CN107963956A - A kind of method and system of methanol light aromatics - Google Patents
A kind of method and system of methanol light aromatics Download PDFInfo
- Publication number
- CN107963956A CN107963956A CN201610905980.9A CN201610905980A CN107963956A CN 107963956 A CN107963956 A CN 107963956A CN 201610905980 A CN201610905980 A CN 201610905980A CN 107963956 A CN107963956 A CN 107963956A
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- Prior art keywords
- methanol
- light aromatics
- circulating air
- gas
- superheater
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- 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
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/12—Liquefied petroleum gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/56—Specific details of the apparatus for preparation or upgrading of a fuel
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention provides a kind of method and system for realizing methanol light aromatics.Described method includes following steps：By material benzenemethanol by boosting, preheating, vaporization, overheat, catalysis, cooling, separation and etc. handled, finally obtain light aromatics product.Meanwhile the accessory substance circulating air produced in process of production carries out Recycling, and heat exchange loop is devised in systems, improve utilization rate of the system to material and energy.The method and system of the present invention realizes methanol light aromatics, produces the light aromatics of high value, meets China market light aromatics demand in short supply, improves the economy and commercial value of methanol light aromatics technology.
Description
Technical field
It is being catalyzed the present invention relates to a kind of process and system of methanol hydrocarbon, more particularly to using methanol as raw material
Light aromatics processed is realized under the action of agent（Benzene,toluene,xylene mixture）Method and system, the present invention be suitable for methanol system
Aromatic hydrocarbons improves the selectivity of methanol light aromatics.
Background technology
At present, it is increasing to light aromatics demand with the development of Chinese national economy.In order to meet market need
Will, the economy of methanol enterprise is improved, a kind of methanol of present invention offer is realized under the action of catalyst produces light aromatics, and
The method for recycling its byproduct dry gas.
The content of the invention
The technical problems to be solved by the invention are：Methanol and circulating air are raw material, under the action of catalyst, catalysis weight
Whole reduction heavy hydrocarbons content, increases light aromatics content, improves the selectivity of methanol light aromatics, improves that methanol system is with light packs to put
Economy.
The present invention solves above-mentioned technical problem by following technological means：
There is provided a kind of method for realizing methanol light aromatics, it is characterised in that include the following steps：
A. material benzenemethanol feeding methanol booster is boosted；
B. the methanol after boosting is sent into preheating device preheating, is then re-fed into vapourizing unit and vaporizes；Methanol after vaporization and
It is re-fed into superheater and carries out Overheating Treatment；
C. overheat after methanol enter catalytic reactor carry out catalytic reaction, the catalytic reactor must controlling reaction temperature,
Pressure and mass space velocity；
D. the output object of catalytic reactor input cooler is cooled down, be then fed into gas-oil-water three-phase separator into
The isolated liquefied petroleum gas of row and light aromatics product mixture and circulating air, liquefied petroleum gas and the light aromatics production
Product mixture is then sent through stabilizer separating treatment, obtains liquefied petroleum gas product and light aromatics product；Gas-oil-the water three
The water that phase separator is isolated mutually makees outer row's processing.
Preferably：Circulation air pressure is sent to by the circulating air of the gas-oil-water three-phase separator output in the step D
The boosting of contracting machine, circulating air heating devices heat, then again with being sent into superheater one described in step B after the methanol of vaporization converges
With Overheating Treatment is carried out, finally it is sent into catalytic reactor and carries out catalytic reaction；The circulating air of the recycle gas compressor boosting
Superpressure part do outer row processing.
Preferably：The product of catalytic reactor described in step C crosses hot charging before cooler is entered, followed by described
Put, circulating air heating unit, vapourizing unit, preheating device carry out heat exchange.
Preferably：The purity of methanol in the step A is：90~99.9%, its pressure after boosting is 2.0~2.5
MPa；Pressure after the boosting of the circulating air is 2.0~2.5 MPa.
Preferably：The outlet temperature of superheater is 300 DEG C ± 10 DEG C in the step B；Cooling in the step D
The cooling temperature of device is 45 DEG C ± 5 DEG C.
