CN102977914B - Catalytic reforming process and catalytic reforming reactor - Google Patents
Catalytic reforming process and catalytic reforming reactor Download PDFInfo
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- CN102977914B CN102977914B CN201210427866.1A CN201210427866A CN102977914B CN 102977914 B CN102977914 B CN 102977914B CN 201210427866 A CN201210427866 A CN 201210427866A CN 102977914 B CN102977914 B CN 102977914B
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Abstract
The invention discloses a catalytic reforming process with small loss of a reforming catalyst and a catalytic reforming reactor specially used therein. According to the process, oil gas is introduced into a membrane filtration apparatus; when the oil gas passes through a membrane filtration element in the membrane filtration apparatus, interception and catalysis effects of the membrane filtration element allow filtration and catalytic reforming of the oil gas to be simultaneously realized, the oil gas having undergone catalytic reforming is output from an air outlet of the membrane filtration apparatus, and intercepted oil residue is output from a slag removal outlet of the membrane filtration apparatus, wherein the membrane filtration element comprises a substrate composed of a porous material skeleton and a reforming catalyst attached in the porous material skeleton, and the average pore size of the substrate is 1 to 100 mu m. The membrane filtration element can intercept at least a part of dust in the oil gas and can carry out catalytic reforming on hydrocarbon molecules in the oil gas, the reforming catalyst does not flow in the membrane filtration apparatus, and thus, the process provided by the invention can prevent coking of the reforming catalyst to some extent and reduces loss of the reforming catalyst.
Description
Technical field
The present invention relates to a kind of catalytic reforming process and catalytic reforming reactor.
Background technology
The application's said " catalytic reforming " refers to the process utilizing catalyzer (calling reforming catalyst in the following text) to rearrange hydrocarbon molecules structure.Catalytic reforming itself is an important step in petroleum refining process, and its main purpose improves the octane value of oil product.The reforming catalyst of industrial use generally can be divided into two large classes, and a class is non-precious metal catalyst, and the oxide compound of the VIth race's metallic element in its main active component many genus periodic table of elements, as Cr
2o
3, MoO
3deng, the performance of this kind of catalyzer is lower, has substantially been eliminated at present; Another kind of is noble metal catalyst, and its active ingredient is the metallic element of the VIIIth race in the periodic table of elements mainly, as platinum, palladium, iridium, rhodium etc.Existing catalytic reforming process is passed in fluidized-bed catalytic reactor by oil gas to react with reforming catalyst, not only there is the larger problem of the loss of reforming catalyst in this technique, also to contact with reforming catalyst because of the dust in oil gas simultaneously and cause reforming catalyst coking, thus affect the work-ing life of reforming catalyst.
Summary of the invention
It is the catalytic reforming process and special catalytic reforming reactor that reforming catalyst number of dropouts is little that the application aims to provide a kind of.
For this reason, the catalytic reforming process of the application is passed into by oil gas in a membrane filter appts, when the film filtering element of described oil gas in this membrane filter appts, retain the filtration and the catalytic reforming that realize oil gas with katalysis by this film filtering element simultaneously, oil gas after catalytic reforming exports from the venting port of this membrane filter appts, and the dregs of fat be trapped export from the slag-drip opening of this membrane filter appts; Wherein, described film filtering element comprises by porous material skeleton and is attached to the matrix that the reforming catalyst in this porous material skeleton forms, and the mean pore size of this matrix is 1 μm-100 μm.Need point out, in the application, the mensuration of mean pore size adopts steam bubble assay method conventional in sintered porous material manufacture field.Another it is noted that according to measuring and calculating, when the mean pore size of matrix is less than 1 μm, easily cause matrix to block; When the mean pore size of matrix is greater than 100 μm, the filtering accuracy of the obvious reduction oil gas of meeting, therefore the mean pore size of matrix is set as 1 μm-100 μm.Obviously, dust at least partially in oil gas can either be trapped in the surface of film filtering element by " film filtering element " in the application, catalytic reforming can be carried out to hydrocarbon molecules in oil gas again simultaneously, and reforming catalyst does not flow in membrane filter appts, therefore, this catalytic reforming process can prevent reforming catalyst coking to a certain extent, and reduces the number of dropouts of reforming catalyst, can control the product of reforming reaction in addition preferably.
