CN108300508A - Heavy oil millisecond is classified gas phase catalysis and cracks producing light olefins coupling device - Google Patents
Heavy oil millisecond is classified gas phase catalysis and cracks producing light olefins coupling device Download PDFInfo
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- CN108300508A CN108300508A CN201810341314.6A CN201810341314A CN108300508A CN 108300508 A CN108300508 A CN 108300508A CN 201810341314 A CN201810341314 A CN 201810341314A CN 108300508 A CN108300508 A CN 108300508A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one catalytic cracking step
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides heavy oil millisecond classification gas phase catalysis and cracks producing light olefins coupling device, and downlink modified-reaction pipe is connected to one circular response system of composition by gas-solid separator, returning charge controller and flow control device with modification regeneration reactor；High-efficiency atomizing nozzle is arranged in downlink modified-reaction pipe top, and lower part is equipped with gas-solid quick disconnector；Modification regeneration reactor bottom is equipped with regenerant inlet, and top is equipped with gas-solid separator；Millisecond cracking reactor, which is connected to by gas-solid separator, returning charge controller and flow control device with pyrolysis recycle reactor, forms another circular response system；Pyrolysis oil gas vent and the outlet of returning charge controller are directly accessed a millisecond cracking reactor entrance, millisecond cracking reactor outlet connection gas-solid quick disconnector together；Pyrolysis recycle reactor bottom is equipped with air intake, and top is connected equipped with gas-solid separator with returning charge controller, and returning charge controller accesses millisecond cracking reactor, and gas-solid separator gas vent is connected by heat exchanger with exhanst gas outlet.
Description
1. technical field
The present invention provides heavy oil millisecond classification gas phase catalysis and cracks producing light olefins coupling device, belongs to PETROLEUM PROCESSING neck
Domain.
2. background technology
The very important basic organic chemical industry raw material of the low-carbon alkenes such as ethylene, propylene, butylene and butadiene, especially ethylene
Production capacity is considered increasingly as the mark of a countries and regions petrochemical industry development level.Due to energy-storage battery technology blowout
Develop and be known as six discharge standard of motor-vehicle tail-gas state most tight in the world and implement the phase and close on, electric vehicle is close by driving process
No pollution, energy saving, low use cost and it is easy to intelligentized advantage, is a dark horse, replacing fuel oil automobile becomes irreversible
Development trend will be that oil universal consumption figure is handed over drastically to decline thereupon, oil-processing enterprises from " fuel combustion type " to " chemical industry type "
Transition and upgrade is extremely urgent.
Currently, about 95% ethylene of the whole world and 66% propylene are light using natural gas, naphtha or light diesel fuel etc.
Matter raw material is produced by tube furnace steam thermal cracking process.However in the 21st century, is with conventional crude resource increasingly depleted, generation
Boundary's oil supply shows heaviness, in poor quality development trend, causes steamcracker feed relatively deficient, and low in world wide
The carbon olefin market demand increasingly rapid growth.In order to alleviate this contradiction, the raw materials for production of low-carbon alkene are widened, while being also more
Heavy raw oil is utilized well, develops using heavy oil as raw material, " the chemical industry of low-carbon alkene is directly produced by Deep Catalytic Cracking process
Type " technology path becomes the emphasis and hot spot of petroleum refining industry research both at home and abroad and concern at present, but being capable of industrialized maturation
Technology is very few.
