CN107963954A - A kind of method and system of coupling between methanol light naphtha light aromatics - Google Patents
A kind of method and system of coupling between methanol light naphtha light aromatics Download PDFInfo
- Publication number
- CN107963954A CN107963954A CN201610905970.5A CN201610905970A CN107963954A CN 107963954 A CN107963954 A CN 107963954A CN 201610905970 A CN201610905970 A CN 201610905970A CN 107963954 A CN107963954 A CN 107963954A
- Authority
- CN
- China
- Prior art keywords
- methanol
- light
- naphtha
- gas
- circulating air
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- 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
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/86—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon
- C07C2/862—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon the non-hydrocarbon contains only oxygen as hetero-atoms
- C07C2/864—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon the non-hydrocarbon contains only oxygen as hetero-atoms the non-hydrocarbon is an alcohol
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a kind of method and system for realizing coupling between methanol light naphtha light aromatics.Described method includes following steps：By material benzenemethanol, light naphtha 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 coupling between methanol light naphtha light aromatics, produces the light aromatics of high value, meets China market aromatic hydrocarbon product demand in short supply, improves the economy and commercial value of methanol and naphtha light aromatics technology.
Description
Technical field
The present invention relates to a kind of process and system of coupling between methanol light naphtha hydrocarbon, more particularly to use methanol
Light naphtha is coupled as raw material, the method and system of realization light aromatics processed, the present invention are applicable under the action of catalyst
The selectivity of methanol light aromatics is improved in methanol light aromatics process.
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, and realize that the high value of refinery factory byproduct liquefied petroleum gas and dry gas resource utilizes, the economy of enterprise of refinery factory is improved,
The present invention provides a kind of coupling between methanol light naphtha and the method for producing light aromatics is realized under the action of catalyst.
The content of the invention
The technical problems to be solved by the invention are：With methanol and feed naphtha, 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 takes following technical proposal to solve above-mentioned technical problem：
There is provided a kind of method for realizing coupling between methanol light naphtha light aromatics, it is characterised in that include the following steps：
A. material benzenemethanol and raw material light naphtha are respectively fed to methanol booster and naphtha booster boosts；
B. preheating device preheating is sent into after converging the methanol after boosting and naphtha, is then re-fed into vapourizing unit and vaporizes；
Methanol and light naphtha after vaporization are re-fed into superheater and carry out Overheating Treatment；
C. methanol and light naphtha after overheating enter catalytic reactor and carry out catalytic reaction, and the catalytic reactor is necessary
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 mixtures and circulating air, liquefied petroleum gas and the light aromatics production
Thing mixture is then sent through stabilizer separating treatment, obtains light aromatics product；Gas-oil-the water three-phase separator is isolated
Water 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, send after then converging again with the methanol and light naphtha described in step B through vaporization
Enter superheater and together carry out Overheating Treatment, be finally sent into catalytic reactor and carry out catalytic reaction；The recycle gas compressor
Do outer row's processing in the superpressure part of the circulating air of boosting.
Preferably：The liquefied petroleum gas that the step D is isolated by stabilizer be sent to liquefied petroleum gas booster into
Row boosting, then converge latter same vapourizing unit of being sent into the methanol after preheating described in the step B and light naphtha and carry out
Vaporization process, is then fed into superheater and carries out Overheating Treatment.
