CN111099948B - Acetylene production method and system - Google Patents
Acetylene production method and system Download PDFInfo
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- CN111099948B CN111099948B CN201811251017.9A CN201811251017A CN111099948B CN 111099948 B CN111099948 B CN 111099948B CN 201811251017 A CN201811251017 A CN 201811251017A CN 111099948 B CN111099948 B CN 111099948B
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
- C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
- C07C4/06—Catalytic processes
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- C—CHEMISTRY; METALLURGY
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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
- C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
- C01B3/26—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using catalysts
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0266—Processes for making hydrogen or synthesis gas containing a decomposition step
- C01B2203/0277—Processes for making hydrogen or synthesis gas containing a decomposition step containing a catalytic decomposition step
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/06—Integration with other chemical processes
- C01B2203/062—Hydrocarbon production, e.g. Fischer-Tropsch process
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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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Abstract
The invention relates to an acetylene production method and system, wherein the method comprises the following steps: introducing the cracking raw material and carrier gas into a cracking reactor heated by electromagnetic induction to carry out cracking reaction from top to bottom, and rapidly cooling and gas-solid separating the obtained reaction product by a quenching medium to obtain a gas product containing acetylene; wherein the conditions of the cleavage reaction include: the temperature is 1000-2500 ℃, the reaction time is 5-100 ms, and the feeding ratio of carrier gas to pyrolysis raw material in unit time is 5-100L/g; the cracking raw material comprises inferior oil and/or catalytic cracking reaction products. The method and the system have high acetylene and hydrogen yield.
Description
Technical Field
The invention relates to an acetylene production method and system.
Background
In China, the availability of inferior oil and the increase of processing profits are caused by the reduction of crude oil reserves and the enhancement of environmental awareness, so that the market share of low-quality gasoline and diesel is reduced. Meanwhile, the demand of high-quality gasoline is increased, the diesel oil is structurally excessive due to economic slowing, the market share of the diesel oil is smaller and smaller, and chemical raw materials such as low-carbon olefin, aromatic hydrocarbon and the like still run short, and the development of oil refining transformation is required to be realized, so that the high-temperature cracking technology for producing the chemical raw materials by inferior heavy oil is required to be developed, and the transformation from oil refining to chemical industry is realized.
Acetylene is an important basic organic chemical raw material. The industrial method for producing acetylene mainly comprises a calcium carbide method, a methane partial oxidation method and a methane arc cracking method, wherein the calcium carbide method acetylene is mature in process, and occupies absolute proportion in industrial production, but pollution and energy consumption are relatively high. The plasma pyrolysis of coal to acetylene is a new and promising direct chemical conversion path for coal, and the related research starts from the university of Sheffield in the united kingdom in the 60 s of the 20 th century: in high temperature, high enthalpy, high reactivity arc thermal plasma jet, coal volatiles and even fixed carbon can be directly converted to acetylene. Thereafter, a great deal of research has been focused on the united kingdom, the united states, germany, india, soviet union, etc. countries. Since the 90 s, a great deal of basic research and engineering research are performed in the field by the scholars and engineering technicians in China. With the development of technology, researchers also use plasmas in the research of producing acetylene by coal tar, asphaltenes, slurry oil and the like, but no industrial report is seen.
In the traditional gasification hydrogen production technology, coal is generally adopted as a raw material, quartz sand is adopted as a bed material, air (oxygen), water vapor or mixed gas of the oxygen and the water vapor is adopted as fluidizing gas, partial combustion and gasification are carried out on coal particles in a gasification reactor, combustion products and gasification products are respectively generated, fuel gas with certain purity is obtained after collection, and heat required by gasification is provided by the combustion process of the coal; the disadvantage is that the flue gas produced by the combustion of coal is blended into the gasification product produced by coal gasification, and the fuel gas quality is low.
Disclosure of Invention
The invention aims to provide an acetylene production method and system, which have high acetylene and hydrogen yield.
