CN109821495B - Multistage reaction device for preparing ethylene and/or acetylene from hydrocarbon and preparation method - Google Patents
Multistage reaction device for preparing ethylene and/or acetylene from hydrocarbon and preparation method Download PDFInfo
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- CN109821495B CN109821495B CN201910154812.4A CN201910154812A CN109821495B CN 109821495 B CN109821495 B CN 109821495B CN 201910154812 A CN201910154812 A CN 201910154812A CN 109821495 B CN109821495 B CN 109821495B
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Abstract
Provided is a multistage reaction apparatus for producing ethylene and/or acetylene from hydrocarbons, comprising: the device comprises a first reaction chamber (13) and a second reaction chamber (23), wherein the two reaction chambers are respectively provided with a burner, a common or separated fuel gas inlet, an oxygen inlet and a preheating tube array, a gas distributor is arranged between the two reaction chambers, and the preheating tube arrays in the two reaction chambers are connected with the gas distributor; the cracking raw gas enters a preheating tube array of a first reaction chamber from a cracking raw gas inlet (16) positioned in the first reaction chamber through a gas distributor, is cracked in a fuel gas and oxygen combustion heat carrier region at the other outlet of the preheating tube array, the mixed gas of the cracking product and the uncracked raw gas formed after cracking enters the preheating tube array in a second reaction chamber through the gas distributor between the two reaction chambers, is cracked again in the fuel gas and oxygen combustion heat carrier region at the other outlet of the preheating tube array, and the cracking product is discharged out of the second reaction chamber through a reaction product outlet (26) positioned in the second reaction chamber.
Description
Technical Field
The invention belongs to the technical field of preparation of ethylene and/or acetylene generally, and particularly relates to a multistage reaction device for preparing ethylene and/or acetylene by cracking hydrocarbon and a method for preparing ethylene and/or acetylene by using the multistage reaction device.
Background
Ethylene is one of the chemical products with the largest output in the world, plays a very important role in national economy, is mainly used for producing polyethylene, ethylene propylene rubber, polyvinyl chloride and the like, and is mainly prepared by steam cracking of naphtha, ethane and the like in the industry at present; acetylene is another very important basic chemical raw material, downstream products of the acetylene mainly comprise vinyl chloride, vinyl acetate, 1, 4-butadiene and the like, at present, acetylene is mainly produced by a calcium carbide method in China, and a natural gas partial oxidation method is mainly adopted in foreign natural gas rich areas.
The steam cracking method is to prepare ethylene by thermally cracking a mixture of hydrocarbons and water at high temperature, and has the advantages of high yield and high energy consumption and has a complicated reactor structure; the calcium carbide method is to utilize calcium carbide (calcium carbide CaC)2) Generating acetylene (C) in water2H2) The method for preparing acetylene has the advantages of high product purity, simple and convenient operation and high energy consumption and pollution.
Cracking by steamThe tubular cracking furnace reactor is adopted for ethylene preparation, although the tubular furnace has different types, the tubular furnace structurally comprises a furnace tube, a tube frame, a burner, a furnace wall, a furnace frame and the like, and mainly comprises a convection section and a radiation section. The amplification of the tubular furnace reactor is realized by increasing the number of reaction tubes, so that the reactor has a complex structure. The specific reactor structure can be found in ethylene plant technology and operation, mainly compiled by Wang Song Han et al. The reactor for preparing acetylene by partial oxidation of natural gas is mainly divided into a mixer, a combustion nozzle and a reaction chamber, the amplification of the reactor is realized by increasing the number of the nozzles, and the specific reactor structure can be seen in Peter of BASF company
Acetylene entry written in encyclopedia of Ullmann Industrial Chemicals (DOI:10.1002/14356007.a 01-097. pub 4).
There are some reports on the use of fuel gas fuel as a heat carrier to directly mix with hydrocarbons for cracking. CN01145130.0 discloses an apparatus for producing ethylene by cracking a supersonic heat carrier and hydrocarbons after they are mixed rapidly; US2941021 uses a rotary reactant injection method, in which a stirring action is added during the mixing of the heat carrier and the reactant to achieve the purpose of enhancing mixing; US4256565, by means of injecting the hydrocarbon to be cracked in the vicinity of the fuel nozzle, achieves a rapid mixing of the heat carrier generated by combustion with the hydrocarbon. These patents all mix the heat carrier directly with the hydrocarbons in one step, resulting in low cracking rate and low yield of the raw hydrocarbon gas.
Disclosure of Invention
The invention provides a multistage reaction device for producing ethylene and/or acetylene from low-carbon alkane, aiming at the defects of the prior art, the reaction device is provided with two independent heat carrier areas, so that the mixed gas of a cracking product of raw material gas subjected to first cracking in the first heat carrier area and the raw material gas not subjected to cracking enters the second heat carrier area to be cracked again, the cracking reaction of the raw material gas in the two heat carrier areas can be realized, the yield of the ethylene and/or acetylene is obviously improved, the device has the advantages of simple structure, no amplification effect arrangement, uniform mixing of the heat carrier and the reaction materials, high yield and selectivity of the ethylene and/or acetylene and the like.
According to an aspect of the present invention, there is provided a multi-stage reaction apparatus for producing ethylene and/or acetylene from hydrocarbons, comprising a first reaction chamber, a second reaction chamber, and a first gas distributor disposed between the first reaction chamber and the second reaction chamber; the wall of each of the first reaction chamber and the second reaction chamber is provided with a burner, a common or separate fuel gas inlet and an oxygen inlet, the wall of the first reaction chamber is also provided with a cracking feed gas inlet for cracking feed gas to enter the first reaction chamber, the first reaction chamber is used for cracking reaction of the cracking feed gas therein, and the second reaction chamber is used for cracking reaction of the unreacted cracking feed gas therein; the first gas distributor is provided with a first passage communicated with the cracking raw gas inlet and the first reaction chamber and used for enabling the cracking raw gas to be uniformly distributed on the section of the first reaction chamber, and a second passage communicated with the first reaction chamber and the second reaction chamber and used for introducing mixed gas containing unreacted cracking raw gas into the second reaction chamber to further perform cracking reaction; and a reaction product outlet is formed in the wall of the second reaction chamber and used for discharging the cracking product out of the second reaction chamber.
The multistage reaction device for preparing ethylene and/or acetylene from hydrocarbon comprises two reaction chambers which are communicated through a second passage of a first gas distributor, wherein the two reaction chambers are respectively provided with a burner, a common or separated fuel gas inlet and an oxygen inlet, fuel gas and oxygen are respectively introduced into the two reaction chambers, independent heat carrier areas can be formed after the burners are ignited, and the temperature of the heat carrier areas is up to 2200-2800 ℃ so as to crack raw material hydrocarbon gas or mixed gas which is formed after primary cracking and comprises cracked products and uncracked products. The cracking raw material gas enters from a cracking raw material gas inlet, enters a first reaction chamber through a first passage of a first gas distributor, is subjected to high-temperature thermal cracking in a heat carrier area in the first reaction chamber to form a mixed gas of partial cracking products (ethylene and/or acetylene) and the raw material gas which is not cracked, the mixed gas is dispersed in the first reaction chamber, enters a second reaction chamber through a second passage on the gas distributor, is subjected to thermal cracking again in the heat carrier area in the second reaction chamber, and then is discharged out of the reaction chamber through a reaction product outlet on the wall of the second reaction chamber. It can be seen that the raw material cracking raw material gas is cracked in the heat carrier region of the first reaction chamber through the first gas distributor and then continuously enters the heat carrier region of the second reaction chamber for re-cracking, i.e. the high-temperature heat carrier is mixed with hydrocarbons step by step for cracking through the design of the reaction chambers, and the average temperature of the reaction is reduced by adding the heat carriers step by step (in a single reaction chamber device with one-step addition of the heat carrier, the cracking raw material gas is subjected to cracking reaction at the temperature of 1100-1400 ℃, while in a multi-stage reaction chamber device with step-by-step addition of the heat carrier, the cracking raw material gas is subjected to cracking reaction at the temperature of 900-1200 ℃), the production of byproducts is reduced, the selectivity of the target product is improved, and the yield of the product is obviously improved.
