CN104232125A - Powdery carbon material deashing method - Google Patents
Powdery carbon material deashing method Download PDFInfo
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- CN104232125A CN104232125A CN201310240080.3A CN201310240080A CN104232125A CN 104232125 A CN104232125 A CN 104232125A CN 201310240080 A CN201310240080 A CN 201310240080A CN 104232125 A CN104232125 A CN 104232125A
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Abstract
The invention relates to a powdery carbon material deashing method. A low-ash carbon material is produced by taking high-temperature gas hot carriers as a fluidized medium and deashing the powdery carbon material through a fluidized bed, and the cooled deashed carbon material returns the deashing fluidized bed for circulating processing. The powdery carbon deashing method is especially suitable for the process of producing the low-ash carbon material through deashing a raw material, namely pulverized coal carbonized semicoke, the operating temperature and circulating processing time of the deashing fluidized bed can be flexibly adjusted to adapt to the requirements of different varieties of carbon materials and deashing rates, and low-value carbon materials such as the powdery semicoke can be processed into high-value high-purity carbon materials.
Description
Technical field
The present invention relates to a kind of powdery carbon material deashing method, particularly the present invention relates to a kind of method using fluidized-bed to carry out powdery carbon material deliming production low ash carbon material, use high-temperature gas thermal barrier, the carbon material of low value such as powdery semicoke is processed into the high-purity carbon material of high value.
Background technology
Powdery carbon material of the present invention, is often referred to the carbon material containing more ash content, comprises fine coal, semicoke etc.
Powdery carbon material deliming of the present invention, refers to and makes under certain condition to be separated from each other containing the ash content inorganics in grey carbon material and organic matter, obtains the process of low ash carbon material and height ash material.
Along with the industrialization development of Coal Chemical Industry, the industrialization of fine coal destructive distillation is by powdery semicokes a large amount of for direct production or the clean clean coal of powdery, and lump coal semicoke or clean clean coal process also create a large amount of powdery semicokes or the clean clean coal of powdery, it is higher that these powdery semicokes or the clean clean coal of powdery have carbon content, the advantage that fugitive constituent is lower, reductive agent and fuel can be used as, but because ash oontent is higher, its purposes is restricted greatly, the object of this invention is to provide a kind of method that powdery carbon material deliming produces low ash carbon material, use high-temperature gas thermal barrier, the carbon material of low value such as powdery semicoke is processed into the high-purity carbon material of high value.
Conception of the present invention is: use high-temperature gas thermal barrier, fluidized-bed deliming device is used to complete powdery carbon material deliming, at the melting ash cooled rear discharge grey cooling segment of grey cooling segment from deliming device, at cooling part R1C, the temperature that deliming gas-solid logistics reduces below temperature to its ash content fusing point becomes cooling logistics, cooling logistics carries out carbon material that gas solid separation obtains and gas at separate part, after cooling, deliming carbon material returns the processing of deliming section fluidized bed circulation, by flexible deliming section temperature and cyclic process time, adapt to the requirement of different carbon material kind and deliming rate, the carbon material of low value such as powdery semicoke is processed into the high-purity carbon material of high value.
The circulating fluidized bed method for pyrolysis of fine coal of the present invention has no report.
The first object of the present invention is to propose a kind of method using the powdery carbon material deliming of tandem two-section flowing bed to produce low ash carbon material.
The second object of the present invention is to propose a kind of method using the powdery semicoke deliming of tandem two-section flowing bed to produce low ash carbon material.
Summary of the invention
A kind of powdery carbon of the present invention material deashing method, is characterized in that:
1. raw material powdery carbon material F11 adds system and flows to deliming part R1A;
Using the deliming part R1A of fluidized-bed, high-temperature gas thermal barrier F15 uses as fluidizing agent, make carbon granules heat, rotate, collision, collision rift bonding or be separated, and move upwards through fluidized-bed bed as deliming gas-solid logistics F17 enter cooling part R1C; In deliming fluidized-bed bed, carbon material F131 is heated to the temperature of more than its ash content fusing point, ash content in carbon granules moves to carbon grain surface, enters grey cooling segment R1B after the part of the melting ash of carbon grain surface flies away from carbon, C contact deliming stove stove inwall along inwall dirty formation lixivium F18; In carbon granules collision process, part carbon granules is bonded together manufacture macrobead by the ash content on surface, and part carbon granules is bonded together by the ash content on surface and is then separated into rich ash particle and poor ash particle;
2. at grey cooling segment R1B, from the grey cooling segment R1B of the cooled rear discharge of melting ash of deliming part R1A;
3. the temperature being cooled to below its ash content fusing point at cooling part R1C, deliming gas-solid logistics F17 becomes cooling logistics F19 and enters separate part S1;
4. carry out carbon material F13 that gas solid separation obtains and gas F20 at separate part S1, logistics F19 and leave separate part S1 respectively.
