CN101880540A - Low-coalification degree pulverized coal pyrolysis method and product prepared through the same - Google Patents
Low-coalification degree pulverized coal pyrolysis method and product prepared through the same Download PDFInfo
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Abstract
The invention relates to a low-coalification degree pulverized coal pyrolysis method and a product prepared through the same. The method comprises the following four steps: low-coalification degree pulverized coal pre-drying, low-coalification degree pulverized coal pyrolysis reaction, gas cooling and tar recovery, and hot semi-coke cooling. The method is applicable to heat treatment to low-coalification degree pulverized coal resources so as to obtain high-quality pyrolysis gas and tar products, wherein the gas contains low inert component content, tar contains high light component content and low dust content, and semi-coke products with wide purposes are obtained. The process method is characterized by high comprehensive utilization rate of energy, large amount of treated material, low device investment, easy industrialization realization, environmental friendliness and the like while improving the raw material utilization efficiency.
Description
[technical field]
The present invention relates to a kind of fine coal heat treatment technics field, more specifically, the present invention relates to a kind of low degree of coalification pulverized coal pyrolysis method, and the product that adopts this method to obtain.
[background technology]
In the energy structure ratio of China, coal resources reserves and consumption account for more than 70% of primary energy source total amount, and along with the further shortage of resources such as oil, Sweet natural gas, coal will become the main body of China's energy structure in a very long time.In the coal resources total amount of China, low rank coal (as brown coal, long-flame coal, non-caking coal, weakly caking coal) proven reserve account for more than 30%, mainly be distributed in ground such as Inner Mongol, Shaanxi, Yunnan, can a large amount of fine coal of generation in exploitation and transportation, this fine coal resource exists little, the easy oxidation and spontaneous combustion of granularity, water content height, efficiency of utilization is low, non-caked or defective such as bad adhesion.How to utilize this class resource to improving the coal resources in China utilising efficiency, promote local economic development, realizing that Sustainable development has very important significance high-efficiency cleaning.
The pyrolysis of coal as the basis of whole Coal Chemical Industry, is the effective way of the young coal resource of present processing treatment, also is the main path that obtains chemical industry basic raw material (as triphen, triphenol, naphthalene) etc.Pyrolytic technique to low rank coal can be divided into internal heat type and external-heat technology according to heat-supplying mode at present.
The internal heat type technology mainly contains the strange three sections stoves in SJ low-temperature pyrolysis side stove (ZL200610111733.8), Shandong, the new method retorting technique of DG based on helical mixer (ZL94228582.4), TOSCOAL retorting technique, Lu Qi-Rule (L-R) retorting technique of Shenmu County, northern Shensi three river Coal Chemical Industry company limiteds and at present based on the retorting technique of circulating fluidized bed.Though the internal heat type retorting technique has heat transfer efficiency height and the fast advantage of heating rate, but the outstanding problem that exists is that quality product is low, for example inert component content height, semicoke ash content significantly increase in coal gas and tar dustiness height, the coal gas, thereby cause being difficult to high value added utilization, especially gas internal heat type technology has also increased the load of subsequent product purification and separation system.
The external-heat technology mainly contains the multi-stage rotary pyrolytic process (ZL92104624.3) of Coal Mining Research Institute at present, the particulate weakly caking coal low-temperature pyrolysis technology (ZL200610012400.X) of people such as Zhang Ji's space exploitation etc., but have all that rate of heat transfer and integrated heat efficiency are low, product coal gas and tar yield and the low inferior problem of quality, and in tar recovery and coal gas cooling, semicoke cooling and dedusting process, produced and contained phenol dust-laden waste water and dust-laden exhaust gas in a large number, environment has been caused great pollution.
