KR20150037398A - The apparatus for dry reforming of methane - Google Patents

The apparatus for dry reforming of methane Download PDF

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KR20150037398A
KR20150037398A KR20130116944A KR20130116944A KR20150037398A KR 20150037398 A KR20150037398 A KR 20150037398A KR 20130116944 A KR20130116944 A KR 20130116944A KR 20130116944 A KR20130116944 A KR 20130116944A KR 20150037398 A KR20150037398 A KR 20150037398A
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methane
carbon dioxide
catalyst
dry reforming
containing gas
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KR20130116944A
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KR101528037B1 (en
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이인범
황희원
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주식회사 포스코
포항공과대학교 산학협력단
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    • 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
    • B01J12/00—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C9/00—Aliphatic saturated hydrocarbons
    • C07C9/02—Aliphatic saturated hydrocarbons with one to four carbon atoms
    • C07C9/04—Methane
    • 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
    • Y02P20/584—Recycling of catalysts

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)

Abstract

The present invention relates to an apparatus for dry reforming of methane, which performs the reaction of dry reforming of methane using flowing catalysts, collects and regenerates catalysts which are discharged along with hydrogen and carbon monoxide generated by the reaction, and make the catalysts available for reuse in the reaction. The present invention removes carbon deposited on catalysts to regenerate the catalysts, thereby resolving the conventional problem related to inactivation of catalysts by deposition of carbon and also reducing input amount of new catalysts due to regeneration of the catalysts to lower process operation costs for economic benefits. Also, the present invention allows for catalysts to float and flow in a reactor with introduction of gas containing carbon dioxide and methane and to induce the reaction of dry reforming of methane, thereby increasing contact efficiency of catalysts and reactants such as carbon dioxide and methane to improve the conversion rate of methane to hydrogen, i.e. to increase the generated amount of hydrogen significantly.

Description

[0001] The present invention relates to a dry reforming apparatus for methane,

The present invention relates to a process for reforming methane by performing a dry reforming reaction of methane using a flowing catalyst and collecting the catalyst discharged together with hydrogen and carbon monoxide generated by the reaction and regenerating the same for reuse in the reforming reaction Methane dry reforming equipment.

And this gas affects the global warming include carbon dioxide, chlorofluorocarbons (CFC), nitrous oxide (N 2 O), methane (CH 4), etc., of which carbon dioxide is known to account for more than about 55%.

Recently, efforts to regulate carbon dioxide emissions have been expanding internationally, and related process technologies for improving energy efficiency, development of alternative energy, and recycling of carbon dioxide have been highlighted.

Techniques for recycling carbon dioxide include a method in which carbon dioxide is reacted with methane to form a mixture of hydrogen and carbon monoxide (hereinafter referred to as "dry reforming reaction of methane"). Methane, which accounts for 80% of the natural gas, is rich in reserves and has been actively studied since it reacts with carbon dioxide to obtain synthetic gas with high added value as a chemical raw material.

The dry reforming reaction of methane with carbon dioxide is carried out as shown in the following reaction formula (1).

CH 4 + CO 2 ? 2CO + 2H 2 (1)

In the dry reforming reaction of methane, hydrogen generated in the reaction of the reaction formula (1) and carbon dioxide, which is a reactant, react with not only the reaction of the reaction formula (1) but also the side reaction to form a reverse aqueous gasification reaction And the Boudouard reaction as shown in the following reaction formula (3) or the carbon precipitation reaction of the following reaction formulas (4) to (6) are performed in addition to the above.

CO 2 + H2 → CO + H 2 O Reaction (2)

2CO → C + CO 2 Reaction formula (3)

CO + H 2 → C + H 2 O Reaction formula (4)

CH 4 → C + 2H 2 Reaction formula (5)

CO 2 → C + O 2 Reaction formula (6)

Meanwhile, the dry reforming reaction of methane in the reaction formula (1) corresponds to endothermic reaction enthalpy of ΔH ° 298 = 247.44 kJ / mol, and the standard free energy change is known as ΔG ° <0 at 640 ° C. or higher , The reverse aqueous gasification reaction of the reaction formula (2) corresponds to 815 ° C, and the reaction of the reaction formula (3) corresponds to? G ° <0 at 710 ° C or lower. Therefore, in the dry reforming reaction of carbon dioxide, a side reaction is suppressed, and a high-temperature condition of 700 ° C or more is required for the conversion to synthesis gas to be dominant.