The present invention uses circulating fluidized bed deliming mode usually, it is characterized in that: 4. at separate part S1, and by returning charge circulation tube 131, carbon material F13 returns in the deliming fluidized-bed bed of deliming part R1A at least partially.
In order to ensure deliming efficiency, the present invention is characterised in that: 1. at deliming part R1A, and in deliming fluidized-bed bed, carbon material F131 is heated to the temperature of more than its ash fusion temperature; 3. at cooling part R1C; deliming gas-solid logistics F17 enters in cooling fluidized-bed bed, and mixing the temperature reducing below temperature to solid particulate ash content texturing temperature becomes the logistics F19 that lowers the temperature enter separate part S1 with raw material powdery carbon material F11 and the cold air that uses as required.
In order to improve deliming efficiency, the present invention is characterised in that: 1. at deliming part R1A, and in deliming fluidized-bed bed, carbon material F131 is heated to the temperature of more than its ash stream dynamic temperature; 3. at cooling part R1C; deliming gas-solid logistics F17 enters cooling fluidized-bed; mix the temperature reducing below temperature to solid particulate ash content texturing temperature to become the logistics F19 that lowers the temperature enter separate part S1 with raw material powdery carbon material F11 and the cold air that uses as required, cooling logistics F19 temperature is lower at least 30 DEG C than ash content texturing temperature in its solid particulate.
Cooling logistics F19 carries out two-stage when being separated, and the present invention is characterised in that: 5. carry out carbon material F22 that gas solid separation obtains and gas F21 at separate part S2, logistics F20 and leave separate part S2 respectively; By returning charge circulation tube 221, carbon material F22 returns the deliming fluidized-bed bed interior formation carbon material recycle stream F221 of deliming part R1A at least partially, and all the other carbon material F22 is as deliming carbon material logistics F222; The Action Target of separate part S2 is the particle isolating expection characteristic diameter D2, and characteristic diameter D2 is less than characteristic diameter D1, and the Action Target of separate part S1 is the particle isolating expection characteristic diameter D1.
When cooling logistics F19 carries out three grades of separation, the present invention is characterised in that: 5. at separate part S2, uses cyclonic separator to carry out gas solid separation; 6. carry out carbon material F32 that gas solid separation obtains and gas F31 at separate part S3, logistics F21 and leave separate part S3 respectively; By returning charge circulation tube 321, carbon material F32 returns the deliming fluidized-bed bed interior formation carbon material recycle stream F321 of deliming part R1A at least partially, and all the other carbon material F32 is as deliming carbon material logistics F222; The Action Target of separate part S3 is the particle isolating expection characteristic diameter D3, and characteristic diameter D3 is less than characteristic diameter D2; Usually, when passing through the filtering surface of the strainer made by intermetallic compound asymmetric membrane filtering material at separate part S3, logistics F21, particle diameter is greater than 1 micron particle thing and is blocked, and gas becomes dust-removing gas body by filtering surface; At the filtering surface of strainer, the particulate matter that part is blocked forms filter cake, departs from filtering surface at the regenerative process filter cake of the filtering surface of strainer, and the particulate matter of the filtering surface interception of strainer is collected as leaching solid.
Operational condition of the present invention is generally:
1. raw material powdery carbon material F11 particle size distribution is 0.001 ~ 6 millimeter; High-temperature gas thermal barrier F15 is from carbon material gasification, and the service temperature of high-temperature gas thermal barrier F15 is 1350 ~ 2000 DEG C;
Deliming part R1A operational condition: working pressure is normal pressure ~ 15MPa, service temperature is 1250 ~ 1750 DEG C, solid retention time is 10 ~ 1200 seconds;
2. grey cooling segment R1B operational condition: working pressure is normal pressure ~ 15MPa, ash temperature is 40 ~ 200 DEG C;
3. lower the temperature part R1C, cooling logistics F19 operational condition: working pressure is normal pressure ~ 15MPa, temperature is 800 ~ 1100 DEG C; Cooling logistics F19 temperature is lower at least 50 DEG C than ash content texturing temperature in its solid particulate;
4. separate part S1 operational condition: working pressure is normal pressure ~ 15MPa, temperature is 800 ~ 1100 DEG C; Separate part S1 uses cyclonic separator to carry out gas solid separation.
Operational condition of the present invention is generally:
1. raw material powdery carbon material F11 is semicoke; High-temperature gas thermal barrier F15 is from char Gasification process, and service temperature is 1350 ~ 1800 DEG C;
Raw material powdery carbon material F11 particle size distribution is 0.001 ~ 6 millimeter; Deliming part R1A operational condition: working pressure is normal pressure ~ 8MPa, service temperature is 1350 ~ 1650 DEG C, solid retention time is 30 ~ 600 seconds;
2. grey cooling segment R1B operational condition: working pressure is normal pressure ~ 8MPa, ash temperature is 40 ~ 200 DEG C;
3. lower the temperature part R1C, cooling logistics F19 operational condition: working pressure is normal pressure ~ 8MPa, temperature is 900 ~ 1000 DEG C; Cooling logistics F19 temperature is lower at least 100 DEG C than grain ash content texturing temperature in its solid;
4. separate part S1 operational condition: working pressure is normal pressure ~ 8MPa, temperature is 900 ~ 1000 DEG C.
