CN1015171B - Improved syngas conversion catalyst - Google Patents
Improved syngas conversion catalystInfo
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- CN1015171B CN1015171B CN 90104171 CN90104171A CN1015171B CN 1015171 B CN1015171 B CN 1015171B CN 90104171 CN90104171 CN 90104171 CN 90104171 A CN90104171 A CN 90104171A CN 1015171 B CN1015171 B CN 1015171B
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Abstract
The present invention relates to a method for preparring hydrocarbons with more than one carbon atoms by synthesis gas, which includes, in the temperature from 190 to 400.degree.C and under the pressure from 1 to 100, contacting synthesis gas with reductive activation as a catalyst, having formula(I): RuzAbCeOx (I), wherein A is an alkali metal, x is a number such that the valence requirements of the other elements for oxygen is satisfied, a is greater than zero and less than 5% w/w, based on the total weight of the composition, b is in the range from zero to 10% w/w, based on the total weight of the composition.
Description
The present invention relates to a kind of mixed gas (hereinafter being referred to as synthetic gas) that is used for mainly to contain carbon monoxide and hydrogen and change into carbonatoms greater than 1 hydrocarbon, especially change into the preparation method of the improved catalyst of gasoline boiling spread aliphatic hydrocrbon, also relate to the catalyzer that makes thus and make synthetic gas change into application aspect the above-mentioned hydrocarbon.
Be used to make synthetic gas to change into the Fischer-Tropsch process of hydrocarbon, known for many years by people, but this method is in the country in dominant South Africa of unique economic factors and so on, just has industrial meaning.The importance of this class alternate energy source of coal and Sweet natural gas is growing, and people are taken up to Fischer-Tropsch process again, thinks that it is attractive, and is an acceptable approach of producing the high quality transport fuel in environmental protection.
Everybody knows for a long time, and the ruthenium in the VIII family metal is one of the highest catalyzer of synthetic gas activity of conversion.Medium and be higher than under the medium pressure, its product is a high molecular paraffin; Under low pressure mainly be methane.Recent some patents of announcing, for example United States Patent (USP) the 4th, 042,614,4,171,320,4,206,134,4,413,064 and 4,410, No. 637, with English Patent A-2,119, No. 277, description also claims that adopting with the ruthenium is the catalyzer of active ingredient, can make different products by synthetic gas.
United States Patent (USP) the 4th, 042, No. 614 have been described a kind of employing is the ruthenium catalyst of carrier with the titanium-containing oxide, is selected to synthesize by synthetic gas to comprise that chain length is C
2To C
10Method at interior alkene.Titanium-containing oxide carrier in the above-mentioned catalyzer is selected from TiO
2, ZrTiO
4, TiO
2-C, TiO
2-Al
2O
3, TiO
2-SiO
2, titanates of alkali-earth metals, rare earth metal titanate and its mixture.
United States Patent (USP) the 4th, 171 has been described a kind of employing ruthenium catalyst for No. 320 and has been comprised that by synthetic gas is synthetic chain length is C
2To C
5Method at interior alkene.The carrier of ruthenium catalyst is selected from V
2O
3, Nb
2O
5, Ta
2O
5, Al
2O
3-V
2O
3, Al
2O
3-Nb
2O
5, Al
2O
3-Ta
2O
5, SiO
2-V
2O
5, SiO
2-Nb
2O
5, SiO
2-Ta
2O
5, V
2O
3-C, Nb
2O
5-C, Ta
2O
5The oxide compound of-C, alkaline-earth metal-VB family, oxide compound and its mixture of the oxide compound of basic metal-VB family, IV B family-VB family.
United States Patent (USP) the 4th, 206 has been described a kind of employing to contain the ruthenium catalyst that Mn oxide is a carrier No. 134, is forcing down under the situation of methane production, strengthens synthetic C by synthetic gas
2～C
4The method of alkene.The wherein said Mn oxide carrier that contains is selected from MnO, Al
2O
3-MnO, SiO
2The oxide compound of the oxide compound of-MnO, MnO-C, IV B family-manganese, VB family-manganese, the oxide compound of alkaline-earth metal-manganese and its mixture.
