CN116496809A - Conical cracking reactor, hydrocarbon cracking method and reaction system - Google Patents
Conical cracking reactor, hydrocarbon cracking method and reaction system Download PDFInfo
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- CN116496809A CN116496809A CN202310575711.0A CN202310575711A CN116496809A CN 116496809 A CN116496809 A CN 116496809A CN 202310575711 A CN202310575711 A CN 202310575711A CN 116496809 A CN116496809 A CN 116496809A
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- 238000005336 cracking Methods 0.000 title claims abstract description 214
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 78
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 78
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 78
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 73
- 238000000034 method Methods 0.000 title claims abstract description 44
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 45
- 238000010791 quenching Methods 0.000 claims abstract description 45
- 239000003546 flue gas Substances 0.000 claims abstract description 44
- 238000002485 combustion reaction Methods 0.000 claims abstract description 43
- 239000002994 raw material Substances 0.000 claims abstract description 42
- 230000000171 quenching effect Effects 0.000 claims abstract description 39
- 239000000446 fuel Substances 0.000 claims abstract description 22
- 239000000295 fuel oil Substances 0.000 claims description 38
- 239000007789 gas Substances 0.000 claims description 34
- 238000000197 pyrolysis Methods 0.000 claims description 29
- 229920006395 saturated elastomer Polymers 0.000 claims description 24
- 238000011084 recovery Methods 0.000 claims description 22
- 238000001816 cooling Methods 0.000 claims description 17
- 239000002826 coolant Substances 0.000 claims description 14
- 239000007788 liquid Substances 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 10
- 239000000498 cooling water Substances 0.000 claims description 7
- 239000011555 saturated liquid Substances 0.000 claims description 6
- 238000005194 fractionation Methods 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 238000003776 cleavage reaction Methods 0.000 claims 8
- 230000007017 scission Effects 0.000 claims 7
- 230000015572 biosynthetic process Effects 0.000 claims 1
- 238000004939 coking Methods 0.000 abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 13
- 229910001868 water Inorganic materials 0.000 description 11
- 230000006835 compression Effects 0.000 description 5
- 238000007906 compression Methods 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 5
- 230000002829 reductive effect Effects 0.000 description 5
- 239000000463 material Substances 0.000 description 4
- 230000005855 radiation Effects 0.000 description 4
- 238000010517 secondary reaction Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical group O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 239000000956 alloy Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000005235 decoking Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 239000003779 heat-resistant material Substances 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 230000000670 limiting effect Effects 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- -1 naphtha Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking step
-
- 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
- C10G9/002—Cooling of cracked gases
-
- 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
- C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
- C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
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 provides a conical cracking reactor, a hydrocarbon cracking method and a reaction system, wherein the conical cracking reactor comprises a conical reactor body and a quenching heat exchanger communicated with the lower end of the conical reactor body, at least one cracking raw material inlet is arranged at the top of the conical reactor body, and at least one high-temperature flue gas inlet is arranged on the side wall of the conical reactor body. The cone-shaped cracking reactor of the invention greatly shortens the reaction residence time, prevents the problem of easy coking during the reaction under high pressure, and in addition, the invention directly mixes the high-temperature flue gas generated in the combustion chamber with the raw materials for heat exchange and cracking reaction, thereby improving the cracking reaction temperature and the cracking reaction depth, and simultaneously maximally utilizing the heat energy of fuel combustion.
Description
Technical Field
The invention relates to the technical field of hydrocarbon cracking, in particular to a conical cracking reactor, a hydrocarbon cracking method and a reaction system.
