CN106608800A - Methanol-to-aromatic hydrocarbon lightweight product treatment method - Google Patents
Methanol-to-aromatic hydrocarbon lightweight product treatment method Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
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- C07C7/005—Processes comprising at least two steps in series
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- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
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- C—CHEMISTRY; METALLURGY
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- 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
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
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- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
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Abstract
The present invention relates to a methanol-to-aromatic hydrocarbon lightweight product treatment method. A purpose of the present invention is mainly to solve the problem of high gas separation energy consumption in the methanol-to-aromatic hydrocarbon lightweight product utilization process. The technical scheme of the present invention comprises that a methanol aromatization product is separated into a gas phase, an oil phase and a water phase in a three-phase separation unit; the gas phase is compressed and then is conveyed into a membrane separation unit so as to be separated into hydrogen-rich gas and poor hydrogen gas; the poor hydrogen gas is cooled and then is conveyed into a first gas-liquid separation unit so as to be separated into first methane-rich gas and a first poor methane liquid; the first methane-rich gas is separated into second methane-rich gas and a second poor methane liquid; the second methane-rich gas is conveyed into a gas separation unit so as to be separated into methane gas and the streams of hydrocarbons having a carbon atom number of more than or equal to 2; and the streams of the hydrocarbons having a carbon atom number of more than or equal to 2, the first poor methane liquid and the second poor methane liquid are conveyed into a light hydrocarbon reactor and are converted into the light hydrocarbon aromatization product. With the technical scheme, the problem in the prior art is well solved. The method of the present invention can be used for the industrial production of aromatic hydrocarbons.
Description
Technical field
The present invention relates to a kind of processing method of methanol arene light product.
Technical background
Aromatic hydrocarbons, particularly light aromatics BTX (benzene,toluene,xylene), are important basic organic chemical industry raw materials, its
Yield is with scale inferior to ethylene and propylene.The main source of aromatic hydrocarbons is Petroleum catalytic reforming.It is rich with reference to coal resources in China
The rich and higher and higher national conditions of oil interdependency, coal aromatic hydrocarbons technology of the development with cost of material advantage becomes grinding for last decade
Study carefully focus, and break through in acquisition of technology in recent years, especially coal-based methanol aromatic hydrocarbons technology has been completed that Industrial demonstration is tested.
One big feature of methanol aromatic hydrocarbons technology is that product species is various, not only comprising target products such as aromatic hydrocarbons, is also included
The third low-carbon (LC) hydro carbons of methane, the carbon of carbon two, and a large amount of hydrogen of by-product.In order to improve the yield of aromatic hydrocarbons, need to lower carbon number hydrocarbons
Class is reclaimed and aromatisation, and separates hydrogen as high value added product to improve the overall economy quality of device.Due to light
The separation of the separation of matter hydro carbons, especially methane and carbon two, needs to consume substantial amounts of cold, causes plant energy consumption height, flow process
Long, investment is big, constrains popularization and the industrial applications of methanol aromatic hydrocarbons technology.
