CN1319643A - apparatus for producing low carbon olefines by high-tmep. catalyzing contact cracking from heavy petroleum hydrocarbon - Google Patents
apparatus for producing low carbon olefines by high-tmep. catalyzing contact cracking from heavy petroleum hydrocarbon Download PDFInfo
- Publication number
- CN1319643A CN1319643A CN 01106480 CN01106480A CN1319643A CN 1319643 A CN1319643 A CN 1319643A CN 01106480 CN01106480 CN 01106480 CN 01106480 A CN01106480 A CN 01106480A CN 1319643 A CN1319643 A CN 1319643A
- Authority
- CN
- China
- Prior art keywords
- reactor
- settling section
- revivifier
- riser
- coke
- 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.)
- Granted
Links
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 15
- 238000005336 cracking Methods 0.000 title claims abstract description 14
- 239000003209 petroleum derivative Substances 0.000 title claims abstract description 13
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title description 2
- 238000006243 chemical reaction Methods 0.000 claims abstract description 29
- 238000000926 separation method Methods 0.000 claims abstract description 19
- 230000003197 catalytic effect Effects 0.000 claims abstract description 12
- 238000010438 heat treatment Methods 0.000 claims description 20
- 239000003054 catalyst Substances 0.000 claims description 17
- 239000004215 Carbon black (E152) Substances 0.000 abstract description 3
- 229930195733 hydrocarbon Natural products 0.000 abstract description 3
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract 2
- 230000008929 regeneration Effects 0.000 description 9
- 238000011069 regeneration method Methods 0.000 description 9
- 239000007789 gas Substances 0.000 description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 5
- 239000003546 flue gas Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 230000000977 initiatory effect Effects 0.000 description 4
- 238000012423 maintenance Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 238000010276 construction Methods 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 229910000851 Alloy steel Inorganic materials 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 235000011089 carbon dioxide Nutrition 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000002010 green coke Substances 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 238000007233 catalytic pyrolysis Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000009719 regenerative response Effects 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 238000010517 secondary reaction Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The equipment for producing low-carbon olefin hydrocarbon includes reactor, regenerator and heat-supplementing lifting device, its reactor includes lift pipe, lift pipe reactor outlet quick separation facility, reactor settling section and reaction stripping section, and its regenerator includes coke-burning pipe, coke-burning pipe outlet quick separation facility, regenerator settling section, regenerator stripping section and one group of single-stage external cyclone separators. The heat-supplementing lifting device is set under the coke-burning pipe. Said invention can meet the requirements for producing low-carbon olefin hydrocarbon by means of high-temp. catalytic contact cracking heavy petroleum hydrocarbon, and can reduce cost.
Description
The invention belongs to refining of petroleum and petrochemical industry, relate to the device that heavy petroleum hydrocarbon high-temperature catalytic contact cracking is produced low-carbon alkene, specifically, relate to the reactor and the revivifier of this type of device.
Heavy petroleum hydrocarbon high-temperature catalytic contact cracking is produced the technology of low-carbon alkene, be to adopt fluidization to react a regeneration technology, heavy petroleum hydrocarbon is contacted with solid particle catalyst in fluidized-bed, in the presence of high temperature and water vapor, catalytic pyrolysis takes place, and generates the technology based on the low-carbon alkene of ethene, propylene.Chinese patent CN1083092A, CN1218786A, CN1030313C etc. all disclose similar Technology.On engineering, use the reactor and the revivifier pattern of fluidized catalytic cracker (to call FCC in the following text), realize the reaction and the regenerative process of heavy petroleum hydrocarbon high-temperature catalytic contact cracking production low-carbon alkene, have problems, make a concrete analysis of in following:
The temperature of FCC reactor and revivifier is low, its temperature of reaction is less than 550 ℃, regeneration temperature is less than 750 ℃, reactor and revivifier inner member are more, and adopt built-in cyclonic separator more, heat-resisting alloy steel is adopted in many places, and the inner member of various complexity is set in the FCC reaction stripping stage usually, makes maintenance and lining construction inconvenience; Because regeneration temperature is low, regenerative response speed is slow, reach the effect of burning of expection, and the device diameters of revivifier is very big, and the fixed investment of equipment is bigger; Along with raw material becomes heavy day by day, reaction green coke amount increases, and the FCC process is the heat surplus generally, need set up heat collector at revivifier; Because the agent-oil ratio of FCC is little, and is after the flue gas that regenerator carries enters reactor, little to the influence of subsequent separation system.The FCC revivifier is because operating linear velocity is low, and the gas solid separation in the device relies on the free setting of catalyzer to realize that separation efficiency is low, makes that the settling section of revivifier is very high, and diameter is very big, the facility investment height.
