CN113070003A - Reactor for preparing methane from coke oven gas or synthesis gas - Google Patents

Reactor for preparing methane from coke oven gas or synthesis gas Download PDF

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CN113070003A
CN113070003A CN202110424033.9A CN202110424033A CN113070003A CN 113070003 A CN113070003 A CN 113070003A CN 202110424033 A CN202110424033 A CN 202110424033A CN 113070003 A CN113070003 A CN 113070003A
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gas
fixed bed
bed reactor
reactor
temperature
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李光
曹建亮
梁楚宁
张亚坤
张玉龙
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Henan University of Technology
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Henan University of Technology
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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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
    • B01J8/025—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical in a cylindrical shaped bed
    • 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
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0278—Feeding reactive fluids
    • 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
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0285—Heating or cooling the reactor
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
    • C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
    • C07C1/0485—Set-up of reactors or accessories; Multi-step processes
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/00044—Temperature measurement
    • B01J2208/00053—Temperature measurement of the heat exchange medium
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/0007—Pressure measurement
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/00088—Flow rate measurement
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00389—Controlling the temperature using electric heating or cooling elements
    • B01J2208/00398—Controlling the temperature using electric heating or cooling elements inside the reactor bed
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00893—Feeding means for the reactants
    • B01J2208/00911—Sparger-type feeding elements

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  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
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  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

The invention provides a reactor for preparing methane from coke oven gas or synthesis gas, which comprises: a fixed bed reactor filled with a solid catalyst; the heating unit is arranged in the middle of the fixed bed reactor along the axial direction; the gas preheating unit is arranged on a gas inlet of the fixed bed reactor; the flow regulating unit is arranged on one side of the gas preheating unit; the temperature measuring unit is axially arranged in the bed layer region of the fixed bed reactor, on the surface of the heating unit and on the air inlet and the air outlet of the fixed bed reactor; the pressure difference of the fixed bed reactor, the shape/particle size of the solid catalyst, the flow rate of gas entering the fixed bed reactor and the preheating temperature are designed to realize the generation and near-in-situ removal of methanation reaction heat. The reactor can realize a new technology of single-stage isothermal low-temperature methanation, and has the advantages of obviously shortened process, reduced energy consumption, enhanced load change resistance and reduced investment cost.

Description

Reactor for preparing methane from coke oven gas or synthesis gas
Technical Field
The invention relates to a reactor, in particular to a reactor for preparing methane from coke oven gas or synthesis gas.
Background
China is a country rich in coal, less in oil and poor in gas, and coal accounts for 94.3% of the proven fossil energy reserves, and oil and natural gas only account for 5.7%. Therefore, in view of the energy resource condition of China, China will maintain the energy consumption structure mainly comprising coal for a long time, the proportion of coal is always maintained at about 2/3, the proportion of petroleum is maintained at 18% -19%, and the proportion of natural gas and other energy forms tends to increase.
At present, "liquid fuel or chemical products made of coal" has been researched and demonstrated as a key project. Compared with the technologies of oil, methanol, dimethyl ether and the like prepared from coal, the energy utilization efficiency of the alternative natural gas (SNG) prepared from coal is high, the water consumption of unit heat value is low, and the generated CO is2Less. Meanwhile, the SNG can be transported by utilizing the existing natural gas transportation pipe network in China. The SNG which is transported to the end user through the pipeline can be used as fuel for civil use, industrial use and even compressed into vehicles, has high heat value as natural gas, and is safe and clean energy. Therefore, the new coal utilization industry chain "coal mining → coal gasification/pyrolysis → methanation → pipeline transportation → end user" has good practicability and operability, and has a successful paradigm abroad. The consumption of natural gas in China has rapidly increased since 2006, the supply-demand gap has begun to emerge in 2009 and has expanded year by year, and by 2020, the gap for natural gas reaches 900 billionths of cubic meters, and the external dependency has expanded to 30% -40%. However, the demand and import quantity of oil and gas resources in China are huge, and the gas price is high abroad, so that the requirements of domestic markets at the present stage are difficult to be completely met.
