CN102399575A - Control method of regenerated catalyst for gas-solid reaction - Google Patents
Control method of regenerated catalyst for gas-solid reaction Download PDFInfo
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- CN102399575A CN102399575A CN2011102956069A CN201110295606A CN102399575A CN 102399575 A CN102399575 A CN 102399575A CN 2011102956069 A CN2011102956069 A CN 2011102956069A CN 201110295606 A CN201110295606 A CN 201110295606A CN 102399575 A CN102399575 A CN 102399575A
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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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Abstract
The invention discloses a control method of regenerated catalyst for gas-solid reaction, such as alcohol oxygenated chemicals, hydrocarbon catalytic cracking and the like, which belongs to the technology field of petrochemical industry. The regenerated catalyst enters into a reactor after the regenerated catalyst is cooled and gaseous impurities are purified in a catalyst control unit, the catalyst control unit conveys and fluidizes medium by using water vapour as catalyst, the gas (including smoke) entered into the catalyst control unit by being picked up by the regenerated catalyst is replaced by water vapour, the gas and water vapour gaseous components return to regenerator dilute phase through a special delivery line. The catalyst control unit is provided with heat exchange tubes for controlling temperature of the regenerated catalyst. Supercharged air is replaced by water vapour for fluidizing the catalyst control unit, which can reduce the load of a supercharger; the gaseous impurities in the catalyst are purified; the reaction yield is increased, and the smoke amount in dried gas is reduced; the fluidized water vapour returns to regenerator dilute phase, which does not cause dilute phase combustion and the like.
Description
Technical field
The present invention relates to the petrochemical technology field, particularly relate to the regenerated catalyst control method of gas-solid reactions such as a kind of alcohols oxygenatedchemicals, catalytic cracking of hydrocarbon.
Background technology
The catalytic unit of conventional gas-solid reaction process comprises reaction-regeneration section; The regenerated catalyst of revivifier directly gets into reactor drum through the regeneration standpipe; The flue gas that catalyst entrainment accounts for material quantity 1-1.2% gets into reactor drum together, because this part oxygen content of smoke gas low (below 8%, being generally 2-4%); Flue gas is not participated in catalytic reaction process after being brought into reactor drum basically; Finally discharge reaction-regenerative device with dry gas, the flue gas that gets into because of catalyst entrainment generally accounts for the 20-25% of dry gas yied, and these flue gases cause the pneumatic press energy consumption to increase.
Existing research shows, in gas-solid reaction processes such as catalytic cracking, can improve the reagent oil ratio to the suitable cooling of regenerated catalyst; Suppress heat cracking reaction, improve product and distribute, thus the economic benefit of raising gas-solid reaction device; So produced through heat collector and the technology of catalyzer be provided, like technological ZL99120517.0, the US4 of following discloses, 875 to reactor drum; 994, US5; 800,697, ZL200610113673.3, ZL200610127585.9 and ZL200710054738.6 etc. all are that water cooler or cooling area are set between reaction-regenerative device, make the regenerated catalyst cooling introduce reactor drum afterwards again and participate in reaction.
Above-mentioned disclosed cooling catalyst technology exists two common ground:
1, adopts lifting and the fluidizing medium of air as water cooler or cooling area;
2, the gases such as flue gas of water cooler or cooling area all return the close phase of revivifier, and it is higher that this is that the gas of considering water cooler or cooling area contains oxygen, returns revivifier and possibly cause the burning of revivifier dilute phase.
But the way that existing employing air is done the water cooler fluidizing medium has been ignored following problems:
1, because these air need supercharging, use the forced air operation, compressor needs driven by motor, has increased plant energy consumption;
2, owing to temperature in external warmer or the cooler reduces; And the catalyzer carbon content in it is also very low; The air that gets into does not react basically, contains a large amount of oxygen, and oxygen level is much higher than the regenerated flue gas that the regenerated catalyst carried through the regeneration standpipe from revivifier carries; This part contains the oxygen air and has also got into reactor drum with catalyst entrainment, O
2With fcc raw material oil reaction (1KgO
2Produce the consumption of 1.4Kg oil product approximately), greatly reduce product yield;
3, also contained N in the air of catalyst entrainment entering reactor drum
2, CO
2Deng composition, these compositions are finally discharged reaction-regenerative device with dry gas, further increase the pneumatic press load.
In a word, owing to get into the gas entrainment of the catalyzer of reactor drum, setting of operation at present or the gas-solid reaction catalytic unit that water cooler is not set are all being born above-mentioned processing charges more or less.
