CN109694730B - Method and device for preparing low-carbon olefin by cracking crude oil - Google Patents
Method and device for preparing low-carbon olefin by cracking crude oil Download PDFInfo
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- CN109694730B CN109694730B CN201711002046.7A CN201711002046A CN109694730B CN 109694730 B CN109694730 B CN 109694730B CN 201711002046 A CN201711002046 A CN 201711002046A CN 109694730 B CN109694730 B CN 109694730B
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- 238000005336 cracking Methods 0.000 title claims abstract description 77
- 239000010779 crude oil Substances 0.000 title claims abstract description 55
- 238000000034 method Methods 0.000 title claims abstract description 34
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 30
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 title claims abstract description 25
- 238000000926 separation method Methods 0.000 claims abstract description 33
- 239000007788 liquid Substances 0.000 claims abstract description 29
- 230000005855 radiation Effects 0.000 claims abstract description 18
- 239000012808 vapor phase Substances 0.000 claims abstract description 18
- 239000007791 liquid phase Substances 0.000 claims abstract description 17
- 150000001336 alkenes Chemical class 0.000 claims abstract description 8
- 238000010438 heat treatment Methods 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 15
- 230000008569 process Effects 0.000 claims description 7
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- 239000001257 hydrogen Substances 0.000 claims description 3
- 238000010791 quenching Methods 0.000 abstract description 5
- 238000004939 coking Methods 0.000 abstract description 4
- 230000000171 quenching effect Effects 0.000 abstract description 4
- 238000002360 preparation method Methods 0.000 abstract description 3
- 239000002994 raw material Substances 0.000 description 13
- 238000004230 steam cracking Methods 0.000 description 10
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 8
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 8
- 239000005977 Ethylene Substances 0.000 description 8
- 230000000052 comparative effect Effects 0.000 description 7
- -1 ethylene, propylene, isobutene Chemical class 0.000 description 7
- 239000000047 product Substances 0.000 description 7
- 238000004458 analytical method Methods 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 239000003921 oil Substances 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 3
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 3
- 150000005671 trienes Chemical class 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000010763 heavy fuel oil Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000009835 boiling Methods 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000003776 cleavage reaction Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000010747 number 6 fuel oil Substances 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000007017 scission Effects 0.000 description 1
- 229930195735 unsaturated hydrocarbon Natural products 0.000 description 1
Classifications
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
- C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
- C07C4/04—Thermal processes
-
- 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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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention belongs to the field of low-carbon olefin preparation, and discloses a method and a device for preparing low-carbon olefin by cracking crude oil. The method comprises the following steps: 1) sending crude oil into a first pipe group of a convection section of a cracking furnace for preheating; 2) carrying out gas-liquid separation on the preheated crude oil through a cyclone separator to form a vapor phase and a liquid phase; 3) sending the vapor phase into a second tube group of a convection section of the cracking furnace, heating to a cross temperature, and then directly sending into a radiation section for cracking to generate cracking gas containing low-carbon olefin; 4) the liquid phase is contacted with superheated steam in a convection section for stripping. The method can effectively improve the cracking efficiency of crude oil, increase the yield of olefin products, reduce coking and blockage of the cracking furnace in a radiation section and a quenching part, and reduce the operation cost.
Description
Technical Field
The invention relates to the field of preparation of low-carbon olefins, in particular to a method and a device for preparing low-carbon olefins by cracking crude oil.
Background
The low-carbon olefin is generally referred to as unsaturated hydrocarbon with four carbon atoms or less, mainly comprises organic chemical raw materials with high economic value, such as ethylene, propylene, isobutene, butadiene and the like, and with the development of economy in China, the demand of the organic chemical raw materials is increased year by year, and although the production scale of the low-carbon olefin is also increased year by year, the increased demand cannot be met. Therefore, the technology for effectively improving the yield of the low-carbon olefin has wide application prospect.
For a long time, China always prepares low-carbon olefin products from naphtha. However, in recent years, along with the mass exploitation of middle east oilfield associated gas and U.S. shale gas, these cheap oil and gas resources are used in large quantities as ethylene raw materials, which causes a sharp drop in the price of ethylene-related products. In order to cope with the impact of market competition, the raw material source of the ethylene cracking device is expanded, the raw material cost is reduced, and the method becomes an effective means for cost reduction and efficiency improvement of the traditional ethylene enterprises. Therefore, special heavy hydrocarbons, especially unprocessed crude oil, are used as the raw materials of the cracking furnace to produce low-carbon olefin, which is beneficial to reducing the raw material cost and energy consumption of an olefin production device and is quickly adapted to the supply and demand change of the cracking raw materials in the market.
