CN1014401B - Motor fuel alkylation catalyst and process for the use thereof - Google Patents
Motor fuel alkylation catalyst and process for the use thereofInfo
- Publication number
- CN1014401B CN1014401B CN86106451A CN86106451A CN1014401B CN 1014401 B CN1014401 B CN 1014401B CN 86106451 A CN86106451 A CN 86106451A CN 86106451 A CN86106451 A CN 86106451A CN 1014401 B CN1014401 B CN 1014401B
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- weight
- alkylation
- rolling mill
- ether
- catalyzer
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- 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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- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a six-roll skew rolling hot pipe rolling mill used for rolling seamless steel pipes with a large diameter and seamless steel pipes with an extra large diameter. The pipe rolling mill is invented according to the 'negative characteristic angle skew rolling theory', and the present invention has the key that the technological state of a 'traditional' Mannesmann skew rolling mill is changed. The host machine of the pipe rolling mill is a six-roll vertical type skew rolling pipe rolling mill, and the auxiliary machine of the pipe rolling mill is provided with a core rod positioning machine roll type centering machine and a wabbler mechanism with two telescopic top rods to control semi-floating core rods to roll pipes. A pipe rolling group can be constituted by using the pipe rolling mill of the present invention, so that the prospect of the industrial production of seamless steel pipes with a large diameter and seamless steel pipes with an extra large diameter is exploited.
Description
The present invention relates to a kind ofly make the alkylating new catalyst of isoalkane with olefin agent.Simultaneously, the invention still further relates to the method for utilizing this new catalyst, have the alkylate oil of the good capability of antidetonance with production.Therefore, the present invention is specially adapted to produce high-octane alkylate oil, to make the blending component of motor spirit.
Utilize this class alkene of propylene, butylene and amylene or other is as C
3-C
5The olefin agent of alkyl halide class, and use mineral acid to make such as Trimethylmethane and this class isoalkane alkylation of iso-pentane as hydrofluoric acid, be well-known important method with industrial-scale production gasoline boiling range hydrocarbon.In the alkylation operation process of isoalkane-alkene, the C that obtains usually
5-C
10Hydrocarbon be called " alkylate oil ".Alkylate oil mainly is used as the blending component oil plant of motor spirit.It has sufficiently high engine and research octane number (RON), and it can be used for improveing the total octane value from the gasoline of gasoline storage, so that the motor spirit that meets the requirement of Hyundai Motor engine to be provided.When hope was avoided using lead alkyl antiknock compound in gasoline, it was particularly important that the blending component of high-octane rating alkylate oil has enough high-octane motor spirit to preparation.The target of constantly pursuing on the technology is that a kind of cheapness, attractive acid catalyzed alkylation will be provided, and the alkylate oil product that this method obtains is compared with common alkylation, and higher engine and research octane number (RON) are arranged.This target adopts lead alkyl antiknock compound to have special meaning as gasoline blender for progressively eliminating by the government regulations requirement.
In using the technical scale isoalkane alkylation operation of acid catalyst, usually with Trimethylmethane as the isoalkane raw material, and with propylene, butylene and amylene or its mixture as olefin agent.Typical acid catalyst has hydrofluoric acid.In routine operation, at first allow isoalkane, olefin agent and hydrofluoric acid catalyst in alkylation reactor, contact and thorough mixing, to form reaction mixture or milk sap.Through the short time, alkylated reaction is just finished substantially, and reaction mixture is discharged from alkylation reactor, and in settling vessel by the gravity clarification, to form immiscible hydrocarbon phase and catalyzer mutually.Isolated hydrofluoric acid catalyst turns back to again in the alkylation reactor and uses once again.Isolated hydrocarbon phase will as fractionation, with the recovery alkylation products, and be isolated unspent isoalkane through further processing in the sedimentation operation, makes it turn back to recirculation in the alkylation reactor.The alkylation products that reclaims is sent in the motor spirit octane storage tank and is used as blending component.Therefore, wish that alkylation products has high as far as possible research octane number (RON).
