CN111282602A - Method and system for oxidizing and regenerating catalyst - Google Patents
Method and system for oxidizing and regenerating catalyst Download PDFInfo
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- CN111282602A CN111282602A CN201811505423.3A CN201811505423A CN111282602A CN 111282602 A CN111282602 A CN 111282602A CN 201811505423 A CN201811505423 A CN 201811505423A CN 111282602 A CN111282602 A CN 111282602A
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- 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
- B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
- B01J38/12—Treating with free oxygen-containing gas
- B01J38/30—Treating with free oxygen-containing gas in gaseous suspension, e.g. fluidised bed
- B01J38/32—Indirectly heating or cooling material within regeneration zone or prior to entry into regeneration zone
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- 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
- B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
- B01J38/12—Treating with free oxygen-containing gas
- B01J38/14—Treating with free oxygen-containing gas with control of oxygen content in oxidation gas
Abstract
The present disclosure relates to a method and system for oxidative regeneration of a catalyst. The method comprises the following steps: under the condition of oxidation regeneration, the spent catalyst is in contact with preheated oxygen-containing gas in a regenerator for regeneration, and heat is released to obtain high-temperature regeneration flue gas and a high-temperature regeneration catalyst; a first heat taking pipe is arranged in the regenerator; enabling the liquid heat exchange medium to enter a first heat taking pipe for heat taking to obtain a gas-liquid mixed medium, and enabling the gas-liquid mixed medium to be subjected to gas-liquid separation to obtain a heat exchange medium condensate and a gaseous heat exchange medium; and the high-temperature gaseous heat exchange medium is subjected to heat exchange with the regeneration flue gas to obtain a high-temperature gaseous heat exchange medium, and the high-temperature gaseous heat exchange medium is subjected to heat exchange with the oxygen-containing gas to obtain a preheated oxygen-containing gas. The catalyst oxidation regeneration method and the catalyst oxidation regeneration system can fully utilize the heat release of the catalyst oxidation regeneration reaction in the regenerator and the heat energy of each temperature position in the system to preheat the oxygen-containing gas and generate superheated steam to supply to other devices, thereby realizing energy conservation and consumption reduction in the regeneration process.
Description
Technical Field
The disclosure relates to the technical field of oil refining and chemical engineering, in particular to a method and a system for oxidizing and regenerating a catalyst.
Background
In the technical fields of oil refining and chemical industry, the condition of catalyst deactivation generally exists. In order to achieve catalyst regeneration without shutdown, cyclic oxidation regeneration is generally employed. In the regenerator, air is used as an oxidant to perform oxidation reaction with carbon deposit on the catalyst, so that the activity of the catalyst is recovered. The oxidation regeneration of the catalyst is a heat release process, and in order to maintain a proper temperature, the existing catalyst regeneration device generally adopts boiler feed water to take out excess heat in a regeneration bed layer, and the excess heat is directly sent out of the device after generating steam. Or, the flue gas is subjected to waste heat recovery, and the steam is generated and then sent out of the device. These methods are not reasonable in terms of energy use from the viewpoint of the whole system, and thus are insufficient in utilization of heat generated by the oxidation regeneration.
Disclosure of Invention
The invention aims to provide a method and a system for oxidizing and regenerating a catalyst, which can improve the utilization rate of the heat generated by oxidizing and regenerating the catalyst and meet the requirements of large-scale industrial devices on energy conservation and consumption reduction.
In order to achieve the above object, a first aspect of the present disclosure provides a method for oxidative regeneration of a catalyst, the method comprising the steps of:
under the condition of oxidation regeneration, the spent catalyst is in contact with preheated oxygen-containing gas in a regenerator for regeneration, and heat is released to obtain high-temperature regeneration flue gas and a high-temperature regeneration catalyst; a first heat taking pipe is arranged in the regenerator;
enabling the liquid heat exchange medium to enter the first heat taking pipe for heat taking to obtain a gas-liquid mixed medium, and enabling the gas-liquid mixed medium to be subjected to gas-liquid separation to obtain a heat exchange medium condensate and a gaseous heat exchange medium;
and exchanging heat between the gaseous heat exchange medium and the high-temperature regeneration flue gas to obtain a high-temperature gaseous heat exchange medium, and exchanging heat between the high-temperature gaseous heat exchange medium and an oxygen-containing gas to obtain the preheated oxygen-containing gas.
Optionally, the oxidative regeneration conditions comprise: the temperature is 470-680 ℃; the volume content of oxygen in the oxygen-containing gas is 5-25%.
Optionally, the liquid heat exchange medium is water; in the gas-liquid mixed medium, the mass ratio of the heat exchange medium condensate to the gaseous heat exchange medium is (5-18): 1.
optionally, the temperature of the liquid heat exchange medium is 100-120 ℃; the temperature of the gas-liquid mixed medium is 150-160 ℃, the temperature of the high-temperature gaseous heat exchange medium is 390-420 ℃, and the temperature of the preheated oxygen-containing gas is 220-280 ℃.