Wherein, described porous material skeleton can adopt any one material in the multiple materials such as Intermatallic Ti-Al compound porous material, intermetallic Fe-Al compound porous material, stainless steel porous material, ceramic porous material to form.This several porous material skeleton above-mentioned only plays a supportive role to reforming catalyst, and does not participate in catalytic reforming reaction.The application preferably adopts intermetallic Ni-Al compound porous material to form porous material skeleton, this is mainly because " nickel " belongs to the metallic element of the VIIIth race in the periodic table of elements, itself just plays certain catalytic reforming effect to hydrocarbon molecules, therefore the porous material skeleton adopting intermetallic Ni-Al compound porous material to form obviously can assisted reaction, improves catalytic efficiency.Intermetallic Ni-Al compound porous material is a kind of known materials, and its preparation method can with reference to the record of CN101358304B.In order to further improve catalytic efficiency, also on the basis of existing intermetallic Ni-Al compound porous material, the weight ratio of nickel in material and aluminium can be increased between 10:1 to 12:1.
Theoretically, all active ingredients in existing catalytic reforming process in used reforming catalyst all can be used as in the application for being attached to the reforming catalyst in porous material skeleton.As preferably, the reforming catalyst of the application is at least made up of one or more metals in platinum, rhodium, iridium, palladium.Wherein, preferably adopt the monometallic reforming catalyst be only made up of platinum, or the dual metal reforming catalyst be made up of " platinum-rhenium " or " platinum-Xi ", or the multimetal reforming catalyst be made up of " platinum-rhenium-titanium ".In the art, the advantage adopting the reforming catalyst be at least made up of one or more metals in platinum, rhodium, iridium, palladium is known, therefore no longer repeats this herein.
As the improvement to technique scheme, described film filtering element also comprises the rete be positioned on described matrix windward side, and the mean pore size of this rete is 1 μm-20 μm.According to alleged cause, described rete is preferably made up of intermetallic Ni-Al compound porous material.Wherein, term " windward side " refers to a side surface of hydrocarbons contact first and to be filtered on matrix.After arrange rete on matrix windward side, in fact this film filtering element forms a matrix material be made up of matrix and rete.Due to the existence of rete, treat that the oil gas of catalytic reforming must first contact with rete, thus by rete, the dust at least partially in oil gas is tackled, reduce the touch opportunity even eliminating dust and matrix, thus further prevent reforming catalyst coking.When being provided with rete, the mean pore size of this rete preferably by as far as possible the dust in oil gas is removed clean for the purpose of set (therefore the mean pore size of rete is set as within the scope of less 1 μm-20 μm by the application), and the mean pore size of matrix preferably by make catalytic reforming reaction more fully for the purpose of set.Consider the factors such as Membrane Filtration Flux, (mean pore size of matrix is advisable at 20 μm-50 μm the mean pore size of matrix can be set greater than the mean pore size of rete, the mean pore size of rete is advisable at 3 μm-15 μm), such film filtering element will form unsymmetric structure, thus obtain certain portfolio effect in filtration flux, filtering accuracy, catalytic reforming effect three.
The catalytic reforming reactor for above-mentioned catalytic reforming process that the application provides, comprise the membrane filter appts being provided with inlet mouth, venting port and slag-drip opening, in this membrane filter appts, film filtering element is installed, this film filtering element comprises by porous material skeleton and is attached to the matrix that the reforming catalyst in this porous material skeleton forms, and the mean pore size of this matrix is 1 μm-100 μm.When this catalytic reforming reactor uses, the oil gas that stock oil adds thermosetting enters membrane filter appts from the inlet mouth of membrane filter appts, then, described oil gas passes through the film filtering element in this membrane filter appts again, at this moment, retain by this film filtering element the filtration and the catalytic reforming that realize oil gas with katalysis, the oil gas after catalytic reforming exports from the venting port of this membrane filter appts, and the dregs of fat be trapped export from the slag-drip opening of this membrane filter appts simultaneously.