Heavy petroleum hydrocarbon high-temperature catalytic contact cracking is produced the temperature of reaction and the regeneration temperature height of low-carbon alkene, and its temperature of reaction is often greater than 700 ℃, and regeneration temperature is greater than 800 ℃.Reactions such as the strict control secondary cracking reaction of pyroreaction, condensation green coke.Pyroreaction and high temperature regeneration should reduce the device interior member to greatest extent simultaneously, fully use non-metallic liner, thereby use common iron, reduce the use of heatproof steel alloy, reduce investment cost, and are convenient to maintenance.Because the temperature of reaction height, reaction depth is dark, and institute's heat requirement is big, and the heat that revivifier burns generation can not satisfy the required heat of reaction, need be in the burning of regeneration section postcombustion, to satisfy the thermally equilibrated needs of two devices.Foreign gas with reactive system is brought in the circulation of regenerator into as nitrogen, carbonic acid gas, oxygen etc., enters follow-up ethylene recovery and separation system, can increase isolating difficulty.Owing to burn the temperature height, the intensification of afterburner is arranged simultaneously, the combustion initiation temperature height, scorching speed is fast, simultaneously, the heavy hydrocarbon cracking allows the regenerator carbon content higher, therefore based on thermal response, burning of spent agent can be adopted efficient coke-burning riser regeneration, to reduce the diameter of revivifier, saves the investment of equipment.Gas solid separation high efficiency separation equipment and rational the layout will reduce the device diameters of reacting settling section and regenerating settling section.
By above analysis as can be known, heavy petroleum hydrocarbon high-temperature catalytic contact cracking is produced low-carbon alkene, be different from normal stream fluidized catalytic cracking (FCC) process, therefore, be necessary to develop the high efficiency reactor and the revivifier that are fit to heavy petroleum hydrocarbon high-temperature catalytic contact cracking production low-carbon alkene, purpose of the present invention just is being this.
The total design concept of the present invention is: a kind of heavy petroleum hydrocarbon high-temperature catalytic contact cracking is produced the device of low-carbon alkene, comprise reactor, revivifier and concurrent heating lifter, reactor adopts riser reactor, establishes sharp separation facility, reactor settling section and reaction stripping stage in the riser reactor outlet.Revivifier is the coke-burning riser revivifier, whirlwind separator outside sharp separation equipment, revivifier settling section, regenerator stripping stage and one group of single-stage are established in coke-burning riser outlet.The concurrent heating lifter is established in the coke-burning riser bottom, concurrent heating lifter and the coke-burning riser formula structure that becomes one.Be connected with the regenerated catalyst inclined tube by the reclaimable catalyst inclined tube between reactor and revivifier and the concurrent heating lifter.
Reactor, revivifier and the concurrent heating lifter pattern of the present invention's design, the processing condition that heavy petroleum hydrocarbon high-temperature catalytic contact cracking is produced low-carbon alkene have been satisfied, the particularly design of coke-burning riser revivifier and bottom concurrent heating lifter, both satisfied the requirement of burning, reduced the investment of equipment again with concurrent heating.
Describe device of the present invention in detail below in conjunction with accompanying drawing.
Accompanying drawing and drawing explanation:
Accompanying drawing 1: a kind of typical structure synoptic diagram that apparatus of the present invention are reactor used;
Accompanying drawing 2: the another kind of typical structure synoptic diagram that apparatus of the present invention are reactor used;
Accompanying drawing 3: a kind of typical structure synoptic diagram of used concurrent heating lifter of apparatus of the present invention and revivifier;
Accompanying drawing 4: the another kind of typical structure synoptic diagram of used concurrent heating lifter of apparatus of the present invention and revivifier.
