WO2021036098A1 - 一种涉及催化剂再生及反应器双在线切换的丙烷脱氢工艺 - Google Patents

一种涉及催化剂再生及反应器双在线切换的丙烷脱氢工艺 Download PDF

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WO2021036098A1
WO2021036098A1 PCT/CN2019/124940 CN2019124940W WO2021036098A1 WO 2021036098 A1 WO2021036098 A1 WO 2021036098A1 CN 2019124940 W CN2019124940 W CN 2019124940W WO 2021036098 A1 WO2021036098 A1 WO 2021036098A1
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reactor
catalyst
standby
gas
catalyst regeneration
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PCT/CN2019/124940
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French (fr)
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高军
杨卫东
田俊凯
范凌达
陆朝阳
范昌海
寇亮
周轶
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浙江卫星能源有限公司
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
    • C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
    • C07C5/333—Catalytic processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J38/00—Regeneration or reactivation of catalysts, in general
    • B01J38/02—Heat treatment
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts

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  • the invention relates to the field of propane dehydrogenation production to propylene, and in particular to a propane dehydrogenation process involving catalyst regeneration and dual on-line switching of reactors
  • the main difference between the above two processes is mainly in the catalyst.
  • the fixed bed in the Lummus process uses a chromium-based catalyst, which is poisonous, and it is difficult to treat the catalyst after it is scrapped.
  • the UOP process uses platinum-based catalysts, which are non-toxic, have good thermal stability, and low investment, which is why it currently occupies a relatively large domestic market share.
  • UOP process Propane is mixed with a certain proportion of hydrogen and then passes through the first reactor, the second reactor, the third reactor and the fourth reactor in sequence to obtain products, and then enters the subsequent separation system.
  • the flow direction of the catalyst is the same as that of the raw material.
  • the regenerated catalyst enters the first reactor, the second reactor, the third reactor and the fourth reactor successively, and then carries out catalyst elutriation, enters the regeneration tower, the catalyst is regenerated, and the regenerated catalyst Enter the reactor to participate in the reaction.
  • the process gas has the highest olefin content after reacting in the first three reactors. At this time, the catalyst has the highest carbon content and the lowest catalyst activity. When the high olefin content meets the lowest catalyst activity, the reaction can only be carried out by increasing the reaction temperature. High temperature can easily lead to carbon deposits, so the fourth reactor has the shortest online time in the traditional UOP design process, which seriously affects the production capacity.
  • the purpose of the present invention is to provide a propane dehydrogenation process involving catalyst regeneration and dual on-line switching of the reactor, which solves the problems of short reactor operation period, frequent maintenance and the like, and has the characteristics of saving cost, increasing output, increasing operation period and the like.
  • a propane dehydrogenation process involving catalyst regeneration and dual on-line switching of reactors which includes: raw materials undergo heat exchange with product gas through a heat exchanger, and then are heated by a heating furnace and then sequentially enter a multi-stage reactor; each stage of the reactor Equipped with an intermediate heating furnace, the process gas is heated to the reaction temperature by the heating furnace, and then enters the next stage reactor.
  • the product gas flowing out of the last stage reactor exchanges heat with the raw materials, and then is cooled, and then sent to the next stage through the compressor
  • the separation system separates and obtains the final product.
  • the last stage reactor is equipped with two reactors, which are divided into the formation of switchable one-use one-standby reactor and standby reactor modes. The two reactors can be switched freely;
  • the catalyst to be regenerated containing carbon deposits is burned through the catalyst regeneration tower to remove the carbon deposits to obtain a regenerated catalyst.
  • the regenerated catalyst is lifted into the first-stage reactor by the heated lifting gas, and then passes through the reactors of various stages for reaction, and finally
  • the catalyst to be regenerated containing carbon deposits after the completion of the reaction in the primary reactor is collected by the catalyst collector, then enters the lock hopper for elutriation, and then enters the catalyst regeneration tower for coking after elutriation, thereby achieving continuous catalyst regeneration .
  • the gas filled into the reactor is nitrogen.
  • the gas used in the replacement of the gas environment in the standby reactor is dry gas, replaced to a content of oxygen+nitrogen less than 5%, preferably 2%, and the replaced gas is discharged into the wet torch system.
