Energy-saving and water-saving type propane dehydrogenation catalyst regeneration system and method

Abstract

The present application relates to a kind of energy-saving water-saving type propane dehydrogenation catalyst regeneration system and method, the present application is directly heat exchanged with fresh air and reaction vacuum outlet high-temperature material, the temperature of high-temperature gas is reduced below dew point, and condensate is precipitated;Fresh air is pressurized and initially preheated by air compressor, and then is divided into two ways, one way is heat exchanged with the high-temperature material of reactor vacuum ejector outlet, to recover the waste heat and condensate in vacuum pump outlet material, and heat regeneration air, condensate is recycled by separation tank and condensate pump;The other way is heat exchanged with regeneration flue gas, and waste heat is recovered, finally realizes the efficient recovery of high-temperature material in reactor regeneration system and regeneration flue gas waste heat of vacuum pump outlet, simultaneously realizes the recycling of a large amount of condensate, to reach the purpose of high energy utilization efficiency, low energy consumption of device, little water consumption.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of chemical production, in particular to the technical field of propane dehydrogenation, and specifically to a propane dehydrogenation catalyst regeneration system and method. BACKGROUND

[0002] Propylene is an important organic chemical raw material, which has the characteristics of wide application and large market demand. In recent years, with the rapid development of chemical industry, manufacturing industry and other industries, the demand for propylene continues to rise. In recent years, with the development of propylene production technology and the commissioning of production devices, the production capacity of propylene has increased rapidly. Compared with the traditional petroleum chemical industry and coal chemical industry, the propane dehydrogenation process has the advantages of less project investment, high product yield, low production cost, wide raw material sources, and environmental friendliness, and has become a popular propylene synthesis process.

[0003] In a certain propane dehydrogenation process device with high market share, during the reactor heating and regeneration process, the fresh air is pressurized and preheated and then enters the heating furnace. The high-temperature gas after heating is mixed with the device injection gas and then goes to the reactor heating and regeneration process. The regeneration flue gas is then passed through the waste heat boiler system to produce superheated and saturated high-pressure steam. The allowable flue gas is directly discharged to the waste gas discharge system. The high-temperature gas at the outlet of the reaction vacuum pump is directly discharged into the waste heat boiler or the chimney.

[0004] In the existing propane dehydrogenation process device, the high-temperature gas at the outlet of the reaction vacuum pump is discharged into the waste heat boiler to recover heat or directly discharged into the chimney. A large amount of steam carried by the high-temperature gas is also discharged into the atmosphere with the flue gas. The sensible heat, latent heat and water of the large amount of steam are not recovered and utilized, resulting in increased energy consumption and water consumption of the device. SUMMARY

[0005] The first technical problem to be solved by the present application is to provide a propane dehydrogenation catalyst regeneration system with high energy utilization efficiency, low device energy consumption and low water consumption in view of the status of the prior art.

[0006] The second technical problem to be solved by the present application is to provide a propane dehydrogenation catalyst regeneration method in view of the status of the prior art.

[0007] The technical scheme adopted by the present application to solve at least one of the above technical problems is as follows:

[0008] An energy-saving and water-saving propane dehydrogenation catalyst regeneration system comprises:

[0009] A waste heat boiler E-101 is used for waste heat recovery of high-temperature regenerated flue gas, which comprises flue gas filtering section, heat exchange section 1, heat exchange section 2, heat exchange section 3, heat exchange section 4, heat exchange section 5 and heat exchange section 6 connected in series, and a non-methane hydrocarbon removal bed arranged upstream and a flue gas treatment bed arranged downstream between the heat exchange sections;

[0010] A heat exchanger E-102 is provided with an air inlet for fresh air input and an air outlet for heat-exchanged fresh air output, and the air outlet is connected with a first pipeline capable of carrying air through the heat exchange section M of the waste heat boiler E-101, M is an integer greater than or equal to five, and the first pipeline part of the heat exchange section M of the waste heat boiler E-101 is arranged through the heat exchange section N of the waste heat boiler E-101, N is an integer less than or equal to four;

[0011] A heating furnace H-101 is used for heating the mixture material entering therein, which is provided with a fuel gas inlet at the lower side, a mixture material inlet at the bottom for input of the mixture material output after at least twice heat exchange of the waste heat boiler E-101, and a mixture material outlet at the top for output of the heated mixture material;

[0012] A reactor R-101 is used for heating regeneration of the mixture material, which is provided with an input port at the top in communication with the mixture material outlet of the heating furnace H-101, and an output port at the bottom for output of high-temperature regenerated flue gas, which is in communication with the flue gas filtering section inlet of the waste heat boiler E-101, and the flue gas filtering section, heat exchange section 1, non-methane hydrocarbon removal bed, heat exchange section 2, heat exchange section 3, heat exchange section 4, heat exchange section 5, flue gas treatment bed and heat exchange section 6 are connected in series to form a heat exchange channel for heat exchange of the high-temperature regenerated flue gas; the heat exchanger E-102 is provided with a heat exchange inlet at the first side in communication with the end heat exchange section of the reactor R-101, and a heat exchange output port at the second side for output of the heat-exchanged material;