In order to achieve the above object, the present invention provides a method for producing acetylene, comprising:
introducing the cracking raw material and carrier gas into a cracking reactor heated by electromagnetic induction to carry out cracking reaction from top to bottom, and rapidly cooling and gas-solid separating the obtained reaction product by a quenching medium to obtain a gas product containing acetylene; wherein the conditions of the cleavage reaction include: the temperature is 1000-2500 ℃, the reaction time is 5-100 ms, and the feeding ratio of carrier gas to cracking raw material in unit time is 3-150L/g; the cracking raw material comprises inferior oil and/or catalytic cracking reaction products.
Optionally, the method further comprises: preheating the cracking raw material and the carrier gas, and then feeding the preheated cracking raw material and the carrier gas into the cracking reactor, wherein the temperature of the preheated cracking raw material is 200-500 ℃, and the temperature of the preheated carrier gas is 500-2000 ℃.
Optionally, the inferior oil is selected from one or more of vacuum residuum, coal tar and solvent deasphalted oil, and the catalytic cracking reaction product is selected from one or more of catalytic cracking slurry oil, catalytic cracking diesel oil and catalytic cracking recycle oil;
the carrier gas is selected from one or more of nitrogen, helium, argon, methane and C2-C4 light hydrocarbons.
Optionally, the quenching medium used for rapid cooling is selected from one or more of water, nitrogen and argon;
the temperature of the reaction product after rapid cooling is 200-500 ℃.
Optionally, the conditions of the cleavage reaction include: the temperature is 1200-2000 ℃, the reaction time is 10-70 ms, and the feeding ratio of carrier gas to pyrolysis raw material in unit time is 10-80L/g.
Optionally, the cracking reactor is a metal tubular reactor vertically arranged along the axial direction;
the cracking raw material and carrier gas are introduced into the metal tubular reactor from the top of the metal tubular reactor, the reaction product is led out of the metal tubular reactor from the bottom of the metal tubular reactor, and the quenching medium is introduced into the metal tubular reactor from the lower part of the metal tubular reactor.
Optionally, the material of the metal tubular reactor is selected from one or more of tungsten, molybdenum, tantalum, niobium, vanadium, chromium, titanium, zirconium, rare earth boride, rare earth carbide, rare earth nitride, rare earth silicide, rare earth phosphide and rare earth sulfide, and the rare earth is selected from one or more of lanthanum, cerium, praseodymium and neodymium.
The invention also provides an acetylene production system, which comprises: a pyrolysis reactor, an electromagnetic induction coil, high-frequency electric induction heating equipment and a gas-solid separator;
the cracking reactor is provided with a raw material inlet at the top, a product outlet at the bottom and a quenching medium inlet at the lower part, and the gas-solid separator is provided with a material inlet and a material outlet; the electromagnetic induction coil is wound on the periphery of the cracking reactor, and the high-frequency electric induction heating equipment is connected with the electromagnetic induction coil;
and a product outlet of the cracking reactor is communicated with a material inlet of the gas-solid separator.
Optionally, the cracking reactor is a metal tubular reactor vertically arranged along an axial direction, the material of the metal tubular reactor is selected from one or more of tungsten, molybdenum, tantalum, niobium, vanadium, chromium, titanium, zirconium, rare earth boride, rare earth carbide, rare earth nitride, rare earth silicide, rare earth phosphide and rare earth sulfide, and the rare earth is selected from one or more of lanthanum, cerium, praseodymium and neodymium.
Optionally, one or more reticular interlayer(s) for promoting raw material cracking are arranged in the cracking reactor.
Optionally, the cracking reactor comprises a first expanding section, a reaction section and a second expanding section from top to bottom, the inner diameters of the first expanding section and the second expanding section are larger than the inner diameter of the reaction section, and the electromagnetic induction coil is wound on the periphery of the reaction section.
Optionally, the system further comprises a filter and a gas collector, wherein the material outlet of the gas-solid separator is communicated with the gas collector through the filter.
Optionally, the system further comprises a first preheating furnace and a second preheating furnace, wherein the first preheating furnace is provided with a cracking raw material inlet and a preheating material outlet, the second preheating furnace is provided with a carrier gas inlet and a preheating material outlet, and the preheating material outlet of the first preheating furnace and the preheating material outlet of the second preheating furnace are communicated with the raw material inlet of the cracking reactor.