  • dry gas is used to pressurize the standby reactor until the pressure in the operating reactor is reached.
  • the standby reactor is preheated by a heater, and the preheating rate is 20-30° C./h, until the temperature in the operating reactor is reached.
  • the raw material exchanges heat with the product gas through the heat exchanger, and then enters the multi-stage reactor after being heated by the heating furnace; each reactor is equipped with an intermediate heating furnace, and the process gas is heated to the reaction temperature by the heating furnace and then enters the next In the first stage reactor, the product gas from the last stage reactor exchanges heat with the raw materials, and then is cooled, and then sent to the separation system through a compressor for separation to obtain the final product.
  • the last stage reactor is equipped with two reactors. It is divided into the formation of a switchable one-use one-standby reactor and a standby reactor mode. The two reactors can be switched freely.
  • the operating reactor in the final stage reactor has a significant increase in the pressure difference between the internal and external networks, and the reaction temperature continues to decrease, which makes the operating state of the operating reactor poor. At this time, it is necessary to connect the operating reactor to The standby reactor is switched to realize the efficient operation of the device.
  • the reactor Before the standby reactor needs to be switched to the operating reactor, the reactor cannot be switched directly in the cold state, which will result in a large temperature difference and damage the internal components.
  • the pressure and temperature in the standby reactor need to be adjusted to make it compatible with the operating reactor. Switch after the same pressure and temperature.
  • the nitrogen in the spare reactor needs to be replaced with process gas.
  • Use dry gas to replace the nitrogen in the spare reactor first, and replace it until the volume ratio of oxygen + nitrogen content is less than 5%, preferably less than 2%, and the replaced gas is discharged Wet torch system. After the replacement is qualified, use dry gas to fill the standby reactor with the same pressure as the operating reactor, then open the outlet of the standby reactor and continue to fill with dry gas.
  • the temperature is controlled by the steam heater
  • the speed is heated at 20 ⁇ 30°C/h to 380 ⁇ 400°C, and then heated to the reaction temperature of 600 ⁇ 650°C by the heater, so that the temperature of the standby reactor is consistent with the temperature of the running reactor; then the process gas is switched through the hand valve To the spare reactor, close the hand valve at the inlet and outlet of the original operating reactor. This completes the switching of the standby reactor to the running state.
  • the dry gas enters the standby reactor through the steam heater, heater, flow meter, and valve. After opening the outlet of the standby reactor, the dry gas passing through the standby reactor enters the buffer tank and mixes with the product gas and enters the separation system.
  • the above-mentioned dry gas process is used to perform operations such as cooling and nitrogen replacement of the original operating reactor; after that, the original operating reactor is subjected to online maintenance and other operations without affecting the continuous online operation of the device.
  • the catalyst to be regenerated containing carbon deposits is burned through the catalyst regeneration tower to remove the carbon deposits to obtain a regenerated catalyst.
  • the regenerated catalyst is lifted into the first-stage reactor by the heated lifting gas, and then passes through the reactors of various stages for reaction, and finally
  • the catalyst to be regenerated containing carbon deposits after the completion of the reaction in the primary reactor is collected by the catalyst collector, then enters the lock hopper for elutriation, and then enters the catalyst regeneration tower for coking after elutriation, thereby achieving continuous catalyst regeneration .
  • the propane dehydrogenation process involving catalyst regeneration and dual on-line switching of the reactor can complete the on-line switching of the reactor under the premise of ensuring continuous catalyst regeneration, and avoid the long-period operation of the device due to the clogging of the last-stage reactor.
  • the frequency of equipment maintenance is reduced, so that the operation cycle of the equipment becomes longer, the output is increased, and the maintenance cost is reduced.
  • Fig. 1 is a flowchart of a catalyst cycle regeneration according to an embodiment of the present invention.
  • Fig. 2 is a flow chart of a catalytic hydrogen production process according to an embodiment of the present invention.
  • the propane dehydrogenation process involving catalyst regeneration and dual on-line switching of reactors according to the present invention includes the following steps:
  • Catalytic dehydrogenation The raw material exchanges heat from the heat exchanger E01A (E01B standby) with the product gas, and then is heated to the reaction temperature through the heating furnace H01, enters the reactor R1, and then is heated by the heating furnace H02, enters the reactor R2, and then It is heated by heating furnace H03 into reactor R3, and then heated by heating furnace H04A into reactor R4A (R4B standby).
