CN111218298A - Preparation method for producing aromatic hydrocarbon and olefin by using mixed alcohol - Google Patents

Preparation method for producing aromatic hydrocarbon and olefin by using mixed alcohol Download PDF

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Publication number
CN111218298A
CN111218298A CN202010035622.3A CN202010035622A CN111218298A CN 111218298 A CN111218298 A CN 111218298A CN 202010035622 A CN202010035622 A CN 202010035622A CN 111218298 A CN111218298 A CN 111218298A
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gas
tower
mixed alcohol
dehydration reaction
hydrocarbon
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郝金付
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Hebei Xiyao New Energy Technology Co ltd
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Hebei Xiyao New Energy Technology Co ltd
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/42—Catalytic treatment
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/60—Controlling or regulating the processes
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Abstract

The invention relates to a separation and purification method of mixed alcohol, which comprises the following steps of carrying out vaporization treatment, first dehydration reaction, second dehydration reaction, gas-liquid separation, oil-water separation, LPG separation and alkyl purification on the mixed alcohol in sequence. The invention can produce olefin, alkane and aromatic hydrocarbon by using mixed alcohol, and has high production efficiency and high product purity.

Description

Preparation method for producing aromatic hydrocarbon and olefin by using mixed alcohol
Technical Field
The invention belongs to the technical field of mixed alcohol treatment, and relates to a preparation method for producing aromatic hydrocarbon and olefin by using mixed alcohol.
Background
The mixed alcohol refining, separating and purifying process includes the steps of refining mixed alcohol containing ethanol, fusel, water and other matters in different boiling points to obtain refined product. The bottleneck problem of mixed alcohol treatment is that water in mixed alcohol is difficult to separate, so that the mixed alcohol treatment has the disadvantages of high energy consumption, high cost and prominent environmental protection problem, and therefore, a new mixed alcohol treatment process needs to be developed.
Disclosure of Invention
The invention aims to provide a preparation method for producing aromatic hydrocarbon and olefin by using mixed alcohol, which can produce olefin, alkane and aromatic hydrocarbon by using mixed alcohol, and has high production efficiency and high product purity.
In order to achieve the purpose, the technical scheme of the invention comprises the following steps of carrying out vaporization treatment, first dehydration reaction, second dehydration reaction, gas-liquid separation, oil-water separation, LPG separation and alkyl purification on mixed alcohol in sequence.
Further, the mixed alcohol comprises the following components in percentage by mass: 10-20% of methanol, 40-50% of ethanol, 0-10% of other fusel and the balance of water. The fusel is alcohol, such as propanol, butanol, etc.
Further, during the vaporization treatment, the mixed alcohol is heated to vaporize, the heating temperature is 180-230 ℃, and the vaporization pressure is 1.4 Mpa.
Further, carrying out a first dehydration reaction on the gas subjected to the vaporization treatment;
the first dehydration reaction is to mix the vaporized gas with a dimethyl ether catalyst, wherein the pressure is 1.2Mpa-1.4Mpa, the temperature is 260-320 ℃, and the volume ratio of the dimethyl ether catalyst to the gas is 0.5-1.4: 1.
Further, carrying out a second dehydration reaction on the gas subjected to the first dehydration reaction; the second dehydration reaction is to mix the gas after the first dehydration reaction with a ZSM-5 molecular sieve catalyst for catalytic reaction, wherein the reaction temperature is 340-400 degrees, and the pressure is 1.3-1.4 Mpa;
the volume ratio of the ZSM-5 molecular sieve catalyst to the gas is 0.5-1.4: 1.
further, the gas-liquid separation is to cool the gas after the second dehydration reaction at 30-45 ℃.
Further, the oil-water separation is as follows: precipitating the liquid obtained after gas-liquid separation, and separating to remove water after layering.
