CN117883929B - Device and process for treating and recovering tail gas discharged by carbon five processing industrial chain - Google Patents
Device and process for treating and recovering tail gas discharged by carbon five processing industrial chain Download PDFInfo
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- CN117883929B CN117883929B CN202410294948.6A CN202410294948A CN117883929B CN 117883929 B CN117883929 B CN 117883929B CN 202410294948 A CN202410294948 A CN 202410294948A CN 117883929 B CN117883929 B CN 117883929B
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a device and a process for treating and recycling tail gas discharged by a carbon five processing industrial chain, which belong to the technical field of treatment and comprehensive utilization and recycling of tail gas discharged by chemical equipment, and comprise the following steps: (1) The hydrocarbon tail gas containing hydrogen is subjected to combustion treatment in an overhead torch after acid gases such as H 2 S are removed; (2) The hydrocarbon tail gas containing oxygen is collected by a pipeline and then is burnt by a heat accumulating type thermal incinerator; (3) The hydrocarbon-containing tail gas without hydrogen and oxygen is controlled by a flowmeter and then enters a compressor to be boosted, then enters a drying tower to be dehydrated after being condensed and cooled, the dehydrated tail gas is cooled by a first heat exchanger and then enters a low-temperature liquid separating tank, nitrogen after the mixed light hydrocarbon at the bottom and the top of the tank are decompressed by a turbine expander is subjected to heat exchange and temperature rise by the first heat exchanger respectively, the mixed light hydrocarbon is sent to a raw material tank to be recovered, the warmed nitrogen enters a deoxidizing reactor to be deoxidized after second heat exchange and then is directly sent to a nitrogen pipe network of a whole plant as supplementary nitrogen, the recovery rate of the mixed light hydrocarbon is more than 98%, and the recovery rate of the nitrogen is more than 98%.
Description
Technical Field
The invention relates to the technical field of treatment and comprehensive utilization and recovery of tail gas discharged by a chemical device, in particular to a device and a process for treating and recovering tail gas discharged by a carbon five processing industrial chain.
Background
The cracking carbon five is a byproduct of ethylene cracking, and accounts for about 10% -15% of the total yield of ethylene, and in recent years, with the rapid development of the ethylene industry in China, comprehensive utilization of the cracking carbon five is emphasized, and most production enterprises start to be matched with a cracking carbon five separation and hydrogenation device, a piperylene comprehensive utilization device and an isoprene comprehensive utilization device. The exhaust pipe network discharged by the carbon five processing and utilizing device has a large amount of effective components, and the exhaust pipe network has more and more expensive components such as: isoprene, piperylene, isopentene, isopentane, n-pentane, isobutene, isobutane, n-butane, and the like; in order to reduce the emission of effective tissues in the flare gas, part of the flare gas is pressurized by a compressor, water-cooled to 40 ℃ for separation, and after heavy components in the flare gas are recovered, light components are directly discharged into a fuel gas pipe network for combustion, so that great waste of resources is caused.
CN103252107B discloses a method and a device for recovering high boiling point material flare gas with an atmospheric boiling point of not less than 80 ℃, the method and the device for recovering high boiling point material flare gas with an atmospheric boiling point of not less than 80 ℃ are used for recovering high yield, and the method has the advantages of low investment, low energy consumption and high efficiency, but cannot recover carbon five components with the boiling point of less than 80 ℃.
CN114752401B discloses a method for recovering flare gas during overhauling of an oilfield associated gas treatment plant, which processes and recovers the flare gas during overhauling of the oilfield associated gas treatment plant, and produces heavy hydrocarbon and Compressed Natural Gas (CNG) products through four times of decompression heat exchange and separation, but when the system is used for refrigerating, an additional mixed hydrocarbon refrigerant compression throttling refrigerating unit is needed, and the energy consumption is relatively high.
CN111578619a discloses a method for recovering light hydrocarbon and nitrogen in an olefin flare pipe network, which is to condense and cool gas in the olefin flare pipe network, separate two towers to obtain products such as nitrogen, methane-rich gas and light hydrocarbon, compress the external refrigerant by a compressor, exchange heat, decompress and cool the refrigerant by a throttle valve to obtain cold energy, and has higher energy consumption.
Disclosure of Invention
The invention aims to solve the technical problems of insufficient recovery of carbon five components, high energy consumption in the recovery process and substandard recovery quality in the prior art, and provides a device and a process for treating and recovering tail gas discharged from a carbon five processing industry chain, wherein light hydrocarbon and nitrogen products are recovered from hydrocarbon-containing waste gas in a cryogenic separation mode, the recovered light hydrocarbon products are used as carbon five separation raw materials, and refined nitrogen is used as supplementary nitrogen and is directly fed into a nitrogen pipe network of a whole plant, so that the effective components in the hydrocarbon-containing waste gas are fully utilized, and the recovery benefit is remarkable.
