CN101797508B - Coking oven gas hydrodesulfurization catalyst and method for preparing same - Google Patents

Coking oven gas hydrodesulfurization catalyst and method for preparing same Download PDF

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CN101797508B
CN101797508B CN 200910273123 CN200910273123A CN101797508B CN 101797508 B CN101797508 B CN 101797508B CN 200910273123 CN200910273123 CN 200910273123 CN 200910273123 A CN200910273123 A CN 200910273123A CN 101797508 B CN101797508 B CN 101797508B
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catalyst
oxide
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oven gas
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CN101797508A (en
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王国兴
雷家珩
张先茂
王天元
王泽�
刘志凯
赵志杰
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Wuhan Kelin Chemical Industry Group Co ltd
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WUHAN KELIN FINE CHEMICAL CO Ltd
Wuhan University of Technology WUT
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Abstract

The invention discloses coking oven gas hydrodesulfurization catalyst and a method for preparing the same. The coking oven gas hydrodesulfurization catalyst is prepared by loading active components on the carrier of Gamma-Al2O3 with the immersion method. The active components comprises iron oxide, molybdenum oxide and cobalt oxide, wherein the weight of the iron oxide is 2-10 percent of the total weight of the coking oven gas hydrodesulfurization catalyst, the weight of the molybdenum oxide is 5-20 percent of the total weight of the coking oven gas hydrodesulfurization catalyst, the weight of the cobalt oxide is 0.1-5 percent of the total weight of the coking oven gas hydrodesulfurization catalyst, and the balance is Gamma-Al2O3. The coking oven gas hydrodesulfurization catalyst has the characteristic of high hydrodesulfurization activity, less methanation reaction and CO disproportionation reaction and good thermal stability, etc.

Description

A kind of coking oven gas hydrodesulfurizationcatalyst catalyst and preparation method thereof
Technical field
The present invention relates to a kind of coking oven gas hydrodesulfurizationcatalyst catalyst and preparation method thereof.
Background technology
Oven gas is the gas that produces in process of coking, wherein comprises the chemical products of the recoverables such as hydrogen, methane, carbon monoxide, carbon dioxide, ethene.Oven gas must pass through purified treatment before utilizing, sulfide especially wherein because sulphur can cause murder by poisoning to postorder workshop section catalyst, makes it permanent poisoning and deactivation.In existing oven gas desulfurization process, most H 2S is removed in process of wet desulphurization, and the method that removes need employing hydro-conversion of the organic sulfurs such as cos, mercaptan, thioether, thiophene namely under the effect of Hydrobon catalyst, is converted into hydrogen sulfide with organic sulfur, absorbs H with desulfurizing agent again 2S.
Contain about 8% CO and 3% CO in the oven gas 2, the Co-Mo catalyst easily makes it that strong exothermal reactions such as methanation, CO disproportionation carbon distribution occur when using in this environment, and these reaction liberated heats can cause bed temperature to be ascended to heaven, the operating mode big ups and downs, the service life of catalyst is short.At present, the Fe-Mo/ γ-Al of hydrodesulfurization normal operation China of oven gas exploitation 2O 3Catalyst because this catalyst in use, methanation reaction, CO disproportionation carbon distribution reacting phase be to less, but Fe to the promoting catalysis of Mo a little less than, Fe-Mo/ γ-Al 2O 3The hydrodesulfurization rate of catalyst only is about 60%, and serviceability temperature is high, is 350 ℃~420 ℃, and the activity of catalyst is also unstable.
Summary of the invention
Technical problem to be solved by this invention is: a kind of coking oven gas hydrodesulfurizationcatalyst catalyst and preparation method thereof is provided, and it is high that this catalyst has a low temperature active, and methanation, the reaction of CO disproportionation carbon distribution are few, the characteristics of Heat stability is good.