As shown in Figure 1, reactor of the present invention comprises that riser tube 11, riser tube go out outspoken branch 14, reactor settling section 15, reaction stripping stage 13, effuser 16 and one group of outer whirlwind separator 17 of single-stage.Riser tube 11 bottoms connect regenerated catalyst inclined tube 1, will import riser tube 11 from the hot regenerated catalyst of revivifier.Feed nozzle 12 is arranged on regenerated catalyst inclined tube 1 import top, establishes stripped vapor sparger 3 in the reaction stripping stage 13, and catalyzer inclined tube 2 is given birth in its below reception, and the reclaimable catalyst behind the stripping is imported revivifier.Riser tube goes out outspoken branch 14, optional with sophisticated inertia on the engineering divide soon, elasticity is divided soon, whirlwind-type is graded pattern soon, the present invention recommends to select for use the high whirlwind-type of separation efficiency to divide soon.In the reaction stripping stage 13, except that steam distributor 3 was set, the present invention recommended not to be provided with other internals, and this is because the temperature of reaction height, reaction depth is dark, institute's heat requirement is big, and the heat that revivifier burns generation can not satisfy the required heat of reaction, and the difference of the catalyst property that is adopted (low specific surface area, low pore volume etc.), therefore, inner member be can not establish in the reaction stripping stage 13 of the present invention, lining construction and maintenance also are convenient to simultaneously.The dipleg of outer whirlwind separator 17 can be located at dilute phase space, and adopts weight or flutter valve, also can be located at the fluidized-bed layer district, but all not stretch in the wall.Reactor of the present invention utilizes riser tube to go out outspoken branch 14 and the outer whirlwind separator 17 of single-stage, reaction oil gas is hightailed with catalyzer contact, and with the minimizing secondary reaction, and the height of reactor settling section 15 is reduced, and saves the fixed investment expense.
Reactor shown in the accompanying drawing 2 and accompanying drawing 1 difference are riser tube 11 outlet sharp separation facilities, accompanying drawing 1 goes out outspoken branch 14 by riser tube and forms with the outer whirlwind separator 17 of one group of single-stage that is arranged on the reactor settling section 15, and accompanying drawing 2 is three grades of fast 14a that divide-once divide soon, secondary divides 14b soon, three times the fast 14c of branch forms, reactor settling section 15 is by the corresponding once reactor settling section 15a that is divided into, secondary reactor settling section 15b, third-order reaction device settling section 15c, once reactor settling section 15a and secondary reactor settling section 15b are connected by the equipment annular space, and third-order reaction device settling section 15c is connected with reaction stripping stage 13 tops by catalyst transport 29.
Reactor shown in the accompanying drawing 2 has saved cyclonic separator, has reduced cost and maintenance cost.Once divide pattern the present invention that 14a, secondary divide the fast 14c of branch of 14b, three times soon without limits soon, sophisticated fast subset and structural shape all can use.
The direction of arrow is catalyzer or oil gas flow direction in the accompanying drawing 1,2.
Concurrent heating lifter of the present invention and revivifier shown in the accompanying drawing 3, mainly by concurrent heating lifter 31, coke-burning riser 32, revivifier settling section 33, coke-burning riser go out outspoken branch 34, and outer whirlwind separator 37 of 36, one groups of single-stages of effuser and regenerator stripping stage 38 are formed.Concurrent heating lifter 31 is located at coke-burning riser 32 bottoms, becomes one with coke-burning riser 32.Concurrent heating lifter 31 bottoms establish afterburning oil inlet 40 and afterburning promotes wind inlet 41, and both can be provided with nozzle or sparger respectively, also parallel feeding nozzle or sparger can be set.Reclaimable catalyst enters concurrent heating lifter 31 by reactor through inclined tube 2 to be generated, and concurrent heating lifter 31 has and improves the initial effect that temperature accelerates to burn speed of response of burning, and also has the effect that cloth wind promotes catalyzer.On coke-burning riser 32 different heights, also can one or more afterburning wind inlets 42 be set, to replenish in the burning process needs to oxygen according to the situation of burning.Coke-burning riser goes out outspoken branch 34, optional with sophisticated inertia on the engineering divide soon, elasticity is divided soon, whirlwind-type is graded pattern soon, the present invention recommends to select for use the high whirlwind-type of separation efficiency to divide soon.Revivifier settling section 33 bottoms are provided with sparger 35, and sparger 35 can advance steam, and can carry out preliminary stripping earlier this moment to regenerated catalyst, also can advance air, and play aid burning this moment, and regenerated catalyst is further burnt.Regenerator stripping stage 38 is connected with revivifier settling section 33 bottoms by regenerator conduit 44, and for making things convenient for lining construction, regenerator stripping stage 38 can be no inner member stripping stage, also can be efficient structured packing formula stripping stage.Stripped vapor enters bottom stripping sparger 43, and the foreign gas that stripping goes out is returned revivifier settling section 33 tops by upper catheter 39 and entered regenerated flue gas, and the regenerated catalyst behind stripping enters reactor through regenerator sloped tube 1.The dipleg of the outer whirlwind separator 37 of single-stage can be located at the dilute phase space of revivifier settling section 33, and adopts weight or flutter valve, also can be located at the fluidized-bed layer district of revivifier settling section 33 bottoms, but not stretch out wall.
