CN101433821A - Sorbent for reducing sulfur content in hydrocarbon oils - Google Patents
Sorbent for reducing sulfur content in hydrocarbon oils Download PDFInfo
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- CN101433821A CN101433821A CNA2007101774118A CN200710177411A CN101433821A CN 101433821 A CN101433821 A CN 101433821A CN A2007101774118 A CNA2007101774118 A CN A2007101774118A CN 200710177411 A CN200710177411 A CN 200710177411A CN 101433821 A CN101433821 A CN 101433821A
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Abstract
The invention relates to a sorbent for reducing sulfer content in hydrocarbon oil, which comprises 1 to 30 weight percent of rare earth faujasite, 5 to 40 weight percent of active metal oxide and 30 to 94 weight percent of carrier, wherein the carrier comprises alumina and zinc oxide. The mixture of the rare earth faujasite and the carrier is preformed into porous heat-resistant solid particles which are introduced with the metal active ingredient to prepare the sorbent; sulfer-containing light hydrocarbon oil raw material and hydrogen donors enter a reactor filled with the sorbent for separating reaction; materials and products after the separating reaction are sent to a subsequent separation system for product separation; sorbent to be regenerated after the reaction is burnt to be regenerated after steam stripping; and the regenerated sorbent is reduced by the hydrogen donors and returned to the reactor for recycling. The sorbent realizes deep removal of sulfer in the light hydrocarbon oil; meanwhile, the product gasoline has high octane number, low benzene content and high strength.
Description
Technical field
The invention belongs in a kind of adsorbent that reduces sulfur content in the light petroleum hydrocarbon and preparation thereof, application.
Background technology
Along with the pay attention to day by day of people, more and more stricter to the restriction of the sulfur content in the light hydrocarbon oil that acts as a fuel to environmental protection.With gasoline is example, and EPA (EPA) regulation sulphur limit value is 30 μ g/g (TierII); Europe requires content of sulfur in gasoline to be lower than 50 μ g/g (Europe IV discharge standard); China will be progressively in line with international standards also to the restriction of content of sulfur in gasoline.Thereby, the hydrocarbon ils deep desulfuration just can be meeted the requirements.
At present, the process for deep desulphurization of oil product is except that hydrogen addition technology, and the sulfur-containing compound that absorption method removes in the fuel oil also is a very attracting in recent years technology.As US6350422, US6955752, US6482314, US6428685, US6346190 is described, adopt adsorbent that light oil is faced H-H reaction absorption, the hydrogen consumption is lower, the desulfuration efficiency height, can the production sulfur content at following gasoline of 30 μ g/g or diesel oil, its adsorbent is by going back the ortho states cobalt, nickel, iron, manganese, copper, molybdenum, tungsten, silver, tin, in the vanadium metal one or both are stated from the carrier and constitute, described carrier adopts the zinc oxide oxide, the mixture of silica and aluminium oxide, zinc oxide accounts for 10～90 heavy % in the carrier, silica accounts for 5～85 heavy %, aluminium oxide accounts for 5～30 heavy %.Carrier component and metal component through mix, granulating, drying, calcining make bimetallic junction configuration desulfuration adsorbent, 0.7～2.1MPa, 343～413 ℃ with face the sulphur of catching under the operating condition of hydrogen in the gasoline, generate metal sulfide or utilize sulfide polarity to remove sulphur, the regeneration of sulfur-bearing catalyst circulation.Though above-mentioned patent has realized the deep desulfuration of hydrocarbon ils under the low hydrogen consumption, however the still slightly loss of its gasoline product octane number.
CN1261218C, CN1583973A, CN1583972A all adopt the zeolite desulfurizing agent to light-end products cracking desulfurization under conditions of non-hydrogen, selective cracking sulfide converts it into hydrocarbon and inorganic sulphide, no hydrogen consumption, no loss of octane number, but, the same with the mink cell focus catalytic cracking and desulfurizing, its desulfurization degree is influenced by feed sulphur content, catalyst property and conversion level etc., be not enough to realize deep desulfuration, desulfurization degree is generally at 50-80%, can only be used to produce the low-sulfur product oil, loss of octane number is low.
Summary of the invention
One of purpose of the present invention is that a kind of adsorbent that reduces sulfur content in hydrocarbon oils is provided on the basis of existing technology.
Two of purpose of the present invention provides described preparation of adsorbent method.
Three of purpose of the present invention provides a kind of method that described adsorbent reduces sulfur content in hydrocarbon oils of using.
The adsorbent of sulfur content comprises in the reduction hydrocarbon ils provided by the invention: the rare earth faujasite of the heavy % of 1-30, the carrier of the reactive metal oxides of 5～40 heavy % and 30～94 heavy % serves as to calculate benchmark with the adsorbent gross weight all.
Described rare earth faujasite accounts for the heavy % of 1-30 of adsorbent gross weight, preferred 3～20 heavy %.With the weight of rare earth faujasite serves as to calculate benchmark, rare earth faujasite composed as follows: rare earth is with RE
2O
3Meter accounts for the heavy % of 1-35; Faujasite accounts for the heavy % of 65-99.
Described rare earth all is selected from one or more elements among La, Ce, Pr, Nd, the Sm.
Described faujasite is that X type series zeolite is or/and Y type series zeolite.The preferred Y-type rare earth series zeolite of rare earth faujasite comprises one or more the mixture in REY type, REHY type, the REUSY type zeolite.
Described reactive metal oxides accounts for 5～40 heavy % of adsorbent total amount, the heavy % of preferred 15-30.Described reactive metal is selected from one or more metals in the transition metal such as cobalt, nickel, iron, manganese, copper, molybdenum, tungsten, silver, tin, vanadium, and preferred cobalt is or/and nickel.