The invention provides a carbon five processing industry chain exhaust treatment and recovery process: the method comprises the following steps:
(1) Hydrogen-containing hydrocarbon tail gas overhead torch combustion treatment
The low-pressure separation tank exhaust and the stripping tower top exhaust of the hydrogenation reactor enter a hydrogen-containing hydrocarbon exhaust buffer tank, the gas phase at the top of the hydrogen-containing hydrocarbon exhaust buffer tank enters a desulfurizing tank to remove H 2 S gas, then enter a liquid separation tank to separate liquid drops with the diameter of more than 300 mu m, and the hydrogen-containing hydrocarbon exhaust enters an overhead torch for burning after being sealed by a water seal tank;
(2) Incineration treatment of hydrocarbon tail gas containing oxygen
The hydrocarbon tail gas containing oxygen discharged from a vacuum system, a normal pressure storage tank and other equipment and facilities enters an oxygen-containing hydrocarbon tail gas buffer tank, and the gas phase at the top of the oxygen-containing hydrocarbon tail gas buffer tank is pressurized by a centrifugal fan and then enters a heat accumulating type thermal incinerator for incineration, and the tail gas reaches the standard and is discharged;
(3) Compression condensation recovery treatment of hydrocarbon-containing tail gas without hydrogen and oxygen
The pressure of the hydrocarbon-containing tail gas which is discharged by the carbon five processing and utilizing device and does not contain hydrogen and oxygen is controlled to be 100-110kPa, one part of the hydrocarbon-containing tail gas is metered by a flowmeter I and then enters an oxygen-containing hydrocarbon tail gas buffer tank through a cut-off valve II and a regulating valve, the other part of the hydrocarbon-containing tail gas enters the hydrocarbon-containing tail gas buffer tank through the cut-off valve I, the top gas phase enters a compressor to be boosted to be more than 2000kPa under the control of the flowmeter II and then enters a water cooler, the temperature is controlled to be 20-50 ℃ and then enters a drying tower to be dehydrated, a 3A molecular sieve is filled in the drying tower, the tower top dehydrated tail gas is cooled to be less than 80 ℃ through a first heat exchanger and then enters a low-temperature separation tank, mixed light hydrocarbon at the bottom of the low-temperature separation tank and nitrogen at the top of the low-temperature separation tank after being decompressed to be less than 400kPa through a turbine expander are respectively subjected to heat exchange and temperature rise, the mixed light hydrocarbon is fed into a raw material tank to be recovered after being heated to be subjected to heat exchange through a second heat exchanger to be 20-40 ℃ and then enters a deoxidization reactor to be deoxidized, and then enters a whole factory nitrogen pipe network, and the deoxidization catalyst is filled in the reactor to be charged with brand-2000 UT.
Further, in the step (1), the zinc oxide desulfurizing agent with high sulfur capacity is filled in the desulfurizing tank, the sulfur capacity is more than 30%, and the operating temperature of the desulfurizing tank is 20-60 ℃.
In order to achieve the above object, the device for the carbon five processing industry chain exhaust gas treatment and recovery process provided by the invention comprises: a hydrogen-containing hydrocarbon tail gas treatment device, a hydrogen-free oxygen-containing hydrocarbon tail gas treatment device, and an oxygen-containing hydrocarbon tail gas treatment device;
the hydrogen-containing hydrocarbon tail gas treatment device comprises a hydrogen-containing hydrocarbon tail gas buffer tank, a desulfurizing tank, a liquid separating tank, a water sealing tank and an overhead torch which are sequentially communicated;
the oxygen-containing hydrocarbon tail gas treatment device comprises an oxygen-containing hydrocarbon tail gas buffer tank, a centrifugal fan and a heat accumulating type thermal incinerator which are sequentially communicated;
The hydrocarbon-containing tail gas treatment device without hydrogen and oxygen comprises a hydrocarbon-containing tail gas buffer tank, a compressor, a water cooler and a drying tower which are sequentially communicated, wherein an outlet of the drying tower is communicated with a gas inlet in the middle of a first heat exchanger, a gas outlet in the middle of the first heat exchanger is communicated with a low-temperature liquid separating tank, a gas outlet in the top of the low-temperature liquid separating tank is communicated with a turboexpander, an outlet of the turboexpander is communicated with a gas inlet in the top of the first heat exchanger, a gas outlet in the top of the first heat exchanger is communicated with a second heat exchanger, the second heat exchanger is communicated with an oxygen removal reactor, a liquid outlet in the bottom of the low-temperature liquid separating tank is communicated with a liquid inlet in the bottom of the first heat exchanger, and a liquid outlet in the bottom of the first heat exchanger is communicated with a mixed light hydrocarbon collecting device.