The bottom of revivifier of the present invention shown in the accompanying drawing 3 is provided with concurrent heating lifter 31, solve reaction regeneration process self thermal equilibrium and had the insufficient problem of serious heat supply, satisfied the thermally equilibrated needs of two devices, simultaneously, owing to be located at the bottom of revivifier, improved the combustion initiation temperature of coke.Owing to burn the temperature height, the intensification of concurrent heating lifter 31 arranged simultaneously, the combustion initiation temperature height, scorching speed is fast, so the pattern of burning employing coke-burning riser 32 of reclaimable catalyst agent of the present invention, has reduced the diameter of equipment greatly, device diameters can be reduced more than one times, thus the investment of having saved equipment.The regenerator stripping stage 38 that is provided with uses steam that strippings such as the nitrogen in the regenerator, carbonic acid gas, oxygen are come out to enter regenerated flue gas, reduced these rare gas elementes and brought reactive system into the circulation of regenerator, enter the recovery of product and the possibility of isolating system again, reduced the difficulty of product separation.Because the coke-burning riser linear gas velocity is higher, the coke-burning riser outlet adopts sharp separation facility and outer whirlwind separator to come minute separable flue gas and catalyzer, and the separation efficiency height has reduced the diameter of revivifier settling section 33 and highly, has reduced the inner member of revivifier.
The difference of revivifier shown in the accompanying drawing 4 and accompanying drawing 3 only is; Regenerator stripping stage 38 directly is located at revivifier settling section 33 bottoms, be connected with revivifier settling section 33, and with coke-burning riser 32 coaxial arrangement.Make the layout of equipment compacter like this.
The direction of arrow is catalyzer or flow of flue gas direction in the accompanying drawing 3,4.
Claims (5)
1, a kind of heavy petroleum hydrocarbon high-temperature catalytic contact cracking is produced the device of low-carbon alkene, comprise reactor, revivifier and concurrent heating lifter (31), reactor adopts riser reactor, comprise riser tube (11), riser reactor outlet sharp separation facility, reactor settling section (15) and reaction stripping stage (13), revivifier is the coke-burning riser revivifier, comprise coke-burning riser (32), coke-burning riser goes out outspoken branch (34), revivifier settling section (33), regenerator stripping stage (38), one group of outer whirlwind separator (37) of single-stage, concurrent heating lifter (31) is located at coke-burning riser (32) bottom, become one structure with coke-burning riser (32), be connected with regenerated catalyst inclined tube (1) by reclaimable catalyst inclined tube (2) between reactor and revivifier and the concurrent heating lifter (31).
2, install according to claim 1, it is characterized in that: riser reactor outlet sharp separation facility goes out outspoken branch 14 by riser tube and forms with the outer whirlwind separator 17 of one group of single-stage that is arranged on the reactor settling section (15).
3, install according to claim 1, it is characterized in that: riser reactor outlet sharp separation facility is by once dividing (14a) soon, secondary divides (14b) soon, three times fast divide (14c) forms, reactor settling section (15) is by once reactor settling section (15a), secondary reactor settling section (15b), third-order reaction device settling section (15c) is formed, once reactor settling section (15a) and secondary reactor settling section (15b) are connected by the equipment annular space, and third-order reaction device settling section (15c) is connected with reaction stripping stage (13) top by catalyst transport (29).
4, as device as described in claim 1 or 2 or 3, it is characterized in that: regenerator stripping stage (38) is connected with revivifier settling section (33) bottom by regenerator conduit (44), top is connected with revivifier settling section (33) top by conduit (39), and revivifier settling section (33) bottom is provided with sparger (35).