Optionally, the method further includes that the high-temperature regenerated catalyst enters a regenerator receiver, a second heat taking pipe is arranged in the regenerator receiver, and the gaseous heat exchange medium enters the second heat taking pipe to exchange heat with the high-temperature regenerated catalyst and then exchanges heat with the high-temperature regenerated flue gas, so that the high-temperature gaseous heat exchange medium is obtained.
Optionally, the method further includes arranging a third heat extraction pipe in the regenerator, so that the gaseous heat exchange medium enters the third heat extraction pipe to extract heat and then exchanges heat with the high-temperature regeneration flue gas, thereby obtaining the high-temperature gaseous heat exchange medium.
Optionally, the method further comprises heating the oxygen-containing gas with a heater during cold start-up to initiate the regeneration reaction.
The second aspect of the present disclosure provides a system for oxidation regeneration of a catalyst, which includes an oxygen-containing gas inlet, a heat exchange medium inlet, a regenerator, a gas-liquid separator, a regeneration flue gas cooler, an oxygen-containing gas preheater, a flue gas outlet, and a gaseous heat exchange medium outlet; the oxygen-containing gas inlet, the oxygen-containing gas preheater and the regenerator are communicated in sequence;
the regenerator comprises a regeneration reaction zone, a first heat taking pipe is arranged in the regeneration reaction zone, the inlet of the first heat taking pipe is communicated with the heat exchange medium inlet, the outlet of the first heat taking pipe is communicated with the inlet of the gas-liquid separator, the gas outlet of the gas-liquid separator is communicated with the gaseous heat exchange medium inlet of the regeneration flue gas cooler, the liquid outlet of the gas-liquid separator is communicated with the heat exchange medium inlet, the gaseous heat exchange medium outlet of the regeneration flue gas cooler is communicated with the heat medium inlet of the oxygen-containing gas preheater, the flue gas outlet of the regenerator is communicated with the hot medium inlet of the regeneration flue gas cooler, the hot medium outlet of the regeneration flue gas cooler is communicated with the flue gas outlet, the heat medium outlet of the oxygen-containing gas preheater is communicated with the gaseous heat exchange medium outlet of the system.
Optionally, the system further comprises a regenerator receiver, a regenerant inlet of the regenerator receiver is communicated with a regenerant outlet of the regenerator, a second heat extraction pipe is arranged in the regenerator receiver, an inlet of the second heat extraction pipe is communicated with a gas outlet of the gas-liquid separator, and an outlet of the second heat extraction pipe is communicated with a gaseous heat exchange medium inlet of the regeneration flue gas cooler; and/or
The system also includes an oxygen-containing gas electric heater disposed between the oxygen-containing gas preheater and the regenerator.
Optionally, the first heat taking pipe is arranged at the lower part of the regeneration reaction zone, a third heat taking pipe is further arranged at the upper part of the regeneration reaction zone, an inlet of the third heat taking pipe is communicated with a gas outlet of the gas-liquid separator, and an outlet of the third heat taking pipe is communicated with a gaseous heat exchange medium inlet of the regeneration flue gas cooler.
Optionally, the regenerator is a fluidized bed regenerator, a regeneration flue gas outlet, a cyclone separator and a fluidized regeneration reaction zone are sequentially arranged in the fluidized bed regenerator from top to bottom, and the first heat taking pipe is arranged in the fluidized regeneration reaction zone; the first heat taking pipe is a U-shaped coil pipe, a coiled pipe, a vertical heat exchange pipe or a horizontal heat exchange pipe, or a combination of two or three or four of the U-shaped coil pipe, the coiled pipe, the vertical heat exchange pipe and the horizontal heat exchange pipe.
According to the technical scheme, the catalyst oxidation regeneration method and the catalyst oxidation regeneration system enable a liquid heat exchange medium to enter the regenerator for heat extraction to generate heat exchange medium steam, further improve the steam temperature by utilizing the heat exchange of the heat exchange medium steam and regeneration flue gas to obtain high-temperature heat exchange medium steam, the high-temperature steam can be preheated for oxygen-containing gas in the regeneration process, and by designing the generation, overheating, heat exchange and condensate circulation processes and devices of the heat exchange medium steam, the heat generated in the catalyst oxidation regeneration reaction in the regenerator and the heat energy of each temperature position in the system including the heat of the regeneration flue gas can be fully utilized, the superheated steam is generated and supplied to other devices on the premise of maintaining the temperature of a bed layer in the regenerator, the oxygen-containing gas is preheated, the energy of the catalyst oxidation regeneration is fully and effectively utilized, and the energy conservation and consumption reduction of the regeneration process.
Additional features and advantages of the disclosure will be set forth in the detailed description which follows.
Drawings
The accompanying drawings, which are included to provide a further understanding of the disclosure and are incorporated in and constitute a part of this specification, illustrate embodiments of the disclosure and together with the description serve to explain the disclosure without limiting the disclosure. In the drawings:
FIG. 1 is a process flow diagram of a method for oxidative regeneration of a catalyst according to one embodiment of the present disclosure;
FIG. 2 is a process flow diagram of a method for oxidative regeneration of a catalyst according to another embodiment of the present disclosure;
FIG. 3 is a process flow diagram of a method for oxidative regeneration of a catalyst according to a third embodiment of the present disclosure.