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
The ratio of MPa, 2.0~2.5 MPa of pressure after the light naphtha boosting, the methanol and light naphtha is 4:6~10:
0；Pressure after the boosting of the circulating air is 2.0~2.5 MPa；Pressure is 2.0~2.5 after the liquefied petroleum gas boosting
MPa。
Preferably：The temperature of superheater is 300 DEG C ± 10 DEG C in the step B；Cooler in the step D
Cooling temperature 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 2.0~2.5MPa, and quality is empty
Speed is 0.9~1.2h-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 coupling between methanol light naphtha light aromatics, it is characterised in that：
Including methanol booster, naphtha booster, preheating device, vapourizing unit, superheater, catalytic reactor, cooler,
The main preparation system that gas-oil-water three-phase separator, stabilizer are linked in sequence；
Material benzenemethanol and raw material light naphtha converge feeding preheating after methanol booster and the boosting of naphtha booster respectively
Device preheating, vapourizing unit heating vaporizes, superheater is overheated, catalytic reactor catalytic reaction, then send again to cooling
Device cools down, finally by gas-oil-water three-phase separator output circulating air and liquefied petroleum gas and light aromatics mixture and outer row
Water, liquefied petroleum gas therein obtain liquefied petroleum gas and lightweight virtue through stabilizer separating treatment again with thick light aromatics mixture
Hydrocarbon 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-circulation is sequentially connected between the gas phase outlet of oil-water three-phase separator and the input terminal of superheater
Air compressor and circulating air heating unit are added with being formed by the gas-oil-water three-phase separator, recycle gas compressor, circulating air
The bypath system for the circulating air recycling that thermal and superheater are formed；
The circulating air send again to recycle gas compressor boosting, circulating heater heating, then again with the first after the vaporization
Alcohol and light naphtha enter the superheater after converging and carry out cycling and reutilization.
Preferably：The liquefied petroleum gas port of export of the stabilizer connects liquefied petroleum gas booster pump inlet end to form liquid
The recycling circuit of liquefied oil gas cycling and reutilization；The liquefied petroleum gas that the stabilizer is isolated is carried out into oil gas booster
Boosting, then with the preheating device output preheating after methanol and light naphtha converge it is latter with enter vapourizing unit into
Row vaporization.
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：The output terminal of the recycle gas compressor, institute are connected in the second segment input terminal of the catalytic reactor
The input terminal that the circulating air after the boosting of recycle gas compressor generation is sent to the catalytic reactor second segment is stated, to reduce body
It is temperature.
Brief description of the drawings
Fig. 1 is the process flow chart that the present invention realizes coupling between methanol light naphtha light aromatics method and system.
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 coupling between methanol light naphtha light aromatics includes：Methanol booster
1st, naphtha booster 2, preheating device 3, vapourizing unit 4, superheater 5, catalytic reactor 6, cooler 7, gas-oil-water three
The main preparation system that phase separator 8, stabilizer 9 are linked in sequence.
Be additionally included between the gas phase outlet of the gas-oil-water three-phase separator 8 and the input terminal of superheater 5 according to
Secondary connection recycle gas compressor 10 and circulating air heating unit 11 are with formation by the gas-oil-water three-phase separator 8, circulating air
The bypath system for the circulating air recycling that compressor 10, circulating air heating unit 11 and superheater 5 are formed.
Preheating device 3, vapourizing unit 4, superheater 5 and circulating air heating unit 12 include electric heater and heat exchange
Device.
12 arrival end of liquefied petroleum gas port of export connection liquefied petroleum gas booster of the stabilizer 9 is additionally included in shape
Into the recycling circuit of liquefied petroleum gas cycling and reutilization.
Be additionally included between the input terminal of 6 output terminal of catalytic reactor and cooler 7, be sequentially connected superheater 5,
Circulating air heating unit 11, vapourizing unit 4, preheating device 3 with formed thermal energy recycling thermal cycle passage；The catalytic reaction
The product that device 6 exports passes through superheater 5, circulating air heating unit 11, vapourizing unit 4, preheating device 3 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.
The middle catalytic reactor 6 is divided to for two sections：ZSM-5 catalyst is housed at first and second section, in first segment catalytic reaction
During controlling reaction temperature be 400~420 DEG C, pressure is 2.0~2.5 MPa, and mass space velocity is 20~50 h-1；Second
Controlling reaction temperature is 390~410 DEG C in section catalytic reaction process, and pressure be 1.9~2.5 MPa, mass space velocity is 0.9~
1.2 h-1；In the second segment front end of the catalytic reactor 6, after boosting caused by the recycle gas compressor 11 can be passed through
Circulating air, to reduce system temperature.
