CN102942958A - Long chain paraffin hydrogenation heterogeneous condensation freezing point depressing method and catalyst thereof - Google Patents
Long chain paraffin hydrogenation heterogeneous condensation freezing point depressing method and catalyst thereof Download PDFInfo
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Abstract
The invention relates to a long chain paraffin hydrogenation heterogeneous condensation freezing point depressing method and a catalyst thereof and belongs to the technical field of energy. A single-section or two-section serial connection hydrogenation heterogeneous process is adopted; raw oil and hydrogen pass through a hydrogenation heterogeneous catalyst bed layer, wherein the raw oil comprises vegetable oil, Fischer-Tropsch wax oil or waste lubricating oil which are hydrogenated; and an obtained hydrogenation heterogeneous product has the characteristics of low freezing point, high cetane number and the like. An adopted hydrogenation heterogeneous condensation freezing point depressing catalyst is a molecular sieve catalyst, and comprises a molecular sieve carrier and a metal active component. The total weight of a molecular sieve is 20 weight percent to 90 weight percent of the weight of the molecular sieve carrier, and the weight of the metal active component is 0.05 weight percent to 0.5 weight percent of the total weight of the total catalyst. The process is simple, the operation is stable, the freezing point of the raw oil can be effectively reduced to 10DEG C below zero to 20DEG C below zero by selecting appropriate hydrogenation heterogeneous conditions, so that the fluidity of an oil product at low temperature is ensured, and wide industrial application prospect is realized.
Description
Technical field
The invention belongs to energy technology field, relate to a kind of method of long chain alkane hydroisomerizing pour point depression.More detail is and adopt molecular sieve catalyst under suitable processing condition, vegetables oil or the long chain alkane in the coal tar through hydrotreatment to be carried out the hydroisomerizing processing, reduce the condensation point of oil product, can in low temperature environment, be more widely used.
Background technology
The alkane hydroisomerization is one of important reaction of petroleum refining process, is mainly used in to produce high-grade fuel oil and top-grade lubricating oil.Wherein, the hydroisomerization of light paraffins can be produced high-octane gasoline blending component, and the long chain alkane hydroisomerization is mainly used in improving the low temperature flowability of intermediate oil (rocket engine fuel and diesel oil) and lubricating oil.
Catalyzer plays central role in the reaction of alkane hydroisomerizing, hydroisomerization catalyst is dual-function catalyst, has metal active constituent and acid carrier.Metal active constituent provides hydrogenation-dehydrogenation, and acid carrier provides effective specific surface area, suitable pore passage structure and acid sites.Metal active constituent commonly used mainly is family's Pt metal, Pd etc., and carrier adopts the solid acid of differing molecular sieve or similar molecular sieve usually.Molecular sieve also has good thermostability simultaneously owing to have the pore passage structure of larger specific surface area, pore volume and rule, therefore is widely used in experimental study and actual production.Si-Al molecular sieve commonly used has Y, Beta, MOR, ZSM-5, ZSM-22, ZSM-23, ZSM-48 etc., and phosphate aluminium molecular sieve such as SAPO-11, SAPO-31, SAPO-41 etc. also have and relate to.Wherein, use wider through Hydrogen Y, Beta, the MOR type molecular sieve of ion-exchange.Chinese patent CN1091150A has proposed a kind of with ZSM-5 and Beta molecular sieve mechanically mixing, and then extruded moulding is applied in the hydroisomerizing reaction of 300-510 ℃ of distillate as support of the catalyst.CN1952074A after with modification ZSM-5 and the ZSM-22 molecular sieve be applied to diesel oil the hydroisomerizing pour point depression in, when reducing condensation point of diesel oil, also guaranteed the yield of diesel fuel oil.CN101596462A has introduced the two microporous molecular sieve catalysts of a kind of employing loading type Y/Beta C6-C9 small molecules alkane has been carried out hygrogenating isomerization reaction, has improved the octane value of oil product.
