CN104907076A - Coal carbon dioxide gasification catalyst and preparation method thereof - Google Patents

Abstract

The invention discloses a coal carbon dioxide gasification catalyst and a preparation method thereof. The catalyst is composed of carbon active site loaded on a carrier, the carrier can provide machinery support and can transfer the oxygen atoms or oxygen ions, the carrier contains CO2 active site; the carbon active site and CO2 active site in the carrier are taken as catalytic activity components, transfer for oxygen ions is realized by a oxidation reduction reaction; the carrier transfers the oxygen atoms or oxygen ions, CO2 is taken as an oxidizing agent, and then ground state carbon is gasified to CO. The catalyst has good catalytic activity, compared with a traditional catalyst, the catalyst in the invention has stronger catalysis performance, and the catalysis condition is more peaceful.

Description

A kind of coal carbon dioxide gasification Catalysts and its preparation method

Technical field:

The invention belongs to Coal Gasification Technology field, particularly a kind of coal carbon dioxide gasification Catalysts and its preparation method.

Background technology:

According to bibliographical information, be all play a role under the environment of steam or air for the catalyst major part of gasification of coal, such as U.S. Exxon company is at 20 century 70s, proposes with K ₂cO ₃as catalyst, under 3MPa, 700 DEG C of conditions, utilize steam as gasifying agent, develop by the pressurised fluidized bed catalysis gasification technique of coal produced for the purpose of artificial natural gas, Chinese patent CN103301865A has also done further improvement to this.Compared with steam, carbon dioxide is a kind of more weak oxidant.Due to the structural stability of himself, carbon dioxide has very strong chemical inertness.So the catalytic activity of existing coal gasification catalyst under carbon dioxide atmosphere can significantly reduce, this causes the arch-criminal of greenhouse effects to be synchronously converted into the actual demand of high value added product by coal and carbon dioxide to cause it cannot meet in application process far away.In addition, existing gasifying catalyst is loaded on carbon-based solid reactant by using infusion process.The benefit of this way of contact effectively achieves catalyst to contact with coal solid particle " intimately ", substantially increases catalysis area.But this has created the problem that gasification reaction rear catalyst is difficult to because forming strong interaction (such as chemical bond) with carbon-based solid reactant granular residue recycle completely, greatly reduce the cyclic utilization rate of catalyst, cause the significantly raising of catalyst use amount, thus result in the remarkable rising of coal gasification cost.

Summary of the invention:

The object of the invention is for the deficiencies in the prior art, provides a kind of coal carbon dioxide gasification Catalysts and its preparation method, with solve above-mentioned in the technical problem mentioned.Catalyst prepared by the present invention has can reach high catalytic activity under gentle catalytic condition.

For achieving the above object, the present invention adopts following technical scheme to be achieved:

A kind of coal carbon dioxide gasification catalyst, be made up of on carrier the load of carbon active sites, described carrier for can providing mechanical support and can transmitting oxygen atom or oxonium ion, and includes CO ₂the carrier of active sites; The CO comprised in described carbon active sites and carrier ₂active sites is catalytic active component, realizes the transfer to oxonium ion by redox reaction;

Carrier transfer oxygen atom or oxonium ion, by CO ₂as oxidant, ground state carbon gasification is become CO.

The present invention further improves and is: described carrier is the compound of Multimetal oxide composition, and wherein, carrier mass percent is in the catalyst 80-90%.

The present invention further improves and is: in described carrier, a part of metal oxide plays as active sites provides the effect of mechanical support, and this partial metal oxide thing is Al ₂o ₃, SiO ₂, TiO ₂or ZrO ₂in the composition of any one or more, and mass percent is in the carrier 30-70%;

In described carrier, another part metal oxide plays the effect of transmitting oxygen atom or oxonium ion, and this partial metal oxide thing is CeO ₂or La ₂o ₃, and mass percent is in the carrier 10-30%;

In described carrier, remainder metal oxide plays activation CO ₂effect, be CO ₂active sites, this partial metal oxide thing is ZnO, SnO ₂, Fe ₂o ₃, Ga ₂o ₃, PbO, CuO, Bi ₂o ₃, CeO ₂or La ₂o ₃in the composition of any one or two kinds of, and mass percent is in the carrier 20-60%.