Further, the LPG separation is: separating oil from water, and delivering the water-removed liquid to a debutanizer, wherein the tower pressure is controlled to be 1.2-1.3 Mpa, the tower kettle temperature is 170-185 degrees, the tower top temperature is 65-70 degrees, and the tower top cooling temperature is 30-45 degrees;
after the reaction is completed, LPG is separated from the top of the tower.
Further, the alkyl purification is: after LPG separation, the product at the bottom of the tower is conveyed into a hydrocarbon-based fuel tower for purification, the temperature at the top of the tower is controlled to be 120-130 degrees, the temperature at the bottom of the tower is controlled to be 220-240 degrees, the pressure of the tower is 0-0.05Mpa, the cooling temperature at the top of the tower is 30-45 degrees, and the fraction at the top of the tower is collected.
Further, in the gas-liquid separation process, the cooled liquid enters the next oil-water separation process, and the gas which is not cooled is used as fuel gas or participates in the second dehydration reaction again.
The invention has the following positive effects:
the invention solves the environmental protection problem that the water in the mixed alcohol is difficult to separate in the prior art, greatly reduces the environmental pollution, simultaneously reduces the energy consumption, saves the production cost and creates a new direction for the utilization of the mixed alcohol.
Drawings
FIG. 1 is a schematic process flow diagram of the present invention;
FIG. 2-1 is a gas chromatogram of the overhead product finally obtained in example 1 of the present invention, with retention time on abscissa between 0-15.5 min;
FIG. 2-2 is a gas chromatogram of the top product finally obtained in example 1 of the present invention, with retention time on abscissa between 15.5-36 min.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail below with reference to examples. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
In order to better illustrate the invention, the following examples are given by way of further illustration.
Example 1
This example provides a process for producing aromatic hydrocarbons and olefins from a mixed alcohol, which comprises subjecting the mixed alcohol to (1) vaporization treatment, (2) first dehydration reaction, (3) second dehydration reaction, (4) gas-liquid separation, (5) oil-water separation, (6) LPG separation, and (7) alkyl purification in this order.
The mixed alcohol of the embodiment comprises the following components in percentage by mass: 15% of methanol, 45% of ethanol, 7% of other fusel and the balance of water.
Firstly, carrying out vaporization treatment on the mixed alcohol (1) so as to change the mixed alcohol into gas completely, namely heating the mixed alcohol to vaporize, wherein the heating temperature is 200 ℃, and the vaporization pressure is 1.4 Mpa.
Treating the gas obtained by vaporization in the step (1) in the step (2), wherein the step (2) is a first dehydration reaction, the first dehydration reaction is to mix the gas subjected to vaporization treatment with a dimethyl ether catalyst at the temperature of 300 ℃ and the pressure of 1.3Mpa, the volume ratio of the dimethyl ether catalyst to the gas is 1:1, and in the embodiment, the volume of the dimethyl ether catalyst is 10m3The volume of the gas treated by the dimethyl ether catalyst is 10m3. The first dehydration reaction is laid for the next catalytic reaction, and the step can promote the water to be separated from the alcohol, thereby increasing the reaction effect and the recovery rate of the subsequent steps. After the treatment of the step (2), the gas state is still maintained.
Carrying out the second dehydration reaction in the step (3) on the gas subjected to the first dehydration reaction in the step (2); and in the second dehydration reaction, the gas subjected to the first dehydration reaction is mixed with a ZSM-5 molecular sieve catalyst for catalytic reaction, the reaction temperature is 370 ℃, and the pressure is 1.35 Mpa. The volume ratio of the ZSM-5 molecular sieve catalyst to gas is 1: 1. in this example, the ZSM-5 molecular sieve catalyst had a volume of 10m3The volume of the gas treated by the ZSM-5 molecular sieve catalyst is 10m3. After the treatment of the step (3), the gas state is still maintained. The second dehydration reaction is a catalytic reaction, most of the catalyst is converted into hydrocarbon gas after the reaction, namely the mixture of olefin, alkane, aromatic hydrocarbon, water and the like is converted by the second catalytic reaction, and the recovery rate of the product is improved.