The invention has the advantages that:
(1) The electromagnetic induction coil heats the cracking reactor, so that the rapid temperature rise of the cracking reactor can be realized, and the reaction temperature is simple to control and stable to operate.
(2) Can provide ultra-high temperature and extremely short reaction time, realize the direct cracking of inferior oil and/or low-value catalytic cracking reaction products, and has high acetylene and hydrogen yields.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The accompanying drawings are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate the invention and together with the description serve to explain, without limitation, the invention. In the drawings:
FIG. 1 includes a schematic flow diagram of one embodiment of the method of the present invention, and also includes a schematic structural diagram of one embodiment of the system of the present invention.
Description of the reference numerals
1 pipeline 2 second preheating furnace 3 first preheating furnace
4 cracking reactor 5 high-frequency electric induction heating equipment 6 pipeline
7 pipeline 8 gas-solid separator 9 filter
10 gas collector 11 line 12 line
13 pipeline 14 pipeline 15 electromagnetic induction coil
Detailed Description
The following describes specific embodiments of the present invention in detail. It should be understood that the detailed description and specific examples, while indicating and illustrating the invention, are not intended to limit the invention.
The invention provides an acetylene production method, which comprises the following steps: introducing the cracking raw material and carrier gas into a cracking reactor heated by electromagnetic induction to carry out cracking reaction from top to bottom, and rapidly cooling and gas-solid separating the obtained reaction product by a quenching medium to obtain a gas product containing acetylene; wherein the conditions of the cleavage reaction include: the temperature is 1000-2500 ℃, the reaction time is 5-100 ms, and the feeding ratio of carrier gas to cracking raw material in unit time is 3-150L/g; the cracking raw material comprises inferior oil and/or catalytic cracking reaction products.
The invention adopts the electromagnetic induction heating cracking reactor, can realize the rapid temperature rise of the cracking reactor, has stable temperature, simpler equipment, smaller volume and easy implementation and operation compared with a plasma reactor, and can achieve the level of plasma cracking of acetylene and hydrogen yield.
According to the invention, in order to bring the cracking feedstock and carrier gas to the reaction temperature rapidly in the cracking reactor, the process further comprises: preheating the cracking raw material and the carrier gas, and then feeding the preheated cracking raw material and the carrier gas into the cracking reactor, wherein the temperature of the preheated cracking raw material can be 200-500 ℃, and the temperature of the preheated carrier gas can be 500-2000 ℃.
According to the present invention, inferior oil and catalytic cracking reaction products are well known to those skilled in the art, for example, the inferior oil may be selected from one or more of vacuum residuum, coal tar and solvent deasphalted oil, the catalytic cracking reaction products may be selected from one or more of catalytic cracking slurry oil, catalytic cracking diesel oil and catalytic cracking recycle oil, the values of the above products are low, and other cracking raw materials may be adopted or incorporated by those skilled in the art, which is not described in detail herein. The carrier gas is used for controlling the reaction time on one hand, enabling the cracking raw materials to quickly pass through the cracking reactor, and on the other hand, providing a raw material cracking high-temperature reaction gas environment, and improving the yield of acetylene and hydrogen, and can be selected from one or more of nitrogen, helium, argon, methane and C2-C4 light hydrocarbons.
According to the invention, the rapid cooling is used for rapidly cooling the reaction products to terminate the reaction and improve the yield of acetylene and hydrogen products, the quenching medium used for rapid cooling can be selected from water and/or nitrogen, the water can be selected from one or more of water, nitrogen and argon, and the nitrogen can be liquid nitrogen; the temperature of the reaction product after rapid cooling may be 200-500 ℃.
According to the invention, the cracking reaction is carried out at ultrahigh temperature and in a very short time, and compared with a plasma reactor, the cracking reactor has the advantages of simple structure, convenient implementation, easier control of the process and reduced energy consumption. The conditions of the cleavage reaction preferably include: the temperature is 1200-2000 ℃, the reaction time is 10-70 ms, and the feeding ratio of carrier gas to pyrolysis raw material in unit time is 10-80L/g.
