CN1170632A - Catalyst for isobutane preparing reaction by normal butane isomerization and its use - Google Patents
Catalyst for isobutane preparing reaction by normal butane isomerization and its use Download PDFInfo
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- CN1170632A CN1170632A CN 96115456 CN96115456A CN1170632A CN 1170632 A CN1170632 A CN 1170632A CN 96115456 CN96115456 CN 96115456 CN 96115456 A CN96115456 A CN 96115456A CN 1170632 A CN1170632 A CN 1170632A
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- molecular sieve
- catalyzer
- reaction
- normal butane
- isobutane
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Abstract
The superstrong acid type molecular sieve catalyst is prepared with hydrogen type ZSM -5, ZSM -11 or beta-molecular sieve, adhesive and pore-creating agent and through forming, drying at room temperature to 120 deg. c and roast at 300-700 deg. c. This kind of catalyst can isomerize n-butane into isobutane at 100-300 deg. c with n-butane converting rate reaching 53% and isobutane selectivity reaching 85%. The said reaction course is suitable for application in industry.
Description
The present invention relates to a kind of normal butane isomerization system Trimethylmethane catalyzer that is used for, this Preparation of catalysts and be used for normal butane isomery isobutane preparing reaction process.Specifically providing a kind of molecular sieve type ultrastrong acid with Ti or the modification of Zr metallic element is that catalyzer carries out isobutane preparing reaction by normal butane isomerization.
Along with the development of petrochemical complex, environment protection is harsh gradually to the requirement of quality of gasoline, iso-butylene demand rapid growth.Iso-butylene is except that can directly changing the volume increase of FCC catalytic cracking process condition, still can adopt the dehydration of the n-butene skeletal isomerization and the trimethyl carbinol, and dehydrogenation of isobutane, and the Trimethylmethane utilization obtains from normal butane isomerization, and be a technological line that obtains pay attention to day by day.Most representative butane isomerization process is the Butomer technology of American UOP company exploitation.This technology is used the Pt/Al of oxide modifying
2O
3Catalyzer feeds the polyreaction that small quantity of hydrogen suppresses the small amounts of olefins of cracking generation in reaction process, to prolong catalyst life, n-butane conversion is about 50%.Domestic patent report such as the CN109499A that normal butane body plan Trimethylmethane is also arranged, it is a kind of compound Pt-ZrO of loading type zirconium white system
2/ SO
4 2-Catalyzer.
Began from 1979 on the other hand the research of solid super-strong acid is increased day by day, compare, use solid super-strong acid that many advantages are arranged in the catalyzed reaction, also be convenient to industrialization with liquid superacid such as oleum.So far the synthetic solid super-strong acid can be divided into two big classes: a class is halogen-containing, and another kind of is not halogen-containing solid super-strong acid.Halogen-containing solid super-strong acid has SbF
3-SiO
2-TiO
2, FSO
3H-SiO
2.ZrO
2, SbF
3-TrO
2.ZrO
2And FSO
3H-SiO
2.Al
2O
3Non-halogen solid super-strong acid is SO
4 2-/ MxOy type, SO
4 2-/ ZrO
2, SO
4 2-/ Fe
2O
3, SO
4 2-/ TiO
2Be representative.
The present invention went into once and proposed patent application with regard to this molecular sieve analog type solid super-strong acid and preparation method thereof, the Chinese invention patent application number is 96115289.3 to describe in detail with ZSM-5, ZSM-11, beta molecular sieve floods with the metallic salt aqueous solution of Ti or Zr and prepares the molecular sieve with superpower acidity.But this molecular sieve type ultrastrong acid is a catalyzer to be used for normal butane isomerization reaction system Trimethylmethane and then not to appear in the newspapers.
The objective of the invention is provides a kind of have high reactivity and catalyzer and utilize this catalyzer to select suitable reaction condition for isobutane preparing reaction by normal butane isomerization optionally for isobutane preparing reaction by normal butane isomerization, this reaction conditions gentleness, easy to control, be suitable in industrial production, using.