So the objective of the invention is provides a kind of new catalyst for make the isoalkane alkylation with olefin agent.Another purpose is to use new catalyst in alkylation, the alkylate oil that has senior knock characteristic with production.
Therefore, in one embodiment of the invention, the present invention a kind ofly makes the alkylating catalyzer of isoalkane with olefin agent, and this catalyzer is to contain about 50-99%(weight) mineral acid and about 1-50%(weight) ether anhydrous, do not have a pure mixture.
In another embodiment, the present invention a kind ofly makes the alkylating method of isoalkane with olefin agent, it is included under the alkylation conditions of catalyzer existence, isoalkane is mixed mutually with olefin agent, and this catalyzer is a kind of about 50-99%(weight that contains) mineral acid and about 1-50%(weight) ether anhydrous, do not have a pure mixture.
To prior art and more detailed commentary of the present invention, above-mentioned purpose and embodiment will be expressly understood more by following.
Prior art has realized that the application of the acid catalyst of modification in make the alkylating method of isoalkane with alkene.For example, United States Patent (USP) 3,761 discloses for No. 540 with hydrofluoric acid catalyst and a spot of BF
3Can make isoalkane and alkene generation alkylation.It is said BF
3Improved alkylated reaction, made the generation of ethyl fluorochemical reduce to minimum.This reference substance shows, when the ratio of reaction zone isoalkane and alkene during less than about 4: 1, uses BF
3Improve the HF catalyzer and can obtain the high-octane rating alkylate oil, make the generation of alkyl fluoride reduce to minimum simultaneously.
United States Patent (USP) 3,531 discloses at the alkylation that organic compound in the presence of novel hydrofluoric acid-carbonic acid gas multicomponent catalyst is arranged for No. 546.This method is utilized hydrofluoric acid-carbonic acid gas multicomponent catalyst, can obtain having the motor spirit alkylate oil of higher research octane number (RON).Higher octane value is owing to improved in the alkylate oil due to the distribution of isomer.
United States Patent (USP) 3,778, No. 489 is particularly important.This part reference substance discloses a kind ofly has promotor to exist down, adopts to comprise that the various strong acid of hydrofluoric acid make alkene and alkane that alkylating method take place.Introduce in the 3rd section 61 row of this reference substance, promotor or contain a hydroxyl as alcohols, or contains the hydroxyl parent preferably, and as ethers, these ethers are cracked into alcohol under the acidic conditions of this invention.Make a declaration of the alcohol that best compound is a lower molecular weight, as ethanol, or the ether of lower molecular weight, as ether and water.This part reference substance shows, can promote ether to be cracked under the condition of alcohol, and ether compound can be used for the alkylation of alkane and alkene.Therefore, these ethers do not play catalyzer, and they are not inert, but can be cracked into all cpds, and exhaust in alkylated reaction.Different is, the present invention uses ether compound as real catalyzer, and the various conditions in the alkylation process can prevent and suppress ether and be cracked into alcohol.
In a word, prior art discloses the use of promotor, especially uses the parent of ether as pure promotor.Yet the unexposed so far mistake of prior art is by strong acid, and as the catalyst system of hydrofluoric acid and ether compound composition, ether maintains the original state and is not cracked into alcohol in this catalyst system.Exactly, ether is a kind of real catalyst component in the present invention, and it does not consume in fact in alkylation process.
In brief, the present invention relates to a kind ofly make the alkylating catalyzer of isoalkane with olefin agent, this catalyzer is a kind of about 50-99%(weight that contains) mineral acid and about 1-50%(weight) ether anhydrous, do not have a pure mixture.In addition, the invention still further relates to the alkylation of using this new catalyst.