Further, as an example, the first passage is a plurality of first through holes on the first gas distributor, and the second passage is a plurality of second through holes on the first gas distributor; the first through hole is connected with the cracking raw material gas inlet and the first reaction chamber, so that the cracking raw material gas enters the cracking raw material gas inlet and then enters the first reaction chamber through the first through hole; the second through hole is connected with the first reaction chamber and the second reaction chamber, so that mixed gas formed after cracking of the cracking feed gas in the first reaction chamber enters the second reaction chamber through the second through hole.
The first passage and the second passage are designed into a plurality of through holes, so that cracking raw material gas passing through the first passage, uncracked raw material gas passing through the second passage and cracking products can enter the first reaction chamber and the second reaction chamber through the independent through holes, gas is dispersed or uniformly distributed, a plurality of reaction points can be formed in heat carrier areas in the respective reaction chambers, the cracking reaction areas are prevented from being too concentrated, and the reaction process is insufficient.
Further, as an example, the multistage reaction apparatus for producing ethylene and/or acetylene from hydrocarbons further includes: the gas distributor comprises a first gas distributor, a second gas distributor, a gas collecting chamber baffle and a gas collecting chamber, wherein a gas collecting chamber is formed between the gas collecting chamber baffle and the second gas distributor; one end of the communicating tube is connected with the second through hole of the first gas distributor, and the other end of the communicating tube is connected with the through hole on the partition plate of the gas collection chamber, so that the first reaction chamber and the gas collection chamber are communicated; and the second gas distributor is provided with a through hole for communicating the gas collection chamber and the second reaction chamber, so that the mixed gas containing the unreacted cracking raw gas sequentially enters the gas collection chamber through the communicating tube nest and the through hole of the gas collection chamber partition plate and then enters the second reaction chamber from the gas collection chamber through the through hole on the second gas distributor.
As an alternative scheme that the cracked mixed gas in the first reaction chamber directly enters the second reaction chamber through the second through hole of the first gas distributor, the communicating tubes, the gas collection chamber partition plate and the second gas distributor can form a gas collection device between the first distributor and the second reaction chamber, namely the communicating tubes, the gas collection chamber partition plate and the second gas distributor which are sequentially connected, and the other end of the communicating tubes is connected with a gas outlet of the second through hole of the first gas distributor, so that the cracked mixed gas coming out of the gas outlet of the second through hole of the first gas distributor enters the gas collection chamber formed between the gas collection chamber partition plate and the second gas distributor through the communicating tubes and the gas collection chamber partition plate, and then enters the second reaction chamber through the through hole of the second gas distributor after being collected by the gas collection chamber. The advantage of designing gas collecting device lies in can making the schizolysis gaseous mixture that forms after the first reaction chamber schizolysis gather at the plenum chamber, then gets into the second reaction chamber through the second distributor and carries out the second schizolysis, so, can wait to make it get into the second reaction chamber again after the plenum chamber gathers sufficient schizolysis gaseous mixture to reduce the combustion time of fuel gas and oxygen in the second reaction chamber, the energy saving.
Further, be connected with first preheating shell and tube on the gas outlet of first through-hole on the first gas distributor, preheating the shell and tube and being a plurality of both ends open-ended hollow tubes, the gas outlet is connected to hollow tube one end opening, and the other end opening is in the combustion area of fuel gas and oxygen in the first reaction chamber for send into fuel gas and oxygen combustion area after preheating the schizolysis feed gas of first gas distributor equipartition in it, wherein when the schizolysis reaction goes on, the reaction product spreads around the hollow tube, thereby preheats the schizolysis feed gas in the hollow tube.
Furthermore, the device of the invention also comprises a second preheating array pipe arranged in the second reaction chamber, wherein the second preheating array pipe is a plurality of hollow pipes with openings at two ends, one end of each hollow pipe is connected with the second passage of the first gas distributor or the through holes on the second gas distributor through an opening, the other end of each hollow pipe is arranged in a fuel gas and oxygen combustion area in the second reaction chamber through an opening, and the hollow pipes are used for preheating cracking raw material gas or mixed gas uniformly distributed through the second passage of the first gas distributor or the through holes of the second gas distributor and then sending the cracking raw material gas or the mixed gas into the fuel gas and oxygen combustion area, wherein when the cracking reaction is carried out, reaction products are diffused around the hollow pipes, so that the mixed gas in the hollow pipes is preheated.
The gas distributor and the preheating tubes in the multistage reaction device for preparing the ethylene and/or the acetylene from the hydrocarbon are combined, so that the gas distribution and the gas flow direction after cracking raw material gas or mixed gas after cracking enters the reaction chamber are obviously different from those in the traditional device for preparing the ethylene and/or the acetylene from the hydrocarbon by cracking: firstly, the first gas distributor and the first preheating tubes are matched to ensure that the cracking raw material gas entering the first reaction chamber from the cracking raw material gas inlet passes through the first gas distributor and the first preheating tubes and then is dispersed or even uniformly distributed on the cross section of the first reaction chamber; the second gas distributor and the second preheating tubes are matched to ensure that the cracked mixed gas generated in the first reaction chamber is dispersed and even uniformly distributed on the cross section of the second reaction chamber after passing through the second gas distributor and the second preheating tubes, the traditional highly concentrated gas flow taking a gas inlet as a center is avoided, and the cracked raw material gas or the cracked mixed gas is uniformly distributed, so that the gas is uniformly contacted and mixed with a heat carrier, and the subsequent cracking reaction is more sufficient and uniform; the preheating tubes communicated with the gas distributor preheat and uniformly distribute cracking raw gas or cracked mixed gas in a dispersion mode, the cracking raw gas or the cracked mixed gas is kept uniformly distributed and then sprayed out from the hollow tube to enter a heat carrier area formed by combustion of fuel gas and oxygen to carry out cracking reaction, high-temperature cracking products are dispersed around the hollow tube, heat is transferred to the hollow tube and the gas continuously entering the hollow tube, and therefore the gas to be cracked in the hollow tube is preheated.
The invention alleviates or even solves the problem of the amplification effect of the traditional reaction chamber: in the prior art, when a reaction chamber is enlarged, a cracking raw material and a heat carrier are mixed unevenly, so that the reaction effect is poor, and the yield is obviously reduced. The invention adopts the preheating tubes to preheat and uniformly distribute the cracking feed gas, so that the cracking feed gas and the heat carrier are uniformly contacted and mixed, and the yield is not influenced by the amplification of the reaction chamber.