  • the product gas from reactor R4A passes through buffer tank L and enters heat exchanger E01A (E01B standby). After the heat exchange, it passes through the water cooler E02A (E02B corresponds to the heat exchanger E01B), and then is sent to the separation system GS through the compressor for separation to obtain the final product propylene.
  • Reactor switching With the increase of the operating cycle, the operating reactor in the last-stage reactor has a significant increase in the pressure difference between the internal and external networks, and the reaction temperature continues to decrease, so that the operating state of the operating reactor is not good. The operating reactor and the standby reactor are switched to realize the efficient operation of the device.
  • the dry gas flow When the dry gas flow reaches a certain flow rate, it is heated by steam Reactor E03 controls the heating rate to be heated to 380°C at 20°C/h, and then heated to the reaction temperature of 650°C by heater H, so that the temperature of the standby reactor R4B is consistent with the temperature of the running reactor R4A; then the process gas is passed through the hand valve Switch to the backup reactor R4B, the dry gas passing through the backup reactor enters the buffer tank L and mixes with the product gas, and then enters the separation system GS. Close the hand valve at the inlet and outlet of the reactor R4A that was originally operating. This completes the switching of the standby reactor to the running state.
  • the above dry gas process is used to cool the original operating reactor R4A, nitrogen replacement and other operations; then the original operating reactor R4A is online maintenance and other operations, without affecting the continuous online operation of the device.
  • Catalyst regeneration After the reaction, the catalyst to be regenerated with carbon deposits passes through the catalyst regeneration tower V10 to burn coke to remove the carbon deposits.
  • the flow control hopper V11 controls the catalyst circulation rate, and then enters the locked hopper V12 in the nitrogen environment for cooling, and then regenerates after cooling.
  • the catalyst enters the lock hopper V14. In the lock hopper V14, the nitrogen environment is switched to the hydrogen environment.
  • the lift gas heated by the steam heater E02 is used to send the regenerated catalyst into the reactor R01, and the catalyst after the reactor R1 is in the catalyst
  • the catalyst collected in the catalyst collector V01 is sent to the reactor R02 using the lift gas heated by the steam heater E01, and the catalyst after participating in the reaction in the R02 is collected in the catalyst collector V03, and then the steam is used
  • the lift gas heated by the heater E01 sends the catalyst collected in the catalyst collector V03 to the reactor R03, the catalyst participating in the reaction in R03 is collected in the catalyst collector V04, and then the lift gas heated by the steam heater E01 is used to
  • the catalyst collected in the catalyst collector V04 is sent to the reactor R4A (R4B standby).
  • the catalyst to be regenerated after the reaction in the reactor R4A is collected in the catalyst collector V07 (V07B corresponds to R4B), and then the catalyst to be regenerated flows through the lock hopper V13A (V13B corresponds to R4B), where the hydrogen environment is converted to the nitrogen environment in the lock hopper V13A. Then the catalyst to be regenerated is sent to the catalyst collector V08 by the blower C01, and then enters the separation hopper V09.
  • the blower C02 is used for elutriation to remove excess dust, and finally to the catalyst regeneration tower V10 for regeneration, thereby realizing continuous catalyst regeneration.

