connected to the decarburization absorption tower 3 through a semi-lean amine liquid air cooler 12, the semi-lean amine liquid feed pump 9 is connected to the inlet of the lean-rich liquid heat exchanger 8 through, The lean liquid water cooler 13 and the lean liquid circulating pump 14 are connected to the decarburization absorption tower 3, the other outlet of the lean-rich liquid heat exchanger 8 is connected to the lower half section of the amine liquid regeneration tower 7 through a pipeline, the lower half section of the amine liquid regeneration tower 7 and the reboiler 19 form a closed circulation pipeline through a pipeline, and the reboiler 19 is respectively connected with a heat conduction oil 32 pipeline and a heat conduction oil return 33 pipeline;
the outlet at the top of the amine liquid regeneration tower 7 is connected with a reflux tank 17 through an overhead air cooler 15 and an overhead water cooler 16, the reflux tank 17 is provided with two outlets, one outlet is used for discharging regeneration tail gas 30, the other outlet is connected to the upper half section of the amine liquid regeneration tower 7 through a reflux pump 18, and the inlet of the reflux tank 17 is also connected with a pipeline for conveying desalted water 31.
Further, an inlet of the lean water cooler 13 and an inlet of the tower top water cooler 16 are connected to a pipeline for feeding the circulating water 28, respectively, and an outlet of the lean water cooler 13 and an outlet of the tower top water cooler 16 are connected to a pipeline for feeding the circulating water 29, respectively.
It should be noted that, in the above embodiment, the amine liquid is a novel selective desulfurization and decarburization solvent with excellent performance, and can be used for absorbing hydrogen sulfide in dry gas or liquid hydrocarbon, or carbon dioxide in acid gas. The amine liquid after absorbing the raw material gas impurities is called rich amine liquid, the amine liquid after heating regeneration (namely, removing hydrogen sulfide or carbon dioxide) is called poor amine liquid, and the amine liquid without completely removing hydrogen sulfide or carbon dioxide is called semi-poor amine liquid.
Mass transfer is a mass transfer process that occurs due to non-uniform mass concentration in the chemical industry field, in the material field, using gas-liquid systems. In particular, mass transfer is the process of mass transfer that occurs in a system due to non-uniform concentration of a substance. The entropy in the system automatically moves to the maximum value, namely, the entropy tends to be uniform, if the temperature of each part is not uniform, the entropy tends to be an average temperature, if the concentration is not uniform, the entropy also tends to be an average concentration, but the concentration transfer must occur between the fluids, can be between the two fluids, can also be between a fluid and a solid for mass transfer (such as extraction), but the mass transfer process cannot occur between the two solids (although the heat transfer process can occur). In the chemical industry, gas-liquid systems are commonly used; mass transfer process between liquid-liquid system and solid-liquid system.
Second embodiment:
the second embodiment of the present invention relates to a method for producing a high-content CO2Referring to fig. 1, the process method for deeply purifying ethane gas comprises the following steps:
s1, high CO content2The ethane feed gas 1 is heated by the gas-gas heat exchanger 2 and then enters the lower part of the decarburization absorption tower 3 to reversely contact with the semi-lean amine liquid and the lean amine liquid in the decarburization absorption tower 3 and carry out mass transfer to remove high CO content2CO in ethane feed gas 12And H2S, the treated ethane gas is generated, and CO is remained and absorbed2And H2The rich amine liquid of S is arranged at the bottom of the decarburization absorption tower 3;
s2, pumping ethane gas out of the top of the decarbonization absorption tower 3, enabling the ethane gas to enter a gas-gas heat exchanger 2, cooling, enabling the ethane gas to enter a wet ethane purification and gas separator 4 for gas-liquid separation, separating wet ethane purified gas 5 and liquid-phase amine-rich liquid, and enabling the wet ethane purified gas 5 to enter a downstream processing device;
