CN101497826B - Catalytic modifying production process for methanol fuel - Google Patents
Catalytic modifying production process for methanol fuel Download PDFInfo
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- CN101497826B CN101497826B CN200810080300A CN200810080300A CN101497826B CN 101497826 B CN101497826 B CN 101497826B CN 200810080300 A CN200810080300 A CN 200810080300A CN 200810080300 A CN200810080300 A CN 200810080300A CN 101497826 B CN101497826 B CN 101497826B
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Abstract
The invention relates to a catalyst modification production process of methanol fuel, which comprises the following steps: obtaining light components and heavy components after flashing and steaming the methanol fuel, performing catalytic reforming on at least one of the light components and the heavy components in a catalytic reactor, and obtaining the catalytic reformed methanol fuel after mixing again. The methanol fuel comprises methanol gasoline, methanol-diesel or methanol-lubricant which is prepared by any proportion. The invention changes the internal composition of the methanol fuel by the catalytic reaction, lowers the saturation vapor pressure of the low-proportion methanol-fuel, avoids the vapor lock phenomenon in the use, solves the cold starting problem of the high-proportion methanol-fuel in winter, increases the octane number of the methanol-fuel by 2-3, reduces the cetane number of the methanol-fuel by 5-9 and improves the fuel quality and the power property of the methanol-fuel.
Description
Technical field
The present invention relates to methanol fuel modification technology field, be specifically related to a kind of catalytic modifying production process that changes the inner composition of methanol fuel through catalyzed reaction.
Background technology
Greatly developing substitute energy is a major action of safeguarding national security, alleviating petroleum import pressure, alleviating the resource environment constraint.Through facts have proved for many years, in multiple vehicle alternative fuel, the methanol fuel raw material extensively, technology maturation, economically feasible, environmental friendliness, safe and reliable, have a extensive future, be the novel substitute energy that is fit to China's national situation.The extensive Industry Promotion that realizes methanol fuel will be to adjusting China's energy industry structure, promote comprehensive utilization of resources, improving the ecological environment, realize that recycling economy has important pushing effect with application.
Methanol fuel mainly is to be mixed through certain allocating technology by a certain percentage by industrial methanol and existing processed oil.What need stress is; Industrial methanol is not using under the situation of any additives, problems such as will producing in the methanol fuel use with the direct allotment of processed oil that mutual solubility is relatively poor according to a certain percentage, be prone to take place vapour lock in the high temperature season driving process, corrodibility, cold-starting difficulty, dynamic property are bad.The common practices that addresses these problems is through adding composite additive, according to certain concocting method methanol fuel being carried out the modification modulation.Some methanol fuels allotment producers of China have carried out multi-faceted, comprehensive research trial to problems such as dynamic property, economy, the feature of environmental protection, security and the toxicity of methanol fuel, swelling corrodibility; And developed compound additive for methanol gasoline, developed special function additives such as vapour lock suppressor factor, corrosion inhibitor, solubility promoter with leading domestic level.Under present competition situation, the composition proportioning of additive and concocting method become the core technology of methanol fuel manufacturing enterprise.
Yet these technology also have certain limitation.At first, produce the raw oil of methanol fuel and form and the source complicacy, wayward.Bring influence with regard to the stability of giving the methanol fuel product like this.Up to now do not have stable automobile-used performance after also having a kind of stable additive formulations can make dissimilar processed oils and methyl alcohol allotment.Therefore, in order to make the methanol fuel product, particularly each item index of low ratio product can possibly comprise the additive with different adding purposes in the methanol fuel after the final optimization pass near existing processed oil; The second, because additive often is not limited only to general C, H, O material, the variety of the element of additive own is also brought new problem for the treating tail gas after the methanol fuel burning; The 3rd, also often be wanting in consideration for the interaction between the additive of various objectives; The 4th, there is contradiction between additive agent modified effect and the economy consumption.The additive technology limitation of methanol fuel will have influence on the quality product and the economy of methanol fuel to a certain extent.
