CN108017492B - Method for preparing aromatic hydrocarbon by aromatization of mixed light hydrocarbon - Google Patents
Method for preparing aromatic hydrocarbon by aromatization of mixed light hydrocarbon Download PDFInfo
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Abstract
The invention relates to a method for preparing aromatic hydrocarbon by mixed light hydrocarbon aromatization, which mainly solves the problems that a light hydrocarbon aromatization catalyst is easy to coke and deactivate quickly and the yield of aromatic hydrocarbon is low in the prior art. The invention adopts the following steps: 1) separating the light hydrocarbon raw material into absorption tail gas and absorption liquid in an absorption tower; 2) absorbing tail gas and separating ethylene, hydrogen and fuel gas in an ethylene recovery unit, wherein the ethylene is removed to a light hydrocarbon aromatization reactor; 3) separating the absorption liquid into an aromatization reaction raw material and a heavy component stream in a depentanizer; 4) the heavy component material flow is divided into two material flows, one material flow is used as an absorbent to return to the absorption tower, and the other material flow is used as a first aromatic hydrocarbon material flow product; 5) feeding an aromatization reaction raw material and ethylene into a light hydrocarbon aromatization reactor; 6) cooling the light hydrocarbon aromatization reaction product, and separating the cooled light hydrocarbon aromatization reaction product into a circulating light hydrocarbon and a second aromatic hydrocarbon material flow product in a gas-liquid separator; 7) the technical proposal that the circulating light hydrocarbon returns to the absorption tower better solves the problems and can be used in the industrial production of light hydrocarbon aromatization.
Description
Technical Field
The invention relates to a method for preparing aromatic hydrocarbon by aromatization of mixed light hydrocarbon.
Technical Field
Aromatic hydrocarbons, in particular the light aromatic hydrocarbons BTX (benzene, toluene, xylene), are important basic organic chemicals, second only to ethylene and propylene in terms of yield and scale. Among the aromatic hydrocarbons, para-xylene is a product with high added value. Para-xylene is an important feedstock for the polyester industry, primarily for the production of Purified Terephthalic Acid (PTA) or purified dimethyl terephthalate (DMT), from which Polyester (PET) is produced.
Light aromatics are usually produced by a catalytic reforming and aromatics complex using naphtha as a feedstock. The preparation of the aromatic hydrocarbon by the methanol is a new technical route for preparing the aromatic hydrocarbon by taking coal-based methanol as a raw material. China is rich in coal resources, and the development of a methanol-to-aromatic technology is an important supplement for the preparation of aromatic hydrocarbons by the traditional petrochemical route.
The technology for preparing aromatic hydrocarbon from methanol is a process for producing aromatic hydrocarbon by the steps of dehydrogenation, cyclization and the like under the catalytic action of a bifunctional (acidic and dehydrogenation) active catalyst by taking methanol as a raw material. In the aromatization process, aromatic hydrocarbons such as benzene, toluene and xylene are generated, and by-products comprise hydrocarbons such as methane, ethylene and propylene and hydrogen. Generally, the yield of the carbon-based aromatic hydrocarbon is only about 50%, and the aromatization of byproduct light hydrocarbon has important significance for improving the total aromatic hydrocarbon yield and the overall technical economy of preparing the aromatic hydrocarbon from methanol.
A light hydrocarbon aromatization technology is a new petroleum processing technology developed in recent 20 years and is characterized in that low-molecular hydrocarbons such as liquefied gas, topped oil and the like are directly converted into light aromatic hydrocarbons such as BTX or gasoline and the like by utilizing a modified zeolite molecular sieve catalyst. The ZSM-5 molecular sieve has wide industrial application due to the special shape selectivity, good hydrothermal stability and strong anti-carbon capacity. On the catalyst with ZSM-5 zeolite as main active component, low molecular alkane or olefin can be directly converted into arene, and there is no requirement for arene content in the material. By utilizing the characteristic, a plurality of light hydrocarbon aromatization industrial technologies for directly producing light aromatic hydrocarbons such as BTX and the like or high-octane gasoline blending components by different processes and different raw materials are developed at home and abroad.