The production cost of the coal-based synthetic natural gas is higher than that of natural gas, the exploitation cost of natural gas per cubic meter is within 1 yuan, but the cost of the coal-based natural gas is mainly influenced by the price of coal, the coal consumption of natural gas per cubic meter per thousand is about 3 tons, the water consumption is about 10 tons, and the cost of raw material coal accounts for more than 40%. The production cost price of the natural gas prepared from Xinjiang Qinghua coal is 1.2-1.6 yuan cubic meter according to the measurement of 150 yuan per ton of coal, and the synthetic natural gas prepared from coal has no cost advantage. However, in terms of selling price, the price of natural gas in China is increased approximately at the end of 2017 years, a natural gas supply gap exists for a long time, and the price of Liquefied Natural Gas (LNG) imported in China reaches more than 4 yuan per cubic meter. Therefore, the coal-based synthetic natural gas has wide market prospect and competitive economy.
The methanation of raw material gases such as synthesis gas, coke oven gas and the like is a rapid strong exothermic reaction, the adiabatic temperature rise is rapid, the increase of the operation temperature can reduce the reaction equilibrium conversion rate, the purity of the product gas is reduced, and the carbon deposition, sintering and inactivation of the catalyst are caused at the same time. At present, technical means such as multi-section fixed bed reaction, multi-section gas cooling, raw gas shunting and product gas circulation are generally adopted to solve the problem of rapid and large amount of reaction heat of methanation, and meanwhile, the service life of the catalyst is ensured by using a large amount of excessive catalyst. Therefore, the existing technology depends on gas flow to transfer reaction heat, and as the heat capacity of gas is small, technical means such as multi-stage reaction, feed gas shunting, product gas circulation and the like are formed, so that the system is complex, the control is complex, and the anti-interference capability of the process is weak, such as the capability of antigen gas flow and composition change. Becomes a main bottleneck restricting the popularization and the application of the technology, and also provides strict requirements for the development of a new methanation process.
Since methanation is a strongly exothermic catalytic reaction in which the product volume is significantly reduced, which is strongly limited by the thermodynamic equilibrium of the reaction, the difficulty of large-scale industrialization techniques lies in the contradiction between the rapid generation and rapid removal of the reaction heat. Therefore, the project aims to develop a single-section low-temperature short-flow methanation technology, takes coal-based natural gas and coke oven purified gas as raw materials, prepares synthetic natural gas on a large scale, develops a large-scale coal-based synthetic natural gas industry, can open up a wide application prospect for value-added utilization of low-rank coal, and accords with a modern clean coal technology development mode of 'intensification, large-scale poly-generation, clean utilization and effective utilization'.
Disclosure of Invention
In order to solve the above problems, an object of the present invention is to provide a reactor for producing methane from coke oven gas or syngas, which can generate and remove the heat of methanation reaction in situ, and which can realize a new technology of low-temperature methanation such as single stage, etc., and has significantly shortened process, reduced energy consumption, enhanced load change resistance, and reduced investment cost, compared to the existing multi-stage fixed bed methanation industrial technology that relies on gas circulation, raw material splitting, multi-stage adiabatic, and multi-stage heat transfer.
In order to achieve the above object, the technical solution of the present invention is as follows.
A reactor for producing methane from coke oven gas or syngas, comprising:
a fixed bed reactor filled with a solid catalyst;
the heating unit is arranged in the middle of the fixed bed reactor along the axial direction;
the gas preheating unit is arranged on a gas inlet of the fixed bed reactor;
the flow regulating unit is arranged on one side of the gas preheating unit;
the temperature measuring unit is axially arranged in the bed layer interval of the fixed bed reactor, on the surface of the heating unit and on the air inlet and the air outlet of the fixed bed reactor;
the method is characterized in that the generation and the near-in-situ removal of methanation reaction heat are realized by designing the pressure difference between a gas inlet and a gas outlet of the fixed bed reactor, the shape/particle size of the solid catalyst, and the flow rate and the preheating temperature of gas entering the fixed bed reactor.
Further, the pressure difference between the air inlet and the air outlet of the fixed bed reactor is 1.0-1.5 MPa.
