CN201485421U - Catalyst cooling equipment for gas-solid reaction - Google Patents
Catalyst cooling equipment for gas-solid reaction Download PDFInfo
- Publication number
- CN201485421U CN201485421U CN2009202233551U CN200920223355U CN201485421U CN 201485421 U CN201485421 U CN 201485421U CN 2009202233551 U CN2009202233551 U CN 2009202233551U CN 200920223355 U CN200920223355 U CN 200920223355U CN 201485421 U CN201485421 U CN 201485421U
- Authority
- CN
- China
- Prior art keywords
- catalyst
- cooling
- gas
- dividing plate
- district
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Images
Abstract
The utility model discloses catalyst cooling equipment for gas-solid reaction, which comprises a casing, a catalyst inlet and a catalyst outlet; a cooling partition board and a catalyst flow control partition board are arranged in the casing; the interior space of the cooling equipment or a cooler is divided into a catalyst conveying area, a catalyst cooling area and a cooling control area; the cooling control area is formed between the catalyst flow control partition board and the cooling partition board; the top edge of the cooling partition board is higher or lower than a catalyst inlet; a heat exchange pipe is mounted in the catalyst cooling area; and one layer of or multiple layers of gas distributors are arranged in the catalyst conveying area, the catalyst cooling area and the cooling control area. The temperature of catalyst entering into a riser reactor can be flexibly adjusted, so that the optimization and control of the catalytic converting reactor-oil ratio can be realized; the partition boards with low cost are combined with the gas distributors to realize cooling control, so that the catalyst can be flexibly adjusted between non-cooling and cooling; and the heat exchange pipe facilitates overhaul and replacement, thereby reducing the use cost.
Description
Technical field
The utility model relates to a kind of petrochemical industry technology, particularly relates to a kind of cooling catalyst equipment that is used for gas-solid phase reaction.
Background technology
Reaction conditions is the important factor of gas-solid phase reaction.The selection of reaction conditions and control are directly connected to reaction conversion ratio and reaction preference in the gas-solid phase reaction process, the technology of existing optimization reactive system operation is a lot, with the catalytic conversion reaction is example, the pre-lift technique of dry gas, mixing temperature control techniques, outlet area sharp separation technology, chilling termination tech etc. all to the reaction result influence obviously, are better used industrial.Many gas-solid reaction process need solid formations such as catalyzer cool off, after being improved, reaction conditions carries out, and especially to gas-solid reaction process as catalytic conversion reaction, can the rising agent oil ratio the suitable cooling of catalyzer, suppress heat cracking reaction, improve the product distribution.
ZL99120517.0 discloses a kind of pipeline of heavy oil catalytic cracking regenerating agent cool-down method, is on the regenerator transfer line heat exchange sleeve to be installed, and the regenerated catalyst after the cooling enters riser reactor and stock oil contact reacts.US4,875, in 994 disclosed residual oil catalysis conversion methods and the device thereof, from in cooler 310, lowering the temperature earlier before demetalization half regenerated catalyst of one section breeding blanket 115 and the vacuum residuum VB contact reacts, enter riser reactor 30 and vacuum distillate VGO contact reacts after lowering the temperature in cooler 410 from the holomorphosis catalyzer of two sections breeding blankets 135, to satisfy the needs of system response control, 310,410 all are provided with heat transfer tube.US5,800,697 disclose a kind of catalytic conversion reaction-renovation process, on revivifier 12 next doors cooling catalyst district 72 is set, from the thermal regenerant of dense bed 66 from export 70 enter cooling area 72 heat exchange to optimal temperature after regeneration standpipe 24, guiding valve 26 enter riser reactor 16 bottoms and participate in reaction, thereby make temperature of reaction become independent variable.ZL200610113673.3 discloses a kind of method for transformation of petroleum hydrocarbon, the regenerated catalyst of heat turns back to reactor bottom by water cooler cooling and contacts with stock oil and carry out cracking reaction, and reclaimable catalyst is through being transported to the mixing tank that recycles after revivifier carries out coke burning regeneration or partly directly enter reactor bottom behind the stripping.ZL200610127585.9 discloses a kind of cracking method for hydrocarbon oil, and the heat exchange in interchanger with hydrocarbon ils and regenerated catalyst makes hydrocarbon ils and the contact reacts in reactor of the regenerated catalyst after the heat exchange after the heat exchange then.ZL200710054738.6 discloses a kind of regenerated catalyst thermoregulation equipment of catalytic cracking unit, on the next door of revivifier dense bed the cooling catalyst device is set, be provided with heat transfer tube in the cooling catalyst device, top is provided with the flue gas return mechanism, along the segmentation of cooling catalyst device vertical height the fluidisation ring is set, the regenerated catalyst through lowering the temperature enters the pre-lifter of riser reactor and participates in reaction.ZL200710054737.1 also discloses a kind of regenerated catalyst thermoregulation device for catalytic cracking equipment, one dividing plate is set in the revivifier dense bed, the revivifier dense bed is divided into two districts, a district is the regeneration scorch region, another district is the cooling catalyst district, the lower partition is provided with the cooler catalyst inlet, and cooling catalyst is provided with heat transfer tube in the district, and the regenerated catalyst through lowering the temperature enters the pre-lifter of riser reactor and participates in reaction.
