CN102407170B - Device for simultaneously scorching at multiple sections in catalyst device of fixed bed reactor and process thereof - Google Patents
Device for simultaneously scorching at multiple sections in catalyst device of fixed bed reactor and process thereof Download PDFInfo
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- CN102407170B CN102407170B CN 201010288598 CN201010288598A CN102407170B CN 102407170 B CN102407170 B CN 102407170B CN 201010288598 CN201010288598 CN 201010288598 CN 201010288598 A CN201010288598 A CN 201010288598A CN 102407170 B CN102407170 B CN 102407170B
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Abstract
The invention relates to a novel regenerative scorching device for a fixed bed catalyst and a process thereof, in particular to a device for simultaneously scorching in a fixed bed multi-bed catalyst reactor and a process thereof as well as a device for simultaneously scorching catalysts in multiple fixed bed reactor series connectors and a process thereof. The technical scheme of the invention is that: a device for simultaneously scorching at multiple sections in a catalyst device of a fixed bed reactor comprises a heating furnace, a regenerative recycle gas compressor, a catalyst reactor and a regenerative recycle gas liquid separation tank, wherein a catalyst bed is formed in the reactor; a pipeline which is communicated with an outlet pipeline of the regenerative recycle gas compressor is arranged between the outlet pipeline and the lower section bed inlets of two adjacent beds; and the pipeline is provided with a compressed air replenishing pipeline which is communicated with the pipeline. Due to the adoption of the device and the process, the scorching time of a catalyst can be shortened, gas, industrial electricity and circulating water can be saved, the energy consumption of the device can be lowered, the scorching safety can be ensured, and the production capability of the device can be increased.
Description
Technical field
The New Regenerated that the present invention relates to a kind of fixed bde catalyst burns device and technique thereof, particularly burns device and technique thereof in many beds of fixed bed hydrogen-catalyst reactor and a plurality of fixed bed reactors serializer inner catalyst burns device and technique thereof simultaneously.
Background technology
The industrial fixed bed catalyst regeneration mode of burning commonly used has two kinds of in-situ regeneration and device regeneration outward at present.The in-situ regeneration that the present invention only relates to many beds of fixed bed catalyst burns or the regeneration of a plurality of fixed bed reactors serializer inner catalyst is burnt.It all is to fill into compressed air at the hydrogen-catalyst reactor top that traditional multi-stage fixed-bed catalyst burns, and down burns from level to level from the top, until penetrate whole bed, and temperature rise is burnt end after without significant change.Although it is chronic that this method simply, is burnt in the actual production, energy consumption is also relatively large.
Burn simultaneously technology about fixed bde catalyst, Tianjin Petrochemical Factory of Lanxing Petrochemical Ltd. discloses a kind of method in its application for a patent for invention Publication Specification 200810052415.8 " device and method of charring straight-run gasoline gasoline upgrading catalyst regeneration ", its hydrogen-catalyst reactor is three-section fixed-bed, carbon four feeding lines after the 3rd section bed entrance has ether, compressed-air line is incorporated into behind the ether on carbon four pipelines, carbon four charging control valves are controlled air supply after utilizing ether, realize that beds burns simultaneously up and down.Although this invention has realized the multistage catalyst and has burnt simultaneously, but it is uncontrollable that thereafter two-stage catalytic agent bed burns temperature, and its oxygen content is also uncontrollable, very easily causes the beds overtemperature, in case and overtemperature does not have the measure of cooling, the easy high temperature sintering inactivation of catalyst yet.
Summary of the invention
Technical problem to be solved by this invention is on the basis of existing fixed bed catalyst regeneration method, develop and a kind ofly can reduce the coke burning regeneration time, can reduce operation energy consumption again, can also guarantee that the regeneration of burning safe many beds of fixed bed catalyst burns method and apparatus.
Technical scheme of the present invention is specific as follows: multistage burns device simultaneously in a kind of fixed bed reactor catalyst device, comprise that heating furnace, regeneration cycle air compressor, hydrogen-catalyst reactor and regeneration recycle gas divide flow container, be provided with beds in the reactor, the pipeline C12 that is communicated with pipeline A10 is set, the ftercompction contracting air line F15 that is communicated with it in pipeline C12 setting between the hypomere bed entrance of the outlet line A10 of regeneration cycle air compressor and two adjacent beds.
