CN112662436A - Anthracite low-methane gasification process and gasifier - Google Patents
Anthracite low-methane gasification process and gasifier Download PDFInfo
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Abstract
The invention discloses a low-methane anthracite gasification process and a gasifier. The disclosed gasification process comprises gasifying anthracite coal to produce raw coal gas by fixed bed pressurized gasification process, introducing high temperature gas of more than 1500 ℃ from the outside of the fixed bed pressurized gasification furnace to the working region with the temperature of 800-1000 ℃ in the gasification process, wherein the high temperature gas of more than 1500 ℃ is natural gas, coal gas and H2Or gas produced by the combustion of petroleum and natural gas. The middle area of the disclosed gasification furnace is provided with a high-temperature flue gas inlet. The invention directly introduces high-temperature gas into the gasification process, the temperature of the coal bed is raised by the heat of the high-temperature gas, the conversion of methane is promoted, the temperature in the operation process is controllable, and the coal melting cannot be generated to influence the operation of the gasification furnace.
Description
Technical Field
The invention relates to a coal gasification technology, in particular to a low-methane gasification process of an anthracite fixed bed and a gasification furnace.
Background
Anthracite coal is the most coalified coal. The anthracite has the characteristics of high fixed carbon content, low volatile matter yield, high density, high hardness, high ignition point and no smoke during combustion. At present, anthracite is mainly used in the industries of chemical fertilizer, metallurgy and the like.
When the existing fixed bed gasification furnace is adopted to gasify the anthracite, coal is added from the top and contacts and reacts with a gasifying agent from the bottom of the furnace in a countercurrent way, the coal undergoes several stages of drying, dry distillation, gasification and combustion in the furnace, the generated crude gas is discharged from the upper part of the furnace, and slag is discharged from the bottom of the gasification furnace; the fixed bed gasification furnace mainly comprises a Lurgi furnace and a BGL furnace, and crude gas generated by the Lurgi furnace and the BGL furnace has high methane content and has great influence on subsequent applications such as an ammonia synthesis system.
Disclosure of Invention
Aiming at the defects or shortcomings of the prior art, the invention provides a low-methane anthracite gasification process and a gasification furnace.
The anthracite low-methane gasification process provided by the invention comprises the step of gasifying anthracite to produce raw coal gas by adopting a fixed bed pressurization gasification process, wherein in the gasification process, high-temperature gas with the temperature of more than 1500 ℃ is introduced from the outside of a fixed bed pressurization gasification furnace to a working region with the temperature of 800-1000 ℃ in a furnace, and the high-temperature gas with the temperature of more than 1500 ℃ is natural gas, coal gas and H2Or gas produced by the combustion of petroleum and natural gas.
Optionally, the particle size of the anthracite in the process is 6-50 mm.
In some embodiments, in the process, a fluxing agent is added to anthracite raw material coal, so that the melting point of the anthracite coal is 1350-1400 ℃, and the fluxing agent is limestone.
Furthermore, the temperature of the crude gas produced in the process is 900-1000 ℃ when the crude gas is discharged from the furnace.
Furthermore, the methane content in the crude gas produced by the process is less than 1.5 percent.
Preferably, the steam-oxygen ratio in the gasification process is 0.8-1.5 kg steam/Nm3The amount of the oxygen and the natural gas is 0.018-0.050 Nm3/kg of anthracite.
Further, the process of the invention comprises the following steps: the anthracite is dried and then is subjected to dry distillation, the coal subjected to dry distillation enters a secondary gasification stage, and then sequentially enters secondary gasification and primary gasification for gasification and then enters a combustion stage for combustion; in the process, high-temperature flue gas is introduced into a secondary gasification stage, and a gasification agent is introduced into a combustion stage;
the primary gasification is that gasification agent, gas generated by combustion and carbon existing in the primary gasification stage are subjected to gasification reaction;
the secondary gasification is that the gas generated by dry distillation and the gas generated by primary gasification have gasification reaction with carbon existing in the secondary gasification stage under the action of high-temperature gas, and methane in the gas has cracking reaction at high temperature during the reaction.
