CN109694739A - A kind of crude oil pyrolysis prepares the method and device of low-carbon alkene - Google Patents
A kind of crude oil pyrolysis prepares the method and device of low-carbon alkene Download PDFInfo
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- CN109694739A CN109694739A CN201711002031.0A CN201711002031A CN109694739A CN 109694739 A CN109694739 A CN 109694739A CN 201711002031 A CN201711002031 A CN 201711002031A CN 109694739 A CN109694739 A CN 109694739A
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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
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
- C10G69/06—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of thermal cracking in the absence of hydrogen
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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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/20—C2-C4 olefins
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Abstract
The invention belongs to low-carbon alkene preparation field, the method and device that a kind of crude oil pyrolysis prepares low-carbon alkene is disclosed.This method comprises: 1) crude oil feeding the first pipe of convection section group is preheated, the crude oil after preheating carries out gas-liquid separation by the first cyclone separator, forms the first vapor phase and the first liquid phase；2) the first liquid phase carries out adding hydrogen processing, mixes with liquid hydrocarbon, obtains mixture；3) convection section the first pipe group that mixture is sent into pyrolysis furnace is preheated, and the mixture after preheating carries out gas-liquid separation by the second cyclone separator, forms the second vapor phase and second liquid phase；4) the first vapor phase and the second vapor phase are sent into convection section the second pipe group of pyrolysis furnace, are heated to being sent directly into radiant section after temperature and are cracked, and generate the cracking gas containing low-carbon alkene；5) second liquid phase is contacted with the superheated steam of convection section, is stripped.Method of the invention can improve crude oil pyrolysis efficiency, increase the yield of olefin product.
Description
Technical field
The present invention relates to low-carbon alkene preparation fields, and the side of low-carbon alkene is prepared more particularly, to a kind of crude oil pyrolysis
Method and device.
Background technique
Low-carbon alkene is often referred to the general name of carbon four and the unsaturated hydrocarbon below of carbon four, mainly includes ethylene, third
Alkene, isobutene, butadiene etc. have the Organic Chemicals of high economic value, and with China's expanding economy, these have
The demand of machine industrial chemicals increases year by year, although the production scale of low-carbon alkene is also increasing year by year, is also unable to satisfy day
The demand that benefit increases.Therefore, the technology for effectively improving light olefins output has a wide range of applications.
For a long time, China prepares low-carbon alkene product always with naphtha.But in recent years, with Middle East associated gas
And a large amount of exploitations of U.S.'s shale gas, these cheap petroleum resources are largely used as ethylene raw, cause ethylene related
The sharply decline of product price.In order to cope with the impact of market competition, the raw material sources of ethylene cracker are expanded, raw material is reduced
Cost becomes the effective means of conventional ethylene enterprise cost efficiency.So by special heavy hydrocarbon, it is especially not processed
Crude oil is handled, as pyrolysis furnace raw material, low-carbon alkene advantageously reduces olefin production plant cost of material and the energy disappears to produce
Consumption rapidly adapts to the supply and demand variation of market cracking stock.
Crude oil is generally divided into saturation point, four fragrance point, resin and asphalt components, wherein saturation point and asphalitine difference
Represent component most stable and most unstable in crude oil.It comprising boiling point is more than non-volatile group of high molecular weight of 590 DEG C in crude oil
Point, these nonvolatile elements have fraction not gasified when the convection section of conventional ethane cracking furnace is preheated, not by
The nonvolatile element of gasification is entrained to radiant section with mixed airflow, be easy to cause the coke deposition of radiant section, or even blocking
Radiant section influences the yield for cracking product.
In order to improve yield of light olefins, crude resources is utilized to greatest extent, US3617493 and CN1957068A are disclosed
Using the method for steam cracking device processing crude oil, it is all made of external flash tank preheated by convection section in cracking furnace to handle
Crude oil, realize gas-liquid separation after, gas phase enters radiant section and is cracked, liquid phase can be used as bunker fuel oil use.Wherein pass through
After crossing flash distillation, there are also 5% hydrocarbon raw materials to stay in a liquid, and such flash separation efficiency is lower, moreover, flash vessel equipment is taken up an area
Larger, space utilization rate is low.