Based on above consideration; Methanol fuel wants on quality product, to improve; Must eliminate or slow down some problems that methyl alcohol and processed oil allotment back exist through the change of being based on self internal composition, and the choice of technology that realizes this process can only to be method through catalyst modification realize.Like this; Fixture investment through increasing catalytic modification substitutes the pro rata depletion of additive of existing persistence with interim catalyst change expense, and this has reduced methanol fuel manufacturer to a certain extent and has bought the sc risk on the link at additive raw material.
Catalytic modification for methanol fuel can be divided into two kinds of methods; First kind of realization before the methanol fuel allotment that is the catalytic modification process simply allocated with methyl alcohol after can shifting to an earlier date the fine setting of foresight to some key indexs (like saturated vapor pressure, octane value etc.) of gasoline component again; Such catalytic modification process can be directly in the refining of petroleum smeltery auxiliary carrying out, adapt with production model, but this method can not thoroughly be eliminated the drawback in original production process with existing methanol fuel allotment enterprise.Second method is that methyl alcohol is carried out catalyst modification production by a certain percentage with after processed oil directly mixes again; The major advantage of this process is to make full use of the principal status of public economy of methyl alcohol in methanol fuel; Carry out some technological reaction schemes relevant and regulate methyl alcohol and in oil product, form, control the final product quality of methanol fuel according to this with methyl alcohol.
Summary of the invention
The purpose of this invention is to provide and a kind ofly change through catalyzed reaction that methanol fuel is inner to be formed, adapting to the catalytic modifying production process for methanol fuel of driving process each item index, thereby solve some common problems in the existing methanol fuel use.
The methanol fuel that relates among the present invention is mainly methyl alcohol and gasoline product, finished diesel fuel and existing lubricating oil methanol gasoline, methanol diesel-oil or the methyl alcohol lubricating oil after by the arbitrary proportion allotment.
Catalytic modifying production process for methanol fuel of the present invention is at first with obtaining light component and two kinds of oil products of heavy component after the flash distillation under the methanol fuel process certain temperature; Then, the two-way oil product after the modification is converged carry out obtaining the catalytic modification methanol fuel behind the line-blending then carrying out catalytic modification at least a entering catalyticreactor in the heavy component bottom the light component at flashing tower top and the flashing tower.
The confirming of methanol fuel flash vaporization point plays a major role according in the methanol fuel application process, going wrong, and the boiling spread of cut confirms.
Generally speaking; The M15 methanol gasoline is in order to suppress the saturated vapor pressure rising problem that high temperature causes and carry out catalytic modification; Need with the M15 methanol gasoline at common 50～80 ℃ of the high temperature ranges of summer engine interior and pipeline road, be under the maximum temperature condition of oil product volatility, volatile components is carried out flash separation; In order to improve the low-temperature cool starting performance of M85 methanol gasoline, the heavy ends that needs to be higher than in the flash separation M85 methanol gasoline 70～100 ℃ carries out catalytic modification; Therefore, the flash vaporization point of confirming methanol gasoline is 50～100 ℃.
In order to suppress the vapour lock problem and the bad problem of other oil product consistencies that low-proportion methanol diesel fuel possibly occur in summer; The light component that need flash off temperature and be 140～180 ℃ carries out catalytic modification; Therefore, the flash vaporization point of confirming methanol diesel-oil is 140～180 ℃.
Methyl alcohol lubricating oil can be according to lubricating oil quality and application target different, flash vaporization point is set at 70～120 ℃.
Catalyticreactor of the present invention comprises existing various type of reactor such as fixed-bed reactor, fluidized-bed reactor, paste state bed reactor, membrane reactor.
