CN1704160A - Catalyst for hydrogen oxidation reaction in ethylbenzene dehydrogenation process - Google Patents
Catalyst for hydrogen oxidation reaction in ethylbenzene dehydrogenation process Download PDFInfo
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- CN1704160A CN1704160A CNA200410024727XA CN200410024727A CN1704160A CN 1704160 A CN1704160 A CN 1704160A CN A200410024727X A CNA200410024727X A CN A200410024727XA CN 200410024727 A CN200410024727 A CN 200410024727A CN 1704160 A CN1704160 A CN 1704160A
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- Prior art keywords
- catalyst
- reaction
- ethylbenzene dehydrogenation
- dehydrogenation process
- ethylbenzene
- Prior art date
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- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 title claims abstract description 92
- 238000006356 dehydrogenation reaction Methods 0.000 title claims abstract description 51
- 238000000034 method Methods 0.000 title claims abstract description 32
- 239000003054 catalyst Substances 0.000 title claims description 74
- 238000007254 oxidation reaction Methods 0.000 title description 11
- 239000001257 hydrogen Substances 0.000 title description 7
- 229910052739 hydrogen Inorganic materials 0.000 title description 7
- 125000004435 hydrogen atom Chemical class [H]* 0.000 title 1
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims abstract description 41
- 229910052697 platinum Inorganic materials 0.000 claims abstract description 20
- 229910052719 titanium Inorganic materials 0.000 claims abstract description 19
- 239000010936 titanium Substances 0.000 claims abstract description 19
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims abstract description 18
- QCWXUUIWCKQGHC-UHFFFAOYSA-N Zirconium Chemical compound [Zr] QCWXUUIWCKQGHC-UHFFFAOYSA-N 0.000 claims abstract description 18
- 229910052735 hafnium Inorganic materials 0.000 claims abstract description 18
- VBJZVLUMGGDVMO-UHFFFAOYSA-N hafnium atom Chemical compound [Hf] VBJZVLUMGGDVMO-UHFFFAOYSA-N 0.000 claims abstract description 18
- 229910052726 zirconium Inorganic materials 0.000 claims abstract description 18
- 238000006243 chemical reaction Methods 0.000 claims description 64
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 claims description 32
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 23
- 229910052751 metal Inorganic materials 0.000 claims description 17
- 239000002184 metal Substances 0.000 claims description 17
- 229910052718 tin Inorganic materials 0.000 claims description 12
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 claims description 7
- KZHJGOXRZJKJNY-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Si]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O KZHJGOXRZJKJNY-UHFFFAOYSA-N 0.000 claims description 6
- 229910052863 mullite Inorganic materials 0.000 claims description 6
- 229910000323 aluminium silicate Inorganic materials 0.000 claims description 3
- CNLWCVNCHLKFHK-UHFFFAOYSA-N aluminum;lithium;dioxido(oxo)silane Chemical compound [Li+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O CNLWCVNCHLKFHK-UHFFFAOYSA-N 0.000 claims description 3
- 229910052878 cordierite Inorganic materials 0.000 claims description 3
- JSKIRARMQDRGJZ-UHFFFAOYSA-N dimagnesium dioxido-bis[(1-oxido-3-oxo-2,4,6,8,9-pentaoxa-1,3-disila-5,7-dialuminabicyclo[3.3.1]nonan-7-yl)oxy]silane Chemical compound [Mg++].[Mg++].[O-][Si]([O-])(O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2)O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2 JSKIRARMQDRGJZ-UHFFFAOYSA-N 0.000 claims description 3
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 3
- -1 spinelle Chemical compound 0.000 claims description 3
- 229910052642 spodumene Inorganic materials 0.000 claims description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 34
- 239000001301 oxygen Substances 0.000 abstract description 34
- 229910052760 oxygen Inorganic materials 0.000 abstract description 34
