CN102218354A - Hydrocarbon conversion catalyst regeneration burning method and regenerator burning area structure - Google Patents
Hydrocarbon conversion catalyst regeneration burning method and regenerator burning area structure Download PDFInfo
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- CN102218354A CN102218354A CN2010101448661A CN201010144866A CN102218354A CN 102218354 A CN102218354 A CN 102218354A CN 2010101448661 A CN2010101448661 A CN 2010101448661A CN 201010144866 A CN201010144866 A CN 201010144866A CN 102218354 A CN102218354 A CN 102218354A
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Abstract
The invention discloses a hydrocarbon conversion catalyst regeneration burning method and a regenerator burning area structure, and solves the problems that a hydrocarbon conversion catalyst burning area has a temperature runaway risk and the like in the prior art. The method comprises the following steps of: introducing a catalyst to be regenerated into a radial catalyst moving bed burning area by means of gravity, contacting oxygen-containing regeneration gas, and burning carbon deposit on the catalyst; and introducing into a chlorine oxidation area under the action of gravity, wherein a catalyst moving bed in the burning area is provided with a quick firing section, a transition section and a superheat section from top to bottom in turn; and the thickness ratio of catalyst beds in the quick firing section and the superheat section is 0.25-1 and the height ratio is 1-8.
Description
Technical field
The invention belongs to petrochemical industry, relate to the new structure that a kind of regeneration of hyolrocarbon conversion catalyst burns method and regenerator scorch region.
Background technology
Catalytic reforming is one of important process of oil refining and petrochemical industry, and it is a kind of hydrocarbon conversion process, is raw material with the naphtha, generates the reformed oil that is rich in aromatic hydrocarbons, by-product hydrogen and liquefied petroleum gas by the catalytic hydroprocessing reaction.The conversion of reforming is accompanied by the carbon deposit reaction, and the dehydrogenation of the hydro carbons degree of depth generates alkene, and cyclization of olefines and polymerization form condensed-nuclei aromatics, is adsorbed on the final carbon deposit that forms on the surface of catalyst, makes catalysqt deactivation.The catalyst of inactivation need recover active through regeneration, and the most important first step of regenerative process is exactly a burning process, removes the coke that deposits on the catalyst with oxygen containing regeneration gas burning, has taken away the burning liberated heat when gas is discharged.
Hydrocarbon conversion catalyst realizes that the catalyst activity in the reaction remains higher level, has improved the yield and the quality of product greatly after the cyclic regeneration.In the regenerator device of hydrocarbon conversion catalyst cyclic regeneration system, scorch region is one of chief component, and its agent structure is generally formed by radially burning bed and regeneration gas discrepancy runner.Catalyst relies on the gravity effect to move down slowly in annular bed, and oxygen containing regeneration gas then radially contacts with the catalyst cross-flow by bed, has realized continuous burning process.
The humidity of environment and temperature, and the high-temperature residence time of catalyst are the principal elements that influences the specific area fall off rate of hydrocarbon conversion catalyst, have determined the service life of hydrocarbon conversion catalyst.Because hydrogeneous coke can generate aqueous vapor in combustion process, illustrate that burning process carries out under high temperature and aqueous environment, so the regeneration burning process of hydrocarbon conversion catalyst is the main process that influences catalyst life.
In the porch of burning bed, catalyst has higher carbon content and lower temperature.Along with the heating of gas and the generation of combustion reaction, temperature is rapid ascendant trend.On bed top, a large amount of heats of emitting of making charcoal make bed temperature reach higher level.In the bed bottom, along with the consumption of burning, coke content reduces gradually, and thermal discharge reduces, and temperature rise is less.Analyze from the carbon content variation tendency of beds, hot environment generally appears at bed top, and temperature is too high brings adverse effect easily with the excessive performance to catalyst of high-temperature area.