Further, a gas outlet of the first passage on the first gas distributor and a hollow pipe of the first preheating tube nest communicated with the gas outlet are uniformly distributed on the cross section between the two reaction chambers; the gas outlet of the second passage on the first gas distributor, the through holes on the second gas distributor and the hollow tubes of the second preheating tubes communicated with the through holes on the first gas distributor and the second gas distributor are uniformly distributed on the cross section between the two reaction chambers. The gas outlet of the first passage on the first gas distributor and the hollow pipes of the first preheating tubes communicated with the gas outlet are uniformly distributed on the cross sections of the two reaction chambers, so that cracking feed gas uniformly enters the hollow pipes communicated with the gas outlet along the uniformly distributed gas outlet on the cross section of the first reaction chamber and then reaches a heat carrier area in the first reaction chamber, a plurality of uniform cracking reaction points are formed in the heat carrier area, and the generated benefit is that the reaction is more uniform and sufficient; similarly, the gas outlet of the second passage on the first gas distributor, the through hole on the second gas distributor and the hollow pipe of the second preheating tube communicated with the through hole are uniformly distributed on the cross section between the two reaction chambers, so that the cracked mixed gas in the first reaction chamber uniformly enters the hollow pipe communicated with the second reaction chamber along the uniformly distributed gas outlet on the cross section of the second reaction chamber and then reaches the heat carrier area in the second reaction chamber, a plurality of uniform cracking reaction points are formed in the heat carrier area, and the generated benefit is that the cracking is more uniform and sufficient.
Furthermore, the fuel gas inlet and the oxygen inlet in the first reaction chamber and/or the second reaction chamber are the same common inlet, and the fuel gas and the oxygen are premixed and then enter the reaction chambers through the same common inlet.
Preferably, the apparatus, in which the fuel gas inlet and the oxygen inlet are the same common inlet, further comprises a mixer, connected to the common inlet of the fuel gas inlet and the oxygen inlet, for mixing the preheated fuel gas and oxygen respectively and then injecting them into the reaction chamber. In the preferred embodiment, the fuel gas and oxygen share the same inlet, and the premixed pre-heated fuel gas and pre-heated oxygen in the mixer are premixed flames, which premixed pre-heated fuel gas and pre-heated oxygen are then injected into the reaction chamber through the shared inlet to assist in complete combustion of the fuel gas, but in the event of flashback, may occur.
As an alternative to the fuel gas inlet and the oxygen inlet being the same common inlet, the fuel gas inlet and the oxygen inlet in the first reaction chamber and/or the second reaction chamber of the apparatus of the present invention are separate inlets, and the fuel gas and the oxygen gas enter the reaction chamber through the separate fuel gas inlet and the separate oxygen inlet, respectively. The advantage of the separate injection of fuel gas and oxygen into the reaction chamber via separate inlets is that the operation is simple, but the time required for complete combustion is long, resulting in an increase in reactor volume.
Further, the first gas distributor and/or the second gas distributor are plate-shaped; the first through holes on the first gas distributor are uniformly distributed on the whole plate surface of the first gas distributor; or the second through holes are uniformly distributed on the whole plate surface of the first gas distributor at intervals of the first through holes, or the through holes on the second gas distributor are uniformly distributed on the whole plate surface of the second gas distributor, and the gas outlets of the first through holes on the first gas distributor are connected with hollow tubes of the first preheating tubes; and the gas outlet of the second through hole on the first gas distributor or the gas outlet of the through hole on the second gas distributor is connected with a hollow pipe of a second preheating tube nest. The gas distributor can be in various forms, the distributor optimized by the device is in a plate surface shape and is arranged on the cross section of the reaction chamber, the first through holes on the first gas distributor are uniformly distributed on the whole plate surface of the first gas distributor, the first through holes are uniformly distributed on the plate surface, namely, hollow pipes are uniformly distributed on the cross section of the first reaction chamber, namely, cracking feed gas enters through a gas inlet of the first distributor, then exits from a gas outlet through the shortest path and enters into uniformly distributed hollow pipes connected with the gas outlet; if the scheme that the second through holes of the first gas distributor are directly communicated with the second preheating tubes in the second reaction chamber is adopted, the second through holes are evenly distributed on the whole plate surface of the first gas distributor at intervals from the first through holes, namely the first through holes and the second through holes are evenly arranged on the plate surface at intervals or the first through holes and the second through holes are explained as gaps of the first through holes evenly distributed on the plate surface; to the hollow tube scheme that the second through-hole that takes first gas distributor connects gradually UNICOM tubulation, plenum chamber baffle, second gas distributor and second and preheats the tubulation, through-hole evenly distributed is on the whole face of second gas distributor on the second gas distributor, and the benefit of above-mentioned arranging is: all there is the hollow tube in each region on first reaction chamber and the second reaction chamber cross section, and the schizolysis feed gas in the hollow tube or the mixed gas after the schizolysis are heated, and form the schizolysis reaction point in each region on the reaction chamber cross section, do not have the schizolysis reaction dead angle in the reaction chamber, do not have the too concentrated situation that leads to the reaction of insufficiency of splitting reaction.
Furthermore, the shape of the through holes on the first gas distributor, the communicating tube nest, the gas collection chamber partition plate and the second gas distributor is one of circular, square, triangular and pentagonal, and the cross section of the hollow tube of the preheating tube nest is one of circular, square and triangular. The diameter of the hollow tube is preferably in the range of 5mm to 60 mm.
Further, the common or separate fuel gas inlet and oxygen inlet are uniformly distributed at the top or bottom of the reaction chamber, so that the fuel gas and the oxygen form a plurality of heat carrier areas on the cross section of the reaction chamber.
Furthermore, each hollow pipe is provided with a retraction which plays the roles of gas uniform distribution and pressure regulation. Preferably, the setback is in a position close to the gas distributor, which is more advantageous for the process.
It can be seen that the working process of the device of the invention is as follows:
in the first reaction chamber, fuel gas and oxygen are sprayed into the first reaction chamber through a common or separated fuel gas inlet and an oxygen inlet, and are ignited by a burner to form a heat carrier region around a combustion point; meanwhile, the cracking raw material gas is sent into a gas inlet of a first through hole in a first gas distributor from a cracking raw material gas inlet, then enters a hollow pipe of a first preheating row pipe from a gas outlet of the first through hole in the first gas distributor, flows along the inside of the hollow pipe under the impact of the continuously introduced cracking raw material gas flow, is heated by a high-temperature cracking product when flowing in the hollow pipe, and enters a heat carrier area formed by combustion of fuel gas and oxygen when being sprayed out from the other port of the hollow pipe, the cracking raw material gas is subjected to thermal cracking to form cracking products such as alkyne and alkene, the cracking product is diffused in the area around the hollow pipe, and the high temperature of the cracking product enables the hollow pipe and the cracking raw material gas continuously entering the hollow pipe to be continuously heated.