Based on the above-mentioned system for realizing coupling between methanol light naphtha light aromatics, the present invention realizes coupling between methanol lightweight
The process of naphtha light aromatics includes the following steps：
A. material benzenemethanol and raw material light naphtha are respectively fed to methanol booster 1 and naphtha booster 2 boosts；
B. preheating device 3 is sent into after converging the methanol after boosting and naphtha to preheat, and is then re-fed into vapour in vapourizing unit 4
Change；Methanol and light naphtha after vaporization are re-fed into superheater 5 and carry out Overheating Treatment；
C. methanol and light naphtha after overheating enter catalytic reactor 6 and carry out catalytic reaction, and the catalytic reactor 6 must
Must controlling reaction temperature, pressure and mass space velocity；
D. the output object input cooler 7 of the catalytic reactor 6 is cooled down, is then fed into gas-oil-water three-phase separator
8 carry out isolated liquefied petroleum gas and thick light aromatics product and circulating air, liquefied petroleum gas and the light aromatics production
Thing is then sent through 9 separating treatment of stabilizer, obtains light aromatics product and heavy hydrocarbon；Gas-oil-the water three-phase separator 8 is isolated
Water mutually make outer row processing.
Pass through circulating air recycling in the circulating air that the step D is exported by the gas-oil-water three-phase separator 8
Bypath system be sent to that recycle gas compressor 10 boosts, circulating air heating unit 11 heats, then again with the step B
Superheater 5 is sent into after the methanol and light naphtha of vaporization converge and together carries out Overheating Treatment, is finally sent into catalytic reaction
Catalytic reaction is carried out in device 6；Do outer row's processing in the superpressure part for the circulating air that the recycle gas compressor 10 boosts.
In the step D by the liquefied petroleum gas that the stabilizer 9 is isolated by liquefied petroleum gas cycling and reutilization
Recycling circuit is sent to liquefied petroleum gas booster 12 and boosts, then with the methanol after preheating described in the step B and gently
Matter naphtha converges latter same vapourizing unit 4 of being sent into and is vaporized processing, is then fed into superheater 5 and carries out Overheating Treatment.
Embodiment one
According to the requirement of above-mentioned technological process, 100 kg/h of methanol flow, methanol composition are controlled：99.9%, control light naphtha
100 kg/h of flow, 300 kg/h of circulating air flow, circulating air composition:H2 10% CH4 60% C2H4 10% C2H620%；On
State methanol, light naphtha and circulating air and boost to 2.0 MPa.
6 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:In the isolated light aromatics product of stabilizer 9, it is through analyzing its component：Benzene 3.41%, toluene
14.29%, dimethylbenzene 33.41%.
Embodiment two
According to the requirement of above-mentioned technological process, 200 kg/h of methanol flow, methanol composition are controlled：95.0%, control light naphtha
300 kg/h of flow, 500 kg/h of circulating air flow.Circulating air forms：H2 10% CH4 60% C2H4 10% C2H620%；On
State methanol, light naphtha and circulating air and boost to 2.1 MPa.
6 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, 390 DEG C of temperature, the process conditions of 2.5 MPa of pressure；
Reaction result is as follows:In the isolated light aromatics product of stabilizer 9, it is through analyzing its component：Benzene 5.73%, toluene
23.24% dimethylbenzene 45.85%.
Embodiment three
According to the requirement of above-mentioned technological process, 100 kg/h of methanol flow, methanol composition are controlled：90.0%, control light naphtha
80 kg/h of flow, 320 kg/h of circulating air flow, circulating air composition:H2 10% CH4 60% C2H4 10% C2H620%；It is above-mentioned
Methanol, light naphtha and circulating air boost to 2.5 MPa.