More than in the disclosed patented technology, heat transfer tube directly is arranged in the thermocatalyst, be that catalyzer is always under the heat exchange state, the catalyzer that participates in follow-up catalyzed reaction all is the catalyzer after the cooling, but in the project implementing process, because feedstock property, field working conditions change, wish that the catalyst temperature that enters reactor can more than have falling temperature technique now and be difficult to reach this requirement according to the needs flexible to the reactive system operation optimization.
The utility model content
The main technical problems to be solved in the utility model, be to provide a kind of cooling catalyst equipment that is used for gas-solid phase reaction, by subregion in cooling system, the catalyzer that needs are sent into reactor is divided into cooling area and cooling area not, control is through the catalyst flow ratio in two districts, flexible enters the catalyst temperature of reactor, thereby improves the agent-oil ratio of catalytic conversion reaction.
The technical solution adopted in the utility model is as follows:
A kind of cooling catalyst equipment that is used for gas-solid phase reaction, this equipment also claims cooler, comprise housing, catalyst inlet, catalyst outlet, it is characterized in that: cooling dividing plate, catalyst flow control dividing plate are set in its housing, is cooling system that the cooler internal space is divided into catalyst transport district, cooling catalyst district and cooling control region, forms the cooling control region between catalyst flow control dividing plate and cooling dividing plate; Cooling dividing plate upper edge is higher or lower than catalyst inlet, in the cooling catalyst district heat transfer tube is installed; In catalyst transport district, cooling catalyst district and the cooling control region one or more layers gas distributor is set.
A kind of cooling catalyst equipment that is used for gas-solid phase reaction of the present utility model, its concrete technical scheme can be that described cooler top is provided with the flue gas purger.
A kind of cooling catalyst equipment that is used for gas-solid phase reaction of the present utility model, its concrete technical scheme also can be: described cooling dividing plate, catalyst flow control dividing plate are interior bucket formulas or cut apart baffle plate type.
A kind of cooling catalyst equipment that is used for gas-solid phase reaction of the present utility model, its concrete technical scheme also can be: when cooling dividing plate upper edge is higher than catalyst inlet, can on this lowers the temperature dividing plate, opening be set catalyst inlet height zone, make catalyzer can enter cooling dividing plate both sides simultaneously.
A kind of cooling catalyst equipment that is used for gas-solid phase reaction of the present utility model, its concrete technical scheme also can be: the partition flange is installed on housing top, housing is divided into the heat transfer tube construction section on top, main housing two parts of bottom, and heat transfer tube is installed on the heat transfer tube construction section; To solve the problem that heat transfer tube is fragile in the cooler, inconvenience is overhauled.
Heat transfer tube described in the utility model can be along the inboard coil pipe that is provided with of cooling catalyst device housing, also can be along the tubular distance piece of housing medial shaft to setting, also can be other forms of heat transfer tube.
