CN1789379A - Method for catalytic conversion of hydrocarbon stock and riser reactor - Google Patents
Method for catalytic conversion of hydrocarbon stock and riser reactor Download PDFInfo
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- CN1789379A CN1789379A CN 200410060322 CN200410060322A CN1789379A CN 1789379 A CN1789379 A CN 1789379A CN 200410060322 CN200410060322 CN 200410060322 CN 200410060322 A CN200410060322 A CN 200410060322A CN 1789379 A CN1789379 A CN 1789379A
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Abstract
The invention relates the hydrocarbons catalytic cracking method and lift leg reactor. The raw oil and secondary raw material is entered in the each reaction channel of the same lift leg reactor cracking zone to crack. Then the raw oil and secondary raw material is carried out reaction. The catalyst from oil gas lead-out segment is leaded out to modified segment to improve the catalyst/oil ratio. The regenerated catalyst is cooled in prelifting segment. Realizing the two catalytic conversions in one lift leg with only one catalyst circulation loop between reactor and reactivator, the product quality is improved and the olefin content is lower. Utilizing the invention, the light oil productivity is improved by 1% and the olefin content is reduced by 10-15%.
Description
Technical field
The invention belongs to the refining of petroleum equipment technical field, particularly a kind of hydrocarbon raw material catalytic cracking method and riser reactor.
Background technology
Catalytic cracking unit is one of visual plant of refinery stock oil secondary processing, and the catalytic cracking reaction process realizes in riser reactor.In the conventional catalytic cracking unit, riser reactor only is a common pipe, always is about 40 meters, and stock oil is pressed mean flow rate 10-15 meter per second left and right sides speed through atomizing, finishes reaction through 3 seconds left and right sides time.Result of study shows that the reaction result of catalytic cracking directly depends on the structure and the design variable of riser reactor.
Over past ten years, catalytic cracking technology has been obtained very much progress.These progressive mainly giving the credit to going deep into that reaction process base reason is studied.Discover that different fractions is vaporized in the stock oil, cracking process has nothing in common with each other, and also can the phase mutual interference under the common environment under the catalyzer environment.At first cracking reaction mainly occurs in the zone of riser tube bottom 1/5th to 1/4th, and activity of such catalysts generally also has only original 50% in most of zone at rear portion; Secondly, the circulation slurry oil is easier to vaporization than other cut and is adsorbed by catalyzer, makes catalyst active center's inactivation very soon, has influenced the cracking of other cuts; And gasoline fraction forms higher olefin(e) centent again under the influence of other oil gas compositions.In view of the above, proposed to design the mentality of designing of reaction conditions by cut.
Stock oil and circulation slurry oil enter riser tube respectively at different positions scheme has at first appearred.The slurry oil (downstream) above stock oil that normally circulates is introduced riser tube.Make regenerated catalyst earlier with the stock oil reaction, and then with circulation slurry oil contact reacts, avoided the slurry oil influence of absorption too early.The MED technology and the Chinese patent application 01119807.9 of domestic a large amount of uses are typical example.
Further develop in the process, people have proposed " two-stage catalytic cracking " scheme.Promptly directly design two riser reactors, make different cuts, solved mutual interferential problem completely at different riser tube internal reactions.The core of two sections designs is: (1) shortens the reaction times, and (2) press the cut torpedo.
Interfere with each other problem in order to solve the reaction of stock oil, circulation slurry oil and gasoline simultaneously, Chinese patent application 0311944109 has proposed to build three riser reactors, respectively in order to the scheme of the oil that processes raw material, turning oil and gasoline.