As indicated, catalyzer of the present invention is to make in the isoalkane alkylation process applied with olefin agent.Spendable isoalkane is generally Trimethylmethane, iso-pentane and similar isoalkane among the present invention.Better be that particularly Trimethylmethane is better with Trimethylmethane and iso-pentane.If desired, also can use the mixture of two or more isoalkane.Common isobutane alkylation raw material all is applicable to process of the present invention.This common isobutane feedstock may contain some nullvalent hydrocarbon, as normal alkane.For example, general commercially available isobutane alkylation raw material contains the 95%(weight of having an appointment usually) Trimethylmethane, 4%(weight) normal butane and 1 weight %(weight) propane.
Be applicable to that olefin agent of the present invention comprises C
3-C
6Monoolefine, alkyl halide or its mixture.Be preferably C
3-C
6Alkene.Method of the present invention can be used for the alkylation process of two or more olefin agent mixtures, its benefit with improve obtain with the monoolefine agent time identical.For example, the many common alkene hydrocarbon feed that uses in the technical scale alkylation operation all is the mixture that contains propylene and butylene, or contains the mixture of propylene, butylene and amylene.Present method is used for the quality that such alkene mixture also can improve product, and this improvement is with suitable with the resulting improvement of monoolefine.Equally, the C of any ratio
3-C
5The mixture of alkyl halide and alkene also is suitable in many cases, for example, and when halogenide is fluorochemical.Chang Yong C especially
3-C
5Olefin feedstock normally obtains from the refining process of oil, and such as catalytic cracking, simultaneously raw material can contain quite a large amount of saturatess, lighter and heavier alkene or the like.The olefin feedstock that is obtained by the common source of this class can be used as olefin agent and is used for present method.
As indicated, catalyzer of the present invention is anhydrous, the mixture that do not have alcohol that contains mineral acid and ether.Should be appreciated that the connotation of anhydrous this speech is meant that the content of water in the acid should not surpass the 3%(weight of sour phase gross weight).The existence of water can greatly increase corrodibility, the especially hydrofluoric acid of mineral acid in the acid mutually, and causes ether to be cracked into alcohol.Attached example will more prove absolutely, pure component replaces the ether component among the present invention can cause the result of difference.After all characteristics of the present invention catalyzer just are not have alcohol.Do not have alcohol and mean that content pure in the acid mutually is not more than about 3%(weight of sour phase weight).
Operable in the present invention mineral acid comprises normally used any mineral acid in the alkylation process.This class acid comprises sulfuric acid; Halogenosulfuric acids, for example fluoro sulfuric acid; Or haloid acid, as hydrofluoric acid or the like.It is also noted that the purpose of mineral acid one speech comprises that also those make the solid peracid of isoalkane generation alkylated reaction applicable to catalysis with olefin agent, as acidic resins or zeolite.Preferably use hydrofluoric acid.
Select for use hydrofluoric acid to be because it is one of the most stable mineral acid.It can bear high temperature, high pressure and not decompose under the effect of other catalyzer.Its many organic compound or only with heating or in the presence of catalyzer, just can decompose and produce hydrofluoric acid again.This makes that the consumption of catalyzer reduces in the process.So using a main advantages of hydrofluoric acid is that its chemical stability and low freezing point can be used under the operational condition of broad.Can adopt on thermokinetics and the most satisfied economically condition, and not be subjected to the restriction of specificity of catalyst.For example, make the alkylated reaction of catalyzer, can under the condition of envrionment temperature or a little higher than envrionment temperature, carry out with hydrofluoric acid.So just removed resembling refrigeration requirement required when making alkylation catalyst from,, do not needed to utilize king-sized pressure that its maintenance is in a liquid state according to the vapour pressure characteristic of hydrofluoric acid with other mineral acid.Its freezing point characteristic can be used it under lower temperature, and when so low temperature, most of catalyzer can freeze, and perhaps become the high viscosity shape.When making Trimethylmethane generation alkylated reaction come the production aviation to use propellant combination with alkene, though common operational condition is about 30 ℃,, also have many catalyzed reactions more favourable when low temperature.Because these reactions of hydrofluoric acid energy catalysis, therefore, with regard to its physical properties, hydrofluoric acid is particularly advantageous.Moreover because the thermostability of hydrofluoric acid, so it can use under temperature much higher than with other alkylation catalyst the time.This is the unique characteristic of hydrofluoric acid.