And (4) carrying out gas-liquid separation on the gas treated in the step (3) in the step (4), wherein the gas-liquid separation is to cool the gas subjected to the second dehydration reaction at 40 ℃. The cooled liquid enters the next oil-water separation process, and the gas which is not cooled can be used as fuel gas or participate in the second dehydration reaction again to play a role in maintaining the pressure of the reaction system. In this embodiment, the gas treated in step (3) is subjected to heat exchange, and gradually changed into liquid, and reaches the gas-liquid separator, the gas which is not cooled enters a circulation reaction for use, and the cooled liquid is a mixed hydrocarbon liquid. The gas-liquid separator is stably controlled at 40 ℃, liquid is cooled down and flows away from the lower part, and gas which is not cooled is discharged from the upper part for circular reaction.
And (5) carrying out oil-water separation on the liquid cooled down in the step (4), wherein the oil-water separation is to precipitate the liquid cooled down in the step (4), namely the mixed hydrocarbon liquid, and after layering, separating and removing water. The cooled mixed hydrocarbon liquid contains water, so that water needs to be further separated, and in this embodiment, precipitation separation is performed in an oil-water separator, and depending on the specific gravity of oil and water, the free water is discharged at the lower part, and the oil remains. The remaining part of the oil is a mixed hydrocarbon, and the surface contains a plurality of substances, namely 3-4 carbon atoms, 5-12 carbon atoms and gasoline and the like in terms of carbon molecules.
And (3) after the oil and the water in the step (5) are separated, carrying out LPG separation on the part of the oil in the step (6) so as to separate the LPG in the oil. LPG is an abbreviation for liquidized Petroleum Gas, Liquefied Petroleum Gas.
LPG separation is: and (3) after oil-water separation, conveying the liquid after water removal, namely the mixed hydrocarbon obtained after treatment in the step (5), to a debutanizer, controlling the tower pressure at 1.25Mpa, heating by heat transfer oil, controlling the tower kettle temperature at 180 degrees, the tower top temperature at 68 degrees and the tower top cooling temperature at 40 degrees. LPG from the top is sent to a liquefied gas storage tank, and alkyl is arranged at the bottom of the tower. This step effectively extracts the carbon 3 and carbon 4 substances in the mixed hydrocarbon obtained after the treatment in the step (5).
And (4) performing alkyl purification in the step (7) on the tower bottom material separated from the LPG in the step (6).
The alkyl purification is: after LPG separation, the product at the bottom of the tower is conveyed into a hydrocarbon-based fuel tower for purification, the temperature at the top of the tower is controlled at 125 degrees, the temperature at the bottom of the tower is 230 degrees, the pressure of the tower is 0.03MPa, the cooling temperature at the top of the tower is 40 degrees, and the fraction at the top of the tower is collected. Heavy aromatics are at the bottom of the tower, and carbon 5-carbon 12 substances are mainly at the top of the tower.
The method comprises the steps of vaporizing raw material mixed alcohol to change mixed alcohol liquid into gas, promoting dehydration through a first dehydration reaction, converting mixed gas of olefin, alkane, aromatic hydrocarbon, water and the like through a second dehydration reaction through a catalytic reaction, separating gas from liquid, cooling to obtain mixed hydrocarbon liquid, separating oil from water to remove free water, separating LPG (liquefied petroleum gas) and purifying alkyl to finally separate substances of olefin, alkane, aromatic hydrocarbon and the like, and effectively separating and purifying the mixed alcohol.
After the treatment of example 1, 27.40% of olefins, 20.60% of alkanes, 42% of aromatics and a small amount of LPG were obtained finally after vaporization treatment, first dehydration reaction, second dehydration reaction and gas-liquid separation, a mixture of olefins and aromatics was obtained by oil-water separation, and 99.9% of olefins, alkanes and 99.9% of aromatics were separated and purified by a rectifying tower.