The present invention further improves and is: described carbon active sites is alkali metal, or the mixture of alkali and alkaline earth metal ions; Wherein,

When carbon active sites is alkali metal, alkali-metal mass percent is in the catalyst 10-20%;

When carbon active sites is the mixture of alkali and alkaline earth metal ions, alkali-metal mass percent is in the catalyst 5-15%, and alkaline-earth metal mass percent is in the catalyst 5-15%.

A preparation method for coal carbon dioxide gasification catalyst, comprises the following steps:

1) CO is contained by coprecipitation preparation ₂the carrier of active sites:

1-1) dissolve in deionized water by soluble salt, obtained total ion concentration is the solution A of 0.1 ~ 2mol/L, and wherein, soluble salt is Zn (NO ₃) ₂6H ₂o, Ce (NO ₃) ₃6H ₂o, La (NO ₃) ₃6H ₂o, SnCl ₄, Fe (NO ₃) ₃9H ₂o, Al (NO ₃) ₃9H ₂o, Ga (NO ₃) ₃xH ₂o, Pb (NO ₃) ₂, Cu (NO ₃) ₂2.5H ₂o, Bi (NO ₃) ₃5H ₂one or more in O;

1-2) using ammonia spirit as B solution;

1-3) by solution A with the speed of 2.5mL/min pump into temperature be 30 ~ 50 DEG C containing deionized water pretipitatin jar in;

Speed is added to maintain pH value in pretipitatin jar for 8 ± 0.2 1-4) by adjustment B solution;

1-5) when solution A is pumped into pretipitatin jar completely, orderly close-down, for carrying the peristaltic pump of solution A and B solution, obtains slurry;

Be 1-6) under the condition of 8 ± 0.2 and 30 ~ 50 DEG C, stir rear water and the filtration of methyl alcohol cyclic washing in pH value by slurry, obtain filter cake;

1-7) filter cake obtained is put into baking oven, drying 12 hours at 90 ~ 110 DEG C;

1-8) under moving air, calcine filter cake: be first heated to 120 DEG C and maintain 0.3 hour, being then warmed up to 550 DEG C with the rate of heat addition of 3 DEG C/min, and keeping 4 hours, obtaining containing CO ₂the carrier of active sites;

2) by infusion process, carbon back activated sites is introduced step 1) in obtained containing CO ₂on the carrier of active sites, make coal carbon dioxide gasification catalyst:

2-1) by step 1) obtained containing CO ₂the carrier grinding of active sites becomes A powder;

2-2) magnesium nitrate hexahydrate or calcium nitrate tetrahydrate are dissolved in deionized water, be made into the C solution that concentration is 2 ~ 6mol/L;

2-3) C solution is impregnated on A powder and also stirs simultaneously;

2-4) impregnated A powder is put into drying oven, drying 12 hours at 90 ~ 110 DEG C;

2-5) repeat step 2-3) and 2-4), until all C solution are impregnated into A powder surface, wherein, in the A powder of every g, flood the C solution of 0.65 ~ 2mL;

A powder 2-6) under moving air after calcining dipping: be first heated to 120 DEG C and maintain 0.5 hour, being then warmed up to 600 DEG C with the rate of heat addition of 3 DEG C/min, and keeping 3 hours;

After 2-7) naturally cooling to room temperature, collect calcined product, the calcined product obtained is C powder;

2-8) potassium nitrate is dissolved in ionized water, be made into the transparent solution D that concentration is 2 ~ 6mol/L;

2-9) solution D is impregnated on C powder and also stirs simultaneously;

2-10) impregnated C powder is put into drying oven, drying 12 hours at 90 ~ 110 DEG C;

2-11) repeat step 2-9) and 2-10), until all solution D are impregnated into C powder surface, wherein, in the C powder of every g, flood the solution D of 0.65 ~ 1.5mL;

C powder 2-12) under moving air after calcining dipping: be first heated to 120 DEG C and maintain 0.5 hour, being then warmed up to 800 DEG C with the rate of heat addition of 3 DEG C/min, and keeping 3 hours;

After 2-13) naturally cooling to room temperature, obtained coal carbon dioxide gasification catalyst.

Compared with traditional gasifying catalyst, had the following advantages by the present invention:

1, carbon dioxide gasification is active strong.Described catalyst is because of containing CO ₂active sites, and the oxygen atom generated in carbon dioxide reduction process or oxonium ion effectively can be passed to carbon-based solid raw material (as brown coal etc.) for its partial oxidation.Based on this reason, described catalyst at least exceeds more than one times compared with traditional catalyst activity under carbon dioxide atmosphere.