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Abstract

一种涉及催化剂再生及反应器双在线切换的丙烷脱氢工艺，包括催化脱氢过程和催化剂再生过程；原料在换热器中与从最后一级反应器中流出的产品气进行换热，之后经过加热炉加热进入反应器，每一级反应器都配一个中间加热炉，工艺气经加热炉加热到反应温度进入到下一级反应器，其中最后一级反应器设置两台反应器，分为运行反应器和备用反应器，两台反应器可以进行自由切换，从最后一级反应器流出的产品气与原料进行换热，之后冷却，随后进入分离系统进行分离得到最终产物丙烯。从最后一级反应器参与完反应的待再生的催化剂通过催化剂收集器收集后进行淘析、烧焦获得再生后的催化剂，再生后的催化剂依次进入各级反应器参与反应，实现催化剂循环使用。

Description

一种涉及催化剂再生及反应器双在线切换的丙烷脱氢工艺 技术领域
本发明涉及丙烷脱氢生产制丙烯领域，具体涉及一种涉及催化剂再生及反应器双在线切换的丙烷脱氢工艺
背景技术
目前世界范围内丙烷脱氢制丙烯工艺主要有两种，分别是美国UOP工艺及美国Lummus两种工艺。
上述两种工艺的主要差别主要是在催化剂方面的不同。
Lummus工艺中固定床采用铬系催化剂，该铬系催化剂有毒，催化剂报废后处理难度大。
UOP工艺采用铂系催化剂，其无毒，热稳定性好，投资低，因此也是目前占据国内市场份额比较大的原因。
UOP工艺：丙烷与一定比例的氢气混合后依次经过第一反应器，第二反应器，第三反应器和第四反应器反应得到产品后，进入后续分离系统。催化剂的流动方向与原料一致再生后的催化剂依次进入第一反应器，第二反应器，第三反应器和第四反应器，然后进行催化剂淘析，进入再生塔，催化剂再生，再生后的催化剂进入反应器参与反应。工艺气经过前三个反应器反应后烯烃含量最高，此时催化剂上面含碳量最高催化剂活性最低，当烯烃含量高与催化剂活性最低相遇时，只能通过提高反应温度进行反应。高温容易导致积碳，所以在UOP传统设计工艺中第四反应器在线时间最短，严重影响到产能。
但是上述UOP工艺具有终端反应器容易堵塞，运行周期短等缺点。
发明内容
本发明的目的是提供一种涉及催化剂再生及反应器双在线切换的丙烷脱氢工艺，解决反应器运行周期短，检修频繁等问题，具有节约成本，提高产量，增长运行周期等特点。
为达到上述目的，本发明采取的技术方案是：
一种涉及催化剂再生及反应器双在线切换的丙烷脱氢工艺，其包括：原料通过换热器与产品气进行换热，随后经过加热炉加热后依次进入多级反应器；每一级反应器配一个中间加热炉，工艺气经加热炉加热到反应温度后进入到下一级反应器，从最后一级反应器流出的产品气与原料进行换热，之后再冷却，随后通过压缩机送往分离系统进行分离得到最终产物，其中最后一级反应器设置两台反应器，分为形成可切换的一用一备运行反应器和备用反应器模式，两台反应器可以自由切换；
当备用反应器需要切换为运行反应器之前，对备用反应器内的压力、温度进行调整，使之与运行反应器内的压力、温度相同后再进行切换；
含有积碳的待再生催化剂经过催化剂再生塔进行烧焦去除积碳，得到再生催化剂，再生催化剂利用加热后的提升气提升进入第一级反应器，随后依次经过各级反应器进行反应，到最后一级反应器中参与反应完成之后的含有积碳的待再生催化剂经过催化剂收集器进行收集，随后进入闭锁料斗中进行淘析，淘析之后进入催化剂再生塔进行烧焦，从而实现催化剂的连续再生。
优选的，备用反应器在备用状态下反应器内部充入的气体为氮气。
优选的，对备用反应器中气体环境进行置换时使用的气体为干气，置换到氧气+氮气含量＜5％，优选2％，置换出的气体排入湿火炬系统。
优选的，在进行切换前，利用干气对备用反应器进行充压，直至达到运行反应器内的压力。
优选的，在进行切换前，通过加热器对备用反应器进行预热，预热升温速度为20～30℃/h，直至达到运行反应器内的温度。
在本发明所述涉及催化剂再生及反应器双在线切换的丙烷脱氢工艺中：