A pipeline for allowing hydrocarbon-containing tail gas without hydrogen and oxygen to enter the hydrocarbon-containing tail gas buffer tank is provided with a first flowmeter and a first cut-off valve, and a second flowmeter is arranged between the hydrocarbon-containing tail gas buffer tank and the compressor;
Two branch lines are arranged between the first flowmeter and the first pipeline of the shut-off valve, one branch line is communicated with the inlet of the liquid separating tank, and the third shut-off valve is arranged on the branch line; the other branch line is communicated with the inlet of the oxygen-containing hydrocarbon tail gas buffer tank, and a second cut-off valve and a regulating valve are arranged on the branch line.
Compared with the prior art, the invention has the beneficial effects that:
1. According to the invention, a hydrocarbon-containing tail gas recovery control system is added in the process, so that the safe and stable recovery of hydrocarbon-containing tail gas is ensured, a conventional gas holder is eliminated, the investment and the operation cost are reduced to the greatest extent, in case of emergency, the hydrocarbon-containing tail gas without hydrogen and oxygen directly enters a liquid separation tank, and then enters an overhead torch for combustion treatment after being sealed by a water seal tank, thereby improving the safety of the whole application of the device;
2. The cryogenic separation in the process adopts the production method of the cryogenic technology, and under the condition that the gas does not need any extra power, the pressure energy of the gas is utilized to convert the pressure energy into cold energy through cyclic expansion refrigeration, and then the cold energy is utilized to fully cool and liquefy hydrocarbons in hydrocarbon-containing waste gas and then separate the hydrocarbons, namely, tail gas is subjected to thermal expansion in an expander to consume internal energy of the tail gas to do work externally, so that nitrogen and hydrocarbons are separated, and the operation energy consumption and cost are reduced;
3. The process of the invention classifies and recovers the discharged tail gas of each device in the carbon five industrial chain, ensures the standard discharge of the final tail gas, recovers the light hydrocarbon to the maximum extent, simultaneously obtains refined nitrogen, the recovery rate of the mixed light hydrocarbon is more than 98%, the recovery rate of the refined nitrogen is more than 98%, and the refined nitrogen is directly sent into a nitrogen pipe network of the whole plant as supplementary nitrogen, so that the effective components in the discharged tail gas are fully and reasonably recycled, and the process is safe and stable, has low operation energy consumption and obvious recovery benefit.
Drawings
FIG. 1 is a schematic diagram of an apparatus and process for treating and recovering tail gas from a carbon-five process industrial chain of the present invention.
Reference numerals:
1. A hydrogen-containing hydrocarbon tail gas buffer tank; 2. a desulfurizing tank; 3. a liquid separating tank; 4. a water sealed tank; 5. an overhead torch; 6. a first flowmeter; 7. a first cut-off valve; 8. a hydrocarbon-containing tail gas buffer tank; 9. a second flowmeter; 10. a compressor; 11. a water cooler; 12. a drying tower; 13. a first heat exchanger; 14. a low-temperature liquid separating tank; 15. a turbine expander; 16. a second heat exchanger; 17, deoxidizing reactor; 18. a second shut-off valve; 19. a regulating valve; 20. an oxygen-containing hydrocarbon tail gas buffer tank; 21. a centrifugal fan; 22. a regenerative thermal incinerator; 23. and a shut-off valve III.
Detailed Description
The invention is described in further detail below with reference to fig. 1 and the examples.
