CN106281400A - A kind of synthesis gas converts the integrated technology process of gasoline processed - Google Patents
A kind of synthesis gas converts the integrated technology process of gasoline processed Download PDFInfo
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Abstract
The present invention relates to a kind of synthesis gas and convert the integrated technology process of gasoline processed.This integrated technology process includes that synthesis gas is converted into the product containing methanol and dimethyl ether, product containing methanol and dimethyl ether is converted into middle distillate hydrocarbon, in middle distillate hydrocarbon, lower carbon number hydrocarbons is converted into three steps of gasoline fraction, in the final hydrocarbon product that integrated process is obtained, gasoline fraction is mainly C5-C11Hydrocarbon, at the carbon distribution of product hydrocarbon up to 87%, wherein isoparaffin accounts for～60%, alkene < 5%, aromatic hydrocarbons～25%.The invention provides an economic route effectively obtaining high-quality liquid fuel with non-oil resource for raw material.
Description
Technical field
The present invention relates to a kind of synthesis gas from coal, biomass, natural gas etc. and convert the collection of gasoline processed
Become process.Specifically, this integrated technique refers to that synthesis gas sequentially passes through synthesis gas and converts first processed
Alcohol/dimethyl ether catalyst, methanol/dimethyl ether conversion are the molecular sieve of middle distillate hydrocarbon or metal-modified point
Sub-sieve catalyst system and or lower carbon number hydrocarbons be converted into molecular sieve or the metal modified molecular screen of gasoline fraction
Catalyst system prepares low alkene, low aromatic hydrocarbons, gasoline fraction rich in isoparaffin.
Technical background
Gasoline is as the indispensable fuel of the modern means of communication, and its source is generally petrochemical industry.
However as the continuous minimizing of petroleum resources reserves, obtaining liquid fuel by other routes becomes research
Emphasis.Synthesis gas can pass through steam reformation technology, Partial Oxidation technology, self-heating recapitalization technology
Deng, obtain from non-oil resources such as coal, natural gas, biomass, therefore synthesis gas prepares liquid fuel
Can effectively alleviate oil shortage pressure.
The standard weighing quality of gasoline is octane number, i.e. gasoline energy of Ulva Pertusa burning in automobile cylinder
Power.In gasoline fraction, isoparaffin, alkene, aromatic hydrocarbons etc. are the main contributions components of octane number.
But, the imperfect combustion of alkene and aromatic hydrocarbons can cause the discharge of harmful substance in vehicle exhaust, too much
Automobile engine is also adversely affected by alkene and the aromatic hydrocarbons of content.Isoparaffin, have octane number high,
The features such as sensitivity is good, steam forces down, are the high octane value gasoline blending components of preferable clean environment firendly.
The increasingly stringent limited alkene in gasoline and arene content along with environmental regulation, improves in gasoline fraction
The importance day of isoparaffin content is aobvious prominent.The production of current industrial isoparaffin is mainly derived from
Petrochemical industry, is concentrated mainly on Fischer-Tropsch from the synthesis gas preparation collection of reports rich in isoparaffin gasoline and closes
Become in technique, as Shanxi Coal-Chemical Inst., Chinese Academy of Sciences reports (Applied Catalysis A:General
408 (2011) 38 46) CoZr/H-ZSM-5 composite catalyst, Japan folic hill university reports
The Co base of the mesoporous ZSM-5 parcel of (Catalysis Communications 55 (2014) 53 56) is urged
Agent, Co/M (Ru, the Ni)/HZSM-5 of Zhejiang University's report (Fuel 108 (2013) 597 603)
Catalyst etc. although can improve the selectivity of gasoline fraction and different in gasoline fraction by modification
The content of structure hydrocarbon, but C12+The by-product such as heavy hydrocarbon and methane is the most a lot.
Synthesis gas also has been reported that for the technique of gasoline through dimethyl ether, in Russian Academy Of Sciences document
The synthesis gas warp that (Kinetics and Catalysis, 2007, Vol.48, No.6, pp.789 793) reports
The process of dimethyl ether one step gasoline, although the selectivity of gasoline fraction can reach 60% in product
Left and right, in gasoline fraction, isoparaffin is more than 54%, but due in composite catalyst methanol-fueled CLC urge
The hydrogenation changed, C2-C4Hydrocarbon is all saturated hydrocarbons, and reaction pressure is at 10MPa, related process
Document (Chemical Engineering Science 55 (2000) 1845-1855) also report, this mistake
The water gas shift reation of Cheng Yin strengthening, produces substantial amounts of CO2, cause CO the lowest to the transformation efficiency of hydrocarbon.
