Device and method for producing olefin through alkane catalytic dehydrogenation by quenching and rapidly separating oil agent

Abstract

The invention provides an alkane catalytic dehydrogenation olefin production device and method capable of quenching and rapidly separating an oil agent. A reaction unit comprises a pre-lifting zone, an oil agent contact zone, a reaction zone, a product quenching zone, a reaction outlet zone, an oil agent separation zone and a steam stripping zone; a quick separation device is arranged between the product quenching area and the reaction outlet area, and the oil agent separation area is provided with a first two-stage cyclone separator; an outlet of the product quenching area is communicated with a quick separation oil agent inlet of the quick separation device, a quick separation catalyst outlet of the quick separation device is communicated with a catalyst inlet of the steam stripping area, and a quick separation oil gas outlet of the quick separation device is communicated with an inlet of the reaction outlet area. According to the invention, the oil agent mixture after the reaction is rapidly cooled, is rapidly separated by the rapid separation device and then is further separated, rapid cooling is combined with two-stage separation, so that the reaction is rapidly terminated, the side reaction is inhibited, and the olefin selectivity and the alkane conversion rate are obviously improved.

Description

Technical Field

[0001] The present invention relates to the technical field of petrochemical industry, and in particular to a device and method for catalytic dehydrogenation of alkanes to produce olefins for rapid cooling and rapid separation of oil. Background Art

[0002] Catalytic dehydrogenation of alkanes involves the removal of one molecule of hydrogen from an alkane to produce an olefin over a catalyst. The reaction is simple, with high yields of the target product, and has been widely adopted in industry worldwide. Based on the reactor type, alkane catalytic dehydrogenation technology can be categorized into three types: fixed-bed, moving-bed, and fluidized-bed. Lummus' Catofin process is the most widely used fixed-bed process. However, its development has been limited by the toxicity of its Cr-based catalyst, which poses environmental risks. Furthermore, the frequent switching of fixed-bed reactors during operation complicates operation and requires a large footprint. Moving-bed processes, exemplified by UOP's Oleflex process, utilize Pt-based catalysts, which have high production costs, demanding raw material requirements, and prone to deactivation during the reaction. With the increasing scale and expansion of alkane dehydrogenation equipment, the fluidized-bed process is gaining popularity. Its flexible operation, efficient and stable production process, and the use of environmentally friendly, non-precious metal, and highly efficient dehydrogenation catalysts have led to its increasing popularity among major manufacturers.

[0003] US5656243A discloses a fluidized bed reactor and its application method. In this reactor, gas and solid fluids flow in countercurrents. Horizontal baffles are provided in the reactor, separating the gas and solid fluids as they flow through the baffles, causing gas to flow upward and solid particles to flow downward, with the gas exiting the baffle at a higher position than the solid particles. This reactor is capable of maintaining at least 70% of the gas and solid particles in a fluidized bed during a reaction. US20080161624A1 discloses a fluidized bed reactor for dehydrogenating low-carbon alkanes with backmixing. Alkanes react with a catalyst in a single fluidized bed reactor with backmixing. The deactivated catalyst is then heated and regenerated, and the regenerated catalyst is returned to the fluidized bed reactor with backmixing for recycling, thereby maintaining a reasonable heat level in the fluidized bed reactor. This reactor can improve alkane conversion and olefin selectivity, while reducing equipment construction and operating costs. US20160272559A1 discloses a catalytic dehydrogenation method using an ascending fluidized bed reactor capable of processing feedstocks containing alkanes or alkylaromatics. The fluidized bed reactor comprises one or more reactors, with a reaction temperature of 500-800°C, a weight hourly space velocity of 0.1-1000, and a gas residence time of 0.1-10 seconds. A cyclone separator is used to separate the reacted oil mixture. A cooling device is provided between the reactor and the cyclone separator to terminate the thermal cracking reaction by cooling, thereby effectively improving the overall selectivity of the olefin product. WO2020 / 186937A1 discloses a circulating fluidized bed apparatus for alkane dehydrogenation, comprising a reaction unit and a regeneration unit. The reaction unit includes a reactor and a reaction settler, the reaction settler communicating with the reactor. A catalyst distributor is provided within the reactor, through which the catalyst is sprayed into the reactor along the reactor wall toward the central axis. The regeneration unit includes a regenerator containing the catalyst and a regenerator settler, the regenerator settler being located above the regenerator. The device can achieve higher alkane conversion rate and olefin yield.

[0004] A review of the prior art reveals that enhancing the contact between the alkane feedstock and the catalyst, optimizing reaction conditions, and optimizing the content and formulation of active components in the catalyst can effectively improve the conversion rate and olefin selectivity of alkane catalytic dehydrogenation reactions. However, due to the presence of restricted reaction zones in the reactors used, failure to promptly terminate the reaction afterward, and the presence of acidic centers in the catalyst, side reactions of the alkanes can hinder further improvements in olefin selectivity. Therefore, given the challenges of the prior art, finding an apparatus and method for catalytic dehydrogenation of alkanes to produce olefins that rapidly terminates the post-reaction oil mixture, avoids or reduces side reactions, and ultimately improves the selectivity of the target olefin product and the conversion rate of the alkane feedstock remains a pressing technical challenge. Summary of the Invention

[0005] To this end, the present invention provides an apparatus and method for catalytic dehydrogenation of alkanes to produce olefins by rapidly cooling and quickly separating the oil agent. The purpose is to improve olefin selectivity and alkane conversion rate by rapidly cooling the oil agent mixture after the reaction, then quickly separating it in a quick separation device and then further separating it in a first two-stage cyclone separator.

[0006] In a first aspect, the present invention provides an alkane catalytic dehydrogenation device for rapidly cooling and separating an oil agent to produce olefins, comprising a reaction unit and a regeneration unit;

[0007] The reaction unit includes a pre-lifting zone, an oil-agent contact zone, a reaction zone, a product quenching zone, a reaction outlet zone, an oil-agent separation zone and a stripping zone in sequence;

[0008] A quick separation device is provided between the product quenching zone and the reaction outlet zone, and the oil agent separation zone is provided with a first two-stage cyclone separator; the outlet of the product quenching zone is communicated with the quick separation oil agent inlet of the quick separation device, the quick separation catalyst outlet of the quick separation device is communicated with the catalyst inlet of the stripping zone, the quick separation oil and gas outlet of the quick separation device is communicated with the inlet of the reaction outlet zone; the outlet of the reaction outlet zone is communicated with the inlet of the first two-stage cyclone separator;

[0009] The catalyst outlet of the first two-stage cyclone separator is connected to the catalyst inlet of the stripping zone, and the oil and gas outlet of the first two-stage cyclone separator is connected to the reaction oil and gas outlet;

[0010] The catalyst outlet of the stripping zone is communicated with the catalyst inlet to be regenerated of the regeneration unit, and the regenerated catalyst outlet of the regeneration unit is communicated with the catalyst inlet of the oil-agent contact zone.

