CN205115391U - Catalytic cracking reactor - Google Patents
Catalytic cracking reactor Download PDFInfo
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- CN205115391U CN205115391U CN201520785184.7U CN201520785184U CN205115391U CN 205115391 U CN205115391 U CN 205115391U CN 201520785184 U CN201520785184 U CN 201520785184U CN 205115391 U CN205115391 U CN 205115391U
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- 238000004523 catalytic cracking Methods 0.000 title abstract description 15
- 239000003054 catalyst Substances 0.000 claims abstract description 37
- 230000000116 mitigating effect Effects 0.000 claims description 19
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 17
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 17
- 239000004571 lime Substances 0.000 claims description 17
- 238000012546 transfer Methods 0.000 claims description 17
- 230000002040 relaxant effect Effects 0.000 claims description 8
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 239000003921 oil Substances 0.000 abstract description 32
- 239000007789 gas Substances 0.000 abstract description 22
- 238000006243 chemical reaction Methods 0.000 abstract description 21
- 238000005336 cracking Methods 0.000 abstract description 14
- 238000000034 method Methods 0.000 abstract description 11
- 230000035484 reaction time Effects 0.000 abstract description 11
- 239000000295 fuel oil Substances 0.000 abstract description 10
- 239000003915 liquefied petroleum gas Substances 0.000 abstract description 7
- 239000002006 petroleum coke Substances 0.000 abstract 1
- 239000012492 regenerant Substances 0.000 abstract 1
- 239000000571 coke Substances 0.000 description 7
- 239000000047 product Substances 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 238000011160 research Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000004231 fluid catalytic cracking Methods 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 239000003209 petroleum derivative Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000010517 secondary reaction Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000012512 characterization method Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000006276 transfer reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model provides a catalytic cracking reactor is applied to heavy oil catalytic cracking process with it. Include: the regenerant conveyer pipe, finish mixed zone, abundant contact zone and the relaxed contact zone that from top to bottom connect gradually, set up the catalyst deconcentrator of cone at the top of finish mixed zone, the maximum diameter department of finish mixed zone sets up a plurality of nozzles that tilt up set up. Traditional riser reactor has been overcome because riser overlength and the problem of the catalyst landing that leads to the fact, the aggravation of back mixing degree and two secondary responses of cracking result to catalyst and oil gas downward flow to the reaction degree of cracking has been reduced, current down tubular reactor's the finish contact problem that efficiency is not high, the heavy oil conversion degree of depth is not enough has been avoided again. The utility model discloses a suitable short contact reaction time of finish to reduce dry gas, liquefied petroleum gas and coke yield, improve the productivity and the quality of light oil yield.
Description
Technical field
The utility model belongs to the catalytic cracking technology field of petroleum hydrocarbon in non-hydrogen situation, particularly be a kind of catalyst cracker, be mainly used in the technological process of heavy oil fluid catalytic cracking.
Background technology
Catalytic cracking is a most important course of processing in oil secondary processing.In recent years, demand that is heavy and environmentally friendly fuel oil is day by day become for stock oil, domestic and international each major oil companies, research institution and large universities and colleges around optimizing catalytic cracking reaction further, improve transformation efficiency, improve product slates and conduct in-depth research, various new technology, new installation and new catalyst constantly occur, facilitate the development of catalytic cracking process technology to some extent.
But, along with heaviness and the in poor quality of crude oil, as traditional riser reactor of catalytic cracking reaction process, be mainly manifested in that riser tube is long causes the reaction times long; Catalyzer due to downward action of gravity, inevitably produces landing and air-teturning mixed phenomenon in riser tube; Along with the heaviness of stock oil and the raising to product selectivity requirement, the problem that riser reactor brings because of catalyzer landing and back-mixing is also day by day obvious.
Riser catalytic cracking makes its activity and selectivity decline and owing to warmly changing and the phenomenon such as nonideal secondary reaction generation due to catalyst carbon deposit, the selectivity of catalytic cracking product and the quality of cracked product are had a great impact, dry gas and coke yield high, light oil yield is low, poor product quality, in catalytically cracked gasoline, olefin(e) centent is high.
In order to overcome above-mentioned shortcoming, domestic and international each major oil companies, research unit and refining of petroleum investigator do a lot of work, in succession develop multi-form finish short contact catalytic cracking technology, its objective is the back-mixing overcome to greatest extent between oil gas and catalyzer, reduce the generation of secondary cracking and hydrogen transfer reactions, make the selectivity of cracked product good, dry gas, coke yield reduce, light oil yield is high, and the quality of cracked product is good.