According to the invention, the cracking reactor is a reactor which can be heated by electromagnetic induction, for example, a metal tubular reactor which is vertically arranged along the axial direction; the cracking raw material and the carrier gas can be introduced into the metal tubular reactor from the top of the metal tubular reactor, the reaction product can be led out of the metal tubular reactor from the bottom of the metal tubular reactor, the quenching medium can be introduced into the metal tubular reactor from the lower part of the metal tubular reactor, and the mixed flow of the reaction materials is reduced through the reaction from top to bottom, so that the reaction effect is improved. The material of the metal tubular reactor can be selected from one or more of tungsten, molybdenum, tantalum, niobium, vanadium, chromium, titanium, zirconium, rare earth boride, rare earth carbide, rare earth nitride, rare earth silicide, rare earth phosphide and rare earth sulfide, wherein the rare earth can be selected from one or more of lanthanum, cerium, praseodymium and neodymium; an electromagnetic induction coil may be sleeved on the outer circumference of the metal tubular reactor to heat the reactor by an alternating magnetic field generated by the electromagnetic induction coil.
The invention also provides an acetylene production system which comprises a cracking reactor, an electromagnetic induction coil, high-frequency electric induction heating equipment and a gas-solid separator; the cracking reactor is provided with a raw material inlet at the top, a product outlet at the bottom and a quenching medium inlet at the lower part, and the gas-solid separator is provided with a material inlet and a material outlet; the electromagnetic induction coil is wound on the periphery of the cracking reactor, and the high-frequency electric induction heating equipment is electrically connected with the electromagnetic induction coil; and a product outlet of the cracking reactor is communicated with a material inlet of the gas-solid separator.
According to the invention, the cracking reactor is a reactor which can be heated by electromagnetic induction, for example, a metal tubular reactor which is vertically arranged along the axial direction; the preheated cracking raw material and the preheated carrier gas can be introduced into the metal tubular reactor from the top of the metal tubular reactor, the reaction product can be led out of the metal tubular reactor from the bottom of the metal tubular reactor, and the quenching medium can be introduced into the metal tubular reactor from the lower part of the metal tubular reactor to fully contact with the reaction product gas from top to bottom, so that the cooling effect is improved. The material of the metal tubular reactor can be selected from one or more of tungsten, molybdenum, tantalum, niobium, vanadium, chromium, titanium, zirconium, rare earth boride, rare earth carbide, rare earth nitride, rare earth silicide, rare earth phosphide and rare earth sulfide, wherein the rare earth can be selected from one or more of lanthanum, cerium, praseodymium and neodymium; an electromagnetic induction coil may be sleeved on the outer circumference of the metal tubular reactor to heat the reactor by an alternating magnetic field generated by the electromagnetic induction coil. High-frequency electric induction heating apparatuses are well known to those skilled in the art, and on the one hand, can supply power to an electromagnetic induction coil, and on the other hand, an electromagnetic heating controller may be provided to control the frequency of alternating current input into the electromagnetic induction coil, and the electromagnetic heating controller is well known to those skilled in the art, and the present invention will not be repeated.
According to the invention, one of the products of the cracking reaction is carbon black, and the carbon black is solid and can block the subsequent pipelines carried in the reaction product, so that one or more net-shaped interlayers for promoting the cracking of the raw materials can be arranged in the cracking reactor, the heating area can be enlarged, the thermal efficiency can be improved, and the function of filtering part of the carbon black can be realized, thereby improving the full thermal contact of the cracked raw materials and effectively collecting the carbon black in the reactor for centralized treatment.
According to the invention, in order to facilitate feeding, discharging and quenching, the cracking reactor can comprise a first diameter expansion section, a reaction section and a second diameter expansion section from top to bottom, wherein the inner diameters of the first diameter expansion section and the second diameter expansion section can be larger than the inner diameter of the reaction section, and the electromagnetic induction coil can be wound on the periphery of the reaction section. The first expanding section and the second expanding section can be in a horn pipe or straight cylinder shape, if the first expanding section is a horn pipe, the pipe diameter is sequentially reduced from top to bottom, if the second expanding section is a horn pipe, the pipe diameter is gradually increased from top to bottom, and the quenching medium inlet can be arranged on the second expanding section and is communicated with the inside of the second expanding section.