原料通过换热器与产品气进行换热，随后经过加热炉加热后依次进入多级反应器；每一级反应器配一个中间加热炉，工艺气经加热炉加热到反应温度后进入到下一级反应器，从最后一级反应器流出的产品气与原料进行换热，之后再冷却，随后通过压缩机送往分离系统进行分离得到最终产物，其中最后一级反应器设置两台反应器，分为形成可切换的一用一备运 行反应器和备用反应器模式，两台反应器可以自由切换。
随着运行周期的增加，最后一级反应器中的运行反应器由于内外网压差大幅增加，反应温度持续降低，从而使运行反应器的运行状态不佳，这时就需要把运行反应器与备用反应器进行切换，实现装置的高效运行。
当备用反应器需要切换为运行反应器之前，反应器不能冷态直接切换，会导致温差太大，损伤内部件，需要对备用反应器内的压力、温度进行调整，使之与运行反应器内的压力、温度相同后再进行切换。首先备用反应器中的氮气需要置换为工艺气，利用干气先对备用反应器中的氮气进行置换，置换到氧气+氮气含量体积比＜5％，优选2％以下，置换出来的气体排入湿火炬系统。置换合格后，利用干气把备用反应器与运行反应器压力充成一样后，把备用反应器的出口打开，继续充入干气，当干气流量到达一定流量之后，通过蒸汽加热器控制升温速度在20～30℃/h加热到380～400℃，之后经过加热器加热到反应温度600～650℃，使备用反应器的温度与运行反应器的温度一致；然后把工艺气经过手阀切换到备用反应器，把原运行的反应器出入口手阀关闭。这样就完成了备用反应器到运行状态的切换。
干气经过蒸汽加热器，加热器，流量计，阀进入备用反应器，打开备用反应器的出口之后，经过备用反应器的干气进入缓冲罐与产品气混合后进入分离系统。
原运行反应器停止运行之后利用上述干气流程，对原运行的反应器进行降温，氮气置换等操作；之后对原运行反应器进行在线检修等作业，不影响装置的连续在线运行。
含有积碳的待再生催化剂经过催化剂再生塔进行烧焦去除积碳，得到再生催化剂，再生催化剂利用加热后的提升气提升进入第一级反应器，随后依次经过各级反应器进行反应，到最后一级反应器中参与反应完成之后的含有积碳的待再生催化剂经过催化剂收集器进行收集，随后进入闭锁料斗中进行淘析，淘析之后进入催化剂再生塔进行烧焦，从而实现催化剂的连续再生。
与现有技术相比，本发明的优点在于：
本发明所述涉及催化剂再生及反应器双在线切换的丙烷脱氢工艺，在 保证催化剂连续再生的前提下，完成反应器的在线切换，避免因最后一级反应器堵塞问题影响装置长周期运行，降低了装置检修的次数，从而使装置的运行周期变长，提高产量，降低检修费用。
附图说明
图1为本发明实施例的催化剂循环再生流程图。
图2为本发明实施例的催化制氢工艺流程图。
具体实施方式
参见图1，本发明所述涉及催化剂再生及反应器双在线切换的丙烷脱氢工艺，其包括以下步骤：
催化脱氢：原料从换热器E01A(E01B备用)与产品气进行换热，随后经过加热炉H01加热到反应温度，进入反应器R1，然后通过加热炉H02加热，进入反应器R2，并再通过加热炉H03加热进入反应器R3，再后来经过加热炉H04A加热进入反应器R4A(R4B备用)，从反应器R4A出来的产品气经过缓冲罐L进入换热器E01A(E01B备用)，与原料进行换热之后经过水冷却器E02A(E02B对应换热器E01B)，之后通过压缩机送往分离系统GS进行分离得到最终产物丙烯。
反应器切换：随着运行周期的增加，最后一级反应器中的运行反应器由于内外网压差大幅增加，反应温度持续降低，从而使运行反应器的运行状态不佳，这时就需要把运行反应器与备用反应器进行切换，实现装置的高效运行。
首先利用干气经过蒸汽加热器E03，加热器H，流量计FI，阀V1B，V2B，V3B，V4B，V5B(R4A为备用反应器时对应阀V1A，V2A，V3A，V4A，V5A)进入备用R4B，先对备用反应器R4B中的氮气进行置换，置换到氧气+氮气含量体积比＜1.5％，置换出来的气体排入湿火炬系统WF。置换合格后，利用干气把备用反应器R4B与运行反应器R4A压力充成一样后，把备用反应器R4B的出口打开，继续充入干气，当干气流量到达一定流量之后，通过蒸汽加热器E03控制升温速度在20℃/h加热到380℃，之后经过加热器H加热到反应温度650℃，使备用反应器R4B的温度与运 行反应器R4A的温度一致；然后把工艺气经过手阀切换到备用反应器R4B，经过备用反应器的干气进入缓冲罐L与产品气混合后进入分离系统GS。把原运行的反应器R4A出入口手阀关闭。这样就完成了备用反应器到运行状态的切换。