The technical solution adopted in the present invention is: it is with γ-Al 2O 3Be carrier, by infusion process that active constituent loading is prepared on the catalyst carrier, wherein active component comprises the oxide of iron, the oxide of molybdenum and the oxide of cobalt, and the oxide weight content of iron is 2%~10% of catalyst total amount, the oxide weight content of molybdenum is 5%~20% of catalyst total amount, the oxide weight content of cobalt is 0.1%~5% of catalyst total amount, and all the other are γ-Al 2O 3
Another object of the present invention provides a kind of preparation method of above-mentioned coking oven gas hydrodesulfurizationcatalyst catalyst, and this method may further comprise the steps:
1) chooses in type γ-Al 2O 3Carrier, with it in 120 ℃ of dryings 2~10 hours;
2) take by weighing a certain amount of ammonium molybdate and be dissolved in deionized water, under constantly stirring, add a certain amount of organic acid, then add cobalt salt, add again at last molysite, join to get maceration extract;
3) adopt the equivalent impregnation method with 1) carrier impregnation to 2 of step gained) in the maceration extract of step preparation, dip time 2~12 hours then in 120 ℃ of oven dry, namely got coking oven gas hydrodesulfurizationcatalyst catalyst in 2~4 hours in 500 ℃ of roastings again.
Advantage of the present invention: it is active component that catalyst of the present invention adopts Fe, Mo and a certain amount of Co, adds simultaneously trace rare-earth element, alkali metal as auxiliary agent, adopts the infusion process preparation, and Active components distribution is even, and utilization rate is high.Experiment shows, this catalyst uses in oven gas, and the hydrodesulfurization rate is greater than 90%, 300 ℃ of hydrodesulfurization rates of low temperature approximately 80%, and methanation, the reaction of CO disproportionation carbon distribution are few, the long-term operation stable performance.
The specific embodiment
It is active component that catalyst of the present invention adopts Fe, Mo and a certain amount of Co, adds simultaneously trace rare-earth element, alkali metal as auxiliary agent, and preparation technology adopts infusion process, chooses in type γ-Al 2O 3Be carrier, flood by the soluble salt solution of above-mentioned element, through super-dry, roasting, vulcanizing treatment, obtain the active phase catalyst of ternary metal sulfide, Active components distribution is even, and utilization rate is high.Experiment shows, this catalyst uses in oven gas, and the hydrodesulfurization rate is up to about 96%, and 300 ℃ of hydrodesulfurization rates of low temperature reach about 80%, and methanation, the reaction of CO disproportionation carbon distribution are few, the long-term operation stable performance.
Particularly, catalyst of the present invention is with γ-Al 2O 3Be carrier, by infusion process that active constituent loading is prepared on the catalyst carrier, wherein active component comprises the oxide of iron, the oxide of molybdenum and the oxide of cobalt, and the oxide weight content of iron is 2%~10% of catalyst total amount, the oxide weight content of molybdenum is 5%~20% of catalyst total amount, the oxide weight content of cobalt is 0.1%~5% of catalyst total amount, and all the other are γ-Al 2O 3
The preparation method of catalyst of the present invention may further comprise the steps:
1) chooses in type γ-Al 2O 3Carrier, with it in 120 ℃ of dryings 2~10 hours;
2) take by weighing a certain amount of ammonium molybdate and be dissolved in deionized water, under constantly stirring, add a certain amount of organic acid, then add cobalt salt, add again at last molysite, join to get maceration extract; Described organic acid can be citric acid, lactic acid or tartaric acid, optimization citric acid.Described cobalt salt and molysite can be nitrate, carbonate or acetate, preferably nitrate.Mo, Fe among the maceration extract A, the Co of preparing, organic acid mol ratio are (14~55): (10~50): (0.5~24): (19~57).
3) adopt the equivalent impregnation method with 1) carrier impregnation to 2 of step gained) in the maceration extract of step preparation, dip time 2~12 hours then in 120 ℃ of oven dry, namely got coking oven gas hydrodesulfurizationcatalyst catalyst in 2~4 hours in 500 ℃ of roastings again.
