CN110607181A - Equipment and method for preparing light hydrocarbons by pressurizing and directly heating cracking - Google Patents
Equipment and method for preparing light hydrocarbons by pressurizing and directly heating cracking Download PDFInfo
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- CN110607181A CN110607181A CN201911018066.2A CN201911018066A CN110607181A CN 110607181 A CN110607181 A CN 110607181A CN 201911018066 A CN201911018066 A CN 201911018066A CN 110607181 A CN110607181 A CN 110607181A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
- C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
- C10B49/08—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form
- C10B49/10—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form according to the "fluidised bed" technique
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
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- 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
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- Oil, Petroleum & Natural Gas (AREA)
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- Dispersion Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides equipment and a method for preparing light hydrocarbons by pressurizing and directly heating cracking. The reaction device comprises a combustion chamber and a cracking chamber, wherein the combustion chamber is used for combusting fuel and oxygen to generate flue gas with the temperature of 2500-3000 ℃, the cracking chamber is positioned below the combustion chamber and is in fluid communication with the combustion chamber, the cracking chamber is constructed into a reducing structure along the longitudinal direction, and the inner diameter of the cracking chamber is smaller than that of the combustion chamber, so that the cracking raw material is mixed with the flue gas from the combustion chamber in the cracking chamber for heat exchange and reacts for a preset time under a preset pressure to generate a cracking product; the heat exchange device is positioned below the reaction device and is communicated with the fluid of the cracking chamber, and the heat exchange device is used for cooling the cracking product. According to the equipment disclosed by the invention, the reaction temperature and pressure are increased, the reaction time is shortened, and the yield of heavy energy after lightening is improved.
Description
Technical Field
The invention relates to the field of chemical industry, in particular to equipment and a method for preparing light hydrocarbons by pressurizing and directly heating cracking.
Background
The light energy of low carbon hydrocarbons and other small molecular hydrocarbons are mainly from the pyrolysis of petroleum hydrocarbons. High reaction temperatures and short residence times are advantageous for obtaining the highest possible yields of light hydrocarbons and also for reducing the formation of secondary by-products, which requires a large amount of heat to be supplied to the cracking reaction in a very short time.
From the perspective of heat transfer, the conventional thermal cracking can be divided into direct thermal cracking and indirect thermal cracking, wherein the former means that heat is directly transferred into a reaction system without a heat transfer medium by a heat source, and the latter means that heat is transferred to the reaction system through the heat transfer medium (a reaction tube wall).
The typical representative of indirect heating cracking is the steam cracking technology using a tubular cracking furnace, which is the core of the steam cracking technology, and the performance of the tubular cracking furnace is nearly perfect after long-term continuous improvement.
Numerous studies have shown that an increase in the cracking reaction temperature significantly increases the yield of light hydrocarbons, particularly light olefins. To further increase the cracking yield, a directly heated cracking unit was developed.
However, the pressure of the cracking reaction of the existing direct heating cracking equipment is lower, which is 0.1-0.5MPa, and the lower pressure causes the volume handling capacity of the equipment to be small, so that the investment on large-scale ethylene equipment is greatly increased. In addition, the pyrolysis gas is compressed before the cryogenic cooling and separation steps for preparing the low-carbon hydrocarbons, namely, higher pressure is needed, so that the equipment investment and energy consumption of a process compressor are increased, and the production efficiency is low.
Therefore, there is a need to provide an apparatus and a method for preparing light hydrocarbons by pressurized direct thermal cracking, which at least partially solve the problems in the prior art.
Disclosure of Invention
In this summary, concepts in a simplified form are introduced that are further described in the detailed description. This summary of the invention is not intended to identify key features or essential features of the claimed subject matter, nor is it intended to be used as an aid in determining the scope of the claimed subject matter.
According to a first aspect of the present invention, there is provided an apparatus for producing light hydrocarbons by pressurized direct thermal cracking, comprising:
at least one reaction apparatus, the reaction apparatus comprising:
a combustion chamber for combusting fuel and oxygen to generate flue gas with temperature of 2500-3000 ℃,
the pyrolysis chamber is positioned below the combustion chamber and is communicated with the combustion chamber in a fluid mode, the pyrolysis chamber is of a reducing structure along the axial direction, and the inner diameter of the pyrolysis chamber is smaller than that of the combustion chamber, so that pyrolysis raw materials are mixed with the flue gas from the combustion chamber in the pyrolysis chamber to exchange heat, and react for a preset time at a preset pressure to generate pyrolysis products; and
a heat exchange device located below the reaction device and in fluid communication with the cracking chamber, the heat exchange device being configured to cool the cracked product.