[0011] In a second aspect, the present invention provides a method for catalytic dehydrogenation of alkanes to produce olefins by quenching and quickly separating the oil agent. The method is implemented based on the above-mentioned catalytic dehydrogenation of alkanes to produce olefins device. The alkane feedstock and the catalyst react in the reaction zone to obtain an oil agent mixture which enters a product quenching zone for cooling. After cooling, the oil agent mixture enters a quick separation device for separation. The separated catalyst enters a stripping zone for stripping. The separated oil and gas enter an oil agent separation zone after passing through a reaction outlet zone.

[0012] Beneficial effects:

[0013] The catalytic dehydrogenation device and method for producing olefins from alkanes for rapid cooling and rapid separation of oil agents of the present invention allows the oil agent mixture to be rapidly cooled after the reaction, and then rapidly separated by a rapid separation device and then further separated by a first two-stage cyclone separator. The rapid cooling combined with the two-stage separation allows the reaction to be quickly terminated, suppresses the occurrence of side reactions, and significantly improves the olefin selectivity and alkane conversion rate. BRIEF DESCRIPTION OF THE DRAWINGS

[0014] Figure 1 This is a schematic structural diagram of a specific embodiment of the alkane catalytic dehydrogenation device for rapidly cooling and quickly separating the oil agent of the present invention to produce olefins;

[0015] Figure 2 and Figure 3 This is a schematic structural diagram of a specific embodiment of a heat exchange coil in an alkane catalytic dehydrogenation device for rapidly cooling and quickly separating an oil agent according to the present invention;

[0016] Figure 4 This is a schematic structural diagram of a specific embodiment of a quick separation device in an alkane catalytic dehydrogenation device for rapidly cooling and quickly separating an oil agent according to the present invention;

[0017] Figure 5 This is a schematic structural diagram of another specific embodiment of a quick separation device in an alkane catalytic dehydrogenation device for rapidly cooling and quickly separating an oil agent according to the present invention;

[0018] Figure 6 This is a schematic structural diagram of a specific embodiment of the oil agent contact zone in the alkane catalytic dehydrogenation device for rapidly cooling and quickly separating the oil agent of the present invention;

[0019] Figure 7 This is a schematic structural diagram of another specific embodiment of the oil agent contact zone in the alkane catalytic dehydrogenation device for rapidly cooling and quickly separating the oil agent of the present invention;

[0020] Description of Reference Numerals

[0021] 11 Pre-lifting zone 12 Oil-agent contact zone 13 Reaction zone

[0022] 14 Product quenching zone 15 Reaction outlet zone 16 Stripping zone

[0023] 17 Oil separation area 18 Heat exchange coil

[0024] 101 Pre-lift gas pipe 102 Alkane feed pipe 103 Alkane feed distributor

[0025] 104 Catalyst feed distribution 105 Transport of catalyst to be regenerated 106 Slide valve to be regenerated

[0026] tube

[0027] 107 Quick separation device 108 First two-stage cyclone separation 109 Gas collection chamber

[0028] Separator

[0029] 110 Reaction oil and gas outlet 111 Stripping gas inlet

[0030] 21 Regeneration heating area 22 Regeneration area

[0031] 201 Fuel pipe 202 Fuel heating pipe 203 Regeneration catalyst delivery pipe

[0032] 204 regeneration slide valve 205 second two-stage cyclone 206 regeneration air collecting chamber

[0033] Separator

[0034] 207 Regeneration flue gas outlet 208 Oxygen-containing gas inlet

[0035] 301 Quick separation oil agent inlet 302 Quick separation catalyst outlet 303 Quick separation oil and gas outlet DETAILED DESCRIPTION

[0036] The present application will be further described in detail below through the accompanying drawings and examples, through which the features and advantages of the present application will become more clear and distinct.

[0037] The word "exemplary" is used exclusively herein to mean "serving as an example, example, or illustration." Any embodiment described herein as "exemplary" is not necessarily to be construed as preferred or advantageous over other embodiments. Although various aspects of the embodiments are shown in the drawings, the drawings are not necessarily drawn to scale unless otherwise indicated.

[0038] In this specification, the terms "upstream" and "downstream" are based on the flow direction of the reactants. For example, when the reactants flow from bottom to top, "upstream" refers to a position below, while "downstream" refers to a position above.

[0039] In addition, the technical features involved in different embodiments of the present application described below can be combined with each other as long as they do not conflict with each other.

[0040] In the first aspect, the present invention provides a device for catalytic dehydrogenation of alkanes to produce olefins for rapid cooling and rapid separation of oil, such as Figure 1 As shown, it includes a reaction unit and a regeneration unit;

[0041] The reaction unit includes a pre-elevation zone 11, an oil-agent contact zone 12, a reaction zone 13, a product quenching zone 14, a reaction outlet zone 15, an oil-agent separation zone 17 and a stripping zone 16 in sequence;

[0042] A quick separation device 107 is provided between the product quenching zone 14 and the reaction outlet zone 15, and the oil agent separation zone 17 is provided with a first two-stage cyclone separator 108; the outlet of the product quenching zone 14 is communicated with the quick separation oil agent inlet 301 of the quick separation device 107, the quick separation catalyst outlet 302 of the quick separation device 107 is communicated with the catalyst inlet of the stripping zone 16, and the quick separation oil and gas outlet 303 of the quick separation device 107 is communicated with the inlet of the reaction outlet zone 15; the outlet of the reaction outlet zone 15 is communicated with the inlet of the first two-stage cyclone separator 108;

[0043] The catalyst outlet of the first two-stage cyclone separator 108 is connected to the catalyst inlet of the stripping zone 16, and the oil and gas outlet of the first two-stage cyclone separator 108 is connected to the reaction oil and gas outlet 110;

[0044] The catalyst outlet of the stripping zone 16 is communicated with the catalyst inlet to be regenerated of the regeneration unit, and the regenerated catalyst outlet of the regeneration unit is communicated with the catalyst inlet of the oil-agent contact zone 12 .

