CN102653683A - Internal heating type coal carbonization gas production process based on pressurization method - Google Patents
Internal heating type coal carbonization gas production process based on pressurization method Download PDFInfo
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Abstract
The invention provides an internal heating type coal carbonization gas production process based on a pressurization method, as a conventional internal heating type coal carbonization gas production process based on a non-pressure method has the defects that the coal carbonization time is long, the pressure of produced coal gas is low, and the like, since a heat transfer coefficient is small due to a low operation pressure (generally, the operation pressure being 0.2 MPa lower than an absolute pressure) and a low gas phase density. The internal heating type coal carbonization gas production process can be used for increasing the operation pressure to be above 0.5 MPa more than the absolute pressure; as the quantity of gas molecules in a unit volume is increased due to pressurization, the heat transfer time and the carbonization time can be shortened; and high-pressure externally-output coal gas can be acquired. For a coal carbonization procedure with the increment of the quantity of a gas volume, when the externally-output coal gas is needed to be further pressurized to be subjected to processing treatment, the internal heating type coal carbonization gas production process can also be used for reducing the energy consumption in a whole procedure.
Description
Technical field
The present invention relates to a kind of pressurization internally heated coal carbonization gas-making process; Compare with conventional non-pressure process internally heated coal carbonization gas-making process and to have improved the gas phase operation pressure in the charring furnace, can dwindle the gassy system volume significantly, save floor space, improve dry distillation of coal gas making production efficiency, reduce and consume, widen the coal charge scope.
Background technology
The present invention uses following conceptual description internally heated coal carbonization gas-making process process:
1. internally heated coal carbonization gas making part: with coal, water (coal charge carry water with or outer water supply), oxygen donator, fuel body be raw material; Obtain charcoal, from ring coal gas, tar, contain the technological process of solid such as tar sewage, gas, liquid product, comprise that coal charge goes into furnace system, charring furnace ST system, charcoal and go out furnace system, raw gas cooling separation, heat-carrying gas and return the stove recycle system etc.;
2. the logistics of gas making part internal recycle: the recycle stream of gas making partial interior is as returning stove heat-carrying gas;
3. from ring coal gas processing part: leave the machining process of the coal gas in coal gas internal recycle loop (promptly discharging the gas making part), like wet desulphurization hydrogen process, pressure swing adsorption process detar process etc.;
4. gas making part outer circulation logistics: by leaving ring coal gas processing part to gas making part mobile recycle stream.
The thermal equilibrium of the heat transfer process that internally heated coal carbonization furnace is comprised; The mass ratio that relates to solid amount of vaporization and gas stream; The solid voidage is exactly gas-phase space in essence; Represent gas phase operation pressure (absolute pressure) with PV, represent bed voidage with ε, then the gaseous stream quality is expressed as with the ratio KW of solid amount of vaporization quality:
KW=(PV * gas-phase space volume * gas phase average density)/(coal charge entity volume * solid mean density * solid vaporization rate)
For the particular coal retort process, because gas phase average density, solid mean density, solid vaporization rate are constant relatively, following formula is changed to the volume ratio KV of gaseous phase materials and solid amount of vaporization:
KV=(PV * gas-phase space volume)/(coal charge entity volume * solid vaporization rate)
=(PV * ε/(1-ε))/solid vaporization rate
=(KW * solid mean density)/gas phase average density
The suitable operational condition of any specific internally heated coal carbonization process all must satisfy the thermal equilibrium requirement; Kinetics requirement based on the heat supply cascade process; During gas phase heating coal charge: gas phase (heat supply side) ability of conducting heat must be more than or equal to solid phase (side of the being heated) ability of being heated; During gas phase cooling charcoal material: gas phase is conducted heat (endothermic side) ability must be more than or equal to solid phase heat release (side of being cooled) ability; Therefore there is corresponding minimum KW; That is to say to have corresponding minimum KV, have specific minimum PV, must keep specific minimum bed voidage ε for specific " PV and solid vaporization rate " in other words for specific " bed voidage ε and solid vaporization rate ".
Because it is that PV is about 0.12～0.18MPa (absolute pressure) that the PV of existing internally heated coal carbonization furnace is normal pressure; For coal charge and the definite destructive distillation operating process of destructive gasifying rate thereof; There is a lower value in the bed voidage ε that adapts with it, when bed voidage ε reaches or be lower than this lower value, only says from the thermal equilibrium angle; Internally heated coal carbonization furnace can't works better, a basic reason of Here it is existing internally heated coal carbonization furnace restriction coal charge granularity lower limit.
Can find out that from KV=((PV * ε/(1-ε))/solid vaporization rate) improving one of fine coal destructive distillation manipulating approach is to reduce the solid vaporization rate, the inventor has related application in addition.
Can find out that from KV=((PV * ε/(1-ε))/solid vaporization rate) improving one of fine coal destructive distillation manipulating approach is to increase bed voidage ε, the inventor has related application in addition.
Can find out that from KV=((PV * ε/(1-ε))/solid vaporization rate) improving one of fine coal destructive distillation manipulating approach is to increase PV, this is the present invention's target.
As everyone knows; Anshan Thermal Energy Inst. of China Steel Group begins " is that raw material is at the special-purpose blue charcoal of vertical retort refining iron alloy with non-caking coal or weakly caking coal lump coal " technology (hereinafter to be referred as middle steel internally heated coal carbonization gas making technology BT) of constantly research and development the early 1980s; Adopt and be fit to coal source (such as Chinese Datong District, the geographic coal in refreshing mansion); The blue charcoal of refining and by-product raw gas and middle coalite tar in vertical retort; Be the mature industryization technology that a kind of blue charcoal good quality of product, coal tar productive rate are high, lower, the supporting green technology of construction costs is perfect, obtained already widely applying.
Middle steel internally heated coal carbonization gas making technology BT; General feature with the blue charcoal technology of similar internally heated coal carbonization system: the destructive distillation furnace inner gas pressure is normal pressure (pressure is between 0.12～0.18MPa (absolute pressure) usually), and the raw gas that gas retort produces belongs to normal pressure gas.In this conventional non-pressure process internally heated coal carbonization gas-making process; It is main because gas-operated pressure lowly is that gas density is low in the gas retort, gas and the solid probability of collision is low, rate of heat transfer is low; Cause that dry distillation efficiency is low, the gas retort equipment volume is huge, floor space is big, investment is high, the tar yield is low; Produced simultaneously coal gas is normal pressure gas, numerous shortcomings such as have that gas system is bulky, floor space is big, investment is high, gas pressure can be low, coal gas process of cooling water consumption is high, the defeated coal gas concentration height, gas wet depriving hydrogen sulphide decreasing ratio ground, the circulation heat-carrying gas working cycle compression ratio that carry water and macromole hydrocarbon be big outward.