Further, the shape of the solid catalyst is a cylindrical block shape and/or a cylindrical strip shape; the particle size of the solid catalyst is 1.5-5 mm, and the particle height is 1.5-5 mm.
Further, the flow rate of gas entering the fixed bed reactor is 20-50L/min; the preheating temperature of the gas entering the fixed bed reactor is 220-300 ℃.
Further, the fixed bed reactor comprises a shell and an inner tube, and the heating unit is axially arranged in the middle of the inner tube;
the temperature measuring unit comprises a plurality of temperature measuring elements, wherein one temperature measuring element is arranged on the outer wall of the heating unit along the axial direction;
a plurality of sleeves are axially distributed in the inner pipe, the inner diameter of each sleeve is matched with the outer diameter of the heating unit, and the outer diameter of each sleeve is matched with the inner diameter of the inner pipe;
each sleeve is radially provided with a plurality of temperature measuring points, and the plurality of temperature measuring elements are respectively arranged on the corresponding temperature measuring points.
Furthermore, gas distribution plates are arranged at two ends of the inner pipe and used for enabling the gas entering and discharging the fixed bed reactor to be uniformly distributed; wherein the two temperature measuring elements are respectively arranged on the corresponding gas distribution plates;
the heating unit comprises an electric heating rod, and two ends of the electric heating rod are respectively abutted to the middle parts of the corresponding gas distribution plates.
Furthermore, the system also comprises a circulating conveying mechanism which is used for transferring the reaction heat generated by methanation; the circulating conveying mechanism comprises a refrigerating box, a circulating pump, and a pipeline and a valve which are connected with corresponding devices; a chamber for circulating water to flow is formed between the shell and the inner pipe;
the refrigeration box can refrigerate the cooling liquid; the refrigerating box enables the refrigerated cooling liquid to enter the cavity through the circulating pump; and the refrigerant flows back into the refrigerating box after heat exchange. .
Further, the gas preheating unit comprises a preheater and a temperature controller, and the temperature controller is electrically connected with the preheater and the temperature measuring unit respectively; the temperature controller can display the temperature of the corresponding temperature measuring unit and adjust the preheating temperature of the preheater for the gas entering the fixed bed reactor.
Further, all be provided with pressure measurement unit on fixed bed reactor's the air inlet and the gas outlet to in statistics the pressure differential of fixed bed reactor's air inlet and gas outlet.
Further, the device also comprises a compressor, a dryer, and a pipeline and a valve which are connected with corresponding devices; the flow regulating unit comprises a flowmeter;
wherein, gaseous warp the compressor compression back gets into the desicator, warp the desicator is dry after purifying, passes through the flowmeter measurement, and process the heating of gas preheating unit, then get into in the fixed bed reactor, again by fixed bed reactor's gas outlet is discharged.
The invention has the beneficial effects that:
1. the reactor can realize the generation and the near-in-situ removal of methanation reaction heat, can realize a new technology of single-stage low-temperature methanation and the like, obviously shortens the flow, reduces the energy consumption, enhances the load change resistance and reduces the investment cost compared with the existing multi-stage fixed bed methanation industrial technology which depends on gas circulation, raw material flow distribution, multi-stage heat insulation and multi-stage heat transfer.
2. The reactor of the present invention is designed to improve heat transfer efficiency by designing the pressure difference of the fixed bed reactor, the shape/particle size of the solid catalyst, and the flow rate and preheating temperature of the gas entering the fixed bed reactor.
Drawings
FIG. 1 is a schematic diagram of a reactor for producing methane from coke oven gas or synthesis gas according to an embodiment of the present invention.
FIG. 2 is a schematic structural view of a fixed bed reactor according to an embodiment of the present invention.
FIG. 3 is a top view of the fixed bed reactor of FIG. 2 and a thermocouple profile for measuring bed radial temperature.
FIG. 4 is a schematic view of a temperature measuring unit of an embodiment of the present invention in an axial thermometry position of a fixed bed reactor.
FIG. 5 is a schematic view of a temperature measuring unit of an embodiment of the present invention in a radial thermometry position of a fixed bed reactor.