Description of the reference numerals
1-a regenerator; 2-a first heat-taking pipe; 3-a cyclone separator; 4-regeneration flue gas cooler; 5-a gas-liquid separator; 6-medium circulating pump; 7-an oxygen-containing gas preheater; 8-an electric heater containing oxygen gas; 9-a regenerator receiver; 10-a third heat taking pipe; 11-a second heat-taking pipe; a-regenerating flue gas; b-a liquid heat exchange medium; c-an oxygen-containing gas; d-a gaseous heat exchange medium; e-inert gas.
Detailed Description
The following detailed description of specific embodiments of the present disclosure is provided in connection with the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present disclosure, are given by way of illustration and explanation only, not limitation.
In the present disclosure, unless otherwise stated, the use of directional words such as "up" and "down" generally refers to the up and down of the device in normal use, and specifically refers to the orientation of the drawing in fig. 1. The "inner and outer" are with respect to the outline of the device itself.
The first aspect of the present disclosure provides a method for oxidative regeneration of a catalyst, comprising the steps of:
under the condition of oxidation regeneration, the spent catalyst is in contact with preheated oxygen-containing gas in a regenerator for regeneration, and heat is released to obtain high-temperature regeneration flue gas and a high-temperature regeneration catalyst; a first heat taking pipe is arranged in the regenerator;
enabling the liquid heat exchange medium to enter a first heat taking pipe for heat taking to obtain a gas-liquid mixed medium, and enabling the gas-liquid mixed medium to be subjected to gas-liquid separation to obtain a heat exchange medium condensate and a gaseous heat exchange medium;
and the high-temperature gaseous heat exchange medium is subjected to heat exchange with the high-temperature regeneration flue gas to obtain a high-temperature gaseous heat exchange medium, and the high-temperature gaseous heat exchange medium is subjected to heat exchange with the oxygen-containing gas to obtain the preheated oxygen-containing gas.
The disclosed catalyst oxidation regeneration method enables a liquid heat exchange medium to enter a regenerator for heat extraction to generate heat exchange medium steam, and utilizes the heat exchange of the heat exchange medium steam and regeneration flue gas to further improve the steam temperature to obtain high-temperature heat exchange medium steam which can be used for preheating oxygen-containing gas in the regeneration process.
In the process of the present disclosure, the conditions under which the oxidative regeneration is carried out in the regenerator may be conventional in the art, for example, in one embodiment, the oxidative regeneration conditions may include: the temperature is 470-680 ℃, preferably 500-530 ℃; the volume content of oxygen in the oxygen-containing gas can be 5-25%, preferably 10-21%; the oxygen-containing gas satisfying the above conditions is not particularly limited, and is preferably air.
In the process of the present disclosure, the catalyst entering and exiting the regenerator may be operated in a manner conventional in the art, for example, in one embodiment, the spent catalyst may be lifted into the regenerator by an inert gas, preferably from the upper middle portion of the regenerator; the high-temperature regenerated catalyst obtained by the regeneration reaction is preferably discharged from the lower part of the regenerator, so that the catalyst can form a fluidized bed layer in the regenerator, the contact with oxygen-containing gas is promoted, and the regeneration reaction efficiency is improved.
In the method disclosed by the disclosure, the heat exchange medium has no special requirement and can be conventional in the field, and preferably, the liquid heat exchange medium is water, so as to be convenient to obtain and obtain a better heat exchange effect; further, in the gas-liquid mixed medium, the mass ratio of the heat exchange medium condensate to the gaseous heat exchange medium can be (5-18): 1, preferably (8-16): 1, in the preferable mass ratio range of the heat exchange medium condensate to the gaseous heat exchange medium, the heat exchange medium can exchange heat in the regenerator more effectively so as to fully take out the exothermic heat of the oxidation regeneration reaction.
In the method disclosed by the disclosure, the temperature of the heat exchange medium before and after entering the first heat extraction pipe can be changed within a large range, and in order to improve the heat exchange efficiency and effect, in one embodiment, the temperature of the liquid heat exchange medium before entering the first heat extraction pipe of the regenerator for heat extraction can be 100-120 ℃, and is preferably 105-110 ℃; the temperature of the gas-liquid mixed medium obtained after heat extraction can be 150-160 ℃, and is preferably 153-157 ℃; the temperature of the high-temperature regeneration flue gas before and after heat exchange with the gaseous heat exchange medium can be changed in a large range, in one embodiment, in order to further increase the temperature of the high-temperature gaseous heat exchange medium, the temperature of the high-temperature gaseous heat exchange medium obtained after the high-temperature gaseous heat exchange medium is further heat exchanged with the high-temperature regeneration flue gas can be 390-420 ℃, preferably 395-405 ℃, and the temperature of the regeneration flue gas discharged out of the system after heat exchange can be 190-210 ℃, preferably 200-205 ℃; the temperature of the oxygen-containing gas before and after being preheated by the high-temperature heat exchange medium can also be changed in a large range, for example, in one embodiment, the oxygen-containing gas is air at normal temperature, and the temperature of the high-temperature gaseous heat exchange medium after being subjected to heat exchange with the oxygen-containing gas can be 220-240 ℃, preferably 225-235 ℃; the temperature of the preheated oxygen-containing gas obtained by heat exchange with the high-temperature gaseous heat exchange medium can be 220-280 ℃, and is preferably 245-265 ℃.