Depending on the reaction conditions, the carbon precipitation reaction proceeds as in the above reaction formulas (3) to (6) to generate coke and deactivation of the catalyst. In addition, nickel catalysts for the dry reforming reaction of methane and noble metal catalysts Nickel-based catalysts are more easily immersed in carbon than noble metal catalysts, and catalyst deactivation due to carbon deposition is a problem as the reaction performance is repeated.

On the other hand, in the case of using a noble metal catalyst, inactivation due to carbon deposition hardly appears or is relatively low, but there is also a practical problem due to a high catalyst price.

Therefore, in recent years, there is a need to continuously study a method of solving the problem of deactivation of nickel-based catalysts, further improving the efficiency of methane reforming reaction, and further improving the amount of hydrogen production.

The present invention can remove carbon deposited on the catalyst by collecting the catalyst discharged together with hydrogen and carbon monoxide generated by the reforming reaction of methane and then injecting oxygen to reuse the catalyst thus regenerated, Thereby solving the problem of inactivation of the catalyst.

In addition, the present invention allows the catalyst to flow due to the injection of the carbon dioxide-containing gas and the methane, thereby inducing the reforming reaction of the methane, thereby further improving the efficiency of the methane reforming reaction.

According to one embodiment of the present invention, a preheater for preheating carbon dioxide-containing gas and methane;

A fluidized bed reactor for performing a dry reforming reaction of methane in the presence of a preheated carbon dioxide-containing gas and a methane reforming catalyst through which methane flows;

A cyclone which is generated by the dry reforming reaction of methane and is discharged together with hydrogen and carbon monoxide discharged from the reactor and collects the catalyst discharged and discharges hydrogen and carbon monoxide; And

And a regenerator for removing the deposited carbon by supplying oxygen to the catalyst collected in the cyclone,

The carbon-depleted catalyst in the regenerator provides a dry reforming facility for methane that is re-fed to the reactor.

And a heat exchanger positioned at a front end of the preheater and performing heat exchange between hydrogen and carbon monoxide discharged from the cyclone and carbon dioxide-containing gas supplied to the preheater and methane.

A compressor located at a front end of the preheater and compressing carbon dioxide-containing gas and methane; And

And an inflator for expanding the volume of hydrogen and carbon monoxide discharged from the cyclone.

The preheater may preheat the carbon dioxide-containing gas and methane to 700 to 900 占 폚.

The methane reforming catalyst may be a nickel catalyst.

The carbon dioxide-containing gas supplied to the fluidized bed reactor may be supplied at a flow rate of 2 to 20 Nm 3 / s.

Methane supplied to the fluidized bed reactor may be supplied at a flow rate of 2 to 20 Nm 3 / s.

The methane reforming catalyst in the fluidized bed reactor may be charged in an amount of 200 to 2,000 tons.

The oxygen supplied to the regenerator can be supplied at a flow rate of 0.006 to 0.06 Nm 3 / s.

The compressor compresses the carbon dioxide-containing gas and methane to a pressure of 6 to 10 bar,

The inflator may expand hydrogen and carbon monoxide to a pressure below atmospheric pressure.

In the fluidized bed reactor, the catalyst can circulate in the reactor in a fluidized bed by floating with carbon dioxide-containing gas and methane supplied from the lower part of the fluidized bed reactor.

The carbon dioxide-containing gas may be blast furnace gas.

The present invention can regenerate the catalyst by removing the carbon deposited on the catalyst by collecting the catalyst discharged to the outside of the reactor together with hydrogen and carbon monoxide generated by the reforming reaction of methane and then injecting oxygen, It is possible to solve the problem of inactivation of the catalyst due to the deposition of carbon which has been a problem in the past and to reduce the amount of the new catalyst to be supplied according to the regeneration of the catalyst, have.