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 abstract description 11
- 239000007809 chemical reaction catalyst Substances 0.000 abstract 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 14
- 230000009257 reactivity Effects 0.000 description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 13
- 238000005516 engineering process Methods 0.000 description 8
- 238000005470 impregnation Methods 0.000 description 8
- 239000002253 acid Substances 0.000 description 7
- 239000002245 particle Substances 0.000 description 6
- 238000002360 preparation method Methods 0.000 description 6
- 238000011282 treatment Methods 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- 239000007788 liquid Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 239000003570 air Substances 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 4
- 235000011150 stannous chloride Nutrition 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 150000007513 acids Chemical class 0.000 description 3
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 150000002823 nitrates Chemical class 0.000 description 3
- 229910001220 stainless steel Inorganic materials 0.000 description 3
- 239000010935 stainless steel Substances 0.000 description 3
- VEFXTGTZJOWDOF-UHFFFAOYSA-N benzene;hydrate Chemical compound O.C1=CC=CC=C1 VEFXTGTZJOWDOF-UHFFFAOYSA-N 0.000 description 2
- 208000012839 conversion disease Diseases 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000009938 salting Methods 0.000 description 2
- TXUICONDJPYNPY-UHFFFAOYSA-N (1,10,13-trimethyl-3-oxo-4,5,6,7,8,9,11,12,14,15,16,17-dodecahydrocyclopenta[a]phenanthren-17-yl) heptanoate Chemical compound C1CC2CC(=O)C=C(C)C2(C)C2C1C1CCC(OC(=O)CCCCCC)C1(C)CC2 TXUICONDJPYNPY-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 229910021626 Tin(II) chloride Inorganic materials 0.000 description 1
- DKCGSKXEOYYMOR-UHFFFAOYSA-N [O].[Hf].[N+](=O)(O)[O-] Chemical compound [O].[Hf].[N+](=O)(O)[O-] DKCGSKXEOYYMOR-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 229910052784 alkaline earth metal Inorganic materials 0.000 description 1
- 150000001342 alkaline earth metals Chemical class 0.000 description 1
- 150000001805 chlorine compounds Chemical class 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000007598 dipping method Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 229910052758 niobium Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 229910052703 rhodium Inorganic materials 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000001119 stannous chloride Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052715 tantalum Inorganic materials 0.000 description 1
- XJDNKRIXUMDJCW-UHFFFAOYSA-J titanium tetrachloride Chemical class Cl[Ti](Cl)(Cl)Cl XJDNKRIXUMDJCW-UHFFFAOYSA-J 0.000 description 1
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
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a hydroxidizing reaction catalyst in the process of ethyl benzene dehydrogenation which mainly resolves the problem of lower oxygen change rate or lower oxygen selectivity of hydroxidizing reaction catalyst in the process of ethyl benzene dehydrogenation. It charges platinum and at least one kind of titanium, zirconium and hafnium on the carrier which can be used in the process of styrene by ethyl benzene dehydrogenation.
Description
Technical field
The present invention relates to be used for the catalyst of ethylbenzene dehydrogenation process hydroxide reaction.
Background technology
Styrene is basic Organic Chemicals.Ethylbenzene dehydrogenation technology is to produce cinnamic main method.Ethylbenzene dehydrogenation generates styrene and hydrogen is a balanced reaction that heat absorption, molecular number increase.Improve reaction temperature, reduce reaction pressure, use dynamical dehydrogenation, can improve the conversion per pass of ethylbenzene, but still be subjected to the restriction of thermodynamical equilibrium.
