CN107200335B - A kind of isobaric ammonia synthesis technology of segmentation - Google Patents

A kind of isobaric ammonia synthesis technology of segmentation Download PDF

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Publication number
CN107200335B
CN107200335B CN201710325406.0A CN201710325406A CN107200335B CN 107200335 B CN107200335 B CN 107200335B CN 201710325406 A CN201710325406 A CN 201710325406A CN 107200335 B CN107200335 B CN 107200335B
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ammonia
synthesis
ammonia synthesis
ruthenium
convertor
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CN107200335A (en
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江莉龙
林建新
倪军
林炳裕
林科
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Beijing Haixin Energy Technology Co ltd
Fuzhou University National Engineering Research Center Of Chemical Fertilizer Catalyst
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CHEMICAL FERTILIZER CATALYST STATE ENGINEERING RESEARCH CENTER FUZHOU UNIV
Beijing SJ Environmental Protection and New Material Co Ltd
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/02—Preparation, purification or separation of ammonia
    • C01C1/04—Preparation of ammonia by synthesis in the gas phase
    • C01C1/0405—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst
    • C01C1/0411—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst characterised by the catalyst
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/002—Mixed oxides other than spinels, e.g. perovskite
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/56—Platinum group metals
    • B01J23/64—Platinum group metals with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/652—Chromium, molybdenum or tungsten
    • B01J23/6527—Tungsten
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • B01J37/0201—Impregnation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/08—Heat treatment
    • B01J37/082—Decomposition and pyrolysis
    • B01J37/088—Decomposition of a metal salt
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/16—Reducing
    • B01J37/18—Reducing with gases containing free hydrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Abstract

The present invention provides a kind of isobaric ammonia synthesis technologies of segmentation, include the following steps: that syngas for synthetic ammonia 1) is carried out level-one ammonia synthesis in the first ammonia convertor of filling ferrum-based catalyst, the synthesis pressure of the level-one ammonia synthesis is 5-7MPa, and the molar ratio of hydrogen and nitrogen is (1.5-2.5) in the syngas for synthetic ammonia: 1；2) second level ammonia synthesis is carried out from the second ammonia convertor that the gaseous mixture come out in first ammonia convertor enters filling ruthenium-based catalyst, the synthesis pressure of the second level ammonia synthesis is 4-6MPa.Ammonia synthesis process is divided into two sections by the present invention, specified pressure, particular kind of catalyst, specific H-N ratio unstripped gas under carry out, it not only meets ammonia synthesis process requirement, guarantee technique even running, also improve the utilization rate of ammonia convertor outlet ammonia net value and nitrogen and hydrogen；Furthermore every section is to carry out at low pressures, greatly reduces the energy consumption of ammonia synthesis technology.

Description

A kind of isobaric ammonia synthesis technology of segmentation
Technical field
The invention belongs to ammonia synthesis technical fields, and in particular to a kind of segmentation ammonia synthesis technology.
Background technique
Ammonia is important one of inorganic chemical product, occupies an important position in national economy.Except liquefied ammonia can be directly as Outside fertilizer, the nitrogenous fertilizer agriculturally used, such as urea, ammonium nitrate, ammonium phosphate, ammonium chloride and it is various contain nitrogen composite fertilizer, be all Using ammonia as raw material.Therefore, synthesis ammonia plays a significant role national economy, and the world synthesizes hydrazine yield every year and has reached 100,000,000 tons More than, wherein being used to produce chemical fertilizer, 20% raw material as other chemical products there are about 80% ammonia.
It is well known that synthesis ammonia is directly synthesized under high temperature, high pressure and catalyst by nitrogen and hydrogen.German chemist Haber began one's study from 1902 and directly synthesizes ammonia by nitrogen and hydrogen.It was applied for a patent in 1908, i.e. " round-robin method ".At present Common ammonia synthesis technology mainly there are several types of: 1) isobaric technique: water-coal-slurry gas under 8.5MPa through desulfurization, transformation, takes off Carbon after mending nitrogen, synthesizes ammonia at 7.5MPa；2) micro- pressing technology: the water-coal-slurry gas at 8.5MPa through desulfurization, transformation, takes off After carbon, benefit nitrogen, micro- pressurization (being attached to the micro- pressurized segment of unstripped gas by systemic circulation machine) to 9.0-10.0MPa synthesizes ammonia；3) boosting work Skill: the water-coal-slurry gas at 5.0MPa after the purified benefit nitrogen of gas, boosts to 15-22MPa synthesis ammonia.
In above-mentioned several ammonia synthesis technologies, the ammonia synthesis stage carries out under a certain pressure, still, with ammino At the progress of reaction, parameters in reaction process, as temperature, pressure, reaction raw materials and ammonia level can become Change, causes the stability in entire ammonia synthesis stage low.In order to reduce drawbacks described above to the influence degree of ammonia synthesis, Chinese patent Document CN106315619A discloses a kind of low pressure ammonia synthesis technology of ferrum-based catalyst string ruthenium-based catalyst.Technology setting Iron based ammonia synthesis catalyst is arranged in the ammonia convertor of upstream along ammonia synthesis path at least two concatenated ammonia convertors, Ruthenium-based catalyst is set in the ammonia convertor of downstream.By the way that different types of ammonia synthesis catalyst is arranged, adapt to a certain extent The variation of response parameter, ensure that the stable operation in ammonia synthesis stage during ammonia synthesis.
Above-mentioned technology more deacclimatizes the variation of response parameter from the angle of catalyst, to ensure the steady of ammonia synthesis stage Fixed operation.But ammonia synthesis reaction is the balanced reaction carried out under high temperature, high pressure and catalyst, influence factor is numerous, only Iron based ammonia synthesis catalyst is set in the ammonia convertor of upstream, ruthenium-based catalyst is set in the ammonia convertor of downstream, it is difficult to meet Ammonia synthesis process requirement, also result in ammonia convertor outlet ammonia net value it is not high, the utilization rate of nitrogen and hydrogen is relatively low.Therefore, such as The ammonia synthesis technology what provides a kind of high utilization rate for exporting ammonia net value, high nitrogen and hydrogen is that those skilled in the art need The technical problem solved.
Summary of the invention
Therefore, technical problem to be solved by the present invention lies in overcome exist in the prior art outlet ammonia net value it is not high, nitrogen The relatively low defect of the utilization rate of gas and hydrogen, and then a kind of high outlet ammonia net value, high nitrogen and hydrogen utilization ratio, low energy are provided The segmentation equipressure ammonia synthesis technology consume, to run smoothly.