The heavy oil catalytic pyrolysis low-carbon olefines high-output technology developed in recent years is more, the DCC/ developed such as sinopec Shi Ke institutes
CPP techniques [4-5], the PetroFCC techniques of Uop Inc.'s exploitation, the HS-FCC techniques of Japan petroleum energy centre exploitation, THR
Technique, German organic chemistry research institute TCSC techniques, INDMAX (UCC) technique of Indian Oil Corporation's exploitation, Exxon mobil
Two-stage riser catalytic pyrolysis (TMP) work that the Maxofin techniques and China Petroleum developed jointly with Kellog companies propose
Skill etc., by the extensive concern and Demonstration Application of industry.There is olefin feedstock range to broaden compared with steam cracking, reaction temperature
Low, product distribution is easy to adjustment and low power consumption and other advantages.But when on the one hand these Deep Catalytic Cracking process preferably use high temperature, short stop
Between, the mode of operation of high agent-oil ratio, big water-oil factor, on the other hand due in catalytic pyrolysis operating process, raw material composition and catalysis
Agent property is an important factor for influencing catalytic pyrolysis product yield and distribution.However the work of heavy oil catalytic pyrolysis shape selective catalysis agent
Property component is mainly ZSM-5 and Y type molecular sieve, and pore passage structure is smaller, larger heavy oil molecules spread in mass transport process by
Limit is not easily accessible inside molecular sieve and carries out shape slective cracking, in addition the stronger hydrogen migration performance of acidic molecular sieve, the yield of alkene and
Selective increase rate is restricted；In addition, the heavy oil macromolecular for being gathered in molecular sieve surface is easy under the action of acid site
Overcracking causes product distribution bad or coking condensation, to blocking catalyst duct.Current existing industry is selected type and is urged
Agent often brings catalysis using inferior raw materials preparing low-carbon olefin by catalytically cracking such as reduced crude, decompression residuum, deasphalted oils
The problems such as agent poisoning, atomizing effect are poor, green coke amount is big and conversion ratio and selectivity are greatly lowered.
In addition in existing heavy oil hot procedure, liquid phase reactor mainly occurs for hydrocarbon reaction.Hydrocarbon molecules in the gas phase
It can scatter quickly after being split into free radical, and free radical in the liquid phase is surrounded by surrounding molecular as " cage "
Come, polycondensation reaction will aggravate.So that the free radical to be formed is scatter, it is necessary to overcome diffused out from " cage " it is additional
Potential barrier, here it is so-called " cage effects ".For gas phase reaction, this " cage effect " can change liquid reactive
Activation energy and reaction speed.Wu etc. compared the liquid phase reactor and gas phase reaction process of hexadecane, find liquid phase reaction course
Gaseous product selectivity can be reduced while can also generate more polymer, and gas phase reaction process can then increase in gaseous product
Olefin(e) centent.
The pollution for eliminating carbon residue and heavy metal pollution in heavy oil is how developed, the technique for obtaining low-carbon alkene is maximized and is set
The standby China's oil chemical industry type processing transition and upgrade process that becomes compels key subjects to be solved.
3. invention content
The purpose of the present invention is exactly to overcome existing for existing processing of heavy oil device insufficient and a kind of heavy oil millisecond classification
Gas phase catalysis cracks producing light olefins coupling device, is pyrolyzed using heavy oil down pipe millisecond and maximizes production oil gas, high temp oil gas
Without condensation separation, high temperature millisecond shape selective catalysis cracking producing light olefins are directly carried out, to make full use of pyrolysis oil gas
Heat increases substantially yield of light olefins and selectivity, overcomes liquid reactive " cage effect ", reduces Mass and heat transfer pair
The influence of catalytic pyrolysis drastically reduces the green coke amount and energy consumption of cracking process, to realize the efficient high yield chemical industry of heavy oil
Type is processed.
Technical scheme of the present invention：
Heavy oil millisecond is classified gas phase catalysis and cracks producing light olefins coupling device, by gas-solid separator, returning charge controller, height
Imitate atomizer, downlink modified-reaction pipe, gas-solid quick disconnector, pyrolysis oil gas vent, flow control device, millisecond cracking reaction
Device, regenerant inlet, modification regeneration reactor, heat exchanger, regeneration gas outlet, pyrolysis recycle reactor, air intake, flue gas go out
Mouth composition.Downlink modified-reaction pipe is connected by gas-solid separator, returning charge controller and flow control device and modification regeneration reactor
One circular response system of logical composition；Downlink modified-reaction pipe top is provided with symmetrical high-efficiency atomizing nozzle, and lower part is equipped with gas
Gu quick disconnector, gas-solid quick disconnector gas vent is pyrolysis oil gas vent, and gas-solid quick disconnector solid outlet passes through
Flow regulator is connected to modification regeneration reactor lower part；Modification regeneration reactor bottom is equipped with regenerant inlet, and top is equipped with
Gas-solid separator；Gas-solid separator solid outlet opens below into returning charge controller, and access downlink in returning charge controller outlet is modified anti-
Tube top portion, gas-solid separator gas vent is answered to be connected with regeneration gas outlet by heat exchanger；Millisecond cracking reactor passes through gas-solid
Separator, returning charge controller and flow control device are connected to pyrolysis recycle reactor forms another circular response system；Pyrolysis
Oil gas vent and the outlet of returning charge controller are directly accessed a millisecond cracking reactor entrance, millisecond cracking reactor outlet connection together
Gas-solid quick disconnector；Gas-solid quick disconnector solid outlet is connected to by flow regulator with pyrolysis recycle reactor lower part,
Gas-solid quick disconnector gas vent is cracking oil gas vent；Pyrolysis recycle reactor bottom is equipped with air intake, and top is equipped with
Gas-solid separator；Gas-solid separator solid outlet opens below into returning charge controller, and access millisecond cracking in returning charge controller outlet is anti-
Device entrance, gas-solid separator gas vent is answered to be connected with exhanst gas outlet by heat exchanger.
