CN116445181B - Hot carrier gas direct cracking system with decoking and coking monitoring functions - Google Patents
Hot carrier gas direct cracking system with decoking and coking monitoring functions Download PDFInfo
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- CN116445181B CN116445181B CN202310291093.7A CN202310291093A CN116445181B CN 116445181 B CN116445181 B CN 116445181B CN 202310291093 A CN202310291093 A CN 202310291093A CN 116445181 B CN116445181 B CN 116445181B
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- 238000005235 decoking Methods 0.000 title claims abstract description 116
- 238000004939 coking Methods 0.000 title claims abstract description 47
- 239000012159 carrier gas Substances 0.000 title claims abstract description 44
- 238000012544 monitoring process Methods 0.000 title claims abstract description 39
- 238000005336 cracking Methods 0.000 title claims description 94
- 239000007789 gas Substances 0.000 claims abstract description 118
- 238000000197 pyrolysis Methods 0.000 claims abstract description 79
- 239000002994 raw material Substances 0.000 claims abstract description 73
- 239000000567 combustion gas Substances 0.000 claims abstract description 50
- 238000002485 combustion reaction Methods 0.000 claims abstract description 41
- 239000000571 coke Substances 0.000 claims abstract description 40
- 238000000926 separation method Methods 0.000 claims abstract description 26
- 239000002918 waste heat Substances 0.000 claims abstract description 16
- 238000001816 cooling Methods 0.000 claims abstract description 15
- 238000010791 quenching Methods 0.000 claims abstract description 15
- 230000000171 quenching effect Effects 0.000 claims abstract description 14
- 239000007788 liquid Substances 0.000 claims abstract description 12
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 28
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 21
- 229910052760 oxygen Inorganic materials 0.000 claims description 21
- 239000001301 oxygen Substances 0.000 claims description 21
- 230000008859 change Effects 0.000 claims description 15
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 14
- 239000001569 carbon dioxide Substances 0.000 claims description 14
- 238000004321 preservation Methods 0.000 claims description 12
- 230000000694 effects Effects 0.000 claims description 8
- 239000007791 liquid phase Substances 0.000 claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 239000004215 Carbon black (E152) Substances 0.000 claims description 5
- 229930195733 hydrocarbon Natural products 0.000 claims description 5
- 150000002430 hydrocarbons Chemical class 0.000 claims description 5
- 239000003112 inhibitor Substances 0.000 claims description 3
- 229910017053 inorganic salt Inorganic materials 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 239000012071 phase Substances 0.000 claims description 2
- 238000009422 external insulation Methods 0.000 claims 1
- 238000001514 detection method Methods 0.000 abstract description 9
- 238000000034 method Methods 0.000 description 18
- 230000008569 process Effects 0.000 description 15
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 11
- 238000005265 energy consumption Methods 0.000 description 11
- 239000000446 fuel Substances 0.000 description 8
- 150000001336 alkenes Chemical class 0.000 description 7
- 229910002091 carbon monoxide Inorganic materials 0.000 description 7
- 238000004230 steam cracking Methods 0.000 description 6
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 5
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 4
- 239000005977 Ethylene Substances 0.000 description 4
- 239000003546 flue gas Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 230000002035 prolonged effect Effects 0.000 description 4
- 238000010517 secondary reaction Methods 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- WYTGDNHDOZPMIW-RCBQFDQVSA-N alstonine Natural products C1=CC2=C3C=CC=CC3=NC2=C2N1C[C@H]1[C@H](C)OC=C(C(=O)OC)[C@H]1C2 WYTGDNHDOZPMIW-RCBQFDQVSA-N 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- -1 ethylene, propylene Chemical group 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 239000012774 insulation material Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000004065 semiconductor Substances 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
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
- C10G9/18—Apparatus
- C10G9/20—Tube furnaces
- C10G9/206—Tube furnaces controlling or regulating the tube furnaces
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a direct pyrolysis system of a hot carrier gas with decoking and coking monitoring, which comprises a combustion reaction section, a pyrolysis tube section, a quenching cooling section and a gas-liquid and coke separation section which are sequentially connected along the advancing direction of the hot carrier gas, wherein the combustion reaction section comprises a burner, the burner is provided with a plurality of combustion gas inlets and at least one ignition device, the burner is provided with a combustion cavity, the combustion gas inlets and the ignition device extend to the combustion cavity, the pyrolysis tube section is provided with a plurality of decoking gas tubes, decoking gas outlet nozzles, a resistance monitoring unit and a temperature detection unit along the tube direction, the outer side of the burner is provided with a pyrolysis furnace raw material waste heat device and a pyrolysis furnace raw material conveying tube which is spirally arranged, and the pyrolysis furnace raw material conveying tube extends to the inner cavity of the pyrolysis tube section through the pyrolysis furnace raw material inlet tube. The invention solves the problems of real-time monitoring of coking, real-time decoking, fixed-point decoking and the like.
Description
Technical Field
The invention relates to the field of olefin production, in particular to a hot carrier gas direct cracking system with decoking and coking monitoring functions.