The raw material powdery carbon material F11 of the present invention's processing is powdery semicoke or powdery coal, and particle size distribution is generally 0.001 ~ 6 millimeter, is generally 0.001 ~ 3 millimeter.
One of system operating mode of the present invention is for interval is reinforced, interval discharges product: high-temperature gas thermal barrier F15 enters continuously, and gas F20 discharges continuously; Raw material powdery carbon material F11 interval adds, and deliming carbon material product interval is discharged, and raw material powdery carbon material F11 adds and to be converted into deliming carbon material product after system carries out for some time deliming processing and to discharge; The raw material powdery carbon material F11 at every turn added measures for system solid reserves 10 ~ 60%, and the deliming carbon material product volume of each discharge system is 10 ~ 60% of system solid reserves.
One of system operating mode of the present invention is continuous charging, discharges product continuously: the carbon material F131 of deliming carbon material product discharge mass flow rate and deliming part R1A measures the ratio of mass flow rate, is generally 1 ~ 30 % by weight, is generally 5 ~ 10 % by weight.
High-temperature gas thermal barrier F15 of the present invention can be the coal gas from coal gasification process vapourizing furnace, can be the coal gas from coke breeze gasification process vapourizing furnace, can be fuel combustion flue gas, and fuel is selected from coal or combustion gas or oil.
In order to reclaim the heat energy of the discharge gas of separate part, use as raw material powdery carbon material F11 after the raw material powdery carbon material F01 of low-temperature condition and the discharge gas Contact Heating of the separate part of cooling logistics F19 heat up.
Deliming part R1A fluidized-bed of the present invention, grey cooling segment R1B cooling room, cooling part R1C fluidized-bed, can being combined into one equipment, cooling part R1C fluidized-bed is positioned on deliming part R1A fluidized-bed, and grey cooling segment R1B cooling room is positioned under deliming part R1A fluidized-bed.
As required, the present invention arranges macrobead carbon material pulverising step: 4. at separate part S1, enter crushing system as material F132 after part carbon material F13 cooling and change pulverizing logistics FF132 into, pulverize logistics FF132 and return in the fluidized-bed bed of deliming part R1A.
Action Target of the present invention is generally: raw material powdery carbon material F11 is converted into deliming carbon material product, and deliming rate is greater than 50%, and deliming carbon material product ash oontent is lower than 7 % by weight.
Action Target of the present invention is generally: raw material powdery carbon material F11 is converted into deliming carbon material product, and deliming rate is greater than 70%, and deliming carbon material product ash oontent is lower than 4 % by weight.
Action Target of the present invention is preferably: raw material powdery carbon material F11 is converted into deliming carbon material product, and deliming rate is greater than 85%, and deliming carbon material product ash oontent is lower than 2 % by weight.
Accompanying drawing explanation
Accompanying drawing 1 is the schematic flow sheet of general planning of the present invention, and in accompanying drawing 1, major equipment has: deliming part R1A fluidized-bed, grey cooling segment R1B cooling room, cooling part R1C fluidized bed integration equipment R1ABC, separate part S1, returning charge circulation tube 131; The pipeline relevant to deliming part R1A: powdery carbon material F131 input tube 11, vaporized chemical F15 input tube 13, lixivium F18 vent pipe 18; The pipeline relevant to grey cooling segment R1B: water coolant FW11 input tube W11, water coolant FW12 vent pipe W12, lime-ash outlet valve V1, lime-ash F14 vent pipe 14; The pipeline relevant to cooling part R1C: raw material powdery carbon material F11 input tube 11, cold air F12 input tube 12, logistics F19 vent pipe 19 of lowering the temperature; The pipeline relevant to separate part S1: feed-pipe 19, gaseous stream F20 vent pipe 20, solid phase logistics F13 vent pipe 13; Separate part S1, selects cyclonic separator usually; Logistics F13 can be divided into two-way: returning charge circulation tube 13 of leading up to returns in the deliming fluidized-bed bed of deliming part R1A, and a road is discharged through pipeline 132 as logistics F132.
Accompanying drawing 2 represents that the gas solid separation part of cooling logistics F19 is three grades of separation.At separate part S1, logistics F19 carries out carbon material F13 that gas solid separation obtains and gas F20 and leaves separate part S1 respectively, separate part S1 can use inertia device such as separating tank or cyclonic separator, logistics F13 can be divided into two-way: returning charge circulation tube 13 of leading up to returns in the deliming fluidized-bed bed of deliming part R1A, and a road is discharged through pipeline 132 as logistics F132; At separate part S2, logistics F20 carries out carbon material F22 that gas solid separation obtains and gas F21 and leaves separate part S2 respectively, separate part S1 uses cyclonic separator usually, logistics F22 can be divided into two-way: returning charge circulation tube 221 of leading up to returns in the deliming fluidized-bed bed of deliming part R1A, and a road is discharged through pipeline 222 as logistics F222; At separate part S3, logistics F21 carries out carbon material F32 that gas solid separation obtains and gas F31 and leaves separate part S3 respectively, during the filtering surface of the strainer that separate part S3 can use intermetallic compound asymmetric membrane filtering material to make, make particle diameter be greater than 1 micron particle thing to be blocked, logistics F32 can be divided into two-way: returning charge circulation tube 321 of leading up to returns in the deliming fluidized-bed bed of deliming part R1A, and a road is discharged through pipeline 322 as logistics F322.