Crude oil is generally divided into four components, a saturates, an aromatics, a gums and asphaltenes, wherein saturates and asphaltenes represent the most stable and the least stable components of the crude oil, respectively. The crude oil contains high molecular weight nonvolatile components with the boiling point of more than 590 ℃, and when the convection section of a conventional ethylene cracking furnace is preheated, a small part of the nonvolatile components are not gasified, and the unvaporized nonvolatile components are carried to the radiation section along with the mixed gas flow, so that coking deposition of the radiation section is easily caused, even the radiation section is blocked, and the yield of cracked products is influenced.
In order to improve the yield of low-carbon olefin and utilize crude oil resources to the maximum extent, US3617493 and CN1957068A disclose methods for treating crude oil by using a steam cracking device, wherein an external flash tank is used for treating crude oil preheated in a convection section of a cracking furnace, after gas-liquid separation is realized, a gas phase enters a radiation section for cracking, and a liquid phase can be used as bunker fuel oil. Wherein, after flash evaporation, 5 percent of hydrocarbon raw materials are remained in liquid, the flash evaporation separation efficiency is lower, and the flash evaporator device occupies larger space and has low space utilization rate.
CN1018552B and US5580443 disclose a process for treating a low grade feedstock containing a large amount of heavy fractions with a cracking furnace. The raw material is pumped out in the middle of the convection section, then mixed with a certain amount of superheated dilution steam, separated from heavy fraction by gas-liquid separation, returned to the convection section, and sent to the radiation section for decomposition. Wherein, the low-grade raw materials are mixed with steam and then are subjected to flash separation, only 5 to 20 percent of liquid can be separated, and the separation efficiency is lower.
In the above patent documents, the vapor-liquid separation is carried out by using a flash vessel as a method for treating the effluent in the convection section, but the separation efficiency in the flash vessel is low for the vapor-liquid separation of the heavy raw material, and the vessel type separation equipment such as the flash vessel is large in volume, heavy in weight, and wide in floor space, and is not suitable for the case of small space.
Therefore, it is highly desirable to provide a crude oil cracking method which can effectively improve the crude oil cracking efficiency, increase the yield of low carbon olefin products, and reduce the coking and blockage of the cracking device in the radiant section and the quenching section, thereby reducing the operation cost.
Disclosure of Invention
In view of the above problems in the prior art, the present invention is to provide a method for preparing low carbon olefins by cracking crude oil, and an apparatus for preparing low carbon olefins by cracking crude oil. The method adopts the cyclone separator to carry out gas-liquid separation, overcomes the defects that the radiation degree and quenching part of a cracking furnace are easy to coke and even cause blockage when crude oil is directly subjected to steam cracking, and can effectively improve the cracking efficiency of the crude oil and increase the yield of olefin products.
The first aspect of the invention provides a method for preparing low-carbon olefins by cracking crude oil, which comprises the following steps:
1) sending crude oil into a first pipe group of a convection section of a cracking furnace for preheating;
2) carrying out gas-liquid separation on the preheated crude oil through a cyclone separator to form a vapor phase and a liquid phase;
3) sending the vapor phase into a second tube group of a convection section of the cracking furnace, heating to a cross temperature, and then directly sending into a radiation section for cracking to generate cracking gas containing low-carbon olefin;
4) the liquid phase is contacted with superheated steam in a convection section for stripping.
The invention provides a device for preparing low-carbon olefin by cracking crude oil, which comprises a cracking furnace and a cyclone separator, wherein a convection section of the cracking furnace comprises a convection section first tube bank and a convection section second tube bank, the convection section first tube bank is connected with an inlet of the cyclone separator, and the convection section second tube bank is connected with a vapor phase outlet of the cyclone separator.