Wherein, The catalyzer that uses for the catalytic modification of top light component can be Fe system or Co series catalysts, methyl alcohol system MTBE process catalyzer, the aromatic alkylation catalysts that is used for the Fischer-Tropsch building-up process, also can be other common load-type solid acids, solid super acid catalyst; Modified catalyst for the bottom heavy component can use existing Industrial Catalysis cracking and catalytic reforming catalyst, also can use the modified product of these two types of catalyzer.The reaction velocity of top light component modification and bottom heavy component modification catalytic process is generally 200～2000h
-1, temperature of reaction is 200～500 ℃, reaction pressure 1～3MPa.
Further, flashing tower top light component is carried out catalytic modification, oil product after the modification and flashing tower bottom heavy component carry out blended methanol fuel working method and may further comprise the steps:
1) finished product raw oil is injected the methanol fuel storage tank, even according to allotment ratio adding methanol mixed then;
2) will allocate good methanol fuel and control, offer back segment with the constant flow, make the light component gasification, and, get into flashing tower and separate through reducing valve through constent temperature heater by volume pump via feed valve;
3) heavy component after the separation gets into the condensing surface cooling from the bottom through liquid meter, variable valve;
4) light component after the separation, gets into catalyticreactor through under meter and carries out catalytic modification after the machine that is compressed pressurizes through surge tank;
5) light component after the modification mixes with heavy component through stopping valve through after the condenser condenses, gets into methanol fuel product storage tank together.
Flashing tower bottom heavy component is carried out catalytic modification, and oil product after the modification and flashing tower top light component carry out blended methanol fuel working method and may further comprise the steps:
1) finished product raw oil is injected the methanol fuel storage tank, even according to allotment ratio adding methanol mixed then;
2) will allocate good methanol fuel and control, offer back segment with the constant flow, make the light component gasification, and, get into flashing tower and separate through reducing valve through constent temperature heater by volume pump via feed valve;
3) light component after the separation gets into the condensing surface cooling from top through liquid meter, variable valve;
4) heavy component after the separation, gets into catalyticreactor through under meter and carries out catalytic modification after the machine that is compressed pressurizes through surge tank;
5) heavy component after the modification mixes with light component through stopping valve through after the condenser condenses, gets into methanol fuel product storage tank together.
Simultaneously flashing tower top light component and bottom heavy component are carried out catalytic modification, the oil product after the modification carries out blended methanol fuel working method and may further comprise the steps:
1) finished product raw oil is injected the methanol fuel storage tank, even according to allotment ratio adding methanol mixed then;
2) will allocate good methanol fuel and control, offer back segment with the constant flow, make the light component gasification, and, get into flashing tower and separate through reducing valve through constent temperature heater by volume pump via feed valve;
3) heavy component after the separation, gets into catalyticreactor through under meter and carries out catalytic modification after the machine that is compressed pressurizes through surge tank;
4) light component after the separation, gets into catalyticreactor through under meter and carries out catalytic modification after the machine that is compressed pressurizes through surge tank;
5) light component after the modification and heavy component after condenser condenses separately, mix through stopping valve respectively, get into methanol fuel product storage tank together.
Catalytic modifying production process for methanol fuel of the present invention obviously is different from other traditional additive agent modified technology, has following beneficial effect:
1) reduces additive persistence consumption in original methanol fuel production process, reduced the raw material supply chain risk of methanol fuel.
2) can reduce the saturated vapor pressure 8～12KPa of low-proportion methanol fuel through modification, avoid the air-resistance phenomenon in the use to greatest extent light component.
3) can solve the cold start-up problem that high-proportion methanol fuel exists in the winter time through modification to heavy component.
4) through the methyl alcohol in the methanol fuel is rationally transformed, can further improve oil quality, improve 2～3 of the octane values of methanol gasoline, reduce by 5～9 of the cetane value of methanol diesel-oil, improve the power attribute of methanol fuel.