In order to solve the above technical problems, The technical solution adopted by the invention is as follows:
The isobaric ammonia synthesis technology of segmentation provided by the present invention, includes the following steps:
1) syngas for synthetic ammonia is subjected to level-one ammonia synthesis in the first ammonia convertor of filling ferrum-based catalyst, it is described The synthesis pressure of level-one ammonia synthesis is 5-7MPa, and the molar ratio of hydrogen and nitrogen is (1.5- in the syngas for synthetic ammonia 2.5): 1；
2) from the second ammonia convertor that the gaseous mixture come out in first ammonia convertor enters filling ruthenium-based catalyst Second level ammonia synthesis is carried out, the synthesis pressure of the second level ammonia synthesis is 4-6MPa.
Further, in step 1), the synthesis temperature of the level-one ammonia synthesis is 430-500 DEG C；
The air speed of the syngas for synthetic ammonia is 4000-6000h-1。
Further, in step 2), the synthesis temperature of the second level ammonia synthesis is 350-435 DEG C；
The air speed of the gaseous mixture is 5000-12000h-1。
Further, the top half of second ammonia convertor loads the ruthenium-based catalyst, and institute is loaded in lower half portion Ferrum-based catalyst is stated, the syngas for synthetic ammonia enters wherein from the lower half portion of first ammonia convertor.
Further, the number of first ammonia convertor is at least one；
The number of second ammonia convertor is at least one.
Further, it when the number of the first ammonia convertor is at least two, is connected in series between each ammonia convertor；When When the number of two ammonia convertors is at least two, it is connected in series between each ammonia convertor.
Further, further include to from second ammonia convertor come out gaseous mixture cool and recycle heat, Isolated liquefied ammonia and remaining gas, and the step of remaining gas and the syngas for synthetic ammonia are mixed.
Further, the syngas for synthetic ammonia obtains after desulfurization, transformation, desulfuration of shift gas decarburization and refining, described S < 5ppm, CO < 10ppm, CO in syngas for synthetic ammonia2< 10ppm.
Further, the ruthenium-based catalyst, the component including following parts by weight:
Preferably, the active carbon is the active carbon of N doping.
Further, further include the component of following parts by weight:
6-9 parts of barium monoxide
3-9 parts of potassium oxide.
Further, the preparation method of the ruthenium-based catalyst, includes the following steps:
(1) by basic magnesium carbonate, active carbon, basic carbonate cerium, molybdenum oxide and tungsten oxide ground and mixed, or by alkali formula Magnesium carbonate, active carbon, basic carbonate cerium, molybdenum oxide, tungsten oxide, potassium carbonate and barium carbonate ground and mixed collect mixture, and The mixture is formed, molding is obtained；
(2) by the molding be impregnated in ruthenium compound aqueous solution or urea-containing ruthenium compound aqueous solution in, After the dipping, take out；
(3) molding after the dipping is restored under reducing atmosphere；
(4) molding after the reduction is roasted at 1600-2500 DEG C, obtains ruthenium system ammonia synthesis catalyst.
Further, the granularity of the mixture is 0.05-0.5mm.
Further, in step (2), the temperature of the dipping is 10-40 DEG C；
The ruthenium compound aqueous solution or the urea-containing ruthenium compound aqueous solution are potassium ruthenate and/or ruthenic acid sodium Aqueous solution, wherein the mass fraction of ruthenium compound is 8-15%；
The mass fraction of urea is 5-8% in the urea-containing ruthenium compound aqueous solution.
Further, in step (3), the reducing atmosphere is hydrogen atmosphere；
The temperature of the reduction is 300-400 DEG C, time 6-12h.
Further, the temperature of the roasting is 1800-2000 DEG C.
Preferably, described to be ground to ball milling；
The dipping is incipient impregnation.
Further, the ferrum-based catalyst is with mass ratio for (2-3): (1-2): 1 Fe3O4, FeO and K2O is activity Ingredient, with rare earth oxide and MgAl2O4For auxiliary agent.
Further, the content of active constituent is 2-5wt%, rare earth oxide content in the ferrum-based catalyst For 0.1-0.2wt%, MgAl2O4Content is 0.1-0.2wt%；
The rare earth oxide is CeO.
Compared with prior art, there are following advantages by the present invention:
1) it is segmented isobaric ammonia synthesis technology provided by the embodiment of the present invention, ammonia synthesis process is divided into two sections, specific Pressure, particular kind of catalyst, specific H-N ratio unstripped gas under carry out, not only meet ammonia synthesis process requirement, guarantee Technique even running also improves the utilization rate of ammonia convertor outlet ammonia net value and nitrogen and hydrogen；Furthermore every section is It carries out at low pressures, greatly reduces the energy consumption of ammonia synthesis technology.After tested, ammonia convertor outlet ammonia net value is up to 14.2%, nitrogen utilization rate is up to 85%, and hydrogen utilization ratio is up to 90%, and process operation is steady.
2) isobaric ammonia synthesis technology is segmented provided by the embodiment of the present invention, by the synthesis temperature for limiting level-one ammonia synthesis Degree, the air speed of syngas for synthetic ammonia, the air speed of the synthesis temperature of second level ammonia synthesis, gaseous mixture are guaranteeing technique even running Meanwhile outlet ammonia net value, nitrogen and hydrogen utilization ratio are improved to the maximum extent；By in the upper half of the first ammonia convertor Ruthenium-based catalyst is filled out in packing, and lower half portion loads ferrum-based catalyst, further improves outlet ammonia net value.
3) isobaric ammonia synthesis technology is segmented provided by this bright embodiment, wherein ruthenium system ammonia synthesis catalyst, using ruthenium, Magnesia, active carbon, cerium oxide, molybdenum oxide and tungsten oxide, and limit the ratio between each component.It is carried reducing carbon content, improving While body stability, using the mutual cooperation between each component, synergistic effect, the Viability reduction of ammino is not resulted in not only, instead It is Viability to improve ammino.It is 3:1, air speed 10000h in mixed gas H-N ratio through detecting-1, reaction pressure 10MPa, Reaction temperature is to reach 25% or more using the ammonia convertor outlet ammonia density of the ruthenium system ammonia synthesis catalyst at 425 DEG C；? 1000 DEG C are heated under the atmosphere that hydrogen content is 25%, and maintains 100h, further takes out carry out ammonia synthesis, ammonia convertor outlet Ammonia density still can reach 24% or more, show that it, with high heat resistance, and is not easy methanation；Ruthenium metal active ingredient Dispersion degree is high, can reach 50% or more, finally improves the outlet ammonia density and stability of ammonia synthesis technology.