In this example, after the last alkyl purification step, the resulting overhead product was pale yellow in color and was visually observed to be clear and free of impurities. The product was analyzed on an a5000 gas chromatography workstation with the following results:
retention time: 7.62- - - -38.87
Based on a full component chain of stable light hydrocarbons, of which aromatic hydrocarbons
Toluene content: 3.12 percent;
total content of xylene: 9.63 percent;
content of methylethylbenzene: 4.53 percent;
total content of trimethylbenzene: 25.68 percent;
durene content: 4.15 percent;
hydrocarbon distribution:
aromatic hydrocarbon content: 42%;
olefin content: 27.40 percent;
alkane content: 20.60 percent.
In this example, after the last alkyl purification step, the gas chromatogram of the obtained overhead product is shown in fig. 2, and the analysis report of the purification process is as follows:
analysis report sheet for preparing light hydrocarbon (crude oil) sample from mixed alcohol
Initial boiling point 33°c End point of distillation 204°c
5ml 47°c Recovering 91ml
10ml 57°c Residue is remained 1.10％
20ml 74°c ρ 0.765
30ml 95°c ρ20 0.760 (Biaomi)
40ml 119°c RON national standard 95.2/86.2
50ml 137°c MON motor 96.75/MON
60ml 151°c Benzene content (BZ) 1.20％
70ml 161°c S 4.25PPM
80ml 169°c N 1.28PPM
90ml 184°c
The products such as high-purity olefin, alkane, aromatic hydrocarbon and the like produced by scientific design and innovation of the process meet the industrial standard through detection.
The invention solves the environmental protection problem of difficult water separation in mixed alcohol for many years, greatly reduces the environmental pollution, simultaneously reduces the energy consumption, saves the production cost and creates a new direction for the utilization of the mixed alcohol.
Example 2
This example provides a process for producing aromatic hydrocarbons and olefins from a mixed alcohol, which comprises subjecting the mixed alcohol to (1) vaporization treatment, (2) first dehydration reaction, (3) second dehydration reaction, (4) gas-liquid separation, (5) oil-water separation, (6) LPG separation, and (7) alkyl purification in this order.
The mixed alcohol of the embodiment comprises the following components in percentage by mass: 10% of methanol, 50% of ethanol and the balance of water.
Firstly, carrying out vaporization treatment on the mixed alcohol (1) so as to change the mixed alcohol into gas completely, namely heating the mixed alcohol to vaporize, wherein the heating temperature is 180 degrees, and the vaporization pressure is 1.4 Mpa.
Treating the gas obtained by vaporization in the step (1) in the step (2), wherein the step (2) is a first dehydration reaction, the first dehydration reaction is to mix the gas subjected to vaporization treatment with a dimethyl ether catalyst at the temperature of 320 ℃ and the pressure of 1.2Mpa, the volume ratio of the dimethyl ether catalyst to the gas is 0.5:1, and in the embodiment, the volume of the dimethyl ether catalyst is 5m3The volume of the gas treated by the dimethyl ether catalyst is 10m3. After the treatment of the step (2), the gas state is still maintained.
Carrying out the second dehydration reaction in the step (3) on the gas subjected to the first dehydration reaction in the step (2); and the second dehydration reaction is to mix the gas subjected to the first dehydration reaction with a ZSM-5 molecular sieve catalyst for catalytic reaction, wherein the reaction temperature is 340 degrees and the pressure is 1.3 Mpa. The volume ratio of the ZSM-5 molecular sieve catalyst to gas is 1.4: 1. in this example, the ZSM-5 molecular sieve catalyst had a volume of 14m3The volume of the gas treated by the ZSM-5 molecular sieve catalyst is 10m3. After the treatment of the step (3), the gas state is still maintained. The second dehydration reaction is a catalytic reaction, most of the catalyst is converted into hydrocarbon gas after the reaction, namely the mixture of olefin, alkane, aromatic hydrocarbon, water and the like is converted by the second catalytic reaction, and the recovery rate of the product is improved.