[0045] It should be noted that, from upstream to downstream, the reaction unit includes multiple zones, such as a pre-lifting zone, an oil-agent contact zone, etc. Any two adjacent zones are fluidically connected.

[0046] It should be noted that the alkane feedstock and the catalyst are fully contacted in the oil-agent contact zone 12, and then introduced into the reaction zone together with the pre-lifting gas from the pre-lifting zone for reaction. The oil-agent mixture after the reaction is introduced into the product quenching zone. After the temperature of the oil-agent mixture is rapidly reduced, it enters the quick separation device for rapid separation of the catalyst and oil and gas. The quickly separated catalyst enters the stripping zone for stripping. The quickly separated oil and gas carrying catalyst fine powder are introduced into the oil-agent separation zone after passing through the reaction outlet zone and are further separated from the oil by the first two-stage cyclone separator. The reaction oil and gas separated by the cyclone are drawn out of the device, and the catalyst separated by the cyclone is introduced into the stripping zone for stripping. The catalyst to be regenerated after stripping is introduced into the regeneration unit for regeneration, and the regenerated catalyst is returned to the oil-agent contact zone for recycling.

[0047] In the present invention, Figure 1 In the device shown, the reaction zone can be selected from a combination of one or more of a bubbling bed, a turbulent bed, a fast bed, and a transport bed. The reaction zone can be a constant diameter reaction zone, and the diameter to height ratio can be 1:5 to 50, preferably 1:10 to 30.

[0048] In the present invention, Figure 1In the illustrated device, the reaction outlet zone can be located within the oil-agent separation zone. After rapid cooling, the reacted oil-agent mixture is first rapidly separated by a quick separation device. The separated catalyst enters the stripping zone for stripping. The separated oil vapor carrying catalyst fines passes through the reaction outlet zone and enters the first two-stage cyclone separator for more thorough oil-agent separation. The coordinated operation of these two separation devices allows for rapid separation of the reacted oil-agent mixture, further suppressing side reactions and improving olefin selectivity. Furthermore, the quick separation device's initial separation of the reacted oil-agent mixture not only reduces the load on the first two-stage cyclone separators, improving separation efficiency, but also reduces the oil vapor and catalyst gas velocities at the inlets of the first two-stage cyclone separators, minimizing catalyst wear and loss.

[0049] The device of the present invention strengthens the contact between the alkane raw material and the catalyst through the high-efficiency oil contact zone, thereby promoting better initiation of the catalytic dehydrogenation reaction; Figure 1 The reasonable reactor type shown provides a suitable reaction environment for the catalytic dehydrogenation reaction of alkanes, promotes the progress of the catalytic dehydrogenation reaction, and improves the alkane conversion rate; through the product quenching zone, the quick separation device and the first two-stage cyclone separator, the reaction product is quickly cooled to a lower temperature and the catalyst and oil and gas are efficiently and quickly separated, so that the reaction is quickly terminated, the occurrence of side reactions is suppressed, and the olefin selectivity is improved.

[0050] In one embodiment of the above-mentioned alkane catalytic dehydrogenation device to produce olefins of the present invention, the ratio of the diameter to the height of the product quenching zone (14) is 1:(1-3), preferably 1:(1-1.5);

[0051] like Figure 2 and Figure 3 As shown, the product quenching zone 14 is provided with a heat exchange coil 18, and the heat exchange coil 18 includes a plurality of annular tubes connected end to end; a quenching medium inlet is provided on one side of the top of the heat exchange coil 18, and a quenching medium outlet is provided on one side of the bottom of the heat exchange coil.

[0052] It should be noted that multiple annular tubes are connected end-to-end to form a heat exchange coil. The area surrounded by the heat exchange coil forms the product quench zone. The oil-solvent mixture from the reaction zone rapidly cools down after passing through the product quench zone. The quench medium inlet can be located on one side of the top annular tube, and the quench medium outlet can be located on one side of the bottom annular tube. The quench medium inlet and outlet can be on the same side or on different sides. By introducing quench medium into the quench medium inlet of the heat exchange coil, the reaction product can be rapidly cooled to a lower temperature, suppressing side reactions and improving olefin selectivity.

[0053] In another embodiment of the above-mentioned alkane catalytic dehydrogenation to olefins device of the present invention, the quick separation device 107 is selected from a combination of one or more of a cyclone quick separator, a three-leaf quick separator, a catapult quick separator, a U-shaped tube separator, a wall-cutting quick separator and a cantilever quick separator, and is preferably a cyclone quick separator.

[0054] It should be noted that in the device of the present invention, the quick separation device is selected from a combination of one or more of the above-mentioned separators, especially when it is a cyclone-type quick separator. The oil-agent mixture after rapid cooling in the product quenching zone can be quickly separated in the first step by the quick separation device, and then separated in the second step by the first two-stage cyclone separator. This can enable the oil-agent mixture to be efficiently and quickly separated into oil, gas and catalyst, prevent the catalyst from catalyzing side reactions of oil and gas, and further improve the olefin selectivity and alkane conversion rate.

[0055] In one embodiment of the above-mentioned alkane catalytic dehydrogenation device for producing olefins of the present invention, Figure 4 As shown, the quick separation device 107 includes a variable diameter section and a constant diameter section that are connected to each other. The constant diameter section is connected to the downstream end of the variable diameter section, and the diameter of the variable diameter section gradually increases from upstream to downstream. The quick separation oil agent inlet 301 is opened on the upper side of the constant diameter section, the quick separation catalyst outlet 302 is located at the bottom of the variable diameter section, and the quick separation oil and gas outlet 303 is located at the top of the constant diameter section; or,

[0056] like Figure 5 As shown, the quick separation device 107 includes an external structure and an internal structure. The external structure includes an external constant diameter section, an external variable diameter section and an external outlet constant diameter section that are connected in sequence, and the diameter of the external variable diameter section gradually decreases from upstream to downstream; the internal structure includes an equal diameter separation section that is sleeved inside the external constant diameter section, the quick separation oil agent inlet 301 is located at the bottom of the equal diameter separation section, the quick separation catalyst outlet 302 is opened on the upper side of the equal diameter separation section, and the quick separation oil and gas outlet 303 is located at the top of the external outlet constant diameter section.