The tail gas discharged from the carbon five processing industry chain is divided into hydrogen-containing hydrocarbon tail gas, oxygen-containing hydrocarbon tail gas and hydrocarbon-containing tail gas without hydrogen and oxygen, and then the hydrogen-containing hydrocarbon tail gas is treated respectively, the tail gas discharged from a low-pressure separating tank of a hydrogenation reactor and the tail gas discharged from the top of a stripping tower are mainly hydrogen-containing hydrocarbon tail gas, the tail gas discharged from a vacuum system, a normal-pressure storage tank and other equipment facilities is mainly oxygen-containing hydrocarbon tail gas, and the hydrocarbon-containing tail gas discharged from a device is hydrogen-free and oxygen-free except the two types of tail gas;
the invention provides a carbon five processing industry chain emission tail gas treatment and recovery process, which comprises the following steps:
(1) Hydrogen-containing hydrocarbon tail gas overhead torch combustion treatment
The low-pressure separation tank exhaust and the stripping tower top exhaust of the hydrogenation reactor enter a hydrogen-containing hydrocarbon exhaust buffer tank 1, the gas phase at the top of the hydrogen-containing hydrocarbon exhaust buffer tank 1 enters a desulfurization tank 2, a zinc oxide desulfurizing agent with high sulfur capacity is filled in the desulfurization tank 2, the sulfur capacity is more than 30%, the operation temperature of the desulfurization tank 2 is controlled to be 20-60 ℃, then the hydrogen-containing hydrocarbon exhaust enters a liquid separation tank 3 to separate liquid drops with the diameter of more than 300 mu m, and the hydrogen-containing hydrocarbon exhaust enters an overhead torch 5 for combustion after being sealed by a water seal tank 4;
(2) Incineration treatment of hydrocarbon tail gas containing oxygen
The hydrocarbon tail gas containing oxygen discharged from a vacuum system, a normal pressure storage tank and other equipment and facilities enters an oxygen-containing hydrocarbon tail gas buffer tank 20, the gas phase at the top of the oxygen-containing hydrocarbon tail gas buffer tank 20 is pressurized by a centrifugal fan 21 and enters a heat accumulating type thermal incinerator 22 for incineration, and the tail gas reaches the standard and is discharged;
(3) Compression condensation recovery treatment of hydrocarbon-containing tail gas without hydrogen and oxygen
The pressure of the hydrocarbon-containing tail gas which is discharged by the carbon five processing and utilizing device and does not contain hydrogen and oxygen is controlled to be 100-110kPa, one part of the hydrocarbon-containing tail gas is metered by a first flowmeter and then enters an oxygen-containing hydrocarbon tail gas buffer tank 20 through a second cut-off valve 18 and a regulating valve 19, the other part of the hydrocarbon-containing tail gas enters a hydrocarbon-containing tail gas buffer tank 8 through a first cut-off valve 7, the gas phase at the top of the hydrocarbon-containing tail gas buffer tank 8 enters a compressor 10 to be boosted to be more than 2000kPa and then enters a water cooler 11 under the control of a second flowmeter 9, the outlet temperature of the water cooler 11 is controlled to be 20-50 ℃, the hydrocarbon-containing tail gas enters a drying tower 12 filled with a 3A molecular sieve for dehydration, the dehydrated tail gas is cooled to be below-80 ℃ through a first heat exchanger 13, then enters a low-temperature liquid separating tank 14, mixed light hydrocarbon at the bottom of the low-temperature separating tank 14 enters a heat exchange from a liquid inlet at the bottom of the first heat exchanger 13, the temperature is controlled to be below-5 ℃, and the mixed light hydrocarbon at the bottom liquid outlet of the first heat exchanger 13 can be collected;
Nitrogen in the low-temperature liquid separating tank 14 enters the turbine expander 15 from a gas outlet at the top of the low-temperature liquid separating tank 14 to be depressurized to 400kPa, then enters the first heat exchanger 13 from a gas inlet at the top to exchange heat, nitrogen discharged from the gas outlet at the top of the first heat exchanger 13 enters the second heat exchanger 16, the temperature is controlled to be 20-40 ℃, the nitrogen enters the deoxidizing reactor 17 to deoxidize, deoxidizing catalyst with the brand UT-2000 is filled in the deoxidizing reactor 17, and the obtained refined nitrogen is sent into a nitrogen pipe network of the whole plant.
Further, specific examples of the process according to the present invention are given below:
example 1
(1) Hydrogen-containing hydrocarbon tail gas overhead torch combustion treatment
The hydrogen-containing hydrocarbon tail gas enters a hydrogen-containing hydrocarbon tail gas buffer tank 1, the gas phase at the top of the hydrogen-containing hydrocarbon tail gas buffer tank 1 enters a desulfurizing tank 2, a zinc oxide desulfurizing agent with high sulfur capacity is filled in the desulfurizing tank 2, the sulfur capacity is 30%, the temperature of the desulfurizing tank is controlled at 20 ℃, H 2 S gas is removed, the desulfurizing tank enters a liquid separating tank 3, liquid drops with the diameter of more than 300 mu m are separated, and the liquid drops enter an overhead torch 5 for combustion after being sealed by a water sealing tank 4;
(2) The hydrocarbon tail gas containing oxygen enters an oxygen-containing hydrocarbon tail gas buffer tank 20, the gas phase at the top of the oxygen-containing hydrocarbon tail gas buffer tank 20 is pressurized by a centrifugal fan 21 and then enters a heat accumulating type thermal incinerator 22 for incineration, and the tail gas reaches the standard and is discharged;
(3) Compression condensation recovery treatment of hydrocarbon-containing tail gas without hydrogen and oxygen
The pressure of the hydrocarbon-containing tail gas without hydrogen and oxygen is controlled at 100kPa, one part of the hydrocarbon-containing tail gas is metered by a flowmeter I and then enters an oxygen-containing hydrocarbon tail gas buffer tank 20 through a cut-off valve II 18 and a regulating valve 19, the other part of the hydrocarbon-containing tail gas is fed into a hydrocarbon-containing tail gas buffer tank 8 through a cut-off valve I7, the top gas phase of the hydrocarbon-containing tail gas buffer tank 8 enters a compressor 10 under the control of a flowmeter II and a regulating valve 19 to be boosted to more than 2000kPa and then enters a water cooler 11, the outlet temperature of the water cooler 11 is controlled at 20 ℃, the hydrocarbon-containing tail gas enters a drying tower 12 from the bottom to be dehydrated, a 3A molecular sieve is filled in the drying tower 12 and is used for removing trace moisture in the hydrocarbon-containing tail gas, the dehydrated hydrocarbon-containing tail gas is cooled to-80 ℃ through a first heat exchanger 13, the top nitrogen enters a turbo expander 15 for expansion refrigeration, the outlet pressure of the turbo expander 15 is controlled at 400kPa, the temperature of the expanded nitrogen enters a first heat exchanger 13 to supply cold energy, the nitrogen is controlled at 20 ℃ through a second heat exchanger 16, and then enters a deoxidizing catalyst 17 filled in a UT-2000 oxygen-removing catalyst, and is directly fed into a full-nitrogen pipe network as a full-supply nitrogen source.