Preferably：Catalytic reactor is divided into two sections in the step C：ZSM-5 catalyst is housed at first and second section,
Controlling reaction temperature is 400~420 DEG C in one section of catalytic reaction process, and pressure be 2.0~2.5 MPa, mass space velocity is 20~
50 h-1；Controlling reaction temperature is 390~410 DEG C in second segment catalytic reaction process, and pressure is 2.0~2.5 MPa, quality
Air speed is 0.9~1.2 h-1。
Preferably：Circulating air after the boosting that recycle gas compressor produces is delivered to the second segment of the catalytic reactor
Input terminal, to reduce system temperature.
Additionally provide a kind of system for realizing methanol light aromatics, it is characterised in that：
Including methanol booster, preheating device, vapourizing unit, superheater, catalytic reactor, cooler, gas-oil-water three-phase
The main preparation system that separator, stabilizer are linked in sequence；
Material benzenemethanol is sent into preheating device preheating after the boosting of methanol booster, vapourizing unit heating vaporizes, superheater carries out
Overheat, catalytic reactor catalytic reaction, then send to cooler and cool down again, finally by gas-oil-water three-phase separator output circulation
Gas and liquefied petroleum gas and light aromatics mixture and outer draining, liquefied petroleum gas therein pass through again with light aromatics mixture
Stabilizer separating treatment obtains liquefied petroleum gas product and light aromatics product.
Preferably：Between the catalytic reactor output terminal and the input terminal of cooler, it is sequentially connected superheater, follows
Ring gas heating unit, vapourizing unit, preheating device with formed thermal energy recycling thermal cycle passage；The catalytic reactor output
Product pass through superheater, circulating air heating unit, vapourizing unit, preheating device carry out heat exchange；
Also in the gas-connection circulation air pressure between the gas phase outlet of oil-water three-phase separator and the input terminal of superheater
Contracting machine and circulating air heating unit are filled with being formed by the gas-oil-water three-phase separator, recycle gas compressor, circulating air heating
Put the bypath system of the circulating air recycling formed with superheater；
The circulating air send again to recycle gas compressor boosting, circulating air heating devices heat, then again with after the vaporization
Methanol enters the superheater after converging and carries out cycling and reutilization.
Preferably：The catalytic reactor is divided into two sections：ZSM-5 catalyst is housed at first and second section, is catalyzed in first segment
Controlling reaction temperature is 400~420 DEG C in reaction process, and pressure is 2.0~2.5 MPa, and mass space velocity is 20~50 h-1；
Controlling reaction temperature is 390~410 DEG C in second segment catalytic reaction process, and pressure is 1.9~2.5 MPa, mass space velocity 0.9
~1.2 h-1。
Preferably：It is described to follow in the output terminal of the second segment input terminal connection recycle gas compressor of the catalytic reactor
Circulating air after the boosting that ring air compressor produces is sent to the input terminal of the catalytic reactor second segment, to reduce system temperature
Degree.
Brief description of the drawings
Fig. 1 is the process flow chart for the method and system that the present invention realizes methanol light aromatics.
Embodiment
With reference to the accompanying drawings and embodiments to further instruction of the present invention.
As shown in Figure 1, the present invention realizes that the system of methanol light aromatics includes：Methanol booster 1, preheating device 2, vapour
The master that 3, superheater 4, catalytic reactor 5, cooler 6, gas-oil-water three-phase separator 7, stabilizer 8 are linked in sequence is put in makeup
Preparation system.
Be additionally included between the gas phase outlet of the gas-oil-water three-phase separator 7 and the input terminal of superheater 4 according to
Secondary connection recycle gas compressor 9 and circulating air heating unit 10 are with formation by the gas-oil-water three-phase separator 7, circulation air pressure
The bypath system for the circulating air recycling that contracting machine 9, circulating air heating unit 10 and superheater 4 are formed.
Be additionally included between the input terminal of 5 output terminal of catalytic reactor and cooler 6, be sequentially connected superheater 4,
Circulating air heating unit 10, vapourizing unit 3, preheating device 2 with formed thermal energy recycling thermal cycle passage；The catalytic reaction
The product that device 5 exports passes through superheater 4, circulating air heating unit 10, vapourizing unit 3, preheating device 2 and carries out heat exchange
And by heat exchange to above device, and the high-temperature product is cooled down, improve the heat utilization rate of system.