5) through rational catalyzed conversion, the oxygen in the methyl alcohol is obtained transforming with other forms, promoted the burning attribute of methanol fuel, reduced the routine discharging and the unconventional discharging of oil product to greatest extent.Find through experiment, decrease that this is significant for the benzene content that reduces in the motor vehicle exhaust, helps environment protection, reduce topsoil through benzene series thing content such as benzene, toluene in the gaseous fraction after the catalyzed reaction.
6) whole catalytic modification process only need increase optional equipments such as flashing tower and catalyticreactor in original allotment factory, and equipment is simple, and the scrap build expense is relatively low.
7) after the whole production flow process is controlled through strictness, can accomplish that zero pollutes and zero release, not have environmental problem, easily popularization.
8) this production technique is adapted to the catalytic modification of the methanol fuel in various raw material oil products source; The various finished product raw material oil products of various catalytic cracking, CR and shortening both be applicable to; For some low grade oilses, also can reach the purpose of improving the oil product use attribute through special catalytic treatment.
Description of drawings
Fig. 1 is a methanol fuel top light component catalytic modification process flow sheet;
Fig. 2 is a methanol fuel bottom heavy component catalytic modification process flow sheet;
Fig. 3 is the process flow sheet of methanol fuel top light component and bottom heavy component while catalytic modification;
Among the figure: 1---the methanol fuel storage tank; 2---feed valve; 3---volume pump; 4---constent temperature heater; 5---reducing valve; 6---flashing tower; 7---surge tank; 8---compressor; 9---under meter; 10---catalyticreactor; 11---tensimeter; 12---under meter; 13---variable valve; 14---condensing surface, 15---stopping valve; 16---condensing surface; 17---the product storage tank.
Embodiment
As shown in Figure 1, the 90# gasoline product is injected methanol fuel storage tank 1, even according to 17: 3 volume ratios adding methanol mixed, the M15 methanol gasoline is processed in allotment.
The M15 methanol gasoline that allotment is good via feed valve 2 with volume pump 3 with the constant flow through constent temperature heater 4, be heated to 80 ℃, with the light component gasification, get into flash tanks 6 through reducing valve 5 and separate into light component and heavy component; Heavy component after the separation gets into condensing surface 14 coolings from the bottom through liquid meter 12, variable valve 13.
Light component then gets in the surge tank 7; After compressor 8 pressurizations, get into catalyticreactor 10 through under meter 9, after the catalyzer of filling is the ZSM-5 reaming in the catalyticreactor 10; The supported rare earth metal catalyst; The control feed rate is 20mL/min, and temperature of reaction is carried out catalytic modification for 250 ℃, through the pressure in the tensimeter 11 online demonstration reactor drums.
Light component after the modification mixes with heavy component through stopping valve 15 through after condensing surface 16 condensations again, feeds at last in the methanol fuel product storage tank 17.
Through stratographic analysis, the alkene in the M15 methanol gasoline after the modification, alkane and benzene content all decrease, and volatile constituent content reduces about 30% with respect to the M15 methanol gasoline that does not contain additive.The experimental determination saturated vapor pressure reduces about 10KPa, and after high temperature season was applied to the vehicle of air-resistance phenomenon often occur, air-resistance phenomenon obviously reduced.
As shown in Figure 1, the 90# gasoline product is injected methanol fuel storage tank 1, even according to 7: 3 volume ratios adding methanol mixed, the M30 methanol gasoline is processed in allotment.
The M30 methanol gasoline that allotment is good via feed valve 2 with volume pump 3 with the constant flow through constent temperature heater 4, be heated to 80 ℃, with the light component gasification, get into flash tanks 6 through reducing valve 5 and separate into light component and heavy component; Heavy component after the separation gets into condensing surface 14 coolings from the bottom through liquid meter 12, variable valve 13.
Light component then gets in the surge tank 7; After compressor 8 pressurizations, get into catalyticreactor 10 through under meter 9, after the catalyticreactor 10 interior filling ZSM-5 reamings; Carried noble metal type catalyzer; The control feed rate is 20mL/min, and temperature of reaction is carried out catalytic modification for 250 ℃, through the pressure in the tensimeter 11 online demonstration reactor drums.
