阅读说明：本技术 一种无烟煤水蒸气气化的方法 (Steam gasification method for smokeless coal ) 是由 李娜 刘鲁峰 刘全生 史肃龙 于 2020-07-24 设计创作，主要内容包括：本发明提供了一种无烟煤水蒸气气化的方法,包括以下步骤：将无烟煤进行酸洗脱矿,再氧化处理,最后与钙源混合,得到的添钙煤样与水蒸气进行气化反应。本发明通过氧化为脱矿无烟煤添加大量的羧基官能团,且降低了无烟煤的石墨化程度,再结合钙源中的Ca<Sup>2+</Sup>,提高了气化性能,并且使反应温区提前。实施例结果表明,本发明提供的无烟煤水蒸气气化的方法,水蒸气气化的起始温度为560℃,710℃时合成气的生成速率达到最大；H<Sub>2</Sub>最大生成速率为1.480mmol·min<Sup>-1</Sup>·g<Sup>-1</Sup>,CO<Sub>2</Sub>最大生成速率为0.493mmol·min<Sup>-1</Sup>·g<Sup>-1</Sup>,碳转化率在750℃后趋于平缓,在850℃时达到最高。(The invention provides a method for gasifying smokeless coal steam, which comprises the following steps: the anthracite is subjected to acid washing and demineralization, then is subjected to oxidation treatment, and finally is mixed with a calcium source, so that the obtained calcium-added coal sample is subjected to gasification reaction with steam. According to the invention, a large amount of carboxyl functional groups are added to the demineralized anthracite through oxidation, the graphitization degree of the anthracite is reduced, and Ca in a calcium source is combined 2+ The gasification performance is improved, and the reaction temperature zone is advanced. The results of the examples show that the steam gasification starting temperature of the smokeless coal provided by the invention is 560 ℃, and the generation rate of the synthesis gas reaches the maximum at 710 ℃; h 2 The maximum generation rate is 1.480 mmol/min ‑1 ·g ‑1 ，CO 2 The maximum generation rate is 0.493 mmol/min ‑1 ·g ‑1 Carbon conversion levels off after 750 ℃ and reaches a maximum at 850 ℃.)

1. A method for steam gasification of anthracite is characterized by comprising the following steps:

(1) carrying out acid washing and demineralization on the anthracite to obtain demineralized anthracite;

(2) carrying out oxidation treatment on the demineralized anthracite obtained in the step (1) to obtain oxidized anthracite;

(3) mixing the oxidized anthracite obtained in the step (2) with a calcium source to obtain a calcium-added coal sample;

(4) and (4) taking inert gas as carrier gas, and carrying water vapor to carry out gasification reaction with the calcium-added coal sample obtained in the step (3).

2. The method according to claim 1, wherein the acid pickling and demineralizing in the step (1) comprises: washing the anthracite by sequentially adopting a hydrochloric acid solution and a hydrofluoric acid solution;

the mass concentration of the hydrochloric acid solution is 15-20%, and the mass concentration of the hydrofluoric acid solution is 30-40%.

3. The method according to claim 1, wherein the size of the demineralized anthracite coal in step (2) is 200-400 mesh.

4. The method according to claim 1, wherein the oxidation treatment in step (2) is a modified Hummer method.

5. The method of claim 4, wherein the modified Hummer method comprises the steps of:

mixing the demineralized anthracite with concentrated sulfuric acid to obtain black turbid liquid;

mixing potassium permanganate with the black turbid liquid at the temperature of between 2 ℃ below zero and 6 ℃ below zero to obtain a mixed liquid;

carrying out a first oxidation-reduction reaction on the mixed solution at the temperature of 30-40 ℃ to obtain a brown turbid solution;

mixing the brown turbid liquid with distilled water to obtain a yellow brown turbid liquid;

and carrying out a second oxidation reduction reaction on the yellow brown turbid liquid and hydrogen peroxide to obtain the oxidized anthracite.

6. The method of claim 1, wherein the calcium source in step (3) comprises calcium hydroxide.

7. The method according to claim 1, wherein the oxidized anthracite coal in step (3) is mixed with Ca from a calcium source²⁺The mass ratio of (1) to (5-6) is 100.

8. The method of claim 1, wherein the inert gas in step (4) comprises one or more of argon, neon, and helium.

9. The method according to claim 1, wherein the volume ratio of the inert gas to the water vapor in the step (4) is 1: 1.