In the second reaction chamber, fuel gas and oxygen are sprayed into the second reaction chamber through a common or separated fuel gas inlet and an oxygen inlet, and are ignited by a burner to form a heat carrier area around a combustion point, meanwhile, mixed gas formed by diffused cracking products and uncracked products is discharged out of the first reaction chamber through a second through hole on a first gas distributor, or directly enters a hollow pipe of a second preheating tube array connected with the second through hole on the first gas distributor, or sequentially enters a gas collection chamber through a second through hole gas outlet, a communication tube array and a gas collection chamber partition plate through hole on the first gas distributor, enters a second preheating tube array connected with the through hole through a second gas distributor through hole after being enriched, flows along the inside of the hollow pipe under the impact of continuously introduced cracked mixed gas flow, and is heated by high-temperature cracking products when flowing in the hollow pipe, when the gas is sprayed out from the other port of the hollow tube, the gas enters a heat carrier area formed by combustion of fuel gas and oxygen, the uncracked raw gas in the mixed gas after the first cracking is subjected to thermal cracking again to form cracking products of alkyne, alkene and the like, the cracking products are spread in the area around the hollow tube, the high temperature of the cracking products enables the hollow tube and the mixed gas continuously entering the hollow tube to be continuously heated, and finally the cracking products are discharged out of the reaction chamber from a reaction product outlet of the second reaction chamber. Therefore, the cracking raw gas is subjected to a first cracking reaction in the first reaction chamber, and then the cracking product and the uncracked cracking raw gas are discharged into the second reaction chamber, so that the uncracked cracking raw gas is subjected to a cracking reaction; the gas distributors in the two reaction chambers are combined with the preheating tubes to uniformly distribute gas in the hollow tubes of the preheating tubes, the port of each hollow tube is sprayed by heated raw material gas to be cracked, the sprayed cracking raw material gas is contacted with a heat carrier to form a cracking raw material gas cracking reaction point, so that a plurality of cracking reaction points are formed in the two reaction chambers, the preheating tubes play a role in heating the cracking raw material gas and simultaneously amplify the reaction quantity, namely, a cracking raw material gas channel adopts a plurality of tubes and can uniformly spray the cracking raw material gas into the two reactors to be mixed with the heat carrier, the amplification of the reactors is realized by a quantity amplification method, and the problems of insufficient reaction and yield reduction caused by uneven contact of the cracking raw material gas and the heat carrier during amplification of the traditional reactor can be avoided.
According to another aspect of the present invention, there is provided a method for preparing ethylene and/or acetylene from hydrocarbon using the above multistage reaction apparatus for preparing ethylene and/or acetylene from hydrocarbon, comprising the steps of:
a) spraying fuel gas and oxygen into the first reaction chamber through a common or separated fuel gas inlet and an oxygen inlet; starting a burner in the first reaction chamber to combust fuel gas and oxygen entering the first reaction chamber to generate a high-temperature heat carrier;
b) introducing cracking raw gas into a first reaction chamber from a cracking raw gas inlet, wherein the cracking raw gas uniformly distributes the cracking raw gas from the cracking raw gas inlet through a first passage of a first gas distributor, then enters the first reaction chamber, enters a heat carrier area and is thermally cracked;
c) spraying fuel gas and oxygen into the second reaction chamber through a common or separated fuel gas inlet and an oxygen inlet; starting a burner in the second reaction chamber to combust the fuel gas and the oxygen entering the second reaction chamber to generate a high-temperature heat carrier;
d) introducing the mixed gas containing the unreacted cracking feed gas into a second reaction chamber through a second passage of the first distributor, and further carrying out cracking reaction;
e) and the cracked product is discharged through a reaction product outlet on the wall of the second reaction chamber.
Further, in the step b): the cracking raw material gas enters the first gas distributor through a gas inlet of the first through hole in the first gas distributor, then enters the hollow pipe of the first preheating tube nest from a gas outlet of the first through hole in the gas distributor, is preheated by the hollow pipe and then is sprayed out from the other port of the hollow pipe, enters a heat carrier area and is thermally cracked; the thermal cracking products are filled in the area around the hollow tubes of the first preheating tubes, and heat is transferred to the hollow tubes and the cracking raw gas continuously introduced into the hollow tubes.
Further, in the step d): the mixed gas formed by the thermal cracking product and the uncracked raw material gas in the first reaction chamber diffuses, is discharged from the second through hole in the first gas distributor out of the first reaction chamber, directly enters the hollow tube of the second preheating tube array of the second reaction chamber from the gas outlet of the second through hole in the first gas distributor, or passes through the through hole in the partition plate of the gas collection chamber through the communicating tube array connected with the gas outlet of the second through hole in the first gas distributor, enters the gas collection chamber after being uniformly distributed by the second gas distributor, enters the hollow tube of the second preheating tube array of the second reaction chamber, is preheated by the hollow tube of the second preheating tube array, is sprayed out from the other port of the hollow tube, enters the heat carrier area of the second reaction chamber, and is thermally cracked.
Further, the step a) may be preceded by the step of preheating fuel gas and oxygen, respectively, and then mixing the fuel gas and the oxygen, wherein the temperature at which the fuel gas and the oxygen are preheated is in the range of 30 ℃ to 600 ℃. The preheating temperature of the fuel gas and the oxygen is improved, the stability of fuel combustion is facilitated, and more heat is provided for the subsequent cracking of the cracking raw material gas.
Further, the mass ratio of the input amount of the cracking raw gas from the cracking raw gas inlet in the step b) to the sum of the fuel gas and the oxygen sprayed in the step a) is as follows: 0.5 to 1.6. The mass ratio of the gas hydrocarbon to the sum of the fuel gas and the oxygen is reduced, so that the thermal cracking temperature is improved, and the acetylene yield is improved; increasing the mass ratio lowers the thermal cracking temperature and is beneficial to the production of ethylene.
Further, the fuel gas in the step a) is one or a mixture of hydrogen, carbon monoxide, methane and ethane; the cracking raw material gas in the step b) is one or a mixture of methane, ethane and propane.
Further, the cracking raw material gas in the steps b) and d) enters a heat carrier area for cracking after being preheated to the temperature of 200-600 ℃ in the hollow pipe. The initial preheating temperature of the cracking feed gas is improved, the heat required by cracking the cracking feed gas is favorably reduced, and the yields of ethylene and acetylene are improved.
Compared with the prior art, the invention has the following advantages:
1) the device provided by the invention is designed by two reaction chambers, the high-temperature heat carrier is mixed with hydrocarbons step by step to carry out cracking, and the heat carrier is added step by step, so that the average temperature of reaction is reduced, the production of byproducts is reduced, and the selectivity of a target product is improved.
2) The device of the invention utilizes the combination of a gas distributor and a preheating tube nest, changes the direction of cracking feed gas entering a heat carrier area from traditional inclined spraying into vertical spraying, and enables the cracking feed gas flow to be evenly distributed in the whole cross section area of a reaction chamber; the cracking feed gas channel adopts the form of a plurality of hollow tube pipes, firstly, the cracking feed gas can be preheated by the high-temperature heat of the heat carrier and the cracking products before being sprayed into the heat carrier area, secondly, the cracking feed gas is uniformly sprayed into the heat carrier area through the hollow tubes connected with the gas distributor to be mixed with the heat carrier, and cracking is carried out.
