CN1180061C - Selective hydrogenation process for eliminating C10-C10 straight chain diolefine - Google Patents
Selective hydrogenation process for eliminating C10-C10 straight chain diolefine Download PDFInfo
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- CN1180061C CN1180061C CNB011165847A CN01116584A CN1180061C CN 1180061 C CN1180061 C CN 1180061C CN B011165847 A CNB011165847 A CN B011165847A CN 01116584 A CN01116584 A CN 01116584A CN 1180061 C CN1180061 C CN 1180061C
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- diolefine
- hydrogen
- hydrogenation
- carrier
- hydrotreating
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Abstract
The present invention provides an improved method of a selective hydrogenation process for eliminating C10-C10 straight chain diolefine in monoolefin products produced by C10-C16 long chain olefin dehydrogenation, which comprises the following steps: making the mixed material flows of alkane olefin containing C10-C16 monoolefin and C10-C16 straight chain diolefine in a plurality of hydrogenation reactors connected in series to come into contact with a specific hydrogenation catalyst under a hydrogenation reaction condition; respectively injecting hydrogen gas into each hydrogenation reactor. The hydrogenation catalyst uses gamma-aluminum oxide of which the specific surface area is from 50 to 300m<2>/g and the pore volume is from 0.2 to 2.0cm<3>/g as a carrier. Palladium loaded on the carrier is used as a main catalyst element, and an element selected from silver, gold, tin, plumbum or potassium loaded on the carrier is used as a cocatalyst element. The diolefine in the mixed material flows of alkane olefin is converted into the monoolefin in a hydrogenation way.
Description
Technical field
The present invention relates to a kind of C of being used for
10-C
16Long chain alkane C in dehydrogenation manufacture order olefin product
10-C
16The selection method of hydrotreating of straight chain diolefine relates more specifically to adopt a kind of specific catalyst and adopts multistage hydrogenation mode to combine, to realize improving C simultaneously under relatively mild condition
10-C
16The transformation efficiency of straight chain diolefin hydrogenate and method optionally.
Background technology
C in the technology of the raw material-linear alkylbenzene of dehydriding production washing composition
10-C
16Long chain alkane in the monoolefine material of dehydrogenation unit production, contain the diolefine of 1-3 weight %, existing in the follow-up alkylation process of these diolefine can cause a large amount of side reactions, reduced the productive rate and the quality of alkylbenzene.Utilize the diolefin hydrogenate method with the diolefin hydrogenate in the dehydrogenation product, generate monoolefine, can on the basis of improving the alkylbenzene productive rate, improve the quality of alkylbenzene effectively.
United States Patent (USP): 4695560,4523048,4520214,4761509 and Chinese patent CN1032157 disclose and be used for C
8-C
20Diolefin hydrogenate method in the dehydrating alkanes product.Catalyzer that this method is used be characterized as nickeliferous 1.0-25 weight %, sulfur-bearing 0.05-1.5 weight %, carrier are the Al with the drop method preparation
2O
3Bead, the pore volume of this carrier are 1.44-3.0cm
3/ g, specific surface area＞150m
2/ g does not contain precious metal and not halogen-containing substantially, alkaline-earth metal and basic metal (＜0.1 weight %).Because for sponsoring element, for reaching the certain reaction activity, selective hydrogenation reaction will carry out under greater than 200 ℃ condition the employed catalyzer of this method with nickel, have the part cracking side-reaction and produce, increased the consumption of material.This method adopts the single hop reaction simultaneously, and the disposable injection of hydrogen that selective hydrogenation reaction is required in order to make hydrogen fully dissolving in alkane olefin liquid, must maintain reaction pressure more than the 1.1MPa.In addition,, need often catalyzer to be vulcanized, suppress the reactive behavior of catalyzer in order to improve the selectivity that diolefine changes into the monoolefine reaction.And annotate sulphur technological operation complexity, and be difficult to control notes sulfur content in operating process, if it is too high to annotate sulfur content, then the reactive behavior of catalyzer is very low, if annotate the sulfur content deficiency, then selectivity of catalyst is very poor.In addition, this notes sulphur system has also increased the investment of equipment.
Chinese patent CN1236333A has reported and has a kind ofly contained palladium and be selected from the selection hydrogenization catalyst preparation method of at least a element in tin, the lead and the scope of use thereof.The catalyzer of this patent report is with specific surface area 5-200m
2/ g, pore volume 0.3-0.95cm
3The aluminum oxide of/g is a carrier, adopts the method for surface impregnation, and the active element palladium with at least 80% is distributed in around the particle and among the particle volume between the depth 500um.The selected promoter elements that is used to improve reaction preference is tin and lead, and this catalyzer is applicable to the selection hydrogenation of lower carbon number hydrocarbons such as divinyl.Because the specific surface area and the pore volume of this catalyzer used carrier are all smaller, are unsuitable for C
10-C
16The selection hydrogenation of long-chain diolefine.