In addition, the present invention enables the catalyst to induce the reforming reaction of methane while floating in the reactor according to the injection of the carbon dioxide-containing gas and methane, thereby improving the contact efficiency between the catalyst and the reactant carbon dioxide-containing gas and methane, The conversion rate to hydrogen, that is, the amount of hydrogen production can be remarkably improved.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 schematically shows an embodiment of the dry reforming apparatus for methane of the present invention. FIG.
2 schematically shows another embodiment of the dry reforming apparatus for methane of the present invention.
Fig. 3 schematically shows another embodiment of the methane dry reforming plant of the present invention.

Hereinafter, preferred embodiments of the present invention will be described with reference to the accompanying drawings. However, the embodiments of the present invention can be modified into various other forms, and the scope of the present invention is not limited to the embodiments described below.

In the dry reforming reaction of methane and carbon dioxide, high temperature operation is essential because more than 80% of methane shows conversion to hydrogen at a high temperature of 700 ° C or higher. However, under such reaction conditions, not only the dry reforming reaction of methane but also the carbon precipitation reaction occurs at the same time, so that the carbon precipitated in the methane reforming catalyst is deposited, and the efficiency of the dry reforming reaction of methane is remarkably reduced by deactivation of the catalyst there was.

Therefore, when the carbon dioxide-containing gas and the methane are injected into the reactor, the methane reforming catalyst flows in the reactor while circulating in the reactor, so that the dry reforming reaction of methane can be efficiently activated, And recovering and recovering oxygen by collecting the catalyst discharged together with the generated hydrogen and carbon monoxide, thereby solving the problem of inactivation of the catalyst, which has hitherto been a problem.

Specifically, according to one embodiment of the present invention, a fluidized bed reactor for performing a dry reforming reaction of methane in the presence of a preheater for preheating carbon dioxide-containing gas and methane, a preheated carbon dioxide-containing gas, and a methane- A cyclone that is generated by the dry reforming reaction of methane and collects the catalyst discharged along with hydrogen and carbon monoxide discharged from the reactor and discharges hydrogen and carbon monoxide, and oxygen which is supplied to the catalyst collected in the cyclone to remove the deposited carbon Wherein the carbon-depleted catalyst in the regenerator provides a dry reforming facility for methane that is re-fed to the reactor.

FIG. 1 schematically shows an example of the dry reforming apparatus for methane of the present invention. Since the dry reforming reaction of methane must be maintained at a high temperature of 700 ° C. or higher as described above, the present invention is characterized in that the carbon dioxide- And methane may be supplied to the preheater 200 to ensure high-temperature reaction conditions.

In the present invention, the temperature for heating the carbon dioxide-containing gas and methane in the preheater is preferably 700 to 900 ° C. If the preheating temperature is lower than 700 ° C., the heat of the dry reforming reaction of methane, which is an endothermic reaction, Can be significantly reduced. The upper limit of the preheating temperature is not particularly limited. However, if the preheating temperature is too high, it may be economically problematic during the operation of the process.

The carbon dioxide-containing gas and methane preheated in the preheater 200 are then supplied to the lower portion of the fluidized bed reactor 100. Each of the carbon dioxide-containing gas and the methane may be preheated and then supplied to the fluidized bed reactor, And the mixed gas of methane may be preheated and the preheated mixed gas may be supplied to the lower portion of the fluidized bed reactor 100.

In the present invention, the flow rate of carbon dioxide-containing gas and methane supplied to the fluidized bed reactor 100 is not particularly limited, but it is preferably set at a flow rate of 2.0 to 20 Nm 3 / s based on a blast furnace producing more than 3.8 million tons of pig iron per year Or a mixed gas of carbon dioxide-containing gas and methane mixed at a ratio of 1: 1 at a flow rate of 4.0 to 40 Nm 3 / s is most preferable in view of the conversion efficiency of methane to hydrogen.

