CN106582636B - Composite catalyst bed - Google Patents
Composite catalyst bed Download PDFInfo
- Publication number
- CN106582636B CN106582636B CN201510661623.8A CN201510661623A CN106582636B CN 106582636 B CN106582636 B CN 106582636B CN 201510661623 A CN201510661623 A CN 201510661623A CN 106582636 B CN106582636 B CN 106582636B
- Authority
- CN
- China
- Prior art keywords
- grams
- hours
- catalyst
- segment
- segment catalyst
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Abstract
The present invention relates to the methods of the material hydrotreating of composite catalyst bed and the hydrocarbon containing triple carbon-carbon bonds, mainly solve the problems, such as that hydrocarbon containing triple carbon-carbon bonds adds hydrogen alkynes conversion ratio into the reaction of alkane low low with butane yield, the present invention is by using compound hydrogenation catalyst bed, including first segment catalyst and second segment catalyst, first segment catalyst includes carrier 1 and palladium or its oxide, second segment catalyst includes carrier 2 and nickel or the technical solution of its oxide, it preferably solves the technical problem, can be used in the recycling of the hydrocarbon containing triple carbon-carbon bonds.
Description
Technical field
The present invention relates to the methods of the material hydrotreating of composite catalyst bed and the hydrocarbon containing triple carbon-carbon bonds, more particularly to place
Manage method of hydrotreating of the acetylene by-product containing the advanced alkynes such as diacetylene and vinylacetylene.
Background of invention
Gas by partial oxidation of natural acetylene process by-product partial higher alkynes gas.It mainly contains diacetylene
The insatiable hungers such as (37.17V%), allylene, propine (6.74V%), vinylacetylene (10.51V%) and acetylene (19.85V%)
With hydrocarbon and part C6H6+(25.72V%) heavy constituent.These unsaturated hydrocarbons properties are extremely unstable, such as the decomposition pressure of diacetylene
Power be only 0.02MPa, vinylacetylene be easy polymerization form explosive polymerisation object etc., to enterprise production bring very big safety hidden
Suffer from, need to be diluted with a large amount of synthesis gas, is then sent for torch burn-up.In carrier gas containing 50% or more CO, H2Etc. groups
Point, economic value with higher.Containing there are many widely used industrial chemicals in advanced alkynes, but due to its complicated components, point
From difficulty, it is difficult to be fully utilized, cause the waste in resource.Therefore, no matter from the angle of production safety, or from money
The angle that source utilizes is set out, and the advanced alkynes of acetylene unit is recycled, is all had great importance.
DE-A-1468206 discloses a kind of method of acetylene purification, and vinylacetylene and diacetylene are absorbed in N- methyl
In pyrrolidones (NMP) solvent, with Pd/Al2O3For anti-applications catalyst, carry out catalytic hydrogenation reaction, hydrogenated products polarity compared with
It is weak, easily separated from solvent.US4128595 disclose it is a kind of will contain alkynes material and inert hydrocarbon solvent together enter reaction
Device is contacted with palladium-based catalyst carries out hydrogenation reaction, the disadvantages of the method are as follows material containing alkynes is at reaction conditions in hydrocarbon solvent
Solubility is poor；The patent disclosure shows to carry out hydrogenation reaction in polar solvent such as n,N dimethylformamide (DMF), be catalyzed
Agent deactivation rate is very fast.US2010/0016646A1 discloses a kind of diacetylene method of hydrotreating, and diacetylene is absorbed in polar solvent
In NMP or DMF, using loading type Pd/Al2O3Catalyst, 0~100 DEG C of reaction temperature, 1~40bar of pressure is carried out plus hydrogen is anti-
It answers, obtains butane and butylene, catalyst is gradually inactivated because showing carbon distribution in operational process.Alkynes has active three because of it
Key, in continuously hydrogen adding reaction process, easily generation polymerization process generates green oil and colloid, leads to catalyst inactivation.Therefore it develops
A kind of new alkynes method of hydrotreating improves hydrogenation plant operation stability, has significance.
But in the prior art, add hydrogen alkynes conversion ratio into the reaction of alkane low and butane yield for hydrocarbon containing triple carbon-carbon bonds
It is low.
Summary of the invention
The technical problem to be solved in the present invention first is that adding hydrogen anti-to alkane for hydrocarbon containing triple carbon-carbon bonds in the prior art
The low problem low with butane yield of middle alkynes conversion ratio is answered, a kind of compound hydrogenation catalyst bed is provided, the composite catalyst bed accessory
There is the advantages of alkynes high conversion rate and butane high income.
The second technical problem to be solved by the present invention be using above-mentioned technical problem the catalyst containing triple carbon-carbon bonds
The method of the material hydrotreating of hydrocarbon.
One of to solve above-mentioned technical problem, technical scheme is as follows: compound hydrogenation catalyst bed, including first
Section catalyst and second segment catalyst, first segment catalyst include carrier 1 and palladium or its oxide, and second segment catalyst includes carrying
Body 2 and nickel or its oxide.
In above-mentioned technical proposal, the weight ratio of first segment catalyst and second segment catalyst is preferably 0.5~1.
In above-mentioned technical proposal, first segment catalyst preferably includes following components by weight percentage:
(a) 0.02~0.2% metal Pd or its oxide；
(b) 0.04~1% selected from least one of IB metal from the periodic table of elements or its oxide.
In above-mentioned technical proposal, when Pd element is oxide pattern, one skilled in the art will appreciate that gold should be reduced into
Belong to Pd and exercises use again.
In above-mentioned technical proposal, second segment catalyst preferably includes following components by weight percentage:
(a) 10~25% metallic nickel or its oxide；
(b) 0.2~1% selected from least one of rare earth metal or its oxide；
(c) 0.2~2.0% at least one of IIA metal in the periodic table of elements or its oxide；
(d) 2~5% Zr or its oxide.
In above-mentioned technical proposal, when nickel element is oxide pattern, one skilled in the art will appreciate that gold should be reduced into
Belong to nickel and exercises use again.
In above-mentioned technical proposal, carrier 1 and/or carrier 2 are not particularly limited, but preferred aluminium oxide, and carrier 1 is more preferable
30~90m of BET specific surface20.65~0.85ml/g of/g, Kong Rongwei, carrier 2 are more preferably 120~200m of BET specific surface2/ g, hole
Holding is 0.42~0.70ml/g.