Though that above scheme can solve preferably is long because of the reaction times, each cut disturbs low, the ropy problem of the purpose product yield that brings mutually, but the measure of taking is to repeat to increase device basically, implement quite difficulty on the actual engineering, what have almost can not implement.In addition, each riser reactor adopts conventional pattern usually in the prior art, still has the very low problem of reactor top reaction efficiency.The duo-lift tube reactor scheme that Chinese patent application 99213769.1,00134054.9 proposes, duo-lift tube reactor is two sections and arranges, first section (first riser reactor) is used for the stock oil cracking, reaction product is after gas solid separation, gasoline enters second riser reactor in top, introduces new regenerated catalyst again in second riser tube.Its two riser tubes are all shorter, and the oil gas reaction times shortens one times than the popular response device, solved the inefficient problem in conventional riser reactor top, but each riser reactor is conventional structure.
In these schemes, all be provided with pipeline between each riser reactor and the revivifier, on each pipeline guiding valve be housed, with the control catalyst internal circulating load for catalyst recirculation.Several riser tubes are arranged, just form the circulation of several roads.Some also will establish independent settling vessel and stripping stage, and structure is quite complicated.
Summary of the invention
The object of the invention is to provide a kind of can realize the requirement of two-stage catalytic, can satisfy hydrocarbon raw material catalytic cracking method and the riser reactor of producing the low-alkene gasoline processing condition again, utilizes the present invention not increase equipment such as settling vessel, stripping stage.
For reaching above-mentioned purpose, the present invention adopts following technical scheme: a kind of hydrocarbon raw material catalytic cracking method, after making stock oil and secondary reaction raw material enter same riser reactor soaking section to carry out cracking in the reaction channel separately, enter upgrading reaction and subsequent disposal operation.
Stock oil and secondary reaction raw material hybrid cooling after cracking carries out the upgrading reaction then.
Draw catalyzer to upgrading section from the oil gas section of drawing and increase this section agent-oil ratio.
Regenerated catalyst is in the pre lift zone processing of lowering the temperature.
A kind of hydrocarbon raw material riser reactor, comprise and connect pre lift zone, soaking section, upgrading section and the oil gas section of drawing that connects from bottom to top, be provided with in pre lift zone and the soaking section space and its axial identical secondary reaction passage, the pre lift zone upper portion side wall is provided with the stock oil inlet, the bottom is provided with and the secondary reaction feed(raw material)inlet of secondary reaction channel connection.
Secondary reaction passage axis and reactor axis are staggeredly arranged, and are arranged near the reactor wall place.
Leave spacing between secondary reaction passage top and the upgrading section and form the oil gas mixing section, the mixing section sidewall is provided with coolant entrance.
The oil gas section of drawing is connected with the upgrading pars infrasegmentalis by the catalyzer return line.
Pre lift zone inside is provided with heat-exchanger rig, and upgrading section diameter is 2-3 a times of soaking section diameter, and backflow catalyzer outlet place riser diameter enlarges, and the secondary reaction material inlet is located at the pre lift zone bottom.
Pre lift zone height 4-6 rice, the soaking section height is a 8-20 rice, mixing section height 1-3 rice, the upgrading section highly is a 6-15 rice.