The equipment for preparing the light hydrocarbon by pressurizing and directly heating cracking improves the reaction temperature and pressure, greatly reduces the reaction time and effectively improves the yield of the light hydrocarbon.
Further, the reducing structure is a venturi structure or a cone structure.
Furthermore, the horizontal section of the heat exchange device is circular, and at least three reaction devices are arranged above the heat exchange device at intervals along a circular ring shape; or
The horizontal section of the heat exchange device is square, and at least two reaction devices are arranged above the heat exchange device at intervals in a linear arrangement mode.
Further, the equipment also comprises a quenching device, wherein the quenching device is arranged at the joint of the reaction device and the heat exchange device and is in fluid communication with the heat exchange device, the number of the quenching devices corresponds to that of the reaction device, and the quenching device is used for quenching and cooling the pyrolysis product.
Further, at least one heat exchanger extending along the height direction of the heat exchange device is arranged inside the heat exchange device, so that back mixing of internal air flow is reduced, waste heat is recovered, and the temperature of the cracking product is reduced to 200-300 ℃.
Further, the apparatus further comprises:
a fuel inlet nozzle located above and in communication with the combustion chamber;
a pyrolysis feedstock input tube orifice in fluid communication with the pyrolysis chamber; and
a steam attemperation nozzle in fluid communication with the combustion chamber.
Further, the side wall of the reaction device comprises a heat insulation layer and/or a cooling layer from inside to outside.
According to a second aspect of the present invention, there is provided a method for producing light hydrocarbons by pressurized direct thermal cracking, using the apparatus for producing light hydrocarbons by pressurized direct thermal cracking according to the first aspect, the apparatus comprising a steam attemperating nozzle, the method comprising the steps of:
s1: pressurizing the cracking raw material to 0.5-4.0 MPa, and preheating to 200-400 ℃;
s2: inputting fuel and oxygen into the combustion chamber for combustion to generate flue gas with the temperature of 2500-3000 ℃, and enabling the flue gas to enter the cracking chamber;
s3: atomizing and spraying the cracking raw material in the step S1 into the cracking chamber, mixing the cracking raw material with the flue gas for heat exchange, heating to 800-1200 ℃, and reacting for a preset time under the pressure of 0.5-4.0 MPa to generate a cracking product;
s4: quenching and cooling the pyrolysis product to 400-500 ℃;
s5: the heat exchange device exchanges heat with the cracked product so as to cool the cracked product to 200-300 ℃;
s6: sequentially decarbonizing and cooling the pyrolysis product to obtain pyrolysis gas;
s7: and separating light hydrocarbons in the cracked gas.
According to the method for preparing the light hydrocarbon by the pressurized direct heating cracking, the equipment for preparing the light hydrocarbon by the pressurized direct heating cracking of the first aspect of the invention is used, and the high pressure in the cracking chamber is combined with the diameter-variable structure of the cracking chamber, so that the operation speed of a cracking product in the cracking chamber is very high, the cracking product can enter a heat exchange device at a speed close to the speed of sound, and the reaction time is greatly reduced; and further increases the reaction temperature and increases the yield of hydrocarbons.
Further, the predetermined time in the step S3 is greater than 0.05 second and less than 0.2 second.
Further, the step S2 further includes: steam is input through the steam temperature adjusting pipe orifice and the flow of the fuel is controlled, so that the smoke reaches 800-1200 ℃.
Further, the reaction pressure in the step S1 is 0.5-3.5MPa, and between the step S5 and the step S6, the method further includes:
s8: compressing the pyrolysis product such that the pressure of the pyrolysis product is greater than 3.5 MPa.