To solve above-mentioned technical problem two, technical scheme is as follows: the material of the hydrocarbon containing triple carbon-carbon bonds adds at hydrogen
The method of reason, includes the following steps:
(1) make first segment described in any one of technical solution described in hydrogen and one of material elder generation and above-mentioned technical problem
Catalyst haptoreaction generates the intermediate material containing monoene；
(2) above-mentioned intermediate hydrogenation of net product obtains the material containing alkane in the presence of second segment catalyst.
In above-mentioned technical proposal, there is no limit for remaining alkynes Specific amounts in intermediate material, but the lower residual the better, preferably
Within the residual quantity 1% of alkynes, intermediate material preferably comprises monoolefine, can also contain alkane.Such as, but not limited to alkane and list
The weight ratio of alkene is 0.5~1.5.
In above-mentioned technical proposal, if be able to satisfy first pass through step (1) then using step (2) the step of, this
Field technical staff can rationally determine upper feeding, lower charging or cross-feed.For example, when selecting upper feeding bottom discharge, it can
First segment catalyst and second segment catalyst to be placed in same reactor, by first segment catalyst as second segment catalyst
On；When using lower charging, first segment catalyst and second segment catalyst can be placed in same reactor, by first segment
Catalyst is placed under second segment catalyst.Can also be placed in above-mentioned two-stage catalytic agent two reactors being connected in series.
In above-mentioned technical proposal, the reaction temperature of step (1) and/or step (2) is preferably 40~90 DEG C；More preferable 60~
80℃
In above-mentioned technical proposal, the reaction pressure of step (1) and/or step (2) is preferably 1.2~2.2MPa；More preferably
1.6~2.2MPa
In above-mentioned technical proposal, the feed weight air speed of triple carbon-carbon bonds hydrocarbon is preferably 0.05~0.2h in step (1)-1.More
0.08~0.15h of preferred weight air speed-1。
In above-mentioned technical proposal, hydrogen/triple carbon-carbon bonds hydrocarbon molar ratio is preferably 20~50 in step (1).
In above-mentioned technical proposal, the material of the hydrocarbon containing triple carbon-carbon bonds preferably contains diluent.
In above-mentioned technical proposal, in the material, by weight triple carbon-carbon bonds hydrocarbon preferred content be greater than zero and 3.0% with
Under；Amount of diluent is preferably 95~99%.
In above-mentioned technical proposal, the diluent can be selected from N-Methyl pyrrolidone, n,N dimethylformamide, in acetone
At least one.
In above-mentioned technical proposal, hydrocarbon containing triple carbon-carbon bonds is not particularly limited, such as, but not limited to propine, vinylacetylene and
Diacetylene etc..
More specific non limiting example, by weight, the material contain 0.1~2% vinylacetylene, 0.1~2%
Benzene, 0.1~3% diacetylene, 95~99%N- methyl pyrrolidone.
The preparation method of two-stage catalytic agent carrier of the present invention is not particularly limited, as non limiting example, including
Following steps:
Aluminium oxide and modifying agent, peptizing agent, water are mixed, in the desired amount after extruded moulding, it is first dry at 60~110 DEG C
It 5~24 hours, is then roasted 4~10 hours at 500~1000 DEG C, obtains carrier.
The preparation method of preferred carrier 1, comprising:
Aluminium oxide and modifying agent, peptizing agent, water are mixed, in the desired amount after extruded moulding, it is first dry at 60~110 DEG C
It 5~24 hours, is then roasted 4~10 hours at 800~1000 DEG C, obtains carrier 1.
The preparation method of preferred carrier 2, comprising:
Aluminium oxide and modifying agent, peptizing agent, water are mixed, in the desired amount after extruded moulding, it is first dry at 60~110 DEG C
It 5~24 hours, is then roasted 4~10 hours at 500~700 DEG C, obtains carrier 2.
The preparation method of two-stage catalytic agent of the present invention is not particularly limited, and as non limiting example, first segment is urged
The preparation method of agent includes the following steps: that the solution even for being made into carrier with the desired amount of IB race impregnates, then through drying,
It roasts in air up to modified aluminium oxide supports for 350~500 DEG C.The carrier is put in excess chlorination palladium solution and is impregnated, mistake
After filter through drying, in air 450~800 DEG C roast up to oxidized form palladium-based catalyst.
The preparation method of two-stage catalytic agent of the present invention is not particularly limited, and as non limiting example, second segment is urged
The preparation method of agent includes the following steps: to impregnate and then use aequum for the solution that carrier is made into cocatalyst component first
The solution dipping that is made into of nickel compound, or by carrier co-catalyst used in the desired amount of nickel compound and catalyst
The solution dipping that group is distributed into；Carrier after dipping through drying, in air 350~500 DEG C roast and urged up to oxidized form is Ni-based
Agent.
Above-mentioned oxidation catalyst can also be restored, the mode those skilled in the art specifically restored can rationally slap
It holds, as long as the palladium or compound state nickel of compound state are reduced to metallic state.For example, the reduction side of first segment catalyst of the present invention
Method includes 0.2~0.5MPa of pressure, is warming up to 120 DEG C with 30~60 DEG C/h heating rate, maintains 6~12h.For example,
The restoring method of second segment catalyst of the present invention includes that catalyst is reduced directly on hydrogenation plant, reducing process condition
Are as follows: 0.2~0.5MPa of pressure is warming up to 230~280 DEG C of 3~6h of maintenance with 30~60 DEG C/h heating rate, then with 15 DEG C/h
Rate be warming up to 330~380 DEG C, maintain 6~12h, be warming up to 420~500 DEG C again later with 15 DEG C/h, maintain 6~12h,
?.
Using the present invention, at 70 DEG C of reaction temperature, reaction pressure 1.8MPa, the feed weight air speed of triple carbon-carbon bonds hydrocarbon
0.1h-1, hydrogen/alkynes molar ratio 20, alkynes conversion ratio 99.2%, butane yield 99% obtains preferable technical effect.
The present invention will be further described below by way of examples, but these embodiments are not anyway to this hair
Bright range is construed as limiting.
Specific embodiment
Test the raw materials used higher alkyne for Sichuan vinylon plant natural gas acetylene unit by-product, specific nature such as table
Shown in 1.
