CN105925301B - Combination cot preparing gasoline by methanol technique - Google Patents
Combination cot preparing gasoline by methanol technique Download PDFInfo
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- CN105925301B CN105925301B CN201610537517.3A CN201610537517A CN105925301B CN 105925301 B CN105925301 B CN 105925301B CN 201610537517 A CN201610537517 A CN 201610537517A CN 105925301 B CN105925301 B CN 105925301B
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- Prior art keywords
- catalyst
- gas
- tube
- fin
- warm tube
- Prior art date
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 60
- 238000000034 method Methods 0.000 title claims abstract description 17
- 239000000463 material Substances 0.000 claims abstract description 23
- WVDDGKGOMKODPV-UHFFFAOYSA-N Benzyl alcohol Chemical compound OCC1=CC=CC=C1 WVDDGKGOMKODPV-UHFFFAOYSA-N 0.000 claims abstract description 22
- 229960004217 benzyl alcohol Drugs 0.000 claims abstract description 22
- 239000007788 liquid Substances 0.000 claims abstract description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 12
- 238000007599 discharging Methods 0.000 claims abstract description 11
- 239000002994 raw material Substances 0.000 claims abstract description 9
- 239000003054 catalyst Substances 0.000 claims description 50
- 238000006243 chemical reaction Methods 0.000 claims description 19
- 238000002309 gasification Methods 0.000 claims description 5
- 230000005611 electricity Effects 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 2
- 239000004744 fabric Substances 0.000 claims 1
- 238000009776 industrial production Methods 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 10
- 238000004519 manufacturing process Methods 0.000 description 7
- 230000033228 biological regulation Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 230000006641 stabilisation Effects 0.000 description 2
- 238000011105 stabilization Methods 0.000 description 2
- -1 Alcohol alkene Chemical class 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000003541 multi-stage reaction Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of combination cot preparing gasoline by methanol technique.It is comprised the technical steps that：Material benzenemethanol is preheated by preheater；Material benzenemethanol after preheating is input in evaporator and is gasified totally；Gasified raw material methyl alcohol and circulating air enter in Combined constant temperature reactor from combi inlet port pipe, from the discharge of Combined constant temperature reactor outlet；Product enters in gas-liquid separator from after discharging opening output after being condensed in point two tunnels input condenser；The gas isolated is output into circulating air, is separated in liquid output to oil water separator, obtains required product oil and water.It overcomes operating pressure greatly, and feed temperature is high, and recycle ratio is big, and the invalid Low Temperature Thermal of generation is relatively more, is not easy to reuse, and is not easy to the shortcoming of large-scale industrial production.
Description
Technical field
The present invention relates to chemical process flow field, specifically combination cot preparing gasoline by methanol technique.
Background technology
Combination cot preparing gasoline by methanol is a kind of strong exothermal reaction, and fixed bed reactors, fluid bed are included now with reactor
Reactor and multi-tubular reactor.Fixed bed reactors have the drawback that in use：Liberated heat can not be moved well
Go out reactor and produce temperature runaway, it is necessary to carry out temperature control with the circulating air more than more than 7 times of methyl alcohol of charging, serious have impact on
The stability of product and the service life of catalyst so that the regeneration period of catalyst shortens, and technical process and equipment
Complexity, high energy consumption, investment are high；Fluidized-bed reactor has the drawback that in use：Need urging for being carried secretly in product
Agent is separated, and increases the cost of investment of equipment；Because catalyst is motion in fluid bed, the broken of catalyst can be caused
Broken, the catalyst of powder is difficult to be separated with product, and catalyst attrition can be increased；What multi-tubular reactor existed in use
Have the disadvantage：Common tube is used, due to being strong exothermal reaction, the temperature difference of tube side and shell side is too big, can only be big with specific heat capacity
The raw material heating of continuous feed can not be met after material removes heat, but heat is moved out of；Such as remove heat few, bed meeting again
Overtemperature influences catalyst, and only increasing the quantity of heat exchanger tube, but increase heat exchanger tube can greatly increase equipment cost；Multitubular reactor
Because no gas distributor at charging, the regeneration of catalyst has not exclusively.These three reactors all can not be individually complete
Ground meets catalyst and is used in the relative efficiency of reactor.
Prior art has the drawback that：In more than 2.2MPa, feed temperature is high (to need 300 to the operating pressure of charging aperture
More than DEG C), reaching reaction temperature could enter reactor；Fixed bed recycle ratio is 7:More than 1, to ensure reaction condition and difference
The performance of catalyst, there is various reactors, complex process in the flow of exothermic reaction；To the volume needs of equipment
Greatly, it is not easy to realize that large industrialized is produced；Equipment investment is big, production cost is high, and the yield of product oil is not high.