Accompanying drawing 3 is a kind of application scheme schemas that the present invention is applied to coke breeze raw material deliming, compared with scheme shown in accompanying drawing 1, the raw material powdery carbon material F01 of low-temperature condition mix with the discharge gas F20 of the separate part of cooling logistics F19 complete heat temperature raising by fluidized-bed RO after enter separator SO as logistics F02 through piping 02 and carry out carbon material F04 that gas solid separation obtains and gas F03, separate part S0 uses cyclonic separator usually; Carbon material F04 uses as raw material powdery carbon material F11.
Accompanying drawing 4 is a kind of application scheme schemas that the present invention is applied to fine coal raw material deliming, compared with scheme shown in accompanying drawing 3, carbon material F04 is divided into two-way: returning charge circulation tube 041 of leading up to returns fluidized-bed R0 circulating-heating as cycle stock F041 and carries out destructive distillation devolatilization, and a road uses as raw material powdery carbon material F11.
Embodiment
Below describe the present invention in detail.
Pressure of the present invention, refers to absolute pressure.
Technical solution of the present invention is described in detail below in conjunction with accompanying drawing.Accompanying drawing in order to illustrate that the present invention draws, but can not limit range of application of the present invention.
Accompanying drawing 1 is the schematic flow sheet of general planning of the present invention, system is discharged as deliming carbon material as general planning solid phase logistics F13 of the present invention, in order to improve deliming efficiency, usual logistics F13 is divided into two-way: returning charge circulation tube 13 of leading up to returns in the deliming fluidized-bed bed of deliming part R1A, and a road is discharged through pipeline 132 as logistics F132.
Accompanying drawing 2 represents that the gas solid separation part of cooling logistics F19 is three grades of separation.The strainer that separate part S3 can use intermetallic compound asymmetric membrane filtering material to make.The present invention containing solid dust and or containing the high-temperature gas of tar gas, part dust granules diameter be wherein less than 5 microns with, service temperature is between 500 ~ 900 DEG C, and gas filtration process entails leaches the particle that diameter is greater than 1 micron, with this understanding, conventional filter material cannot efficiently work for a long time.The Al series intermetallic compound asymmetric membrane filtering material such as FeAl series intermetallic compound asymmetric membrane filtering material of Chengdu YiTai Science Co., Ltd, characteristics such as there is excellent high temperature oxidation resisting, easily seal, processibility is good, particularly under the severe rugged environments such as high temperature, there is the irreplaceable advantage of conventional filter material, be applicable to the gas solid separation purification in the technique such as the purification of high temperature sulfurous gas, iron alloy high-temperature furnace gas Recovery Purifying, blast furnace, RECOVERY OF CONVERTER GAS utilization, coal transforms, calcium carbide is industrial, biogas is industrial, oil shale industry.Separate part S3 of the present invention, based under high-temperature pressurizing (or normal pressure) condition containing solid dust, be in gas phase state containing the coal gas of micro-tar gas is coal-tar middle oil, use Al series intermetallic compound asymmetric membrane filtering material to leach diameter and be greater than 1 micron of particle even leaching diameter and be greater than 0.3 micron, obtain the coal gas of solid.In order to give full play to filter core function, usually requiring the unstripped gas entering strainer to be the logistics of gas-solid mixed phase, not wishing to occur gas, oil, solid three-phase logistics, may need to reduce feeding temperature to ensure filter element life simultaneously.
When the gas solid separation part of the logistics F19 that lowers the temperature is the second-order separation, the strainer that separate part S2 can use intermetallic compound asymmetric membrane filtering material to make.When under particular case, such as raw material powdery carbon material F11 granularity is less than 100 microns, the strainer that separate part S1 also can use intermetallic compound asymmetric membrane filtering material to make.
Accompanying drawing 3 is a kind of application scheme schemas that the present invention is applied to coke breeze raw material deliming, separate part S0, when under particular case, such as raw material powdery carbon material F01 granularity is less than 100 microns, the strainer that separate part S0 also can use intermetallic compound asymmetric membrane filtering material to make.
Accompanying drawing 4 is a kind of application scheme schemas that the present invention is applied to fine coal raw material deliming, separate part SO, when under particular case, such as raw material powdery carbon material F01 granularity is less than 100 microns, the strainer that separate part S0 also can use intermetallic compound asymmetric membrane filtering material to make.