Background
In the hydrocarbon cracking field, the existing industrial cracking furnaces mainly comprise a heat accumulating type cracking furnace, a sand cracking furnace, a molten salt cracking furnace and a tubular cracking furnace, wherein the tubular cracking furnace is widely applied worldwide due to continuous production, high quality of cracking gas and mature technology. The tubular cracking furnace mainly comprises a convection section and a radiation section. After the pyrolysis raw material is preheated, diluted steam is added into the pyrolysis raw material, the pyrolysis raw material is heated in a convection section, then enters a radiation section for pyrolysis reaction, and the generated pyrolysis gas is quenched after leaving the furnace and is sent into a downstream device. After the fuel is combusted, heat exchange is carried out through the radiation section and the convection section, and finally the flue gas is discharged into the atmosphere. However, as the cracking device is continuously developed to be large-sized, the defects of the tubular cracking furnace are increasingly revealed, and the following defects mainly exist at present:
(1) The reaction temperature of the tubular cracking furnace generally does not exceed 1100 ℃ due to the heat resistance limit temperature of the heat-resistant alloy material of the furnace tube of the tubular cracking furnace, so that the cracking depth of the tubular cracking furnace cannot be further improved within a quite long time without breakthrough progress of the heat-resistant material;
(2) The tube type cracking furnace has the advantages that the tube diameter of the tube type cracking furnace is smaller, the operating pressure is lower, the density of raw gas is low under the normal condition, the operating capacity of the tube type cracking furnace is limited, a plurality of tube type cracking furnaces are usually required to be arranged along with the increasing of the size of the cracking device, the occupied area is increased, the construction investment is increased, and meanwhile, great test is brought to safety management;
(3) The heating mode adopted by the tubular cracking furnace is as follows: the fuel is combusted in the burner to generate high-temperature gas and indirectly exchange heat through the cracking furnace tube, and although the heat in the high-temperature gas is recovered through the convection section, more than 5% of the heat generated by the combustion of the fuel is not effectively utilized;
(4) The combustion improver used in the tube type cracking furnace is generally air, and during the process of mixing and burning with fuel, NO is inevitably generated x Contaminants of the likeFlue gas, which is currently directly discharged into the atmosphere, causes environmental pollution.
Disclosure of Invention
The invention aims to solve the problems that the cracking temperature cannot be continuously improved, the residence time is shortened, the single cracking furnace is limited in scale, the heat generated by fuel combustion is not fully utilized and the like in the prior art.
In order to achieve the above purpose, the invention provides a conical cracking reactor, which comprises a conical reactor body and a quenching heat exchanger communicated with the lower end of the conical reactor body, wherein the top of the conical reactor body is provided with at least one cracking raw material inlet, and the side wall of the conical reactor body is provided with at least one high-temperature flue gas inlet.
In the conical cracking reactor, cracking raw materials enter the conical cracking reactor through a nozzle, and are subjected to multistage mixed heat exchange with high-temperature gas from a high-temperature high-pressure combustion chamber and quickly undergo cracking reaction. The conical reactor body is narrowed from the feeding end to the quencher (namely along the material flowing direction), and the reactor body with conical design can accelerate the flow rate of pyrolysis gas, thereby reducing the reaction residence time and reducing the coking phenomenon.
In the above conical cracking reactor, preferably, the side wall of the conical reactor body is provided with at least two high-temperature flue gas inlets distributed at intervals along the diameter length of the reactor. The temperature of the plurality of high-temperature flue gas inlets can continuously provide heat for the cracking reaction, the cracking reaction is facilitated, and the arrangement structure is required to be distributed along the diameter of the reactor from the raw material inlet to the product outlet.
In the above conical cracking reactor, preferably, the conical reactor body is communicated with the quenching heat exchanger through a reducing structural member; the reducing structure is preferably a venturi connection section. The arrangement of the reducing structural member can ensure that higher flow velocity of pyrolysis gas is obtained in the conical pyrolysis reactor, shorten the reaction residence time, relatively uniformly distribute the pyrolysis gas and enhance the heat exchange effect of the quenching heat exchanger.
In the conical cracking reactor, preferably, a cracking product outlet is arranged at the bottom of the quenching heat exchanger.
In the above conical cracking reactor, preferably, the quenching heat exchanger is a dividing wall type heat exchanger, preferably a shell-and-tube heat exchanger.
The present invention also provides a hydrocarbon cracking process comprising: directly contacting the cracking raw material with high-temperature flue gas at 1000-1300 ℃ and 1-6Mpa for cracking reaction, and then quenching and cooling to obtain a cracking product; wherein the cracking reaction and the rapid cooling are carried out in the conical cracking reactor.