As indicated, the content of mineral acid is about 70-95%(weight of acid catalyst weight in the catalyzer of the present invention), preferably be selected in 85-95%(weight) between.When adopting hydrofluoric acid especially like this.The content of hydrofluoric acid is the 90%(weight of sour phase weight in the optimal catalyzer).
Second feature of the present invention is the ether component.As indicated, prior art has recognized that and utilizes the additive of ether as alkylation process; But ether is the parent of alcohol in prior art.Therefore prior art is at such alkylation process, and promptly in this process, pure or pure parent has constituted modified catalyst.Completely contradict therewith, in catalyzer of the present invention, ether is a kind of real catalyst component, and ether does not consume in the reaction.
Any suitable ether all can be used as the ether component.For example the ether component can comprise lower molecular weight ether, as methyl ether, ether, propyl ether or the like.Yet, preferably select the ether that under alkylation reaction condition, is in a liquid state for use.Best ether component is a methyl tertiary butyl ether.Certainly, the ether component can be single ether, for example methyl tertiary butyl ether; Perhaps the ether component is the mixture of two or more ethers.
The alkylation conditions that adopts among the present invention is: temperature is about 0 °F to 200 °F (17.8 to 83.3 ℃); Pressure is enough to keep reagent and catalyzer is in a liquid state; Be about 0.1 minute to 30 minutes the duration of contact between hydrocarbon and the catalyzer.In the preferred embodiment that uses hydrofluoric acid and methyl tertiary butyl ether as catalyzer, preferably about 1: 1 to 5: 1 of the volume ratio of catalyzer and hydrocarbon, preferably about 50 to 150 of the temperature in alkylation reaction zone (10 ℃ to 65.6 ℃).
In a preferred embodiment, by the catalyzer of hydrofluoric acid containing and methyl tertiary butyl ether, the reaction mixture that reaction product constituted that forms in reagent and the alkylation reactor will pass through a reaction soaking pit.In the description of this embodiment, attempt alkylation reactor and reaction soaking pit (if you are using) all be can be regarded as " alkylation reaction zone ".The reaction soaking pit that is suitable for is well-known in prior art.For example, at United States Patent (USP) 3,560, No. 587 and 3,607, the reaction soaking pit of No. 970 descriptions is applicable to present method.These reaction soaking pits normally one be equipped with porous plate, the container of plate washer or plate like that is so that make alkylation reaction mixture be the state of complete uniformly mixture or milk sap within the predetermined time.The time that the alkylation reaction mixture of catalyzer and hydrocarbon stops in the reaction soaking pit is depended on the composition of reaction mixture.In general, the residence time in the reaction soaking pit is about 1 minute to 30 minutes.The temperature and pressure of reaction in the soaking pit is identical with temperature and pressure in the alkylation reactor that links to each other in fact.
From the effusive reaction mixture of alkylation reaction zone, handle through sedimentation, so that the hydrocarbon phase of separate and subside and acid catalyst are mutually, settled method formerly has in the alkylation techniques well-known.Usually, from the alkylation reaction mixture that alkylation reactor or soaking pit obtain, contain unreacted isoalkane, alkylation reaction product, acid catalyst and dissolve in the organism of catalyzer, may also have a spot of light hydrocarbon or the like.When alkylation reaction mixture leaves standstill, sedimentation promptly takes place, alkylation reaction product, isoalkane and light hydrocarbon form lighter sedimentation hydrocarbon phase.The acid catalyst of being made up of mineral acid and ether then forms segregation mutually.Settled hydrocarbon phase can be separated mutually with catalyzer with simple mechanical means.The temperature and pressure of sedimentation operating period maintenance is identical with employed alkylation conditions in the above-mentioned reaction zone in fact.Hydrocarbon and catalyzer preferably all are in liquid state in settlement separate operation.