The content of the invention
The invention aims to overcome the weak point of above-mentioned background technology, and provide a kind of combination cot methyl alcohol vapour
Oily technique.Reduce reaction condition, simplification of flowsheet.
In order to realize the purpose of the present invention, the technical scheme is that：Combination cot preparing gasoline by methanol technique, its feature exists
In：It is comprised the technical steps that：
Step 1：Material benzenemethanol is preheated by preheater；
Step 2：Material benzenemethanol after preheating is input in evaporator, gasification temperature is 120~160 DEG C, makes raw material first
Alcohol reaches the state of being gasified totally；
Step 3：The circulating air of gasified raw material methyl alcohol and the gas-liquid separator output exported in evaporator is from combi inlet port
In pipe input Combined constant temperature reactor, from the output of mixed gas outlet pipe, then reacted from charging aperture input catalyst, instead
The product answered is discharged from discharging opening.
Step 4：Product is divided into two tunnels from after discharging opening output, and condenser is directly entered all the way, into before condenser,
Its high warm can be used to generate electricity；Another road enters condenser after passing sequentially through evaporator and preheater；
Step 5：By the condensed product of condenser into being separated in gas-liquid separator, the gas isolated is from gas
Liquid/gas separator upper end is output into circulating air, and liquid is exported in oil water separator from gas-liquid separator lower end；
Step 6：By the separation circuit of oil water separator, water and required product oil are obtained.
In the above-mentioned technical solutions, the material benzenemethanol is reacted in the Combined constant temperature reactor, material benzenemethanol
It it is 120~160 DEG C into temperature during Combined constant temperature reactor, pressure is 0.6MPa~1.6MPa；Material benzenemethanol is in combination
Reaction temperature when catalyst is contacted in formula isothermal reactor is 300~350 DEG C.Reduce reaction condition, simplification of flowsheet.
In the above-mentioned technical solutions, circulating air is not more than 1 with the recycle ratio of material benzenemethanol:1.Reducing place capacity needs
Ask, greatly reduce production cost.
In the above-mentioned technical solutions, there is catalyst in the Combined constant temperature reactor, the catalyst is selected from MTO (first
Alcohol alkene), MTP (preparing propylene from methanol naphtha), MTD (methyl alcohol diesel oil) device select catalyst.Catalyst can be with root
Adjustment is needed according to production, catalyst source is wide, is easy to industrialized production.
In the above-mentioned technical solutions, the Combined constant temperature reactor includes cylinder, fixed bed, fin constant warm tube, gas
Distributor, has charging aperture to be located at the cylinder upper end, has discharging opening to be located at the cylinder lower end；There are combi inlet port pipe and mixing
Gas outlet is located at the side of the cylinder, there is tube sheet, catalyst fixator, gas distributor, fin constant warm tube and fixation
Bed is in the cylinder；The fin constant warm tube is fixed between two tube sheets；There is catalyst fixator to be located at described
Fin constant warm tube two ends.
In the above-mentioned technical solutions, the fin constant warm tube is located at the cylinder top, and the fixed beds are in described
Fin constant warm tube lower section, has two people's hole positions to be respectively positioned on the gas distributor in the side of the cylinder, and the manhole
Side.Reaction condition needed for differential responses step can be met so that multistep reaction can simultaneously be carried out in a reactor；
It is easy to observe and overhauls.
In the above-mentioned technical solutions, the fin constant warm tube is arranged vertically, and has multiple；The fin constant warm tube upper end
It is provided with expansion joint.The substantial amounts of heat transfer released when preferably inner reaction tube allows reaction temperature to obtain stabilization to shell side；It is anti-
The infringement only expanded with heat and contract with cold to equipment.
In the above-mentioned technical solutions, top board and fin constant warm tube top are equipped with the gas distributor.Make
Gas distribution in the reactor is more uniform, and the utilization rate of catalyst is higher.
In the above-mentioned technical solutions, the catalysis for being seated in the fin constant warm tube and being seated in the fixed bed
Agent kind is identical, or different；The catalyst is seated in the fin constant warm tube and in the fixed bed respectively, described solid
Fixed bed includes the top board, supporting plate；The catalyst is located between two catalyst fixators, and on described
Between pressing plate and the supporting plate.It is easy to fixed, regulation catalyst, the need for meeting reaction condition.