s3, respectively feeding the amine-rich liquid in the step S1 and the liquid phase-amine-rich liquid in the step S2 into a flash tank 6, after flash evaporation, feeding the gas phase 34 in the flash tank into a downstream processing device, and feeding the amine-rich liquid into an amine liquid regeneration tower 7;
s4, the amine-rich liquid is contacted with the regenerated gas rising in the amine liquid regeneration tower 7 in a countercurrent mode to carry out mass transfer, and CO in the amine-rich liquid is extracted2Extracting a regeneration tail gas 30 from the top of the amine liquid regeneration tower 7, cooling the regeneration tail gas 30 by an overhead air cooler 15 and an overhead water cooler 16, feeding the cooled regeneration tail gas into a reflux tank 17, feeding a gas phase in the reflux tank 17 into a subsequent tail gas treatment device, and feeding a liquid phase into the amine liquid regeneration tower 7 after the liquid phase is pressurized by a reflux pump 18;
s5, extracting semi-lean amine liquid from the middle part of an amine liquid regeneration tower 7, wherein the semi-lean amine liquid is divided into two paths, and one path of the semi-lean amine liquid enters a decarburization absorption tower 3 as absorption liquid after being pressurized by a circulating pump 10 and cooled by a semi-lean amine liquid air cooler 12; the other path of semi-lean amine liquid enters the upper part of a stripping section of an amine liquid regeneration tower 7 after being pressurized by a semi-lean amine liquid feeding pump 9 and heated by a lean-rich liquid heat exchanger 8;
s6, the semi-lean amine liquid entering the upper part of the stripping section of the amine liquid regeneration tower 7 descends in the amine liquid regeneration tower 7, is in countercurrent contact with ascending regeneration gas for mass transfer, and rectifies CO remaining in the semi-lean amine liquid2And H2S；
S7, pumping out the bottom tower plate of the amine liquid regeneration tower 7, conveying the amine liquid on the tower plate to a reboiler 19, heating and raising the temperature through heat transfer oil, refluxing the gas to a gas phase space at the bottom of the amine liquid regeneration tower 7, and allowing the liquid to enter a product buffer section at the bottom of the amine liquid regeneration tower 7;
and S8, pumping the liquid in the tower bottom product buffer section, sending the liquid to a lean and rich liquid heat exchanger 8 for cooling, then entering a lean liquid booster pump 11 for boosting, entering a lean liquid water cooler 13 for cooling, and entering the upper half part of the decarburization absorption tower 3 through boosting by a lean liquid circulating pump 14.
It is particularly noted that the high content of CO2The ethane gas of (a) means CO contained in the ethane gas2The mass fraction of the lean amine liquid is less than 10 percent, and the gas-gas heat exchanger 2, the decarburization absorption tower 3, the wet ethane purification gas separator 4, the flash tank 6, the amine liquid regeneration tower 7, the lean solution heat exchanger 8, the semi-lean amine liquid feed pump 9, the semi-lean amine liquid circulating pump 10, the lean solution booster pump 11, the semi-lean amine liquid air cooler 12, the lean solution water cooler 13, the lean solution circulating pump 14, the tower top air cooler 15, the tower top water cooler 16, the reflux tank 17, the reflux pump 18, the reboiler 19, the liquid levelThe regulating valve 20, the liquid level meter 21, the pressure regulating valve 22, the pressure gauge 23, the flow regulating valve 24, the flow meter 25, the temperature regulating valve 26 and the thermometer 27 are all existing structures, and are commercially available, and the specific structures thereof do not serve as protection points of the present invention, and detailed description is not provided herein.
The utility model adopts the activated MDEA solution (amine liquid) as the absorption liquid, and the double-circulation absorption and removal of CO of the combination of the semi-barren solution and the barren solution2、H2S and other impurities ensure CO in ethane2The content is reduced from 18.7 percent by mass to less than 100ppm, H2The S content is reduced to below 1ppm from 0.02 percent by mass, and the energy consumption index reaches the international advanced level. The method is that the high CO content is in China2Deep removal of CO from ethane gas2、H2S and other impurities for the first time.