Catalyst of the present invention can also be introduced auxiliary agent during step impregnation, and auxiliary agent comprises the oxide of caesium and/or praseodymium; And the oxide weight content of caesium is 0.01%~0.25% of catalyst total amount, and the oxide weight content of praseodymium is 0.01%~0.25% of catalyst total amount.This moment, the preparation method of coking oven gas hydrodesulfurizationcatalyst catalyst was as follows:
1) chooses in type γ-Al 2O 3Carrier, with it in 120 ℃ of dryings 2~10 hours.
2) take by weighing a certain amount of ammonium molybdate and be dissolved in deionized water, under constantly stirring, add a certain amount of organic acid, then add cobalt salt, add again at last molysite, join to get maceration extract A.Described organic acid can be citric acid, lactic acid or tartaric acid, optimization citric acid.Described cobalt salt and molysite can be nitrate, carbonate or acetate, preferably nitrate.Mo, Fe among the maceration extract A, the Co of preparing, organic acid mol ratio are (14~55): (10~50): (0.5~24): (19~57).
3) adopt the equivalent impregnation method with 1) carrier in step immerses 2) in the solution in step, dip time 2~12 hours then in 120 ℃ of oven dry, in 500 ℃ of roastings 2~4 hours, gets catalyst precarsor again.
4) a certain amount of cesium nitrate and/or praseodymium nitrate is soluble in water, stir, be made into dipping solution B.
5) with 3) catalyst precarsor of step gained is impregnated into 4) among the dipping solution B of step preparation, dip time 2~12 hours then in 120 ℃ of oven dry, in 600 ℃ of roastings 2~4 hours, obtains coking oven gas hydrodesulfurizationcatalyst catalyst at last.
Catalyst of the present invention need be used CS before use 2Or H 2The S sulfuration.
Further specify the present invention below in conjunction with specific embodiment, but the defined invention scope of the present invention is not limited to the following example.
Embodiment 1
1) takes by weighing γ-Al of 2~10 hours of drying under 120 ℃ of conditions 2O 3Carrier 100g, for subsequent use;
2) ammonium molybdate that takes by weighing 24.5g is dissolved in the 50ml deionized water, under constantly stirring, add the citric acid of 30g, then add the 0.35g cobalt nitrate, add again at last the 25.3g ferric nitrate, make maceration extract A, wherein Mo, Fe, Co, organic acid mol ratio are 55: 25: 2.4: 57;
3) with 1) carrier impregnation to 2 that obtains of step) among the maceration extract A in step, dip time 2~12 hours, then in 120 ℃ of oven dry, again in 500 ℃ of roastings 2~4 hours, get catalyst FC-1, wherein the shared mass fraction of the oxide of the oxide of the oxide of molybdenum, iron, cobalt is respectively 20%, 5%, 0.5%.
Embodiment 2
1) takes by weighing γ-Al of 2~10 hours of drying under 120 ℃ of conditions 2O 3Carrier 100g, for subsequent use;
2) ammonium molybdate that takes by weighing 6.13g is dissolved in the 50ml deionized water, under constantly stirring, add the citric acid of 10g, then add the 0.35g cobalt nitrate, add again at last the 10.1g ferric nitrate, make maceration extract A, wherein Mo, Fe, Co, organic acid mol ratio are 14: 10: 0.5: 19;
3) with 1) carrier impregnation to 2 that obtains of step) step obtains among the maceration extract A, and dip time 2~12 hours then in 120 ℃ of oven dry, in 500 ℃ of roastings 2~4 hours, gets catalyst precarsor again;
4) take by weighing cesium nitrate 0.013g, join in the deionized water of 60ml, be made into maceration extract B;
5) with 3) catalyst precarsor that obtains of step joins 4) step join maceration extract B in flood, dip time 2~12 hours, then in 120 ℃ of oven dry, again in 600 ℃ of roastings 2~4 hours, obtain catalyst FC-2, wherein the shared mass fraction of the oxide of the oxide of the oxide of the oxide of caesium, molybdenum, iron, cobalt is respectively 0.01%, 5%, 2%, 0.1%.
