CN102463087A - Device for discharging carbon-containing fluidized-bed catalyst - Google Patents

Device for discharging carbon-containing fluidized-bed catalyst Download PDF

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Publication number
CN102463087A
CN102463087A CN2010105539693A CN201010553969A CN102463087A CN 102463087 A CN102463087 A CN 102463087A CN 2010105539693 A CN2010105539693 A CN 2010105539693A CN 201010553969 A CN201010553969 A CN 201010553969A CN 102463087 A CN102463087 A CN 102463087A
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catalyst
carbon
regenerator
charcoal
equipment
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CN102463087B (en
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齐国祯
张惠明
李晓红
杨远飞
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production

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Abstract

The invention relates to a device for discharging a carbon-containing fluidized-bed catalyst, which is used for mainly solving the problem of incapability of burning off carbon deposit in the event of discharging the carbon-containing fluidized-bed catalyst in the prior art. The problem is well solved by adopting the technical scheme as follows: the device for discharging the carbon-containing fluidized-bed catalyst disclosed by the invention mainly comprises a regenerator 4, a catalyst discharging line 3, a fluidized-bed carbon burner 7 and a catalyst conveying line 5; the inlet end of the catalyst discharging line 3 is positioned above distribution equipment 18 of the regenerator 4; the outlet end of the catalyst discharging line 3 is connected with the fluidized-bed carbon burner 7; a gas outlet is arranged on the top of the fluidized-bed carbon burner 7 and connected with the regenerator 4 through a pipeline 16; a catalyst outlet is arranged at the lower part of the fluidized-bed carbon burner 7 and connected with the catalyst conveying line 5; and carbon-burning medium distribution equipment 17 is arranged at the lower part of the fluidized-bed carbon burner 7. The device for discharging the carbon-containing fluidized-bed catalyst disclosed by the invention can be applied to evaluation of the fluidized-bed catalyst.