[0013] A heat exchanger E-103 is arranged downstream of the heat exchanger E-102, which is provided with a medium-low temperature waste heat recovery inlet in communication with the heat exchange output port of the heat exchanger E-102, and a tail gas outlet for output of the heat-exchanged tail gas;

[0014] A heat exchanger E-104 is used for preheating part of fresh air with the high-temperature material from the reaction vacuum pump outlet as heat source, and the heat exchanger E-104 is connected with a second pipeline for output of the preheated fresh air, which is in communication with the first pipeline and connected between the heat exchange section M and the heat exchange section N and includes the inlet of the heat exchange section M;

[0015] A cooler E-105 is used for cooling the output material after heat exchange of the heat exchanger E-104, which is provided with a cooling inlet and a cooling outlet;

[0016] A liquid-vapor separation tank V-102 is arranged downstream of the aftercooler E-105, and is provided with a liquid-vapor separation inlet for input of material, a gas outlet at the top for output of separated gas phase, and a liquid outlet at the bottom for output of separated liquid phase. The gas outlet is connected to the tail gas pipeline downstream of the heat exchanger E-103, and the liquid outlet is connected to the condensate pump P-101.

[0017] Preferably, the air inlet of the heat exchanger E-102 is connected to a third pipeline for conveying fresh air, and an air blower / compressor C-101 is arranged at the inlet end of the third pipeline for pressurizing the fresh air. The third pipeline is divided into a first branch pipeline and a second branch pipeline downstream of the air blower / compressor C-101. The outlet of the first branch pipeline is connected to the air inlet of the heat exchanger E-102, and the outlet of the second branch pipeline is connected to the fresh air inlet of the heat exchanger E-104.

[0018] Preferably, the bottom of the heat exchanger E-104 is provided with a material outlet for output of the medium-high temperature vacuum pump outlet material after cooling of the high temperature vacuum pump outlet material, and the cooling inlet of the aftercooler E-105 is connected to the material outlet.

[0019] Preferably, the third pipeline is provided with a heat exchanger E-106 upstream of the first branch pipeline and the second branch pipeline. The bottom of the heat exchanger E-104 is provided with a material outlet for output of the medium-high temperature vacuum pump outlet material after cooling of the high temperature vacuum pump outlet material, and the material outlet is connected to the heat exchange inlet of the heat exchanger E-106. The bottom of the heat exchanger E-106 is further provided with a heat exchange outlet connected to the cooling inlet of the aftercooler E-105.

[0020] Preferably, the third pipeline is further provided with a bypass for directly conveying fresh air downstream without heat exchange in the heat exchanger E-106.

[0021] Preferably, the non-methane hydrocarbon removal bed is connected between the heat exchange second section and the heat exchange third section, the flue gas treatment bed is connected between the heat exchange fifth section and the heat exchange sixth section, the heat exchange M section is the heat exchange fifth section, and the heat exchange N section is the heat exchange third section.

[0022] The connection between the second pipeline and the first pipeline is located at the inlet of the heat exchange fifth section; or

[0023] The connection between the second pipeline and the first pipeline is located on the portion of the first pipeline that passes through the heat exchange fifth section without passing through the heat exchange third section.

[0024] Preferably, a steam tank V-101 is further included, and the heat exchange sixth section is connected with a first pipeline for input of boiler water and a second pipeline for output of boiler water, and the outlet of the second pipeline is connected with the inlet of the steam tank V-101;

[0025] The bottom of the steam tank V-101 is provided with a third pipeline for conveying heat exchange liquid to the heat exchange fourth section and a fourth pipeline for output of heat exchanged liquid;

[0026] The top of the steam tank V-101 is provided with a fifth pipeline for conveying heat exchange liquid to the heat exchange second section, and the fifth pipeline is provided with a saturated steam exchange port;

[0027] The top of the heat exchange second section is provided with a sixth pipeline for conveying heat exchange liquid to the heat exchange first section, and the top of the heat exchange first section is provided with a seventh pipeline for output of superheated steam.

[0028] Preferably, a heat exchange seventh section is further included and connected after the heat exchange sixth section, the non-methane hydrocarbon removal bed is connected between the heat exchange second section and the heat exchange third section, the flue gas treatment bed is connected between the heat exchange sixth section and the heat exchange seventh section, the heat exchange M section is the heat exchange sixth section, and the heat exchange N section is the heat exchange fourth section;

[0029] The connection between the second pipeline and the first pipeline is located on the part of the first pipeline which passes through the heat exchange fifth section and does not pass through the heat exchange third section;

[0030] The first pipeline passes through the heat exchange fourth section and then passes through the heat exchange first section.