Among the present invention, use a riser reactor can realize the two-stage catalytic cracking process of stock oil and secondary reaction raw material (as circulation slurry oil, freshening gasoline etc.) torpedo, and reduce olefin(e) centent in the gasoline.Riser reactor is along being divided into regenerator pre lift zone, pyrolytic cracking conversion zone, cryogenic product upgrading section and the oil gas section of drawing highly from bottom to top.Pyrolytic cracking conversion zone in the bottom, the Bian Biqu of close reactor is provided with the secondary reaction passage, thereby forms two reaction channels at soaking section, realizes the two-stage catalytic cracking reaction in a reactor.The secondary reaction passage of pyrolytic cracking section and stock oil reaction channel height account for 1/2nd of conventional riser reactor, and the reaction times presses 0.5-1.2 and controls second.Both can guarantee the requirement of cracking time, also overcome the inefficient shortcoming of riser reactor latter half.Cryogenic product upgrading section adopts the structure design of enlarged-diameter, in this section, is suppressed from the cracking reaction of the oil gas of pyrolytic cracking section, carries out the product upgrading under low temperature, high solvent-oil ratio operating mode, helps the content of olefin in gasoline reduction.This section diameter is generally 2-3 times of pyrolytic cracking district, bottom.More than be mixing section between two conversion zones, highly be 1-2 rice, oily steam flow speed 10～20 meter per seconds, be used to make raw material oil gas and secondary reaction raw material oil gas to mix from bottom differential responses passage, and, make the oil gas cooling at this district's introducing quenched water, stop cracking reaction.For strengthening cold zone upgrading effect, establish the catalyzer return line on riser tube top, draw the part catalyzer from the oil gas section of drawing of cryogenic reaction zone top and return in the cryogenic reaction zone, increase the agent-oil ratio in it.So, from the catalyst recirculation measuring angle, low agent-oil ratio and two reaction zones of top high solvent-oil ratio of bottom have been formed.Reaction oil gas and recycling catalyst flow out riser reactor through outlet pipe, enter settling vessel and interior cyclone thereof, and catalyzer is isolated from oil gas, enters stripping stage.Enter the catalytic amount of cyclone separator and stripping stage and equate, do not increase the load of follow-up equipment with the catalytic amount that enters riser reactor through the regeneration standpipe.Be that the interior high solvent-oil ratio of reactor is realized at reactor itself, also only cause the change of riser tube itself.Product oil gas enters follow-up product separation unit at settling vessel top discharger.The heat transfer tube that is provided with in pre lift zone can be taken the heat of part catalyzer away, reduces temperature, and the agent-oil ratio of reaction zone is increased, and reduces olefin(e) centent in the gasoline.Used water is made heat-eliminating medium in the heat transfer tube.
Has only a catalyst recirculation passage between the revivifier of reactor of the present invention and catalytic cracking unit, the settling vessel.The stock oil reaction is reacted a shared regenerator standpipe and a pre lift zone with secondary raw material.Stock oil is from the incoming stock oily reaction channel of sidewall, and the secondary reaction raw material enters the turning oil reaction channel vertically in the bottom.The stock oil import is located at side-walls, and the stock oil logistics that sprays into through atomizing nozzle still can converge in channel center.
The temperature of reaction of cracking zone of the present invention is 510-560 degree (Celsius), and the reaction times is 0.6-1.2 second; The temperature of reaction of upgrading section is 490-530 degree (Celsius), and the reaction times is 3-6 second; The fuel oil preheating temperature is 200-250 degree (Celsius), the secondary raw material temperature is 340-360 degree (Celsius), the pre lift zone catalyzer 30-80 degree (Celsius) that cools, and rate of catalyst flow is the 1.5-2.5 meter per second, the mixing section flow velocity is the 10-20 meter per second, and upgrading section flow velocity is the 3-6 meter per second.Upgrading section catalyzer reflux ratio is 0.5-2.
Riser reactor total height of the present invention is a 35-50 rice, pre lift zone height 4-6 rice wherein, and the soaking section height is a 8-20 rice, mixing section 1-3 rice, the upgrading section highly is a 6-15 rice.
The simple frame mode of the present invention has been realized the two-stage catalytic conversion in a riser tube, instead realized the cracking reaction requirement of short riser tube, short reaction time and the requirement of decreasing by gasoline olefin simultaneously on the device again in routine, can improve light oil yield 1-2%; Low temperature upgrading section can make the content of olefin in gasoline of being produced reduce 7-10 percentage point, and the effect that low temperature upgrading section catalyzer refluxes can make gasoline olefin reduce 5-10 percentage point, and total can reduce content of olefin in gasoline more than 15 percentage points.Except that riser tube changes, do not increase equipment, do not establish settling vessel, stripping stage etc. in addition; Do not change the load and the operating mode of original device settling vessel, cyclone and pre lift zone; Do not increase and revivifier and settling vessel between catalyst return, and have only a catalyst recirculation system between former revivifier and settling vessel.