The heat extraction of alkylation zone perhaps needs concerning the optimizing of process operation.Known have various heat discharging methods.For example, the heat that produces in the alkylated reaction can be got rid of from alkylation reactor by the indirect heat exchange between the reaction mixture in cold water and the reactor.
For the present invention being described than there being alkylation that higher benefit and advantage are arranged earlier, the spy lists following example.Certainly these examples just are used for ocular description, and anything but of the present invention other are implemented binding character widely, and this shows in the claims.
Example 1
This example is to carry out in the device of pilot-scale.The pilot-scale device comprises a Monel metal autoclave, and in autoclave, isoalkane contacts with acid catalyst with olefin agent.Behind time enough, hydrocarbon is sent into settling vessel with acid by autoclave, reaches to be separated in settling vessel.Autoclave is told and turned back to acid by settling vessel, and contact with other hydrocarbon.The hydrocarbon phase that contains alkylate oil is sent into neutralising arrangement from settling vessel.Then, collecting hydrocarbon phase is used for analyzing.
Two kinds of different operations have been carried out hereinto in the plant size device.Manipulate for first kind and contain 90%(weight) hydrofluoric acid and 10%(weight) acid catalyst of organic thinner.Organic thinner is that the carbon atoms scope is C
7To C
+ 23The oligomerisation iso-butylene, major part is C
8To C
12Hydrocarbon.Manipulate for second kind and contain 90%(weight) hydrofluoric acid and 10%(weight) catalyzer of methyl tert-butyl ether.In these two kinds of tests, the temperature in the autoclave is 20 ℃; Pressure is 130 pounds/inch
2(896 kPas) (gauge pressure); The residence time is 10 minutes; Stir speed (S.S.) is 1800 rev/mins.Acid is 1.5 with the volume ratio of hydrocarbon phase in the autoclave.Trimethylmethane and C
4The mole ratio of alkene is 7.9.C
4The 2-butylene that is assigned as of alkene accounts for 48.2%, 1-butylene account for 23.2% and iso-butylene account for 28.6%.
All analyze the alkylate oil product in every kind of operation, the composition of product and the analytical results of research octane number (RON) thereof are as follows:
Catalyzer
The organic attenuant HF/ of HF/ methyl tert-butyl ether
Alkylate oil is formed:
C
- 88.3%(weight) 6.4%(weight)
Trimethylpentane 72.6%(weight) 75.7%(weight)
Dimethylhexane 13.9%(weight) 12.0%(weight)
C
+ 85.2%(weight) 5.9%(weight)
Research octane number (RON) 95.5 96.4
Be not difficult to find out, use when containing the acid catalyst of ether that the gained research octane number (RON) is high by 0.9 when using the acid catalyst of being made up of hydrofluoric acid and organic thinner.The higher octane value that reaches with the inventive method is owing to formed in alkylate oil than the more trimethylpentane of dimethylhexane content fully.The minimizing of the increase of trimethylpentane content and dimethylhexane content is that ether compound exists the result who is caused in the alkylate oil.
The example II
Two kinds of other alkylation experiments have been carried out in this example, to measure the stability of ether component in the acid catalyst.These two kinds of alkylation operation are carried out in the described pilot-scale device of above-mentioned routine I.Employed condition is identical with the employed condition of test of carrying out in the routine I basically in these two kinds of alkylation experiments.First kind of experiment carried out 24 hours in this example, only about 5 hours of its hydrocarbon charging.Second kind of experiment carried out 16 days, and its hydrocarbon charging only is 54 hours.Yet acid catalyst but kept respectively in device 24 hours and 16 days.Each EO all carries out sour facies analysis.Analytical results sees the following form.