Further, in order to fully utilize the heat in the regeneration system, in an embodiment, the method may further include that the high-temperature regenerated catalyst obtained by the regeneration reaction enters a regenerator receiver, a second heat taking pipe may be disposed in the regenerator receiver, and a gaseous heat exchange medium enters the second heat taking pipe to exchange heat with the high-temperature regenerated catalyst and then exchanges heat with the high-temperature regenerated flue gas, so as to obtain the high-temperature gaseous heat exchange medium, so that the gaseous heat exchange medium may be further heated by using the heat in the high-temperature regenerated catalyst, so as to fully utilize the heat in the high-temperature regenerated catalyst, and the regenerator receiver is disposed to facilitate storage of the regenerated catalyst, and to adjust the flow stability of the regenerated catalyst to a subsequent process.
In another embodiment, a third heat extraction pipe may be disposed in the regenerator, and the method may further include allowing the gaseous heat exchange medium to enter the third heat extraction pipe of the regenerator to extract heat, and then exchanging heat with the high-temperature regeneration flue gas to obtain the high-temperature gaseous heat exchange medium. In this embodiment, the heat exchange medium enters the first heat extraction pipe of the regenerator to perform the first heat extraction, and the gas-liquid mixed medium after the heat extraction enters the third heat extraction pipe of the regenerator again to perform the second heat extraction after the gas-liquid separated gas-liquid mixed medium, so that the heat of the oxidation regeneration reaction can be further extracted, and the temperature of the high-temperature gas-state heat exchange medium can be increased.
Furthermore, the heat exchange medium condensate flowing out of the bottom of the gas-liquid separator can be returned to the heat exchange medium inlet for recycling, so that the consumption of the heat exchange medium is reduced.
In the process of the present disclosure, as shown in fig. 1, an oxygen-containing gas heater, for example, an oxygen-containing gas electric heater 8, may be provided between the oxygen-containing gas inlet and the regenerator 1 for heating the oxygen-containing gas from a cold start-up, starting the regeneration reaction and controlling the regeneration temperature, or for performing supplementary heating after the heat exchange between the oxygen-containing gas and the high-temperature gaseous heat exchange medium. In one embodiment, the flow rate of the superheated steam entering the oxygen-containing gas preheater 7 may be controlled according to the relationship between the heat release of the catalyst regeneration and the oxygen-containing gas required for the regeneration, and the superheated steam may be used as a by-product if the superheated steam is rich and may be replenished by the oxygen-containing gas electric heater 8 if the superheated steam is insufficient, while ensuring the preheating temperature of the oxygen-containing gas.
In the process of the present disclosure, the catalyst may be of a type conventional in the art, such as a clay-based catalyst, a molecular sieve catalyst, or a metal oxide-based catalyst, or a combination of two or three thereof.
As shown in fig. 1, the second aspect of the present disclosure provides a system for oxidative regeneration of a catalyst, which comprises an oxygen-containing gas inlet, a heat exchange medium inlet, a regenerator 1, a gas-liquid separator 5, a regeneration flue gas cooler 4, an oxygen-containing gas preheater 7, a flue gas outlet, and a gaseous heat exchange medium outlet; the oxygen-containing gas inlet, the oxygen-containing gas preheater 7 and the regenerator 1 are communicated in sequence;
the regenerator 1 comprises a regeneration reaction zone, a first heat taking pipe 2 is arranged in the regeneration reaction zone, an inlet of the first heat taking pipe 2 is communicated with a heat exchange medium inlet, an outlet of the first heat taking pipe 2 is communicated with an inlet of a gas-liquid separator 5, a gas outlet of the gas-liquid separator 5 is communicated with a gaseous heat exchange medium inlet of a regeneration flue gas cooler 4, a gaseous heat exchange medium outlet of the regeneration flue gas cooler 4 is communicated with a heat medium inlet of an oxygen-containing gas preheater 7, a flue gas outlet of the regenerator 1 is communicated with a heat medium inlet of the regeneration flue gas cooler 4, a heat medium outlet of the regeneration flue gas cooler 4 is communicated with a flue gas outlet, and a heat medium outlet of the oxygen-containing gas preheater 7 is communicated with a gaseous heat exchange medium outlet of.