Light component after the modification mixes with heavy component through stopping valve 15 through after condensing surface 16 condensations again, feeds at last in the methanol fuel product storage tank 17.
Through stratographic analysis, alkene, alkane content in the M30 methanol gasoline after the modification all decrease, and the experimental determination saturated vapor pressure reduces about 6KPa, and after high temperature season was applied to the vehicle of air-resistance phenomenon often occur, air-resistance phenomenon obviously reduced.
As shown in Figure 2, the 90# gasoline product is injected methanol fuel storage tank 1, even according to 3: 17 volume ratios adding methanol mixed, the M85 methanol gasoline is processed in allotment.
The M85 methanol gasoline that allotment is good via feed valve 2 with volume pump 3 with the constant flow through constent temperature heater 4, be heated to 90 ℃, with the light component gasification, get into flash tanks 6 through reducing valve 5 and separate into light component and heavy component; Light component after the separation gets into condensing surface 14 coolings from the top through liquid meter 12, variable valve 13.
Heavy component gets in the surge tank 7; After compressor 8 pressurizations; Get into catalyticreactor 10 through under meter 9, the H beta catalyst in the catalyticreactor 10 after the filling modification, the control feed rate is 20mL/min; Temperature of reaction is carried out catalytic modification for 350 ℃, through the pressure in the tensimeter 11 online demonstration reactor drums.
Heavy component after the modification mixes with light component through stopping valve 15 through after condensing surface 16 condensations again, feeds at last in the methanol fuel product storage tank 17.
Through stratographic analysis, the alkene in the M85 methanol gasoline after the modification, alkane total content increase by 50%, and the oil product volatility increases greatly.The measuring octane value remains unchanged basically, vp rising 8～10KPa.After when low temperature, being applied to the vehicle of cold start-up problem occur, vehicle is one-shot, and difficult phenomenon does not take place to start.
Embodiment 4
As shown in Figure 3, the 90# gasoline product is injected methanol fuel storage tank 1, even according to 1: 1 volume ratio adding methanol mixed, the M50 methanol gasoline is processed in allotment.
The M50 methanol gasoline that allotment is good via feed valve 2 with volume pump 3 with the constant flow through constent temperature heater 4, be heated to 80 ℃, with the light component gasification, get into flash tanks 6 through reducing valve 5 and separate into light component and heavy component.
Light component after the separation upwards gets in the surge tank 7; After compressor 8 pressurizations; Get into catalyticreactor 10 through under meter 9, filling mordenite modified load noble metal type catalyzer in the catalyticreactor 10, the control feed rate is 15mL/min; Temperature of reaction is carried out catalytic modification for 250 ℃, through the pressure in the tensimeter 11 online demonstration reactor drums.
Heavy component then gets in the surge tank 7 downwards; After compressor 8 pressurizations; Get into catalyticreactor 10 through under meter 9, the H beta catalyst in the catalyticreactor 10 after the filling modification, the control feed rate is 20mL/min; Temperature of reaction is carried out catalytic modification for 380 ℃, through the pressure in the tensimeter 11 online demonstration reactor drums.
The component of two-way catalytic modification respectively through after condensing surface 16 condensations, is compiled through stopping valve 15 again, mixed the back and feed in the methanol fuel product storage tank 17.
Through stratographic analysis, alkene, alkane content in the M50 methanol gasoline after the modification all decrease, and the oil product octane value raises, and oxidation-resistance and stability obviously strengthen.Show through road tests: the oil product dynamic property after the modification is close with 90# gasoline or fair.
As shown in Figure 1, the 0# finished diesel fuel is injected methanol fuel storage tank 1, even according to 9: 1 volume ratios adding methanol mixed, the M10 methanol diesel-oil is processed in allotment.