A kind of powdery carbon of the present invention material deashing method, is characterized in that:
1. raw material powdery carbon material F11 adds system and flows to deliming part R1A;
Using the deliming part R1A of fluidized-bed, high-temperature gas thermal barrier F15 uses as fluidizing agent, make carbon granules heat, rotate, collision, collision rift bonding or be separated, and move upwards through fluidized-bed bed as deliming gas-solid logistics F17 enter cooling part R1C; In deliming fluidized-bed bed, carbon material F131 is heated to the temperature of more than its ash content fusing point, ash content in carbon granules moves to carbon grain surface, enters grey cooling segment R1B after the part of the melting ash of carbon grain surface flies away from carbon, C contact deliming stove stove inwall along inwall dirty formation lixivium F18; In carbon granules collision process, part carbon granules is bonded together manufacture macrobead by the ash content on surface, and part carbon granules is bonded together by the ash content on surface and is then separated into rich ash particle and poor ash particle;
2. at grey cooling segment R1B, from the grey cooling segment R1B of the cooled rear discharge of melting ash of deliming part R1A;
3. the temperature being cooled to below its ash content fusing point at cooling part R1C, deliming gas-solid logistics F17 becomes cooling logistics F19 and enters separate part S1;
4. carry out carbon material F13 that gas solid separation obtains and gas F20 at separate part S1, logistics F19 and leave separate part S1 respectively.
The present invention uses circulating fluidized bed deliming mode usually, it is characterized in that: 4. at separate part S1, and by returning charge circulation tube 131, carbon material F13 returns in the deliming fluidized-bed bed of deliming part R1A at least partially.
In order to ensure deliming efficiency, the present invention is characterised in that: 1. at deliming part R1A, and in deliming fluidized-bed bed, carbon material F131 is heated to the temperature of more than its ash fusion temperature; 3. at cooling part R1C; deliming gas-solid logistics F17 enters in cooling fluidized-bed bed, and mixing the temperature reducing below temperature to solid particulate ash content texturing temperature becomes the logistics F19 that lowers the temperature enter separate part S1 with raw material powdery carbon material F11 and the cold air that uses as required.
In order to improve deliming efficiency, the present invention is characterised in that: 1. at deliming part R1A, and in deliming fluidized-bed bed, carbon material F131 is heated to the temperature of more than its ash stream dynamic temperature; 3. at cooling part R1C; deliming gas-solid logistics F17 enters cooling fluidized-bed; mix the temperature reducing below temperature to solid particulate ash content texturing temperature to become the logistics F19 that lowers the temperature enter separate part S1 with raw material powdery carbon material F11 and the cold air that uses as required, cooling logistics F19 temperature is lower at least 30 DEG C than ash content texturing temperature in its solid particulate.
Cooling logistics F19 carries out two-stage when being separated, and the present invention is characterised in that: 5. carry out carbon material F22 that gas solid separation obtains and gas F21 at separate part S2, logistics F20 and leave separate part S2 respectively; By returning charge circulation tube 221, carbon material F22 returns the deliming fluidized-bed bed interior formation carbon material recycle stream F221 of deliming part R1A at least partially, and all the other carbon material F22 is as deliming carbon material logistics F222; The Action Target of separate part S2 is the particle isolating expection characteristic diameter D2, and characteristic diameter D2 is less than characteristic diameter D1, and the Action Target of separate part S1 is the particle isolating expection characteristic diameter D1.
When cooling logistics F19 carries out three grades of separation, the present invention is characterised in that: 5. at separate part S2, uses cyclonic separator to carry out gas solid separation; 6. carry out carbon material F32 that gas solid separation obtains and gas F31 at separate part S3, logistics F21 and leave separate part S3 respectively; By returning charge circulation tube 321, carbon material F32 returns the deliming fluidized-bed bed interior formation carbon material recycle stream F321 of deliming part R1A at least partially, and all the other carbon material F32 is as deliming carbon material logistics F222; The Action Target of separate part S3 is the particle isolating expection characteristic diameter D3, and characteristic diameter D3 is less than characteristic diameter D2; Usually, when passing through the filtering surface of the strainer made by intermetallic compound asymmetric membrane filtering material at separate part S3, logistics F21, particle diameter is greater than 1 micron particle thing and is blocked, and gas becomes dust-removing gas body by filtering surface; At the filtering surface of strainer, the particulate matter that part is blocked forms filter cake, departs from filtering surface at the regenerative process filter cake of the filtering surface of strainer, and the particulate matter of the filtering surface interception of strainer is collected as leaching solid.