Description

The discharge equipment that is used for the carbon-bearing fluid catalyst
Technical field
The present invention relates to a kind of discharge equipment that is used for the carbon-bearing fluid catalyst, especially be applied in the burn off process of carbon distribution when the carbon-bearing catalyst need draw off under the regenerator incomplete regen-eration mode.
Technical background
At present; Fluidized-bed reaction technology has been widely used in fields such as petrochemical industry, Coal Chemical Industry, fine chemistry industry; Control easily owing to it has temperature, the rapid deactivation catalyst be prone to realize advantages such as cyclic regeneration, easy realization large-scale production, fluid bed obtains increasing attention in the application of chemical field.
Fluidized-bed reaction-regeneration technology is used in catalytic cracking (FCC) field in a large number, and the basic at present riser reactor that all adopts of the reactor of FCC loops back riser and continues to use after the FCC catalyst of inactivation is regenerated in regenerator.In order to keep the activity of FCC catalyst in reactor, the regenerator coke-burning regeneration generally all is controlled at the regenerated catalyst carbon deposition quantity below 0.5%.And use the field of fluidized-bed reaction-regeneration technology for some; The regeneration of regenerator inner catalyst does not need the so big intensity of making charcoal; And because regenerated catalyst contains the raising that a certain amount of carbon distribution helps purpose selectivity of product in the reactor on the contrary; At this moment regenerator just needs to adopt the incomplete regen-eration mode, makes to contain a certain amount of carbon distribution on the regenerated catalyst.As in the methanol-to-olefins reaction process; Because the deactivation rate of SAPO-34 catalyst is also very fast; So adopt fluidized-bed reaction-regeneration technology, and for this aperture of SAPO-34 and have the molecular sieve of basket structure, need improve its shape selectivity by the carbon distribution of catalyst can; This just needs regenerated catalyst to contain a certain amount of carbon distribution, and regenerator need adopt the incomplete regen-eration mode.
The field that needs incomplete regen-eration for regenerator as preparing light olefins from methanol; Owing to reasons such as the race of catalyst is decreased, ground, inactivations; Can descend to some extent after catalyst activity levels in the reaction-regeneration system is long-time; Usually the measure of adopting is regular active higher catalyst, the irregular lower equilibrium catalyst of intrasystem activity that draws off simultaneously in this reaction-regeneration system, added.
When needs draw off catalyst, generally all in regenerator, draw off catalyst through small-sized catalyst discharge equipment, as the FCC regenerator, owing to adopt the holomorphosis mode, the general phosphorus content of the catalyst that draws off is extremely low, can directly advance the catalyst storage tank.But for the such regenerator of preparing light olefins from methanol, owing to adopt the incomplete regen-eration mode, the phosphorus content of regenerator inner catalyst may be up to 2～3%, after the catalyst of high like this carbon deposition quantity draws off, can't directly advance the catalyst storage tank.
Because the extensive use of fluidized-bed reaction-regeneration technology, various countries unit or company have developed packing into of multiple catalyst in succession or have drawn off equipment, are used for packing into or drawing off of regenerator inner catalyst.Because packing into or drawing off of catalyst is a contrary operation process, so the principle of the load facility of some catalyst can be used for designing the equipment that draws off of catalyst usually.Research or to develop more be the load facility of catalyst; Promptly in the catalyst storage tank, catalyst is packed under certain flow the regenerator, like Ketjen feeder (catalytic cracking process and engineering, the Chen Junwu chief editor of extensive use; Sinopec publishing house; 2005, the 380th～381 page), comprise the fairlead of 6 millimeters of a vertical dense-phase fluidized bed and φ; Conveying air with certain flow is conveyed into regenerator with catalyst from storage tank again, and the magnitude of recruitment of this feeder is about 0.2～3 ton/day.
Domestic Luoyang petroleum chemical engineering company has developed a kind of quantitative automatic in batches reinforced LPEC-2 type catalyst load facility (Su Qinyu etc., oil refining design, 32 volumes; 2002; The 12nd page), the catalyst in the catalyst storage tank relies on gravity to get into the fluidisation gravimetric tank that has load sensor, closes charging valve automatically and opens fluidization air after reaching predetermined weight; After the jar internal pressure reaches setting, open charging valve automatically, make fluidized catalyst get into regenerator along the small-sized agent line that adds.This feeder maximum feeding quantity every day is 14.4 tons.