FIG. 6 is a pressure-temperature scattergram showing the effect of different pressures on temperature in the first experimental example.
FIG. 7 is a flow-temperature scatter plot of the effect of measuring different flow metrics on temperature in working example two.
FIG. 8 is a flow-temperature dispersion plot diagram for measuring the effect of catalyst shape on temperature in the third experimental example of operation.
Fig. 9 is a flow-temperature scattergram in which the influence of the air preheating temperature on the heat transfer is measured in the fourth experimental example of operation.
Fig. 10 is a flow rate-temperature scattering diagram in the fifth experimental example of operation in which the catalyst particle diameter was measured with respect to the influence of heat.
In the figure: 1. a fixed bed reactor; 101. a housing; 102. an inner tube; 103. a sleeve; 104. a gas distribution plate; 2. a heating unit; 201. an electrical heating rod; 3. a gas preheating unit; 301. a preheater; 302. a temperature control instrument; 4. a flow rate adjusting unit; 401. a flow meter; 5. a temperature measuring unit; 501. a temperature measuring element; 6. a circulating conveying mechanism; 601. a refrigeration case; 602. a circulation pump; 7. a pressure measurement unit; 8. a compressor; 9. and (7) a dryer.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is described in further detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit 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.
Fig. 1 is a schematic structural diagram of a reactor for producing methane from coke oven gas or synthesis gas according to an embodiment of the present invention. The reactor comprises a fixed bed reactor 1, a heating unit 2, a gas preheating unit 3, a flow regulating unit 4 and a temperature measuring unit 5; the device also comprises a circulating conveying mechanism 6, a pressure measuring unit 7, a compressor 8, a dryer 9, and pipelines and valves connected with corresponding devices.
The fixed bed reactor 1 is filled with a solid catalyst. The fixed-bed reactor 1 includes a housing 101 and an inner tube 102, and the heating unit 2 is disposed in the middle of the inner tube 102 in the axial direction. Of course, the pressure measuring units 7 are disposed on both the air inlet and the air outlet of the fixed bed reactor 1, so as to count the pressure difference between the air inlet and the air outlet of the fixed bed reactor 1.
The heating unit 2 is axially arranged in the middle of the fixed bed reactor 1; for example, the heating unit 2 includes an electric heating rod 201. The two ends of the inner pipe 102 are both provided with gas distribution plates 104 for uniformly distributing the gas entering and discharging the fixed bed reactor 1; two ends of the electric heating rod 201 are respectively abutted against the middle parts of the corresponding gas distribution plates 104.
The gas preheating unit 3 is arranged on a gas inlet of the fixed bed reactor 1; the gas preheating unit 3 comprises a preheater 301 and a temperature controller 302, and the temperature controller 302 is electrically connected with the preheater 301 and the temperature measuring unit 5 respectively; the temperature controller 302 can display the temperature of the corresponding temperature measuring unit 5 and adjust the preheating temperature of the preheater 301 for the gas introduced into the fixed bed reactor 1.
The flow regulating unit 4 is arranged at one side of the gas preheating unit 3; the flow rate adjustment unit 4 includes a flow meter 401. Wherein, gas enters the desicator 9 after the compressor 8 is compressed, after the drying of desicator 9 is purified, measures through the flowmeter 401 to heat through the gas preheating unit 3, then in entering fixed bed reactor 1, discharge by the gas outlet of fixed bed reactor 1 again.
The temperature measuring unit 5 includes a plurality of temperature measuring elements 501, and is disposed in the bed region of the fixed bed reactor 1, on the surface of the heating unit 2, and on the air inlet and the air outlet of the fixed bed reactor 1 along the axial direction, as shown in fig. 2 to 3. One of the temperature measuring elements 501 is axially disposed on the outer wall of the heating unit 2; two of the temperature measuring elements 501 are respectively disposed on the corresponding gas distribution plates 104. A plurality of sleeves 103 are axially distributed in the inner pipe 102, the inner diameter of each sleeve 103 is matched with the outer diameter of the heating unit 2, and the outer diameter of each sleeve 103 is matched with the inner diameter of the inner pipe 102; each sleeve 103 is radially provided with a plurality of temperature measurement points, and the plurality of temperature measurement elements 501 are respectively arranged on the corresponding temperature measurement points. In this embodiment, the arrangement of the sleeve can realize the installation of a plurality of temperature measuring elements on the one hand, and can realize the generation and the near-in-situ shift-out of the methanation reaction heat on the other hand, and of course, the sleeve is mainly made of metal materials, such as stainless steel, and is beneficial to the near-in-situ shift-out of the reaction heat.