Unlike the heat convection and radiation of the tubular cracking furnace in the prior art, the hydrocarbon cracking method of the invention ensures that the cracking raw material and the high-temperature flue gas are directly mixed and contacted in the reactor for heat exchange, maximally utilizes the heat energy in the high-temperature flue gas, ensures that the theoretical energy utilization efficiency is 100 percent, and ensures that the cracking reaction temperature maintains higher level. In addition, in the cracking reaction of the hydrocarbon cracking method, the pressure in the reactor is pressurized from the outside of the boundary region by the raw material tank bottom pump, and the pressure of the liquid feed liquid can be adjusted according to the feed liquid combination and properties, so that the cracking raw material and high-temperature flue gas can be directly mixed and contacted in the cracking reaction process to keep higher reaction pressure, and meanwhile, the generated cracking product has higher pressure along with higher cracking reaction pressure, so that the compression energy consumption of the cracking product in the subsequent separation treatment can be greatly reduced. In the invention, the hydrocarbon cracking method can provide pressure through upstream raw material with pressure, and meanwhile, equipment such as a downstream tower and the like can help to realize pressure stabilization.
In the above hydrocarbon cracking method, preferably, the hydrocarbon cracking method further comprises: cooling the pyrolysis gas to 150-350 ℃ again, and then fractionating to obtain heavy oil and light components.
In the above hydrocarbon cracking method, preferably, the hydrocarbon cracking method further comprises: optionally compressing the light components and then carrying out CO 2 Recovering and treating to obtain pyrolysis gas.
In the above hydrocarbon cracking process, preferably, the high temperatureThe smoke is obtained by mixing and burning fuel and combustion improver, the temperature of the high-temperature smoke is 1000-1300 ℃, and the pressure is 1-6Mpa. If the pressure of the light component is already higher than that of CO 2 The air pressure standard value of the recovery treatment is not needed to be compressed, so that the compression energy consumption can be greatly saved.
In the above hydrocarbon cracking method, preferably, the fuel is a gaseous fuel or a liquid fuel, the gaseous fuel may be ethane, propane or natural gas, and the liquid fuel may be gasoline or diesel; the combustion improver is pure oxygen, oxygen-enriched or air, more preferably pure oxygen. In the hydrocarbon cracking method, the fuel and the combustion improver are controlled by calculating the setting proportion, so that on one hand, the high-temperature gas is ensured to contain no oxygen (namely, the fuel is completely combusted) so as to avoid safety problems or consume downstream raw materials, and on the other hand, the temperature of the high-temperature gas after combustion can be controlled.
In the above hydrocarbon cracking method, preferably, the hydrocarbon cracking method rapidly cools the product to 300-600 ℃ to prevent secondary reaction of the cracked product.
In the above hydrocarbon cracking method, preferably, the cooling medium used for quenching and cooling is saturated cooling water provided by a steam drum, and the saturated cooling water used for quenching and cooling rapidly removes heat in the cracking gas through rapid gasification; and the saturated cooling water is used for cooling the cracking product in a quenching way, gasifying the cracking product into saturated steam and returning the saturated steam to the steam drum.
In the above hydrocarbon cracking method, preferably, the hydrocarbon cracking method further includes heat exchanging the cracking product with an external cooling medium, and the cooling medium after heat exchanging enters a steam drum to form the saturated cooling water.
In the above hydrocarbon cracking method, preferably, the hydrocarbon cracking method further comprises: preheating a cracking raw material by adopting part of the heavy oil, and then cooling a cracking product; preferably, the hydrocarbon cracking process further comprises heat recovery of the heavy oil.
In the above hydrocarbon cracking method, the cracking raw material may be a plurality of raw materials such as ethane, liquefied gas, naphtha, diesel oil, tail oil, crude oil, etc., and may be mainly from a refinery or an oilfield resource.
In the above hydrocarbon cracking method, preferably, the hydrocarbon cracking method comprises:
directly contacting the preheated cracking raw material with high-temperature flue gas at 1000-1300 ℃ and 1-6Mpa for cracking reaction, and then quenching and cooling reactants to 300-600 ℃ to obtain a cracking product; wherein the cracking reaction and the rapid cooling are carried out in the conical cracking reactor;
cooling the pyrolysis gas again and then fractionating to obtain heavy oil and light components; optionally compressing the light components and then carrying out CO 2 Recovering and treating to obtain pyrolysis gas.