Drawings
The following drawings of embodiments of the invention are included as part of the present invention for an understanding of the invention. The drawings illustrate embodiments of the invention and, together with the description, serve to explain the principles of the invention. In the drawings, there is shown in the drawings,
FIG. 1 is a schematic configuration diagram of an apparatus for producing light hydrocarbons by pressurized direct thermal cracking according to a first embodiment of the present invention;
FIG. 2 is a schematic view of the reaction apparatus in FIG. 1;
FIG. 3 is a schematic top view of an apparatus for producing light hydrocarbons by pressurized direct thermal cracking according to a first embodiment of the present invention;
FIG. 4 is a schematic top view of an apparatus for producing light hydrocarbons by pressurized direct thermal cracking according to a second embodiment of the present invention;
FIG. 5 is a schematic flow diagram of a process for producing light hydrocarbons by pressurized direct thermal cracking according to one embodiment of the present invention;
FIG. 6 is a schematic flow diagram of a process for producing light hydrocarbons by pressurized direct thermal cracking according to another embodiment of the present invention; and
FIG. 7 is a process flow diagram of a process for producing light hydrocarbons by pressurized direct thermal cracking in accordance with the present invention;
description of reference numerals:
100: equipment for preparing light hydrocarbon by pressurizing and direct heating cracking
1: reaction apparatus 11: combustion chamber
12: the cracking chamber 13: cooling layer
2: the heat exchange device 21: heat exchanger
3: fuel inlet nozzle 4: cracking raw material input pipe orifice
5: the quenching device 6: steam temperature adjusting pipe orifice
Detailed Description
In the following description, numerous specific details are set forth in order to provide a more thorough understanding of the present invention. It will be apparent, however, to one skilled in the art, that embodiments of the invention may be practiced without one or more of these specific details. In other instances, well-known features have not been described in detail so as not to obscure the embodiments of the invention.
In the following description, a detailed structure will be presented for a thorough understanding of embodiments of the invention. It is apparent that the implementation of the embodiments of the invention is not limited to the specific details familiar to those skilled in the art.
The first embodiment of the present invention provides a device 100 for preparing light hydrocarbons by pressurized direct thermal cracking, referring to fig. 1, comprising at least one reaction device 1 and a heat exchange device 2. Wherein the heat exchange means 2 is located below the reaction means 1 and is in fluid communication with the cracking chamber 12.
The reaction apparatus 1 further comprises a combustion chamber 11 and a cracking chamber 12. The combustion chamber 11 is used for combusting fuel and oxygen to generate flue gas with the temperature of 2500-3000 ℃; the cracking chamber 12 is located below the combustion chamber 11 and is in fluid communication with the combustion chamber 11, the cracking chamber 12 is configured as a reducing structure along an axial direction, and an inner diameter of the cracking chamber 12 is smaller than that of the combustion chamber 11, so that the cracking raw material is mixed with the flue gas from the combustion chamber 11 in the cracking chamber 12 for heat exchange and reacts at a predetermined pressure for a predetermined time to generate a cracking product. The heat exchange device 2 is used for cooling the cracked product.
The equipment 100 for preparing light hydrocarbon by pressurizing and directly heating cracking improves the reaction temperature and pressure, greatly reduces the reaction time and effectively improves the yield of the light hydrocarbon.
In order to further increase the gas running speed in the device and shorten the reaction time, the reducing structure of the cracking chamber 12 is preferably a venturi structure, and specifically, the inner diameter of the cracking chamber 12 is firstly reduced and then increased from top to bottom. Alternatively, the diameter-variable structure of the cracking chamber 12 may be a cone structure, specifically, the inner diameter of the cracking chamber 12 gradually decreases from top to bottom.
Referring to fig. 1 and 2, a fuel input pipe 3 communicated with the combustion chamber 11 is disposed at the top of the combustion chamber 11, and a fuel input device (not shown) inputs fuel and oxygen into the combustion chamber 11 through the fuel input pipe 3 for combustion to generate flue gas at 2500-3000 ℃, and the flue gas enters the cracking chamber 12. During the combustion process, the equivalence ratio of oxygen and fuel is controlled to be kept to be capable of complete combustion or oxygen-deficient combustion.
A cracking raw material input pipe orifice 4 which is communicated with the cracking chamber 12 in fluid is arranged on the side wall of the cracking chamber 12, and a cracking raw material input device (not shown) atomizes and sprays the pre-pressurized and preheated cracking raw material into the cracking chamber 12 through the cracking raw material input pipe orifice 4.
The cracking raw material is preheated to 200-400 ℃ through a preheating heat exchanger or a preheating heating furnace, and is pressurized to 0.5-4.0 MPa through a pre-pressurizing device.