And (4) carrying out gas-liquid separation on the gas treated in the step (3) in the step (4), wherein the gas-liquid separation is to cool the gas subjected to the second dehydration reaction at 30 ℃. The cooled liquid enters the next oil-water separation process, and the gas which is not cooled can be used as fuel gas or participate in the second dehydration reaction again to play a role in maintaining the pressure of the reaction system. In this embodiment, the gas treated in step (3) is subjected to heat exchange, and gradually changed into liquid, and reaches the gas-liquid separator, the gas which is not cooled enters a circulation reaction for use, and the cooled liquid is a mixed hydrocarbon liquid. The gas-liquid separator is stably controlled at 30 ℃, liquid is cooled down and flows away from the lower part, and gas which is not cooled is discharged from the upper part for circular reaction.
And (5) carrying out oil-water separation on the liquid cooled down in the step (4), wherein the oil-water separation is to precipitate the liquid cooled down in the step (4), namely the mixed hydrocarbon liquid, and after layering, separating and removing water. The cooled mixed hydrocarbon liquid contains water, so that water needs to be further separated, and in this embodiment, precipitation separation is performed in an oil-water separator, and depending on the specific gravity of oil and water, the free water is discharged at the lower part, and the oil remains. The remaining part of the oil is a mixed hydrocarbon, and the surface contains a plurality of substances, namely 3-4 carbon atoms, 5-12 carbon atoms and gasoline and the like in terms of carbon molecules.
And (3) after the oil and the water in the step (5) are separated, carrying out LPG separation on the part of the oil in the step (6) so as to separate the LPG in the oil. LPG is an abbreviation for liquidized Petroleum Gas, Liquefied Petroleum Gas.
LPG separation is: and (3) after oil-water separation, conveying the liquid after water removal, namely the mixed hydrocarbon obtained after treatment in the step (5), to a debutanizer, controlling the tower pressure at 1.2Mpa, heating by heat transfer oil, controlling the temperature of a tower kettle at 185 degrees and controlling the temperature of the tower top at 70 degrees. The cooling temperature at the top of the tower is 30 degrees, LPG discharged from the top of the tower is sent to a liquefied gas storage tank, and alkyl is arranged at the bottom of the tower. This step effectively extracts the carbon 3 and carbon 4 substances in the mixed hydrocarbon obtained after the treatment in the step (5).
And (4) performing alkyl purification in the step (7) on the tower bottom material separated from the LPG in the step (6).
The alkyl purification is: after LPG separation, the product at the bottom of the tower is conveyed into a hydrocarbon-based fuel tower for purification, the temperature at the top of the tower is controlled at 130 degrees, the temperature at the bottom of the tower is 220 degrees, the pressure of the tower is 0Mpa, the cooling temperature at the top of the tower is 45 degrees, and the fraction at the top of the tower is collected. Heavy aromatics are at the bottom of the tower, and carbon 5-carbon 12 substances are mainly at the top of the tower.
Example 3
This example provides a process for producing aromatic hydrocarbons and olefins from a mixed alcohol, which comprises subjecting the mixed alcohol to (1) vaporization treatment, (2) first dehydration reaction, (3) second dehydration reaction, (4) gas-liquid separation, (5) oil-water separation, (6) LPG separation, and (7) alkyl purification in this order.
The mixed alcohol of the embodiment comprises the following components in percentage by mass: 20% of methanol, 40% of ethanol, 10% of other fusel and the balance of water.
Firstly, carrying out vaporization treatment on the mixed alcohol (1) so as to change the mixed alcohol into gas completely, namely heating the mixed alcohol to vaporize, wherein the heating temperature is 230 ℃ and the vaporization pressure is 1.4 MPa.