10. The method as claimed in claim 1, wherein the temperature of the gasification reaction in the step (4) is 560-870 ℃.

Technical Field

The invention relates to the technical field of coal gasification, in particular to a smokeless coal steam gasification method.

Background

In the world energy reserves, coal accounts for about 79%, and research and development of coal utilization technologies are one of important contents of energy strategies. Coal gasification is used as a process of converting combustible parts in coal or coal coke into gas fuel or downstream raw materials by taking the coal or the coal coke as a raw material and taking oxygen, water vapor or hydrogen and the like as a gasification agent through chemical reaction under a high-temperature condition, so that the utilization efficiency of the coal can be improved, the emission of nitrogen oxide compounds and sulfur-containing compounds in the gasification process can be reduced, and the clean and efficient utilization of the coal is realized.

The anthracite as the coal with the largest coalification degree has high fixed carbon content, low volatile component, compact structure and high ignition point, so the reactivity is poorer when the anthracite is gasified with steam, and the gasification reaction needs to be carried out at higher temperature, thereby restricting the application of the anthracite in the technical field of coal gasification.

Disclosure of Invention

The invention aims to provide a method for gasifying smokeless coal steam, which can improve the gasification performance of the smokeless coal steam gasification reaction and reduce the temperature zone of the gasification reaction, so that the smokeless coal steam gasification reaction can be carried out in a lower temperature zone, and synthesis gas with higher hydrogen content is generated.

In order to achieve the above object, the present invention provides the following technical solutions:

the invention provides a method for gasifying smokeless coal steam, which comprises the following steps:

(1) carrying out acid washing and demineralization on the anthracite to obtain demineralized anthracite;

(2) carrying out oxidation treatment on the demineralized anthracite obtained in the step (1) to obtain oxidized anthracite;

(3) mixing the oxidized anthracite obtained in the step (2) with a calcium source to obtain a calcium-added coal sample;

(4) and (4) taking inert gas as carrier gas, and carrying water vapor to carry out gasification reaction with the calcium-added coal sample obtained in the step (3).

Preferably, the acid pickling and demineralizing in the step (1) comprises: washing the anthracite by sequentially adopting a hydrochloric acid solution and a hydrofluoric acid solution; the mass concentration of the hydrochloric acid solution is 15-20%, and the mass concentration of the hydrofluoric acid solution is 30-40%.

Preferably, the particle size of the demineralized anthracite in the step (2) is 200-400 meshes.

Preferably, the method of oxidation treatment in step (2) is a modified Hummer method.

Preferably, the modified Hummer method comprises the steps of:

mixing the demineralized anthracite with concentrated sulfuric acid to obtain black turbid liquid;

mixing potassium permanganate with the black turbid liquid at the temperature of between 2 ℃ below zero and 6 ℃ below zero to obtain a mixed liquid;

carrying out a first oxidation-reduction reaction on the mixed solution at the temperature of 30-40 ℃ to obtain a brown turbid solution;

mixing the brown turbid liquid with distilled water to obtain a yellow brown turbid liquid;

and carrying out a second oxidation reduction reaction on the yellow brown turbid liquid and hydrogen peroxide to obtain the oxidized anthracite.

Preferably, the calcium source in step (3) comprises calcium hydroxide.

Preferably, the oxidized anthracite in the step (3) and Ca in the calcium source²⁺The mass ratio of (1) to (5-6) is 100.

Preferably, the inert gas in step (4) includes one or more of argon, neon and helium.

Preferably, the volume ratio of the inert gas to the water vapor in the step (4) is 1: 1.

Preferably, the temperature of the gasification reaction in the step (4) is 560-870 ℃.