Use when burning in many beds of fixed bed hydrogen-catalyst reactor, hydrogen-catalyst reactor is provided with two beds at least.
When using a plurality of series connection fixed bed reactors inner catalysts to burn, described two adjacent beds lay respectively in two adjacent reactors of series connection.Be provided with one or at least two beds in the reactor.
Multistage burns device simultaneously in the described fixed bed reactor catalyst device, comprises online oxygen analyzer 16, and it is arranged between the next bed entrance of the connectivity part of ftercompction contracting air line F15 and pipeline C12 and two adjacent catalyst bed layers.
Multistage burns device simultaneously in the described fixed bed reactor catalyst device, at the arrival end of pipeline C12 and the port of export of ftercompction contracting air line F15 regeneration recycle gas control valve 6 and compressed air regulating valve A5 is set respectively.
Multistage while scorching process in a kind of fixed bed reactor catalyst device, concrete steps comprise:
(1) start the regeneration cycle air compressor, be filled with nitrogen from its porch, circulation boosts to 0.3MPa-0.4MPa;
(2) heating furnace firing up carries out the displacement of hot nitrogen to system, and being warming up to the furnace outlet temperature is 395 ℃-405 ℃, until in the system content of fuel gas (hydrocarbon+hydrogen) less than 0.5%;
(3) open compressed air regulating valve B7 and fill into compressed air from the regeneration recycle gas suction port of compressor, begin to burn operation, simultaneously, regeneration recycle gas control valve 6 and the control of the compressed air regulating valve A5 on the ftercompction contracting air line F15 oxygen content of opening on the pipeline C12 are 0.1%-0.5%, preferred 0.3%-0.5%, up and down two beds that hydrogen-catalyst reactor is adjacent begin to burn simultaneously, and limit of temperature rise is 0 ℃-50 ℃, for the phase I burns;
(4) when hydrogen-catalyst reactor inner catalyst bed temperature be 395 ℃-405 ℃, when catalyst burns bed without temperature rise, the hydrogen-catalyst reactor inlet temperature is mentioned 450 ℃-455 ℃ carries out second stage and burns, the control oxygen content is 0.1-0.5%, preferred 0.3%-0.5%, limit of temperature rise is 0 ℃-50 ℃;
(5) when hydrogen-catalyst reactor inner catalyst bed during without obvious temperature rise, slowly regulate compressed air regulating valve A5 and regeneration recycle gas control valve 6, to system's oxygen content be 18%-21%, preferred 19%-20%, when temperature was 450 ℃-455 ℃, carrying out the phase III burnt;
(6) when bed during without obvious temperature rise, stop to fill into compressed air, use the nitrogen blowing exchange system, until oxygen content is burnt end when being lower than 0.5% in the system.
Beneficial effect of the present invention is:
1, according to the practical operation data in producing, with respect to prior art, the present invention can shorten catalyst and burn 70～80 hours time, thereby has indirectly improved the production capacity of device;
2, because shortening is burnt the time, save gas, commercial power and recirculated water, reduced operating cost, reduced plant energy consumption;
3, can control enter the lower catalyst bed layer burn the temperature degree, can be because not entering the more and more higher bed overtemperature that causes of lower catalyst bed layer temperature;
But 4 real-time monitoring system oxygen contents can be because not causing the bed overtemperature to hyperoxia.
Description of drawings
Fig. 1 is the structural representation that multistage burns device simultaneously in many bed reactors of fixed bed catalyst device of the present invention;
Fig. 2 is the structural representation that the interior multistage of the catalyst device of a plurality of series connection fixed bed reactors of the present invention burns device simultaneously;
Fig. 3 is the structural representation that prior art is burnt device.
Among the figure: the 1-heating furnace, 2-regeneration cycle air compressor, the 3-reactor, the 4-regeneration recycle gas divides flow container, 5-compressed air regulating valve A, 6-regeneration recycle gas control valve, 7-compressed air regulating valve B, 8-reactor top bed, 9-reactor lower part bed, 10-pipeline A, 11-pipeline B, 12-pipeline C, 13-pipeline D, 14-ftercompction contracting air line E, 15-ftercompction contracting air line F, the online oxygen analyzer of 16-.
The specific embodiment
Take 350,000 ton/years of naphtha non-hydrogen modifying apparatus as example.