Ethylbenzene dehydrogenation-hydroxide technology is the new technology that increases H 2 selective oxidation on the basis of ethylbenzene dehydrogenation, that is to say that the first step is a dehydrogenation reaction, second step was a hydroxide reaction, be the hydrogen of first step reaction generation and the oxygen generation combustion reaction of adding, the 3rd step was that the product in second step is proceeded dehydrogenation reaction.Also can be continuous carry out hydroxide-dehydrogenation reaction again.For ethylbenzene dehydrogenation technology, ethylbenzene dehydrogenation-hydroxide technology mainly has 2 advantages: (1) ethylbenzene dehydrogenation is the endothermic reaction, and hydrogen burning produces heat and provides heat for next step dehydrogenation; (2), thereby improve the conversion ratio of reaction because the hydrogen of one of product, helps ethylbenzene dehydrogenation reaction by reaction consumes moves to generating the styrene direction.
The general catalyst that adopts the Fe series catalysts as ethylbenzene dehydrogenation reaction.The catalyst that is used for ethylbenzene dehydrogenation reaction such as the catalyst that adopts patent CN1400052A or CN1443738A to describe.
Introduced PtSnLi/Al among patent US4914249 and the US4812597
2O
3Catalyst is used for the hydroxide reaction of ethylbenzene dehydrogenation process, and wherein Li also can be other alkali metal or alkaline-earth metal, adopts α-Al
2O
3As carrier.Introduced among the patent US5994606 and adopted the Pt of support type or the hydroxide reaction that the Pd catalyst is used for ethylbenzene dehydrogenation process, the oxide of employing Sn, Ti, Ta, Nb or their mixture are as carrier.Patent US5872075 has introduced employing Pt/Al
2O
3Catalyst is used for the hydroxide reaction of ethylbenzene dehydrogenation process, wherein Al
2O
3Have specific specific surface and acid strength.US5001291 adopts Pd, Pt, Rh or Ru catalyst on the oxide that loads on tin, is used for the hydroxide reaction of ethylbenzene dehydrogenation process.
When the catalyst of above-mentioned patent preparation was used for the hydroxide reaction of ethylbenzene dehydrogenation process, oxygen conversion or oxygen selectivity were high not enough.Oxygen conversion or oxygen selectivity are two important indicators in the hydroxide reaction in the ethylbenzene dehydrogenation process.If unconverted oxygen is arranged, this part oxygen enters the dehydrogenation bed may cause the reaction that is unfavorable for dehydrogenation, consumes aromatic hydrocarbons simultaneously in the hydroxide stage.The oxygen selectivity is meant oxygen expenditure the percentage on the feed hydrogen (remaining oxygen then consumes side reaction takes place) on aromatic hydrocarbons, the oxygen molal quantity that promptly is used for hydroxide accounts for the percentage of total conversion oxygen molal quantity.Because the aromatic hydrocarbons loss can cause cost of material and rise, so the high oxygen selectivity is the important goal of catalyst for hydroxide reaction preparation.
Summary of the invention
Technical problem to be solved by this invention is oxygen conversion or the not high enough problem of oxygen selectivity that has catalyst for hydroxide reaction in the ethylbenzene dehydrogenation process in the prior art, and a kind of new catalyst that is used for the ethylbenzene dehydrogenation process hydroxide reaction is provided.When this catalyst is used for the ethylbenzene dehydrogenation process hydroxide reaction, has the oxygen conversion height, the characteristics that the oxygen selectivity is high.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of catalyst that is used for the ethylbenzene dehydrogenation process hydroxide reaction, to be selected from least a in Alpha-alumina, mullite, mullite, spinelle, cordierite, alumino-silicate or the spodumene is carrier, by weight percentage, catalyst comprises following component:
A) in the platinum of metal 0.02～5%;
B) at least a in titanium, zirconium or the hafnium of being selected from of metal 0.05～10%;
C) 85～99.9% carrier.
In the technique scheme, the carrier preferred version is an Alpha-alumina.By weight percentage, be 0.02～2% in the consumption preferable range of metal platinum, at least a consumption preferable range that is selected from titanium, zirconium or the hafnium in metal is 0.1～5%.By weight percentage, preferred version is also to contain in the catalyst to count 0.02～10% tin with metal, is 0.06～6% in the consumption preferable range of metal tin.