Background
Light olefins such as ethylene and propylene are basic raw materials in petrochemical industry, and the light olefin productivity is one of important marks for measuring the national petrochemical development level. Although steam cracking is the most widespread way of light olefin production and has optimized olefin yield to the greatest extent, the current steam cracking process has high comprehensive energy consumption, large steam consumption and long residence time, and in addition, the cracking furnace tube adopts indirect heating of a boiler, so that the fuel consumption and the carbon emission are large. Therefore, research on a new naphtha cracking process based on the current production process has practicability and practical value. The cracking furnace is a high energy consumption device in the ethylene device, and researches show that the total of the steam cracking furnaceAbout 43.4% efficiency, the radiant section combustion processThe losses are greatest. Therefore, it would be a focus problem to reasonably implement thermal management for energy consuming devices such as ethylene. Although steam cracking has been put into operation industrially for many years, the heating mode of indirectly heating the cracking furnace tube by the boiler is not changed, the tube blocking phenomenon in the operation process is not improved essentially, and huge economic loss is caused by replacing the furnace tube. Thus, development has highThe olefin cracking technology with efficiency, low carbon emission and long operation period has great industrial application prospect.
Steam cracking is the most commonly used method for industrial ethylene production, after the raw materials of a cracking furnace and steam are mixed, the high-temperature cracking furnace is introduced to radiate a furnace tube, and cracking reaction is carried out in the furnace tube to produce hydrocarbon products such as ethylene, propylene and the like. The hydrocarbon is subjected to steam cracking reaction in the radiant section of the cracking furnace, and the cracking reaction is accompanied by secondary reaction, coke is deposited on the pipe wall in the furnace pipe in the radiant section, and coke powder is deposited continuously in the furnace pipe, so that coking is finally caused. The coking phenomenon can increase the thermal resistance of the tube wall and reduce the heat transfer coefficient of the tube wall, so that the tube wall temperature of the furnace tube needs to be increased to reach the reaction temperature, and the local temperature of the tube wall of the furnace tube is overhigh, thereby reducing the service life of the furnace tube and increasing the energy consumption in the reaction process. The inner diameter of the furnace tube is continuously reduced under the continuous deposition of the coke layer, so that the pressure drop of raw material fluid in the furnace tube is increased, the amount of cracking raw materials participating in the reaction is reduced, the yield of olefins is reduced, the furnace tube is finally blocked even along with the continuous addition of the coking degree, and the safety problem is generated. When the coking limit of a certain process requirement is reached, decoking treatment is needed to be carried out on the radiant furnace tube of the cracking furnace, and meanwhile, the accumulation of coke on the inner wall of the furnace tube can cause carburization of the inner wall of the furnace tube, damage to high-temperature alloy and reduction of the service life of the furnace tube.
The decoking process needs to be carried out after the furnace is stopped periodically, decoking gas generally enters from a cracking inlet and cannot directly act on coking parts, and the decoking gas cannot be decoked under the condition of partial coking in the operation process. The coking position cannot be monitored in real time, and the like.
There is a need for improvement and development in the art.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a direct pyrolysis system of a hot carrier gas with decoking and coking monitoring, which can perform decoking operation by introducing decoking gas into a decoking gas pipe corresponding to a furnace pipe.
In order to achieve the above purpose, the present invention may be performed by the following technical scheme:
a direct pyrolysis system for hot carrier gas comprises a combustion reaction section, a pyrolysis section, a quenching cooling section and a gas-liquid and coke separation section which are sequentially connected along the travelling direction of the hot carrier gas.
The combustion reaction section comprises a burner provided with a plurality of combustion gas inlets and at least one ignition device, the burner is provided with a combustion cavity, and the plurality of combustion gas inlets and the ignition device extend to the combustion cavity;
The cracking pipe section is provided with a plurality of decoking gas pipes, decoking gas outlet nozzles, a resistance monitoring unit and a temperature detecting unit along the pipeline direction;
The cracking furnace raw material waste heat device is arranged at the outer side of the combustor and spirally provided with a cracking furnace raw material conveying pipeline, the cracking furnace raw material conveying pipeline extends to the inner cavity of the cracking pipe section through a cracking furnace raw material inlet pipe, the tail end of the cracking furnace raw material inlet pipe is provided with a cracking furnace raw material atomizing head, and the cracking furnace raw material waste heat device is used for preheating the cracking furnace raw material conveying pipeline;
The gas fuel and combustion-supporting oxygen enter the combustor from a plurality of combustion gas inlets respectively, the combustion gas is ignited in the combustion chamber through the ignition device, high-temperature flue gas generated after combustion enters the cracking pipe section, meanwhile, after the raw material of the cracking furnace is preheated and heated through the raw material conveying pipeline of the cracking furnace, the raw material is atomized by the raw material atomizing head of the cracking furnace and then directly cracked into the cracking pipe section, during the period, the resistance monitoring unit obtains real-time related data of the coking quantity in the pipe by monitoring the resistance value change among the sections, the temperature detecting unit detects the coking thickness condition and the pipe wall temperature during normal operation through the temperature change of the surface of the furnace pipe, and the decoking gas pipe is introduced into the decoking gas to remove the coking in the pipe of the cracking pipe section according to the data fed back by the resistance monitoring unit, and the gas enters the cooling section for quenching and cooling after the cracking and then is separated into the gas-liquid quenching and coke separation section.