Described carrier argillaceous 5～85 heavy %, preferred 35～80 heavy %.With the weight of carrier serves as to calculate benchmark, carrier composed as follows: aluminium oxide 5～30 heavy %, preferred 5～15 heavy %; Zinc oxide 10～65 heavy %, preferred 15～50 heavy %; Surplus is a clay.Described zinc oxide can adopt zinc oxide, also can adopt its presoma, comprises zinc hydroxide and zinc-containing metal salt such as zinc sulfate, zinc nitrate, zinc acetate, zinc halide and contains the zinc ammonium salt, contains zinc sodium salt etc.Described clay is selected from silica, amorphous aluminum silicide, natural porous carrier materials such as kaolin, halloysite, imvite, bentonite, diatomite, sepiolite, tires out one or more mixtures in the inorganic oxides such as taking off soil, preferred silica, kaolin, the tired mixture that takes off in the soil two or more, weight ratio between wherein any two kinds of clay compositions is 0.1～100:1, preferred 0.5～50:1.
Adsorbent preparation method provided by the invention is configured as the porous heat-resistant solid particle in advance with above-mentioned rare earth faujasite and carrier mixture, introduces the method for metal active constituent again on this solid particle.
The rare earth zeolite can mix formation mixture, dry forming, roasting more uniformly basically by any suitable mode with carrier mixture.Rare earth zeolite and carrier mixture preferred manufacturing procedure are sol-gel processes.
The present invention introduces the method for metal active constituent on solid particle, can adopt existing various metal oxide-loaded method, and the method as dipping promptly adopts above-mentioned one or more metal salt solutions to flood in type carrier; Perhaps Chen Dian method promptly adopts above-mentioned one or more metal salt solutions or its oxide, hydroxide to deposit on the porous heat-resistant carrier; Perhaps soild oxide and/or its precursor-slaine or its hydroxide and carrier mechanical mixture are ground or abrasive method not; Perhaps colloidal sol facture, gelling process and hydro-thermal method etc.Described slaine mainly is sulfate, nitrate, acetate, halide and metal ammonium salt, metal sodium salt of above-mentioned metal etc.The metal active constituent of adsorbent of the present invention adopts the form of slaine in preparation process, thereby the method for optimizing of introducing metal active constituent is the method for precipitation or the method for dipping.
Metal active constituent and carrier mixture thereof can adopt method moulding such as granulation, extrusion or spray-drying; Drying, roasting etc. after the moulding.Its baking temperature can be a room temperature to 400 ℃, is preferably 100～200 ℃, also can adopt microwave drying.Sintering temperature can be 400～1200 ℃, is preferably 500～800 ℃; Roasting time 0.5～100 hour is preferably 1～10 hour.
According to method provided by the present invention, the adsorbent preferred manufacturing procedure is as follows:
(1) rare earth faujasite colloidal sol preparation
With commercially available faujasite molecular sieve according to zeolite: the weight ratio of ammonium salt: deionized water=1:0～1:3～40 (preferred 1:1:20) is 50～100 ℃ of following ion-exchanges 0.1～5 hour, filters, washing back repeated exchanged once obtains ammonium type zeolite, its Na
2O content is not more than 0.15 heavy %.At room temperature the aqueous solution with above-mentioned ammonium type zeolite and metering rare earth chloride stirred dipping 2 hours, 120～200 ℃ of oven dry, and 450～850 ℃ of roastings 0.5～4 hour obtain with RE
2O
3The content of rare earth of meter is the faujasite of the heavy % of 1.0-35, the faujasite that makes mixed according to solid-liquid weight ratio 1:1～1:10 with decationized Y sieve water, and making beating, stirring makes faujasite colloidal sol;
(2) carrier colloidal sol preparation
The powder carrier material of reservation amount or the solid sediment of carrier are mixed making beating with deionized water, obtain the slurries that solid content is 5～30 weight %, the aqueous solution that under agitation adds hydrochloric acid or nitric acid, make slurries pH=2～4, stir, under 30～100 ℃, leave standstill and made carrier colloidal sol at least in aging 0.5 hour;
(3) solid particle preparation
With step (1) and step (2) make aging after carrier colloidal sol mixes, and add an amount of aluminium colloidal sol, adsorbent solid content and aluminium colloidal sol solid content (in aluminium oxide) weight ratio are 10～50, continue stirring up to the formation uniform sol; Is 250～300 ℃ with this colloidal sol at the control exhaust temperature, and atomisation pressure is 50～60 atmospheric pressure, and spray drying forming makes microspheric solid carrier particle.Free Na is removed in the microspheroidal solid particle washing that obtains
+, 100～200 ℃ of down oven dry after at least 2 hours, roasting at least 2 hours under 500～800 ℃ of conditions again obtains the particle of microspheroidal rare earth faujasite and carrier mixture;
(4) the metal oxide active component is introduced
One or more slaine of the containing metal active component of reservation amount is made into the aqueous solution that concentration of metal ions is 1～10mol/L, at room temperature add the microspheroidal rare earth faujasite that step (3) makes and the particle of carrier mixture according to the ratio of metal oxide and carrier, add the ammoniacal liquor that concentration is 0.5～5mol/L while stirring, keeping pH is 7～10, constantly be stirred to precipitation fully after, being warming up to 60～100 ℃ also placed aging 0.5 hour at least, filter, washing leaching cake is to there not being the mixture that acid ion makes metal hydroxides rare earth faujasite and carrier material, after drying at least 2 hours under 100～200 ℃, roasting at least 2 hours under 500～800 ℃ of conditions is again pulverized, sieve and obtain the microspheroidal absorbent particles.