4) it is segmented isobaric ammonia synthesis technology provided by the embodiment of the present invention, using the active carbon of N doping, and uses Barium monoxide and potassium oxide, stability and the ammino for further increasing ruthenium system ammonia synthesis catalyst are Viability；Using specific preparation Method, first by basic magnesium carbonate, active carbon, basic carbonate cerium, molybdenum oxide and tungsten oxide ground and mixed, alternatively, by basic carbonate Magnesium, active carbon, basic carbonate cerium, molybdenum oxide, tungsten oxide, potassium carbonate and barium carbonate ground and mixed, molding, make each solid material Between be uniformly mixed, conducive to improve ruthenium system ammonia synthesis catalyst in ingredient homogeneity；The molding is impregnated in ruthenium again It closes in object aqueous solution or in urea-containing ruthenium compound aqueous solution, is sufficiently submerged in ruthenium compound in each solid material；It connects , ruthenium compound is reduced to simple substance ruthenium with hydrogen；Finally, the molding after reduction is roasted at 1600-2500 DEG C, Basic magnesium carbonate, basic carbonate cerium, potassium carbonate and barium carbonate are changed into corresponding metal oxide during roasting, meanwhile, Carbon dioxide and basic group can be generated, carbon dioxide can dredge the duct of ruthenium system ammonia synthesis catalyst, and basic group then mentions The high alkalinity of carrier, changes carrier surface electron density and structure, improve ruthenium system ammonia synthesis catalyst stability and Ammino is Viability.High-temperature roasting also can activated carbon, played active carbon improve the active ability of ammonia synthesis.
5) isobaric ammonia synthesis technology, the wherein preparation of ruthenium system ammonia synthesis catalyst are segmented provided by the embodiment of the present invention Method, first molding is impregnated in urea-containing ruthenium compound aqueous solution, in conjunction with subsequent high-temperature roasting, to ruthenium system ammonia Each ingredient, especially active carbon in synthetic catalyst, have carried out N doping, improve the stability of ruthenium system ammonia synthesis catalyst It is Viability with ammino；Second ruthenium compound uses potassium ruthenate and/or ruthenic acid sodium, and it is anti-that with it redox occurs for basic carbonate cerium It answers, reduces ruthenium, reduce subsequent hydrogen usage and Methanation, meanwhile, it is also added in ruthenium system ammonia synthesis catalyst Alkali metal, improves ammino Viability；The binder added in three forming processes can be waved in subsequent high temperature roasting process Hair, has dredged carrier duct, has increased catalysis area.
6) isobaric ammonia synthesis technology is segmented provided by the embodiment of the present invention, wherein ferrum-based catalyst is used with specific matter Measure the Fe of ratio3O4, FeO and K2O is active constituent, with rare earth oxide and MgAl2O4For auxiliary agent, during ammonia synthesis, MgAl2O4To N2It exerts one's influence, weakens its chemical bond；Then Fe3O4With FeO under the action of rare earth oxide, it can add Speed is to N2Electronics is conveyed, itrogen-to-nitrogen bonds is dismantled；Finally, generating ammonia in hydrogen ion in conjunction with the nitrogen of negative valency.Thus using above-mentioned Ferrum-based catalyst improves outlet ammonia net value.
Specific embodiment
Technical solution of the present invention will be clearly and completely described below, it is clear that described embodiment is this Invention a part of the embodiment, instead of all the embodiments.Based on the embodiments of the present invention, those of ordinary skill in the art Every other embodiment obtained without making creative work, shall fall within the protection scope of the present invention.
Embodiment 1
A kind of isobaric ammonia synthesis technology of segmentation is present embodiments provided, is included the following steps:
1) syngas for synthetic ammonia obtains after desulfurization, transformation, desulfuration of shift gas decarburization and refining, wherein S < 5ppm, CO < 10ppm, CO2The molar ratio of < 10ppm, hydrogen and nitrogen is 1.7:1；
It 2) is 5000h with air speed by above-mentioned syngas for synthetic ammonia-1Filling ferrum-based catalyst the first ammonia convertor in into Row level-one ammonia synthesis, the synthesis pressure of the level-one ammonia synthesis is 6MPa, synthesis temperature is 450 DEG C；
Wherein, it is the Fe of 2:2:1 that the ferrum-based catalyst, which is with mass ratio,3O4, FeO and K2O is active constituent, with rare earth Element oxide CeO and MgAl2O4For auxiliary agent, the content of active constituent is 4wt%, rare earth element oxygen in the ferrum-based catalyst Compound content is 0.1wt%, MgAl2O4Content is 0.2wt%.
3) gaseous mixture come out from first ammonia convertor is with air speed 8000h-1Into the of filling ruthenium-based catalyst Second level ammonia synthesis is carried out in two ammonia convertors, the synthesis pressure of the second level ammonia synthesis is 5MPa, synthesis temperature is 380 DEG C；
Wherein, ruthenium system ammonia synthesis catalyst is by the ruthenium of 5g, the magnesia of 5g, the active carbon of 80g, the cerium oxide of 7g, 1.5g Molybdenum oxide and 1.5g tungsten oxide composition；
The preparation method of above-mentioned ruthenium system ammonia synthesis catalyst, includes the following steps:
(1) by basic magnesium carbonate, active carbon, basic carbonate cerium, molybdenum oxide and tungsten oxide ball milling mixing, collecting granularity is The mixture of 0.1mm, and add binder-epoxy resin into the mixture and formed, obtain molding；
(2) by the molding incipient impregnation in mass fraction be 12% potassium ruthenate aqueous solution in, control dipping Temperature be 25 DEG C, after dipping, take out；
(3) molding after the dipping is restored in hydrogen, the temperature for controlling reduction is 350 DEG C, and the time is 9h；
(4) molding after the reduction is roasted at 1900 DEG C, obtains ruthenium system ammonia synthesis catalyst.