Embodiment 1:
The interior multistage of many bed reactors of fixed bed catalyst device burns simultaneously device and comprises that heating furnace, regeneration cycle air compressor, hydrogen-catalyst reactor, regeneration recycle gas divide flow container, online oxygen analyzer and control valve, be provided with two beds in the reactor, be divided into top bed 8 and bottom bed 9, the pipeline C12 that is communicated with pipeline A10 is set, the ftercompction contracting air line F15 that is communicated with it in pipeline C12 setting between the outlet line A10 of regeneration cycle air compressor and bottom bed 9 entrances.At the arrival end of pipeline C12 and the port of export of ftercompction contracting air line F15 regeneration recycle gas control valve 6 and compressed air regulating valve A5 are set respectively.Online oxygen analyzer is arranged between the connectivity part and bottom bed 9 entrances of ftercompction contracting air line F15 and pipeline C12.
The scorching process that the interior multistage of many bed reactors of fixed bed catalyst device burns device simultaneously comprises following concrete steps:
(1) start the regeneration cycle air compressor, be filled with nitrogen from its porch, circulation boosts to 0.3MPa-0.4MPa;
(2) heating furnace firing up carries out the displacement of hot nitrogen to system, and being warming up to the furnace outlet temperature is 395-405 ℃, until in the system content of fuel gas (hydrocarbon+hydrogen) less than 0.5%;
3) open compressed air regulating valve B7 and fill into compressed air from the regeneration recycle gas suction port of compressor, begin to burn operation, simultaneously, regeneration recycle gas control valve 6 on the unlatching pipeline C12 and the compressed air regulating valve A5 on the ftercompction contracting air line F15, the control oxygen content is 0.5%, bed 8 and bed 9 begin to burn simultaneously, and limit of temperature rise is 0 ℃-50 ℃, for the phase I burns;
(4) when hydrogen-catalyst reactor inner catalyst bed temperature be 400 ℃, when catalyst burns bed without temperature rise, the hydrogen-catalyst reactor inlet temperature is mentioned 450 ℃ carries out second stage and burn, the control oxygen content is preferred 0.5%, limit of temperature rise is 0 ℃-50 ℃;
(5) when hydrogen-catalyst reactor inner catalyst bed during without obvious temperature rise, slowly regulate compressed air regulating valve A5 and regeneration recycle gas control valve 6, to system's oxygen content be 21%, when temperature was 450 ℃, carrying out the phase III burnt;
(6) when beds during without obvious temperature rise, stop to fill into compressed air, use the nitrogen blowing exchange system, until oxygen content is burnt end when being lower than 0.5% in the system.
The related process parameter sees Table 1.
Table 1
The used time of each processing step sees Table 2.
| Burning process | Time spent (h) |
| System's nitrogen boosts, heats up, replaces | 48 |
| 400 ℃ of constant temperature, oxygen contents 0.5% are burnt | 118 |
| 450 ℃ of constant temperature, oxygen contents 0.5% are burnt | 6 |
| 450 ℃ of constant temperature, oxygen contents 21% are burnt | 2 |
| Total time spent | 174 |
Table 2
Consumption in the burning process sees Table 3.
| Name of material | The consumption that single burns |
| Gas | 10400Nm 3 |
| Recirculated water | 17400t |
| Electricity | 51730Kw/h |
| Nitrogen | 52200Nm 3 |
| Compressed air | 34718Nm 3 |
Table 3
Embodiment 2:
The interior multistage of a plurality of series connection fix bed catalyst reactor burns simultaneously device and comprises that heating furnace, regeneration cycle air compressor, hydrogen-catalyst reactor, regeneration recycle gas divide flow container, online oxygen analyzer and control valve, reactor A and reactor B series connection, be equipped with single bed in the reactor, be respectively bed 8 and bed 9, the pipeline C12 that is communicated with pipeline A10 is set, the short covering gas pipeline F15 that is communicated with it in pipeline C12 setting between the outlet line A10 of regeneration cycle air compressor and bed B entrance.At the arrival end of pipeline C12 and the port of export of short covering gas pipeline F15 flow control valve is set respectively.Online oxygen analyzer is arranged between the connectivity part and bed B entrance of short covering gas pipeline F15 and pipeline C12.
The interior multistage of a plurality of series connection fix bed catalyst reactor burns simultaneously scorching process and related process parameter, the used time of device and consumes with embodiment 1.
Embodiment 3:
Many bed reactors of fixed bed catalyst in-situ regeneration burns device and comprises that heating furnace, regeneration cycle air compressor, hydrogen-catalyst reactor, regeneration recycle gas divide flow container and control valve.