Ethylbenzene of the present invention prepares cinnamic ethylbenzene dehydrogenation-hydroxide technology, may further comprise the steps: (1) first dehydrogenation reaction.Ethylbenzene and water are passed through catalyst for phenylethylene dehydrogenation; (2) hydroxide reaction.In first products of dehydrogenation reactions, add oxygen or contain the gas of oxygen, pass through hydro-oxidation catalyst; (3) second dehydrogenation reactions.The product that hydroxide reaction is produced passes through dehydrogenation.
The temperature of above-mentioned ethylbenzene dehydrogenation-hydroxide reaction is 500～700 ℃ of scopes, and reaction pressure is in 0.1～10 kg/cm scope.
Before hydroxide reaction, add oxygen or oxygenous gas, such as the mist of air, oxygen and nitrogen.
Stream temperature behind the hydroxide reaction is generally more than 580 ℃, better more than 600 ℃.
The preparation method who is used for the ethylbenzene dehydrogenation process catalyst for hydroxide reaction of the present invention is as follows:
Carrier can be selected Alpha-alumina, mullite, mullite, spinelle, cordierite, alumino-silicate or spodumene for use.
The adding of titanium, zirconium or hafnium can add carrier in platinum prior to platinum or with platinum while or back.
The adding of titanium, zirconium or hafnium can be adopted the method for carrier impregnation in corresponding soluble metal salting liquid, as adopt nitrate, sulfate, the chloride of titanium, zirconium or hafnium, add suitable solvent such as water-soluble separating, carrier was immersed solution more than 1 minute, take out, dry more than 1 hour through 90～150 ℃; The solubility solution of platinum-impregnated again, after the oven dry, 250～600 ℃ of roastings obtained the hydro-oxidation catalyst of ethylbenzene dehydrogenation more than 1 hour.Also can adopt the soluble metal salting liquid of carrier direct impregnation platinum and titanium, zirconium or hafnium, more than 1 hour, 250～600 ℃ of roastings obtained the hydro-oxidation catalyst of ethylbenzene dehydrogenation more than 1 hour through 90～150 ℃ of oven dry.All right first platinum-impregnated, oven dry; Flood titanium, zirconium or hafnium again, dry the back roasting, obtain the hydro-oxidation catalyst of ethylbenzene dehydrogenation.
The adding of tin can add carrier simultaneously with platinum, titanium, zirconium or hafnium; Perhaps, add carrier simultaneously with titanium, zirconium or hafnium prior to platinum; Also can add carrier separately prior to platinum.Each dipping is after 90～150 ℃ of oven dry more than 1 hour; After all element adds, oven dry, 250～600 ℃ of roastings are more than 1 hour.
The weight content of titanium, zirconium or hafnium counts 0.05～10% with metal in the catalyst in the catalyst, better 0.1～5%.In the catalyst weight content of platinum in metal in the catalyst in 0.02～5% scope, better 0.02～2%.The weight content of tin in metal in the catalyst in 0.02～10% scope, better in 0.06～6% scope.
The oxygen conversion of indication of the present invention and oxygen selectivity obtain by following account form.
The present invention owing to added in carrier is selected from least a as the catalyst activity main body in titanium, zirconium or the hafnium, overcome the oxygen conversion and the not high enough shortcoming of oxygen selectivity of hydro-oxidation catalyst in the previous patent, the hydro-oxidation catalyst that provides, have high oxygen conversion reach 100% and high oxygen selectivity reach 92%, obtained better technical effect.
The invention will be further elaborated below by embodiment.
The specific embodiment
[comparative example 1]
Ethylbenzene dehydrogenation reaction carries out in two negative pressure adiabatic reactors, can heat between two reactors.750 milliliters of Fe-series catalysts by patent CN1400052A preparation are housed respectively in the stainless steel reaction pipe that two internal diameters are 50.8 millimeters.The second reactor outlet pressure is 50Kpa, liquid air speed 0.5 hour
-1, water/ethylbenzene weight ratio 1.3, the first and second temperature of reactor are respectively 615 ℃ and 620 ℃.Reaction conversion ratio is 65.3%, single receipts 63.6%.