The invention provides a method for gasifying smokeless coal steam, which comprises the following steps: carrying out acid washing and demineralization on the anthracite to obtain demineralized anthracite; carrying out oxidation treatment on the demineralized anthracite to obtain oxidized anthracite; mixing the oxidized anthracite coal with a calcium source to obtain a calcium-added coal sample; and taking inert gas as carrier gas, and loading water vapor in the inert gas to carry out gasification reaction with the calcium-added coal sample. The invention removes the inherent mineral in the anthracite by acid cleaning, thereby eliminating the interference of the inherent mineral, and then adds a large amount of carboxyl to the demineralized anthracite by the method of oxidationFunctional group, and destroying macromolecular benzene ring structure in coal molecule to reduce its graphitization degree, and finally adding calcium source and Ca in calcium source²⁺The synergistic effect of the carboxyl functional group in the oxidized anthracite coal improves the gasification performance of the steam gasification reaction of the anthracite coal, and can also reduce the temperature area of the gasification reaction, so that the steam gasification reaction of the anthracite coal can be carried out in a lower temperature area. The results of the examples show that the method for steam gasification of anthracite provided by the invention has the advantages that the initial temperature of the gasification reaction is 560 ℃, and the generation rate of the synthesis gas can be maximized when the temperature is 710 ℃; synthesis gas consisting essentially of H₂With CO₂Composition of, wherein H₂The maximum generation rate of (A) is 1.480 mmol/min^-1·g^-1，CO₂The maximum generation rate of (2) is 0.493 mmol/min^-1·g^-1，H₂With CO₂The cumulative amounts of (a) and (b) are 97.54mmol · g, respectively^-1And 32.69 mmol. multidot.g^-1(ii) a The carbon conversion rate tends to be flat after the temperature reaches 750 ℃ and reaches the maximum at 850 ℃.

Drawings

FIG. 1 is TT obtained in example 1 of the present invention⁺SEM picture and EDS spectrum of O-Ca;

FIG. 2 is TT obtained in comparative example 1⁺SEM images and EDS spectra of (a);

FIG. 3 is TT obtained in comparative example 2⁺SEM picture and EDS spectrum of Ca;

FIG. 4 is TT obtained in comparative example 3⁺SEM images and EDS spectra of O;

FIG. 5 is TT obtained in comparative example 4⁺-SEM picture and EDS spectrum of D-Ca;

FIG. 6 is TT obtained in comparative example 5⁺SEM picture and EDS spectrum of C-Ca;

FIG. 7 is a Raman spectrum of coal samples of comparative examples 1 to 5 and example 1 of the present invention;

FIG. 8 is a graph showing R values of coal samples in comparative examples 1 to 5 and example 1 of the present invention_dA graph of values;

FIG. 9 is an FTIR spectrum of a coal sample of comparative examples 1-5 and inventive example 1;

FIG. 10 is TT obtained in example 1 of the present invention⁺-a syngas generation rate map of O-Ca;

FIG. 11 is TT obtained in comparative example 1⁺A syngas generation rate map of;

FIG. 12 is TT obtained in comparative example 2⁺-a syngas generation rate map of Ca;

FIG. 13 is TT obtained in comparative example 3⁺-a syngas generation rate map of O;

FIG. 14 is TT obtained from comparative example 4⁺-a syngas generation rate map of D-Ca;

FIG. 15 is TT obtained in comparative example 5⁺-a syngas generation rate map for C-Ca;

FIG. 16 is a graph showing cumulative yields of syngas produced from coal samples in comparative examples 1 to 5 and example 1 of the present invention;

FIG. 17 is a composition diagram of generated gas of coal samples in comparative examples 1 to 5 and example 1 of the present invention;

FIG. 18 shows synthesis gas H generated from coal samples in comparative examples 1 to 5 and example 1 of the present invention₂a/CO content ratio diagram;

FIG. 19 is a graph of carbon conversion for coal samples of comparative examples 1-5 and inventive example 1.

Detailed Description

The invention provides a method for gasifying smokeless coal steam, which comprises the following steps:

(1) carrying out acid washing and demineralization on the anthracite to obtain demineralized anthracite;

(2) carrying out oxidation treatment on the demineralized anthracite obtained in the step (1) to obtain oxidized anthracite;

(3) mixing the oxidized anthracite obtained in the step (2) with a calcium source to obtain a calcium-added coal sample;

(4) and (4) taking inert gas as carrier gas, and carrying water vapor to carry out gasification reaction with the calcium-added coal sample obtained in the step (3).

The invention carries out acid washing and demineralization on the anthracite to obtain the demineralized anthracite. The type and source of the anthracite coal are not particularly limited, and the steam gasification method of the anthracite coal provided by the invention is suitable for various anthracite coals which are well known to those skilled in the art. In the present invention, the anthracite is preferably a Tabon ceramic cover anthracite in Mongolia.

The method of acid pickling and demineralizing is not particularly limited in the present invention, and any method known to those skilled in the art can be used. In the invention, the time for acid washing and demineralization is preferably 20-30 h, and more preferably 24 h. In the invention, the acid pickling and demineralization can remove the interference of inherent minerals in the anthracite, and the gasification performance of the steam gasification reaction of the anthracite is improved after calcium is added, thereby showing Ca²⁺The catalytic action on the smokeless coal gasification.