[0031] An energy-saving and water-saving type propane dehydrogenation catalyst regeneration method, comprising the following steps:

[0032] Fresh air is pressurized by a blower / compressor C-101, preheated by a heat exchanger E-106, and then divided into two paths, the first path of fresh air is preheated by the heat exchanger E-104 using high-temperature material at the outlet of a reaction vacuum pump as a heat source, and the second path is preheated by the heat exchanger E-102 using regenerated flue gas, and the two preheated materials are mixed and then pass through the fifth section and the third section of a waste heat boiler E-101, and then enter a regeneration air heating furnace H-101, and the mixed gas heated by fuel gas is sent to the heating regeneration process of a reactor R-101;

[0033] The high-temperature regenerated flue gas at the outlet of the reactor passes through the flue gas filtering section, the heat exchange first section, the non-methane hydrocarbon removal bed, the heat exchange second section, the heat exchange third section, the heat exchange fourth section, the heat exchange fifth section, the flue gas treatment bed, and the heat exchange sixth section of the waste heat boiler E-101 in sequence, and then is subjected to medium and low-temperature waste heat recovery by the heat exchanger E-102 and the heat exchanger E-103;

[0034] The high-temperature material at the outlet of the reaction vacuum pump is cooled in the heat exchanger E-104, the heat exchanger E-106 and the aftercooler E-105 in sequence, the high-temperature material after cooling is separated in the liquid separation tank V-102, the condensate obtained is pressurized by a condensate pump and then returned to the device for recycling after treatment, and the tail gas at the top of the tank is mixed with the regenerated flue gas and then discharged to the exhaust system;

[0035] The operating temperature of the high-temperature material at the outlet of the vacuum pump in the aftercooler E-105 is reduced from 115-120℃ to 90-115℃, and the cooling medium is at least one of boiler water, warm water in a warm water system, organic medium in an organic Rankine cycle, ammonia in an ammonia refrigeration system and water in a lithium bromide heat generation system;

[0036] The operating conditions of the cold and hot sides of the material in the heat exchanger E-104 are that the operating temperature of the high-temperature material at the outlet of the vacuum pump is reduced from 320-450℃ to 120-150℃, and the fresh air is preheated from 100-120℃ to 150-430℃;

[0037] The operating conditions of the cold and hot sides of the material in the heat exchanger E-106 are that the operating temperature of the high-temperature material at the outlet of the vacuum pump is reduced from 120-150℃ to 115-120℃, and the fresh air is preheated from 80-100℃ to 100-120℃;

[0038] The ratio of the amount of fresh air preheated by the high-temperature material at the outlet of the reaction vacuum pump in the heat exchanger E-104 to the total amount of fresh air is 5%-95%;

[0039] The operating pressure of the material at the outlet of the reaction vacuum pump is 0.005MPag-0.1MPag.

[0040] An energy-saving and water-saving type propane dehydrogenation catalyst regeneration method, comprising the following steps:

[0041] The fresh air is pressurized by the air blower / compressor C-101, preheated in the heat exchanger E-106, and then divided into two paths, the first path of fresh air is preheated in the heat exchanger E-104 by using the high-temperature material at the outlet of the reaction vacuum pump as a heat source, and the second path is preheated in the heat exchanger E-102 and the waste heat boiler E-101 six stages in sequence, the two materials after preheating are mixed, and then pass through the waste heat boiler E-101 heat exchange four stages and heat exchange one stage to enter the regeneration air heating furnace H-101, and the mixed gas after heating by fuel gas is sent to the heating regeneration process of the reactor R-101;

[0042] The high-temperature regeneration flue gas at the reactor outlet is sequentially passed through a flue gas filtering section, a heat exchange section 1, a heat exchange section 2, a non-methane hydrocarbon removal bed, a heat exchange section 3, a heat exchange section 4, a heat exchange section 5, a heat exchange section 6, a flue gas treatment bed and a heat exchange section 7 in the waste heat boiler E-101, and then is subjected to medium and low-temperature waste heat recovery through the heat exchanger E-102 and the heat exchanger E-103.

[0043] The high-temperature material at the outlet of the reaction vacuum pump is sequentially cooled through the heat exchanger E-104, the heat exchanger E-106 and the aftercooler E-105, the condensed liquid obtained after separation of the high-temperature material cooled is pressurized by a condensed liquid pump and then is returned to the device for recycling after treatment, and the tail gas at the top of the tank is mixed with the regeneration flue gas tail gas and then is discharged to the exhaust system.

[0044] The operating temperature of the high-temperature material at the outlet of the aftercooler E-105 is reduced from 115-120℃ to 90-115℃, and the cooling medium is at least one of boiler water, warm water in a warm water system, organic medium in an organic Rankine cycle, ammonia in an ammonia refrigeration system and water in a lithium bromide heat generation system.

[0045] The operating conditions of the cold and hot sides of the heat exchanger E-104 are that the operating temperature of the high-temperature material at the outlet of the reaction vacuum pump is reduced from 320-450℃ to 120-150℃, and the fresh air is preheated from 100-120℃ to 150-430℃.

[0046] The operating conditions of the cold and hot sides of the heat exchanger E-106 are that the operating temperature of the high-temperature material at the outlet of the reaction vacuum pump is reduced from 120-150℃ to 115-120℃, and the fresh air is preheated from 80-100℃ to 100-120℃.

[0047] The ratio of the amount of fresh air preheated by the high-temperature material at the outlet of the reaction vacuum pump in the heat exchanger E-104 to the total amount of fresh air is 5%-95%.

[0048] The operating pressure of the material at the outlet of the reaction vacuum pump is 0.005-0.1 MPag.

[0049] An energy-saving and water-saving type regeneration method of a propane dehydrogenation catalyst, comprising the following steps:

[0050] The fresh air is pressurized by the air blower / compressor C-101 and is divided into two routes, the first route of fresh air is preheated by the high-temperature material at the outlet of the reaction vacuum pump in the heat exchanger E-104 as a heat source, and the second route is preheated by the regeneration flue gas in the heat exchanger E-102, the two preheated materials are mixed and then are sequentially passed through the fifth section and the third section of the waste heat boiler E-101 to enter the regeneration air heating furnace H-101, and the mixed gas heated by fuel gas is sent to the heating and regeneration process of the reactor R-101.

