CN105505432A - Comprehensive heat utilization method in methanol to gasoline process - Google Patents
Comprehensive heat utilization method in methanol to gasoline process Download PDFInfo
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- CN105505432A CN105505432A CN201610060193.9A CN201610060193A CN105505432A CN 105505432 A CN105505432 A CN 105505432A CN 201610060193 A CN201610060193 A CN 201610060193A CN 105505432 A CN105505432 A CN 105505432A
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- 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
- C10G3/42—Catalytic treatment
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- 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
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- 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
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Abstract
The invention provides a comprehensive heat utilization method in a methanol to gasoline process. The method comprises the following steps: heating and gasifying a methanol raw material and allowing the gasified material to enter a reactor, and taking out heat discharged in the reaction process by utilizing a heat removal medium, wherein after heat exchange, the heat removal medium is used for one or more processes of A1-producing of a byproduct middle-pressure steam, A2-gasification of the methanol raw material and A3-heating before the operation of allowing a recycle gas to enter the reactor; transferring heat and cooling the discharge product by utilizing a heat-transfer medium, wherein the heat-transfer medium after heat transfer is used for one or more processes of B1-heating of the methanol raw material, B2-heating before the operation of allowing the recycle gas to enter the reactor and B3-producing of a byproduct low-pressure steam; further cooling the discharge product, performing gas-liquid separation, so as to obtain a crude product, condensate and a dry gas; pressurizing and heating partial or total of the dry gas serving as the recycle gas, mixing with feed methanol, and allowing the mixture to enter the reactor for reacting. According to the method provided by the invention, the recycle quantity of the recycle gas and the total energy consumption can be greatly reduced.
Description
Technical field
The invention belongs to technique for preparing gasoline by methanol field, particularly the method for comprehensive utilization of heat in a kind of preparing gasoline by methanol process.
Background technology
The development of technique for preparing gasoline by methanol (MTG) comes from eighties of last century, is invented in the seventies by Mobil company of the U.S., but along with the fluctuation of international oil price, MTG technical development also experienced by larger fluctuating.Along with the reduction of scarcity and the methanol production cost day by day of world petroleum resource, preparing gasoline by methanol project received much concern in recent years.Due to the few energy structure of oil of the many coals of China and the situation of methyl alcohol production capacity surplus, MTG technology is very fast in China's development, has many cover MTG devices to put into effect successively.
The ultimate principle of MTG process is that methyl alcohol is converted into hydrocarbon mixture under an acidic catalyst effect.Methyl alcohol first dehydration generation dme (DME) under Protic Acid Catalyzed effect, DME transforms the alkene generating C2-C5 further, C2-C5 alkene realizes further selecting type conversion reaction under the effect of ZSM-5 catalyzer total acidic, comprise alkene to generate, alkylation (hydrocarbonylation, refer to that an alkene and alkane are combined into the reaction of a high collateralization alkane), oligomerisation (the polymkeric substance of a kind of molecular weight lower (less than 1500) of the polymerization degree between monomer and final polymkeric substance, also referred to as oligopolymer), aromizing (main naphthenic hydrocarbon processed or alkane change the process of aromatic hydrocarbon into), cracking (referring to that hydro carbons at high temperature molecular chain chain rupture becomes the process of the unsaturated hydrocarbons of small-molecular-weight) and disproportionation (also claim selfoxidation-reduction reaction, refer to by one or more hydrogen atom from a molecular transfer to another molecule, make a molecular oxidation, the reduction of molecule) etc. polystep reaction, finally obtain alkane, the mixture of alkene and aromatic hydrocarbons, can be used as high-quality gasoline.
Its reaction principle is as follows:
CH
3oH → CH
3oCH
3+ H
2o → light olefin+alkane+aromatic hydrocarbons+Q
The total reaction heat that carbinol condensation is converted into hydro carbons and water is about 1400kJ/kg methyl alcohol, the Re Genggao that the reacting condition along with hydrocarbon composition is released, and the adiabatic heating of reaction can reach 600 DEG C.Current MTG production technique mainly comprises fixed-bed process, fluidized-bed process and calandria type fixed bed technique, no matter adopts the technique of which kind of form, and the strong exothermic effect of reaction is that production process must be considered.