United States Patent (USP) the 4th, described the method that a kind of synthetic gas transforms for 413, No. 064, the straight-chain paraffin content in the product that is obtained by synthetic gas in the diesel oil boiling range is very high, the catalyzer that adopts mainly contains cobalt, Thorotrast or lanthanum trioxide and ruthenium, and carrier is r-aluminum oxide, η-aluminum oxide or its mixture.Described catalyzer is that the organic dipping solution of non-water by the water soaking solution of the aluminum oxide pulverized and (A) cobalt salt and (B) ruthenium salt and thorium salt or lanthanum salt contacts and makes.
United States Patent (USP) the 4th, 410, described for No. 637 a kind of by synthesis gas preparation basically by C
5～C
12The method of the hydrocarbon mixture that hydrocarbon is formed.Catalyst system therefor iron content, nickel, cobalt, chromium and (or) in the ruthenium etc. one or more, carrier is magadite, is a kind of crystalline layered silicate, can absorb metal ion or metal-salt at interlayer.
People such as Kieffer have described the reaction on rare earth metal oxide catalyst of carbon monoxide and hydrogen in " chemical communication (Chemical Communication) " (nineteen eighty-three, 763～764 pages).The catalyzer of being studied has Pd-La
2O
3And Pd-Dy
2O
3, the both uses immersion process for preparing.
At last, English Patent A-2 has described a kind of mixture or the mixture of hydrogen and carbonic acid gas catalyzer of selecting synthetic alkene by hydrogen and carbon monoxide for 119, No. 277.This catalyzer comprises the ruthenium carbonyl compound that is deposited in the carrier that contains cerium dioxide.Disclose among the embodiment 3 and used RuCl
33H
2The catalyzer that the O aqueous solution [ruthenium content is a 0.62%(weight)] dipping cerium dioxide makes.(test 9) produced undesirable high yield methane (35.7%) when this impregnated catalyst was used for the synthetic gas conversion, and the olefine selective very low (1.6%) that hope is wanted.
At our European patent application publication No. 10169743(BP Case No.5890) in, a kind of method for compositions of preparation has been described.Prepared composition as catalyzer, changes into carbonatoms greater than 1 hydrocarbon with synthetic gas after reductibility activation.The chemical formula of this composition is:
In the formula:
A is a kind of basic metal,
X is a numeral, and the valency needs number of other element to oxygen satisfied in expression,
A is greater than 0 and less than 1%(weight) (pressing the total weight of composition),
B 0 to 10%(weight) in the scope (pressing the total weight of composition),
Ce and O are the rest part of composition.
Its preparation method may further comprise the steps:
(A) with the carbonate of the soluble salt of metal Ru and cerium and alkali metal containing or ammonium and (or) supercarbonate and (or) precipitation agent of oxyhydroxide mixes in solution, so just can form the throw out that contains ruthenium and cerium, but this throw out thermolysis is its oxide compound;
(B) throw out of recycling step (A) gained.
In the specific embodiments of this invention of special in the above narration, the aqueous solution of precipitation agent is added in the aqueous solution of metal water-soluble salt.
We are surprised to find that now, when one or more solution with ruthenium and cerium compound and a kind of alkali metal compound of choosing wantonly join in the precipitant solution, can obtain high reactivity and long-life catalyzer, but the adding order is opposite with previously described order.
Therefore, the invention provides a kind of preparation after reductibility activation, can be used as and make synthetic gas change into the method for compositions of carbonatoms greater than the catalyzer of 1 hydrocarbon, the chemical formula of said composition is:
In the formula:
A is a kind of basic metal;
X is a numeral, and the valency needs number of other element to oxygen satisfied in expression;
A is greater than 0 and less than 5%(weight) (pressing the total weight of composition);
B 0 to 10%(weight) in the scope (pressing the total weight of composition);
Ce and O are the rest part of composition.
The preparation method may further comprise the steps:
(A) with the soluble compounds of metal Ru and cerium and one or more solution of a kind of alkali metal compound of choosing wantonly, join alkali metal containing or ammonium carbonate and (or) supercarbonate and (or) in the precipitant solution of oxyhydroxide, formation contains ruthenium and cerium and optional alkali-metal throw out, throw out be can thermolysis become metal and (or) compound of metal oxide;
(B) throw out of recycling step (A) gained.