The multistage bed technique (Fuel 134 (2014) 11 16) of other technique such as Dalian Chemistry and Physics Institute report,Report TIGAS (Integrated GAsoline Synthesis) technique (J.Stud.Surf.Sci.Catal.1988,36,293.) etc., the group of gasoline in product
Although divide and the content of isoparaffin is the highest, but such as multistage bed technique (Fuel 134 (2014)
11 16) reported in, by-product C2-C4Hydrocarbon is mainly saturated hydrocarbons, reduces the utilization of by-product
It is worth.A kind of synthesis gas that Primus Green company (US20120116137A1) reports is through diformazan
Ether gasoline process, gasoline fraction (C4+In), linear paraffin and isoparaffin sum account for 30-45%,
Cycloalkane 15-25%, aromatic hydrocarbons 30%-55%, and Pioneer Energy company (US20140172191A1)
A kind of synthesis gas of report is through dimethyl ether gasoline process, and this technique is combined with membrane reactor, obtains
The C5+ of 59.1% in product hydrocarbon, all aromatic hydrocarbons of gasoline fraction.
A kind of synthesis gas of present invention report converts the integrated technology process of gasoline processed, can realize high selection
Property ground produced rich in isoparaffin, low alkene, the gasoline fraction of low arene content by synthesis gas, will be
Reduce dependence aspect and environmental conservation aspect to petroleum resources and make bigger contribution.
Summary of the invention
The present invention is directed in traditional gasoline production method, isoparaffin content is low, alkene and virtue
The problem that hydrocarbon content is high provides the integrated technology process that a kind of new a kind of synthesis gas converts gasoline processed.Adopt
Can produce by this process and there is the gasoline that isoparaffin content height, aromatic hydrocarbons and olefin(e) centent are low.
Technical solution of the present invention comprises the following steps:
Synthesis gas is converted into the product containing methanol and dimethyl ether, and above-mentioned product is converted into midbarrel
Hydrocarbon, middle distillate hydrocarbon isolated gasoline, or middle distillate hydrocarbon is isolated lower carbon number hydrocarbons, lower carbon number hydrocarbons turns
Turn to gasoline.
This technique with synthesis gas as raw material, wherein H2The ratio of/CO is 0.5-5, preferably 0.5-3；
Synthesis gas is converted into the reaction temperature containing methanol and the product of dimethyl ether and is 210-350 DEG C, preferably
240-320 DEG C, reaction pressure is 0.001-8.0MPa, preferably 2-5MPa, and mass space velocity is
500h-1-10000h-1, preferably 500-6000h-1；Product containing methanol and dimethyl ether is converted into centre
The reaction temperature of fraction hydrocarbon is 300-500 DEG C, preferably 320-450 DEG C, and reaction pressure is
0.001-8.0MPa, preferably 2-5MPa, air speed is 500h-1-10000h-1, preferably 500-6000h-1；
Mixing lower carbon number hydrocarbons is converted into the reaction temperature of gasoline and is 50-500 DEG C, preferably 50-350 DEG C, reaction pressure
For 0.001-8.0MPa, preferably 0-4MPa, air speed is 500h-1-10000h-1, preferably 500-6000h-1。
Final gasoline products component distribution has the following characteristics that obtained hydrocarbon product, and gasoline evaporates
Divide predominantly C5-C11Hydrocarbon, at the carbon distribution of product hydrocarbon up to 87%, wherein isoparaffin accounts for～60%,
Alkene < 5%, aromatic hydrocarbons～25%.
The present invention uses catalyst mainly to include, and synthesis gas converts methanol/dimethyl ether catalyst processed and metal changes
The molecular sieve of property.
Described synthesis gas is converted into containing methanol and the process of the product of dimethyl ether, and catalysts is first
The composite catalyst that alcohol synthetic catalyst forms with solid acid catalyst.Preparation method is as follows:
Weigh methanol synthesis catalyst and the solid acid catalyst of certain mass respectively, close by wherein methanol
Becoming catalyst is 0.5-4:1, preferably 1-3:1 with the mass ratio of solid acid catalyst, powder in mortar
End uniformly mixing, compression molding.
