CN1345913A - Method for hydroisomerization of light hydrocarbon - Google Patents
Method for hydroisomerization of light hydrocarbon Download PDFInfo
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Abstract
The hydroisomerization method of light hydrocarbon includes the following step of the under the condition of isomerization, in the presence of hydrogen gas making light hydrocarbon raw material contact with an isomerization catalyst to formed from 0.01-2.0 wt% of metal of VIII family and carrier, and the described carrier is composed of 20-80 wt% of beta-zeolite, 10-70 wt% of flokite and 10-50 wt% of alumina. Said method is applicable to isomerization reaction of C5-C6 straight chain light hydrocarbon, and can effectively raise the octane number of light hydrocarbon component.
Description
The present invention is a kind of isomerization method for light hydrocarbon, specifically, is a kind of with C
5～C
6Paraffinic hydrocarbons generates more branched paraffin to improve the method for light hydrocarbon feedstocks octane value by isomerization reaction.
As everyone knows, because environmental requirement, low lead or white gasoline just progressively replace doped fuel.Because isoparaffin has higher octane value, therefore with small molecular weight (C
5, C
6) normal paraffin change into the octane value that isoparaffin improves the light oil fraction, thereby the octane value that improves gasoline has very noticeable application prospect.
One of isomerization method for light hydrocarbon commonly used is to carry out hydroisomerization reaction more than 250 ℃ with the zeolite type dual-function catalyst.The difunctional isomerization catalyst of described zeolite type mainly is meant with the crystalline silicate to be carrier, and aluminum oxide or other refractory oxide are binding agent, and supported V III family metal mainly is the catalyzer of platinum or palladium preparation.The carrier of this class catalyzer has acid function, can impel normal alkane isomerization, and used carrier mainly contains X type zeolite, y-type zeolite and mordenite at present.Because mordenite has good high-temperature stability, therefore be that the isomerization catalyst of preparing carriers is developed rapidly with the mordenite.As USP4,232,181, GB1039246, GB1189850, USP4,665,272 patent documentations such as grade are all described this kind Preparation of catalysts method in detail.But because the application of temperature of zeolite type dual-function catalyst is higher, and the equilibrium concentration of isomerized products is lower under the high temperature, particularly to normal hexane, higher temperature of reaction will influence in the isomerized products 2, and the 2-dimethylbutane (2, concentration 2-DMB), and 2,2-DMB has very high octane value, if its concentration reduces, will directly influence the octane value of isomerized products.Therefore, further improve the acidity of mordenite, the isomery selectivity that improves it seems very necessary.USP3,527,835 adopt the ammonium ion used when increasing the preparation h-mordenite and the ratio of zeolite metallic cation, promptly when ion-exchange, make the ratio of ammonium ion and zeolite metallic cation reach 100: 1 above methods and prepare acid strong h-mordenite, improve the performance of isomerization catalyst.CN87103444A then by increasing the surface-area of catalyzer, makes it reach 580 meters
2The above method of/gram is improved the performance of catalyzer.
The simple acidity of improving mordenite often can't make the isomery selectivity of catalyzer be greatly improved, and therefore, people are by introducing the acidity that chlorine or fluorine improve catalyzer in carrier.As USP4,789,655 introduce chlorine by the gas phase oxi-chlorination in the mordenite catalyst that carries platinum, described oxi-chlorination is to feed to contain oxygen, water, chlorine and/or muriatic gaseous mixture under 200～500 ℃ in catalyzer, and each component with respect to the ratio of mordenite is in the gaseous mixture: water 0.03～4 heavy %, chlorine and/or muriate (in chlorine) 0.5～10 heavy %.USP3,932,554 adopt fluorine-containing halon such as CF
4, CCl
3F, CHCl
2F etc. contact with the mordenite catalyst that carries platinum or palladium, make the modified catalyst that fluorine content is at least 0.86 heavy %.Though the catalyzer of above-mentioned chlorine or fluorine modification has good isomerization performance, in the catalyzer use, chlorine or fluorine can run off gradually along with the carrying out of reaction, cause catalyst activity reduction, corrosion of equipment.