Patent CN101823929 discloses the system and technique of a kind of methanol or dimethyl ether conversion preparing aromatic hydrocarbon.Material benzenemethanol
Or dimethyl ether is reacted first in raw material aromatization reactor, reacted product Jing three phase separation units are separated into gas
Oil phase and water based on phase lighter hydrocarbons, aromatic hydrocarbons.In order to improve the selectivity and yield of aromatic hydrocarbons, three technical sides are the patent provides
Case.In first technical scheme, the C separated in product2+ non-aromatics is first in low-carbon alkene aromatization
Aromatization is carried out in device, aromatic hydrocarbons and lighter hydrocarbons are then demultiplex out, hydrogen methane blended gas is isolated from lighter hydrocarbons, then from
In isolate hydrogen product and methane product, remaining lighter hydrocarbons send into low-carbon (LC) hydro carbons aromatization reactor, and product returns three-phase separate
From unit.In addition, benzene, toluene and part C9+ hydro carbons sends into aromatic disproportion reactor and generates C8 aromatic hydrocarbons, same to return
Three phase separation unit.Hydrogen, methane, mixing C8Aromatic hydrocarbons and part C9+ hydro carbons is used as output of products system.The second of patent
Individual technical scheme provides simplified technological process, and lighter hydrocarbons isolate first hydrogen methane blended gas, then therefrom isolate
Hydrogen product and methane product, the lighter hydrocarbons for removing methane, hydrogen send into low-carbon (LC) hydro carbons aromatization reactor, and product returns three
Separation units, that is, be not provided with low-carbon alkene aromatization reactor.3rd technical scheme of patent is in previous technical scheme
On the basis of done further simplification, detached benzene, toluene and part C from oil phase aromatic hydrocarbons9+ hydro carbons does not send into aromatic hydrocarbons
Disproportionation reactor, directly returns in raw material aromatization reactor.The technical scheme is adopted and second technical scheme phase to lighter hydrocarbons
Same processing method.Three technical schemes of the patent all adopt from lighter hydrocarbons separation of methane hydrogen mixture and then therefrom first
The processing method of separation of methane and hydrogen.The method disclosed in the patent is proposed with the first that absorption and desorption or rectification are separated in lighter hydrocarbons
Alkane hydrogen mixture.Because hydrogen content is high in lighter hydrocarbons, when the method using absorption and desorption, ethylene concentration is low in lighter hydrocarbons,
Substantial amounts of absorbent is needed just to can guarantee that the response rate of ethylene, therefore high energy consumption；When using cryogenic separation, due in hydro carbons
Hydrogen content is high, and tower top temperature is very low, and cold consumes big, high energy consumption.
Prior art has that gas separating energy consumption is high during methanol arene light product utilization, and the present invention is directed to
Property solves the problems referred to above.
The content of the invention
The technical problem to be solved is the presence of gas during methanol arene light product utilization in prior art
A kind of high problem of separating energy consumption, there is provided processing method of new methanol arene light product.The device has energy consumption low
Advantage.
To solve the above problems, the technical solution used in the present invention is as follows：A kind of processing method of methanol arene light product,
Comprise the following steps：1) methanol is converted into aromatization of methanol product in methanol reactor；2) aromatization of methanol product is three
Gas phase, oil phase and water phase are separated in separation units；3) gas phase sends into after compression film separation unit and is separated into hydrogen rich gas
Body and hydrogen depleted gas；4) hydrogen depleted gas send into after cooling the first gas-liquid separation unit and are separated into the first methane-rich gas and
One poor methane liquid；5) the first methane-rich gas are further compressed, send into the second gas-liquid separation unit and be separated into after cooling
Second methane-rich gas and the second poor methane liquid；6) the second methane-rich gas send into edema caused by disorder of QI unit and are separated into methane gas and carbon
Two and more heavy hydrocarbons logistics；7) carbon two and more heavy hydrocarbons logistics, the first poor methane liquid and the second poor methane liquid are sent into light
Hydrocarbon reactor is converted into light-hydrocarbon aromatized product；8) light-hydrocarbon aromatized product returns three phase separation unit.
In above-mentioned technical proposal, it is preferable that the step 2) in gas phase the volume fraction of hydrogen be 40～70%.
In above-mentioned technical proposal, it is preferable that the step 3) in film separation unit using rolled film, hollow fiber form film or
One kind in plate and frame film.
In above-mentioned technical proposal, it is preferable that the step 3) in gas phase after compression pressure limit be 2～3MPa.
In above-mentioned technical proposal, it is preferable that the step 3) in gas phase send into film separation unit before be first fed into caustic wash tower
Sour gas and water are removed with exsiccator.
In above-mentioned technical proposal, it is preferable that the step 3) in hydrogen-rich gas Jing supercharging after send into PSA unit obtain it is high-purity
Hydrogen.