The catalyzer that the present invention provides for isobutane preparing reaction by normal butane isomerization is a kind of molecular sieve type ultrastrong acid catalyzer, this catalyzer be the applicant in earlier stage once provided carry out Hydrogen ZSM-5, ZSM-11 or the beta molecular sieve catalyzer that upgrading is handled with metal Ti or Zr.Specifically this catalyzer is to adopt ZSM-5, ZSM-11, and beta molecular sieve is handled and is obtained containing the hydrogen type molecular sieve of Ti or Zr through upgrading, TiHZSM-5, TiHZSM-11, TiH β, ZrHZSM-5, ZrHZSM-11, or ZrH β, the content of metal element Ti or Zr (weight) is 0.1～20%.Be to increase the intensity of catalyzer, and change pore structure behind the shaping of catalyst and the active of high catalyst is provided and, in the Preparation of catalysts process, in above-mentioned molecular sieve super acids, adds binding agent the selectivity of Trimethylmethane, as clay, SiO
2(adding) or Al with silicon sol
2O
3(adding) and pore-forming material with hydrated aluminum oxide or aluminium hydroxide, as the sesbania powder, Mierocrystalline cellulose or starch.Molecular sieve, binding agent and pore-forming material be 50～70%, 29～49% and 0.1～5% adding by weight ratio, and Preparation of catalysts is pressed process:
One. the preparation of molecular sieve super acids
With ZSM-5, ZSM-11 or beta-zeolite molecular sieve NH
4NO
3, HNO
3Or HCl solution exchange is for several times, drying again, and roasting obtains HZSM-5, HZSM-11, H β (the residual amount of Na＜5%).Then with containing Ti, the nitrate aqueous solution of Zr, Ti (SO
4)
2Or ZrOCl
2Aqueous solution dipping H type molecular sieve, drying again, various types of super acids are made in roasting.
Used Ti (NO in the preparation of above-mentioned molecular sieve type ultrastrong acid
3)
4, Zr (NO
3)
4, ZrOCl
2, Ti (SO
4)
2Concentration be 0.05N-3N, be preferably 0.5N～2.0N, in encloses container,, be preferably under 120 ℃～280 ℃ and flood in room temperature to 300 ℃, carry out drying in 25～120 ℃ again, under 300～700 ℃, carried out roasting 1～10 hour.
Two. Preparation of catalysts
The above-mentioned molecular sieve that makes and binding agent and pore-forming material are mixed in proportion, (0.1～2N) makes it can carry out moulding to add water or rare nitric acid, ℃ following drying and dehydrating through room temperature～120, made finished catalyst in 1～10 hour in 300～700 ℃ of roastings again, shaping of catalyst process technology is routinely carried out.
The reaction conditions that catalyzer of the present invention is used for normal butane isomerization reaction system Trimethylmethane is: 1. gas-phase reaction, and reaction pressure 0.01～1.0MPa is preferably in 0.05～0.5MPa, and 80～500 ℃ of temperature of reaction are preferably in 100～300 ℃; The gas space velocity GHSV=100 of normal butane～1000h
-1, be preferably in 300～800h
-12. liquid phase reaction, reaction pressure 1.0MPa～8.0MPa, best 2.0～6.0MPa, 80～350 ℃ of temperature of reaction are preferably in 120～250 ℃, liquid air speed (weight) 0.05～10h
-1, be preferably in 0.1～5h
-1
Relevant detailed technology contents of the present invention can give to illustrate further from following example.
Embodiment 1
Take by weighing 15g amine process synthetic ZSM-5 molecular screen primary powder, through 350 ℃ 1 hour, 400 ℃ of half an hour, 450 ℃ of half an hour, 500 ℃ of half an hour, 550 ℃ of roastings of 2 hours obtain burning the NaZSM-5 sample of organic amine template, again with this sample 1NH
4NO
3Each consumption is 80ml, exchange 4 times, after filtration, airing, after 120 ℃ of oven dry, again in 350 ℃ 1 hour, 400 ℃ of half an hour, 500 ℃ 1 hour, 550 ℃ of roastings in 2 hours obtain the HZSM-5 sample A of exchange degree＞95%.
Embodiment 2
Use 1NHNO respectively
3And NH
4NO
3Solution carries out ion exchange reaction to ZSM-11 and the former powder of beta molecular sieve, adopts embodiment 1 identical method can obtain HZSM-11 sample B, H β sample C.
Embodiment 3
Take by weighing 5g sample A, place 60ml 0.5NTi (SO is housed
4)
2In the aqueous solution stainless steel synthesis reactor (in teflon lined is arranged), synthesis reactor is heated to 180 ℃ under air-tight state, and it was kept 48 hours, take out reactant after reducing to room temperature, after filtration, with washed with de-ionized water to there not being free state Ti (SO
4)
2Till, through airing, 120 ℃ of oven dry in 2 hours, 550 ℃ of roastings 2 hours obtain super acids TiHZSM-5, are labeled as D.