In the present invention, the acid pickling demineralization preferably includes: and washing the anthracite by sequentially adopting a hydrochloric acid solution and a hydrofluoric acid solution. In the invention, the washing time of the hydrochloric acid solution is preferably 8-15 h, and more preferably 10-12 h; the washing time of the hydrofluoric acid solution is preferably 10-15 hours, and more preferably 12-14 hours. In the invention, the mass concentration of the hydrochloric acid solution is preferably 15-20%, and more preferably 17%; the mass concentration of the hydrofluoric acid solution is preferably 30-40%, and more preferably 40%. In the present invention, the solvent of the hydrochloric acid solution and the hydrofluoric acid solution is preferably water. The method for preparing the hydrochloric acid solution and the hydrofluoric acid solution is not particularly limited in the present invention, and the hydrochloric acid solution and the hydrofluoric acid solution may be prepared by a method known to those skilled in the art. In the invention, the volume ratio of the mass of the anthracite to the hydrochloric acid solution is preferably 1g to 10 mL; the ratio of the mass of the anthracite to the volume of the hydrofluoric acid solution is preferably 1g to 10 mL. According to the invention, the anthracite is preferably washed by sequentially adopting the hydrochloric acid solution and the hydrofluoric acid solution, so that inherent minerals in the anthracite can be better removed.

In the present invention, the acid pickling demineralization is preferably performed under stirring conditions; the rotation speed of stirring in the washing process of the hydrochloric acid solution and the washing process of the hydrofluoric acid solution is preferably 200-240 r.min independently^-1More preferably 200 r.min^-1。

After the acid pickling and demineralization are finished, the product of the acid pickling and demineralization is preferably filtered and dried to obtain the demineralized anthracite. The filtration method is not particularly limited in the present invention, and a filtration method known to those skilled in the art may be used. In the present invention, the filtration is preferably suction filtration. The filtration apparatus of the present invention is not particularly limited, and a filtration apparatus known to those skilled in the art may be used. In the present invention, the filtration device is preferably a buchner funnel.

The drying method is not particularly limited in the present invention, and a drying method known to those skilled in the art may be used. In the invention, the drying temperature is preferably 100-110 ℃, and more preferably 105 ℃; the drying time is preferably 12 h; the drying atmosphere is preferably a nitrogen atmosphere.

In the invention, the particle size of the demineralized anthracite is preferably 200-400 meshes, and more preferably 200 meshes. In the present invention, when the particle size of the demineralized anthracite coal does not meet the above-mentioned conditions, it is preferred that the demineralized anthracite coal is first crushed. The crushing mode of the demineralized anthracite is not particularly limited, and the crushing mode known by the person skilled in the art can be adopted.

After the demineralized anthracite is obtained, the invention carries out oxidation treatment on the demineralized anthracite to obtain the oxidized anthracite. In the invention, a large amount of carboxyl functional groups appear in the demineralized anthracite through oxidation treatment, and the benzene ring structure in coal molecules is damaged to reduce the graphitization degree, thereby improving the steam gasification reaction performance of the anthracite.

In the present invention, the method of the oxidation treatment is not particularly limited, and a method of the oxidation treatment known to those skilled in the art may be used. In the present invention, the oxidation treatment is preferably a modified Hummer method. In the present invention, the modified Hummer method preferably comprises the steps of: mixing the demineralized anthracite with concentrated sulfuric acid to obtain black turbid liquid; mixing potassium permanganate with the black turbid liquid at the temperature of between 2 ℃ below zero and 6 ℃ below zero to obtain a mixed liquid; carrying out a first oxidation-reduction reaction on the mixed solution at the temperature of 30-40 ℃ to obtain a brown turbid solution; mixing the brown turbid liquid with distilled water to obtain a yellow brown turbid liquid; and carrying out a second oxidation reduction reaction on the yellow brown turbid liquid and hydrogen peroxide to obtain the oxidized anthracite.