The third embodiment:
the embodiment is based on protection on high CO content2The practical implementation of the process for deeply purifying ethane gas, in particular, the high CO content2Has an ethane feed gas throughput of 76 × 104m3D, the pressure of the incoming gas is 3.0MPa, the temperature is 9.5 ℃, and the 'high CO content in pairs' with the same scale are set2The ethane gas deep purification device comprises 4 sets of devices, and comprises the following specific steps:
s1, high CO content2The temperature of the ethane feed gas 1 is raised from 9.5 ℃ to 30 ℃ through a gas-gas heat exchanger 2, then the ethane feed gas enters the lower part of a decarburization absorption tower 3, rises, reversely contacts with the semi-lean amine liquid and the lean amine liquid which descend in the decarburization absorption tower 3 and carries out mass transfer to remove CO in the ethane feed gas 12And H2S and other impurities to generate treated ethane gas, and the remaining impurities absorb CO2And H2The rich amine liquid of S is arranged at the bottom of the decarburization absorption tower 3;
s2, pumping out ethane gas from the top of a decarbonization absorption tower 3, feeding the ethane gas into a gas-gas heat exchanger 2, reducing the temperature from 50 ℃ to 26 ℃, then feeding the ethane gas into a wet ethane purification and gas separator 4 for gas-liquid separation, separating wet ethane purification gas 5 and liquid phase-amine-rich liquid, and feeding the wet ethane purification gas 5 into a downstream treatment device;
s3, absorbing CO in the step S12And H2S and other impurities in the rich amine liquid are extracted from the bottom of the decarburization absorption tower 3, the extracted rich amine liquid and the liquid-rich amine liquid in the step S2 respectively enter a flash tank 6 through a liquid level regulating valve 20, the pressure is reduced from 3.0MPa to 0.6MPa, after flash evaporation, the gas phase 34 in the flash tank enters a downstream processing device, and the rich amine liquid enters an amine liquid regeneration tower 7;
s4, the amine-rich liquid enters the upper half part of the rectifying section of the amine liquid regeneration tower 7, flows through the filler to descend under the action of gravity and is mixed with the CO ascending in the amine liquid regeneration tower 72The CO is contacted with regeneration gas such as water in a counter-current way for mass transfer, and CO in the amine-rich liquid is extracted2After impurities are mixed, the regeneration tail gas 30 is extracted from the top of the amine liquid regeneration tower 7, the regeneration tail gas 30 is cooled by an overhead air cooler 15 and an overhead water cooler 16, the temperature is reduced to 40 ℃ from 62.6 ℃, the regeneration tail gas enters a reflux tank 17, the gas phase in the reflux tank 17 enters a subsequent tail gas treatment device, and the liquid phase enters the amine liquid regeneration tower 7 after being pressurized by a reflux pump 18;
s5, extracting semi-lean amine liquid from the middle part of an amine liquid regeneration tower 7, wherein the semi-lean amine liquid is divided into two paths, one path of the semi-lean amine liquid (accounting for 63% of the total mass of the semi-lean amine liquid) is pressurized by a circulating pump 10, cooled by a semi-lean amine liquid air cooler 12 and then enters a decarburization absorption tower 3 to serve as absorption liquid, the pressure is increased from 0.06MPa.g to 3.0MPa.g, and the temperature is reduced from 70 ℃ to 55 ℃ to enter the middle part of the decarburization absorption tower 3 to serve as absorption liquid; pressurizing the other path of semi-lean amine liquid (accounting for 37 percent of the total mass of the semi-lean amine liquid) by a semi-lean amine liquid feeding pump 9, heating the semi-lean amine liquid by a lean rich liquid heat exchanger 8, pressurizing the semi-lean amine liquid from 0.06MPa.g to 0.08MPa.g, and raising the temperature from 70 ℃ to 93 ℃ to enter the upper part of a stripping section of an amine liquid regeneration tower 7;
s6, allowing the semi-lean amine liquid entering the upper part of the stripping section of the amine liquid regeneration tower 7 to flow through a filler to descend and to be mixed with rising CO under the action of gravity2、H2S and water are contacted with the regeneration gas in a countercurrent way for mass transfer, and CO remained in the semi-lean amine liquid is rectified2And H2S and other impurities;
s7, pumping out the bottom tower plate of the amine liquid regeneration tower 7, sending the amine liquid on the tower plate to a kettle type reboiler 19, heating the tower plate to 118 ℃ from 117 ℃ after heating the tower plate by heat-conducting oil, and generating 8.5% of gasGas (mainly water vapor, CO)2And H2S gas) flows back to the gas phase space at the bottom of the amine liquid regeneration tower 7, and the liquid enters the product buffer section at the bottom of the amine liquid regeneration tower 7;
s8, extracting 118 ℃ high-temperature lean amine liquid qualified in the buffer section of the tower bottom product, sending the high-temperature lean amine liquid to a lean and rich liquid heat exchanger 8 for cooling, reducing the temperature from 118 ℃ to 73 ℃, entering a lean liquid booster pump 11 for boosting, boosting the pressure from 0.08MPa to 0.1MPa, cooling to 50 ℃ through a lean liquid water cooler 13, boosting the pressure through a lean liquid circulating pump 14, boosting the pressure from 0.1MPa to 3.0MPa, and entering the upper half part of a decarburization absorption tower 3 through a liquid level regulating valve 20.