Yet in these disclosed hydroisomerization catalysts, employed molecular sieve major part all is to have macroporous structure.When the isoparaffin molecule of a large amount of multiple-limbs exists, these large pore molecular sieve selectivity of catalyst are not enough to preferentially transform the alkane of straight chain or low branch, the molecular sieve of small structure then can optionally transform the alkane of straight-chain paraffin and low branch, reaches the effect that reduces the oil product condensation point.The ZSM-48 molecular sieve is the new-type high silicon aluminum ratio molecular sieve that U.S. Mobil company developed at the initial stage eighties, has rhombic system or the false rhombic system symmetry of ten-ring linear passageway, has less aperture than the molecular sieve that adopts before.Studies show that out that in a large number the catalyzer take the ZSM-48 molecular sieve as main component demonstrates good catalytic effect in the dewaxing pour point depression of heavy oil.Chinese patent CN101330976A has reported a kind of preparation of high activity ZSM-48 molecular sieve and demonstrated good activity in the hydroisomerizing catalytically active assessment take positive structure C10 as model compound, isomery C10 alkane has been had than highly selective.CN1703273A is by relatively ZSM-22, ZSM-23, ZSM-35, ZSM-48, several molecular sieve catalysts of ZSM-57, SSZ-32 find that to after the fischer-tropsch wax oil isomerization dewaxing performance ZSM-48 is better than other several molecular sieves.CN102245294A with ZSM-48 with can keep isoparaffin optionally improve transformation efficiency under the prerequisite after ZSM-23 mixes.Same CN1703490A and CN1703491A are applied to fischer-tropsch wax dewaxing pour point depression production lubricating oil with Beta and ZSM-48 molecular sieve catalyst formation tandem process, and its reaction result is better than only using the single hop technique of ZSM-48 molecular sieve catalyst.All in all, adopt ZSM-48 and other molecular sieves (for example Beta) to unite use and can obtain better hydroisomerizing performance, but present research also just is applied to the molecular sieve catalyst take ZSM-48 as main body the production of lubricating oil.And through containing a large amount of long chain alkanes in the vegetables oil of hydrotreatment, can add in the petrol and diesel oil as blend component, because long chain alkane wherein mainly is straight-chain paraffin, its condensation point is low not, has greatly limited the use at cold district.Chinese patent 201110425819.9 has been introduced the hydrotreatment of vegetables oil, although also related in the patent isomerization-visbreaking of petrol and diesel oil component behind the hydrogenation is processed, and its effect is not too obvious.And the petrol and diesel oil component oil product that obtains after adopting molecular sieve catalyst take ZSM-48 as main body to the vegetables oil hydrotreatment carries out isomerization-visbreaking report is not yet arranged.
Summary of the invention
The method and the catalyzer thereof that the purpose of this invention is to provide a kind of long chain alkane hydroisomerizing pour point depression, be further characterized in that stock oil can also be, high-quality to produce, the diesel oil of low condensation point is target, realized the hydroisomerizing processing to vegetables oil, fischer-tropsch wax oil or the lubricating oil of process hydrotreatment, whole technological process is simple to operation, the production process environmental protection and energy saving.By the hydroisomerizing of oil product is processed, decrease the condensation point of petrol and diesel oil distillate, improved the quality of oil product, widened its use range, can in the low temp operation environment, guarantee the flowability of oil product.
Specifically technical scheme of the present invention comprises the steps:
Adopt single hop or two sections serial hydrogenation isomerization processes flow processs, under the hydroisomerizing condition, the control reaction pressure is 1-12MPa, and temperature of reaction is 200-380 ℃, and volume space velocity is 0.2-4h
-1, hydrogen to oil volume ratio is 200-1200, stock oil and hydrogen are by the hydroisomerization catalyst bed.Stock oil can be the vegetables oil through hydrotreatment, and wherein vegetables oil comprises various plam oils, curcas oil, Viscotrol C, soybean oil, rape seed oil, algae oil, sweet oil, peanut oil, cereal oil.Stock oil can also be the waste lubricating oil of fischer-tropsch wax oil or process hydrotreatment.
