CN105396514A - Apparatus and method for preparing gasoline from methanol - Google Patents

Apparatus and method for preparing gasoline from methanol Download PDF

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Publication number
CN105396514A
CN105396514A CN201511026372.2A CN201511026372A CN105396514A CN 105396514 A CN105396514 A CN 105396514A CN 201511026372 A CN201511026372 A CN 201511026372A CN 105396514 A CN105396514 A CN 105396514A
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gas
fixed bed
communicated
outlet
tower
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CN201511026372.2A
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CN105396514B (en
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萧锦诚
王刃
区绍伟
冯宝林
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DALIAN LONGTAI TECHNOLOGY DEVELOPMENT Co Ltd
TOWNGAS ENVIRONMENTAL PROTECTION ENERGY RESEARCH INSTITUTE CO LTD
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DALIAN LONGTAI TECHNOLOGY DEVELOPMENT Co Ltd
TOWNGAS ENVIRONMENTAL PROTECTION ENERGY RESEARCH INSTITUTE CO LTD
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0446Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
    • B01J8/0461Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds
    • B01J8/0465Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds the beds being concentric
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G3/00Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/54Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids characterised by the catalytic bed
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/50Improvements relating to the production of bulk chemicals
    • Y02P20/52Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00Technologies relating to oil refining and petrochemical industry
    • Y02P30/20Technologies relating to oil refining and petrochemical industry using bio-feedstock

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  • Chemical & Material Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The invention discloses an apparatus for preparing gasoline from methanol and a method of using the apparatus to prepare gasoline from methanol through a catalytic reaction. A reaction system comprises a raw material feeding terminal, a vaporizer, a heating furnace and a fixed bed reactor. The top of the fixed bed reactor is provided with a raw material input terminal, and the bottom of the fixed bed reactor is provided with a product output terminal; at least two bed layers are vertically arranged in the fixed bed reactor, and a gas distributor is arranged between the at least two layers; the raw material feeding terminal is communicated with the vaporizer and the heating furnace; the outlet of the heating furnace is communicated with the raw material input terminal of the fixed bed reactor; and the outlet of the vaporizer is communicated with the gas distributor. A system used in conventional methods for preparing gasoline from methanol has the disadvantages of high pressure, great energy consumption and long process flow. The apparatus and method provided by the invention have the advantages of simple process, short process flow, low energy consumption in operation, low investment, few by-products and capacity of allowing the content (mass percentage) of durene in gasoline to be less than 2%.

Description

Preparing gasoline by methanol device and method
Technical field
Of the present inventionly relate to technique for preparing gasoline by methanol field, particularly preparing gasoline by methanol device and method.
Background technology
Coal in China rich reserves, ammonia from coal, preparing gasoline by methanol are more and more subject to domestic attention, adopt that the octane number made of methyl alcohol is high, anti-knock properties good, and the impurity such as sulfur-bearing nitrogen, meets the requirement of clean fuel, have good application prospect hardly.
Preparing gasoline by methanol represents the two-stage method transformation technology that technology is the exploitation of MOBIL company of the U.S., adopt ZSM-5 molecular sieve catalyst, methanol conversion is dimethyl ether by one section, enter second-stage reaction after water-oil separating and generate the products such as gasoline, MOBIL patent has US3931349, US4579999, US4035430 are fixed bed two-stage method technique for preparing gasoline by methanol.Two-stage method shortcoming is that technological process is complicated, and capital cost of reactor is high.
CN101775310A, CN102049292A disclose a kind of process of fluid bed preparing gasoline by methanol, and wherein in CN102049292A patent, methyl alcohol is directly separated after reacting with catalyst exposure in fluidized-bed reactor and obtains the product such as gasoline and liquefied gas; Isolated light hydrocarbon gas is then sent into fluidized-bed reactor and is carried out lighter hydrocarbons circulation by CN101775310A again, lighter hydrocarbons circulation to raising reaction speed and yield of gasoline favourable.Application fluid bed preparing gasoline by methanol technique, shifting out conveniently of reaction heat, in heavy oil product, durol content is lower, and gasoline quality improves, but compared with fixed bed, object product gasoline yield is on the low side.