Drawings
These and/or other aspects and advantages of the present invention will become more apparent and more readily appreciated from the following detailed description of the embodiments of the invention, taken in conjunction with the accompanying drawings of which:
FIG. 1 is a schematic structural diagram of a multistage reaction apparatus for producing ethylene and/or acetylene from hydrocarbons, which includes a gas distributor according to an embodiment of the present invention;
FIG. 2 is a schematic structural diagram of a multistage reaction apparatus for producing ethylene and/or acetylene from hydrocarbons, which includes two gas distributors according to an embodiment of the present invention;
FIG. 3 is a schematic top view of a first stage gas distributor according to an embodiment of the present invention;
FIG. 4 is a schematic top view of a plenum partition in accordance with an embodiment of the invention;
FIG. 5 is a schematic top view of a second stage gas distributor according to an embodiment of the present invention;
wherein: 11. a first burner; 12. a first fuel gas and/or oxygen inlet; 13. a first reaction chamber; 14. a first preheating pipe array; 15. a first gas distributor; 16. a cracking raw gas inlet; 17. is communicated with the tube; 18. a gas collection chamber baffle; 21. a second burner; 22. a second fuel gas and/or oxygen inlet; 23. a second reaction chamber; 24. a second array of tubes; 25. a second gas distributor; 26. an outlet of the reactor; 150. a first through hole of the first gas distributor 15; 151. a second through hole of the first gas distributor 15; 181. through holes in the plenum partition 18; 251. through holes in the second gas distributor 25.
Detailed Description
In order that those skilled in the art will better understand the present invention, the following detailed description of the invention is provided in conjunction with the accompanying drawings and the detailed description of the invention.
It should be noted that in the present invention, "the wall of the reaction chamber" includes the top, bottom and side walls of the reaction chamber, and "the upper portion of the reaction chamber" and "the lower portion of the reaction chamber" are spatially relative to each other, and may include the wall and the inner space.
The "high-temperature heat carrier" in the present invention means a heat carrier whose temperature reaches a temperature at which a cracking raw material gas is cracked, and for example, in the case of a cracking raw material gas for producing acetylene from hydrocarbons, the temperature is higher than 900 ℃.
Example 1
A multi-stage reaction device for preparing ethylene and/or acetylene from hydrocarbon is shown in a structural cross-sectional view in figure 1, and comprises a first reaction chamber 13 and a second reaction chamber 23, wherein the wall of the first reaction chamber 13 is provided with a first burner 11, a first common or separated fuel gas inlet and an oxygen inlet 12 (in the figure, the common situation is the case of common situation), a cracking raw material gas inlet 16, and a first preheating tube array 14 is arranged inside; the wall of the second reaction chamber 23 is provided with a second burner 21, a second common or separate fuel gas inlet and oxygen inlet 22 (in the figure, common situation), a reaction product outlet 26, and a second preheating tube array 24 inside; a first gas distributor 15 arranged between the first reaction chamber 13 and the second reaction chamber 23, wherein the first reaction chamber 13 is a cavity structure in which reaction raw materials are reacted as can be seen from FIG. 1; the first fuel gas inlet and the oxygen inlet 12 are provided at the top of the reaction chamber 13 for introducing fuel gas and oxygen into the first reaction chamber 13, and the first fuel gas inlet and the oxygen inlet 12 may be provided in such a manner that the first fuel gas inlet and the oxygen inlet 12 share one inlet, in this common inlet scheme, the apparatus of this embodiment may further include a mixer connected to the front end of the common inlet at the front end of the common inlet, so that the fuel gas and oxygen, which are respectively preheated, are rapidly mixed in the mixer and then injected into the first reaction chamber 13 through the common inlet, and the other is that the first fuel gas and oxygen are respectively introduced into the first reaction chamber 13 through respective independent inlets, and the common inlet or the independent inlets in both schemes are preferably provided at the top or the bottom of the reaction chamber 13 (when the first reaction chamber 13 is located at the upper end of the second reaction chamber 23, the fuel gas and/or oxygen inlet of the first reaction chamber 13 is provided at the top of the first reaction chamber 13, correspondingly, the fuel gas and/or oxygen inlet of the second reaction chamber 23 is at the bottom of the second reaction chamber 23; conversely, when the first reaction chamber 13 is located at the lower end of the second reaction chamber 23, the fuel gas and/or oxygen inlet of the first reaction chamber 13 is at the bottom of the first reaction chamber 13, correspondingly, the fuel gas and/or oxygen inlet of the second reaction chamber 23 is at the top of the second reaction chamber 23), and the inlets are uniformly arranged on the top or bottom wall to form a plurality of ignited combustion zones on the cross section of the reaction chamber, and finally a plurality of heat carrier areas are formed; the first burner 11 is used for igniting fuel gas and oxygen and is also arranged near a common or separated fuel gas inlet and an oxygen inlet on the wall of the reaction chamber; it can be seen that the arrangement of the second burner 21, the second common or separate fuel gas inlet and oxygen inlet 22 on the wall of the second reaction chamber 23 mirrors the arrangement of the first burner 11, the first common or separate fuel gas inlet and oxygen inlet 12 in the first reaction chamber 13; a cracking raw material gas inlet 16 for cracking raw material hydrocarbon to enter the first reaction chamber 13 and arranged on the wall of the first reaction chamber 13; the reaction product outlet 26 is used for discharging the cracking product out of the second reaction chamber 23 and is arranged on the side wall of the middle part of the second reaction chamber 23; the first gas distributor 15 has a first passage communicating the cracking raw gas inlet 16 and the first reaction chamber 13, and a second passage communicating the first reaction chamber 13 and the second reaction chamber 23, the preferred structure of the first gas distributor 15 is a plate arranged on the cross section between the first reaction chamber 13 and the second reaction chamber 23, as shown in fig. 3, the first passage is a plurality of first through holes 150 uniformly distributed on the plate surface, the second passage is a plurality of second through holes 151 uniformly distributed on the plate surface, the first through holes 150 and the second through holes 151 are uniformly spaced on the plate surface, the first preheating tubes 14 and the second preheating tubes 24 are both composed of a plurality of fuel gas with openings at two ends, one end of the hollow tube of the first preheating tube 14 is connected with the first through holes 150 in the first reaction chamber 13, and the other end is close to or enters the heat carrier region formed by the first burner 11 for ignition and oxygen; one end of a hollow pipe of the second preheating pipe array 24 is connected with a second through hole 151 in the second reaction chamber 23, and the other end of the hollow pipe is close to or enters a heat carrier area formed by igniting fuel gas and oxygen by the second burner 21; thus, the cracking raw material gas entering from the cracking raw material gas inlet 16 is uniformly distributed on the cross section of the first reaction chamber 13 through the first through holes 150 of the gas distributor 15, and then enters each hollow tube of the first preheating shell and tube 14; in the reaction process, the hollow tube is surrounded by the high-temperature cracking product, so that the hollow tube and the cracking raw material gas in the hollow tube are continuously heated by the heat of the cracking product, and the preheated cracking raw material gas is sprayed out from the other end of the hollow tube and is directly contacted with a heat carrier formed by combustion of fuel gas and oxygen to carry out thermal cracking; the mixture of cracked products and uncracked products formed by thermal cracking is spread around the hollow tubes of the first preheating tubes 14, and enters the hollow tubes of the second preheating tubes 24 in the second reaction chamber 23 through the second through holes 151, and similarly, the hollow tubes are surrounded by the high-temperature cracked products, so that the hollow tubes and the mixed gas inside the hollow tubes are continuously heated by the heat of the cracked products, the preheated mixed gas is ejected from the other end of the hollow tubes and directly contacts with a heat carrier formed by combustion of fuel gas and oxygen to carry out thermal cracking again, and the cracked products are discharged out of the second reaction chamber 23 through the reaction product outlet 26. The scheme of the embodiment can be changed as follows: 1) the shapes of the first through hole 150 and the second through hole 151 are one of circular, square, triangular and pentagonal, the cross section of the hollow tube is one of circular, square and triangular, the gas outlet of the first through hole 150 and/or the second through hole 151 can be directly matched with the hollow tube or connected and matched through a shape adapter, and when the cross section of the hollow tube is circular, the diameter of the hollow tube is within the range of 5 mm-60 mm, so that the cracking feed gas is ensured to form enough gas flow in the hollow tube, the carbon deposition formed by the cracking feed gas in the hollow tube is reduced, and the cracking feed gas is not easy to clean; 2) the preheating time before the cracking raw material gas is mixed with the heat carrier is controlled by setting the length of the hollow tubes of the first preheating tubes 14 and/or the second preheating tubes 24, the preheating temperature of the cracking raw material gas in the hollow tubes is generally within the range of 200-600 ℃, namely, the reaction temperature of the cracking raw material gas during cracking can be controlled to a certain extent by setting the distance between the first preheating tubes 14 and/or the second preheating tubes 24 and a fuel gas and oxygen combustion area; 3) the gas outlets of the first through holes 150 of the first gas distributor 15 and the first preheating tubes 14 connected thereto are disposed at an angle of 70 to 110 ° with respect to the upper and lower bottom surfaces of the first reaction chamber 13, and/or the gas outlets of the first through holes 151 and the second preheating tubes 24 connected thereto are disposed at an angle of 70 to 110 ° with respect to the upper and lower bottom surfaces of the second reaction chamber 23, more preferably 90 °.