The above-mentioned oxidation state reactive metal adsorbent that makes adopts the specific method activation processing before use, makes the oxidation state reactive metal be converted into the zero-valent state reactive metal.Processing method provided by the invention is that the reducing agent that adopt to be fit to such as hydrogen etc. make above-mentioned adsorbent activity metal precursor 200～400 ℃ temperature, reduction is at least 30 minutes under the hydrogen partial pressure 0.5-2.5MPa condition, contains the adsorbent composition of zero-valent state reactive metal basically thereby produce.
Adsorbent used in the present invention is preferably microspheroidal for ease of fluidisation, and its average grain diameter is at 40-200 μ m, and its abrasion index is preferably less than 2.5%h
-1
The method of reduction sulfur content of light hydrocarbon oil provided by the invention is:
Sulfur-bearing light hydrocarbon oil raw material and hydrogen donor after the preheating enter in the reactor that adsorbent is housed, at temperature 350-450 ℃, and pressure 0.5-2.5MPa, feedstock oil weight (hourly) space velocity (WHSV) 0.5-10h
-1, preferred 4-8h
-1The weight ratio 1-20 of adsorbent total amount and hydrocarbon oil crude material, react under the condition of preferred 5-15, material behind the separating reaction, product is sent into subsequent separation system and is carried out the product separation, reacted adsorbent to be generated coke burning regeneration behind stripping, the adsorbent after regeneration Returning reactor after the hydrogen donor reduction recycles.
The hydrocarbon oil crude material of described sulfur-bearing is selected from one or more the mixture in gasoline, kerosene, diesel oil, the gas oil fraction, and preferred gasoline is or/and diesel oil.Above-mentioned gasoline, kerosene, diesel oil, gas oil fraction are that its full cut is or/and its part narrow fraction.The hydrocarbon oil crude material sulfur content of described sulfur-bearing is preferably in more than the 500 μ g/g more than 100 μ g/g.
Described hydrogen donor is selected from one or more the mixture in hydrogen, hydrogen-containing gas, the hydrogen supply agent, wherein hydrogen is the hydrogen of various purity, the mixture of one or more in hydrogen-containing gas dry gas that preferred this method is produced, catalytic cracking (FCC) dry gas, coking dry gas, the thermal cracking dry gas, more than the hydrogeneous best 30 volume %, hydrogen supply agent is selected from one or more the mixture in naphthane, decahydronaphthalene, the dihydro indenes.
Described reactor can adopt the reactor of fluidized-bed reactor, fixed bed reactors, moving-burden bed reactor or other type and compound, the preferred streams fluidized bed reactor comprises in fixed fluidized bed, dispersion fluidized bed, bubbling bed, turbulent bed, fast bed, conveying bed, the dense-phase fluidized bed one or more.
The present invention compared with prior art has following unforeseeable technique effect:
1, adsorbent provided by the invention is made up of inorganic oxides such as going back metals such as ortho states cobalt, nickel, rare earth faujasite, zinc oxide and silica, aluminium oxide, kaolin, the adsorbent that adopts sol-gel process to make, characteristics such as it is desulphurizing activated good to have, and adsorbent is evenly distributed, and intensity is good;
2, the preferred cobalt of adsorbent provided by the invention, the ortho states of going back of one or both metals in the nickel is an active component, preferred silica, aluminium oxide, the above mixture of in the kaolin two or three is a carrier, add a certain amount of rare earth faujasite, by the cooperative effect between these components, make when this adsorbent is realized in deep removal light hydrocarbon oil sulfide, kept higher liquid to receive, during in particular for gasoline desulfur, compared with prior art, the product octane number is higher, and its benzene content is lower, and adsorbent provided by the invention is suitable for production super-low sulfur clean gasoline.
When 3, adopting method provided by the present invention to handle gasoline stocks, can even not have under the condition of hydrogen consumption and realize deep desulfuration in low hydrogen consumption, the removal efficiency of sulphur can reach more than the 97 heavy %, can be used for the production sulfur content be lower than 10 μ g/g's and improved octane number when having reduced gasoline olefin, the yield of gasoline is more than the 98 heavy %, the product benzene content in gasoline is low, can be used for the high-octane rating clean gasoline that the production sulfur content is lower than 10 μ g/g.
When 4, adopting method provided by the present invention to handle diesel raw material, facing under the condition of hydrogen, diesel raw material has desulfurized effect preferably, and desulfurization degree reaches more than the 99 heavy %.The aromatic content of diesel oil Cetane number of producing slightly improves.
Description of drawings
Accompanying drawing is that hydrocarbon ils provided by the invention faces the method flow schematic diagram that the hydrogen adsoption catalysis transforms desulfurization in fluidized-bed reactor.
The specific embodiment
Below in conjunction with accompanying drawing method provided by the invention is given further instruction, but therefore do not make the present invention be subjected to any restriction.
Accompanying drawing is that hydrocarbon ils provided by the invention faces the method flow schematic diagram that the hydrogen adsoption catalysis transforms desulfurization in fluidized-bed reactor.Accompanying drawing adopts a fluidized-bed reactor, a regenerator and a regenerative agent reductor.Described regenerator, regenerative agent reductor are fluid bed.