CN1018552B and US5580443, which is disclosed, handles the low grade material containing a large amount of heavy distillat using pyrolysis furnace
Method.Raw material is extracted out in convection section midway, is then mixed with a certain amount of superheated dilution steam, then will be weighed by gas-liquid separation
Convection section is returned again to after fraction seperation, is sent into radiant section and is decomposed.After wherein low grade material is mixed with steam, flashed
Separation, can only separate the liquid of 5-20%, separative efficiency is lower.
In above patent document about the processing method of convection section effluent all be using flash vessel carry out gas-liquid separation, but
It is that for the gas-liquid separation containing heavy charge, the separative efficiency of flash vessel is lower, moreover, this container type of flash vessel
Separation equipment volume is big, weight is big, land occupation is wide, in the case of space is small and is not suitable for.
Therefore, it is urgent to provide one kind can effectively improve crude oil pyrolysis efficiency, increases the crude oil of low-carbon alkene product yield
Cleavage method, and cracker can be reduced in the coking and blocking of radiant section and chilling part, to reduce operating cost.
Summary of the invention
In view of the above-mentioned problems existing in the prior art, the object of the present invention is to provide a kind of crude oil pyrolysiss to prepare low-carbon alkene
Method and a kind of crude oil pyrolysis prepare the device of low-carbon alkene.It by adding hydrogen processing, mixes, and adopts with lightweight material
It carries out the techniques such as gas-liquid separation with cyclone separator to combine, when crude oil being overcome directly to carry out steam cracking, in the spoke of pyrolysis furnace
Degree of penetrating and chilling part are easy to happen coking, or even the defect to result in blockage, can effectively improve crude oil pyrolysis efficiency, increase alkene
The yield of hydrocarbon products.
The first aspect of the present invention provides a kind of method that crude oil pyrolysis prepares low-carbon alkene, and this method includes following step
It is rapid:
1) convection section the first pipe group that crude oil is sent into pyrolysis furnace is preheated, the crude oil after preheating passes through the first whirlwind point
Gas-liquid separation is carried out from device, forms the first vapor phase and the first liquid phase；
2) first liquid phase is carried out adding hydrogen processing, is then mixed with liquid hydrocarbon, obtains mixture；
3) convection section the first pipe group that the mixture is sent into pyrolysis furnace is preheated, the mixture after preheating passes through the
Two cyclone separators carry out gas-liquid separation, form the second vapor phase and second liquid phase；
4) the first vapor phase and the second vapor phase are sent into convection section the second pipe group of pyrolysis furnace, are heated to after temperature
It is sent directly into radiant section to be cracked, generates the cracking gas containing low-carbon alkene；
5) second liquid phase is contacted with the superheated steam of convection section, is stripped.
The second aspect of the present invention provides the device that a kind of crude oil pyrolysis prepares low-carbon alkene, which includes cracking
Furnace, hydrogenator and at least two groups cyclone separator, the convection section of the pyrolysis furnace include convection section the first pipe group and convection current
The second pipe group of section, the entrance of convection section the first pipe group and the first cyclone separator, the liquid-phase outlet of the first cyclone and adds
Hydrogen reactor forms closed loop connection, and convection section the first pipe group is connect with the second cyclone inlet, the second cyclone separator
Vapor phase is exported to be connect with the outlet of the vapor phase of the first cyclone separator and convection section the second pipe group.
In the present invention, gas-liquid separation is carried out to the crude oil after preheating using cyclone separator, cyclone separator has structure
Simply, small in size, light weight and cost is low, separative efficiency is high and the advantages of being easily installed operation, lacking for flash vessel can be overcome
Point is particularly suitable for the transformation of existing cracking furnace installation, and the separation of crude oil after preheating is realized in small space；In addition, the party
Method further includes plus hydrogen processing, and using liquid hydrocarbon with to add the material after hydrogen processing mix etc. technique in combination, effectively mention
High crude oil pyrolysis efficiency increases the yield of olefin product, reduces pyrolysis furnace in the coking and blocking of radiant section and chilling part, drop
Low operating cost.