Example 2
A multi-stage reaction device structure for preparing ethylene and/or acetylene from hydrocarbon, the component composition and component scheme of which are basically the same as those of the embodiment 1, as shown in figure 2, except that: the device of the embodiment further comprises: a communication tube nest 17, a gas collection chamber partition plate 18 and a second gas distributor 25 which are arranged between the first gas distributor 15 and the second reaction chamber 23, wherein a gas collection chamber is formed between the gas collection chamber partition plate 18 and the second gas distributor 25; the communicating tube array 17 is a hollow tube array with two open ends, one end of the communicating tube array is connected with a gas outlet of the second through hole 151 of the first gas distributor 15, and the other end of the communicating tube array is connected with a through hole 181 on the gas collection chamber partition plate 18, so that the first reaction chamber 13 and the gas collection chamber are communicated; the second gas distributor 25 has through holes 251 to communicate the gas collection chamber with the second preheating tubes 24 in the second reaction chamber 25, so that the mixed gas containing the unreacted cracking raw gas enters the gas collection chamber through the communicating tubes 17 and the through holes 181 of the gas collection chamber partition plate 18 in sequence, and then enters the hollow tubes of the second preheating tubes 24 in the second reaction chamber 23 from the gas collection chamber through the through holes 251 on the second gas distributor 25, and the scheme of the embodiment can be changed as follows: the shape of the through hole on the communicating tube 17 and the air collecting chamber partition plate 18 is one of circular, square, triangular and pentagonal. Compared with the embodiment 1, the device of the embodiment has the advantages that the arrangement of the parts for enriching the mixed gas after the first cracking before entering the second reaction chamber 23 is increased, the combustion time of oxygen and fuel gas is saved, and the energy is saved.
Example 3
A method for producing ethylene and/or acetylene from a hydrocarbon, using the multistage reaction apparatus for producing ethylene and/or acetylene from a hydrocarbon according to embodiment 1 or 2, comprising the steps of:
a) injecting fuel gas and oxygen into a first reaction chamber 13 through a first common or separate fuel gas inlet and oxygen inlet 12; starting a first burner 11 in a first reaction chamber 13 to combust fuel gas and oxygen entering the first reaction chamber 13 to generate a high-temperature heat carrier; preferably, in the embodiment where the fuel gas inlet and the oxygen inlet share a common inlet, the fuel gas and the oxygen may be preheated separately and then rapidly mixed in a mixer preferably provided in the apparatus before being injected into the first reaction chamber 13, and the temperature at which the fuel gas and the oxygen are preheated is in the range of 30 ℃ to 600 ℃ in the operation including preheating the fuel gas and the oxygen; wherein the fuel gas is one or more of hydrogen, carbon monoxide, methane and ethane;
b) cracking raw material gas (selected from one or more of methane, ethane and propane; the preferred introduction amount is: the mass ratio of the total of the fuel gas and the oxygen injected through the first shared or separated fuel gas inlet and the oxygen inlet 12 in the step a) is as follows: 0.5-1.6, controlled by spraying speed and time), and introducing the cracking raw material gas into the first reaction chamber 13 from the cracking raw material gas inlet 16, wherein the cracking raw material gas enters the first gas distributor 15 through the gas inlet of the first through hole 150 on the first gas distributor 15 and then enters the hollow tube of the first preheating tube array 14 from the gas outlet of the first through hole 150 on the gas distributor 15, and the cracking raw material gas is preheated by the hollow tube, sprayed out from the other port of the hollow tube, enters a heat carrier area and is thermally cracked; the thermal cracking products are diffused around the hollow tubes of the first preheating tubes 14, and heat is transferred to the hollow tubes and the cracking raw gas continuously introduced into the hollow tubes;
c) injecting fuel gas and oxygen into a second reaction chamber 23 through a second common or separate fuel gas inlet and oxygen inlet 22; starting a second burner 21 in a second reaction chamber 23, and combusting the fuel gas and the oxygen entering the second reaction chamber 23 to generate a high-temperature heat carrier;
d) and the mixed gas containing the unreacted cracking raw gas is introduced into the second reaction chamber 23 through the second path of the first distributor 15: wherein the mixed gas formed by the thermal cracking product and the un-cracked raw material gas in the first reaction chamber 13 diffuses, is discharged from the second through hole 151 on the first gas distributor 15 out of the first reaction chamber 23, directly enters the hollow tube of the second preheating tube array 24 of the second reaction chamber 23 from the gas outlet of the second through hole 151 on the first gas distributor 15, or passes through the through hole on the partition plate 18 of the gas collection chamber through the communicating tube array 17 connected with the gas outlet of the second through hole 151 on the first gas distributor 15, enters the gas collection chamber, is uniformly distributed by the second gas distributor 25, enters the hollow tube of the second preheating tube array 24 of the second reaction chamber 23, and is preheated by the second preheating tube array 24, then is ejected from the other port of the hollow tube, enters the heat carrier region of the second reaction chamber 23, and is thermally cracked;
e) the pyrolysis product is discharged through a reaction product outlet 26 on the wall of the second reaction chamber, and the pyrolysis feed gas in steps b) and d) is preferably preheated in a hollow tube at a temperature in the range of 200 ℃ to 600 ℃.