[0057] It should be noted that the oil mixture after rapid cooling enters the quick separation device through the quick separation oil inlet 301 for rapid separation of catalyst and oil gas. The separated catalyst is output through the quick separation catalyst outlet 302 and enters the stripping zone for stripping. The separated oil gas is output through the quick separation oil and gas outlet 303 and enters the reaction outlet zone. Figure 4 or Figure 5 The quick separation device of the structure shown can better and quickly separate the oil-agent mixture after cooling, inhibit the occurrence of side reactions, and further improve the alkane conversion rate and olefin selectivity.

[0058] In one embodiment of the above-mentioned alkane catalytic dehydrogenation to olefins device of the present invention, the oil agent contact zone 12 is provided with an alkane feed distributor 103 and a catalyst feed distributor 104, and the regenerated catalyst outlet of the regeneration unit is connected to the catalyst feed distributor 104; the pre-lifting zone 11 is provided with a pre-lifting gas pipe 101, and the stripping zone 16 is provided with a stripping gas inlet 111.

[0059] It should be noted that the pre-lift gas pipe 101 can be disposed at the bottom of the pre-lift zone 11. By introducing pre-lift gas into the pre-lift zone, the pre-lift gas and the fully contacted alkane feedstock and catalyst mixture from the oil-agent contact zone enter the reaction zone. The pre-lift gas can be well known to those skilled in the art, for example, one or more of water vapor, nitrogen, and dry gas, preferably water vapor. Stripping gas can be introduced into the stripping zone through a stripping gas inlet to remove residual reaction oil and gas on the spent catalyst. The stripping gas can be well known to those skilled in the art, for example, one or more of water vapor, nitrogen, and dry gas, preferably water vapor.

[0060] like Figure 6 As shown, an alkane feed distributor may be provided in the middle and lower part of the oil agent contact zone, and the height of the alkane feed distributor from the bottom of the oil agent contact zone may be 0 to 1 / 2 of the height of the oil agent contact zone, preferably 0 to 1 / 4. The preheated alkane feedstock is introduced into the alkane feed distributor, and then introduced into the oil agent contact zone through the feed hole on the alkane feed distributor. A catalyst feed distributor may be provided in the middle and upper part of the oil agent contact zone, and the height of the catalyst feed distributor from the bottom of the oil agent contact zone may be 1 / 2 to 1 of the height of the oil agent contact zone, preferably 3 / 4 to 1. The catalyst feed distributor is connected to the regenerated catalyst delivery pipe, and the regenerated catalyst from the regeneration zone is introduced into the oil agent contact zone, so that the alkane feedstock and the regenerated catalyst are in sufficient countercurrent contact in the oil agent contact zone, thereby promoting the initiation of the catalytic dehydrogenation reaction. Alternatively, as Figure 7 As shown, an alkane feed distributor can be set in the middle and upper part of the oil contact zone, and the height of the alkane feed distributor from the bottom of the oil contact zone can be 1 / 2 to 1, preferably 3 / 4 to 1 of the height of the oil contact zone. At this time, a catalyst feed distributor can be set in the middle and lower part of the oil contact zone, and the height of the catalyst feed distributor from the bottom of the oil contact zone can be 0 to 1 / 2, preferably 0 to 1 / 4 of the height of the oil contact zone. Figure 1 As shown, the alkane feedstock can be introduced into the alkane feed distributor 103 through the alkane feed pipe 102.

[0061] The alkane feed distributor can be an annular structure with multiple alkane feed holes spaced apart, with an opening ratio of 80-90%. The diameter of the alkane feed holes can be 1 / 2-3 / 4 of the width of the annular structure, and the angle between the alkane feed holes and the central axis of the alkane feed distributor can be 30-50 degrees. The catalyst feed distributor can be a disc structure with multiple catalyst feed holes, with an opening ratio of 80-90%, and the axes of the feed holes are parallel to the central axis of the catalyst distributor. The opening direction of the alkane feed holes in the alkane feed distributor is opposite to the opening direction of the catalyst feed holes in the catalyst feed distributor, i.e., one is upward and the other is downward.

[0062] In one embodiment of the above-mentioned alkane catalytic dehydrogenation device for producing olefins of the present invention, the regeneration unit includes a regeneration and heating zone 21 and a regeneration zone 22;

[0063] The regeneration and heating zone 21 is located inside or outside the regeneration zone 22. The regeneration and heating zone 21 is provided with a fuel pipe 201 for introducing fuel. The heat outlet of the regeneration and heating zone 21 is connected to the regeneration zone 22 via a fuel heating pipe 202.

[0064] The inlet of the catalyst to be regenerated of the regeneration unit is connected to the regeneration zone 22, and the regeneration zone 22 is provided with an oxygen-containing gas inlet 208. The catalyst outlet of the regeneration zone 22 is connected to the inlet of the second two-stage cyclone separator 205; the catalyst outlet of the second two-stage cyclone separator 205 is connected to the regenerated catalyst outlet of the regeneration unit 2, and the flue gas outlet of the second two-stage cyclone separator 205 is connected to the inlet of the regeneration collecting chamber 206, and the regeneration collecting chamber 206 is provided with a regeneration flue gas outlet 207.

[0065] It should be noted that fuel is introduced into the regeneration heating zone through a fuel pipe to be burned, thereby supplementing heat for the regeneration zone and allowing the entire reaction unit and regeneration unit to reach thermal equilibrium. The fuel may be well known to those skilled in the art, for example, it may include one or more of methane, ethane, dry gas, liquefied gas, and fuel oil, preferably dry gas produced by this device. The catalyst to be regenerated obtained by stripping is introduced into the regeneration zone through a catalyst delivery pipe to be regenerated, and an oxidizing gas is introduced into the regeneration zone through an oxygen-containing gas inlet to burn off the coke deposited on the catalyst to be regenerated, and the active components in the catalyst are converted into an oxidized state, thereby restoring the dehydrogenation activity of the catalyst. The oxidizing gas includes oxygen, air, and other mixed gases containing oxygen. After regeneration, the catalyst is separated from the regeneration flue gas carried by the second two-stage cyclone separator, and the regeneration flue gas passes through the regeneration gas collecting chamber and is led out of the regeneration unit through the regeneration flue gas outlet.

[0066] In one embodiment of the above-mentioned alkane catalytic dehydrogenation to olefins device of the present invention, the catalyst outlet of the stripping zone 16 is connected to the catalyst inlet of the regeneration unit via a catalyst delivery pipe 105, and the catalyst delivery pipe 105 is provided with a regeneration slide valve 106; the regenerated catalyst outlet of the regeneration unit is connected to the catalyst feed distributor 104 of the oil contact zone 12 via a regenerated catalyst delivery pipe 203, and the regenerated catalyst delivery pipe 203 is provided with a regeneration slide valve 204;

[0067] The oil and gas outlet of the first two-stage cyclone separator 108 is communicated with the inlet of the gas collecting chamber 109 , and the outlet of the gas collecting chamber 109 is communicated with the reaction oil and gas outlet 110 .