The foreign technologies comprise a Cyclar technology, an Alpha technology, a Z-Forming technology, an M2-Forming technology, an Aro-Forming technology and a Zeoforming technology. The domestic technologies comprise the GTA aromatization technology of Luoyang engineering company, the petrochemical aromatization technology of Shikou and the Nano-forming aromatization technology of Daqi science and technology company. The yield of the aromatic hydrocarbon is about 50%, meanwhile, 20-30% of liquefied gas is byproduct, and the components with three or more carbon atoms can be continuously aromatized to further provide the total yield of the aromatic hydrocarbon. The above process does not recycle the carbon three and above components in the liquefied gas, so the yield of the aromatic hydrocarbon is not high.
Patent No. CN101759512A discloses a method for producing aromatic hydrocarbons by using light hydrocarbons with high olefin content. The method aims at the defects of large coking probability, large carbon deposition amount, high catalyst deactivation speed, short one-way period and the like of aromatization reaction of light hydrocarbon raw materials with high olefin content, and provides a method for producing aromatic hydrocarbon by using light hydrocarbon with high olefin content, which comprises the following steps: gasifying high-olefin-content light hydrocarbon subjected to impurity pretreatment at the temperature of 100-109 ℃ through a high-efficiency anti-coking feeding evaporator, then heating the high-olefin-content light hydrocarbon to 450-570 ℃, then feeding the high-olefin-content light hydrocarbon into a composite heating furnace from top to bottom under the driving of circulating return carrier gas, and carrying out aromatization reaction under the action of a catalyst, wherein the reaction temperature is 500-600 ℃, the pressure is 0-0.4 MPa, and the space velocity is 0.4-0.8 h-1. The invention adopts anti-coking technical equipment, novel aromatization catalyst and circulationGas return, etc. to solve the above problems.
Patent No. CN101759515A discloses a method for on-line switching of light hydrocarbon aromatization reaction regeneration. The method comprises two sets of completely same reaction systems, wherein each set of reaction system comprises a feeding vaporizer, a heating furnace and a reactor which are sequentially connected according to a process sequence, reaction products of the two sets of reaction systems enter the same gas-liquid separator after being cooled, the top of the gas-liquid separator is connected with a buffer tank through a gas-phase pipeline, and the buffer tank is respectively connected with the heating furnaces of the two sets of reaction systems; before the reaction system is switched, introducing the circulating dry gas of the gas-liquid separator into a reactor of a system to be switched for preheating and heating to 450-570 ℃, and then switching feeding to finish on-line continuous switching production. The invention leads out dry gas at the top end of the reactant gas-liquid separation tank, shortens the return line and saves the switching time.
Although the total aromatic yield is improved by light hydrocarbon circulation, the hydrogen and the aromatic hydrocarbon are carried in the circulating dry gas, and the components are directly returned to the reactor without being treated, so that the aromatic hydrocarbon yield is low, the catalyst deactivation is accelerated, and the long-term stable operation of the device is influenced.
Therefore, the prior art has the problems of quick catalyst deactivation and low total aromatic hydrocarbon yield, and the invention aims to solve the problems.
Disclosure of Invention
The invention aims to solve the technical problems of quick catalyst deactivation and low total yield of aromatic hydrocarbon in the prior art, and provides a novel method for aromatizing mixed light hydrocarbon. The device has the advantages of long service life of the catalyst and high yield of the aromatic hydrocarbon.