Temperature rise due to beds must control at 60-70 DEG C to avoid catalyzer coking and active reduction.The light gas circulation that typical MTG Technology is all produced by reaction at present controls the reaction temperature rising of reactor.Namely reaction product is hydrocarbon gas, gasoline products and water in gas-liquid separator separates after heat exchange cooling, after a small amount of emptying of hydrocarbon gas, major part is through compressor pressurizes, after well heater heats up and reactor feed gaseous state methanol mixed enter the control of reactor realization response device temperature rise, its recycle ratio is up to 5-12 the ratio of charging methyl alcohol amount of substance (circulation gas with).In whole production process, reaction liberated heat part is used for material benzenemethanol heating and gasifying and circulation gas heats up, and most of heat is taken away with temperature-fall period before the gas-liquid separation of product and circulation gas, causes the waste of energy.Simultaneously because reactor reacts under 2.5-3.5MPa (a), circulation gas need send into reactor after compressor pressurizes, and when recycle ratio is higher, energy consumption of compressor can account for 40% of MTG technological process total energy consumption, and economic benefit is poor.
Summary of the invention
The invention is for solving the problems of the prior art, provide a kind of preparing gasoline by methanol process heat method of comprehensive utilization, can make full use of the energy of reaction process release, effectively control reactor temperature rise, reduce the internal circulating load of preparing gasoline by methanol process circulation gas, and then reduce circulation gas cooling water amount and energy consumption of compressor, thus reduce facility investment expense and total energy consumption.
A kind of preparing gasoline by methanol process heat method of comprehensive utilization that the invention provides, comprise following process, methanol feedstock through heat up and gasify laggard enter reactor react, reaction process liberated heat utilizes heat-obtaining media for heat exchange to take out, the heat-obtaining medium carrying heat of reaction for: the gasification of A1-by-product middle pressure steam, A2-methanol feedstock, A3-circulation gas enter in the intensification before reactor one or more; First reactor discharge product utilizes heat transferring medium heat exchange to lower the temperature, the heat transferring medium (i.e. heat transferring medium heat up after) carrying discharging product heat for: the intensification of B1-methanol feedstock, B2-circulation gas enter the intensification before reactor, B3-by-product low-pressure steam one or more; After heat exchange cooling, discharge product is by cooling further, and after cooling, discharge product obtains product coarse product, lime set and dry gas by gas-liquid separation; Part or all of dry gas as circulation gas by entering reactor and react after pressurizeing and heating up with after charging methanol mixed; Wherein, the recycle ratio of circulation gas can be 0 or not be 0.
Wherein, described heat-obtaining medium and heat transferring medium can recycle; When A1-by-product middle pressure steam or B3-by-product low-pressure steam, the demand for heat that steam pipe system meets other devices can be incorporated to.Preferably the preferential gasification for A2-methanol feedstock and/or A3-circulation gas enter the intensification before reactor to carry the described heat-obtaining medium of heat of reaction; Preferably the preferential intensification for B1-methanol feedstock and/or B2-circulation gas enter the intensification before reactor to carry the heat transferring medium of discharging product heat.
Wherein, consider the reaction efficiency of total energy approach efficiency, heat-obtaining and heat exchange efficiency and preparing gasoline by methanol process, controlling methanol feedstock temperature after heating up is 150-180 DEG C, enter reactor through the methanol feedstock of gasification or the mixture temperature of itself and circulation gas be 320-350 DEG C, reactor discharge product temperature is 400-430 DEG C, after heat exchange cooling, discharge product temperature is 140-170 DEG C, and after cooling, discharge product temperature is 40-50 DEG C.Wherein, methanol feedstock reaction temperature rising in reactor controls within 70 DEG C.