480 DEG C -850 DEG C of the reaction temperature of downlink modified-reaction pipe, solid thermal carriers be semicoke microballoon, aluminum oxide micro-sphere,
Calcium aluminate porous microsphere, magnesium aluminate spinel porous microsphere, alumina silicate porous microsphere, calcium silicates porous microsphere, magnesium silicate are porous micro-
One or more mixture in the porous microsphere carrier of ball, carrying alkali metal or/and alkaline-earth metal.
650 DEG C -1250 DEG C of the reaction temperature of modification regeneration reactor, modification regeneration reactor are riser regenerator, rapids
One or more combinations in fluid bed regenerator, bubbling fluidized bed regenerator are flowed, regenerative agent is oxidant and vapor
Mixture or oxidant, oxidant are one kind in oxygen, air and oxygen-enriched air；Regeneration gas is synthesis gas or flue gas.
530 DEG C -750 DEG C of the reaction temperature of cracking reactor, catalyst for cracking are ZSM-5 molecular sieve catalyst, FCC molecules
Sieve catalyst selects one or more mixtures in type molecular sieve catalyst, alkali solid porous catalyst, and millisecond cracking is anti-
It is that downer reactor, the rotation of horizontal inertia divide reactor and cross to interlock one kind in short contact reactor to answer device.
630 DEG C -900 DEG C of the reaction temperature of pyrolysis recycle reactor, pyrolysis recycle reactor are riser regenerator, turbulent flow
One or more combinations in fluid bed regenerator, bubbling fluidized bed regenerator.
Gas-solid separator is inertia separator, horizontal cyclone separator, combination one or more in vertical cyclone device.
Returning charge controller and flow controller are on-mechanical control valve or mechanically controlled valve, and on-mechanical control valve returns for L-type
One or more combinations in glassware, U-shaped material returning device, J-type material returning device and N-type material returning device, mechanically controlled valve are hydraulic pressure sliding plug
Valve and electronic sliding plug valve.
The present invention will describe the features of the present invention in detail by embodiment.
4. description of the drawings
Accompanying drawing 1 is the structural representation of the present invention.
The drawing of attached drawing sets bright as follows：
1. gas-solid separator, 2. returning charge controllers, 3. high-efficiency atomizing nozzles, 4. downlink modified-reaction pipes, 5. gas-solids are quick
Separator, 6. pyrolysis oil gas vents, 7. flow control devices, 8. milliseconds of cracking reactors, 9. regenerant inlets, 10. modification regenerations
Reactor, 11. heat exchangers, the outlet of 12. regeneration gases, 13. pyrolysis recycle reactors, 14. air intakes, 15. exhanst gas outlets.
The features of the present invention is described in detail with reference to the accompanying drawings and examples.