The catalyst oxidation regeneration system disclosed by the invention can fully utilize heat released by the catalyst oxidation regeneration reaction in the regenerator and heat energy of each temperature position in the system including the heat of regenerated flue gas, generate superheated steam to supply to other devices on the premise of maintaining the temperature of the bed layer in the regenerator, preheat oxygen-containing gas, and realize energy conservation and consumption reduction in the regeneration process.
In order to further improve the heat utilization rate in the regeneration system, in a specific embodiment, as shown in fig. 2, the system may further include a regenerator receiver 9, a regenerant inlet of the regenerator receiver 9 may be communicated with a regenerant outlet of the regenerator 1, a second heat extraction pipe 11 may be disposed in the regenerator receiver 9, an inlet of the second heat extraction pipe 11 may be communicated with a gas outlet of the gas-liquid separator 5, and an outlet of the second heat extraction pipe 11 may be communicated with a gaseous heat exchange medium inlet of the regeneration flue gas cooler 4. In this embodiment, the heat exchange medium enters the first heat extraction pipe of the regenerator to perform the first heat extraction, and the gas-liquid mixed medium after the heat extraction enters the second heat extraction pipe of the regenerator receiver through the gas-liquid separated gaseous heat exchange medium to perform the second heat extraction, so that the heat in the high-temperature regenerated catalyst can be further extracted, and the temperature of the high-temperature gaseous heat exchange medium can be increased.
In another specific embodiment, as shown in fig. 3, the regeneration reaction zone may further be provided with a third heat extraction pipe 10, an inlet of the third heat extraction pipe 10 may be communicated with the gas outlet of the gas-liquid separator 5, and an outlet of the third heat extraction pipe 10 may be communicated with the gaseous heat exchange medium inlet of the regeneration flue gas cooler 4. In this embodiment, the heat exchange medium enters the first heat extraction pipe of the regenerator to perform the first heat extraction, and the gas-liquid mixed medium after the heat extraction enters the third heat extraction pipe of the regenerator again to perform the second heat extraction after the gas-liquid separated gas-liquid mixed medium, so that the heat of the oxidation regeneration reaction can be further extracted, and the temperature of the high-temperature gas-state heat exchange medium can be increased. The position of the third heat taking pipe has no special requirement, preferably, the first heat taking pipe can be arranged at the lower part of the regeneration reaction zone, and the third heat taking pipe can be arranged at the upper part of the regeneration reaction zone, so as to further improve the efficiency of extracting heat from the regeneration reaction zone.
According to the present disclosure, the regenerator may be of a type conventional in the art, and preferably, the regenerator 1 may be a fluidized bed regenerator, so as to sufficiently contact the spent catalyst with the oxygen-containing gas, thereby improving the oxidative regeneration efficiency of the catalyst; further, in a specific embodiment, as shown in fig. 1, a regeneration flue gas outlet, a cyclone separator 3 and a fluidized regeneration reaction zone may be sequentially disposed from top to bottom in the fluidized bed regenerator, and the first heat taking pipe 2 may be disposed in the fluidized regeneration reaction zone; in this embodiment, the oxygen-containing gas inlet may be disposed at the bottom of the fluidized bed regeneration reaction zone, the oxygen-containing gas may make the catalyst to be regenerated entering the regenerator in a fluidized state and perform contact reaction regeneration, the regenerated flue gas generated by regeneration flows upward to the cyclone separator 3 for gas-solid two-phase fluid separation, the catalyst solid particles contained in the regenerated flue gas may return to the fluidized bed regeneration reaction zone at the lower part of the regenerator through the cyclone separator dipleg, and the regenerated flue gas may be discharged from the top of the regenerator.
Further, the first heat taking pipe 2, the second heat taking pipe 11 and the third heat taking pipe 10 may be of a kind conventional in the art, and in order to further improve the heat exchange efficiency, preferably, the first heat taking pipe 2, the second heat taking pipe 11 and the third heat taking pipe 10 may be each independently a U-shaped coil, a serpentine pipe, a vertical heat exchange pipe or a horizontal heat exchange pipe, or a combination of two or three or four of them. The first heat extraction pipe 2, the second heat extraction pipe 11 and the third heat extraction pipe 10 can be independently provided with 1 group or a plurality of groups, preferably, 2-10 groups of first heat extraction pipes 2 can be arranged in the regenerator, 2-6 groups of second heat extraction pipes 11 can be arranged in the regenerator, and 2-6 groups of third heat extraction pipes 10 can be arranged in the regenerator receiver.
In accordance with the present disclosure, the gas-liquid separator may be of a type conventional in the art, such as a condensate drum; further, the liquid outlet of the gas-liquid separator can be communicated with the heat exchange medium inlet, so that the heat exchange medium condensate flowing out of the bottom of the gas-liquid separator returns to the heat exchange medium inlet for recycling, and the consumption of the heat exchange medium is reduced. The liquid outlet of the gas-liquid separator can be provided with a medium circulating pump, so that the flowing heat exchange medium condensate enters the first heat taking pipe for recycling after being boosted by the medium circulating pump.