In recent years, the β zeolite is owing to the characteristic Application Areas that itself has constantly enlarges.The existing report that the β zeolite is used for light hydrocarbon isomerization in the patent documentation, as USP5,095,169 to disclose a kind of be the isomerization catalyst of preparing carriers with activatory β zeolite, and this patent mainly is to improve the activation method of β zeolite, this method with the β zeolite at 600～700 ℃, being preferably in 650 ℃ handles, remove the strong acid in the β zeolite, keep weak acid, obtain activatory β zeolite.This activatory β zeolite is made the h-type zeolite carrier through ammonium exchange, increase with the selectivity of the isomerization catalyst of this preparing carriers.
The purpose of this invention is to provide a kind of method for hydroisomerization of light hydrocarbon, this method can make the C that contains in the light hydrocarbon feedstocks
5And/or C
6Normal paraffin is converted into isoparaffin effectively, thereby obtains high-octane isomerization product.
Method of the present invention be included in make under the isomerisation conditions light hydrocarbon feedstocks in the presence of hydrogen with a kind of isomerization catalyst contact reacts, wherein isomerization catalyst is made up of VIII family metal and the carrier of 0.01～2.0 heavy %, and described carrier is made up of the β zeolite of 20～80 heavy %, the mordenite of 10～70 heavy % and the aluminum oxide of 10～50 heavy %.
VIII family metal is selected from platinum, palladium, ruthenium, rhodium, osmium, iridium in the described isomerization catalyst, and preferred VIIl family metal is platinum or palladium.VlII family metal is at catalyst content preferred 0.15～0.8 heavy %, and its existence form can be oxidation state or goes back ortho states.
Mordenite content preferred 10～50 heavy % in the described support of the catalyst, the content of β zeolite preferred 40～60 heavy %, aluminum oxide preferred 10～30 heavy %.
The high purity aluminium oxide that the preferred aluminum alkoxide hydrolysis of aluminum oxide in the support of the catalyst makes, this high purity aluminium oxide can be C
4The aluminum oxide that above high-carbon aluminum alkoxide hydrolysis makes also can be C
4The aluminum oxide that following low-carbon alkoxy aluminium hydrolysis makes, or the mixture of the two.The method preparation that the high purity aluminium oxide that described low-carbon alkoxy aluminium hydrolysis makes adopts CN1032951A to announce.
Mordenite in the support of the catalyst and β zeolite are sodium content all less than 0.3 heavy %, and preferably sodium content is at the h-type zeolite of 0.01～0.08 heavy % scope.It is natural mordenite zeolite that described mordenite can be selected for use, also can select synthesizing flokite for use.The mol ratio of silica in β zeolite and the mordenite in the carrier, promptly silica alumina ratio is 5～80, and is preferred 10～60, and more preferably 15～40.
The suitable isomerisation conditions of using the inventive method is 200～400 ℃ of temperature, preferred 230～300 ℃, pressure 0.5～5.0MPa, preferred 1.0～3.0MPa, raw material feed weight air speed 0.2～10.0 hour
-1, preferred 0.5～3.0 hour
-1For avoiding side reactions such as cracking to take place, should there be a certain amount of hydrogen to exist in the isomerization reaction, therefore, should imports small quantity of hydrogen during reaction feed, the mol ratio of hydrogen and hydrocarbon feed is 0.05～5.0 during charging, in reaction process, the amount of hydrogen is few more good more, can reduce hydrogen recycle like this, reduce plant energy consumption, but the amount of hydrogen can not take place otherwise be difficult to suppress side reaction, so hydrogen hydrocarbon mol ratio is 0.1～3.0 preferably very little.
Remove in the described light hydrocarbon feedstocks and contain C
5And/or C
6Outside the paraffinic hydrocarbons, also contain a spot of C
4And greater than C
7The hydrocarbon component, specifically, C in the raw material
5And/or C
6The content of paraffinic hydrocarbons is at least 70 heavy %, C
4The content of hydrocarbon is less than 10 heavy %, greater than C
7Hydrocarbon content less than 3 heavy %, but the effective material content of isomerization is at least 50 heavy % in the raw material, the effective raw material of so-called isomerization refers to C
5, C
6Normal paraffin and methylpentane.
For guaranteeing catalyst life, sulphur content should be less than 35ppm in the light hydrocarbon feedstocks, and water-content should can adopt conventional method to remove foreign matter content less than 50ppm, as removing sulphur with hydrodesulfurization, removes water with molecular sieve adsorption.