In order to solve the problems, the technical scheme adopted by the invention is as follows: a method for preparing aromatic hydrocarbon by mixed light hydrocarbon aromatization comprises the following steps: 1) separating the light hydrocarbon raw material into absorption tail gas and absorption liquid in an absorption tower; 2) absorbing tail gas and separating ethylene, hydrogen and fuel gas in an ethylene recovery unit, wherein the ethylene is removed to a light hydrocarbon aromatization reactor; 3) separating the absorption liquid into an aromatization reaction raw material and a heavy component stream in a depentanizer; 4) the heavy component material flow is divided into two material flows, one material flow is used as an absorbent to return to the absorption tower, and the other material flow is used as a first aromatic hydrocarbon material flow product; 5) feeding an aromatization reaction raw material and ethylene into a light hydrocarbon aromatization reactor; 6) cooling the light hydrocarbon aromatization reaction product, and separating the cooled light hydrocarbon aromatization reaction product into a circulating light hydrocarbon and a second aromatic hydrocarbon material flow product in a gas-liquid separator; 7) and returning the circulating light hydrocarbon to the absorption tower.
In the technical scheme, the light hydrocarbon raw material comprises hydrogen, methane, ethylene, ethane, propylene, propane, C four, C five, benzene, toluene, xylene and other components.
In the technical scheme, the mass fraction of BTX contained in the absorbent is more than 80%.
In the technical scheme, the operating pressure of the absorption tower is 1.5-2.5 MPA.
In the technical scheme, the operating pressure of the depentanizer is 0.5-0.8 MPA.
In the above technical scheme, the light hydrocarbon aromatization reaction conditions are as follows: the reaction temperature is 500-600 ℃, the reaction pressure is 0.1-0.6 MPA, and the reaction mass airspeed is 0.1-3 HR-1。
In the technical scheme, preferably, the weight ratio of the absorbent material flow to the first aromatic hydrocarbon material flow in the step 4) is 150-50; more preferably, the weight ratio of the absorbent material flow and the first aromatic hydrocarbon material flow in the step 4) is 120-80.
In the technical scheme, the circulating light hydrocarbon enters the absorption tower after being pressurized by the compressor until the pressure is greater than the operating pressure of the absorption tower.
In the technical scheme, after the light hydrocarbon raw material is cooled to the temperature lower than 10 ℃, the light hydrocarbon raw material is subjected to gas-liquid separation operation, a gas phase is sent to an absorption tower, and a liquid phase is sent to a depentanizer.
In the technical scheme, the light hydrocarbon raw material is subjected to membrane separation to remove part of hydrogen and then is sent into an absorption tower.
By adopting the method, the light hydrocarbon raw material contains hydrogen, methane and hydrocarbons above two carbon atoms. The light hydrocarbon raw material and the circulating light hydrocarbon are pretreated by an absorption desorption system. The light hydrocarbon raw material and the circulating light hydrocarbon are absorbed tail gas by the absorption tower, and the tail gas is discharged from the top of the absorption tower and contains hydrogen, methane and ethylene ethane. The absorption liquid discharged from the bottom of the absorption tower effectively removes heavy components (including benzene, toluene, xylene and other aromatic hydrocarbons) in the depentanizer, and avoids the catalyst deactivation caused by coking of the heavy components on the surface of the catalyst. The material extracted from the top of the depentanizer comprises propylene, propane, a carbon four-carbon five-component and part of ethylene and ethane absorbed by the absorbent in the absorption tower. These components, except ethane, can be efficiently converted to aromatics in the aromatization reactor.
By adopting the method, the hydrogen is removed from the absorption tower, the content of the hydrogen in the reaction feed is controlled, and the conversion rate of light hydrocarbon is improved. In the ethylene recovery system, hydrogen products are separated from the absorption tail gas, ethylene and ethane are separated from the carbon two components, wherein the ethane is discharged out of the system as fuel gas, the accumulation of the ethane is avoided, and the total yield of the aromatic hydrocarbon is improved by converting the ethylene into the aromatic hydrocarbon through a light hydrocarbon removing aromatization reactor.
By adopting the method, the reaction product is cooled and then sent into the gas-liquid separator, and the gas phase discharged from the gas-liquid separator is pressurized by the compressor and then returns to the absorption tower to remove methane, hydrogen and part of ethane in the reaction product. And recovering ethylene via an ethylene recovery system.