According to the invention, in order to further purify and collect the gas product, the system may further comprise a filter and a gas collector, wherein the material outlet of the gas-solid separator may be communicated with the gas collector through the filter, the gas-solid separator is used for coarse separation of the reaction product, cyclone separation, sedimentation separation and other manners, the filter further separates the gas product obtained by separating the gas-solid separator, and may be a metal sintered filter element or a container filled with a washing liquid, the filtering precision of the metal sintered filter element may be less than 5 micrometers, the washing liquid may be water and the like, and the gas collector may be a container such as a gas tank, a gas bag and the like.
According to the present invention, in order to rapidly reach a reaction temperature of the pyrolysis feedstock and carrier gas in the pyrolysis reactor, the system may further include a first preheating furnace and a second preheating furnace, the first preheating furnace may be provided with a pyrolysis feedstock inlet and a preheating feedstock outlet, the second preheating furnace may be provided with a carrier gas inlet and a preheating feedstock outlet, and the preheating feedstock outlet of the first preheating furnace and the preheating feedstock outlet of the second preheating furnace may be in communication with the feedstock inlet of the pyrolysis reactor.
The invention is further illustrated by the following detailed description, which is not, however, intended to be limiting in any way.
As shown in fig. 1, the pyrolysis feedstock is first heated to 200-500 c in the first preheating furnace 3 and the carrier gas preheated to 500-2000 c by the line 1 into the second preheating furnace 2 is introduced into the tubular pyrolysis reactor 4 through the lines 11 and 12, respectively, and the pyrolysis reactor 4 is heated to the reaction temperature by the high-temperature heat source provided by the high-frequency electric induction heating apparatus 5 and the electromagnetic induction coil 15. The cracking raw material entering the reactor 4 is driven by a carrier to rapidly pass through the cracking reactor from top to bottom and carry out cracking reaction, quenching media from a pipeline 6 and a pipeline 7 are sprayed into the bottom of the cracking reactor 4 through two cooling medium inlets arranged at the bottom of the cracking reactor 4, quenching treatment is carried out on reaction products, the temperature of the reaction products is reduced to about 200-500 ℃, reaction products carrying carbon black are generated and enter a gas-solid separator 8 for coarse separation of carbon black, the carbon black is mostly collected in the cooling medium and the gas-solid separator 8, gas products carrying a small amount of carbon black after quenching enter a filter 9 for filtering and washing through a pipeline 13, and the gas products after washing enter a gas collector 10 through a pipeline 14.
The invention is further illustrated by the following examples, which are not intended to be limiting in any way.
Examples and comparative examples:
the reaction temperature refers to the temperature of the middle part of the reactor covered by the electromagnetic induction coil;
reaction time = reactor length/flow rate of reaction mass in the reactor;
hydrogen yield = weight of hydrogen in gas product/weight of cracking feedstock x 100%;
acetylene yield = weight of acetylene in gas product/weight of cracking feedstock x 100%;
the gaseous reaction products were determined by gas chromatography.
Example 1
According to the flow of the specific embodiment, catalytic diesel with the properties shown in table 1 is taken as a cracking raw material, the preheating temperature is 300 ℃, carrier gas is nitrogen, the preheating temperature is 800 ℃, a molybdenum tube is taken as a reactor, the molybdenum tube is vertically arranged along the length direction, the inner diameter is 10mm, the length is 38mm, and an electromagnetic induction coil is sleeved on the periphery of the molybdenum tube. Liquid nitrogen is introduced into the outlet of the reactor as a quenching medium, the flow rate of the liquid nitrogen is 4 liters/min, and the reaction temperature at the outlet of the reactor is controlled to be 300 ℃. The outlet of the reactor is provided with a filter screen, the filter precision of the filter screen is 300 meshes, the gas-solid separator is a carbon black filter bottle, the filter is a carbon black washing bottle, water is filled in the carbon black washing bottle, the gas collector is a gas collecting bag, and the specific reaction conditions and the reaction results are shown in Table 3.
Examples 2 to 5
Examples 2 to 5 were substantially the same as the reaction system and the reaction scheme of example 1 except that the reaction conditions were different, and the specific reaction conditions and the reaction results are shown in Table 3.