Embodiment 3
1) takes by weighing γ-Al of 2~10 hours of drying under 120 ℃ of conditions 2O 3Carrier 100g, for subsequent use;
2) ammonium molybdate that takes by weighing 12.26g is dissolved in the 50ml deionized water, under constantly stirring, add the citric acid of 18g, then add the 1.05g cobalt nitrate, add again at last the 25.3g ferric nitrate, make maceration extract A, wherein Mo, Fe, Co, organic acid mol ratio are 28: 25: 1.5: 34.5;
3) with 1) carrier impregnation to 2 that obtains of step) step obtains among the maceration extract A, and dip time 2~12 hours then in 120 ℃ of oven dry, in 500 ℃ of roastings 2~4 hours, gets catalyst precarsor again;
4) take by weighing cesium nitrate 0.325g, join in the deionized water of 60ml, be made into maceration extract B;
5) with 3) catalyst precarsor that obtains of step joins 4) step join maceration extract B in flood, dip time 2~12 hours then in 120 ℃ of oven dry, in 600 ℃ of roastings 2~4 hours, obtains catalyst FC-3 again.Wherein the shared mass fraction of the oxide of the oxide of the oxide of the oxide of caesium, molybdenum, iron, cobalt is respectively 0.25%, 10%, 5%, 0.3%.
Embodiment 4
1) takes by weighing γ-Al of 2~10 hours of drying under 120 ℃ of conditions 2O 3Carrier 100g, for subsequent use;
2) ammonium molybdate that takes by weighing 24.5g is dissolved in the 50ml deionized water, under constantly stirring, add the citric acid of 24g, then add the 17.5g cobalt nitrate, add again at last the 50.6g ferric nitrate, make maceration extract A, wherein Mo, Fe, Co, organic acid mol ratio are 55: 50: 24: 46;
3) with 1) carrier impregnation to 2 that obtains of step) step obtains among the maceration extract A, and dip time 2~12 hours then in 120 ℃ of oven dry, in 500 ℃ of roastings 2~4 hours, gets catalyst precarsor again;
4) take by weighing praseodymium nitrate 0.025g, join in the deionized water of 60ml, be made into maceration extract B;
5) just 3) catalyst precarsor that obtains joins 4 the step) step join maceration extract B in flood, dip time 2~12 hours then in 120 ℃ of oven dry, in 600 ℃ of roastings 2~4 hours, obtains catalyst FC-4 again.Wherein the shared mass fraction of the oxide of the oxide of the oxide of the oxide of praseodymium, molybdenum, iron, cobalt is respectively 0.01%, 20%, 10%, 5%.
Embodiment 5
1) takes by weighing γ-Al of 2~10 hours of drying under 120 ℃ of conditions 2O 3Carrier 100g;
2) ammonium molybdate that takes by weighing 18.4g is dissolved in the 50ml deionized water, under constantly stirring, add the citric acid of 24g, then add the 1.75g cobalt nitrate, add again at last the 25.3g ferric nitrate, make maceration extract A, wherein Mo, Fe, Co, organic acid mol ratio are 42: 25: 2.5: 46;
3) with 1) carrier impregnation to 2 that obtains of step) step obtains in the maceration extract, and dip time 2~12 hours then in 120 ℃ of oven dry, in 500 ℃ of roastings 2~4 hours, gets catalyst precarsor again;
4) take by weighing praseodymium nitrate 0.625g, join in the deionized water of 60ml, be made into maceration extract B;
5) just 3) catalyst precarsor that obtains joins 4 the step) step join maceration extract B in flood, dip time 2~12 hours then in 120 ℃ of oven dry, in 600 ℃ of roastings 2~4 hours, obtains catalyst FC-5 again.Wherein the shared mass fraction of the oxide of the oxide of the oxide of the oxide of praseodymium, molybdenum, iron, cobalt is respectively 0.25%, 15%, 5%, 0.5%.