Task of the present utility model is achieved in that the thermocatalyst after the regeneration enters the cooling catalyst device, when the catalytic conversion reaction system does not require when thermocatalyst lowered the temperature,
Task of the present utility model is achieved in that
1, the thermocatalyst after the regeneration enters the cooling catalyst device, when the catalytic conversion reaction system does not require when thermocatalyst lowered the temperature, the cooling catalyst district or (with) cooling control region gas distributor be in closing condition, this moment, the catalyzer in cooling catalyst district did not carry out heat exchange with heat transfer tube, thermocatalyst from revivifier only enters the catalyst transport district, thermocatalyst directly flow through under the fluidizing medium effect in catalyst transport district catalyst transport district, catalyst outlet flow out cooler and enter reactor and participate in reaction;
2, thermocatalyst after the regeneration enters the cooling catalyst device, when the catalytic conversion reaction system requirements is lowered the temperature to thermocatalyst, the cooling catalyst district, the gas distributor of catalyst transport district and cooling control region is in opened condition simultaneously, this moment, the catalyzer in above-mentioned three districts all was in fluidized state, thermocatalyst from revivifier enters cooling catalyst district and catalyst transport district simultaneously, thermocatalyst and the heat transfer tube that enter the cooling catalyst district this moment carry out heat exchange, temperature reduces, regulate the fluidizing medium amount of cooling catalyst district or cooling control region, the cooling catalyst district, the catalyzer in the pressure official post cooling catalyst district of cooling control region is constantly carried to the cooling control region, thereby the exchange of realization catalyzer reaches and mixes with the thermocatalyst in catalyst transport district, form the mixed catalyst of lesser temps, flow out cooler through catalyst outlet, enter reactor and participate in catalyzed reaction; When the regenerated catalyst in the utility model is flowed through cooler, can make 0 ℃-160 ℃ of regenerator coolings, the regenerator after the cooling do not return revivifier but directly the dereaction device contact with stock oil and carry out catalytic conversion reaction.
Fluidizing medium described in the utility model is generally pressurized air or water vapor.When being fluidizing medium with the water vapor, water vapor both can play rheomorphism, also can play the effect of the nitrogenous gas of carrying secretly in the stripping catalyst such as nitrogen simultaneously, can partly avoid causing the problem of catalytic conversion reaction selectivity variation because of the catalyst entrainment nitrogenous gas.The fluidizing medium of respectively distinguishing described in the utility model is all independently controlled separately, and flow can be regulated by corresponding gas distributor respectively according to processing requirement.
The utility model compared with prior art, its beneficial effect is:
At first, the utility model is because subregion is carried out in employing in the cooling catalyst device, make the catalyst temperature that enters riser reactor can flexible, can select thermocatalyst " zero " heat exchange or part heat exchange according to reactive system processing condition needs and working condition requirement, thereby realization is to the optimization and the control of catalytic conversion reaction agent-oil ratio;
The second, adopt cost to drop into the dividing plate bound gas divider of easily making on low, the engineering and realize the Creative Design of cooling control region, efficiently solve the flexible of catalyzer between not lowering the temperature, lowering the temperature;
The 3rd, the utility model is that the partition flange is installed on the cooler housing at cooling system, and heat transfer tube easy access and replacing have reduced use cost;
The 4th, cooling system of the present utility model be cooler finish regulate enter the catalyst temperature of reactor in, can also play the effect of degassing vessel, adopt cool-down method of the present utility model and equipment, can save the degassing vessel that existing regenerating unit generally adopts, perhaps the existing degassing vessel of regenerating unit is transformed, be transformed into cooler thereby heat transfer tube is installed.
Description of drawings
Fig. 1: a kind of cooling catalyst method reaction-regenerative device synoptic diagram that is used for gas-solid phase reaction of the present utility model.
Fig. 2-4: a kind of cooling catalyst equipment that is used for gas-solid phase reaction of the present utility model is the cooler structural representation.
Fig. 5-7: cooling catalyst device A-A, B-B, C-C sectional view among Fig. 2 of the present utility model-4.
Fig. 8: catalyst stream is through cooler shown in Figure 2 temperature reduction technology schematic flow sheet not.
Fig. 9: catalyst stream is through cooler temperature reduction technology schematic flow sheet shown in Figure 3.
Figure 10: catalyst stream is through cooler temperature reduction technology schematic flow sheet shown in Figure 4.