Be applicable to the C of containing of the present invention
5And/or C
6Refinery's hydrocarbon feed comprise light condensate oil, light virgin naphtha, gas condensate oil, gently raffinate oil, light reformate and final boiling point are 77 ℃ straight run tops.
In the isomerization reaction raw material, contain more isoparaffin, when its content weighs % greater than 50, preferably adopt the method for rectifying that the isoparaffin in the raw material is separated earlier, and then the raw material that will tell isomeric alkane carries out isomerization, can enhance productivity like this, and the octane value of the finished product is improved.
The preparation method of isomerization catalyst of the present invention comprises the steps:
(1) h-mordenite, Hydrogen β zeolite and aluminum oxide are mixed by the butt weight ratio, pinch through mixing, moulding, roasting make Zeolite support,
(2) with the above-mentioned Zeolite support of solution impregnation that contains VlII family metal, dry, roasting makes catalyzer.
The h-mordenite in (1) step or Hydrogen β zeolite all can adopt conventional ion-exchange techniques to be prepared by na-pretreated zeolite in the described method.As na-pretreated zeolite is carried out ion-exchange with acid or acidic salt solution under 90～95 ℃, to make sodium content less than 0.3 heavy %, preferably sodium content is the h-type zeolite of 0.01～0.08 heavy %.Hydrochloric acid is generally selected in acid used in the ion exchange process for use, and its concentration is preferably 0.1～5.0 mol, and used acidic salt solution is generally selected ammonium chloride solution for use.Described ion exchange process can repeat repeatedly, till the sodium content of zeolite reaches requirement.
After h-mordenite, Hydrogen β zeolite and aluminum oxide pressed butt weight ratio mixing, adding rare nitric acid or extrusion aids such as acetic acid, citric acid mixes and pinches, and then extrusion moulding, room temperature～150 ℃ drying, 450～850 ℃, preferably 500～600 ℃ of roastings make the composite zeolite carrier, the carrier of extrusion moulding is stripe shape preferably, also can be other shape, as sheet shape, cloverleaf pattern.The method of carrier moulding also can adopt the method for dripping ball or spin to make the ball-type carrier except that extrusion moulding.
The preferred Platinic chloride of solution, the acid of chlorine palladium, the platinum ammonium complex ion that contain VIII family metal described in the catalyst preparation step (2), the amount of flooding the solution of the used VIII of containing family metal should make bullion content wherein satisfy desired content in the catalyzer.During dipping, the volume ratio of steeping fluid and carrier is preferably 3～1.2: 1.Dipping back carrier promptly gets isomerization catalyst in room temperature～150 ℃ drying, 450～850 ℃ of roastings.
Described drying of above-mentioned preparation catalyzer and roasting time are 1～8 hour, are preferably 3～6 hours.
Below accompanying drawing is described.
Fig. 1 is the process flow sheet of the inventive method.
Fig. 2 is the process flow sheet of a preferred version of the inventive method.
Fig. 3 is the reaction times of the isomerization catalyst of the present invention's use and the graph of a relation of isomerisation conversion.
By shown in Figure 1, C
5And/or C
6Light hydrocarbon feedstocks enters reactive system by pipeline 2 and mixes from the hydrogen of pipeline 1, after well heater 3 heating, entering isomerization reactor 5 through pipeline 4 by the top contacts with catalyzer, reacted product is by pipeline 6 outflow reactors, through entering gas-liquid separator 8 after condenser 7 coolings, isolated light constituent is discharged from reactive system as combustion gas or liquefied gas, and product liquid is an isomerization product, as the blend component of clean gasoline.
In the refinery as the C of isomerization raw material
5And/or C
6In the component, contain more iso-pentane sometimes, during actual production, need iso-pentane wherein to be separated as the purpose product through rectifying or other method, and remaining component is carried out isomerization reaction as raw material, isomerization reaction product and process rectifying or the isolated iso-pentane of other method mix as the finished product the finished product octane value height of the technical process that the finished product octane value that obtains like this is more shown in Figure 1.This technical process as shown in Figure 2, isomerization stock oil enters rectifying tower 11 by pipeline 2, the component that rectifying tower top is rich in iso-pentane is discharged as product by pipeline 13, the content of iso-pentane is greater than 85 heavy % in this product, component at the bottom of the rectifying tower is squeezed into pipeline 14 as the isomerization raw material by fresh feed pump 12, hydrogen enters pipeline 14 by pipeline 1 to be mixed with raw material, again through process furnace 3 preheatings after pipeline 4 enters reactor 5 by the top contacts with catalyzer, reacting rear material is discharged from the bottom of reactor 5 by pipeline 6, after condenser 7 condensations, enter gas-liquid separator 8, by the light constituent of telling in the gas-liquid separator 8 by pipeline 9 discharge systems, liquid phase component by pipeline 10 drain separators 8 as isomerization product.Promptly can be used as the gasoline blend component after the isomerization product fusion that pipeline 13 and pipeline 10 are discharged.