In one embodiment according to the present disclosure, an oxygen-containing gas electric heater 8 may be provided between the oxygen-containing gas preheater 7 and the regenerator 1, as shown in fig. 1, for heating the oxygen-containing gas from a cold start-up process, initiating the regeneration reaction and controlling the regeneration temperature. In the embodiment, the flow rate of the superheated steam entering the oxygen-containing gas preheater 7 can be controlled according to the relationship between the heat release of the catalyst regeneration and the oxygen-containing gas required for the regeneration, and on the premise of ensuring the preheating temperature of the oxygen-containing gas, the superheated steam is used as a by-product if the superheated steam is surplus, and is replenished by the oxygen-containing gas electric heater 8 if the superheated steam is insufficient.
The present disclosure is further illustrated by the following examples, but is not to be construed as being limited thereby.
Example 1
As shown in the attached figure 1, a regeneration bed layer at the lower part of a fluidized bed regenerator 1 generates a catalytic oxidation regeneration reaction to release heat, and a high-temperature regenerated catalyst and high-temperature regenerated flue gas with the temperature of 500-530 ℃ are arranged in the regenerator.
A first heat taking pipe 2 is arranged in the fluidized bed regenerator 1, and 4 groups are arranged in the fluidized bed regenerator by adopting a heat taking coil structure. Boiler feed water with the temperature of 105-110 ℃ enters the first heat extraction pipe 2 to absorb heat to generate steam, and a mixture of the steam and water with the temperature of 150-160 ℃ is formed. The mass ratio of the water to the steam is 5: 1-18: 1. The mixture of the steam and the water enters a condensate water tank (a gas-liquid separator 5) for gas-liquid separation, and the steam flows out from the top of the tank and enters a regeneration flue gas cooler 4; the condensed water flows out from the bottom of the tank, is boosted by the medium circulating pump 6 and then enters the first heat taking pipe 2 for recycling. Boiler feed water is replenished from the utility system.
The cyclone separator 3 of the fluidized bed regenerator 1 separates the gas-solid two-phase fluid in the regenerator 1, the catalyst solid particles contained in the regenerated flue gas return to the regeneration bed layer (regeneration reaction zone) at the lower part of the regenerator 1 through the dipleg of the cyclone separator 3, and the regenerated flue gas is discharged from the top of the regenerator 1.
In the regeneration flue gas cooler 4, the regeneration flue gas at 500-530 ℃ flowing out from the fluidized bed regenerator 1 exchanges heat with steam at 150-160 ℃, the steam further absorbs the heat of the regeneration flue gas, the temperature is raised to the superheated steam at 390-410 ℃, and the temperature of the regeneration flue gas is reduced to 198-210 ℃.
In the oxygen-containing gas preheater 7, the 390-410 ℃ superheated steam exchanges heat with air at normal temperature, the air enters the bottom of the regenerator after being heated to 260-265 ℃, and the superheated steam at 225-235 ℃ obtained after heat exchange is sent to other devices.
An oxygen-containing gas electric heater 8 is arranged between the oxygen-containing gas preheater 7 and the regenerator 1 and is used for heating air to the initial oxidation regeneration temperature of the catalyst, generally 360-420 ℃, starting a regeneration reaction and controlling the regeneration temperature in the cold-state start-up process.
Example 2
As shown in the attached figure 2, a regeneration bed layer at the lower part of the fluidized bed regenerator 1 generates catalytic oxidation regeneration reaction to release heat, and the regenerator is internally provided with a high-temperature regenerated catalyst at 500-530 ℃ and high-temperature regenerated flue gas.
The hot catalyst at the bottom of the regenerator is lifted by nitrogen to the regenerator receiver 9. A second heat taking pipe of the receiver is arranged in the regenerator receiver 9, and a heat taking coil structure is adopted, and the number of the second heat taking pipes is 2.
A first heat taking pipe 2 is arranged in the fluidized bed regenerator 1, and 8 groups of heat taking coil structures are arranged. Boiler feed water at the temperature of 105-108 ℃ enters the heat-absorbing coil to absorb heat to generate steam, and a mixture of the steam and the water at the temperature of 150-160 ℃ is formed. The mass ratio of the water to the steam is 6: 1-12: 1. The mixture of steam and water enters a condensate water tank (a gas-liquid separator 5) for gas-liquid separation, the steam flows out of the top of the tank, enters a second heat taking pipe 11 of a regenerator receiver 9 for heat exchange with a catalyst of the regenerator receiver 9, and is further heated to 155-170 ℃; the condensed water flows out from the bottom of the tank, is boosted by the medium circulating pump 6 and then enters the first heat taking pipe 2 for recycling. Boiler feed water is replenished from the utility system.
The cyclone separator 3 of the fluidized bed regenerator 1 separates the gas-solid two-phase fluid in the regenerator 1, the catalyst solid particles contained in the regenerated flue gas return to the regeneration bed layer at the lower part of the regenerator 1 through the dipleg of the cyclone separator 3, and the regenerated flue gas is discharged from the top of the regenerator 1.