In above-mentioned technical proposal, it is preferable that the step 4) in hydrogen depleted gas Jing heat exchangers be cooled to less than 50 DEG C and send into
One gas-liquid separation unit.
In above-mentioned technical proposal, it is preferable that the step 5) in the first methane-rich gas Jing after being pressurized to 3～4MPa, Jing
Heat exchanger is cooled to less than 10 DEG C and sends into the second gas-liquid separation unit.
In above-mentioned technical proposal, it is preferable that the step 6) in edema caused by disorder of QI unit using cryogenic separation methane and carbon two and heavier
Hydrocarbon material flow.
Using the method for the present invention, water phase is obtained from the high-temperature product Jing three phase separations of methanol aromatic hydrocarbons reactor, comprising weight
The oil phase of matter hydro carbons such as benzene,toluene,xylene and comprising hydrogen and light hydrocarbons product for example methane, ethylene, ethane, propylene,
The gas phase of propane.Due in methanol aromatization course of reaction with substantial amounts of hydrogen, therefore in gas phase containing be more than 30% volume integral
Several hydrogen.Because the reaction of methanol aromatization generally occurs under the pressure less than 0.5MPa, therefore from three phase separation list
The gas phase of unit generally boosts to more than 2MPa firstly the need of through compressor, is beneficial to membrance separation hydrogen.In addition, in order to keep away
Exempt to ensure the efficiency of membrance separation and the service life of film, the gas after boosting is first fed into caustic wash tower and exsiccator removes respectively acid
Property gas and water, then isolate the hydrogen-rich gas of hydrogen volume fraction about 90% in film separation unit, and hydrogen recovery rate is big
In 85%.In preferably scheme, this part hydrogen-rich gas sends into PSA devices and volume fraction 99% is obtained after being pressurized
Pure hydrogen production above, improves value of the product.The pressure drop of film separation unit retentate side is little, and the hydrogen depleted gas pressure of acquisition exists
1.5MPa more than.Jing hydrogen depleted gas heat exchanger cooling after, be separated in the first knockout drum the first methane-rich gas and
First poor methane liquid.Wherein the first methane-rich gas send into the second gas-liquid separation unit Jing after supercharging, are further separated into the
Two methane-rich gas and the second poor methane liquid.Second methane-rich gas are separated into first in edema caused by disorder of QI unit using the method for rectification
Alkane and carbon two and more heavy constituent.
In preferably scheme, hydrogen depleted gas are separated into the first high methane gas after being cooled to 40 DEG C in the first gas-liquid separator
Body and the first poor methane liquid, wherein the first methane-rich gas include the methane at least 80% hydrogen depleted gas.Subsequently, first
Methane-rich gas are pressurized to after 3.5MPa to be sent into after being cooled to 10 DEG C be separated in the second gas-liquid separator the second methane-rich gas
With the second poor methane liquid, wherein the second methane-rich gas include the methane at least the 80% the first methane-rich gas.Second is rich
Methane gas sends into domethanizing column, is separated using cryogenic rectification method well known to those skilled in the art, the carbon two of acquisition and more
Heavy hydrocarbons logistics is sent into together light-hydrocarbon aromatized as light-hydrocarbon aromatized raw material and from the poor methane liquid of gas-liquid separator
In reactor, further increase production aromatic hydrocarbons.
Using technical scheme, have the advantage that：1) removing is most of before hydrogen depleted gas enter edema caused by disorder of QI unit
Hydrogen, reduces the energy consumption of the first high methane gas gas compressor, at the same reduce the first methane-rich gas cooler energy consumption and
Improve the tower top temperature of domethanizing column；2) poor methane liquid is isolated by two-stage gas-liquid separation unit, is further reduced
Edema caused by disorder of QI unit feed load, is especially reduction of the concentration of carbon three and more heavy constituent in edema caused by disorder of QI unit feed, reduces separating energy
Consumption.Using the method for the present invention front dehydrogenation high pressure cryogenic separation methane, hydrogen more widely used than prior art method energy consumption extremely
36% is reduced less, achieves preferable technique effect.