Test period: 1 day 16 days
The acid facies analysis:
HF 90.3%(weight) 90.2%(weight)
Methyl tert-butyl ether 9.0%(weight) 8.2%(weight)
Methyl alcohol 0.1%(weight) 0.7%(weight)
H
2O 0.5%(weight) 0.6%(weight)
Other 0.1%(weight) 0.3%(weight)
From above-mentioned data as can be seen, have only a spot of methyl tert-butyl ether to resolve into methyl alcohol.Can think and be situated between from the amount of the methyl tert-butyl ether that becomes methyl alcohol just because of due to the existence of the water of impurity.As not considering this point, can see that most methyl tert-butyl ethers still do not get transformed into methyl alcohol.
The example III
In this example, in replica plant's device, carried out another kind of alkylation operation.The condition of using in this operation is identical with condition in above-mentioned two examples basically.Yet in this operation, acid catalyst contains 90%(weight) hydrofluoric acid and 10%(weight) methyl alcohol.
Test-results sees the following form.Except the test-results of this example, also list the result who makes the example I of catalyzer with hydrofluoric acid and methyl tert-butyl ether in the table.
Catalyzer HF/ methyl alcohol HF/ methyl tert-butyl ether
Alkylate oil is formed:
C
- 89.8%(weight) 6.4%(weight)
Trimethylpentane 72.9%(weight) 75.7%(weight)
Dimethylhexane 11.7%(weight) 12.0%(weight)
C
+ 85.6%(weight) 5.9%(weight)
Research octane number (RON) 96.0 96.4
Relatively the data that go up in the table are not difficult to find out, the result who uses the acid catalyst that contains ether is better than the result that application contains pure acid catalyst.The result who contains the acid catalyst of methyl alcohol with application compares, and the application of ether component can make research octane number (RON) increase 0.4.Increasing of octane value is attributable to have produced more trimethylpentane (75.7%(weight) than 72.9%(weight)) and the dimethylhexane concomitant product reduced.
Can see in a word, use the alkylate oil that the alkylation catalyst that contains ether can obtain higher octane, and the distribution of isomer be even more ideal.
Claims (2)
1, a kind of usefulness has olefin agent to make the alkylating catalyzer of isoalkane, and it is characterized by it is anhydrous, the no alcohol mixture that contains 85-95% (weight) hydrofluoric acid and 5-15% (weight) methyl tertiary butyl ether.
2, according to the catalyzer of claim 1, it is characterized by it is a kind of homogeneous catalyst.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN86106451A CN1014401B (en) | 1985-08-12 | 1986-09-22 | Motor fuel alkylation catalyst and process for the use thereof |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US06/764,707 US4636488A (en) | 1985-08-12 | 1985-08-12 | Novel motor fuel alkylation catalyst and process for the use thereof |
| CN86106451A CN1014401B (en) | 1985-08-12 | 1986-09-22 | Motor fuel alkylation catalyst and process for the use thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN86106451A CN86106451A (en) | 1988-04-06 |
| CN1014401B true CN1014401B (en) | 1991-10-23 |
Family
ID=25742246
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN86106451A Expired CN1014401B (en) | 1985-08-12 | 1986-09-22 | Motor fuel alkylation catalyst and process for the use thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1014401B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2022089108A1 (en) | 2020-10-30 | 2022-05-05 | 上海洛启生物医药技术有限公司 | Anti-il5 nanoantibody and use thereof |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107653003B (en) * | 2016-07-25 | 2020-05-19 | 中国石油化工股份有限公司 | Method for preparing alkylate |
-
1986
- 1986-09-22 CN CN86106451A patent/CN1014401B/en not_active Expired
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2022089108A1 (en) | 2020-10-30 | 2022-05-05 | 上海洛启生物医药技术有限公司 | Anti-il5 nanoantibody and use thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN86106451A (en) | 1988-04-06 |
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