Wherein, the recycle ratio of described circulation gas can be 0-15, preferably can be down to 0-5, and lower ground recycle ratio is conducive to more effectively reducing energy consumption, medicine drops into and facility investment.In this case, the recycle ratio of scheme optimum can be down to 0, when recycle ratio is 0, can be considered the participation not having circulation gas in this case preparing gasoline by methanol process heat method of comprehensive utilization, namely dry gas directly enters subsequent processing, do not exist part or all of dry gas as circulation gas through pressurization, heat up, enter with methanol mixed the process that reactor carries out reacting.
Wherein, described heat-obtaining medium is preferably fused salt or thermal oil; Described heat-obtaining medium in the reactor with reactant heat exchange in a counter-current fashion; The middle pressure steam pressure of described heat-obtaining medium by-product is 2-4MPa.
Wherein, described heat transferring medium is preferably thermal oil or low pressure saturation water; Described heat transferring medium and the heat exchange in a counter-current fashion of reactor discharge product.
Wherein, in described preparing gasoline by methanol process heat method of comprehensive utilization, also comprise following one or more processes: one is the pressure process of methanol feedstock, preferably methanol feedstock is forced into 2.5-3.5MPa, be also preferably and pressurize before methanol feedstock heats up; It two is catalyst recovery process, be preferably after discharge product heat exchange cooling, cool before carry out catalyst recovery.
The advantage that the present invention is compared with the prior art had and positively effect are:
(1) heat-obtaining medium and heat transferring medium is adopted to carry out heat exchange to reaction process liberated heat and reactor discharge product, make production process more stable, relatively traditional employing product stream stock direct heating and gasification feed methyl alcohol, improve capacity usage ratio, simplify production process.
(2) heat-obtaining medium maintains reactor temperature rise in the reasonable scope to reactor heat-obtaining, reaction steadily can be carried out, and ensure that catalyst activity, and heat removal is used for charging methanol gasifying and circulation gas heats up, and decreases outside energy input.
(3) heat transferring medium is used for the intensification of charging methyl alcohol and circulation gas intensification to the heat exchange of reactor discharge product and by heat, decreases the energy of reaction product cooling dissipation, the process that cools before simultaneously reducing gas-liquid separation energy consumption.
(4) to reactor heat-obtaining to control reactor temperature rise, greatly reduce circulation gas intake, and then decreasing reactor catalyst admission space, the energy consumption of compressor simultaneously for circulation gas pressurization declines to a great extent even inactive, decreases catalyzer and facility investment.
(5) relatively traditional MTG technological cycle ratio can be down to less than 5, and be even 0, total energy consumption can be reduced to original less than 10%, and even total energy consumption reduces to 0 or be negative energy consumption, has very large economic benefit.
Accompanying drawing explanation
Fig. 1-Fig. 2 is the process flow diagram under the different operating mode of the present invention.
Embodiment
Below by being further described the invention by reference to the accompanying drawings, but do not limit protection scope of the present invention.
The invention proposes a kind of preparing gasoline by methanol process heat method of comprehensive utilization for MTG Energy harvesting.Material benzenemethanol a enters feed preheater 2 after being pressurizeed by fresh feed pump 1, and after pressurization, material benzenemethanol a pressure is advisable with 2.5-3.5MPa, enters gasifier 3 and heat up further gasification in feed preheater 2 after heating up.Feed preheater preheats medium charging m2 is effluent exchanger 5 heat transferring medium discharging c2, specific form can be thermal oil or low-pressure saturated steam, after pre-thermal medium charging m2 carries out preheating to material benzenemethanol a, pre-thermal medium discharging n2 can return effluent exchanger 5 as heat transferring medium charging b2 continuation circulation, and material benzenemethanol charging is warming up to 150-180 DEG C; In gasifier 3, gasifying medium charging m1 is heat-obtaining medium discharging c1 in reactor 4, heat-obtaining medium discharging c1 recycles as heat-obtaining medium charging b1 bottom Returning reactor 4 after material benzenemethanol a gasifies, in gasifier 3, gasifying medium also can use middle pressure steam, according to concrete performance, heat-obtaining medium can select thermal oil or fused salt, and the temperature that material benzenemethanol a enters reactor is 320-350 DEG C.Wherein, the reactor 4 used for there being the reactor of outside heat removing function, as external heat exchanging type fixed-bed reactor.Because reactor 4 is in the continuous heat release of reaction process, heat-obtaining medium can enter bottom reactor 4, takes away energy with reactant flow counter current contact, releases after intensification from reactor 4 top.Heat-obtaining medium except for except the above-mentioned gasification to material benzenemethanol a, also can be used for the intensification to circulation gas h below or by-product middle pressure steam (being incorporated to steam pipe system).