[embodiment 1]
Hydroxide reaction carries out in internal diameter is 25 millimeters stainless steel reaction pipe, in adorn 30 milliliters of hydro-oxidation catalysts.Reaction pressure is a normal pressure, liquid air speed 3 hours
-1, 500～650 ℃ of reaction temperatures are adjustable.In comparative example 1 first reactor through the oil phase after the dehydrogenation reaction, and the water that adds, oxygen, hydrogen, nitrogen are as the hydroxide reaction thing.The hydroxide reaction thing is formed as table 1.
The raw material of table 1 hydroxide reaction is formed
| Raw material | Content (molar percentage) |
| Styrene | ????2.4％ |
| Ethylbenzene | ????5.4％ |
| Benzene and toluene | ????0.08％ |
| ????H 2 | ????2.4％ |
| ????O 2 | ????1.1％ |
| ????N 2 | ????0.11％ |
| Water | ????88.51％ |
By measuring the composition of reactant and product, calculate oxygen conversion and the oxygen selectivity of catalyst in hydroxide reaction.
[embodiment 2]
Get 100 gram alpha aluminium oxide particle carrier impregnation in the 100 ml water solution that contain 4.0 gram chloroplatinic acids, 7.32 gram zirconyl nitrates, 8.3 milliliters of hydrochloric acid, take out back 110 ℃ of oven dry 3 hours, 500 ℃ of air-treatments 2 hours obtain catalyst 1.
Contain 0.60% (weight) Pt and 1.0% (weight) zirconium in the catalyst 1.
With the method for embodiment 1 catalyst 1 is carried out reactivity worth and investigate, the reactivity worth under 580 ℃ of reaction temperatures the results are shown in Table 2.
[comparative example 2]
Get in the solution of 100 gram alpha aluminium oxide particle carrier impregnation in the 100 ml water solution that contain 6.0 gram chloroplatinic acids, 8.3 milliliters of hydrochloric acid, take out the back oven dry, 450 ℃ of air-treatments 1 hour obtain catalyst 2.
Contain 0.90% (weight) Pt in the catalyst 2.
With the method for embodiment 1 catalyst 2 is carried out reactivity worth and investigate, the reactivity worth under 580 ℃ of reaction temperatures the results are shown in Table 2.
[embodiment 3]
Get 100 gram alpha aluminium oxide particle carrier impregnation in the 100 ml water solution that contain 24.8 gram titanium tetrachlorides, take out back 120 ℃ of oven dry 2 hours; Be immersed in the solution in the 100 ml water solution that contain 8.0 gram chloroplatinic acids, 16 gram stannous chlorides, 18.3 gram zirconyl nitrates, 8.3 milliliters of hydrochloric acid again, take out back 120 ℃ of oven dry, 450 ℃ of air-treatments 2 hours obtain catalyst 3.
Contain 1.20% (weight) Pt, 4.0% (weight) Sn, 2.5% (weight) titanium and 2.5% (weight) zirconium in the catalyst 3.
With the method for embodiment 1 catalyst 3 is carried out reactivity worth and investigate, the reactivity worth under 580 ℃ of reaction temperatures the results are shown in Table 2.
[embodiment 4]
Get in the solution of 100 gram alpha aluminium oxide particle carrier impregnation in the 100 ml water solution that contain 0.32 gram stannous chloride, 8.3 milliliters of hydrochloric acid, take out back 120 ℃ of oven dry 2 hours; Be immersed in the solution in the 100 ml water solution that contain 0.26 gram chloroplatinic acid, 0.50 gram nitric acid oxygen hafnium, 8.3 milliliters of hydrochloric acid again, take out the back oven dry, 250 ℃ of air-treatments 3 hours obtain catalyst 4.