The anthracite low-methane gasification furnace provided by the invention comprises a fixed bed pressurized gasification furnace, wherein a steam oxidizing agent inlet is arranged in the bottom area of the fixed bed pressurized gasification furnace, and a crude gas outlet is arranged in the upper area of the fixed bed pressurized gasification furnace.
Preferably, the middle area of the fixed bed pressurized gasification furnace is provided with a plurality of high-temperature flue gas inlets which are uniformly distributed in the circumferential direction of the furnace body.
Furthermore, a combustion chamber for generating high-temperature gas is connected to the high-temperature flue gas inlet of the gasification furnace.
The technical scheme of the invention has the following beneficial effects:
(1) the invention directly introduces high-temperature gas (such as natural gas and air which are combusted in a combustion chamber outside the gasification furnace) into the gasification process, the temperature of the coal bed is raised by the heat of the high-temperature gas, the conversion of methane is promoted, the temperature in the operation process is controllable, and the coal melting cannot be generated to influence the operation of the gasification furnace.
(2) The invention has high carbon conversion rate, low steam consumption, high steam decomposition rate and less wastewater discharge, wherein: carbon conversion rate: the carbon conversion rate of the invention is more than 99 percent, and the Lurgi is about 95 percent; steam consumption: the steam consumption of the invention: 0.4-0.6 kg steam/kg coal, and Lurgi is 1.6kg steam/kg coal; the steam decomposition rate is high: the steam decomposition rate of the invention is more than 90 percent, and the Lurgi steam decomposition rate is about 40 percent; the waste water discharge amount is about 30 percent of Lurgi due to the improvement of steam decomposition rate and reduction of waste water.
(3) The temperature of the raw gas is 900-1000 ℃, the raw gas can be treated by adopting a Venturi scrubber for dedusting and cooling, a gas-liquid separator is used for separating gas water, the temperature is reduced to 170-190 ℃, the water content of the raw gas is 30-50%, the raw gas is directly fed into a subsequent conversion section, and the amount of water vapor supplemented into the conversion section can be greatly reduced.
Drawings
Fig. 1 is a schematic structural view of a gasification furnace according to an embodiment of the present invention.
Detailed Description
The fixed bed pressure gasification process is a process for realizing coal gasification under the condition of pressurization (the specific pressurization range is 2.0-6.5 Mpa), and a solid or liquid slag discharging mode can be adopted in the subsequent process; the traditional fixed bed pressure gasification process comprises drying, dry distillation, gasification and combustion, the produced crude gas is discharged from an exhaust port arranged above a coal bed, a gasification agent required by the process is added in a combustion stage, the gasification agent is specifically mixed gas of steam and oxygen, and the heat required by the process mainly comes from the gasification agent and the heat released in the combustion stage; the zone reaction temperature range for each stage was about: and (3) drying: and (3) performing dry distillation at the temperature of less than 280 ℃: and (3) gasifying at 280-800 ℃: combustion at 800-1400 deg.C: 1400-1800 ℃ and the core area can reach more than 2000 ℃;
the process comprises drying, dry distillation, secondary gasification, primary gasification and combustion, wherein a gasification agent required by the process is added in a combustion stage, and heat required by the process mainly comes from the gasification agent, high-temperature gas and heat released in the combustion stage; the reaction temperature range for each stage is approximately: and (3) drying: and (3) performing dry distillation at the temperature of less than 280 ℃: and (3) carrying out secondary gasification at 280-800 ℃: carrying out primary gasification at 1000-1200 ℃: burning at 1200-1400 deg.C: 1400-1800 deg.c and core area over 2000 deg.c.