Description of the drawings
Fig. 1 is the schematic flow sheet of the method for the invention.
In Fig. 1,1 is methanol；2 is aromatization of methanol product；3 is gas phase；4 is gas phase compressor outlet logistics；5
For hydrogen-rich gas；6 is hydrogen depleted gas；7 is the first methane-rich gas；8 is the first poor methane liquid；9 is the second methane rich
Gas；10 is the second poor methane liquid；11 is methane；12 is carbon two and more heavy hydrocarbons；13 is light-hydrocarbon aromatized product；
14 is oil phase；15 is non-aromatics；16 is aromatic hydrocarbons；17 is water；100 is methanol reactor；101 is three phase separator；
102 is gas phase compressor；103 is membrane separator；E1 is hydrogen depleted gas heat exchanger；104 is the first gas-liquid separator；105
For the first high methane gas gas compressor；E2 is the first methane-rich gas heat exchanger；106 is the second gas-liquid separator；107 are
Domethanizing column；108 is light hydrogen cracking device；109 is Aromatics Extractive Project unit.
In Fig. 1, methanol sends into methanol reactor and aromatization occurs in the presence of catalyst, generates high temperature methanol aromatization
Change product.It is separated into water phase in three phase separator after cooling, the oil phase comprising aromatic hydrocarbons such as benzene,toluene,xylenes and bag
The gas phase of the hydro carbons such as hydrogen and methane, ethylene, ethane, propylene, propane.Gas phase is sent first Jing after compressor boosting
Enter caustic wash tower and exsiccator removes respectively sour gas and water, hydrogen is then isolated in film separation unit.Film separation unit
Retentate side be hydrogen depleted gas, Jing hydrogen depleted gas heat exchanger cooling after, the first methane rich is separated in the first knockout drum
Gas and the first poor methane liquid.Wherein the first methane-rich gas send into the second gas-liquid separation unit Jing after supercharging, cooling, enter
One step is separated into the second methane-rich gas and the second poor methane liquid.Second methane-rich gas are separated into methane in domethanizing column
With carbon two and more heavy constituent.Carbon two and more heavy hydrocarbons logistics, from the first poor methane liquid and second of the first gas-liquid separator
Second poor methane liquid of gas-liquid separator is sent into together in light dydrocarbon aromatization reaction device, obtains lighter hydrocarbons aromatization product, and returns
Return three phase separator.
Below by embodiment, the invention will be further elaborated, but is not limited only to the present embodiment.
Specific embodiment
【Embodiment 1】
Technological process as shown in Figure 1.Scale is that the methanol Jing methanol reactors reaction of 225 ton hours is generated containing 1.2wt%
Hydrogen, 1.3wt% methane, 0.2wt% carbon dioxide, 55.4wt% water, carbon two are to carbon five hydro carbons 16.5wt% and 23.6wt%
The aromatization of methanol product of other hydro carbons, Jing heat exchange coolings, three phase separation obtain water phase, oil phase and gas phase, wherein gas phase matter
Amount flow is 45.6 ton hours, the hydrogen containing 53% volume fraction, the methane of 8% volume fraction, 0.5% volume fraction
The carbon two and its above hydro carbons of carbon dioxide, the carbon monoxide of 1.5% volume fraction and 34% volume fraction.The gas phase is through pressure
Contracting machine is boosted to after 2.8MPa, Jing caustic wash towers removing sour gas so as in the mass content of carbon dioxide be less than
5wppm, drying device removing water so as in water mass content be less than 3wppm, be then fed into film separation unit.Adopt
With hollow-fibre membrane, the infiltration gas of hydrogen volume fraction 89.7% is obtained, pressure is 2.1MPa.The infiltration gas is sent directly into
PSA devices are obtained 99.9% High Purity Hydrogen.The hydrogen depleted gas pressure of film separation unit retentate side is 2.7MPa, and temperature is 60 DEG C,
Mass flow is 38.9 ton hours, and the first gas-liquid separator is sent into Jing after hydrogen depleted gas heat exchanger is cooled to 40 DEG C, obtains matter
Amount flow is the first methane-rich gas of 28.9 ton hours and the first poor methane liquid of 10 ton hours.First methane-rich gas
The first methane-rich gas cooler is sent into Jing after compressor is pressurized to 3.8MPa and is cooled to 9 DEG C, then in the second gas-liquid separation
The second methane-rich gas and the second poor methane liquid are separated in device, wherein the mass fraction of methane is in the second poor methane liquid
2.4%.Methane-rich gas send into domethanizing column, and using cryogenic separation well known to those skilled in the art, operating pressure is
3.6MPa, tower top temperature is -118.8 DEG C, and bottom temperature is 21.4 DEG C, obtains methane and carbon two and more heavy hydrocarbons.Demethanation
Tower ethylene loss is less than 0.2%.Wherein methane can be utilized as fuel gas.Carbon two and more heavy hydrocarbons and the first poor methane liquid,
Second poor methane liquid then sends into light hydrogen cracking device generation aromatization and further increases production aromatic hydrocarbons, and product returns three-phase
Separator.