A in the chemistry formula I is preferably less than 1%(weight).
A in the chemistry formula I is a kind of basic metal, preferably potassium.Alkali-metal amount b is more preferably greater than 0, can be up to 5%(weight); With up to 2%(weight) be optimum.
In the step (A) of present method, one or more solution with metal Ru and cerium and optional alkali-metal soluble compounds, be added to alkali metal containing or ammonium carbonate and (or) supercarbonate and (or) in the precipitant solution of oxyhydroxide, generation contains ruthenium and cerium and optional alkali-metal throw out, sedimentary form be can thermolysis become metal and (or) compound of its oxide compound.
In the specific embodiments of present method preferably, step (A) can operate continuously, way is to send into one or more solution of metal Ru and cerium and optional alkali-metal soluble compounds simultaneously to the settling region, and precipitant solution, and mixed, generation contains ruthenium and cerium and optional alkali-metal throw out, and throw out is the compound form that can thermolysis becomes metal oxide.The settling region can be a container, this container is equipped with and introduces ruthenium and cerium and the optional alkali-metal soluble compounds solution and the device of precipitant solution respectively, the device of introducing solution respectively will be arranged to such an extent that can reach the mixing of solution, also is furnished with whipping appts, PH determinator and draws the device (as upflow tube) of suspended sediment continuously.
Solutions employed is preferably the aqueous solution.The compound of ruthenium and cerium and optional alkali metal compound can be dissolved in the solution separately, and by any order it are added in the precipitant solution, or above-claimed cpd is dissolved in the single solution, are added in the precipitation agent together.
Though can it has been generally acknowledged that it is the ruthenium of using chloride form easily with the compound of any solubility ruthenium and cerium, because this is the ruthenium compound of ready-made form on the market, the cerium of employing is its nitrate, for example cerous nitrate.If desired, can adopt the cerous nitrate of supplying on the market that except that cerium, also contains rare earth metal.
The precipitation agent of step (A) can be alkali-metal carbonate and (or) supercarbonate and (or) oxyhydroxide.Can be without ready-formed carbonate or supercarbonate and with the parent of above-mentioned salt, for example water-soluble salt and carbonic acid gas.But can also adopt thermolysis to become the urea of carbonic acid gas and ammonia.Under any circumstance, the value of the b in the above-mentioned chemical formula I if desired, can or add other alkali metal compound by washing the b value is regulated all greater than 0.In addition, can also adopt volatile salt and (or) bicarbonate of ammonia and (or) ammonium hydroxide makes precipitation agent, in the case, the b value of the catalyzer of initial preparation is zero, but when needing, can adjust this value by adding basic metal later on.Preferably make precipitation agent with the bicarbonate of ammonia of sneaking into (or not sneaking into) alkali metal hydrocarbonate (for example saleratus).
Can make the compound of soluble metal ruthenium and cerium is to combine under 0 to 100 ℃ in temperature range suitably.Suitable temperature range is 60 to 100 ℃ preferably in the embodiment at one of the present invention, and optimum is 80 to 100 ℃.In another embodiment of the present invention, suitable temperature is lower than 50 ℃, and optimum temperature is lower than 30 ℃, for example envrionment temperature.
Sedimentary generation can be approximately higher than 6 times at pH value aptly to be carried out, and optimum pH value scope is 6 to 10.In whole settling step, preferably make pH value constant substantially in above-mentioned scope.By using excessive precipitator (for example being about 7 times that precipitate required theoretical chemistry calculated amount fully) greatly, can guarantee suitably that pH value is constant basically.Another kind of way is to adopt suitable buffer reagent.
In the operate continuously of step (A), preferably to guarantee making pH value constant substantially relative rate in above-mentioned scope supply with solution.In order to obtain constant substantially pH value, may need to send in addition inorganic alkali solution, for example ammoniacal liquor.
In order to improve the homogeneity of catalyzer, preferably in precipitation process, suitably stir the mixture with mechanical stirrer.
