CN212284057U - Online high-temperature lean gas circulation activation system for fixed bed catalyst - Google Patents
Online high-temperature lean gas circulation activation system for fixed bed catalyst Download PDFInfo
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Abstract
The utility model relates to an on-line high-temperature lean gas circulation activation system for fixed bed catalysts, wherein top inlets of a first reactor and a second reactor are connected with an in-use process feed valve and a circulating gas feed valve in parallel, bottom outlets of the first reactor and the second reactor are connected with an in-use process discharge valve and a circulating gas discharge valve in parallel, inlets of the two in-use process feed valves are connected with an in-use process feed pipe, and outlets of the two in-use process discharge valves are connected with an in-use process discharge pipe; the inlet of the two circulating gas feeding valves is connected with the circulating gas feeding pipe, the outlet of the two circulating gas discharging valves is connected with the circulating gas discharging pipe, the outlet of the circulating gas discharging pipe is connected with the inlet of the cyclone coalescer, the nitrogen supply pipe is connected with the inlet of the cyclone coalescer through the flow regulating valve, the outlet of the cyclone coalescer is connected with the inlet of the compressor, the outlet of the compressor is connected with the gas inlet of the heating furnace, and the gas outlet of the heating furnace is connected with the circulating gas feeding pipe. The system can realize the on-line high-temperature gel punching activation of the catalyst, and greatly prolongs the one-way operation period.
Description
Technical Field
The utility model relates to a poor gas activation system of oil refinery especially relates to an online high temperature poor gas circulation activation system of fixed bed catalyst, belongs to oil refining technical field.
Background
The dry gas of the oil refinery mainly comes from the secondary processing process of crude oil, such as heavy oil catalytic cracking, thermal cracking, delayed coking, etc., wherein the dry gas generated by catalytic cracking is large and generally accounts for 4% -5% of the processing amount of the crude oil, and the catalytic cracking dry gas mainly contains components such as hydrogen, ethylene, methane, ethane, etc. The ethylene recycling device utilizes a high-activity and high-stability catalyst and a fixed bed reactor to make ethylene in dry gas undergo the reactions of superposition, cyclization, dehydrogenation, hydrogen transfer, isomerization and the like to produce a gasoline blending component with a high octane value and liquefied gas with a low olefin content.
The catalyst is metal modified acidic molecular sieve catalyst, and the acidic active center and the metal active center have synergistic effect. In the reaction process, 16 alkene as a reaction intermediate product is further subjected to superposition and cyclization to form a polycyclic compound; as the reaction proceeds further, a portion of the polycyclic compounds undergo condensation reactions such as dehydrogenation and cracking to form coke. The polycyclic compound and coke are attached to the surface of the catalyst to cover the acidic active center and the metal active center of the catalyst, so that the reaction activity of the catalyst is reduced, and the yield and the selectivity of the product are correspondingly reduced. Only after the reactor is cut out from the system, the reactor is purged, and after the nitrogen is replaced to be qualified, the catalyst is discharged and sent out of the reactor for regeneration. The carbon deposit on the surface of the catalyst is mainly some highly dehydrogenated hydrocarbon, such as polycyclic aromatic hydrocarbon, graphite precursor, graphite and the like; the catalyst is regenerated, usually by a rotary kiln regenerator, to restore activity, with a regeneration period of typically 20 to 25 days. The system regeneration from the production of the reactor input system to the regeneration of the reactor cut-out system becomes a one-way operation period, and the one-way operation period is generally 50 days to 70 days. Short one-way operation period, low fuel oil output of the production line, frequent catalyst regeneration and high regeneration cost.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to overcome the problem that exists among the prior art, provide an online high temperature lean gas circulation activation system of fixed bed catalyst, under the state of not stopping working, can realize the online high temperature towards the gluey activation of catalyst, resume catalyst activity, prolong one-way operating cycle greatly.
In order to solve the technical problem, the utility model discloses an online high temperature lean gas circulation activation system of fixed bed catalyst, including reactor one and reactor two that set up side by side, reactor one and reactor two's top entry parallel connection have in-use process feed valve and circulation gas feed valve, reactor one and reactor two's bottom export parallel connection have in-use process bleeder valve and circulation gas bleeder valve, the entry of dual-use process feed valve links to each other with in-use process inlet pipe, the export of dual-use process bleeder valve links to each other with in-use process discharging pipe; the inlet of two circulation gas feed valves links to each other with the circulation gas inlet pipe, and the export of two circulation gas bleeder valves links to each other with the circulation gas discharging pipe, and the export of circulation gas discharging pipe links to each other with the entry of cyclone coalescer, and the nitrogen gas supply pipe also links to each other with the entry of cyclone coalescer through flow control valve one, and the export of cyclone coalescer links to each other with the entry of compressor, and the export of compressor passes through the compressor outlet pipe and links to each other with the air inlet of heating furnace, the gas vent of heating furnace with the circulation gas inlet pipe links to each other.