Examples 6 to 10
Examples 6 to 10 were substantially the same as the reaction system and reaction scheme of example 1 except that the reaction conditions were different, and the specific reaction conditions and the reaction results are shown in Table 4.
Examples 11 to 15
Examples 6 to 10 were substantially the same as the reaction system and reaction scheme of example 1, except that the reaction conditions were different, and the cleavage feed used was vacuum residuum (properties are shown in Table 2), and specific reaction conditions and reaction results are shown in Table 5.
Comparative examples 1 to 4
Comparative examples 1 to 4 were substantially the same as the reaction system and the reaction scheme of example 1 except that the reaction conditions were different, and the specific reaction conditions and the reaction results are shown in Table 6.
Example 16
Example 16 was substantially the same as the reaction system and reaction scheme of example 1, except that the cleavage feed at room temperature and the carrier gas were directly fed into the reactor without preheating to carry out the reaction, and the specific reaction conditions and the reaction results are shown in Table 6.
As can be seen from tables 3-6, the production process of the present invention can achieve high acetylene and hydrogen yields. Specifically, the reaction temperature of comparative example 1 was only 900 ℃ compared to example 1, and the hydrogen and acetylene yields were much lower than example 1; in contrast, in comparative example 2, even if the reaction temperature was increased to 2600 ℃, the hydrogen and acetylene yields were not increased but decreased; the reaction time of comparative example 3 increased to 110 ms compared to example 6, while the reaction time of comparative example 4 shortened to 3 ms, both hydrogen and acetylene yields were also reduced, indicating that even a short reaction time is detrimental to acetylene production at low cracking temperatures; compared with example 1, the cracking raw material and carrier gas of example 16 are directly reacted without preheating, and the yields of hydrogen and acetylene are greatly reduced. As can be seen from Table 4, the reaction temperature of example 6 is lower, even though the reaction time is shorter, whereas the reaction temperature of example 10 is higher, but the reaction time is longer, and the yields of both are also reduced, compared with examples 7 to 9, and therefore, the cracking temperature is preferably 1500 to 2000℃and the reaction time is preferably 5 to 20 ms, in order to obtain higher yields of acetylene and hydrogen according to the present invention.
The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited to the specific details of the above embodiments, and various simple modifications can be made to the technical solution of the present invention within the scope of the technical concept of the present invention, and all the simple modifications belong to the protection scope of the present invention.
In addition, the specific features described in the above embodiments may be combined in any suitable manner, and in order to avoid unnecessary repetition, various possible combinations are not described further.
Moreover, any combination of the various embodiments of the present invention can be made, as long as it does not depart from the gist of the present invention, which is also regarded as the content of the present invention.
TABLE 1
| Raw material name | Catalytic diesel |
| Density (20 ℃ C.)/(g/cm) 3 ) | 0.8965 |
| Refractive index (20 ℃ C.) | 1.5579 |
| Sulfur content/(wt%) | 0.231 |
| Nitrogen content/(micrograms/gram) | 548 |
| Carbon in% by weight | 89.23 |
| Hydrogen in% by weight | 10.32 |
| Hydrocarbon composition/°c | |
| Paraffin, weight percent | 16.9 |
| Naphthene, weight percent | 6.0 |
| Monocyclic aromatic hydrocarbon, weight percent | 56.0 |