Operational condition of the present invention is generally:
1. raw material powdery carbon material F11 particle size distribution is 0.001 ~ 6 millimeter; High-temperature gas thermal barrier F15 is from carbon material gasification, and the service temperature of high-temperature gas thermal barrier F15 is 1350 ~ 2000 DEG C;
Deliming part R1A operational condition: working pressure is normal pressure ~ 15MPa, service temperature is 1250 ~ 1750 DEG C, solid retention time is 10 ~ 1200 seconds;
2. grey cooling segment R1B operational condition: working pressure is normal pressure ~ 15MPa, ash temperature is 40 ~ 200 DEG C;
3. lower the temperature part R1C, cooling logistics F19 operational condition: working pressure is normal pressure ~ 15MPa, temperature is 800 ~ 1100 DEG C; Cooling logistics F19 temperature is lower at least 50 DEG C than ash content texturing temperature in its solid particulate;
4. separate part S1 operational condition: working pressure is normal pressure ~ 15MPa, temperature is 800 ~ 1100 DEG C; Separate part S1 uses cyclonic separator to carry out gas solid separation.
Operational condition of the present invention is generally:
1. raw material powdery carbon material F11 is semicoke; High-temperature gas thermal barrier F15 is from char Gasification process, and service temperature is 1350 ~ 1800 DEG C;
Raw material powdery carbon material F11 particle size distribution is 0.001 ~ 6 millimeter; Deliming part R1A operational condition: working pressure is normal pressure ~ 8MPa, service temperature is 1350 ~ 1650 DEG C, solid retention time is 30 ~ 600 seconds;
2. grey cooling segment R1B operational condition: working pressure is normal pressure ~ 8MPa, ash temperature is 40 ~ 200 DEG C;
3. lower the temperature part R1C, cooling logistics F19 operational condition: working pressure is normal pressure ~ 8MPa, temperature is 900 ~ 1000 DEG C; Cooling logistics F19 temperature is lower at least 100 DEG C than grain ash content texturing temperature in its solid;
4. separate part S1 operational condition: working pressure is normal pressure ~ 8MPa, temperature is 900 ~ 1000 DEG C.
The raw material powdery carbon material F11 of the present invention's processing is powdery semicoke or powdery coal, and particle size distribution is generally 0.001 ~ 6 millimeter, is generally 0.001 ~ 3 millimeter.
One of system operating mode of the present invention is for interval is reinforced, interval discharges product: high-temperature gas thermal barrier F15 enters continuously, and gas F20 discharges continuously; Raw material powdery carbon material F11 interval adds, and deliming carbon material product interval is discharged, and raw material powdery carbon material F11 adds and to be converted into deliming carbon material product after system carries out for some time deliming processing and to discharge; The raw material powdery carbon material F11 at every turn added measures for system solid reserves 10 ~ 60%, and the deliming carbon material product volume of each discharge system is 10 ~ 60% of system solid reserves.
One of system operating mode of the present invention is continuous charging, discharges product continuously: deliming carbon material product discharges the ratio of the carbon material F131 mass flow rate of mass flow rate and deliming part R1A, is generally 1 ~ 30 % by weight, is generally 5 ~ 10 % by weight.
High-temperature gas thermal barrier F15 of the present invention can be the coal gas from coal gasification process vapourizing furnace, can be the coal gas from coke breeze gasification process vapourizing furnace, can be fuel combustion flue gas, and fuel is selected from coal or combustion gas or oil.
In order to reclaim the heat energy of the discharge gas of separate part, use as raw material powdery carbon material F11 after the raw material powdery carbon material F01 of low-temperature condition and the discharge gas Contact Heating of the separate part of cooling logistics F19 heat up.
Deliming part R1A fluidized-bed of the present invention, grey cooling segment R1B cooling room, cooling part R1C fluidized-bed, can being combined into one equipment, cooling part R1C fluidized-bed is positioned on deliming part R1A fluidized-bed, and grey cooling segment R1B cooling room is positioned under deliming part R1A fluidized-bed.
As required, the present invention arranges macrobead carbon material pulverising step: 4. at separate part S1, enter crushing system as material F132 after part carbon material F13 cooling and change pulverizing logistics FF132 into, pulverize logistics FF132 and return in the fluidized-bed bed of deliming part R1A.
Action Target of the present invention is generally: raw material powdery carbon material F11 is converted into deliming carbon material product, and deliming rate is greater than 50%, and deliming carbon material product ash oontent is lower than 7 % by weight.
Action Target of the present invention is generally: raw material powdery carbon material F11 is converted into deliming carbon material product, and deliming rate is greater than 70%, and deliming carbon material product ash oontent is lower than 4 % by weight.
Action Target of the present invention is preferably: raw material powdery carbon material F11 is converted into deliming carbon material product, and deliming rate is greater than 85%, and deliming carbon material product ash oontent is lower than 2 % by weight.