6 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 mass space velocity
0.9 h-1, 410 DEG C of temperature, the process conditions of 1.9 MPa of pressure；
Reaction result is as follows:In the isolated light aromatics product of stabilizer 9, it is through analyzing its component：1.72% toluene of benzene
21.32% dimethylbenzene 49.65%.
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 (13)
- A kind of 1. method for realizing coupling between methanol light naphtha light aromatics, it is characterised in that include the following steps：A. material benzenemethanol and raw material light naphtha are respectively fed to methanol booster（1）With naphtha booster（2）Risen Pressure；B. preheating device is sent into after converging the methanol after boosting and naphtha（3）Preheating, is then re-fed into vapourizing unit（4） Middle vaporization；Methanol and light naphtha after vaporization are re-fed into superheater（5）Carry out Overheating Treatment；C. methanol and light naphtha after overheating enter catalytic reactor（6）Carry out catalytic reaction, the catalytic reactor （6）Must controlling reaction temperature, pressure and mass space velocity；D. by the catalytic reactor（6）Output object input cooler（7）Cooled down, be then fed into gas-oil-water three-phase separate From device（8）Carry out isolated liquefied petroleum gas and light aromatics product mixtures and circulating air, the liquefied petroleum gas and Light aromatics product mixtures are then sent through stabilizer（9）Separating treatment, obtains light aromatics product；Gas-oil-water the three-phase separate From device（8）The water isolated mutually makees outer row's processing.
- 2. the method according to claim 1 for realizing coupling between methanol light naphtha light aromatics, it is characterised in that： The step D is by the gas-oil-water three-phase separator（8）The circulating air of output is sent to recycle gas compressor（10）Boost, follow Ring gas heating unit（11）Heating, is sent into overheat after then converging again with the methanol and light naphtha described in step B through vaporization Device（5）Overheating Treatment is together carried out, is finally sent into catalytic reactor（6）Middle carry out catalytic reaction；The recycle gas compressor （10）Do outer row's processing in the superpressure part of the circulating air of boosting.
- 3. the method according to claim 1 for realizing coupling between methanol light naphtha light aromatics, it is characterised in that： The step D is by stabilizer（9）The liquefied petroleum gas isolated is sent to liquefied petroleum gas booster（12）Boost, then with Methanol and light naphtha after being preheated described in the step B converge latter with feeding vapourizing unit（4）It is vaporized processing, It is then fed into superheater（5）Carry out Overheating Treatment.
- 4. the method according to claim 1 for realizing coupling between methanol light naphtha light aromatics, it is characterised in that：Step Catalytic reactor described in rapid C（6）Product into cooler（7）Before, followed by the superheater（5）, circulating air Heating unit（11）, vapourizing unit（4）, preheating device（3）Carry out heat exchange.
- 5. the method according to any one of claims 1 to 3 for realizing coupling between methanol light naphtha light aromatics, it is special Sign is：The purity of methanol in the step A is：90.0~99.9%, pressure after it boosts is 2.0~2.5 MPa, institute 2.0~2.5 MPa of pressure after light naphtha boosting is stated, the ratio of the methanol and light naphtha is 4:6~10:0；It is described Pressure after the boosting of circulating air is 2.0~2.5 MPa；Pressure is 2.0~2.5 MPa after the liquefied petroleum gas boosting.
- 6. the method according to claim 1 for realizing coupling between methanol light naphtha light aromatics, it is characterised in that：Institute State superheater in step B（5）Temperature be 300 DEG C ± 10 DEG C；Cooler in the step D（7）Cooling temperature be 45 ℃±5℃。
- 7. the method according to claim 1 for realizing coupling between methanol light naphtha light aromatics, it is characterised in that：Institute State catalytic reactor in step C（6）It is divided into 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 2.0~2.5 MPa, and mass space velocity is 0.9~1.2 h-1。
- 8. the method according to claim 7 for realizing coupling between methanol light naphtha light aromatics, it is characterised in that：Follow Ring air compressor（10）Circulating air after the boosting of generation is delivered to the catalytic reactor（6）Second segment input terminal, with Reduce system temperature.