Regeneration gas for the radial centripetal formula burns mode, since the flow direction of oxygen-containing gas be radially by outward toward in, oxygen consumes by bed the time gradually, so under the situation that the carbon deposit of catalyst does not burn down, same horizontal cross-section is burnt abundant more the closer to outer screen cloth place catalyst, high more the closer to the catalyst carbon content of interior screen cloth.So just one section zone near interior screen cloth has formed high charcoal district at the bed top.Under the operating mode that oxygen content increases suddenly, the contained coke of this part high charcoal district catalyst is able to abundant burning, emits a large amount of heats rapidly, in gas flow accumulates near the screen cloth, this part bed temperature is sharply raise, and this situation is called " temperature runaway ".Temperature runaway produces very big thermal stress near the weld seam of interior screen cloth top, weld seam is broken, and causes catalyst to leak into the regeneration gas circulatory system.Therefore adopt suitable bed structure to regulate the interior Temperature Distribution of bed, limit the volume in high charcoal district, reduce the heat of temperature runaway and emit, the protection regenerator is had positive effect.
At USP4,859,643 and USP5, in 277,880 regeneration technologies that provide, the scorch region of regenerator is a pyramidal structure, the thickness of bed has improved the gas flow distribution of axial location from top to bottom by thick attenuation.The bed resistance that top approaches is less, the tolerance of distributing is bigger, the thicker bed resistance in bottom is bigger, the tolerance that is assigned to is just few, alleviated to a certain extent that the high oxygen demand of catalyst dropping process mid-early stage carbon content is big, the low less actual conditions of oxygen demand of later stage carbon content, reduced the time of staying of catalyst in high-temperature region, bed top.Yet because the thickness of bed layer that above-mentioned patent is described is to be in axial height a progressive formation that increases gradually, the high charcoal district volume on bed top still needs further reduction, and the risk of temperature runaway still exists.And drying system is not set, water content height in the regeneration gas in the closed circuit of regeneration gas.The regeneration burning process of catalyst is to finish under the harsh operating mode of high temperature, Gao Shui, and this high temperature, high water content environment very easily cause the loss of specific surface area of catalyst, thereby shortens the service life of catalyst.
At USP5,034,117 and the regeneration technology that provides of CN1045411A in, the regenerator scorch region is two sections structures of burning.The beds of scorch region is divided into two sections, carries catalyst from top to bottom by dipleg.Two sections beds have identical physical dimension and different regeneration gas entry conditions, and the inlet temperature of hypomere bed regeneration gas is higher than the epimere bed, and the space make-up air between two sections beds is regulated the inlet oxygen content of two-stage regeneration gas.Regeneration cycle is provided with drying system in the loop, and has adopted segmentation supercharging regeneration, so water content in regeneration recycle gas is lower, and bed gaseous mass flux is bigger, and therefore the temperature rise of whole bed is burnt compared with the single hop bed obvious reduction is arranged.But the high charcoal district volume at bed top does not reduce, and the risk of temperature runaway fails effectively to avoid.The measure of bed segmentation has strengthened the complexity of burning segment structure in addition, has improved manufacture difficulty and cost of investment, has increased the burden of Operation and maintenance.
Summary of the invention
The present invention be directed to hydrocarbon conversion catalyst in the prior art (as reforming catalyst) scorch region and have shortcomings such as temperature runaway risk, and provide a kind of new catalyst regeneration to burn method and scorch region structure, use the present invention can effectively avoid failing in time to burn because of carbon residue in the catalyst regeneration process, when gas oxygen content increases suddenly in the system, near Johnson's Intranet of bed top, produce temperature runaway, cause the bad phenomenon of Johnson's network loss to occur.
The invention provides a kind of regeneration of hyolrocarbon conversion catalyst and burn method, reclaimable catalyst outer from regenerator or the regenerator buffering area enters radially moving-bed of catalyst scorch region by gravity, contact carbon deposit on the burning-off catalyst with containing the oxygen regeneration gas, under the gravity effect, enter chlorine oxidation zone then.It is characterized in that: the reclaimable catalyst that enters scorch region enters scorch region the top section of burning, middle part changeover portion and bottom superheat section soon successively by gravity, reclaimable catalyst scorch region soon the time of staying of the section of burning be 0.25～1 with ratio in time of staying of scorch region superheat section, preferred 0.4～0.8.