The M10 methanol diesel-oil that allotment is good via feed valve 2 with volume pump 3 with the constant flow through constent temperature heater 4, be heated to 160 ℃, with the light component gasification, get into flash tanks 6 through reducing valve 5 and separate into light component and heavy component; Heavy component after the separation gets into condensing surface 14 coolings from the bottom through liquid meter 12, variable valve 13.
Light component then gets in the surge tank 7; After compressor 8 pressurizations; Get into catalyticreactor 10 through under meter 9, the activated carbon modified supported precious metal catalyst of filling in the catalyticreactor 10, the control feed rate is 30mL/min; Temperature of reaction is carried out catalytic modification for 250 ℃, through the pressure in the tensimeter 11 online demonstration reactor drums.
Light component after the modification mixes with heavy component through stopping valve 15 through after condensing surface 16 condensations again, feeds at last in the methanol fuel product storage tank 17.
Through stratographic analysis, 55 before by the modification of the cetane value of M10 methanol diesel-oil is reduced to 49 after the modification, and cold filter clogging temperature reduces by 11 ℃, has solved the compatibility problem of methanol diesel-oil, and the quality of methanol diesel-oil is improved.
Embodiment 6
As shown in Figure 1, the 0# finished diesel fuel is injected methanol fuel storage tank 1, even according to 8: 1 volume ratios adding methanol mixed, the M20 methanol diesel-oil is processed in allotment.
The M20 methanol diesel-oil that allotment is good via feed valve 2 with volume pump 3 with the constant flow through constent temperature heater 4, be heated to 180 ℃, with the light component gasification, get into flash tanks 6 through reducing valve 5 and separate into light component and heavy component; Heavy component after the separation gets into condensing surface 14 coolings from the bottom through liquid meter 12, variable valve 13.
Light component then gets in the surge tank 7; After compressor 8 pressurizations; Get into catalyticreactor 10 through under meter 9, filling ZSM-5 modified load noble metal catalyst in the catalyticreactor 10, the control feed rate is 30mL/min; Temperature of reaction is carried out catalytic modification for 350 ℃, through the pressure in the tensimeter 11 online demonstration reactor drums.
Light component after the modification mixes with heavy component through stopping valve 15 through after condensing surface 16 condensations again, feeds at last in the methanol fuel product storage tank 17.
Through stratographic analysis, 58 before by the modification of the cetane value of M20 methanol diesel-oil is reduced to 52 after the modification, and cold filter clogging temperature reduces by 11 ℃, and original methanol diesel-oil vapour lock in summer problem that occurs was effectively solved, and oil quality is able to obvious raising.
Claims (6)
1. catalytic modifying production process for methanol fuel; Described methanol fuel is methanol gasoline, methanol diesel-oil or the methyl alcohol lubricating oil that methyl alcohol and gasoline product, finished diesel fuel or lubricating oil are processed according to the arbitrary proportion allotment; It is characterized in that obtaining light component and two kinds of oil products of heavy component after the methanol fuel flash distillation; In the light component and at least a entering catalyticreactor in the heavy component bottom the flashing tower with the flashing tower top, at reaction velocity 200～2000h
-1, 200～500 ℃ of temperature of reaction are carried out catalytic modification under the condition of reaction pressure 1～3MPa; Wherein, the catalyzer that uses of top light component catalytic modification is Fe system or Co series catalysts, methyl alcohol system MTBE process catalyzer, the aromatic alkylation catalysts that is used for the Fischer-Tropsch building-up process; The catalyzer that bottom heavy component catalytic modification uses is Industrial Catalysis cracking and catalytic reforming catalyst or its modified product; Two-way oil product after the modification converges and carries out obtaining the catalytic modification methanol fuel behind the line-blending.
2. catalytic modifying production process for methanol fuel according to claim 1, the flash vaporization point that it is characterized in that described methanol fuel flash distillation is according to one of below the type selecting of methanol fuel:
A, when methanol fuel is methanol gasoline, flash vaporization point is 50～100 ℃;
B, when methanol fuel is methanol diesel-oil, flash vaporization point is 140～180 ℃;
C, when methanol fuel is methyl alcohol lubricating oil, flash vaporization point is 70～120 ℃.