5. specific implementation mode
Embodiment, heavy oil millisecond are classified gas phase catalysis and crack producing light olefins coupling device, by gas-solid separator (1), return
Expect controller (2), high-efficiency atomizing nozzle (3), downlink modified-reaction pipe (4), gas-solid quick disconnector (5), pyrolysis oil gas vent
(6), flow control device (7), millisecond cracking reactor (8), regenerant inlet (9), modification regeneration reactor (10), heat exchanger
(11), regeneration gas outlet (12), pyrolysis recycle reactor (13), air intake (14), exhanst gas outlet (15) composition.Downlink is modified
Reaction tube (4) is connected by gas-solid separator (1), returning charge controller (2) and flow control device (7) and modification regeneration reactor (10)
One circular response system of logical composition；Downlink modified-reaction pipe (4) top is provided with symmetrical high-efficiency atomizing nozzle (3), lower part
Equipped with gas-solid quick disconnector (5), gas-solid quick disconnector (5) gas vent is pyrolysis oil gas vent (6), and gas-solid quickly divides
It is connected to modification regeneration reactor (10) lower part by flow regulator (7) from device (5) solid outlet；Modification regeneration reactor
(10) bottom is equipped with regenerant inlet (9), and top is equipped with gas-solid separator (1)；Gas-solid separator (1) solid outlet opens below into
Returning charge controller (2), returning charge controller (2) outlet access downlink modified-reaction pipe (4) top, gas-solid separator (1) gas go out
Mouth is connected by heat exchanger (11) with regeneration gas outlet (12)；Millisecond cracking reactor (8) passes through gas-solid separator (1), returning charge
Controller (2) and flow control device (7) are connected to pyrolysis recycle reactor (13) forms another circular response system；Pyrolysis oil
Gas exports (6) and returning charge controller outlet (2) is directly accessed a millisecond cracking reactor (8) entrance, millisecond cracking reactor together
(8) outlet connection gas-solid quick disconnector (5)；Gas-solid quick disconnector (5) solid outlet passes through flow regulator (7) and cracking
Regeneration reactor (13) lower part is connected to, and gas-solid quick disconnector (1) gas vent is cracking oil gas vent；Pyrolysis recycle reactor
(13) bottom is equipped with air intake (14), and top is equipped with gas-solid separator (1)；Gas-solid separator (1) solid outlet opens below into
Returning charge controller (2), returning charge controller (2) outlet access millisecond cracking reactor (8) entrance, gas-solid separator (1) gas go out
Mouth is connected by heat exchanger (11) with exhanst gas outlet (15).
480 DEG C -850 DEG C of the reaction temperature of downlink modified-reaction pipe (4), solid thermal carriers are semicoke microballoon, aluminium oxide is micro-
Ball, calcium aluminate porous microsphere, magnesium aluminate spinel porous microsphere, alumina silicate porous microsphere, calcium silicates porous microsphere, magnesium silicate are porous
One or more mixture in the porous microsphere carrier of microballoon, carrying alkali metal or/and alkaline-earth metal.
650 DEG C -1250 DEG C of the reaction temperature of modification regeneration reactor (10), modification regeneration reactor (10) be riser again
One or more combinations in raw device, turbulent fluidized bed regenerator, bubbling fluidized bed regenerator, regenerative agent are oxidant and water
The mixture or oxidant of steam, oxidant are one kind in oxygen, air and oxygen-enriched air；Regeneration gas is synthesis gas or cigarette
Gas.
Millisecond cracking reactor (8) 530 DEG C -750 DEG C of reaction temperature, catalyst for cracking be ZSM-5 molecular sieve catalyst,
FCC molecular sieve catalysts select one or more mixtures in type molecular sieve catalyst, alkali solid porous catalyst, milli
Second cracking reactor (8) be downer reactor, the rotation of horizontal inertia divide reactor and cross interlock in short contact reactor one
Kind.
630 DEG C -900 DEG C of the reaction temperature of pyrolysis recycle reactor (13), pyrolysis recycle reactor (13) be riser again
One or more combinations in raw device, turbulent fluidized bed regenerator, bubbling fluidized bed regenerator.
Gas-solid separator (1) is inertia separator, horizontal cyclone separator, group one or more in vertical cyclone device
It closes.
Returning charge controller (2) and flow controller (7) are on-mechanical control valve or mechanically controlled valve, and on-mechanical control valve is
One or more combinations in L-type material returning device, U-shaped material returning device, J-type material returning device and N-type material returning device, mechanically controlled valve are hydraulic pressure
Slide plug valve and electronic sliding plug valve.