The flue gas from the combustion chamber 11 and the heated and pressurized atomized cracking raw material are rapidly mixed in the cracking chamber 12, and react for 0.05 to 0.2 seconds under the conditions that the pressure is 0.5 to 4.0MPa and the temperature is 800 to 1200 ℃ to generate a cracking product.
The connection part of the reaction device 1 and the heat exchange device 2 is provided with a quenching device 5 which is communicated with the heat exchange device 2 in a fluid way, and the number of the quenching devices 5 corresponds to that of the reaction devices 1. Specifically, two quenching devices 5 are arranged at the joint of each reaction device 1 and the heat exchange device 2. The number of quench units 5 can be set as desired, for example in an embodiment not shown, one, three or four quench units 5 can also be provided at each junction of the reaction unit 1 and the heat exchange unit 2. And (3) spraying quenching water into the heat exchange device 2 by the quenching device 5 to quench and cool the pyrolysis product to 400-500 ℃, and terminating the secondary reaction.
With continued reference to fig. 1, the heat exchanger 2 is provided with a plurality of heat exchangers 21 extending along the height direction of the heat exchanger 2, and is used for guiding the quenched cracked product to reduce back mixing of the internal airflow, recovering the waste heat, and cooling the cracked product to 200-300 ℃. The plurality of heat exchangers 21 are arranged in parallel with each other. The heat exchanger 21 is preferably a flow-guiding heat exchange tube bundle, more preferably a water-cooled heat exchange panel. The heat exchanger 21 has a cleaner thereon. The cleaner is preferably a sootblower or rapper. The heat exchanger 2 is preferably a waste heat boiler, and recovers waste heat and utilizes the waste heat.
Referring now to fig. 2, the side wall of the reaction apparatus 1 includes a heat insulating layer (not shown) and a cooling layer 13 in this order from inside to outside. The cooling layer 13 is configured to provide cooling water coils or tubes in the sandwich of the side walls. Or the cooling layer 13 is configured as a water jacket. The insulation layer (not shown) is preferably made of a refractory insulating material. In an alternative embodiment, the side walls of the reactor apparatus 1 consist only of insulating layers.
The side wall of the reaction device 1 is further provided with a steam temperature adjusting pipe orifice 6 which is in fluid communication with the combustion chamber 11, and a steam temperature adjusting device (not shown) inputs high-temperature steam into the combustion chamber 11 through the steam temperature adjusting pipe orifice 6 for maintaining the temperature in the combustion chamber 11 within a predetermined range.
Referring to fig. 3, the horizontal section of the heat exchanger 2 is circular, and a plurality of reactors 1 are disposed above the heat exchanger 2 at intervals along the ring. Specifically, the reaction devices may be arranged along one circular ring shape, or may be arranged along two or more concentric circular rings, and the central angles between two adjacent reaction devices 1 on each circular ring are equal. In other words, the arc lengths between every two adjacent reaction apparatuses 1 may be equal.
As shown in fig. 3, the arrangement of the illustrated embodiment is: the eight reaction devices 1 are encircled into a first ring shape by taking the axis of the heat exchange device 2 as an axis, and the eight reaction devices 1 form the vertex of the first ring shape internally connected with the regular octagon; the four reaction devices 1 are encircled into a second ring shape by taking the axis of the heat exchange device 2 as the axis, and the four reaction devices 1 form the vertex of a second ring shape inscribed with a regular quadrangle. Wherein the two rings are concentric. Further, the radius of the first annulus may be twice the radius of the second annulus.
In addition, the front ends of the pipelines in the fuel input pipe orifice 3, the cracking raw material input pipe orifice 4 and the steam temperature adjusting pipe orifice 6 are provided with flow equipartition devices (not shown); a flame video combustion detection system (not shown) is arranged at the top of the fuel input pipe orifice 3; thermocouple temperature monitors (not shown) are provided in both the cracking chamber 12 and the heat exchange means 2.
Fig. 4 shows a second embodiment of the present invention, which is an apparatus 100 for producing light hydrocarbons by pressurized direct thermal cracking, and the basic structure is similar to the first embodiment of the present invention, except that the horizontal section of the heat exchange device 2 is square, and a plurality of reaction devices 1 are arranged above the heat exchange device 2 at intervals in a linear arrangement. Specifically, four reaction devices 1 are arranged above the heat exchange device 2 in a straight line shape, and the intervals between every two adjacent reaction devices 1 are equal.