Summary of the invention
The invention provides a kind of gas-solid reaction regenerated catalyst control method; Purpose is both to have realized not using the regenerated catalyst temperature control of forced air; Realize the purification of the gas-entrained impurity of regenerated catalyst again, reducing the gas-solid reaction dry gas that causes because of catalyst entrainment increases; Both realized getting into the control and the reduction of reactor drum oxygen, realized the control and the reduction of the gas gross of entering reactor drum again, increased economic efficiency.
The technical scheme that the present invention adopts is following:
A kind of gas-solid reaction regenerated catalyst control method; Regenerated catalyst in the catalyzer control unit, lower the temperature with Purge gas impurity after get into reactor drum; It is characterized in that: said catalyzer control unit is catalyst transport and fluidizing medium with water vapour; Carry the gas that comprises flue gas that gets in the catalyzer control unit secretly with regenerated catalyst and replaced by water vapour, these gases and water vapour gaseous component return the revivifier dilute phase through the dedicated transport pipeline; In the catalyzer control unit, heat transfer tube is set and controls regenerated catalyst temperature.
Further; The heat transfer tube lower zone is provided with dividing plate or grid stripping internals in the said catalyzer control unit; Increase the replacement result of gas-entrained of water vapour and regenerated catalyst, lower the temperature and the regenerated catalyst that displaces behind the gas of carrying secretly gets into reactor drum again.
Further, water vapour perhaps all gets into the catalyzer control unit respectively below the stripping internals in said stripping internals above and below.
Further, flue gas that displaces and water vapour flow out in catalyzer control unit top area, get into revivifier top freeboard of fluidized bed through line of pipes, avoid with revivifier in catalyzer contact.
Adopt technical scheme of the present invention, solved following problem at least:
1, the present invention uses steam to replace forced air fluidisation catalyzer control unit, cancels the pressurized air fluidizing medium that uses in the conventional catalysis, has reduced the supercharger load;
2, use steam fluidized catalyst control unit, steam is realizing that fluidizing simultaneously, displaces the flue gas of carrying secretly in the catalyzer, prevents that the flue gas that regenerated catalyst carries from getting into reactor drum, realized the purification of gaseous impurities in the catalyzer;
3, go out the flue gas of carrying secretly in the catalyzer with steam stripped, avoided air or O
2Get into reactor drum, prevent the reaction of oxygen and oil product, reduce oil product consumption, improve reaction yield, reduce the exhaust gas volumn in the reaction dry gas, reduce the energy consumption of handling the air compressor machine of dry gas in the conventional catalysis;
4, in the catalyzer control unit stripping member is set, improves the gas displacement effect;
5, fluidization steam vapor returns the revivifier dilute phase, avoid with revivifier in burn the part high-temperature regenerated catalyst contact, prevent the water vapour inactivation, do not influence regeneration, can not cause problems such as dilute phase burning yet.
Description of drawings
Fig. 1 for conventional gas-solid reaction catalytic cracking in the prior art anti--refill and put synoptic diagram.
Fig. 2 for the conventional gas-solid reaction catalytic cracking that water cooler is set in the prior art anti--refill and put synoptic diagram.
Fig. 3 for the gas-solid reaction catalytic cracking that the catalyzer control unit is set of the present invention anti--refill and put synoptic diagram.
Fig. 4-5 is a catalyzer control unit structural representation of the present invention.
Numbering explanation among the figure: 1, reactor drum; 2 settling vessels; 3 stripping stages; 4 reclaimable catalysts; 5 revivifiers; 6 regenerated catalysts; 7 water coolers; 8 cooled catalysts; 9 air; 10 gaseous fractions; 11 reaction oil gas; 12 regenerated flue gas; 13 superchargers; 14 catalyzer control units; 15 revivifier dilute phases; The close phase of 16 revivifiers; 17 catalyst inlets; 18 heat transfer tubes; 19 catalyst outlets; 20 gas distributors; 21 pneumatic outlets; 22 steam; 23 grids.
Embodiment
Gas-solid reaction process catalytic cracking reaction-regenerating unit below in conjunction with conventional in the accompanying drawing specifies technical scheme of the present invention, but protection scope of the present invention includes, but are not limited to this:
As shown in Figure 1, in the prior art conventional catalytic cracking anti--device comprises reactor drum 1 and revivifier 5 again, revivifier 5 comprises the revivifier dilute phase 15 on close phase 16 of the revivifier of bottom and top, is provided with settling vessel 2 and stripping stage 3 in reactor drum 1 outlet.