The amount of the ruthenium that is adopted and the compound of cerium and precipitation agent should be able to satisfy the relation of stoichiometric quantity in the formula I.In addition, the arbitrary subsequent point in preparation process by adding alkali again, is perhaps passed through the method for washing and so on, to replenish or to reduce the alkali metal content of composition.
In step (B), resulting throw out in the step (A) is reclaimed.Can suitably take to filter this process of finishing, but also can adopt other method to come separate solid and liquid, for example adopt centrifuging.After the recovery, preferably suitably wash throw out with water, so that remove unwanted remaining solvend.It also is necessary that throw out is carried out drying, is advisable for example about 100 to 150 ℃ with the temperature that is lower than 180 ℃.Some pyrolysis may take place in drying step.
Be contained in the heat decomposable compound in the throw out that is reclaimed in the step (B), preferably further thermolysis in independent step (C).This can in 150 to 600 ℃ optimal temperature scope, realize by the thermal precipitation thing in suitable non-reduced atmosphere (for example in the inert gas at nitrogen and so on).
For changing into, the composition with chemical formula I is used for synthetic gas is changed into the catalyzer of carbonatoms greater than 1 hydrocarbon, generally need at high temperature suitably to contact, with reductibility activatable said composition with reducing gas (for example hydrogen, carbon monoxide or its gas mixture).The example of suitable reducing gas is a hydrogen, available argon one class indifferent gas dilution.In general, the suitable condition that is adopted can be: pressure range is 1 to 100 crust, and temperature range is 150 to 600 ℃, and the time is 24 hours or longer.The reductibility activation can be finished as an independent step as before the syngas conversion catalyst, perhaps can be used as a pre-treatment step and incorporates synthetic gas conversion process, the preferably latter into.
Person skilled in the art person recognizes easily, in some cases, thermal decomposition steps and reductibility activation step can be merged into a single step.
It is believed that co-precipitated catalyst is different from impregnated catalyst basically, and this difference can be reflected on its catalytic performance.
It is a kind of by the method for synthesis gas preparation carbonatoms greater than 1 hydrocarbon that the present invention also provides.This method be included in temperature range be about 1 to 100 crust of 190～400 ℃ and pressure range down, synthetic gas is contacted with the catalyzer that contains reductibility activatory formula I composition.Said composition makes as follows:
(A) with the soluble compounds of metal Ru and cerium and one or more solution of a kind of alkali metal compound of choosing wantonly, join alkali metal containing or ammonium carbonate and (or) supercarbonate and (or) in the precipitant solution of oxyhydroxide, formation contains ruthenium and cerium and optional alkali-metal throw out, this throw out be can thermolysis become metal and (or) compound of metal oxide;
(B) the resulting throw out of recycling step (A).
The reductibility activation of the composition of chemistry formula I can be carried out as an independent step outside the synthetic gas conversion reactor, also can within synthetic conversion reactor, before synthetic gas transforms, carry out, perhaps can within synthetic conversion reactor, under the condition that synthetic gas transforms, carry out as an independent step.
We have been noted that can be by periodically acquiring benefit with the hydrogen treat catalyzer.This can suitably realize by cutting off the carbon monoxide charging during the course every now and then.
Know as those skilled in the art, synthetic gas mainly contains carbon monoxide and hydrogen, but different according to the source of synthetic gas and degree of purification also may be contained a spot of carbonic acid gas, nitrogen and other rare gas element.
The method for preparing synthetic gas is sophisticated technically, generally comprises the partial oxidation of carbonaceous material (for example coal).In addition, the method preparation of catalyzed conversion that synthetic gas also can be by steam methane and so on.To achieve the object of the present invention, the suitable proportion scope of carbon monoxide and hydrogen can be at 2: 1 to 1: 6.Though the ratio by carbon monoxide in the synthetic gas of aforesaid method production and hydrogen may be different from above-mentioned scope, but can be by increasing carbon monoxide or hydrogen, suitably change perhaps can be adjusted in known by those skilled in the art, so-called transformationreation.
Aspect the improvement of hydrocarbon production method, can in catalyzer, add a kind of inert substance, for example silicon oxide.