Number description: I cooling catalyst district; II catalyst transport district; The III control region that lowers the temperature; 1 reactor; 2 settling vessels; 3 stripping stages; 4 inclined tubes to be generated; 5 guiding valves to be generated; 6 revivifiers; 7,9 regenerator sloped tubes; 71 catalyst inlets; 8a, 8b, 8c cooling catalyst device; 91 catalyst outlets; 10 regeneration guiding valves; 11 flue gas purgers; 12 housings; 19 main housings; 20 heat transfer tube construction sections; 13a, the 13b dividing plate of lowering the temperature; 14 heat transfer tubes; 15a, 15b catalyst flow control dividing plate; 16a, 16b, 16c gas distributor; 17 cooling dividing plate openings; 18 partition flanges; 22,23,24 catalyzer; 33,34,35 pressurized air; 44 flue gases; α cooling dividing plate opening angle.
Embodiment
Describe the technical solution of the utility model in detail below in conjunction with accompanying drawing, but protection domain of the present utility model includes, but are not limited to this:
Fig. 1 is a kind of cooling catalyst method reaction-regenerative device synoptic diagram that is used for gas-solid phase reaction of the present utility model.Cooling catalyst device 8a is installed on the regenerator sloped tube 7,9 between reactor 1 and the revivifier 6, and the 8a top is provided with flue gas purger 11; Its technical process is as follows: the catalyzer in revivifier 6 after the regeneration enters cooler 8a through regenerator sloped tube 7, flue gas returns revivifier 6 by 11, thermocatalyst is not through lowering the temperature or partly flowing out 8a after the cooling, enter reactor 1 by regenerator sloped tube 9, guiding valve 10, the conveying that continues to make progress under the lifting vapor action contacts with stock oil reacts, and catalyzer enters revivifier 6 by regeneration standpipe 4, guiding valve 5 at settling vessel 2, stripping stage 3 respectively and regenerates behind separation, stripping.
Fig. 2 is the cooler structural representation for a kind of cooling catalyst equipment that is used for gas-solid phase reaction of the present utility model, cooling catalyst device 8a of the present utility model, its A-A to sectional view as shown in Figure 5, comprise housing 12, catalyst inlet 71, catalyst outlet 91, the interior bucket of housing 12 usefulness formula cooling dividing plate 13a, catalyst flow control dividing plate 15a is divided into catalyst transport district II, cooling catalyst district I and cooling control region III three parts, vertically be provided with heat transfer tube 14 in the cooling control region III, I, each district of II and III is provided with gas distributor 16a respectively, 16c and 16b, cooling dividing plate 13a upper edge is lower than catalyst inlet 71, and cooler 8a top is provided with flue gas purger 11.
Fig. 3 is the cooler structural representation for the cooling catalyst equipment that another kind of the present utility model is used for gas-solid phase reaction, cooling catalyst device 8b of the present utility model, its A-A to sectional view as shown in Figure 5, B-B to sectional view as shown in Figure 6, an interior bucket formula cooling dividing plate 13a upper edge is higher than catalyst inlet 71, arc cooling dividing plate opening 17 is set in catalyst inlet 71 vertical height zones, and cooling dividing plate opening 17 opening angle α are between 30 °-360 °; Partition flange 18 is installed on housing 12, housing 12 is divided into the heat transfer tube construction section 20 on top, main housing 19 2 parts of bottom, heat transfer tube 14 is installed on 20; The same Fig. 2 of all the other position structures; Can pull down 20 during maintenance, change maintenance heat transfer tube 14, need not large-scale lifting rig.
Fig. 4 is the cooler structural representation for the cooling catalyst equipment that the third is used for gas-solid phase reaction of the present utility model, cooling catalyst device 8c of the present utility model, its C-C to sectional view as shown in Figure 7, housing 12 usefulness separation baffles formulas coolings dividing plate 13b, catalyst flow control dividing plate 15b are divided into catalyst transport district II, cooling catalyst district I and cooling control region III three parts; The same Fig. 2 of all the other position structures.
Fig. 8 is the not temperature reduction technology schematic flow sheet of thermocatalyst by cooler 8a shown in Figure 2: thermocatalyst 22 enters cooler 8a through catalyst inlet 71, enter catalyst transport district II by cooling dividing plate 13a upper edge, flow downward along II, flow out cooler 8a through catalyst outlet 91, flue gas 44 is returned in the revivifier 6 by the flue gas purger 11 at housing 12 tops.Cooler 8a plays the effect of circulation pipeline and degassing vessel in this scheme.