The present invention is the energy structure ratio situation according to China, efficiently utilize difficulty big at low degree of coalification fine coal, the traditional treatment method integrated heat efficiency is low, and coal gas and tar yield and quality are low, and the problem that environmental pollution is serious proposes on the basis of carrying out big quantity research and test., pyrolytic reaction predrying, coal gas cooling and tar reclaims, the semicoke refrigerating work procedure reaches the low degree of coalification fine coal of efficient utilization, the productive rate that improves coal gas and tar and character, raising thermo-efficiency and reduce the purpose of environmental pollution by fine coal.
[summary of the invention]
[wanting the technical solution problem]
The objective of the invention is to propose a kind of low degree of coalification pulverized coal pyrolysis method.
The objective of the invention is a kind of product that adopts aforesaid method to obtain.
[technical scheme]
The objective of the invention is to realize the efficient utilization of low degree of coalification fine coal resource, at first low degree of coalification fine coal carries out pre-dried, moisture content in the former low degree of coalification fine coal is reduced to below the 5.0 weight %, avoid large quantity of moisture to bring the problem that pyrolysis oven causes the pyrolysis oven thermal load to increase into, effectively utilized used heat simultaneously; Dried low degree of coalification fine coal carries out pyrolytic reaction in the external-heat pyrolysis oven, obtain high-quality coal gas and tar products, obtain broad-spectrum semicoke product simultaneously, this product can be used for for example wet method gasification, blast furnace blowing, technical fields such as Industrial Stoves, production silicon carbide, metallurgical reductive agent.The mode that coal gas, tar and the water that pyrolysis produces combines with direct Quench by indirect cooling realizes that coal gas cooling and tar reclaim, and is guaranteeing to have significantly reduced wastewater discharge under the prerequisite that tar high efficiente callback and coal gas are effectively lowered the temperature; And hot semicoke that pyrolysis produces and heat-eliminating medium carry out the purpose that indirect heat exchange reaches the semicoke cooling, and heat-eliminating medium recycle fully can not pollute environment.
The present invention is achieved through the following technical solutions.
The present invention relates to a kind of low degree of coalification pulverized coal pyrolysis method.This method comprises the steps:
A, low degree of coalification fine coal predrying:
Described low degree of coalification fine coal is delivered in the drying oven 1 by pipeline 12, carried out indirect heat exchange 20-70 minute with the drying medium that is transported to described drying oven 1 by pipeline 22 down at drying temperature 120-200 ℃, thereby the moisture content of described fine coal reaches below the 5.0 weight %, dry fine coal is discharged from described drying oven 1 by pipeline 15, the water vapor that drying process obtains and the heat exchange drying medium respectively by pipeline 13 and 14 from described drying oven 1 discharge;
The pyrolysis of B, low degree of coalification fine coal:
The dry fine coal that allows above-mentioned steps A obtain is delivered to pyrolysis oven 2 by pipeline 15 and was carried out pyrolytic reaction 30-400 minute for 300 ℃-650 ℃ in temperature, obtain containing the pyrolysis gaseous product and the semicoke of coal gas, water and tar, described pyrolysis gaseous product is discharged from described pyrolysis oven 2 by pipeline 16, and described semicoke is discharged from described pyrolysis oven 2 by pipeline 17; Described fine coal carries out the required heat of pyrolytic reaction fuel that to be the air supplied with by pipeline 39 supply with pipeline 38 is at the heat indirect supply of described pyrolysis reactor furnace 2 internal combustion generation;
C, the condensation of pyrolysis gaseous product and tar reclaim:
The pyrolysis gaseous product that contains coal gas, water and tar that above-mentioned steps B obtains delivers to condenser system 4 by pipeline 16 and heat-eliminating medium wherein carries out the adverse current indirect heat exchange, the temperature of this pyrolysis gaseous product is reduced to is lower than below 180 ℃, discharge described condenser system 4 by pipeline 27 again; What discharge from described condenser system 4 bottoms is the tar liquid product, is discharged by pipeline 28.