Preheating device 3, vapourizing unit 4, superheater and circulating air heating unit 12 include electric heater and heat exchanger.
The catalytic reactor 5 is divided to for two sections：ZSM-5 catalyst is housed at first and second section, in first segment catalytic reaction mistake
Controlling reaction temperature is 400~420 DEG C in journey, and pressure is 2.0~2.5 MPa, and mass space velocity is 20~50 h-1；In second segment
Controlling reaction temperature is 390~410 DEG C in catalytic reaction process, and pressure is 1.9~2.5 MPa, and mass space velocity is 0.9~1.2
h-1；In the second segment front end of the catalytic reactor 5, following after boosting caused by the recycle gas compressor 9 can be passed through
Ring gas, to reduce system temperature.
Based on the above-mentioned system for realizing methanol light aromatics, the present invention realizes the process bag of methanol light aromatics
Include following steps：
A. material benzenemethanol is respectively fed to methanol booster 1 to boost；
B. the methanol after boosting is sent into preheating device 2 to preheat, is then re-fed into vapourizing unit 3 and vaporizes；Methanol after vaporization
It is re-fed into superheater 4 and carries out Overheating Treatment, the outlet temperature of superheater 4 is 300 DEG C ± 10 DEG C；
C. the methanol after overheating enters catalytic reactor 5 and carries out catalytic reaction, and the catalytic reactor 5 must control reaction temperature
Degree, pressure and mass space velocity；
D. the output object input cooler 6 of the catalytic reactor 5 is cooled down, cooling temperature is 45 DEG C ± 5 DEG C, is then sent
Enter gas-oil-water three-phase separator 7 and carry out isolated liquefied petroleum gas and light aromatics product mixtures and circulating air, institute
State liquefied petroleum gas and light aromatics product mixtures are then sent through 8 separating treatment of stabilizer, obtain light aromatics product and liquefaction
Oil gas product；The water that the gas-oil-water three-phase separator 7 is isolated mutually makees outer row's processing.
Pass through circulating air recycling in the circulating air that the step D is exported by the gas-oil-water three-phase separator 7
Bypath system be sent to that recycle gas compressor 9 boosts, circulating air heating unit 10 heats, then again with the step B
Superheater 4 is sent into after the methanol of vaporization converges and together carries out Overheating Treatment, is finally sent into catalytic reactor 5 and is catalyzed
Reaction；Do outer row's processing in the superpressure part for the circulating air that the recycle gas compressor 9 boosts.
Embodiment one
According to the requirement of above-mentioned technological process, 100 kg/h of methanol flow, methanol composition are controlled：99.9%, circulating air flow 500
Kg/h, circulating air composition:H2 10% CH4 60% C2H4 10% C2H620%；Above-mentioned methanol and circulating air boost to 2.0
MPa。
5 first segment of catalytic reactor is in 20 h of mass space velocity-1, 410 DEG C of temperature, 2.2 MPa of pressure；, second segment is in quality
1.2 h of air speed-1, 390 DEG C of temperature, the process conditions of 2.1 MPa of pressure；
Reaction result is as follows:The isolated light aromatics product of stabilizer 8, contains through analysis：1.32% toluene 13.18% of benzene
Dimethylbenzene 32.54%.
Embodiment two
According to the requirement of above-mentioned technological process, 200 kg/h of methanol flow, methanol composition are controlled：95.0%, circulating air flow 900
kg/h.Circulating air forms：H2 10% CH4 60% C2H4 10% C2H620%；Above-mentioned methanol and circulating air boost to 2.1
MPa。
5 first segment of catalytic reactor is in 25 h of mass space velocity-1, 400 DEG C of temperature, 2.0 MPa of pressure；, second segment is in quality
1.0 h of air speed-1, 380 DEG C of temperature, the process conditions of 2.5 MPa of pressure；
Reaction result is as follows:The isolated light aromatics product of stabilizer 8, contains through analysis：1.67% toluene 18.29% of benzene
Dimethylbenzene 42.75%.