Compared with the prior art, the utility model discloses following beneficial effect has been obtained: for example, when the first reactor works and the second reactor works, if the ethylene conversion rate of the first reactor is lower than 70 percent and the device cannot run economically, the second reactor is put into operation by opening the second feeding valve of the current process and the second discharging valve of the current process, then closing the second feeding valve of the circulating gas and the second discharging valve of the circulating gas; and then closing the first in-use process feeding valve and the first in-use process discharging valve, and opening the first circulating gas feeding valve and the first circulating gas discharging valve to cut the first reactor into the process. Aiming at the characteristic that polycyclic compounds can be removed in a reactor under the conditions of high temperature and high linear velocity, in a single-pass period, the reacted lean gas is used as a circulating carrier, colloid, coke and condensate in the lean gas are firstly separated in a cyclone coalescer, a nitrogen supply pipe introduces fresh nitrogen into an air inlet line of the cyclone coalescer through a flow regulating valve I, the pressure in the process is increased to 0.3MPa, a compressor provides circulating power, namely high linear velocity airflow of about 5500kg/h, the high linear velocity airflow is heated to 350-. The activation process is in a nitrogen atmosphere, so that the safety of the activation process is ensured; meanwhile, clean nitrogen is used as circulating gas, so that the activation effect can be improved. The catalyst is activated by punching glue at high temperature on line so as to recover the activity of the catalyst, and the two reactors are switched for use and activated alternately. The ethylene conversion rate after the catalyst is put into use is improved, the daily average yield of the product fuel oil is improved from 4t/d to about 4.5t/d, and the one-way operation period of the catalyst can be prolonged from 70 days to 200 days; the regeneration frequency outside the catalyst device is reduced, the regeneration time outside the catalyst device can be reduced to 1-2 times from 5-6 times per year, the regeneration cost outside the catalyst device is saved by 28 ten thousand yuan per year, the service life of the catalyst is prolonged to about 5 years from 3 years, and the catalyst loss caused by the regeneration outside the catalyst device can be reduced.
As an improvement of the utility model, the outlet of the circulating gas discharging pipe is connected with the hot side inlet of the first heat exchanger, the hot side outlet of the first heat exchanger is connected with the first effective nitrogen pipe, and the outlet of the first effective nitrogen pipe is connected with the inlet of the cyclone coalescer; and an outlet pipe of the compressor is connected with a cold side inlet of the first heat exchanger, and a cold side outlet of the first heat exchanger is connected with an air inlet of the heating furnace. The temperature of the activated gas flowing out of the circulating gas discharge pipe can reach about 400 ℃, the activated gas firstly enters the heat exchanger to preheat the exhaust gas of the compressor, and the lean gas preheated to the temperature of 220-240 ℃ enters the heating furnace to be heated, so that the heat in the lean gas is recovered, the load of the heating furnace is reduced, the gas temperature at the inlet of the compressor is reduced, the load of the compressor is reduced, and the mass flow at the outlet of the compressor is increased.
As a further improvement of the utility model, the outlet of the first-effect nitrogen pipe is connected with the inlet of the hot side of the second heat exchanger, the outlet of the hot side of the second heat exchanger is connected with the second-effect nitrogen pipe, and the outlet of the second-effect nitrogen pipe is connected with the inlet of the cyclone coalescer; and an outlet pipe of the heating furnace blower is connected with a cold side inlet of the second heat exchanger, a cold side outlet of the second heat exchanger is connected with a hot air pipe, and an outlet of the hot air pipe is connected with an air inlet of the heating furnace. The activation air temperature of the first-effect nitrogen pipe can reach about 200 ℃, the activation air continuously enters the second heat exchanger, the air at the outlet pipe of the blower of the heating furnace enters the heating furnace to be heated, the hot air enters the heating furnace to be combusted in cooperation with the fuel gas, the fuel gas is supplied by the fuel gas pipe, and the flow rate of the fuel gas is adjusted by the fuel gas adjusting valve. The air is heated by the waste heat of the lean air, so that the energy efficiency is further improved.