Claims (26)
1. a powdery carbon material deashing method, is characterized in that:
1. raw material powdery carbon material F11 adds system and flows to deliming part R1A;
Using the deliming part R1A of fluidized-bed, high-temperature gas thermal barrier F15 uses as fluidizing agent, make carbon granules heat, rotate, collision, collision rift bonding or be separated, and move upwards through fluidized-bed bed as deliming gas-solid logistics F17 enter cooling part R1C; In deliming fluidized-bed bed, carbon material F131 is heated to the temperature of more than its ash content fusing point, ash content in carbon granules moves to carbon grain surface, enters grey cooling segment R1B after the part of the melting ash of carbon grain surface flies away from carbon, C contact deliming stove stove inwall along inwall dirty formation lixivium F18; In carbon granules collision process, part carbon granules is bonded together manufacture macrobead by the ash content on surface, and part carbon granules is bonded together by the ash content on surface and is then separated into rich ash particle and poor ash particle;
2. at grey cooling segment R1B, from the grey cooling segment R1B of the cooled rear discharge of melting ash of deliming part R1A;
3. the temperature being cooled to below its ash content fusing point at cooling part R1C, deliming gas-solid logistics F17 becomes cooling logistics F19 and enters separate part S1;
4. carry out carbon material F13 that gas solid separation obtains and gas F20 at separate part S1, logistics F19 and leave separate part S1 respectively.
2. method according to claim 1, is characterized in that:
4. at separate part S1, by returning charge circulation tube 131, carbon material F13 returns in the deliming fluidized-bed bed of deliming part R1A at least partially.
3. method according to claim 1, is characterized in that:
1., at deliming part R1A, in deliming fluidized-bed bed, carbon material F131 is heated to the temperature of more than its ash fusion temperature;
3. at cooling part R1C; deliming gas-solid logistics F17 enters in cooling fluidized-bed bed, and mixing the temperature reducing below temperature to solid particulate ash content texturing temperature becomes the logistics F19 that lowers the temperature enter separate part S1 with raw material powdery carbon material F11 and the cold air that uses as required.
4. method according to claim 2, is characterized in that:
1., at deliming part R1A, in deliming fluidized-bed bed, carbon material F131 is heated to the temperature of more than its ash stream dynamic temperature;
3. at cooling part R1C; deliming gas-solid logistics F17 enters cooling fluidized-bed; mix the temperature reducing below temperature to solid particulate ash content texturing temperature to become the logistics F19 that lowers the temperature enter separate part S1 with raw material powdery carbon material F11 and the cold air that uses as required, cooling logistics F19 temperature is lower at least 30 DEG C than ash content texturing temperature in its solid particulate.
5. method according to claim 4, is characterized in that:
5. carry out carbon material F22 that gas solid separation obtains and gas F21 at separate part S2, logistics F20 and leave separate part S2 respectively; By returning charge circulation tube 221, carbon material F22 returns the deliming fluidized-bed bed interior formation carbon material recycle stream F221 of deliming part R1A at least partially, and all the other carbon material F22 is as deliming carbon material logistics F222; The Action Target of separate part S2 is the particle isolating expection characteristic diameter D2, and characteristic diameter D2 is less than characteristic diameter D1, and the Action Target of separate part S1 is the particle isolating expection characteristic diameter D1.
6. method according to claim 5, is characterized in that:
5. at separate part S2, cyclonic separator is used to carry out gas solid separation;
6. carry out carbon material F32 that gas solid separation obtains and gas F31 at separate part S3, logistics F21 and leave separate part S3 respectively; By returning charge circulation tube 321, carbon material F32 returns the deliming fluidized-bed bed interior formation carbon material recycle stream F321 of deliming part R1A at least partially, and all the other carbon material F32 is as deliming carbon material logistics F222; The Action Target of separate part S3 is the particle isolating expection characteristic diameter D3, and characteristic diameter D3 is less than characteristic diameter D2.
7. method according to claim 6, is characterized in that:
When 6. passing through the filtering surface of the strainer made by intermetallic compound asymmetric membrane filtering material at separate part S3, logistics F21, particle diameter is greater than 1 micron particle thing and is blocked, and gas becomes dust-removing gas body by filtering surface; At the filtering surface of strainer, the particulate matter that part is blocked forms filter cake, departs from filtering surface at the regenerative process filter cake of the filtering surface of strainer, and the particulate matter of the filtering surface interception of strainer is collected as leaching solid.
8. the method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, is characterized in that:
1. raw material powdery carbon material F11 particle size distribution is 0.001 ~ 6 millimeter; High-temperature gas thermal barrier F15 is from carbon material gasification, and the service temperature of high-temperature gas thermal barrier F15 is 1350 ~ 2000 DEG C;
Deliming part R1A operational condition: working pressure is normal pressure ~ 15MPa, service temperature is 1250 ~ 1750 DEG C, solid retention time is 10 ~ 1200 seconds;
2. grey cooling segment R1B operational condition: working pressure is normal pressure ~ 15MPa, ash temperature is 40 ~ 200 DEG C;
3. lower the temperature part R1C, cooling logistics F19 operational condition: working pressure is normal pressure ~ 15MPa, temperature is 800 ~ 1100 DEG C; Cooling logistics F19 temperature is lower at least 50 DEG C than ash content texturing temperature in its solid particulate;
4. separate part S1 operational condition: working pressure is normal pressure ~ 15MPa, temperature is 800 ~ 1100 DEG C; Separate part S1 uses cyclonic separator to carry out gas solid separation.