When carrying out practically, high-efficiency atomizing nozzle (3) will be preheating to 150 DEG C -350 DEG C of heavy oil from downlink modified-reaction pipe
(4) feed inlet sprays into downlink modified-reaction pipe (4) top, mist of oil and 650 DEG C of -1200 DEG C of height flowed down from returning charge controller (2)
Warm solid thermal carriers millisecond mixing, heating, vaporization and pyrolysis, pyrolysis reaction temperature are 480 DEG C -850 DEG C；Oil gas and solid to be generated
Gas solid separation is carried out in the downward high speed fair current of heat carrier to the gas-solid quick disconnector of downlink modified-reaction pipe (4) bottom；Coking
Solid thermal carriers to be generated enter what modification regeneration reactor (10) lower part was flowed into regenerant inlet (9) through flow controller (7)
Regenerative response occurs for regenerative agent, and regenerative response temperature is 680 DEG C -1250 DEG C, and regeneration gas and high-temp solid heat carrier are being modified again
Gas solid separation is carried out in gas-solid separator (1) at the top of raw reactor (10), high-temp solid heat carrier presses the carrier oil ratio of 1-14
It is flowed at the top of modified downlink reaction tube (4) through returning charge controller (2) and participates in cycle, cracking masout, regeneration gas passes through heat exchanger
(11) it is exported from regeneration gas outlet (12) after exchanging heat；The not condensed direct gas phase of high-temperature oil gas enters a millisecond cracking reactor (8)
Mixed with 600 DEG C -850 DEG C of regeneration catalyst for cracking, occur gas phase catalysis cracking reaction, cracking reaction temperature be 530 DEG C -
750 DEG C, then cracking gas and catalyst for cracking to be generated carry out millisecond gas solid separation by gas-solid separator (1)；Cracking to be generated is urged
Agent enters pyrolysis recycle reactor (13) lower part through flow controller (7) and occurs with the air entered from air intake (14)
Regenerative response, regenerative response temperature are 630 DEG C -900 DEG C, and flue gas and thermal cracking catalyst are in pyrolysis recycle reactor (13)
Gas solid separation is carried out in the gas-solid separator (1) at top, thermal cracking catalyst is by the oil ratio of 1-8 through returning charge controller (2)
It flows into millisecond cracking reactor (8) and participates in circular response, flue gas exports after heat exchanger (11) heat exchange from exhanst gas outlet (15)；
Cracking oil gas enters later separation device separation low-carbon alkene and aromatic hydrocarbons.
Heavy oil millisecond classification gas phase catalysis provided by the present invention cracks producing light olefins coupling device, utilizes inferior heavy oil
Quick alkaline is catalyzed pyrolysis and maximizes production oil gas, and high temp oil gas is selected type and urged without condensation separation, directly progress high temperature millisecond
Change cracking producing light olefins, to make full use of the heat of pyrolysis oil gas, overcomes liquid reactive " cage effect ", reduce heat
Matter transmits the influence to catalytic pyrolysis, drastically reduces the green coke amount and energy consumption of cracking process；Reaction temperature and time are easy to
Regulation and control, while being pyrolyzed the rich characteristic for producing alkene using base catalysis and carrying out shape selective catalysis, increase substantially yield of light olefins
And selectivity, inferior heavy oil triolefin " ethylene, propylene and butylene " total recovery of residual carbon content 15% are up to 50%, wherein propylene
28% and ethylene 15%, far above the total recovery of pyrolysis wax catalysis cracking triolefin 35%；Avoid conventional pyrolytic modification-wax oil
The wax oil of catalytic pyrolysis group technology reheats heating atomization, but still remains liquid reactive " cage effect " and lead to polycondensation
Reaction aggravation, to reduce the general character problem of yield of light olefins and selectivity；In addition flow is short, and equipment steel consumption is low, Gu
Fixed investment substantially reduces；Atmospheric operation is simple, and driving and parking is convenient, and continuity is good, and oil kind is adaptable.