CN104099121A discloses a kind of fluid bed and fixed bed combined technical method of preparing gasoline by methanol, both having had fluidized-bed process reaction heat shifts out convenient timely, the advantage that in gasoline, durol content is low, there is again the advantage that fixed-bed process yield of gasoline is high, but invest high, complicated operation, catalyst easily weares and teares.
CN104099121A proposes a kind of knockout tower, adopts the mode of multiple lateral line withdrawal function to carry out separation of products, and flow process is simple, but product is easily with water, and is not separated the diesel oil in product.CN103865562A proposes a kind of separation method, high score tank gas, liquid, water is adopted to be separated, liquid phase (raw gasoline) enters two knockout towers of series connection successively, carry out the separation of liquefied gas, gasoline, diesel oil (C9+) step by step, the method separating effect improves, but high score tank gas phase is not effectively separated, and separating energy consumption is higher step by step.
Summary of the invention
Preparing gasoline by methanol device, comprises reaction system, and described reaction system comprises raw material supplying end, vaporizer, heating furnace and fixed bed reactors; Raw material input is established at described fixed bed reactors top, product output is established in bottom; In described fixed bed reactors, vertical direction arranges at least two beds, between bed, gas distributor is set; Described raw material supplying end is communicated with vaporizer, heating furnace respectively; The outlet of described heating furnace is communicated with the raw material input of described fixed bed reactors.The outlet of described vaporizer is communicated with described gas distributor.
As preferred technical scheme, in described fixed bed reactors, vertical direction is arranged three beds, gas distributor A and gas distributor B is set between three beds respectively;
As preferred technical scheme, the outlet of described vaporizer, through two pipelines of parallel connection, is communicated with gas distributor A and gas distributor B respectively.
As preferred technical scheme, described preparing gasoline by methanol device also comprises piece-rate system, and described piece-rate system comprises cooler, high-pressure gas-liquid knockout drum, gas compressor, point flow container, absorption and desorption tower, stabilizer, fractionating column; Described high-pressure gas-liquid knockout drum has water side, outlet side, outlet end; Described point of flow container has outlet side, outlet end; Described absorption and desorption tower has feed end, enters absorbent end, outlet side, outlet end; Described stabilizer has outlet side, outlet end; The product output of described fixed bed reactors is communicated with cooler, high-pressure gas-liquid knockout drum successively; The outlet side of described high-pressure gas-liquid knockout drum is communicated with gas compressor, point flow container successively; The outlet end of described high-pressure gas-liquid knockout drum is communicated with stabilizer; Outlet side, the outlet end of described point of flow container are communicated with the feed end of absorption and desorption tower respectively; The outlet end of described absorption and desorption tower is communicated with the import of stabilizer; The outlet end of described stabilizer is communicated with the entrance entering absorbent end and fractionating column of described absorption and desorption tower respectively.
Absorption and desorption tower is provided with bottom reboiler, and bottom reboiler adopts conduction oil or Steam Heating.
Stablize tower top and adopt cold reflux, at the bottom of tower, adopt kettle type reboiler.
The present invention also provides employing said apparatus, is that raw material prepares the method for gasoline through catalytic reaction with methyl alcohol.
As preferred technical scheme,
(1) material benzenemethanol divides two strands of materials, and one material is vaporized through vaporizer, enters the bed of fixed bed reactors from gas distributor, another strand of material is vaporized through heating furnace, enter the bed of fixed bed reactors from raw material input, under catalysts conditions, carry out catalytic reaction; Described heating in-furnace temperature 200-260 DEG C; Temperature 65-70 DEG C in described vaporizer;
Methyl alcohol enters fixed bed reactors, and at catalyst action, next step generates the products such as gasoline; The effect of vaporizer makes methanol gasifying; The effect of heating furnace is that methyl alcohol is heated to 200-260 DEG C, to meet the inlet temperature that methyl alcohol reacts in the reactor.Methyl alcohol preferably through the gasification of vaporizer divides two strands to enter fixed bed reactors, and the heat of releasing by the preparing gasoline by methanol reaction occurred in fixed bed reactors heats the methyl alcohol entered by vaporizer, to reduce energy consumption and effective temperature controlling each bed of reactor.