The circulating conveying mechanism (6) can transfer the reaction heat generated by methanation. Specifically, the circulating conveying mechanism 6 comprises a refrigeration box 601, a circulating pump 602, and a pipeline and a valve for connecting corresponding devices; a chamber for circulating water to flow is formed between the shell 101 and the inner pipe 102; the water outlet of the refrigeration box 601 is connected with a circulating pump 602 through a pipeline, and the circulating pump 602 is communicated with the water inlet of the chamber through a pipeline; the water outlet of the chamber is communicated with the water inlet of the refrigeration box 601 through a pipeline. In the using process, the refrigerating box 601 can refrigerate the cooling liquid; the refrigeration box 601 makes the refrigerated cooling liquid enter the cavity through the circulating pump 602; after heat exchange, the refrigerant flows back into the refrigeration box 601. Wherein, the material of fixed bed reactor is stainless steel, helps the transfer of reaction heat.
The pressure difference between the gas inlet and the gas outlet of the fixed bed reactor 1, the shape/particle size of the solid catalyst, the flow rate of the gas entering the fixed bed reactor 1 and the preheating temperature are designed to realize the generation and the near-in-situ shift-out of the methanation reaction heat. For example, the pressure difference between the inlet and outlet of the fixed bed reactor 1 is 1.0 to 1.5MPa, preferably 1.5 MPa. The solid catalyst is NiO/Al2O3 catalyst. The shape of the solid catalyst is a cylindrical block and/or a cylindrical bar, and the preferred shape is a cylindrical block; the particle size of the solid catalyst is preferably 1.5-5 mm, preferably 1.5-2.6mm, and the particle height is 1.5-5 mm, preferably 1.5-2.6 mm. The flow rate of the gas entering the fixed bed reactor 1 is 20-50L/min, preferably 50L/min; the preheating temperature of the gas entering the fixed bed reactor 1 is 220-300 ℃, and preferably 300 ℃.
The following will track and detect the temperature change of the reactor for producing methane from coke oven gas or synthesis gas.
1. Experimental procedure
Under the condition of continuously slightly vibrating the pipe wall, NiO/Al is slowly added2O3Catalyst to ensure packing tightness and uniformity of the pores, and then regulated compressed air at a constant pressure is introduced into the system. The air is compressed by a compressor, dried and purified by a drying pipe, metered by a flowmeter, heated to the temperature required by the experiment by an air preheater, enters the fixed bed reactor, and then discharged from the fixed bed to be emptied. The temperature change of the bed layer is tracked, and the required temperature can be measured after the temperature is stabilized.
2. Device
2.1 fixed bed reactor
The outer diameter of the fixed bed reactor is 160 mm; the fixed bed reactor had an inner tube with an inner diameter of 100mm and a height of 500mm, made of stainless steel. An electric heating rod with the diameter of 40mm is arranged in the center of the tube, a thermocouple with the diameter of 3mm is added on the outer wall of the heating rod along the axial direction, and the wall surface temperature of the heating rod is measured. The upper and lower ends of the fixed bed reactor are provided with gas distribution plates for uniformly distributing gas, and the upper and lower ends are respectively provided with a thermocouple for measuring the temperature of gas at the inlet and the outlet. Meanwhile, a plurality of thermocouple sleeves are arranged in the middle section in the inner pipeline according to a certain axial distance, and the radial temperature distribution of the inner pipe is measured. The distribution of the positions of the thermocouples in the specific temperature measuring cross section is shown in table 1 and fig. 4 to 5. The shell side of the fixed bed can be communicated with a heat carrier or not.