On the basis of above-mentioned catalytic reforming reactor, described porous material skeleton is preferably made up of intermetallic Ni-Al compound porous material.In addition, described reforming catalyst is preferably at least made up of one or more metals in platinum, rhodium, iridium, palladium.As the improvement to catalytic reforming reactor, described film filtering element also comprises the rete be positioned on described matrix windward side, and the mean pore size of this rete is 1 μm-20 μm.In addition, described rete is preferably made up of intermetallic Ni-Al compound porous material.In above-mentioned intermetallic Ni-Al compound porous material, the weight ratio of nickel and aluminium is preferably 10:1 to 12:1.In above-mentioned film filtering element, the mean pore size of matrix is advisable at 20 μm-50 μm, and the mean pore size of rete is advisable at 3 μm-15 μm.
Film filtering element of above-mentioned catalytic reforming process and catalytic reforming reactor and preparation method thereof will be provided for below the application.This film filtering element can realize the filtration of oil gas and the dual function of catalytic reforming simultaneously.
Concrete, this film filtering element comprises by porous material skeleton and is attached to the matrix that the reforming catalyst in this porous material skeleton forms, and the mean pore size of this matrix is 1 μm-100 μm.On this basis, described porous material skeleton is preferably made up of intermetallic Ni-Al compound porous material.In addition, described reforming catalyst is preferably at least made up of one or more metals in platinum, rhodium, iridium, palladium.As the improvement to this film filtering element, described film filtering element also comprises the rete be positioned on described matrix windward side, and the mean pore size of this rete is 1 μm-20 μm.In addition, described rete is preferably made up of intermetallic Ni-Al compound porous material.In above-mentioned intermetallic Ni-Al compound porous material, the weight ratio of nickel and aluminium is preferably 10:1 to 12:1.In above-mentioned film filtering element, the mean pore size of matrix is advisable at 20 μm-50 μm, and the mean pore size of rete is advisable at 3 μm-15 μm.
The preparation method of film filtering element, the step comprised is: 1) prepare the porous material skeleton that mean pore size is 50 μm-150 μm; 2) reforming catalyst precursor solution is prepared; 3) described porous material skeleton is put into precursor solution and flooded for some time; 4) the porous material skeleton being attached with precursor solution taken out and carry out drying and roasting, making reforming catalyst presoma deposit in porous material skeleton; 5) make reforming catalyst presoma change reforming catalyst into through chemical treatment, obtain by porous material skeleton and be attached to the matrix that the reforming catalyst in this porous material skeleton forms.Wherein, the blank sample of target product made a general reference in term " presoma ", namely just can the prime product of realize target product through some step.
Dipping ratio juris conventional in the preparation method of above-mentioned film filtering element and catalyst preparing is similar, has both been applicable to prepare noble metal catalyst class, and has also been applicable to and prepares non-precious metal catalyst class.If reforming catalyst belongs to noble metal catalyst, class (comprises single-metal reforming catalyst, as platinum catalyst etc., and two/multimetallic catalyst, as Pt Re catalyst etc.), the reforming catalyst presoma generated preferably directly by being calcination into required metal active constituent and unwanted volatiles in chemical treatment step, can certainly obtain required metal active constituent by method of reducing.If reforming catalyst belongs to non-precious metal catalyst class (as Cr
2o
3, MoO
3deng), the reforming catalyst presoma generated can obtain required metal oxide active component by method for oxidation in chemical treatment step, or directly by being calcination into required metal active constituent and unwanted volatiles in chemical treatment step.Need point out, for the preparation of reforming catalyst precursor solution, the dipping of porous material skeleton, the drying of material and roasting, and chemically treated concrete operations, those skilled in the art can be determined in conjunction with this area Conventional wisdom according to the pickling process in catalyst preparing.
To arrange rete on matrix windward side, in above-mentioned steps 5) after also to carry out following operation: form the slurry of rete be attached to matrix windward side by for sintering, and then carry out sintering and obtain rete.The concrete operations (comprising slurry preparation, sintering condition etc.) arranging rete are determined according to the preparation method of asymmetric membrane in sintered porous material preparation field.