Treating the gas obtained by vaporization in the step (1) in the step (2), wherein the step (2) is a first dehydration reaction, the first dehydration reaction is to mix the gas subjected to vaporization treatment with a dimethyl ether catalyst at the temperature of 260 ℃ and the pressure of 1.4Mpa, the volume ratio of the dimethyl ether catalyst to the gas is 1.4:1, and in the embodiment, the volume of the dimethyl ether catalyst is 14m3The volume of the gas treated by the dimethyl ether catalyst is 10m3. After the treatment of the step (2), the gas state is still maintained.
Carrying out the second dehydration reaction in the step (3) on the gas subjected to the first dehydration reaction in the step (2); and the second dehydration reaction is to mix the gas subjected to the first dehydration reaction with a ZSM-5 molecular sieve catalyst for catalytic reaction, wherein the reaction temperature is 400 ℃ and the pressure is 1.4 Mpa. The volume ratio of the ZSM-5 molecular sieve catalyst to the gas is 0.5: 1. in this example, the ZSM-5 molecular sieve catalyst had a volume of 5m3The volume of the gas treated by the ZSM-5 molecular sieve catalyst is 10m3. After the treatment of the step (3), the gas state is still maintained. The second dehydration reaction is a catalytic reaction, most of the catalyst is converted into hydrocarbon gas after the reaction, namely the mixture of olefin, alkane, aromatic hydrocarbon, water and the like is converted by the second catalytic reaction, and the recovery rate of the product is improved.
And (4) carrying out gas-liquid separation on the gas treated in the step (3) in the step (4), wherein the gas-liquid separation is to cool the gas subjected to the second dehydration reaction at 45 ℃. The cooled liquid enters the next oil-water separation process, and the gas which is not cooled can be used as fuel gas or participate in the second dehydration reaction again to play a role in maintaining the pressure of the reaction system. In this embodiment, the gas treated in step (3) is subjected to heat exchange, and gradually changed into liquid, and reaches the gas-liquid separator, the gas which is not cooled enters a circulation reaction for use, and the cooled liquid is a mixed hydrocarbon liquid. The gas-liquid separator is stably controlled at 30 ℃, liquid is cooled down and flows away from the lower part, and gas which is not cooled is discharged from the upper part for circular reaction.
And (5) carrying out oil-water separation on the liquid cooled down in the step (4), wherein the oil-water separation is to precipitate the liquid cooled down in the step (4), namely the mixed hydrocarbon liquid, and after layering, separating and removing water. The cooled mixed hydrocarbon liquid contains water, so that water needs to be further separated, and in this embodiment, precipitation separation is performed in an oil-water separator, and depending on the specific gravity of oil and water, the free water is discharged at the lower part, and the oil remains. The remaining part of the oil is a mixed hydrocarbon, and the surface contains a plurality of substances, namely 3-4 carbon atoms, 5-12 carbon atoms and gasoline and the like in terms of carbon molecules.
And (3) after the oil and the water in the step (5) are separated, carrying out LPG separation on the part of the oil in the step (6) so as to separate the LPG in the oil. LPG is an abbreviation for liquidized Petroleum Gas, Liquefied Petroleum Gas.
LPG separation is: and (3) after oil-water separation, conveying the liquid after water removal, namely the mixed hydrocarbon obtained after treatment in the step (5), to a debutanizer, controlling the tower pressure at 1.3Mpa, heating by heat transfer oil, controlling the tower kettle temperature at 170 degrees and the tower top temperature at 65 degrees. The cooling temperature at the top of the tower is 45 degrees, LPG discharged from the top of the tower is sent to a liquefied gas storage tank, and alkyl is arranged at the bottom of the tower. This step effectively extracts the carbon 3 and carbon 4 substances in the mixed hydrocarbon obtained after the treatment in the step (5).
And (4) performing alkyl purification in the step (7) on the tower bottom material separated from the LPG in the step (6).