[embodiment 1]
1, prepared by carrier 1
It weighs and is equivalent to 12 grams of aluminium oxide of boehmite, 170 grams of aluminium oxide, 9 grams of sesbania powders, mixing is added later
Containing 20 grams of poly-vinyl alcohol solution (mass concentration 5%), mass concentration is 4.0 grams of nitric acid of 68%, 280 milliliters of water, is squeezed out, wet
Item roasts 4 hours after 120 DEG C 4 hours dry in 900 DEG C, obtains the carrier Z1 that a length of 2 mm dia is 1 millimeter, specific surface
Product 74m2/ g, Kong Rong 0.72ml/g.
2, first segment catalyst preparation
Above-mentioned 98.8 grams of carrier Z1 are mixed with 100 grams of silver nitrate aqueous solution of 1.0 grams of argentiferous, 60 DEG C drying 8 hours,
450 DEG C roast 4 hours, and modified aluminium oxide supports are made.Then, it mixes, passes through with 100 grams of the chlorine palladium aqueous acid containing 0.2 gram of palladium
110 DEG C roast 4 hours in 600 DEG C after drying 4 hours, and with hydrogen reducing 4 hours, 450 DEG C of reduction temperature, hydrogen volume air speed was
50 hours-1, first segment catalyst is obtained, concrete composition is shown in Table 2.
3, prepared by carrier 2
It weighs and is equivalent to 12 grams of aluminium oxide of boehmite, 69.5 grams of aluminium oxide, 9 grams of sesbania powders, mixing is added later
Containing 20 grams of poly-vinyl alcohol solution (mass concentration 5%), mass concentration is 4.0 grams of nitric acid of 68%, is equivalent to 0.5 gram of La2O3's
La(NO3)3.6H2O is equivalent to the Ca (NO of 1 gram of CaO3)2.4H2O is equivalent to 3.0 grams of ZrO2ZrOCl2.8H2O, 130 milli of water
It rises, squeezes out, wet bar roasts 4 hours after 120 DEG C 4 hours dry in 700 DEG C, obtains the carrier that a length of 2 mm dia is 1 millimeter
Z2, specific surface area 147m2/ g, Kong Rong 0.56ml/g.
4, second segment catalyst preparation
Above-mentioned carrier Z2 is mixed with 90 grams of nickel ammonia solution of nickeliferous 14 grams, 60 DEG C drying 8 hours, 110 DEG C drying 2 hours
It is roasted 4 hours in 450 DEG C afterwards, with hydrogen reducing 4 hours, 450 DEG C of reduction temperature, hydrogen volume air speed was 50 hours-1, obtain
Two sections of catalyst, concrete composition are shown in Table 3.
5, evaluating catalyst
Hydroprocessing is carried out in fixed bed reactors.First segment prepared by upper bed layer filling embodiment 1 in reactor
Catalyst, lower bed layer load second segment catalyst prepared by embodiment 1, the quality of first segment catalyst and second segment catalyst
Than being 0.8.The material of the hydrocarbon containing triple carbon-carbon bonds carries out hydroprocessing, reactor head charging, bottom discharge in a continuous manner.
During the experiment, operating condition is as follows: reaction temperature: 70 DEG C, reaction pressure 1.60MPa, triple carbon-carbon bonds hydrocarbon charging weight is empty
Fast 0.1h-1, hydrogen/triple carbon-carbon bonds hydrocarbon molar ratio 20, is carried out continuously 300 hours plus hydrogen is evaluated, and hydrogen average result is added to be shown in Table 4.
[comparative example 1]
First segment catalyst and second segment catalyst are placed upside down, other process conditions are identical with embodiment 1, tool
Body are as follows:
1, prepared by carrier 1
It weighs and is equivalent to 12 grams of aluminium oxide of boehmite, 170 grams of aluminium oxide, 9 grams of sesbania powders, mixing is added later
Containing 20 grams of poly-vinyl alcohol solution (mass concentration 5%), mass concentration is 4.0 grams of nitric acid of 68%, 280 milliliters of water, is squeezed out, wet
Item roasts 4 hours after 120 DEG C 4 hours dry in 900 DEG C, obtains the carrier Z1 that a length of 2 mm dia is 1 millimeter, specific surface
Product 74m2/ g, Kong Rong 0.72ml/g.
2, first segment catalyst preparation
Above-mentioned 98.8 grams of carrier Z1 are mixed with 100 grams of silver nitrate aqueous solution of 1.0 grams of argentiferous, 60 DEG C drying 8 hours,
450 DEG C roast 4 hours, and modified aluminium oxide supports are made.Then, it mixes, passes through with 100 grams of the chlorine palladium aqueous acid containing 0.2 gram of palladium
110 DEG C roast 4 hours in 600 DEG C after drying 4 hours, and with hydrogen reducing 4 hours, 450 DEG C of reduction temperature, hydrogen volume air speed was
50 hours-1, first segment catalyst is obtained, concrete composition is shown in Table 2.
3, prepared by carrier 2
It weighs and is equivalent to 12 grams of aluminium oxide of boehmite, 69.5 grams of aluminium oxide, 9 grams of sesbania powders, mixing is added later
Containing 20 grams of poly-vinyl alcohol solution (mass concentration 5%), mass concentration is 4.0 grams of nitric acid of 68%, is equivalent to 0.5 gram of La2O3's
La(NO3)3.6H2O is equivalent to the Ca (NO of 1 gram of CaO3)2.4H2O is equivalent to 3.0 grams of ZrO2ZrOCl2.8H2O, 130 milli of water
It rises, squeezes out, wet bar roasts 4 hours after 120 DEG C 4 hours dry in 700 DEG C, obtains the carrier that a length of 2 mm dia is 1 millimeter
Z2, specific surface area 147m2/ g, Kong Rong 0.56ml/g.
4, second segment catalyst preparation
Above-mentioned carrier Z2 is mixed with 90 grams of nickel ammonia solution of nickeliferous 14 grams, 60 DEG C drying 8 hours, 110 DEG C drying 2 hours
It is roasted 4 hours in 450 DEG C afterwards, with hydrogen reducing 4 hours, 450 DEG C of reduction temperature, hydrogen volume air speed was 50 hours-1, obtain
Two sections of catalyst, concrete composition are shown in Table 3.