The invention also provides a hydrocarbon cracking reaction system which comprises the conical cracking reactor and a combustion chamber, wherein the combustion chamber is provided with one or more flue gas channels, and the flue gas channels are respectively connected with a high-temperature flue gas inlet of the conical cracking reactor.
In the hydrocarbon cracking reaction system, preferably, the cross-sectional areas of the flue gas channels are different. The flue gas channel pipeline or a high-temperature gas channel constructed by refractory and pressure-resistant materials. When the combustion chamber is provided with a plurality of flue gas channels, each flue gas channel is connected with the conical cracking reactor at intervals so as to ensure that the temperature in the cracking reactor is relatively constant, and meanwhile, the sectional areas (inner diameters) of the flue gas channels can be different so as to ensure reasonable distribution of high-temperature gas flow.
In the hydrocarbon cracking reaction system, preferably, the hydrocarbon cracking reaction system further comprises a steam drum, and a heat remover is further arranged on the outer wall of the flue gas channel; the saturated liquid outlet of the steam drum is connected with the heat exchange medium inlet of the quenching heat exchanger of the conical cracking reactor, the heat exchange medium outlet of the quenching heat exchanger is connected with the saturated steam inlet of the steam drum, and the steam outlet of the steam drum is connected with the heat remover of the combustion chamber.
In the hydrocarbon cracking reaction system, the steam drum is fed with boiler feed water heated by a heat recovery heat exchanger, a cooling medium (which can be boiler feed water) in the steam drum is conveyed to a quenching heat exchanger, gasified saturated steam returns to the steam drum, is heated by a heat remover, and superheated steam is conveyed to a downstream device as a product. In the invention, saturated steam is heated into superheated steam, the temperature of a flue can be adjusted, the control on the raw material cracking reaction is easier to realize, and in addition, the superheated steam can be used as turbine driving power for a compressor of a downstream device, thereby being beneficial to reducing comprehensive energy consumption of a whole plant.
In the hydrocarbon cracking reaction system, preferably, the combustion chamber is provided with a fuel inlet and a combustion improver inlet.
In the hydrocarbon cracking reaction system, preferably, the combustion chamber is further provided with a temperature-adjusting water vapor inlet. The temperature-regulating water vapor inlet is normally closed, and is started when the temperature of the high-temperature gas is too high, so that the temperature of the high-temperature gas is quickly reduced, the operating pressure of the high-temperature high-pressure combustion chamber can be between 1 and 6Mpa, and the operating temperature can be between 1000 and 1300 ℃.
In the above hydrocarbon cracking reaction system, preferably, the hydrocarbon cracking reaction system further includes a fractionating tower, the fractionating tower is provided with an inlet, a cracked gas outlet and a heavy oil outlet, and a cracked product outlet of the quenching heat exchanger is connected with the inlet of the fractionating tower.
The primary fractionating tower may be one single tower or multiple towers, and the cracked product is further cooled in the primary fractionating tower to recover heat while realizing preliminary separation, and the separated cracked gas is fed into downstream unit, with one part of heavy oil as the heat source of the material preheater for heating or gasifying the cracked material, cooled and fed into the temperature controller as the cold source for mixing with the cracked product to cool, and the other part of the cracked gas is fed into the heavy oil heat exchanger for heat recovery.
In the above hydrocarbon cracking reaction system, preferably, the hydrocarbon cracking reaction system further includes a heavy oil heat exchanger for recovering heat of the heavy oil. The heavy oil heat exchanger may be single or multiple, and is aimed at recovering heat from the heavy oil extracted from the primary fractionating tower to raise heat utilization rate.
In the hydrocarbon cracking reaction system, preferably, a pipeline between a cracked product outlet of the quenching heat exchanger and an inlet of the fractionating tower sequentially passes through the heat recovery heat exchanger and the temperature controller; the cooling medium channel of the heat recovery heat exchanger is connected with the liquid inlet of the steam drum, and the heating medium inlet of the temperature controller is connected with the heavy oil outlet.