United States Patent (USP) 4704492 has been reported a kind of multistage selection hydrogenation technique of removing ethynyl impurity from natural divinyl gas, the characteristics of this technology are that the method for utilizing segmentation to inject hydrogen reduces the mol ratio of hydrogen and required hydrogenation material, thereby improve the selectivity of hydrogenation reaction effectively.
Summary of the invention
The objective of the invention is to remove effectively C
10-C
16Produced simultaneously by product diolefine in the dehydrogenation of long-chain alkane manufacture order olefin hydrocarbon, and use the required High Temperature High Pressure of nickel-containing catalyst in the selection method of hydrotreating of avoiding prior art generally to use, need regularly to shortcomings such as hydrogenation catalyst vulcanize.
In order to adapt to C
10-C
16The needs of long-chain diolefine reaction are by adopting specific surface area 50-300m
2/ g, pore volume 0.2-2.0cm
3The gama-alumina of/g is a carrier, makes long linear alkene middle energy rapid diffusion in the hole of catalyzer, makes this hydrogenation catalyst can be used for C
10-C
16The selection hydrogenation of diolefine; Because the activity of palladium-containing catalyst can reduce temperature of reaction and reaction pressure significantly far above nickeliferous catalyzer; Owing to adopt the multistage method of hydrotreating, by the hydrogen/diolefine mol ratio in each reactor of control adding, increase selectivity and transformation efficiency that diolefine is converted into monoolefine, avoided monoolefin hydrogenation is converted into alkane and the product yield that causes descends, thereby improved the yield of monoolefine.Because the present invention need not to use notes sulphur method to improve the selectivity that diene hydrogenation is converted into monoolefine, thereby has also avoided nickel-containing catalyst need annotate the caused complicated operation of sulphur, fluctuation of service, the high shortcoming of investment.By with above-mentioned several method applied in any combination in C
10-C
16The long-chain diolefin hydrogenate has improved C
10-C
16The long-chain diene hydrogenation is converted into the selectivity and the yield of monoolefine.
Fig. 1 is the synoptic diagram of multistage hydrogenation technique flow process of the present invention.Wherein R is a reactor, and H is the hydrogen inlet, and C is for containing C
10-C
16Monoolefine and C
10-C
16The alkane alkene mixture of long-chain diolefine flows to mouth.
The invention provides and be used to remove C
10-C
16C in the product of dehydrogenation of long-chain alkane manufacture order alkene
10-C
16Improving one's methods of the selection hydrogenation of straight chain diolefine is included in a plurality of placed in-line hydrogenators, makes this contain C
10-C
16Monoolefine and C
10-C
16The alkane olefin logistics of straight chain diolefine contacts with a kind of specific hydrogenation catalyst under hydrogenation conditions, and the inlet of each reactor all has the hydrogen inlet, and hydrogen is injected each reactor respectively, and described hydrogenation catalyst is with specific surface area 50-300m
2/ g, pore volume 0.2-2.0cm
3The gama-alumina of/g is a carrier, is the Primary Catalysts element with the palladium of institute's load on this carrier, is promoter elements be selected from silver, gold, tin, lead or the potassium of institute's load on this carrier, and the diene hydrogenation in this alkane olefin logistics is converted into monoolefine.
To intend the method moulding that thin water aluminum oxide powder adopts spin, through 100-200 ℃ of dry 1-10 hour, at 300-800 ℃ of following roasting 1-10 hour, it was 50-300m that specific surface area is provided
2/ g, preferred 100-200m
2/ g, pore volume are 0.2-2.0cm
3/ g, preferred 0.5-1.5cm
3The gamma-aluminium oxide carrier of/g.Adopt dipping method, supported palladium is the Primary Catalysts element on this carrier, and it is promoter elements that load is selected from silver, gold, tin, lead or potassium.With impregnated sample 100-200 ℃ dry 2-8 hour down, dried sample in air 300-600 ℃ following roasting 2-8 hour.Sample hydrogen reducing after the roasting, reductive temperature are room temperature to 300 ℃, and particularly 60-150 ℃, the time is 0.5-10 hour, particularly 1-5 hour, obtains hydrogenation catalyst of the present invention.