[0068] It should be noted that the stripped regenerated catalyst is introduced into the regeneration unit through the regenerated catalyst delivery pipe for regeneration. The flow rate of the regenerated catalyst in the regenerated catalyst delivery pipe can be adjusted by adjusting the opening of the regeneration slide valve. The flow rate of the regenerated catalyst in the regenerated catalyst delivery pipe can be adjusted by adjusting the opening of the regeneration slide valve. The reaction oil and gas separated in the oil separation zone passes through the gas collection chamber and is then led out of the device through the reaction oil and gas outlet.

[0069] In a second aspect, the present invention provides a method for rapidly cooling and quickly separating an oil agent by catalytic dehydrogenation of alkanes to produce olefins. The method is implemented based on the above-mentioned catalytic dehydrogenation of alkanes to produce olefins apparatus. The alkane feedstock and the catalyst react in the reaction zone 13 to obtain an oil agent mixture which enters the product rapid cooling zone 14 for cooling. After cooling, the oil agent mixture enters the quick separation device 107 for separation. The separated catalyst enters the stripping zone 16 for stripping. The separated oil and gas enter the oil agent separation zone 17 after passing through the reaction outlet zone 15.

[0070] It should be noted that the above method of the present invention may further include a step of preheating the alkane feedstock, wherein the alkane feedstock is preheated to 350-500° C. and then introduced into the oil contact zone.

[0071] In one embodiment of the above method of the present invention, the temperature of the product quenching zone 14 is 200 to 550°C, preferably 250 to 500°C;

[0072] The quenching medium entering the heat exchange coil through the quenching medium inlet is selected from one or more of quenching oil, quenching water, quenching gas and alkane feedstock, preferably one or more of alkane feedstock.

[0073] It should be noted that in the method of the present invention, by controlling the temperature of the product quenching zone as described above, the oil mixture after the reaction can be quickly cooled, and then the catalyst and oil gas are quickly separated to quickly terminate the reaction, avoid the occurrence of side reactions, and improve olefin selectivity and alkane conversion rate.

[0074] In one embodiment of the above method of the present invention, the oil agent linear speed of the quick separation oil agent inlet 301 of the quick separation device 107 is 2 to 20 m / s, preferably 5 to 18 m / s; the oil and gas linear speed of the quick separation oil and gas outlet 303 of the quick separation device 107 is 2 to 15 m / s, preferably 5 to 10 m / s.

[0075] It should be noted that by controlling the oil linear velocity at the quick separation oil inlet and the oil and gas linear velocity at the quick separation oil and gas outlet of the quick separation device as described above, the cooled oil mixture can be efficiently and quickly subjected to preliminary separation in the quick separation device, and then subjected to cyclone separation in the first two-stage cyclone separator to quickly and thoroughly separate the catalyst and oil and gas, quickly terminate the reaction, effectively suppress the occurrence of side reactions, and further improve the olefin selectivity and alkane conversion rate.

[0076] In another embodiment of the above method of the present invention, the conditions in the oil contact zone 12 include:

[0077] The temperature is 500-700°C, preferably 520-680°C, and the catalyst density is 100-500 kg / m 3 , preferably 150~400kg / m 3 The residence time of the alkane feedstock and the catalyst in the oil contact zone is 0.05 to 0.5 s, preferably 0.1 to 0.3 s;

[0078] The conditions in the reaction zone 13 include:

[0079] The temperature at the bottom of the reaction zone is 520-680°C, preferably 540-660°C, and the catalyst density is 150-400 kg / m 3 , preferably 200~350kg / m 3 , the pressure is 0.05-0.2MPa, preferably 0.05-0.15MPa; the temperature at the top of the reaction zone is 480-640℃, preferably 500-620℃, and the catalyst density is 30-200kg / m 3 , preferably 50 to 150 kg / m 3 , the pressure is 0.05-0.15 MPa, preferably 0.05-0.12 MPa;

[0080] The alkane raw material is selected from C2 to C8 alkanes.

[0081] It should be noted that the above pressures represent gauge pressures. By controlling the temperature, catalyst density, and residence time in the oil-contact zone, as well as the temperature, pressure, and catalyst density in the reaction zone, the alkane feedstock can be more effectively dehydrogenated to olefins, further improving olefin selectivity and alkane conversion.

[0082] In one embodiment of the above method of the present invention, the conditions of the regeneration unit include:

[0083] The regeneration temperature is 600-720°C, preferably 620-700°C, and the catalyst density is 50-500 kg / m 3 , preferably 100~400kg / m 3 , the pressure is 0.05-0.2MPa, preferably 0.05-0.15MPa;

[0084] The fuel introduced into the regeneration and heating zone 21 through the fuel pipe 201 includes one or more of methane, ethane, dry gas, liquefied gas and fuel oil, and is preferably the dry gas generated by the device.

[0085] It should be noted that the aforementioned pressures may represent gauge pressures. By controlling the temperature, catalyst density, and pressure of the regeneration unit as described above, the catalyst can be regenerated effectively, while maintaining a good thermal balance between the entire reaction unit and the regeneration unit, thereby promoting the alkane dehydrogenation reaction to produce olefins, thereby increasing alkane conversion and olefin selectivity.

[0086] In another embodiment of the above method of the present invention, the catalyst comprises an active component and a support;

[0087] The active component is selected from one or more metals or oxides of Zn, Fe, Co, Ni, V, Sn and Mg, and the carrier is selected from one or more of Al2O3, SiO2, ZrO2, TiO2 and molecular sieves;

[0088] Based on the weight of the catalyst, the content of the active component is 10-90%, and the content of the carrier is 10-90%; preferably, the content of the active component is 20-70%, and the content of the carrier is 30-80%.

[0089] It should be noted that, in the method of the present invention, the catalytic reaction is carried out using a catalyst composed of the above active components and the carrier according to the above proportions, which can enable the catalytic dehydrogenation of alkanes to have a higher alkane conversion rate and olefin selectivity.

[0090] The present invention is further described in detail below by way of examples, but the present invention is not limited thereto. In the following examples, unless otherwise specified, the experimental instruments and raw materials involved are all commercially available products.