By adopting the method of the invention, through operations such as absorption and rectification, the content of impurities such as hydrogen, methane, ethane, benzene, toluene and the like in the reaction feed of the light hydrocarbon aromatization reactor is controlled below certain control values, so that the influence of the trace impurities on the service life of the catalyst is reduced to an acceptable degree.
By adopting the method, a preferable scheme is that the light hydrocarbon raw material is firstly cooled to 10 ℃ before being sent into the absorption tower, and the load of the absorption tower and the depentanizing tower can be effectively reduced by carrying out gas-liquid separation operation on the light hydrocarbon raw material, removing a gas phase from the absorption tower and removing a liquid phase from the depentanizing tower.
By adopting the method, a preferable scheme is that before the light hydrocarbon raw material is sent into the absorption tower, partial hydrogen is removed by adopting a membrane separation or adsorption separation technology, so that the consumption of an absorbent is reduced, and the energy consumption is reduced.
By adopting the method, the components causing the coking of the catalyst are removed from the light hydrocarbon raw material through pretreatment, and the total aromatic hydrocarbon yield is improved by recycling the recycled light hydrocarbon, thereby obtaining better technical effect.
Drawings
FIG. 1 is a schematic flow diagram of the process of the present invention.
In FIG. 1, 1 is a light hydrocarbon feedstock; 2, absorbing tail gas; 3 is absorption liquid; 4 is an absorbent; 5 is hydrogen and fuel gas; 6 is ethylene; 7 is aromatization reaction raw material; 8 is an aromatization reaction product; 9 is a second aromatic hydrocarbon stream; 10 is a first aromatic hydrocarbon stream; 11 is circulating light hydrocarbon. I is an absorption tower, II is an ethylene recovery unit, III is a depentanizer, IV is a light hydrocarbon aromatization reactor, and V is a gas-liquid separator.
The process is briefly described as follows: the light hydrocarbon raw material and the circulating light body are converged and then separated into absorption tail gas and absorption liquid in an absorption tower; separating the absorption tail gas into hydrogen, methane and carbon dioxide material flows through operations such as rectification and/or membrane separation in an ethylene recovery system, separating the carbon dioxide material flows into an ethylene rectifying tower to be separated into ethylene and ethane, wherein the ethylene is removed with a light hydrocarbon aromatization reactor; separating the absorption liquid into aromatization reaction raw materials and heavy components in a depentanizer; returning the heavy component part as an absorbent to the absorption tower, and removing the rest heavy component part to the depentanizer; an aromatization reaction raw material light hydrocarbon aromatization reactor is extracted from the top of the depentanizing tower, and tower bottom liquid is a first aromatic hydrocarbon material flow; cooling the light hydrocarbon aromatization reaction product, and separating the cooled light hydrocarbon aromatization reaction product into a circulating light hydrocarbon stream and a second aromatic hydrocarbon stream in a gas-liquid separator; and returning the circulating light hydrocarbon to the absorption tower.
The present invention will be further illustrated by the following examples, but is not limited to these examples.
Detailed Description
[ COMPARATIVE EXAMPLE 1 ]
The flow rate of light hydrocarbon raw material is 47 tons/hour, and the volume components of hydrogen gas 54%, methane 8%, carbon two 12%, carbon three and above 26%. The mass content of aromatic hydrocarbon in the light hydrocarbon raw material is 4.9%. Directly feeding the light hydrocarbon raw material after waste heat into a light hydrocarbon aromatization reactor, wherein the reaction temperature is 560 ℃, the reaction pressure is 0.25MPa, and the reaction mass space velocity is 1HR-1. After the reaction product is cooled, the aromatic hydrocarbon of 17 tons/h, ethane of 7 tons/h and carbon are obtained by conventional separation means of absorption operation, rectification operation and the likeThree 8 tons/hour and tail gas 15 tons/hour. In this comparative example, carbon three was not recycled, and the aromatic yield (hydrogen, methane and ethane in the light hydrocarbon feedstock were not calculated as non-aromatizable components) was 44.7%.