Fig. 5 is a schematic flow chart of a method for preparing light hydrocarbons by pressurized direct thermal cracking according to an embodiment of the present invention, fig. 6 is a schematic flow chart of a method for preparing light hydrocarbons by pressurized direct thermal cracking according to another embodiment of the present invention, and fig. 7 is a process flow chart of the method. The method is implemented on a device 100 for preparing light hydrocarbons by pressurizing and directly heating cracking.
The method of the embodiment shown in fig. 5 includes:
s1, pressurizing the cracking raw material to 3.5-4.0MPa, and preheating to 200-400 ℃.
Preheating of cracking raw materials is completed by a preheating heat exchanger or a preheating heating furnace, and pressurizing is completed by a pre-pressurizing device. The cracking raw material is at least one of light hydrocarbon (such as liquefied petroleum gas, liquefied natural gas, ethane propane or butane), naphtha or light diesel oil fraction.
S2, inputting fuel and oxygen into the combustion chamber 11 for combustion to generate flue gas with the temperature of 2500-3000 ℃, and enabling the flue gas to enter the cracking chamber 12.
The fuel and oxygen are preferably pre-pressurized. During combustion, the equivalence ratio of oxygen and fuel is maintained to enable complete combustion or under-oxygen combustion.
The temperature of the flue gas is regulated by controlling the flow of the fuel. Preferably, the temperature of the flue gas is double regulated by the flow of steam and fuel input from the steam tempering nozzles 6.
The fuel is a gaseous fuel or a liquid fuel. Wherein the gas fuel is at least one of ethane, propane, natural gas and hydrogen-rich gas; the liquid fuel is at least one of gasoline, diesel oil or ethanol.
S3, atomizing and spraying the cracking raw material in the step S1 into the cracking chamber 12, mixing the cracking raw material with the flue gas for heat exchange, heating to 800-1200 ℃, and reacting for a preset time under the pressure of 3.5-4.0MPa to generate a cracking product.
Wherein the predetermined time is greater than 0.05 seconds and less than 0.2 seconds.
The cracked product contains light hydrocarbon, carbon dioxide, water, hydrogen and other components, and the carbon dioxide, water and other components can reduce the partial pressure of light hydrocarbon, facilitate the forward cracking reaction and raise yield.
S4, cooling the cracked product to 400-500 ℃.
Specifically, the quenching device 5 injects atomized quenching water into the heat exchange device 2 to quench and cool the cracked product, so as to terminate the secondary reaction of the cracked product.
S5, the heat exchange device exchanges heat with the pyrolysis product to enable the pyrolysis product to be cooled to 200-300 ℃.
And S6, sequentially decarbonizing and cooling the cracked product to obtain cracked gas.
The decarbonation step is generally carried out under a pressure of 3.5MPa or more, and the compression step is considered again from the actual pressure. And in the carbon dioxide removing process, carbon dioxide, acid gas and water in the cracking product are removed. For example, when the pressure is more than 3.5MPa, that is, the pressure of the cracked product is 3.5 to 4.0MPa, the decarbonation step can be directly performed without recompressing the cracked product.
S7, separating light hydrocarbon components in the cracked gas.
The separated light hydrocarbon components contain components such as ethylene, propylene, methane, ethane, propane and the like. The remaining components, including hydrogen, carbon monoxide, etc., can be recycled, for example, as fuel for the combustor 11.
According to the method for preparing the light hydrocarbon by the pressurized direct heating cracking, which is disclosed by the invention, the equipment 100 for preparing the light hydrocarbon by the pressurized direct heating cracking is implemented, the high pressure in the cracking chamber 12 is combined with the reducing structure of the cracking chamber 12, so that the operation speed of a cracking product in the cracking chamber 12 is very high, the cracking product can enter the heat exchange device 2 at the speed of the transonic speed, the reaction time is greatly reduced, about 0.1 second is reduced compared with the prior art, the temperature of the cracking reaction is about 200 ℃ higher than that of the prior art, and the yield of the light hydrocarbon is improved. In addition, when the pressure is more than 3.5MPa, a compression step is not required to be added in the subsequent process, and the production efficiency is high.