Example 2
The procedure of this embodiment is the same as that of embodiment one
In the step (1), a zinc oxide desulfurizing agent is added into a desulfurizing tank 2, the sulfur capacity is 40%, and the temperature of the desulfurizing tank is controlled at 40 ℃;
In the step (3), hydrocarbon-containing tail gas without hydrogen and oxygen is controlled at 110kPa, enters a compressor 10 to be boosted to 3000kPa, enters a water cooler 11, enters a drying tower 12 to be dehydrated after the outlet temperature of the water cooler 11 is 35 ℃, then enters a low-temperature liquid separation tank 14 after being cooled to-80 ℃ by a first heat exchanger 13, enters a turbo expander 15 to be expanded and refrigerated at top nitrogen, the outlet pressure of the turbo expander 15 is controlled at 400kPa, and after the depressurized nitrogen is subjected to heat exchange by the first heat exchanger 13, the temperature of the depressurized nitrogen is controlled at 20 ℃ by a second heat exchanger 16 and enters a deoxidizing reactor 17 filled with UT-2000 oxygen catalyst.
Example 3
The procedure of this embodiment is the same as that of embodiment one
In the step (3), hydrocarbon-containing tail gas without hydrogen and oxygen is controlled at 110kPa, enters a compressor 10 to be boosted to 3000kPa, enters a water cooler 11, enters a drying tower 12 to be dehydrated after the outlet temperature of the water cooler 11 is 40 ℃, then enters a low-temperature liquid separating tank 14 after being cooled to minus 100 ℃ by a first heat exchanger 13, enters a turbine expander 15 to be expanded and refrigerated at top nitrogen, the outlet pressure of the turbine expander 15 is controlled at 400kPa, and after the depressurized nitrogen is subjected to heat exchange by the first heat exchanger 13, the temperature of the depressurized nitrogen is controlled at 40 ℃ by a second heat exchanger 16 and enters a deoxidizing reactor 17 filled with UT-2000 oxygen catalyst.
Example 4
The procedure of this embodiment is the same as that of embodiment one
In the step (1), a zinc oxide desulfurizing agent is added into a desulfurizing tank 2, the sulfur capacity is 40%, and the temperature of the desulfurizing tank is controlled at 60 ℃;
In the step (3), hydrocarbon-containing tail gas without hydrogen and oxygen is controlled at 110kPa, enters a compressor 10 to be boosted to 3000kPa, enters a water cooler 11, enters a drying tower 12 to be dehydrated after the outlet temperature of the water cooler 11 is 50 ℃, then enters a low-temperature liquid separation tank 14 after being cooled to-85 ℃ by a first heat exchanger 13, enters a turbo expander 15 to be expanded and refrigerated at top nitrogen, the outlet pressure of the turbo expander 15 is controlled at 380kPa, and after the depressurized nitrogen is subjected to heat exchange by the first heat exchanger 13, the temperature of the depressurized nitrogen is controlled at 40 ℃ by a second heat exchanger 16 and enters a deoxidizing reactor 17 filled with UT-2000 oxygen catalyst.
