CN115724401A - Method for preparing synthesis gas by using unconventional methane gas containing carbon dioxide and water - Google Patents
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Abstract
The invention provides a method for preparing synthesis gas by using unconventional methane gas containing carbon dioxide and water. The method comprises the following steps: filling a catalyst into a reactor; will contain CO 2 The unconventional methane gas and water are input into a reactor to be contacted with a catalyst to be converted into CO and H 2 The synthesis gas of (2); wherein the catalyst is a bifunctional catalyst capable of simultaneously catalyzing methane steam reforming and CO 2 Dry reforming reaction. The invention developsA bifunctional catalyst containing CO 2 Adding water into the unconventional methane gas, introducing the gas into a bifunctional catalyst bed layer, mainly performing methane steam reforming reaction at a lower temperature, and performing methane steam reforming and CO conversion at a high temperature region 2 The dry reforming reaction is converted simultaneously, and the CO can be converted by unconventional natural gas 2 Conversion with methane to CO + H 2 And (3) synthesis gas. The synthesis gas obtained by the invention can be used for producing reduced iron, and can also be used for separating H through CO exchange reaction and pressure swing adsorption 2 。
Description
Technical Field
The invention relates to a method for preparing synthesis gas by using unconventional methane gas containing carbon dioxide and water, belonging to the technical field of unconventional natural gas application.
Background
Human activities lead to CO 2 A large amount of emission causes global warming, frequent extreme weather and CO recycling 2 Has important significance.
Much CO 2 Natural gas produced by unconventional gas fields contains CO with different concentrations 2 Some of them contain more than 90%, and these unconventional CO 2 Gas well production costs are increasingly challenging. Without separating CO 2 Direct utilization has good market opportunities, e.g. with CO 2 And CH 4 Syngas production followed by methanol production and the like.
Various kinds of garbage such as domestic garbage and the like produced by people are increasing, and the domestic garbage such as sludge, kitchen waste, agricultural and forestry waste including straws, leaves and livestock and poultry manure are utilized to produce biogas through anaerobic fermentation, wherein about 55% of the biogas is methane, and 45% of the biogas is CO 2 And is also an unconventional natural gas. The hydrogen is produced by converting the marsh gas and is used for urban public transportation and logistics, so that the method has good environmental benefit and economic benefit. Because the hydrogen production by the methane not only has the advantage of in-situ, namely, places with many people must have more garbage, and public transportation and logistics are more in demand, but also the hydrogen production by the methane is realized 2 The hydrogen is green hydrogen which is renewable hydrogen and is coupled with the existing refueling and gas filling station to form a low-carbon energy supply station, the cost of the supplied hydrogen is low, and the hydrogen reaches 12 yuan/kgH at present 2 And has good economic benefit.
Disclosure of Invention
In order to solve the technical problems, the invention provides a method for preparing synthesis gas by taking unconventional methane gas containing carbon dioxide as a raw material, which adopts a catalyst with double functions to prepare CO and H 2 The synthesis gas of (2).
In order to achieve the above object, the present invention further provides a method for producing synthesis gas using unconventional methane gas containing carbon dioxide and water, comprising the steps of:
filling a catalyst into a reactor;
will contain CO 2 The unconventional methane and water are input into a reactor to be contacted with a catalyst to be converted into CO and H 2 The synthesis gas of (2);
wherein the catalyst is a bifunctional catalyst capable of simultaneously catalyzing methane steam reforming and CO 2 And (5) dry reforming reaction.
In the above method, preferably, the reactor is a variable temperature bed reactor, and the inlet temperature of the variable temperature bed reactor is 400-750 ℃, the outlet temperature is 700-950 ℃, the pressure is normal pressure-1.0 MPa, and the space velocity is 500-4000h -1 The water-carbon ratio is 0.5-3:1.
In the method, preferably, the reactor is an isothermal bed reactor, the temperature of the isothermal bed reactor is controlled to be 700-900 ℃, the pressure is normal pressure-1.0 MPa, and the space velocity is 500-4000h -1 The water-carbon ratio is 0.5-3:1.
In the above method, preferably, the catalyst is a nickel catalyst to which an alkali metal or/and an alkaline earth metal is added. Wherein, the alkali metal as the auxiliary agent comprises K and the like, and the alkaline earth metal comprises Ca, mg and the like. Wherein, the active component and the auxiliary agent are both in the form of oxides in the catalyst.
In the above method, preferably, in the catalyst, the amount of the alkali metal or/and the alkaline earth metal added is 0.01 to 10%, the content of nickel is 1 to 20%, and the balance is alumina as a carrier.