2, catalyst recovery utilization rate is high.Described catalyst is because taking self supporting structure, to come in contact by means of only physical impacts with carbon-based solid raw material thus chemical reaction occurs, instead of form the chemical bond of certain form as traditional catalyst by the method for chemical impregnation and carbon-based solid raw material thus realize " intimately " and contact.By the change of this way of contact, catalyst provided by the invention fundamentally can solve traditional catalyst and generate in the loose structure of residue after diffusing into carbon-based solid material gasification, form strong interaction and cannot effectively reclaim, catalyst is caused to run off in a large number, the actual application problem that cost significantly rises.The process of the promotion coal gasification industrialization that therefore extensive use of catalyst of the present invention will be strong.

3, without washing recycling step.Compared with traditional gasifying catalyst, catalyst prepared by the present invention is because having very strong mechanical strength, good physical aspect can be kept in recirculating fluidized bed application process, thus can effectively by particle diameter difference realize in cyclone separator with carbon-based solid material gasification after the effective of residue that generate be separated, and can return in gasification burner and again participate in reaction.And traditional catalyst participate in needing after gasification reaction can being realized by the method for washing with carbon-based solid material gasification after the physical separation of residue that generates.This extra water-washing step not only can cause production cost to rise, and inevitably a certain amount of small residue is taken back reaction system, adds secondary separation burden.In addition, for carbon dioxide gasification, water-washing step can produce the industrial wastewater that considerable alkali metal content exceeds standard.Wastewater treatment can bring further cost to increase.

4, the preparation method of catalyst of the present invention, its process is simple, workable, cost performance is high.The catalyst reported in the present invention adopts the method for co-precipitation to prepare carrier, the metal oxide playing different function in carrier is organically merged in molecule aspect, thus facilitate the performance of each component synergistic effect in catalyst carrier to greatest extent, produce better catalytic effect.The co-precipitation used in this catalyst preparation process and the method for dipping, be all the means extensively adopted in Catalyst practical application, operating procedure is very ripe, significantly can reduce the risk and cost of this Catalyst volume production.

Accompanying drawing illustrates:

Fig. 1 is the Catalysis Principles schematic diagram of a kind of coal carbon dioxide gasification catalyst of the present invention;

Fig. 2 is the gasification reactivity of the embodiment of the present invention 1 PetroChina Company Limited. coke under different catalysts;

Fig. 3 is the gasification reactivity of brown coal under different catalysts in the embodiment of the present invention 1;

Fig. 4 is that the present invention uses catalyst obtained in embodiment 1 for the long gasification reactivity of brown coal.

Detailed description of the invention:

Below in conjunction with accompanying drawing, be clearly and completely described the technical scheme in the embodiment of the present invention, obviously, described embodiment is only the present invention's part embodiment, instead of whole embodiments.Based on the embodiment in the present invention, those of ordinary skill in the art, not making the every other embodiment obtained under creative work prerequisite, belong to the scope of protection of the invention.

Embodiment 1

10%K-10%Mg/38%SnO ₂-29%Fe ₂o ₃-33%Al ₂o ₃, the meaning of this molecular formula is: carrier is the SnO of 38% by mass ratio ₂, the Fe of 29% ₂o ₃, and the Al of 33% ₂o ₃composition.Carbon active sites is made up of the Mg of the K and 10% that account for total catalyst weight 10%.

Its preparation process is as follows:

1) synthesis is by SnO ₂-Fe ₂o ₃-Al ₂o ₃the carrier of composition:

1-1) take 12.79g stannic chloride (SnCl ₄), 28.12g ferric nitrate (Fe (NO ₃) ₃) and 47.68g aluminum nitrate (Al (NO ₃) ₃), and dissolved in obtained solution A in 200mL deionized water;

1-2) measure 400mL ammonia spirit as B solution;

1-3) solution A is pumped into the speed of 2.5mL/min to fill 200mL temperature be in the pretipitatin jar of 40 DEG C of initial deionized water amounts;

1-4) equal 8 ± 0.2 by the speed that adds of adjustment B solution with the pH-value (pH) maintained in pretipitatin jar simultaneously;

1-5) when solution A is pumped into pretipitatin jar completely, orderly close-down is for carrying the peristaltic pump of A liquid and B liquid;

1-6) obtained slurry is additionally stirred under required pH=8 ± 0.2 and 40 DEG C of temperature, then repeatedly filter with water and methyl alcohol immediately;