[0051] The high-temperature regeneration flue gas at the reactor outlet is sequentially passed through a flue gas filtering section, a heat exchange section 1, a non-methane hydrocarbon removal bed, a heat exchange section 2, a heat exchange section 3, a heat exchange section 4, a heat exchange section 5, a flue gas treatment bed and a heat exchange section 6 in the waste heat boiler E-101, and then is passed through the heat exchanger E-102 and the heat exchanger E-103 for medium and low-temperature waste heat recovery.

[0052] The high-temperature material at the outlet of the reaction vacuum pump is sequentially cooled by the heat exchanger E-104 and the aftercooler E-105, and the cooled high-temperature material is separated by a liquid separator, and the obtained condensate is pressurized by a condensate pump and then returned to the device for recycling, and the tail gas at the top of the tank is mixed with the regeneration flue gas tail gas and then discharged to the exhaust system.

[0053] In the present application, the heat exchanger E-103 is a low-temperature waste heat recovery heat exchanger for high-temperature regeneration flue gas, and the cooling medium includes but is not limited to boiler water, warm water in a warm water system, organic medium in an organic Rankine cycle, ammonia in an ammonia refrigeration system, water in a lithium bromide heating system, working medium in a series of low-temperature energy recovery systems, and circulating water. The heat exchanger can be a high-efficiency heat exchanger, and the heat exchanger types include but are not limited to a spiral pipe heat exchanger, a plate heat exchanger, a plate and shell heat exchanger, a high-flux tube heat exchanger, etc.

[0054] The high-temperature outlet material of the propane dehydrogenation device reactor vacuum pump directly preheats fresh air, recovers heat and water, and simultaneously preheats fresh air.

[0055] The present application directly exchanges heat between fresh air and the high-temperature material at the outlet of the reaction vacuum pump, so that the temperature of the high-temperature gas is reduced below the dew point, and condensate is precipitated, thereby achieving the purpose of recovering the waste heat of the material at the outlet of the vacuum pump and the condensate and the waste heat of the regeneration flue gas. Compared with the existing propane dehydrogenation device reactor regeneration system, the present application has the advantages of low energy consumption, low water consumption, etc., improves the process energy utilization efficiency, saves water resources, and improves the economic benefit of the device.

[0056] Compared with the prior art, the present application has the advantages that: the present application directly exchanges heat between fresh air and the high-temperature material at the outlet of the reaction vacuum pump, so that the temperature of the high-temperature gas is reduced below the dew point, and condensate is precipitated; the fresh air is pressurized and initially preheated by an air compressor and is then divided into two paths, one path exchanges heat with the high-temperature material at the outlet of the reactor vacuum ejector to recover the waste heat and condensate in the material at the outlet of the vacuum pump and to heat the regeneration air, and the condensate is recovered and utilized by a separation tank and a condensate pump; the other path exchanges heat with the regeneration flue gas to recover waste heat, thereby achieving efficient recovery of the waste heat of the high-temperature material at the outlet of the reactor vacuum pump and the regeneration flue gas in the reactor regeneration system and the recovery and utilization of a large amount of condensate, and achieving the purposes of high energy utilization efficiency, low device energy consumption and low water consumption. BRIEF DESCRIPTION OF DRAWINGS

[0057] Figure 1This is a process flow diagram of Embodiment 1 of the present invention;

[0058] Figure 2 This is a process flow diagram of Embodiment 2 of the present invention;

[0059] Figure 3 This is a process flow diagram of Embodiment 3 of the present invention;

[0060] Figure 4 This is a process flow diagram of Embodiment 4 of the present invention. Detailed Implementation

[0061] The present invention will be further described in detail below with reference to the accompanying drawings and embodiments.

[0062] Example 1:

[0063] like Figure 1 As shown, the propane dehydrogenation catalyst regeneration system of this embodiment includes:

[0064] Waste heat boiler E-101 is used to recover waste heat from high-temperature regenerated flue gas. It includes a flue gas filtration section, a heat exchange section 1, a heat exchange section 2, a heat exchange section 3, a heat exchange section 4, a heat exchange section 5 and a heat exchange section 6 connected in series. Each heat exchange section is spaced apart by an upstream non-methane removal bed and a downstream flue gas treatment bed.

[0065] The heat exchanger E-102 has an air inlet at the bottom for fresh air input and an air outlet for fresh air output after heat exchange. The air outlet is connected to a first pipe 01 that can carry air through the heat exchange section M of the waste heat boiler E-101, where M is an integer ≥ five. The pipe 01 passes through the first pipe of the heat exchange section M of the waste heat boiler E-101 and then through the heat exchange section N of the waste heat boiler E-101, where N is an integer ≤ four.

[0066] Heating furnace H-101 is used to heat the mixed material entering it. It has a fuel gas inlet on the lower side, a mixed material inlet at the bottom for the mixed material output after at least two heat exchanges by waste heat boiler E-101, and a mixed material outlet at the top for the heated mixed material to be output.