Hydroisomerization catalyst comprises molecular sieve carrier and metal active constituent, metal in the metal active constituent is one or more among Pt, Pd, Ni, the Ru, the weight of metal active constituent is total catalyst weight 0.05wt%-0.5wt% in the hydroisomerization catalyst, and the hydroisomerizing product that obtains has low condensation point, characteristics that cetane value is high.The molecular sieve that adopts in the molecular sieve carrier is one or more among ZSM-48, ZSM-23, ZSM-22, Beta and the Y, wherein contains at least the ZSM-48 molecular sieve, and the silica alumina ratio of described molecular sieve is 20-180.The gross weight of molecular sieve is the 20wt%-90wt% of molecular sieve supported body weight in the molecular sieve carrier.
Production technique can be selected according to production requirement the technical process of single hop or two sections series connection.Simultaneously, the recycle of hydrogen has reduced production cost.The characteristics such as the ZSM-48 molecular sieve that adopts in the inventive method has that crystal grain is little, even particle size distribution, acidity are suitable.For the molecular sieve of large crystal grain, the molecular sieve that crystal grain is little has reduced the impact of reactant mass transfer effectively in hydroisomerizing, reduces secondary reaction and cracking reaction, is conducive to improve the selectivity of product yield and isomerized products.Suitable acidity distribution also provides certain condition for reducing cracking reaction.The method flexible operation of long chain alkane hydroisomerizing provided by the invention goes for the hydroisomerizing of one or more raw materials, adapts to fully the variation of market raw material supply and demand.
Description of drawings
Accompanying drawing is a kind of production technological process of long chain alkane hydroisomerizing pour point depression.
Implementation
Be described in detail specific embodiments of the invention below in conjunction with technical scheme and accompanying drawing
Embodiment 1
Prepare different Pt/ZSM-48 catalyzer.Be that three kinds of ZSM-48 molecular sieves of 33,96,165 and the aqueous ammonium nitrate solution of 1mol/L carry out ion-exchange with silica alumina ratio, triplicate, keeping the volume of aqueous ammonium nitrate solution and the mass ratio of molecular sieve is 20:1, after having exchanged under 550 ℃ air atmosphere condition roasting become Hydrogen ZSM-48 molecular sieve, guarantee that the weight content of sodium ion in the molecular sieve is less than 0.5%.Adopt equi-volume impregnating to prepare supported Pt catalysts, the Pt metal precursor of employing is Platinic chloride, and the weight of Pt metal accounts for 0.4% of total catalyst weight, makes three kinds of different Pt/ZSM-48 through super-dry, roasting and reduction after having flooded.
Embodiment 2
Preparation Pt/Beta, Pt/ZSM-23, Pt/ZSM-22, Pt/Y catalyzer.The silica alumina ratio of the Beta that selects, ZSM-23, ZSM-22, Y zeolite is respectively 32,46,87,12.Prepare supported Pt catalysts according to embodiment 1 described experimental procedure, the Pt metal precursor of employing is potassium platinichloride, and the weight of Pt metal accounts for 0.4% of total catalyst weight.
Embodiment 3
The preparation of Pt-Pd/ZSM-48 and Pt-Ru/ZSM-48 bimetallic catalyst.Be that two kinds of ZSM-48 molecular sieves of 120 and the aqueous ammonium nitrate solution of 1.0mol/L carry out ion-exchange with silica alumina ratio, triplicate, keeping the volume of aqueous ammonium nitrate solution and the mass ratio of molecular sieve is 20:1, after having exchanged under 550 ℃ air atmosphere condition roasting become Hydrogen ZSM-48 molecular sieve, guarantee that the weight content of sodium ion in the molecular sieve is less than 0.5%.Adopt equi-volume impregnating to prepare load type bimetal catalyst, the impregnating metal Pd of elder generation or Ru, the metal Pd precursor that adopts is that Palladous nitrate, metal Ru precursor are ruthenium trichloride, the weight of metal Pd or Ru accounts for 0.2% of total catalyst weight, carry out drying and roasting after having flooded, and then impregnating metal Pt, the Pt metal precursor of employing is Platinic chloride, the weight of Pt metal accounts for 0.3% of total catalyst weight.Make two kinds of different bimetallic catalysts through super-dry, roasting and reduction after having flooded.