The heat recovery heat exchanger is used for realizing heat exchange between the pyrolysis product and an exogenous cooling medium, and the pyrolysis product is cooled by the heat recovery heat exchanger, so that the occurrence of secondary reaction can be reduced on one hand, and on the other hand, the heat in the pyrolysis product is absorbed by the boiler feed water, so that the aim of producing more steam is fulfilled, and the heat utilization efficiency is improved.
The temperature controller adopts a heavy oil spraying mode to further reduce the temperature of the cracking products.
In the hydrocarbon cracking reaction system, the heat recovery heat exchanger adopts boiler feed water from outside the boundary as a medium, so as to recover residual heat in the cracked product after passing through the quenching heat exchanger to improve the heat utilization rate, and the internal energy of the boiler feed water is improved to generate more saturated steam for downstream devices.
In the above hydrocarbon cracking reaction system, preferably, the hydrocarbon cracking reaction system further includes a raw material preheater, and a heating medium channel of the raw material preheater is connected to the heavy oil outlet. The raw material preheater is used for realizing heat exchange between the cracking raw material and the heavy oil.
In the above hydrocarbon cracking reaction system, preferably, the hydrocarbon cracking reaction system comprises: the device comprises a raw material preheater, a high-temperature high-pressure combustion chamber, a heat remover, a conical cracking reactor, a steam drum, a heat recovery heat exchanger, a temperature controller, a primary fractionating tower and a heavy oil heat exchanger;
the conical cracking reactor comprises a conical reactor body and a quenching heat exchanger communicated with the lower end of the conical reactor body through a Venturi connection section, wherein at least one cracking raw material inlet is formed in the top of the conical reactor body, one or more high-temperature flue gas inlets are formed in the side wall of the conical reactor body, and a cracking product outlet is formed in the bottom of the quenching heat exchanger;
the high-temperature high-pressure combustion chamber is provided with one or more flue gas channels which are respectively connected with a high-temperature flue gas inlet of the conical cracking reactor; the high-temperature high-pressure combustion chamber is also provided with a fuel inlet, a combustion improver inlet and a temperature-adjusting steam inlet, and the heat remover is arranged on the outer wall of the high-temperature high-pressure combustion chamber;
the steam drum is provided with a liquid inlet, a saturated liquid outlet, a saturated steam inlet and a steam outlet, the saturated liquid outlet of the steam drum is connected with a heat exchange medium inlet of a quenching heat exchanger of the conical cracking reactor, the heat exchange medium outlet of the quenching heat exchanger is connected with the saturated steam inlet of the steam drum, and the steam outlet of the steam drum is connected with a heat remover of the combustion chamber;
the fractionating tower is provided with an inlet, a pyrolysis gas outlet and a heavy oil outlet, a pyrolysis product outlet of the quenching heat exchanger is connected with the inlet of the fractionating tower, and a pipeline between the pyrolysis product outlet of the quenching heat exchanger and the inlet of the fractionating tower sequentially passes through the heat recovery heat exchanger and the temperature controller; the cooling medium channel of the heat recovery heat exchanger is connected with the liquid inlet of the steam drum, and the heating medium inlet of the temperature controller is connected with the heavy oil outlet;
the heating medium channel of the raw material preheater and the heavy oil heat exchanger are respectively connected with the heavy oil outlet.
In the hydrocarbon cracking reaction system, the hydrocarbon cracking reaction system is preferably used for carrying out the hydrocarbon cracking method.