Described methanol synthesis catalyst is Cu-ZnO-Al2O3Component, Cu-ZnO-ZrO2Component,
ZnO-Cr2O3Component, Pd/CeO2One or more in component.Described solid acid catalyst refers to:
γ-Al2O3, modified γ-Al2O3, molecular sieve or TiO2In one or two or more kinds, preferably γ-Al2O3；
Above-mentioned molecular sieve is the three dimensional skeletal structure molecular sieve of 10 membered ring channels or has three-dimensional framework knot
One in the metal modified molecular screen of structure or two kinds, the one in preferably HZSM-5 or HY or two
Kind；Metal in above-mentioned metal modified molecular screen is the one in Pd, Pt, Cu, La, Zn or Ga
Or more than two kinds, preferably Zn；
In metal modified molecular screen, metal component accounts for the mass percent of molecular sieve before modified and is
0.01-30wt%, preferred mass percentage ratio is 0.01wt%-20wt%.
The preparation method of metal modified molecular screen is as follows:
Make with infusion process, ion exchange, deposition-precipitation method or coprecipitation, modified product
80-150 DEG C dry 4-12 hour, and then in 400-700 DEG C of roasting 4-12 hour, hydrogen atmosphere is normal
Pressure reduction 4-12 hour, obtains metal modified molecular screen.
It is to there is three-dimensional open-framework HZSM-5 molecular sieve, as a example by metal used is Zn with molecular sieve:
Weigh a certain amount of HZSM-5 molecular sieve, then weigh zinc nitrate by required mass ratio, be dissolved in steaming
In distilled water, being slowly added into by zinc nitrate solution in HZSM-5 molecular sieve, now molecular sieve is immersed in
In zinc nitrate solution.It is after impregnating 10-30 hour, catalyst is dry 4-12 hour at 80-150 DEG C,
Roasting 4-12 hour at 400-700 DEG C afterwards, preferably 500-600 DEG C；Roasting time at least 2
Hour, it was preferred with 4-6 hour；Heating rate is at least 0.5 DEG C/min, is preferred with 1.5-5 DEG C/min,
20-40 mesh granule made by tabletting, and hydrogen atmosphere normal pressure reduces 4-12 hour.
Catalyst is in hydrogen atmosphere, and synthesis gas converts methanol/dimethyl ether catalyst processed at 230-300 DEG C
At a temperature of pretreatment 2-8 hour, metal modified molecular screen 260-400 DEG C of pretreatment 2-8 hour,
Then synthesis gas is incorporated in reaction system, reacts.
The catalyst that product containing methanol and dimethyl ether uses during being converted into middle distillate hydrocarbon
For the metal-modified molecular sieve of one or two or more kinds in Pd, Pt, Cu, La, Zn, Ga.
It is in Pd, Pt, Cu, La, Zn, Ga that mixing lower carbon number hydrocarbons converts gasoline used catalyst processed
One or two or more kinds metal-modified molecular sieve, load phosphoric acid solid acid catalyst, load miscellaneous many
One or two or more kinds in solid acid catalyst, concentrated sulphuric acid or the HF acid of acid, the most metal-modified
Molecular sieve.
Midbarrel isolates heavy end gasoline and light ends mixing lower carbon number hydrocarbons by fractionating process,
Mixing lower carbon number hydrocarbons is in circulating pump is reintroduced back to reactor II, or is directly entered in reactor III
The chain propagation reactions such as row olefinic polymerization and alkylation.
The present invention uses HZSM-5 molecular sieve and metal-modified HZSM-5 molecular sieve as containing first
The product of alcohol and dimethyl ether converts the catalyst of middle distillate hydrocarbon processed.Gasoline fraction in middle distillate hydrocarbon
One way selectivity is up to 74%, and gasoline fraction is mainly carbon number at C5-C11Hydrocarbon, including positive structure
Alkane, isoparaffin, cycloalkane, alkene and aromatic hydrocarbons；C2-C4In lower carbon number hydrocarbons, the content of alkene is 62%
Above.
The present invention uses metal modified molecular screen, or the heteropolyacid catalyst of solid supported or dense sulfur
Lower carbon number hydrocarbons reforming catalyst is made in acid, will be enriched in the C of alkene2-C4Lower carbon number hydrocarbons is converted into gasoline fraction.?