US Patent No. 4985136, USP5462652 disclose a kind of super short contact time catalyst cracking method, i.e. MSCC.In the method, catalyzer flows downward in the form of a curtain whereby, and petroleum hydrocarbon vertically sprays into this catalyzer with in curtain, after reaction product and levels of catalysts pass reaction zone, and oil agent mixture sharp separation; Catalyzer after part stripping directly enters catalyst mix device, with the catalyst mix after holomorphosis, with rising agent oil ratio without regeneration.Although the method improves the concentration of finish initial contact section catalyzer by the way adding high agent-oil ratio, but fully transform required concentration because catalyzer can not reach heavy oil in freely falling body process, therefore also there is finish contact efficiency not high, the problem that the heavy oil conversion degree of depth is inadequate.
Utility model content
The purpose of this utility model is to provide a kind of catalyst cracker, is applied to heavy oil catalytic cracking process process, reduces dry gas, liquefied petroleum gas (LPG) and coke yield, improves productive rate and the quality of light oil yield.
The catalyst cracker that the utility model provides, comprising: the regenerator transfer lime from top to bottom connected successively, finish mixing zone, fully zone of action and mitigation zone of action;
Catalyzer decollator is set at the top of finish mixing zone, and catalyzer decollator is positioned at and rises agent transfer lime again;
Described catalyzer decollator is the cone just put;
Described finish mixing zone is that just to put the top, finish mixing zone of round platform and shape be that the bottom, finish mixing zone of inverted round table is formed by shape, and arranges at the maximum diameter place of finish mixing zone the multiple nozzles being inclined upwardly and arranging.
Further, described regenerator transfer lime, catalyzer decollator, finish mixing zone, fully zone of action and mitigation zone of action are coaxially arranged.
Further, described abundant zone of action is the region that a cylinder is formed.
Further, described mitigation zone of action is formed by relaxing zone of action extension diameter section and relaxing zone of action straight length; Described mitigation zone of action extension diameter section is a round platform just put.
Further, described catalyzer decollator is connected and fixed by web member and regenerator transfer lime.
Further, the ratio of the maximum diameter of described finish mixing zone and the end face diameter on top, finish mixing zone is 1.5 ~ 8.0; The sidewall of bottom, finish mixing zone and horizontal plane angle are 60 ° ~ 85 °.
In finish mixing zone, regenerated catalyst contacts with the fogging oil gas backmixing from nozzle, and the short contact reaction times can be 0.1 ~ 0.3 second.
Further, the ratio of the diameter of described abundant zone of action and the maximum diameter of finish mixing zone is 1/8 ~ 2/3; The ratio of the height of described abundant zone of action and the diameter of abundant zone of action is 0.5 ~ 30.
Abundant zone of action is the straight length space of a undergauge relative to finish mixing zone, and catalyzer is fully contacted with stock oil, and with the mode rapid rundown of piston flow, the reaction times can be 0.1 ~ 0.5 second.
Further, the ratio of the diameter of described mitigation zone of action straight length and the diameter of abundant zone of action is 1.5 ~ 8.0.
The caliber relaxing the relatively abundant zone of action of reaction compartment of zone of action expands gradually, and finish contact probability weakens relatively, owing to reducing the concentration of catalyzer, thus reduces the level of response of cracking, suppresses the generation of cracking reaction.
Further, the base angle of described catalyzer decollator is 5 ° ~ 45 °; The cone surface of described catalyzer decollator is uniformly distributed some small sircle holes, and the diameter of small sircle hole is 5 ~ 50mm;
The ratio of the diameter of described catalyzer decollator and the end face diameter on top, finish mixing zone is 2/3 ~ 5/6.
Further, the angle of described nozzle and horizontal plane is 5 ° ~ 45 °, and the quantity of nozzle is 1 ~ 30, is along the circumferential direction evenly arranged.
Further, the pipeline in described catalyst cracker assembly and connectedness all adopt metal stainless material to make, the equal liner insulated lining of all the other each several parts.