The device for the carbon five processing industry chain exhaust tail gas treatment and recovery technology provided by the invention comprises: a hydrogen-containing hydrocarbon tail gas treatment device, a hydrogen-free oxygen-containing hydrocarbon tail gas treatment device, and an oxygen-containing hydrocarbon tail gas treatment device;
The hydrogen-containing hydrocarbon tail gas treatment device comprises a hydrogen-containing hydrocarbon tail gas buffer tank 1, a desulfurization tank 2, a liquid separating tank 3, a water sealing tank 4 and an overhead torch 5 which are sequentially communicated; the hydrogen-containing hydrocarbon tail gas is subjected to removal of acid gases such as H 2 S and the like through the desulfurization tank 2, the emission of the S-containing gases in the tail gas is reduced, the pollution to the environment is reduced, the liquid drops with the diameters larger than 300 mu m are separated after the hydrogen-containing hydrocarbon tail gas subjected to removal of the acid gases enters the liquid separating tank 3, combustion rain is avoided when the subsequent overhead torch is burnt, corrosion is caused to equipment, meanwhile, the combustion treatment of the tail gas is influenced, tempering cannot occur when the overhead torch is burnt due to the existence of the water sealing tank, and the use safety of the equipment is improved.
The oxygen-containing hydrocarbon tail gas treatment device comprises an oxygen-containing hydrocarbon tail gas buffer tank 20, a centrifugal fan 21 and a heat accumulating type thermal incinerator 22 which are sequentially communicated; the oxygen-containing hydrocarbon tail gas is purified after being burnt by the thermal oxidation furnace 22, and simultaneously the heat released during decomposition can be recovered, thereby achieving the dual purposes of environmental protection and energy saving.
The hydrocarbon-containing tail gas treatment device without hydrogen and oxygen comprises a hydrocarbon-containing tail gas buffer tank 8, a compressor 10, a water cooler 11 and a drying tower 12 which are sequentially communicated, wherein the outlet of the drying tower 12 is communicated with a gas inlet in the middle part of a first heat exchanger 13, and the gas outlet in the middle part of the first heat exchanger 13 is communicated with a low-temperature liquid separating tank 14; the top gas outlet of the low-temperature liquid separating tank 14 is communicated with a turbine expander 15, the outlet of the turbine expander 15 is communicated with the top gas inlet of the first heat exchanger 13, the top gas outlet of the first heat exchanger 13 is communicated with a second heat exchanger 16, and the second heat exchanger 16 is communicated with a deoxidization reactor 17; the bottom liquid outlet of the low-temperature liquid separating tank 14 is communicated with the bottom liquid inlet of the first heat exchanger 13, and the bottom liquid outlet of the first heat exchanger 13 is communicated with the mixed light hydrocarbon collecting device;
The first heat exchanger 13 adopts a plate-fin heat exchanger, the second heat exchanger 16 adopts a tube-type heat exchanger, the temperature of the hydrocarbon-containing tail gas is reduced after being compressed by the compressor 10, the temperature of the hydrocarbon-containing tail gas is reduced again after passing through the water cooler 11, the moisture in the hydrocarbon-containing tail gas can be removed through the drying tower 12, the hydrocarbon-containing tail gas is subjected to heat exchange and temperature reduction by the first heat exchanger 13 and enters the low-temperature liquid separating tank 14, the light hydrocarbon component in the hydrocarbon-containing tail gas is liquefied under the low temperature condition, the liquefied light hydrocarbon component is subjected to heat exchange by the first heat exchanger 13 again, the rest of the liquefied light hydrocarbon component is mainly nitrogen, the nitrogen enters the turbine expander 15 from the top of the low-temperature liquid separating tank 14 to reduce the pressure to 400kPa, the nitrogen is reduced in the pressure reduction process, the nitrogen is subjected to temperature reduction again through the first heat exchanger 13, and the released cold energy can be used for reducing the temperature of the hydrocarbon-containing tail gas entering the first heat exchanger 13, and the temperature of the nitrogen reaches the requirement of the deoxidizing reactor 17 after passing through the second heat exchanger 16;
Meanwhile, the liquefied low-temperature light hydrocarbon component can realize cooling through heat exchange by the first heat exchanger 13 and the hydrocarbon-containing tail gas entering the first heat exchanger 13, a first flowmeter 6 is sequentially arranged between pipelines of the hydrocarbon-containing tail gas which does not contain hydrogen and oxygen and enters the hydrocarbon-containing tail gas buffer tank 8, a second flowmeter 9 is arranged between the hydrocarbon-containing tail gas buffer tank 8 and the compressor 10, a second flowmeter 9 and a regulating valve 19 are arranged between the hydrocarbon-containing tail gas buffer tank 8 and the oxygen-containing hydrocarbon tail gas buffer tank 20, and the second flowmeter 9 and the regulating valve 19 are electrically connected; under normal conditions, the first flowmeter 6 can effectively control the hydrocarbon-containing tail gas to smoothly enter the hydrocarbon-containing tail gas buffer tank 8, the second flowmeter 9 controls the hydrocarbon-containing tail gas to smoothly enter the compressor 10 from the hydrocarbon-containing tail gas buffer tank 8, meanwhile, the second flowmeter 9 monitors the pressure at the outlet of the hydrocarbon-containing tail gas buffer tank 8, and the quantity of the hydrocarbon-containing tail gas which does not contain hydrogen or oxygen entering the oxygen-containing hydrocarbon tail gas buffer tank 20 is controlled in real time through the linkage regulating valve 19.