Embodiment 4
Take by weighing 5g sample A, place 80ml 0.6NZrOCl is housed
2Tighten the synthesis reactor loam cake in the stainless steel synthesis reactor of the aqueous solution, be heated to 220 ℃, and kept 36 hours, reduce to the room temperature hypsokinesis and pour out reactant, and with washed with de-ionized water 3～4 times, until no free state ZrOCl
2Through natural airing, 120 ℃ of oven dry of spending the night, and 550 ℃ of roastings 2 hours, obtain having superpower acidity sieve sample ZrHZSM-5 are demarcated and are E.
Embodiment 5
Respectively take by weighing 5g sample B and C, place respectively 50ml 0.8NZr (NO is housed
3)
4In the stainless steel synthesis reactor of the aqueous solution, under the airtight situation of synthesis reactor, be heated to 210 ℃, and kept 36 hours, take out after waiting to reduce to room temperature, with deionized water washing 5～6 times, again through airing, 120 ℃ of drying courses, in 350 ℃ 2 hours, 400 ℃ 1 hour, 500 ℃ of roastings in 2 hours obtain ZrHZSM-11 and ZrH β sample, demarcate respectively to be F, G.
Embodiment 6
Take by weighing D sample 4g and add 2g clay and 0.1g sesbania powder, use 0.1NHNO
35 milliliters of accent all mix the Cylinder that pinchings are made φ 3mm, airing under the room temperature, and 120 ℃ of dryings 1 hour, again in 350 ℃ of roastings 1 hour, 450 roastings 1 hour, it is D that 500 ℃ of roastings made finished catalyst in 4 hours
1Take by weighing E and F sample 4g respectively, each adds 3g alumina trihydrate and sesbania powder 0.1g and takes by weighing G sample 4g, adds the 4g silicon sol and (contains 28%SiO
2) and sesbania powder 0.1g, be E by above-mentioned identical method finished product catalysis
1, F
1And G
1
Embodiment 7
Take by weighing sample D1g, estimate it to the isomerized effect of normal butane on miniature fixed-bed reactor, the reactor outlet of this device is connected to put down to six logical sampling valves and gas chromatograph and links, and can be implemented in line analysis, at reaction conditions be: 100 ℃ of temperature, the gas space velocity GHSV=800h of normal butane
-1, reaction pressure is a normal pressure, and the transformation efficiency of normal butane is 35%, and the selectivity of Trimethylmethane is 78%.
Embodiment 8
Take by weighing sample D
11g, and be crushed to 20～40 orders.Utilizing and estimate it on the device of example 7 to the isomerized effect of normal butane, is 120 ℃ of temperature at reaction conditions, the gas space velocity GHSV=750h of normal butane
-1, reaction pressure is a normal pressure, and the transformation efficiency of normal butane is 52.5%, and the selectivity of Trimethylmethane is 82%.
Embodiment 9
Take by weighing sample E respectively
1, F
1And G
1Each 1g, and be crushed to 20～40 orders utilizes on the micro-reactor of example 7 and estimates it to the isomerized effect of normal butane.At reaction conditions is 120 ℃ of temperature, pressure 3.0MPa, liquid air speed (weight) 2.0h of normal butane
-1, the transformation efficiency of normal butane is respectively 45.7%, 51.1% and 47.8%, and the selectivity of Trimethylmethane is respectively 80.9%, 79.9% and 83.5%.
Embodiment 10
Take by weighing D and D
1Sample 1g also is crushed to 20～40 orders, utilize the performance of estimating its normal butane isomerization on the reaction unit of example 7, reaction conditions is all identical with embodiment 8, react after 1 hour, the transformation efficiency of normal butane is respectively 53.1% and 52.5%, and the selectivity of Trimethylmethane is 79.8% and 82%, reacts after 20 hours, the D activity of such catalysts descends 6%, D
1Activity of such catalysts and selectivity all do not have decline.
By above-mentioned example, after adding binding agent and pore-forming material in the Preparation of catalysts, the catalysis isobutane preparing reaction by normal butane isomerization is had better activity and selectivity, life of catalyst also can prolong simultaneously, therefore is suitable for using in industrial production.
Claims (4)
1. an isobutane preparing reaction by normal butane isomerization is characterized in that with molecular sieve super acid type catalyzer molecular sieve type ultrastrong acid is the H type ZSM-5 that contains Ti or Zr metallic element, and ZSM-11 or beta molecular sieve, the content of metallic element are 0.1～20% of molecular sieve.
2. by the described catalyzer of claim 1, it is characterized in that containing in the catalyzer binding agent, binding agent is a clay, SiO
2Or Al
2O
3, weight of binder accounts in the catalyzer 25～45%.