Drawing off in a large number of regenerator inner catalyst, when stopping, the large-scale agent line that adds from design draws off at a certain temperature usually, draws off in regenerator, can accomplish the operation of making charcoal as last.And for operating reaction-regenerative device, and when needing regularly to draw off catalyst on a small quantity, comparatively commonly used in the industry at present is the equipment that is similar to the Ketjen feeder, but material require is selected the high temperature material.
But, go wrong for unloading of carbon-bearing catalyst, though can adopt the equipment of similar Ketjen feeder that catalyst is drawn off from regenerator, prior art does not all solve the problem of making charcoal of catalyst, the present invention has solved this problem targetedly.
Summary of the invention
Technical problem to be solved by this invention be can't the burn off carbon distribution when carbon-bearing fluid catalyst draws off in the prior art problem, a kind of new discharge equipment that is used for the carbon-bearing fluid catalyst is provided.This device is used for the carbon-bearing fluid catalyst when device draws off, but has the advantage of the carbon distribution that the burn off catalyst carries.
For addressing the above problem; The technical scheme that the present invention adopts is following: a kind of discharge equipment that is used for the carbon-bearing fluid catalyst, mainly comprise regenerator 4, catalyst discharge line 3, fluid bed make charcoal device 7, catalyst transfer line 5, and catalyst discharge line 3 arrival ends are positioned at regenerator 4 distribution apparatus 18 tops; The port of export and the fluid bed device 7 of making charcoal links to each other; Fluid bed device 7 tops of making charcoal have gas vent, link to each other with regenerator 4 through pipeline 16, and fluid bed device 7 bottoms of making charcoal have catalyst outlet; Link to each other with catalyst transfer line 5, fluid bed device 7 bottoms of making charcoal are provided with the dielectric distribution equipment 17 of making charcoal.
In the technique scheme, the catalyst stream control valve in said catalyst discharge line 3 and the catalyst transfer line 5 is plug valve or guiding valve; Said catalyst discharge line 3 arrival ends are positioned at 1～4 meter, regenerator 4 distribution apparatus, 18 tops; The distribution apparatus 18 of said regenerator 4 is distribution grid or branch type wind-distributing pipe; The make charcoal dielectric distribution equipment 17 of device 7 bottoms of said fluid bed is distribution grid; Said fluid bed device 7 tops of making charcoal have gas vent, and pipeline 16 links to each other with regenerator 4 dilute phase sections 9, is provided with gas-solid separation equipment before the gas vent, and gas-solid separation equipment is filter or cyclone separator; Make charcoal device 7 of said fluid bed is dense-phase fluidized bed, its charcoal temperature of heat maintenance that heat that carries through the catalyst that comes from regenerator 4 or regenerated flue gas carry.
The carbon distribution of catalyst is generally the high-carbon hydrocarbon that accumulates in the catalyst duct; After the carbon-bearing catalyst draws off from regenerator, if the carbon distribution that carried of burn off catalyst not, after this part catalyst would cool down; Some high-carbon hydrocarbon can slowly diffuse out; Cause moist, the bonding of catalyst to a certain extent, the infringement activity of such catalysts, even influence reusing of catalyst.Adopt the discharge equipment of carbon-bearing catalyst of the present invention, can accomplish the operation of making charcoal, make that the phosphorus content of catalyst of entering catalyst storage tank is extremely low the drawing off in the process of catalyst.
Adopt technical scheme of the present invention: the catalyst stream control valve in said catalyst discharge line 3 and the catalyst transfer line 5 is plug valve or guiding valve; Said catalyst discharge line 3 arrival ends are positioned at 1～4 meter, regenerator 4 distribution apparatus, 18 tops; The distribution apparatus 18 of said regenerator 4 is distribution grid or branch type wind-distributing pipe; The make charcoal dielectric distribution equipment 17 of device 7 bottoms of said fluid bed is distribution grid; Said fluid bed device 7 tops of making charcoal have gas vent, and pipeline 16 links to each other with regenerator 4 dilute phase sections 9, is provided with gas-solid separation equipment before the gas vent, and gas-solid separation equipment is filter or cyclone separator; Make charcoal device 7 of said fluid bed is dense-phase fluidized bed; The heat that heat that carries through the catalyst that comes from regenerator 4 or regenerated flue gas carry keeps its charcoal temperature; Can the carbon deposition quantity of the carbon-bearing catalyst that draws off be controlled at below 05% before getting into the catalyst storage tank; Greatly reduce the probability of catalyst impairment, obtained better technical effect.
Description of drawings
Fig. 1 is the schematic flow sheet of device according to the invention;
Among Fig. 1,1 is regenerator sloped tube; 2 is the regenerating medium charging; 3 is the catalyst discharge line; 4 is regenerator; 5 is catalyst transfer line; 6 is the pumped (conveying) medium charging; 7 are the catalyst device of making charcoal; 8 is gas-solid cyclone separator; 9 is the dilute phase section; 10 is the flue gas pipeline; 11 is inclined tube to be generated; 12 for catalyst is made charcoal gas returns the regenerator pipeline in the device; 13 is gas-solid separation equipment; 14 are the medium charging of making charcoal; 15 get into the catalyst pipeline of making charcoal for flue gas; 16 is blowback air; 17 is distribution apparatus; 18 is distribution apparatus.