In a kind of embodiment preferably, the acidic components of catalyzer and zeolite or pillared clays (pallared clay) and so on can be lumped together.
Zeolite or pillared clays can with the composition physical mixed, form intimately mixed bed, perhaps with the form of layering bed separately, zeolite or pillared clays become the part of bed, catalyzer becomes another part of bed.When physical mixed, zeolite or pillared clays can be mixed with composition before or after the reductibility activation.In addition, in the composition process of the chemical formula I of preparation, co-precipitation (steps A) can have zeolite or pillared clays in the presence of carry out, particularly when precipitation agent be volatile salt and (or) bicarbonate of ammonia with (or) during ammonium hydroxide.
The zeolite that is fit to is a MFI type zeolite, for example at United States Patent (USP) the 3rd, 702, and the ZSM-5 described in No. 886, but can also adopt other high silicon crystalline aluminium that is fit to-or gallium-silicate zeolite.
For example at English Patent A-2,059, No. 408, United States Patent (USP) A-4,216, No. 188, United States Patent (USP) A-4,248, No. 739, United States Patent (USP) A-4,515, No. 901 and United States Patent (USP) A-4 have described the pillared clays that is fit in 367, No. 163.Particularly suitable pillared clays is the silylanizing pillared clays described in the European patent A-015 of our issued for approval No. 0898 (BP Case No.6035).Above-mentioned patent publication document is cited here as a reference.
Preferably in 250 to 350 ℃ scope, pressure is preferably in the scope of 10 to 50 crust for temperature.The gas volume air speed scope that is fit to can be 100 to 20,000 hours
-1
Present method can or be carried out continuously on fixed-bed reactor, fluidized-bed reactor, moving-burden bed reactor or slurry-phase reactor discontinuous ground.
The catalyzer that is made by the inventive method is except that having high reactivity and the long lifetime, also having low methane and carbon dioxide selectivity, therefore, can reduce at the carbon depletion that forms aspect the unwanted by product as far as possible.
Now, the invention will be further described by the following examples.
A. Preparation of Catalyst
Embodiment 1
To be dissolved in the RuCl in the distilled water (100 cubic centimetres)
3(H
2O)
3(0.3974 gram, 1.52 mmoles) is added drop-wise to volume under the vigorous stirring is 750 cubic centimetres Ce(NO
3)
3(H
2O)
6In the distilled water solution of (75.40 grams, 173.64 mmoles).Then, with KNO
3Distilled water (50 cubic centimetres) drips of solution of (1.1421 grams, 11.30 mmoles) is added in the aqueous solution of the ruthenium chloride/cerous nitrate under stirring.The volume that is added to new preparation with about solution that will contain ruthenium/cerium and potassium in 1 hour is 2500 cubic centimetres NH
4HCO
3In the distilled water solution of (299.7 grams, 3.79 mmoles).In whole precipitation process, the pH value of alkali maintains 8.7～8.8.After all reagent add, continue to stir 0.25 hour, with the mixture vacuum filtration, obtain grayish slurry and lurid filtrate.With slurry with distilled water (3000 cubic centimetres) vigorous stirring 0.25 hour, vacuum filtration then.Repeat above-mentioned steps three times, in final vacuum oven drying (116 ℃, 17 mmhg, about 24 hours) before, dry to the gray solid part on vacuum filter.Dried solid (about 25 gram) is worn into fine powder, then under 10～11 ton forces, press forming in 3.5 centimetres of pressing molds.The solid of compacting is ground, and be screened into 500～1400 microns small-particle.Get a part (about 20 grams) and supply following thermal treatment:
(a) use N
2Purge (about 50 cc/min): 20 ℃ of 450 ℃/3 hours (10 ℃/minute)/() of 20 ℃ of (10 ℃/minute)/()
(b) use H
2Purge (about 50 cc/min): 320 ℃/6 hours → 20 ℃ of 225 ℃/8 hours (2 ℃/minute)/() of 20 ℃ of (2 ℃/minute)/()
With heat treated catalyst exposure in air, and be housed in contain air and with screw-cap the bottle in.