The beneficial effects of the utility model are:
Finish contact reacts mainly in finish mixing zone, fully, carry out by zone of action and mitigation these three regions, zone of action.After finish contact, catalyzer and oil gas flow downward, overcome conventional lift pipe reactor long due to riser tube and cause catalyzer landing, the aggravation of back-mixing degree and the problem of cracked reaction product secondary reaction, thus reduce the level of response of cracking; Turn avoid in existing descending tubular reactor simultaneously, fully transform required concentration and the problem that finish contact efficiency is not high, the heavy oil conversion degree of depth is inadequate brought because catalyzer can not reach heavy oil in freely falling body process.
The catalyst cracker that the utility model provides, due to the structure formation of uniqueness, have employed the short contact reaction times that finish is suitable, thus reduces dry gas, liquefied petroleum gas (LPG) and coke yield, improves productive rate and the quality of light oil yield.
The catalyst cracker that the utility model provides is compared with Conventional catalytic cracking riser reactor, reaction times shortens greatly, in finish mixing zone and mitigation zone of action, owing to reducing the concentration of catalyzer, because this reducing the level of response of cracking, thus inhibit the generation of cracking phenomenon, reduce dry gas and coke yield.
Accompanying drawing explanation
In order to be illustrated more clearly in the utility model embodiment or technical scheme of the prior art, be briefly described to the accompanying drawing used required in embodiment or description of the prior art below, apparently, accompanying drawing in the following describes is embodiments more of the present utility model, for those of ordinary skill in the art, under the prerequisite not paying creative work, other accompanying drawing can also be obtained according to these accompanying drawings.
The one-piece construction schematic diagram of the catalyst cracker that Fig. 1 provides for the utility model embodiment;
Fig. 2 is the front view of the conical catalyzer decollator in Fig. 1;
Fig. 3 is the vertical view of the conical catalyzer decollator in Fig. 1;
Reference numeral:
1-regenerator transfer lime; 2-catalyzer decollator;
3-web member; Top, 4-finish mixing zone;
5-nozzle; Bottom, 6-finish mixing zone;
7-abundant zone of action cylindrical shell; 8-relaxes zone of action extension diameter section;
9-relaxes zone of action straight length; I-finish mixing zone;
II-fully zone of action; III-relax zone of action;
The base angle of α-catalyzer decollator; The angle of β-nozzle and horizontal plane;
The sidewall of γ-bottom, finish mixing zone and horizontal plane angle
The end face diameter on top, D1-finish mixing zone;
The diameter of D2-catalyzer decollator;
The maximum diameter of D3-finish mixing zone;
The diameter of the abundant zone of action of D4-;
D5-relaxes the diameter of zone of action straight length;
The height of the abundant zone of action of H-;
The diameter of M-small sircle hole.
Embodiment
Be clearly and completely described the technical solution of the utility model below in conjunction with accompanying drawing, obviously, described embodiment is the utility model part embodiment, instead of whole embodiments.Based on the embodiment in the utility model, those of ordinary skill in the art are not making the every other embodiment obtained under creative work prerequisite, all belong to the scope of the utility model protection.
In description of the present utility model, it should be noted that, orientation or the position relationship of the instruction such as term " " center ", " on ", D score, "left", "right", " vertically ", " level ", " interior ", " outward " they be based on orientation shown in the drawings or position relationship; be only the utility model and simplified characterization for convenience of description; instead of instruction or imply the device of indication or element must have specific orientation, with specific azimuth configuration and operation, therefore can not be interpreted as restriction of the present utility model.In addition, term " first ", " second ", " the 3rd " only for describing object, and can not be interpreted as instruction or hint relative importance.
In description of the present utility model, it should be noted that, unless otherwise clearly defined and limited, term " installation ", " being connected ", " connection " should be interpreted broadly, and such as, can be fixedly connected with, also can be removably connect, or connect integratedly; Can be mechanical connection, also can be electrical connection; Can be directly be connected, also indirectly can be connected by intermediary, can be the connection of two element internals.For the ordinary skill in the art, particular case the concrete meaning of above-mentioned term in the utility model can be understood.
The one-piece construction schematic diagram of the catalyst cracker that Fig. 1 provides for the utility model embodiment.
In the present embodiment, catalyst cracker forms primarily of the regenerator transfer lime 1 from top to bottom coaxially arranged successively, finish mixing zone I, fully zone of action II, mitigation zone of action III.
Described finish mixing zone I is made up of top, finish mixing zone 4 and bottom, finish mixing zone 6.Top, finish mixing zone 4 and bottom, finish mixing zone 6 are coaxially arranged, and top, finish mixing zone 4 is positive round platforms, and bottom, finish mixing zone 6 is inverted round stages.