As a further improvement of the utility model, the outlet of the secondary-effect nitrogen pipe is connected with the inlet of the hot side of the third heat exchanger, the outlet of the hot side of the third heat exchanger is connected with the tertiary-effect nitrogen pipe, and the outlet of the tertiary-effect nitrogen pipe is connected with the inlet of the cyclone coalescer; the softened water inlet pipe is connected with a cold side inlet of the heat exchanger III, and a cold side outlet of the heat exchanger III is connected with a softened water outlet pipe. The activated temperature of the secondary nitrogen pipe can reach about 150 ℃, the secondary nitrogen pipe continuously enters the third heat exchanger to heat softened water, the softened water can be heated to 80 ℃, and the softened water is sent to a sulfur recovery device nearby and serves as a preheating source of sulfur recovery feeding gas. After the activated gas is used for three times, the temperature is reduced to 40-60 ℃, and the activated gas enters a cyclone coalescer for three-phase separation.
As a further improvement of the present invention, a flow meter is installed at the outlet of the cyclone coalescer, and is connected to the compressor outlet pipe through a bypass valve. The outlet flow of the cyclone coalescer can be accurately monitored by a flow meter, and under certain conditions, the bypass valve can be slightly opened to adjust the load of the compressor.
As a further improvement of the utility model, the middle upper parts of the side walls of the first reactor and the second reactor are respectively provided with a second reactor section feed inlet, and the second reactor section feed inlets are respectively provided with a second flow regulating valve; and the outlet pipe of the compressor is connected with a two-section side line feeding pipe, and the outlet of the two-section side line feeding pipe is respectively connected with the inlet of the flow regulating valve II. Considering the influence of resistance of the heating furnace, part of the gas flow after heat exchange of the compressor is, for example, 500-1000kg/h, and is introduced into a second-section feed inlet of the reactor, the flow is adjusted by the flow adjusting valve II to be used as a span line of the heating furnace, so that the gas flow linear speed of the second section of the reactor can be increased, and the high linear speed condition of the on-line activation of the catalyst is met.
As a further improvement of the utility model, the middle parts of the side walls of the first reactor and the second reactor are respectively provided with a three-section feed inlet of the reactor, and the three-section feed inlet of the reactor is respectively provided with a third flow regulating valve; and the outlet of the cold side of the first heat exchanger is connected with three sections of lateral line feeding pipes, and the outlets of the three sections of lateral line feeding pipes are respectively connected with the inlet of the flow regulating valve III. Part of the gas flow at the outlet of the first cold side of the heat exchanger is, for example, 500kg/h, and is introduced into a feed inlet of a third section of the reactor, the flow is adjusted by the flow adjusting valve II, and the gas flow is also used as the overline of the heating furnace, so that the gas flow linear speed of the lower section of the reactor can be increased, and the high linear speed condition of the on-line activation of the catalyst is further met.
Drawings
FIG. 1 is a flow chart of a first embodiment of the on-line high-temperature lean gas circulation activation system for fixed bed catalysts of the present invention.
FIG. 2 is a flow chart of the second embodiment of the on-line high-temperature lean gas circulation activation system for fixed bed catalyst of the present invention.
FIG. 3 is a flow chart of the third embodiment of the on-line high-temperature lean gas circulation activation system for fixed bed catalyst of the present invention.
FIG. 4 is a flow chart of the fourth embodiment of the on-line high-temperature lean gas circulation activation system for fixed bed catalyst of the present invention.
In the figure: l1. a cyclone coalescer; C1. a compressor; F1. heating furnace; r1, a first reactor; r2, a second reactor; E1. a first heat exchanger; E2. a second heat exchanger; E3. a third heat exchanger; FC1, a first flow regulating valve; FC2, a flow regulating valve II; FC3, flow control valve III; v1a. in-use flow feed valve one; v1b, an in-use flow inlet valve II; v2a, a first discharge valve of the in-use process; v2b, discharging a valve II in the using process; v3a, a first circulating gas feeding valve; v3b, a circulating gas feeding valve II; v4a, a first circulating gas discharge valve; v4b, a second circulating gas discharge valve; v5. a bypass valve; v6. fuel gas regulating valve; G1. feeding a material pipe in the using process; G2. discharging a pipe in the using process; G3. a nitrogen gas supply pipe; G4. a compressor outlet pipe; G5. a recycle gas feed pipe; G6. a circulating gas discharge pipe; G7. a nitrogen gas pipe; G8. a secondary nitrogen pipe; G9. a triple-effect nitrogen pipe; G10. a two-section side line feeding pipe; G11. three sections of side line feeding pipes; G12. an outlet pipe of a blower of the heating furnace; G13. a hot air pipe; G14. a fuel gas pipe; G15. a softened water inlet pipe; G16. a softened water outlet pipe; q1. flow meter.