Other features and advantages of the present invention will then part of the detailed description can be specified.
Specific embodiment
Detailed description of the preferred embodiments below.It should be understood that described herein specific
Embodiment is merely to illustrate and explain the present invention, and is not intended to restrict the invention.
According to the first aspect of the invention, the present invention provides a kind of method that crude oil pyrolysis prepares low-carbon alkene, the party
Method the following steps are included:
1) convection section the first pipe group that crude oil is sent into pyrolysis furnace is preheated, the crude oil after preheating passes through the first whirlwind point
Gas-liquid separation is carried out from device, forms the first vapor phase and the first liquid phase；
2) first liquid phase is carried out adding hydrogen processing, is then mixed with liquid hydrocarbon, obtains mixture；
3) convection section the first pipe group that the mixture is sent into pyrolysis furnace is preheated, the mixture after preheating passes through the
Two cyclone separators carry out gas-liquid separation, form the second vapor phase and second liquid phase；
4) the first vapor phase and the second vapor phase are sent into convection section the second pipe group of pyrolysis furnace, are heated to after temperature
It is sent directly into radiant section to be cracked, generates the cracking gas containing low-carbon alkene；
5) second liquid phase is contacted with the superheated steam of convection section, is stripped.
In the present invention, the second liquid phase after stripping can make heavy oil.
According to the present invention, the method also includes adding steam and/or hydrogen at least once, the step is settable
In any step before being sent into radiant section, when it is set in step 2), carried out after Ying Jia hydrogen processing.Steam
And/or the addition of hydrogen, the hydrocarbon partial pressure of cracking stock is reduced, the generation of low-carbon alkene is conducive to.
The steam can be acid processing steam or the processing steam handled by depickling.The steam can be using this
Any mode well known to field is heated, and the preferably described steam is overheated in the convection section of pyrolysis furnace.
In the present invention, add hydrogen processing that can select in hydrotreating, hydrogenation and hydrogenation cracking at least the first liquid phase
One kind, preferably hydrotreating.
In the present invention, in adding the first liquid phase after hydrogen processing be added liquid hydrocarbon be in order to make pyrolysis furnace have than it is original more
High coil outlet temperature (COT), and improve the yield of low-carbon alkene in product.It is preferred that the boiling point of the liquid hydrocarbon is 37-
565℃.The specific example of the liquid hydrocarbon includes but is not limited to: light straight-run naphtha, kerosene, weight normal pressure tail oil, hydrogenation tail oil,
Isocrackate etc..
According to the present invention, hydrogen is added to add in the mixture (mixture of the first liquid phase and liquid hydrocarbon i.e. plus after hydrogen processing)
The weight percent of the first liquid phase after work can be 1-99%, preferably 20-95%.
According to the present invention, the outflow temperature of the crude oil after preheating is 315-565 DEG C, pressure 0.1-1.5MPa.
In the present invention, the Crude Oil Transportation after preheating to the first cyclone separator is subjected to gas-liquid separator, the original after preheating
Liquid phase volume content of the oil in the first cyclone inlet is preferably 0.01-5%, more preferably 0.02-2%.
According to the present invention, the outflow temperature of the mixture after preheating is 315-565 DEG C, pressure 0.1-1.5MPa.
In the present invention, the mixture after preheating is delivered to the second cyclone separator and carries out gas-liquid separator, after preheating
Liquid phase volume content of the mixture in the second cyclone inlet is preferably 0.01-5%, more preferably 0.02-2%.
In the present invention, " cyclone separator " refers to the cyclone separator of broad sense, has both included the " cyclonic separation of narrow sense
Device " also includes separator similar with its principle in this field, such as cyclone separator.If not otherwise specified, it is mentioned in the present invention
And cyclone separator be broad sense cyclone separator.