[0067] The reactor R-101 is used for heating and regenerating the mixture, and is provided with an input port at the top communicated with the mixture outlet of the heating furnace H-101, and an output port at the bottom communicated with the flue gas filtering section inlet of the waste heat boiler E-101, and the flue gas filtering section, the heat exchange section 1, the non-methane hydrocarbon removal bed, the heat exchange section 2, the heat exchange section 3, the heat exchange section 4, the heat exchange section 5, the flue gas treatment bed and the heat exchange section 6 are sequentially connected to form a heat exchange channel for heat exchange of the high-temperature regenerated flue gas.

[0068] The heat exchanger E-103 is arranged downstream of the heat exchanger E-102, and is provided with a medium-low temperature waste heat recovery inlet communicated with the heat exchange output port of the heat exchanger E-102, and a tail gas outlet for output of the heat-exchanged tail gas.

[0069] The heat exchanger E-104 is used for preheating part of the fresh air by taking the high-temperature material from the reaction vacuum pump outlet as a heat source, and is connected with a second pipeline 02 for output of the preheated fresh air, and the second pipeline 02 is communicated with the first pipeline 01 and is connected at a position between the heat exchange section M and the heat exchange section N and including the inlet of the heat exchange section M.

[0070] The aftercooler E-105 is used for cooling the output material after heat exchange of the heat exchanger E-104, and is provided with a cooling inlet and a cooling outlet.

[0071] The liquid-vapor separation tank V-102 is arranged downstream of the aftercooler E-105, and is used for gas-liquid separation of the input material, and is provided with a liquid-vapor separation inlet at the side for input of the material, a gas phase outlet at the top for output of the separated gas phase, and a liquid phase outlet at the bottom for output of the separated liquid phase, and the gas phase outlet is communicated with the tail gas pipeline downstream of the heat exchanger E-103, and the liquid phase outlet is connected with a condensate pump P-101.

[0072] The air inlet of the heat exchanger E-102 is connected with a third pipeline 03 for conveying fresh air, and the inlet end of the third pipeline 03 is provided with a blower / compressor C-101 for pressurizing the fresh air, and the third pipeline 03 is divided into a first branch pipeline 031 and a second branch pipeline 032 downstream, and the outlet of the first branch pipeline 031 is communicated with the air inlet of the heat exchanger E-102, and the outlet of the second branch pipeline 032 is communicated with the fresh air inlet of the heat exchanger E-104.

[0073] The bottom of the heat exchanger E-104 is provided with a material output port for outputting the medium-high temperature vacuum pump outlet material obtained after the high temperature material outlet by the reaction vacuum pump is cooled, and the cooling inlet of the aftercooler E-105 is connected to the material output port.

[0074] The third pipeline 03 is provided with a heat exchanger E-106 upstream of the first branch pipeline 031 and the second branch pipeline 032, the bottom of the heat exchanger E-104 is provided with a material output port for outputting the medium-high temperature vacuum pump outlet material obtained after the high temperature material outlet by the reaction vacuum pump is cooled, and the heat exchange inlet of the heat exchanger E-106 is connected to the material output port, and the bottom of the heat exchanger E-106 is also provided with a heat exchange outlet connected to the cooling inlet of the aftercooler E-105.

[0075] The third pipeline 03 is also provided with a bypass 033 for directly conveying fresh air downstream without heat exchange by the heat exchanger E-106.

[0076] The non-methane hydrocarbon removal bed is connected between the heat exchange second section and the heat exchange third section, the flue gas treatment bed is connected between the heat exchange fifth section and the heat exchange sixth section, the heat exchange M section is the heat exchange fifth section, and the heat exchange N section is the heat exchange third section.

[0077] The connection between the second pipeline 02 and the first pipeline 01 is located on the part of the first pipeline 01 that passes through the heat exchange fifth section but does not pass through the heat exchange third section.

[0078] The embodiment also includes a steam tank V-101, the heat exchange sixth section is connected with a first pipeline for inputting boiler water and a second pipeline for outputting boiler water, the outlet of the second pipeline is connected to the inlet of the steam tank V-101; the bottom of the steam tank V-101 is provided with a third pipeline for conveying heat exchange liquid to the heat exchange fourth section and a fourth pipeline for outputting the heat exchanged liquid; the top of the steam tank V-101 is provided with a fifth pipeline for conveying heat exchange liquid to the heat exchange second section, and the fifth pipeline is provided with a saturated steam exchange port; the top of the heat exchange second section is provided with a sixth pipeline for conveying heat exchange liquid to the heat exchange first section, and the top of the heat exchange first section is provided with a seventh pipeline for outputting superheated steam.

[0079] The propane dehydrogenation catalyst regeneration method of the embodiment includes the following steps:

[0080] Fresh air is preheated by heat exchanger E-106, then divided into two streams. The first stream of fresh air is preheated by the high-temperature material from the outlet of the reaction vacuum pump in heat exchanger E-104, and the second stream is preheated by the regenerated flue gas in heat exchanger E-102. The two streams of preheated material are mixed and then passed through five stages of waste heat boiler E-101 and three stages of heat exchanger E-101, and then into the heating regeneration process of reactor R-101. The mixed gas heated by fuel gas is sent to the heating regeneration process of reactor R-101.