Described abundant zone of action II is a cylindrical area.Relaxing zone of action III is be made up of mitigation zone of action extension diameter section 8 and mitigation zone of action straight length 9, and mitigation zone of action extension diameter section 8 is a positive round platform.
Nozzle 5 is arranged at the maximum diameter place of finish mixing zone I, i.e. the interfaces place of top, finish mixing zone 4 and bottom, finish mixing zone 6.
Catalyzer decollator 2 is a cone just put, and is arranged at the top of finish mixing zone I, and is positioned at the central position of regenerator transfer lime 1, and catalyzer decollator 2 is linked together by web member 3 and regenerator transfer lime 1.
In finish mixing zone, regenerated catalyst contacts with the fogging oil gas backmixing from nozzle 5, and short contact is reacted.Reaction times can be 0.1 ~ 0.3 second; The maximum dimension D 3 of finish mixing zone can be 1.5 ~ 8.0, in the present embodiment with the ratio of the end face diameter D1 (i.e. the diameter of regenerator transfer lime) on top, finish mixing zone, and this ratio set is 2; The sidewall of bottom, finish mixing zone and horizontal plane angle γ can be 60 ° ~ 85 °.
Described abundant zone of action II is the straight length space of a undergauge relative to finish mixing zone I, and make catalyzer and stock oil fully contact mode rapid rundown with piston flow, the reaction times can be 0.1 ~ 0.5 second.The ratio of the diameter D4 of abundant zone of action and the maximum dimension D 3 of finish mixing zone can be 1/8 ~ 2/3, in the present embodiment, and this ratio set is 3/8.According to reaction times requirement, the ratio of the height H of abundant zone of action and the diameter D4 of abundant zone of action can be 0.5 ~ 30, in the present embodiment, and this ratio set is 0.6.
The reaction compartment of described mitigation zone of action III expands gradually relative to the caliber of abundant zone of action II, and finish contact probability weakens relatively, owing to reducing the concentration of catalyzer, thus reduces the level of response of cracking, suppresses the generation of cracking reaction.The ratio relaxing the diameter D5 of zone of action straight length and the diameter D4 of abundant zone of action can be 1.5 ~ 8.0, in the present embodiment, and this ratio set is 2.
The base angle of described catalyzer decollator can be 5 ° ~ 45 °.Cone surface is uniformly distributed a lot of small sircle hole, the diameter M of small sircle hole can be 5 ~ 50mm.The ratio of the diameter D2 of catalyzer decollator and the end face diameter D1 on top, finish mixing zone can be 2/3 ~ 5/6.
The angle β of nozzle and horizontal plane can be 5 ° ~ 45 °, and the quantity of nozzle 5 can be 1 ~ 30, is uniformly distributed circumferentially.
Pipeline in catalyst cracker assembly and connectedness all adopt metal stainless material to make, the equal liner insulated lining of all the other each several parts.
Regenerated catalyst is sent into by regenerator transfer lime 1 in catalyst cracker top, and bottom is by relaxing zone of action straight length 9 ligation settlement separator.
The technological process that use utility model carries out heavy oil fluid catalytic cracking is as follows:
The conical catalyzer decollator 2 that is regenerated catalyst through from regenerator transfer lime 1 enters finish mixing zone I;
In finish mixing zone I, small sircle hole on part catalyzer is distributed by cone surface is dispersed, the annular space that another part catalyzer is then formed by catalyzer decollator 2 and regenerator transfer lime 1 falls downwards, contact to of short duration with the fogging oil circulation of vital energy in the wrong direction from nozzle 5, the oil gas that reaction generates and unreacted raw material oil gas and catalyzer flow downward, by abundant zone of action II;
Abundant zone of action II is the straight length space of undergauge, and in this region, catalyzer and stock oil fully contact the mode rapid rundown with piston flow, and short contact catalytic cracking reaction occurs; The oil gas that reaction generates and unreacted oil gas and catalyzer continue to flow downward to enter and relax zone of action III;
In mitigation zone of action III, the catalyzer having neither part nor lot in reaction continues and the reaction of unreacted oil gas generation short contact, and flows rapidly into reaction settlement separator, carries out reaction oil gas and catalyst separating.