A first flowmeter 6 and a first cut-off valve 7 are arranged on a pipeline of the hydrocarbon-containing tail gas which does not contain hydrogen and oxygen and enters the hydrocarbon-containing tail gas buffer tank 8, a second flowmeter 9 is arranged between the hydrocarbon-containing tail gas buffer tank 8 and the compressor 10, two branch lines are arranged between the first flowmeter 6 and the first cut-off valve 7, one branch line is communicated with an inlet of the liquid separating tank 3, and a third cut-off valve 23 is arranged on the branch line; the other branch line is communicated with the inlet of the oxygen-containing hydrocarbon tail gas buffer tank 20, and a second cut-off valve 18 and a regulating valve 19 are arranged on the branch line, so that when an emergency situation occurs in the hydrocarbon-containing tail gas pipeline which does not contain hydrogen and oxygen, the first cut-off valve 7 and the hydrocarbon-containing tail gas buffer tank 8 can be linked through a controller; when the pressure in the hydrocarbon-containing tail gas buffer tank 8 exceeds a limit value, the first cut-off valve 7 is closed, the second cut-off valve 18 is closed, the third cut-off valve 23 is opened, and the hydrocarbon-containing tail gas directly enters the liquid separating tank 3 and is combusted through the overhead torch 5 after passing through the water sealed tank 4.
The hydrocarbon-containing tail gas contains nitrogen, propane, propylene, n-butane, isobutane, 1-butene, 2-butene, isobutene, n-pentane, isopentane, isopentene, isoprene, piperylene, and small amounts of ethane, ethylene, other carbon five and trace amounts of methane, hexane and oxygen.
The hydrocarbon-containing tail gas without hydrogen and oxygen is subjected to compression condensation treatment, the recovery rate of mixed light hydrocarbon is more than 98%, the recovery rate of refined nitrogen is more than 98%, the content of N 2 in the refined nitrogen product is more than 99.5%, and the content of O 2 is less than 5 mL/m; the tail gas is treated in advance in the carbon five processing process, so that the recovery rate of the mixed light hydrocarbon is higher than 92% in the prior art, and the recovery rate of nitrogen is also higher than 95% in the prior art.
According to the carbon five processing industry chain emission tail gas treatment and recovery device and process, the emission tail gas is classified and then treated and recovered, so that the emission of the final tail gas reaches the standard, the light hydrocarbon is recovered to the maximum extent, a cracking carbon five comprehensive utilization factory with the emission amount of flare gas of about 0.6 ton to 1 ton per year is realized, the weight of an effective component is about 0.1 ton to 0.2 ton per hour, 400 to 800 yuan per hour is burnt according to 4000 yuan of the light hydrocarbon, the annual burning cost is about 320 to 640 ten yuan according to 8000 hours per year, and the carbon five processing industry chain emission tail gas treatment and recovery device disclosed by the invention can benefit from 200 to 380 ten thousand yuan per year; refined nitrogen can be obtained while recycling, and the refined nitrogen is directly fed into a nitrogen pipe network of a whole plant as supplementary nitrogen, so that effective components in the discharged tail gas are fully and reasonably recycled, the process is safe and stable, the operation energy consumption is low, and the recycling benefit is remarkable.
The device and the process for treating and recovering the tail gas discharged by the carbon five processing industry chain can also have various changes and modifications, are not limited to the specific structure of the embodiment, and in summary, the protection scope of the invention should include those changes or substitutions and modifications obvious to those skilled in the art.