The invention has the advantages that：
(1) material benzenemethanol only needs to gasification can just enter Combined constant temperature reactor, and evaporator and combination cot constant temperature are anti-
As long as answering device to there is pressure difference just to enter in reactor the material benzenemethanol after gasification to react, it is not necessary to which the pressure in reactor reaches
More than 2.2MPa, the pressure used in present patent application is determined to preferably reaction pressure for 0.6MPa~1.6MPa,
The present invention reduces reaction condition, simplification of flowsheet；
(2) heat of Combined constant temperature reactor discharge is high-quality heat, can be provided from oneself and use needs, while can be used to
Generate electricity, raw material availability is high；
(3) remove superheater device, overheat is completed while carrying out temperature control by reactor, simplify technique stream
Journey, reduces equipment investment；
(4) finished product yield is improved, finished product yield brings up to more than 97% by original 85%；
(5) production cost is reduced, 100,000 tons of production costs of product oil drop to 1.6 hundred million or so by original 2.6 hundred million or so；
(6) recycle ratio is substantially reduced, recycle ratio is reduced to no more than 1 ﹕ 1 by 7 original ﹕ 1；
(7) bulk temperature and inlet amount of the controllable reaction tower of regulation circulating air flow；
(8) volume needs of equipment are reduced, equipment investment is reduced, industrialized production is easy to implement；
(9) stabilization is produced, it is easy to operate.
Brief description of the drawings
Fig. 1 is classical fixed bed process MTG process charts.
Fig. 2 is combination cot process chart of the present invention.
Fig. 3 is Combined constant temperature structure of reactor schematic diagram of the present invention.
1- charging apertures in figure, 2- manholes, 3- gas distributors, 4- supporting plates, 5- tube sheets, 51- upper perforated plates, 52- lower perforated plates,
6- top boards, 7- cylinders, 8- combi inlet port pipes, 9- mixed gas outlet pipes, 10- catalyst, 11- catalyst fixators, 111-
Upper end catalyst fixator, 112- lower ends end catalyst fixator, 12- fin constant warm tubes, 13- expansion joints, 14- discharging openings, 15-
Skirt, 16- base plates, 17- fixed beds, 18- preheaters, 19- evaporators, 20- gas-liquid separators, 21- Combined constant temperature reactors,
22- condensers, 23- oil water separators, 24- water, 25- product oils, 26- circulating air.
Specific embodiment
The performance that the invention will now be described in detail with reference to the accompanying drawings, but they do not constitute limitation of the invention, only
It is for example.Make advantages of the present invention more clear by explanation simultaneously and be readily appreciated that.
Understood refering to accompanying drawing：Combination cot preparing gasoline by methanol technique, it is comprised the technical steps that：
Step 1：Material benzenemethanol is preheated by preheater 18；
Step 2：Material benzenemethanol after preheating is input in evaporator 19, gasification temperature is 120~160 DEG C, makes raw material
Methyl alcohol reaches the state of being gasified totally；
Step 3：The circulating air 26 of gasified raw material methyl alcohol and gas-liquid separator 20 output exported in evaporator 19 is from mixing
In the input Combined constant temperature of gas inlet tube 8 reactor 21, exported from mixed gas outlet pipe 9, then catalyst 10 is input into from charging aperture 1
In reacted, the product of reaction is discharged from discharging opening 14.
Step 4：Product from discharging opening 14 output after, be divided into two tunnels, condenser 22 is directly entered all the way, into condenser it
Before, its high warm can be used to generate electricity；Another road enters condenser 22 after passing sequentially through evaporator 19 and preheater 18；
Step 5：By the condensed product of condenser 22 into being separated in gas-liquid separator 20, the gas isolated
Circulating air 26 is output into from the upper end of gas-liquid separator 20, liquid is exported to oil water separator 23 from the lower end of gas-liquid separator 20
In；
Step 6：By the separation circuit of oil water separator 23, water 24 and required product oil 25 are obtained.
The material benzenemethanol is reacted in the Combined constant temperature reactor 21, and it is anti-that material benzenemethanol enters Combined constant temperature
It is 120~160 DEG C to answer temperature during device 21, and pressure is 0.6MPa~1.6MPa；Material benzenemethanol is in Combined constant temperature reactor 21
Reaction temperature during middle contact catalyst is 300~350 DEG C.
Circulating air 26 is not more than 1 with the recycle ratio of material benzenemethanol:1, i.e., less than or equal to 1:1, wherein preferable during 1 ﹕ 1.