Step (1) products therefrom (dry gas, liquefied gas, gasoline, a small amount of diesel oil, water) enter cooler and cool, the outlet temperature of cooler is 40-50 DEG C;
(3) the material (2) cooled through step enters high-pressure gas-liquid knockout drum and carries out gas-liquid separation, and gas phase enters a point flow container through compressor; Liquid phase enters stabilizer; High-pressure gas-liquid knockout drum carry out gas (i.e. rich gas, containing liquefied gas, dry gas, containing a small amount of gasoline), the three phase separation of oil (i.e. gasoline, also contain a small amount of diesel oil, liquefied gas), water;
(4) enter the material of point flow container through gas-liquid separation, gas-liquid two-phase enters absorption and desorption tower respectively; Gas phase is compression rich gas (liquefied gas, dry gas, containing a small amount of gasoline); Liquid phase is rich gas lime set (gasoline, liquefied gas, containing a small amount of dry gas);
The effect dividing flow container is effectively separated the gas of compressor outlet, liquid two-phase.Gas-liquid two-phase enters absorption and desorption tower respectively, can reduce the resistance of ducting, the liquid phase of tower is distributed more reasonable.
(5), through the liquid phase that the process of absorption and desorption tower obtains, namely rich absorbent oil (absorbing the gasoline after liquefied gas, containing liquefied gas, a small amount of diesel oil) enters stabilizer; In tower, material is through stable gasoline (absorbent) absorption and desorption, and tower top discharges dry gas (gas phase);
(6) the oil of high-pressure gas-liquid knockout drum discharge and the rich absorbent oil of absorption and desorption tower discharge enter systems stabilisation, isolate gas phase (liquefied gas) and liquid phase (stable gasoline) through stabilizer; Stable gasoline part returns absorption and desorption tower as absorbent (absorbing oil), and residue stable gasoline enters fractionating column;
(7) be separated through fractionating column, isolate and do qualified gasoline (gas phase) and a small amount of diesel oil.
As preferred technical scheme, the methyl alcohol through vaporizer gasification divides two strands to enter fixed bed reactors; Bed is entered respectively through gas distributor A and gas distributor B.
As preferred technical scheme, the reaction pressure 0.8 ~ 1.8Mpa of described fixed bed reactors, reaction temperature 260 ~ 450 DEG C; , reaction velocity 1 ~ 4h -1.
As preferred technical scheme, the catalyst of described catalytic reaction is methanol conversion catalyst.Be preferably ZSM-5, ZSM-11, MCM-68, ZSM-12 or ZSM-48.
As preferred technical scheme, the operating pressure 0.4 ~ 0.5Mpa of described high-pressure gas-liquid knockout drum, operating temperature 40 ~ 55 DEG C; The outlet pressure of described compressor is 1.1-1.4MPa; .
As preferred technical scheme, the operating pressure 1.1-1.4MPa of described absorption and desorption tower, tower top operating temperature 40-50 DEG C, operating temperature 170-180 DEG C at the bottom of tower; Described stabilizer tower top adopts cold reflux, adopts kettle type reboiler, operating pressure 1.1 ~ 1.3Mpa at the bottom of tower; Tower top operating temperature 50 ~ 60 DEG C; Operating temperature 200-210 DEG C at the bottom of tower; Operating pressure 0.1 ~ the 0.15Mpa of described fractionating column; Tower top operating temperature 131-142 DEG C, operating temperature 200-210 DEG C at the bottom of tower.
The method system for use in carrying pressure of existing preparing gasoline by methanol is high, and energy consumption is large, long flow path.Technique of the present invention is simple, and flow process is short, and operation energy consumption is low, and invest low, accessory substance is few, and in gasoline, the content (mass fraction) of durol is lower than 2%.