In the present embodiment, the second methane-rich gas energy consumption of compressor is 0.24MW, and compressor aftercooler energy consumption is 2.88MW,
The mass flow of domethanizing column charging is 12.1 ton hours, and the energy consumption of domethanizing column is 1.69MW.
【Comparative example 1】
Constituted using the product of embodiment 1, using the most widely used front dehydrogenation high pressure cryogenics in this area first is separated
Alkane, hydrogen and carbon two and more heavy hydrocarbons.Four sections of energy consumption of compressor are 0.79MW, and compressor aftercooler energy consumption is 4.1MW,
The mass flow of domethanizing column charging is 39.6 ton hours, and domethanizing column energy consumption is 2.5MW.
【Embodiment 2】
Technological process as shown in Figure 1.Scale is that 1,800,000 tons/year of methanol Jing methanol reactors reaction is generated containing 0.7wt%
Hydrogen, 1.5wt% methane, 0.2wt% carbon dioxide, 56.3wt% water, carbon two to carbon five hydro carbons 16.8wt% and 24.5wt%
The aromatization of methanol product of other hydro carbons, Jing heat exchange cooling, three phase separation obtain water phase, comprising heavy hydrocarbon for example benzene, toluene,
The oil phase of dimethylbenzene and the gas phase comprising hydrogen and light hydrocarbons product such as methane, ethylene, ethane, propylene, propane, wherein
Containing the hydrogen of 40.4% volume fraction in gas phase.After compressor boosts to 2.1MPa, Jing caustic wash towers are removed the gas phase
Sour gas so as in the mass content of carbon dioxide be less than 10wppm, drying device removing water so as in water
Mass content is less than 8wppm, is then fed into film separation unit.Using rolled film, oozing for hydrogen volume fraction 90.3% is obtained
Ventilative, pressure is 1.3MPa.The infiltration gas is sent directly into PSA devices and 99.9% High Purity Hydrogen is obtained.Film separation unit oozes remaining
The hydrogen depleted gas pressure of side is 2.0MPa, and mass flow is 38.9 ton hours, Jing after hydrogen depleted gas heat exchanger is cooled to 30 DEG C
Send into the first gas-liquid separator, obtain the of the first methane-rich gas that mass flow is 23.5 ton hours and 15.4 ton hours
One poor methane liquid.First methane-rich gas send into the first methane-rich gas cooler drop Jing after compressor is pressurized to 3.2MPa
Then temperature is separated into the second methane-rich gas and the second poor methane liquid, wherein second to 5 DEG C in the second gas-liquid separator
The mass fraction of methane is 2.1% in poor methane liquid.Methane-rich gas send into domethanizing column, using those skilled in the art
Well known cryogenic separation, operating pressure is 3.12MPa, and tower top temperature is -119.5 DEG C, and bottom temperature is 14 DEG C, obtains first
Alkane and carbon two and more heavy hydrocarbons.Demethanizer ethylene loss is less than 0.2%.Wherein methane can be utilized as fuel gas.Carbon two
And more heavy hydrocarbons and the first poor methane liquid, the second poor methane liquid then send into light hydrogen cracking device occur aromatization it is further
Volume increase aromatic hydrocarbons, and product returns three phase separator.