Example 4
When the cracking raw material is pure ethane, in a first-stage reactor, when the combined yield of acetylene and ethylene reaches the maximum, the acetylene yield is 21%, the ethylene yield is 44%, the combined yield of acetylene and ethylene is 65%, the CO yield is 23%, the ethane conversion rate is 97%, and the selectivity of acetylene and ethylene is 66%. In the secondary reactor, when the combined yield of acetylene and ethylene reaches the maximum, the operation conditions are that 40% of heat carrier is added into the first-stage reaction chamber, 60% of heat carrier is added into the second-stage reaction chamber, after the first-stage reaction chamber completely reacts, the yield of acetylene is 8%, the yield of ethylene is 38%, the combined yield of acetylene and ethylene is 46%, the yield of CO is 13%, the conversion rate of ethane is 60%, and the selectivity of acetylene and ethylene is 77%. After the reaction in the second-stage reaction chamber was completed, i.e., at the outlet of the reactor, the acetylene yield was 22%, the ethylene yield was 47%, the combined yield of acetylene and ethylene was 70%, the CO yield was 23%, the ethane conversion was 97%, and the acetylene and ethylene selectivity was 72%.
Example 5
When the cracking feedstock was pure methane, the acetylene yield was 45.8%, the CO yield was 32%, the ethane conversion was 78%, and the acetylene selectivity was 59% in the first reactor when the acetylene yield reached the maximum. In the second-stage reactor, when acetylene reaches the maximum, the operation conditions are that 40% of heat carrier is added into the first-stage reaction chamber, 60% of heat carrier is added into the second-stage reaction chamber, and after the first-stage reaction chamber completely reacts, the acetylene yield is 43%, the CO yield is 26%, the methane conversion rate is 55%, and the acetylene selectivity is 77%. After the reaction in the secondary reaction chamber was completed, i.e., at the reactor outlet, the acetylene yield was 51%, the CO yield was 29%, the ethane conversion was 80%, and the acetylene and ethylene selectivity was 64%.
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (22)
1. A multi-stage reaction device for producing ethylene and/or acetylene from hydrocarbon, characterized in that it comprises a first reaction chamber (13), a second reaction chamber (23) and a first gas distributor (15) arranged between the first reaction chamber and the second reaction chamber;
the walls of the first reaction chamber (13) and the second reaction chamber (23) are respectively provided with a burner, a common or separated fuel gas inlet and an oxygen inlet, the wall of the first reaction chamber (13) is also provided with a cracking raw material gas inlet (16) for cracking raw material gas to enter the first reaction chamber (13), the cracking raw material gas is supplied to the first reaction chamber (13) for cracking reaction, and the unreacted cracking raw material gas is supplied to the second reaction chamber (23) for cracking reaction;
the first gas distributor (15) is provided with a first passage communicated with a cracking raw gas inlet (16) and the first reaction chamber (13) and is used for uniformly distributing the cracking raw gas on the section of the first reaction chamber; the device is also provided with a second passage which is communicated with the first reaction chamber (13) and the second reaction chamber (23) and is used for introducing mixed gas containing unreacted cracking raw gas into the second reaction chamber (23) to further carry out cracking reaction;
the wall of the second reaction chamber (23) is provided with a reaction product outlet (26) for discharging the pyrolysis product out of the second reaction chamber (23).
2. The multistage reaction device for producing ethylene and/or acetylene from hydrocarbons according to claim 1, wherein the first passage is a plurality of first through holes (150) on the first gas distributor (15), and the second passage is a plurality of second through holes (151) on the first gas distributor (15); the first through hole (150) is connected with the cracking raw material gas inlet (16) and the first reaction chamber (13), so that the cracking raw material gas enters the cracking raw material gas inlet (16) and then enters the first reaction chamber (13) through the first through hole (150); the second through hole (151) is connected with the first reaction chamber (13) and the second reaction chamber (23), so that mixed gas formed after cracking of the cracking raw gas in the first reaction chamber (13) enters the second reaction chamber (23) through the second through hole (151).
3. The multi-stage reaction apparatus for producing ethylene and/or acetylene from hydrocarbons according to claim 2, further comprising:
a communication tube nest (17), a gas collection chamber partition plate (18) and a second gas distributor (25) which are arranged between the first gas distributor (15) and the second reaction chamber (23), wherein a gas collection chamber is formed between the gas collection chamber partition plate (18) and the second gas distributor (25);
one end of the communicating tube (17) is connected with the second through hole (151) of the first gas distributor (15), and the other end of the communicating tube is connected with the through hole on the gas collection chamber partition plate (18), so that the first reaction chamber (13) and the gas collection chamber are communicated; the second gas distributor (25) is provided with a through hole (251) which is communicated with the gas collection chamber and the second reaction chamber (23), so that the mixed gas containing the unreacted cracking raw gas enters the gas collection chamber through the communicating tube array (17) and the through hole of the gas collection chamber partition plate (18) in sequence, and then enters the second reaction chamber (23) from the gas collection chamber through the through hole (251) on the second gas distributor (25).
4. The multistage reaction device for producing ethylene and/or acetylene from hydrocarbon according to claim 2 or 3, wherein the first gas distributor (15) is connected with a first preheating array tube (14) at the gas outlet of the first through holes (150), the first preheating array tube (14) is a plurality of hollow tubes with two open ends, one end of each hollow tube is open and connected with the gas outlet, and the other end of each hollow tube is open and located in the combustion area of fuel gas and oxygen in the first reaction chamber (13) and used for preheating the cracking raw material gas uniformly distributed by the first gas distributor (15) in the hollow tubes and then sending the cracking raw material gas into the combustion area of fuel gas and oxygen, wherein when the cracking reaction is carried out, the reaction products are spread around the hollow tubes, so that the cracking raw material gas in the hollow tubes is preheated.
5. The multi-stage reaction device for producing ethylene and/or acetylene from hydrocarbons according to claim 4, further comprising a second preheating pipe array (24) in the second reaction chamber (23), the second preheating tubes (24) are hollow tubes with two open ends, one end of each hollow tube is open and connected with a second passage of the first gas distributor (15) or a through hole (251) of the second gas distributor (25), the other end of each hollow tube is open and positioned in a combustion area of fuel gas and oxygen in the second reaction chamber (23), used for preheating cracked mixed gas uniformly distributed by a second passage of the first gas distributor (15) or through holes (251) of the second gas distributor (25) in the mixed gas, and then sending the preheated mixed gas into a fuel gas and oxygen combustion area, wherein, when the cracking reaction is carried out, the reaction product is spread around the hollow tube, thereby preheating the cracking raw material gas or the mixed gas in the hollow tube.
6. The multistage reaction device for producing ethylene and/or acetylene from hydrocarbons according to claim 5, wherein the gas outlet of the first passage on the first gas distributor (15) and the hollow tube of the first preheating shell and tube (14) communicated with the first passage are uniformly distributed on the cross section of the reaction device; the gas outlet of the second passage on the first gas distributor (15), the through hole (251) on the second gas distributor (25) and the hollow pipe of the second preheating tube nest (24) communicated with the through hole and the through hole are uniformly distributed on the cross section of the reaction device.