The flow process of multistage hydrogenation technique of the present invention as shown in Figure 1, alkane olefin liquid flows through placed in-line R successively
1, R
2... R
nReactor has hydrogen inlet H respectively in the ingress of each stage reactor
1, H
2... H
n, the amounts of hydrogen of controlling each inlet can be regulated the H of each conversion zone
2/ diolefine molar ratio, wherein the amounts of hydrogen injected of each reactor inlet is the 10-50%, particularly 20-30% that hydrogen/diolefine mol ratio that each reactor is injected accounts for the total mol ratio of this selective hydrogenation reaction hydrogen/diolefine respectively.Thereby guaranteeing that fully diolefine changes on the basis of monoolefine, suppressing the conversion of monoolefine to alkane.
C of the present invention
10-C
16The condition of long-chain diolefin hydrogenate is: temperature of reaction is 30-250 ℃, and particularly 50-200 ℃, reaction pressure is 0.1-2.0MPa, particularly 0.5-1.0MPa, and the liquid hourly space velocity of reaction is 1-20hr
-1, 5-10hr particularly
-1, total mol ratio of hydrogen and diolefine is 0.1-5.0, particularly 0.5-2.0.
By with above-mentioned several method applied in any combination in containing C
10-C
16Long-chain monoolefine and C
10-C
16The selection hydrogenation of the alkane olefin logistics of long-chain diolefine carries out this hydrogenation reaction under the condition of gentleness, and avoids using and annotate sulphur technology, has improved C
10-C
16The long-chain diene hydrogenation is converted into the selectivity and the transformation efficiency of monoolefine, has removed contained C in this hydrocarbon alkane olefin logistics effectively
10-C
16The long-chain diolefine is improving C
10-C
16Increased C in the time of the quality product of long-chain monoolefine
10-C
16The productive rate of long-chain monoolefine.
The following examples are used for the present invention is specifically described, and scope of the present invention is not limited.
Embodiment
Embodiment 1
With of the method moulding of pseudo-boehmite powder with spin, make the bead of φ 1.8-2.2mm, drying is 5 hours under 120 ℃, 600 ℃ of following roastings 5 hours, obtains specific surface area 220m
2/ g, pore volume 1.5cm
3γ-Al of/g
2O
3Bead.
Embodiment 2
The preparation of carrier is with embodiment 1.This carrier is used the PdCl of 0.85N earlier
2Solution impregnation was dried 5 hours down at 120 ℃, 550 ℃ of following roastings 6 hours.Carrier after the roasting is after dechlorination is handled, with the AgNO of 0.5N
3Solution impregnation was dried 5 hours down at 120 ℃, 550 ℃ of following roastings 8 hours.With purity greater than 99% hydrogen at 120 ℃ of following reductase 12s hour, make catalyzer.Contain palladium 0.3 weight % in the finished catalyst, silver-colored 1 weight %.
Embodiment 3
Preparation of catalysts is with embodiment 2.With prepared 100 liter catalyzer, in the reactor of packing into, control reaction temperature is 130 ℃, and pressure is 0.8MPa, LSHV=5.0hr
-1, H
2/ diolefine (mol ratio)=1.Contain C
10～C
14The material of long-chain diolefine 2.5 weight % after selecting hydrogenation, diolefine transformation efficiency 65.5%, the selectivity that generates monoolefine is 32.6%.
Embodiment 4
Preparation of catalysts is with embodiment 2.With prepared 100 liter catalyzer, average mark is loaded in 4 reactors, and 4 reactors in series are used, and control reaction temperature is 130 ℃, and pressure is 0.8MPa, LSHV=5.0hr
-1, H
2/ diolefine (mol ratio)=1.It is 1/4 of total amount that every stage reactor injects amounts of hydrogen.Contain C
10～C
14The material of long-chain diolefine 2.5 weight % after selecting hydrogenation, diolefine transformation efficiency 88.0%, the selectivity that generates monoolefine is 60.2%.
Hydrogenation conditions from embodiment 3 and 4 as can be seen, owing to adopted a kind of specific hydrogenation catalyst of the present invention, hydrogenation reaction of the present invention can be carried out under the temperature and pressure of gentleness, owing to adopt the multistage hydrogenation technique, hydrogen/diolefine the mol ratio of every stage reactor is injected in control, and the transformation efficiency and the selectivity that make diolefine be converted into monoolefine are significantly improved.