Embodiment 2
A kind of isobaric ammonia synthesis technology of segmentation is present embodiments provided, is included the following steps:
1) syngas for synthetic ammonia obtains after desulfurization, transformation, desulfuration of shift gas decarburization and refining, wherein S < 5ppm, CO < 10ppm, CO2The molar ratio of < 10ppm, hydrogen and nitrogen is 1.5:1；
It 2) is 6000h with air speed by above-mentioned syngas for synthetic ammonia-1Filling ferrum-based catalyst the first ammonia convertor in into Row level-one ammonia synthesis, the synthesis pressure of the level-one ammonia synthesis is 5MPa, synthesis temperature is 500 DEG C；
Wherein, it is the Fe of 3:1:1 that the ferrum-based catalyst, which is with mass ratio,3O4, FeO and K2O is active constituent, with rare earth Element oxide CeO and MgAl2O4For auxiliary agent, the content of active constituent is 2wt%, rare earth element oxygen in the ferrum-based catalyst Compound content is 0.2wt%, MgAl2O4Content is 0.1wt%；
3) gaseous mixture come out from first ammonia convertor is with air speed 12000h-1Into filling ruthenium-based catalyst Second level ammonia synthesis is carried out in second ammonia convertor, the synthesis pressure of the second level ammonia synthesis is 4MPa, synthesis temperature is 350 DEG C；
Wherein, ruthenium system ammonia synthesis catalyst is by the ruthenium of 2g, the magnesia of 8g, the active carbon of 70g, the cerium oxide of 3g, 2g The tungsten oxide of molybdenum oxide and 1g composition；
The preparation method of above-mentioned ruthenium system ammonia synthesis catalyst, includes the following steps:
(1) by basic magnesium carbonate, active carbon, basic carbonate cerium, molybdenum oxide and tungsten oxide ball milling mixing, collecting granularity is The mixture of 0.05mm, and the mixture is formed, obtain molding；
(2) by the molding incipient impregnation in mass fraction be 8% ruthenic acid sodium aqueous solution in, control dipping Temperature be 40 DEG C, after dipping, take out；
(3) molding after the dipping is restored in hydrogen, the temperature for controlling reduction is 300 DEG C, and the time is 12h；
(4) molding after the reduction is roasted at 2500 DEG C, obtains ruthenium system ammonia synthesis catalyst.
Embodiment 3
A kind of isobaric ammonia synthesis technology of segmentation is present embodiments provided, is included the following steps:
1) syngas for synthetic ammonia obtains after desulfurization, transformation, desulfuration of shift gas decarburization and refining, wherein S < 5ppm, CO < 10ppm, CO2The molar ratio of < 10ppm, hydrogen and nitrogen is 2.5:1；
It 2) is 4000h with air speed by above-mentioned syngas for synthetic ammonia-1Filling ferrum-based catalyst the first ammonia convertor in into Row level-one ammonia synthesis, the synthesis pressure of the level-one ammonia synthesis is 7MPa, synthesis temperature is 430 DEG C；
Wherein, it is the Fe of 2.5:1.5:1 that the ferrum-based catalyst, which is with mass ratio,3O4, FeO and K2O is active constituent, with Rare earth oxide CeO and MgAl2O4For auxiliary agent, the content of active constituent is 3wt%, rare earth member in the ferrum-based catalyst Plain oxide content is 0.15wt%, MgAl2O4Content is 0.1wt%；
3) gaseous mixture come out from first ammonia convertor is with air speed 5000h-1Into the of filling ruthenium-based catalyst Second level ammonia synthesis is carried out in two ammonia convertors, the synthesis pressure of the second level ammonia synthesis is 6MPa, synthesis temperature is 535 DEG C；
Wherein, the ruthenium system ammonia synthesis catalyst is by the ruthenium of 8g, the magnesia of 2g, the active carbon of 85g, the cerium oxide of 3g, 1g Molybdenum oxide and 2g tungsten oxide composition；
The preparation method of above-mentioned ruthenium system ammonia synthesis catalyst, includes the following steps:
(1) by basic magnesium carbonate, active carbon, basic carbonate cerium, molybdenum oxide and tungsten oxide ball milling mixing, collecting granularity is The mixture of 0.5mm, and the mixture is formed, obtain molding；
(2) by the molding incipient impregnation in mass fraction be 15% potassium ruthenate aqueous solution in, control dipping Temperature be 10 DEG C, after dipping, take out；
(3) molding after the dipping is restored in hydrogen, the temperature for controlling reduction is 400 DEG C, and the time is 6h；
(4) molding after the reduction is roasted at 1600 DEG C, obtains ruthenium system ammonia synthesis catalyst.
Embodiment 4
A kind of isobaric ammonia synthesis technology of segmentation is present embodiments provided, is included the following steps:
1) syngas for synthetic ammonia obtains after desulfurization, transformation, desulfuration of shift gas decarburization and refining, wherein S < 5ppm, CO < 10ppm, CO2The molar ratio of < 10ppm, hydrogen and nitrogen is 1.5:1；
It 2) is 4500h with air speed by above-mentioned syngas for synthetic ammonia-1Filling ferrum-based catalyst the first ammonia convertor in into Row level-one ammonia synthesis, the synthesis pressure of the level-one ammonia synthesis is 5.5MPa, synthesis temperature is 460 DEG C；
Wherein, it is the Fe of 3:2:1 that the ferrum-based catalyst, which is with mass ratio,3O4, FeO and K2O is active constituent, with rare earth Element oxide CeO and MgAl2O4For auxiliary agent, the content of active constituent is 3wt%, rare earth element oxygen in the ferrum-based catalyst Compound content is 0.2wt%, MgAl2O4Content is 0.15wt%；
3) gaseous mixture come out from first ammonia convertor is with air speed 7000h-1Into the of filling ruthenium-based catalyst Second level ammonia synthesis is carried out in two ammonia convertors, the synthesis pressure of the second level ammonia synthesis is 5MPa, synthesis temperature is 400 DEG C；
Wherein, the ruthenium system ammonia synthesis catalyst by the ruthenium of 5g, the magnesia of 5g, the active carbon of 80g, 7g cerium oxide, The molybdenum oxide of 1.5g, the tungsten oxide of 1.5g, the barium monoxide of 8g and 7g potassium oxide composition；
The preparation method of above-mentioned ruthenium system ammonia synthesis catalyst, includes the following steps:
(1) basic magnesium carbonate, active carbon, basic carbonate cerium, molybdenum oxide, tungsten oxide, potassium carbonate and barium carbonate ball milling are mixed It closes, collects the mixture that granularity is 0.1mm, and add binder-epoxy resin into the mixture and formed, obtain Molding；
(2) by the molding incipient impregnation in mass fraction be 11% potassium ruthenate aqueous solution in, control dipping Temperature be 30 DEG C, after dipping, take out；
(3) molding after the dipping is restored in hydrogen, the temperature for controlling reduction is 350 DEG C, and the time is 9h；
(4) molding after the reduction is roasted at 1900 DEG C, obtains ruthenium system ammonia synthesis catalyst；
4) it cools to the gaseous mixture come out from second ammonia convertor and recycles heat, isolated liquefied ammonia With remaining gas, and syngas for synthetic ammonia described in the remaining gas and step 1) is mixed.