Catalyst in the regenerator 4 is made charcoal from catalyst discharge line 3 entering catalyst the device 7; Contact with the medium of making charcoal from pipeline 14; Catalyst self-catalysis agent pipeline 5 after completion is made charcoal is getting into the catalyst storage tank under the transport medium of pipeline 6, the dilute phase section 9 that catalyst is made charcoal and got into regenerator 4 after device 7 interior gases separate through gas-solid separation equipment 13.
Through embodiment the present invention is done further elaboration below, but be not limited only to present embodiment.
The specific embodiment
[embodiment 1]
In the process of methanol-to-olefins reaction, reaction unit is as shown in Figure 1, and regenerator adopts the incomplete regen-eration mode; Regeneration temperature is 664 ℃, and regenerating medium is an air, and regenerated catalyst carbon deposition quantity mass fraction is 2.4%; When needs drew off catalyst, catalyst was made charcoal and is fed make charcoal medium and regenerated flue gas in the device in advance, and the medium of making charcoal is 200 ℃ a air; The regenerated flue gas temperature is about 689 ℃, and the make charcoal temperature of device of catalyst is remained on about 625 ℃.The arrival end of catalyst discharge line is positioned at 2.5 meters, regenerator distribution apparatus top, and the regenerator distribution apparatus is a distribution grid, and the distribution apparatus that catalyst is made charcoal in the device is a distribution grid.Open the flow control valve of catalyst discharge line, control valve adopts guiding valve, and keeping catalyst flow is 3.2 kilograms/hour; The carbon-bearing catalyst gets into catalyst and makes charcoal behind the device, and the make charcoal temperature of device of catalyst is about about 652 ℃, along with the carrying out of making charcoal; Gradually cut off regenerated flue gas; Only adopt air to make charcoal, the gas that produces of making charcoal separates the dilute phase section that the back gets into regenerator through gas-solid separation equipment, and gas-solid separation equipment is a ceramic filter.The make charcoal density of catalyst of device of catalyst is about 453 kilograms per cubic meter, is dense-phase fluidized bed.The catalyst flow that guarantees catalyst transfer line and catalyst discharge line is roughly the same; Pumped (conveying) medium is an air; With catalyst transport to catalyst storage tank; Carry out the catalyst sampling from the catalyst tank bottom, and adopt infrared carbon sulfur analyzer to carry out the carbon deposition quantity analysis, analysis result is that the carbon deposition quantity of catalyst mass fraction of catalyst storage tank is about 0.146%.
[embodiment 2]
According to condition and the step of embodiment 1, regeneration temperature is 683 ℃, and when needs drew off catalyst, catalyst was made charcoal and fed the medium of making charcoal in the device in advance, and the medium of making charcoal is the air about 400 ℃, and the make charcoal temperature of device of catalyst is remained on more than 380 ℃.The arrival end of catalyst discharge line is positioned at 3.5 meters, regenerator distribution apparatus top, and the regenerator distribution apparatus is a branch type wind-distributing pipe, and the distribution apparatus that catalyst is made charcoal in the device is a distribution grid.Open the flow control valve of catalyst discharge line; Control valve adopts plug valve; Keeping catalyst flow is 1.7 kilograms/hour; The carbon-bearing catalyst gets into catalyst and makes charcoal behind the device, and the make charcoal temperature of device of catalyst is about about 626 ℃, and the gas-solid separation equipment that catalyst is made charcoal in the device is small-sized cyclone separator.The make charcoal density of catalyst of device of catalyst is about 374 kilograms per cubic meter.The catalyst flow that guarantees catalyst transfer line and catalyst discharge line is roughly the same; With catalyst transport to catalyst storage tank; Carry out the catalyst sampling from the catalyst tank bottom; And adopting infrared carbon sulfur analyzer to carry out the carbon deposition quantity analysis, analysis result is that the carbon deposition quantity of catalyst mass fraction of catalyst storage tank is about 0.453%.
[comparative example]
Condition and step according to embodiment 1; The catalyst device of making charcoal just is not set; Carbon-bearing catalyst in the regenerator gets into catalyst transfer line from catalyst discharge line diameter; Under the conveying of air, get into the catalyst storage tank, carry out the catalyst sample analysis from the catalyst tank bottom, analysis result is 2.21% for the carbon deposition quantity of catalyst mass fraction.
Obviously, adopt device of the present invention, be used for the carbon-bearing fluid catalyst when device draws off, but have the advantage of the carbon distribution that the burn off catalyst carries, have bigger technical advantage, can be used for commercial production.