Claims (9)
1. one kind is used to remove C
10-C
16Long chain alkane is C in the product of dehydrogenation manufacture order alkene
10-C
16The selection method of hydrotreating of straight chain diolefine is characterized in that making this contain C in a plurality of placed in-line hydrogenators
10-C
16Monoolefine and C
10-C
16The alkane olefin logistics of straight chain diolefine contacts with a kind of specific hydrogenation catalyst under hydrogenation conditions, and the inlet of each reactor all has the hydrogen inlet, and hydrogen is injected each reactor respectively, and described hydrogenation catalyst is with specific surface area 50-300m
2/ g, pore volume 0.2-2.0cm
3The gama-alumina of/g is a carrier, palladium with institute's load on this carrier is the Primary Catalysts element, be selected from silver, gold, tin, lead or potassium with institute's load on this carrier are promoter elements, hydrogenation conditions wherein is: temperature of reaction is 50-200 ℃, reaction pressure is 0.5-1.0MPa, and the liquid hourly space velocity of reaction is 5-10hr
-1, total mol ratio of hydrogen and diolefine is 0.5-2.0.
2. the selection method of hydrotreating of claim 1, wherein the amounts of hydrogen injected of each reactor inlet is the 10-50% that hydrogen/diolefine mol ratio that each reactor is injected accounts for the total mol ratio of this selective hydrogenation reaction hydrogen/diolefine respectively.
3. the selection method of hydrotreating of claim 2, wherein the amounts of hydrogen injected of each reactor inlet is the 20-30% that hydrogen/diolefine mol ratio that each reactor is injected accounts for the total mol ratio of this selective hydrogenation reaction hydrogen/diolefine respectively.
4. the selection method of hydrotreating of claim 1, catalyst carrier for hydrgenating wherein are to adopt following method preparation: to intend thin water aluminum oxide powder is raw material, uses the rolling ball method moulding; Descended dry 1-10 hour at 100-200 ℃; At 300-800 ℃ of following roasting 1-10 hour.
5. the selection method of hydrotreating of claim 1, wherein the specific surface area as the gamma-aluminium oxide carrier of catalyst carrier for hydrgenating is 100-200m
2/ g, pore volume are 0.5-1.5cm
3/ g.
6. each selection method of hydrotreating among the claim 1-5, hydrogenation catalyst wherein is to adopt following method preparation: with pickling process Primary Catalysts element palladium is loaded on the gamma-aluminium oxide carrier, the promoter elements that will be selected from silver, gold, tin, lead or potassium with pickling process loads on the gamma-aluminium oxide carrier; Descended dry 2-8 hour at 100-200 ℃; At 300-600 ℃ of following roasting 2-8 hour; In room temperature-300 ℃ following hydrogen reducing 0.5-10 hour of using.
7. the selection method of hydrotreating of claim 6, hydrogen reducing temperature wherein is 60-150 ℃, the recovery time is 1-5 hour.
8. each selection method of hydrotreating among the claim 1-5 wherein contains C
10-C
16Straight chain mono-olefins and C
10-C
16The alkane olefin logistics of diolefine is from C
10-C
16Long chain alkane produce C through dehydriding
10-C
16Produce in the technology of straight chain mono-olefins.
9. the selection method of hydrotreating of claim 8, wherein C in the logistics of alkane olefin
10-C
16The content of diolefine is 1-3 weight %.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011165847A CN1180061C (en) | 2000-04-19 | 2001-04-13 | Selective hydrogenation process for eliminating C10-C10 straight chain diolefine |
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 00112211 CN1268549A (en) | 2000-04-19 | 2000-04-19 | Preparation method of selective hydrogenation catalyst for C10-C16 straight chain diolefine |
| CN00112211.8 | 2000-04-19 | ||
| CN 00112212 CN1269394A (en) | 2000-04-19 | 2000-04-19 | Selective hydrogenation process for C10-C16 straight-chain diene |
| CN00112212.6 | 2000-06-09 | ||
| CNB011165847A CN1180061C (en) | 2000-04-19 | 2001-04-13 | Selective hydrogenation process for eliminating C10-C10 straight chain diolefine |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1318621A CN1318621A (en) | 2001-10-24 |
| CN1180061C true CN1180061C (en) | 2004-12-15 |
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|---|---|---|---|
| CNB011165847A Expired - Fee Related CN1180061C (en) | 2000-04-19 | 2001-04-13 | Selective hydrogenation process for eliminating C10-C10 straight chain diolefine |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101612569B (en) * | 2009-07-24 | 2011-07-20 | 中国石油化工集团公司 | Deoxidation catalyst for oil product, preparation method thereof and catalytic hydrogenation method for removing dissolved oxygen in oil product by adopting catalyst |
| CN109126779B (en) * | 2018-08-03 | 2020-11-20 | 北京化工大学 | Controllable preparation method for small-molecule multi-carbon straight-chain olefin alkylation and isomerization |
| CN112898111B (en) * | 2019-12-03 | 2022-04-01 | 中国石化集团金陵石油化工有限责任公司 | Method for preparing mono-olefin by hydrogenating diolefin |
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