When the carbon dioxide-containing gas and the methane are supplied through the lower part of the fluidized bed reactor 100, the methane reforming catalyst packed in the fluidized bed reactor 100 is supplied with the gas (carbon dioxide-containing gas and methane, The reforming reaction of the methane and the carbon dioxide-containing gas can be activated by flowing and circulating the fluidized bed reactor 100 in accordance with the flow of the gas.

In the present invention, the catalyst for reforming methane used for the dry reforming reaction of methane may be a nickel catalyst and a noble metal catalyst such as platinum, palladium or rhodium. However, since the noble metal catalyst has a problem in practical use due to its high price, It is preferable to use a nickel catalyst. However, carbon deposition, which is a problem in using a nickel catalyst, can be solved through a regenerator described below in the present invention.

Although the amount of the methane reforming catalyst packed in the fluidized bed reactor 100 is not particularly limited, it is preferable that the amount of the methane reforming catalyst packed in the fluidized bed reactor 100 exceeds the amount of the carbon dioxide- The catalyst is preferably used in an amount of 200 to 2,000 tons, considering the preferable flow rate of the carbon dioxide-containing gas and methane.

The dry reforming reaction of methane performed in the present invention corresponds to the surface catalytic reaction. As described above, as the methane reforming catalyst fl ows in the reactor 100, the contact ratio with methane and carbon dioxide as reactants is improved , And as a result, the efficiency of dry reforming reaction of methane can be remarkably improved.

That is, according to the present invention, the catalyst flows in the fluidized bed reactor 100 and efficiently activates the reforming reaction of methane and carbon dioxide, and the conversion of methane to hydrogen is remarkably increased. As a result, A large amount of carbon monoxide is generated.

The generated hydrogen and carbon monoxide are discharged to the outside of the reactor through the upper part of the fluidized bed reactor 100. At this time, the catalyst particles for methane reforming, which are floating, are entrained together with the flow of hydrogen and carbon monoxide, Respectively.

Therefore, in the present invention, hydrogen and carbon monoxide discharged to the outside of the reactor 100 can be sent to the cyclone 300 to separately collect the methane reforming catalyst contained therein, To the reservoir of hydrogen and carbon monoxide, or to other required locations.

Meanwhile, the catalyst collected in the cyclone 300 may be sent to the regenerator 101. In the regenerator 101, the catalyst may be regenerated by supplying oxygen to remove carbon which lowers the activity of the catalyst . Specifically, the carbon immersed in the catalyst reacts rapidly with oxygen supplied to the gaseous phase and can be converted to carbon dioxide and removed from the catalyst.

In the present invention, oxygen supplied to the regenerator 101 for regeneration of the catalyst is preferably supplied at a flow rate of 0.006 to 0.06 Nm 3 / s. Considering the preferable supply flow rate of the carbon dioxide-containing gas and methane described above and the preferable supply amount of the catalyst described above in the present invention, carbon of 0.3 ppm or more is deposited in the catalyst in a general fixed bed reactor. Therefore, it is preferable that oxygen is supplied at a flow rate of 0.006 to 0.06 Nm &lt; 3 &gt; / s to remove the carbon deposited in the above amount.

When the catalyst for regeneration of methane in the regenerator 101 is regenerated, it can be supplied to the fluidized bed reactor 100 to be reused as a catalyst for the methane dry reforming reaction. Thus, the problem of deactivation of the catalyst can be solved And the conventional catalyst is not continuously supplied for the dry reforming reaction of methane as in the prior art. Thus, the cost can be greatly reduced. Further, the process can be continuously performed, and the hydrogen production rate can be remarkably improved Can be improved.

In addition, another embodiment of the present invention includes the heat exchanger 201 at the upstream of the preheater 200, so that the heat exchange between the high temperature hydrogen and carbon monoxide discharged from the cyclone and the carbon dioxide-containing gas, which is the reactant of the methane reforming reaction, To be performed.

FIG. 2 schematically illustrates another embodiment of the present invention. Referring to FIG. 2, since the methane dry reforming reaction requires a high heat of reaction, hydrogen and carbon monoxide generated by the reaction also become high temperatures. By including the heat exchanger 201 before the preheater 200, the heat of the high temperature hydrogen and carbon monoxide discharged to the top of the cyclone 300 can be exchanged with the carbon dioxide-containing gas used as the reactant of the dry reforming reaction of methane, .