5, as device as described in claim 1 or 2 or 3, it is characterized in that: regenerator stripping stage (38) directly is located at revivifier settling section (33) bottom, be connected with revivifier settling section (33), and with coke-burning riser 32 coaxial arrangement.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011064803A CN1140607C (en) | 2001-02-14 | 2001-02-14 | apparatus for producing low carbon olefines by high-tmep. catalyzing contact cracking from heavy petroleum hydrocarbon |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011064803A CN1140607C (en) | 2001-02-14 | 2001-02-14 | apparatus for producing low carbon olefines by high-tmep. catalyzing contact cracking from heavy petroleum hydrocarbon |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1319643A true CN1319643A (en) | 2001-10-31 |
| CN1140607C CN1140607C (en) | 2004-03-03 |
Family
ID=4655483
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB011064803A Expired - Lifetime CN1140607C (en) | 2001-02-14 | 2001-02-14 | apparatus for producing low carbon olefines by high-tmep. catalyzing contact cracking from heavy petroleum hydrocarbon |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1140607C (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101134160B (en) * | 2006-08-30 | 2010-06-30 | 中国石油天然气股份有限公司 | Reaction device for producing low-carbon olefins by catalytic cracking |
| CN103509595A (en) * | 2012-06-26 | 2014-01-15 | 中国石油化工股份有限公司 | Light hydrocarbon oil catalytic conversion method |
| CN106753511A (en) * | 2015-11-25 | 2017-05-31 | 中国石化工程建设有限公司 | The method of afterburner, catalytic pyrolysis regenerating unit and outer concurrent heating amount |
| CN111774015A (en) * | 2019-04-03 | 2020-10-16 | 上海卓然工程技术股份有限公司 | Reaction device of circulating fluidized bed |
| US11473019B2 (en) | 2018-09-27 | 2022-10-18 | Shanghai Supezet Engineering Technology Co., Ltd. | Naphtha catalytic cracking catalyst, catalytic cracking method and reaction device |
| CN116212973A (en) * | 2021-12-03 | 2023-06-06 | 中国石油化工股份有限公司 | Catalytic cracking regeneration equipment and regeneration method suitable for maintaining heat balance |
| CN116212974A (en) * | 2021-12-03 | 2023-06-06 | 中国石油化工股份有限公司 | Fluid catalytic cracking regenerator and regeneration method |
-
2001
- 2001-02-14 CN CNB011064803A patent/CN1140607C/en not_active Expired - Lifetime
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101134160B (en) * | 2006-08-30 | 2010-06-30 | 中国石油天然气股份有限公司 | Reaction device for producing low-carbon olefins by catalytic cracking |
| CN103509595A (en) * | 2012-06-26 | 2014-01-15 | 中国石油化工股份有限公司 | Light hydrocarbon oil catalytic conversion method |
| CN103509595B (en) * | 2012-06-26 | 2015-07-29 | 中国石油化工股份有限公司 | A kind of Light hydrocarbon oil catalytic conversion method |
| CN106753511A (en) * | 2015-11-25 | 2017-05-31 | 中国石化工程建设有限公司 | The method of afterburner, catalytic pyrolysis regenerating unit and outer concurrent heating amount |
| CN106753511B (en) * | 2015-11-25 | 2019-03-05 | 中国石化工程建设有限公司 | The method of afterburner, catalytic pyrolysis regenerating unit and outer concurrent heating amount |
| US11473019B2 (en) | 2018-09-27 | 2022-10-18 | Shanghai Supezet Engineering Technology Co., Ltd. | Naphtha catalytic cracking catalyst, catalytic cracking method and reaction device |
| CN111774015A (en) * | 2019-04-03 | 2020-10-16 | 上海卓然工程技术股份有限公司 | Reaction device of circulating fluidized bed |
| CN111774015B (en) * | 2019-04-03 | 2022-06-24 | 上海卓然工程技术股份有限公司 | Reaction device of circulating fluidized bed |
| CN116212973A (en) * | 2021-12-03 | 2023-06-06 | 中国石油化工股份有限公司 | Catalytic cracking regeneration equipment and regeneration method suitable for maintaining heat balance |
| CN116212974A (en) * | 2021-12-03 | 2023-06-06 | 中国石油化工股份有限公司 | Fluid catalytic cracking regenerator and regeneration method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1140607C (en) | 2004-03-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103540345B (en) | Catalytic cracking method | |
| CN111807916B (en) | Device for producing low-carbon olefin by efficient oxygen-containing compound | |
| CN103540346B (en) | A kind of Desending catalytic cracking device | |