The direct pyrolysis system for hot carrier gas, as described above, further, the outlet of the gas-liquid and coke separation section is provided with a plurality of gas sensors, and a plurality of the gas sensors are used for detecting the specific gas content so as to obtain the final decoking effect.
The direct pyrolysis system for the hot carrier gas is further characterized in that a power section is arranged at the upper part of the gas-liquid and coke separation section, a plurality of gas sensors are arranged at the outlet of the power section, and the plurality of gas sensors are used for detecting specific gas content so as to obtain the final decoking effect.
The direct pyrolysis system for hot carrier gas, as described above, further comprises a rectifier at the gas inlet of the burner, wherein the multiple combustion gas inlets comprise a first combustion gas inlet, a second combustion gas inlet and a third combustion gas inlet, the first combustion gas inlet is arranged at the axle center of the rectifier and extends to the combustion chamber through the rectifier, the second combustion gas inlet is inclined to the first combustion gas inlet, and the third combustion gas inlet is perpendicular to the first combustion gas inlet and extends to the inner chamber of the rectifier.
The direct pyrolysis system of carrier gas of heat as described above, further, the combustor has a combustor inner wall, the enclosure space that the combustor inner wall encloses is for the combustion chamber, the skin of combustor inner wall is equipped with the interior heat preservation of combustor, the interior heat preservation skin of combustor is equipped with the combustor surface, the skin of combustor surface is equipped with pyrolysis furnace raw materials waste heat device.
The direct pyrolysis system for hot carrier gas as described above, further, the decoking gas pipe is provided with a decoking gas valve at a portion outside the pyrolysis pipe section, and the decoking gas pipe is provided with a decoking gas outlet nozzle at a portion inside the pyrolysis pipe section.
The direct pyrolysis system for the hot carrier gas is further characterized in that the outer layer of the pyrolysis tube section is provided with a furnace tube for external heat preservation.
The direct pyrolysis system for the hot carrier gas is characterized in that the upper part of the gas-liquid-coke separation section is further provided with a light hydrocarbon separation system connected with a gas phase, and the lower part of the gas-liquid-coke separation section is further provided with a liquid-phase multilayer rectification system and/or a liquid-phase oil decoking system.
The direct pyrolysis system for hot carrier gas as described above, further, the burner is further provided with a raw material inlet of the pyrolysis furnace.
The hot carrier gas direct pyrolysis system as described above, further, the pyrolysis tube sections are arranged horizontally, obliquely or in one or more layers of serpentine bends.
The thermal carrier gas direct cracking system as described above, further, the decoking gas may be a mixture of oxygen and/or water vapor and/or carbon dioxide and/or inorganic salt inhibitors.
The direct pyrolysis system for hot carrier gas as described above, further, the pyrolysis furnace raw material inlet is provided with an atomization device.
The thermal carrier gas direct cracking system can be high pressure or normal pressure.
Compared with the prior art, the invention has the beneficial effects that:
1. According to the embodiment of the invention, the outer pipe wall of the cracking pipe section of the thermal carrier gas direct cracking system is provided with a plurality of resistance monitoring units and temperature detection units, and the positions of the coking section furnace pipes can be found by comparing reference data of real-time coking monitoring of the furnace pipes in each section with real-time coking data of the furnace pipes in each section when the system is operated through primary operation measurement after the system is newly built or the furnace is shut down for overhaul and the furnace pipes are cleaned of coke.
2. The direct pyrolysis system of the hot carrier gas provided by the embodiment of the invention is provided with the decoking gas valve, so that the decoking operation can be performed without stopping the furnace, and the decoking gas is directly introduced into the corresponding furnace tube to perform the decoking operation by opening the corresponding decoking gas valve. Oxygen in the decoking gas reacts with the coke to produce carbon monoxide and carbon dioxide. Carbon monoxide, carbon dioxide and carried water vapor generated in the decoking process have certain effects on cracking, and simultaneously, the amount of carbon dioxide and water vapor corresponding to the raw material inlet of the cracking furnace can be reduced, the continuous operation time of the equipment is prolonged, the product cost is greatly reduced, the operation efficiency of the equipment is improved, the energy consumption in the furnace shutdown restarting process is also reduced, and the like.
3. The direct pyrolysis system of the hot carrier gas is provided with the decoking gas valve, when the furnace is shut down for decoking, the decoking gas can be directly introduced into the corresponding furnace tube by opening the corresponding decoking gas valve, so that the decoking gas directly acts on the coke, the oxidation of the furnace tube can be reduced, and the time required by the furnace shutdown decoking process is reduced. Meanwhile, by comparing real-time coking data of furnace tubes in each section during operation, the entering position of decoking gas is adjusted in time, so that decoking is effectively realized.