3. press the described Preparation of catalysts method of claim 1 for one kind, it is characterized in that in molecular sieve and binding agent, adding in the preparation process pore-forming material and mix moulding, in room temperature～120 ℃ drying, 300 ℃～700 ℃ roastings in 1～10 hour are made, the weight ratio of each component is a molecular sieve: 50～70%, binding agent: 29～49%, pore-forming material: 0.1～5%.
4. a utilization is carried out isobutane preparing reaction by normal butane isomerization by the described catalyzer of claim 1, it is characterized in that reaction conditions is: 1) for gas-phase reaction, temperature is at the air speed GHSV=300～800h of 100～300 ℃ of normal butanes
-1, pressure 0.05MPa～0.5MPa; 2) for liquid phase reaction, pressure 2.0～6.0MPa, 120 ℃～250 ℃ of temperature, liquid air speed WHSV 0.1～5h
-1
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96115456A CN1087660C (en) | 1996-07-15 | 1996-07-15 | Catalyst for isobutane preparing reaction by normal butane isomerization and its use |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96115456A CN1087660C (en) | 1996-07-15 | 1996-07-15 | Catalyst for isobutane preparing reaction by normal butane isomerization and its use |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1170632A true CN1170632A (en) | 1998-01-21 |
| CN1087660C CN1087660C (en) | 2002-07-17 |
Family
ID=5122708
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN96115456A Expired - Fee Related CN1087660C (en) | 1996-07-15 | 1996-07-15 | Catalyst for isobutane preparing reaction by normal butane isomerization and its use |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101722056B (en) * | 2008-10-24 | 2011-11-30 | 中国科学院大连化学物理研究所 | Preparation method of non-loading type boride catalyst |
| CN101745407B (en) * | 2008-11-28 | 2012-05-09 | 中国石油化工股份有限公司 | Solid super acidic catalyst and preparation method thereof |
| CN106076401A (en) * | 2016-06-14 | 2016-11-09 | 天津大学 | Superacid-coated HZSM-5 molecular sieve catalyst, and preparation method and application thereof |
| CN108080009A (en) * | 2016-11-21 | 2018-05-29 | 中国石油大学(华东) | A kind of alkane isomerization reaction-regenerative device and method |
| CN111018650A (en) * | 2018-10-10 | 2020-04-17 | 中国石油化工股份有限公司 | Butene isomerization process |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101537369B (en) * | 2008-03-21 | 2012-02-15 | 上海宝钢化工有限公司 | ZSM-5 catalyst and preparation thereof and use thereof |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3420707A1 (en) * | 1984-06-02 | 1985-12-05 | Hoechst Ag, 6230 Frankfurt | METHOD FOR ISOMERIZING O-, M-, AND / OR P-TOLUIDINE |
| FR2601601A1 (en) * | 1986-07-16 | 1988-01-22 | Total France | HYDROCARBON ISOMERIZATION CATALYST, PROCESS FOR THE PREPARATION AND APPLICATION OF SAID CATALYST. |
| US5095169A (en) * | 1988-03-30 | 1992-03-10 | Uop | Normal paraffin hydrocarbon isomerization process using activated zeolite beta |
| US4899012A (en) * | 1988-10-17 | 1990-02-06 | Uop | Catalyst for the isomerization of aromatics |
| CN1040846C (en) * | 1993-05-11 | 1998-11-25 | 中国石油化工总公司 | Method for preparation of superstrong acid of carried oxide system |
-
1996
- 1996-07-15 CN CN96115456A patent/CN1087660C/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101722056B (en) * | 2008-10-24 | 2011-11-30 | 中国科学院大连化学物理研究所 | Preparation method of non-loading type boride catalyst |
| CN101745407B (en) * | 2008-11-28 | 2012-05-09 | 中国石油化工股份有限公司 | Solid super acidic catalyst and preparation method thereof |
| CN106076401A (en) * | 2016-06-14 | 2016-11-09 | 天津大学 | Superacid-coated HZSM-5 molecular sieve catalyst, and preparation method and application thereof |
| CN106076401B (en) * | 2016-06-14 | 2019-01-15 | 天津大学 | Superacid-coated HZSM-5 molecular sieve catalyst, and preparation method and application thereof |
| CN108080009A (en) * | 2016-11-21 | 2018-05-29 | 中国石油大学(华东) | A kind of alkane isomerization reaction-regenerative device and method |
| CN111018650A (en) * | 2018-10-10 | 2020-04-17 | 中国石油化工股份有限公司 | Butene isomerization process |
| CN111018650B (en) * | 2018-10-10 | 2023-09-29 | 中国石油化工股份有限公司 | Butene isomerization process |
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| Publication number | Publication date |
|---|---|
| CN1087660C (en) | 2002-07-17 |
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