1-7) clean filter cake until thoroughly remove chlorion, with silver nitrate chlorine detection ion;

1-8) then the filter cake after cleaning to be placed in baking oven at 110 DEG C dry 12 hours;

1-9) under moving air, calcine filter cake: be first heated to 120 DEG C and maintain 0.3 hour, then with the rate of heat addition of 3 DEG C/min, filter cake being warmed to 550 DEG C, and keeping 4 hours, obtaining consisting of 38%SnO ₂-29%Fe ₂o ₃-33%Al ₂o ₃catalyst carrier;

2) synthesis is by K-Mg/SnO ₂-Fe ₂o ₃-Al ₂o ₃the catalyst of composition:

2-1) take carrier material that 16g generates by first step coprecipitation and be ground into as A powder;

2-2) take the magnesium nitrate hexahydrate (Mg (NO of 18.77g ₃) ₂6H ₂o) and dissolved in 18mL deionized water, C solution is made into;

2-3) C solution dropper be impregnated into carefully A powder and stir (note the C solution amount at every turn added, ensure that carrier does not want excess humidity) simultaneously;

2-4) impregnated A powder is put into drying oven, be arranged on 110 C overnight dry 12 hours;

2-5) repeat step 2-3) and 2-4), until all C solution are impregnated into A powder surface;

A powder 2-6) under moving air after calcining dipping: be first heated to 120 DEG C and maintain 0.5 hour, then with the rate of heat addition of 3 DEG C/min, filter cake being warmed to 600 DEG C, and keeping 3 hours;

After 2-7) naturally cooling to room temperature, regather calcining powder C;

2-8) take the potassium nitrate (KNO of 5.46g ₃) and dissolved in 15mL ionized water, be made into certain density transparent solution D;

2-9) solution D dropper be impregnated into carefully C powder and stir (note the solution D amount at every turn added, ensure that carrier does not want excess humidity) simultaneously;

2-10) impregnated C powder is put into drying oven, be arranged on 110 C overnight dry 12 hours;

2-11) repeat step 2-9) and 2-10), until all solution D are impregnated into C powder surface;

C powder 2-12) under moving air after calcining dipping: be first heated to 120 DEG C and maintain 0.5 hour, then with the rate of heat addition of 3 DEG C/min, filter cake being warmed to 800 DEG C, and keeping 3 hours;

After 2-13) naturally cooling to room temperature, finally to obtain required catalyst.

The catalyst prepared according to this principle shows good catalytic activity in laboratory stage experiment.As shown in Figure 2, our choice for use petroleum coke (at the knot carbon that catalyst for cracking is formed on the surface in crude refinement processes) is because the high inertia of participation gasification reaction that causes of himself high carbon content (94.8%) as carbon-based solid raw material object of reference.A series of carbonaceous solids raw materials of testing in advance at us (comprise coal, living beings, and domestic waste) in, the gasification reactivity of petroleum coke is the poorest.The catalytic activity developing catalyst can be better assessed like this by being used as object of reference with it.As shown in Figure 2, as predicting before, before not adding catalyst, petroleum coke does not almost have gasification reactivity.When adding traditional optimal catalyst [Wang, the J. that prepare according to literature procedure; Yao, Y.; Cao, J.; Jiang, M.Fuel, 2010,89,310-317] (K-Ca/Al afterwards ₂o ₃), the gasification reactivity of carbon-based solid raw material obtains significant raising.As the new catalyst (K-Mg/SnO using us to prepare ₂-Fe ₂o ₃-Al ₂o ₃) after, gasification reactivity obtains the raising of a nearly step.As shown in Figure 2, improve close to 100 times after the new catalyst of the CO generating rate of petroleum coke after adding optimization.Compared with traditional catalyst, the gasification reactivity of petroleum coke can be enhanced about more than once by catalyst of the present invention further.We select brown coal to be the low combustion value caused because of its elevated oxygen level as the representative of coal simultaneously, are unsuitable for combustion power generation.And it discharges in combustion and causes serious environmental problem to further limit its utilization of simply burning than the more pollutant of other high-grade dants.China's brown coal reserves huge (proved reserves: 1,300 hundred million tons), account for 13.3% of world's coal reserves, are only second to the U.S. and Russia, occupy third place in the world.Therefore one is found can the approach of brown coal to be utilized can to play vital effect to the sustainable development of domestic economy by clean and effective.Research shows, brown coal hydrogasification (controllable oxidization) be the effective approach that its clean and effective utilizes by the generating of obtained syngas combustion or the liquefaction preparation fuel oil of high added value or chemicals.As shown in Figure 3, traditional catalyst (K-Ca/Al is being added ₂o ₃) after, the gasification reactivity of brown coal adds more than 2 times.Even so, (K-Mg/SnO after adding the new catalyst of optimization ₂-Fe ₂o ₃-Al ₂o ₃), the gasification reactivity of brown coal further increases close to 2 times.