| Bicyclic aromatic hydrocarbons, wt% | 21.1 |
| Tricyclic aromatic hydrocarbons, wt% | 0.0 |
| Total aromatic hydrocarbon, weight percent | 77.1 |
| Colloid, weight percent | 0.0 |
TABLE 2
| Raw material name | Vacuum residuum |
| Density (20 ℃ C.)/(g/cm) 3 ) | 0.97 |
| Viscosity (100 ℃ C.)/mm 2 Per second | 850 |
| Elemental analysis/(wt%) | |
| C | 85.3 |
| H | 11.8 |
| S | 1.28 |
| N | 0.92 |
| Residual carbon (weight%) | 13.9 |
| Relative molecular mass | 930 |
| Metal analysis/(micrograms/gram) | |
| Ni | 47 |
| V | 2.2 |
TABLE 3 Table 3
| Project | Example 1 | Example 2 | Example 3 | Example 4 | Example 5 |
| Cracking feedstock | Catalytic firewoodOil (oil) | Catalytic diesel | Catalytic diesel | Catalytic diesel | Catalytic diesel |
| Reaction temperature, DEG C | 1400 | 1400 | 1400 | 1400 | 1400 |
| Carrier gas flow, liter/min | 4 | 6 | 7 | 8 | 9 |
| Oil feed rate, g/min | 0.3 | 0.3 | 0.3 | 0.3 | 0.3 |
| Oil time, |
5 | 5 | 5 | 4 | 4 |
| Reaction time, ms | 47 | 33 | 28 | 24 | 22 |
| Hydrogen yield, wt% | 13.29 | 10.67 | 11.66 | 11.68 | 11.07 |
| Acetylene yield, wt% | 8.63 | 10.99 | 10.67 | 12.08 | 12.94 |
| Aggregate, percent | 21.92 | 21.66 | 22.23 | 23.76 | 24.01 |
TABLE 4 Table 4
| Project | Example 6 | Example 7 | Example 8 | Example 9 | Example 10 |
| Cracking feedstock | Catalytic diesel | Catalytic diesel | Catalytic diesel | Catalytic diesel | Catalytic diesel |
| Reaction temperature, DEG C | 1100 | 1300 | 1600 | 1800 | 2200 |
| Carrier gas flow, liter/min | 42 | 2.8 | 4 | 15 | 1.2 |
| Oil feed rate, g/min | 0.3 | 0.3 | 0.3 | 0.3 | 0.3 |
| Oil time, |
5 | 5 | 5 | 4 | 4 |
| Reaction time, |
5 | 70 | 40 | 10 | 100 |
| Hydrogen yield, wt% | 8.98 | 11.29 | 15.23 | 16.36 | 8.67 |
| Acetylene yield, wt% | 7.89 | 10.63 | 8.60 | 10.23 | 10.20 |
| Total weight percent | 16.87 | 21.92 | 23.83 | 26.59 | 18.87 |
TABLE 5
| Project | Example 11 | Example 12 | Example 13 | Example 14 | Example 15 |
| Cracking feedstock | Vacuum residuum | Vacuum residuum | Vacuum residuum | Vacuum residuum | Vacuum residuum |
| Reaction temperature, DEG C | 1400 | 1400 | 1400 | 1400 | 1400 |
| Carrier gas flow, liter/min | 4 | 6 | 7 | 8 | 9 |
| Oil feed rate, g/min | 0.3 | 0.3 | 0.3 | 0.3 | 0.3 |
| Oil time, |
5 | 5 | 5 | 4 | 4 |
| Reaction time, ms | 47 | 33 | 28 | 24 | 22 |
| Hydrogen yield, wt% | 14.29 | 11.67 | 12.86 | 12.68 | 12.07 |
| Acetylene yield, wt% | 10.15 | 11.99 | 12.67 | 13.58 | 13.84 |
| Total weight percent | 24.44 | 23.66 | 25.53 | 26.26 | 25.91 |
TABLE 6
| Project | Comparative example 1 | Comparative example 2 | Comparative example 3 | Comparative example 4 | Example 16 |
| Cracking feedstock | Catalytic diesel | Catalytic diesel | Catalytic diesel | Catalytic diesel | Catalytic diesel |
| Reaction temperature, DEG C | 900 | 2600 | 1100 | 1100 | 1400 |
| Carrier gas flow, liter/min | 4 | 6 | 1.8 | 70.1 | 4 |
| Oil feed rate, g/min | 0.3 | 0.3 | 0.3 | 0.3 | 0.3 |
| Oil time, |
5 | 5 | 5 | 4 | 5 |
| Reaction time, ms | 47 | 33 | 110 | 3 | 47 |
| Hydrogen yield, wt% | 6.85 | 7.80 | 7.89 | 2.56 | 10.29 |
| Acetylene yield, wt% | 3.67 | 8.01 | 2.30 | 3.20 | 8.20 |
| Total weight percent | 10.52 | 15.81 | 10.19 | 5.76 | 18.49 |
Claims (12)
1. A method of producing acetylene, the method comprising:
introducing the cracking raw material and carrier gas into a cracking reactor heated by electromagnetic induction to carry out cracking reaction from top to bottom, and rapidly cooling and gas-solid separating the obtained reaction product by a quenching medium to obtain a gas product containing acetylene; wherein the conditions of the cleavage reaction include: the temperature is 1200-2000 ℃, the reaction time is 10-70 ms, and the feeding ratio of carrier gas to pyrolysis raw material in unit time is 10-80L/g; the cracking raw material is inferior oil and/or catalytic cracking reaction products.