| CN114262624B (en) | Method and device for catalytic cracking of double-component granular catalyst coupling fluidized bed | |
| CN1140607C (en) | apparatus for producing low carbon olefines by high-tmep. catalyzing contact cracking from heavy petroleum hydrocarbon | |
| CN111875464B (en) | Method for producing low-carbon olefin by high-efficiency oxygen-containing compound | |
| CN111875465B (en) | Method for producing low-carbon olefin by oxygen-containing compound | |
| CN103788993A (en) | Catalytic cracking unit | |
| CN108654526A (en) | A kind of reactor and preparation method of the dehydrating alkanes alkene reducing back-mixing | |
| CN103788992A (en) | Catalytic cracking method | |
| US11473019B2 (en) | Naphtha catalytic cracking catalyst, catalytic cracking method and reaction device | |
| CN102311767B (en) | Gasoline olefin reducing catalytic cracking method and device | |
| CN113087584A (en) | Method for producing low-carbon olefin by using oxygen-containing compound | |
| CN102268291A (en) | Catalytic cracking technology and device for reducing olefins in gasoline | |
| CN102212382B (en) | Catalytic cracking process and device | |
| CN1258560A (en) | Catalytic cracking riser reactor | |
| CN113509893A (en) | Method for producing low-carbon olefin by using efficient oxygen-containing compound | |
| CN1345911A (en) | Method for regulating heat balance of catalytic conversion technological reaction-regeneration system | |
| CN108079912B (en) | Reaction device and reaction method for catalytic dehydrogenation of alkane | |
| CN2791050Y (en) | Fluidized catalytic-cracking lift pipe reactor | |
| CN202829956U (en) | Petroleum hydrocarbon catalytic cracking device | |
| CN202658136U (en) | Petroleum hydrocarbon catalytic cracking device | |
| CN115364775B (en) | Device for controlling reaction temperature in olefin preparation by crude oil catalytic pyrolysis | |
| CN202297500U (en) | Catalytic cracker for petroleum hydrocarbon | |
| CN202705313U (en) | Petroleum hydrocarbon catalytic cracker |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| ASS | Succession or assignment of patent right |
Owner name: FUSHUN PETROLEUM AND CHEMICAL BRANCH OF CHINA NAT Free format text: FORMER OWNER: NONE |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| COR | Change of bibliographic data |
Free format text: CORRECT INVENTOR; FROM: ZHANG FUYI; ZHANG LIXIN; SHI BAOZHEN; ZHANG ZHENQIAN; LIU XIANLING; ZHANG JUYUE; LIU YU; TO: ZHANG FUYI; LIU QIANG; ZHANG LIXIN; KUANG ZHUOXIAN; SHI BAOZHEN; SUN JIMIN; ZHANG ZHENQIAN; QIAN XI Effective date: 20020912 |
|
| TA01 | Transfer of patent application right |
Effective date of registration: 20020912 Address after: 471003 No. 27 West Zhongzhou Road, Henan, Luoyang Applicant after: Luoyang Petrochemical Engineering Co.,Ltd./SINOPEC Co-applicant after: PETROCHINA FUSHUN PETROCHEMICAL CO. Inventor after: Zhang Fudai Inventor after: Zhang Juyue Inventor after: Liu Yu Inventor after: Liu Qiang Inventor after: Zhang Lixin Inventor after: Kuang Zhuoxian Inventor after: Shi Baozhen Inventor after: Sun Jimin Inventor after: Zhang Zhenqian Inventor after: Qian Xinhua Inventor after: Liu Xianling Address before: 471003 No. 27 West Zhongzhou Road, Henan, Luoyang Applicant before: Luoyang Petrochemical Engineering Co.,Ltd./SINOPEC Inventor before: Zhang Fudai Inventor before: Zhang Lixin Inventor before: Shi Baozhen Inventor before: Zhang Zhenqian Inventor before: Liu Xianling Inventor before: Zhang Juyue Inventor before: Liu Yu |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee |
Owner name: SINOPEC LUOYANG ENGINEERING CO., LTD. Free format text: FORMER NAME: CHINA PETROCHEMICAL CORPORATION |
|
| CP01 | Change in the name or title of a patent holder |
Address after: 471003 Zhongzhou West Road, Henan, China, No. 27, No. Co-patentee after: PETROCHINA FUSHUN PETROCHEMICAL CO. Patentee after: LUOYANG PETROCHEMICAL ENGINEERING CORPORATION, SINOPEC Address before: 471003 Zhongzhou West Road, Henan, China, No. 27, No. Co-patentee before: PETROCHINA FUSHUN PETROCHEMICAL CO. Patentee before: Luoyang Petrochemical Engineering Co.,Ltd./SINOPEC |
|
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20040303 |