More specifically, hydrogen and carbon monoxide of about 600 ° C or more are generated as a product by the dry reforming reaction of methane in the fluidized bed reactor 100, and this high temperature gas is sent to the cyclone 300, And then to the heat exchanger 201 through the top of the cyclone 300. [

In the heat exchanger 201, hot hydrogen and carbon monoxide can heat the carbon dioxide-containing gas and methane to about 300 ° C through heat exchange with methane and carbon dioxide-containing gas that has not been preheated.

However, in order to perform the methane reforming reaction, a reaction condition of 700 ° C or more is required. Therefore, the carbon dioxide-containing gas and methane heated by the heat exchange are sent to the preheater 200 to perform an additional preheating process. However, It is possible to reach the reaction condition even if only a relatively small amount of energy is applied, compared with the case where heat exchange is not performed, and it is possible to recover a part of the energy from the preheater 200 through heat exchange, .

In another embodiment of the present invention, electric energy can be produced by further including a compressor for compressing carbon dioxide-containing gas and methane at the front end of the preheater, and an expander for expanding the volume of hydrogen and carbon monoxide discharged from the cyclone.

Figure 3 schematically illustrates another embodiment of the present invention wherein the carbon dioxide containing gas and methane are introduced into the preheater 200 through the compressor 400 or a mixture thereof at a pressure of 6 to 8 bar The pressurized high-pressure gas can be sent to the preheater 200, heated to 700 ° C or higher, and then sent to the fluidized bed reactor 100.

In the fluidized bed reactor 100, high-temperature and high-pressure hydrogen and carbon monoxide are generated by the reforming reaction of the supplied high-temperature and high-pressure carbon dioxide-containing gas and methane, and these gases are supplied to the cyclone 300 After the catalyst contained in the cyclone 300 is removed, it is sent to the inflator 401 through the upper part of the cyclone 300.

In the inflator (401), hydrogen and carbon monoxide at a high temperature and a high pressure can be inflated to pressures below atmospheric pressure to lower both the temperature and the pressure of the gas, and electric energy can be produced using the large inflating force generated at this time.

That is, according to the present invention, since the compressor 400 and the inflator 401 are further included, energy required for compression and preheating can be recovered through the production of electric energy, thereby achieving a great economical effect.

Since the carbon dioxide-containing gas supplied as a reactant for the dry reforming reaction of methane is a gas containing carbon dioxide and methane reacts with carbon dioxide for the dry reforming reaction of methane, the higher the content of carbon dioxide is, It is most preferable to use only carbon dioxide.

Further, the present invention can use an exhaust gas discharged from the blast furnace as a carbon dioxide-containing gas. The blast furnace gas contains more than 20% of carbon dioxide. If it is discharged into the atmosphere, it may cause environmental pollution problem such as greenhouse effect. In contrast, in the present invention, blast furnace gas contains a large amount of carbon dioxide By using this for the dry reforming reaction of methane instead of carbon dioxide, it is possible to produce hydrogen and carbon monoxide, which have a high utilization value, from the blast furnace exhaust gas, and can further reduce the problem of air pollution.

However, in the present invention, when blast furnace gas is used as the carbon dioxide-containing gas, a large amount of dust and sludge are contained in the blast furnace flue gas, so that the flue gas is passed through the gas- And then passed through a gas scrubber to remove H 2 S, SO 2 It is preferable to perform a pretreatment step of removing the above-mentioned material.