Gasoline fraction raw material after the preheating and hydrogen donor enter carrier pipe 2 bottoms through pipeline 1, and contact from the adsorbent after the regeneration of regenerator sloped tube 17, and at temperature 350-450 ℃, pressure 0.5-2.5MPa, feedstock oil weight (hourly) space velocity (WHSV) 0.5-10h
-1, preferred 4-8h
-1The weight ratio 1-20 of adsorbent total amount and hydrocarbon oil crude material reacts under the condition of preferred 3-15, and reactant flows to into the settler 7 that has the dense fluidized bed bioreactor, and reaction oil gas is sent into follow-up product piece-rate system through pipeline 8.Adsorbent to be generated enters stripper 3, by from the entrained reaction oil gas of the steam stripping of pipeline 4 adsorbent to be generated, spent agent behind the stripping enters regenerator 13 through inclined tube 5 to be generated, oxygen-containing gas is introduced regenerator 13 through pipeline 14, desulfurizing agent to be generated is coke burning regeneration under the effect of oxygen-containing gas, regenerated flue gas is drawn regenerator through pipeline 12, the reproducing adsorbent of high temperature enters regenerative agent reductor 16 through pipeline 15, adopt the nitrogen stripping, after the cooling, with hydrogen reducing, desulfurizing agent after the reduction returns carrier pipe 2 bottom cycle by regenerator sloped tube 17 and uses, and loosening wind nitrogen enters regenerative agent reductor 16 through pipeline 18.
The following examples will give further instruction to method provided by the invention, but therefore not make the present invention be subjected to any restriction.
Employed feedstock property is listed in table 1 among the embodiment.Zeolite and carrier mixture solid particle adopt sol-gel process to produce.
The composition of adsorbent adopts x ray fluorescence spectrometry (RIPP 134-90 sees Science Press's " petrochemical industry analytical method (RIPP test method) ").Wherein the mensuration of adsorbent attrition rate adopts RIPP 29-90 method, with compressed air as fluidizing agent, pressure 0.6MPa, 20 liters/minute of flows are measured adsorbent hourly average abrasion index.
Present embodiment adopts being prepared as follows of adsorbent solids particle:
The primary raw material of carrier that present embodiment adopts is as follows:
1
#Carrier: (solid content is 64 heavy % to 10 kilograms of boehmites, Shandong Zibo aluminium manufacturer industrial products, down together)+(solid content is 25 weight % to 1.0 kilograms of Ludox, produces in upright sail chemical plant, Qingdao, down together)+13.1 kilograms of zinc oxide (purity 99.7%, the outstanding waffle worker in Cangzhou Co., Ltd product);
2
#Carrier: 4 kilograms of boehmite+1.0 kilogram Ludox+6 kilograms of kaolin (solid content is 73 weight %, and the industry of Suzhou china clay company is produced)+10 kg of hydrogen zinc oxide (zinc oxide content 71.5%, Pei County zinc oxide factory product);
3
#Carrier: 5 kilograms of boehmite+4 kilogram kaolin+2 kilograms of tired soil (solid content is 68 weight %, and Zhongxiang City, Hubei produces)+3.5 kilo sulfuric acid zinc (purity 98%, sea, Jinan chemical industry Co., Ltd product) that take off;
The above-mentioned support material that will mix is respectively mixed making beating with deionized water, obtain the slurries that solid content is 15 weight %, under agitation adds 1.6 kilograms aqueous hydrochloric acid solution (volumetric concentration 30%), continues to stir, and up to forming uniform sol, makes 1 respectively
#, 2
#, 3
#Carrier colloidal sol, stand-by.
8.0 kilograms of NaY zeolite molecular sieves (silica alumina ratio 3.5) that Qilu Petrochemical company catalyst plant is produced, 3.0 kilograms of HY zeolite molecular sieves (silica alumina ratio 3.8), 6.0 kilograms of 13X zeolite molecular sieves (silica alumina ratio 2.3) are according to zeolite respectively: the weight ratio of ammonium nitrate: deionized water=1:1:20 was 90 ℃ of following ion-exchanges 2 hours, filter, wash the back repeated exchanged and once obtain ammonium type shape-selective molecular sieve, its Na
2O content is not more than 0.15 heavy %.At room temperature with above-mentioned ammonium type zeolite molecular sieve respectively with 0.38 kilogram, 2.31 kilograms, 7.85 rare earth chlorides (Baotou rare earth factory in the Inner Mongol produces, dry basis 48 heavy %, wherein the contents on dry basis of each component is La
2O
325.0%, Ce
2O
36.0%, Pr
2O
35.0%, Nd
2O
310.0%) aqueous solution of preparation stirred dipping 2 hours, 120 ℃ of oven dry, and 550 ℃ of roastings 2 hours make REY, REHY, REX molecular sieve.The rare earth containing zeolite that makes is mixed according to solid-liquid weight ratio 1:1～1:10 with decationized Y sieve water, making beating, stirring makes rare earth containing zeolite colloidal sol.
The above-mentioned REY that makes, REHY, REX phosphorus modified RE faujasite colloidal sol are respectively with above-mentioned 1
#, 2
#, 3
#Carrier colloidal sol mixes, and adds an amount of aluminium colloidal sol, and adsorbent solid content and aluminium colloidal sol solid content (in aluminium oxide) weight ratio are 15, continues to stir up to forming uniform sol; Is 250～300 ℃ with this colloidal sol at the control exhaust temperature, and atomisation pressure is 50～60 atmospheric pressure, and spray drying forming makes the solid particle of the microspheric REY of containing, REHY, REX.Free Na is removed in the microspheroidal solid particle washing that obtains
+, 100～200 ℃ of down oven dry after at least 2 hours, roasting at least 2 hours under 500～800 ℃ of conditions again obtains microspheroidal REY/1
#, REHY/2
#, REX/3
#Solid particle.
Embodiment 1-3
Embodiment 1-3 explanation contains adsorbent composition, the preparation method of rare earth faujasite.