In the above method, preferably, the variable temperature bed reactor is energized by using an induction coil wound around the outside of the reaction tube, and the reaction tube is wound around the induction coil with different turns at different positions from the inlet to the outlet to control the temperature at the different positions.
In the above method, preferably, the isothermal bed reactor is energized using an induction coil which is uniformly wound around the outside of the reaction tube.
According to the specific embodiment of the invention, the isothermal bed reactor and the variable temperature bed reactor adopted by the invention can be both tubular, the catalyst is filled in the reaction tube, the induction coil is uniformly wound on the outer wall of the reaction tube, after the induction coil is electrified, electromagnetic induction is generated between the reaction tube and the induction coil, and the reaction tube generates heat, so that the heating of the raw materials in the reaction tube is realized. Wherein, the space between the reaction tube and the induction coil can be filled with heat insulation materials (such as cement, fireproof materials and the like).
According to the specific embodiment of the invention, when the isothermal bed reactor is powered by the induction coil, the induction coil is uniformly wound outside the reaction tube. Conventional CO 2 Methanation apparatus, CH 4 Steam reformer provides the heat through the burning of fuel, gas, burns the heat supply through the nozzle in the combustion chamber, then realizes the heating to the reaction tube through the heat transfer with the reaction tube, and then the raw materials in the heating reaction tube, however because the temperature of different regions is inhomogeneous in the combustion chamber, it is often all inhomogeneous to lead to this kind of heat transfer, and the heat can be concentrated at local region, can't realize that the temperature homoenergetic of each part of catalyst is evenly controlled, and the conversion reaction is also inhomogeneous. The reaction tube is heated by the induction coil, so that the heating efficiency is high, and the induction coil is uniformly distributed in the reaction tube, so that the reaction tube can uniformly generate electromagnetic induction, and isothermal reaction can be really realized.
According to the specific embodiment of the invention, when the induction coil is used for supplying energy to the temperature-variable bed reactor, the induction coil is wound outside the reaction tube, and the number of turns of the induction coil wound at different positions of the reaction tube from the inlet to the outlet is different so as to control the temperature at different positions, the temperature at the inlet is lower, the number of turns of the induction coil can be smaller, and the temperature gradually rises along with the gradual transition from the inlet to the outlet, and the number of turns of the induction coil also gradually increases. Although the conventional apparatus can make different positions of the reaction tube have different temperatures due to the problems of the conventional apparatus, the temperature control of the different positions of the reaction tube cannot be truly realized because the combustion is uncontrollable, and the temperature change degree of the variable temperature bed reactor cannot be controlled. The invention can control the degree of electromagnetic induction heating by controlling the winding mode of the induction coil outside the reaction tube, thereby relatively and accurately controlling the temperature of the catalyst at different positions inside the reaction tube and realizing the control of the temperature change degree. Moreover, the technical scheme of the invention can adopt a plurality of reaction tubes simultaneously, and can realize different temperature control for different reaction tubes, thereby controlling the reaction processes and reaction results in different reaction tubes, which cannot be realized by the existing heating equipment.
In the above method, preferably, the frequency of the current input to the induction coil is a medium frequency or a high frequency, wherein the high frequency is 5-20KHz, preferably 8-16KHz, more preferably 10-15KHz, further preferably 12-14KHz, and specifically may be 8KHz, 8.5KHz, 9KHz, 9.5KHz, 10KHz, 10.5KHz, 11KHz, 11.5KHz, 12KHz, 12.5KHz, 13KHz, 13.5KHz, 14KHz, 14.5KHz, 15KHz, 15.5KHz, 16KHz, or may be a range in which the endpoints of the above range and the enumerated specific frequency values are combined with each other, such as 5-16KHz, 5-15KHz, 5-10KHz, 8-20KHz, 8-15KHz, 8-10KHz, 10-20KHz, 10-16KHz, 10-12KHz, 9-20KHz, 9-15KHz, 12-14KHz, 12-20KHz; the intermediate frequency is 50 to 3000Hz, preferably 300 to 2000Hz, more preferably 600 to 1500Hz, and specifically may be 300Hz, 400Hz, 500Hz, 600Hz, 700Hz, 800Hz, 900Hz, 1000Hz, 1100Hz, 1200Hz, 1300Hz, 1400Hz, 1500Hz, 1600Hz, 1700Hz, 1800Hz, 1900Hz, 2000Hz, and also may be a range in which the endpoints of the above ranges and the specific frequency values enumerated are combined with each other, for example, 300 to 3000Hz, 300 to 1500Hz, 600 to 3000Hz, 600 to 2000Hz, 1000 to 3000Hz, 1000 to 2000Hz, 1200 to 3000Hz, 1200 to 2000Hz, 1500 to 3000Hz, 1500 to 2000Hz, and the like.