The inventive method adopts the isomerization catalyst with specific composition, and C5 and/or C6 component that octane value in the refinery is lower become high-octane number component by isomerization reaction, and this component both can be used as the gasoline blend component, can be used as a kind of clean gasoline component again.The used support of the catalyst of present method contains the zeolite component of two kinds of different structures, make carrier have moderate acidity, help C5 and/or the isomerization effectively of C6 component, improve the octane value of product, catalyzer has long work-ing life simultaneously, is convenient to the isomerization operation.
Further specify the present invention below by example, but the present invention is not limited to this.
Example 1
Prepare isomerization catalyst of the present invention.
Get 100 gram sodium type mordenites (Fushun No.3 Petroleum Factory's production), its composition sees Table 1, is put in the three-necked bottle, adds the NH of 800 milliliter of 1 mol
4Cl solution was 90～95 ℃ of exchanges 3 hours, filter, the gained solid washs with deionized water, 120 ℃ of dryings 3 hours, repetitive operation twice, the HCl with 800 milliliter of 1 mol handled 3 hours at 90～95 ℃ again, filter, wash to filtrate with deionized water and be neutral, 600 ℃ of roastings 6 hours, making sodium content is 0.03 heavy %, the h-mordenite of silica alumina ratio 23.4 (fluorescence spectrum method for measuring).
Get 100 gram sodium type β zeolites (Fushun No.3 Petroleum Factory's production), its composition sees Table 1, adds the NH of 800 milliliter of 1 mol
4 Cl solution filters 90～95 ℃ of exchanges 3 hours, and the gained solid washs with deionized water, 120 ℃ of dryings 3 hours, and the Hydrogen β zeolite that sodium content is 0.03 heavy % was made in twice, 600 ℃ of roasting of repetitive operation in 6 hours.
With above-mentioned h-mordenite, Hydrogen β zeolite and high purity aluminium oxide (SB powder, Germany CONDEA company produces) mix by 40: 40: 20 vehicle group is proportional, the salpeter solution that added volume ratio and be 1: 1 mixes to be pinched, add nitric acid and solid powder volume ratio be 1: 1.6, extruded moulding, 120 ℃ of dryings 2 hours, 550 ℃ of roastings made the composite zeolite carrier in 4 hours.
Get composite zeolite carrier 100 gram, with the platinum acid chloride solution room temperature dipping of 45 milliliter of 8.6 mol 24 hours, 120 ℃ of dryings 4 hours, roasting made catalyst A of the present invention in 4 hours in 550 ℃ of air, and platinum content is 0.35 weight % in the gained catalyzer.
Example 2
Method by CN1032951A prepares the HP aluminum oxide powder, method by example 1 prepares h-mordenite and Hydrogen β zeolite again, then in butt weight by h-mordenite: Hydrogen β zeolite: the HP aluminum oxide is that 40: 40: 20 feed ratio is mixed with catalyst B, and its platinum content is 0.35 heavy %.
Example 3
According to the method described in the example 1 sodium type mordenite, sodium type Beta zeolite are carried out the ammonium exchange, handled 3 hours at 90～95 ℃ with the HCl of 500 milliliter of 1 mol respectively again, make silica alumina ratio and be 59.0 h-mordenite and silica alumina ratio and be 58.0 Hydrogen Beta zeolite, then in butt weight by h-mordenite: Hydrogen β zeolite: the SB aluminum oxide is that 20: 60: 20 feed ratio is mixed with catalyzer C, and platinum content is 0.35 heavy %.
Example 4～6
Following example is that raw material carries out isomerization experiments with pure N-alkanes.