Respectively Zhangjagang City China adopted chemical industry Co., Ltd is produced 7.5 kilograms of nickel chlorides, reach each metal salt mixture of 8.5 kilograms of cobalt nitrate and nickel nitrate and be made into the aqueous solution that concentration of metal ions is 1～10mol/L, stand-by.
At room temperature with nickel chloride aqueous solution and REY/1
#Carrier mixes, add the ammoniacal liquor that concentration is 3mol/L while stirring, keeping pH is 7～10, constantly be stirred to precipitation fully after, being warming up to 90 ℃ also placed aging 0.5 hour at least, filter, washing leaching cake is washed to no chlorion to there not being the mixture that acid ion makes nickel hydroxide and REY and alumina supporting material.100～200 ℃ of down oven dry after at least 2 hours, roasting at least 2 hours under 500～800 ℃ of conditions is again pulverized, sieving obtains microspheroidal adsorbent Ni-Zn/REY/1
#, called after YS-1.
At room temperature the aqueous solution saturation with cobalt nitrate and nickel nitrate floods REHY/2
#Carrier constantly stirred dipping after at least 4 hours, and 100～200 ℃ of oven dry at least 2 hours down, roasting at least 2 hours under 500～800 ℃ of conditions is again pulverized, sieving obtains microspheroidal adsorbent Co-Ni-Zn/REHY/2
#, called after YS-2.
With 7.3 kilograms of cobalt oxides (Zhangjagang City China adopted chemical industry Co., Ltd product) and REX/3
#Rare earth faujasite/carrier granular adds the making beating of 60 kg of water; Perhaps cobalt oxide is pulled an oar separately the back directly with REX zeolite sol and 3
#Carrier colloidal sol mixes, and after stirring, adds an amount of aluminium colloidal sol, and adsorbent solid content and aluminium colloidal sol solid content (in aluminium oxide) weight ratio are 15, continues to stir up to forming uniform sol; Is 250～300 ℃ with this colloidal sol at the control exhaust temperature, and atomisation pressure is 50～60 atmospheric pressure, and spray drying forming makes the microspheric solid particle that contains cobalt oxide and REX.Wash its solid particle and remove free Na
+After, 100～200 ℃ of down oven dry at least 2 hours, roasting at least 2 hours under 500～800 ℃ of conditions again obtains microspheroidal adsorbent Co-Zn/REX/3
#, called after XS-3.
The composition of adsorbent YS-1, YS-2, XS-3 (each component serves as to calculate benchmark with the gross weight of adsorbent all) and polishing machine see Table 2.
Comparative Examples 1-3
Compare with the adsorbent composition of embodiment 1-3, the explanation of this Comparative Examples does not contain composition, conventional preparation method and the performance of the adsorbent of rare earth faujasite.
According to 1
#, 2
#, 3
#Carrier is formed wet mixing, grinds, and dry forming, roasting (drying, method of roasting are with embodiment 1-3), the impregnating metal ion concentration is the nickel sulfate solution of 1～10mol/L respectively again, the cobalt nitrate-nickel nitrate mixed aqueous solution and the cobalt acetate aqueous solution.Oven dry, roasting once more, the microspheroidal adsorbent Ni-Zn/1 that pulverizes, sieves and do not contained rare earth faujasite
#, Co-Ni-Zn/2
#, Co-Zn/3
#, difference called after S-4, S-5, S-6.It is formed and polishing machine is listed in table 2.
As can be seen from Table 2, adsorbent YS-1, YS-2, XS-3 intensity are all better, and its wear rate is all less than 1.0%h
-1More than, all greater than adsorbent S-4, the S-5, the S-6 that do not contain rare earth faujasite that adopt the conventional method preparation.
Embodiment 4-5
Embodiment 4-5 explanation contains the adsorbent of rare earth faujasite and uses aspect gasoline desulfur.
With the feed gasoline A in the table 1, B is raw material, and investigation feed gasoline raw material fully contacts with adsorbent YS-1, YS-2 respectively in the small-sized fluidized bed reactor and adsorbs and the catalyzed conversion situation.Adsorbent loadings 500 gram adopts hydrogen 360 ℃ temperature before use, and reduction is 60 minutes under the condition that hydrogen flowing quantity is 1.5 liters/hour.Product, steam and adsorbent mixtures to be generated separate in settler, and reaction product isolated obtains gaseous product and product liquid, and adsorbent to be generated is gone out the hydrocarbon product that adsorbs on the adsorbent mixtures to be generated by the water vapour stripping.Adsorbent behind the stripping contacts with the air that heated regenerates, and the catalyst mixture after the regeneration recycles behind cooling, hydrogen reducing.Experimental condition, result of the test and product gasoline property and sulfur content thereof are all listed in table 3.
Comparative Examples 4-5
Compare with the adsorbent application test of embodiment 4-5, the explanation of this Comparative Examples does not contain the adsorbent S-4 of rare earth faujasite, the situation that S-5 is used for gasoline desulfur.
Feed gasoline A, B contact with adsorbent S-4, S-5 behind the hydrogen reducing respectively in the small-sized fluidized bed reactor and react.Other test technology conditions and test method are with embodiment 4～5.Experimental condition, result of the test and product gasoline property and sulfur content thereof are all listed in table 3.
As can be seen from Table 3, with the gasoline desulfur product oil phase contrast that does not add the faujasite adsorbent, add the gasoline desulfur rate height of phosphorous faujasite adsorbent, all more than 97.11 heavy %; Octane number is higher, all is higher than feedstock oil; And its benzene content is lower, all is lower than feedstock oil.