Material benzenemethanol a discharge product after reactor 4 reaction terminates is warming up to 400-430 DEG C, reactor discharge product temperature and heat-obtaining medium material inlet valve interlocked control heat-obtaining medium charging b1 flow, ensures that in reactor, temperature rise is 60-70 DEG C.Discharge product mainly comprises dry gas e and (is mainly CO
2, CO, H
2, CH
4and C
2h
6deng), lime set g (being mainly water), thick product f (being mainly LPG, gasoline, diesel component).Discharge product needs to cool before entering gas-liquid separator 8, and traditional technology directly adopts air cooler+water-to-water heat exchanger cooling, causes heat directly to be wasted.Discharge product of the present invention by heat transferring medium charging b2 heat exchange, considers effective utilization of discharge product heat, heat exchange efficiency and heat transferring medium temperature rise by effluent exchanger 5, and the rear discharge product of heat exchange cooling is cooled to 140-170 DEG C and is advisable.Heat transferring medium can select thermal oil or low pressure saturation water (≤1MPa), and the heat transferring medium discharging c2 after intensification, except for except above-mentioned raw materials methyl alcohol a intensification, can also be used for circulation gas h intensification below or by-product low-pressure steam.After heat exchange cooling, discharge product enters discharging water cooler 7 through catalyst filter 6 and to cool with p of intake by water coolant and be cooled to 40-50 DEG C further, and now in discharge product, water and part hydrocarbon are condensed into the lime set g of liquid state.In gas-liquid separator 8, lime set g as bottom product discharging, thick product f through oily water separation discharging, dry gas e as fuel gas from tower top discharging.
In above process, methanol feedstock a heats up and gasification institute heat requirement can partly or entirely be provided by reaction self-heat generation, greatly reduces Process Energy input, improves capacity usage ratio.
Consider that the variation of startup procedure operational condition is comparatively large, and the not plateau that actual implementation process may exist, part dry gas e returns as circulation gas h and is mixed into reactor 4 to maintain reactor 4 temperature rise with charging methyl alcohol a.Circulation gas h is through compressor 9 supercharging, be advisable with 2.5-3.5MPa, enter circulating gas heater 10 and be warming up to reactor 4 inlet temperature 320-350 DEG C, circulating-heating medium charging m3 in circulating gas heater 10 is heat-obtaining medium discharging c1, circulating-heating medium discharging n3 can recycle for heat-obtaining medium charging b1, and the circulating-heating medium in circulating gas heater 10 also can use middle pressure steam.Because reactor 4 in smooth running process is by heat-obtaining medium charging b1 heat-obtaining, relatively traditional MTG technological cycle ratio can be down to less than 5, is even 0.Energy consumption when low recycle ratio can reduce compressor 9 facility investment and run.
embodiment 1
With year methanol feeding 4 × 10
5t, the preparing gasoline by methanol device of 8000 hours working times of year is example.Methanol feeding is 50t/h (1560kmol/h), feeding temperature 40 DEG C.Recycle ratio is 0, and namely Fig. 1 is shown without working cycle.