100: Fluidized bed reactor
101: Player
200: preheater
201: Heat exchanger
300: Cyclone
400: Compressor
401: inflator

Claims (12)

A preheater for preheating the carbon dioxide-containing gas and methane;
A fluidized bed reactor for performing a dry reforming reaction of methane in the presence of a preheated carbon dioxide-containing gas and a methane reforming catalyst through which methane flows;
A cyclone which is generated by the dry reforming reaction of methane and is discharged together with hydrogen and carbon monoxide discharged from the reactor and collects the catalyst discharged and discharges hydrogen and carbon monoxide; And
And a regenerator for removing the deposited carbon by supplying oxygen to the catalyst collected in the cyclone,
Wherein the carbon-depleted catalyst in the regenerator is fed back to the reactor.
The dry reforming apparatus for methane according to claim 1, further comprising a heat exchanger located at a front end of the preheater and performing heat exchange between hydrogen and carbon monoxide discharged from the cyclone and carbon dioxide- .
[2] The compressor of claim 1, further comprising: a compressor located at a front end of the preheater and compressing carbon dioxide-containing gas and methane; And
Further comprising an expander for expanding the volume of hydrogen and carbon monoxide discharged from the cyclone.
4. The dry reforming apparatus for methane according to any one of claims 1 to 3, wherein the preheater preheats the carbon dioxide-containing gas and the methane to 700 to 900 占 폚.
The dry reforming apparatus according to any one of claims 1 to 3, wherein the methane reforming catalyst is a nickel-based catalyst.
The dry reforming apparatus for methane according to any one of claims 1 to 3, wherein the carbon dioxide-containing gas supplied to the fluidized bed reactor is supplied at a flow rate of 2.0 to 20 Nm 3 / s.
The dry reforming apparatus for methane according to any one of claims 1 to 3, wherein methane supplied to the fluidized bed reactor is supplied at a flow rate of 2.0 to 20 Nm 3 / s.
4. The dry reforming apparatus for methane according to any one of claims 1 to 3, wherein the methane reforming catalyst in the fluidized bed reactor is charged in an amount of 200 to 2,000 tons.
The dry modifying equipment for methane according to any one of claims 1 to 3, wherein oxygen supplied to the regenerator is supplied at a flow rate of 0.006 to 0.06 Nm 3 / s.
4. The compressor according to claim 3, wherein the compressor compresses the carbon dioxide-containing gas and methane to a pressure of 6 to 10 bar,
Wherein the expander expands hydrogen and carbon monoxide to a pressure lower than the atmospheric pressure.
4. The dry reforming apparatus of claim 1, wherein the catalyst in the fluidized bed reactor is circulated in the reactor in a fluidized bed state by floating with carbon dioxide-containing gas and methane supplied from the lower part of the fluidized bed reactor.
4. The dry reforming apparatus for methane according to any one of claims 1 to 3, wherein the carbon dioxide-containing gas is a blast furnace gas.
KR1020130116944A 2013-09-30 2013-09-30 The apparatus for dry reforming of methane KR101528037B1 (en)

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Cited By (2)

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KR101896425B1 (en) * 2017-10-16 2018-09-07 한주현 Oxidation dissolution system of methane gas generated by hydrogen embrittlement from washing process of metal wire in the Hydrogen Chloride flush tank
WO2018187213A1 (en) * 2017-04-03 2018-10-11 Qatar Foundation For Education, Science And Community Development System and method for carbon and syngas production

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KR100888247B1 (en) * 2007-08-02 2009-03-10 성균관대학교산학협력단 A fluidized bed reactor for hydrogen production without co2 from hydrocarbon over carbon catalyst and an apparatus comprising the same
KR20090067429A (en) * 2007-12-21 2009-06-25 주식회사 포스코 Method for making composite gas using carbon dioxide
CN102159313A (en) * 2008-09-24 2011-08-17 新日本制铁株式会社 Method for producing catalyst for reforming tar-containing gas, method for reforming tar and method for regenerating catalyst for reforming tar-containing gas

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2018187213A1 (en) * 2017-04-03 2018-10-11 Qatar Foundation For Education, Science And Community Development System and method for carbon and syngas production
US11591213B2 (en) 2017-04-03 2023-02-28 Qatar Foundation For Education, Science And Community Development System and method for carbon and syngas production
KR101896425B1 (en) * 2017-10-16 2018-09-07 한주현 Oxidation dissolution system of methane gas generated by hydrogen embrittlement from washing process of metal wire in the Hydrogen Chloride flush tank

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