Embodiment 6-7
Embodiment 6-7 illustrates that the adsorbent that contains rare earth faujasite is used for the situation of diesel fuel desulfurization.
With raw material diesel oil C, D in the table 1 is raw material, and the investigation diesel raw material fully contacts with adsorbent YS-2, XS-3 respectively in the small-sized fluidized bed reactor adsorbs and the catalyzed conversion situation.Adsorbent loadings 500 gram adopts hydrogen 360 ℃ temperature before use, and reduction is 60 minutes under the condition that hydrogen flowing quantity is 1.5 liters/hour.Product, steam and adsorbent mixtures to be generated separate in settler, and reaction product isolated obtains gaseous product and product liquid, and adsorbent to be generated is gone out the hydrocarbon product that adsorbs on the adsorbent mixtures to be generated by the water vapour stripping.Adsorbent behind the stripping contacts with the air that heated regenerates, and the catalyst mixture after the regeneration recycles behind cooling, hydrogen reducing.Experimental condition, result of the test and product diesel oil character and sulfur content thereof are all listed in table 4.
Comparative Examples 6-7
Compare with the adsorbent application test of embodiment 6-7, the explanation of this Comparative Examples does not contain the adsorbent S-5 of rare earth faujasite, the situation that S-6 is used for diesel fuel desulfurization.
Raw material diesel oil C, D contact with adsorbent S-5, S-6 behind the hydrogen reducing respectively in the small-sized fluidized bed reactor and react.Other test technology conditions and test method are with embodiment 4～5.Experimental condition, result of the test and product diesel oil character and sulfur content thereof are all listed in table 4.
As can be seen from Table 4, with the diesel fuel desulfurization product oil phase contrast that does not add the faujasite adsorbent, the diesel fuel desulfurization rate of adsorbent that adds phosphorous faujasite is higher, all more than 98.99 heavy %; Diesel cetane-number is higher, all is higher than feedstock oil.
Table 1
| The raw material numbering | A | B | C | D |
| Type of feed | Gasoline | Gasoline | Diesel oil | Diesel oil |
| Density (20 ℃), kilogram/rice 3 | 787.5 | 708.3 | 886.8 | 911.6 |
| Octane number | ||||
| RON | 89.8 | 93.6 | - | - |
| MON | 78.8 | 79.4 | - | - |
| Cetane number | - | - | 29.5 | 22.0 |
| Sulphur, μ g/g | 1696.5 | 124.6 | 1060 | 10267.6 |
| Alkali nitrogen, μ g/g | 92.4 | 73.6 | 682 | 878.7 |
| Carbon, heavy % | 86.28 | 86.46 | 88.24 | 87.68 |
| Hydrogen, heavy % | 12.98 | 13.15 | 11.48 | 10.80 |
| Alkene, heavy % | 24.8 | 32.5 | 2.1 | 1.9 |
| Aromatic hydrocarbons, heavy % | 19.4 | 17.1 | 22.5 | 24.6 |
| Benzene, heavy % | 3.6 | 2.5 | - | - |
| Boiling range, ℃ | ||||
| Initial boiling point | 90 | 62 | 191 | 195 |
| 10％ | 92 | 75 | 208 | 234 |
| 30％ | 121 | 89 | 226 | 267 |
| 50％ | 154 | 112 | 247 | 298 |
| 70％ | 175 | 141 | 277 | 328 |
| 90％ | 189 | 173 | 324 | 358 |
| The end point of distillation | 203 | 202 | 361 | 374 |
Table 2
| |
Comparative Examples 1 | |
Comparative Examples 2 | |
Comparative Examples 3 | |
| The adsorbent numbering | YS-1 | S-4 | YS-2 | S-5 | XS-3 | S-6 |
| SiO 2, heavy % | 2.1 | 1.18 | 17.4 | 22.19 | 14.7 | 25.59 |
| Al 2O 3, heavy % | 29.0 | 29.43 | 15.6 | 17.75 | 17.5 | 31.29 |
| ZnO, heavy % | 54.0 | 59.39 | 32.5 | 40.06 | 4.7 | 8.13 |
| Reactive metal oxides, heavy % | NiO/10 | NiO/10 | CoO/10 NiO/10 | CoO/10 NiO/10 | CoO/35 | CoO/35 |
| Rare earth, heavy % | 0.06 | - | 2.5 | - | 6.1 | - |
| Zeolite, heavy % | Y /4.84 | - | HY /12.0 | - | 13X/22.0 | - |
| Wear rate, %h -1 | 0.8 | 1.4 | 1.0 | 1.6 | 1.2 | 2.1 |
Table 3
| |
Comparative Examples 4 | |
Comparative Examples 5 | |
| Adsorbent | YS-1 | S-4 | YS-2 | S-5 |
| Feedstock oil | B | B | A | A |
| Medium | Dry gas | Dry gas | H 2 | H 2 |
| Reaction condition | ||||
| Temperature, ℃ | 370 | 370 | 425 | 425 |
| Pressure, MPa | 2.0 | 2.0 | 1.0 | 1.0 |
| The gasoline weight (hourly) space velocity (WHSV), |
4 | 4 | 8 | 8 |
| |
5 | 5 | 10 | 10 |
| Hydrogen and gasoline volume ratio | 300 | 300 | 500 | 500 |
| Product distributes, heavy % | ||||
| Gas | 0.15 | 0.56 | 0.18 | 0.49 |
| Gasoline | 99.49 | 99.14 | 99.5 | 99.1 |
| Diesel oil | 0.18 | 0.15 | 0.15 | 0.15 |
| Coke | 0.17 | 0.14 | 0.16 | 0.24 |
| Loss | 0.01 | 0.01 | 0.01 | 0.02 |
| The gasoline main character | ||||
| RON | 94.5 | 88.3 | 90.9 | 83.4 |
| MON | 80.4 | 74.1 | 79.8 | 72.8 |
| Sulphur, μ g/g | 3.6 | 36.2 | 8.2 | 23.1 |
| Alkali nitrogen, μ g/g | 5.6 | 9.8 | 8.7 | 10.2 |
| Benzene, heavy % | 1.1 | 2.4 | 0.7 | 3.5 |
| Alkene, heavy % | 24.7 | 26.5 | 15.5 | 20.34 |
| Desulfurization degree, heavy % | 97.11 | 70.95 | 99.52 | 98.64 |
Table 4
| Embodiment 6 | Comparative Examples 6 | Embodiment 7 | Comparative Examples 7 | |
| Adsorbent | YS-2 | S-5 | XS-3 | S-6 |
| Feedstock oil | C | C | D | D |
| Reaction condition | ||||
| Temperature, ℃ | 400 | 400 | 450 | 450 |
| Pressure, MPa | 0.5 | 0.5 | 2.5 | 2.5 |
| The diesel oil weight (hourly) space velocity (WHSV), hour -1 | 10 | 3.0 | 0.5 | 50 |
| Oil ratio | 20 | 15 | 1 | 8 |
| The volume ratio of hydrogen donor and diesel raw material | Naphthane/0.1 | Naphthane/0.1 | Coking dry gas/500 | Coking dry gas/500 |
| Product distributes, heavy % | ||||
| Dry gas | 0.19 | 0.34 | 0.22 | 0.28 |
| Liquefied gas | 0.28 | 0.32 | 0.65 | 0.87 |
| Gasoline | 1.65 | 1.24 | 2.92 | 1.15 |
| Diesel oil | 97.5 | 97.52 | 95.71 | 97.04 |
| Coke | 0.36 | 0.56 | 0.48 | 0.64 |
| Loss | 0.02 | 0.02 | 0.02 | 0.02 |
| The diesel oil main character | ||||
| Sulphur, μ g/g | 9.8 | 17.3 | 103.4 | 165.0 |
| Desulfurization degree, heavy % | 99.08 | 98.37 | 98.99 | 98.39 |
| Density (20 ℃), kilogram/rice 3 | 877.8 | 878.2 | 887.9 | 893.2 |
| Cetane number | 31.8 | 28.0 | 25.0 | 21.2 |
Claims (14)
1, a kind of adsorbent that reduces sulfur content in hydrocarbon oils, it is characterized in that, serve as to calculate benchmark with the adsorbent gross weight, and this adsorbent comprises: the rare earth faujasite of the heavy % of 1-30, the carrier of the reactive metal oxides of 5～40 heavy % and 30～94 heavy %, wherein carrier comprises aluminium oxide and zinc oxide.
2, according to the adsorbent of claim 1, it is characterized in that, serves as to calculate benchmark with the weight of rare earth faujasite, rare earth faujasite composed as follows: rare earth is with RE
2O
3Meter accounts for the heavy % of 1-35; Faujasite accounts for the heavy % of 65-99.
3,, it is characterized in that described rare earth faujasite is that X type series zeolite is or/and Y type series zeolite according to the adsorbent of claim 1 or 2.
4,, it is characterized in that described rare earth Y type zeolite is selected from one or more in REY type, REHY type, the REUSY type zeolite according to the adsorbent of claim 3.
5,, it is characterized in that described rare earth faujasite is a rare earth Y type zeolite according to the adsorbent of claim 1.
6,, it is characterized in that described reactive metal is selected from one or more metals in cobalt, nickel, iron, manganese, copper, molybdenum, tungsten, silver, tin, the vanadium according to the adsorbent of claim 1.
7,, it is characterized in that described reactive metal is that cobalt is or/and nickel according to the adsorbent of claim 1.
8, according to the adsorbent of claim 1, it is characterized in that, serves as to calculate benchmark with the weight of carrier, and described carrier comprises the aluminium oxide of 5～30 heavy %, the zinc oxide of 10～65 heavy %, the clay of surplus.
9,, it is characterized in that described clay is selected from silica, amorphous aluminum silicide, kaolin, halloysite, imvite, bentonite, diatomite, sepiolite, tired one or more mixtures that take off in the soil according to the adsorbent of claim 1.
10, a kind of method for preparing the described adsorbent of claim 1 is characterized in that this method comprises the following steps:
(1) rare earth faujasite colloidal sol preparation
With commercially available faujasite molecular sieve according to zeolite: the weight ratio of ammonium salt: deionized water=1:0～1:3～40 is 50～100 ℃ of following ion-exchanges 0.1～5 hour, filters, washing back repeated exchanged once obtains ammonium type zeolite, its Na
2O content is not more than 0.15 heavy %.At room temperature the aqueous solution with above-mentioned ammonium type zeolite and metering rare earth chloride stirred dipping 2 hours, 120～200 ℃ of oven dry, and 450～850 ℃ of roastings 0.5～4 hour obtain with RE
2O
3The content of rare earth of meter is the faujasite of the heavy % of 1.0-35, the faujasite that makes mixed according to solid-liquid weight ratio 1:1～1:10 with decationized Y sieve water, and making beating, stirring makes faujasite colloidal sol;
(2) carrier colloidal sol preparation
The powder carrier material of reservation amount or the solid sediment of carrier are mixed making beating with deionized water, obtain the slurries that solid content is 5～30 weight %, the aqueous solution that under agitation adds hydrochloric acid or nitric acid, make slurries pH=2～4, stir, under 30～100 ℃, leave standstill and made carrier colloidal sol at least in aging 0.5 hour;
(3) solid particle preparation
With step (1) and step (2) make aging after carrier colloidal sol mixes, and add an amount of aluminium colloidal sol, adsorbent solid content and aluminium colloidal sol solid content weight ratio are 10～50, continue stirring up to the formation uniform sol; Is 250～300 ℃ with this colloidal sol at the control exhaust temperature, and atomisation pressure is 50～60 atmospheric pressure, and spray drying forming makes microspheric solid carrier particle.Free Na is removed in the microspheroidal solid particle washing that obtains
+, 100～200 ℃ of down oven dry after at least 2 hours, roasting at least 2 hours under 500～800 ℃ of conditions again obtains the particle of microspheroidal rare earth faujasite and carrier mixture;
(4) the metal oxide active component is introduced
One or more slaine of the containing metal active component of reservation amount is made into the aqueous solution that concentration of metal ions is 1～10mol/L, at room temperature add the microspheroidal rare earth faujasite that step (3) makes and the particle of carrier mixture according to the ratio of metal oxide and carrier, add the ammoniacal liquor that concentration is 0.5～5mol/L while stirring, keeping pH is 7～10, constantly be stirred to precipitation fully after, being warming up to 60～100 ℃ also placed aging 0.5 hour at least, filter, washing leaching cake is to there not being the mixture that acid ion makes metal hydroxides rare earth faujasite and carrier material, after drying at least 2 hours under 100～200 ℃, roasting at least 2 hours under 500～800 ℃ of conditions is again pulverized, sieve and obtain the microspheroidal absorbent particles.
11, a kind of application rights requires 1 described adsorbent to reduce the method for sulfur content in hydrocarbon oils, it is characterized in that sulfur-bearing light hydrocarbon oil raw material and hydrogen donor after the preheating, enter in the reactor that adsorbent is housed, at temperature 350-450 ℃, pressure 0.5-2.5MPa, feedstock oil weight (hourly) space velocity (WHSV) 0.5-10h
-1React under the condition of the weight ratio 1-20 of adsorbent total amount and hydrocarbon oil crude material, material behind the separating reaction, product is sent into subsequent separation system and is carried out the product separation, reacted adsorbent to be generated coke burning regeneration behind stripping, the adsorbent after regeneration Returning reactor after the hydrogen donor reduction recycles.
12, according to the method for claim 11, the hydrocarbon oil crude material that it is characterized in that described sulfur-bearing is selected from one or more the mixture in gasoline, kerosene, diesel oil, the gas oil fraction.
13, according to the method for claim 11, it is characterized in that described hydrogen donor is selected from one or more the mixture in hydrogen, hydrogen-containing gas, the hydrogen supply agent, wherein hydrogen is the hydrogen of various purity, hydrogen-containing gas is one or more the mixture in dry gas that this method is produced, catalytic cracked dry gas, coking dry gas, the thermal cracking dry gas, and hydrogen supply agent is selected from one or more the mixture in naphthane, decahydronaphthalene, the dihydro indenes.
14,, it is characterized in that described reactor is selected from the reactor of fluidized-bed reactor, fixed bed reactors, moving-burden bed reactor or other type and compound according to the method for claim 11.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102895946A (en) * | 2011-07-28 | 2013-01-30 | 中国石油化工股份有限公司 | Hydrocarbon oil desulphurization adsorbent, and preparation method and application thereof |
| US9446381B2 (en) | 2011-07-28 | 2016-09-20 | China Petroleum & Chemical Corporation | Hydrocarbon oil desulfurization adsorbing agent, production and use thereof |
| CN106853973A (en) * | 2015-12-08 | 2017-06-16 | 中国石油天然气股份有限公司 | A kind of method for preparing highly acid Y type molecular sieve |
| CN109718833A (en) * | 2017-10-30 | 2019-05-07 | 中国石油化工股份有限公司 | Modified molecular screen and its preparation method and application |
| CN111514849A (en) * | 2020-04-26 | 2020-08-11 | 东营科尔特新材料有限公司 | Dechlorination adsorbent, preparation method and regeneration method thereof and application of dechlorination adsorbent to organic chlorine |
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2007
- 2007-11-15 CN CN 200710177411 patent/CN101433821B/en active Active
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102895946A (en) * | 2011-07-28 | 2013-01-30 | 中国石油化工股份有限公司 | Hydrocarbon oil desulphurization adsorbent, and preparation method and application thereof |
| US9446381B2 (en) | 2011-07-28 | 2016-09-20 | China Petroleum & Chemical Corporation | Hydrocarbon oil desulfurization adsorbing agent, production and use thereof |
| CN106853973A (en) * | 2015-12-08 | 2017-06-16 | 中国石油天然气股份有限公司 | A kind of method for preparing highly acid Y type molecular sieve |
| CN106853973B (en) * | 2015-12-08 | 2019-08-06 | 中国石油天然气股份有限公司 | A method of preparing highly acid Y type molecular sieve |
| CN109718833A (en) * | 2017-10-30 | 2019-05-07 | 中国石油化工股份有限公司 | Modified molecular screen and its preparation method and application |
| CN111514849A (en) * | 2020-04-26 | 2020-08-11 | 东营科尔特新材料有限公司 | Dechlorination adsorbent, preparation method and regeneration method thereof and application of dechlorination adsorbent to organic chlorine |
| CN111514849B (en) * | 2020-04-26 | 2023-10-31 | 东营科尔特新材料有限公司 | Dechlorination adsorbent, preparation method thereof, regeneration method thereof and application of dechlorination adsorbent in removal of organic chlorine |
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