2. The method of claim 1, the method further comprising: preheating the cracking raw material and the carrier gas, and then feeding the preheated cracking raw material and the carrier gas into the cracking reactor, wherein the temperature of the preheated cracking raw material is 200-500 ℃, and the temperature of the preheated carrier gas is 500-2000 ℃.
3. The method of claim 1, wherein the poor oil is selected from one or more of vacuum residuum, coal tar, and solvent deasphalted oil, and the catalytic cracking reaction product is selected from one or more of catalytic cracking slurry oil, catalytic cracking diesel oil, and catalytic cracking recycle oil;
the carrier gas is selected from one or more of nitrogen, helium, argon, methane and C2-C4 light hydrocarbons.
4. The process of claim 1 wherein the quench medium used for the quench is selected from one or more of water, nitrogen and argon;
the temperature of the reaction product after rapid cooling is 200-500 ℃.
5. The method of claim 1, wherein the cleavage reactor is a metal tubular reactor disposed vertically in an axial direction;
the cracking raw material and carrier gas are introduced into the metal tubular reactor from the top of the metal tubular reactor, the reaction product is led out of the metal tubular reactor from the bottom of the metal tubular reactor, and the quenching medium is introduced into the metal tubular reactor from the lower part of the metal tubular reactor.
6. The method of claim 5, wherein the material of the metal tubular reactor is selected from one or more of tungsten, molybdenum, tantalum, niobium, vanadium, chromium, titanium, zirconium, rare earth boride, rare earth carbide, rare earth nitride, rare earth silicide, rare earth phosphide, and rare earth sulfide, and the rare earth is selected from one or more of lanthanum, cerium, praseodymium, and neodymium.
7. A system suitable for use in the acetylene production process of any of claims 1-6, the system comprising: a pyrolysis reactor, an electromagnetic induction coil, high-frequency electric induction heating equipment and a gas-solid separator;
the cracking reactor is provided with a raw material inlet at the top, a product outlet at the bottom and a quenching medium inlet at the lower part, and the gas-solid separator is provided with a material inlet and a material outlet; the electromagnetic induction coil is wound on the periphery of the cracking reactor, and the high-frequency electric induction heating equipment is connected with the electromagnetic induction coil;
and a product outlet of the cracking reactor is communicated with a material inlet of the gas-solid separator.
8. The system of claim 7, wherein the cracking reactor is a metallic tubular reactor disposed vertically in an axial direction, the metallic tubular reactor being of a material selected from one or more of tungsten, molybdenum, tantalum, niobium, vanadium, chromium, titanium, zirconium, rare earth boride, rare earth carbide, rare earth nitride, rare earth silicide, rare earth phosphide, and rare earth sulfide, the rare earth being selected from one or more of lanthanum, cerium, praseodymium, and neodymium.
9. The system of claim 7, wherein one or more mesh barriers are disposed in the cracking reactor to facilitate cracking of the feedstock.
10. The system of claim 7, wherein the cracking reactor comprises a first expanding section, a reaction section and a second expanding section from top to bottom, wherein the inner diameters of the first expanding section and the second expanding section are larger than the inner diameter of the reaction section, and the electromagnetic induction coil is wound on the periphery of the reaction section.
11. The system of claim 7, further comprising a filter and a gas collector, the material outlet of the gas-solid separator being in communication with the gas collector through the filter.
12. The system of claim 7, further comprising a first preheating furnace provided with a cracking feed inlet and a preheating feed outlet, and a second preheating furnace provided with a carrier gas inlet and a preheating feed outlet, the preheating feed outlet of the first preheating furnace and the preheating feed outlet of the second preheating furnace being in communication with the feed inlet of the cracking reactor.
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