原运行反应器R4A停止运行之后利用上述干气流程，对原运行的反应器R4A进行降温，氮气置换等操作；之后对原运行反应器R4A进行在线检修等作业，不影响装置的连续在线运行。
催化剂再生：反应后带有积碳的待再生催化剂经过催化剂再生塔V10进行烧焦去除积碳，通过流量控制料斗V11控制催化剂循环速率，之后进入氮气环境的闭锁料斗V12进行降温，降温之后再生后的催化剂进入闭锁料斗V14中，在闭锁料斗V14中将氮气环境切换成氢气环境，利用蒸汽加热器E02加热过的提升气将再生后的催化剂送入反应器R01，经过反应器R1的催化剂在催化剂收集器V01中收集，随后利用蒸汽加热器E01加热过的提升气将催化剂收集器V01中收集催化剂送入反应器R02，在R02中参与反应后的催化剂在催化剂收集器V03中收集，随后利用蒸汽加热器E01加热过的提升气将催化剂收集器V03中收集催化剂送入反应器R03，在R03中参与反应后的催化剂在催化剂收集器V04中收集，随后利用蒸汽加热器E01加热过的提升气将催化剂收集器V04中收集催化剂送入最终到反应器R4A(R4B备用)中。经过反应器R4A反应后的待再生催化剂收集在催化剂收集器V07(V07B对应R4B)中，然后待再生催化剂流经闭锁料斗V13A(V13B对应R4B)，在闭锁料斗V13A中氢气环境转换成氮气环境，然后利用风机C01将待再生的催化剂送往催化剂收集器V08，后进入到分离料斗V09中利用风机C02进行淘析，去除多余粉尘，最后去往催化剂再生塔V10进行再生，从而实现催化剂连续再生。

Claims (5)

  1. 一种涉及催化剂再生及反应器双在线切换的丙烷脱氢工艺，其特征是，包括：
    原料通过换热器与产品气进行换热，随后经过加热炉加热后依次进入多级反应器；每一级反应器配一个中间加热炉，工艺气经加热炉加热到反应温度后进入到下一级反应器，从最后一级反应器流出的产品气与原料进行换热，之后再冷却，随后通过压缩机送往分离系统进行分离得到最终产物，其中最后一级反应器设置两台反应器，分为形成可切换的一用一备运行反应器和备用反应器模式，两台反应器可以自由切换；
    当备用反应器需要切换为运行反应器之前，对备用反应器内的压力、温度进行调整，使之与运行反应器内的压力、温度相同后再进行切换；
    含有积碳的待再生催化剂经过催化剂再生塔进行烧焦去除积碳，得到再生催化剂，再生催化剂利用加热后的提升气提升进入第一级反应器，随后依次经过各级反应器进行反应，到最后一级反应器中参与反应完成之后的含有积碳的待再生催化剂经过催化剂收集器进行收集，随后进入闭锁料斗中进行淘析，淘析之后进入催化剂再生塔进行烧焦，从而实现催化剂的连续再生。
  2. 如权利要求1所述的涉及催化剂再生及反应器双在线切换的丙烷脱氢工艺，其特征是，备用反应器在备用状态下反应器内部充入的气体为氮气。
  3. 如权利要求1所述的涉及催化剂再生及反应器双在线切换的丙烷脱氢工艺，其特征是，对备用反应器中气体环境进行置换时使用的气体为干气，置换到氧气+氮气含量体积比＜5％，优选为2％，置换出的气体排入湿火炬系统。
  4. 如权利要求3所述的涉及催化剂再生及反应器双在线切换的丙烷脱氢工艺，其特征是，对备用反应器中气体环境进行置换完成之后，利用干气继续对备用反应器进行充压，直至达到运行反应器内的压力。
  5. 如权利要求3所述的涉及催化剂再生及反应器双在线切换的丙烷脱氢 工艺，其特征是，对备用反应器中气体环境进行置换完成之后，通过加热器对干气进行加热，使备用反应器进行预热，预热升温速度为20～30℃/h，直至达到运行反应器内的温度。
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