TABLE 1 position distribution of temperature-measuring section thermocouples
Figure BDA0003029129840000091
2.2 air compressor
Medium: air; maximum working pressure difference: 1 MPa; working pressure: 3 MPa; designing pressure: 3.6 MPa; working temperature: 0-200 ℃; volume: 50L; measuring range: 0-10m3/h。
2.3 flow meter
Measuring range: 0-20m3H; the material is as follows: and (3) glass material.
The range is 0-13 m3H, the maximum bearing pressure is 3 MPa; the material is as follows: stainless steel rotameter.
2.4 silica gel dryer
Stainless steel material; allochroic silica gel.
2.5 preheater
The stainless steel material is internally provided with a spiral electric heating wire, and the heating power is 500 and 1000W; the air may be heated to 400 ℃.
2.6 thermocouple
The K-type thermocouple has the length of 600mm for the measurement section, the length of 2000mm for the compensation line and the temperature measurement range of 0-1000 ℃.
2.7 others
The pipeline is made of stainless steel/carbon steel, the inner diameter is 20mm, and the wall thickness is 2 mm. The valve is a stainless steel ball valve. The maximum working pressure of the circulating pump is 1MPa, the maximum working temperature is 50 ℃, and the range is 0-10m3H is used as the reference value. Refrigerating box with 20m capacity3The plastic refrigeration box.
3. Procedure of experiment
Operation experimental example one: influence of pressure on Heat transfer
Catalyst NiO/Al2O3Cylindrical strip shape with the grain diameter of 1.6 mm; the air preheating temperature is 220 ℃; the air pressure is 1MPa, 1.5MPa and 2MPa respectively, and the gas flow is 20L/min. The pressure-temperature scatter plot at the different positions is shown in fig. 6.
Operation example two: influence of flow on Heat transfer
Catalyst NiO/Al2O3The cylinder bar is 1.6mm, the air preheating temperature is 220 ℃, the air pressure is 1MPa, and the gas flow is 20L/min, 30L/min, 40L/min and 50L/min. A flow-temperature scatter plot at various locations is shown in fig. 7.
Operation example three: effect of catalyst shape on Heat transfer
Catalyst NiO/Al2O3The air preheating temperature was 220 ℃, the air pressure was 1.5MPa, the gas flow rates were 20L/min, 30L/min, 40L/min, and 50L/min, the catalyst shapes were cylindrical bar-shaped 1.6mm, cylindrical block-shaped 5 x 5mm, and the flow-temperature scatter plot at the same position is shown in fig. 8.
Operation experimental example four: influence of air preheating temperature on heat transfer
Catalyst NiO/Al2O3The air pressure was 1.5MPa, the gas flow was 20L/min, the catalyst shape was 1.6mm in the form of a cylindrical bar, the air preheating temperature was 220 deg.C, 250 deg.C, 300 deg.C, and the flow-temperature scatter plot at the same position is shown in FIG. 9.
Operation example five: effect of catalyst particle size on Heat transfer
Catalyst NiO/Al2O3The air preheating temperature was 220 ℃, the air pressure was 1.5MPa, the gas flow rates were 20L/min, 30L/min, 40L/min, and 50L/min, the catalyst particle diameters were 1.5-2.6mm, and 3-5mm, respectively, and the flow-temperature scatter plot at the same position is shown in FIG. 10.
4. Results of the experiment
As can be seen from FIG. 6, the temperature at the same location increases and then decreases as the pressure increases, with the temperature being highest at 1.5 MPa. It is found that the heat transfer effect is best at 1.5 MPa.
As can be seen from FIG. 7, at the same position, the temperature gradually increases with the increase of the air flow, and the heat transfer effect is the best at 50L/min.
As can be seen from fig. 8, the cylindrical block shape has the best heat transfer effect than the cylindrical strip shape at the same position and the same air flow rate.
It can be seen from fig. 9 that different preheating air temperatures have influence on heat transfer, and the higher the preheating temperature is, the larger the heat transfer temperature difference is, the better the heat transfer effect is.