Embodiment 6
1) takes by weighing γ-Al of 2~10 hours of drying under 120 ℃ of conditions 2O 3Carrier 100g;
2) ammonium molybdate that takes by weighing 18.4g is dissolved in the 50ml deionized water, under constantly stirring, add the citric acid of 24g, then add the 1.75g cobalt nitrate, add again at last the 25.3g ferric nitrate, make maceration extract A, wherein Mo, Fe, Co, organic acid mol ratio are 42: 25: 2.5: 46;
3) with 1) carrier impregnation to 2 that obtains of step) step obtains in the maceration extract, and dip time 2~12 hours then in 120 ℃ of oven dry, in 500 ℃ of roastings 2~4 hours, gets catalyst precarsor again;
4) take by weighing cesium nitrate 0.13g, praseodymium nitrate 0.25g joins in the deionized water of 60ml, is made into maceration extract B;
5) just 3) catalyst precarsor that obtains joins 4 the step) step join maceration extract B in flood, dip time 2~12 hours then in 120 ℃ of oven dry, in 600 ℃ of roastings 2~4 hours, obtains catalyst FC-6 again.Wherein the shared mass fraction of the oxide of the oxide of the oxide of the oxide of the oxide of caesium, praseodymium, molybdenum, iron, cobalt is respectively 0.1%, 0.1%, and 15%, 5%, 0.5%.
The comparative example 1 of prior art
1) takes by weighing γ-Al of 2~10 hours of drying under 120 ℃ of conditions 2O 3Carrier 100g;
2) ammonium molybdate that takes by weighing 18.4g is dissolved in the 50ml deionized water, adds the citric acid of 12g under constantly stirring, and then adds the 25.3g ferric nitrate, joins to get maceration extract;
3) with 1) carrier impregnation to 2 that obtains of step) step join maceration extract in, dip time 2~12 hours then in 120 ℃ of oven dry, in 500 ℃ of roastings 2~4 hours, gets catalyst FM again, wherein molybdenum, the shared mass fraction of iron are respectively 15%, 5%.
Experimental result:
Listed the Evaluation results of above-mentioned each routine catalyst.Above-mentioned catalyst is at 350 ℃ of reaction temperatures, reaction pressure 2.0Mpa, volume space velocity 1000h -1, former granularity appreciation condition under, carry out activity rating with the simulation oven gas, side reaction evaluation and stability test are simultaneously at 300 ℃ of low temperature actives of investigating catalyst.Simulation oven gas composition is H 2: 50v%, CO:8v%, CO 2: 2v%, CH 4: 20v%, N 2: 10v%, total sulfur: 100mg/m 3, H 2S:50mg/m 3, COS:20mg/m 3, CS 2: 15mg/m 3, thiophene: 15mg/m 3, the organic sulfur conversion ratio of catalyst calculates by following formula:
Figure G2009102731231D00051
Wherein, S Before the reactionBe the sulfur content in the unstripped gas, unit is mg/m 3S After the reactionFor reacting the sulfur content in the rear gas, unit is mg/m 3
Catalyst desulfurizing activity and methanation side reaction situation see Table 1, and stability test the results are shown in Table 2.
Table 1 evaluating catalyst result
Figure G2009102731231D00052
Table 2 catalyst stability result of the test
Figure G2009102731231D00053
As can be seen from Table 1, catalyst of the present invention is compared with reference catalyst, and the adding of cobalt makes the organic sulfur hydrogenation conversion improve about 30%, but methanation and CO disproportionation side reaction aggravation; The adding of caesium can obviously suppress the generation of methanation side reaction, but Hydrogenation is had certain influence; The adding of praseodymium can improve the cryogenic property of catalyst preferably, in the time of 300 ℃, still has good activity, organic sulfur hydrogenation conversion approximately 80%; The stability test of table 2 explanation, the adding of caesium can obviously suppress the generation of CO disproportionation side reaction, and catalyst is through the basic carbon distribution not of long-play.