As far as the heat transfer process that internally heated coal carbonization gas making process comprises, relate to solid, liquids and gases logistics.Pressure is small to solid conductive heat coefficient and intermolecular distance influence.Small to liquid thermal conductivity factor and intermolecular distance influence, pressure mainly is to influence solubleness and liquid ingredient in gas the equilibrium concentration of gas in liquid to the liquid physical behavior.Pressure is small to the influence of gas conduction coefficient; But pressure then influences huge to distance between gas molecule; Pressurize can produce following effect: first aspect; Significantly improve working pressure at double the pressurized gas volume, significantly improve gas density, at double shortened gas heat-transfer migration stroke prolonged in other words the residence time promptly conduct heat the time, significantly improve rate of heat transfer; Can significantly improve dry distillation efficiency, significantly shorten the destructive distillation time, significantly reduce investment, can adapt to the fine coal retort process that porosity is little between coal charge more; Second aspect; Improve working pressure and utilize the pressure energy work of expansion that reduction gas making product is made when producing a large amount of high pressure raw coal gas in the solid; Significantly reduced invalid work of expansion consumption; Can significantly reduce gas making process energy consumption and promptly reduce the oxygen consumption, reduce fuel consumption, reduce breaking of coal charge dehydration water evaporated volume ratio of expansion, reduction coal charge gasification oil gas volume expansion ratio thereby minimizing coal charge simultaneously and reduce the powder productive rate; The third aspect; Significantly improve working pressure and can significantly improve raw gas pressure, significantly improve raw gas density, significantly improve water and macromole hydrocarbon dividing potential drop in coal gas, can dwindle at double the gas system volume, significantly save floor space, reduce investment outlay significantly, the coal gas process of cooling can adopt air-cooler significantly reduce water consumption, at double reduce outer defeated coal gas carry the concentration of water and macromole hydrocarbon, at double reduce concentration of hydrogen sulfide in the gas wet depriving hydrogen sulphide after gas, reduce circulation heat-carrying gas working cycle compression ratio at double; Fourth aspect; Improve the inevitable supporting use pressure combustion of working pressure chamber; Its unit volume intensity of combustion is with proportional enhancing, and this is that liquid fuel (such as coal tar heavy oil) or solid fuel partly or entirely replace the gas-fired heat supply to realize certain favourable condition has been created in the displacement of synthesis gas components in the fuel gas.In the description of the effect that above-mentioned raising gas retort working pressure brings, " at double " notion of use belongs to substantially and compares, and is not definite ratio explanation.
Therefore; It is considered herein that conventional internally heated coal carbonization technology belongs to non-pressure process internally heated coal carbonization technology, does not form complete " internally heated coal carbonization gas-making process " notion; There is a great technological deficiency that gas phase operation pressure is low in the pressure characteristic of having ignored gaseous stream.Based on this concept nature understanding, the present invention proposes a kind of pressurization internally heated coal carbonization gas-making process that improves internally heated coal carbonization gas making process operation pressure, to realize following efficient low-consume purpose:
1. because of having increased the quantity of gas molecule in the unit volume, shortened gas heat-transfer migration distance, first effect is to dwindle gas retort os volume significantly, save and take up an area of, reduce investment outlay, improve unit volume distillation apparatus charcoal product production capacity;
2. because of having increased the quantity of gas molecule in the unit volume, shortened gas heat-transfer migration distance, second effect is to shorten the destructive distillation time significantly, be beneficial to and reduce pyrolysis temperature, be beneficial to and improve the tar yield, be beneficial to and improve quality of coke tar; Because the coal charge destructive distillation time shortens significantly, shortened coal charge simultaneously or the charcoal material is bonded to the piece time, widened dry distillation of coal raw material range to a certain extent, for the fine coal distillation process has been created certain favourable condition;
3. because of having increased the quantity of gas molecule in the unit volume, having shortened gas heat-transfer migration distance, the 3rd effect is to adapt to the fine coal retort process that porosity is little between coal charge more;
4. based on the internally heated coal carbonization process be outer defeated coal gas body volume amount usually greater than coal carbonization furnace outward the gas stream volume of defeated oxygenant volume amount increase process and promptly belong to macroscopical gas making process; Improve working pressure and can utilize pressure energy volume production in the solid to give birth to the raw gas of a large amount of high pressures, quadruple effect really is can obtain the defeated gas pressure of high pressure outward, to save coal gas process of cooling water consumption, reduce outer defeated coal gas and carry water and macromole hydrocarbon quantity, improve gas wet depriving hydrogen sulphide efficient, reduce circulation heat-carrying gas working cycle compression ratio etc.;
5. improving working pressure utilizes the interior pressure energy of solid when producing a large amount of high pressure raw coal gas, to reduce the work of expansion that the gas making product is made; Reduced ineffective power consumption, the 5th effect is can reduce gas making process energy consumption promptly to reduce the oxygen consumption, reduce fuel consumption;
6. improving working pressure utilizes the interior pressure energy of solid when producing a large amount of high pressure raw coal gas, to reduce the work of expansion that the gas making product is made; Reduced ineffective power consumption; The 6th effect is to reduce coal charge dehydration water evaporated volume ratio of expansion, reduction coal charge gasification oil gas volume expansion ratio; That reduces coal charge breaks, reduces the powder productive rate, has created certain favourable condition for the fine coal distillation process especially;
7. improve working pressure, pressure combustion chamber unit volume intensity of combustion is with proportional enhancing, and the 7th effect is to widen fuel source, has created certain favourable condition for realization " with low (the rudimentary energy) generation high (high energy) " promptly realizes fuel energy-saving.
Core feature of the present invention is to utilize the characteristics that have a large amount of gases in the internally heated retort oven, shortens intermolecular distance and then obtains required effect through increasing pressure.The correlative thermal conductivity is listed below.
The coke powder thermal conductivity, when 100 ℃ of temperature be 0.164 kilocalorie/when rice (℃).