Embodiment 4
Be that 85 ZSM-48 molecular sieve and silica alumina ratio are that 23 Beta molecular sieve fully mixes with silica alumina ratio, keeping the weight ratio of ZSM-48 molecular sieve and Beta molecular sieve is 7:3, remember that mixed molecular sieve is the ZB molecular sieve, adopt the method for preparing catalyst among the embodiment 1 to prepare load type metal Pt catalyzer, the Pt metal precursor of selecting is platinum nitrate, the weight of Pt metal accounts for 0.4% of total catalyst weight, obtains at last the Pt/ZB molecular sieve.
Embodiment 5
It is 135 ZSM-48 molecular sieve with silica alumina ratio, silica alumina ratio is that 50 Beta molecular sieve and silica alumina ratio are that 45 ZSM-23 molecular screen fully mixes, keep ZSM-48, Beta, the weight ratio 8:1:1 of ZSM-23 molecular screen, remember that mixed molecular sieve is the ZBZ molecular sieve, with ZBZ molecular sieve and a certain amount of aluminium sesquioxide, coupler is extrusion together, become the support of the catalyst of trifolium shape, be of a size of 4-10mm, prepare load type metal Pt catalyzer with the method for preparing catalyst among the embodiment 1, the Pt metal precursor of selecting is platinum nitrate, the weight of Pt metal accounts for 0.2% of total catalyst weight, obtains at last the Pt/ZBZ molecular sieve.
Embodiment 6
Three kinds of catalyzer of preparation among the embodiment 1 are applied in the hydroisomerizing reaction take n-Hexadecane as model compound.N-hexadecane is dissolved in obtains stock oil in the perhydronaphthalene, wherein the mass ratio of the quality of n-hexadecane and perhydronaphthalene is 3:97, and the control temperature of reaction is 260 ℃, reaction pressure 5.0MPa, and air speed is 1.0h
-1, hydrogen-oil ratio is 800:1, resulting product mainly is the long chain alkane of isomery.Reaction result is as shown in table 1, the ZSM-48 molecular sieve of high silica alumina ratio is applied in the hydroisomerizing reaction of n-Hexadecane can obtain higher liquid yield, but its transformation efficiency is lower, and the molecular sieve of low silica alumina ratio will cause generating more gas, and cracking side-reaction is larger on whole reaction impact.The ZSM-48 molecular sieve of silica alumina ratio 96 can with the more isomerized products of n-hexadecane selective catalysis production, also can keep higher transformation efficiency simultaneously relatively in reaction.Therefore select the ZSM-48 molecular sieve of suitable silicon al mole ratio to have great importance in the reaction of n-hexadecane hydroisomerizing, the suitable ZSM-48 of silica alumina ratio has relatively abundant middle strong acid acid sites, and promoter action is played in whole hydroisomerizing reaction.