The technical scheme provided by the invention has the following beneficial effects:
(1) According to the invention, high-temperature flue gas generated in the combustion chamber is directly mixed with raw materials for heat exchange and cracking reaction occurs, so that the cracking reaction temperature can be increased, the cracking reaction depth is increased, and meanwhile, the heat energy of fuel combustion is utilized to the greatest extent (the theoretical energy utilization efficiency is 100%);
(2) The operation pressure of the cracking reactor breaks the limit of the traditional tubular cracking furnace, the cracking reaction can be carried out within 1-7Mpa, the reaction residence time of the conical cracking reactor is greatly shortened, and the problem that the reaction is easy to coke under the high-pressure condition is prevented; meanwhile, with higher cracking reaction pressure, the generated cracking product also has higher pressure, so that the compression energy consumption of the cracking product in the subsequent separation treatment can be greatly reduced; (3) The invention directly mixes the high-temperature gas with the cracking raw material for cracking, and carbon dioxide, carbon monoxide, water and the like in the high-temperature gas are used as inert gases to reduce the partial pressure of the reacted hydrocarbon so as to facilitate the cracking reaction; compared with the traditional tubular cracking furnace, a large amount of dilution steam can be saved;
(4) The invention adopts the sectional design between the high-temperature high-pressure combustion chamber and the cracking reactor, and the two are connected only through the flue gas channel, so that the safety risk of direct contact between open fire in the combustion chamber and raw materials in the cracking reactor is avoided; meanwhile, the multiple channels are discretely distributed on the cracking reactor, so that the relatively constant reaction temperature of the cracking reactor can be ensured to the greatest extent, and the cracking reaction depth is ensured.
Drawings
FIG. 1 is a schematic flow diagram of a hydrocarbon cracking reaction system according to example 2 of the present invention, which includes a conical cracking reactor according to example 1.
Reference numerals illustrate:
01-high-temperature high-pressure combustion chamber, 02-heat remover, 03-connecting channel, 04-cracking reactor, 05-Venturi connecting section, 06-quenching heat exchanger, 07-heat recovery heat exchanger, 08-steam drum, 09-temperature controller, 10-primary fractionating tower, 11-raw material preheater and 12-heavy oil heat exchanger;
001-cracking raw material, 002-fuel, 003-combustion improver, 004-high-temperature flue gas, 005-cracking product, 006-heavy oil, 007-cracking gas, 008-boiler water supply, 009-saturated boiler water supply, 010-saturated steam and 011-superheated steam.
Detailed Description
The technical solution of the present invention will be described in detail below for a clearer understanding of technical features, objects and advantageous effects of the present invention, but should not be construed as limiting the scope of the present invention.
Example 1
The embodiment provides a conical cracking reactor, as shown in fig. 1, which comprises a conical reactor body 04 and a quenching heat exchanger 06 communicated with the lower end of the conical reactor body through a Venturi connection section 05, wherein at least one cracking raw material inlet is arranged at the top of the conical reactor body 04, and a plurality of high-temperature flue gas inlets distributed at intervals are arranged on the side wall of the conical reactor body 04; the bottom of the quenching heat exchanger 06 is provided with a pyrolysis product outlet.
Example 2
The present embodiment provides a hydrocarbon cracking reaction system, as shown in fig. 1, which includes: a high temperature and high pressure combustion chamber 01, a heat remover 02, a conical cracking reactor of the embodiment 1, a heat recovery heat exchanger 07, a steam drum 08, a temperature controller 09, a fractionating tower 10, a raw material preheater 11 and a heavy oil heat exchanger 12;
the high-temperature high-pressure combustion chamber 01 is provided with one or more flue gas channels 03, and the flue gas channels 03 are respectively connected with a high-temperature flue gas inlet of the conical cracking reactor; the high-temperature high-pressure combustion chamber 01 is also provided with a fuel inlet, a combustion improver inlet and a temperature-adjusting steam inlet, and the heat remover 02 is arranged on the outer wall of the flue gas channel 03;
the steam drum 08 is provided with a liquid inlet, a saturated liquid outlet, a saturated steam inlet and a steam outlet, the saturated liquid outlet of the steam drum 08 is connected with the heat exchange medium inlet of the quenching heat exchanger 06 of the conical cracking reactor, the heat exchange medium outlet of the quenching heat exchanger 06 is connected with the saturated steam inlet of the steam drum 08, and the steam outlet of the steam drum 08 is connected with the heat remover 02;
the fractionating tower 10 is provided with an inlet, a pyrolysis gas outlet and a heavy oil outlet, a pyrolysis product outlet of the quenching heat exchanger 06 is connected with the inlet of the fractionating tower 10, and a pipeline between the pyrolysis product outlet of the quenching heat exchanger 06 and the inlet of the fractionating tower 10 sequentially passes through the heat recovery heat exchanger 07 and the temperature controller 09; the cooling medium channel of the heat recovery heat exchanger is connected with the liquid inlet of the steam drum 08, and the heating medium inlet of the temperature controller 09 is connected with the heavy oil outlet; the heating medium channel of the raw material preheater 11 and the heavy oil heat exchanger 12 are connected to the heavy oil outlet, respectively.