According to the present invention, the big portion of working media of the first cyclone separator and the second cyclone separator of gas-liquid separation is carried out
It is divided into gas, cyclone separator commonly used in the art can be selected, as long as can be realized separation of high-concentration, height at high temperature
The liquid of viscosity, and separative efficiency is up to 90% or more.
The specific example of first cyclone separator and the second cyclone separator includes but is not limited to: rectangle entrance whirlwind
Separator, volute cyclone separator, axis conductance vane type cyclone separator, straight barrel type cyclone separator, the combined rotation of cone cylinder
More tornadotron separators of wind separator, reverse-flow cyclone separator, single flow cyclone separator, single flow etc..First whirlwind point
It may be the same or different from device and the second cyclone separator.Under preferable case, first cyclone separator and the second rotation
Wind separator each is selected from volute cyclone separator, axis conductance vane type cyclone separator, straight barrel type cyclone separator, cone cylinder
Combined cyclone separator or single flow cyclone separator.
Crude oil or mixture after the preheating of convection section in cracking furnace the first pipe group have high temperature, high liquid hold-up, liquid viscous
Spend larger feature.The first rotation for this kind of gas-liquid mixture, in order to guarantee the separative efficiency of cyclone separator, in the present invention
Wind separator and the second cyclone separator are preferably provided with the cyclone separator of internal component, for example increase in cyclone separator
Fluid cylinder is skimmed to reduce the loss of the liquid film on the wall surface of cyclone separator top in top, can also simultaneously or it is different when under cyclone separator
Portion increases isolation board and vortex breaker to reduce gas swirl tail portion to the liquid on the liquid and wall surface of cyclone separator lower part
It carries under one's arms.
In the present invention, cyclone separator number, which can according to need, to be selected, the first cyclone separator and the second whirlwind
Separator may include one or more cyclone separators.When comprising multiple cyclone separators, multiple cyclone separators be can be used
Mode is connected in parallel or series.
In the present invention, the liquid content in first vapor phase and the second vapor phase is lower than 10g/m3, preferably shorter than
200mg/m3。
Pyrolysis furnace of the present invention can be the pyrolysis furnace of steam cracking producing light olefins commonly used in the art.
Under preferable case, the pyrolysis furnace used is tube cracking furnace.Pyrolysis furnace usually mainly includes convection section, radiant section, chilling part
And gas burning system.In pyrolysis furnace, crude oil is sent into the first pipe of convection section group, and (convection section includes convection section the first pipe group and convection current
The second pipe group of section), it is contacted with superheated steam and is preheated (315-565 DEG C), be then provided with the crude oil feeding after preheating interior
First cyclone separator of component carries out gas-liquid separation, and the first isolated liquid phase carries out plus hydrogen processing, after adding hydrogen processing
First liquid phase is mixed with liquid hydrocarbon, obtains mixture, and convection section the first pipe group that mixture is sent into pyrolysis furnace is preheated
(315-565 DEG C), the mixture after preheating carry out gas-liquid separation by the second cyclone separator, form the second vapor phase and second
First vapor phase and the second vapor phase are continued to be preheated to across temperature (425-705 DEG C), so by liquid phase in convection section the second pipe group
Enter radiant section afterwards and carry out steam cracking reaction, generates the cracking gas for being rich in low-carbon alkene, cracking gas is laggard out from radiant section
Enter chilling part, to obtain low-carbon alkene.
Pyrolysis furnace of the present invention and the method that low-carbon alkene is obtained from pyrolysis furnace have been those skilled in the art
Known, details are not described herein.
According to the second aspect of the invention, the present invention provides the device that a kind of crude oil pyrolysis prepares low-carbon alkene, the dresses
It sets including pyrolysis furnace, hydrogenator and at least two groups cyclone separator, the convection section of the pyrolysis furnace includes convection section first
Pipe group and convection section the second pipe group, convection section the first pipe group and the entrance of the first cyclone separator, the liquid of the first cyclone
Mutually outlet forms closed loop with hydrogenator and connects, and convection section the first pipe group is connect with the second cyclone inlet, the second rotation
The vapor phase outlet of wind separator is connect with the outlet of the vapor phase of the first cyclone separator and convection section the second pipe group.