Working process of the present invention is: enter the pre lift zone of reactor from the catalyzer of revivifier through the regeneration standpipe, regenerator is divided into two-way in pre lift zone, respectively incoming stock oily passage and secondary reaction material channel.These catalyzer upwards flow under the effect of pre-lifting steam, enter reaction zone.Stock oil and secondary reaction raw material such as recycle stock enter reaction zone through atomizing nozzle separately, carry out cracking reaction under the catalyzer environment.After finishing cracking reaction, cooled off by chilled water, stop cracking reaction at mixing section.Enter the low flow velocity reaction zone of low temperature then, carry out the product upgrading and transform.Reaction oil vapour and recycling catalyst enter settling vessel through the outlet at top, join with cyclone in it, carry out gas solid separation.Reaction oil vapour is drawn through oily steam pipe line at the settling vessel top, enters follow-up product separation device.The catalyzer that cyclone is told is introduced into stripping stage, displaced entrained oil vapour by steam after, enter revivifier, under the temperature of 700 degree about (Celsius) and oxygen reaction, remove the collection carbon that forms in reaction process, recover active.Catalyzer after the regeneration enters riser tube through the regeneration standpipe.
Description of drawings
Fig. 1 be have the hydrocarbon raw material riser reactor anti--refill the interposed structure synoptic diagram;
Fig. 2 for anti-among the embodiment 2-refill the interposed structure synoptic diagram;
Fig. 3 is a hydrocarbon raw material riser reactor cracking zone cross sectional representation, and arrow is the stock oil heading;
Fig. 4 is that agent-oil ratio changes synoptic diagram in the hydrocarbon raw material riser reactor;
Fig. 5 is a temperature variation synoptic diagram in the hydrocarbon raw material riser reactor.
Embodiment
Embodiment 1, as shown in Figure 1, the hydrocarbon raw material riser reactor is formed by connecting the pre lift zone 11, soaking section 12, upgrading section 15 and the oil gas section of drawing that connect from bottom to top, pre lift zone 11 top sidewalls are provided with stock oil inlet 25, its inside is provided with cooling heat transferring pipe 19, can lead to cold water in the heat transfer tube 19 catalyzer is cooled off.Be provided with in pre lift zone 11 and soaking section 12 spaces and its axial identical circulation slurry oil reaction channel 13, circulation slurry oil opening for feed 24 is located at pre lift zone 11 bottoms.Circulation slurry oil reaction channel 13 axis and reactor axis are staggeredly arranged, and are arranged near the reactor wall place, leave spacing between circulation slurry oil reaction channel 13 tops and the upgrading section 15, form mixing section 14.Upgrading section 15 diameters are 2 times of soaking section 12 diameters.Soaking section 12 top sidewalls are provided with coolant entrance 23, and the oil gas section of drawing is connected with upgrading section 15 bottoms by catalyzer return line 17.