[0081] The high-temperature regenerated flue gas from the outlet of the reactor is passed through the flue gas filtration stage, heat exchange stage one, non-methane hydrocarbon removal bed, heat exchange stage two, heat exchange stage three, heat exchange stage four, heat exchange stage five, flue gas treatment bed, and heat exchange stage six in waste heat boiler E-101, and then through heat exchanger E-102 and heat exchanger E-103 for medium and low-temperature waste heat recovery.

[0082] The high-temperature material from the outlet of the reaction vacuum pump is cooled by heat exchanger E-104, heat exchanger E-106, and aftercooler E-105. The cooled high-temperature material is separated by liquid separation tank V-102, and the condensate obtained is pressurized by a condensate pump and returned to the device for recycling. The tail gas from the top of the tank is mixed with the regenerated flue gas tail gas and sent to the exhaust system.

[0083] The operating temperature of the high-temperature vacuum pump outlet material in aftercooler E-105 is reduced from 115-120°C to 90-115°C. The cooling medium is at least one of boiler water, warm water in the warm water system, organic medium in the organic Rankine cycle, ammonia in the ammonia refrigeration system, and water in the lithium bromide heating system.

[0084] The operating conditions of the cold and hot side materials in heat exchanger E-104 are that the operating temperature of the high-temperature vacuum pump outlet material is reduced from 320-450°C to 120-150°C, and the fresh air is preheated from 100-120°C to 150-430°C.

[0085] The operating conditions of the cold and hot side materials in heat exchanger E-106 are that the operating temperature of the high-temperature vacuum pump outlet material is reduced from 120-150°C to 115-120°C, and the fresh air is preheated from 80-100°C to 100-120°C.

[0086] The ratio of the amount of fresh air preheated by the high-temperature material from the outlet of the reaction vacuum pump in heat exchanger E-104 to the total amount of fresh air is 5%-95%.

[0087] The operating pressure of the material from the outlet of the reaction vacuum pump is 0.005 MPag-0.1 MPag.

[0088] Taking a 600,000-ton / year propane dehydrogenation unit as an example, considering the total flow rate of high-temperature material at the outlet of the reaction vacuum pump is 29-35 t / h, the material temperature is 425-440℃, and the total flow rate of fresh air required for regeneration is 800-1000 t / h, after adopting the energy-saving and water-saving propane dehydrogenation catalyst regeneration system proposed in this embodiment, 18.23MW-22.29MW of waste heat can be recovered from the high-temperature material at the outlet of the reaction vacuum pump, and 26.82-32.78 t / h of condensate can be recovered, achieving a condensate recovery rate of over 95%. Simultaneously, by further increasing the preheating temperature of the regeneration air, natural gas consumption can be reduced by 2304-2816 tons / year. This technical solution can reduce the unit's operating costs by approximately 12 million RMB / year or more, effectively improving energy utilization efficiency. It has advantages such as low energy consumption and low water consumption, thus enhancing the unit's economic benefits.

[0089] The corresponding main logistics data is shown in the table below:

[0090]

[0091]

[0092] Note: Waste heat boilers have functions for removing non-methane hydrocarbons and NO. X Bed layer, non-methane and NO in the exhaust gas X All quantities meet emission requirements.

[0093] Example 2:

[0094] like Figure 2 As shown, the difference between this embodiment and embodiment 1 is that the connection between the second pipe 02 and the first pipe 01 is located at the inlet of the heat exchange section 5.

[0095] Example 3:

[0096] like Figure 3 As shown, the difference between this embodiment and embodiment 1 is that this embodiment does not include heat exchanger E-106.

[0097] The propane dehydrogenation catalyst regeneration method in this embodiment includes the following steps:

[0098] Fresh air is pressurized by blower / compressor C-101 and then divided into two streams. The first stream of fresh air goes to heat exchanger E-104 to preheat the high-temperature material at the outlet of the reaction vacuum pump as a heat source. The second stream goes to heat exchanger E-102 to preheat the material with regenerated flue gas. The two preheated streams are then mixed and passed through the fifth and third stages of waste heat boiler E-101 before entering regenerated air heater H-101. The mixed gas, after being heated by fuel gas, goes to reactor R-101 for heating and regeneration.

[0099] The high-temperature regenerated flue gas at the reactor outlet passes through the flue gas filtration section, heat exchange section 1, non-methane removal bed, heat exchange section 2, heat exchange section 3, heat exchange section 4, heat exchange section 5, flue gas treatment bed and heat exchange section 6 in the waste heat boiler E-101, and then passes through heat exchangers E-102 and E-103 for medium and low temperature waste heat recovery.

[0100] The high-temperature material at the outlet of the reaction vacuum pump is cooled by heat exchanger E-104 and aftercooler E-105. After cooling, the high-temperature material is separated by a separator. The resulting condensate is pressurized by a condensate pump and returned to the unit for processing and recycling. The exhaust gas from the top of the tank is mixed with the regenerated flue gas and then sent to the emission system.

[0101] Example 4:

[0102] like Figure 4 As shown, the difference between this embodiment and embodiment 1 is that this embodiment also includes a heat exchange section 7 connected after the heat exchange section 6, a non-methane removal bed connected between the heat exchange section 2 and the heat exchange section 3, a flue gas treatment bed connected between the heat exchange section 6 and the heat exchange section 7, heat exchange section M is the heat exchange section 6, and heat exchange section N is the heat exchange section 4.