Below in conjunction with the drawings and specific embodiments, the present invention is described further.The aspect that the application adds and advantage will part provide in the following description, and part will become obvious from the following description, or be recognized by the practice of the application.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of the application's catalytic reforming reactor.
Fig. 2 is the structural representation of the application's film filtering element.
Fig. 3 be in Fig. 2 A-A to sectional view.
Embodiment
As shown in Figure 1, catalytic reforming reactor comprises a membrane filter appts 100, this membrane filter appts 100 is provided with inlet mouth T1, venting port T2, slag-drip opening T3, and blowback medium entrance T4, described inlet mouth T1, venting port T2, slag-drip opening T3, blowback medium entrance T4 place are respectively equipped with control valve K1, K2, K3, K4, be provided with film filtering element 110 in the shell of membrane filter appts 100, the existence of this film filtering element 110 makes to define in membrane filter appts 100 two each other through space that this film filtering element 110 is kept apart.As shown in Figure 2, film filtering element 110 is wherein made up of matrix 111 and the rete 112 be positioned on this matrix 111 windward side, the thickness of matrix 111 is obviously greater than rete 112 thickness, and the mean pore size of matrix 111 is 20 μm-50 μm, and the mean pore size of rete 112 is 3 μm-15 μm.As shown in Figure 3, above-mentioned matrix 111 is made up of porous material skeleton 111a and the reforming catalyst 111b be attached in this porous material skeleton 111a again, wherein, reforming catalyst 111b is evenly distributed on the surface of porous material skeleton 111a and the inwall in duct substantially.Fig. 3 also image show in porous material skeleton 111a, adhere to reforming catalyst 111b after the reducing of 111c aperture, material duct: in Fig. 3, dotted line is original duct profile on porous material skeleton 111a, after attachment reforming catalyst 111b, the profile be illustrated by the broken lines is reduced, and the wall thickness therefore reduced can be considered the thickness of reforming catalyst 111b.
The catalytic reforming process of this catalytic reforming reactor is used to be: opening controlling valve K1, K2, closed control valve K3, K4, the oil gas that stock oil adds heat deflection enters membrane filter appts 100 from inlet mouth T1, and then the film filtering element 110 in this membrane filter appts 100, at this moment, oil gas is first by rete 112, the filtering accuracy of rete 112 is higher, most dusts in oil gas can be tackled and entered the dregs of fat, oil gas after filtration is again by matrix 111, this process fully contacts with the reforming catalyst 111b in matrix 111 and catalytic reforming reaction occurs, by setting matrix 111 thickness, filter pressure, the conditions such as filtration velocity also can control catalytic reforming reaction comparatively accurately, thus control the product of reforming reaction preferably.Oil gas after catalytic reforming exports from the venting port T2 of this membrane filter appts 100.After continuing for some time, closed control valve K1, K2, opening controlling valve K4, thus utilize blowback medium to regenerate film filtering element 110.When needing deslagging, open control valve K3, the dregs of fat export from the slag-drip opening T3 of this membrane filter appts 100.
Embodiment 1
Porous material skeleton 111a in film filtering element 110 and rete 112 are formed by intermetallic Ni-Al compound porous material, and reforming catalyst 111b is platinum catalyst.The preparation process of this film filtering element 110 is: first prepare by existing method the intermetallic Ni-Al compound porous material skeleton that mean pore size is 80 μm, in this intermetallic Ni-Al compound porous material skeleton, the weight ratio of nickel and aluminium is 11:1.Then platinum chloride is added solvating agent (available pure water, ethanol etc.) carry out dissolving thus prepare reforming catalyst precursor solution, in this precursor solution, the content of platinum is 1%(weight) (preferably choosing between 0.1%-2%), heating makes its temperature 60 DEG C (preferably choosing between 50-80 DEG C), and mix and blend is well rear stand-by.The intermetallic Ni-Al compound porous material skeleton prepared is put into precursor solution, and use gas to stir, soak about 1.5 hours, intermetallic Ni-Al compound porous material skeleton is taken out and dries, put into baking oven, dry 20 hours (preferably choosing between 6-48 hour) 120 DEG C (preferably choosing between 80-200 DEG C).Then the intermetallic Ni-Al compound porous material skeleton of oven dry is put into calcining furnace inherent 850 DEG C (preferably choosing between 500-1000 DEG C) and carry out calcining 4 hours after (preferably choosing between 2-8 hour), prepare matrix 111.Afterwards, previously prepd composite mortar (is mixed by nickel powder, aluminium powder and organic additive (at least one in ethanol, ethylene glycol, glycerine, polyoxyethylene glycol, polyvinyl alcohol), wherein, the weight ratio of nickel and aluminium is 11:1, the weight sum of nickel and aluminium and the weight ratio of organic additive are 1:1, the median size of nickel powder and aluminium powder is 2 μm) be sprayed on the windward side of matrix 111, then sintering obtains rete 112.