700 degree (Celsius) left and right sides temperature of regenerating in the revivifier 4, high activated catalyst enter the pre lift zone 11 of riser reactor 1 bottom through standpipe 5 under 6 controls of regeneration guiding valve.Catalyzer is in pre lift zone and heat transfer tube 19 heat exchange, the catalyzer 30-80 degree (Celsius) that is cooled, lowers the temperature.Cooled catalyzer is upwards carried under the vapor action from pre-lifting steam inlet 22, enters the soaking section 12 of reactor.The steam apparent velocity of pre lift zone 11 is about 2 meter per seconds.Stock oil is preheated to 200-250 degree (Celsius) earlier, above pre lift zone 11, after nozzle atomization from riser tube sidewall import 25 incoming stock oily reaction channels.About circulation slurry oil temperature 350 degree (Celsius),,, upwards enter the turning oil reaction channel along the riser tube axis direction in pre lift zone 11 bottoms.Be divided into two-way after the catalyzer cooling in the pre lift zone 11, the incoming stock oily reaction channel of 70%-80%, 20%-30% enters turning oil reaction channel 13.Reacted stock oil oil gas mixes in mixing section 14 with circulation slurry oil oil gas, and is cooled off by the chilled water from import 23 at this, suppresses cracking reaction.Oil gas after the cooling and catalyzer enter product upgrading section 15 jointly, carry out aromizing, alkylation and hydrogen transfer reactions.After oil gas enters upgrading section 15, and contact through return line 17 and by the make-up catalyst 34 that guiding valve 18 is controlled, the reagent oil ratio is increased, the upgrading effect further improves.The catalyzer that refluxes is drawn from the oil gas section of drawing, and sends in upgrading section 12 bottoms.Reaction oil gas and with the catalyzer of regenerator standpipe 5 equivalent of flowing through through exporting 16 cyclonic separators 8 that enter settling vessel 2 in, after sub-argument went out catalyzer, oil gas was sent instead-again through pipeline 7 and is installed the product separation part that enters the back.Cyclonic separator 8 isolated catalyzer then flow into stripper 3 downwards, contact with stripped vapor, displace the oil gas of catalyst entrainment after, flow into revivifier 4, oxygen 21 reactions with from the regenerator bottoms import recover to enter reactor 1 again after the activity, finish reaction cycle.27 is external warmer.
At a cover amount of finish 100 * 10
4Adopted above-mentioned riser reactor in t/a, the catalytic cracking unit based on production gasoline and diesel oil, anti--as to refill and put 50 meters of height overalls, 40 meters of riser reactor 1 length.5.0 meters of settling vessel 2 diameters, 9.0 meters of revivifier 4 diameters, 2.5 meters of stripper 3 diameters.1.6 meters of riser reactor 1 pre lift zone 11 diameters, high 5.0 meters, 800 millimeters of stock oil passage (soaking section 12) diameters, 15 meters of height, 300 millimeters of recycle stock passage 13 diameters, high 18 meters, 1000 millimeters of mixing section 14 diameters, high 2.0 meters, 2.0 meters of upgrading section 15 diameters, high 10 meters.900 millimeters of reactor outlet (the oil gas section of drawing) diameters, 500 millimeters of catalyzer return line 17 diameters, 700 millimeters of regeneration standpipe 5 diameters.
Stock oil at sustained height from four nozzles 25, the 90 ° of incoming stock oily reaction channels of circumferentially being separated by; The circulation slurry oil enters circulation slurry oil reaction channel from a nozzle 24 in the bottom; Chilled water enters mixing section 14 from two nozzles 23.200 ℃ of fuel oil preheating temperature, 350 ℃ of circulation slurry oil temperature, 510 ℃ of stock oil cracking reaction temperature, 500 ℃ of circulation slurry oil cracking reaction temperature; 490 ℃ of upgrading section temperature.The pre-quantity of steam 2.0t/h that promotes, stock oil atomizing steam amount 6.0t/h, circulation slurry oil atomizing steam amount is 1.0t/h; Chilled water consumption 8.0t/h.
Enter through regeneration standpipe 5 that the catalyst recirculation amount is 1000t/h between riser reactor and revivifier, wherein 20% enter circulation slurry oil reaction channel 13.The catalytic amount that returns upgrading section 15 through return line 17 is 1500t/h; The catalytic amount that enters settling vessel cyclone, stripper and revivifier through reactor outlet is 1000t/h.Riser reactor top operational pressure 0.35MPa (a-absolute pressure), revivifier 4 working pressure 0.38MPa (a).
Product is respectively: gasoline 45%, and diesel oil 30%, liquefied petroleum gas (LPG) 15%, dry gas adds loss 3%, coke 7%.Content of olefin in gasoline reduces by 15 percentage points.
Embodiment 2, as shown in Figure 2 in the present embodiment, at riser tube backflow catalyzer outlet place, is provided with the catalyzer draw-out area 31 of hole enlargement, more helps catalyzer and draws and reflux.Other are with embodiment 1.