4. The direct pyrolysis system of the hot carrier gas is provided with the decoking gas valve, and by opening the decoking Jiao Qiti valve at a proper position and adjusting a proper small flow to be reserved as the constant decoking Jiao Qiti, the coke generated by secondary reaction accompanied by partial pyrolysis reaction is counteracted, so that the formation of the coke can be slowed down, the normal operation time of equipment is prolonged, the operation cost of the product is reduced, and the operation efficiency of the equipment is improved.
5. The direct pyrolysis system of the hot carrier gas of the embodiment of the invention can reduce the energy consumption and the emission of the device by direct pyrolysis of the hot carrier gas generated by combustion, has no heat transfer resistance in direct heat exchange, has far higher heat exchange efficiency than indirect heat exchange, can greatly reduce the energy consumption and the emission of the device and improves the energy consumption and the emission of the deviceEfficiency, increased cracking temperature, reduced reaction residence time, convenient operation, low cost and the like.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present application, the following description will briefly explain the drawings needed in the embodiments, and it is obvious that the drawings in the following description are only some embodiments of the present application, and other drawings can be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of a thermal carrier gas direct cracking system according to an embodiment of the invention.
Wherein, 1, a combustion reaction section; 2, a cracking pipe section, 3, a quenching cooling section, 4, a gas-liquid and coke separation section, 5, a power section, 10, a first combustion gas inlet, 11, a second combustion gas inlet, 12, an ignition device, 13, a third combustion gas inlet, 14, a rectifier, 15, a combustor inner wall, 16, a combustor inner heat preservation, 17, a combustor outer surface, 18, a combustion cavity, 19, a combustion reaction section outlet, 20, a cracking furnace raw material waste heat device, 21, a cracking furnace raw material inlet pipe, 22, a cracking furnace raw material atomizing head, 23, decoking gas, 24, a decoking Jiao Qiti valve, 25, a decoking gas pipe, 26, a decoking gas outlet nozzle, 27, a resistance monitoring unit, 28, a temperature detection unit, 29, a furnace pipe outer heat preservation, 30, a cracking furnace raw material inlet, 40 gas product outlet, 50, and a non-gas product outlet.
Detailed Description
The following description of the embodiments of the present application will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present application, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the application without making any inventive effort, are intended to be within the scope of the application.
Examples:
It should be noted that the terms "first," "second," and the like in the description and the claims of the present invention and the above figures are used for distinguishing between similar objects and not necessarily for describing a particular sequential or chronological order. It is to be understood that the data so used may be interchanged where appropriate such that the embodiments of the invention described herein may be implemented in sequences other than those illustrated or otherwise described herein. Furthermore, the terms "comprises," "comprising," and "having," and any variations thereof, are intended to cover a non-exclusive inclusion, such that a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements expressly listed or inherent to such process, method, article, or apparatus.
It is to be understood that the terms "center," "longitudinal," "transverse," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counter-clockwise," "axial," "radial," "circumferential," and the like are directional or positional relationships as indicated based on the drawings, merely to facilitate describing the invention and to simplify the description, and do not indicate or imply that the devices or elements referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore should not be construed as limiting the invention.
In the description of the present invention, the meaning of "plurality" means at least two, for example, two, three, etc., unless specifically defined otherwise. Furthermore, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "coupled," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected, mechanically connected, electrically connected, directly connected, or indirectly connected via an intervening medium, or may be in communication between two elements. The specific meaning of the above terms in the present invention will be understood in specific cases by those of ordinary skill in the art.
In the present invention, unless expressly stated or limited otherwise, a first feature "up" or "down" a second feature may be the first and second features in direct contact, or the first and second features in indirect contact via an intervening medium. Moreover, a first feature being "above," "over" and "on" a second feature may be a first feature being directly above or obliquely above the second feature, or simply indicating that the first feature is level higher than the second feature. The first feature being "under", "below" and "beneath" the second feature may be the first feature being directly under or obliquely below the second feature, or simply indicating that the first feature is less level than the second feature.
Referring to fig. 1, fig. 1 is a schematic structural diagram of an embodiment of a thermal carrier gas direct cracking system with decoking and coking monitoring according to the present invention. The direct pyrolysis system for the heat carrier gas with coke cleaning and coking monitoring comprises a combustion reaction section 1, a pyrolysis tube section 2, a quenching cooling section 3 and a gas-liquid-coke separation section 4 which are sequentially connected along the travelling direction of the heat carrier gas, wherein the combustion reaction section 1 comprises a combustor, the combustor is provided with a plurality of combustion gas inlets and at least one ignition device 12, the combustor is provided with a combustion cavity 18, a plurality of combustion gas inlets and the ignition device 12 extend to the combustion cavity 18, the pyrolysis tube section 2 is provided with a plurality of coke removal gas pipes 25, a resistance monitoring unit 27 and a temperature detection unit 28 along the pipeline direction, a pyrolysis furnace raw material waste heat device 20 and a pyrolysis furnace raw material conveying pipeline which is spirally arranged are arranged on the outer side of the combustor, the pyrolysis furnace raw material conveying pipeline extends to the inner cavity of the pyrolysis tube section 2 through a pyrolysis furnace raw material inlet pipe 21, the tail end of the pyrolysis furnace raw material inlet pipe 21 is provided with a pyrolysis furnace raw material atomizing head 22, and the pyrolysis furnace raw material waste heat device 20 is used for preheating the pyrolysis furnace raw material conveying pipeline.