Material benzenemethanol a is forced into 2.5MPa through fresh feed pump 1, is heated to 150 DEG C in feed preheater 2, feed preheater 2 heating power 6.1MW.Be further heated gasification at gasifier 3 Raw methyl alcohol a, before making it enter reactor 4, temperature rises to 340 DEG C, gasifier 3 heating power 16.8MW.Material benzenemethanol a is converted to water and hydro carbons, transformation efficiency 100% under the effect of reactor 4 inner catalyst, and wherein each component molar ratio of primary product is water 56%, and thick product is 36.1%, and dry gas is 7.9%, exothermic heat of reaction 20MW, and discharge product temperature is 400 DEG C.Adopt thermal oil as heat-obtaining medium, heat-obtaining medium charging b1 temperature 350 DEG C, heat-obtaining medium discharging c1 temperature 380 DEG C, heat-obtaining rate-of flow is by reactor 4 temperature out instrument interlocked control.Consider that partial heat energy is taken away in heat exchange efficiency and discharge product temperature rise, heat-obtaining medium discharging c1 only enters gasifier 3 as gasifying medium charging m1 and material benzenemethanol a is heated up to gasify no longer by-product middle pressure steam, with material benzenemethanol a heat exchange after gasifying medium discharging n1 use as heat-obtaining medium charging b1 Returning reactor 4 bottom cycle.
Discharge product warp is at effluent exchanger 5 and the low pressure saturation water (0.6MPa (a) as heat transferring medium charging b2,160 DEG C) heat exchange, produce saturated low-pressure steam as heat transferring medium discharging c2, discharge product is cooled to 170 DEG C simultaneously, and heat release power is about 8MW.The saturated low-pressure steam produced is as the intensification of pre-thermal medium charging m2 for material benzenemethanol a, and also can be used for the heating of other devices, the lime set after saturated low-pressure steam heat exchange and pre-thermal medium discharging n2 return effluent exchanger 5 and recycle.Before gas-liquid separator 8 import, discharge product is cooled to 45 DEG C further through discharging water cooler 7, and discharging water cooler 7 power is about 10.5MW.In gas-liquid separator 8, water is released at the bottom of tower as lime set g, and thick product f enters subsequent processing and processes further after oily water separation, and dry gas e releases as overhead product, can be used as fuel gas or processes further.
Whole Transformation Engineering achieves heat Equilibrium, decreases external heat input, and reduces the facility investment of reactor 4, compressor 9 and discharging water cooler 7.
embodiment 2
With year methanol feeding 4 × 10
5t, the preparing gasoline by methanol device of 8000 hours working times of year is example.Methanol feeding is 50t/h (1560kmol/h), feeding temperature 40 DEG C.Recycle ratio is 3, i.e. process shown in Fig. 2.
Material benzenemethanol a is forced into 2.5MPa through fresh feed pump 1, is heated to 160 DEG C in feed preheater 2, feed preheater 2 heating power 7.5MW.Be further heated gasification at gasifier 3 Raw methyl alcohol a, before making it enter reactor 4, temperature rises to 330 DEG C, gasifier 3 heating power 16.1MW.Circulation gas h is to be mixed into reactor 4 with material benzenemethanol a uniform temp and pressure and material benzenemethanol a, and circulation gas h is a part of dry gas e, and amount of substance flow is 4680kmol/h.Material benzenemethanol a is converted into water and hydro carbons in the reactor 4, transformation efficiency 100%, and each component molar of discharge product is than being water 14%, and thick product is 9%, and dry gas is 77%.Exothermic heat of reaction is still 20MW, but about 6MW is used for circulation gas h is warming up to discharge product temperature 400 DEG C from 330 DEG C.Adopt thermal oil to do heat-obtaining medium, heat-obtaining medium charging b1 temperature 350 DEG C, heat-obtaining medium discharging c1 temperature 380 DEG C, heat-obtaining rate-of flow is by reactor 4 temperature out instrument interlocked control.After heating up, heat-obtaining medium discharging c1 is used for making circulation gas h heat up or as gasifying medium charging m1, material benzenemethanol a be gasified as circulating-heating medium charging m3, and recycles.