[ example 1 ]
According to the flow shown in figure 1, the flow rate of light hydrocarbon raw material is 47 tons/hour, and the volume components are 54% of hydrogen, 8% of methane, 12% of carbon two and more than 26% of carbon three. The mass content of aromatic hydrocarbon in the light hydrocarbon raw material is 4.9%. The operating pressure of the absorption tower is 1.6MPa, and the flow rate of the absorption tail gas is 28.6 tons/hour. The absorbent usage was 600 tons/hour and the weight ratio of the absorbent stream and the first aromatic stream was 120, with a mass fraction of BTX of 87%. After the absorption tail gas is pressurized to 3.2MPa by a compressor, 3.2 tons of hydrogen per hour are separated in a membrane separator, 12.6 tons of methane per hour are separated in a demethanizer, and 5.7 tons of ethylene per hour and 7.1 tons of ethane per hour are separated in an ethylene rectifying tower. The absorption liquid is separated in a depentanizer. The operating pressure of the depentanizer is 0.7MPa, the flow rate of the material flow at the top of the depentanizer is 60.2 tons/hour, the flow rate at the bottom of the depentanizer is 605 tons/hour, wherein 600 tons/hour is absorbent, and the rest 5 tons/hour is the first aromatic hydrocarbon material flow, and the material flow is discharged out of the system. The ethylene and the gas phase at the top of the depentanizer are converged and then enter a light hydrocarbon aromatization reactor. The aromatization reaction temperature of the light hydrocarbon is 560 ℃, the reaction pressure is 0.25MPa, and the reaction mass space velocity is 1HR-1. The pressure of the compressed circulating light hydrocarbon is 1.6MPa, and the flow rate is 47.5 tons/hour. The second aromatic stream flow rate was 18 tons/hr. The aromatics yield (hydrogen, methane and ethane in the light hydrocarbon feedstock were not calculated as non-aromatizable components) for this example was 60.5%. The catalyst regeneration period is prolonged by 33% compared with the comparative example.
[ example 2 ]
According to the conditions and procedures described in example 1, after the light hydrocarbon feedstock and the recycled light hydrocarbon are combined, they are first cooled to 10 ℃ before being sent to the absorption tower, after the gas-liquid separation operation, the gas phase is sent to the absorption tower, and the liquid phase is sent to the depentanizer. The absorbent dosage of the embodiment is 450 tons/hour, and the weight ratio of the absorbent material flow to the first aromatic hydrocarbon material flow is 90, so that the load of the absorption tower can be effectively reduced by about 25 percent. The yield of aromatic hydrocarbon is 59.3%, and the regeneration period of the catalyst is prolonged by 30% compared with the comparative example.
[ example 3 ]
According to the conditions and steps described in example 1, after the light hydrocarbon raw material and the recycled light hydrocarbon are merged, 90% of hydrogen is removed by adopting a membrane separation technology before the merged material is sent to an absorption tower, the partial pressure of carbon dioxide and above components in absorption feed is improved, the absorption efficiency is improved, the consumption of the absorbent is 560 tons/hour, and the weight ratio of the absorbent material flow to the first aromatic hydrocarbon material flow is 112. The yield of aromatic hydrocarbon is 59.6%, and the regeneration period of the catalyst is prolonged by 31% compared with the comparative example.
[ example 4 ]
According to the conditions and steps described in example 1, after the light hydrocarbon raw material and the circulating light hydrocarbon are converged, 90% of hydrogen is removed by adopting a membrane separation technology, then the mixture is cooled to 10 ℃, and after gas-liquid separation operation, the gas phase is sent to an absorption tower, and the liquid phase is sent to a depentanizer. The absorbent was used in this example at 420 tons/hour and the weight ratio of the absorbent stream to the first aromatic hydrocarbon stream was 84. The yield of aromatic hydrocarbon is 58.7%, and the regeneration period of the catalyst is prolonged by 33% compared with the comparative example.