In the above method, preferably, the frequency of the current input to the induction coil is adjusted by a power supply and a capacitor. The induction coil is connected with the power supply to form a loop, and the power supply is connected with the capacitor in parallel, as shown in fig. 1. The power supply used in the present invention may be a common industrial power supply, such as a medium frequency power supply and a high frequency power supply. The power of the power supply, which may be adjusted to a desired frequency, is preferably rated at 100-1000KW, more preferably 200-500KW. The specification of the capacitor can be selected according to the requirement, and the capacitor can be matched with a power supply to meet the frequency control requirement.
The induction coil used in the present invention may be one or a combination of two or more selected from ferrite coil, iron core coil, air core coil, copper core coil, and the like.
According to the specific embodiment of the present invention, the size of the reaction tube used in the present invention can be selected according to the need, wherein the inner diameter of the reaction tube can be 50-250mm, and the length can be selected according to the need of the reaction.
According to embodiments of the present invention, the material of the reaction tubes may be a metal or an alloy, respectively, including but not limited to the materials of reaction tubes generally used for steam reforming, reaction tubes for dry reforming. The metal or alloy is preferably one that can withstand a temperature of 1000 c, more preferably one that can withstand a temperature of 1200 c. The material of the reaction tube can be selected from 316L stainless steel, 304S stainless steel, HK40 high-temperature furnace tube material, HP Micro Alloy steel or material for Manauritex (TM) steam cracking furnace, and the like.
According to the specific embodiment of the invention, the catalyst bed layer for the unconventional conversion of methane gas by adding water can be a temperature-changing bed or an isothermal bed, and when the energy is supplied by electric heating, such as a medium-frequency furnace, the isothermal bed is preferably adopted, and CO is easy to be generated in the high-temperature section 2 And the conversion of methane.
In the above process, preferably, the CO-containing component 2 The unconventional methane gas is unconventional natural gas or methane gas. Among them, CO of unconventional natural gas 2 Content of 20-60% (preferably 30-45%), CH 4 The content is 40-80% (preferably 55-70%).
In the above process, preferably, the CO is contained 2 H of unconventional methane gas 2 The S content is controlled to be 100ppm or less, preferably 50ppm or less, and more preferably 30ppm or less.
In the above process, preferably, the obtained CO and H are produced 2 The synthesis gas is subjected to CO exchange reaction and pressure swing adsorption to separate out H 2 。
The invention develops a bifunctional catalyst containing CO 2 Adding water into unconventional methane gas, introducing into a dual-function catalyst bed layer, mainly performing methane steam reforming reaction at a lower temperature of 450-700 deg.C, and performing methane steam reforming and CO conversion at a high temperature of 700-950 deg.C 2 The dry reforming reaction is converted simultaneously, and CO can be converted by unconventional natural gas 2 Conversion with methane to CO + H 2 The concentration of CO in the synthetic gas is high and can reach more than 20 percent.
The synthesis gas obtained by the invention can be used for producing reduced iron, and can also be used for separating H through CO exchange reaction and Pressure Swing Adsorption (PSA) 2 Is used for public transportation and logistics, thereby realizing the purpose of saving one CO for the hydrogen production by the methane 2 The front removal section only needs to adopt PSA to remove CO once 2 Can produce green H 2 Thereby making the methane produce green H 2 The cost is lower.
Drawings
FIG. 1 is a schematic circuit diagram of a power supply, an induction coil, and a capacitor according to the present invention.
FIG. 2 is a schematic diagram of the isothermal bed reactor used in examples 1 and 2.
FIG. 3 is a schematic of a variable temperature bed reactor used in example 3.
Detailed Description
The technical solutions of the present invention will be described in detail below in order to clearly understand the technical features, objects, and advantages of the present invention, but the present invention is not limited to the practical scope of the present invention.
Example 1
This example is for samples containing at different temperaturesCO 2 The conversion condition of the unconventional methane gas is evaluated, wherein the raw material gas and the catalyst are as follows:
containing CO 2 Unconventional methane gas of (2): CH (CH) 4 、55％，CO 2 、45％，H 2 S<30ppm。
Catalyst: the content of active component nickel is 8wt.%, and adjuvant K 2 O is 1wt.%, the balance being alumina.