In particular, the high content of CO in the step S12The ethane content of the ethane raw material gas 1 was 76.43% by mass, and CO was contained2The mass content of the liquefied gas and the heavy hydrocarbon is 18.71 percent, the mass content of the methane is 0.48 percent, the mass content of the liquefied gas and the heavy hydrocarbon is 4.36 percent, and the mass content of the hydrogen sulfide is 0.02 percent; the ethane content of the ethane gas decarbonized in the steps S1 and S2 was 93.58% by mass, and CO was contained in the ethane gas2The mass content of the liquefied gas and the heavy hydrocarbon is 0.000085%, the mass content of the methane is 0.59%, the mass content of the liquefied gas and the heavy hydrocarbon is 5.75%, the mass content of the saturated water is 0.0799%, and the content of the hydrogen sulfide is lower than 1 ppm; in the step S3, the mass content of methane, the mass content of ethane and the mass content of CO in the gas phase 34 in the flash tank are respectively 0.24%, 61.16% and233.20% by mass, 3.27% by mass of liquefied gas, 2.09% by mass of saturated water and 0.04% by mass of hydrogen sulfide; the ethane content of the regeneration tail gas 30 in the step S4 is 0.33% by mass, and CO297.28% by mass, 0.02% by mass of liquefied gas, 2.26% by mass of saturated water and 0.11% by mass of hydrogen sulfide.
The decarbonization absorption tower 3, the wet ethane purification-gas separator 4, the flash tank 6, the upper half section and the lower half section of the amine liquid regeneration tower 7 and the reflux tank 17 are all provided with a liquid level meter 21 and a liquid level regulating valve 20; a pressure gauge 23 and a pressure regulating valve 22 are arranged on a pipeline for discharging a gas phase from the flash tank 6 and a pipeline for discharging regeneration tail gas 30 from the return tank 17; the inlet of the reflux tank 17 is also connected with a pipeline for delivering desalted water, the pipeline is connected with a flow meter 25 and a flow regulating valve 24 in series, and the connecting pipeline between the outlet of the semi-lean amine liquid air cooler 12 and the decarburization absorption tower 3 is also connected with the flow meter 25 and the flow regulating valve 24 in series; the reboiler 19 is respectively connected with a coming heat transfer oil 32 pipeline and a returning heat transfer oil 33 pipeline, the temperature of the coming heat transfer oil 32 is 225 ℃, the temperature of the returning heat transfer oil 33 is 185 ℃, and a thermometer 27 and a temperature regulating valve 26 are connected in series with a connecting pipeline between the coming heat transfer oil 32 pipeline and the amine liquid regeneration tower 7. In the above-described process, referring to fig. 1, the installation positions of the level control valve 20, the level meter 21, the pressure control valve 22, the pressure gauge 23, the flow control valve 24, the flow meter 25, the temperature control valve 26, and the temperature gauge 27 are shown, and specifically, in the present process, there are 2 flow meters 25, 6 level meters 21, 1 temperature gauge 27, 2 pressure gauges 23, 2 flow control valves 24, 2 pressure control valves 22, 1 temperature control valve 26, and 6 level control valves 20 in total.
In the present embodiment, the heating power of the reboiler 19 is 5005Kw, the temperature of the heat transfer oil is 225 degrees celsius, and the temperature of the oil return is 185 degrees celsius.
To sum up, the utility model adopts the activated MDEA solution (amine liquid) as the absorption liquid, the semi-barren solution and the barren solution to combine the double circulation absorption and removal of CO2、H2S and other impurities ensure CO in ethane2The content is reduced from 18.7 percent by mass to less than 100ppm, H2The S content is reduced to below 1ppm from 0.02 percent by mass, and the energy consumption index reaches the international advanced level. The method is that the high CO content is in China2Deep removal of CO from ethane gas2、H2S and other impurities for the first time.
It will be understood by those skilled in the art that the foregoing embodiments are specific to the implementation of the present invention and that various changes in form and details may be made therein without departing from the spirit and scope of the invention in its practical application.