The invention is superiorAnd mixing the demineralized anthracite with concentrated sulfuric acid to obtain black turbid liquid. In the invention, the mass concentration of the concentrated sulfuric acid is preferably 98%, and the volume ratio of the mass of the demineralized anthracite to the concentrated sulfuric acid is preferably (10-15) g: (160-180) mL, more preferably 10 g: 180 mL. The operation of mixing the demineralized anthracite and the concentrated sulfuric acid is not particularly limited in the invention, and the technical scheme for preparing the mixture which is well known to the skilled person can be adopted. In the invention, the mixing of the demineralized anthracite and concentrated sulfuric acid is preferably carried out under the condition of stirring; the rotating speed of the stirring is preferably 200-240 r.min^-1More preferably 200 r.min^-1The stirring time is preferably 2-6 h, and more preferably 3 h. In the invention, the strong acid environment is formed by mixing the demineralized anthracite and concentrated sulfuric acid.

After the black turbid liquid is obtained, the potassium permanganate is preferably added into the black turbid liquid at the temperature of between 2 ℃ below zero and 6 ℃ below zero to obtain a mixed liquid. In the invention, the mixing temperature of the potassium permanganate and the black turbid liquid is more preferably-4 ℃. In the invention, the mass ratio of the potassium permanganate to the demineralized anthracite is preferably 3-5: 1, and more preferably 3: 1.

And (3) after a mixed solution is obtained, carrying out a first oxidation-reduction reaction at the temperature of 30-40 ℃ to obtain a brown turbid solution. In the present invention, the temperature of the first redox reaction is more preferably 35 ℃. In the invention, the time of the first oxidation-reduction reaction is preferably 1-4 h, and more preferably 2-3 h. In the invention, through the first oxidation reaction, the anthracite contains a large amount of carboxyl functional groups, and further the gasification performance of the steam gasification reaction of the anthracite is improved.

In the present invention, the first redox reaction is preferably carried out under stirring conditions; the rotating speed of the stirring is preferably 100-200 r.min^-1More preferably 200 r.min^-1。

After the brown turbid solution is obtained, the brown turbid solution is preferably mixed with distilled water to obtain a yellow brown turbid solution. The operation of mixing the brown turbid liquid and the distilled water is not particularly limited in the invention, and the technical scheme for preparing the mixture, which is well known to those skilled in the art, can be adopted.

After the yellow brown turbid liquid is obtained, hydrogen peroxide is added for the second oxidation reduction reaction, and the oxidized anthracite is obtained. In the invention, the mass concentration of the hydrogen peroxide is preferably 25-35%, and more preferably 30%; the dosage of the hydrogen peroxide is preferably that no bubbles are generated in the reaction. In the invention, the temperature of the second redox reaction is preferably 80-100 ℃, and more preferably 85-95 ℃; the time of the second redox reaction is preferably 1-2 h, and more preferably 2 h. In the invention, the residual potassium permanganate and manganese dioxide by-products in the first oxidation-reduction reaction are reduced into soluble salts by adding hydrogen peroxide, and then the soluble salts are removed by post-treatment.

After the second redox reaction is completed, the present invention preferably post-treats the product of the second redox reaction to obtain oxidized anthracite. In the present invention, the post-treatment preferably includes filtration, washing and drying, which are performed in this order. The operation of filtering, washing and drying is not particularly limited in the present invention, and the technical scheme of filtering, washing and drying known to those skilled in the art can be adopted. In the present invention, the filtration is preferably suction filtration. In the present invention, the washing detergent is preferably distilled water. In the invention, the drying temperature is preferably 50-80 ℃, and more preferably 60 ℃; the drying time is preferably 10-15 h, and more preferably 12 h.

After the oxidized anthracite is obtained, the oxidized anthracite is mixed with a calcium source to obtain a calcium-added coal sample. In the invention, the calcium source is added to reduce the temperature zone of the steam gasification reaction of the anthracite, and the calcium source can be combined with the carboxyl functional group contained in the oxidized anthracite, thereby improving the gasification performance of the steam gasification reaction of the anthracite.

The source of the calcium source is not particularly limited in the present invention, and a calcium source known to those skilled in the art may be used. In the present invention, the calcium source is preferably calcium hydroxide; ca in the oxidized anthracite and the calcium source²⁺The mass ratio of (A) to (B) is preferably 100 (5-6), more preferably 100: 5. The invention preferably combines the oxidized anthracite coal with Ca in a calcium source²⁺Quality of (1)The amount ratio is defined within the above range, and the resulting mixture has better vaporization performance in the vaporization reaction with water vapor.