[ example 5 ]
According to the flow shown in figure 1, the flow rate of light hydrocarbon raw material is 47 tons/hour, and the volume components are 54% of hydrogen, 8% of methane, 12% of carbon two and more than 26% of carbon three. The mass content of aromatic hydrocarbon in the light hydrocarbon raw material is 4.9%. The operating pressure of the absorption tower is 1.6MPa, and the flow rate of the absorption tail gas is 28.6 tons/hour. The amount of absorbent used was 590 ton/h and the weight ratio of the absorbent stream and the first aromatic stream was 59, wherein the mass fraction of BTX was 78%. After the absorption tail gas is pressurized to 3.2MPa by a compressor, 3.2 tons of hydrogen per hour are separated in a membrane separator, 12.6 tons of methane per hour are separated in a demethanizer, and 5.7 tons of ethylene per hour and 7.1 tons of ethane per hour are separated in an ethylene rectifying tower. The absorption liquid is separated in a depentanizer. The operating pressure of the depentanizer is 0.9MPa, the flow rate of the material flow at the top of the depentanizer is 65.2 tons/hour, the flow rate of the material flow at the bottom of the depentanizer is 600 tons/hour, wherein 590 tons/hour is absorbent, and the rest 10 tons/hour is first aromatic hydrocarbon material flow, and the first aromatic hydrocarbon material flow is discharged out of the system. The ethylene and the gas phase at the top of the depentanizer are converged and then enter a light hydrocarbon aromatization reactor. The aromatization reaction temperature of light hydrocarbon is 560 deg.C, reaction pressure is 0.25MPa, reactionResponse mass airspeed 1HR-1. The pressure of the compressed circulating light hydrocarbon is 1.6MPa, and the flow rate is 47.5 tons/hour. The second aromatic stream flow rate was 18 tons/hr. The aromatics yield (hydrogen, methane and ethane in the light hydrocarbon feedstock were not calculated as non-aromatizable components) for this example was 57.6%. The catalyst regeneration period is prolonged by 23% compared with the comparative example.
[ COMPARATIVE EXAMPLE 2 ]
According to the conditions and procedures described in example 1, only by changing the ethylene recovery unit without an ethylene rectifying tower, i.e. without separating ethylene and ethane, the mixed gas of ethylene and ethane is directly fed into an aromatization reactor, and the recycle gas is firstly subjected to carbon two component removal in a deethanizer to avoid ethane accumulation in the system, and then is recycled to an absorption tower. The comparative example has higher energy consumption than that of example 1, the flow rate of the mixture of ethylene and ethane is smaller, the equipment scale of the ethylene rectifying tower is smaller, so that the energy consumption and the equipment investment are lower, and the energy consumption and the scale of the deethanizer are higher, which are caused by the large amount of propane mixed. In addition, the flow of the comparative example is unreasonable, the pressure of the ethylene rectifying tower is higher than 2MPaG, the pressure of the aromatization reaction system is lower than 0.6MPaG, and the pressure of the deethanizer is higher than 2MPaG, so that ethane needs to be reduced from high pressure to low pressure and increased from low pressure to high pressure in the flow, and serious energy loss exists.