In the invention, the preheated crude oil is subjected to gas-liquid separation by adopting the cyclone separator, the cyclone separator has the advantages of simple structure, small volume, light weight, low cost, high separation efficiency and convenient installation and operation, can overcome the defects of a flash evaporator, is particularly suitable for the reconstruction of the conventional cracking furnace device, and realizes the separation of the preheated crude oil in a narrow space; in addition, the high-efficiency gas-liquid separation of the cyclone separator can effectively improve the cracking efficiency of crude oil, increase the yield of olefin products, reduce the coking and blockage of the cracking furnace in a radiation section and a quenching part and reduce the operation cost.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Detailed Description
The following describes in detail specific embodiments of the present invention. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.
According to a first aspect of the present invention, the present invention provides a method for preparing low carbon olefins by cracking crude oil, comprising the following steps:
1) sending crude oil into a first pipe group of a convection section of a cracking furnace for preheating;
2) carrying out gas-liquid separation on the preheated crude oil through a cyclone separator to form a vapor phase and a liquid phase;
3) sending the vapor phase into a second tube group of a convection section of the cracking furnace, heating to a cross temperature, and then directly sending into a radiation section for cracking to generate cracking gas containing low-carbon olefin;
4) the liquid phase is contacted with superheated steam in a convection section for stripping.
In the invention, the stripped liquid phase can be used as heavy fuel oil.
According to the invention, the method also comprises, before being sent to the radiant section, at least one step of adding steam and/or hydrogen. The addition of steam and/or hydrogen reduces the hydrocarbon partial pressure of the cracking raw material, and is beneficial to the generation of low-carbon olefin.
The steam may be sour process steam or deacidified process steam. The steam may be heated by any means known in the art, and is preferably superheated in the convection section of the furnace.
According to the invention, in the step 1), the outflow temperature of the preheated crude oil is 315-565 ℃, and the pressure is 0.1-1.5 MPa.
In the present invention, the preheated crude oil is transferred to the cyclone separator to be subjected to gas-liquid separation, and the liquid phase volume content of the preheated crude oil at the inlet of the cyclone separator may be 0.01 to 5%, preferably 0.02 to 2%.
In the present invention, the "cyclone" refers to a cyclone in a broad sense, and includes both a "cyclone" in a narrow sense and a separation device similar to the principle thereof in the art, such as a cyclone. Unless otherwise specified, the cyclone separators mentioned in the present invention are all cyclone separators in a broad sense.
According to the invention, most of working media of the cyclone separator for gas-liquid separation are gas, and the cyclone separator which is conventionally used in the field can be selected as long as the cyclone separator can separate high-concentration and high-viscosity liquid at high temperature and the separation efficiency is more than 90%.
Specific examples of the cyclone separator include, but are not limited to: the cyclone separator comprises a rectangular inlet cyclone separator, a volute type cyclone separator, an axial flow guide vane type cyclone separator, a straight cylinder type cyclone separator, a cone cylinder combined type cyclone separator, a counter-flow type cyclone separator, a straight-flow type multi-cyclone pipe separator and the like. Preferably, the cyclone separator is selected from a spiral shell type cyclone separator, an axial flow guide vane type cyclone separator, a straight cylinder type cyclone separator, a cone and cylinder combination type cyclone separator or a straight flow type cyclone separator.
The crude oil preheated by the first tube group of the convection section of the cracking furnace has the characteristics of high temperature, high liquid content and high liquid viscosity. For such gas-liquid mixture, in order to ensure the separation efficiency of the cyclone separator, the cyclone separator in the invention is preferably provided with an internal component, such as a top skimming cylinder is added in the cyclone separator to reduce the loss of liquid film on the wall surface of the upper part of the cyclone separator, and a separation plate and a vortex breaker are added in the lower part of the cyclone separator to reduce the entrainment of the tail part of the gas vortex to the liquid in the lower part of the cyclone separator and the liquid on the wall surface.
In the invention, the number of the cyclone separators can be selected according to the requirement, and one or more cyclone separators can be included. When a plurality of cyclone separators are included, the plurality of cyclone separators may be connected in parallel or in series.