The gasoline fraction of this integrated technique carbon selectivity in hydrocarbon can reach more than 87% eventually, wherein isomery
Determination of Alkane Content is about 60%, and the product of the method generation is separated can be as a kind of eco-friendly car
With gasoline products, thus this technique has good application prospect.
Accompanying drawing explanation
Fig. 1 synthesis gas converts gasoline integrated technique schematic diagram I processed.
Fig. 2 synthesis gas converts gasoline integrated technique schematic diagram II processed.
Detailed description of the invention
The technology of the present invention details is by the detailed description in addition of following embodiment.It should be noted that lifted reality
Executing example, its effect simply further illustrates the technical characteristic of the present invention rather than limits the present invention.
Following example are carried out on synthesizer shown in Fig. 1, Fig. 2, process base.
Embodiment 1
The present embodiment technique as shown in Figure 1 is carried out.
By H type ZSM-5 molecular sieve fine powder, roasting 4 hours at 550 DEG C, 20 mesh made by tabletting
Grain, the methanol/dimethyl ether conversion midbarrel hydrocarbon catalyst in integrated process.
0.6gCu-ZnO-Al is loaded in reactor I2O3/γ-Al2O3Dimethyl ether synthetic catalyst, quality
Ratio 1.8:1, reaction temperature 260 DEG C, pressure 3MPa, air speed 2500ml.h-1.g-1；Reactor II
The HZSM-5 of interior filling 0.45g, reaction temperature 350 DEG C, pressure 3MPa, mass space velocity is
3333ml.h-1.g-1；H2React under/CO=1, use gas chromatographic analysis product.Product
Hydrocarbon distribution is shown in Table 1.CO conversion ratio about 60%, C in middle distillate hydrocarbon5-C11Fraction selectivity exists
More than 74%, wherein isoparaffin selectivity is about 40%, C2-C4In hydrocarbon, alkene accounts for 9.6%.
Embodiment 2
The present embodiment technique as shown in Figure 1 is carried out.
By HZSM-5 molecular sieve at two parts of Zn (NO Han different quality3)2Zn (NO3)2Solution is (molten
Zn (NO in liquid3)2Quality be respectively in this solution 1% He of HZSM-5 molecular sieve of dipping
10%) in after dipping 12-24min, take out, carry out following operation respectively: 120 DEG C are dried 4 hours,
Roasting 4 hours in 550 DEG C of air, tabletting makes 20 mesh granules, and hydrogen atmosphere normal pressure reduces 4 hours,
Methanol/dimethyl ether conversion middle distillate hydrocarbon process catalyst in integrated process:
In ZnZSM-5, Zn accounts for the mass percent of original molecule sieve, and wt% is respectively 1 and 10.
0.6g Cu-ZnO-Al is loaded in reactor I2O3/γ-Al2O3Dimethyl ether synthetic catalyst, quality
Ratio 1.8:1, reaction temperature 260 DEG C, 3MPa, mass space velocity is 2500ml.h-1.g-1；Reactor II
Interior filling 0.45g above-mentioned methanol/dimethyl ether conversion middle distillate hydrocarbon process catalyst, reaction temperature
350 DEG C, reaction pressure 3MPa, mass space velocity is 3333ml.h-1.g-1；H2React under/CO=1.
Use gas chromatographic analysis product.Owing to the conversion ratio of CO is converted methanol/diformazan processed by synthesis gas
Ether process control, in the case of in ensureing every secondary response, in reactor I, reaction condition is identical, CO
Conversion ratio about 60%, C in middle distillate hydrocarbon5-C11The selectivity of fraction, C5-C11In fraction different
The selectivity of structure alkane, and other product hydrocarbon are distributed and the relation of Zn content is shown in Table 1.
Compare with embodiment 1, do methanol/dimethyl ether conversion midbarrel with ZnZSM-5 molecular sieve
Hydrocarbon process catalyst, C5-C11In fraction, the content of aromatic hydrocarbons is substantially reduced, and the content of isoparaffin is significantly
Degree increases.Along with the increase of Zn content, C in ZnZSM-55-C11In fraction, the content of aromatic hydrocarbons reduces,
C simultaneously2-C4In fraction, the content of alkene increases, and illustrates that molecular sieve modified for Zn is possible not only to reduce vapour
The content of aromatic hydrocarbons in oil distillate, it is also possible to stop C2-C4The hydrogenation of alkene in hydrocarbon, improves by-product
C2-C4The content of alkene in fraction, and then improve the value of by-product.