Example 3
This example provides a hydrocarbon cracking process carried out using the hydrocarbon cracking reaction system of example 2, the hydrocarbon cracking process comprising the steps of:
s1: the fuel 002 and the combustion improver 003 are completely combusted and released in the high-temperature high-pressure combustion chamber 01 to generate high-temperature flue gas 004 with the temperature of 1300 ℃ and the pressure of 5Mpa, and the high-temperature flue gas 004 enters the conical cracking reactor through the flue gas channel 03; meanwhile, when the temperature of the high-temperature flue gas 004 is too high, temperature-adjusting steam is introduced to cool;
s2: the cracking raw material 001 enters a conical reactor body 04 of a conical cracking reactor after being preheated or gasified by a raw material preheater 11, and is directly mixed with high-temperature flue gas 004 from a high-temperature high-pressure combustion chamber 01 for heat exchange, cracking reaction (millisecond level) occurs in extremely short time, the cracking reaction temperature is 1300 ℃, the pressure is 5Mpa, and the obtained product enters a quenching heat exchanger 06 through a Venturi connection section 05 for quenching and cooling to 400 ℃ to inhibit secondary reaction, so as to obtain a cracking product 005; the quenching heat exchanger 06 uses saturated boiler feed water 009 from the steam drum 08 as a cooling medium, and saturated steam 010 passing through the quenching heat exchanger 06 is returned to the steam drum 08, and is heated by the heat remover 02 to form superheated steam 011 for a downstream user;
s3: the pyrolysis product is cooled to 170-300 ℃ through a heat recovery heat exchanger 07 and a temperature controller 09 in sequence, and then enters an initial fractionating tower 10 with a single tower or double tower structure for fractionation, so as to obtain light components and heavy oil; wherein the heat recovery heat exchanger 07 uses boiler feed water from the outside as a cooling medium to cool down the pyrolysis products, and then the boiler feed water enters a steam drum; a part of the heavy oil is used as a heat source of the raw material preheater 11 to heat or gasify the cracking raw material, and after cooling, the heavy oil enters the temperature controller 07 to be mixed with the cracking product to cool the cracking raw material, and then returns to the primary fractionating tower 10, and the other part of the heavy oil is sent to the heavy oil heat exchanger 12 to recover heat and then returns to the primary fractionating tower 10.
S4: optionally compressing the light components to 5Mpa and then CO 2 Recovering and treating to obtain a pyrolysis gas product; if the pressure of the light component is already higher than that of CO 2 The air pressure standard value of the recovery treatment is not needed to be compressed, so that the compression energy consumption can be greatly saved.
The hydrocarbon cracking method of the embodiment saves 5-10% of heat energy, 40-60% of total compression energy, and the reaction residence time can be reduced to 1-2 milliseconds, thus effectively inhibiting coking and prolonging the decoking period by 20-30%.
Claims (22)
1. The conical cracking reactor comprises a conical reactor body and a quenching heat exchanger communicated with the lower end of the conical reactor body, wherein at least one cracking raw material inlet is formed in the top of the conical reactor body, and at least one high-temperature flue gas inlet is formed in the side wall of the conical reactor body.
2. The conical cleavage reactor of claim 1, wherein the conical reactor body side wall is provided with at least two high temperature flue gas inlets spaced along the reactor diameter.
3. The tapered cleavage reactor of claim 1 wherein the tapered reactor body and quench heat exchanger are in communication via a reducing structure.