Contain 0.04% (weight) Pt, 0.08% (weight) Sn and 0.1% (weight) hafnium in the catalyst 4.
With the method for embodiment 1 catalyst 4 is carried out reactivity worth and investigate, the reactivity worth under 580 ℃ of reaction temperatures the results are shown in Table 2.
[embodiment 5]
Get in the solution of 100 gram alpha aluminium oxide particle carrier impregnation in the 100 ml water solution that contain 0.26 gram chloroplatinic acid, 1.28 gram stannous chlorides, 2.3 gram titanyl nitrates, 1.1 gram hafnyl chlorides, 8.3 milliliters of hydrochloric acid, take out the back oven dry, 600 ℃ of air-treatments 1 hour obtain catalyst 5.
Contain 0.04% (weight) Pt, 0.32% (weight) Sn, 0.2% (weight) titanium and 0.2% (weight) hafnium in the catalyst 5.
With the method for embodiment 1 catalyst 5 is carried out reactivity worth and investigate, the reactivity worth under 580 ℃ of reaction temperatures the results are shown in Table 2.
[comparative example 3]
Get in the solution of 100 gram alpha aluminium oxide particle carrier impregnation in the 100 ml water solution that contain 0.53 gram chloroplatinic acid, 2 gram stannous chlorides, 8.3 milliliters of hydrochloric acid, take out the back oven dry, 450 ℃ of air-treatments 1 hour obtain catalyst 6.
Contain 0.080% (weight) Pt and 0.50% (weight) Sn in the catalyst 6.
With the method for embodiment 1 catalyst 6 is carried out reactivity worth and investigate, the reactivity worth under 580 ℃ of reaction temperatures the results are shown in Table 2.
[embodiment 6]
Ethylbenzene dehydrogenation-hydroxide reaction carries out in three negative pressure adiabatic reactors, 750 milliliters of Fe-series catalysts by patent CN1400052A preparation are housed respectively in the stainless steel reaction pipe that three internal diameters are 50.8 millimeters, wherein on second inherent Fe-series catalyst of reactor 200 milliliters of hydro-oxidation catalysts by embodiment 3 preparations are housed also, the gas after first dehydrogenation reaction carries out second dehydrogenation reaction again through the hydro-oxidation catalyst in second reactor earlier.The 3rd reactor outlet pressure is 50Kpa, liquid air speed 0.5 hour
-1, water/ethylbenzene weight ratio 1.3, first, second and the interior dehydrogenation bed temperature of the 3rd reactor are respectively 615 ℃, 615 ℃ and 620 ℃.Reaction conversion ratio is 75.5%, single receipts 72.5%.
The reactivity worth of table 2 catalyst
| The catalyst activity component weight content | Oxygen conversion | The oxygen selectivity | |
| Catalyst 1 | 0.60%Pt, 1.0% zirconium. | 100% | 89.4% |
| Catalyst 2 | 0.90%Pt | 99.0% | 88.3% |
| Catalyst 3 | 1.20%Pt, 4.0%Sn, 2.5% titanium, 2.5% zirconium | 100% | 91.8% |
| Catalyst 4 | 0.04%Pt, 0.08%Sn, 0.1% hafnium | 100% | 92.0% |
| Catalyst 5 | 0.04%Pt, 0.32%Sn, 0.2% titanium, 0.2% hafnium | 100% | 91.6% |
| Catalyst 6 | 0.080%Pt, 0.50%Sn | 99.5% | 90.2% |
Claims (6)
1, a kind of catalyst that is used for the ethylbenzene dehydrogenation process hydroxide reaction, to be selected from least a in Alpha-alumina, mullite, mullite, spinelle, cordierite, alumino-silicate or the spodumene is carrier, by weight percentage, catalyst comprises following component:
A) in the platinum of metal 0.02～5%;
B) at least a in titanium, zirconium or the hafnium of being selected from of metal 0.05～10%;
C) 85～99.9% carrier.