Specifically, the gas fuel and the combustion-supporting oxygen enter the burner from a plurality of combustion gas inlets respectively, the combustion gas is ignited in the combustion chamber 18 through the ignition device 12, high-temperature flue gas generated after combustion enters the cracking tube section 2, meanwhile, after the raw material of the cracking furnace is preheated and heated by the raw material conveying pipeline of the cracking furnace, the raw material is atomized by the raw material atomizing head 22 of the cracking furnace and then directly cracked into the cracking tube section 2, during the period, the resistance monitoring unit 27 obtains real-time related data of the coking quantity in the tube by monitoring the fine change of the resistance value among each section, the temperature detecting unit 28 detects the coking thickness condition and the tube wall temperature during the decoking through the temperature change of the surface of the furnace tube, the decoking gas tube 25 is introduced into the decoking gas tube 23 to remove the coking in the tube of the cracking tube section 2 according to the data fed back by the resistance monitoring unit 27 and the temperature detecting unit 28, and the cracked gas enters the quenching cooling section 3 to quench cooling and then is separated into the gas-liquid and coke separation section 4.
The direct pyrolysis system with the coke cleaning and coking monitoring function provides a technical scheme for solving the coke cleaning and coking monitoring problems of the pyrolysis system, by arranging the pyrolysis furnace raw material waste heat device 20 and preheating the pyrolysis furnace raw material conveying pipeline, the pyrolysis pipe section 2 does not need to be heated or directly contacted with flame, so that a plurality of decoking gas pipes 25, a resistance monitoring unit 27 and a temperature detecting unit 28 can be arranged on the outer pipe wall of the pyrolysis pipe section 2 to monitor the real-time coking data of each section of furnace pipe of the pyrolysis pipe section 2, and then the monitored real-time coking data is compared with the reference data of the real-time coking monitoring of each section of furnace pipe when the equipment is newly built or the furnace is shut down for overhaul and the furnace pipe is cleaned, the position of the furnace pipe of the coking section can be found in time, and then the decoking gas 23 is introduced into the decoking gas pipe 25 of the corresponding furnace pipe for decoking operation. In addition, oxygen-containing gas within decoking gas 23 reacts with the coke to produce carbon monoxide and/or carbon dioxide. Carbon monoxide, carbon dioxide and vapor brought in during decoking have certain effect on cracking, and simultaneously the amount of carbon dioxide and vapor corresponding to the raw material inlet 30 of the cracking furnace is reduced, so that the continuous operation time of the equipment can be prolonged, the product cost is greatly reduced, the operation efficiency of the equipment is improved, and the energy consumption in the restarting process of the furnace can be reduced. In addition, the direct pyrolysis of the hot carrier gas generated by combustion can reduce the energy consumption and the emission of the device, and the direct heat exchange has no heat transfer resistance, so that the heat exchange efficiency is far higher than that of indirect heat exchange, the energy consumption and the emission of the device can be greatly reduced, and the improvement is realizedEfficiency, increased cracking temperature, reduced reaction residence time, convenient operation, low cost and the like.
In the above technical solution, the burner may be a combustion system comprising pure oxygen, oxygen-enriched conditions, which may be arranged horizontally or upwards or downwards or at any angle. The burner is provided with a burner inner wall 15, a closed space surrounded by the burner inner wall 15 is the combustion cavity 18, an outer layer of the burner inner wall 15 is provided with a burner inner heat preservation 16, an outer layer of the burner inner heat preservation 16 is provided with a burner outer surface 17, and an outer layer of the burner outer surface 17 is provided with a cracking furnace raw material waste heat device 20.