[0091] The raw materials used in the following examples and comparative examples are propane, n-butane and isobutane, and the catalyst used is an alkane dehydrogenation catalyst prepared by the Sinopec Research Institute of Petroleum Processing.

[0092] The chemical composition and properties of the alkane dehydrogenation catalyst are shown in Table 1.

[0093] Table 1 Composition and properties of alkane dehydrogenation catalysts

[0094] project Physical and chemical properties Chemical composition / %(w) <![CDATA[Al2O3]]> 23.30 <![CDATA[SiO2]]> 0.30 MgO 0.43 <![CDATA[TiO2]]> 35.00 <![CDATA[Fe2O3]]> 0.22 <![CDATA[ZrO2]]> 5.00 ZnO 35.30 BET Full Analysis <![CDATA[ BET total surface area / (m 2 ·g -1 )]]> 24.00 <![CDATA[Total pore volume / (cm 3 ·g -1 )]]> 0.1038

[0095] In the following examples and comparative examples, the calculation methods for alkane conversion and olefin selectivity are as follows:

[0096] Alkane conversion rate = (mass fraction of alkanes in the feed - mass fraction of alkanes in the product) ÷ mass fraction of alkanes in the feed;

[0097] Olefin selectivity = (mass fraction of olefins in the product ÷ mass fraction of alkanes in the feed) ÷ alkane conversion.

[0098] In the following examples, Figure 6 As shown, the alkane feed distributor is an annular structure with multiple alkane feed holes spaced apart, with an opening porosity of 85%. The diameter of the feed holes is 3 / 4 of the annular ring width, the feed holes open upward, and the axis of the feed holes is at an angle of 45° with the central axis of the alkane feed distributor. The catalyst feed distributor is a disc structure with multiple catalyst feed holes, with an opening porosity of 85%. The feed holes face downward, and the axis of the feed holes is parallel to the central axis of the catalyst distributor. The distance between the alkane feed distributor and the bottom of the oil contact zone is 1 / 4 of the oil contact zone height, and the distance between the catalyst feed distributor and the bottom of the oil contact zone is 3 / 4 of the oil contact zone height.

[0099] The reaction zone in the following examples is a transport bed of constant diameter with a diameter to height ratio of 1:20.

[0100] Example 1

[0101] The experiment Figure 1 The test was conducted on the reaction-regeneration apparatus shown in Figure 1. The apparatus used in the experiment consisted of a reaction unit and a regeneration unit. The reaction unit consisted, from upstream to downstream, of a pre-elevation zone, an oil-solvent contact zone, a reaction zone, a product quench zone, a reaction outlet zone, an oil-solvent separation zone, and a stripping zone. The regeneration unit consisted of a regeneration and reheating zone and a regeneration zone. The diameter-to-height ratio of the product quench zone was 1:1.5, and the oil-solvent separation zone was equipped with a two-stage cyclone separator. The quench medium in the heat exchange coils of the product quench zone was circulating water.

[0102] The preheated alkane is introduced into the oil-agent contact zone through the alkane feed distributor, fully contacts with the catalyst introduced into the oil-agent contact zone through the catalyst feed distributor, and then introduced into the reaction zone together with the pre-lifting gas from the pre-lifting zone for reaction. The oil-agent mixture after the reaction is introduced into the product quenching zone. After the temperature of the oil-agent mixture is reduced, it enters the quick separation device for quick separation. The catalyst obtained by quick separation enters the stripping zone for stripping. The oil and gas carrying the catalyst powder obtained by quick separation enters the reaction outlet zone and then is introduced into the oil-agent separation zone. The reaction oil and gas separated by the two-stage cyclone separator in the oil-agent separation zone is led out of the device. The catalyst separated by the two-stage cyclone separator in the oil-agent separation zone is introduced into the stripping zone for stripping. The catalyst to be regenerated after stripping is introduced into the regeneration zone for regeneration. The regenerated catalyst is introduced into the catalyst distributor for recycling. The quick separation device is specifically a cyclone-type quick separator, such as Figure 4 shown.

[0103] The raw material used in the examples was propane, the pre-lift gas was steam, the stripping gas was nitrogen, and the fuel used in the regeneration and heating zone was dry gas. The reaction conditions and results are shown in Table 2.

[0104] Example 2

[0105] The experiment Figure 1 The test was conducted on the reaction-regeneration apparatus shown in Figure 1. The apparatus used in the experiment consisted of a reaction unit and a regeneration unit. The reaction unit consisted, from upstream to downstream, of a pre-elevation zone, an oil-solvent contact zone, a reaction zone, a product quenching zone, a reaction outlet zone, an oil-solvent separation zone, and a stripping zone. The regeneration unit consisted of a regeneration and reheating zone and a regeneration zone. The diameter-to-height ratio of the product quenching zone was 1:1.2, and the oil-solvent separation zone was equipped with a two-stage cyclone separator. The quenching medium in the heat exchange coils of the product quenching zone was circulating water.

[0106] The preheated alkane is introduced into the oil-agent contact zone through the alkane feed distributor, fully contacts with the catalyst introduced into the oil-agent contact zone through the catalyst feed distributor, and then introduced into the reaction zone together with the pre-lifting gas from the pre-lifting zone for reaction. The oil-agent mixture after the reaction is introduced into the product quenching zone. After the temperature of the oil-agent mixture is reduced, it enters the quick separation device for quick separation. The catalyst obtained by quick separation enters the stripping zone for stripping. The oil and gas carrying the catalyst powder obtained by quick separation enters the reaction outlet zone and then is introduced into the oil-agent separation zone. The reaction oil and gas separated by the two-stage cyclone separator in the oil-agent separation zone is led out of the device. The catalyst separated by the two-stage cyclone separator in the oil-agent separation zone is introduced into the stripping zone for stripping. The catalyst to be regenerated after stripping is introduced into the regeneration zone for regeneration. The regenerated catalyst is introduced into the catalyst feed distributor for recycling. The quick separation device is specifically a cantilever quick separator, such as Figure 5 shown.

[0107] The raw material used in the examples was propane, the pre-lift gas was steam, the stripping gas was nitrogen, and the fuel used in the regeneration and heating zone was dry gas. The reaction conditions and results are shown in Table 2.