Table 1 weak caking coal thermal conductivity
| t，℃ | λ，J/(cm·s·℃) | λ, kilocalorie/when rice (℃) |
| 50 | 0.00306750 | 0.2638 |
| 100 | 0.00314000 | 0.2700 |
| 150 | 0.00321750 | 0.2767 |
| 200 | 0.00330000 | 0.2838 |
| 250 | 0.00338750 | 0.2913 |
| 300 | 0.00348000 | 0.2992 |
| 350 | 0.00357750 | 0.3076 |
| 400 | 0.00368000 | 0.3164 |
| 450 | 0.00378750 | 0.3257 |
| 500 | 0.00390000 | 0.3353 |
| 550 | 0.00401750 | 0.3455 |
| 600 | 0.00414000 | 0.3560 |
| 650 | 0.00426750 | 0.3669 |
| 700 | 0.00440000 | 0.3783 |
| 750 | 0.00453750 | 0.3902 |
| 800 | 0.00468000 | 0.4024 |
| 850 | 0.00482750 | 0.4151 |
| 900 | 0.00498000 | 0.4282 |
The thermal conductivity of gaseous fraction in table 2 coal gas, kilocalorie/when rice (℃)
| Temperature, ℃ | H 2 | CO | N 2 | CO 2 | H 2O | CH 4 |
| 0 | 0.148 | 0.0200 | 0.0208 | 0.0125 | 0.0258 | |
| 100 | 0.189 | 0.0259 | 0.0269 | 0.0192 | 0.0212 | 0.0384 |
| 200 | 0.227 | 0.0314 | 0.0322 | 0.0259 | 0.0286 | 0.0534 |
| 400 | 0.299 | 0.0417 | 0.0418 | 0.0392 | 0.0477 | 0.0880 |
| 600 | 0.367 | 0.0513 | 0.0498 | 0.0534 | 0.0705 | 0.1240 |
| 800 | 0.454 | 0.0603 | 0.0569 | 0.0658 | ||
| 1000 | 0.547 | 0.0693 | 0.0635 | 0.0790 |
The present invention brings the useful range of the raising working pressure of favourable heat-transfer effect to have higher limit; Be that the working pressure of gas phase heat transfer rate when being equal to or greater than solid heat transfer speed is this operation upper limit; For concrete coal charge; Need test determination, can certainly calculate probable ranges through Theoretical Calculation.But the raising working pressure utilizes the favourable working pressure scope of living high pressure raw coal gas of the interior pressure energy volume production of solid thereby reduction gas making process energy consumption much larger than the aforementioned pressure scope; But receive the restriction that equipment (mainly being Gas-making Furnace) cost raises and increases with pressure; Because gaseous tension can calculate by pressure ratio KP substantially; But the increase ratio of equipment manufacturing cost is greater than this ratio KP, and one of them principal element is that the volume of solid materials and liquid material dwindles very few with the increase of pressure.
Because internally heated retort oven gas-operated pressure of the present invention is higher than normal pressure or far above normal pressure, therefore, the present invention uses the reinforced material of coal charge lock system, charcoal material to go out furnace charge lock system, pressure combustion chamber, withstand voltage gas retort, dry cooling system etc. usually.Facilities such as circulation heat-carrying gas sparger, gas fume of combustion chamber sparger also possibly arranged in coking chamber inside.
Known coal charge pressurization gas-making process has kinds of processes such as water coal slurry pressure gasification Gas-making Furnace gas-making process, polynary slurry Gas-making Furnace gas-making process, liquid bed gas-making process and air flow bed gas-making process; Yet said process uses minimum coal charge or the charcoal material of granularity; Do not produce coke product; Said technology can't realize the object of the invention, and operating process exists different greatly with the present invention.Known coal charge pressurization gas-making process has broken coal moving-bed pressure gasification process, yet said process does not produce coke product, and said technology can't realize the object of the invention, and operating process exists different greatly with the present invention.
The method of the invention is not appeared in the newspapers.
First purpose of the present invention is to propose a kind of pressurization internally heated coal carbonization gas-making process; The gas retort working pressure is higher than or far above normal pressure; Can significantly dwindle gas retort os volume, save and to take up an area of, reduce investment outlay, shorten the destructive distillation time, be beneficial to and reduce pyrolysis temperature, be beneficial to and improve the tar yield, be beneficial to and improve quality of coke tar, be beneficial to and realize dry type breath Jiao, be beneficial to fine coal retort process operation etc., have efficient dry distillation of coal characteristics.
Second purpose of the present invention is to propose a kind of pressurization internally heated coal carbonization gas-making process that produces high pressure gas; Raw gas pressure is higher than or far above normal pressure; Can obtain the defeated gas pressure of high pressure outward and can, save coal gas process of cooling water consumption, reduce outer defeated coal gas and carry water and macromole hydrocarbon quantity, improve gas wet depriving hydrogen sulphide efficient, reduce circulation heat-carrying gas working cycle compression ratio etc., have the advantages that coal gas impurity is few, the tar yield high, the water consumption is low, pressure potential is high.
The 3rd purpose of the present invention is to propose a kind of pressurization internally heated coal carbonization gas-making process, reduces the retort process energy consumption, reduces powder product amount.
The 4th purpose of the present invention is to propose a kind of pressurization internally heated coal carbonization gas-making process, uses the reinforced material of coal charge lock system, charcoal material to go out furnace charge lock system, pressure combustion chamber, withstand voltage gas retort, dry cooling system etc.
The 5th purpose of the present invention is to propose a kind of pressurization internally heated coal carbonization gas-making process, has the production efficiency height, consumes low overall merit.
The result that the present invention pursues is: high dry distillation of coal production capacity, high tar yield, high energy yield, low energy consumption, low construction investment, wideer raw material sources scope.
Summary of the invention
A kind of pressurization internally heated coal carbonization of the present invention gas-making process comprises following steps: gas making partly comprises charring furnace and coking chamber heat-carrying component internal circulation system, and charring furnace comprises the coking chamber of coal and the fuel gas combustion chamber that possibly exist; In coking chamber, according to the advance route of coal charge, being divided into first section is that coal preheating section (or claim gas cooling section), second section are that coal carbonization section, the 3rd section are charcoal cooling section (or claiming gas preheating section); In the 3rd section zone, the first via gas and the two sections process material contact heat-exchangings that comprise coking chamber heat-carrying component reclaim and become three sections process gas after its heats heat up, and three sections process material leave three sections zones; In second section zone; Three sections process gas and the gas fume of combustion chamber that possibly exist; Carry out gas-solid with one section process material and directly contact the charing effect that takes place, two sections process material leave second section zone and get into the 3rd section zone, and two sections process gas leave second section zone and get into first section zone; In first section zone, after transmitting the heat cooling and sneak into one section generation gas with the outside certainly coal charge Contact Heating coal charge that adds, two sections process gas become one section product gas (raw gas), and become one section process material after coal charge heats up and get into second section zone; Raw gas is discharged charring furnace; The charcoal product is discharged charring furnace; In raw gas refrigerated separation part, the raw gas that charring furnace is discharged in cooling and separation obtains from ring coal gas, coal tar, contains tar sewage; At least a portion is returned coking chamber as coking chamber heat-carrying component based on the gas stream of raw gas, constitutes gas making part coking chamber heat-carrying component internal recycle; It is characterized in that: gas phase operation pressure P V is a high pressure in the charring furnace.