Fig. 9 is the part temperature reduction technology schematic flow sheet of thermocatalyst by cooler 8b shown in Figure 3: thermocatalyst 22 is divided into two portions after catalyst inlet 71 enters cooler 8b, the arc opening 17 of part thermocatalyst 24 on cooling dividing plate 13a enters catalyst transport district II and flows downward along II, another part catalyzer 23 enters among the cooling catalyst district I and carries out heat exchange with heat transfer tube 14, the temperature of catalyzer is by the amount control of the pressurized air 35 that enters cooling control region III and cooling area I and 34 among the I, catalyzer 23 after this cooling contacts with thermocatalyst 24 and forms mixed catalyst 25, flow out cooler 8b through catalyst outlet 91, flue gas 44 is returned in the revivifier 6 by flue gas purger 11, and cooler 8b plays the effect of cooler and degassing vessel in this scheme.
Figure 10 is the part temperature reduction technology schematic flow sheet of thermocatalyst by cooler 8c shown in Figure 4: thermocatalyst 22 is divided into two portions after catalyst inlet 71 enters cooler 8c, part thermocatalyst 24 flows downward along catalyst transport district II, another part thermocatalyst 23 enters among the cooling catalyst district I and carries out heat exchange with heat transfer tube 14, the temperature of catalyzer is by the amount control of the pressurized air 35 that enters cooling control region III and cooling area I and 34 among the I, catalyzer 23 after this cooling contacts with thermocatalyst 24 and forms mixed catalyst 25, flow out cooler 8c through catalyst outlet 91, flue gas 44 is returned in the revivifier 6 by flue gas purger 11.
Embodiment:
Embodiment 1, certain annual output 100 * 10
4The catalytic unit of t/a, reaction mass: the defeated atmospheric residue of pipe, 220 ℃ of preheatings; Adopt conventional catalytic cracking catalyst; Reactor is the riser tube form, 500 ℃ of riser tube temperature outs, reaction times 2.5s; 685 ℃ of regeneration temperatures.The cooler of structure as shown in Figure 2 is set on the regenerator sloped tube between reaction-regenerative device, and cooling dividing plate, catalyst flow control dividing plate are interior bucket formula, and heat transfer tube is the sleeve pipe form, adopts water at low temperature to make heat transferring medium; 685 ℃ the catalyzer of 60Kg/h enters cooler, 40% catalyzer is arranged through the delivery area, and delivery area fluidization air flow is per hour 60 liters of every kg catalyst.After the heat exchange temperature be 640 ℃ catalyzer through regeneration guiding valve enter reactor.
Embodiment 2, cooler structure such as Fig. 4, cooling dividing plate, catalyst flow control dividing plate are for cutting apart baffle plate type, and heat transfer tube is the sleeve pipe form, adopts water at low temperature to make heat transferring medium; 685 ℃ the catalyzer of 60Kg/h enters cooler, 60% catalyzer is arranged through the delivery area, and delivery area fluidization air flow is per hour 70 liters of every kg catalyst.After the heat exchange temperature be 655 ℃ catalyzer through regeneration guiding valve enter reactor.Rest part is with embodiment 1.
Claims (6)
1. cooling catalyst equipment that is used for gas-solid phase reaction, comprise housing (12), catalyst inlet (71), catalyst outlet (91), it is characterized in that: cooling dividing plate (13a, 13b), catalyst flow control dividing plate (15a, 15b) are set in the described housing, is cooling system that cooler (8a, 8b, 8c) internal space is divided into catalyst transport district (II), cooling catalyst district (I) and cooling control region (III), forms cooling catalyst control region (III) between catalyst flow control dividing plate (15a, 15b) and cooling dividing plate (13a, 13b); Cooling dividing plate (13a, 13b) upper edge is higher or lower than catalyst inlet (71), and heat transfer tube (14) is installed in cooling catalyst district (I); In catalyst transport district (II), cooling catalyst district (I) and the cooling control region (III) one or more layers gas distributor (16a, 16b, 16c) is set.
2. a kind of cooling catalyst equipment that is used for gas-solid phase reaction according to claim 1 is characterized in that: described cooler (8a, 8b, 8c) top is provided with flue gas purger (11).
3. a kind of cooling catalyst equipment that is used for gas-solid phase reaction according to claim 1 is characterized in that: described cooling dividing plate (13a, 13b), flow control dividing plate (15a, 15b) are interior bucket formulas or cut apart baffle plate type.