[0108] Comparative Example 1

[0109] The apparatus used in the experiment included a reaction unit and a regeneration unit. The reaction unit consisted of, from bottom to top, a pre-lift zone, a reaction zone, a reaction outlet zone, and a stripping zone. The regeneration unit included a regeneration and heating zone and a regeneration zone. The preheated alkanes and catalyst were introduced to the bottom of the reaction zone, along with the pre-lift gas from the pre-lift zone, and then introduced into the reaction zone for reaction. The reacted oil-agent mixture was separated in a two-stage cyclone separator. The separated reaction oil and gas were then withdrawn from the device. The resulting catalyst was introduced into the stripping zone for stripping. The stripped catalyst to be regenerated was then introduced into the regeneration zone for regeneration. The regenerated catalyst was then introduced into a catalyst distributor for recycling. This comparative example lacked an oil-agent contact zone, a product quenching zone, or a rapid separation device.

[0110] The raw material used in the comparative example was propane, the pre-lift gas was steam, the stripping gas was nitrogen, and the fuel used in the regeneration and heating zone was dry gas. The reaction conditions and results are shown in Table 2.

[0111] Comparative Example 2

[0112] The device used in the test includes a reaction unit and a regeneration unit, wherein the reaction unit includes a pre-lifting zone, a reaction zone, a product quenching zone, a reaction outlet zone and a stripping zone from bottom to top, and the regeneration unit includes a regeneration heating zone and a regeneration zone. The ratio of the diameter to the height of the product quenching zone is 1:1.2. The preheated alkanes and catalysts are introduced into the bottom of the reaction zone and introduced into the reaction zone together with the pre-lifting gas from the pre-lifting zone for reaction. The reacted oil mixture is quenched and introduced into a two-stage cyclone separator for separation. The separated reaction oil and gas are drawn out of the device, and the obtained catalyst is introduced into the stripping zone for stripping. The catalyst to be regenerated after stripping is introduced into the regeneration zone for regeneration. The regenerated catalyst is introduced into the catalyst distributor for recycling. There is no oil contact zone and no quick separation device in this comparative example. The quenching medium is circulating water.

[0113] The raw material used in the comparative example was propane, the pre-lift gas was steam, the stripping gas was nitrogen, and the fuel used in the regeneration and heating zone was dry gas. The reaction conditions and results are shown in Table 2.

[0114] Table 2 Reaction conditions and reaction results of Examples 1-2 and Comparative Examples 1-2

[0115]

[0116]

[0117] The oil inlet linear speed and oil and gas outlet linear speed in the table refer to the linear speed of the oil inlet and oil and gas outlet of the quick separation device.

[0118] Example 3

[0119] The method of Example 1 was followed, except that n-butane was used as the raw material. The reaction conditions and product distribution were as shown in Table 3.

[0120] Example 4

[0121] The method of Example 2 was followed, except that the raw material used was isobutane. The reaction conditions and product distribution were shown in Table 3.

[0122] Comparative Example 3

[0123] The method of Comparative Example 1 was followed, except that the raw material used was n-butane. The reaction conditions and product distribution were as shown in Table 3.

[0124] Comparative Example 4

[0125] The method of Comparative Example 2 was followed, except that the raw material used was isobutane. The reaction conditions and product distribution were shown in Table 3.

[0126] Table 3 Reaction conditions and reaction results of Examples 3 to 4 and Comparative Examples 3 to 4

[0127]

[0128]

[0129] As can be seen from Table 2 and Table 3, by adopting the method provided by the present invention, different reactions are all enhanced, and the conversion rate of reactants and the selectivity of target products are greatly improved.

[0130] In the description of this application, it should be noted that the terms "upper", "lower", "inside", "outside", "front", "back", "left", "right", etc. indicate directions or positional relationships based on the directions or positional relationships in the working state of this application. They are only for the convenience of describing this application and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific direction, be constructed and operated in a specific direction. Therefore, they cannot be understood as limitations on this application.

[0131] In the description of this application, it should be noted that, unless otherwise specified or limited, the terms "installed", "connected", and "connected" should be understood in a broad sense. For those skilled in the art, the specific meanings of the above terms in this application can be understood according to specific circumstances.

[0132] The present application has been described above in conjunction with preferred embodiments, but these embodiments are merely exemplary and serve only as an illustrative example. On this basis, various replacements and improvements can be made to the present application, all of which fall within the scope of protection of the present application.

Claims

1. A catalytic dehydrogenation unit for alkane to olefin production with rapid cooling and oil separation, comprising a reaction unit and a regeneration unit; in, The reaction unit sequentially comprises a pre-lifting zone (11), an oil-agent contact zone (12), a reaction zone (13), a product quenching zone (14), a reaction outlet zone (15), an oil-agent separation zone (17) and a stripping zone (16); A quick separation device (107) is provided between the product quenching zone (14) and the reaction outlet zone (15), and the oil agent separation zone (17) is provided with a first two-stage cyclone separator (108); the outlet of the product quenching zone (14) is communicated with the quick separation oil agent inlet (301) of the quick separation device (107), the quick separation catalyst outlet (302) of the quick separation device (107) is communicated with the catalyst inlet of the stripping zone (16), and the quick separation oil and gas outlet (303) of the quick separation device (107) is communicated with the inlet of the reaction outlet zone (15); the outlet of the reaction outlet zone (15) is communicated with the inlet of the first two-stage cyclone separator (108); The catalyst outlet of the first two-stage cyclone separator (108) is connected to the catalyst inlet of the stripping zone (16), and the oil and gas outlet of the first two-stage cyclone separator (108) is connected to the reaction oil and gas outlet (110); The catalyst outlet of the stripping zone (16) is communicated with the catalyst inlet to be regenerated of the regeneration unit, and the regenerated catalyst outlet of the regeneration unit is communicated with the catalyst inlet of the oil contact zone (12).

2. The alkane catalytic dehydrogenation to olefins device according to claim 1, wherein: The ratio of the diameter to the height of the product quenching zone (14) is 1:(1-3), preferably 1:(1-1.5); The product quenching zone (14) is provided with a heat exchange coil (18), and the heat exchange coil (18) includes a plurality of annular tubes connected end to end; a quenching medium inlet is provided on one side of the top of the heat exchange coil (18), and a quenching medium outlet is provided on one side of the bottom of the heat exchange coil.

3. The alkane catalytic dehydrogenation to olefins device according to claim 1 or 2, wherein: The quick separation device (107) is selected from a combination of one or more of a cyclone quick separator, a three-leaf quick separator, a catapult quick separator, a U-shaped tube separator, a wall-cutting quick separator and a cantilever quick separator, and is preferably a cyclone quick separator.