Gas phase operation pressure P V in the charring furnace of the present invention: greater than 0.18MPa (absolute pressure) or greater than 0.20MPa (absolute pressure) or greater than 0.30MPa (absolute pressure) or greater than 0.40MPa (absolute pressure) or greater than 0.50MPa (absolute pressure) or greater than 1.00MPa (absolute pressure) or greater than 1.50MPa (absolute pressure) or greater than 2.0MPa (absolute pressure) or be 0.40～3.0MPa (absolute pressure).
Charring furnace coking chamber coal carbonization section service temperature of the present invention is 500～900 ℃ or is 550～800 ℃ or is 600～750 ℃ or is 600～700 ℃.
The present invention is in order to reduce quantity of circulating cooling water; In raw gas refrigerated separation part; Raw gas sprays behind the direct cooling step through the air-cooler cooling step through water; Generally raw gas is cooled to 60～20 ℃ through the air-cooler cooling step after spraying direct cooling step postcooling to 65～95 ℃ through water, after raw gas sprays direct cooling step postcooling to 70～90 ℃ through water generally speaking, is cooled to 50～35 ℃ through the air-cooler cooling step.
When the present invention is applied to blue charcoal and produces; Operational condition is generally: in coking chamber; Said coal charge is non-caking coal or weakly caking coal; The charcoal product is semicoke (being blue charcoal), and coal carbonization section service temperature is 550～850 ℃, and the long-pending flow rate of circulation heat-carrying gas is 150～450 SCM/cubic meters with the ratio of coal charge volumetric flow rate.
When the present invention is applied to blue charcoal and produces; Operational condition is generally: in coking chamber; Said coal charge is non-caking coal or weakly caking coal; The charcoal product is semicoke (being blue charcoal), and coal carbonization section service temperature is 550～800 ℃, and the long-pending flow rate of circulation heat-carrying gas is 200～400 SCM/cubic meters with the ratio of coal charge volumetric flow rate.
When the present invention is applied to blue charcoal and produces; Operational condition preferably is: in coking chamber; Said coal charge is non-caking coal or weakly caking coal; The charcoal product is semicoke (being blue charcoal), and coal carbonization section service temperature is 600～700 ℃, and the long-pending flow rate of circulation heat-carrying gas is 250～350 SCM/cubic meters with the ratio of coal charge volumetric flow rate.
The present invention uses the reinforced material of coal charge lock system, withstand voltage gas retort, pressure combustion chamber, charcoal material to go out furnace charge lock system, dry cooling system usually.
The used coal charge of coking chamber of the present invention is non-caking coal or weakly caking coal, and granularity is: 25～100mm or 10～40mm or 3～15mm or 1～5mm or 0.5～3mm.
Embodiment
Below describe the present invention in detail.
Pressure of the present invention refers to absolute pressure.
Gas component concentrations of the present invention when not specializing, is volumetric concentration.
This paper is the process modification of example explanation the present invention to the blue charcoal device of internal heat type with the blue charcoal device technique of large-scale upright furnace (600,000 t/a upright furnace) of Anshan Research Inst. of Heat Energy, China Iron & Steel Group and Huang gang, Hubei metallurgical furnace Ltd of Huaxing.Yet this can not limit Application Areas of the present invention.
The technical process of this section internally heated coal carbonization gas making part that is used to describe common process (or be referred to as " carbonization process and charring furnace perolene cyclic part ").The coal gas of upright furnace heating usefulness is through the further cooling of gas purification workshop section and the coal gas after purifying.The air of upright furnace heating usefulness is supplied with by air-blaster pressurization back; Coal gas and air mix through burner, in horizontal quirk internal combustion, and the high-temp waste gas that burning produces; Get into coking chamber through equally distributed air inlet port on the coking chamber side wall, utilize the heat of high-temp waste gas that coal charge is carried out charing.Burner is established two-layer up and down, and heating is main with lower floor, and safety effect is mainly played on the upper strata.
At first pack in the coal groove of furnace roof topmost by being equipped with qualified shove charge coal that coal workshop section ships, pack in the coking chamber through putting coal cock and auxiliary coal bin again.Continuously to the coking chamber coal.The lump coal that adds coking chamber moves from top to bottom, sends into the high-temperature gas counter current contact of coking chamber with the combustion chamber.The top of coking chamber is preheating section, and lump coal is heated to about 350～550 ℃ in this section; Lump coal continues to move down the retort section that gets into the coking chamber middle part, and lump coal is heated to pyrolysis temperature as 550～900 ℃ through this section, and is blue charcoal by charing; When blue charcoal passes through the cooling section of coking chamber bottom; Being passed into this section perolene circulating gas is cooled to 180～250 ℃ and becomes warm charcoal; The temperature charcoal gets into and to put out charcoal section (quenching section) and be cooled to about 80 ℃ by coke quenching water, after putting burnt machine and discharge continuously with scraper plate, falls on the dryer through chute.The gas mixture (raw gas) of the coal gas that produces when the high-temp waste gas of the coal gas that coal charge produces in carbonization process, combustion chamber entering coking chamber and cooling coke; Get into pneumatic trough through upcast, bridge tube; Gas mixture about 150～200 ℃ (raw gas) after the cyclic ammonia water sprinkling is cooled to 80～90 ℃, gets into washing tower along inhaling gas pipe through gas-liquid separator in bridge tube and pneumatic trough; Ammoniacal liquor is by washing tower top spray, and the ammoniacal liquor that the bottom has tar gets into heat ring tank; Coal gas is got into by direct-cooled washing tower bottom, and top is discharged and got into the indirect cooler that uses recirculated water usually; Coal gas is cooled to 40～45 ℃ by 80 ℃.Coal gas gets into the Root's blower pressurization behind straight a, water cooler, behind electrical tar precipitator, use as purifying coal gas.In common process, the part raw gas is directly sent the upright furnace combustion chamber back to and is acted as a fuel, and a large amount of raw gass are directly sent upright furnace back to and used as circulation heat-carrying gas.From the tar ammonia that gas-liquid separator and direct-cooled washing tower come out, flow into heat ring tank standing separation tar certainly, tar dewaters with being pumped to the tar storage tank, and thermal cycling ammoniacal liquor is with being pumped to the furnace roof effuser and direct-cooled washing tower recycles.From the tar ammonia that indirect cooler comes out, flow into cold ring tank standing separation tar certainly, tar is with being pumped to the dehydration of tar storage tank, and cold cyclic ammonia water recycles with being pumped to inter cooler.Tar (moisture＜4%) after the dehydration of tar storage tank is delivered to tar job shop or entrucking outward transport.