In the invention, when the crude oil preheated by the convection section is separated into a vapor phase and a liquid phase, the content of the liquid phase in the vapor phase is lower than 10g/m3Preferably less than 200mg/m3。
The cracking furnace adopted by the invention can be a cracking furnace for preparing low-carbon olefin by steam cracking which is conventionally used in the field. Preferably, the cracking furnace used is a tubular cracking furnace. Cracking furnaces typically include primarily a convection section, a radiant section, a quench section, and a gas fired system. In the cracking furnace, crude oil is sent into a first tube bank of a convection section (the convection section comprises the first tube bank of the convection section and a second tube bank of the convection section), is contacted with superheated steam for preheating (315-.
The cracking furnace used in the present invention and the method for obtaining low carbon olefins from the cracking furnace are well known to those skilled in the art and will not be described herein.
According to a second aspect of the present invention, the present invention provides an apparatus for preparing low carbon olefins by cracking crude oil, the apparatus comprising a cracking furnace and a cyclone separator, wherein a convection section of the cracking furnace comprises a convection section first tube bank and a convection section second tube bank, the convection section first tube bank is connected with an inlet of the cyclone separator, and the convection section second tube bank is connected with a vapor phase outlet of the cyclone separator.
The cyclone separator and the cracking furnace used in the device for preparing low-carbon olefins by cracking crude oil according to the present invention are as described above, and are not described herein again.
The present invention will be described in detail below with reference to examples.
The compositions of the crude oils used in the following examples and comparative examples, which were measured according to the method of ASTM D5307, are shown in table 1 below.
TABLE 1
| Analysis item | ASTM D5307 |
| IP，℃ | 69 |
| 10％，℃ | 192 |
| 20％，℃ | 272 |
| 30％，℃ | 337 |
| 40％，℃ | 393 |
| 50％，℃ | 446 |
| 60％，℃ | 508 |
| 70％，℃ | 595 |
| 75％，℃ | 653 |
| 80％，℃ | - |
| 90％，℃ | - |
| EP，℃ | - |
Example 1
This example illustrates the process of the present invention for the preparation of lower olefins by cracking crude oil.
The method specifically comprises the following steps:
1. the dehydrated and desalted crude oil is injected into a CBL-III type cracking furnace (purchased from China petrochemical industry group company), and is preheated in a first tube group of a convection section of a steam cracking furnace, wherein the temperature of the preheated crude oil is 380 ℃, and the pressure is 0.15 MPa.
2. Sending the preheated crude oil into a guide vane type cyclone separator with internal components, wherein the internal components are a top skimming cylinder, a lower isolation plate and a vortex breaker, and carrying out gas-liquid separation. The inlet liquid content of the cyclone was 0.04% (V/V), wherein the liquid density was 800kg/m3Gas phase density of 0.85kg/m3. The separation efficiency of the cyclone separator was 98%, and the liquid phase in the separated vapor phase was 200mg/m3。
3. And (3) sending the vapor phase separated in the step (2) into a second tube group of a convection section of the steam cracking furnace, preheating to a cross temperature (510 ℃), and then entering a radiation section for cracking. The operation parameters of the radiation section are that the water-oil ratio is 0.75, the outlet temperature of the furnace tube is 840 ℃, and the retention time is 0.21 s. The yield of ethylene in the cleavage product was 23.37 wt%, the yield of propylene was 12.12 wt%, the yield of 1, 3-butadiene was 4.43 wt%, and the yield of triene was 39.92 wt%. And (3) contacting the liquid phase separated in the step (2) with superheated steam in a convection section, and performing steam stripping to obtain the heavy fuel oil.
Comparative example 1
The steam cracking reaction was carried out according to the method of example 1, except that the dehydrated and desalted crude oil was directly fed into a CBL-III type cracking furnace, passed through a convection section, and then directly fed into a radiation section for cracking. The pyrolysis gas adopts a sequential separation process of LUMMUS. Analysis of the steam cracking reaction product revealed that the yield of ethylene was 21.49 wt%, the yield of propylene was 13.29 wt%, the yield of 1, 3-butadiene was 4.03 wt%, and the yield of triene was 38.81 wt%.
Comparative example 2
The steam cracking reaction was carried out according to the method of example 1, except that the crude oil preheated in the first tube group of the convection section of the cracking furnace was sent to the flash evaporator for gas-liquid separation with a separation efficiency of 90%, then the separated gas phase was returned to the second tube group of the convection section of the cracking furnace, after continuing preheating, it entered the radiation section for cracking, and the cracked gas was separated in sequence by LUMMUS. Analysis of the steam cracking reaction product revealed that the yield of ethylene was 22.61% by weight, the yield of propylene was 12.38% by weight, the yield of 1, 3-butadiene was 4.23% by weight, and the yield of triene was 39.22% by weight.