Accompanying drawing explanation
Accompanying drawing 1 width of the present invention,
Fig. 1 is a kind of preparing gasoline by methanol schematic diagram;
In figure, 1 material carburetor; 2 reaction heating furnaces; 3 fixed bed reactors; 4 coolers; 5 high-pressure gas-liquid knockout drums; 6 gas compressors; 7 points of flow containers; 8 absorption and desorption towers; 9 stabilizers; 10 fractionating columns (gasoline weight-removing column); 11 gas distributor A; 12 gas distributor B; I raw material (methyl alcohol); II product (dry gas, liquefied gas, gasoline, a small amount of diesel oil, water); III water; IV rich gas (liquefied gas, dry gas, containing a small amount of gasoline); V gasoline is containing a small amount of diesel oil, liquefied gas; VI compression rich gas (liquefied gas, dry gas, containing a small amount of gasoline); VII rich gas lime set (gasoline, liquefied gas, containing a small amount of dry gas); VIII dry gas; Ⅸ rich absorbent oil (absorbing the gasoline after liquefied gas, containing liquefied gas, a small amount of diesel oil); Ⅹ liquefied gas; Ⅺ gasoline, containing a small amount of diesel oil; Ⅻ gasoline; XIII diesel oil.
Detailed description of the invention
Following non-limiting example can make the present invention of those of ordinary skill in the art's comprehend, but does not limit the present invention in any way.
Embodiment 1 preparing gasoline by methanol device
Preparing gasoline by methanol device, comprises reaction system, and described reaction system comprises raw material supplying end, vaporizer 1, heating furnace 2 and fixed bed reactors 3; Raw material input is established at described fixed bed reactors top, product output is established in bottom; Vertical direction is arranged 3 beds in described fixed bed reactors, gas distributor A11 and gas distributor B12 is set between 3 beds respectively; ; Described raw material supplying end is communicated with vaporizer 1, heating furnace 2 respectively; The outlet of described heating furnace 2 is communicated with the raw material input of described fixed bed reactors 3.The outlet of described vaporizer 1 is communicated with described gas distributor.The outlet of described vaporizer 1, through two pipelines of parallel connection, is communicated with gas distributor A11 and gas distributor B12 respectively.Described piece-rate system comprises cooler 4, high-pressure gas-liquid knockout drum 5, gas compressor 6, point flow container 7, absorption and desorption tower 8, stabilizer 9, fractionating column 10; Described high-pressure gas-liquid knockout drum 5 has water side, outlet side, outlet end; Described point of flow container 7 has outlet side, outlet end; Described absorption and desorption tower 8 has feed end, enters absorbent end, outlet side, outlet end; Described stabilizer 9 has outlet side, outlet end; The product output of described fixed bed reactors 3 is communicated with cooler 4, high-pressure gas-liquid knockout drum 5 successively; The outlet side of described high-pressure gas-liquid knockout drum 5 is communicated with gas compressor 6, point flow container 7 successively; The outlet end of described high-pressure gas-liquid knockout drum 5 is communicated with stabilizer 9; Outlet side, the outlet end of described point of flow container 7 are communicated with the feed end of absorption and desorption tower 8 respectively; The outlet end of described absorption and desorption tower 8 is communicated with the import of stabilizer 9; The outlet end of described stabilizer 9 is communicated with the entrance entering absorbent end and fractionating column 10 of described absorption and desorption tower 8 respectively.
Embodiment 2 adopts the device of embodiment 1, is that raw material prepares the method for gasoline through catalytic reaction with methyl alcohol
(1) material benzenemethanol divides two strands of materials, and one material is vaporized through vaporizer 1, enters the bed of fixed bed reactors 3 from distribution of gas dish, another strand of material is vaporized through heating furnace 2, enter the bed of fixed bed reactors 3 from raw material input, under catalysts conditions, carry out catalytic reaction; Described heating in-furnace temperature 200-260 DEG C; Temperature 65-70 DEG C in described vaporizer;
Step (1) products therefrom enter cooler 4 and cool, the outlet temperature of cooler is 40-50 DEG C;
(3) the material (2) cooled through step enters high-pressure gas-liquid knockout drum 5 and carries out gas-liquid separation, and gas phase enters point flow container 7 through compressor 6; Liquid phase enters stabilizer 9;
(4) enter the material of point flow container 7 through gas-liquid separation, gas-liquid two-phase enters absorption and desorption tower 8 respectively;
(5) process through absorption and desorption tower 8 liquid phase obtained and enter stabilizer 9;
(6) be separated through stabilizer 9 liquid phase obtained and divide two strands of materials, one material returns absorption and desorption tower 8 as absorbent, and another strand of material enters fractionating column 10;
(7) be separated through fractionating column 10.