Claims (6)

1. coking oven gas hydrodesulfurizationcatalyst catalyst, it is characterized in that: it is with γ-Al 2O 3Be carrier, by infusion process that active constituent loading is prepared on the catalyst carrier, wherein active component comprises the oxide of iron, the oxide of molybdenum and the oxide of cobalt, and the oxide weight content of iron is 2%~10% of catalyst total amount, the oxide weight content of molybdenum is 5%~20% of catalyst total amount, and the oxide weight content of cobalt is 0.1%~5% of catalyst total amount; Also introduce auxiliary agent during step impregnation, auxiliary agent comprises the oxide of caesium and/or praseodymium, and the oxide weight content of caesium is 0.01%~0.25% of catalyst total amount, and the oxide weight content of praseodymium is 0.01%~0.25% of catalyst total amount; All the other components of described catalyst are γ-Al 2O 3
2. catalyst according to claim 1 is characterized in that using the front presulfurization processing that needs.
3. the preparation method of catalyst according to claim 1 is characterized in that may further comprise the steps:
1) chooses in type γ-Al 2O 3Carrier, with it in 120 ℃ of dryings 2~10 hours;
2) take by weighing a certain amount of ammonium molybdate and be dissolved in deionized water, under constantly stirring, add a certain amount of organic acid, then add cobalt salt, add again at last molysite, join to get maceration extract A;
3) adopt the equivalent impregnation method with 1) carrier impregnation to 2 of step gained) among the maceration extract A of step preparation, dip time 2~12 hours then in 120 ℃ of oven dry, obtained catalyst precarsor in 2~4 hours in 500 ℃ of roastings again;
4) a certain amount of cesium nitrate and/or praseodymium nitrate is soluble in water, stir, be made into dipping solution B;
5) adopt the equivalent impregnation method with 3) step gained catalyst precarsor immerses 4) among the dipping solution B in step, dip time 2~12 hours then in 120 ℃ of oven dry, in 600 ℃ of roastings 2~4 hours, makes coking oven gas hydrodesulfurizationcatalyst catalyst at last.
4. according to the preparation method of claims 3 described catalyst, it is characterized in that: 2) Mo, Fe, Co, organic acid mol ratio are (14~55) in the maceration extract described in the step: (10~50): (0.5~24): (19~57).
5. according to the preparation method of claims 3 described catalyst, it is characterized in that: 2) cobalt salt and the molysite described in the step is nitrate, carbonate or acetate.
6. according to the preparation method of claims 3 described catalyst, it is characterized in that: 2) organic acid described in the step is citric acid, lactic acid or tartaric acid.
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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2880171A (en) * 1954-10-04 1959-03-31 Gulf Research Development Co Hydrodesulfurization of hydrocarbons with catalyst composed of molybdenum and two members of the iron group metals
US5244858A (en) * 1990-03-23 1993-09-14 Cosmo Research Institute Catalyst composition for hydrodesulfurization of hydrocarbon oil and process for producing the same
CN1302686A (en) * 2001-01-09 2001-07-11 华东理工大学 Deoxidizing agent of molybdenum oxide and its preparing process
CN1778873A (en) * 2004-11-26 2006-05-31 中国石油天然气股份有限公司 Inferior diesel hydrogenation catalyst

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2880171A (en) * 1954-10-04 1959-03-31 Gulf Research Development Co Hydrodesulfurization of hydrocarbons with catalyst composed of molybdenum and two members of the iron group metals
US5244858A (en) * 1990-03-23 1993-09-14 Cosmo Research Institute Catalyst composition for hydrodesulfurization of hydrocarbon oil and process for producing the same
CN1302686A (en) * 2001-01-09 2001-07-11 华东理工大学 Deoxidizing agent of molybdenum oxide and its preparing process
CN1778873A (en) * 2004-11-26 2006-05-31 中国石油天然气股份有限公司 Inferior diesel hydrogenation catalyst

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
侯远东.Co-Mo/γ-Al2O3催化剂的改性和FCC汽油选择性加氢研究.《中国优秀硕士学位论文全文数据库》.2008,22-26. *
彭峰等.烟气直接还原脱硫催化剂研究.《复旦学报(自然科学版)》.2003,第42卷(第03期),435-437. *

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