Many bed reactors of fixed bed catalyst in-situ regeneration scorching process comprises the steps:
(1) start the regeneration cycle air compressor, be filled with nitrogen from its porch, circulation boosts to 0.3MPa-0.4MPa;
(2) heating furnace firing up carries out hot nitrogen displacement to system, and being warming up to the furnace outlet temperature is 395-405 ℃;
(3) open compressed air regulating valve B7 and fill into compressed air from the regeneration recycle gas suction port of compressor, begin to burn from reactor head, the control oxygen content is about 0.5%, for the phase I burns;
(4) when hydrogen-catalyst reactor inner catalyst bed temperature be 395-405 ℃, when burning without temperature rise, the hydrogen-catalyst reactor inlet temperature is mentioned 450 ℃ carries out second stage and burn, the control oxygen content is about 0.5%, limit of temperature rise is 0 ℃-50 ℃;
(5) when hydrogen-catalyst reactor inner catalyst bed during without obvious temperature rise, the control system oxygen content is about 19.5-21%, and when temperature was 450 ℃, carrying out the phase III burnt;
(6) when beds during without obvious temperature rise, stop to fill into compressed air, use the nitrogen blowing exchange system, until oxygen content is burnt end when being lower than 0.5% in the system.
The used time of each processing step sees Table 4.
| Burning process | Time spent (h) |
| System's nitrogen boosts, heats up, replaces | 48 |
| 400 ℃ of constant temperature, oxygen contents 0.5% are burnt | 169 |
| 450 ℃ of constant temperature, oxygen contents 0.5% are burnt | 24 |
| 450 ℃ of constant temperature, oxygen contents 21% are burnt | 3 |
| Total time spent | 244 |
Table 4
Consumption in the burning process sees Table 5.
| Name of material | The consumption that single burns |
| Gas | 14640Nm 3 |
| Recirculated water | 24400t |
| Electricity | 72541Kw/h |
| Nitrogen | 73200Nm 3 |
| Compressed air | 50100Nm 3 |
Table 5
Comparing embodiment 1,2 and implement 3 can draw:
The time of saving in the burning process sees Table 6.
| Burning | Embodiment | 3 times spent (h) | |
(h) saves time |
| System's nitrogen boosts, heats up, replaces | 48 | 48 | 0 | |
| 400 ℃ of constant temperature, oxygen contents 0.5% are burnt | 169 | 118 | 51 | |
| 450 ℃ of constant temperature, oxygen contents 0.5% are burnt | 24 | 6 | 18 | |
| 450 ℃ of constant temperature, oxygen contents 21% are burnt | 3 | 2 | 1 | |
| Total time spent | 244 | 174 | 70 |
Table 6
The energy consumption that single burns saving sees Table 7.
The present invention can shorten single burnt time 70-80 hour, saved gas 4000～6000Nm
3Most importantly it has shortened the time of stopping work and burning, thereby has improved the production capacity of device, burns once by 60 days, and former burning amounts to 10 days, now burns calculating in 7 days, but about 1.8 ten thousand ton/years of multi-processing naphtha.
Claims (8)
1. the interior multistage of fixed bed reactor catalyst device burns device simultaneously, comprise that heating furnace, regeneration cycle air compressor, reactor and regeneration recycle gas divide flow container, be provided with beds in the reactor, it is characterized in that, outlet line A(10 at described regeneration cycle air compressor) arrange and pipeline A(10 and between the next bed entrance of two adjacent catalyst bed layers) the pipeline C(12 that is communicated with), at pipeline C(12) and the ftercompction contracting air line F(15 that is communicated with it of setting);
The described device that burns also comprises online oxygen analyzer (16), and it is arranged on ftercompction contracting air line F(15) and pipeline C(12) connectivity part and the next bed entrance of adjacent catalyst bed layer between.
2. multistage burns device simultaneously in the fixed bed reactor catalyst device according to claim 1, it is characterized in that, is provided with at least two beds in the reactor.
3. multistage burns device simultaneously in the fixed bed reactor catalyst device according to claim 1, it is characterized in that described two adjacent catalyst bed layers lay respectively in two adjacent reactors of series connection.
4. multistage burns device simultaneously in the fixed bed reactor catalyst device according to claim 3, it is characterized in that, is provided with one or at least two beds in the described reactor.