Particularly, taking a BGL furnace known in the field as an example, the main structure of the BGL furnace comprises a coal bunker, a coal lock, a gasification furnace, a slag discharge port, a chilling chamber and a slag lock from top to bottom; the in-furnace gasification process can be divided into a drying zone, a pyrolysis zone, a gasification zone and a combustion zone from top to bottom; in the gasification process in the furnace, the coal material moves from top to bottom, the main gas body moves from bottom to top, and the main reactions carried out in each process zone are as follows:
a drying area: the coal sample is preheated, the reaction temperature of a drying layer is less than 280 ℃, and the main chemical reactions are as follows: coal → dry coal + adsorbed gas + free water;
a dry distillation zone: the pyrolysis tar and pyrolysis coal gas generation layer is also a key area for producing gas-liquid fuel, the reaction temperature of the carbonization area is 280-800 ℃, and the main reactions are as follows: coal → semicoke + tar + pyrolysis gas;
a gasification zone: it is the main generation area of synthesis gas, the reaction temperature is more than 800 ℃, and the main reaction is as follows:
CO2+C→2CO
CO+H2O→CO2+H2
C+H2O→CO+H2
C+2H2→CH4
a combustion zone: the semicoke is fully contacted and combusted with oxygen sprayed from the bottom oxygen evaporation nozzle to form a high-temperature area to promote ash melting, and simultaneously, all heat required by the reaction of the upper layers is provided. The reaction temperature of the combustion zone is 1400-1800 ℃, the core zone can reach more than 2000 ℃, the flow temperature of ash is exceeded, and the main reaction is as follows:
C+O2→CO2
2C+O2→2CO
also taking the BGL furnace known in the field as an example, the process improvement of the invention is that high-temperature gas is introduced near the 900 ℃ region of the gasification zone, namely 800-1000 ℃, to carry out secondary gasification, and the reaction generated by the secondary gasification is mainly as follows:
CH4→C+2H2
CH4+H2O→CO+3H2
C+H2O→CO+H2。
the technological gasifier suitable for the invention can be a gasifier with improved structure on the basis of a BGL furnace, and particularly, a high-temperature gas inlet is arranged in the middle of a furnace body, and further, a combustion chamber is connected to the high-temperature gas inlet.
The operating pressure of the gasification process is 2.0-6.5 Mpa, and different gasification pressures can be selected according to the configuration conditions of subsequent systems. In consideration of economy, the high-temperature gas is generated by burning natural gas, and combustible gas such as coal gas, H2, petroleum and natural gas and the like can also be used; the high-temperature gas has the functions of increasing the temperature of the coal bed by utilizing the heat of the high-temperature gas, promoting the conversion of methane and reducing the content of methane in the outlet gas.
In terms of size design, the position of the high-temperature gas inlet on the gasification furnace can be obtained by calculation according to the process parameters. For the BGL furnace used in the prior art, the high-temperature gas inlet is positioned 2.5-4.0 m above the oxygen evaporation nozzle. ,
example 1:
the embodiment provides a smokeless coal gasifier, the structure of which is shown in figure 1, and the gasifier comprises a gasifier 2, a coal lock 1 is arranged on the top of the gasifier, an oxygen evaporation nozzle 3 is arranged on the side wall of the bottom of the gasifier and used for spraying a gasifying agent 12 into the gasifier, the gasifying agent is steam-oxygen mixed steam, a slag discharge port 14 is arranged at the bottom of the gasifier, a gas outlet 5 for discharging crude gas is arranged at the top of a coal bed in the gasifier, a venturi scrubber 7 for cooling and dedusting the crude gas, a gas-liquid separator 8, a gas-water heat exchanger 9, a gas-water clarifying tank 10 and a gas-water circulating pump 11 are sequentially connected outside the gas outlet, purified gas 16 is discharged from the top of the gas-liquid separator 8, two high-temperature gas inlets 6 are arranged in the middle area of the gasifier body, the two high-temperature gas inlets are uniformly arranged along the circumferential direction of the gasifier body, and a combustion chamber, after the natural gas and the air 13 enter the combustion chamber to be combusted, high-temperature gas 15 is generated; further, in terms of size design, for the gasification furnace of the embodiment with the diameter of 3.6m and the height of the furnace of 14m, the high-temperature flue gas inlet is positioned 3.8m above the steam oxygen nozzle.