5, evaluating catalyst
Hydroprocessing is carried out in fixed bed reactors.Second segment prepared by upper bed layer filling embodiment 1 in reactor
Catalyst, lower bed layer load first segment catalyst prepared by embodiment 1, the quality of first segment catalyst and second segment catalyst
Than being 0.8.The material of the hydrocarbon containing triple carbon-carbon bonds carries out hydroprocessing, reactor head charging, bottom discharge in a continuous manner.
During the experiment, operating condition is as follows: reaction temperature: 70 DEG C, reaction pressure 1.60MPa, triple carbon-carbon bonds hydrocarbon charging weight is empty
Fast 0.1h-1, hydrogen/triple carbon-carbon bonds hydrocarbon molar ratio 20, is carried out continuously 300 hours plus hydrogen is evaluated, and hydrogen average result is added to be shown in Table 4.
[comparative example 2]
Other than second segment catalyst also uses first segment, other process conditions are identical with embodiment 1, specifically:
1, prepared by carrier 1
It weighs and is equivalent to 12 grams of aluminium oxide of boehmite, 170 grams of aluminium oxide, 9 grams of sesbania powders, mixing is added later
Containing 20 grams of poly-vinyl alcohol solution (mass concentration 5%), mass concentration is 4.0 grams of nitric acid of 68%, 280 milliliters of water, is squeezed out, wet
Item roasts 4 hours after 120 DEG C 4 hours dry in 900 DEG C, obtains the carrier Z1 that a length of 2 mm dia is 1 millimeter, specific surface
Product 74m2/ g, Kong Rong 0.72ml/g.
2, first segment catalyst preparation
Above-mentioned 98.8 grams of carrier Z1 are mixed with 100 grams of silver nitrate aqueous solution of 1.0 grams of argentiferous, 60 DEG C drying 8 hours,
450 DEG C roast 4 hours, and modified aluminium oxide supports are made.Then, it mixes, passes through with 100 grams of the chlorine palladium aqueous acid containing 0.2 gram of palladium
110 DEG C roast 4 hours in 600 DEG C after drying 4 hours, and with hydrogen reducing 4 hours, 450 DEG C of reduction temperature, hydrogen volume air speed was
50 hours-1, first segment catalyst is obtained, concrete composition is shown in Table 2.
3, evaluating catalyst
Hydroprocessing is carried out in fixed bed reactors.First segment prepared by upper bed layer filling embodiment 1 in reactor
Catalyst, lower bed layer also load first segment catalyst.The material of the hydrocarbon containing triple carbon-carbon bonds carries out hydroprocessing in a continuous manner,
Reactor head charging, bottom discharge.During the experiment, operating condition is as follows: reaction temperature: 70 DEG C, reaction pressure
1.60MPa, triple carbon-carbon bonds hydrocarbon charging weight space velocity 0.1h-1, hydrogen/triple carbon-carbon bonds hydrocarbon molar ratio 20 is carried out continuously 300 hours plus hydrogen
Evaluation, adds hydrogen average result to be shown in Table 4.
[comparative example 3]
Other than first segment also uses second segment catalyst, other process conditions are identical with embodiment 1, specifically:
1, prepared by carrier 2
It weighs and is equivalent to 12 grams of aluminium oxide of boehmite, 69.5 grams of aluminium oxide, 9 grams of sesbania powders, mixing is added later
Containing 20 grams of poly-vinyl alcohol solution (mass concentration 5%), mass concentration is 4.0 grams of nitric acid of 68%, is equivalent to 0.5 gram of La2O3's
La(NO3)3.6H2O is equivalent to the Ca (NO of 1 gram of CaO3)2.4H2O is equivalent to 3.0 grams of ZrO2ZrOCl2.8H2O, 130 milli of water
It rises, squeezes out, wet bar roasts 4 hours after 120 DEG C 4 hours dry in 700 DEG C, obtains the carrier that a length of 2 mm dia is 1 millimeter
Z2, specific surface area 147m2/ g, Kong Rong 0.56ml/g.
2, second segment catalyst preparation
Above-mentioned carrier Z2 is mixed with 90 grams of nickel ammonia solution of nickeliferous 14 grams, 60 DEG C drying 8 hours, 110 DEG C drying 2 hours
It is roasted 4 hours in 450 DEG C afterwards, with hydrogen reducing 4 hours, 450 DEG C of reduction temperature, hydrogen volume air speed was 50 hours-1, obtain
Two sections of catalyst, concrete composition are shown in Table 3.
3, evaluating catalyst
Hydroprocessing is carried out in fixed bed reactors.Second segment prepared by upper bed layer filling embodiment 1 in reactor
Catalyst, lower bed layer load second segment catalyst prepared by embodiment 1.The material of the hydrocarbon containing triple carbon-carbon bonds in a continuous manner
Carry out hydroprocessing, reactor head charging, bottom discharge.During the experiment, operating condition is as follows: reaction temperature: 70 DEG C,
Reaction pressure 1.60MPa, triple carbon-carbon bonds hydrocarbon charging weight space velocity 0.1h-1, hydrogen/triple carbon-carbon bonds hydrocarbon molar ratio 20 is carried out continuously 300
Hour plus hydrogen evaluation, add hydrogen average result to be shown in Table 4.
[comparative example 4]
Other than being used in mixed way the catalyst of first segment and second segment catalyst, other process conditions and embodiment 1 are complete
It is exactly the same, specifically:
1, prepared by carrier 1
It weighs and is equivalent to 12 grams of aluminium oxide of boehmite, 170 grams of aluminium oxide, 9 grams of sesbania powders, mixing is added later
Containing 20 grams of poly-vinyl alcohol solution (mass concentration 5%), mass concentration is 4.0 grams of nitric acid of 68%, 280 milliliters of water, is squeezed out, wet
Item roasts 4 hours after 120 DEG C 4 hours dry in 900 DEG C, obtains the carrier Z1 that a length of 2 mm dia is 1 millimeter, specific surface
Product 74m2/ g, Kong Rong 0.72ml/g.