According to the preparation method announced in embodiment 1, by changing the parameter in preparation process, also obtaining following examples, systematic research has been carried out to their catalytic performance.The parameter and their relevant catalytic activitys (unlisted parameter is identical with embodiment 1) that use in catalyst process has been itemized in table 1.

Table 1. catalyst 10%K-10%Mg/38%SnO ₂-29%Fe ₂o ₃-33%Al ₂o ₃preparation parameter and gasification reactivity guide look (reaction temperature=800 DEG C, reaction pressure=1atm, gas space velocity=2.36hr ^-1)

According to content disclosed by the invention, by changing the formula of catalyst, also obtaining following examples, systematic research has been carried out to their catalytic performance.The new catalyst and their relevant catalytic activitys partly prepared up till now has been itemized in table 2.

Table 2. catalyst and gasification reactivity guide look (reaction temperature=800 DEG C, reaction pressure=1atm, gas space velocity=2.36hr ^-1)

From above embodiment, can find out, when in catalyst carrier, use only a kind of metal oxide and do not contain CO ₂during active sites, as embodiment 32-43, the maximum CO generating rate of the catalyst of the overwhelming majority and CO ₂conversion ratio all sharply reduces, and its reason can be learnt from the principle of the effect of component and catalysis.

Except testing the above-mentioned reactivity preparing new catalyst, in order to the industrial applications that it is potential, reaction stability also obtains mensuration on a laboratory scale.Fig. 4 shows the brown coal hydrogasification activity of catalyst in 100 hours prepared by the application of the invention embodiment 1.As shown in the figure, CO generating rate and CO ₂conversion ratio all demonstrates certain fluctuation within the testing time of 100 hours.But say from average angle, both maintain stable state roughly.So generally, catalyst presents good catalytic stability at reaction conditions, for it has paved road in the application on more extensive.

The account form of the CO generating rate used in the present invention is as follows:

$r_{\mathrm{CO}}({\min }^{-1}\×{10}^3)=\frac{F_{\mathrm{CO}}/22.414\×28}{W_0}---\left(1\right)$

F in formula (1) _cOrepresent CO volume in normal conditions and generate flow velocity, W ₀the initial mass of reactor carbon back raw material is put in representative.

CO ₂the account form of conversion ratio is as follows:

The foregoing is only preferred embodiment of the present invention, not in order to limit the present invention, within the spirit and principles in the present invention all, any amendment done, equivalent replacement, improvement etc., all should be included within protection scope of the present invention.

Claims (5)

1. a coal carbon dioxide gasification catalyst, is characterized in that: be made up of on carrier the load of carbon active sites, and described carrier for can providing mechanical support and can transmitting oxygen atom or oxonium ion, and includes CO ₂the carrier of active sites; The CO comprised in described carbon active sites and carrier ₂active sites is catalytic active component, realizes the transfer to oxonium ion by redox reaction;

Carrier transfer oxygen atom or oxonium ion, by CO ₂as oxidant, ground state carbon gasification is become CO.

2. coal carbon dioxide gasification catalyst as claimed in claim 1, is characterized in that: described carrier is the compound of Multimetal oxide composition, and wherein, carrier mass percent is in the catalyst 80-90%.

3. coal carbon dioxide gasification catalyst as claimed in claim 2, is characterized in that: in described carrier, a part of metal oxide plays as active sites provides the effect of mechanical support, and this partial metal oxide thing is Al ₂o ₃, SiO ₂, TiO ₂or ZrO ₂in the composition of any one or more, and mass percent is in the carrier 30-70%;

In described carrier, another part metal oxide plays the effect of transmitting oxygen atom or oxonium ion, and this partial metal oxide thing is CeO ₂or La ₂o ₃, and mass percent is in the carrier 10-30%;

In described carrier, remainder metal oxide plays activation CO ₂effect, be CO ₂active sites, this partial metal oxide thing is ZnO, SnO ₂, Fe ₂o ₃, Ga ₂o ₃, PbO, CuO, Bi ₂o ₃, CeO ₂or La ₂o ₃in the composition of any one or two kinds of, and mass percent is in the carrier 20-60%.