The comparison shows that the method for preparing the low-carbon olefin by cracking the crude oil can obviously improve the yield of the low-carbon olefin. Specifically, comparing example 1 with comparative example 1, the crude oil in comparative example 1 is directly subjected to steam cracking reaction, while the crude oil in example 1 is preheated in the convection section and then sent to a cyclone separator for gas-liquid separation, and the separated vapor phase is returned to the radiation section for cracking. It is evident from the cracking results that example 1 gives a significantly higher yield of lower olefins. Comparing example 1 with comparative example 2, the crude oil in comparative example 2 is preheated in the convection section and sent to the flash evaporator for gas-liquid separation, the separated vapor phase is returned to the radiation section for cracking, and the cyclone separator is adopted in example 1 for gas-liquid separation. From the cracking results, it is seen that example 1 achieves a higher yield of lower olefins.
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments.
Claims (6)
1. A method for preparing low-carbon olefin by cracking crude oil is characterized by comprising the following steps:
1) sending crude oil into a first pipe group of a convection section of a cracking furnace for preheating;
2) carrying out gas-liquid separation on the preheated crude oil through a cyclone separator to form a vapor phase and a liquid phase;
3) sending the vapor phase into a second tube group of a convection section of the cracking furnace, heating to a cross temperature, and then directly sending into a radiation section for cracking to generate cracking gas containing low-carbon olefin;
4) the liquid phase is contacted with superheated steam of a convection section for steam stripping;
wherein the process further comprises, before being fed to the radiant section, at least one addition of steam and/or hydrogen;
the cyclone separator is provided with an internal component, and the internal component comprises a skimming cylinder positioned at the top of the cyclone separator and/or a separation plate and a vortex breaker positioned at the lower part of the cyclone separator;
the content of the liquid phase in the vapor phase is less than 200mg/m3；
In the step 1), the outflow temperature of the preheated crude oil is 315-;
in the step 2), the liquid phase volume content of the preheated crude oil at the inlet of the cyclone separator is 0.01-0.04%.
2. A method according to claim 1, wherein the steam is sour process steam or deacidified process steam.
3. The method of claim 1 or 2, wherein the steam is superheated in a convection section of the cracking furnace.
4. The method of claim 1, wherein the cyclone separator is selected from a rectangular inlet cyclone separator, a volute type cyclone separator, an axial flow guide vane type cyclone separator, a straight type cyclone separator, a cone and cone combination type cyclone separator, a counter-flow type cyclone separator, a straight type cyclone separator, or a straight type multi-cyclone tube separator.
5. The method of claim 4, wherein the cyclone separator is selected from a spiral shell type cyclone separator, an axial flow guide vane type cyclone separator, a straight tube type cyclone separator, a cone and cylinder combination type cyclone separator, or a straight flow type cyclone separator.
6. An apparatus for producing lower olefins by cracking crude oil according to the method of any one of claims 1 to 5, wherein the apparatus comprises a cracking furnace and a cyclone separator, the convection section of the cracking furnace comprises a convection section first tube bank and a convection section second tube bank, the convection section first tube bank is connected with the inlet of the cyclone separator, and the convection section second tube bank is connected with the vapor phase outlet of the cyclone separator.
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| CN112694382B (en) * | 2019-10-23 | 2022-11-18 | 中国石油化工股份有限公司 | Method and system for preparing low-carbon olefin from crude oil |
| 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 |
| CN112725019B (en) * | 2019-10-28 | 2022-07-12 | 中国石油化工股份有限公司 | Cracking treatment method and system for crude oil |
| CN112745943B (en) * | 2019-10-30 | 2024-02-13 | 中国石油化工股份有限公司 | Method and system for cracking crude oil |
| 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 |
| CN114478159B (en) * | 2020-10-26 | 2024-06-04 | 中国石油化工股份有限公司 | Method and system for preparing low-carbon olefin |
| 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 |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB814610A (en) * | 1954-12-17 | 1959-06-10 | Exxon Research Engineering Co | Cracking heavy hydrocarbon oils to produce olefins, motor fuels and coke |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
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