Embodiment 2
Porous material skeleton 111a in film filtering element 110 and rete 112 are formed by intermetallic Ni-Al compound porous material, and reforming catalyst 111b is Pt Re catalyst.The preparation process of this film filtering element 110 is: first prepare by existing method the intermetallic Ni-Al compound porous material skeleton that mean pore size is 100 μm, in this intermetallic Ni-Al compound porous material skeleton, the weight ratio of nickel and aluminium is 11:1.Then added in perrhenic acid solution by platinum chloride and prepare reforming catalyst precursor solution, in this precursor solution, the content of platinum is 0.8%(weight), the content of rhenium is 0.6%(weight), heating makes its temperature well rear stand-by at 75 DEG C of mix and blends.The intermetallic Ni-Al compound porous material skeleton prepared is put into precursor solution, and uses gas to stir, soak about 1.5 hours, intermetallic Ni-Al compound porous material skeleton is taken out and dries, put into baking oven, dry 15 hours at 150 DEG C.Then the intermetallic Ni-Al compound porous material skeleton of oven dry is put into inherent 900 DEG C of calcining furnace and carry out calcining after 5 hours, prepare matrix 111.Afterwards, previously prepd composite mortar (is mixed by nickel powder, aluminium powder and organic additive (at least one in ethanol, ethylene glycol, glycerine, polyoxyethylene glycol, polyvinyl alcohol), wherein, the weight ratio of nickel and aluminium is 11:1, the weight sum of nickel and aluminium and the weight ratio of organic additive are 1:1, the median size of nickel powder and aluminium powder is 2 μm) be sprayed on the windward side of matrix 111, then sintering obtains rete 112.
Embodiment 3
Porous material skeleton 111a in film filtering element 110 and rete 112 are formed by intermetallic Ni-Al compound porous material, and reforming catalyst 111b is MoO
3catalyzer.The preparation process of this film filtering element 110 is: first prepare by existing method the intermetallic Ni-Al compound porous material skeleton that mean pore size is 110 μm, in this intermetallic Ni-Al compound porous material skeleton, the weight ratio of nickel and aluminium is 12:1.Then added in pure water by ammonium molybdate and prepare reforming catalyst precursor solution (ammonium molybdate solution), in this precursor solution, the content of molybdenum is 2%(weight), heating makes its temperature well rear stand-by at 75 DEG C of mix and blends.The intermetallic Ni-Al compound porous material skeleton prepared is put into precursor solution, and uses gas to stir, soak about 2 hours, intermetallic Ni-Al compound porous material skeleton is taken out and dries, put into baking oven, dry 15 hours at 150 DEG C.Then the intermetallic Ni-Al compound porous material skeleton of oven dry is put into inherent 1000 DEG C of calcining furnace and carry out calcining after 5 hours, prepare matrix 111.Afterwards, previously prepd composite mortar (is mixed by nickel powder, aluminium powder and organic additive (at least one in ethanol, ethylene glycol, glycerine, polyoxyethylene glycol, polyvinyl alcohol), wherein, the weight ratio of nickel and aluminium is 11:1, the weight sum of nickel and aluminium and the weight ratio of organic additive are 1:1, the median size of nickel powder and aluminium powder is 2 μm) be sprayed on the windward side of matrix 111, then sintering obtains rete 112.