Crude oil pyrolysis of the invention prepares (the first cyclonic separation of cyclone separator employed in the device of low-carbon alkene
Device, the second cyclone separator) and pyrolysis furnace as it was noted above, details are not described herein.
In addition, hydrogenator in the present invention can be according to adding the mode of hydrogen processing to carry out conventional selection.
The present invention is described in detail by the following examples.
The composition of the crude oil used in the following Examples and Comparative Examples is as shown in table 1 below, and the composition is according to ASTM
D5307 method measures.
Table 1
| Analysis project | ASTM D5307 |
| IP, DEG C | 69 |
| 10%, DEG C | 192 |
| 20%, DEG C | 272 |
| 30%, DEG C | 337 |
| 40%, DEG C | 393 |
| 50%, DEG C | 446 |
| 60%, DEG C | 508 |
| 70%, DEG C | 595 |
| 75%, DEG C | 653 |
| 80%, DEG C | - |
| 90%, DEG C | - |
| EP, DEG C | - |
Embodiment 1
The present embodiment is for illustrating the method that crude oil pyrolysis of the invention prepares low-carbon alkene.
Specifically includes the following steps:
1, the crude oil of dewatering and desalting is sent directly into CBL-III type pyrolysis furnace (purchased from Sinopec work group company),
Convection section the first pipe group is preheated, and the crude oil temperature after preheating is 380 DEG C, pressure 0.15MPa.Crude oil after preheating is sent
Enter to be provided with the volute cyclone separator (the first cyclone separator) of isolation board and vortex breaker inner member, carries out gas-liquid separation.
The entrance liquid content of volute cyclone separator is 0.04% (V/V), density of liquid phase 800kg/m3, density of gas phase is
0.85kg/m3.The separative efficiency of volute cyclone separator is 98%, and the liquid phase in vapor phase after separation is 200mg/
m3。
2, the liquid phase isolated is subjected to hydrotreating, the catalyst used is Co-Ni-Mo/Al2O3, hydrogenation temperature 270
DEG C, hydrogenation pressure 2.6MPa, hydrogen-oil ratio 3.0, crude oil volume space velocity is 2.0h-1, monoene hydrogenation rate 95%.After adding hydrogen processing
Logistics mixed with naphtha, mixture is made, wherein plus the mass ratio of the logistics after hydrogen processing and naphtha is 90: 10.
3, the mixture is also fed into CBL-III type pyrolysis furnace (purchased from Sinopec work group company), in convection section
First pipe group is preheated, and the temperature of the mixture after preheating is 380 DEG C, pressure 0.15MPa.Mixture after preheating is sent
Enter to be provided with the guide-vane cyclone separator (the second cyclone separator) that fluid cylinder, isolation board and vortex breaker inner member are skimmed in top, into
Row gas-liquid separation.The entrance liquid content of guide-vane cyclone separator is 0.03% (V/V), density of liquid phase 800kg/m3, gas
Phase density is 0.80kg/m3.The separative efficiency of guide-vane cyclone separator is 98%, the liquid phase in vapor phase after separation
For 200mg/m3。
4, the vapor phase isolated in step 3 is sent into CBL-III steam to split together with the vapor phase isolated in step 1
Convection section the second pipe group for solving furnace is heated to entering radiant section afterwards across temperature (510 DEG C), is cracked, generate olefin-containing
Cracking gas；The operating parameter of the radiant section is water-oil factor 0.75, and coil outlet temperature is 840 DEG C, residence time 0.21s.Product
Yield of ethene be 23.54wt%, the yield of propylene is 12.27wt%, and the yield of 1,3-butadiene is 4.42wt%, and triolefin is received
Rate is 40.22wt%.The liquid phase isolated in step 3 is contacted with the superheated steam of convection section, after being stripped, makees heavy combustion
Material oil.