[ COMPARATIVE EXAMPLE 3 ]
According to the flow shown in figure 1, the flow rate of light hydrocarbon raw material is 47 tons/hour, and the volume components are 54% of hydrogen, 8% of methane, 12% of carbon two and more than 26% of carbon three. The mass content of aromatic hydrocarbon in the light hydrocarbon raw material is 4.9%. The operating pressure of the absorption tower is 1.6MPa, and the flow rate of the absorption tail gas is 28.6 tons/hour. The absorbent usage was 600 tons/hour and the weight ratio of the absorbent stream and the first aromatic stream was 120, with a mass fraction of BTX of 87%. After the absorption tail gas is pressurized to 3.2MPa by a compressor, 3.2 tons of hydrogen per hour are separated in a membrane separator, 12.6 tons of methane per hour are separated in a demethanizer, and 5.7 tons of ethylene per hour and 7.1 tons of ethane per hour are separated in an ethylene rectifying tower. The absorption liquid and ethylene enter a light hydrocarbon aromatization reactor. The aromatization reaction temperature of the light hydrocarbon is 560 ℃, the reaction pressure is 0.25MPa, and the reactantsVolume airspeed 1HR-1. The pressure of the compressed circulating light hydrocarbon is 1.6MPa, and the flow rate is 47.5 tons/hour. The second aromatic stream flow rate was 18 tons/hr. The aromatics yield (hydrogen, methane and ethane in the light hydrocarbon feedstock were not calculated as non-aromatizable components) for this example was 45.5%.
Claims (10)
1. A method for preparing aromatic hydrocarbon by mixed light hydrocarbon aromatization comprises the following steps: 1) separating the light hydrocarbon raw material into absorption tail gas and absorption liquid in an absorption tower; 2) absorbing tail gas and separating ethylene, hydrogen and fuel gas in an ethylene recovery unit, wherein the ethylene is removed to a light hydrocarbon aromatization reactor; 3) separating the absorption liquid into an aromatization reaction raw material and a heavy component stream in a depentanizer; 4) the heavy component material flow is divided into two material flows, one material flow is used as an absorbent to return to the absorption tower, and the other material flow is used as a first aromatic hydrocarbon material flow product; 5) feeding an aromatization reaction raw material and ethylene into a light hydrocarbon aromatization reactor; 6) cooling the light hydrocarbon aromatization reaction product, and separating the cooled light hydrocarbon aromatization reaction product into a circulating light hydrocarbon and a second aromatic hydrocarbon material flow product in a gas-liquid separator; 7) and returning the circulating light hydrocarbon to the absorption tower.
2. The method of aromatizing mixed light hydrocarbons to aromatics according to claim 1, wherein the light hydrocarbon feedstock comprises hydrogen, methane, ethylene, ethane, propylene, propane, C four, C five, benzene, toluene, xylene components.
3. The method for preparing aromatic hydrocarbons by mixed light hydrocarbon aromatization according to claim 1, characterized in that the weight ratio of the absorbent stream to the first aromatic hydrocarbon stream in the step 4) is 150-50.
4. The method for producing aromatic hydrocarbons by mixed light hydrocarbon aromatization according to claim 1 characterized in that the total mass fraction of BTX contained in the absorbent is more than 80%.
5. The method for preparing aromatic hydrocarbons by aromatizing mixed light hydrocarbons according to claim 1, wherein the operating pressure of the absorption tower is 1.5 to 2.5 MPA.
6. The method for preparing aromatic hydrocarbons by aromatization of light mixed hydrocarbons according to claim 1, wherein the operating pressure of the depentanizer is 0.5-0.8 MPA.
7. The method for producing aromatic hydrocarbons by mixed light hydrocarbon aromatization according to claim 1 characterized in that the light hydrocarbon aromatization reaction conditions are: the reaction temperature is 500-600 ℃, the reaction pressure is 0.1-0.6 MPA, and the reaction mass airspeed is 0.1-3 HR-1。
8. The method for preparing aromatic hydrocarbons by aromatization of light hydrocarbons mixture according to claim 1, wherein the recycled light hydrocarbons are pressurized by a compressor to a pressure greater than the operating pressure of the absorption column and then enter the absorption column.
9. The method of claim 1, wherein the light hydrocarbon feedstock is cooled to a temperature below 10 ℃, and then subjected to a gas-liquid separation operation, a gas phase absorption tower, and a liquid phase depentanizer.
10. The method for preparing aromatic hydrocarbons by aromatizing mixed light hydrocarbons according to claim 1, wherein the light hydrocarbon raw material is sent to an absorption tower after being subjected to membrane separation to remove a part of hydrogen.
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