There is catalyst 10 in the Combined constant temperature reactor 21, the catalyst 10 is selected selected from MTO, MTP, MTD device
Catalyst.
The Combined constant temperature reactor 21 includes cylinder 7, and fixed bed 17, fin constant warm tube 12, gas distributor 3 has
Charging aperture 1 is located at the upper end of the cylinder 7, has discharging opening 14 to be located at the lower end of the cylinder 7；There are combi inlet port pipe 8 and gaseous mixture
Outlet 9 be located at the cylinder 7 side, have tube sheet 5, catalyst fixator 11, gas distributor 3, fin constant warm tube 12 with
And fixed bed 17 is located in the cylinder 7；The fin constant warm tube 12 is fixed between two tube sheets 5；There is catalyst to consolidate
Device 11 is determined positioned at the two ends of fin constant warm tube 12；
The fin constant warm tube 12 is located at the top of the cylinder 7, and the fixed bed 17 is located at the fin constant warm tube 12
Lower section, has two manholes 2 to be located at the side of the cylinder 7, and the manhole 2 is respectively positioned on the top of the gas distributor 3.
The fin constant warm tube 12 is arranged vertically, and has multiple；The upper end of fin constant warm tube 12 is provided with expansion joint 13.
There are top board 6 and the top of the fin constant warm tube 12 to be equipped with the gas distributor 3.
The kind of the catalyst 10 or the phase for being seated in the fin constant warm tube 12 and being seated in the fixed bed 17
Together, it is or different；The catalyst 10 is seated in the fin constant warm tube 12 and in the fixed bed 17 respectively, the fixed bed
17 include the top board 6, supporting plate 4；The catalyst 10 is located between two catalyst fixators 11, and positioned at institute
State between top board 6 and the supporting plate 4.
Other unaccounted parts belong to prior art.
Claims (4)
1. combination cot preparing gasoline by methanol technique, it is characterised in that：It is comprised the technical steps that：
Step 1：Material benzenemethanol is preheated by preheater (18)；
Step 2：Material benzenemethanol after preheating is input in evaporator (19), gasification temperature is 120~160 DEG C, makes raw material first
Alcohol reaches the state of being gasified totally；
Step 3：The circulating air (26) of gasified raw material methyl alcohol and gas-liquid separator (20) output of output in evaporator (19) is from mixed
Close gas inlet tube (8) to be input into Combined constant temperature reactor (21), exported from mixed gas outlet pipe (9), then it is defeated from charging aperture (1)
To enter reacted in catalyst (10), the product of reaction is discharged from discharging opening (14)；
Step 4：Product from discharging opening (14) output after, be divided into two tunnels, condenser (22) is directly entered all the way, into condenser it
Before, its high warm can be used to generate electricity；Another road passes sequentially through evaporator (19) and preheater (18) and enters condenser (22) afterwards；
Step 5：Enter by condenser (22) condensed product and separated in gas-liquid separator (20), the gas isolated
Circulating air (26) is output into from gas-liquid separator (20) upper end, liquid is exported to water-oil separating from gas-liquid separator (20) lower end
In device (23)；
Step 6：By the separation circuit of oil water separator (23), water (24) and required product oil (25) are obtained；
The material benzenemethanol is reacted in the Combined constant temperature reactor (21), and material benzenemethanol reacts into Combined constant temperature
Temperature during device (21) is 120~160 DEG C, and pressure is 0.6MPa~1.6MPa；Material benzenemethanol is in Combined constant temperature reactor
(21) reaction temperature in during contact catalyst is 300~350 DEG C；
There is fin constant warm tube (12) in the Combined constant temperature reactor (21)；
Circulating air (26) is not more than 1 with the recycle ratio of material benzenemethanol:1；
The Combined constant temperature reactor (21) includes cylinder (7), fixed bed (17), the fin constant warm tube (12), gas point
Cloth device (3), has charging aperture (1) positioned at the cylinder (7) upper end, has discharging opening (14) positioned at the cylinder (7) lower end；There is mixing
Gas inlet tube (8) and mixed gas outlet pipe (9) have tube sheet (5), catalyst fixator (11), gas positioned at the cylinder (7) side
Body distributor (3), fin constant warm tube (12) and fixed bed (17) are in the cylinder (7)；The fin constant warm tube (12)
It is fixed between two tube sheets (5)；There is catalyst fixator (11) positioned at fin constant warm tube (12) two ends；
The fin constant warm tube (12) is arranged vertically, and has multiple；Fin constant warm tube (12) upper end is provided with expansion joint
(13)；
Be seated in the fin constant warm tube (12) and the catalyst (10) kind that is seated in the fixed bed (17) or
It is identical or different；The catalyst (10) is seated in the fin constant warm tube (12) and in the fixed bed (17) respectively, institute
Stating fixed bed (17) includes the top board (6), supporting plate (4)；The catalyst (10) is fixed positioned at two catalyst
Between device (11), and between the top board (6) and the supporting plate (4).