Embodiment 5
A kind of isobaric ammonia synthesis technology of segmentation is present embodiments provided, is included the following steps:
1) syngas for synthetic ammonia obtains after desulfurization, transformation, desulfuration of shift gas decarburization and refining, wherein S < 5ppm, CO < 10ppm、CO2The molar ratio of < 10ppm, hydrogen and nitrogen is 2:1；
It 2) is 6000h with air speed by above-mentioned syngas for synthetic ammonia-1Filling ferrum-based catalyst the first ammonia convertor in into Row level-one ammonia synthesis, the synthesis pressure of the level-one ammonia synthesis is 6.8MPa, synthesis temperature is 460 DEG C；
Wherein, it is the Fe of 2:1.5:1 that the ferrum-based catalyst, which is with mass ratio,3O4, FeO and K2O is active constituent, with dilute Earth elements oxide CeO and MgAl2O4For auxiliary agent, the content of active constituent is 3wt%, rare earth element in the ferrum-based catalyst Oxide content is 0.1wt%, MgAl2O4Content is 0.15wt%；
3) gaseous mixture come out from first ammonia convertor is with air speed 10000h-1Into filling ruthenium-based catalyst Second level ammonia synthesis is carried out in second ammonia convertor, the synthesis pressure of the second level ammonia synthesis is 6MPa, synthesis temperature is 360 DEG C；
Wherein, the ruthenium system ammonia synthesis catalyst is by the ruthenium of 2g, the magnesia of 8g, the active carbon of 70g, the cerium oxide of 3g, 2g Molybdenum oxide and 1g tungsten oxide composition；
The preparation method of above-mentioned ruthenium system ammonia synthesis catalyst, includes the following steps:
(1) by basic magnesium carbonate, active carbon, basic carbonate cerium, molybdenum oxide and tungsten oxide ball milling mixing, collecting granularity is The mixture of 0.05mm, and the mixture is formed, obtain molding；
(2) by the molding incipient impregnation in mass fraction be 8% urea-containing ruthenic acid sodium aqueous solution in, The temperature of control dipping is 40 DEG C, and the mass fraction of urea is 7%, after dipping, is taken out；
(3) molding after the dipping is restored in hydrogen, the temperature for controlling reduction is 300 DEG C, and the time is 12h；
(4) molding after the reduction is roasted at 1800 DEG C, obtains ruthenium system ammonia synthesis catalyst.
4) it cools to the gaseous mixture come out from second ammonia convertor and recycles heat, isolated liquefied ammonia With remaining gas, and syngas for synthetic ammonia described in the remaining gas and step 1) is mixed.
Embodiment 6
A kind of isobaric ammonia synthesis technology of segmentation is present embodiments provided, is included the following steps:
1) syngas for synthetic ammonia obtains after desulfurization, transformation, desulfuration of shift gas decarburization and refining, wherein S < 5ppm, CO < 10ppm, CO2The molar ratio of < 10ppm, hydrogen and nitrogen is 2:1；
It 2) is 6000h with air speed by above-mentioned syngas for synthetic ammonia-1Into in the first ammonia convertor of filling ferrum-based catalyst Level-one ammonia synthesis is carried out, the synthesis pressure of the level-one ammonia synthesis is 5MPa, synthesis temperature is 450 DEG C；
Wherein, it is the Fe of 2:1.5:1 that the ferrum-based catalyst, which is with mass ratio,3O4, FeO and K2O is active constituent, with dilute Earth elements oxide CeO and MgAl2O4For auxiliary agent, the content of active constituent is 3wt%, rare earth element in the ferrum-based catalyst Oxide content is 0.1wt%, MgAl2O4Content is 0.2wt%；
3) gaseous mixture come out from second ammonia convertor is with air speed 7000h-1, the ruthenium is loaded in top half Base catalyst, lower half portion, which is loaded, carries out second level ammonia synthesis, the secondary amine in the first ammonia convertor of the ferrum-based catalyst The synthesis pressure of synthesis is 4.5MPa, synthesis temperature is 350 DEG C；
Wherein, the ruthenium system ammonia synthesis catalyst is by the ruthenium of 8g, the magnesia of 2g, the active carbon of 85g, the cerium oxide of 9g, 1g Molybdenum oxide, the tungsten oxide of 2g, the barium monoxide of 6g and 9g potassium oxide composition；
The preparation method of above-mentioned ruthenium system ammonia synthesis catalyst, includes the following steps:
(1) basic magnesium carbonate, active carbon, basic carbonate cerium, molybdenum oxide, tungsten oxide, potassium carbonate and barium carbonate ball milling are mixed It closes, collects granularity and be the mixture of 0.5mm, and the mixture is formed, obtain molding；
(2) by the molding incipient impregnation in mass fraction be 15% urea-containing potassium ruthenate aqueous solution in, The temperature of control dipping is 10 DEG C, and the mass fraction of urea is 5%, after dipping, is taken out；
(3) molding after the dipping is restored in hydrogen, the temperature for controlling reduction is 400 DEG C, and the time is 6h；
(4) molding after the reduction is roasted at 1600 DEG C, obtains ruthenium system ammonia synthesis catalyst.
4) it cools to the gaseous mixture come out from second ammonia convertor and recycles heat, isolated liquefied ammonia With remaining gas, and syngas for synthetic ammonia described in the remaining gas and step 1) is mixed.