Table 1 n-hexadecane is in Pt/ZSM-48 catalyst hydrogenation isomerization reaction result
Embodiment 7
Pt/Beta, Pt/ZSM-23, Pt/ZSM-22, the Pt/Y catalyzer of preparation is applied in the hydroisomerizing reaction take n-Hexadecane as model compound.N-hexadecane is dissolved in obtains stock oil in the perhydronaphthalene, wherein the mass ratio of the quality of n-hexadecane and perhydronaphthalene is 3:97, and the control temperature of reaction is 260 ℃, and reaction pressure 5.0MPa, hydrogen-oil ratio are 400:1, and air speed is 1.0h
-1, reaction result is as shown in table 2, can find out the molecular sieve catalyst than ZSM-48, and the transformation efficiency of selected several molecular sieve catalysts obviously reduces, and the acidic site of molecular sieve is stronger, has promoted cracking side-reaction, directly causes the increase of gas recovery ratio.Simultaneously the selectivity of normal paraffin is very high in the product, in the reaction to the DeGrain of the isomerization-visbreaking of alkane molecule.
Table 2 n-hexadecane is at differing molecular sieve catalyst hydroisomerizing reaction result
Embodiment 8
Select the plam oil raw material through hydrotreatment to carry out hygrogenating isomerization reaction, the nature parameters of oil product sees Table 3.
The palmitic nature parameters of table 3 hydrogenation
| 20 ℃ of density/g*cm -3 | 0.87 |
| Sulphur content (massfraction)/% | Less than 0.001 |
| Cetane value | 62 |
| Condensation point/℃ | 0 |
| Acid number/mgKOH/100ml | 1.5 |
The Pt/ZSM-48 molecular sieve embodies excellent isomerization-visbreaking effect in the hygrogenating isomerization reaction of n-Hexadecane, therefore select the Pt/ZSM-48 catalyzer of the silica alumina ratio 96 of preparation among the embodiment 1 to come the plam oil through hydrotreatment is carried out hygrogenating isomerization reaction.Control reaction pressure 3.5MPa, temperature of reaction is 235 ℃, and hydrogen-oil ratio is 300:1, and air speed is 0.5h
-1The cetane value that obtains oil product after the reaction is 58, and condensation point is-23 ℃.Can find out the condensation point that when guaranteeing the cetane value of oil product, can reduce significantly oil product, can be used as through the oil product of hydroisomerizing and be in harmonious proportion oil product and add to and be applied in the diesel oil in the low temp operation environment.
Embodiment 9
Select the fischer-tropsch wax oil to carry out the hydroisomerizing reaction as stock oil, the catalyzer that uses is the Pt/ZSM-23 catalyzer among the embodiment 2 and the Pt/ZB catalyzer among the embodiment 4.Tandem process is adopted in whole technical process, and one section is adopted the Pt/ZSM-23 catalyzer, control reaction pressure 8.0MPa, and temperature of reaction is 300 ℃, and hydrogen-oil ratio is 1200:1, and air speed is 1.0h
-1Two sections are adopted the Pt/ZB catalyzer, control reaction pressure 3.5MPa, and temperature of reaction is 340 ℃, air speed is 1.0h
-1Whole transformation efficiency is 50.6% after the reaction, and the condensation point of the lubricating oil that obtains is-32 ℃.
Embodiment 10
Select the waste lubricating oil through hydrotreatment to carry out the hydroisomerizing reaction as raw material, the nature parameters of oil product sees Table 4.The catalyzer that uses is the Pt/ZBZ catalyzer among the embodiment 5.Control reaction pressure 7.5MPa, temperature of reaction is 340 ℃, and hydrogen-oil ratio is 800:1, and air speed is 0.8h
-1The cetane value that obtains oil product after the reaction is 54, and condensation point is-35 ℃.
The nature parameters of table 4 hydrogenation waste lubricating oil
| 20 ℃ of density/g*cm -3 | 0.88 |
| Sulphur content (massfraction)/% | Less than 0.001 |
| Cetane value | 59 |
| Condensation point/℃ | -5 |
Claims (6)
1. method and the catalyzer thereof of a long chain alkane hydroisomerizing pour point depression, it is characterized in that: adopt single hop or two sections serial hydrogenation isomerization processes, under the hydroisomerizing condition, the control reaction pressure is 1-12MPa, temperature of reaction is 200-380 ℃, and volume space velocity is 0.2-4h
-1, hydrogen to oil volume ratio is 200-1200, stock oil and hydrogen are by the hydroisomerization catalyst bed.