Claims (7)
1. heavy oil millisecond is classified gas phase catalysis and cracks producing light olefins coupling device, it is characterised in that downlink modified-reaction pipe passes through
Gas-solid separator, returning charge controller and flow control device are connected to one circular response system of composition with modification regeneration reactor；Under
Row modified-reaction pipe top is provided with symmetrical high-efficiency atomizing nozzle, and lower part is equipped with gas-solid quick disconnector, gas-solid quick separating
Device gas vent is pyrolysis oil gas vent, and gas-solid quick disconnector solid outlet passes through flow regulator and modification regeneration reactor
Lower part is connected to；Modification regeneration reactor bottom is equipped with regenerant inlet, and top is equipped with gas-solid separator；Gas-solid separator solid goes out
Mouth opens below into returning charge controller, returning charge controller outlet access downlink modified-reaction tube top portion, gas-solid separator gas vent
It is connected with regeneration gas outlet by heat exchanger；Millisecond cracking reactor passes through gas-solid separator, returning charge controller and flow control
Device is connected to pyrolysis recycle reactor forms another circular response system；It is pyrolyzed oil gas vent and the outlet of returning charge controller together
It is directly accessed a millisecond cracking reactor entrance, millisecond cracking reactor outlet connection gas-solid quick disconnector；Gas-solid quick separating
Device solid outlet is connected to by flow regulator with pyrolysis recycle reactor lower part, and gas-solid quick disconnector gas vent is cracking
Oil gas vent；Pyrolysis recycle reactor bottom is equipped with air intake, and top is equipped with gas-solid separator；Gas-solid separator solid outlet
Returning charge controller, returning charge controller outlet access millisecond cracking reactor entrance are opened below into, gas-solid separator gas vent leads to
Heat exchanger is crossed with exhanst gas outlet to be connected.
2. putting forward the heavy oil millisecond classification gas phase catalysis cracking producing light olefins coupling device stated, feature according to claim 1
It is that 480 DEG C -850 DEG C of the reaction temperature of downlink modified-reaction pipe, solid thermal carriers are semicoke microballoon, aluminum oxide micro-sphere, aluminic acid
Calcium porous microsphere, alumina silicate porous microsphere, calcium silicates porous microsphere, magnesium silicate porous microsphere, is born magnesium aluminate spinel porous microsphere
Carry mixture one or more in the porous microsphere carrier of alkali metal or/and alkaline-earth metal.
3. carrying the Combined type lifting riser gasification reactor stated according to claim 2, it is characterised in that modification regeneration reactor
650 DEG C -1250 DEG C of reaction temperature, modification regeneration reactor are riser regenerator, turbulent fluidized bed regenerator, bubbling fluidized bed
One or more combinations in regenerator, regenerative agent are the mixture or oxidant of oxidant and vapor, and oxidant is oxygen
One kind in gas, air and oxygen-enriched air；Regeneration gas is synthesis gas or flue gas.
4. putting forward the heavy oil millisecond classification gas phase catalysis cracking producing light olefins coupling device stated, feature according to claim 1
It is 530 DEG C -750 DEG C of the reaction temperature of cracking reactor, catalyst for cracking is ZSM-5 molecular sieve catalyst, FCC molecular sieves are urged
Agent selects one or more mixtures in type molecular sieve catalyst, alkali solid porous catalyst, millisecond cracking reactor
Reactor and cross is divided to interlock one kind in short contact reactor for downer reactor, the rotation of horizontal inertia.
5. putting forward the heavy oil millisecond classification gas phase catalysis cracking producing light olefins coupling device stated, feature according to claim 1
It is 630 DEG C -900 DEG C of the reaction temperature of pyrolysis recycle reactor, pyrolysis recycle reactor is riser regenerator, turbulent fluidised
One or more combinations in bed regenerator, bubbling fluidized bed regenerator.
6. putting forward the heavy oil millisecond classification gas phase catalysis cracking producing light olefins coupling device stated, feature according to claim 1
It is gas-solid quick disconnector and synthesizes gas separating device to be one in vertical cyclone separator, horizontal cyclone separator, inertia separator
Kind or multiple combinations.
7. putting forward the heavy oil millisecond classification gas phase catalysis cracking producing light olefins coupling device stated, feature according to claim 1
It is that flow regulator is on-mechanical control valve or mechanically controlled valve, on-mechanical control valve is L-type material returning device, U-shaped material returning device, J
One or more combinations in type material returning device and N-type material returning device, mechanically controlled valve are that hydraulic pressure slides plug valve and electronic sliding plug valve.
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Application publication date: 20180720 |