In the present embodiment, the second methane-rich gas energy consumption of compressor is 0.32MW, and compressor aftercooler energy consumption is 3.048MW,
The mass flow of domethanizing column charging is 12.6 ton hours, and the energy consumption of domethanizing column is 1.7MW.
【Embodiment 3】
Technological process as shown in Figure 1.Scale is that 1,800,000 tons/year of methanol Jing methanol reactors reaction is generated containing 2.5wt%
Hydrogen, 1.2wt% methane, 0.2wt% carbon dioxide, 55.5wt% water, carbon two to carbon five hydro carbons 16.6wt% and 24.0wt%
The aromatization of methanol product of other hydro carbons, Jing heat exchange cooling, three phase separation obtain water phase, comprising heavy hydrocarbon for example benzene, toluene,
The oil phase of dimethylbenzene and the gas phase comprising hydrogen and light hydrocarbons product such as methane, ethylene, ethane, propylene, propane, wherein
Containing the hydrogen of 69.5% volume fraction in gas phase.After compressor boosts to 2.5MPa, Jing caustic wash towers are removed the gas phase
Sour gas so as in carbon dioxide mass content be less than 6wppm, drying device removing water so as in water matter
Amount content is less than 3wppm, is then fed into film separation unit.Using plate and frame film, oozing for hydrogen volume fraction 92.3% is obtained
Ventilative, pressure is 1.8MPa.The infiltration gas is sent directly into PSA devices and 99.9% High Purity Hydrogen is obtained.Film separation unit oozes remaining
The hydrogen depleted gas pressure of side is 2.3MPa, and mass flow is 38.1 ton hours, Jing after hydrogen depleted gas heat exchanger is cooled to 45 DEG C
The first gas-liquid separator is sent into, acquisition mass flow is the first of the first methane-rich gas of 28 ton hours and 10.1 ton hours
Poor methane liquid.First methane-rich gas send into the cooling of the first methane-rich gas cooler Jing after compressor is pressurized to 3.5MPa
To 5 DEG C, the second methane-rich gas and the second poor methane liquid are then separated in the second gas-liquid separator, wherein second is lean
The mass fraction of methane is 2.3% in methane liquid.Methane-rich gas send into domethanizing column, ripe using those skilled in the art
The cryogenic separation known, operating pressure is 3.44MPa, and tower top temperature is -119.9 DEG C, and bottom temperature is 18.3 DEG C, obtains first
Alkane and carbon two and more heavy hydrocarbons.Demethanizer ethylene loss is less than 0.2%.Wherein methane can be utilized as fuel gas.Carbon two
And more heavy hydrocarbons and the first poor methane liquid, the second poor methane liquid then send into light hydrogen cracking device occur aromatization it is further
Volume increase aromatic hydrocarbons, and product returns three phase separator.
In the present embodiment, the second methane-rich gas energy consumption of compressor is 0.29MW, and compressor aftercooler energy consumption is 3.31MW,
The mass flow of domethanizing column charging is 11.1 ton hours, and the energy consumption of domethanizing column is 1.62MW.
The energy consumption comparison of comparative example 1 and embodiment 1 understands that, using the method for the present invention, total energy consumption is reduced than prior art
34.9%, achieve preferable technique effect.