- A kind of 9. system for realizing coupling between methanol light naphtha light aromatics, it is characterised in that：Including methanol booster（1）, naphtha booster（2）, preheating device（3）, vapourizing unit（4）, superheater（5）, urge Change reactor（6）, cooler（7）, gas-oil-water three-phase separator（8）, stabilizer（9）The main preparation system being linked in sequence；Material benzenemethanol and raw material light naphtha are respectively through methanol booster（1）With naphtha booster（2）Converge after boosting and send Enter preheating device（3）Preheating, vapourizing unit（4）Heating vaporization, superheater（5）Overheated, catalytic reactor（6）Catalysis is anti- Should, then send again to cooler（7）Cooling, finally by gas-oil-water three-phase separator（8）Export circulating air and liquefied petroleum gas With light aromatics mixture and outer draining, liquefied petroleum gas therein is with thick light aromatics mixture again through stabilizer（9）Point Liquefied petroleum gas and light aromatics product are obtained from processing.
- 10. the system according to claim 9 for realizing coupling between methanol light naphtha light aromatics, it is characterised in that： In the catalytic reactor（6）Output terminal and cooler（7）Input terminal between, be sequentially connected superheater（5）, circulating air adds Thermal（11）, vapourizing unit（4）, preheating device（3）To form the thermal cycle passage of thermal energy recycling；The catalytic reactor （6）The product of output passes through superheater（5）, circulating air heating unit（11）, vapourizing unit（4）, preheating device（3）Carry out Heat exchange；Also in the gas-oil-water three-phase separator（8）Gas phase outlet and superheater（5）Input terminal between connect successively Connect recycle gas compressor（10）With circulating air heating unit（11）To be formed by the gas-oil-water three-phase separator（8）, circulation Air compressor（10）, circulating air heating unit（11）And superheater（5）The bypass system of the circulating air recycling formed System；The circulating air is sent to recycle gas compressor again（10）Boosting, circulating heater（11）Heating, then again with the vapour Methanol and light naphtha after change enter the superheater after converging（5）Carry out cycling and reutilization.
- 11. the system according to claim 9 for realizing coupling between methanol light naphtha light aromatics, it is characterised in that： The stabilizer（9）The liquefied petroleum gas port of export connection liquefied petroleum gas booster（12）Arrival end is to form liquefied petroleum gas The recycling circuit of cycling and reutilization；The stabilizer（9）The liquefied petroleum gas isolated enters oil gas booster（12）Carry out Boosting, then with the preheating device（3）Methanol and light naphtha after the preheating of output converge latter same into vaporization dress Put（4）It is vaporized.