An isothermal bed reactor was used, as shown in fig. 2.
The reaction process is as follows:
at the reaction pressure of 0.3MPa and the space velocity of 2000h -1 Under the condition of (1), adding water into the mixed gas, and controlling the molar ratio to be H 2 O/CH 4 After that, =1.0 (i.e., the water-to-carbon ratio is 1), the conversion performance was evaluated by controlling the reaction temperature of the isothermal bed at 500 ℃, 600 ℃, 700 ℃, 800 ℃, 850 ℃, 900 ℃ respectively, and the conversion results are shown in table 1, wherein the gas compositions are all mole percentages.
TABLE 1
| H 2 | CH 4 | CO 2 | CO | Isothermal bed |
| 0 | 55 | 45 | 0 | Temperature, C |
| 23.0 | 35.8 | 38.2 | 3.0 | 500 |
| 37.9 | 21.5 | 29.2 | 11.5 | 600 |
| 49.3 | 9.1 | 18.2 | 23.3 | 700 |
| 55.3 | 2.2 | 11.3 | 31.2 | 800 |
| 57.4 | 0.88 | 9.5 | 32.2 | 850 |
| 59.0 | 0.45 | 9.0 | 32.6 | 900 |
From the data in table 1 it can be seen that: at 500-600 deg.C, mainly methane steam reforming occurs, and at 600-900 deg.C, methane steam reforming and CO 2 Dry reforming and high-efficiency conversion, and the converted synthetic gas can be used for producing H through CO conversion and pressure swing adsorption 2 。
Example 2
This example deals with the CO content at different temperatures 2 The conversion condition of the unconventional methane gas is evaluated, wherein the raw material gas and the catalyst are as follows:
containing CO 2 Unconventional methane gas of (2): CH (CH) 4 、70％，CO 2 、30％，H 2 S<20ppm。
Catalyst: the content of the active component nickel is 15 wt%, the content of the auxiliary agent CaO is 5 wt%, and the balance is aluminum oxide.
An isothermal bed reactor was used, as shown in fig. 2.
The reaction process is as follows:
at the reaction pressure of 0.3MPa and the space velocity of 3000h -1 Under the condition of (1), adding water into the mixed gas, and controlling the molar ratio to be H 2 O/CH 4 =1.0 (i.e., the water-to-carbon ratio is 1), and then the conversion performance was evaluated by controlling the reaction temperature of the isothermal bed at 500 ℃, 600 ℃, 700 ℃, 800 ℃, 850 ℃, 900 ℃, respectively, and the conversion results are shown in table 2, where the gas compositions are all mole percentages.
TABLE 2
| H 2 | CH 4 | CO 2 | CO | Isothermal bed |
| 0 | 70 | 30 | 0 | Temperature, C |
| 17.7 | 52.8 | 28.3 | 1.2 | 500 |
| 36.7 | 33.7 | 23.6 | 6.0 | 600 |
| 50.5 | 18.1 | 16.4 | 14.9 | 700 |
| 57.6 | 9.8 | 11.0 | 21.5 | 800 |
| 63.4 | 3.7 | 8.0 | 24.6 | 850 |
| 64.8 | 1.8 | 7.0 | 26.4 | 900 |
From the data in table 2 it can be seen that: at 500-600 deg.C, mainly methane steam conversion takes place, and the water addition amount of the converted synthetic gas is regulated to make H 2 the/CO is about 2 and is used for in-situ synthesis of methanol; and the synthesis gas obtained finally has higher CO concentration.
Example 3
This example is for the treatment of CO-containing gas at different temperatures 2 The conversion condition of the unconventional methane gas is evaluated, wherein the raw material gas and the catalyst are as follows:
containing CO 2 Unconventional methane gas of (2): CH (CH) 4 、550v％，CO 2 、45％，H 2 S<30ppm。
Catalyst: the content of the active component nickel is 10wt.%, the content of the auxiliary agent MgO is 10wt.%, and the balance is alumina.
An isothermal bed reactor was used, as shown in fig. 2.
The reaction process is as follows:
at the reaction pressure of normal pressure and space velocity of 2000h -1 Under the condition of (1), adding water into the mixed gas, and controlling the molar ratio to be H 2 O/CH 4 =2.0 (i.e., the water-to-carbon ratio was 2), and then the conversion performance was evaluated by controlling the reaction temperature of the isothermal bed at 500 ℃, 600 ℃, 700 ℃, 800 ℃, 850 ℃, 900 ℃, respectively, and the conversion results are shown in table 3, where the gas compositions are all mole percentages.