In the regeneration flue gas cooler 4, the regeneration flue gas at 510-525 ℃ flowing out from the fluidized bed regenerator 1 exchanges heat with the steam at 155-190 ℃ from the outlet of the second heat taking pipe 11 of the regenerator receiver 9, the steam further absorbs the heat of the regeneration flue gas, the temperature is raised to the superheated steam at 395-420 ℃, and the temperature of the regeneration flue gas is reduced to 198-215 ℃.
In the oxygen-containing gas preheater 7, the superheated steam at 395-420 ℃ exchanges heat with the air at 25 ℃, the air enters the bottom of the regenerator 1 after being heated to 260-265 ℃, and the superheated steam at 227-237 ℃ obtained after heat exchange is sent to other devices.
An oxygen-containing gas electric heater 8 is arranged between the oxygen-containing gas preheater 7 and the regenerator 1 and is used for heating air to the initial oxidation regeneration temperature of the catalyst, generally 360-420 ℃, starting a regeneration reaction and controlling the regeneration temperature in the cold-state start-up process.
Example 3
As shown in the attached figure 3, a regeneration bed layer at the lower part of the fluidized bed regenerator 1 generates catalytic oxidation regeneration reaction to release heat, and the regenerator is internally provided with a high-temperature regenerated catalyst at 500-530 ℃ and high-temperature regenerated flue gas.
The fluidized bed regenerator 1 is internally provided with 6 groups of first heat taking pipes 2 and 2 groups of third heat taking pipes 10 which respectively adopt a coil pipe structure. Boiler feed water at the temperature of 105-109 ℃ enters the first heat extraction pipe 2 to absorb heat to generate steam, and a mixture of steam and water at the temperature of 150-160 ℃ is formed, wherein the mass ratio of the water to the steam is 8: 1-10: 1. The mixture of the steam and the water enters a condensate water tank (a gas-liquid separator 5) for gas-liquid separation, the steam flows out from the top of the tank and enters a third heat taking pipe 10, and the steam is further heated to 155-170 ℃; the condensed water flows out from the bottom of the tank, is boosted by the medium circulating pump 6 and then enters the first heat taking pipe 2 for circulating application.
The cyclone separator 3 of the fluidized bed regenerator 1 separates the gas-solid two-phase fluid in the regenerator 1, the catalyst solid particles contained in the regenerated flue gas return to the regeneration bed layer at the lower part of the regenerator 1 through the dipleg of the cyclone separator 3, and the regenerated flue gas is discharged from the top of the regenerator 1.
In the regeneration flue gas cooler 4, the regeneration flue gas at 500-530 ℃ from the fluidized bed regenerator 1 exchanges heat with steam at 155-170 ℃ from an outlet of the third heat taking pipe 10, the steam further absorbs the superheated steam with the increased temperature of the heat of the regeneration flue gas to 395-420 ℃, and the temperature of the regeneration flue gas is reduced to 198-215 ℃.
In the oxygen-containing gas preheater 7, the superheated steam at 395-420 ℃ exchanges heat with the air at 25 ℃, the air enters the bottom of the regenerator 1 after being heated to 260-265 ℃, and the superheated steam at 230-238 ℃ obtained after heat exchange is sent to other devices.
An oxygen-containing gas electric heater 8 is arranged between the oxygen-containing gas preheater 7 and the regenerator 1 and is used for heating air to the initial oxidation regeneration temperature of the catalyst, generally 360-420 ℃, starting a regeneration reaction and controlling the regeneration temperature in the cold-state start-up process.
According to the embodiment, the catalyst oxidation regeneration method and the catalyst oxidation regeneration system can fully utilize the heat release of the catalyst oxidation regeneration reaction in the regenerator and the heat energy of each temperature position in the system, preheat the oxygen-containing gas, generate superheated steam and supply the superheated steam to other devices, and realize energy conservation and consumption reduction in the regeneration process.
The preferred embodiments of the present disclosure are described in detail with reference to the accompanying drawings, however, the present disclosure is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present disclosure within the technical idea of the present disclosure, and these simple modifications all belong to the protection scope of the present disclosure.
It should be noted that the various features described in the above embodiments may be combined in any suitable manner without departing from the scope of the invention. In order to avoid unnecessary repetition, various possible combinations will not be separately described in this disclosure.
In addition, any combination of various embodiments of the present disclosure may be made, and the same should be considered as the disclosure of the present disclosure, as long as it does not depart from the spirit of the present disclosure.
Claims (10)
1. A method for oxidative regeneration of a catalyst, comprising the steps of:
under the condition of oxidation regeneration, the spent catalyst is in contact with preheated oxygen-containing gas in a regenerator for regeneration, and heat is released to obtain high-temperature regeneration flue gas and a high-temperature regeneration catalyst; a first heat taking pipe is arranged in the regenerator;
enabling the liquid heat exchange medium to enter the first heat taking pipe for heat taking to obtain a gas-liquid mixed medium, and enabling the gas-liquid mixed medium to be subjected to gas-liquid separation to obtain a heat exchange medium condensate and a gaseous heat exchange medium;
and exchanging heat between the gaseous heat exchange medium and the high-temperature regeneration flue gas to obtain a high-temperature gaseous heat exchange medium, and exchanging heat between the high-temperature gaseous heat exchange medium and an oxygen-containing gas to obtain the preheated oxygen-containing gas.