2, first segment catalyst preparation
Above-mentioned 98.8 grams of carrier Z1 are mixed with 100 grams of silver nitrate aqueous solution of 1.0 grams of argentiferous, 60 DEG C drying 8 hours,
450 DEG C roast 4 hours, and modified aluminium oxide supports are made.Then, it mixes, passes through with 100 grams of the chlorine palladium aqueous acid containing 0.2 gram of palladium
110 DEG C roast 4 hours in 600 DEG C after drying 4 hours, and with hydrogen reducing 4 hours, 450 DEG C of reduction temperature, hydrogen volume air speed was
20 hours-1, first segment catalyst is obtained, concrete composition is shown in Table 2.
3, prepared by carrier 2
It weighs and is equivalent to 12 grams of aluminium oxide of boehmite, 69.5 grams of aluminium oxide, 9 grams of sesbania powders, mixing is added later
Containing 20 grams of poly-vinyl alcohol solution (mass concentration 5%), mass concentration is 4.0 grams of nitric acid of 68%, is equivalent to 0.5 gram of La2O3's
La(NO3)3.6H2O is equivalent to the Ca (NO of 1 gram of CaO3)2.4H2O is equivalent to 3.0 grams of ZrO2ZrOCl2.8H2O, 130 milli of water
It rises, squeezes out, wet bar roasts 4 hours after 120 DEG C 4 hours dry in 700 DEG C, obtains the carrier that a length of 2 mm dia is 1 millimeter
Z2, specific surface area 147m2/ g, Kong Rong 0.56ml/g.
4, second segment catalyst preparation
Above-mentioned carrier Z2 is mixed with 90 grams of nickel ammonia solution of nickeliferous 14 grams, 60 DEG C drying 8 hours, 110 DEG C drying 2 hours
It is roasted 4 hours in 450 DEG C afterwards, with hydrogen reducing 4 hours, 450 DEG C of reduction temperature, hydrogen volume air speed was 50 hours-1, obtain
Two sections of catalyst, concrete composition are shown in Table 3.
5, evaluating catalyst
Hydroprocessing is carried out in fixed bed reactors.It is made to load embodiment 1 for upper bed layer and lower bed layer in reactor
Standby first segment catalyst and the mixed catalyst of second segment catalyst.The material of the hydrocarbon containing triple carbon-carbon bonds in a continuous manner
Carry out hydroprocessing, reactor head charging, bottom discharge.During the experiment, operating condition is as follows: reaction temperature: 70 DEG C,
Reaction pressure 1.60MPa, triple carbon-carbon bonds hydrocarbon charging weight space velocity 0.1h-1, hydrogen/triple carbon-carbon bonds hydrocarbon molar ratio 20 is carried out continuously 300
Hour plus hydrogen evaluation, add hydrogen average result to be shown in Table 4.
[embodiment 2]
1, prepared by carrier 1
It weighs and is equivalent to 12 grams of aluminium oxide of boehmite, 170 grams of aluminium oxide, 9 grams of sesbania powders, mixing is added later
Containing 20 grams of poly-vinyl alcohol solution (mass concentration 5%), mass concentration is 4.0 grams of nitric acid of 68%, 280 milliliters of water, is squeezed out, wet
Item roasts 4 hours after 120 DEG C 4 hours dry in 900 DEG C, obtains the carrier Z1 that a length of 2 mm dia is 1 millimeter, specific surface
Product 74m2/ g, Kong Rong 0.72ml/g.
2, first segment catalyst preparation
Above-mentioned 98.8 grams of carrier Z1 are mixed with 100 grams of silver nitrate aqueous solution of 1.0 grams of argentiferous, 60 DEG C drying 8 hours,
450 DEG C roast 4 hours, and modified aluminium oxide supports are made.Then, it mixes, passes through with 100 grams of the chlorine palladium aqueous acid containing 0.2 gram of palladium
110 DEG C roast 4 hours in 600 DEG C after drying 4 hours, and with hydrogen reducing 4 hours, 450 DEG C of reduction temperature, hydrogen volume air speed was
50 hours-1, first segment catalyst is obtained, concrete composition is shown in Table 2.
3, prepared by carrier 2
It weighs and is equivalent to 12 grams of aluminium oxide of boehmite, 69.5 grams of aluminium oxide, 9 grams of sesbania powders, mixing is added later
Containing 20 grams of poly-vinyl alcohol solution (mass concentration 5%), mass concentration is 4.0 grams of nitric acid of 68%, is equivalent to 0.5 gram of Ce2O3's
Ce(NO3)3.6H2O is equivalent to the Ca (NO of 1 gram of CaO3)2.4H2O is equivalent to 3.0 grams of ZrO2ZrOCl2.8H2O, 130 milli of water
It rises, squeezes out, wet bar roasts 4 hours after 120 DEG C 4 hours dry in 700 DEG C, obtains the carrier that a length of 2 mm dia is 1 millimeter
Z2, specific surface area 149m2/ g, Kong Rong 0.56ml/g.
4, second segment catalyst preparation
Above-mentioned carrier Z2 is mixed with 90 grams of nickel ammonia solution of nickeliferous 14 grams, 60 DEG C drying 8 hours, 110 DEG C drying 2 hours
It is roasted 4 hours in 450 DEG C afterwards, with hydrogen reducing 4 hours, 450 DEG C of reduction temperature, hydrogen volume air speed was 50 hours-1, obtain
Two sections of catalyst, concrete composition are shown in Table 3.
5, evaluating catalyst
Hydroprocessing is carried out in fixed bed reactors.First segment prepared by upper bed layer filling embodiment 2 in reactor
Catalyst, lower bed layer load second segment catalyst prepared by embodiment 2, the quality of first segment catalyst and second segment catalyst
Than being 0.8.The material of the hydrocarbon containing triple carbon-carbon bonds carries out hydroprocessing, reactor head charging, bottom discharge in a continuous manner.
During the experiment, operating condition is as follows: reaction temperature: 70 DEG C, reaction pressure 1.60MPa, triple carbon-carbon bonds hydrocarbon charging weight is empty
Fast 0.1h-1, hydrogen/triple carbon-carbon bonds hydrocarbon molar ratio 20, is carried out continuously 300 hours plus hydrogen is evaluated, and hydrogen average result is added to be shown in Table 4.