In the method for preparing light hydrocarbons by pressurized direct thermal cracking according to another embodiment of the present invention, referring to fig. 6, the cracking reaction in step S1 is performed at a pressure of 0.5 to 3.5MPa, so that the pressure of the cracked product is less than 3.5MPa, and the decarbonation step is performed after the cracked product is compressed.
At this time, step S8 is further performed between step S5 and step S6 to compress the cracked product so that the pressure of the cracked product is greater than 3.5 MPa.
Unless defined otherwise, technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. Features described herein in one embodiment may be applied to another embodiment, either alone or in combination with other features, unless the feature is otherwise inapplicable or otherwise stated in the other embodiment.
The present invention has been described in terms of the above embodiments, but it should be understood that the above embodiments are for purposes of illustration and description only and are not intended to limit the invention to the scope of the described embodiments. It will be appreciated by those skilled in the art that many variations and modifications may be made to the teachings of the invention, which fall within the scope of the invention as claimed.
Claims (11)
1. An apparatus for producing light hydrocarbons by pressure direct thermal cracking, comprising:
at least one reaction apparatus, the reaction apparatus comprising:
a combustion chamber for combusting fuel and oxygen to generate flue gas with temperature of 2500-3000 ℃,
a pyrolysis chamber located below and in fluid communication with the combustion chamber, the pyrolysis chamber configured as a reducing structure in an axial direction, and an inner diameter of the pyrolysis chamber being smaller than an inner diameter of the combustion chamber, such that a pyrolysis feedstock is mixed with the flue gas from the combustion chamber in the pyrolysis chamber for heat exchange and reacts at a predetermined pressure for a predetermined time to generate a pyrolysis product; and
a heat exchange device located below the reaction device and in fluid communication with the cracking chamber, the heat exchange device being configured to cool the cracked product.
2. The apparatus for preparing light hydrocarbons by pressurized direct thermal cracking according to claim 1, wherein the diameter-variable structure is a venturi structure or a conical cylinder structure.
3. The apparatus for producing light hydrocarbons by pressurized direct thermal cracking according to claim 1,
the horizontal section of the heat exchange device is circular, and at least three reaction devices are arranged above the heat exchange device at intervals along the circular shape; or
The horizontal section of the heat exchange device is square, and at least two reaction devices are arranged above the heat exchange device at intervals in a linear arrangement mode.
4. The apparatus for producing light hydrocarbons by pressurized direct thermal cracking according to claim 1, further comprising a quenching device disposed at the junction of the reaction device and the heat exchange device and in fluid communication with the heat exchange device, wherein the number of the quenching device corresponds to the number of the reaction device, and the quenching device is used for quenching and cooling the cracked product.
5. The equipment for preparing the light hydrocarbons through the pressurized direct thermal cracking according to claim 4, wherein at least one heat exchanger extending along the height direction of the heat exchange device is arranged inside the heat exchange device so as to reduce back mixing of internal airflow, recover waste heat and cool the cracked products to 200-300 ℃.
6. The apparatus for producing light hydrocarbons by pressurized direct thermal cracking according to claim 1, further comprising:
a fuel inlet nozzle located above and in communication with the combustion chamber;
a pyrolysis feedstock input tube orifice in fluid communication with the pyrolysis chamber; and
a steam attemperation nozzle in fluid communication with the combustion chamber.
7. The apparatus for producing light hydrocarbons by pressurized direct thermal cracking according to claim 1, wherein the side wall of the reaction device comprises a heat insulating layer and/or a cooling layer from inside to outside.
8. A method for producing light hydrocarbons by pressurized direct thermal cracking using the apparatus for producing light hydrocarbons by pressurized direct thermal cracking according to any one of claims 1 to 7, the apparatus including a steam attemperating nozzle, the method comprising the steps of:
s1: pressurizing the cracking raw material to 0.5-4.0 MPa, and preheating to 200-400 ℃;
s2: inputting fuel and oxygen into the combustion chamber for combustion to generate flue gas with the temperature of 2500-3000 ℃, and enabling the flue gas to enter the cracking chamber;
s3: atomizing and spraying the cracking raw material in the step S1 into the cracking chamber, mixing the cracking raw material with the flue gas for heat exchange, heating to 800-1200 ℃, and reacting for a preset time under the pressure of 0.5-4.0 MPa to generate a cracking product;
s4: quenching and cooling the pyrolysis product to 400-500 ℃;
s5: the heat exchange device exchanges heat with the cracked product so as to cool the cracked product to 200-300 ℃;
s6: sequentially decarbonizing and cooling the pyrolysis product to obtain pyrolysis gas;
s7: and separating light hydrocarbons in the cracked gas.