Discharge product and circulation gas h are through effluent exchanger 5 and low pressure saturation water (0.6MPa (a), the 160 DEG C) heat exchange as heat transferring medium charging b2, and be cooled to 160 DEG C, heat release power is about 27MW.After heat exchange as the saturated low-pressure steam of heat transferring medium discharging c2 except as pre-thermal medium charging m2 be used for material benzenemethanol a intensification except, to consider after heat exchange efficiency to be about the low-pressure steam (0.6MPa (a) of 900t/h by by-product, 160 DEG C), low-pressure steam can be incorporated to the demand for heat that steam pipe system meets other devices of plant area.Discharge product and circulation gas h are cooled to 45 DEG C at discharging water cooler 7 further, and discharging water cooler 7 power is about 24MW.In gas-liquid separator 8, water is released at the bottom of tower as lime set g, and thick product f enters subsequent processing and processes further after oily water separation, and dry gas e releases as overhead product, can be used as fuel gas or process further, the dry gas e of about 4680kmol/h enters compressor 9 as circulation gas h.Circulation gas h (1.5MPa) is forced into 2.5MPa by compressor 9, and energy consumption is about 3MW, and circulation gas h is warming up to 96 DEG C.In circulating gas heater 10, circulation gas h continues to be warming up to 330 DEG C, is mixed into reactor 4 with material benzenemethanol a.
Owing to introducing circulation gas h operation, circulation gas h is warming up to 330 DEG C of needs about 13.8MW and adds heat, and in simultaneous reactions device 4, the heat of exothermic heat of reaction takes away a part by circulation gas h, causes heat-obtaining medium charging b1 flow to decline.Meet the temperature that material benzenemethanol a and circulation gas h gasifies, general facilities can be increased temperature outward or heat transferring medium discharging c2 (temperature is at 350-400 DEG C) is gasified for material benzenemethanol a and circulation gas h.
When recycle ratio is less, compressor 9 energy consumption is lower, and as the key equipment of whole MTG technique, compressor 9 energy consumption reduces can make the facility investment of production process and power consumption reduce to strengthen economic benefit.
Energy consumption under above-mentioned for the present invention two kinds of operating modes and support circulation gas temperature control traditional technology are contrasted, according to treatment capacity 50t/h methyl alcohol respectively computation cycles ratio be 0,3,10 (empty calory is recycled, traditional technology) time major equipment needed for the heat that provides of the external world and cold, its result is as shown in table 1 below.
Table 1
Note *: recirculated cooling water Inlet and outlet water temperature is 32 DEG C and 42 DEG C.
As can be seen from Table 1, preparing gasoline by methanol process integration utilizes Posterior circle ratio to decrease, and realizes energy efficient and utilize in whole device, reduces outside energy input.Relatively traditional high recycle ratio temperature control process energy input significantly reduces, and compressor scale and reactor size all reduce along with recycle ratio and reduce simultaneously, have good economic benefit.
Claims (9)
1. a preparing gasoline by methanol process heat method of comprehensive utilization, comprise following process, methanol feedstock through heat up and gasify laggard enter reactor react, reaction process liberated heat utilizes heat-obtaining media for heat exchange to take out, the heat-obtaining medium carrying heat of reaction for: the gasification of A1-by-product middle pressure steam, A2-methanol feedstock, A3-circulation gas enter in the intensification before reactor one or more; First reactor discharge product utilizes heat transferring medium heat exchange to lower the temperature, the heat transferring medium carrying discharging product heat for: the intensification of B1-methanol feedstock, B2-circulation gas enter the intensification before reactor, B3-by-product low-pressure steam one or more; After heat exchange cooling, discharge product is by cooling further, and after cooling, discharge product obtains product coarse product, lime set and dry gas by gas-liquid separation; Part or all of dry gas as circulation gas by entering reactor and react after pressurizeing and heating up with after charging methanol mixed; Wherein, the recycle ratio of circulation gas can be 0 or not be 0.
2. a kind of preparing gasoline by methanol process heat method of comprehensive utilization according to claim 1, is characterized in that, the described heat-obtaining medium carrying heat of reaction preferentially enters the intensification before reactor for the gasification of A2-methanol feedstock and/or A3-circulation gas; The heat transferring medium carrying discharging product heat preferentially enters the intensification before reactor for the intensification of B1-methanol feedstock and/or B2-circulation gas.