Detailed Description
As shown in FIG. 1, the utility model discloses an online high temperature lean gas circulation activation system of fixed bed catalyst, including reactor one R1 and reactor two R2 that set up side by side, the top entry parallel connection of reactor one R1 has with flow feed valve one V1a and circulation gas feed valve one V3a, the bottom export parallel connection of reactor one R1 has with flow bleeder valve one V2a and circulation gas bleeder valve one V4a. The top inlet of the second reactor R2 is connected in parallel with a second used process feed valve V1b and a second recycle gas feed valve V3b, and the bottom outlet of the second reactor R2 is connected in parallel with a second used process discharge valve V2b and a second recycle gas discharge valve V4b. The inlets of the first in-use process feed valve V1a and the second in-use process feed valve V1b are connected with the in-use process feed pipe G1, and the outlet of the first in-use process discharge valve V2b is connected with the in-use process discharge pipe G2; the inlet of a first circulating gas feed valve V3a and a second circulating gas feed valve V3b is connected with a circulating gas feed pipe G5, the outlet of a first circulating gas discharge valve V4a and a second circulating gas discharge valve V4b is connected with a circulating gas discharge pipe G6, the outlet of a circulating gas discharge pipe G6 is connected with the inlet of a cyclone coalescer L1, a nitrogen supply pipe G3 is also connected with the inlet of the cyclone coalescer L1 through a flow regulating valve FC1, the outlet of the cyclone coalescer L1 is connected with the inlet of a compressor C1, the outlet of the compressor C1 is connected with the gas inlet of a heating furnace F1 through a compressor outlet pipe G4, and the gas outlet of the heating furnace F1 is connected with the circulating gas feed pipe G5.
For example, when the first reactor R1 works and the second reactor R2 works, if the ethylene conversion rate of the first reactor R1 is lower than 70 percent and the device can not run economically, the second reactor R2 is put into operation by opening the second feed valve V1b of the used process and the second discharge valve V2b of the used process, then closing the second feed valve V3b of the recycle gas and the second discharge valve V4b of the recycle gas; next, the in-process feed valve V1a and the in-process discharge valve V2a were closed, the recycle gas feed valve V3a and the recycle gas discharge valve V4a were opened, and the reactor one R1 was cut into the process. Aiming at the characteristic that polycyclic compounds can be removed in a reactor under the conditions of high temperature and high linear velocity, in a single-pass period, the reacted lean gas is used as a circulating carrier, colloid, coke and condensate in the lean gas are firstly separated in a cyclone coalescer L1, a nitrogen supply pipe G3 introduces fresh nitrogen into an air inlet line of the cyclone coalescer L1 through a flow regulating valve FC1, the pressure in the process is increased to 0.3MPa, a compressor C1 provides circulating power, namely high linear velocity gas flow of about 5500kg/h is provided, the high linear velocity gas flow is heated to 350-450 ℃ by a heating furnace F1 and then enters the reactor, and the attachments on the surface of the catalyst are removed layer by layer according to a temperature control gradient. The catalyst is activated by punching glue at high temperature on line so as to recover the activity of the catalyst, the ethylene conversion rate after the catalyst is put into use is improved, the product yield is increased, and the one-way operation period of the catalyst can be prolonged from 70 days to 200 days; the regeneration frequency outside the catalyst device is reduced, and the regeneration frequency outside the catalyst device can be reduced from 5-6 times to 1-2 times per year.
As shown in fig. 2, the outlet of the recycle gas outlet pipe G6 is connected with the hot side inlet of the first heat exchanger E1, the hot side outlet of the first heat exchanger E1 is connected with the single-effect nitrogen pipe G7, and the outlet of the single-effect nitrogen pipe G7 is connected with the inlet of the cyclone coalescer L1; the compressor outlet pipe G4 was connected to the cold side inlet of heat exchanger one E1 and the cold side outlet of heat exchanger one E1 was connected to the inlet of furnace F1. The temperature of the activated gas flowing out of the circulating gas discharge pipe G6 can reach about 400 ℃, the activated gas firstly enters a heat exchanger I E1 to preheat the exhaust gas of the compressor, and the lean gas preheated to 220-240 ℃ enters a heating furnace F1 to be heated, so that the heat in the lean gas is recovered, the load of the heating furnace F1 is reduced, the gas temperature at the inlet of the compressor is reduced, the load of the compressor C1 is reduced, and the mass flow at the outlet of the compressor is increased.