2. combination cot preparing gasoline by methanol technique according to claim 1, it is characterised in that：The Combined constant temperature reactor
(21) there is catalyst (10) in, the catalyst (10) is selected from the catalyst selected in MTO, MTP, MTD device.
3. combination cot preparing gasoline by methanol technique according to claim 1 and 2, it is characterised in that：The fin constant warm tube
(12) positioned at the cylinder (7) top, and the fixed bed (17) has two manholes positioned at the fin constant warm tube (12) lower section
(2) positioned at the cylinder (7) side, and the manhole (2) is respectively positioned on the gas distributor (3) top.
4. combination cot preparing gasoline by methanol technique according to claim 3, it is characterised in that：There are top board (6) and the wing
Piece constant warm tube (12) top is equipped with the gas distributor (3).
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610537517.3A CN105925301B (en) | 2016-07-08 | 2016-07-08 | Combination cot preparing gasoline by methanol technique |
| PCT/CN2017/089887 WO2018006714A1 (en) | 2016-07-08 | 2017-06-24 | Process for preparing gasoline from methanol by means of combined bed |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610537517.3A CN105925301B (en) | 2016-07-08 | 2016-07-08 | Combination cot preparing gasoline by methanol technique |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105925301A CN105925301A (en) | 2016-09-07 |
| CN105925301B true CN105925301B (en) | 2017-07-04 |
Family
ID=56827327
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610537517.3A Active CN105925301B (en) | 2016-07-08 | 2016-07-08 | Combination cot preparing gasoline by methanol technique |
Country Status (2)
| Country | Link |
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| CN (1) | CN105925301B (en) |
| WO (1) | WO2018006714A1 (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105925301B (en) * | 2016-07-08 | 2017-07-04 | 鲁盈 | Combination cot preparing gasoline by methanol technique |
| CN108034448B (en) * | 2017-11-20 | 2019-04-05 | 鲁德祥 | Multifunctional efficient methanol derivatives equipment and technique |
| CN109621846B (en) * | 2018-12-29 | 2024-10-22 | 鲁盈 | Hydrocarbon preparation equipment based on normal-temperature methanol feeding reaction and hydrocarbon preparation method thereof |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA1223895A (en) * | 1984-03-05 | 1987-07-07 | Hugo I. De Lasa | Pseudodiabatic reactor for exothermal catalytic conversions |
| CN101723775B (en) * | 2008-11-04 | 2013-05-22 | 杭州林达化工技术工程有限公司 | Method and equipment for preparing hydrocarbon by methyl alcohol or/ and dimethyl ether |
| JP5812781B2 (en) * | 2011-09-21 | 2015-11-17 | 三菱重工業株式会社 | Method and apparatus for producing gasoline and hydrogen from methanol |
| CN105457564B (en) * | 2015-08-31 | 2018-02-16 | 张淮海 | Multistage indirect heat exchange radial fixed-bed reactor |
| CN105154128A (en) * | 2015-09-06 | 2015-12-16 | 华陆工程科技有限责任公司 | Tubular fixed bed methanol to gasoline process |
| CN105419849A (en) * | 2015-11-09 | 2016-03-23 | 赛鼎工程有限公司 | Energy-saving type technology for manufacturing gasoline by converting methanol |
| CN105396514B (en) * | 2015-12-31 | 2018-04-17 | 易高环保能源研究院有限公司 | Preparing gasoline by methanol device and method |
| CN105925301B (en) * | 2016-07-08 | 2017-07-04 | 鲁盈 | Combination cot preparing gasoline by methanol technique |
-
2016
- 2016-07-08 CN CN201610537517.3A patent/CN105925301B/en active Active
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2017
- 2017-06-24 WO PCT/CN2017/089887 patent/WO2018006714A1/en active Application Filing
Also Published As
| Publication number | Publication date |
|---|---|
| CN105925301A (en) | 2016-09-07 |
| WO2018006714A1 (en) | 2018-01-11 |
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