[0103] The connection point between the second and first pipes is located on the portion of the first pipe that passes through the fifth heat exchange section but does not yet enter the third heat exchange section. The first pipe passes through the fourth heat exchange section and then through the first heat exchange section.

[0104] The propane dehydrogenation catalyst regeneration method in this embodiment includes the following steps:

[0105] Fresh air is pressurized by blower / compressor C-101 and preheated by heat exchanger E-106. Then it is divided into two streams. The first stream of fresh air goes to heat exchanger E-104 to preheat with the high-temperature material at the outlet of the reaction vacuum pump as a heat source. The second stream is preheated by heat exchanger E-102 and waste heat boiler E-101 in six stages. The two preheated streams are mixed and then pass through the waste heat boiler E-101 in four stages and one stage before entering the regenerated air heater H-101. The mixed gas, after being heated by fuel gas, goes to reactor R-101 for heating and regeneration.

[0106] The high-temperature regenerated flue gas at the reactor outlet passes through the flue gas filtration section, heat exchange section 1, heat exchange section 2, non-methane removal bed, heat exchange section 3, heat exchange section 4, heat exchange section 5, heat exchange section 6, flue gas treatment bed and heat exchange section 7 in the waste heat boiler E-101, and then passes through heat exchangers E-102 and E-103 for medium and low temperature waste heat recovery.

[0107] The high-temperature material at the outlet of the reaction vacuum pump is cooled in the heat exchanger E-104, the heat exchanger E-106 and the aftercooler E-105 in sequence, the high-temperature material after cooling is separated by a liquid separator, the condensate obtained is pressurized by a condensate pump and then returned to the device for recycling after treatment, and the tail gas at the top of the tank is mixed with the regenerated flue gas tail gas and then discharged to the exhaust system;

[0108] The operating temperature of the high-temperature material at the outlet of the vacuum pump in the aftercooler E-105 is reduced from 115-120℃ to 90-115℃, and the cooling medium is at least one of boiler water, warm water in a warm water system, organic medium in an organic Rankine cycle, ammonia in an ammonia refrigeration system and water in a lithium bromide heat generation system;

[0109] The operating conditions of the cold and hot sides of the material in the heat exchanger E-104 are that the operating temperature of the high-temperature material at the outlet of the vacuum pump is reduced from 320-450℃ to 120-150℃, and the fresh air is preheated from 100-120℃ to 150-430℃;

[0110] The operating conditions of the cold and hot sides of the material in the heat exchanger E-106 are that the operating temperature of the high-temperature material at the outlet of the vacuum pump is reduced from 120-150℃ to 115-120℃, and the fresh air is preheated from 80-100℃ to 100-120℃;

[0111] The ratio of the amount of fresh air preheated by the high-temperature material at the outlet of the reaction vacuum pump in the heat exchanger E-104 to the total amount of fresh air for the feed is 5%-95%;

[0112] The operating pressure of the material at the outlet of the reaction vacuum pump is 0.005-0.1 MPag.

Claims

1. A method for regenerating an energy-saving and water-saving propane dehydrogenation catalyst, characterized in that: Fresh air is pressurized by blower / compressor C-101 and preheated by heat exchanger E-106. Then it is divided into two streams. The first stream of fresh air goes to heat exchanger E-104 to preheat with the high-temperature material at the outlet of the reaction vacuum pump as a heat source. The second stream goes to heat exchanger E-102 to preheat with regenerated flue gas. The two preheated streams are then mixed and passed through the fifth and third stages of waste heat boiler E-101 before entering regenerated air heater H-101. The mixed gas, after being heated by fuel gas, goes to reactor R-101 for heating and regeneration. The high-temperature regenerated flue gas at the reactor outlet passes through the flue gas filtration section, heat exchange section 1, non-methane removal bed, heat exchange section 2, heat exchange section 3, heat exchange section 4, heat exchange section 5, flue gas treatment bed and heat exchange section 6 in the waste heat boiler E-101, and then passes through heat exchangers E-102 and E-103 for medium and low temperature waste heat recovery. The high-temperature material at the outlet of the reaction vacuum pump is cooled by heat exchangers E-104, E-106 and aftercooler E-105. After cooling, the high-temperature material is separated by the separator V-102. The resulting condensate is pressurized by the condensate pump and returned to the unit for processing and recycling. The exhaust gas from the top of the tank is mixed with the regenerated flue gas and then sent to the emission system. The operating temperature of the material at the outlet of the high-temperature vacuum pump in the E-105 aftercooler is reduced from 115~120℃ to 90~115℃. The cooling medium is at least one of the following: boiler water, warm water in a warm water system, organic medium in an organic Rankine cycle, ammonia in an ammonia water refrigeration system, and water in a lithium bromide heating system. The operating conditions for materials on the hot and cold sides of heat exchanger E-104 are as follows: the operating temperature of the material at the outlet of the high-temperature vacuum pump is reduced from 320~450℃ to 120~150℃, and the fresh air is preheated from 100~120℃ to 150-430℃. The operating conditions for materials on the hot and cold sides of heat exchanger E-106 are as follows: the operating temperature of the material at the outlet of the high-temperature vacuum pump is reduced from 120~150℃ to 115~120℃, and the fresh air is preheated from 80~100℃ to 100-120℃. In heat exchanger E-104, the ratio of fresh air preheated by the high-temperature material at the outlet of the reaction vacuum pump to the total feed fresh air is 5%~95%. The operating pressure of the material at the outlet of the reaction vacuum pump is 0.005 MPa~0.1 MPa.