[embodiment 3]
1, prepared by carrier 1
It weighs and is equivalent to 12 grams of aluminium oxide of boehmite, 170 grams of aluminium oxide, 9 grams of sesbania powders, mixing is added later
Containing 20 grams of poly-vinyl alcohol solution (mass concentration 5%), mass concentration is 4.0 grams of nitric acid of 68%, 280 milliliters of water, is squeezed out, wet
Item roasts 4 hours after 120 DEG C 4 hours dry in 900 DEG C, obtains the carrier Z1 that a length of 2 mm dia is 1 millimeter, specific surface
Product 74m2/ g, Kong Rong 0.72ml/g.
2, first segment catalyst preparation
Above-mentioned 98.8 grams of carrier Z1 are mixed with 100 grams of silver nitrate aqueous solution of 1.0 grams of argentiferous, 60 DEG C drying 8 hours,
450 DEG C roast 4 hours, and modified aluminium oxide supports are made.Then, it mixes, passes through with 100 grams of the chlorine palladium aqueous acid containing 0.2 gram of palladium
110 DEG C roast 4 hours in 600 DEG C after drying 4 hours, and with hydrogen reducing 4 hours, 450 DEG C of reduction temperature, hydrogen volume air speed was
50 hours-1, first segment catalyst is obtained, concrete composition is shown in Table 2.
3, prepared by carrier 2
It weighs and is equivalent to 12 grams of aluminium oxide of boehmite, 69.5 grams of aluminium oxide, 9 grams of sesbania powders, mixing is added later
Containing 20 grams of poly-vinyl alcohol solution (mass concentration 5%), mass concentration is 4.0 grams of nitric acid of 68%, is equivalent to 0.25 gram of Ce2O3
Ce (NO3)3.6H2O is equivalent to 0.25 gram of La2O3La (NO3)3.6H2O is equivalent to the Ca (NO of 1 gram of CaO3)2.4H2O, quite
In 3.0 grams of ZrO2ZrOCl2.8H2O, is squeezed out by 130 milliliters of water, and wet bar is small in 700 DEG C of roastings 4 after 120 DEG C 4 hours dry
When, obtain carrier Z2, specific surface area 152m that a length of 2 mm dia is 1 millimeter2/ g, Kong Rong 0.58ml/g.
4, second segment catalyst preparation
Above-mentioned carrier Z2 is mixed with 90 grams of nickel ammonia solution of nickeliferous 14 grams, 60 DEG C drying 8 hours, 110 DEG C drying 2 hours
It is roasted 4 hours in 450 DEG C afterwards, with hydrogen reducing 4 hours, 450 DEG C of reduction temperature, hydrogen volume air speed was 50 hours-1, obtain down
Bed second segment catalyst, concrete composition are shown in Table 3.
5, evaluating catalyst
Hydroprocessing is carried out in fixed bed reactors.First segment prepared by upper bed layer filling embodiment 3 in reactor
Catalyst, lower bed layer load second segment catalyst prepared by embodiment 3, the quality of first segment catalyst and second segment catalyst
Than being 0.8.The material of the hydrocarbon containing triple carbon-carbon bonds carries out hydroprocessing, reactor head charging, bottom discharge in a continuous manner.
During the experiment, operating condition is as follows: reaction temperature: 70 DEG C, reaction pressure 1.60MPa, triple carbon-carbon bonds hydrocarbon charging weight is empty
Fast 0.1h-1, hydrogen/triple carbon-carbon bonds hydrocarbon molar ratio 20, is carried out continuously 300 hours plus hydrogen is evaluated, and hydrogen average result is added to be shown in Table 4.
[embodiment 4]
1, prepared by carrier 1
It weighs and is equivalent to 12 grams of aluminium oxide of boehmite, 170 grams of aluminium oxide, 9 grams of sesbania powders, mixing is added later
Containing 20 grams of poly-vinyl alcohol solution (mass concentration 5%), mass concentration is 4.0 grams of nitric acid of 68%, 280 milliliters of water, is squeezed out, wet
Item roasts 4 hours after 120 DEG C 4 hours dry in 800 DEG C, obtains the carrier Z1 that a length of 2 mm dia is 1 millimeter, specific surface
Product 82m2/ g, Kong Rong 0.7ml/g.
2, first segment catalyst preparation
Above-mentioned 98.2 grams of carrier Z1 are mixed with 100 grams of silver nitrate aqueous solution of 1.5 grams of argentiferous, 60 DEG C drying 8 hours,
450 DEG C roast 4 hours, and modified aluminium oxide supports are made.Then, it mixes, passes through with 100 grams of the chlorine palladium aqueous acid containing 0.3 gram of palladium
110 DEG C roast 4 hours in 600 DEG C after drying 4 hours, and with hydrogen reducing 4 hours, 450 DEG C of reduction temperature, hydrogen volume air speed was
50 hours-1, first segment catalyst is obtained, concrete composition is shown in Table 2.
3, prepared by carrier 2
It weighs and is equivalent to 12 grams of aluminium oxide of boehmite, 69.0 grams of aluminium oxide, 9 grams of sesbania powders, mixing is added later
Containing 20 grams of poly-vinyl alcohol solution (mass concentration 5%), mass concentration is 4.0 grams of nitric acid of 68%, is equivalent to 0.3 gram of La2O3's
La(NO3)3.6H2O is equivalent to the Ca (NO of 0.6 gram of CaO3)2.4H2O is equivalent to 4.0 grams of ZrO2ZrOCl2.8H2O, 130 milli of water
It rises, squeezes out, wet bar roasts 4 hours after 120 DEG C 4 hours dry in 700 DEG C, obtains the carrier that a length of 2 mm dia is 1 millimeter
Z2, specific surface area 152m2/ g, Kong Rong 0.58ml/g.
4, second segment catalyst preparation
Above-mentioned carrier Z2 is mixed with 90 grams of nickel ammonia solution of nickeliferous 14 grams, 60 DEG C drying 8 hours, 110 DEG C drying 2 hours
It is roasted 4 hours in 450 DEG C afterwards, with hydrogen reducing 4 hours, 450 DEG C of reduction temperature, hydrogen volume air speed was 50 hours-1, obtain
Two sections of catalyst, concrete composition are shown in Table 3.