At a cover amount of finish 100 * 10
4In t/a, the catalytic cracking unit, adopted above-mentioned riser reactor based on the production low-carbon alkene.Instead-refill and put 50 meters of height overalls, 40 meters of lifting pipe ranges, 5.0 meters of settling vessel 2 diameters, 9.0 meters of revivifier 4 diameters, 2.5 meters of stripper 3 diameters.1.8 meters of riser reactor pre lift zone 11 diameters, high 6.0 meters; 900 millimeters of stock oil passage (soaking section 12) diameters, 15 meters of height; 280 millimeters of recycle stock passage 13 diameters, high 18 meters; 1000 millimeters of mixing section 14 diameters, high 2.0 meters; 2.0 meters of upgrading section 15 diameters, high 8 meters; 1000 millimeters of reactor outlet diameters; 600 millimeters of catalyzer return line 17 diameters; 700 millimeters of regeneration standpipe 5 diameters.
Stock oil at sustained height from four nozzles 25, the 90 ° of incoming stock oily reaction channels of circumferentially being separated by; The circulation slurry oil enters circulation slurry oil reaction channel from a nozzle 24 in the bottom.Chilled water enters mixing section 14 from two nozzles 23.
200 ℃ of fuel oil preheating temperature, 350 ℃ of circulation slurry oil temperature, 530 ℃ of stock oil cracking reaction temperature, 530 ℃ of reprocessed oil slurry cracking reaction temperature; 505 ℃ of upgrading section temperature.
The pre-quantity of steam 2.0t/h that promotes, stock oil atomizing steam amount 6.0t/h, reprocessed oil slurry atomizing steam amount is 1.0t/h; Chilled water consumption 8.0t/h.
Enter through the regeneration standpipe that the catalyst recirculation amount is 1200t/h between riser reactor and revivifier, wherein 25% enter circulation slurry oil reaction channel.The catalytic amount that returns the upgrading section through return line is 1500t/h; The catalytic amount that enters settling vessel, cyclonic separator, stripper and revivifier through reactor outlet is 1200t/h.Riser tube top operational pressure 0.35MPa (a), revivifier working pressure 0.38MPa (a).
Product is respectively: gasoline 39%, and diesel oil 30%, liquefied petroleum gas (LPG) 20%, dry gas adds loss 4%, coke 7%.Content of olefin in gasoline reduces by 12 percentage points.
Claims (10)
1, a kind of hydrocarbon raw material catalytic cracking method is characterized in that, after making stock oil and secondary reaction raw material enter same riser reactor soaking section to carry out cracking in the reaction channel separately, enters upgrading reaction and subsequent disposal operation.
2, the method for claim 1 is characterized in that, stock oil and secondary reaction raw material hybrid cooling after cracking carries out the upgrading reaction then.
3, method as claimed in claim 1 or 2 is characterized in that, draws catalyzer to upgrading section from the oil gas section of drawing and increases this section agent-oil ratio.
4, method as claimed in claim 3 is characterized in that, regenerated catalyst is in the pre lift zone processing of lowering the temperature.
5, a kind of hydrocarbon raw material riser reactor, comprise and connect pre lift zone, soaking section, upgrading section and the oil gas section of drawing that connects from bottom to top, it is characterized in that, be provided with in pre lift zone and the soaking section space and its axial identical secondary reaction passage, the pre lift zone upper portion side wall is provided with the stock oil inlet, the bottom is provided with and the secondary reaction feed(raw material)inlet of secondary reaction channel connection.
6, the reactor of stating as claim 5 is characterized in that, secondary reaction passage axis and reactor axis are staggeredly arranged, and is arranged near the reactor wall place.
As claim 5 or 6 described reactors, it is characterized in that 7, leave spacing between secondary reaction passage top and the upgrading section and form the oil gas mixing section, the mixing section sidewall is provided with coolant entrance.