Reaction oil gas and after stripping oil gas enter fractionating system, reaction knot carbon catalyzer be transported to after water vapor stripping revivifier regeneration, regenerated flue gas enters flue-gas-cooling system.Regenerated catalyst after regeneration continues and raw material oil gas generation cracking reaction after catalyzer decollator 2 disperses through regenerator transfer lime 1, carries out going round and beginning again circular flow.
The utility model have employed the finish suitable short contact reaction times, thus reduces dry gas, liquefied petroleum gas (LPG) and coke yield, improves productive rate and the quality of light oil yield; Compared with Conventional catalytic cracking riser reactor, the reaction times shortens greatly, in finish mixing zone and mitigation zone of action, owing to reducing the concentration of catalyzer, because this reducing the level of response of cracking, thus inhibit the generation of cracking phenomenon, reducing dry gas and coke yield.
Last it is noted that above each embodiment is only in order to illustrate the technical solution of the utility model, be not intended to limit; Although be described in detail the utility model with reference to foregoing embodiments, those of ordinary skill in the art is to be understood that: it still can be modified to the technical scheme described in foregoing embodiments, or carries out equivalent replacement to wherein some or all of technical characteristic; And these amendments or replacement, do not make the essence of appropriate technical solution depart from the scope of each embodiment technical scheme of the utility model.
Claims (10)
1. a catalyst cracker, is characterized in that, comprising: the regenerator transfer lime from top to bottom connected successively, finish mixing zone, fully zone of action and mitigation zone of action;
Catalyzer decollator is set at the top of finish mixing zone, and catalyzer decollator is positioned at and rises agent transfer lime again;
Described catalyzer decollator is the cone just put;
Described finish mixing zone is that just to put the top, finish mixing zone of round platform and shape be that the bottom, finish mixing zone of inverted round table is formed by shape, and arranges at the maximum diameter place of finish mixing zone the multiple nozzles being inclined upwardly and arranging.
2. catalyst cracker according to claim 1, is characterized in that, described regenerator transfer lime, catalyzer decollator, finish mixing zone, fully zone of action and mitigation zone of action are coaxially arranged.
3. catalyst cracker according to claim 1, is characterized in that, described abundant zone of action is the region that a cylinder is formed.
4. catalyst cracker according to claim 3, is characterized in that, described mitigation zone of action is formed by relaxing zone of action extension diameter section and relaxing zone of action straight length; Described mitigation zone of action extension diameter section is a round platform just put.
5. catalyst cracker according to claim 1, is characterized in that, described catalyzer decollator is connected and fixed by web member and regenerator transfer lime.
6. catalyst cracker according to claim 1, is characterized in that, the ratio of the maximum diameter of described finish mixing zone and the end face diameter on top, finish mixing zone is 1.5 ~ 8.0; The sidewall of bottom, finish mixing zone and horizontal plane angle are 60 ° ~ 85 °.
7. catalyst cracker according to claim 3, is characterized in that, the ratio of the diameter of described abundant zone of action and the maximum diameter of finish mixing zone is 1/8 ~ 2/3; The ratio of the height of described abundant zone of action and the diameter of abundant zone of action is 0.5 ~ 30.
8. catalyst cracker according to claim 4, is characterized in that, the ratio of the diameter of described mitigation zone of action straight length and the diameter of abundant zone of action is 1.5 ~ 8.0.
9. catalyst cracker according to claim 1, is characterized in that, the base angle of described catalyzer decollator is 5 ° ~ 45 °; The cone surface of described catalyzer decollator is uniformly distributed some small sircle holes, and the diameter of small sircle hole is 5 ~ 50mm;
The ratio of the diameter of described catalyzer decollator and the end face diameter on top, finish mixing zone is 2/3 ~ 5/6.
10. catalyst cracker according to claim 1, is characterized in that, the angle of described nozzle and horizontal plane is 5 ° ~ 45 °, and the quantity of nozzle is 1 ~ 30, is along the circumferential direction evenly arranged.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520785184.7U CN205115391U (en) | 2015-10-10 | 2015-10-10 | Catalytic cracking reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520785184.7U CN205115391U (en) | 2015-10-10 | 2015-10-10 | Catalytic cracking reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205115391U true CN205115391U (en) | 2016-03-30 |
Family
ID=55571015
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520785184.7U Expired - Fee Related CN205115391U (en) | 2015-10-10 | 2015-10-10 | Catalytic cracking reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205115391U (en) |
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2015
- 2015-10-10 CN CN201520785184.7U patent/CN205115391U/en not_active Expired - Fee Related
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20160330 |