The gasification furnace is adopted to gasify long flat anthracite:
mixing smokeless lump coal with the particle size of 6-50 mm and limestone according to a certain proportion (the proportion of the fluxing agent is about 3 percent), and conveying the mixture into a coal bunker for storage through a coal preparation conveyor; raw material coal and fluxing agent are added into a coal lock below from a coal bunker by means of gravity, and then are added into the gasification furnace from the top of the gasification furnace; the gasification pressure of the gasification furnace is 2.5Mpa, and the coal feeding amount is 10 t/h; the ash melting point of the long flat anthracite is about 1350-1400 ℃ after the fluxing agent is added;
the raw material coal undergoes several areas of drying, dry distillation, secondary gasification, primary gasification and combustion in the furnace;
435 deg.C, 3.5Mpa, 4000kg/h medium pressure steam, and 40 deg.C, 3.35Mpa, 4165Nm3/h pure oxygen from air separation at a steam-to-oxygen ratio of 0.96kg/Nm3After mixing, the gasifying agent is sprayed into the gasifier through four steam oxygen nozzles at the lower part of the gasifier, and reacts with carbon to generate combustion reaction, a large amount of heat is released, the temperature is raised to be higher than the melting point of coal ash to form slag, the slag is discharged from a slag discharging port of the gasifier, and hot gas generated by combustion rises to a first gasification zone to react with the carbon to generate synthesis gas;
after being combusted in a combustion chamber outside the gasifier, 230Nm3/h natural gas and 2380Nm3/h air generate high-temperature flue gas with the temperature of more than 1500 ℃, the high-temperature flue gas enters the upper part of the gasifier through two high-temperature gas inlets at the upper part of the gasifier, the coal bed is heated, the temperature of the coal bed is raised to 1000-1200 ℃, and a secondary gasification area is formed;
the product water from the drying and dry distillation area and the water generated by the combustion of natural gas and methane are subjected to a rapid gasification reaction in a secondary gasification area to generate CO and H2; meanwhile, the methane can also generate cracking reaction at high temperature to generate C and H2, so that the content of CH4 in the synthetic gas at the outlet of the gasification furnace is greatly reduced;
the temperature of the raw coal gas at the outlet of the gasification furnace is 900-1000 ℃, the amount of the raw coal gas is 212000 Nm3/h, and the composition (dry gas) of the raw coal gas is as follows:
| gas component | CO | H2 | CO2 | CH4 | H2S | N2+Ar | Tar oil |
| Content (wt.) | 58.1％ | 33.1％ | 4.7％ | 1.39％ | 0.09％ | 1.95％ | 0.67％ |
After the raw gas is dedusted and cooled by a Venturi scrubber and the gas-water liquid is separated from the gas-water liquid by a gas-liquid separator, the temperature is reduced to 175 ℃, the water content in the raw gas is 38 percent, and the raw gas is directly sent to a subsequent conversion section, so that the amount of water vapor supplemented in the conversion section can be greatly reduced, and the running economy is improved; cooling the gas water for recycling; the process has carbon conversion rate of 99.2%, steam consumption of 0.4 kg/kg coal, and steam decomposition rate of 93%.
Further adopt above-mentioned gasifier to gasify the temple river anthracite:
mixing smokeless lump coal with the particle size of 6-50 mm and a fluxing agent (limestone) according to a certain proportion (the fluxing agent accounts for 5 percent), and conveying the mixture into a coal bunker for storage through a coal preparation conveyor; raw material coal and fluxing agent are added into a coal lock below from a coal bunker by means of gravity, and then are added into the gasification furnace from the top of the gasification furnace; the gasification pressure of the gasification furnace is 4.0Mpa, and the coal feeding amount is 20 t/h; the ash melting point of the long flat anthracite is about 1350-one 1380 ℃ after the fluxing agent is added;
the raw material coal undergoes several areas of drying, dry distillation, secondary gasification, primary gasification and combustion in the furnace;
435 deg.C, 3.5Mpa, 10920kg/h steam and 40 deg.C, 3.35Mpa, 9100Nm3/h pure oxygen from air separation according to steam-oxygen ratio of 1.2kg/Nm3After mixing, the mixture is sprayed into the gasification furnace through four steam oxygen nozzles at the lower part of the gasification furnace, and the mixture is subjected to combustion reaction with carbon, releases a large amount of heat, is heated to a temperature higher than the melting point of coal ash to form molten slag, is discharged from a slag discharging port of the gasification furnace, and generates hot gas which rises to a first gasification zone and reacts with the carbon to generate synthesis gas;
high-temperature gas with temperature of more than 1500 ℃ generated after natural gas with the speed of 350Nm3/h and air with the speed of 3333Nm3/h are combusted in an independent combustion chamber enters the upper part of the gasification furnace through two high-temperature gas inlets at the upper part of the gasification furnace, the coal bed is heated, the temperature of the coal bed is raised to 1000-1200 ℃, and a secondary gasification area is formed;
the temperature of the crude gas at the outlet of the gasification furnace is 950-:
after the raw gas is dedusted and cooled by a Venturi scrubber and the gas-water liquid is separated from the gas-water liquid by a gas-liquid separator, the temperature is reduced to 181 ℃, the water content in the raw gas is 43 percent, and the raw gas is directly sent to a subsequent conversion section, so that the amount of water vapor supplemented in the conversion section can be greatly reduced, and the running economy is improved; cooling the gas water for recycling; the carbon conversion rate of the process is 99.0 percent, the steam consumption is 0.546kg steam/kg coal, and the steam decomposition rate is 91 percent.