4. A tapered cleavage reactor as claimed in claim 3 wherein the reducing formation is a venturi connection section.
5. The tapered cleavage reactor of claim 1 wherein the quench heat exchanger bottom is provided with a cleavage product outlet.
6. The conical cleavage reactor according to claim 1, wherein the quench heat exchanger is a dividing wall heat exchanger, preferably a shell-and-tube heat exchanger.
7. A hydrocarbon cracking process comprising: directly contacting the cracking raw material with high-temperature flue gas at 1000-1300 ℃ and 1-6Mpa for cracking reaction, and then quenching and cooling to obtain a cracking product; wherein the cleavage reaction and quench cooling are carried out in a conical cleavage reactor according to any one of claims 1 to 6.
8. The hydrocarbon cracking process of claim 7, wherein the hydrocarbon cracking process further comprises: cooling the pyrolysis gas to 170-300 ℃ again, and then fractionating to obtain heavy oil and light components.
9. The hydrocarbon cracking process of claim 7, wherein the hydrocarbon cracking process further comprises: optionally compressing the light components and then carrying out CO 2 Recovering and treating to obtain pyrolysis gas.
10. The hydrocarbon cracking process as claimed in claim 7, wherein the high temperature flue gas is obtained by mixing and burning fuel and combustion improver, the temperature of the high temperature flue gas is 1000-1300 ℃, and the reaction pressure is 1-6Mpa.
11. The hydrocarbon cracking process of claim 7, wherein the hydrocarbon cracking process quenches the product to 300-600 ℃.
12. The hydrocarbon cracking process of claim 11, wherein the cooling medium for quenching is saturated cooling water supplied from a drum; and the saturated cooling water is used for cooling the cracking product in a quenching way, gasifying the cracking product into saturated steam and returning the saturated steam to the steam drum.
13. The hydrocarbon cracking process of claim 12, further comprising exchanging heat between the cracked product and an exogenous cooling medium, the exchanged cooling medium entering a drum to form the saturated cooling water.
14. The hydrocarbon cracking process of claim 12, wherein the hydrocarbon cracking process further comprises: preheating a cracking raw material by adopting part of the heavy oil, and then cooling a cracking product; and further comprises heat recovery of the heavy oil.
15. A hydrocarbon cracking reaction system comprising a conical cracking reactor according to any one of claims 1-6 and a combustion chamber provided with one or more flue gas channels, each of which is connected to a high temperature flue gas inlet of the conical cracking reactor.
16. The hydrocarbon cracking reaction system of claim 15, wherein the hydrocarbon cracking reaction system further comprises a steam drum, and the outer wall of the flue gas channel is further provided with a heat remover; the saturated liquid outlet of the steam drum is connected with the heat exchange medium inlet of the quenching heat exchanger of the conical cracking reactor, the heat exchange medium outlet of the quenching heat exchanger is connected with the saturated steam inlet of the steam drum, and the steam outlet of the steam drum is connected with the heat remover of the combustion chamber.
17. The hydrocarbon cracking reaction system of claim 15, wherein the combustion chamber is provided with a fuel inlet and a combustion improver inlet.
18. The hydrocarbon cracking reaction system of claim 17, wherein the combustion chamber is further provided with a attemperating steam inlet.
19. The hydrocarbon cracking reaction system of claim 15, further comprising a fractionation column having an inlet, a cracked gas outlet, and a heavy oil outlet, the cracked product outlet of the quench heat exchanger being connected to the inlet of the fractionation column.
20. The hydrocarbon cracking reaction system of claim 15, wherein the pyrolysis product outlet and the fractionation column inlet are connected in series through a heat recovery heat exchanger and a temperature controller; the cooling medium outlet of the heat recovery heat exchanger is connected with the liquid inlet of the steam drum, and the heating medium inlet of the temperature controller is connected with the heavy oil outlet.
21. The hydrocarbon cracking reaction system of claim 15, further comprising a feedstock preheater, a heating medium channel of the feedstock preheater being connected to the heavy oil outlet.
22. A hydrocarbon cracking reaction system according to any one of claims 15-21, wherein the hydrocarbon cracking reaction system is for carrying out a hydrocarbon cracking process according to any one of claims 7-14.
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