As can be seen from FIG. 10, at the same position and the same air flow rate, the heat transfer effect is better when the particle size is 1.5-2.6mm than 3-5mm, i.e. the small particle size is more favorable for heat transfer.
Therefore, the optimal value of the pressure difference between the air inlet and the air outlet of the fixed bed reactor is 1.5MPa, the shape of the solid catalyst is selected to be cylindrical block, the particle size is 1.5-2.6mm, the optimal value of the gas flow entering the fixed bed reactor is 50L/min, and the optimal value of the preheating temperature is 300 ℃. And then, the reaction for preparing methane from coke-oven gas or synthesis gas is carried out on the basis of the optimal conditions, which is beneficial to realizing a new technology of low-temperature methanation, and the process is obviously shortened, the energy consumption is reduced, the load change resistance is enhanced, and the investment cost is reduced.
The present invention is not limited to the above preferred embodiments, and any modifications, equivalent substitutions and improvements made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims (10)

1. A reactor for producing methane from coke oven gas or synthesis gas, comprising:
a fixed bed reactor (1) filled with a solid catalyst;
the heating unit (2) is arranged in the middle of the fixed bed reactor (1) along the axial direction;
the gas preheating unit (3) is arranged on a gas inlet of the fixed bed reactor (1);
the flow regulating unit (4) is arranged on one side of the gas preheating unit (3);
the temperature measuring unit (5) is axially arranged in the bed layer interval of the fixed bed reactor (1), on the surface of the heating unit (2) and on the air inlet and the air outlet of the fixed bed reactor (1);
the method is characterized in that the generation and near-in-situ removal of methanation reaction heat are realized by designing the pressure difference between a gas inlet and a gas outlet of the fixed bed reactor (1), the shape/particle size of the solid catalyst, and the flow rate and preheating temperature of gas entering the fixed bed reactor (1).
2. The reactor for producing methane from coke oven gas or synthesis gas as claimed in claim 1, wherein the pressure difference between the gas inlet and the gas outlet of the fixed bed reactor (1) is 1.0-1.5 MPa.
3. The reactor for producing methane according to the coke-oven gas or the synthesis gas as claimed in claim 1, wherein the solid catalyst has a shape of a cylindrical block and/or a cylindrical strip; the particle size of the solid catalyst is 1.5-5 mm, and the particle height is 1.5-5 mm.
4. The reactor for producing methane from coke oven gas or synthesis gas as claimed in claim 1, wherein the flow rate of the gas entering the fixed bed reactor (1) is 20-50L/min; the preheating temperature of the gas entering the fixed bed reactor (1) is 220-300 ℃.
5. The reactor for producing methane from coke oven gas or synthesis gas according to claim 1, characterized in that the fixed bed reactor (1) comprises a shell (101) and an inner tube (102), and the heating unit (2) is axially arranged in the middle of the inner tube (102);
the temperature measuring unit (5) comprises a plurality of temperature measuring elements (501), wherein one temperature measuring element (501) is arranged on the outer wall of the heating unit (2) along the axial direction;
a plurality of sleeves (103) are axially distributed in the inner pipe (102), the inner diameter of each sleeve (103) is matched with the outer diameter of the heating unit (2), and the outer diameter of each sleeve (103) is matched with the inner diameter of the inner pipe (102);
each sleeve (103) is radially provided with a plurality of temperature measuring points, and the plurality of temperature measuring elements (501) are respectively arranged on the corresponding temperature measuring points.
6. The reactor for producing methane from coke oven gas or synthesis gas as claimed in claim 5, wherein gas distribution plates (104) are arranged at both ends of the inner tube (102) for uniformly distributing the gas entering and exiting the fixed bed reactor (1); wherein two temperature measuring elements (501) are respectively arranged on the corresponding gas distribution plate (104);
the heating unit (2) comprises an electric heating rod (201), and two ends of the electric heating rod (201) are respectively abutted to the middle of the corresponding gas distribution plate (104).