TABLE 3
| H 2 | CH 4 | CO 2 | CO | Isothermal bed |
| 0 | 55 | 45 | 0 | Temperature, C |
| 23.2 | 31.2 | 43.4 | 2.1 | 500 |
| 48.9 | 13.0 | 30.7 | 7.3 | 600 |
| 56.8 | 3.6 | 25.5 | 14.1 | 700 |
| 59.5 | 0.95 | 18.1 | 22.5 | 800 |
| 60.4 | 0.07 | 15.1 | 24.4 | 850 |
| 60.1 | 0.03 | 14.8 | 25.1 | 900 |
From the data in table 3 it can be seen that: the methane steam reforming reaction has started to take place at 500 c and when the temperature is above 800 c, the resulting synthesis gas has a higher CO concentration.
Example 4
This example is for the treatment of CO-containing gas at different temperatures 2 The conversion condition of the unconventional methane gas is evaluated, wherein the raw material gas and the catalyst are as follows:
containing CO 2 Unconventional methane gas of (2): CH (CH) 4 、70％，CO 2 、30％，H 2 S<20ppm。
Catalyst: the content of active component nickel is 5wt.%, and adjuvant K 2 O is 0.2wt.%, with the balance being alumina.
An isothermal bed reactor was used, as shown in fig. 2.
The reaction process is as follows:
at the reaction pressure of 0.7MPa and the space velocity of 2000h -1 Under the condition of (1), adding water into the mixed gas, and controlling the molar ratio to be H 2 O/CH 4 After that, =2.0 (i.e., the water-to-carbon ratio is 2), the conversion performance was evaluated by controlling the reaction temperature of the isothermal bed at 500 ℃, 600 ℃, 700 ℃, 800 ℃, 850 ℃, 900 ℃, respectively, and the conversion results are shown in table 4, in which the gas compositions are all mole%.
TABLE 4
| H 2 | CH 4 | CO 2 | CO | Isothermal bed |
| 0 | 70 | 30 | 0 | Temperature, C |
| 28.1 | 43.6 | 27.2 | 1.1 | 500 |
| 43.0 | 26.4 | 25.7 | 4.58 | 600 |
| 54.5 | 15.3 | 20.6 | 9.6 | 700 |
| 64.7 | 4.2 | 13.6 | 17.0 | 800 |
| 68.1 | 0.9 | 11.9 | 19.0 | 850 |
| 68.8 | 0.4 | 10.4 | 20.3 | 900 |
From the data in table 4 it can be seen that: the methane steam conversion reaction is easy to occur at a lower temperature, and the hydrogen production synthetic gas is easy to produce. At higher temperatures, CH 4 、CO 2 Will be converted into CO and H 2 To obtain synthesis gas with higher CO concentration.
Example 5
This example is for the treatment of CO-containing gas at different temperatures 2 The conversion condition of the unconventional methane gas is evaluated, wherein the raw material gas and the catalyst are as follows:
containing CO 2 Unconventional methane gas of (2): CH (CH) 4 、55％，CO 2 、45％，H 2 S<30ppm。
Catalyst: the content of active component nickel is 12wt.%, the content of auxiliary agent CaO is 2wt.%, and the rest is alumina.
A variable temperature bed reactor was used, as shown in fig. 3.
The reaction process is as follows:
at a reaction pressure of 0.7MPa, airspeed 2000h -1 Under the condition of (1), adding water into the mixed gas, and controlling the molar ratio to be H 2 O/CH 4 The conversion performance was evaluated at 500 ℃ inlet temperature and 950 ℃ outlet temperature of the variable temperature bed, with gas compositions all in mole percent, 2.0 (i.e., water to carbon ratio of 2), and the conversion results are shown in table 5.
TABLE 5
| H 2 | CH 4 | CO 2 | CO | Temperature-variable bed |
| 0 | 55 | 45 | 0 | Inlet assembly |
| 59.2 | 1.0 | 15.0 | 25.1 | Outlet assembly |
From the data in table 5 it can be seen that: by the method of the invention, CH can be generated 4 、CO 2 Conversion to CO and H 2 Thereby being CO 2 The methane-containing gas is foundThe new application is that the synthesis gas with high CO concentration (the CO content is over 25 percent) is prepared and can be further used for the process of producing reduced iron by a gas-based shaft furnace.