Claims (9)
1. a kind of processing method of methanol arene light product, comprises the following steps：1) methanol is in methanol reactor transfer
Turn to aromatization of methanol product；2) aromatization of methanol product is separated into gas phase, oil phase and water phase in three phase separation unit；3)
Gas phase sends into after compression film separation unit and is separated into hydrogen-rich gas and hydrogen depleted gas；4) hydrogen depleted gas send into after cooling
One gas-liquid separation unit is separated into the first methane-rich gas and the first poor methane liquid；5) the first methane-rich gas Jing is further
The second gas-liquid separation unit is sent into after compression, cooling be separated into the second methane-rich gas and the second poor methane liquid；6) second
Methane-rich gas send into edema caused by disorder of QI unit and are separated into methane gas and carbon two and more heavy hydrocarbons logistics；7) carbon two and more heavy hydrocarbons logistics,
First poor methane liquid and the second poor methane liquid send into light hydrogen cracking device and are converted into light-hydrocarbon aromatized product；8) lighter hydrocarbons aromatization
Change product and return three phase separation unit.
2. the processing method of methanol arene light product according to claim 1, it is characterised in that the step 2) in
The volume fraction of hydrogen is 40～70% in gas phase.
3. the processing method of methanol arene light product according to claim 1, it is characterised in that the step 3) in
Film separation unit is using the one kind in rolled film, hollow fiber form film or plate and frame film.
4. the processing method of methanol arene light product according to claim 1, it is characterised in that the step 3) in
After compression pressure limit is 2～3MPa to gas phase.
5. the processing method of methanol arene light product according to claim 1, it is characterised in that the step 3) in
Gas phase is first fed into caustic wash tower before film separation unit is sent into and exsiccator removes respectively sour gas and water.
6. the processing method of methanol arene light product according to claim 1, it is characterised in that the step 3) in
Hydrogen-rich gas sends into PSA unit Jing after supercharging and obtains High Purity Hydrogen.
7. the processing method of methanol arene light product according to claim 1, it is characterised in that the step 4) in
Hydrogen depleted gas Jing heat exchangers are cooled to less than 50 DEG C and send into the first gas-liquid separation unit.
8. the processing method of methanol arene light product according to claim 1, it is characterised in that the step 5) in
Jing after being pressurized to 3～4MPa, Jing heat exchangers are cooled to less than 10 DEG C and send into the second gas-liquid separation unit first methane-rich gas.
9. the processing method of methanol arene light product according to claim 1, it is characterised in that the step 6) in
Edema caused by disorder of QI unit is using cryogenic separation methane and carbon two and more heavy hydrocarbons logistics.
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| CN101823929A (en) * | 2010-04-14 | 2010-09-08 | 清华大学 | System and process for preparing aromatic hydrocarbon by converting methanol or dimethyl ether |
| CN103086827A (en) * | 2013-01-28 | 2013-05-08 | 神华集团有限责任公司 | Olefin separation system and olefin separation method |
| CN103864565A (en) * | 2014-03-20 | 2014-06-18 | 华电煤业集团有限公司 | System and method of preparing paraxylene by alcohol/ether conversion |
| US20140171691A1 (en) * | 2012-12-13 | 2014-06-19 | Pioneer Energy Inc. | Synthesis of Drop-in Liquid Fuels and Chemicals from Methanol, Ethanol or Syngas Using Mixed Catalysts |
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2015
- 2015-10-22 CN CN201510690164.6A patent/CN106608800B/en active Active
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101823929A (en) * | 2010-04-14 | 2010-09-08 | 清华大学 | System and process for preparing aromatic hydrocarbon by converting methanol or dimethyl ether |
| US20140171691A1 (en) * | 2012-12-13 | 2014-06-19 | Pioneer Energy Inc. | Synthesis of Drop-in Liquid Fuels and Chemicals from Methanol, Ethanol or Syngas Using Mixed Catalysts |
| CN103086827A (en) * | 2013-01-28 | 2013-05-08 | 神华集团有限责任公司 | Olefin separation system and olefin separation method |
| CN103864565A (en) * | 2014-03-20 | 2014-06-18 | 华电煤业集团有限公司 | System and method of preparing paraxylene by alcohol/ether conversion |
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