7. The reactor for producing methane according to the coke oven gas or the synthesis gas as recited in claim 5, further comprising a circulating conveying mechanism (6) for transferring the reaction heat generated by methanation; the circulating conveying mechanism (6) comprises a refrigeration box (601), a circulating pump (602) and a pipeline and a valve which are connected with corresponding devices; a chamber for circulating water to flow is formed between the shell (101) and the inner pipe (102);
wherein the refrigeration box (601) can refrigerate the cooling liquid; the refrigeration box (601) enables the refrigerated cooling liquid to enter the cavity through the circulating pump (602); after heat exchange, the refrigerant flows back into the refrigeration box (601).
8. The reactor for producing methane from coke oven gas or synthesis gas according to claim 1, wherein the gas preheating unit (3) comprises a preheater (301) and a temperature controller (302), and the temperature controller (302) is electrically connected to the preheater (301) and the temperature measuring unit (5), respectively; the temperature controller (302) can display the temperature of the corresponding temperature measuring unit (5) and adjust the preheating temperature of the preheater (301) for the gas entering the fixed bed reactor (1).
9. The reactor for producing methane according to claim 1, wherein a pressure measuring unit (7) is disposed on each of the inlet and outlet of the fixed bed reactor (1) so as to count the pressure difference between the inlet and outlet of the fixed bed reactor (1).
10. The reactor for producing methane from coke oven gas or synthesis gas according to claim 1, further comprising a compressor (8), a dryer (9), and pipes and valves connected to corresponding devices; the flow regulating unit (4) comprises a flow meter (401);
wherein, gaseous warp compressor (8) compression back entering desicator (9), warp desicator (9) dry purification back, pass through flowmeter (401) measurement, and pass through gas preheating unit (3) heating, then get into in fixed bed reactor (1), again by the gas outlet of fixed bed reactor (1) is discharged.
CN202110424033.9A 2021-04-20 2021-04-20 Reactor for preparing methane from coke oven gas or synthesis gas Pending CN113070003A (en)

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Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101747127A (en) * 2008-12-18 2010-06-23 中国石油化工股份有限公司 Fischer-Tropsch synthesis method for fixed bed
CN201744343U (en) * 2010-07-30 2011-02-16 庞玉学 Methane synthetic reaction unit
US20120277329A1 (en) * 2008-10-14 2012-11-01 Terry Galloway Process and System for Converting Waste to Energy Without Burning
CN104152197A (en) * 2013-05-14 2014-11-19 中国科学院大连化学物理研究所 CO2 enrichment and methanation process in sealed space and reactor
CN204564098U (en) * 2015-03-18 2015-08-19 昊华(成都)科技有限公司 A kind of adiabatic reactor of temperature controllable
CN107206341A (en) * 2014-11-24 2017-09-26 南非大学 A kind of fixed bed reactors
CN207958283U (en) * 2017-12-26 2018-10-12 北京华福工程有限公司 It is a kind of without cycle methanation process in energy Optimum utilization system
CN208583318U (en) * 2018-07-13 2019-03-08 中石化（洛阳）科技有限公司 Fixed bed hydrogenation reactor and wax ester through hydrogenation produce fatty alcohol system

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20120277329A1 (en) * 2008-10-14 2012-11-01 Terry Galloway Process and System for Converting Waste to Energy Without Burning
CN101747127A (en) * 2008-12-18 2010-06-23 中国石油化工股份有限公司 Fischer-Tropsch synthesis method for fixed bed
CN201744343U (en) * 2010-07-30 2011-02-16 庞玉学 Methane synthetic reaction unit
CN104152197A (en) * 2013-05-14 2014-11-19 中国科学院大连化学物理研究所 CO2 enrichment and methanation process in sealed space and reactor
CN107206341A (en) * 2014-11-24 2017-09-26 南非大学 A kind of fixed bed reactors
CN204564098U (en) * 2015-03-18 2015-08-19 昊华(成都)科技有限公司 A kind of adiabatic reactor of temperature controllable
CN207958283U (en) * 2017-12-26 2018-10-12 北京华福工程有限公司 It is a kind of without cycle methanation process in energy Optimum utilization system
CN208583318U (en) * 2018-07-13 2019-03-08 中石化（洛阳）科技有限公司 Fixed bed hydrogenation reactor and wax ester through hydrogenation produce fatty alcohol system

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