The impact of table 1.Zn content middle distillate hydrocarbon composition distribution
Embodiment 3
The present embodiment technique as shown in Figure 2 is carried out.
1g Cu-ZnO-Al is loaded in reactor I2O3/γ-Al2O3Dimethyl ether synthetic catalyst, quality
Ratio 1.8:1, reaction temperature 260 DEG C, pressure 3MPa, mass space velocity is 2500ml.h-1.g-1；Reaction
The Zn1%-ZSM-5 catalyst of filling 0.45g embodiment 2 preparation in device II, reaction temperature 350 DEG C,
Pressure 3MPa, mass space velocity is 3333ml.h-1.g-1；0.5g Pt0.5%-ZSM-5 is loaded in reactor III
Molecular sieve catalyst, reaction pressure 3MPa, mass space velocity is 3333ml.h-1.g-1；H2Under/CO=1,
Synthesis gas converts methanol/dimethyl ether processed, methanol/dimethyl ether conversion gasoline and mixing lower carbon number hydrocarbons convert
Process of gasoline processed is integrated and reacts, and uses gas chromatographic analysis product.CO conversion ratio 65%
Left and right, the gasoline that integrated technique is generated content in product hydrocarbon, each constituent content in gasoline fraction,
And the distribution of other product hydrocarbon is shown in Table 2.As known from Table 2, gasoline fraction selectivity in product hydrocarbon is
88.8%, in gasoline fraction, the selectivity of isoparaffin is 54%, compared with data in table 1, and gasoline
Selectivity and gasoline fraction in the content of isoparaffin all increased considerably.
Table 2 synthesis gas converts the product hydrocarbon distribution of gasoline integrated technique processed
Embodiment 4
The present embodiment technique as shown in Figure 2 is carried out.
0.6g Cu-ZnO-Al is loaded in reactor I2O3/γ-Al2O3Dimethyl ether synthetic catalyst, quality
Ratio 1.8:1, reaction temperature 260 DEG C, pressure 3MPa, mass space velocity is 2500ml.h-1.g-1；Reaction
The Zn1%-ZSM-5 catalyst of filling 0.45g embodiment 2 preparation in device II, reaction temperature 380 DEG C,
Reaction pressure 4MPa, mass space velocity 2500ml.h-1.g-1；The Pd-β of filling 0.5g in reactor III
Molecular sieve catalyst, wherein the mass percent of Pd is 0.5%, and mass space velocity is 3333ml.h-1.g-1；
H2React under/CO=1, use gas chromatographic analysis product.CO conversion ratio brings up to 72%
Above, the gasoline that integrated technique is generated content in product hydrocarbonaceous, isoparaffin in gasoline fraction
Content, and other product hydrocarbon distribution be shown in Table 3.
The product hydrocarbon distribution of integrated technique when table 3 reaction pressure is 4MPa
Embodiment 5
The present embodiment technique as shown in Figure 1 is carried out.
0.6g Cu-ZnO-Al is loaded in reactor I2O3/γ-Al2O3Dimethyl ether synthetic catalyst, quality
Ratio 1.8:1, reaction temperature 260 DEG C, pressure 3MPa, mass space velocity is 3333ml.h-1.g-1；Reaction
The Zn1%-ZSM-5 catalyst of 0.45g embodiment 2 preparation, reaction temperature is loaded in device II
300-350 DEG C, reaction pressure 3MPa, mass space velocity is 3333ml.h-1.g-1；H2/ CO is the conjunction of 3
Becoming and react under gas charging, the mixing lower carbon number hydrocarbons after separation turns in circulation reenters reactor II
Changing, final product uses gas chromatographic analysis.CO conversion ratio is 73.5%, and integrated technique is given birth to
The gasoline become content in product hydrocarbon, each constituent content in gasoline fraction, and the distribution of other product hydrocarbon
It is shown in Table 4.
H in table 4 synthesis gas2The hydrocarbon distribution of integrated technique when/CO is 3
As known from Table 4, after byproduct ethylene, propylene convert in circulating in reactor II, C5-C11
Fraction hydrocarbon-selective can reach 87.5%, and wherein in gasoline fraction, isoparaffin content is 60.1%.
Accordingly it can be seen that the mixing lower carbon number hydrocarbons separated of conversion and cycle, vapour in product hydrocarbon can be effectively improved
Oil distillate and the yield of isoparaffin.