The cracking tube section 2 is provided with a plurality of resistance monitoring units 27 and a temperature detection unit 28 along the direction of the pipeline, wherein the resistance monitoring units 27 obtain real-time related data of the coking quantity in the tube by monitoring the small change of the resistance value among the sections, the change of the resistance value comprises the change of the current value under a constant voltage source or the small signal of the change of the voltage value under a constant current source, and the resistance change of the section is detected to represent the change of the coking quantity of the section. The temperature detection unit 28 is mainly a thermocouple and may include a thermocouple, a thermal resistor, a thermal semiconductor, or other temperature sensor. The temperature detection unit 28 can detect the approximate coking thickness condition during normal operation by temperature change of the furnace tube surface and the tube wall temperature during decoking by detecting temperature change during smooth operation at the same inlet conditions, or at the same outlet conditions, to represent the coking thickness condition at that point. When the device is used, after equipment is newly built or a furnace is shut down for overhaul, and after coke is removed from the furnace tube, reference data of resistance and temperature of coking real-time monitoring of each section of furnace tube is measured by primary operation and is compared with the coking real-time resistance and temperature data of each section of furnace tube in operation, so that the position of the furnace tube in the coking section is found. The resistance data is required to be subjected to temperature coupling treatment to obtain a corresponding resistance value curve under the condition of each operation temperature in the initial operation, and then the calculated reference resistance value corresponding to each detection point temperature in the real-time operation is compared with the actual resistance value detected by each section to obtain a coking region. Meanwhile, the relative coking areas can be obtained through the temperature change condition of each detection point. When the direct pyrolysis system of the hot carrier gas in the embodiment of the invention monitors the coking state, the resistance monitoring unit 27 can collect resistance signals for monitoring, the temperature detecting unit 28 can collect temperature signals for monitoring, and the resistance monitoring unit 27 and the temperature detecting unit 28 can be used in combination for monitoring.
On the basis of the above embodiment, as an optional embodiment, a rectifier 14 is further disposed at the gas inlet of the burner, and the plurality of combustion gas inlets include a first combustion gas inlet 10, a second combustion gas inlet 11 and a third combustion gas inlet 13, where the first combustion gas inlet 10 is disposed at the axis of the rectifier 14 and extends to the combustion chamber 18 through the rectifier 14, the second combustion gas inlet 11 is disposed obliquely to the first combustion gas inlet 10, and the third combustion gas inlet 13 is disposed perpendicular to the first combustion gas inlet 10 and extends to the inner cavity of the rectifier 14. The combustion gas comprises fuel gas and oxygen-containing gas such as air and oxygen. One or two of the first combustion gas inlet 10, the second combustion gas inlet 11 and the third combustion gas inlet 13 are used for feeding fuel gas, and the other combustion gas inlets are used for feeding combustion-supporting gas, and typically, the first combustion gas inlet 10 and the third combustion gas inlet 13 are used for feeding the same gas or different gases.
By providing the rectifier 14 in this embodiment, the gas distribution in the combustion chamber 18 can be made more uniform, so that the combustion is more complete. When in use, the gas fuel and the combustion-supporting oxygen enter the burner from the first combustion gas inlet 10, the second combustion gas inlet 11 and the third combustion gas inlet 13 respectively, are ignited by the ignition device 12 to burn in the combustion chamber 18, and the ratio of the gas fuel to the combustion-supporting oxygen is adjusted so that the burnt product has no oxygen or contains less oxygen. The high-temperature flue gas generated after combustion enters the inlet of the cracking tube section 2 through the outlet 19 of the combustion reaction section. The raw material of the cracking furnace enters the pipeline from the raw material inlet 30 of the cracking furnace and is preheated and heated by the raw material waste heat device 20 of the cracking furnace, and the raw material waste heat device is externally coated with heat insulation materials. In another embodiment, the raw material of the cracking furnace can be preheated by an external heat exchanger or preheated by the external heat exchanger and the raw material waste heat device 20 of the cracking furnace, then is led to the raw material inlet pipe 21 of the cracking furnace, and is atomized by the raw material atomizing head 22 of the cracking furnace and then is directly cracked in the cracking pipe section 2. The cracked gas enters a quenching cooling section 3 for quenching cooling, and then enters a gas-liquid and coke separation section 4 for separation. Furthermore, the lower part of the gas-liquid-coke separation section 4 can be connected with a liquid-phase multilayer rectification system or a liquid-phase oil decoking system, or can be connected with the liquid-phase oil decoking system and then is introduced into the raw material inlet 30 of the cracking furnace, and the upper part of the gas-liquid-coke separation section 4 can be connected with a light hydrocarbon separation system (a cracking gas cryogenic separation system) or can be connected with the power section 5. Further, the outlet of the power section 5 is further provided with a plurality of gas sensors, the plurality of gas sensors comprise carbon monoxide, carbon dioxide, oxygen and other gas sensors, and the plurality of gas sensors are used for detecting specific gas content, and the final decoking effect is obtained by detecting the carbon dioxide and oxygen content. In addition, the direct pyrolysis system for hot carrier gas in this embodiment can also keep the system running at positive pressure by controlling the inlet pressures, including the pressure of the pyrolysis furnace raw material, the gas fuel, the combustion-supporting oxygen and the decoking gas 23 inlet.
In another embodiment, in use, the gas fuel and the combustion-supporting oxygen enter the burner from the first combustion gas inlet 10, the second combustion gas inlet 11 and the third combustion gas inlet 13 respectively, are ignited by the ignition device 12 to burn in the combustion chamber 18, and the ratio of the gas fuel and the combustion-supporting oxygen is adjusted so that the oxygen with more products after combustion. The high-temperature flue gas generated after combustion enters the inlet of the cracking tube section 2 through the outlet 19 of the combustion reaction section. And simultaneously stopping the raw material of the cracking furnace from being fed. The cracked gas enters a quenching cooling section 3 for quenching cooling, and then enters a gas-liquid and coke separation section 4 for separation.