Claims (3)
1. The process for treating and recovering the tail gas discharged by the carbon five processing industrial chain is characterized by comprising the following steps of:
(1) Hydrogen-containing hydrocarbon tail gas overhead torch combustion treatment
The low-pressure separation tank exhaust and the stripping tower top exhaust of the hydrogenation reactor enter a hydrogen-containing hydrocarbon exhaust buffer tank, the gas phase at the top of the hydrogen-containing hydrocarbon exhaust buffer tank enters a desulfurizing tank to remove H 2 S gas, then enter a liquid separation tank to separate liquid drops with the diameter of more than 300 mu m, and the hydrogen-containing hydrocarbon exhaust enters an overhead torch for burning after being sealed by a water seal tank;
(2) Incineration treatment of hydrocarbon tail gas containing oxygen
The hydrocarbon tail gas containing oxygen discharged from a vacuum system, a normal pressure storage tank and other equipment and facilities enters an oxygen-containing hydrocarbon tail gas buffer tank, the gas phase at the top of the oxygen-containing hydrocarbon tail gas buffer tank is boosted by a centrifugal fan and enters a heat accumulating type thermal incinerator for incineration, and the tail gas reaches the standard and is discharged;
(3) Compression condensation recovery treatment of hydrocarbon-containing tail gas without hydrogen and oxygen
The pressure of the hydrocarbon-containing tail gas which is discharged by the carbon five processing and utilizing device and does not contain hydrogen and oxygen is controlled to be 100-110kPa, one part of the hydrocarbon-containing tail gas is metered by a flowmeter I and then enters an oxygen-containing hydrocarbon tail gas buffer tank through a cut-off valve II and a regulating valve, the other part of the hydrocarbon-containing tail gas enters the hydrocarbon-containing tail gas buffer tank through the cut-off valve I, the top gas phase enters a compressor to be boosted to be more than 2000kPa under the control of the flowmeter II and then enters a water cooler, the temperature is controlled to be 20-50 ℃ and then enters a drying tower to be dehydrated, a 3A molecular sieve is filled in the drying tower, the tower top dehydrated tail gas is cooled to be less than 80 ℃ through a first heat exchanger and then enters a low-temperature separation tank, mixed light hydrocarbon at the bottom of the low-temperature separation tank and nitrogen at the top of the low-temperature separation tank after being decompressed to be less than 400kPa through a turbine expander are respectively subjected to heat exchange and temperature rise, the mixed light hydrocarbon is fed into a raw material tank to be recovered after being heated to be subjected to heat exchange through a second heat exchanger to be 20-40 ℃ and then enters a deoxidization reactor to be deoxidized, and then enters a whole factory nitrogen pipe network, and the deoxidization catalyst is filled in the reactor to be charged with brand-2000 UT.
2. The process for treating and recovering tail gas emitted from a carbon-five process industrial chain of claim 1, wherein: in the step (1), the desulfurizing tank is filled with a zinc oxide desulfurizing agent with high sulfur capacity, the sulfur capacity is more than 30%, and the operating temperature of the desulfurizing tank is 20-60 ℃.
3. The apparatus for use in a process for treating and recovering tail gas from a carbon five process industrial chain of claim 1, wherein: comprises a hydrogen-containing hydrocarbon tail gas treatment device, a hydrogen-free and oxygen-free hydrocarbon tail gas treatment device and an oxygen-containing hydrocarbon tail gas treatment device;
the hydrogen-containing hydrocarbon tail gas treatment device comprises a hydrogen-containing hydrocarbon tail gas buffer tank, a desulfurizing tank, a liquid separating tank, a water sealing tank and an overhead torch which are sequentially communicated;
the oxygen-containing hydrocarbon tail gas treatment device comprises an oxygen-containing hydrocarbon tail gas buffer tank, a centrifugal fan and a heat accumulating type thermal incinerator which are sequentially communicated;
The hydrocarbon-containing tail gas treatment device without hydrogen and oxygen comprises a hydrocarbon-containing tail gas buffer tank, a compressor, a water cooler and a drying tower which are sequentially communicated, wherein an outlet of the drying tower is communicated with a gas inlet in the middle of a first heat exchanger, a gas outlet in the middle of the first heat exchanger is communicated with a low-temperature liquid separating tank, a gas outlet in the top of the low-temperature liquid separating tank is communicated with a turboexpander, an outlet of the turboexpander is communicated with a gas inlet in the top of the first heat exchanger, a gas outlet in the top of the first heat exchanger is communicated with a second heat exchanger, the second heat exchanger is communicated with an oxygen removal reactor, a liquid outlet in the bottom of the low-temperature liquid separating tank is communicated with a liquid inlet in the bottom of the first heat exchanger, and a liquid outlet in the bottom of the first heat exchanger is communicated with a mixed light hydrocarbon collecting device;
a pipeline for allowing hydrocarbon-containing tail gas without hydrogen and oxygen to enter the hydrocarbon-containing tail gas buffer tank is provided with a first flowmeter and a first cut-off valve, and a second flowmeter is arranged between the hydrocarbon-containing tail gas buffer tank and the compressor;
Two branch lines are arranged between the first flowmeter and the first pipeline of the shut-off valve, one branch line is communicated with the inlet of the liquid separating tank, and the third shut-off valve is arranged on the branch line; the other branch line is communicated with the inlet of the oxygen-containing hydrocarbon tail gas buffer tank, and a second cut-off valve and a regulating valve are arranged on the branch line.
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