Below describe characteristic of the present invention in detail.
A kind of pressurization internally heated coal carbonization of the present invention gas-making process comprises following steps: gas making partly comprises charring furnace and coking chamber heat-carrying component internal circulation system, and charring furnace comprises the coking chamber of coal and the fuel gas combustion chamber that possibly exist; In coking chamber, according to the advance route of coal charge, being divided into first section is that coal preheating section (or claim gas cooling section), second section are that coal carbonization section, the 3rd section are charcoal cooling section (or claiming gas preheating section); In the 3rd section zone, the first via gas and the two sections process material contact heat-exchangings that comprise coking chamber heat-carrying component reclaim and become three sections process gas after its heats heat up, and three sections process material leave three sections zones; In second section zone; Three sections process gas and the gas fume of combustion chamber that possibly exist; Carry out gas-solid with one section process material and directly contact the charing effect that takes place, two sections process material leave second section zone and get into the 3rd section zone, and two sections process gas leave second section zone and get into first section zone; In first section zone, after transmitting the heat cooling and sneak into one section generation gas with the outside certainly coal charge Contact Heating coal charge that adds, two sections process gas become one section product gas (raw gas), and become one section process material after coal charge heats up and get into second section zone; Raw gas is discharged charring furnace; The charcoal product is discharged charring furnace; In raw gas refrigerated separation part, the raw gas that charring furnace is discharged in cooling and separation obtains from ring coal gas, coal tar, contains tar sewage; At least a portion is returned coking chamber as coking chamber heat-carrying component based on the gas stream of raw gas, constitutes gas making part coking chamber heat-carrying component internal recycle; It is characterized in that: gas phase operation pressure P V is a high pressure in the charring furnace.
Gas phase operation pressure P V in the charring furnace of the present invention: greater than 0.18MPa (absolute pressure) or greater than 0.20MPa (absolute pressure) or greater than 0.30MPa (absolute pressure) or greater than 0.40MPa (absolute pressure) or greater than 0.50MPa (absolute pressure) or greater than 1.00MPa (absolute pressure) or greater than 1.50MPa (absolute pressure) or greater than 2.0MPa (absolute pressure) or be 0.40～3.0MPa (absolute pressure).
Charring furnace coking chamber coal carbonization section service temperature of the present invention is 500～900 ℃ or is 550～800 ℃ or is 600～750 ℃ or is 600～700 ℃.
The present invention is in order to reduce quantity of circulating cooling water; In raw gas refrigerated separation part; Raw gas sprays behind the direct cooling step through the air-cooler cooling step through water; Generally raw gas is cooled to 60～20 ℃ through the air-cooler cooling step after spraying direct cooling step postcooling to 65～95 ℃ through water, after raw gas sprays direct cooling step postcooling to 70～90 ℃ through water generally speaking, is cooled to 50～35 ℃ through the air-cooler cooling step.
When the present invention is applied to blue charcoal and produces; Operational condition is generally: in coking chamber; Said coal charge is non-caking coal or weakly caking coal; The charcoal product is semicoke (being blue charcoal), and coal carbonization section service temperature is 550～850 ℃, and the long-pending flow rate of circulation heat-carrying gas is 150～450 SCM/cubic meters with the ratio of coal charge volumetric flow rate.
When the present invention is applied to blue charcoal and produces; Operational condition is generally: in coking chamber; Said coal charge is non-caking coal or weakly caking coal; The charcoal product is semicoke (being blue charcoal), and coal carbonization section service temperature is 550～800 ℃, and the long-pending flow rate of circulation heat-carrying gas is 200～400 SCM/cubic meters with the ratio of coal charge volumetric flow rate.
When the present invention is applied to blue charcoal and produces; Operational condition preferably is: in coking chamber; Said coal charge is non-caking coal or weakly caking coal; The charcoal product is semicoke (being blue charcoal), and coal carbonization section service temperature is 600～700 ℃, and the long-pending flow rate of circulation heat-carrying gas is 250～350 SCM/cubic meters with the ratio of coal charge volumetric flow rate.
Because internally heated retort oven gas-operated pressure of the present invention is higher than normal pressure or far above normal pressure, therefore, the present invention uses the reinforced material of coal charge lock system, withstand voltage gas retort, pressure combustion chamber, charcoal material to go out furnace charge lock system, dry cooling system usually.
The used coal charge of coking chamber of the present invention is non-caking coal or weakly caking coal, and granularity is: 25～100mm or 10～40mm or 3～15mm or 1～5mm or 0.5～3mm.
The algorithm of roll-over V0 in the coal charge that the reinforced material of coal charge of the present invention lock system uses is below described:
1. the coal gas displacement step before the charging: accomplish that roll-over V0 contains inflammable gas (raw gas) in the coal charge of discharging step, steps of exhausting can be set create conditions for the air of displacement coal charge absorption.All be under the closing condition at discharge valve 02, feed valve 01, open breather valve 0K2 roll-over V0 in coal charge and feed indifferent gas (like CO
2Gas), punching press is closed breather valve 0K2 after accomplishing; Opening breather valve 0K1 then makes in the coal charge among the roll-over V0 gas get into the safety dumping point to accomplish the bleed step such as torch or gas holder, close breather valve 0K1 then; Above-mentioned steps can repeat repeatedly; Open feed valve 01 then and coal charge is discharged into or waits for reinforced, close charging valve 01 after addition step finishes, wait for the subsequent action instruction.
2. the air displacement step after the charging: accomplish that roll-over V0 contains the air compsn that coal charge is brought in the coal charge of addition step, the quantity that gas displacement step reduces the nitrogen of bringing gas retort into, argon gas, oxygen etc. can be set.All be under the closing condition at discharge valve 02, feed valve 01, open gas ventilation valve 0K2 roll-over V0 in coal charge and feed displacement gas (like CO
2Gas), punching press is closed breather valve 0K2 after accomplishing; Open breather valve 0K3 then, gaseous emission to securing point is accomplished displacement bleed step such as characteristics airborne release mouth, displacement step can be carried out repeatedly, reach requirement after, close gas ventilation valve 0K3, wait for the subsequent action instruction.