Isomerization catalyst is packed in the small stationary bed bioreactor, Intake Quantity is 12 milliliters, is warming up to 600 ℃, feeds hydrogen reducing 4 hours, feed normal paraffin then and carry out isomerization reaction under 250 ℃, 1.47MPa condition, the reaction feed weight space velocity is 1.0 hours
-1, hydrogen hydrocarbon mol ratio is 2.7.The used reaction raw materials of each example, catalyzer and experimental result see Table 2.
Isomerization rate and isomerization optionally are defined as follows in the table 2:
Example 7
This example carries out isomerization reaction by the method for example 4, and different is that Skellysolve A and normal hexane are mixed the back as raw material by 60: 40 weight ratio, and catalyst A is selected in isomerization reaction for use, and reaction result sees Table 2.
Example 8
This example carries out isomerization experiments to industrial raw material oil.
Get catalyst A 74 grams (100 milliliters) of embodiment 1 preparation, in the 100 milliliters of fixed-bed reactor of packing into, the flow path device by Fig. 1 on experimental installation carries out the isomerization longevity test.Isomerization reaction is 1.7MPa, 270 ℃, during raw material weight air speed 1.0
-1, 2.6 moles of hydrogen-oil ratios condition under successive reaction 720 hours.The temperature control of separator 8 is 20 ℃ in the reaction process, and pressure is 1.7MPa.With the gas-liquid two-phase of telling in the gas-liquid separator 8, metering and sampling analysis are formed respectively, calculate reacting rear material and always form after normalization method, and calculate isomerization rate, C in the reaction process
5Isomerization rate and C
6Isomerization rate is seen Fig. 3 with the reaction times variation tendency.React raw materials used oil composition and see Table 3, its research octane number (RON) (RON) is 74.4.
As shown in Figure 3, after reaction in 720 hours, the C of catalyzer
5Isomerization rate and C
6Isomerization rate is all higher and steady with the reaction times variation tendency, illustrates that catalyzer has stability preferably, and the RON value of reaction gained liquid product is 80.5.
Example 9
This example is pressed the technical process of Fig. 2, earlier the iso-pentane in the stock oil is removed, and then carries out isomerization reaction.
Get catalyst A 74 grams (100 milliliters) of embodiment 1 preparation, in the 100 milliliters of fixed-bed reactor of packing into, carry out isomerization test by the experimental installation flow process of Fig. 2.To obtain the component shown in the table 4 after 5 rectifying of raw material process rectifying tower in the table 3, the rectifying tower top service temperature is to be that 120 ℃, pressure are 0.5MPa at the bottom of 70 ℃, tower, rectifying tower top is rich in the component of iso-pentane as product, component at the bottom of the rectifying tower is carried out isomerization reaction as the isomerization raw material, is reflected at 270 ℃, when 1.7MPa, raw material weight air speed 1.0
-1, hydrogen/oil mol ratio 2.6 condition under carry out, isomerization product is through gas-liquid separation, and analyzing the product liquid RON that is discharged by pipeline 10 is 80.1, and component mixing its RON of back that this material and rectifying tower top are rich in iso-pentane is 83.4, compare with example 8 products, octane value improves 2.9 units.
Table 1
Table 2
IC in the table 2
5-iso-pentane, nC
5-Skellysolve A, 22DMB-2,2-dimethylbutane, 23DMB-2,3-dimethylbutane, 2MP-2-methylpentane, 3MP-3-methylpentane, nC
6-normal hexane
Table 3
| Component | Content, heavy % |
| ????iC 4 | ????/ |
| ????nC 4 | ????4.34 |
| ????iC 5 | ????27.87 |
| ????nC 5 | ????28.22 |
| ????22DMB | ????1.01 |
| ????23DMB | ????5.01 |
| ????2MP | ????10.43 |
| ????3MP | ????5.6 |
| ????nC 6 | ????10.06 |
| ????MCP | ????4.86 |
| ????B | ????0.97 |
| ????CH | ????1.63 |
MCP-methylcyclopentane in the table 3, B-benzene, CH-hexanaphthene
Table 4
| Component | Rectifying tower top is formed, heavy % | Form heavy % at the bottom of the rectifying tower |
| ????iC 4 | ????/ | ????/ |
| ????nC 4 | ????13.6 | ????/ |
| ????iC 5 | ????73.4 | ????6.2 |
| ????nC 5 | ????13.0 | ????35.4 |
| ????22DMB | ????/ | ????1.5 |
| ????23DMB | ????/ | ????7.4 |
| ????2MP | ????/ | ????15.3 |
| ????3Mp | ????/ | ????8.3 |
| ????nC 6 | ????/ | ????14.9 |
| ????MCP | ????/ | ????7.2 |
| ????B | ????/ | ????1.5 |
| ????CH | ????/ | ????2.3 |
| ????RON | ????90.4 | ????69.3 |
Claims (10)
1, a kind of method for hydroisomerization of light hydrocarbon, be included in make under the isomerisation conditions light hydrocarbon feedstocks in the presence of hydrogen with a kind of isomerization catalyst contact reacts, wherein said isomerization catalyst is made up of VIII family metal and the carrier of 0.01～2.0 heavy %, and described carrier is made up of the β zeolite of 20～80 heavy %, the mordenite of 10～70 heavy % and the aluminum oxide of 10～50 heavy %.