Comparative example 1
Steam cracking reaction is carried out according to the method for embodiment 1, the difference is that, it will be straight by the crude oil of dewatering and desalting
It picks in CBL-III type pyrolysis furnace, after convection section, is directly entered radiant section, is cracked.Cracking gas uses LUMMUS
Sequence separation process.It carries out analysis to steam cracking reaction product to learn, the yield of ethylene is 21.49wt%, the receipts of propylene
Rate is 13.29wt%, and the yield of 1,3-butadiene is 4.03wt%, and triolefin yield is 38.81wt%.
Comparative example 2
Steam cracking reaction is carried out according to the method for embodiment 1, the difference is that, it will be by the convection section the of pyrolysis furnace
Crude oil after the preheating of one pipe group is sent into the first flash tank and carries out gas-liquid separation, separative efficiency 90%, the gas phase being then demultiplex out
Convection section the second pipe group for returning to pyrolysis furnace is cracked after continuing preheating into radiant section, the liquid that the first flash vessel is isolated
Phase product continues plus hydrogen processing, then mixes with naphtha, after the preheating of convection section in cracking furnace the first pipe group, into the
Two flash vessels carry out gas-liquid separation, and separative efficiency 90%, then gas phase, which returns after convection section in cracking furnace continues preheating, enters radiation
Duan Jinhang cracking, cracking gas use the sequence separation process of LUMMUS.It carries out analysis to steam cracking reaction product to learn, ethylene
Yield be 23.36wt%, the yield of propylene is 12.32wt%, and the yield of 1,3-butadiene is 4.37wt%, and triolefin yield is
40.05wt%.
Comparison is received it is found that can significantly improve low-carbon alkene using the method that crude oil pyrolysis of the invention prepares low-carbon alkene
Rate.Specifically, embodiment 1 and comparative example 1 are compared, the crude oil in comparative example 1 directly carries out steam cracking reaction, and real
It applies crude oil in example 1 and carries out gas-liquid separation by cyclone separator twice, add hydrogen processing, the place of techniques such as mix with liquid hydrocarbon
Reason.Find out that embodiment 1 has obviously obtained higher yield of light olefins by cracking result.Embodiment 1 and comparative example 2 are compared
Compared with the gas-liquid separation in comparative example 2 is carried out using flash tank, and carries out gas-liquid separation using cyclone separator in embodiment 1.By
Cracking result finds out that embodiment 1 obtains higher yield of light olefins.
Various embodiments of the present invention are described above, above description is exemplary, and non-exclusive, and
It is not limited to disclosed each embodiment.Without departing from the scope and spirit of illustrated each embodiment, for this skill
Many modifications and changes are obvious for the those of ordinary skill in art field.
Claims (10)
1. a kind of method that crude oil pyrolysis prepares low-carbon alkene, which is characterized in that method includes the following steps:
1) convection section the first pipe group that crude oil is sent into pyrolysis furnace is preheated, the crude oil after preheating passes through the first cyclone separator
Gas-liquid separation is carried out, the first vapor phase and the first liquid phase are formed；
2) first liquid phase is carried out adding hydrogen processing, is then mixed with liquid hydrocarbon, obtains mixture；
3) convection section the first pipe group that the mixture is sent into pyrolysis furnace is preheated, the mixture after preheating passes through the second rotation
Wind separator carries out gas-liquid separation, forms the second vapor phase and second liquid phase；
4) the first vapor phase and the second vapor phase are sent into convection section the second pipe group of pyrolysis furnace, are heated to after temperature directly
It is sent into radiant section to be cracked, generates the cracking gas containing low-carbon alkene；
5) second liquid phase is contacted with the superheated steam of convection section, is stripped.
2. according to the method described in claim 1, wherein, the method also includes adding steam and/or hydrogen at least once
Step；The steam is preferably acid processing steam or the processing steam by depickling processing；The further preferred steam exists
It is overheated in the convection section of pyrolysis furnace.