Embodiment 7
A kind of isobaric ammonia synthesis technology of segmentation is present embodiments provided, is included the following steps:
1) syngas for synthetic ammonia obtains after desulfurization, transformation, desulfuration of shift gas decarburization and refining, wherein S < 5ppm, CO < 10ppm, CO2The molar ratio of < 10ppm, hydrogen and nitrogen is 1.5:1；
It 2) is 7000h with air speed by above-mentioned syngas for synthetic ammonia-1In two concatenated first ammonia of filling ferrum-based catalyst Level-one ammonia synthesis is carried out in synthetic tower, the synthesis pressure of the level-one ammonia synthesis is 6MPa, synthesis temperature is 450 DEG C；
Wherein, it is the Fe of 3:2:1 that the ferrum-based catalyst, which is with mass ratio,3O4, FeO and K2O is active constituent, with rare earth Element oxide CeO and MgAl2O4For auxiliary agent, the content of active constituent is 3wt%, rare earth element oxygen in the ferrum-based catalyst Compound content is 0.2wt%, MgAl2O4Content is 0.2wt%；
3) gaseous mixture come out from first ammonia convertor is with air speed 8000h-1Into two concatenated filling ruthenium bases Second level ammonia synthesis is carried out in second ammonia convertor of catalyst, the synthesis pressure of the second level ammonia synthesis is 5.5MPa, synthesis is warm Degree is 400 DEG C；
Wherein, the ruthenium system ammonia synthesis catalyst by the ruthenium of 4g, the magnesia of 6g, the active carbon of 75g, 8g cerium oxide, The molybdenum oxide of 1.5g, the tungsten oxide of 1g, the barium monoxide of 9g and 3g potassium oxide composition；
The preparation method of above-mentioned ruthenium system ammonia synthesis catalyst, includes the following steps:
(1) basic magnesium carbonate, active carbon, basic carbonate cerium, molybdenum oxide, tungsten oxide, potassium carbonate and barium carbonate ball milling are mixed It closes, collects granularity and be the mixture of 0.2mm, and the mixture is formed, obtain molding；
(2) by the molding incipient impregnation in mass fraction be 9% urea-containing potassium ruthenate aqueous solution in, The temperature of control dipping is 30 DEG C, and the mass fraction of urea is 8%, after dipping, is taken out；
(3) molding after the dipping is restored in hydrogen, the temperature for controlling reduction is 360 DEG C, and the time is 8h；
(4) molding after the reduction is roasted at 2100 DEG C, obtains ruthenium system ammonia synthesis catalyst.
4) it cools to the gaseous mixture come out from second ammonia convertor and recycles heat, isolated liquefied ammonia With remaining gas, and syngas for synthetic ammonia described in the remaining gas and step 1) is mixed.
Comparative example 1
This comparative example provides a kind of ammonia synthesis technology, includes the following steps:
1) syngas for synthetic ammonia obtains after desulfurization, transformation, desulfuration of shift gas decarburization and refining, wherein S < 5ppm, CO < 10ppm, CO2The molar ratio of < 10ppm, hydrogen and nitrogen is 2.8:1；
It 2) is 5000h with air speed by above-mentioned syngas for synthetic ammonia-1Filling ferrum-based catalyst the first ammonia convertor in into Row level-one ammonia synthesis, the synthesis pressure of the level-one ammonia synthesis is 8MPa, synthesis temperature is 300 DEG C；
Wherein, it is the Fe of 2:2:1 that the ferrum-based catalyst, which is with mass ratio,3O4, FeO and K2O is active constituent, with rare earth Element oxide CeO and MgAl2O4For auxiliary agent, the content of active constituent is 4wt%, rare earth element oxygen in the ferrum-based catalyst Compound content is 0.1wt%, MgAl2O4Content is 0.2wt%.
3) gaseous mixture come out from first ammonia convertor is with air speed 8000h-1Into the of filling ruthenium-based catalyst Second level ammonia synthesis is carried out in two ammonia convertors, the synthesis pressure of the second level ammonia synthesis is 5MPa, synthesis temperature is 380 DEG C；
Wherein, ruthenium system ammonia synthesis catalyst is by the ruthenium of 5g, the magnesia of 5g, the active carbon of 80g, the cerium oxide of 7g, 1.5g Molybdenum oxide and 1.5g tungsten oxide composition；
The preparation method of above-mentioned ruthenium system ammonia synthesis catalyst, includes the following steps:
(1) by basic magnesium carbonate, active carbon, basic carbonate cerium, molybdenum oxide and tungsten oxide ball milling mixing, collecting granularity is The mixture of 0.1mm, and add binder-epoxy resin into the mixture and formed, obtain molding；
(2) by the molding incipient impregnation in mass fraction be 12% potassium ruthenate aqueous solution in, control dipping Temperature be 25 DEG C, after dipping, take out；
(3) molding after the dipping is restored in hydrogen, the temperature for controlling reduction is 350 DEG C, and the time is 9h；
(4) molding after the reduction is roasted at 1900 DEG C, obtains ruthenium system ammonia synthesis catalyst.
Comparative example 2
This comparative example provides a kind of ammonia synthesis technology, includes the following steps:
1) syngas for synthetic ammonia obtains after desulfurization, transformation, desulfuration of shift gas decarburization and refining, wherein S < 5ppm, CO < 10ppm, CO2The molar ratio of < 10ppm, hydrogen and nitrogen is 1.5:1；
It 2) is 12000h with air speed by above-mentioned syngas for synthetic ammonia-1In the first ammonia convertor of filling ruthenium-based catalyst Level-one ammonia synthesis is carried out, the synthesis pressure of the level-one ammonia synthesis is 4MPa, synthesis temperature is 350 DEG C；
Wherein, ruthenium system ammonia synthesis catalyst is by the ruthenium of 2g, the magnesia of 8g, the active carbon of 70g, the cerium oxide of 3g, 2g The tungsten oxide of molybdenum oxide and 1g composition；
The preparation method of above-mentioned ruthenium system ammonia synthesis catalyst, includes the following steps:
(1) by basic magnesium carbonate, active carbon, basic carbonate cerium, molybdenum oxide and tungsten oxide ball milling mixing, collecting granularity is The mixture of 0.05mm, and the mixture is formed, obtain molding；
(2) by the molding incipient impregnation in mass fraction be 8% ruthenic acid sodium aqueous solution in, control dipping Temperature be 40 DEG C, after dipping, take out；
(3) molding after the dipping is restored in hydrogen, the temperature for controlling reduction is 300 DEG C, and the time is 12h；
(4) molding after the reduction is roasted at 2500 DEG C, obtains ruthenium system ammonia synthesis catalyst；
3) gaseous mixture come out from first ammonia convertor is with air speed 6000h-1Into the of filling ferrum-based catalyst Second level ammonia synthesis is carried out in two ammonia convertors, the synthesis pressure of the second level ammonia synthesis is 5MPa, synthesis temperature is 500 DEG C；