The operation of mixing the oxidized anthracite coal with the calcium source is not particularly limited in the present invention, and the technical scheme for preparing the mixture, which is well known to those skilled in the art, can be adopted. In the present invention, the mixing of the oxidized anthracite coal with the calcium source is preferably an impregnation process. In the present invention, the impregnation method is preferably: and mixing the water solution of the calcium source with the oxidized anthracite, and drying to obtain a mixture. In the present invention, the mixing of the aqueous solution of the calcium source with the oxidized anthracite coal is preferably mixed under agitation conditions; the rotation speed of the stirring is preferably 200-240 r.min^-1More preferably 220 r.min^-1(ii) a The stirring time is preferably 3-6 h, and preferably 4-5 h. In the invention, the drying temperature is preferably 100-110 ℃, and more preferably 105 ℃; the drying time is preferably 10-15 h, and more preferably 12 h; the drying atmosphere is preferably a nitrogen atmosphere.

The method for preparing the aqueous solution of the calcium source in the present invention is not particularly limited, and a solution preparation method known to those skilled in the art may be used. The invention preferably adds deionized water to the ground calcium source to obtain an aqueous solution of the calcium source.

After the calcium-added coal sample is obtained, the invention takes inert gas as carrier gas, and carries water vapor to carry out gasification reaction with the calcium-added coal sample. The kind of the inert gas is not particularly limited in the present invention, and an inert gas known to those skilled in the art may be used. In the present invention, the inert gas preferably includes one or more of argon, neon and helium, and more preferably argon. In the present invention, the volume ratio of the inert gas to the water vapor is preferably 1: 1. In the present invention, the flow rate of the inert gas is preferably 0.12 to 0.14mL/min, and more preferably 0.13 mL/min. The apparatus for the gasification reaction in the present invention is not particularly limited, and a gasification reaction apparatus known to those skilled in the art may be used. In the present invention, the apparatus for the gasification reaction is preferably a fixed bed reactor of WFSM-3060TL type.

The calcium-added coal sample is preferably subjected to first heating to 200 ℃ in an inert gas atmosphere, then the inert gas is taken as a carrier gas to carry water vapor, the water vapor and the calcium-added coal sample are subjected to second heating to 500 ℃, then the third heating is carried out to 850 ℃, and then the temperature is kept for 50-100 min. In the invention, the coal sample is preheated by first heating, then the calcium-added coal sample and the steam are subjected to gasification reaction by second heating, and finally the gasification reaction is completed by third heating.

In the invention, the rates of the first heating and the second heating are independently preferably 15-20 ℃/min, and more preferably 15 ℃/min; the third heating rate is preferably 2-5 ℃/min, and more preferably 2 ℃/min. In the present invention, after the third heating, a constant temperature treatment is performed, and the time of the constant temperature treatment is preferably 50min to 100min, and more preferably 60 min.

The method for steam gasification of the anthracite provided by the invention starts to have obvious gasification reaction at the temperature of 560 ℃, and the generation rate of the synthesis gas can reach the maximum when the temperature is 710 ℃; h in synthesis gas₂The maximum generation rate of (A) is 1.480 mmol/min^-1·g^-1，CO₂The maximum generation rate of (2) is 0.493 mmol/min^-1·g^-1，H₂With CO₂The cumulative amounts of (a) and (b) are 97.54mmol · g, respectively^-1And 32.69 mmol. multidot.g^-1(ii) a The carbon conversion rate tends to be flat after the temperature reaches 750 ℃ and reaches the maximum at 850 ℃.

In the present invention, the mode of monitoring the generated gas is preferably monitored by using an SP-2100A gas chromatograph.

In the present invention, the calculation of the gas generation rate is preferably calculated using the equations shown in formula 1 and formula 2:

wherein y is_i，out(%, v/v) represents the volume concentration of gas i, i representsH₂，CO，CH₄And CO₂。V_total(ml·min^-1) Indicating the total flow of reaction outlet gas. V is the flow velocity of the carrier gas Ar, m_coalIs the mass of the sample loaded into the reactor.

Cumulative gas yield and cumulative H₂The molar ratio/CO is preferably calculated using the equations shown in formula 3 and formula 4:

wherein, F_T，i，jIs the cumulative amount of gas generated at temperature j. Calculating cumulative H by expression₂Mole ratio of/CO (P)_T)。

The technical solution of the present invention will be clearly and completely described below with reference to the embodiments of the present invention. It is to be understood that the described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.