Except in precipitation process, pH value is controlled at outside the lower scope (pH value is 8.40～8.65), repeats the step of embodiment 1.
Except the reagent that uses nearly 3 times of amounts was produced the product gel of 64.70 grams, all the other methods were similar to embodiment 1.With the speed of 50 cc/min with RuCl
3/ Ce(NO
3)
3Solution is added to NH
4HCO
3In the aqueous solution.So the adding of reagent be with the preparation of on a small scale embodiment 1 and 2 in finish in time of roughly the same (69 minutes).In preparation process, NH
4HCO
3The pH value of solution is elevated to 8.68 by 8.16.
Use NH
4HCO
3Continuous precipitation
The equipment of using in the present embodiment as shown in Figure 1.With reference to accompanying drawing 1,1 is the mixing tank of stainless steel constant level, and 2 are precipitation agent input ring, and 3 for treating sedimentary containing metal solution input tube, and 4 is paddle stirrer, and 5 is the PH electrode, and 6 is upflow tube.
Solution A
With RuCl
3(H
2O)
3(12.085 gram, 46.23 mmoles) are dissolved in the distilled water (0.40 liter), and to be added drop-wise to volume under the vigorous stirring be 3 liters Ce(NO
3)
3(H
2O)
6In the distilled water solution of (303 grams, 0.698 mole).Then with KNO
3Distilled water (0.20 liter) drips of solution of (4.700 gram, 46.24 mmoles) is added in just under agitation ruthenium chloride/cerous nitrate solution.Claim that hereinafter this solution is solution A.
Solution B
With NH
4HCO
3(1.20 kilograms, 15.18 moles) are dissolved in 10 liters of distilled water.Claim that hereinafter this solution is solution B.
Method:
With reference to Fig. 1, with peristaltic pump (not drawing among the figure) solution A is passed through pipe 3, solution B is sent in the constant level mixing tank 1 simultaneously by precipitation agent input ring 2, between the velocity ratio of charging will be just be controlled at 8.0 and 8.7 with the PH of material in the mixing tank (PH electrode 5 is measured).Agitator 4 by rapid rotation mixes solution A and solution B effectively.Stably draw the precipitation of suspension by upflow tube 6, and on 35 liters of Buchner funnel/flasks, filter, to obtain grayish solid and lurid filtrate.With strainer every part of solid is blotted about 2 hours, and be placed in the air 17 hours.In drying process, the solid color deepens a bit.Solid in 3 Buchner funnels is lumped together, and can get total amount is the product of 916.3 grams.
Wet cake is divided into C(279.3 gram) and D(630 restrain) two parts.
D part is carried out vigorous stirring with distilled water (2 liters), and filter.Repeat this washing step secondary again, last, solid is carried out vacuum-drying (100 ℃, 17 mmhg, 17 hours), obtain 60.75 gram xerogel.
The method of introducing with embodiment 1 is suppressed and thermal treatment xerogel then.
Use KHCO
3Continuous precipitation
Remove and use KHCO
3Replace NH
4HCO
3Outward,
The method that embodiment 4 is introduced, and with following amount of reagent.
Solution A
(ⅰ) RuCl
3(H
2O)
3[155 grams; 5.93 mole is dissolved in the distilled water (0.040 liter)],
(ⅱ) KNO
3[4.667 grams, 46.17 mmoles are dissolved in the distilled water (0.20 liter)],
(ⅲ) Ce(NO
3)
3(H
2O)
6[302.86 grams, are dissolved in the distilled water (10 liters) by 0.697 mole].
Solution (ⅰ) is added in the solution (ⅲ), solution (ⅱ) is added in solution (ⅰ) and the mixing solutions (ⅲ).
Solution B
KHCO
3[1520.9 grams, are dissolved in the distilled water (10 liters) by 15.19 moles].
At pH value is to carry out co-precipitation between 7.70 and 7.90.
Vacuum filtration goes out precipitated solid, obtains dense thick metallic silver color slurry.
With (ⅰ) 10 liters of distilled water, (ⅱ) 12 liters of distilled water and (ⅲ) 10 liters of dried solids of distilled water wash, then under 110 ℃ air drying 17 hours.
By method compacting and the thermal treatment drying solid introduced among the embodiment 1.
Use NH
4HCO
3Extensive continuous precipitation
Adopt following amount of reagent, repeat the method that embodiment 4 is introduced.
Solution A
(ⅰ) RuCl
3(H
2O)
3[43.46 grams, 166.21 mmoles are dissolved in the distilled water (11.2 liters)],
(ⅱ) KNO
3[130.66 grams, 1292.47 mmoles are dissolved in the distilled water (5.6 liters)],
(ⅲ) Ce(NO
3)
3(H
2O)
6[8.48 kilograms, are dissolved in the distilled water (84 liters) by 19.53 moles].
Solution (ⅰ) is added in the solution (ⅲ), solution (ⅱ) is added in solution (ⅰ) and the mixing solutions (ⅲ).
Solution B
NH
4HCO
3[4.80 kilograms, are dissolved in the distilled water (40 liters) by 60.72 moles].With 0.880 ammoniacal liquor the pH value of co-precipitation is transferred to 8.50.
The light gray precipitation that co-precipitation is obtained is carried out vacuum filtration, and with 50～55 liters of distilled water washs 3 times.The wet cake of gained under 110 ℃ in air drying 30 hours.
Sift out xerogel less than 1 centimetre, and with the roasting in nitrogen of following method:
N
2Purge 20 ℃ of 7 kilograms of gels of (3 liters/minute)/450 ℃/6 hours (14 hours)/() of 20 ℃ of (3 hours)/()
In " Z " cutter type mixing tank, the baked gel of nitrogen is mixed with distilled water (0.6 liter/kilogram) then.At last, 30 ℃ air drying 30 hours.
Be crushed to powder, and sieve the powder of getting less than 1 millimeter, under dry state, mix (2 gram acid are to 100 gram xerogel) then with stearic acid.
Use Manesty B3 B16 type porous pelleter (Manesty B3 B16 station multiple punch tablet maker) with the mixture compressing tablet then, make the column sheet of 4.0 millimeters of 4.8 millimeters of diameters * length.Before test, with above-mentioned crushing and sift out 250～500 microns powder.
B. catalyst test
Embodiment 7
(ⅰ) method
4 cubic centimetres of catalyzer that embodiment 1 is made and granulometric facies with broken porcelain ball mix the fixed-bed reactor of packing into for 6 cubic centimetres.225 ℃, 75 cubic centimetres hydrogen/minute and normal pressure under the reduction 16 hours.Then by synthetic gas (H
2: CO=2: 1) pressure is raised to 30 crust (gauge pressure), and bed is heated to 305～315 ℃ at 2 hours.At this moment, stop CO stream 2 hours, then, feed CO again, wall temperature is reduced, making bed temperature is 295～300 ℃.Keep above-mentioned condition constant then,, after this change process parameter on request up to reaching stable state.
(ⅱ) result
The data that will obtain under different tests time and differing temps are listed in table 1.Test has been carried out 2200 hours continuously.During this period, bed temperature changes between 300 ℃ and 314 ℃, and CO transformation efficiency correspondingly is between 37% and 88%.In preceding 350 hours of test, press CO transformation efficiency, CH
4Selectivity and CO
2The obtained data of selectivity are plotted in accompanying drawing 2.
By accompanying drawing as seen, catalyzer changes over to stable greatly after 100 hours about running, in whole test, and CO
2Selectivity is very low always.Under constant transformation efficiency, methane selectively is very low always.And, from the different tests time, though there is temperature variation the centre, under the same temperature, can obtain to say on this meaning of same transformation efficiency, catalyzer be have reproducible.
Between on-stream period in 350 hours to 2200 hours, the property retention of catalyzer is constant.
Embodiment 8
(ⅰ) method
The catalyzer that the catalyzer that makes with embodiment 4 replaces embodiment 1 to make, removing catalyzer is outside 305 ℃ (30 crust hydrogen, 111 cc/min) reduced 6 hours down, has repeated the method for embodiment 7.After running in 47 hours, stop CO stream, use hydrogen treat catalyzer 1 hour.
(ⅱ) result
Test-results is listed in table 2.
By data in the table as can be seen, under identical CO transformation efficiency, after the running in 47 hours, use the hydrogen treat catalyzer, methane selectively is reduced greatly, and reduce the CO selectivity.
Embodiment 9
(ⅰ) method
The catalyzer that the catalyzer that makes with embodiment 5 replaces embodiment 1 to make removes catalyzer outside 305 ℃ (30 crust hydrogen, 111 cc/min) reduced 6 hours down, has repeated the method for embodiment 7.
(ⅱ) result
Test-results is listed in table 3.
By data in the table as can be seen, methane selectively is very low.Attractive especially result is, is 81.47%(running 17 hours at transformation efficiency) time, methane selectively only is 10.66%, CO
2Selectivity only is 3.59%.
Embodiment 10
(ⅰ) method
By following temperature requirement, the catalyzer that embodiment 6 is made reduces in hydrogen stream (83.4 cc/min) for 2 cubic centimetres:
100 ℃ 1 hour, then 200 ℃ 1 hour, then 300 ℃ 16 hours, then be cooled to 200 ℃.
Then, with catalyst exposure in synthetic gas (H
2: CO=2: 1) balance 1 hour in (83.4 cubic centimetres total stream/minute).With temperature regulation to 250 ℃, put approximately 0.5 hour, be elevated to 270 ℃ then, rise 10 ℃ more at every turn temperature brought up to 290 ℃, rise 1 ℃ at last at every turn, be raised to service temperature (about 300 ℃).
Test-results is listed in table 4.
Result in the table has proved the handiness of catalyzer, particularly in 500 hours running, at low CH
4And CO
2Under the selectivity, obtained high CO transformation efficiency.
Claims (3)
1, by the method for synthesis gas preparation carbonatoms greater than 1 hydrocarbon, this method is included under 190-400 ℃ of temperature and the about 1-100 bar pressure, and synthetic gas is contacted with the catalyst composition that the reductibility activatory has formula I:
In the formula:
A is a kind of basic metal,
X is a numeral, and the valency needs number of other element to oxygen satisfied in expression,
A is greater than 0 and less than 5% (weight) (pressing the total weight of composition),
B in 0 to 10% (weight) scope (pressing the total weight of composition),
Ce and 0 is the rest part of composition;
Said composition is to prepare by the method that may further comprise the steps:
(A) be under the 6-10 condition at pH value, with the soluble compounds of metal Ru and cerium and one or more solution of a kind of alkali metal compound of choosing wantonly, be added to alkali metal containing or ammonium carbonate and (or) supercarbonate and (or) in the precipitant solution of oxyhydroxide, formation contains ruthenium and cerium and optional alkali-metal throw out, throw out be can thermolysis become metal and (or) compound of metal oxide;
(B) throw out of recycling step (A) gained.
2, according to the process of claim 1 wherein that the composition with formula I is a reductibility activatory in the pre-treatment step of synthetic gas conversion process.
3, according to the method for claim 1 or 2, catalyzer is wherein periodically handled with hydrogen.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB868600445A GB8600445D0 (en) | 1986-01-09 | 1986-01-09 | Syngas conversion catalyst |
| GB8600445 | 1986-01-09 | ||
| CN87100113A CN1011664B (en) | 1986-01-09 | 1987-01-09 | Improved syngas conversion catalyst, production and use thereof |
Related Parent Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN87100113 Division | 1987-01-09 | ||
| CN87100113A Division CN1011664B (en) | 1986-01-09 | 1987-01-09 | Improved syngas conversion catalyst, production and use thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1046928A CN1046928A (en) | 1990-11-14 |
| CN1015171B true CN1015171B (en) | 1991-12-25 |
Family
ID=25742276
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 90104171 Expired CN1015171B (en) | 1986-01-09 | 1987-01-09 | Improved syngas conversion catalyst |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1015171B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1054832C (en) * | 1995-05-26 | 2000-07-26 | 中国科学院山西煤炭化学研究所 | Process for synthesizing gasoline from synthesized gas through olefin |
-
1987
- 1987-01-09 CN CN 90104171 patent/CN1015171B/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| CN1046928A (en) | 1990-11-14 |
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