3. according to the method described in claim 1, wherein, described plus hydrogen processing includes in hydrotreating, hydrogenation and hydrogenation cracking
At least one.
4. according to the method described in claim 1, wherein, the boiling point of the liquid hydrocarbon is 37-565 DEG C；The liquid hydrocarbon is preferred
For at least one of light straight-run naphtha, kerosene, weight normal pressure tail oil, hydrogenation tail oil and isocrackate.
5. according to the method described in claim 1, wherein, in the mixture adding the weight percent of the first liquid phase after hydrogen processing
Number is 1-99%, preferably 20-95%.
6. according to the method described in claim 1, wherein, the outflow temperature of the crude oil after preheating is 315-565 DEG C, and pressure is
0.1-1.5MPa；Liquid phase volume content of the crude oil in the first cyclone inlet after preheating is 0.01-5%, preferably
0.02-2%.
7. according to the method described in claim 1, wherein, the outflow temperature of the mixture after preheating is 315-565 DEG C, and pressure is
0.1-1.5MPa；Liquid phase volume content of the mixture in the second cyclone inlet after preheating is 0.01-5%, preferably
For 0.02-2%.
8. according to the method described in claim 1, wherein, first cyclone separator and the second cyclone separator each are selected from
Volute cyclone separator, axis conductance vane type cyclone separator, straight barrel type cyclone separator, the combined cyclone separator of cone cylinder
Or single flow cyclone separator；
It is preferred that first cyclone separator and the second cyclone separator are provided with internal component, the internal component includes being located at
Isolation board, the vortex breaker for skimming fluid cylinder and/or cyclone separator lower part at the top of cyclone separator.
9. according to the method described in claim 1, wherein, the liquid content in first vapor phase and the second vapor phase is lower than
10g/m3, preferably shorter than 200mg/m3。
10. the device that a kind of crude oil pyrolysis prepares low-carbon alkene, which is characterized in that the device includes pyrolysis furnace, hydrogenator
With at least two groups cyclone separator, the convection section of the pyrolysis furnace includes convection section the first pipe group and convection section the second pipe group, institute
The entrance of convection section the first pipe group and the first cyclone separator, the liquid-phase outlet of the first cyclone and hydrogenator formation is stated to close
Ring connection, convection section the first pipe group connect with the second cyclone inlet, and the vapor phase of the second cyclone separator exports and the
The vapor phase outlet of one cyclone separator is connected with convection section the second pipe group.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111196936A (en) * | 2020-01-17 | 2020-05-26 | 上海竣铭化工工程设计有限公司 | Combined processing method and device for directly producing olefin from crude oil |
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| CN112708455A (en) * | 2019-10-26 | 2021-04-27 | 中国石油化工股份有限公司 | Method and system for preparing low-carbon olefin from crude oil |
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| CN112708454B (en) * | 2019-10-26 | 2022-05-24 | 中国石油化工股份有限公司 | Crude oil processing method and system |
| CN112708455B (en) * | 2019-10-26 | 2022-05-24 | 中国石油化工股份有限公司 | Method and system for preparing low-carbon olefin from crude oil |
| CN112745942A (en) * | 2019-10-29 | 2021-05-04 | 中国石油化工股份有限公司 | Crude oil processing method and system |
| CN112745942B (en) * | 2019-10-29 | 2022-12-13 | 中国石油化工股份有限公司 | Crude oil processing method and system |
| CN111196936A (en) * | 2020-01-17 | 2020-05-26 | 上海竣铭化工工程设计有限公司 | Combined processing method and device for directly producing olefin from crude oil |
| CN114436735A (en) * | 2020-10-30 | 2022-05-06 | 中国石油化工股份有限公司 | Crude oil cracking device and method |
| CN114436735B (en) * | 2020-10-30 | 2024-06-04 | 中国石油化工股份有限公司 | Device and method for cracking crude oil |
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