As shown in fig. 3, the outlet of the first-effect nitrogen pipe G7 is connected with the hot-side inlet of the second heat exchanger E2, the hot-side outlet of the second heat exchanger E2 is connected with the second-effect nitrogen pipe G8, and the outlet of the second-effect nitrogen pipe G8 is connected with the inlet of the cyclone coalescer L1; the outlet pipe of the heating furnace blower is connected with the cold side inlet of the second heat exchanger E2, the cold side outlet of the second heat exchanger E2 is connected with a hot air pipe G13, and the outlet of the hot air pipe G13 is connected with the air inlet of the heating furnace F1. The temperature of the activated air of the first effect nitrogen pipe G7 can reach about 200 ℃, the activated air continuously enters the second heat exchanger E2, the air of the outlet pipe G12 of the blower of the heating furnace enters and is heated, the hot air enters the heating furnace F1 and is combusted in cooperation with fuel gas, the fuel gas is supplied by a fuel gas pipe G14, and the flow is regulated by a fuel gas regulating valve V6. The air is heated by the waste heat of the lean air, so that the energy efficiency is further improved.
As shown in fig. 4, the outlet of the double-effect nitrogen pipe G8 is connected with the hot-side inlet of the heat exchanger three E3, the hot-side outlet of the heat exchanger three E3 is connected with the triple-effect nitrogen pipe G9, and the outlet of the triple-effect nitrogen pipe G9 is connected with the inlet of the cyclone coalescer L1; the softened water inlet pipe G15 is connected with the cold side inlet of the heat exchanger III E3, and the cold side outlet of the heat exchanger III E3 is connected with the softened water outlet pipe G16. The activation temperature of the second-effect nitrogen pipe G8 can reach about 150 ℃, the activation temperature continuously enters a heat exchanger III E3, softened water is heated, the temperature of the softened water can be raised to 80 ℃, and the softened water is sent to a sulfur recovery device nearby and is used as a preheating source of sulfur recovery feed gas. After the activated gas is subjected to three times of waste heat utilization, the temperature is reduced to 40-60 ℃, and the activated gas enters a cyclone coalescer L1 for three-phase separation.
The outlet of cyclone coalescer L1 was fitted with flow meter Q1 and connected to compressor outlet pipe G4 by bypass valve V5. The outlet flow of cyclone coalescer L1 can be accurately monitored by flow meter Q1 and under certain conditions, bypass valve V5 can be slightly opened to adjust the load on compressor C1.
The middle upper parts of the side walls of the first reactor R1 and the second reactor R2 are respectively provided with a second reactor section feed inlet, and the second reactor section feed inlet is respectively provided with a second flow control valve FC 2; the outlet pipe G4 of the compressor is connected with a two-stage side feed pipe G10, and the outlet of the two-stage side feed pipe G10 is respectively connected with the inlet of a flow regulating valve FC2. Considering the influence of resistance of the heating furnace F1, part of the gas flow after heat exchange of the compressor is, for example, 500-1000kg/h, and is introduced into a feed inlet of the second section of the reactor, and the flow is adjusted by the flow adjusting valve II FC2 to be used as the overline of the heating furnace F1, so that the gas flow linear speed of the second section of the reactor can be increased, and the high linear speed condition of the on-line activation of the catalyst is met.
The middle parts of the side walls of the first reactor R1 and the second reactor R2 are respectively provided with a reactor three-section feed inlet, and the reactor three-section feed inlet is respectively provided with a flow control valve three FC 3; the outlet of the cold side of the first heat exchanger E1 is connected with a three-stage side feed pipe G11, and the outlets of the three-stage side feed pipe G11 are respectively connected with the inlet of a flow regulating valve tri FC3. Part of the gas flow at the cold side outlet of the first heat exchanger E1 is introduced into a three-section feed inlet of the reactor at 500kg/h, the flow is regulated by a flow regulating valve second FC2, and the gas flow is also used as the overline of the heating furnace F1, so that the gas flow linear speed at the lower section of the reactor can be increased, and the high linear speed condition of the online activation of the catalyst is further met.