As an alternative embodiment, in some embodiments, the portion of the decoking gas pipe 25 outside the cracking pipe section 2 is provided with a decoking gas valve 24, and the portion of the decoking gas pipe 25 inside the cracking pipe section 2 is provided with a decoking gas outlet nozzle 26.
Specifically, the embodiment can eliminate the need of stopping the furnace for decoking by arranging the decoking gas valve 24, and the embodiment comprises the following steps of opening the corresponding decoking gas valve 24 to adjust the proper flow of each point, introducing the decoking gas 23, and introducing the decoking gas 23 into the decoking gas pipe 25 and then into the decoking gas outlet nozzle 26. Wherein the decoking gas outlet nozzle 26 is as close as possible to the decoking Jiao Qiguan valve. Decoking gas outlet nozzle 26 facilitates adherence of decoking gas 23 to and effective application to the focal surface of the inner surface of the furnace tube. While the high pressure gas from decoking gas outlet nozzle 26 is also effective to blow open the blocked coke. Preferably, the decoking gas 23 can be heated by an external heat exchanger before entering the furnace tube, so that the decoking gas can react immediately after entering the furnace tube, thereby reducing the reaction time and better removing the coke on the inner surface of the furnace tube. Illustratively, the decoking gas 23 may be a mixture of oxygen and/or water vapor and/or carbon dioxide and/or an (inorganic salt) inhibitor. Oxygen-containing gas within decoking gas 23 reacts with the coke to produce carbon monoxide and carbon dioxide. Carbon monoxide, carbon dioxide and carried water vapor generated in the decoking process have a certain effect on cracking, and simultaneously, the amount of the carbon dioxide and the water vapor corresponding to the raw material inlet 30 of the cracking furnace can be reduced, the continuous operation time of the equipment is prolonged, the product cost is greatly reduced, and the energy consumption in the furnace shutdown restarting process can be reduced. In addition, when the furnace is shut down for decoking, the corresponding decoking gas valve 24 can be opened, and the decoking gas 23 is directly introduced into the corresponding furnace tube, so that the decoking gas 23 directly acts on the coke, the oxidation of the furnace tube can be reduced, and the time required for the furnace shut down decoking process is reduced. Meanwhile, by comparing real-time coking data of furnace tubes in each section during operation, the entering position of the decoking gas 23 is adjusted in time, so that the decoking can be effectively performed.
Further, the outer layer of the cracking tube section 2 is provided with an outer heat preservation 29 of a heat preservation material furnace tube, and the heat dissipation loss of heat exchange with the outer surface 17 of the burner can be reduced by the outer heat preservation 29 of the furnace tube, and meanwhile, the temperature of the cracking gas inlet is increased. In addition, the furnace tube of the cracking tube section 2 can be spirally or spirally downward, can be horizontally arranged as shown in fig. 1, can be downward arranged at the outlet, and can be downward inclined. In addition, the direct pyrolysis system of the hot carrier gas can be operated under high pressure conditions or under normal pressure conditions.
On the basis of the above embodiment, as an alternative embodiment, the decoking effect can be maintained by keeping the decoking gas valve 24 open during the smooth operation of the hot carrier gas direct cracking system. The specific operation is that the decoking gas valve 24 is opened at a proper position, and a proper small flow is adjusted to be reserved as the constant decoking gas 23, so as to offset the coke generated by secondary reaction during partial cracking reaction, and simultaneously keep the decoking gas outlet nozzle 26 unobstructed. The flow rates of the sections as the retention gas may be different depending on the coking conditions. Typically there are more intermediate portions and fewer start segments. Meanwhile, the flow of the decoking gas 23 can be adjusted by the data monitored by the resistance monitoring unit 27 and the temperature detecting unit 28, so that the long-term smoothness of the tube furnace is kept. This operation can be maintained for a long period of time without the need for furnace shutdown for decoking. In this embodiment, by opening the decoking gas valve 24 at a suitable position and adjusting a suitable small flow rate to be reserved as the constant decoking gas 23, the formation of coke can be slowed down by counteracting the coke generated by the secondary reaction accompanied by partial cracking reaction, thereby prolonging the normal operation time of the equipment, reducing the operation cost of the product and improving the operation efficiency of the equipment.
In the description of the present specification, a description referring to terms "one embodiment," "some embodiments," "examples," "specific examples," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms are not necessarily directed to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, the different embodiments or examples described in this specification and the features of the different embodiments or examples may be combined and combined by those skilled in the art without contradiction.
The above embodiments are only for illustrating the technical concept and features of the present invention, and are intended to enable those skilled in the art to understand the content of the present invention and implement the same, and are not intended to limit the scope of the present invention. All equivalent changes or modifications made in accordance with the essence of the present invention are intended to be included within the scope of the present invention.