Example 6
This example is for the treatment of CO-containing gas at different temperatures 2 The conversion condition of the unconventional methane gas is evaluated, wherein the raw material gas and the catalyst are as follows:
containing CO 2 Unconventional methane gas of (2): CH (CH) 4 、70％，CO 2 、30％，H 2 S<30ppm。
Catalyst: the content of the active component nickel is 5wt.%, the content of the auxiliary agent MgO is 7wt.%, and the balance is aluminum oxide.
A variable temperature bed reactor was used, as shown in fig. 3.
The reaction process is as follows:
at the reaction pressure of 0.5MPa and the space velocity of 2000h -1 Adding water into the mixed gas under the condition of (1), and controlling the molar ratio to be H 2 O/CH 4 The conversion performance was evaluated at 600 ℃ inlet temperature and 900 ℃ outlet temperature of the variable temperature bed, and the conversion results are shown in table 6, where the gas compositions are all mole percentages, 2.0 (i.e., water to carbon ratio of 2).
TABLE 6
| H 2 | CH 4 | CO 2 | CO | Temperature-variable bed |
| 0 | 70 | 30 | 0 | Inlet assembly |
| 65.0 | 2.0 | 6.3 | 26.5 | Outlet assembly |
From the data in table 6 it can be seen that: the method of the invention can be used for enabling CH 4 、CO 2 Conversion to CO and H 2 Thereby being CO 2 The methane-containing gas finds a new application, and the synthesis gas with high CO concentration (the CO content is over 25%) is prepared, so that the method can be used for the process for producing reduced iron by using the gas-based shaft furnace.
Claims (10)
1. A method for producing synthesis gas by using unconventional methane gas containing carbon dioxide and water, comprising the steps of:
filling a catalyst into a reactor;
will contain CO 2 The unconventional methane gas and water are input into a reactor to be contacted with a catalyst to be converted into CO and H 2 The synthesis gas of (2);
wherein the catalyst is a bifunctional catalyst capable of simultaneously catalyzing methane steam reforming and CO 2 Dry reforming reaction.
2. The method as claimed in claim 1, wherein the reactor is a variable temperature bed reactor, and the variable temperature bed reactor has an inlet temperature of 400-750 ℃, an outlet temperature of 700-950 ℃, a pressure of normal pressure-1.0 MPa, and a space velocity of 500-4000h -1 The water-carbon ratio is 0.5-3:1.
3. The process of claim 1, wherein the reactor is an isothermal bed reactor, andand the temperature of the isothermal bed reactor is controlled to be 700-900 ℃, the pressure is normal pressure-1.0 MPa, and the space velocity is 500-4000h -1 The water-carbon ratio is 0.5-3:1.
4. The process according to claim 1, wherein the catalyst is a nickel catalyst with addition of alkali metals or/and alkaline earth metals; preferably, the alkali metal comprises K and the alkaline earth metal comprises Mg and/or Ca.
5. The process according to claim 4, wherein in the catalyst, the amount of alkali metal or/and alkaline earth metal added is 0.01 to 10%, the content of nickel is 1 to 20%, and the balance is alumina as a carrier.
6. The method of claim 2, wherein the variable temperature bed reactor is powered using an induction coil that is wound around the outside of the reaction tube and wherein the reaction tube is wound with different numbers of turns at different locations from the inlet to the outlet to control the temperature at the different locations.
7. The method of claim 3, wherein the isothermal bed reactor is energized using an induction coil that is uniformly wound around the outside of the reaction tube.
8. The method according to claim 6 or 7, wherein the frequency of the current input to the induction coil is a medium or high frequency, wherein the high frequency is 5-20KHz, preferably 8-16KHz, more preferably 10-15KHz; the intermediate frequency is 50-3000Hz, preferably 300-2000Hz;
preferably, the frequency of the current input to the induction coil is adjusted by a power supply and a capacitor;
preferably, the induction coil is connected with the power supply to form a loop, and the power supply is connected with the capacitor in parallel;
more preferably, the power of the power supply is 100-1000KW, more preferably 200-500KW;
preferably, the induction coil is selected from one or a combination of more than two of ferrite coil, iron core coil, air core coil and copper core coil.
9. The method of any one of claims 1-8, wherein the CO-containing gas is a gas comprising CO 2 The unconventional methane gas is unconventional natural gas or methane gas.
10. The process according to any one of claims 1-9, wherein the produced CO and H 2 The synthesis gas is subjected to CO exchange reaction and pressure swing adsorption to separate out H 2 。
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