Claims (7)

1. discharge equipment that is used for the carbon-bearing fluid catalyst; Mainly comprise regenerator (4), catalyst discharge line (3), fluid bed make charcoal device (7), catalyst transfer line (5); Catalyst discharge line (3) arrival end is positioned at regenerator (4) distribution apparatus (18) top, and the port of export and the fluid bed device (7) of making charcoal links to each other, and fluid bed device (7) top of making charcoal has gas vent; Link to each other with regenerator (4) through pipeline (16); Fluid bed device (7) bottom of making charcoal has catalyst outlet, links to each other with catalyst transfer line (5), and fluid bed device (7) bottom of making charcoal is provided with the dielectric distribution equipment (17) of making charcoal.
2. according to the said discharge equipment that is used for the carbon-bearing fluid catalyst of claim 1, it is characterized in that the catalyst stream control valve in said catalyst discharge line (3) and the catalyst transfer line (5) is plug valve or guiding valve.
3. according to the said discharge equipment that is used for the carbon-bearing fluid catalyst of claim 1, it is characterized in that said catalyst discharge line (3) arrival end is positioned at 1～4 meter, regenerator (4) distribution apparatus (18) top.
4. according to the said discharge equipment that is used for the carbon-bearing fluid catalyst of claim 1, the distribution apparatus (18) that it is characterized in that said regenerator (4) is distribution grid or branch type wind-distributing pipe.
5. according to the said discharge equipment that is used for the carbon-bearing fluid catalyst of claim 1, it is characterized in that the make charcoal dielectric distribution equipment (17) of device (7) bottom of said fluid bed is distribution grid.
6. according to the said discharge equipment that is used for the carbon-bearing fluid catalyst of claim 1; It is characterized in that said fluid bed device (7) top of making charcoal has gas vent; Pipeline (16) links to each other with regenerator (4) dilute phase section (9); Be provided with gas-solid separation equipment before the gas vent, gas-solid separation equipment is filter or cyclone separator.
7. according to the said discharge equipment that is used for the carbon-bearing fluid catalyst of claim 1; It is characterized in that the said fluid bed device (7) of making charcoal is a dense-phase fluidized bed, the heat that heat that carries through the catalyst that comes from regenerator (4) or regenerated flue gas carry keeps its charcoal temperature.
CN201010553969.3A 2010-11-17 2010-11-17 Device for discharging carbon-containing fluidized-bed catalyst Active CN102463087B (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103831063A (en) * 2012-11-23 2014-06-04 洛阳凯美胜石化设备有限公司 Online catalyst addition and unloading apparatus

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3926843A (en) * 1973-03-26 1975-12-16 Mobil Oil Corp Fcc ' 'multi-stage regeneration procedure
US4340566A (en) * 1979-12-07 1982-07-20 Uop Inc. Catalyst regeneration apparatus
US5077251A (en) * 1990-07-17 1991-12-31 Mobil Oil Corporation Control of multistage catalyst regeneration with both partial and full co combustion
CN1511927A (en) * 2002-12-31 2004-07-14 石油大学(北京) Coupling device and method for double reaction-regeneration system gasoline high qualifying and heavy oil catalytic cracking
CN101239874A (en) * 2007-02-07 2008-08-13 中国石油化工股份有限公司 Reaction device for converting oxygen-containing compound to low-carbon olefins
CN101328102A (en) * 2008-06-12 2008-12-24 中国石油化工股份有限公司 Method for keeping regenerator temperature stable in low carbon alkene preparation

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3926843A (en) * 1973-03-26 1975-12-16 Mobil Oil Corp Fcc ' 'multi-stage regeneration procedure
US4340566A (en) * 1979-12-07 1982-07-20 Uop Inc. Catalyst regeneration apparatus
US5077251A (en) * 1990-07-17 1991-12-31 Mobil Oil Corporation Control of multistage catalyst regeneration with both partial and full co combustion
CN1511927A (en) * 2002-12-31 2004-07-14 石油大学(北京) Coupling device and method for double reaction-regeneration system gasoline high qualifying and heavy oil catalytic cracking
CN101239874A (en) * 2007-02-07 2008-08-13 中国石油化工股份有限公司 Reaction device for converting oxygen-containing compound to low-carbon olefins
CN101328102A (en) * 2008-06-12 2008-12-24 中国石油化工股份有限公司 Method for keeping regenerator temperature stable in low carbon alkene preparation

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103831063A (en) * 2012-11-23 2014-06-04 洛阳凯美胜石化设备有限公司 Online catalyst addition and unloading apparatus

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