4. coal carbon dioxide gasification catalyst as claimed in claim 1, is characterized in that: described carbon active sites is alkali metal, or the mixture of alkali and alkaline earth metal ions; Wherein,

When carbon active sites is alkali metal, alkali-metal mass percent is in the catalyst 10-20%;

When carbon active sites is the mixture of alkali and alkaline earth metal ions, alkali-metal mass percent is in the catalyst 5-15%, and alkaline-earth metal mass percent is in the catalyst 5-15%.

5. the preparation method of the coal carbon dioxide gasification catalyst according to any one of claim 1-4, is characterized in that, comprise the following steps:

1) CO is contained by coprecipitation preparation ₂the carrier of active sites:

1-1) dissolve in deionized water by soluble salt, obtained total ion concentration is the solution A of 0.1 ~ 2mol/L, and wherein, soluble salt is Zn (NO ₃) ₂6H ₂o, Ce (NO ₃) ₃6H ₂o, La (NO ₃) ₃6H ₂o, SnCl ₄, Fe (NO ₃) ₃9H ₂o, Al (NO ₃) ₃9H ₂o, Ga (NO ₃) ₃xH ₂o, Pb (NO ₃) ₂, Cu (NO ₃) ₂2.5H ₂o, Bi (NO ₃) ₃5H ₂one or more in O;

1-2) using ammonia spirit as B solution;

1-3) by solution A with the speed of 2.5mL/min pump into temperature be 30 ~ 50 DEG C containing deionized water pretipitatin jar in;

Speed is added to maintain pH value in pretipitatin jar for 8 ± 0.2 1-4) by adjustment B solution;

1-5) when solution A is pumped into pretipitatin jar completely, orderly close-down, for carrying the peristaltic pump of solution A and B solution, obtains slurry;

Be 1-6) under the condition of 8 ± 0.2 and 30 ~ 50 DEG C, stir rear water and the filtration of methyl alcohol cyclic washing in pH value by slurry, obtain filter cake;

1-7) filter cake obtained is put into baking oven, drying 12 hours at 90 ~ 110 DEG C;

1-8) under moving air, calcine filter cake: be first heated to 120 DEG C and maintain 0.3 hour, being then warmed up to 550 DEG C with the rate of heat addition of 3 DEG C/min, and keeping 4 hours, obtaining containing CO ₂the carrier of active sites;

2) by infusion process, carbon back activated sites is introduced step 1) in obtained containing CO ₂on the carrier of active sites, make coal carbon dioxide gasification catalyst:

2-1) by step 1) obtained containing CO ₂the carrier grinding of active sites becomes A powder;

2-2) magnesium nitrate hexahydrate or calcium nitrate tetrahydrate are dissolved in deionized water, be made into the C solution that concentration is 2 ~ 6mol/L;

2-3) C solution is impregnated on A powder and also stirs simultaneously;

2-4) impregnated A powder is put into drying oven, drying 12 hours at 90 ~ 110 DEG C;

2-5) repeat step 2-3) and 2-4), until all C solution are impregnated into A powder surface, wherein, in the A powder of every g, flood the C solution of 0.65 ~ 2mL;

A powder 2-6) under moving air after calcining dipping: be first heated to 120 DEG C and maintain 0.5 hour, being then warmed up to 600 DEG C with the rate of heat addition of 3 DEG C/min, and keeping 3 hours;

After 2-7) naturally cooling to room temperature, collect calcined product, the calcined product obtained is C powder;

2-8) potassium nitrate is dissolved in ionized water, be made into the transparent solution D that concentration is 2 ~ 6mol/L;

2-9) solution D is impregnated on C powder and also stirs simultaneously;

2-10) impregnated C powder is put into drying oven, drying 12 hours at 90 ~ 110 DEG C;

2-11) repeat step 2-9) and 2-10), until all solution D are impregnated into C powder surface, wherein, in the C powder of every g, flood the solution D of 0.65 ~ 1.5mL;

C powder 2-12) under moving air after calcining dipping: be first heated to 120 DEG C and maintain 0.5 hour, being then warmed up to 800 DEG C with the rate of heat addition of 3 DEG C/min, and keeping 3 hours;

After 2-13) naturally cooling to room temperature, obtained coal carbon dioxide gasification catalyst.