Regenerated catalyst 6 from the close phase 16 of revivifier gets into reactor drum 1 bottom; Contact the participation catalytic cracking reaction with raw oil; Reclaimable catalyst 4 behind settling vessel 2 sedimentations, stripping stage 3 strippings gets into revivifiers 5, contacts regeneration with regeneration air 9 after supercharger 13 superchargings; Reaction oil gas 11 is drawn settling vessel 2, gets into the subsequent product fractionation and absorbs the steady component operation; Regenerated flue gas 12 is discharged by revivifier 5 top exhanst gas outlets.
Get in the process of reactor drum 1 bottom at regenerated catalyst 6; Because the space that exists between the vesicular structure of catalyst themselves and catalyzer; Carrying the partial regeneration flue gas in the catalyzer inevitably secretly gets in the reactor drum 1 together; Because oxygen level is low in this part flue gas, entrainment is limited, in the processing charges of existing apparatus, ignores basically.
As shown in Figure 2, be that the catalytic cracking that water cooler is set in the prior art instead-is again installed, be provided with water cooler 7 at reactor drum 1 and 5 of revivifiers.
Regenerated catalyst 6 is introduced in the water cooler 7 and cools, and makes fluidizing medium with the air 9 after supercharger 13 superchargings, and cooled catalyst 8 gets into reactor drum 1 bottom, contacts the gas-solid reaction process of participating in raw oil; Gaseous fraction 10 is returned in the close phase 16 of revivifier.
Because the displacement of air 9; Get into the regenerated flue gas major part of carrying secretly in the catalyzer of water cooler 7 and cemented out entering gas 10 by air 9; And return the close phase 16 of revivifier; Replace air and a spot of flue gas of flue gas then to be carried secretly in the entering reactor drum 1,, get into the O of reactor drum 1 because oxygen level is high in the air by catalyzer 8
2Contact with reaction raw materials oil and to burn, cause that the dry gas amount significantly increases in the reaction oil gas 11, the increase of loading of dry gas air compressor machine, this part processing charges is often out in the cold in the optimization of existing gas-solid reaction processing unit (plant).
Fig. 3 for the catalytic cracking that the catalyzer control unit is set of the present invention anti--refill and put synoptic diagram, catalyzer control unit 14 adopts steam 22 as fluidizing medium, gaseous fraction 10 is returned in the revivifier dilute phase 15.
Compare with prior art shown in Figure 2; Because what introduce catalyzer control unit 14 is fluidization steam vapor 22; Getting into the regenerated flue gas major part of carrying secretly in the catalyzer of catalyzer control unit 14 is cemented out by steam 22; Being carried secretly the gas that gets in the reactor drum 1 by catalyzer 8 almost all is oxygen-free steam, and the steam necessary lifting gas that is cracking reaction, thereby has avoided increasing problem because of the dry gas that adopts air 9 fluidisation water coolers 7 to cause in the prior art of Fig. 2; Correspondingly, for preventing the catalyzer hydrothermal deactivation in the revivifier 5, gaseous fraction 10 is returned in the revivifier dilute phase 15, and what returned revivifier 5 this moment is the steam that comprises a small amount of flue gas, the dilute phase combustion phenomena can not take place.
In the regenerated catalyst control method of the present invention; Catalyzer control unit concrete structure is shown in Fig. 4-5: be provided with heat transfer tube 18 in catalyzer control unit 14 housings; The side is provided with catalyst inlet 17, and bottom and top are respectively arranged with catalyst outlet 19 and pneumatic outlet 21; Be provided with gas distributor 20 in heat transfer tube 18 bottoms.
Among the present invention; Heat transfer tube 18 can for along the cooler casing medial shaft to the uniform sleeve pipe in interval that is provided with; Also can be various possibility structural shapes such as coil pipe along the inboard setting of cooler casing; Under the fluidisation of fluidization steam vapor 22, the temperature that gets into the cooled catalyst 8 of reactor drum 1 is in controllable status.
Particularly, regenerated catalyst 6 is introduced in the catalyzer control unit 14 by inlet 17, and under the fluidisation of the steam 22 of introducing gas distributor 20, catalyzer contacts with heat transfer tube 18 and carries out heat exchange, thus the temperature of controlled chilling catalyzer 8; Cooled catalyst 8 is drawn through outlet 19 and is got in the reactor drum 1, and 10 warp outlets 21 of gaseous fraction are returned in the revivifier dilute phase 15, realize the purification of gaseous impurities in the catalyzer.In addition; As shown in Figure 5, in catalyzer control unit 14, grid 23 can also be set, cooled catalyst 8 is before drawing entering reactor drum 1 through outlet 19; The flue gas that goes out to carry secretly through grid 23 strippings earlier, the gas that the catalyzer of entering reactor drum 1 is carried secretly is almost 100% steam.
Grid 23 can also be other stripping internals such as baffle plate.