2, in accordance with the method for claim 1, it is characterized in that described isomerisation temperature is 200～400 ℃, pressure 0.5～5.0MPa, lighter hydrocarbons feed weight air speed 0.2～10.0 hour
-1, feed hydrogen hydrocarbon mol ratio 0.05～5.0.
3, in accordance with the method for claim 1, it is characterized in that described isomerisation temperature is that 230～300 ℃, pressure are that 1.0～3.0MPa, raw material feed weight air speed are 0.5～3.0 hour
-1, feed hydrogen hydrocarbon mol ratio 0.1～3.0.
4, according to described any one method of claim 1～3, it is characterized in that VIII family metal is platinum or palladium in the described catalyzer, its content is 0.15～0.8 heavy %.
5, according to described any one method of claim 1～3, it is characterized in that mordenite content is 10～50 heavy % in the described carrier, the content of β zeolite is 40～60 heavy %, aluminum oxide is 10～30 heavy %.
6, according to described any one method of claim 1～3, the sodium content that it is characterized in that described mordenite and β zeolite is all less than 0.3 heavy %.
7,, it is characterized in that the silica of described mordenite and β zeolite is 5～80 according to described any one method of claim 1～3.
8,, it is characterized in that the silica of described mordenite and β zeolite is 10～60 according to described any one method of claim 1～3.
9, according to described any one method of claim 1～3, it is characterized in that C in the described light hydrocarbon feedstocks
5And/or C
6The content of paraffinic hydrocarbons is at least 70 heavy %.
10, in accordance with the method for claim 9, the content that it is characterized in that the effective raw material of isomerization in the described lighter hydrocarbons is at least 50 heavy %.
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| CN100395220C (en) * | 2005-03-31 | 2008-06-18 | 中国石油化工股份有限公司 | Method for isomerization of light hydrocarbon |
| CN101851530A (en) * | 2009-03-31 | 2010-10-06 | 中国石油化工股份有限公司 | Paraffin isomerization method of reducing benzene content |
| CN105542845A (en) * | 2014-11-04 | 2016-05-04 | 北京安耐吉能源工程技术有限公司 | Hydroisomerization method |
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| CN100395220C (en) * | 2005-03-31 | 2008-06-18 | 中国石油化工股份有限公司 | Method for isomerization of light hydrocarbon |
| CN101851530A (en) * | 2009-03-31 | 2010-10-06 | 中国石油化工股份有限公司 | Paraffin isomerization method of reducing benzene content |
| CN101851530B (en) * | 2009-03-31 | 2013-04-24 | 中国石油化工股份有限公司 | Paraffin isomerization method of reducing benzene content |
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| CN106622354A (en) * | 2016-12-30 | 2017-05-10 | 山西潞安纳克碳化工有限公司 | N-alkane isomerization catalyst and catalysis method thereof |
| CN108187735A (en) * | 2017-12-30 | 2018-06-22 | 西安元创化工科技股份有限公司 | A kind of catalyst and method that high-knock rating gasoline is produced using coal base light oil |
| CN108187735B (en) * | 2017-12-30 | 2020-07-31 | 西安元创化工科技股份有限公司 | Catalyst and method for preparing high-octane gasoline by using coal-based light oil |
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|---|---|
| CN1108354C (en) | 2003-05-14 |
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