5, evaluating catalyst
Hydroprocessing is carried out in fixed bed reactors.First segment prepared by upper bed layer filling embodiment 4 in reactor
Catalyst, lower bed layer load second segment catalyst prepared by embodiment 4, the quality of first segment catalyst and second segment catalyst
Than being 0.8.The material of the hydrocarbon containing triple carbon-carbon bonds carries out hydroprocessing, reactor head charging, bottom discharge in a continuous manner.
During the experiment, operating condition is as follows: 60 DEG C of reaction temperature, reaction pressure 1.80MPa, triple carbon-carbon bonds hydrocarbon charging weight space velocity
0.08h-1, hydrogen/triple carbon-carbon bonds hydrocarbon molar ratio 30, is carried out continuously 300 hours plus hydrogen is evaluated, and hydrogen average result is added to be shown in Table 4.
[embodiment 5]
1, prepared by carrier 1
It weighs and is equivalent to 12 grams of aluminium oxide of boehmite, 170 grams of aluminium oxide, 9 grams of sesbania powders, mixing is added later
Containing 20 grams of poly-vinyl alcohol solution (mass concentration 5%), mass concentration is 4.0 grams of nitric acid of 68%, 280 milliliters of water, is squeezed out, wet
Item roasts 4 hours after 120 DEG C 4 hours dry in 800 DEG C, obtains the carrier Z1 that a length of 2 mm dia is 1 millimeter, specific surface
Product 82m2/ g, Kong Rong 0.7ml/g.
2, first segment catalyst preparation
Above-mentioned 98.2 grams of carrier Z1 are mixed with 100 grams of silver nitrate aqueous solution of 1.5 grams of argentiferous, 60 DEG C drying 8 hours,
450 DEG C roast 4 hours, and modified aluminium oxide supports are made.Then, it mixes, passes through with 100 grams of the chlorine palladium aqueous acid containing 0.3 gram of palladium
110 DEG C roast 4 hours in 600 DEG C after drying 4 hours, and with hydrogen reducing 4 hours, 450 DEG C of reduction temperature, hydrogen volume air speed was
50 hours-1, first segment catalyst is obtained, concrete composition is shown in Table 2.
3, prepared by carrier 2
It weighs and is equivalent to 12 grams of aluminium oxide of boehmite, 69.7 grams of aluminium oxide, 9 grams of sesbania powders, mixing is added later
Containing 20 grams of poly-vinyl alcohol solution (mass concentration 5%), mass concentration is 4.0 grams of nitric acid of 68%, is equivalent to 0.3 gram of La2O3's
La(NO3)3.6H2O is equivalent to the Ca (NO of 2.0 grams of CaO3)2.4H2O is equivalent to 2.0 grams of ZrO2ZrOCl2.8H2O, 130 milli of water
It rises, squeezes out, wet bar roasts 4 hours after 120 DEG C 4 hours dry in 750 DEG C, obtains the carrier that a length of 2 mm dia is 1 millimeter
Z2, specific surface area 135m2/ g, Kong Rong 0.63ml/g.
4, second segment catalyst preparation
Above-mentioned carrier Z2 is mixed with 90 grams of nickel ammonia solution of nickeliferous 14 grams, 60 DEG C drying 8 hours, 110 DEG C drying 2 hours
It is roasted 4 hours in 400 DEG C afterwards, with hydrogen reducing 4 hours, 450 DEG C of reduction temperature, hydrogen volume air speed was 50 hours-1, obtain
Two sections of catalyst, concrete composition are shown in Table 3.
5, evaluating catalyst
Hydroprocessing is carried out in fixed bed reactors.First segment prepared by upper bed layer filling embodiment 5 in reactor
Catalyst, lower bed layer load second segment catalyst prepared by embodiment 5, the quality of first segment catalyst and second segment catalyst
Than being 0.8.The material of the hydrocarbon containing triple carbon-carbon bonds carries out hydroprocessing, reactor head charging, bottom discharge in a continuous manner.
During the experiment, operating condition is as follows: 80 DEG C of reaction temperature, reaction pressure 1.80MPa, triple carbon-carbon bonds hydrocarbon charging weight space velocity
0.12h-1, hydrogen/triple carbon-carbon bonds hydrocarbon molar ratio 30, is carried out continuously 300 hours plus hydrogen is evaluated, and hydrogen average result is added to be shown in Table 4.
Table 1
| Weight composition | Raw material |
| Vinylacetylene (%) | 0.5 |
| Benzene (%) | 1.0 |
| Diacetylene (%) | 1.8 |
| N-Methyl pyrrolidone (%) | 96.5 |
| Other (%) | 0.2 |
2 first segment catalyst of table composition
| Pd, w% | Ag, w% | |
| Embodiment 1 | 0.2 | 1.0 |
| Embodiment 2 | 0.2 | 1.0 |
| Embodiment 3 | 0.2 | 1.0 |
| Embodiment 4 | 0.3 | 1.5 |
| Embodiment 5 | 0.3 | 1.5 |
| Comparative example 1 | 0.2 | 1.0 |
| Comparative example 2 | 0.2 | 1.0 |
| Comparative example 3 | 0.2 | 1.0 |
| Comparative example 4 | 0.2 | 1.0 |
Table 3
Table 4
Claims (8)
1. compound hydrogenation catalyst bed, including first segment catalyst and second segment catalyst, first segment catalyst includes 1 He of carrier
Palladium or its oxide, second segment catalyst include carrier 2 and nickel or its oxide；
First segment catalyst includes following components by weight percentage:
(a) 0.02~0.2% metal Pd or its oxide；
(b) 0.04~1% at least one of IB metal in the periodic table of elements or its oxide；
Second segment catalyst includes following components by weight percentage:
(a) 10~25% metallic nickel or its oxide；
(b) 0.2~1% selected from least one of rare earth element or its oxide；
(c) 0.2~2.0% at least one of IIA metal in the periodic table of elements or its oxide；
(d) 2~5% Zr or its oxide.
2. catalyst bed according to claim 1, it is characterized in that the weight ratio of first segment catalyst and second segment catalyst
It is 0.5~1.
3. the method for the material hydrotreating of the hydrocarbon containing triple carbon-carbon bonds, use that any one of claim 1~2 is described compound plus hydrogen is urged
Agent bed, includes the following steps:
(1) hydrogen and the material is made first to generate the intermediate material containing monoene with first segment catalyst haptoreaction；
(2) above-mentioned intermediate hydrogenation of net product obtains the material containing alkane in the presence of second segment catalyst.