Wherein, it is the Fe of 3:1:1 that the ferrum-based catalyst, which is with mass ratio,3O4, FeO and K2O is active constituent, with rare earth Element oxide CeO and MgAl2O4For auxiliary agent, the content of active constituent is 2wt%, rare earth element oxygen in the ferrum-based catalyst Compound content is 0.2wt%, MgAl2O4Content is 0.1wt%；
Comparative example 3
This comparative example provides a kind of ammonia synthesis technology, includes the following steps:
1) syngas for synthetic ammonia obtains after desulfurization, transformation, desulfuration of shift gas decarburization and refining, wherein S < 5ppm, CO < 10ppm, CO2The molar ratio of < 10ppm, hydrogen and nitrogen is 1.5:1；
It 2) is 7000h with air speed by above-mentioned syngas for synthetic ammonia-1In filling ferrum-based catalyst Fe3O4Two it is concatenated Level-one ammonia synthesis is carried out in first ammonia convertor, the synthesis pressure of the level-one ammonia synthesis is 6MPa, synthesis temperature is 450 DEG C；
3) gaseous mixture come out from first ammonia convertor is with air speed 8000h-1Into two concatenated filling ruthenium bases Second level ammonia synthesis is carried out in second ammonia convertor of catalyst, the synthesis pressure of the second level ammonia synthesis is 5.5MPa, synthesis is warm Degree is 400 DEG C；
Wherein, the ruthenium system ammonia synthesis catalyst by the ruthenium of 4g, the magnesia of 6g, the active carbon of 75g, 8g cerium oxide, The molybdenum oxide of 1.5g, the tungsten oxide of 1g, the barium monoxide of 9g and 3g potassium oxide composition；
The preparation method of above-mentioned ruthenium system ammonia synthesis catalyst, includes the following steps:
(1) basic magnesium carbonate, active carbon, basic carbonate cerium, molybdenum oxide, tungsten oxide, potassium carbonate and barium carbonate ball milling are mixed It closes, collects granularity and be the mixture of 0.2mm, and the mixture is formed, obtain molding；
(2) by the molding incipient impregnation in mass fraction be 9% urea-containing potassium ruthenate aqueous solution in, The temperature of control dipping is 30 DEG C, and the mass fraction of urea is 8%, after dipping, is taken out；
(3) molding after the dipping is restored in hydrogen, the temperature for controlling reduction is 360 DEG C, and the time is 8h；
(4) molding after the reduction is roasted at 2100 DEG C, obtains ruthenium system ammonia synthesis catalyst.
4) it cools to the gaseous mixture come out from second ammonia convertor and recycles heat, isolated liquefied ammonia With remaining gas, and syngas for synthetic ammonia described in the remaining gas and step 1) is mixed.
Comparative example 4
This comparative example provides a kind of ruthenium system ammonia synthesis catalyst and preparation method thereof.The ruthenium system ammonia synthesis catalyst by The ruthenium of 5g, the magnesia of 5g, the cerium oxide of 7g, the molybdenum oxide of 1.5g and 1.5g tungsten oxide composition；
The preparation method of above-mentioned ruthenium system ammonia synthesis catalyst, includes the following steps:
1) by basic magnesium carbonate, basic carbonate cerium, molybdenum oxide and tungsten oxide ball milling mixing, collecting granularity is the mixed of 0.1mm Material is closed, and adds binder-epoxy resin into the mixture and is formed, obtains molding；
2) by the molding incipient impregnation in mass fraction be 12% potassium ruthenate aqueous solution in, control dipping Temperature be 25 DEG C, after dipping, take out；
3) molding after the dipping is restored in hydrogen, the temperature for controlling reduction is 350 DEG C, and the time is 9h；
4) molding after the reduction is roasted at 1900 DEG C, obtains ruthenium system ammonia synthesis catalyst.
Comparative example 5
This comparative example provides a kind of ruthenium system ammonia synthesis catalyst and preparation method thereof.The ruthenium system ammonia synthesis catalyst by The ruthenium of 5g, the active carbon of 80g, the cerium oxide of 7g, the molybdenum oxide of 1.5g and 1.5g tungsten oxide composition；
The preparation method of above-mentioned ruthenium system ammonia synthesis catalyst, includes the following steps:
1) by active carbon, basic carbonate cerium, molybdenum oxide and tungsten oxide ball milling mixing, the mixing that granularity is 0.1mm is collected Material, and add binder-epoxy resin into the mixture and formed, obtain molding；
2) by the molding incipient impregnation in mass fraction be 12% potassium ruthenate aqueous solution in, control dipping Temperature be 25 DEG C, after dipping, take out；
3) molding after the dipping is restored in hydrogen, the temperature for controlling reduction is 350 DEG C, and the time is 9h；
4) molding after the reduction is roasted at 1900 DEG C, obtains ruthenium system ammonia synthesis catalyst.
Comparative example 6
This comparative example provides a kind of ruthenium system ammonia synthesis catalyst and preparation method thereof.The ruthenium system ammonia synthesis catalyst by The ruthenium of 8g, the magnesia of 2g, the active carbon of 85g, the cerium oxide of 9g, the molybdenum oxide of 1g, the tungsten oxide of 2g, 6g barium monoxide and The potassium oxide of 6g forms；
The preparation method of above-mentioned ruthenium system ammonia synthesis catalyst, includes the following steps:
1) by magnesia, active carbon, cerium oxide, molybdenum oxide, tungsten oxide, potassium oxide and barium monoxide ball milling mixing, grain is collected Degree is the mixture of 0.5mm, and forms to the mixture, obtains molding；
2) by the molding incipient impregnation in mass fraction be 15% urea-containing potassium ruthenate aqueous solution in, The temperature of control dipping is 10 DEG C, and the mass fraction of urea is 5%, after dipping, is taken out；
3) molding after the dipping is restored in hydrogen, the temperature for controlling reduction is 400 DEG C, and the time is 6h；
4) molding after the reduction is dry at 100 DEG C, obtain ruthenium system ammonia synthesis catalyst.
Test example 1
The various embodiments described above and comparative example 1-3 middle outlet ammonia net value, nitrogen utilization rate and hydrogen utilization ratio are surveyed Fixed, corresponding test result is as follows shown in table 1:
Table 1 exports ammonia net value, nitrogen utilization rate and hydrogen utilization ratio
Learn from table 1: ammonia synthesis process is divided into two sections by the present invention, in specified pressure, particular kind of catalyst, spy Determine to carry out under the unstripped gas of H-N ratio, not only meets ammonia synthesis process requirement, guarantees technique even running, also improve ammonia Synthetic tower exports the utilization rate of ammonia net value and nitrogen and hydrogen.And process operation is steady, low energy consumption.