4. The alkane catalytic dehydrogenation to olefins device according to claim 3, wherein: The quick separation device (107) comprises a variable diameter section and a constant diameter section which are connected to each other, the constant diameter section being connected to the downstream end of the variable diameter section, and the diameter of the variable diameter section gradually increasing from upstream to downstream; the quick separation oil agent inlet (301) is opened at the upper side of the constant diameter section, the quick separation catalyst outlet (302) is located at the bottom of the variable diameter section, and the quick separation oil and gas outlet (303) is located at the top of the constant diameter section; or, The quick separation device (107) comprises an external structure and an internal structure, wherein the external structure comprises an external constant diameter section, an external variable diameter section and an external outlet constant diameter section which are connected in sequence, wherein the diameter of the external variable diameter section gradually decreases from upstream to downstream; and the internal structure comprises a constant diameter separation section which is sleeved inside the external constant diameter section, wherein the quick separation oil agent inlet (301) is located at the bottom of the constant diameter separation section, the quick separation catalyst outlet (302) is opened at the upper side of the constant diameter separation section, and the quick separation oil and gas outlet (303) is located at the top of the external outlet constant diameter section.

5. The alkane catalytic dehydrogenation to olefins device according to claim 1, wherein: The oil contact zone (12) is provided with an alkane feed distributor (103) and a catalyst feed distributor (104), and the regenerated catalyst outlet of the regeneration unit is connected to the catalyst feed distributor (104); The pre-lifting zone (11) is provided with a pre-lifting gas pipe (101), and the stripping zone (16) is provided with a stripping gas inlet (111).

6. The alkane catalytic dehydrogenation to olefins device according to claim 1, wherein: The regeneration unit includes a regeneration heating zone (21) and a regeneration zone (22); The regeneration and heating zone (21) is located inside or outside the regeneration zone (22), and the regeneration and heating zone (21) is provided with a fuel pipe (201) for introducing fuel, and the heat outlet of the regeneration and heating zone (21) is connected to the regeneration zone (22) via the fuel heating pipe (202); The inlet of the catalyst to be regenerated of the regeneration unit is communicated with the regeneration zone (22), the regeneration zone (22) is provided with an oxygen-containing gas inlet (208), the catalyst outlet of the regeneration zone (22) is communicated with the inlet of the second two-stage cyclone separator (205); the catalyst outlet of the second two-stage cyclone separator (205) is communicated with the regenerated catalyst outlet of the regeneration unit (2), the flue gas outlet of the second two-stage cyclone separator (205) is communicated with the inlet of the regeneration gas collecting chamber (206), and the regeneration gas collecting chamber (206) is provided with a regeneration flue gas outlet (207).

7. The alkane catalytic dehydrogenation to olefins device according to claim 5, wherein: The catalyst outlet of the stripping zone (16) is connected to the catalyst inlet of the regeneration unit via a catalyst delivery pipe (105), and a regeneration slide valve (106) is provided on the catalyst delivery pipe (105); the regenerated catalyst outlet of the regeneration unit is connected to the catalyst feed distributor (104) of the oil contact zone (12) via a regenerated catalyst delivery pipe (203), and a regeneration slide valve (204) is provided on the regenerated catalyst delivery pipe (203); The oil and gas outlet of the first two-stage cyclone separator (108) is communicated with the inlet of the gas collecting chamber (109), and the outlet of the gas collecting chamber (109) is communicated with the reaction oil and gas outlet (110).

8. A method for catalytic dehydrogenation of alkanes to olefins by quenching and rapidly separating an oil agent, wherein: The method is implemented based on the alkane catalytic dehydrogenation to olefin production device according to any one of claims 1 to 7. The alkane raw material and the catalyst react in the reaction zone (13), and the oil mixture obtained enters the product quenching zone (14) for cooling. After cooling, the oil mixture enters the quick separation device (107) for separation. The separated catalyst enters the stripping zone (16) for stripping. The separated oil and gas enter the oil separation zone (17) after passing through the reaction outlet zone (15).

9. The method according to claim 8, wherein: The temperature of the product quenching zone (14) is 200-550°C, preferably 250-500°C; The quenching medium entering the heat exchange coil through the quenching medium inlet is selected from one or more of quenching oil, quenching water, quenching gas and alkane feedstock, preferably one or more of alkane feedstock.

10. The method according to claim 8, wherein: The linear velocity of the oil agent at the quick separation oil agent inlet (301) of the quick separation device (107) is 2 to 20 m / s, preferably 5 to 18 m / s; the linear velocity of the oil and gas at the quick separation oil and gas outlet (303) of the quick separation device (107) is 2 to 15 m / s, preferably 5 to 10 m / s.

11. The method according to claim 8, wherein: The conditions of the oil contact zone (12) include: The temperature is 500-700°C, preferably 520-680°C, and the catalyst density is 100-500 kg / m 3 , preferably 150~400kg / m 3 The residence time of the alkane feedstock and the catalyst in the oil contact zone is 0.05 to 0.5 s, preferably 0.1 to 0.3 s; The conditions in the reaction zone (13) include: The temperature at the bottom of the reaction zone is 520-680°C, preferably 540-660°C, and the catalyst density is 150-400 kg / m 3 , preferably 200~350kg / m 3 , the pressure is 0.05-0.2MPa, preferably 0.05-0.15MPa; the temperature at the top of the reaction zone is 480-640℃, preferably 500-620℃, and the catalyst density is 30-200kg / m 3 , preferably 50 to 150 kg / m 3 , the pressure is 0.05-0.15 MPa, preferably 0.05-0.12 MPa; The alkane raw material is selected from C2 to C8 alkanes.

12. The method according to claim 8, wherein: The conditions of the regeneration unit include: The regeneration temperature is 600-720°C, preferably 620-700°C, and the catalyst density is 50-500 kg / m 3 , preferably 100~400kg / m 3 , the pressure is 0.05-0.2MPa, preferably 0.05-0.15MPa; The fuel introduced into the regeneration and heating zone (21) through the fuel pipe (201) includes one or more of methane, ethane, dry gas, liquefied gas and fuel oil, preferably dry gas generated by the device.

13. The method according to claim 8, wherein: The catalyst includes an active component and a carrier; The active component is selected from one or more metals or oxides of Zn, Fe, Co, Ni, V, Sn and Mg, and the carrier is selected from one or more of Al2O3, SiO2, ZrO2, TiO2 and molecular sieves; Based on the weight of the catalyst, the content of the active component is 10-90%, and the content of the carrier is 10-90%; preferably, the content of the active component is 20-70%, and the content of the carrier is 30-80%.

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