4. according to the method described in claim 3, it is characterized in that the reaction temperature of step (1) and/or step (2) is 40~90
℃。
5. according to the method described in claim 3, it is characterized in that the reaction pressure of step (1) and/or step (2) be 1.2~
2.2MPa。
6. according to the method described in claim 3, it is characterized in that the feed weight air speed of triple carbon-carbon bonds hydrocarbon is 0.05 in step (1)
~0.2h-1。
7. according to the method described in claim 3, it is characterized in that hydrogen/triple carbon-carbon bonds hydrocarbon molar ratio is 20~50 in step (1).
8. according to the method described in claim 3, it is characterized in that the material of the hydrocarbon containing triple carbon-carbon bonds contains diluent.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510661623.8A CN106582636B (en) | 2015-10-14 | 2015-10-14 | Composite catalyst bed |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510661623.8A CN106582636B (en) | 2015-10-14 | 2015-10-14 | Composite catalyst bed |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106582636A CN106582636A (en) | 2017-04-26 |
| CN106582636B true CN106582636B (en) | 2019-04-12 |
Family
ID=58552931
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510661623.8A Active CN106582636B (en) | 2015-10-14 | 2015-10-14 | Composite catalyst bed |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106582636B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109096032A (en) * | 2017-06-21 | 2018-12-28 | 中国石油化工股份有限公司 | Cracking c_4 selective hydrogenation catalyst |
| CN109092298B (en) * | 2017-06-21 | 2021-09-03 | 中国石油化工股份有限公司 | Four-selective hydrogenation catalyst for cracking carbon |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1081664A (en) * | 1992-04-02 | 1994-02-09 | 法国石油公司 | The method of selective hydrogenation of hydrocarbon |
| CN1141622A (en) * | 1993-12-08 | 1997-01-29 | 化学研究及许可公司 | Selective hydrogenation of highly unsaturated compounds in hydrocarbon streams |
| CN1182067A (en) * | 1996-11-11 | 1998-05-20 | 弗·哈夫曼-拉罗切有限公司 | Catalytic hydrogenation |
| CN101027269A (en) * | 2004-07-27 | 2007-08-29 | Abb路慕斯全球股份有限公司 | Process for the selective hydrogenation of alkynes and/or dienes in an olefin-containing hydrocarbon stream |
| CN101432247A (en) * | 2004-10-20 | 2009-05-13 | 催化蒸馏技术公司 | Selective hydrogenation process and catalyst |
| CN102989476A (en) * | 2011-09-09 | 2013-03-27 | 中国石油天然气股份有限公司 | Nickel-based hydrogenation catalyst and preparation method |
-
2015
- 2015-10-14 CN CN201510661623.8A patent/CN106582636B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1081664A (en) * | 1992-04-02 | 1994-02-09 | 法国石油公司 | The method of selective hydrogenation of hydrocarbon |
| CN1141622A (en) * | 1993-12-08 | 1997-01-29 | 化学研究及许可公司 | Selective hydrogenation of highly unsaturated compounds in hydrocarbon streams |
| CN1182067A (en) * | 1996-11-11 | 1998-05-20 | 弗·哈夫曼-拉罗切有限公司 | Catalytic hydrogenation |
| CN101027269A (en) * | 2004-07-27 | 2007-08-29 | Abb路慕斯全球股份有限公司 | Process for the selective hydrogenation of alkynes and/or dienes in an olefin-containing hydrocarbon stream |
| CN101432247A (en) * | 2004-10-20 | 2009-05-13 | 催化蒸馏技术公司 | Selective hydrogenation process and catalyst |
| CN102989476A (en) * | 2011-09-09 | 2013-03-27 | 中国石油天然气股份有限公司 | Nickel-based hydrogenation catalyst and preparation method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106582636A (en) | 2017-04-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101502802B (en) | Preparation method of catalyst for continuous production of succinic anhydride from hydrogenation of maleic anhydride | |
| CN105251486B (en) | Load type platinum series catalysts applied to preparing propylene by dehydrogenating propane and preparation method thereof | |
| CN105582989B (en) | Cyclohexyl benzene catalyst for synthesizing | |
| CN102614870A (en) | Vinylacetylene hydrogenation catalyst and preparation method thereof | |
| CN102256700B (en) | Selective catalytic hydrogenation of alkynes to corresponding alkenes | |
| KR20160083925A (en) | Supported catalyst, preparation method therefor and use thereof, and method for preparation of isobutylene from halomethane | |
| CN106582636B (en) | Composite catalyst bed | |
| CN106582704B (en) | Two sections of compound nickel-base catalyst beds | |
| CN106582456B (en) | Compound hydrogenation catalyst bed | |
| CN109092298A (en) | For cracking c_4 selective hydrogenation catalyst | |
| CN106964390A (en) | Benzene catalyst processed and its production and use | |
| CN114100653B (en) | Nitride supported palladium catalyst and preparation method and application thereof | |
| CN107175110B (en) | Hydrocarbon hydrogenation catalyst containing carbon-carbon triple bond | |
| CN111054325B (en) | Preparation and application of liquid phase dehydrogenation catalyst | |
| CN106669718B (en) | A kind of synthesis gas alkene catalyst and its preparation method and application | |
| CN106669723B (en) | A kind of catalyst for synthesis gas reaction and its preparation method and application | |
| CN105709775B (en) | A kind of ferrum-based catalyst and its preparation method and application | |
| CN109096032A (en) | Cracking c_4 selective hydrogenation catalyst | |
| CN106669719B (en) | A kind of producing light olefins catalyst and preparation method thereof | |
| CN109529925A (en) | Load Performance of Isomerization Catalysts for Light n-Paraffin, preparation method and its application method of molybdenum boride | |
| CN105709773B (en) | A kind of synthesis gas alkene catalyst and its preparation method and application | |
| CN109529920B (en) | Supported titanium boride catalyst for light alkane isomerization and preparation method and using method thereof | |
| CN105080562B (en) | A kind of CO hydrogenation catalysts and its preparation method and application | |
| CN109569711B (en) | Light alkane isomerization catalyst loaded with nickel carbide, preparation method and use method thereof | |
| CN105709791B (en) | A kind of preparation method of load-type iron-based catalyst |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |