CN104512864A - Method for removing micro-scale carbon monoxide at low temperature - Google Patents
Method for removing micro-scale carbon monoxide at low temperature Download PDFInfo
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Abstract
The invention discloses a method for removing micro-scale carbon monoxide at a low temperature. The method includes following steps: (1) contacting a hydrogen-rich gas containing the carbon oxide with a supported catalyst in a fixed bed reactor; and (2) performing a methanation reaction at a reaction temperature of 90-125 DEG C under a reaction pressure of 0.1-7.0 MPa at a gas space velocity being less than 6000 h<-1> with the concentration of carbon monoxide at an inlet being less than 3000 ppm. The method can allow the micro-scale CO in the hydrogen-rich gas to be removed to be less than 5 ppm.
Description
Technical field
The present invention relates to field of gas purification, the low temperature methanation relating more specifically to micro CO in hydrogen-rich gas removes.
Background technology
In catalytic field, " Lei Nifa " is a kind of preparation method of active metal catalyst, the method is the above alloy of binary first prepared containing active metal, and then by least one METAL EXTRACTION out, the remaining metal with vesicular structure has higher catalytic activity.This method is also referred to as " activation ".Such as, Raney's nickel catalyst (the Industrial and EngineeringChemistry invented by U.S. M.Raney the earliest, 1940, Vol.32,1199), it first prepares alumel, is then dissolved the aluminium element in alloy by strong base solution, remaining nickel metal has vesicular structure, has very high catalytic activity.
Methanation catalyst is mainly used in the deep removal of trace amounts of oxycarbide (mainly CO) in thick hydrogen in ethylene unit or synthetic ammonia installation, and the oxycarbide in the thick hydrogen of general requirement must be removed to through methanator and be less than 5ppm.
Methanation catalyst mainly comprises Ru catalyzer and Ni catalyzer.Because Ru metal is expensive, so the application of industry is little.The methanation catalyst be widely used at present is Ni catalyzer mainly.Ni catalyzer is also divided into high temperature catalyst and low temperature catalyst.In ethylene unit, high temperature catalyst service temperature is generally 280-350 DEG C, and low temperature catalyst service temperature is generally 150-200 DEG C.Catalyst for Low-Temperature Methanation has energy-saving and environmental protection, safe, economic advantage, and therefore, high-temperature methane metallization processes will be replaced by low temperature methanation process gradually.
The temperature of reaction of existing Catalyst for Low-Temperature Methanation is all greater than 150 DEG C.Because require high lower than the reactions of 150 DEG C to catalyst activity, and conventional methanation catalyzer needs high-temperature roasting in preparation process, high-temperature roasting causes considerable metal particles sinter, the utilization ratio of active metal is reduced, finally cause the reactive behavior of catalyzer low, thus the methanation reaction lower than 150 DEG C can not be met.
Therefore, for low temperature methanation reaction, exploitation one (is less than 150 DEG C) at lower temperatures and still has highly active catalyzer and has great importance for methanation process.
Summary of the invention
The object of this invention is to provide a kind of method that low temperature removes trace amounts of oxycarbide in hydrogen-rich gas.The method use one and still there is highly active macromolecular material supported catalyst at low temperatures, achieve, at 90-125 DEG C, the trace amounts of CO in hydrogen-rich gas is removed to below 5ppm.
A kind of low temperature of the present invention removes the method for trace amounts of oxycarbide, it is characterized in that, in fixed-bed reactor, the hydrogen-rich gas containing CO is contacted with a kind of loaded catalyst, temperature of reaction 90-125 DEG C, pressure 0.1-7.0MPa, gas space velocity be less than 6000h
-1, entrance CO concentration carries out methanation reaction under being less than the condition of 3000ppm; Be preferably 90-125 DEG C in temperature of reaction, pressure 2.0-4.0MPa, gas space velocity is less than 3000h
-1, entrance CO concentration carries out methanation reaction under being less than the condition of 3000ppm.
Wherein said loaded catalyst comprises organic polymeric carrier material and the load thunder damping alloy particle at organic polymer material carrier surface, and described thunder damping alloy comprises Raney metal nickel and can by the element of leaching.
Preferably, thunder damping alloy particle in loaded catalyst is to be partially submerged into form load in organic polymer material carrier at carrier surface, and " thunder damping alloy particle fraction embeds in organic polymeric carrier material " refers to each thunder damping alloy particle some embeds in carrier.It is that mold pressing is reached by the carrier that thunder damping alloy particle is coated by under carrier forming process temperature condition or under the condition of uncured sizing that described thunder damping alloy particle fraction embeds in organic polymeric carrier material.Heat and pressure dual function under, organic polymer material carrier produces softening transform, thunder damping alloy particle is pressed in softening carrier by part, while particle fraction press-in, softening carrier can overflow at particle periphery, and the carrier of spilling not only plays the effect firmly fixing particle, and can be pressed into other particles again on the carrier surface overflowed, so repeatedly, thunder damping alloy particle fraction is pressed in the carrier surface be likely pressed into.As mentioned above, the present invention effectively make use of overall surface area, makes the active metallic content of catalyst cupport very high.In addition, because thunder damping alloy particle fraction embeds in carrier, the carrier of particle periphery, as firmly fixing thing, makes catalyzer have good stability.
Described thunder damping alloy comprises Raney metal and can by the element of leaching, and metal insoluble when " Raney metal " refers to and activate with Lei Nifa, most typical Raney metal is nickel." can by the element of leaching " by the element dissolved, can be generally at least one in aluminium, zinc and silicon when referring to and activate with Lei Nifa by the element of leaching.
The present invention does not do requirement to thunder damping alloy size of particles and thunder damping alloy component concentration, and commercially available thunder damping alloy all can use, and the median size of thunder damping alloy particle is generally 0.1 ~ 1000 micron, is preferably 10 ~ 100 microns.Preferably, the content of Raney metal nickel in thunder damping alloy is 55 ~ 80wt%.In order to improve catalyst activity or selectivity, thunder damping alloy can also introduce promotor, promotor is selected from least one in Mo, Cr, Ti, Fe, Pt, Pd, Rh, Ru, and form the thunder damping alloy of multicomponent mixture, the amount of promotor is 0.01 ~ 5wt% of thunder damping alloy total amount.
The preferred plastics of described organic polymer material or its modified product, plastics comprise thermosetting resin and thermoplastics.Concrete plastics comprise: polyolefine, poly-4-methyl isophthalic acid amylene, polyamide resin (as nylon-5, PA-12, nylon-6/6, nylon-6/10, nylon-11), polycarbonate resin, homopolymerization and/or copolymerized methanal, monounsaturated dicarboxylic acid and dibasic alcohol by the obtained linear polyester of polycondensation, (polymkeric substance that aromatic ring polymer and molecule are only made up of aromatic ring and linking group, as polyphenyl, polyphenylene oxide, polyphenylene sulfide, polyarylsulphone, poly aryl ketone for aromatic ring polymer.Aromatic polyester, aromatic polyamides), heterocyclic polymer (heterocyclic polymer and molecular backbone chain also having except aromatic ring the macromolecular material of heterocycle, as polybenzimidazole), fluoropolymer, acrylic resin, mephenesin Carbamate, epoxy resin, resol, urea-formaldehyde resin, terpolycyantoamino-formaldehyde resin etc.At least one in preferred polyolefm resin, polyamide resin, polystyrene, epoxy resin and resol, at least one more preferably in polypropylene, nylon-6, nylon-66, polystyrene, resol and epoxy resin.
Modifying plastics product refers to the modified product adopting existing modifying plastics method to obtain.Modifying plastics method is including, but not limited to following methods: the graft modification of polarity or non-polar monomer or its polymkeric substance; By the melt blending modification etc. with the materials such as inorganic or organic reinforcing, toughening material, the firm material of increasing, increase heat-resisting material.
Invention further provides the preparation method of above-mentioned catalyzer.
The preparation method of catalyzer of the present invention, it comprises: under organic polymer material forming process temperature condition or under the condition of uncured sizing, and mold pressing is by the coated organic polymer material of thunder damping alloy particle.
For different organic polymer material carriers, concrete preparation method is slightly different.
When carrier adopts organic thermoplastic polymer material, (I) or (II) can be specifically selected with the following method to prepare:
Method (I):
(1) thermoplastic carrier is processed into the particle of any shape meeting size needed for fixed bed catalyst or fluid catalyst;
(2) above-mentioned carrier granule is placed in thunder damping alloy particle, namely carrier is completely coated by thunder damping alloy particle;
(3) under corresponding thermoplastic carrier's forming process temperature condition, mold pressing is placed in thunder damping alloy particle thermoplastic carrier, by in thunder damping alloy particle fraction press-in thermoplastic carrier particle, make thunder damping alloy particle load at thermoplastic carrier's particle surface and be partially submerged in carrier, cooling, sieve, obtain granular Catalyst for Low-Temperature Methanation.
The size of pellet type catalyst is can meet particle size needed for fixed bed catalyst or fluid catalyst for benchmark.The shape of particle can be the combination etc. of any irregularly shaped, spherule, hemispherical mass, cylinder, semi-cylindrical body, prism-shaped body, cubes, rectangular parallelepiped, ring bodies, half-annuli, hollow cylinder, profile of tooth or more shape, preferably the combination of spherical, annular, profile of tooth, cylindrical or more shape.Thermoplastic carrier's particle can be shaping by raw material processing, also directly can use commercial shaping thermoplastic carrier's particle.
Or method (II):
(1) thermoplastic carrier is processed into the sheet material of fixed bed catalyst or fluid catalyst desired thickness;
(2) by the surface of coated for thunder damping alloy uniform particle gained support sheet;
(3) under the conventional forming process temperature condition of corresponding thermoplastic carrier, mold pressing is carried out to the sheet material coated by thunder damping alloy particle, thunder damping alloy particle is by part press-in support sheet, any available processing units is adopted after cooling, there is the support sheet of thunder damping alloy particle to be processed into required shape and the particle of size area load by methods such as cutting, cutting, punching press or fragmentations, finally also obtain pellet type catalyst.
Method (I) or the thermoplastic carrier described in method (II) can add as antioxidant, help auxiliary agent conventional in the plastic processes such as antioxidant, thermo-stabilizer, photostabilizer, ozone stabilizers, processing aid, softening agent, tenderizer, anti blocking agent, whipping agent, dyestuff, pigment, wax, extender, organic acid, fire retardant and coupling agent.Adjuvant used consumption is conventional amount used, or adjusts according to the requirement of practical situation.
When carrier adopts thermoset organic polymer material carrier, (III) or (IV) can be specifically selected with the following method to prepare:
Method (III):
(1) be mixed with suitable curing system according to the conventional curing formula of thermoset carrier, liquid system can directly stir; Pulverized solid system can be direct evenly blended; Granulated solid system is evenly blended after can pulverizing with industrial conventional any disintegrating apparatus.
(2) in the mould of any cavity shape that can meet particle size needed for fixed bed catalyst or fluid catalyst, thunder damping alloy powder is first added, add the uncured thermoset organic polymer material prepared again, and then add thunder damping alloy powder, partially cured sizing is carried out under conventional condition of cure, then with any available organic polymer material processing units, molded curing is proceeded to the granular carrier being coated with thunder damping alloy powder of partially cured sizing, after completion of cure, sieve, namely obtain particulate supported type catalyzer;
Or method (IV):
(1) be mixed with suitable curing system according to the conventional curing formula of thermoset organic polymer material, liquid system can directly stir; Pulverized solid system can be direct evenly blended; Granulated solid system is evenly blended after can pulverizing with industrial conventional any disintegrating apparatus.
(2) the thermoset organic polymer material system will prepared, under conventional condition of cure, in blocks with any available equipment mold pressing, incomplete solidification, thickness is determined by fixed bed catalyst or fluid catalyst size, the even coated thunder damping alloy powder of upper and lower surface, continue mold pressing to solidifying completely, in thunder damping alloy pruinescence part press-in thermoset carrier, the surface of thermoset carrier sheet material, by the load of thunder damping alloy powder institute, namely obtains catalyzer.
(3) by catalyzer obtained above, adopt any available organic polymer material processing units, by cutting, cutting, the method such as punching press or fragmentation is processed into fixed bed or the operable particle of fluidized-bed reaction, the size of particle is can meet particle size needed for fixed bed catalyst or fluid catalyst for benchmark, the shape of particle can be any irregularly shaped, spherule, hemispherical mass, cylinder, semi-cylindrical body, prism-shaped body, cubes, rectangular parallelepiped, ring bodies, half-annuli, hollow cylinder, the combination etc. of profile of tooth or more shape, preferably spherical, annular, profile of tooth, the combination of cylindrical or more shape, more preferably spherical.。
In the thermoset organic polymer material curing system preparation process described in method (III) or method (IV), optional one or more can be added and be selected from following additive: curing catalyst, dyestuff, pigment, tinting material, antioxidant, stablizer, softening agent, lubricant, flow ability modifying agent or auxiliary agent, fire retardant, dripping inhibitor, anti-caking agent, adhesion promotor, conductive agent, polyvalent metal ion, impact modifying agent, demolding aids, nucleator etc.Additive therefor consumption is conventional amount used, or adjusts according to the requirement of practical situation.
The catalyzer that the present invention obtains can be easy to be activated, activation condition is generally: at 25 DEG C ~ 95 DEG C, use 0.5-30%(weight) the alkaline solution stripping of concentration is selected from least one in aluminium, zinc and silicon, alkali lye preferably with NaOH or KOH, about 5 minutes ~ 72 hours base extraction time.
By controlling the add-on of thunder damping alloy in catalyst preparation process and/or controlling the activation degree of catalyzer, thus the charge capacity of Raney metal in catalyzer can be controlled easily, such as can obtain Raney metal charge capacity is 1 ~ 90%(weight) loaded catalyst of the activation of (in overall catalyst weight for 100%), preferred Raney metal charge capacity is 10 ~ 80%(weight) the loaded catalyst of activation, more preferably Raney metal charge capacity is 40 ~ 80%(weight).
Inorganic oxide carrier metal supported catalyst prepared by traditional employing pickling process, need repeatedly to flood, repeated calcination, process is complicated, the charge capacity of metal is difficult to more than 40%(weight) (in overall catalyst weight for 100%), and because the high-temperature roasting in preparation process causes considerable metal particles sinter, make the utilization ratio of active metal lower, thus catalyst activity is lower.Catalyzer of the present invention not only can the more active metals of load, and do not have pyroprocessing in preparation process, so the utilization ratio of active metal is very high, thus catalyst activity is high.
Compared with prior art, the method removing trace amounts of oxycarbide of the present invention has the following advantages:
1. in method of the present invention, method for preparing catalyst is simple, and cost is lower.
2. in method of the present invention, the catalyzer of macromolecular material load overcomes the high-temperature roasting of conventional inorganic oxide carrier and causes considerable metal particles sinter problem, make the utilization ratio of active metal high, so the reactive behavior of catalyzer is high, achieves, at 90-125 DEG C, the trace amounts of CO in hydrogen-rich gas is removed to below 5ppm.
Embodiment
The present invention is described further for embodiment below, but not thereby limiting the invention.
Embodiment 1
1, the catalyst preparing of macromolecular material load
(1) polypropylene powder (Maoming Petrochemical, F280M) extruded with twin screw extruder and be cut into Φ 3mm × 3 ~ 5mm particle;
(2) taking 100g polypropylene GRANULES is placed among alumel powder, in alumel, Ni content is 48%(weight), aluminium weight content 52%(weight), with compression molding instrument mold pressing 10min under the condition of temperature 200 DEG C, pressure 7MPa, take out cooling, sieve, sift out spherical particle, particle surface is covered by Nickel Aluminium Alloy Powder completely, namely obtains loaded catalyst, is weighed as 380g;
(3) with deionized water configuration 20%NaOH aqueous solution 400g, add step (2) gained catalyzer 40g, keep temperature 85 DEG C, solution is filtered out after 4 hours, namely the catalyzer activated is obtained, in final catalyzer, nickel content of metal is about 56%(weight), washing, to close to after neutrality, is deposited in deionized water for subsequent use.
2, fixed bed reaction evaluation
Measure 10ml catalyzer and load stainless steel fixed-bed reactor, pass into high pure nitrogen, nitrogen flow is 300ml/min, is heated to 120 DEG C, keeps 2 hours; Then switch to unstripped gas to react, containing CO1000ppm in unstripped gas, other concrete reaction conditionss are listed in table 1.After reaction, gas composition uses gas chromatographic analysis, and chromatographic detector is that FID, CO content can be as accurate as 1ppm.Table 1 gives detailed assessment result.Outlet CO content (ppm) is less, shows that the activity of catalyzer is higher.
Table 1 embodiment 1 catalyst reaction evaluation result
Embodiment 2
1, the catalyst preparing of macromolecular material load
(1) polypropylene powder (Maoming Petrochemical, F280M) extruded with twin screw extruder and be cut into Φ 3mm × 3 ~ 5mm particle;
(2) taking 100g polypropylene GRANULES is placed among alumel powder, in alumel, Ni content is 48%(weight), aluminium weight content 52%(weight), with compression molding instrument mold pressing 10min under the condition of temperature 200 DEG C, pressure 7MPa, take out cooling, sieve, sift out spherical particle, particle surface is covered by Nickel Aluminium Alloy Powder completely, namely obtains loaded catalyst, is weighed as 420g;
(3) with deionized water configuration 20%NaOH aqueous solution 400g, add step (2) gained catalyzer 40g, keep temperature 85 DEG C, solution is filtered out after 8 hours, namely the catalyzer activated is obtained, in final catalyzer, nickel content of metal is about 63%(weight), washing, to close to after neutrality, is deposited in deionized water for subsequent use.
2, fixed bed reaction evaluation
Measure 10ml catalyzer and load stainless steel fixed-bed reactor, pass into high pure nitrogen, nitrogen flow is 300ml/min, is heated to 120 DEG C, keeps 2 hours; Then switch to unstripped gas to react, containing CO2000ppm in unstripped gas, other concrete reaction conditionss are listed in table 2.After reaction, gas composition uses gas chromatographic analysis, and chromatographic detector is that FID, CO content can be as accurate as 1ppm.Table 2 gives detailed assessment result.Outlet CO content (ppm) is less, shows that the activity of catalyzer is higher.
Table 2 embodiment 2 catalyst reaction evaluation result
Comparative example 1
1, the preparation of conventional aluminium oxide supported ni catalyst
The nickel-metal catalyst of alumina load passes through compression produces.First by 1kg basic nickel carbonate NiCO
32Ni (OH)
24H
2after O and a certain amount of pseudo-boehmite kneading, screening is small-particle, dry 24 hours for 160 DEG C, 400 DEG C of roastings 4 hours, compression molding is Φ 3mm × 3mm cylindrical catalyst particle, 450 DEG C of hydrogen reducings 24 hours, obtain containing 56%(weight) the alumina load catalyzer of nickel metal, reacts for fixed bed hydrogenation.
2, fixed bed reaction evaluation,
Measure 10ml catalyzer and load stainless steel fixed-bed reactor, first catalyzer is removed the oxide compound on surface at 240 DEG C with hydrogen reducing, the recovery time is 2 hours; Then switch to unstripped gas to react, containing CO1000ppm in unstripped gas, other concrete reaction conditionss are listed in table 3.After reaction, gas composition uses gas chromatographic analysis, and chromatographic detector is that FID, CO content can be as accurate as 1ppm.Table 1 gives detailed assessment result.Outlet CO content (ppm) is less, shows that the activity of catalyzer is higher.
Table 3 comparative example 1 catalyst reaction evaluation result
The evaluation result of comparative example 1,2 and comparative example 1 can be found out, use the Ni catalyzer of macromolecule loading to can be implemented in 90-125 DEG C (trace amounts of CO to be removed to and to be less than 1ppm, and comparative example 1 catalyzer 90-125 DEG C of activity significantly lower than embodiment 1,2 catalyzer, the purification that can not realize CO removes object.
Embodiment 3
1, the catalyst preparing of macromolecular material load
(1) polypropylene powder (Maoming Petrochemical, F280M) extruded with twin screw extruder and be cut into Φ 3mm × 3 ~ 5mm particle;
(2) taking 100g polypropylene GRANULES is placed among alumel powder, in alumel, Ni content is 48%(weight), aluminium weight content 52%(weight), with compression molding instrument mold pressing 10min under the condition of temperature 200 DEG C, pressure 7MPa, take out cooling, sieve, sift out spherical particle, particle surface is covered by Nickel Aluminium Alloy Powder completely, namely obtains loaded catalyst, is weighed as 420g;
(3) with deionized water configuration 20%NaOH aqueous solution 400g, add step (2) gained catalyzer 40g, keep temperature 85 DEG C, solution is filtered out after 8 hours, namely the catalyzer activated is obtained, in final catalyzer, nickel content of metal is about 63%(weight), washing, to close to after neutrality, is deposited in deionized water for subsequent use.
2, fixed bed reaction evaluation
Measure 10ml catalyzer and load stainless steel fixed-bed reactor, pass into high pure nitrogen, nitrogen flow is 300ml/min, is heated to 120 DEG C, keeps 2 hours; Then unstripped gas is switched to react, containing CO1000ppm in unstripped gas, temperature of reaction 125 DEG C, reaction pressure 3.5MPa, gas space velocity 6000h
-1.After reaction, gas composition uses gas chromatographic analysis, and chromatographic detector is that FID, CO content can be as accurate as 1ppm.Reaction result: outlet CO is 2ppm.
Embodiment 4
1, the catalyst preparing of macromolecular material load
(1) polypropylene powder (Maoming Petrochemical, F280M) extruded with twin screw extruder and be cut into Φ 3mm × 3 ~ 5mm particle;
(2) taking 100g polypropylene GRANULES is placed among alumel powder, in alumel, Ni content is 48%(weight), aluminium weight content 52%(weight), with compression molding instrument mold pressing 10min under the condition of temperature 200 DEG C, pressure 7MPa, take out cooling, sieve, sift out spherical particle, particle surface is covered by Nickel Aluminium Alloy Powder completely, namely obtains loaded catalyst, is weighed as 420g;
(3) with deionized water configuration 20%NaOH aqueous solution 400g, add step (2) gained catalyzer 40g, keep temperature 85 DEG C, solution is filtered out after 8 hours, namely the catalyzer activated is obtained, in final catalyzer, nickel content of metal is about 63%(weight), washing, to close to after neutrality, is deposited in deionized water for subsequent use.
2, fixed bed reaction evaluation
Measure 10ml catalyzer and load stainless steel fixed-bed reactor, pass into high pure nitrogen, nitrogen flow is 300ml/min, is heated to 120 DEG C, keeps 2 hours; Then unstripped gas is switched to react, containing CO3000ppm in unstripped gas, temperature of reaction 125 DEG C, reaction pressure 3.5MPa, gas space velocity 1000h
-1.After reaction, gas composition uses gas chromatographic analysis, and chromatographic detector is that FID, CO content can be as accurate as 1ppm.Reaction result: outlet CO is less than 1ppm.
Claims (9)
1. a low temperature removes the method for trace amounts of oxycarbide, it is characterized in that, in fixed-bed reactor, the hydrogen-rich gas containing oxycarbide is contacted with a kind of loaded catalyst, temperature of reaction 90-125 DEG C, pressure 0.1-7.0MPa, gas space velocity be less than 6000h
-1, entrance CO concentration carries out methanation reaction under being less than the condition of 3000ppm;
Wherein said loaded catalyst comprises organic polymeric carrier material and the load thunder damping alloy particle at organic polymer material carrier surface, described thunder damping alloy comprises Raney metal nickel and can by the element of leaching, the described at least one that can be selected from by the element of leaching in aluminium, zinc and silicon.
2. catalyzer according to claim 1, wherein said thunder damping alloy particle is to be partially submerged into form load in organic polymer material carrier at carrier surface.
3. catalyzer according to claim 2, wherein thunder damping alloy particle fraction embeds in carrier is that mold pressing is reached by the carrier that thunder damping alloy particle is coated by under the forming process temperature condition of carrier or under the condition of uncured sizing.
4. method according to claim 1, in wherein said thunder damping alloy, Raney metal nickel is 55 ~ 80wt% of thunder damping alloy gross weight.
5. method according to claim 1, wherein in described thunder damping alloy, also comprise at least one promotor be selected from Mo, Cr, Ti, Fe, Pt, Pd, Rh, Ru, promotor is 0.01 ~ 5wt% of thunder damping alloy gross weight.
6. method according to claim 1, wherein said organic polymer material is plastics or its modified plastics.
7. method according to claim 6, wherein said plastics are selected from least one in polyolefin resin, polyamide resin, polystyrene, epoxy resin and resol, at least one in optimization polypropylene, nylon-6, nylon-66, polystyrene and epoxy resin.
8. method according to claim 1, catalyst shape is the combination of spherical, annular, profile of tooth, cylindrical, rectangular parallelepiped or more shape, preferably spherical.
9. method according to claim 1, wherein temperature of reaction is 90-125 DEG C, and pressure 2.0-4.0MPa, gas space velocity is less than 3000h
-1, entrance CO concentration is less than 3000ppm.
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| CN114477089A (en) * | 2020-10-26 | 2022-05-13 | 中国石油化工股份有限公司 | Method for removing trace CO at low temperature |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1037283A (en) * | 1988-04-14 | 1989-11-22 | 格雷斯公司 | The catalyst of moulding and preparation method |
| CN101356004A (en) * | 2005-11-14 | 2009-01-28 | 新加坡科技研究局 | Highly dispersed metal catalysts |
| EP1883618B1 (en) * | 2005-05-23 | 2009-10-14 | Teva Pharmaceutical Industries Ltd. | Processes for preparing cinacalcet hydrochloride crystal form i |
| CN101934229A (en) * | 2010-05-07 | 2011-01-05 | 重庆工商大学 | Catalyst for oxidative removal of CO in hydrogen-rich gas and preparation and application thereof |
-
2013
- 2013-09-30 CN CN201310461388.0A patent/CN104512864B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1037283A (en) * | 1988-04-14 | 1989-11-22 | 格雷斯公司 | The catalyst of moulding and preparation method |
| EP1883618B1 (en) * | 2005-05-23 | 2009-10-14 | Teva Pharmaceutical Industries Ltd. | Processes for preparing cinacalcet hydrochloride crystal form i |
| CN101356004A (en) * | 2005-11-14 | 2009-01-28 | 新加坡科技研究局 | Highly dispersed metal catalysts |
| CN101934229A (en) * | 2010-05-07 | 2011-01-05 | 重庆工商大学 | Catalyst for oxidative removal of CO in hydrogen-rich gas and preparation and application thereof |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114477089A (en) * | 2020-10-26 | 2022-05-13 | 中国石油化工股份有限公司 | Method for removing trace CO at low temperature |
| CN114477089B (en) * | 2020-10-26 | 2023-10-27 | 中国石油化工股份有限公司 | Method for removing trace CO at low temperature |
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