Embodiment three
According to the requirement of above-mentioned technological process, 100 kg/h of methanol flow, methanol composition are controlled：90.0%, circulating air flow 300
Kg/h, circulating air composition:H2 10% CH4 60% C2H4 10% C2H620%；Above-mentioned methanol and circulating air boost to
2.5MPa。
5 first segment of catalytic reactor is in 50 h of mass space velocity-1, 420 DEG C of temperature, 2.5 MPa of pressure；Second segment is in quality
Air speed 1.2h-1, 410 DEG C of temperature, the process conditions of 1.9 MPa of pressure；
Reaction result is as follows:The isolated light aromatics product of stabilizer 8, contains through analysis：1.81% toluene 22.14% of benzene
Dimethylbenzene 48.85%.
The foregoing is merely the preferred embodiment of the present invention, is not intended to limit the invention.To those skilled in the art
For, the invention may be variously modified and varied, within the spirit and principles of the invention, any modification for being made, etc.
With replacement, improvement etc., should all be included in the protection scope of the present invention.
Claims (11)
- A kind of 1. method for realizing methanol light aromatics, it is characterised in that include the following steps：A. material benzenemethanol is sent into methanol booster（1）Boost；B. the methanol after boosting is sent into preheating device（2）Preheating, is then re-fed into vapourizing unit（3）Middle vaporization；After vaporization Methanol and it is re-fed into superheater（4）Carry out Overheating Treatment；C. the methanol after overheating enters catalytic reactor（5）Carry out catalytic reaction, the catalytic reactor（5）It must control anti- Answer temperature, pressure and mass space velocity；D. by the catalytic reactor（5）Output object input cooler（6）Cooled down, be then fed into gas-oil-water three-phase separate From device（7）Carry out isolated liquefied petroleum gas and light aromatics product mixture and circulating air, the liquefied petroleum gas and Light aromatics product mixture is then sent through stabilizer（8）Separating treatment, obtains liquefied petroleum gas product and light aromatics product；Institute State gas-oil-water three-phase separator（8）The water isolated mutually makees outer row's processing.
- 2. the method according to claim 1 for realizing methanol light aromatics, it is characterised in that：In the step D by institute State gas-oil-water three-phase separator（7）The circulating air of output is sent to recycle gas compressor（9）Boosting, circulating air heating unit （10）Heating, then again with being sent into superheater after the methanol of vaporization converges described in step B（4）Overheating Treatment is together carried out, Finally it is sent into catalytic reactor（5）Middle carry out catalytic reaction；The recycle gas compressor（9）The superpressure part of the circulating air of boosting Do outer row's processing.
- 3. the method according to claim 1 for realizing methanol light aromatics, it is characterised in that：It is catalyzed described in step C anti- Answer device（5）Product into cooler（6）Before, followed by the superheater（4）, circulating air heating unit（10）、 Vapourizing unit（3）, preheating device（2）Carry out heat exchange.
- 4. the method according to claim 1 or 2 for realizing methanol light aromatics, it is characterised in that：In the step A The purity of methanol is：90~99.9%, the pressure after it boosts is 2.0~2.5 MPa；Pressure after the boosting of the circulating air For 2.0~2.5 MPa.
- 5. the method according to claim 1 for realizing methanol light aromatics, it is characterised in that：Overheated in the step B Device（4）Outlet temperature be 300 DEG C ± 10 DEG C；Cooler in the step D（6）Cooling temperature be 45 DEG C ± 5 DEG C.
- 6. the method according to claim 1 for realizing methanol light aromatics, it is characterised in that：It is catalyzed in the step C Reactor（5）It is divided into two sections：ZSM-5 catalyst is housed at first and second section, the control reaction temperature in first segment catalytic reaction process Spend for 400~420 DEG C, pressure is 2.0~2.5 MPa, and mass space velocity is 20~50 h-1；In second segment catalytic reaction process Controlling reaction temperature is 390~410 DEG C, and pressure is 2.0~2.5 MPa, and mass space velocity is 0.9~1.2 h-1。
- 7. the method according to claim 6 for realizing methanol light aromatics, it is characterised in that：Recycle gas compressor（10） Circulating air after the boosting of generation is delivered to the catalytic reactor（5）Second segment input terminal, to reduce system temperature.