4. a kind of cooling catalyst equipment that is used for gas-solid phase reaction according to claim 1 is characterized in that: when described cooling dividing plate (13a) upper edge was higher than catalyst inlet (71), catalyst inlet height zone was provided with opening on this cooling dividing plate.
5. a kind of cooling catalyst equipment that is used for gas-solid phase reaction according to claim 1, it is characterized in that: partition flange (18) is installed on described housing (12) top, housing is divided into the heat transfer tube construction section (20) on top, main housing (19) two parts of bottom, and heat transfer tube (14) is installed on the heat transfer tube construction section.
6. a kind of cooling catalyst equipment that is used for gas-solid phase reaction according to claim 1 is characterized in that: described heat transfer tube (14) can be along the inboard coil pipe that is provided with of cooling catalyst device housing, also can be along the housing medial shaft to the tubular distance piece that is provided with.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202233551U CN201485421U (en) | 2009-09-01 | 2009-09-01 | Catalyst cooling equipment for gas-solid reaction |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202233551U CN201485421U (en) | 2009-09-01 | 2009-09-01 | Catalyst cooling equipment for gas-solid reaction |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201485421U true CN201485421U (en) | 2010-05-26 |
Family
ID=42424310
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009202233551U Expired - Lifetime CN201485421U (en) | 2009-09-01 | 2009-09-01 | Catalyst cooling equipment for gas-solid reaction |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201485421U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101665714A (en) * | 2009-09-01 | 2010-03-10 | 青岛京润石化设计研究院有限公司 | Method and equipment for cooling catalyst for gas-solid reaction |
| 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 |
| US9353316B2 (en) | 2011-06-15 | 2016-05-31 | Baozhen Shi | Method and device for catalytic cracking |
-
2009
- 2009-09-01 CN CN2009202233551U patent/CN201485421U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101665714A (en) * | 2009-09-01 | 2010-03-10 | 青岛京润石化设计研究院有限公司 | Method and equipment for cooling catalyst for gas-solid reaction |
| CN101665714B (en) * | 2009-09-01 | 2012-09-05 | 青岛京润石化设计研究院有限公司 | Method and equipment for cooling catalyst for gas-solid reaction |
| US9353316B2 (en) | 2011-06-15 | 2016-05-31 | Baozhen Shi | Method and device for catalytic cracking |
| 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 |
| 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 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102942953B (en) | Method for controlling catalyst and heating and cooling regenerant in reaction zone | |
| CN105505441A (en) | Catalytic cracking reaction regeneration method and device | |
| US9353316B2 (en) | Method and device for catalytic cracking | |
| CN1830926B (en) | Oxygenate conversion reactor catalyst coolers | |
| CN102277193B (en) | Method and apparatus for catalytic cracking | |
| CN103540345B (en) | Catalytic cracking method | |
| CN101665714B (en) | Method and equipment for cooling catalyst for gas-solid reaction | |
| CN105849235A (en) | Regeneration method for catalytic cracking reaction | |
| CN101745435A (en) | Regeneration method and device of catalyst of fluid catalytic cracking | |
| EP1664650B1 (en) | Apparatus and process for cooling hot gas | |
| CN201485421U (en) | Catalyst cooling equipment for gas-solid reaction | |
| CN103540346B (en) | A kind of Desending catalytic cracking device | |
| CN1888025B (en) | Catalytic conversion method and apparatus | |
| CN104946305B (en) | A kind of Catalytic Cracking Unit of Measure induction method | |
| CN104342196A (en) | Catalytic cracking method and device thereof | |
| CN104419458A (en) | Catalytic cracking method and device | |
| CN103788993A (en) | Catalytic cracking unit | |
| CN102399579B (en) | Catalytic cracking method | |
| CN206428195U (en) | A kind of catalysis drying gas aromatisation gasoline shell and tube reactor | |
| CN113522371B (en) | Stripping cooling equipment and method for regenerated catalyst | |
| CN210434485U (en) | Slurry bed reactor and reaction system for Fischer-Tropsch synthesis | |
| CN101659601B (en) | Method and device for producing dimethyl ether by using methanol | |
| CN104513670B (en) | A kind of catalyst cracking method and device | |
| CN100455640C (en) | Hydrocarbons raw material double lifting leg catalytic conversion apparatus | |
| CN201962247U (en) | Catalytic cracking device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20100526 Effective date of abandoning: 20090901 |