Example 2:
this embodiment provides an anthracite gasifier, this gasifier is structural improving at current Lurgi, set up two high-temperature gas import in the middle part region of furnace body, and two high-temperature gas import evenly set up along furnace body circumference, two high-temperature gas import departments are connected with the combustion chamber that is used for producing high-temperature gas simultaneously, adopt this gasifier to gasify the temple river anthracite, embodiment 1 technological parameter difference is that the fluxing agent is not added in the raw materials coal among the gasification, and adopt the mode of solid-state row sediment.
Claims (10)
1. An anthracite low-methane gasification process is characterized by comprising the following steps: the method is characterized in that a fixed bed pressure gasification process is adopted to gasify anthracite to produce raw coal gas, high-temperature gas with the temperature of more than 1500 ℃ is introduced from the outside of a fixed bed pressure gasification furnace to a working region with the temperature of 800-1000 ℃ in the gasification process, and the high-temperature gas with the temperature of more than 1500 ℃ is natural gas, coal gas and H2Or gas produced by the combustion of petroleum and natural gas.
2. The anthracite low-methane gasification process as set forth in claim 1, wherein the particle size of the anthracite is 6-50 mm.
3. The anthracite low-methane gasification process as set forth in claim 1, wherein a fluxing agent is added to anthracite raw material coal, so that the melting point of the anthracite coal is 1350-1400 ℃, and the fluxing agent is limestone.
4. The anthracite low-methane gasification process as set forth in claim 3, characterized in that the temperature of the produced raw gas at the time of tapping is 900-.
5. The anthracite low-methane gasification process as set forth in claim 1, wherein the methane content in the raw gas produced is less than 1.5%.
6. The anthracite low-methane gasification process as set forth in claim 1, wherein the steam-to-oxygen ratio in the gasification process is 0.8-1.5 kg steam/Nm3The oxygen gas is used for generating oxygen gas,the amount of the natural gas is 0.018-0.050 Nm3/kg anthracite.
7. The anthracite low methane gasification process as set forth in claim 1, including:
the anthracite is dried and then is subjected to dry distillation, the coal subjected to dry distillation enters a secondary gasification stage, and then sequentially enters secondary gasification and primary gasification for gasification and then enters a combustion stage for combustion; in the process, high-temperature flue gas is introduced into a secondary gasification stage, and a gasification agent is introduced into a combustion stage;
the primary gasification is that gasification agent, hot gas generated by combustion and carbon existing in the primary gasification stage are subjected to gasification reaction;
the secondary gasification is that the gas generated by dry distillation and the gas generated by primary gasification have gasification reaction with carbon existing in the secondary gasification stage under the action of high-temperature gas, and methane in the gas has cracking reaction at high temperature during the reaction.
8. An anthracite low-methane gasification furnace comprises a fixed bed pressure gasification furnace, wherein a steam oxidizing agent inlet is arranged in the bottom area of the fixed bed pressure gasification furnace, and a crude gas outlet is arranged in the upper area of the fixed bed pressure gasification furnace.
9. The anthracite low-methane gasification furnace as set forth in claim 8, wherein a plurality of high-temperature flue gas inlets are arranged in the middle area of the fixed bed pressure gasification furnace, and are uniformly distributed in the circumferential direction of the furnace body.
10. The anthracite low-methane gasifier as set forth in claim 8, wherein a combustion chamber for generating high-temperature gas is connected to said high-temperature flue gas inlet.
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