- A kind of 8. system for realizing methanol light aromatics, it is characterised in that：Including methanol booster（1）, preheating device（2）, vapourizing unit（3）, superheater（4）, catalytic reactor（5）, cooling Device（6）, gas-oil-water three-phase separator（7）, stabilizer（8）The main preparation system being linked in sequence；Material benzenemethanol is through methanol booster（1）Preheating device is sent into after boosting（2）Preheating, vapourizing unit（3）Heating vaporization, overheat Device（4）Overheated, catalytic reactor（5）Catalytic reaction, then send to cooler again（6）Cooling, finally by gas-oil-water Three phase separator（7）Export circulating air and liquefied petroleum gas and light aromatics mixture and outer draining, liquefied petroleum therein Gas is with light aromatics mixture again through stabilizer（8）Separating treatment obtains liquefied petroleum gas product and light aromatics product.
- 9. the system according to claim 8 for realizing methanol light aromatics, it is characterised in that：In the catalytic reactor （5）Output terminal and cooler（6）Input terminal between, be sequentially connected superheater（4）, circulating air heating unit（10）, vaporization Device（3）, preheating device（2）To form the thermal cycle passage of thermal energy recycling；The catalytic reactor（5）The product of output is again Flow through superheater（4）, circulating air heating unit（10）, vapourizing unit（3）, preheating device（2）Carry out heat exchange；Also in the gas-oil-water three-phase separator（7）Gas phase outlet and superheater（4）Input terminal between connect and follow Ring air compressor（9）With circulating air heating unit（10）To be formed by the gas-oil-water three-phase separator（7）, cycle compressor Machine（9）, circulating air heating unit（10）And superheater（4）The bypath system of the circulating air recycling formed；The circulating air is sent to recycle gas compressor again（9）Boosting, circulating air heating unit（10）Heating, then again with the vapour Methanol after change enters the superheater after converging（4）Carry out cycling and reutilization.
- 10. the system according to claim 8 for realizing methanol light aromatics, it is characterised in that：The catalytic reactor （5）It is divided into two sections：ZSM-5 catalyst is housed at first and second section, controlling reaction temperature is in first segment catalytic reaction process 400~420 DEG C, pressure is 2.0~2.5 MPa, and mass space velocity is 20~50 h-1；Controlled in second segment catalytic reaction process Reaction temperature is 390~410 DEG C, and pressure is 1.9~2.5 MPa, and mass space velocity is 0.9~1.2 h-1。
- 11. the system according to claim 10 for realizing methanol light aromatics, it is characterised in that：In the catalytic reaction Device（5）Second segment input terminal connection recycle gas compressor（9）Output terminal, the recycle gas compressor（9）The boosting of generation Circulating air afterwards is sent to the catalytic reactor（5）The input terminal of second segment, to reduce system temperature.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201610905980.9A CN107963956A (en) | 2016-10-19 | 2016-10-19 | A kind of method and system of methanol light aromatics |
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| CN201610905980.9A CN107963956A (en) | 2016-10-19 | 2016-10-19 | A kind of method and system of methanol light aromatics |
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| CN201610905980.9A Pending CN107963956A (en) | 2016-10-19 | 2016-10-19 | A kind of method and system of methanol light aromatics |
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102391888A (en) * | 2011-09-23 | 2012-03-28 | 冯保运 | Process for producing methanol-to-hydrocarbon-based fuel (MTHF) |
| CN104496743A (en) * | 2014-11-27 | 2015-04-08 | 山西沸石科技有限公司 | Method for preparing aromatic hydrocarbon mixture rich in benzene, toluene and xylene (BTX) by conversion of methanol in fixed bed reactor |
-
2016
- 2016-10-19 CN CN201610905980.9A patent/CN107963956A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102391888A (en) * | 2011-09-23 | 2012-03-28 | 冯保运 | Process for producing methanol-to-hydrocarbon-based fuel (MTHF) |
| CN104496743A (en) * | 2014-11-27 | 2015-04-08 | 山西沸石科技有限公司 | Method for preparing aromatic hydrocarbon mixture rich in benzene, toluene and xylene (BTX) by conversion of methanol in fixed bed reactor |
Non-Patent Citations (1)
| Title |
|---|
| 王永刚等: "《煤化工工艺学》", 30 September 2014, 中国矿业大学出版社 * |
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