3. catalytic modifying production process for methanol fuel according to claim 1 is characterized in that described catalyticreactor comprises fixed-bed reactor, fluidized-bed reactor, paste state bed reactor or membrane reactor.
4. catalytic modifying production process for methanol fuel according to claim 1 is characterized in that flashing tower top light component catalytic modification, and oil product mixes with flashing tower bottom heavy component after the modification, may further comprise the steps:
1) finished product raw oil is injected the methanol fuel storage tank, even according to allotment ratio adding methanol mixed;
2) will allocate good methanol fuel through feed valve, volume pump control, make the light component gasification, and, get into flashing tower and separate through reducing valve through constent temperature heater;
3) heavy component after the separation gets into the condensing surface cooling from the bottom through liquid meter, variable valve;
4) light component after the separation, gets into catalyticreactor through under meter and carries out catalytic modification after the machine that is compressed pressurizes through surge tank;
5) light component after the modification mixes with heavy component through stopping valve through after the condenser condenses, gets into methanol fuel product storage tank together.
5. catalytic modifying production process for methanol fuel according to claim 1 is characterized in that oil product mixes with flashing tower top light component after the modification, may further comprise the steps with flashing tower bottom heavy component catalytic modification:
1) finished product raw oil is injected the methanol fuel storage tank, even according to allotment ratio adding methanol mixed;
2) will allocate good methanol fuel through feed valve, volume pump control, make the light component gasification, and, get into flashing tower and separate through reducing valve through constent temperature heater;
3) light component after the separation gets into the condensing surface cooling from top through liquid meter, variable valve;
4) heavy component after the separation, gets into catalyticreactor through under meter and carries out catalytic modification after the machine that is compressed pressurizes through surge tank;
5) heavy component after the modification mixes with light component through stopping valve through after the condenser condenses, gets into methanol fuel product storage tank together.
6. catalytic modifying production process for methanol fuel according to claim 1 is characterized in that simultaneously with flashing tower top light component and bottom heavy component catalytic modification, oil product mixes after the modification, may further comprise the steps:
1) finished product raw oil is injected the methanol fuel storage tank, even according to allotment ratio adding methanol mixed;
2) will allocate good methanol fuel through feed valve, volume pump control, make the light component gasification, and, get into flashing tower and separate through reducing valve through constent temperature heater;
3) heavy component after the separation, gets into catalyticreactor through under meter and carries out catalytic modification after the machine that is compressed pressurizes through surge tank;
4) light component after the separation, gets into another catalyticreactor through under meter and carries out catalytic modification after the machine that is compressed pressurizes through another surge tank;
5) light component after the modification and heavy component after condenser condenses separately, mix through stopping valve respectively, get into methanol fuel product storage tank together.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1994012592A1 (en) * | 1992-11-26 | 1994-06-09 | University Of Waterloo | An improved process for the thermal conversion of biomass to liquids |
| CN1580199A (en) * | 2003-08-05 | 2005-02-16 | 中国科学院大连化学物理研究所 | Process for modifying petrol by etherification and aromatization |
| CN101016468A (en) * | 2007-02-13 | 2007-08-15 | 中国矿业大学 | Method and device of modifying and quality increasing biomass liquefied oil under mild condition |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1994012592A1 (en) * | 1992-11-26 | 1994-06-09 | University Of Waterloo | An improved process for the thermal conversion of biomass to liquids |
| CN1580199A (en) * | 2003-08-05 | 2005-02-16 | 中国科学院大连化学物理研究所 | Process for modifying petrol by etherification and aromatization |
| CN101016468A (en) * | 2007-02-13 | 2007-08-15 | 中国矿业大学 | Method and device of modifying and quality increasing biomass liquefied oil under mild condition |
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