The alkyl purification is: after LPG separation, the product at the bottom of the tower is conveyed into a hydrocarbon-based fuel tower for purification, the temperature at the top of the tower is controlled at 120 degrees, the temperature at the bottom of the tower is 240 degrees, the pressure of the tower is 0.05Mpa, the cooling temperature at the top of the tower is 30 degrees, and the fraction at the top of the tower is collected. Heavy aromatics are at the bottom of the tower, and carbon 5-carbon 12 substances are mainly at the top of the tower.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims (10)

1. A preparation method for producing aromatic hydrocarbon and olefin by mixed alcohol is characterized in that: the method comprises the following steps of carrying out vaporization treatment, primary dehydration reaction, secondary dehydration reaction, gas-liquid separation, oil-water separation, LPG separation and alkyl purification on mixed alcohol in sequence.
2. The method for preparing aromatic hydrocarbon and olefin hydrocarbon with mixed alcohol as claimed in claim 1, wherein: the mixed alcohol comprises the following components in percentage by mass: 10-20% of methanol, 40-50% of ethanol, 0-10% of other fusel and the balance of water.
3. The method for preparing aromatic hydrocarbon and olefin hydrocarbon with mixed alcohol as claimed in claim 1, wherein: during the vaporization treatment, the mixed alcohol is heated to vaporize at 180-230 ℃ and 1.4 Mpa.
4. The method for preparing aromatic hydrocarbon and olefin hydrocarbon with mixed alcohol as claimed in claim 1, wherein: carrying out primary dehydration reaction on the gas after the vaporization treatment;
the first dehydration reaction is to mix the gas after the vaporization treatment with a dimethyl ether catalyst at the temperature of 260-320 ℃ and the pressure of 1.2-1.4 Mpa, and the volume ratio of the dimethyl ether catalyst to the gas is 0.5-1.4: 1.
5. The method for preparing aromatic hydrocarbon and olefin hydrocarbon with mixed alcohol as claimed in claim 1, wherein: carrying out a second dehydration reaction on the gas subjected to the first dehydration reaction;
the second dehydration reaction is to mix the gas after the first dehydration reaction with a ZSM-5 molecular sieve catalyst for catalytic reaction, wherein the reaction temperature is 340-400 degrees, and the pressure is 1.3-1.4 Mpa;
the volume ratio of the ZSM-5 molecular sieve catalyst to the gas is 0.5-1.4: 1.
6. the method for preparing aromatic hydrocarbon and olefin hydrocarbon with mixed alcohol as claimed in claim 1, wherein: the gas-liquid separation is to cool the gas after the second dehydration reaction at 30-45 ℃.
7. The method for preparing aromatic hydrocarbon and olefin hydrocarbon with mixed alcohol as claimed in claim 1, wherein: the oil-water separation is as follows: precipitating the liquid obtained after gas-liquid separation, and separating to remove water after layering.
8. The method for preparing aromatic hydrocarbon and olefin hydrocarbon with mixed alcohol as claimed in claim 1, wherein: the LPG separation is: separating oil from water, and delivering the water-removed liquid to a debutanizer, wherein the tower pressure is controlled to be 1.2-1.3 Mpa, the tower kettle temperature is 170-185 degrees, the tower top temperature is 65-70 degrees, and the tower top cooling temperature is 30-45 degrees;
after the reaction is completed, LPG is separated from the top of the tower.
9. The method for preparing aromatic hydrocarbon and olefin hydrocarbon with mixed alcohol as claimed in claim 1, wherein: the alkyl purification is: after LPG separation, the product at the bottom of the tower is conveyed into a hydrocarbon-based fuel tower for purification, the temperature at the top of the tower is controlled to be 120-130 degrees, the temperature at the bottom of the tower is controlled to be 220-240 degrees, the pressure of the tower is 0-0.05Mpa, the cooling temperature at the top of the tower is 30-45 degrees, and the fraction at the top of the tower is collected.
10. The method for preparing aromatic hydrocarbon and olefin hydrocarbon with mixed alcohol as claimed in claim 1, wherein: in the gas-liquid separation process, the cooled liquid enters the next oil-water separation process, and the gas which is not cooled is used as fuel gas or participates in the second dehydration reaction again.
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