3. to coking chamber discharging step: roll-over V0 in the coal charge; Regularly close feed valve 01; Opening breather valve 0K2 makes displacement gas gas get into that roll-over V0 accomplishes the step of boosting in the coal charge; Open discharge valve 02 then coal charge is discharged into gas retort coking chamber L101 top, the discharging step is closed discharge valve 22 after finishing, is closed breather valve 0K2, waits for the subsequent action instruction.
In the course of normal operation, in any moment, valve 01 can not be in opening state simultaneously with valve 02.
Roll-over V0 operation index comprises material level, pressure, temperature etc. in the coal charge.
The present invention has following typically used, but is not limited thereto:
1. the publication number with inventor's proposition is a kind of with CO of CN102199433A
2Use for the coal carbonization technology combination of combustion processes temperature control component, form the efficient dry distillation of coal and high pressure material gas preparation technology;
2. the publication number with inventor's proposition is a kind of with CO of CN102199433A
2Use for the coal carbonization technology combination of combustion processes temperature control component, form high pressure high performance fuel gas production technique;
3. the application number that proposes with the inventor is that the internally heated coal carbonization multi-production process combination of a kind of coproduction high methane gas of 201110172569.2 is used, and forms the technology of taking product with methane as the leading factor, and Sweet natural gas is defeated outward;
4. the application number that proposes with the inventor is that a kind of usefulness of 201110221627.6 contains H
2, N
2Polycomponent gas prepares the method combination of specific composition hydrogen and nitrogen gas to be used, and forms the technology of taking product with the synthetic ammonia series product as the leading factor;
5. the publication number with inventor's proposition is the treatment process combination use that one kind of CN102198991A contains coal tar sewage, forms raw gas conversion and sewage gas making gas system methyl alcohol integral process;
6. the publication number with inventor's proposition is the treatment process combination use that one kind of CN102198991A contains coal tar sewage, forms maximum gas production capacity integral process;
7. the publication number that proposes with the inventor is that a kind of coal system coke installation dry coke quenching method combination of 201110086594.9 is used, and forms the efficient low-consume optimization internally heated coal carbonization technology of use dry coke quenching technology.
Compare with conventional non-pressure process internally heated coal carbonization gas-making process, major advantage of the present invention is seen table 3.
Table 3 pressurization internally heated coal carbonization gas-making process advantage summary sheet
Compare with conventional non-pressure process internally heated coal carbonization technology, the present invention is more convenient for implementing dry quenching(of coke) technology, and its advantage is: can adopt high working pressure, system bulk is little, reduced investment, energy consumption are low.
The charcoal material goes out furnace charge lock system, dry cooling system, and the publication number that sees also inventor's proposition is a kind of coal system coke installation dry coke quenching method of 201110086594.9.
When the present invention was applied to the fine coal destructive distillation, facilities such as circulation heat-carrying gas sparger, gas fume of combustion chamber sparger also possibly arranged in coking chamber inside.The structure formation of the two can be identical or different.
The circulation heat-carrying gas sparger of coking chamber internal layout; Be positioned at solid bed of material bottom; Can be arranged in charring furnace on vertical 1,2 of solid materials direct of travels or a plurality of gas distributions cross section, each arranges the parallel pipe that many parallel pipes or ring pipe or many subsidiary vertical gas distributionbranch pipes can be set on gas distribution cross section or the ring pipes of many subsidiary vertical gas distributionbranch pipes.Lay out pore on the above-mentioned gas distribution pipe, production well can be an any direction, but the recommendation outgassing direction of gas distribution pipe production well is vertical with the solid materials direct of travel or forward, the outgassing direction of not recommending is reverse with the solid materials direct of travel.
The circulation heat-carrying gas sparger of coking chamber internal layout; Can be arranged on 1,2 or a plurality of gas distributions cross section; Each arranges that the gas distribution pipe that is provided with on the gas distribution cross section constitutes 1,2 or a plurality of independent gas supplies unit usually, and each independent gas supply unit is provided with 1,2 or a plurality of circulation heat-carrying gas inlet mouth.
Reference examples
" is that raw material is at the special-purpose blue charcoal of vertical retort refining iron alloy with non-caking coal or weakly caking coal lump coal " technology and equipment of Anshan Thermal Energy Inst. of China Steel Group; Employing is suitable coal source with China Datong District, the geographic coal in refreshing mansion; Be employed in the blue charcoal of the interior refining of vertical retort and refine blue charcoal and by-product raw gas and middle coalite tar, this technology has the general feature of similar blue charcoal technology: be the main heat-carrying component of combustion processes with nitrogen.In the representative data of this reference examples; Unit scale is 3,600,000 tons/year of blue charcoal production capacities; Be made up of 6 600,000 tons/year blue charcoal unit, year is 7920 hours/year (330 days date manufactured meter per year) when going into operation, and is raw material with Yulin city Shenmu County's coal; Coal gas production capacity 6 * 10.3 hundred million mark cubic meter/years, tar production capacity 6 * 60,000 ton/year.This reference examples, gas retort stove inner bottom part gas phase operation pressure is 0.15MPa (absolute pressure), the purification gas pressure is 0.1065MPa (absolute pressure).
1. typical feedstock coal character
With the report of Shenmu County's coal analysis, design requires as follows the ature of coal of upright furnace with coal:
It is the lump coal of 25～80mm that the used feed coal of the blue charcoal of internal thermal upright carbonization furnace production requires, and project is the screening of feed coal with due regard to, and daily requirement coal amount is 6 * 3000t/d, i.e. 6 * 125t/h.
One group of typical feed coal ature of coal survey report of table 4
| Sequence number | Interventions Requested | Check data | The employing standard |
| 1 | Total water (%) | 10.8 | GB/T211-1996 |
| 2 | Analysis moisture (%) | 3.74 | GB/T212-2001 |
| 3 | Ash content (%) | 4.92 | GB/T212-2001 |
| 4 | Volatile matter (%) | 34.40 | GB/T212-2001 |
| 5 | Characteristic of char residue (1-8) | 2 | GB/T212-2001 |
| 6 | Fixed carbon (%) | 60.04 | GB/T212-2001 |
| 7 | Full sulphur (%) | 0.21 | GB/T214-1996 |
| 8 | Hydrogen richness (%) | 3.69 | GB/T476-2001 |
2. the blue charcoal of major product: have low ash, low-sulfur, hang down excellent properties such as aluminium, hyperergy, high specific resistance; Can be widely used in industries such as iron alloy, calcium carbide, synthetic ammonia and blast furnace blowing, field such as civilian; Can partly replace coking coal, gasification briquette and smokeless piece etc., realize resource rational utilization;
Blue carbon yield 6 * 600,000 ton/year, wherein:
Specification 1: >=5mm, 6 * 520,000 ton/year, specification 2:＜5mm, 6 * 80,000 ton/year
Blue charcoal＞5mm grade can supply domestic ferroalloy works, calcium carbide factory, fertilizer plant and outlet;
Coke powder＜5mm can supply Iron And Steel Plant's blast furnace blowing to use or power plant for self-supply uses.