Methyl alcohol through vaporizer gasification divides two strands to enter fixed bed reactors; Bed is entered respectively through gas distributor A11 and gas distributor B12.
The outlet pressure of compressor 6 is 1.1-1.4MPa.Catalyst is ZSM-5, ZSM-11, MCM-68, ZSM-12 or ZSM-48.Reaction pressure 0.8 ~ the 1.8Mpa of fixed bed reactors 3, reaction temperature 260 ~ 450 DEG C; , reaction velocity 1 ~ 4h -1.Operating pressure 0.4 ~ the 0.5Mpa of high-pressure gas-liquid knockout drum 5, operating temperature 40 ~ 55 DEG C.The operating pressure 1.1-1.4MPa of absorption and desorption tower 8, tower top operating temperature 40-50 DEG C, operating temperature 170-180 DEG C at the bottom of tower.Stabilizer 9 tower top adopts cold reflux, adopts kettle type reboiler, operating pressure 1.1 ~ 1.3Mpa at the bottom of tower; Tower top operating temperature 50 ~ 60 DEG C; Operating temperature 200-210 DEG C at the bottom of tower.Operating pressure 0.1 ~ the 0.15Mpa of fractionating column 10; Tower top operating temperature 131-142 DEG C, operating temperature 200-210 DEG C at the bottom of tower.
Embodiment 3
Certain Methanol process of gasoline section, adopt the method for embodiment 2, reaction feed 220t/h, product index is as follows:
Dry gas forms
Methane wt% 63
Ethane wt% 5.1
Ethene wt% 3.2
Propane wt% 18.4
Hydrogen wt% 0.6
Carbon dioxide wt% 8.2
Carbon monoxide wt% 1.5
Liquefied gas forms
Ethane wt% 8.1
Ethene wt% 1.2
Propane wt% 33.4
Propylene wt% 31.1
Butane wt% 23.2
Butylene wt% 0.9
Pentane wt% 2.1
Target product distributes
Dry gas wt% 2.9
Liquefied gas wt% 8.9
Gasoline wt% 88.2
Gasoline property
Research octane number (RON) RON 95
Density (20 DEG C) g/cm3 0.722
10% evaporating temperature 42
50% evaporating temperature 97
90% evaporating temperature 184
End point temperature 205
Vapour pressure Kpa 80.9
Do not wash solvent colloid Mg/100ml 2.5
Durol content m% 1.8
Olefin(e) centent v% 12.5
Benzene content v% 0.28
Arene content v% 24
Energy consumption 78kg marks oil/gasoline.

Claims (10)

1. preparing gasoline by methanol device, comprises reaction system, it is characterized in that:
Described reaction system comprises raw material supplying end, vaporizer (1), heating furnace (2) and fixed bed reactors (3);
Raw material input is established at described fixed bed reactors top, product output is established in bottom;
In described fixed bed reactors, vertical direction arranges at least two beds, between bed, gas distributor is set;
Described raw material supplying end is communicated with vaporizer (1), heating furnace (2) respectively;
The outlet of described heating furnace (2) is communicated with the raw material input of described fixed bed reactors (3).
The outlet of described vaporizer (1) is communicated with described gas distributor.
2. preparing gasoline by methanol device according to claim 1, is characterized in that:
Described fixed bed reactors (3) interior vertical direction is arranged three beds, gas distributor A (11) and gas distributor B (12) is set between three beds respectively;
The outlet of described vaporizer (1), through two pipelines of parallel connection, is communicated with gas distributor A (11) and gas distributor B (12) respectively.