Claims (8)
1. The direct pyrolysis system for the hot carrier gas is characterized by comprising a combustion reaction section, a pyrolysis tube section, a quenching cooling section and a gas-liquid and coke separation section which are sequentially connected along the travelling direction of the hot carrier gas, wherein the pyrolysis tube section is also provided with a resistance monitoring unit and a temperature detecting unit along the pipeline direction, and the resistance monitoring unit and the temperature detecting unit are matched to find the position of a coking section furnace tube;
The combustion reaction section comprises a burner provided with a plurality of combustion gas inlets and at least one ignition device, the burner is provided with a combustion cavity, and the plurality of combustion gas inlets and the ignition device extend to the combustion cavity; the device comprises a burner, a cracking furnace raw material waste heat device, a cracking furnace raw material conveying pipeline, a rectifier, a plurality of combustion gas inlets, a first combustion gas inlet, a second combustion gas inlet and a third combustion gas inlet, wherein the cracking furnace raw material waste heat device is arranged on the outer side of the burner, the cracking furnace raw material conveying pipeline is spirally arranged, the cracking furnace raw material conveying pipeline extends to an inner cavity of a cracking pipe section through a cracking furnace raw material inlet pipe;
The cracking pipe section is provided with a plurality of decoking gas pipes and decoking gas outlet nozzles along the pipeline direction, and decoking gas is introduced into the decoking gas pipe corresponding to the furnace pipe to decoke.
2. The direct pyrolysis system of carrier gas of claim 1, wherein the burner is further provided with a pyrolysis furnace raw material inlet, the end of the pyrolysis furnace raw material inlet pipe of the pyrolysis pipe section is provided with a pyrolysis furnace raw material atomizing head, and the pyrolysis furnace raw material waste heat device is used for preheating the pyrolysis furnace raw material conveying pipeline;
meanwhile, after the raw material of the cracking furnace is preheated and heated by the raw material conveying pipeline of the cracking furnace, the raw material atomizing head of the cracking furnace is utilized to atomize the raw material and then directly crack the raw material into the cracking pipe section, during the period, the resistance monitoring unit obtains real-time related data of the coking quantity in the pipe by monitoring the resistance value change between each section, the temperature detecting unit detects the coking thickness condition during normal operation and the pipe wall temperature during decoking through the temperature change of the surface of the furnace pipe, and according to the data fed back by the resistance monitoring unit and the temperature detecting unit, the decoking gas pipe is introduced with decoking gas to remove the coking in the pipe of the cracking pipe section, and the cracked gas enters the quenching cooling section for quenching cooling and then enters the gas-liquid and coke separation section for separation.
3. The direct thermal carrier gas pyrolysis system of claim 1 wherein the decoking gas comprises a mixture of oxygen and/or water vapor and/or carbon dioxide and/or inorganic salt inhibitors.
4. The direct pyrolysis system of hot carrier gas according to claim 1 wherein the outlet of the gas-liquid and coke separation section is provided with a plurality of gas sensors for detecting specific gas content to obtain a final decoking effect.
5. The direct pyrolysis system of carrier gas of claim 1, wherein the burner has a burner inner wall, the enclosed space enclosed by the burner inner wall is the combustion chamber, the outer layer of the burner inner wall is provided with an inner burner heat preservation, the inner burner heat preservation outer layer is provided with a burner outer surface, and the outer burner outer surface outer layer is provided with the pyrolysis furnace raw material waste heat device.
6. The direct thermal carrier gas pyrolysis system of claim 1 wherein the portion of the decoking gas conduit outside the pyrolysis conduit section is provided with a decoking gas valve and the portion of the decoking gas conduit within the pyrolysis conduit section is provided with a decoking gas outlet nozzle.
7. The direct pyrolysis system of thermal carrier gas according to claim 1, wherein the upper part of the gas-liquid-coke separation section is further provided with a light hydrocarbon separation system connected with a gas phase, and the lower part of the gas-liquid-coke separation section is further provided with a liquid-phase multi-layer rectification system and/or a liquid-phase oil decoking system.
8. The direct pyrolysis system for thermal carrier gas according to claim 1 wherein the pyrolysis tube sections are arranged horizontally, obliquely or in one or more layers of spiral bends, and the outer layers of the pyrolysis tube sections are provided with furnace tube external insulation.
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| CN106631659A (en) * | 2015-10-29 | 2017-05-10 | 中国石油化工股份有限公司 | Steam cracking method |
| CN113234472A (en) * | 2021-05-11 | 2021-08-10 | 上海寰球工程有限公司 | Pure oxygen ethylene cracking reaction system and process thereof |
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| EP3415587B1 (en) * | 2017-06-16 | 2020-07-29 | Technip France | Cracking furnace system and method for cracking hydrocarbon feedstock therein |
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| CN106631659A (en) * | 2015-10-29 | 2017-05-10 | 中国石油化工股份有限公司 | Steam cracking method |
| CN113234472A (en) * | 2021-05-11 | 2021-08-10 | 上海寰球工程有限公司 | Pure oxygen ethylene cracking reaction system and process thereof |
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