3. one of sub product coalite tar, character better and be rich in lower boiling phenol, it is the petroleum products surrogate that non-phenol distillate is easy to hydrocracking, residual oil (or claiming coal-tar pitch) can coking hot-work be coke and coking distillate (making hydrogenating materials).Coal tar output 6 * 60,000 ton/year, its main character is seen table 3.
The main character of table 5 shenfu coal upright furnace coking gained coal tar
The main character of table 6 dehydrated coal tar
| Sample | Density g/cm 3 | Ash content % | Moisture % | Viscosity E 80 | Remarks |
| Coal tar | ～1.05 | 0.02～0.2 | ≤4 | 2～10 |
The results of elemental analyses (%) of table 7 shenfu coal upright furnace coking gained coal tar
| Sample | C | H | N | 0 | S | The H/C atomic ratio | Remarks |
| Shenfu coal tar 1# | 86.28 | 8.31 | 1.11 | 3.86 | 0.36 | 1.16 | |
| Shenfu coal tar 2# | 86.03 | 8.45 | 1.14 | 3.93 | 0.45 | 1.18 |
4. by-product gas: part is personal, and part is outer to be supplied.
Table 8 reference examples raw gas purposes
| Sequence number | Name of material | Nm 3/a | Ten thousand Nm 3/h |
| 1 | The coal gas ultimate production | 6×1.03×10 9 | 6×13.0050 |
| 2 | Purposes 1: upright furnace internal recycle | 6×5.15×10 8 | 6×6.5025 |
| 3 | Purposes 2: the outer confession | 6×5.15×10 8 | 6×6.5025 |
Table 9 reference examples logistics data (single series)
Personal coal gas, a part is used as coking chamber heat-carrying component, a part is as the combustion chamber fuel of charring furnace, have part not through the combustion chamber but through the coal gas of the cold charcoal section of coking chamber in the thermopositive reaction of coking chamber charing section generation part chemical oxidation.The residual gas that charring furnace produces, a part supply coked waste water burning usefulness, and be most of outer defeated with being used as fuel and hydrogen feedstock.
5. single series project content: the type of furnace is selected ZNZL3082 type internal thermal upright stove for use, and stove group scale is 8 * 8 holes, and corresponding auxiliary facility has fully coal, sieve storage Jiao, charing, bulging cold, WWT and public utility etc.
6. production workshop section
The technological process of production comprises coal workshop section, charing workshop section, the burnt workshop section of sieve fortune, the cold workshop section of drum and WWT workshop section fully.
Charing workshop section: vertical retort takes many grate furnaces body to arrange.The type of furnace is chosen as ZNZL3082 type internal thermal upright carbonization furnace.Furnace binding and characteristics:
● this type of furnace has enlarged heat size than general upright carbonization furnace, and coking chamber length is increased to 3000～3500mm by 2100mm, and height is increased to 8200mm by 7000mm, thereby favourable condition is provided for the stable and high yields of upright carbonization furnace.
● increased the volume of combustion chamber and suitably increased air inlet port quantity, coal gas and air are fully burnt in the combustion chamber, hot waste gas evenly gets into coking chamber, thereby prevents to hang degrading of slag and inlet mouth effectively.
● coking chamber both sides, every hole are respectively equipped with two-layer totally 4 independently horizontal quirks (combustion chamber) up and down, and the temperature distribution that can regulate every hole coking chamber is neatly guaranteed whole stove uniform in quality, stable.
● the steam quenching is carried out in blue charcoal quenching earlier, carries out the water quenching then.Hydrogen richness makes blue carbonaceous amount increase simultaneously in the main raising coal gas.
● blue charcoal is discharged from upright furnace by the scraper plate machine, carries out classification on the sieve apparatus through being transported to behind the drying machine drying, and the blue charcoal after the classification is transported to storage Jiao Chang respectively by conveyor drive.
The technical process of gas purification workshop section: the coal gas → pneumatic trough → gas-liquid separator → direct-cooled one section tower → direct-cooled two sections towers → recirculated water indirect cooler → gas fan → electrical tar precipitator → part coal gas internal recycle that comes out from charring furnace returns outside charring furnace, the part coal gas and supplies the user.
WWT workshop section: industrial sewage adopts burning disposal, can accomplish the industrial sewage zero release.
7. produce the adjusting characteristics
Existing blue charcoal Design of device thought is to be that major product, coal tar and raw gas are sub product with blue charcoal, and the main project of production control is into the up to standard and raw gas requisite quality of charcoal speed carbonaceous amount up to standard, blue, and (calorific value is between 1600～2400KCAL/Nm
3).
Embodiment one
Based on reference examples, be 0.45MPa (absolute pressure) with gas retort gas phase operation pressure design, be 3 times of reference examples; The purification gas pressure is 0.38MPa (absolute pressure), is 3.57 times of reference examples.Present embodiment uses the reinforced material of coal charge lock system, withstand voltage gas retort, pressure combustion chamber, charcoal material to go out furnace charge lock system, dry cooling system.
Embodiment one gas retort gas phase operation pressure increases the advantageous effects of bringing and sees table 10.
Embodiment two
Based on embodiment one, be 0.9MPa (absolute pressure) with gas retort gas-operated pressure design, be 6 times of reference examples; The purification gas pressure is 0.82MPa (absolute pressure), is 7.70 times of reference examples; Compare with embodiment 1, projects number of effects is more huge.
Embodiment two gas retort gas phase operation pressure increase the advantageous effects of bringing and see table 11.
Embodiment three
Based on embodiment two, with the inventor propose " one kind of CN102199433A is with CO
2Coal carbonization technology for combustion processes temperature control component " the combination use, produce poor nitrogen coal gas.
Lift 3 embodiment although this paper just lists, the effect that it shows is present in equally and anyly is suitable for adopting in the coal carbonization process of the present invention.