- 12. the system according to claim 9 for realizing coupling between methanol light naphtha light aromatics, it is characterised in that： The catalytic reactor（6）It is divided into two sections：ZSM-5 catalyst is housed at first and second section, is controlled in first segment catalytic reaction process Reaction temperature processed is 400~420 DEG C, and pressure is 2.0~2.5 MPa, and mass space velocity is 20~50 h-1；It is anti-in second segment catalysis Controlling reaction temperature is 390~410 DEG C during answering, and pressure is 1.9~2.5 MPa, and mass space velocity is 0.9~1.2 h-1。
- 13. the system according to claim 12 for realizing coupling between methanol light naphtha light aromatics, it is characterised in that： It is characterized in that：In the catalytic reactor（6）Second segment input terminal connect the recycle gas compressor（10）Output terminal, The recycle gas compressor（10）Circulating air after the boosting of generation is sent to the catalytic reactor（6）The input of second segment End, to reduce system temperature.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610905970.5A CN107963954A (en) | 2016-10-19 | 2016-10-19 | A kind of method and system of coupling between methanol light naphtha light aromatics |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610905970.5A CN107963954A (en) | 2016-10-19 | 2016-10-19 | A kind of method and system of coupling between methanol light naphtha light aromatics |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107963954A true CN107963954A (en) | 2018-04-27 |
Family
ID=61996841
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610905970.5A Pending CN107963954A (en) | 2016-10-19 | 2016-10-19 | A kind of method and system of coupling between methanol light naphtha light aromatics |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107963954A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111233608A (en) * | 2018-11-29 | 2020-06-05 | 中国科学院大连化学物理研究所 | Naphtha-containing raw material conversion method |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102199446A (en) * | 2010-03-23 | 2011-09-28 | 中国海洋石油总公司 | Method for producing aromatic hydrocarbon by adopting raw materials containing methanol |
| 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 CN201610905970.5A patent/CN107963954A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102199446A (en) * | 2010-03-23 | 2011-09-28 | 中国海洋石油总公司 | Method for producing aromatic hydrocarbon by adopting raw materials containing methanol |
| 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 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111233608A (en) * | 2018-11-29 | 2020-06-05 | 中国科学院大连化学物理研究所 | Naphtha-containing raw material conversion method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102530865B (en) | Be there is the method for being produced hydrogen by steam reformation petroleum fractions of the production of steam of optimization | |
| WO2010117696A1 (en) | Oxidative coupling of hydrocarbons as heat source | |
| CN102775274A (en) | System and method for preparing ethylene glycol through oxalate hydrogenation | |
| KR20230083297A (en) | Thermal Integration of Electrically Heated Reactors | |
| CN107963954A (en) | A kind of method and system of coupling between methanol light naphtha light aromatics | |
| CN109665527A (en) | The tail gas heat quantity recovery system and operation method of production of polysilicon equipment | |
| CN106748631A (en) | A kind of monochloro methane energy-saving processing technique and device | |
| CN102516007B (en) | Process and device for processing and preparing hydrocarbon by utilizing liquefied gas | |
| CN107963953A (en) | A kind of method and system for being used to reduce heavy hydrocarbons content in methanol hydrocarbon | |
| CN107963956A (en) | A kind of method and system of methanol light aromatics | |
| CN107964416A (en) | A kind of method and system of coupling between methanol light naphtha gasoline | |
| CN110681319B (en) | System and process for producing durene through injection circulation methanol aromatic methylation reaction | |
| CN105038839B (en) | Lighter hydrocarbons preparation method and lighter hydrocarbons preparation system using methanol as raw material | |
| CN103910604B (en) | The treatment process of methyl alcohol synthetic reactor outlet high-temperature gas and system for methanol synthesis | |
| CN107964418A (en) | A kind of method and system of methanol lightweight low-coagulation diesel oil | |
| CN107964414A (en) | A kind of method and system of coupling between methanol liquefied petroleum gas lightweight low-coagulation diesel oil | |
| CN207483642U (en) | A kind of novel carbinol extraction and recovery system | |
| CN107721791A (en) | The preparation system and preparation method of a kind of preparing propylene from methanol | |
| CN107964415A (en) | A kind of method and system of coupling between methanol liquefied petroleum gas gasoline | |
| CN107963955A (en) | A kind of method and system of coupling between methanol liquefied petroleum gas light aromatics | |
| CN107964417A (en) | A kind of method and system of preparing gasoline by methanol | |
| CN210187173U (en) | Disproportionation device capable of carrying out toluene and carbon nine-carbon ten reaction and benzene and carbon nine-carbon ten reaction | |
| CN104177235B (en) | A kind of catalyst recycle unit and method preparing polymethoxy dimethyl ether | |
| CN104073284B (en) | Method and relative device for transmitting catalyst | |
| CN207894049U (en) | Heat conduction reconditioner and trough solar power generation system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20180427 |