Claims (7)
1. the integrated technology process of a synthesis gas conversion gasoline processed, it is characterised in that:
Step is as follows: synthesis gas is converted into the product containing methanol and dimethyl ether, and above-mentioned product is converted into
Middle distillate hydrocarbon, middle distillate hydrocarbon isolated gasoline, or middle distillate hydrocarbon is isolated lower carbon number hydrocarbons,
Lower carbon number hydrocarbons is converted into gasoline.
Integrated technology process the most according to claim 1, it is characterised in that: described synthesis gas turns
Turning to containing methanol and the process of the product of dimethyl ether, catalysts is that methanol synthesis catalyst is with solid
The composite catalyst of body acid catalyst composition.
Integrated technology process the most according to claim 2, it is characterised in that:
The composite catalyst that described methanol synthesis catalyst forms with solid acid catalyst, wherein methanol closes
Becoming catalyst is 0.5-4:1, preferably 1-3:1 with the mass ratio of solid acid catalyst；
Described methanol synthesis catalyst is Cu-ZnO-Al2O3Component, Cu-ZnO-ZrO2Component,
ZnO-Cr2O3Component, Pd/CeO2One or more in component；
Described solid acid catalyst refers to: γ-Al2O3, modified γ-Al2O3, molecular sieve or TiO2In
One or two or more kinds, preferably γ-Al2O3；
Above-mentioned molecular sieve is the three dimensional skeletal structure molecular sieve of 10 membered ring channels or has three-dimensional framework knot
One in the metal modified molecular screen of structure or two kinds, the one in preferably HZSM-5 or HY or two
Kind；Metal in above-mentioned metal modified molecular screen is the one in Pd, Pt, Cu, La, Zn or Ga
Or more than two kinds, preferably Zn；
In metal modified molecular screen, metal component accounts for the mass percent of molecular sieve before modified and is
0.01-30wt%, preferred mass percentage ratio is 0.01wt%-20wt%；
The preparation method of above-mentioned metal modified molecular screen is: sink with infusion process, ion exchange, deposition
Shallow lake method or coprecipitation are made, dry 4-12 hour of modified product 80-150 DEG C, then in
400-700 DEG C of roasting 4-12 hour, hydrogen atmosphere normal pressure reduces 4-12 hour, obtains metal-modified point
Son sieve.
Integrated technology process the most according to claim 1, it is characterised in that:
The catalyst that product containing methanol and dimethyl ether uses during being converted into middle distillate hydrocarbon
For the metal-modified molecular sieve of one or two or more kinds in Pd, Pt, Cu, La, Zn, Ga.
Integrated technology process the most according to claim 1, it is characterised in that: mixing lower carbon number hydrocarbons turns
Changing gasoline used catalyst processed is one or two or more kinds gold in Pd, Pt, Cu, La, Zn, Ga
Belong to modified molecular sieve, the load solid acid catalyst of phosphoric acid, the solid acid catalyst of carried heteropoly acid,
One or two or more kinds in concentrated sulphuric acid or HF acid, the most metal-modified molecular sieve.
Integrated technology process the most according to claim 1, it is characterised in that:
Synthesis gas is converted into the reaction temperature containing methanol and the product of dimethyl ether and is 210-350 DEG C, excellent
Selecting 240-320 DEG C, reaction pressure is 0.001-8.0MPa, preferably 2-5MPa, and mass space velocity is
500h-1-10000h-1, preferably 500-6000h-1；Product containing methanol and dimethyl ether is converted into centre
The reaction temperature of fraction hydrocarbon is 300-500 DEG C, preferably 320-450 DEG C, and reaction pressure is
0.001-8.0MPa, preferably 2-5MPa, air speed is 500h-1-10000h-1, preferably 500-6000h-1；
Mixing lower carbon number hydrocarbons is converted into the reaction temperature of gasoline and is 50-500 DEG C, preferably 50-350 DEG C, reaction pressure
For 0.001-8.0MPa, preferably 0-4MPa, air speed is 500h-1-10000h-1, preferably 500-6000h-1。
Integrated technology process the most according to claim 1, it is characterised in that: in described synthesis gas
H2It is 0.5-5, preferably 0.5-3 with the mol ratio of CO.
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| WO2023199557A1 (en) * | 2022-04-15 | 2023-10-19 | 古河電気工業株式会社 | Catalyst for liquefied petroleum gas synthesis, and method for producing liquefied petroleum gas |
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