9. The method according to claim 8, wherein the predetermined time in the step S3 is greater than 0.05 second and less than 0.2 second.
10. The method for producing light hydrocarbons by pressurized direct thermal cracking according to claim 8, wherein the step S2 further comprises:
steam is input through the steam temperature adjusting pipe orifice and the flow of the fuel is controlled, so that the smoke reaches 800-1200 ℃.
11. The method for producing light hydrocarbons by pressurized direct thermal cracking according to claim 8, wherein the reaction pressure in step S1 is 0.5-3.5MPa, and the steps S5 and S6 further include:
s8: compressing the pyrolysis product such that the pressure of the pyrolysis product is greater than 3.5 MPa.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201911018066.2A CN110607181A (en) | 2019-10-24 | 2019-10-24 | Equipment and method for preparing light hydrocarbons by pressurizing and directly heating cracking |
| CN202010713315.6A CN111826173B (en) | 2019-10-24 | 2020-07-22 | Reaction device, production system and production method for preparing low-carbon olefin |
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| CN201911018066.2A CN110607181A (en) | 2019-10-24 | 2019-10-24 | Equipment and method for preparing light hydrocarbons by pressurizing and directly heating cracking |
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| CN111826173A (en) * | 2019-10-24 | 2020-10-27 | 中国船舶重工集团公司第七一一研究所 | Reaction device, production system and production method for preparing low-carbon olefin |
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| CN1068589A (en) * | 1992-07-11 | 1993-02-03 | 苏培 | Fuel-oil cracked gas burning process and equipment |
| DE19925316A1 (en) * | 1999-05-27 | 2000-11-30 | Technip Benelux B V | Process and plant for the autothermal gasification of solid fuels |
| JP4027241B2 (en) * | 2003-02-14 | 2007-12-26 | 之 渡邊 | Waste treatment equipment |
| CN101362669B (en) * | 2007-08-09 | 2012-12-12 | 中国石油化工股份有限公司 | Catalytic conversion method of ethylene, propylene and aromatic hydrocarbon preparation |
| CN101486919A (en) * | 2009-02-17 | 2009-07-22 | 北京海润川投资咨询有限公司 | Sectional temperature-controlled fluidized bed type biomass rapid pyrolysis reactor |
| CN101920187B (en) * | 2010-09-17 | 2012-10-24 | 王仲华 | Equipment and method for preparing low-carbon olefins by cracking reactions |
| US9441887B2 (en) * | 2011-02-22 | 2016-09-13 | Ensyn Renewables, Inc. | Heat removal and recovery in biomass pyrolysis |
| RU2573562C2 (en) * | 2011-10-12 | 2016-01-20 | Индийская Нефтяная Корпорация Лтд. | Method for obtaining olefin c3 in installation for fluid catalystical cracking |
| CN203382725U (en) * | 2013-05-31 | 2014-01-08 | 中国船舶重工集团公司第七一一研究所 | Carbon-containing material gasification-reforming change conversion furnace |
| US9073805B2 (en) * | 2013-11-19 | 2015-07-07 | Uop Llc | Hydrocracking process for a hydrocarbon stream |
| CN105289348A (en) * | 2015-11-16 | 2016-02-03 | 国电科学技术研究院 | Venturi tube type ammonia mixer |
| CN108423702A (en) * | 2018-06-22 | 2018-08-21 | 东北大学秦皇岛分校 | The production equipment and preparation method of rare earth oxide |
| CN110607181A (en) * | 2019-10-24 | 2019-12-24 | 上海齐耀热能工程有限公司 | Equipment and method for preparing light hydrocarbons by pressurizing and directly heating cracking |
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| CN111826173A (en) * | 2019-10-24 | 2020-10-27 | 中国船舶重工集团公司第七一一研究所 | Reaction device, production system and production method for preparing low-carbon olefin |
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