Embodiment:
In the improved gas-solid reaction process in certain chemical plant, 695 ℃ of revivifier service temperatures, the regenerated catalyst internal circulating load that gets into reactor drum through the regenerated catalyst control unit is 2000t/h; Regenerated catalyst control unit diameter 2800mm, 620 ℃ of controlled temperature are arranged heat transfer tube area 130m in it
2, three layers of grid are set in the heat transfer tube bottom; The fluidizing medium of catalyzer control unit changes employing water vapour into by air, gets into total quantity of steam 3.0t/h of catalyzer control unit, 400 ℃ of vapor temperatures, and pressure 0.6Mpa, steam all get into the regenerated catalyst control unit below grid; Regenerated catalyst gets into the catalyzer control unit through the adapter of diameter 1500mm; Catalyzer control unit bottom is provided with diameter 1200mm catalyst outlet pipe; This outlet pipe is communicated with the reactor drum pre lift zone; Catalyzer control unit overhead vapor and exhanst gas outlet line of pipes are pressed flow velocity 8m/s design, and steam and flue gas select the dilute phase at the following 2000mm of subentry place to get into revivifier in the revivifier one-level.
Install the operation practice and show, the processing charges of relevant public project such as fuel, steam, pressurized air is compared with the preceding employing of transformation air fluidisation can reduce 2-5%.
Claims (4)
1. gas-solid reaction regenerated catalyst control method; Regenerated catalyst in the catalyzer control unit, lower the temperature with Purge gas impurity after get into reactor drum; It is characterized in that: said catalyzer control unit is catalyst transport and fluidizing medium with water vapour; Carry the gas that comprises flue gas that gets in the catalyzer control unit secretly with regenerated catalyst and replaced by water vapour, these gases and water vapour gaseous component return the revivifier dilute phase through the dedicated transport pipeline; In the catalyzer control unit, heat transfer tube is set and controls regenerated catalyst temperature.
2. gas-solid reaction regenerated catalyst control method as claimed in claim 1; It is characterized in that: the heat transfer tube lower zone is provided with dividing plate or grid stripping internals in the said catalyzer control unit; Increase the replacement result of gas-entrained of water vapour and regenerated catalyst, lower the temperature and the regenerated catalyst that displaces behind the gas of carrying secretly gets into reactor drum again.
3. gas-solid reaction regenerated catalyst control method as claimed in claim 2 is characterized in that: water vapour perhaps all gets into the catalyzer control unit respectively below the stripping internals in said stripping internals above and below.
4. gas-solid reaction regenerated catalyst control method as claimed in claim 1; It is characterized in that: said water vapour autocatalysis agent control unit bottom section gets into the catalyzer control unit; Flue gas that displaces and water vapour flow out in catalyzer control unit top area; Get into revivifier top freeboard of fluidized bed through line of pipes, avoid with revivifier in catalyzer contact.
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| CN2011102956069A CN102399575A (en) | 2011-09-27 | 2011-09-27 | Control method of regenerated catalyst for gas-solid reaction |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102942953A (en) * | 2012-11-07 | 2013-02-27 | 石宝珍 | Method for controlling catalyst and heating and cooling regenerant in reaction zone |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1485138A (en) * | 2002-09-28 | 2004-03-31 | 中国石油化工股份有限公司 | Method of eliminating fume for regenerated catalyst |
| CN101474582A (en) * | 2009-01-23 | 2009-07-08 | 中国石油化工集团公司 | Equipment for cooling and stripping regenerated catalyst |
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- 2011-09-27 CN CN2011102956069A patent/CN102399575A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1485138A (en) * | 2002-09-28 | 2004-03-31 | 中国石油化工股份有限公司 | Method of eliminating fume for regenerated catalyst |
| CN101474582A (en) * | 2009-01-23 | 2009-07-08 | 中国石油化工集团公司 | Equipment for cooling and stripping regenerated catalyst |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102942953A (en) * | 2012-11-07 | 2013-02-27 | 石宝珍 | Method for controlling catalyst and heating and cooling regenerant in reaction zone |
| WO2014071842A1 (en) * | 2012-11-07 | 2014-05-15 | Shi Baozhen | Process and apparatus for controlling catalyst in reaction zones, purifying, heat exchanging and cooling regenerant |
| CN102942953B (en) * | 2012-11-07 | 2015-03-04 | 石宝珍 | Method for controlling catalyst and heating and cooling regenerant in reaction zone |
| US9428698B2 (en) | 2012-11-07 | 2016-08-30 | Baozhen Shi | Method and apparatus for controlling catalyst in reaction zones and purifying and cooling regenerated catalyst |
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Application publication date: 20120404 |