8, reactor as claimed in claim 7 is characterized in that, the oil gas section of drawing is connected with the upgrading pars infrasegmentalis by the catalyzer return line.
9, reactor as claimed in claim 8, it is characterized in that pre lift zone inside is provided with heat-exchanger rig, upgrading section diameter is 2-3 a times of soaking section diameter, backflow catalyzer outlet place riser diameter enlarges, and the secondary reaction material inlet is located at the pre lift zone bottom.
10, reactor as claimed in claim 9 is characterized in that, pre lift zone height 4-6 rice, and the soaking section height is a 8-20 rice, mixing section height 1-3 rice, the upgrading section highly is a 6-15 rice.
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| CNB2004100603221A CN100343368C (en) | 2004-12-13 | 2004-12-13 | Method for catalytic conversion of hydrocarbon stock and riser reactor |
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| CNB2004100603221A CN100343368C (en) | 2004-12-13 | 2004-12-13 | Method for catalytic conversion of hydrocarbon stock and riser reactor |
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| CN1789379A true CN1789379A (en) | 2006-06-21 |
| CN100343368C CN100343368C (en) | 2007-10-17 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102925207A (en) * | 2011-08-12 | 2013-02-13 | 中国石油天然气股份有限公司 | Catalytic cracking method for processing heavy oil, and apparatus thereof |
| CN103031148A (en) * | 2011-09-30 | 2013-04-10 | 中国石油化工股份有限公司 | Catalytic conversion method for processing high-nitrogen raw material |
| CN103834430A (en) * | 2013-01-23 | 2014-06-04 | 洛阳瑞泽石化工程有限公司 | Design method of feed nozzle of catalytic cracking device |
| CN115637166A (en) * | 2021-07-20 | 2023-01-24 | 青岛京润石化设计研究院有限公司 | Catalytic conversion method and reactor for raw oil and light hydrocarbon |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5104517A (en) * | 1990-05-17 | 1992-04-14 | Uop | Vented riser apparatus and method |
| CN1118539C (en) * | 2000-12-13 | 2003-08-20 | 中国石油天然气股份有限公司 | Catalytic cracking process with two-segment lift pipe |
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2004
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102925207A (en) * | 2011-08-12 | 2013-02-13 | 中国石油天然气股份有限公司 | Catalytic cracking method for processing heavy oil, and apparatus thereof |
| CN102925207B (en) * | 2011-08-12 | 2014-11-19 | 中国石油天然气股份有限公司 | Catalytic cracking method for processing heavy oil, and apparatus thereof |
| CN103031148A (en) * | 2011-09-30 | 2013-04-10 | 中国石油化工股份有限公司 | Catalytic conversion method for processing high-nitrogen raw material |
| CN103031148B (en) * | 2011-09-30 | 2015-09-23 | 中国石油化工股份有限公司 | The catalysis conversion method of processing high-nitrogen stock |
| CN103834430A (en) * | 2013-01-23 | 2014-06-04 | 洛阳瑞泽石化工程有限公司 | Design method of feed nozzle of catalytic cracking device |
| CN103834430B (en) * | 2013-01-23 | 2015-09-09 | 洛阳瑞泽石化工程有限公司 | A kind of catalytic cracking feeds device |
| CN115637166A (en) * | 2021-07-20 | 2023-01-24 | 青岛京润石化设计研究院有限公司 | Catalytic conversion method and reactor for raw oil and light hydrocarbon |
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Effective date of registration: 20110607 Address after: 471003 Tsinghua Science Park, three mountain road, hi tech Zone, Henan, Luoyang 609 Patentee after: Shi Baozhen Address before: 471003 Zhongzhou West Road, Henan, China, No. 27, No. Patentee before: Luoyang Petro-Chemical Equipment Inst. |
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| DD01 | Delivery of document by public notice |
Addressee: Shi Baozhen Document name: Notification of Termination of Patent Right |
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| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20071017 Termination date: 20141213 |
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| EXPY | Termination of patent right or utility model |