3. preparing gasoline by methanol device according to claim 1 and 2, is characterized in that: also comprise piece-rate system,
Described piece-rate system comprises cooler (4), high-pressure gas-liquid knockout drum (5), gas compressor (6), point flow container (7), absorption and desorption tower (8), stabilizer (9), fractionating column (10);
Described high-pressure gas-liquid knockout drum (5) has water side, outlet side, outlet end;
Described point of flow container (7) has outlet side, outlet end;
Described absorption and desorption tower (8) has feed end, enters absorbent end, outlet side, outlet end;
Described stabilizer (9) has outlet side, outlet end;
The product output of described fixed bed reactors (3) is communicated with cooler (4), high-pressure gas-liquid knockout drum (5) successively;
The outlet side of described high-pressure gas-liquid knockout drum (5) is communicated with gas compressor (6), point flow container (7) successively;
The outlet end of described high-pressure gas-liquid knockout drum (5) is communicated with stabilizer (9);
Outlet side, the outlet end of described point of flow container (7) are communicated with the feed end of absorption and desorption tower (8) respectively;
The outlet end of described absorption and desorption tower (8) is communicated with the import of stabilizer (9);
The outlet end of described stabilizer (9) is communicated with the entrance entering absorbent end and fractionating column (10) of described absorption and desorption tower (8) respectively.
4. adopting the device described in claim 1-3 any one, is that raw material prepares the method for gasoline through catalytic reaction with methyl alcohol.
5. method according to claim 4, is characterized in that,
(1) material benzenemethanol divides two strands of materials, one material is vaporized through vaporizer (1), the bed of fixed bed reactors (3) is entered from gas distributor, another strand of material is vaporized through heating furnace (2), the bed of fixed bed reactors (3) is entered from raw material input, under catalysts conditions, carry out catalytic reaction; Described heating in-furnace temperature 200-260 DEG C; Temperature 65-70 DEG C in described vaporizer;
Step (1) products therefrom enter cooler (4) and cool, the outlet temperature of cooler is 40-50 DEG C;
(3) the material (2) cooled through step enters high-pressure gas-liquid knockout drum (5) and carries out gas-liquid separation, and gas phase enters a point flow container (7) through compressor (6); Liquid phase enters stabilizer (9);
(4) enter the material of a point flow container (7) through gas-liquid separation, gas-liquid two-phase enters absorption and desorption tower (8) respectively;
(5) process through absorption and desorption tower (8) liquid phase obtained and enter stabilizer (9);
(6) be separated through stabilizer (9) liquid phase obtained and divide two strands of materials, one material returns absorption and desorption tower (8) as absorbent, and another strand of material enters fractionating column (10);
(7) be separated through fractionating column (10).
6. the method according to claim 5 or 6, is characterized in that,
The methyl alcohol gasified through vaporizer (1) divides two strands to enter fixed bed reactors (3); Bed is entered respectively through gas distributor A (11) and gas distributor B (12).
7. the method according to claim 5 or 6, is characterized in that,
Reaction pressure 0.8 ~ the 1.8Mpa of described fixed bed reactors (3), reaction temperature 260 ~ 450 DEG C; , reaction velocity 1 ~ 4h -1.
8. the method according to claim 5 or 6, is characterized in that,
Described catalyst is ZSM-5, ZSM-11, MCM-68, ZSM-12 or ZSM-48.
9. the method according to claim 5 or 6, is characterized in that,
Operating pressure 0.4 ~ the 0.5Mpa of described high-pressure gas-liquid knockout drum (5), operating temperature 40 ~ 55 DEG C; The outlet pressure of described compressor (6) is 1.1-1.4MPa; .
10. the method according to claim 5 or 6, is characterized in that,
The operating pressure 1.1-1.4MPa of described absorption and desorption tower (8), tower top operating temperature 40-50 DEG C, operating temperature 170-180 DEG C at the bottom of tower;
Described stabilizer (9) tower top adopts cold reflux, adopts kettle type reboiler, operating pressure 1.1 ~ 1.3Mpa at the bottom of tower; Tower top operating temperature 50 ~ 60 DEG C; Operating temperature 200-210 DEG C at the bottom of tower;
Operating pressure 0.1 ~ the 0.15Mpa of described fractionating column (10); Tower top operating temperature 131-142 DEG C, operating temperature 200-210 DEG C at the bottom of tower.
CN201511026372.2A 2015-12-31 2015-12-31 Preparing gasoline by methanol device and method Expired - Fee Related CN105396514B (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106518592A (en) * 2016-11-04 2017-03-22 中石化炼化工程(集团)股份有限公司 Method and device for preparing gasoline and durene through methyl alcohol
WO2018006714A1 (en) * 2016-07-08 2018-01-11 鲁盈 Process for preparing gasoline from methanol by means of combined bed

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