9. method according to claim 8, is characterized in that:
1. raw material powdery carbon material F11 is semicoke; High-temperature gas thermal barrier F15 is from char Gasification process, and service temperature is 1350 ~ 1800 DEG C;
Raw material powdery carbon material F11 particle size distribution is 0.001 ~ 6 millimeter; Deliming part R1A operational condition: working pressure is normal pressure ~ 8MPa, service temperature is 1350 ~ 1650 DEG C, solid retention time is 30 ~ 600 seconds;
2. grey cooling segment R1B operational condition: working pressure is normal pressure ~ 8MPa, ash temperature is 40 ~ 200 DEG C;
3. lower the temperature part R1C, cooling logistics F19 operational condition: working pressure is normal pressure ~ 8MPa, temperature is 900 ~ 1000 DEG C; Cooling logistics F19 temperature is lower at least 100 DEG C than grain ash content texturing temperature in its solid;
4. separate part S1 operational condition: working pressure is normal pressure ~ 8MPa, temperature is 900 ~ 1000 DEG C.
10. the method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, is characterized in that:
Raw material powdery carbon material F11 is powdery semicoke, and particle size distribution is 0.001 ~ 6 millimeter.
11. methods according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, is characterized in that:
Raw material powdery carbon material F11 is powdery semicoke, and particle size distribution is 0.001 ~ 3 millimeter.
12. methods according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, is characterized in that:
Raw material powdery carbon material F11 is powdery coal, and particle size distribution is 0.001 ~ 6 millimeter.
13. methods according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, is characterized in that:
Raw material powdery carbon material F11 is powdery coal, and particle size distribution is 0.001 ~ 3 millimeter.
14. methods according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, is characterized in that:
System operating mode is for interval is reinforced, interval discharges product: high-temperature gas thermal barrier F15 enters continuously, and gas F20 discharges continuously; Raw material powdery carbon material F11 interval adds, and deliming carbon material product interval is discharged, and raw material powdery carbon material F11 adds and to be converted into deliming carbon material product after system carries out for some time deliming processing and to discharge.
15. methods according to claim 14, is characterized in that:
System operating mode is for interval is reinforced, interval discharges product: the raw material powdery carbon material F11 at every turn added measures for system solid reserves 10 ~ 60%, and the deliming carbon material product volume of each discharge system is 10 ~ 60% of system solid reserves.
16. methods according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, is characterized in that:
System operating mode is continuous charging, discharges product continuously: it is 1 ~ 30% of the carbon material F131 mass flow rate of deliming part R1A that deliming carbon material product discharges mass flow rate.
17. methods according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, is characterized in that:
System operating mode is continuous charging, discharges product continuously: it is 5 ~ 10% of the carbon material F131 mass flow rate of deliming part R1A that deliming carbon material product discharges mass flow rate.
18. methods according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, is characterized in that:
High-temperature gas thermal barrier F15 is the coal gas from coal gasification process vapourizing furnace.
19. methods according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, is characterized in that:
High-temperature gas thermal barrier F15 is the coal gas from coke breeze gasification process vapourizing furnace.
20. methods according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, is characterized in that:
High-temperature gas thermal barrier F15 is fuel combustion flue gas, and fuel is selected from coal or combustion gas or oil.
21. methods according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, is characterized in that:
Use as raw material powdery carbon material F11 after the raw material powdery carbon material F01 of low-temperature condition and the discharge gas Contact Heating of the separate part of cooling logistics F19 heat up.
22. methods according to claim 5 or 6 or 7, is characterized in that:
4. at separate part S1, enter crushing system as material F132 after a part of carbon material F13 lowers the temperature and change pulverizing logistics FF132 into, pulverize logistics FF132 and return in the fluidized-bed bed of deliming part R1A.
23. methods according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, is characterized in that:
Raw material powdery carbon material F11 is converted into deliming carbon material product, and deliming rate is greater than 50%, and deliming carbon material product ash oontent is lower than 7 % by weight.
24. methods according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, is characterized in that:
Raw material powdery carbon material F11 is converted into deliming carbon material product, and deliming rate is greater than 70%, and deliming carbon material product ash oontent is lower than 4 % by weight.
25. methods according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, is characterized in that:
Raw material powdery carbon material F11 is converted into deliming carbon material product, and deliming rate is greater than 85%, and deliming carbon material product ash oontent is lower than 2 % by weight.
26. methods according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, is characterized in that:
Deliming part R1A fluidized-bed, grey cooling segment R1B cooling room, cooling part R1C fluidized-bed, being combined into one equipment, cooling part R1C fluidized-bed is positioned on deliming part R1A fluidized-bed, and grey cooling segment R1B cooling room is positioned under deliming part R1A fluidized-bed.
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| CN104774670A (en) * | 2015-03-24 | 2015-07-15 | 石家庄新华能源环保科技股份有限公司 | Production method and device for ashless coal |
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Application publication date: 20141224 |