Use the film filtering element 110 of embodiment 1-3 to carry out the filter analogue test of petroleum naphtha, test method is carried out according to the catalytic reforming process described in the application's embodiment.Systems stay detects three kinds of film filtering elements 110 after running for some time, all do not find reforming catalyst coking phenomenon, and the reforming catalyst in three kinds of film filtering elements 110 does not run off substantially.
Claims (10)
1. catalytic reforming process, it is characterized in that: oil gas is passed into a membrane filter appts (100), when described oil gas passes through film filtering element (110) in this membrane filter appts (100), retain the filtration and the catalytic reforming that realize oil gas with katalysis by this film filtering element (110) simultaneously, oil gas after catalytic reforming exports from the venting port of this membrane filter appts (100), and the dregs of fat be trapped export from the slag-drip opening of this membrane filter appts (100); Wherein, described film filtering element (110) comprises by porous material skeleton (111a) and is attached to the matrix (111) that the reforming catalyst (111b) in this porous material skeleton (111a) forms, and the mean pore size of this matrix (111) is 1 μm-100 μm.
2. catalytic reforming process as claimed in claim 1, is characterized in that: described porous material skeleton (111a) is made up of intermetallic Ni-Al compound porous material.
3. catalytic reforming process as claimed in claim 1, is characterized in that: described reforming catalyst (111b) is at least made up of one or more metals in platinum, rhodium, iridium, palladium.
4. catalytic reforming process as claimed in claim 1, it is characterized in that: described film filtering element (110) also comprises the rete (112) be positioned on described matrix (111) windward side, the mean pore size of this rete (112) is 1 μm-20 μm.
5. catalytic reforming process as claimed in claim 4, is characterized in that: described rete (112) is made up of intermetallic Ni-Al compound porous material.
6. catalytic reforming reactor, comprise the membrane filter appts (100) being provided with inlet mouth, venting port and slag-drip opening, film filtering element (110) is installed in this membrane filter appts (100), it is characterized in that: described film filtering element (110) comprises by porous material skeleton (111a) and is attached to the matrix (111) that the reforming catalyst (111b) in this porous material skeleton (111a) forms, and the mean pore size of this matrix (111) is 1 μm-100 μm.
7. catalytic reforming reactor as claimed in claim 6, is characterized in that: described porous material skeleton (111a) is made up of intermetallic Ni-Al compound porous material.
8. catalytic reforming reactor as claimed in claim 6, is characterized in that: described reforming catalyst (111b) is at least made up of one or more metals in platinum, rhodium, iridium, palladium.
9. catalytic reforming reactor as claimed in claim 6, it is characterized in that: described film filtering element (110) also comprises the rete (112) be positioned on described matrix (111) windward side, the mean pore size of this rete (112) is 1 μm-20 μm.
10. catalytic reforming reactor as claimed in claim 9, is characterized in that: described rete (112) is made up of intermetallic Ni-Al compound porous material.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7060118B1 (en) * | 1998-07-21 | 2006-06-13 | Haldor Topse A/S | Synthesis gas production by steam reforming |
| CN101524609A (en) * | 2009-04-15 | 2009-09-09 | 成都易态科技有限公司 | Asymetric membrane FeAl intermetallic compound porosint filter element and application thereof |
| JP2011195393A (en) * | 2010-03-19 | 2011-10-06 | Jx Nippon Oil & Energy Corp | Membrane separation type reactor, membrane separation type hydrogen production apparatus and method for producing hydrogen |
-
2012
- 2012-10-31 CN CN201210427866.1A patent/CN102977914B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7060118B1 (en) * | 1998-07-21 | 2006-06-13 | Haldor Topse A/S | Synthesis gas production by steam reforming |
| CN101524609A (en) * | 2009-04-15 | 2009-09-09 | 成都易态科技有限公司 | Asymetric membrane FeAl intermetallic compound porosint filter element and application thereof |
| JP2011195393A (en) * | 2010-03-19 | 2011-10-06 | Jx Nippon Oil & Energy Corp | Membrane separation type reactor, membrane separation type hydrogen production apparatus and method for producing hydrogen |
Non-Patent Citations (1)
| Title |
|---|
| 焦炉煤气在透氧膜反应器中的重整机理;丁伟中等;《上海大学学报》;20110831;第17卷(第4期);第529-534页 * |
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