2. method according to claim 1 is characterized in that: stock oil be through hydrotreatment vegetables oil, fischer-tropsch wax oil or through the waste lubricating oil of hydrotreatment.
3. method according to claim 2 is characterized in that: wherein vegetables oil comprises various plam oils, curcas oil, Viscotrol C, soybean oil, rape seed oil, algae oil, sweet oil, peanut oil, cereal oil.
4. the catalyzer that is used for claim 1 or 2 or 3 described methods, it is characterized in that, this is crossed hydroisomerization catalyst and comprises molecular sieve carrier and metal active constituent, wherein the metal in the metal active constituent is one or more among Pt, Pd, Ni, the Ru, and the weight of metal active constituent is total catalyst weight 0.05wt%-0.5wt% in the hydroisomerization catalyst.
5. catalyzer according to claim 4, it is characterized in that: the molecular sieve that adopts in the molecular sieve carrier is one or more among ZSM-48, ZSM-23, ZSM-22, Beta and the Y, wherein contain at least the ZSM-48 molecular sieve, the silica alumina ratio of the molecular sieve that adopts is 20-180.
6. catalyzer according to claim 5, be further characterized in that: the gross weight of molecular sieve is the 20wt%-90wt% of molecular sieve supported body weight in the molecular sieve carrier.
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| CN104624225A (en) * | 2015-01-21 | 2015-05-20 | 南开大学 | Low-temperature aqueous-phase catalyst for lignin phenol derivative hydrodeoxygenation and preparation method thereof |
| CN105728023A (en) * | 2014-12-08 | 2016-07-06 | 中国石油天然气股份有限公司 | Molecular sieve catalyst for Fischer-Tropsch wax hydroisomerization reaction, and preparation method thereof |
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| CN105728023A (en) * | 2014-12-08 | 2016-07-06 | 中国石油天然气股份有限公司 | Molecular sieve catalyst for Fischer-Tropsch wax hydroisomerization reaction, and preparation method thereof |
| CN104624225A (en) * | 2015-01-21 | 2015-05-20 | 南开大学 | Low-temperature aqueous-phase catalyst for lignin phenol derivative hydrodeoxygenation and preparation method thereof |
| CN106190286A (en) * | 2015-04-29 | 2016-12-07 | 中国石油化工股份有限公司 | A kind of method preparing jet fuel |
| CN106190279A (en) * | 2015-04-29 | 2016-12-07 | 中国石油化工股份有限公司 | A kind of method of hydrotreating preparing jet fuel |
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| CN106190280B (en) * | 2015-04-29 | 2019-05-21 | 中国石油化工股份有限公司 | A method of jet fuel is prepared with renewable raw materials |
| CN106190286B (en) * | 2015-04-29 | 2018-03-20 | 中国石油化工股份有限公司 | A kind of method for preparing jet fuel |
| CN106190279B (en) * | 2015-04-29 | 2018-04-13 | 中国石油化工股份有限公司 | A kind of method of hydrotreating for preparing jet fuel |
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| CN109988638A (en) * | 2017-12-29 | 2019-07-09 | 中国石油化工股份有限公司 | The flexibly hydrogenation technique of production low freezing point diesel fuel |
| CN109988638B (en) * | 2017-12-29 | 2021-07-09 | 中国石油化工股份有限公司 | Hydrogenation process for flexibly producing low-condensation-point diesel oil |
| CN108816277A (en) * | 2018-05-31 | 2018-11-16 | 上海华谊（集团）公司 | Long chain hydrocarbons isomerization catalyst and its preparation method and application |
| CN115779960A (en) * | 2022-11-15 | 2023-03-14 | 国家能源集团宁夏煤业有限责任公司 | Catalyst for normal hydrocarbon isomerization and application thereof in Fischer-Tropsch wax hydroconversion process |
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