5. multistage burns device simultaneously in the fixed bed reactor catalyst device according to claim 1, it is characterized in that, respectively at pipeline C(12) arrival end and ftercompction contracting air line F(15) the port of export regeneration recycle gas control valve (6) and compressed air regulating valve A(5 are set).
6. the interior multistage of each described fixed bed reactor catalyst device burns the multistage while scorching process of device simultaneously according to claim 1-5, it is characterized in that concrete steps comprise:
(1) start the regeneration cycle air compressor, be filled with nitrogen from its porch, circulation boosts to 0.3MPa-0.4MPa;
(2) heating furnace firing up carries out the displacement of hot nitrogen to system, and being warming up to the furnace outlet temperature is 395 ℃ 405 ℃, until in the system content of fuel gas less than 0.5%;
(3) open compressed air regulating valve B(7) fill into compressed air from the regeneration recycle gas suction port of compressor, begin to burn operation, simultaneously, open pipeline C(12) on regeneration recycle gas control valve (6) and ftercompction contracting air line F(15) on compressed air regulating valve A(5), the control oxygen content is 0.1%-0.5%, up and down two beds that reactor is adjacent begin to burn simultaneously, and limit of temperature rise is 0 ℃-50 ℃, for the phase I burns;
(4) when the catalyst in reactor bed temperature be 395 ℃-405 ℃, when catalyst burns bed without temperature rise, reactor inlet temperature is mentioned 450 ℃-455 ℃ carries out second stage and burn, the control oxygen content is 0.1%-0.5%, limit of temperature rise is 0 ℃-50 ℃;
(5) when catalyst in reactor bed during without obvious temperature rise, slowly regulate compressed air regulating valve A(5) and regeneration recycle gas control valve (6), to system's oxygen content be 18%-21%, when temperature was 450 ℃-455 ℃, carrying out the phase III burnt;
(6) when bed during without obvious temperature rise, stop to fill into compressed air, use the nitrogen blowing exchange system, until oxygen content is burnt end when being lower than 0.5% in the system.
7. the interior multistage of fixed bed reactor catalyst device according to claim 6 burns the multistage while scorching process of device simultaneously, it is characterized in that the oxygen content that described step (3) phase I burns and step (4) second stage is burnt is 0.3%-0.5%.
8. the interior multistage of fixed bed reactor catalyst device according to claim 6 burns the multistage while scorching process of device simultaneously, it is characterized in that the oxygen content that described step (5) phase III burns is 19%-20%.
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| CN102744111B (en) * | 2012-07-06 | 2015-02-11 | 宁夏宝塔石化集团有限公司 | Method for recycling hydrocarbons during catalyst regeneration process of benzene/toluene and methanol alkylation reaction |
| CN103203254B (en) * | 2013-04-09 | 2014-12-10 | 高玉华 | Methylamine catalyst regenerating method and device |
| CN110013887B (en) * | 2018-01-09 | 2021-11-05 | 中国石油化工股份有限公司 | In-situ regeneration method for catalyst deactivation |
| CN110013886B (en) * | 2018-01-09 | 2021-11-02 | 中国石油化工股份有限公司 | Catalyst in-situ regeneration device |
| CN109759148B (en) * | 2019-01-31 | 2019-12-13 | 东方傲立石化有限公司 | Regeneration method of aromatization catalyst |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6987078B2 (en) * | 2003-10-03 | 2006-01-17 | Fina Technology, Inc. | Alkylation and catalyst regenerative process |
| CN101244395A (en) * | 2008-03-11 | 2008-08-20 | 蓝星石化有限公司天津石油化工厂 | Device and method for charring straight-run gasoline gasoline upgrading catalyst regeneration |
| CN101658799A (en) * | 2009-09-14 | 2010-03-03 | 洛阳瑞泽石化工程有限公司 | Continuous catalyst regeneration method and device thereof |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6987078B2 (en) * | 2003-10-03 | 2006-01-17 | Fina Technology, Inc. | Alkylation and catalyst regenerative process |
| CN101244395A (en) * | 2008-03-11 | 2008-08-20 | 蓝星石化有限公司天津石油化工厂 | Device and method for charring straight-run gasoline gasoline upgrading catalyst regeneration |
| CN101658799A (en) * | 2009-09-14 | 2010-03-03 | 洛阳瑞泽石化工程有限公司 | Continuous catalyst regeneration method and device thereof |
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