7. The multistage reaction apparatus for producing ethylene and/or acetylene from hydrocarbons according to claim 5, wherein the fuel gas inlet and the oxygen inlet in the first reaction chamber (13) and/or the second reaction chamber (23) are the same common inlet, and the fuel gas and the oxygen are premixed and then enter the reaction chambers through the same common inlet.
8. The multi-stage reaction device for producing ethylene and/or acetylene from hydrocarbons according to claim 7, further comprising a mixer connected to a common inlet of the fuel gas inlet and the oxygen inlet for mixing the fuel gas and the oxygen, which are preheated, respectively, and then injecting the mixed fuel gas and oxygen into the reaction chamber.
9. The multistage reaction device for producing ethylene and/or acetylene from hydrocarbons according to claim 5, wherein the fuel gas inlet and the oxygen inlet in the first reaction chamber (13) and/or the second reaction chamber (23) are independent inlets, and the fuel gas and the oxygen form a non-premixed flame through the fuel gas inlet and the oxygen inlet, respectively, and enter the reaction chambers.
10. The multistage reaction apparatus for producing ethylene and/or acetylene from hydrocarbons according to claim 5, wherein the first gas distributor (15) and the second gas distributor (25) have a plate shape; the first through holes (150) on the first gas distributor (15) are uniformly distributed on the whole plate surface of the first gas distributor (15); or the second through holes (151) are uniformly distributed on the whole plate surface of the first gas distributor (15) at intervals of the first through holes (150), or the through holes (251) on the second gas distributor (25) are uniformly distributed on the whole plate surface of the second gas distributor (25), and the gas outlets of the first through holes (150) on the first gas distributor (15) are connected with hollow pipes of the first preheating tubes (14); and the gas outlet of the second through hole (151) on the first gas distributor (15) or the gas outlet of the through hole (251) on the second gas distributor (25) is connected with a hollow pipe of a second preheating array pipe (24).
11. The multistage reaction device for producing ethylene and/or acetylene from hydrocarbons according to claim 5, wherein the shape of the through holes of the first gas distributor (15), the communicating tubes (17), the plenum partition (18) and the second gas distributor (25) is one of circular, oval, square, rectangular, triangular, pentagonal and hexagonal, and the cross-sectional shape of the hollow tubes of the preheating tubes is one of circular, oval, square, rectangular and triangular.
12. The multistage reaction apparatus for producing ethylene and/or acetylene from hydrocarbon according to claim 5, wherein the hollow tube has a circular cross section and a diameter of 5mm to 60 mm.
13. The multi-stage reaction device for producing ethylene and/or acetylene from hydrocarbon according to claim 5, wherein the common or separate fuel gas inlet and oxygen inlet are uniformly distributed at the top or bottom of the reaction chamber, so that the fuel gas and oxygen form a plurality of heat carrier areas on the cross section of the reaction chamber.
14. The multi-stage reaction apparatus for producing ethylene and/or acetylene from hydrocarbon according to claim 5, wherein each hollow tube is provided with a setback for uniform distribution of gas and adjustment of pressure.
15. The multi-stage reaction apparatus for producing ethylene and/or acetylene from hydrocarbons according to claim 14, wherein the setback is located near the gas distributor.
16. A method for producing ethylene and/or acetylene from hydrocarbons, which comprises the following operations, using the multi-stage reaction apparatus for producing ethylene and/or acetylene from hydrocarbons according to any one of claims 1 to 15:
a) injecting fuel gas and oxygen into the first reaction chamber (13) through a first common or separate fuel gas inlet and oxygen inlet; starting a first burner (11) in a first reaction chamber (13) to combust fuel gas and oxygen entering the first reaction chamber (13) to generate a high-temperature heat carrier;
b) introducing cracking raw gas into a first reaction chamber (13) from a cracking raw gas inlet (16), wherein the cracking raw gas uniformly distributes by a first gas distributor from the cracking raw gas inlet (16) through a first passage of the first gas distributor (15), enters the first reaction chamber (13), enters a heat carrier area and is thermally cracked;
c) injecting fuel gas and oxygen into a second reaction chamber (23) through a second common or separate fuel gas inlet and oxygen inlet; starting a second burner (21) in the second reaction chamber (23) to combust fuel gas and oxygen entering the second reaction chamber (23) to generate a high-temperature heat carrier;
d) the mixed gas containing the unreacted cracking feed gas is introduced into a second reaction chamber (23) through a second passage of the first gas distributor (15) to further carry out cracking reaction;
e) the cleavage product is discharged through a reaction product outlet (26) in the wall of the second reaction chamber (23).
17. The method of producing ethylene and/or acetylene from hydrocarbons according to claim 16, wherein in step b):
cracking raw gas enters the first gas distributor (15) through a gas inlet of a first through hole (150) in the first gas distributor (15), then enters hollow tubes of the first preheating tubes (14) from a gas outlet of the first through hole (150) in the first gas distributor (15), is preheated by the hollow tubes and then is sprayed out from the other end of the hollow tubes, enters a heat carrier area and is thermally cracked;
the thermal cracking products are filled in the area around the hollow tubes of the first preheating tubes (14) to transfer heat to the hollow tubes and the cracking raw gas continuously introduced into the hollow tubes.
18. The method of producing ethylene and/or acetylene from hydrocarbons according to claim 16, wherein in step d):
the mixed gas formed by the thermal cracking product and the uncracked raw material gas in the first reaction chamber (13) diffuses, the mixed gas is discharged from the second through hole (151) on the first gas distributor (15) out of the first reaction chamber (13), the gas from the gas outlet of the second through hole (151) on the first gas distributor (15) directly enters the hollow pipe of the second preheating tube array (24) of the second reaction chamber (23), or the mixed gas passes through the through hole on the gas collection chamber partition plate (18) through the communicating tube array (17) connected with the gas outlet of the second through hole (151) on the first gas distributor (15) and enters the gas collection chamber after being uniformly distributed by the second gas distributor (25) and then enters the hollow pipe of the second preheating tube array (24) of the second reaction chamber (23), the mixed gas is preheated by the hollow pipe (24) and then is sprayed out from the other port of the hollow pipe and enters the heat carrier region of the second reaction chamber (23), is thermally cracked.
19. The method of producing ethylene and/or acetylene from hydrocarbons according to claim 16, further comprising the step of preheating fuel gas and oxygen separately and then mixing the fuel gas and oxygen before the step a), wherein the temperature at which the fuel gas and oxygen are preheated is in the range of 30 ℃ to 600 ℃.
20. The method for producing ethylene and/or acetylene from hydrocarbons according to claim 16, wherein the mass ratio of the input amount of the cracking raw material gas from the cracking raw material gas input (16) in the step b) to the sum of the injected fuel gas and oxygen in the step a) is: 0.5 to 1.6.
21. The process of claim 16, wherein the fuel gas in step a) comprises a mixture of one or more of hydrogen, carbon monoxide, methane, ethane, propane; the cracking raw gas in the step b) comprises one or more of methane, ethane and propane.
22. The process for producing ethylene and/or acetylene from hydrocarbons according to claim 16, wherein the raw cracking gas in steps b) and d) enters the heat carrier zone for cracking after being preheated in the hollow tube to a temperature in the range of 200 ℃ to 600 ℃.
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