Claims (3)
1. For high content of CO2The ethane gas deep purification device is characterized in that: comprises a decarburization absorption tower (3), the top of the decarburization absorption tower (3) is connected with a gas-gas heat exchanger (2) through a pipeline, and the inlet of the gas-gas heat exchanger (2) is connected with a high CO content delivery pipe2The pipeline of ethane raw material gas (1), the gas-gas heat exchanger (2) is provided with two outlets, one outlet is connected to a decarburization absorption tower (3), the other outlet is connected to a wet ethane purification-gas separator (4), the outlet of the wet ethane purification-gas separator (4) and the outlet at the bottom of the decarburization absorption tower (3) are respectively connected to a flash tank (6) through pipelines, flash steam is discharged out of a gas phase discharge port of the flash tank (6), a liquid phase discharge port of the flash tank (6) is connected to the upper half section of an amine liquid regeneration tower (7) through a pipeline, the outlet of the upper half section of the amine liquid regeneration tower (7) is connected with a semi-lean amine liquid feed pump (9) and a semi-lean amine liquid circulating pump (10) which are connected in parallel through pipelines, the semi-lean amine liquid circulating pump (10) is connected to the decarburization absorption tower (3) through a semi-lean amine liquid air cooler (12), and the semi-lean amine liquid feed pump, the lean-rich liquid heat exchanger (8) is provided with two outlets, one outlet is connected to the decarburization absorption tower (3) sequentially through a lean liquid booster pump (11), a lean liquid water cooler (13) and a lean liquid circulating pump (14), the other outlet of the lean-rich liquid heat exchanger (8) is connected to the lower half section of the amine liquid regeneration tower (7) through a pipeline, the lower half section of the amine liquid regeneration tower (7) forms a closed circulating pipeline with a reboiler (19) through a pipeline, and the reboiler (19) is respectively connected with a heat conduction oil (32) pipeline and a heat conduction oil return (33) pipeline;
the top outlet of the amine liquid regeneration tower (7) is connected with a reflux tank (17) through an overhead air cooler (15) and an overhead water cooler (16), the reflux tank (17) is provided with two outlets, one outlet is used for discharging regeneration tail gas (30), the other outlet is connected with the upper half section of the amine liquid regeneration tower (7) through a reflux pump (18), and the inlet of the reflux tank (17) is also connected with a pipeline for conveying desalted water (31).
2. The method of claim 1 for high CO content2The ethane gas deep purification device is characterized in that: the inlet of the lean liquid water cooler (13) and the inlet of the tower top water cooler (16) are respectively connected with a pipeline for conveying circulating water (28), and the outlet of the lean liquid water cooler (13) and the outlet of the tower top water cooler (16) are respectively connected with a pipeline for conveying circulating water (29).
3. Such as rightThe method according to claim 1 for high CO content2The ethane gas deep purification device is characterized in that: the upper half section and the lower half section of the decarburization absorption tower (3), the wet ethane purification-gas separator (4), the flash tank (6), the amine liquid regeneration tower (7) and the reflux tank (17) are respectively provided with a liquid level meter (21) and a liquid level regulating valve (20);
a pressure gauge (23) and a pressure regulating valve (22) are arranged on a pipeline for discharging a gas phase from the flash tank (6) and a pipeline for discharging regeneration tail gas (30) from the reflux tank (17);
the inlet of the reflux tank (17) is also connected with a pipeline for conveying desalted water, a flow meter (25) and a flow regulating valve (24) are connected on the pipeline in series, and a connecting pipeline between the outlet of the semi-lean amine liquid air cooler (12) and the decarburization absorption tower (3) is also connected on the pipeline in series with the flow meter (25) and the flow regulating valve (24);
the reboiler (19) is respectively connected with a coming heat conduction oil (32) pipeline and a returning heat conduction oil (33) pipeline, the temperature of the coming heat conduction oil (32) is 225 ℃, the temperature of the returning heat conduction oil (33) is 185 ℃, and a thermometer (27) and a temperature regulating valve (26) are connected in series with a connecting pipeline between the coming heat conduction oil (32) pipeline and the amine liquid regeneration tower (7).
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| CN110256188A (en) * | 2019-07-16 | 2019-09-20 | 西安长庆科技工程有限责任公司 | One kind containing CO to height2Ethane gas carry out deep purifying process and device |
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Effective date of registration: 20201106 Address after: 710018 Shaanxi province Xi'an Weiyang road Fengcheng four Changqing building Patentee after: XI'AN CHANGQING TECHNOLOGY ENGINEERING Co.,Ltd. Patentee after: CHINA NATIONAL PETROLEUM Corp. Address before: 710018 Shaanxi province Xi'an Weiyang road Fengcheng four Changqing building B201 Patentee before: XI'AN CHANGQING TECHNOLOGY ENGINEERING Co.,Ltd. |