3. a kind of preparing gasoline by methanol process heat method of comprehensive utilization according to claim 1, it is characterized in that, controlling methanol feedstock temperature after heating up is 150-180 DEG C, enter reactor through the methanol feedstock of gasification or the mixture temperature of itself and circulation gas be 320-350 DEG C, reactor discharge product temperature is 400-430 DEG C, after heat exchange cooling, discharge product temperature is 140-170 DEG C, and after cooling, discharge product temperature is 40-50 DEG C.
4. a kind of preparing gasoline by methanol process heat method of comprehensive utilization according to claim 1, it is characterized in that, methanol feedstock reaction temperature rising in reactor controls within 70 DEG C.
5. a kind of preparing gasoline by methanol process heat method of comprehensive utilization according to claim 1, is characterized in that, the recycle ratio of described circulation gas can be 0-15, is preferably 0-5.
6. a kind of preparing gasoline by methanol process heat method of comprehensive utilization according to claim 1, it is characterized in that, described heat-obtaining medium is fused salt or thermal oil; Described heat transferring medium is thermal oil or low pressure saturation water.
7. a kind of preparing gasoline by methanol process heat method of comprehensive utilization according to claim 1, is characterized in that, described heat-obtaining medium in the reactor with reactant heat exchange in a counter-current fashion; Described heat transferring medium and the heat exchange in a counter-current fashion of reactor discharge product.
8. a kind of preparing gasoline by methanol process heat method of comprehensive utilization according to claim 1, is characterized in that, also comprise following one or more processes: one is the pressure process of methanol feedstock; It two is catalyst recovery process.
9. a kind of preparing gasoline by methanol process heat method of comprehensive utilization according to claim 1, it is characterized in that, methanol feedstock is forced into 2.5-3.5MPa by the pressure process of described methanol feedstock.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105907417A (en) * | 2016-06-21 | 2016-08-31 | 北斗航天软件（北京）有限公司 | Method for preparing high-octane-value gasoline blending components from methyl alcohol |
| CN106010626A (en) * | 2016-07-08 | 2016-10-12 | 成都赛普瑞兴科技有限公司 | Process of preparing stable light hydrocarbon through methanol conversion in isothermal method |
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|---|---|---|---|---|
| EP0108482B1 (en) * | 1982-10-01 | 1986-05-14 | Mobil Oil Corporation | Heat transfer circuit for generation of steam in conversion of methanol to gasoline |
| CN101705106A (en) * | 2009-10-22 | 2010-05-12 | 王揽月 | New energy-saving process for preparing MTG (or DME) with rough (refined) methanol |
| CN101723775A (en) * | 2008-11-04 | 2010-06-09 | 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 |
| CN104557371A (en) * | 2014-12-12 | 2015-04-29 | 赛鼎工程有限公司 | Method for preparing hydrocarbon mixture by using one-step methanol conversion in adiabatic fixed bed reactor |
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2016
- 2016-01-28 CN CN201610060193.9A patent/CN105505432A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0108482B1 (en) * | 1982-10-01 | 1986-05-14 | Mobil Oil Corporation | Heat transfer circuit for generation of steam in conversion of methanol to gasoline |
| CN101723775A (en) * | 2008-11-04 | 2010-06-09 | 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 |
| CN101705106A (en) * | 2009-10-22 | 2010-05-12 | 王揽月 | New energy-saving process for preparing MTG (or DME) with rough (refined) methanol |
| CN104557371A (en) * | 2014-12-12 | 2015-04-29 | 赛鼎工程有限公司 | Method for preparing hydrocarbon mixture by using one-step methanol conversion in adiabatic fixed bed reactor |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105907417A (en) * | 2016-06-21 | 2016-08-31 | 北斗航天软件（北京）有限公司 | Method for preparing high-octane-value gasoline blending components from methyl alcohol |
| CN106010626A (en) * | 2016-07-08 | 2016-10-12 | 成都赛普瑞兴科技有限公司 | Process of preparing stable light hydrocarbon through methanol conversion in isothermal method |
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