2. The method of claim 1, wherein the oxidative regeneration conditions comprise: the temperature is 470-680 ℃; the volume content of oxygen in the oxygen-containing gas is 5-25%.
3. The method of claim 1, wherein the liquid heat exchange medium is water; in the gas-liquid mixed medium, the mass ratio of the heat exchange medium condensate to the gaseous heat exchange medium is (5-18): 1;
the temperature of the liquid heat exchange medium is 100-120 ℃; the temperature of the gas-liquid mixed medium is 150-160 ℃, the temperature of the high-temperature gaseous heat exchange medium is 390-420 ℃, and the temperature of the preheated oxygen-containing gas is 220-280 ℃.
4. The method according to claim 1, further comprising the step of feeding the high-temperature regenerated catalyst into a regenerator receiver, wherein a second heat taking pipe is arranged in the regenerator receiver, and feeding the gaseous heat exchange medium into the second heat taking pipe to exchange heat with the high-temperature regenerated catalyst and then exchange heat with the high-temperature regenerated flue gas to obtain the high-temperature gaseous heat exchange medium.
5. The method according to claim 1, further comprising arranging a third heat extraction pipe in the regenerator, so that the gaseous heat exchange medium enters the third heat extraction pipe to extract heat and then exchanges heat with the high-temperature regeneration flue gas to obtain the high-temperature gaseous heat exchange medium.
6. The method of claim 1, further comprising heating the oxygen-containing gas with a heater during cold start-up to initiate the regeneration reaction.
7. The system for oxidizing and regenerating the catalyst is characterized by comprising an oxygen-containing gas inlet, a heat exchange medium inlet, a regenerator (1), a gas-liquid separator (5), a regeneration flue gas cooler (4), an oxygen-containing gas preheater (7), a flue gas outlet and a gaseous heat exchange medium outlet; the oxygen-containing gas inlet, the oxygen-containing gas preheater (7) and the regenerator (1) are communicated in sequence;
the regenerator (1) comprises a regeneration reaction zone, a first heat taking pipe (2) is arranged in the regeneration reaction zone, an inlet of the first heat taking pipe (2) is communicated with a heat exchange medium inlet, an outlet of the first heat taking pipe (2) is communicated with an inlet of a gas-liquid separator (5), a gas outlet of the gas-liquid separator (5) is communicated with a gaseous heat exchange medium inlet of a regeneration flue gas cooler (4), a liquid outlet of the gas-liquid separator (5) is communicated with the heat exchange medium inlet, a gaseous heat exchange medium outlet of the regeneration flue gas cooler (4) is communicated with a heat medium inlet of an oxygen-containing gas (7), a flue gas outlet of the regenerator (1) is communicated with a heat medium inlet of the regeneration flue gas cooler (4), and a heat medium outlet of the regeneration flue gas cooler (4) is communicated with the flue gas outlet, the heat medium outlet of the oxygen-containing gas preheater (7) is in communication with the gaseous heat exchange medium outlet of the system.
8. The system according to claim 7, further comprising a regenerator receiver (9), wherein a regenerant inlet of the regenerator receiver (9) is communicated with a regenerant outlet of the regenerator (1), a second heat extraction pipe (11) is arranged in the regenerator receiver (9), an inlet of the second heat extraction pipe (11) is communicated with a gas outlet of the gas-liquid separator (5), and an outlet of the second heat extraction pipe (11) is communicated with a gaseous heat exchange medium inlet of the regeneration flue gas cooler (4); and/or
The system further comprises an oxygen containing gas electric heater (8), said oxygen containing gas electric heater (8) being arranged between said oxygen containing gas preheater (7) and said regenerator (1).
9. The system according to claim 7, wherein the first heat taking pipe (2) is arranged at the lower part of the regeneration reaction zone, a third heat taking pipe (10) is further arranged at the upper part of the regeneration reaction zone, the inlet of the third heat taking pipe (10) is communicated with the gas outlet of the gas-liquid separator (5), and the outlet of the third heat taking pipe (10) is communicated with the gaseous heat exchange medium inlet of the regeneration flue gas cooler (4).
10. The system according to claim 7, wherein the regenerator (1) is a fluidized bed regenerator, a regeneration flue gas outlet, a cyclone separator (3) and a fluidized regeneration reaction zone are sequentially arranged in the fluidized bed regenerator from top to bottom, and the first heat taking pipe (2) is arranged in the fluidized regeneration reaction zone; the first heat taking pipe (2) is a U-shaped coil pipe, a coiled pipe, a vertical heat exchange pipe or a horizontal heat exchange pipe, or a combination of two, three or four of the U-shaped coil pipe, the coiled pipe, the vertical heat exchange pipe and the horizontal heat exchange pipe.
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