The above description is only a preferred embodiment of the present invention, and not intended to limit the scope of the present invention. In addition to the above embodiments, the present invention may have other embodiments. All the technical solutions formed by adopting equivalent substitutions or equivalent transformations fall within the protection scope claimed by the present invention. The undescribed technical features of the present invention can be realized by or using the prior art, and are not described herein again.
Claims (7)
1. The utility model provides an online high temperature lean gas circulation activation system of fixed bed catalyst, includes reactor one and reactor two that parallel arrangement, its characterized in that: the top inlets of the first reactor and the second reactor are connected with an in-use process feed valve and a recycle gas feed valve in parallel, the bottom outlets of the first reactor and the second reactor are connected with an in-use process discharge valve and a recycle gas discharge valve in parallel, the inlets of the two in-use process feed valves are connected with an in-use process feed pipe, and the outlets of the two in-use process discharge valves are connected with an in-use process discharge pipe; the inlet of two circulation gas feed valves links to each other with the circulation gas inlet pipe, and the export of two circulation gas bleeder valves links to each other with the circulation gas discharging pipe, and the export of circulation gas discharging pipe links to each other with the entry of cyclone coalescer, and the nitrogen gas supply pipe also links to each other with the entry of cyclone coalescer through flow control valve one, and the export of cyclone coalescer links to each other with the entry of compressor, and the export of compressor passes through the compressor outlet pipe and links to each other with the air inlet of heating furnace, the gas vent of heating furnace with the circulation gas inlet pipe links to each other.
2. The fixed bed catalyst on-line high temperature lean gas recycle activation system of claim 1, wherein: an outlet of the circulating gas discharging pipe is connected with a hot side inlet of the first heat exchanger, a hot side outlet of the first heat exchanger is connected with a first-effect nitrogen pipe, and an outlet of the first-effect nitrogen pipe is connected with an inlet of the cyclone coalescer; and an outlet pipe of the compressor is connected with a cold side inlet of the first heat exchanger, and a cold side outlet of the first heat exchanger is connected with an air inlet of the heating furnace.
3. The fixed bed catalyst on-line high temperature lean gas recycle activation system of claim 2, wherein: an outlet of the first-effect nitrogen pipe is connected with a hot-side inlet of the second heat exchanger, a hot-side outlet of the second heat exchanger is connected with a second-effect nitrogen pipe, and an outlet of the second-effect nitrogen pipe is connected with an inlet of the cyclone coalescer; and an outlet pipe of the heating furnace blower is connected with a cold side inlet of the second heat exchanger, a cold side outlet of the second heat exchanger is connected with a hot air pipe, and an outlet of the hot air pipe is connected with an air inlet of the heating furnace.
4. The fixed bed catalyst on-line high temperature lean gas recycle activation system of claim 3, wherein: an outlet of the second-effect nitrogen pipe is connected with a hot-side inlet of the third heat exchanger, a hot-side outlet of the third heat exchanger is connected with a third-effect nitrogen pipe, and an outlet of the third-effect nitrogen pipe is connected with an inlet of the cyclone coalescer; the softened water inlet pipe is connected with a cold side inlet of the heat exchanger III, and a cold side outlet of the heat exchanger III is connected with a softened water outlet pipe.
5. The fixed bed catalyst on-line high temperature lean gas recycle activation system of claim 1, wherein: and the outlet of the cyclone coalescer is provided with a flow meter and is connected with the outlet pipe of the compressor through a bypass valve.
6. The fixed bed catalyst on-line high temperature lean gas recycle activation system according to any one of claims 2 to 5, characterized in that: the middle upper parts of the side walls of the first reactor and the second reactor are respectively provided with a second reactor section feeding hole, and the second reactor section feeding holes are respectively provided with a second flow regulating valve; and the outlet pipe of the compressor is connected with a two-section side line feeding pipe, and the outlet of the two-section side line feeding pipe is respectively connected with the inlet of the flow regulating valve II.
7. The fixed bed catalyst on-line high temperature lean gas recycle activation system according to any one of claims 2 to 4, characterized in that: the middle parts of the side walls of the first reactor and the second reactor are respectively provided with a third reactor section feed inlet, and a third flow regulating valve is respectively arranged at the third reactor section feed inlet; and the outlet of the cold side of the first heat exchanger is connected with three sections of lateral line feeding pipes, and the outlets of the three sections of lateral line feeding pipes are respectively connected with the inlet of the flow regulating valve III.
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