2,, it is characterized in that carrier is an Alpha-alumina according to the described catalyst that is used for the ethylbenzene dehydrogenation process hydroxide reaction of claim 1.
3,, it is characterized in that by weight percentage the consumption in metal platinum is 0.02～2% according to the described catalyst that is used for the ethylbenzene dehydrogenation process hydroxide reaction of claim 1.
4,, it is characterized in that at least a consumption that is selected from titanium, zirconium or the hafnium in metal by weight percentage is 0.1～5% according to the described catalyst that is used for the ethylbenzene dehydrogenation process hydroxide reaction of claim 1.
5,, it is characterized in that also containing in the catalyst by weight percentage and count 0.02～10% tin with metal according to the described catalyst that is used for the ethylbenzene dehydrogenation process hydroxide reaction of claim 1.
6,, it is characterized in that by weight percentage the consumption in metal tin is 0.06～6% according to the described catalyst that is used for the ethylbenzene dehydrogenation process hydroxide reaction of claim 5.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200410024727XA CN1318132C (en) | 2004-05-28 | 2004-05-28 | Catalyst for hydrogen oxidation reaction in ethylbenzene dehydrogenation process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200410024727XA CN1318132C (en) | 2004-05-28 | 2004-05-28 | Catalyst for hydrogen oxidation reaction in ethylbenzene dehydrogenation process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1704160A true CN1704160A (en) | 2005-12-07 |
| CN1318132C CN1318132C (en) | 2007-05-30 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB200410024727XA Expired - Lifetime CN1318132C (en) | 2004-05-28 | 2004-05-28 | Catalyst for hydrogen oxidation reaction in ethylbenzene dehydrogenation process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1318132C (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101733097B (en) * | 2009-12-07 | 2012-11-14 | 中国科学院山西煤炭化学研究所 | Catalyst for preparing gamma-valerolactone by alpha-angelica lactone, preparation method and application |
| CN105646125A (en) * | 2014-11-20 | 2016-06-08 | 中国石油化工股份有限公司 | Ethylbenzene dehydrogenation-hydrogen oxidation reaction process |
| CN105669355A (en) * | 2014-11-20 | 2016-06-15 | 中国石油化工股份有限公司 | Process for preparation of styrene from ethylbenzene |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| IT1238085B (en) * | 1990-02-07 | 1993-07-05 | Snam Progetti | CATALIC COMPOSITION FOR THE DEHYDROGENATION OF C2-C5 PARAFFINS |
| US5994606A (en) * | 1995-03-08 | 1999-11-30 | Mitsubishi Chemical Corporation | Method for dehydrogenation of hydrocarbon |
| CN1039917C (en) * | 1995-11-14 | 1998-09-23 | 中国石油化工总公司 | Pt-Sn-Ti multi-metal reforming catalyst |
-
2004
- 2004-05-28 CN CNB200410024727XA patent/CN1318132C/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101733097B (en) * | 2009-12-07 | 2012-11-14 | 中国科学院山西煤炭化学研究所 | Catalyst for preparing gamma-valerolactone by alpha-angelica lactone, preparation method and application |
| CN105646125A (en) * | 2014-11-20 | 2016-06-08 | 中国石油化工股份有限公司 | Ethylbenzene dehydrogenation-hydrogen oxidation reaction process |
| CN105669355A (en) * | 2014-11-20 | 2016-06-15 | 中国石油化工股份有限公司 | Process for preparation of styrene from ethylbenzene |
| CN105646125B (en) * | 2014-11-20 | 2018-04-06 | 中国石油化工股份有限公司 | Ethylbenzene dehydrogenation hydroxide reaction technique |
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| Publication number | Publication date |
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| CN1318132C (en) | 2007-05-30 |
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