The present invention also provides a kind of regenerator scorch region structure, comprises radially moving-bed of catalyst, and radially moving-bed of catalyst is made of screen cloth in the tubular and the outer screen cloth of tubular.It is characterized in that: the interior screen cloth upper diameter that constitutes moving-bed of catalyst radially is bigger than lower diameter, connect by pyramidal structure between upper and lower two parts of interior screen cloth, the different interior screen cloth of diameter forms scorch region the top section of burning, middle transition section and bottom superheat section soon from top to bottom with outer screen cloth, wherein fast burning section is 0.25～1 with the catalyst bed layer thickness ratio of superheat section, preferred 0.3～0.8, fast burning section is 1～8 with the bed height ratio of superheat section, preferred 2～5.
The present invention compared with prior art, its advantage is:
1) at scorch region, because the upper catalyst bed layer thickness of scorch region is less than the lower catalyst bed layer thickness, and thin top bed can limit near the volume in the high charcoal district of interior screen cloth top weld seam, with USP4,859,643, USP5,277,880, USP5,034,117 compares with the regeneration technology that CN1045411A provides, and the thickness of the section of burning is thinner soon on equal bed volume lower bed layer top, therefore limit near the high charcoal district volume in Johnson's Intranet top better, effectively reduced the risk that the bed temperature runaway burns out interior screen cloth.
2) beds by upper-thin-lower-thick burns step by step, has regulated the catalyst time of staying and the distribution of regeneration gas flow in bed.The catalyst time of staying of scorch region top bed shortens, and the regeneration gas flow increases, and has satisfied the needs of diverse location burning to oxygen, makes and has improved coke all burnt faster and burnt efficient.
3) directly the single hop bed is divided into the structure that two parts thickness does not wait, with patent USP5,034,117 compare with two sections methods of burning in the regeneration technology that CN1045411A provides, simplified the structure of regenerator scorch region, reduce the regenerator height, and saved dipleg under the catalyst that connects two sections beds, saved equipment investment.
Accompanying drawing and description of drawings
Fig. 1 burns the method simple flow chart for catalyst regeneration provided by the invention.
Fig. 2 is a regenerator scorch region structural representation of the present invention.
Among the figure:
The 1-reclaimable catalyst; The 2-buffering area;
Dipleg under the 3-catalyst; 4-is the section of burning soon;
The 5-changeover portion; The 6-superheat section;
The regeneration gas space that outer screen cloth of 7-and regenerator inwall surround;
The regeneration gas space that screen cloth surrounds in the 8-; 9-scorch region catalyst outlet;
The 11-heat exchanger; 13-circulating air caustic wash tower;
15-circulating air alkali cleaning circulating pump; The 19-drier;
The 20-compressor; 23-regeneration gas electric heater;
The overheated pneumoelectric heater of 26-; The 31-caustic wash tower of dropping a hint;
The 35-alkali circulating pump of dropping a hint; Screen cloth in the 39-;
The outer screen cloth of 40-; 41-regenerator scorch region;
42-regeneration gas inlet; 43-crosses the hot gas inlet;
The outlet of 44-regeneration cycle oxygen deprivation gas;
10,12,14,16,17,18,21,22,24,25,27,28,29,30,32,33,34,36,37,38-pipeline.
The specific embodiment
As shown in Figure 2, the beds of regenerator scorch region 41 is made of screen cloth in the tubular 39 and the outer screen cloth 40 of tubular, and wherein the upper diameter of interior screen cloth 39 is bigger than lower diameter, is connected by pyramidal structure between upper and lower two parts.Regenerator scorch region 41 is positioned at buffering area 2 belows, between be communicated with by dipleg under the catalyst 3.
The top of the tubular top of described interior screen cloth 39 and outer screen cloth 40 formation scorch region beds is the section of burning 4 soon, the cylindrical lower of interior screen cloth 39 and outer screen cloth 40 constitute the bottom superheat section 6 of scorch region beds, and the taper connection structure division of interior screen cloth 39 and outer screen cloth 40 constitute the middle transition section 5 of scorch region beds.The scorch region thickness of bed layer ratio of the section of burning 4 and scorch region superheat section 6 soon is 0.25～1, and is preferred 0.4～0.8, and the scorch region aspect ratio of the section of burning 4 and scorch region superheat section 6 soon is 1～8, preferred 2～5.
In conjunction with Fig. 1 and Fig. 2 to the description of simple process flow of the present invention be: reclaimable catalyst 1 enters regenerator buffering area 2, enters regenerator scorch region 41 by dipleg under the catalyst 3.Shown in the figure under the catalyst dipleg 3 be two.The present invention does not limit the radical of dipleg under the catalyst 3.Reclaimable catalyst 1 is the middle transition section 5 of the section of burning 4, scorch region beds and the bottom superheat section 6 of scorch region beds soon of the top by the scorch region beds successively by gravity, with contain the oxygen regeneration gas and contact carbon deposit on the burning-off catalyst, under the gravity effect, go out scorch region then, enter chlorine oxidation zone afterwards by scorch region catalyst outlet 9.On the top of scorch region beds soon the time of staying of the section of burning 4 be 0.25～1 at the time of staying of the bottom of scorch region beds superheat section 6 ratio, preferred 0.3～0.8.
Regeneration gas is through pipeline 24, cross hot gas through pipeline 27, introduce regenerator by the regeneration gas inlet 42 at regenerator scorch region 41 middle parts and the hot gas inlet 43 of crossing of bottom respectively, regeneration gas 42 temperature that enter the mouth are 400～470 ℃, crossing hot gas 43 temperature that enter the mouth is 450～500 ℃, regeneration gas and the oxygen content of crossing in the hot gas are 0.3～1.0 volume %, vapour content is 50～200ppmv, regeneration gas and cross the hot gas regeneration gas space 7 interior axial distribution that surround of screen cloth and regenerator inwall outside, and radially pass through carbon deposit on scorch region beds and the burn off reclaimable catalyst to the center, collect in the regeneration gas space 8 that screen cloth surrounds in the regenerator then, draw regenerator through regeneration cycle oxygen deprivation gas outlet 44 by pipeline 10.
Operation absolute pressure in the regenerator scorch region 41 is 0.6～1.0Mpa.
In the regeneration cycle gas return path, regeneration gas from pipeline 10 enters heat exchanger 11 heat exchange after enter circulating air caustic wash tower 13 by pipeline 12, pipeline 33 water fillings, pipeline 16 is annotated alkali, and pipeline 14,17 and circulating air alkali cleaning circulating pump 15 are formed the tower rising pouring alkali circulation of circulating air caustic wash tower 13.Alkali cleaning removes HCl and CO
2After regeneration gas through pipeline 18, successively by drier 19 and compressor 20.Regeneration gas after the dry supercharging is through pipeline 21, heat exchanger 11 and the gas converting heat that goes out regenerator, be divided into two stocks then and introduce regeneration gas electric heater 23 and overheated pneumoelectric heaters 26, return regenerator scorch region 41 after being heated to 400～470 ℃ and 400～490 ℃ respectively to recycle by pipeline 22,25.
By the gas that pipeline 28 is drawn from chlorine oxidation zone, a part is replenished into regeneration gas circulation through pipeline 29.Another part enters the caustic wash tower 31 of dropping a hint along pipeline 30, pipeline 32 water fillings, and pipeline 37 is annotated alkali, and the pipeline 34,36 and the alkali cleaning circulating pump 35 of dropping a hint are formed the tower rising pouring alkali circulation of the caustic wash tower 31 of dropping a hint.Gas after the alkali cleaning is through pipeline 38 emptying.
Claims (4)
1. a regeneration of hyolrocarbon conversion catalyst burns method, reclaimable catalyst outer from regenerator or the regenerator buffering area enters radially moving-bed of catalyst scorch region by gravity, with contain the oxygen regeneration gas and contact carbon deposit on the burning-off catalyst, under the gravity effect, enter chlorine oxidation zone then, it is characterized in that: the reclaimable catalyst that enters scorch region enters scorch region the top section of burning, middle part changeover portion and bottom superheat section soon successively by gravity, and the time of staying of the section of burning is 0.25～1 with ratio in time of staying of scorch region superheat section to reclaimable catalyst soon at scorch region.
2. method according to claim 1 is characterized in that: the time of staying of the section of burning is 0.4～0.8 with ratio in time of staying of scorch region superheat section to reclaimable catalyst soon at scorch region.
3. regeneration of hyolrocarbon conversion catalyst device scorch region structure, comprise radially moving-bed of catalyst, radially moving-bed of catalyst is made of screen cloth in the tubular and the outer screen cloth of tubular, it is characterized in that: the interior screen cloth upper diameter that constitutes moving-bed of catalyst radially is bigger than lower diameter, on the interior screen cloth, connect by pyramidal structure between following two parts, the different interior screen cloth of diameter forms the scorch region top section of burning soon from top to bottom with outer screen cloth, middle transition section and bottom superheat section, wherein fast burning section is 0.25～1 with the catalyst bed layer thickness ratio of superheat section, and fast burning section is 1～8 with the bed height ratio of superheat section.
4. regenerator scorch region structure according to claim 3 is characterized in that: fast burning section is 0.3～0.8 with the catalyst bed layer thickness ratio of superheat section, and fast burning section is 2～5 with the bed height ratio of superheat section.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010144866.1A CN102218354B (en) | 2010-04-13 | 2010-04-13 | Hydrocarbon conversion catalyst regeneration burning method and regenerator burning area structure |
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| CN201010144866.1A CN102218354B (en) | 2010-04-13 | 2010-04-13 | Hydrocarbon conversion catalyst regeneration burning method and regenerator burning area structure |
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| CN102218354A true CN102218354A (en) | 2011-10-19 |
| CN102218354B CN102218354B (en) | 2015-04-08 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102218353A (en) * | 2010-04-13 | 2011-10-19 | 中国石油化工集团公司 | Coke-burning method for hydrocarbon conversion catalyst regeneration and structure of coke-burning area of regenerator |
| CN111378510A (en) * | 2018-12-28 | 2020-07-07 | 中国石油化工股份有限公司 | Method and system for preparing synthesis gas by using biomass |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1045411A (en) * | 1989-01-13 | 1990-09-19 | 法国石油公司 | The renovation process of aromatic hydrocarbon preparation or reforming catalyst |
| US5277880A (en) * | 1988-05-11 | 1994-01-11 | Uop | Catalyst regeneration apparatus with radial flow distribution |
| CN1724166A (en) * | 2005-07-19 | 2006-01-25 | 白跃华 | Tech. for regenerating reforming catalyst back charring and its regenerator |
| CN102218353A (en) * | 2010-04-13 | 2011-10-19 | 中国石油化工集团公司 | Coke-burning method for hydrocarbon conversion catalyst regeneration and structure of coke-burning area of regenerator |
-
2010
- 2010-04-13 CN CN201010144866.1A patent/CN102218354B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5277880A (en) * | 1988-05-11 | 1994-01-11 | Uop | Catalyst regeneration apparatus with radial flow distribution |
| CN1045411A (en) * | 1989-01-13 | 1990-09-19 | 法国石油公司 | The renovation process of aromatic hydrocarbon preparation or reforming catalyst |
| CN1724166A (en) * | 2005-07-19 | 2006-01-25 | 白跃华 | Tech. for regenerating reforming catalyst back charring and its regenerator |
| CN102218353A (en) * | 2010-04-13 | 2011-10-19 | 中国石油化工集团公司 | Coke-burning method for hydrocarbon conversion catalyst regeneration and structure of coke-burning area of regenerator |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102218353A (en) * | 2010-04-13 | 2011-10-19 | 中国石油化工集团公司 | Coke-burning method for hydrocarbon conversion catalyst regeneration and structure of coke-burning area of regenerator |
| CN102218353B (en) * | 2010-04-13 | 2015-04-08 | 中国石油化工集团公司 | Coke-burning method for hydrocarbon conversion catalyst regeneration and structure of coke-burning area of regenerator |
| CN111378510A (en) * | 2018-12-28 | 2020-07-07 | 中国石油化工股份有限公司 | Method and system for preparing synthesis gas by using biomass |
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| CN102218354B (en) | 2015-04-08 |
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Address after: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant after: China Petrochemical Group Corp. Co-applicant after: Luoyang Petrochemical Engineering Corporation /SINOPEC Address before: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant before: China Petrochemical Group Corp. Co-applicant before: Luoyang Petrochemical Engineering Co., China Petrochemical Group |
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