Test example 2
The Viability survey of ammino is carried out to ruthenium system obtained ammonia synthesis catalyst in above-described embodiment 1-7 and comparative example 4-6 Examination, test process are as follows: the ruthenium system ammonia synthesis catalyst of above-mentioned equivalent be loaded on respectively in stainless steel high pressure ammonia convertor, Reaction gas is hydrogen nitrogen mixed gas, and hydrogen nitrogen volume ratio is 3:1, air speed 10000h-1, reaction pressure 10MPa, reaction temperature It is 425 DEG C.It is corresponding that test result is as follows shown in table 1:
2 ammonia convertor of table is worked off one's feeling vent one's spleen the concentration (V%) of middle ammonia
Learn from table 2: the present invention uses ruthenium, magnesia, active carbon, cerium oxide, molybdenum oxide and tungsten oxide, and limits each Ratio between component.While reducing carbon content, improving vector stabilisation, made using mutual cooperation, the collaboration between each component With not resulting in the Viability reduction of ammino not only, it is Viability to improve ammino instead, has ruthenium system ammonia synthesis catalyst high Ammino is Viability.Specific raw material and maturing temperature are used simultaneously, improve the stability and ammino of ruthenium system ammonia synthesis catalyst It is Viability.
Test example 3
Heat stability testing is carried out to ruthenium system obtained ammonia synthesis catalyst in above-described embodiment 1-7 and comparative example 4-6, Corresponding test process is as follows: being heated to 1000 DEG C in the case where hydrogen content is 25% atmosphere, and maintains 100h, further takes out, press Ammonia synthesis active testing process in test example 2 is tested, and test result is as follows shown in table 3:
3 ammonia convertor of table is worked off one's feeling vent one's spleen the concentration (V%) of middle ammonia
Learnt from table 3: ruthenium system produced by the present invention ammonia synthesis catalyst above-mentioned high temperature and hydrogeneous atmosphere processing after, then Ammonia synthesis active testing is carried out, ammonia convertor outlet ammonia density still can reach 24% or more, show it with high heat resistance Can, and it is not easy methanation, resistance to hydrogen.
Test example 4
Ruthenium system obtained ammonia synthesis in above-described embodiment 1-7 and comparative example 4-6 is tested using Pulse Chemisorption method to be catalyzed The dispersion degree of ruthenium metal in agent, test result is as follows shown in table 4:
The dispersion degree of ruthenium metal in 4 ruthenium system ammonia synthesis catalyst of table
Learn from table 4: the dispersion degree of ruthenium metal reaches 50% or more in ruthenium system produced by the present invention ammonia synthesis catalyst, Show that preparation method of the invention can improve the dispersion degree of ruthenium metal.
Obviously, the above embodiments are merely examples for clarifying the description, and does not limit the embodiments. For those of ordinary skill in the art, other various forms of changes can also be made on the basis of the above description Change or changes.There is no necessity and possibility to exhaust all the enbodiments.And obvious change extended from this Change or changes still within the protection scope of the invention.

Claims (8)

1. a kind of isobaric ammonia synthesis technology of segmentation, includes the following steps:
1) syngas for synthetic ammonia is subjected to level-one ammonia synthesis, the synthesis ammonia in the first ammonia convertor of filling ferrum-based catalyst The air speed of unstripped gas is 4000-6000h-1, the synthesis pressure of the level-one ammonia synthesis is 5-7MPa, the conjunction of the level-one ammonia synthesis It is 430-500 DEG C at temperature, the molar ratio of hydrogen and nitrogen is (1.5-2.5) in the syngas for synthetic ammonia: 1；It is described iron-based Catalyst is with mass ratio for (2-3): (1-2): 1 Fe3O4, FeO and K2O is active constituent, with rare earth oxide and MgAl2O4For auxiliary agent, the content of active constituent is 2-5wt% in the ferrum-based catalyst, and rare earth oxide content is 0.1- 0.2wt%, MgAl2O4Content is 0.1-0.2wt%；
2) it is carried out from the second ammonia convertor that the gaseous mixture come out in first ammonia convertor enters filling ruthenium-based catalyst Second level ammonia synthesis, the air speed of the gaseous mixture are 5000-12000h-1, the synthesis pressure of the second level ammonia synthesis is 4-6MPa, institute The synthesis temperature for stating second level ammonia synthesis is 350-435 DEG C；
The ruthenium-based catalyst, the component including following parts by weight: 2-8 parts of ruthenium, 2-8 parts of magnesia, 70-85 parts of active carbon, oxygen Change cerium 3-10 parts, 1-2 parts of molybdenum oxide, 1-2 parts of tungsten oxide.
2. the isobaric ammonia synthesis technology of segmentation according to claim 1, which is characterized in that the upper half of second ammonia convertor The ruthenium-based catalyst is loaded in part, and the ferrum-based catalyst is loaded in lower half portion, and the syngas for synthetic ammonia is from described first The lower half portion of ammonia convertor enters wherein.
3. the isobaric ammonia synthesis technology of segmentation according to claim 1 or 2, which is characterized in that first ammonia convertor Number is at least one；
The number of second ammonia convertor is at least one.
4. segmentation equipressure ammonia synthesis technology described in any one of -2 according to claim 1, which is characterized in that further include to from institute It states the gaseous mixture come out in the second ammonia convertor to cool and recycle heat, isolated liquefied ammonia and remaining gas, and will be described The step of remaining gas and the syngas for synthetic ammonia mix.
5. the isobaric ammonia synthesis technology of segmentation according to claim 4, which is characterized in that the active carbon is the work of N doping Property charcoal.
6. segmentation equipressure ammonia synthesis technology described in any one of -2 according to claim 1, which is characterized in that the ruthenium-based catalytic Agent further includes the component of following parts by weight:
6-9 parts of barium monoxide
3-9 parts of potassium oxide.
7. the isobaric ammonia synthesis technology of segmentation according to claim 6, which is characterized in that the preparation side of the ruthenium-based catalyst Method includes the following steps:
(1) by basic magnesium carbonate, active carbon, basic carbonate cerium, molybdenum oxide and tungsten oxide ground and mixed, or by basic carbonate Magnesium, active carbon, basic carbonate cerium, molybdenum oxide, tungsten oxide, potassium carbonate and barium carbonate ground and mixed collect mixture, and to described Mixture is formed, and molding is obtained；
(2) by the molding be impregnated in ruthenium compound aqueous solution or urea-containing ruthenium compound aqueous solution in, the leaching After stain, take out；
(3) molding after the dipping is restored under reducing atmosphere；
(4) molding after the reduction is roasted at 1600-2500 DEG C, obtains the ruthenium-based catalyst.
8. segmentation ammonia synthesis technology according to claim 7, which is characterized in that the rare earth oxide is CeO.
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