2. A method for regenerating an energy-saving and water-saving propane dehydrogenation catalyst, characterized in that: Fresh air is pressurized by blower / compressor C-101 and then divided into two streams. The first stream of fresh air goes to heat exchanger E-104 to preheat the high-temperature material at the outlet of the reaction vacuum pump as a heat source. The second stream goes to heat exchanger E-102 to preheat the material with regenerated flue gas. The two preheated streams are then mixed and passed through the fifth and third stages of waste heat boiler E-101 before entering regenerated air heater H-101. The mixed gas, after being heated by fuel gas, goes to reactor R-101 for heating and regeneration. The high-temperature regenerated flue gas at the reactor outlet passes through the flue gas filtration section, heat exchange section 1, non-methane removal bed, heat exchange section 2, heat exchange section 3, heat exchange section 4, heat exchange section 5, flue gas treatment bed and heat exchange section 6 in the waste heat boiler E-101, and then passes through heat exchangers E-102 and E-103 for medium and low temperature waste heat recovery. The high-temperature material at the outlet of the reaction vacuum pump is cooled by heat exchanger E-104 and aftercooler E-105. After cooling, the high-temperature material is separated by a separator. The resulting condensate is pressurized by a condensate pump and returned to the unit for processing and recycling. The exhaust gas from the top of the tank is mixed with the regenerated flue gas and then sent to the emission system. The operating temperature of the material at the outlet of the high-temperature vacuum pump in the E-105 aftercooler is reduced from 115~120℃ to 90~115℃. The cooling medium is at least one of the following: boiler water, warm water in a warm water system, organic medium in an organic Rankine cycle, ammonia in an ammonia water refrigeration system, and water in a lithium bromide heating system. The operating conditions for materials on the hot and cold sides of heat exchanger E-104 are as follows: the operating temperature of the material at the outlet of the high-temperature vacuum pump is reduced from 320~450℃ to 120~150℃, and the fresh air is preheated from 100~120℃ to 150-430℃. In heat exchanger E-104, the ratio of fresh air preheated by the high-temperature material at the outlet of the reaction vacuum pump to the total feed fresh air is 5%~95%. The operating pressure of the material at the outlet of the reaction vacuum pump is 0.005 MPa~0.1 MPa.

3. A method for regenerating an energy-saving and water-saving propane dehydrogenation catalyst, characterized in that: Fresh air is pressurized by blower / compressor C-101 and preheated by heat exchanger E-106. Then it is divided into two streams. The first stream of fresh air goes to heat exchanger E-104 to preheat with the high-temperature material at the outlet of the reaction vacuum pump as a heat source. The second stream is preheated by heat exchanger E-102 and waste heat boiler E-101 in six stages. The two preheated streams are mixed and then pass through the waste heat boiler E-101 in four stages and one stage before entering the regenerated air heater H-101. The mixed gas, after being heated by fuel gas, goes to reactor R-101 for heating and regeneration. The high-temperature regenerated flue gas at the reactor outlet passes through the flue gas filtration section, heat exchange section 1, heat exchange section 2, non-methane removal bed, heat exchange section 3, heat exchange section 4, heat exchange section 5, heat exchange section 6, flue gas treatment bed and heat exchange section 7 in the waste heat boiler E-101, and then passes through heat exchangers E-102 and E-103 for medium and low temperature waste heat recovery. The high-temperature material at the outlet of the reaction vacuum pump is cooled by heat exchangers E-104, E-106 and aftercooler E-105. After cooling, the high-temperature material is separated by a separator. The resulting condensate is pressurized by a condensate pump and returned to the unit for processing and recycling. The exhaust gas from the top of the tank is mixed with the regenerated flue gas and then sent to the emission system. The operating temperature of the material at the outlet of the high-temperature vacuum pump in the aftercooler E-105 is reduced from 115~120℃ to 90~115℃. The cooling medium is at least one of the following: boiler water, warm water in the warm water system, organic medium in the organic Rankine cycle, ammonia in the ammonia water refrigeration system, and water in the lithium bromide heating system. The operating conditions for the hot and cold sides of the heat exchanger E-104 are as follows: the operating temperature of the material at the outlet of the high-temperature vacuum pump is reduced from 320~450℃ to 120~150℃, and the fresh air is preheated from 100~120℃ to 150-430℃. The operating conditions for the hot and cold sides of the heat exchanger E-106 are as follows: the operating temperature of the material at the outlet of the high-temperature vacuum pump is reduced from 120~150℃ to 115~120℃, and the fresh air is preheated from 80~100℃ to 100-120℃. In the heat exchanger E-104, the ratio of the amount of fresh air preheated by the high-temperature material at the outlet of the reaction vacuum pump to the total feed fresh air is 5%~95%. The operating pressure of the material at the outlet of the reaction vacuum pump is 0.005 MPa~0.1 MPa.

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