Table 10 embodiment one gas retort gas phase operation pressure increases the advantageous effects of bringing
Table 11 embodiment two gas retort gas phase operation pressure increase the advantageous effects of bringing
Claims (26)
1. pressurization internally heated coal carbonization gas-making process, comprise following steps: gas making partly comprises charring furnace and coking chamber heat-carrying component internal circulation system, charring furnace comprises the coking chamber of coal and the fuel gas combustion chamber that possibly exist; In coking chamber, according to the advance route of coal charge, being divided into first section is that coal preheating section (or claim gas cooling section), second section are that coal carbonization section, the 3rd section are charcoal cooling section (or claiming gas preheating section); In the 3rd section zone, the first via gas and the two sections process material contact heat-exchangings that comprise coking chamber heat-carrying component reclaim and become three sections process gas after its heats heat up, and three sections process material leave three sections zones; In second section zone; Three sections process gas and the gas fume of combustion chamber that possibly exist; Carry out gas-solid with one section process material and directly contact the charing effect that takes place, two sections process material leave second section zone and get into the 3rd section zone, and two sections process gas leave second section zone and get into first section zone; In first section zone, after transmitting the heat cooling and sneak into one section generation gas with the outside certainly coal charge Contact Heating coal charge that adds, two sections process gas become one section product gas (raw gas), and become one section process material after coal charge heats up and get into second section zone; Raw gas is discharged charring furnace; The charcoal product is discharged charring furnace; In raw gas refrigerated separation part, the raw gas that charring furnace is discharged in cooling and separation obtains from ring coal gas, coal tar, contains tar sewage; At least a portion is returned coking chamber as coking chamber heat-carrying component based on the gas stream of raw gas, constitutes gas making part coking chamber heat-carrying component internal recycle; It is characterized in that: gas phase operation pressure P V is a high pressure in the charring furnace.
2. method according to claim 1 is characterized in that:
Gas phase operation pressure P V is greater than 0.18MPa (absolute pressure) in the charring furnace.
3. method according to claim 1 is characterized in that:
Gas phase operation pressure P V is greater than 0.20MPa (absolute pressure) in the charring furnace.
4. method according to claim 1 is characterized in that:
Gas phase operation pressure P V is greater than 0.30MPa (absolute pressure) in the charring furnace.
5. method according to claim 1 is characterized in that:
Gas phase operation pressure P V is greater than 0.40MPa (absolute pressure) in the charring furnace.
6. method according to claim 1 is characterized in that:
Gas phase operation pressure P V is greater than 0.50MPa (absolute pressure) in the charring furnace.
7. method according to claim 1 is characterized in that:
Gas phase operation pressure P V is greater than 1.00MPa (absolute pressure) in the charring furnace.
8. method according to claim 1 is characterized in that:
Gas phase operation pressure P V is greater than 1.50MPa (absolute pressure) in the charring furnace.
9. method according to claim 1 is characterized in that:
Gas phase operation pressure P V is greater than 2.0MPa (absolute pressure) in the charring furnace.
10. method according to claim 1 is characterized in that:
Gas phase operation pressure P V is 0.40～3.0MPa (absolute pressure) in the charring furnace.
11., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 described methods:
Coking chamber coal carbonization section service temperature is 500～900 ℃.
12. method according to claim 11 is characterized in that:
Coking chamber coal carbonization section service temperature is 550～800 ℃.
13. method according to claim 11 is characterized in that:
Coking chamber coal carbonization section service temperature is 600～750 ℃.
14. method according to claim 11 is characterized in that:
Coking chamber coal carbonization section service temperature is 600～700 ℃.
15. method according to claim 11 is characterized in that:
In raw gas refrigerated separation part, after raw gas sprays direct cooling step through water, through the air-cooler cooling step.
16. method according to claim 11 is characterized in that:
In raw gas refrigerated separation part, raw gas is cooled to 60～20 ℃ through the air-cooler cooling step after spraying direct cooling step postcooling to 65～95 ℃ through water.
17. method according to claim 11 is characterized in that:
In raw gas refrigerated separation part, raw gas is cooled to 50～35 ℃ through the air-cooler cooling step after spraying direct cooling step postcooling to 70～90 ℃ through water.
18. method according to claim 11 is characterized in that:
In coking chamber, said coal charge is non-caking coal or weakly caking coal, and the charcoal product is semicoke (being blue charcoal), and coal carbonization section service temperature is 550～850 ℃, and the long-pending flow rate of circulation heat-carrying gas is 150～450 SCM/cubic meters with the ratio of coal charge volumetric flow rate.
19. method according to claim 11 is characterized in that:
In coking chamber, said coal charge is non-caking coal or weakly caking coal, and the charcoal product is semicoke (being blue charcoal), and coal carbonization section service temperature is 550～800 ℃, and the long-pending flow rate of circulation heat-carrying gas is 200～400 SCM/cubic meters with the ratio of coal charge volumetric flow rate.
20. method according to claim 11 is characterized in that:
In coking chamber, said coal charge is non-caking coal or weakly caking coal, and the charcoal product is semicoke (being blue charcoal), and coal carbonization section service temperature is 600～700 ℃, and the long-pending flow rate of circulation heat-carrying gas is 250～350 SCM/cubic meters with the ratio of coal charge volumetric flow rate.
21. method according to claim 11 is characterized in that:
Use the reinforced material of coal charge lock system, withstand voltage gas retort, pressure combustion chamber, charcoal material to go out furnace charge lock system, dry cooling system.
22. method according to claim 11 is characterized in that:
In coking chamber, said coal charge is non-caking coal or weakly caking coal, and granularity is 25～100mm.
23. method according to claim 11 is characterized in that:
In coking chamber, said coal charge is non-caking coal or weakly caking coal, and granularity is 10～40mm.
24. method according to claim 11 is characterized in that:
In coking chamber, said coal charge is non-caking coal or weakly caking coal, and granularity is 3～15mm.
25. method according to claim 11 is characterized in that:
In coking chamber, said coal charge is non-caking coal or weakly caking coal, and granularity is 1～5mm.
26. method according to claim 11 is characterized in that:
In coking chamber, said coal charge is non-caking coal or weakly caking coal, and granularity is 0.5～3mm.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110330984A (en) * | 2019-07-25 | 2019-10-15 | 内蒙古万众炜业科技环保股份公司 | The cracking sub-prime that a kind of small particle coal prepares moulded coal utilizes production technology |
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| GB1184944A (en) * | 1966-04-08 | 1970-03-18 | Basse Sambre Sa Etudes Rech S | Improvements in and relating to the Continuous Production ofCode |
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| CN110330984A (en) * | 2019-07-25 | 2019-10-15 | 内蒙古万众炜业科技环保股份公司 | The cracking sub-prime that a kind of small particle coal prepares moulded coal utilizes production technology |
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