Directly contact with 0.2-5 weight % ammoniacal liquor in gas scrubber 8 from the pyrolysis gaseous product of described condenser system 4,, remove the tar of in above-mentioned pyrolysis gaseous product, carrying secretly simultaneously so reduce the temperature of pyrolysis gaseous product from ammonia vessel 10; The water that contains tar of discharging from described gas scrubber 8 bottoms is delivered to the tar clarifying tank 9 by pipeline 29 again, the clarification back is the tar that contains water from described tar clarifying tank 9 tops by pipeline 30 ejectas, the water of discharging from described tar clarifying tank 9 bottoms does not contain tar, this water major part is delivered to gas scrubber 8 after sending into ammonia vessel 10 and fresh ammoniacal liquor from pipeline 33 mixes by pipeline 32, and remainder water effluxes by pipeline 31;
Deliver to micro-tar trap 11 from the pyrolysis gaseous product that described scrubber 8 is discharged by pipeline 35, make the tar content in the pyrolysis gaseous product be reduced to 60mg/m
3Below obtain a kind of raw gas, it is discharged from described micro-tar trap 11 tops, wherein a part of raw gas is discharged by pipeline 37 and is sent outside, another part raw gas again by pipeline 37,38 with the urceolus 54 of delivering to described pyrolysis oven 2 by the air of pipeline 39 or combustion chamber (83); What discharge from described micro-tar trap 11 bottoms is that the liquid form mixt that contains micro-tar and water of condensation is discharged by pipeline 36;
The cooling of D, pyrolysis product semicoke:
The semicoke that above-mentioned steps B obtains is by pipeline 17 or deliver in the cool furnace 3 and cool, perhaps directly efflux, lower the temperature when cooling when delivering to described cool furnace 3, cooled off indirectly 30-90 minute with the heat-eliminating medium that enters described cool furnace 3 by pipeline 41 therein, the temperature of semicoke is reduced to below 200 ℃ discharges from described cool furnace 3, the heat-eliminating medium after the heat exchange is discharged from described cool furnace 3 by pipeline 42.
A preferred embodiment of the invention, described low rank coal is selected from brown coal, long-flame coal, non-caking coal or weakly caking coal; Described fine coal is the powdery coal of largest particle diameter less than 15mm and median size 1-10mm.
According to another kind of preferred implementation of the present invention, described drying oven 1 is a kind of horizontal sleeve formula structure, by inner core 46, urceolus 44 and hinge dragon 45 3 parts are formed, described coal dust enters in the inner core 46 of described drying oven 1, the inlet 48 of drying medium from described drying oven 1 enters described drying oven 1 urceolus 44, the heat of drying medium passes to low degree of coalification fine coal in described inner core 46 by the wall between described inner core 46 and the urceolus 44, low degree of coalification fine coal in the described inner core 46 moves to Way out under the drive of described hinge dragon 45, fine coal is heated in moving process and carries out drying and dehydrating, the water vapor that in drying process, produces and the heat exchange drying medium discharge from having exported 49 and 50 respectively, the low degree of coalification fine coal of exsiccant is discharged from exporting 51.
According to another kind of preferred implementation of the present invention, described drying medium is waste heat flue gas or the steam that combustion exhaust that comes out from described pyrolysis oven 2 or other fuel combustions that replenish by pipeline 21 produce.
According to another kind of preferred implementation of the present invention, described pyrolysis oven 2 is external-heat reactors, it is the horizontal sleeve formula structure that there is driving member in a kind of portion within it, by inner core 53, urceolus 54, hinge dragon 52 3 parts are formed, described inner core 53 is passages of low degree of coalification fine coal, described urceolus 54 is fuel combustion chambers, fuel enters described urceolus combustion chamber 54 heat release of burning with air by a plurality of inlets 56, its heat passes to fine coal in the described inner core 53 by the wall between described inner core 53 and the urceolus 54, the hinge dragon 52 that slow rotation is arranged in the described inner core 53, fine coal moves fine coal generation pyrolytic reaction in moving process under the drive of described hinge dragon 52; Perhaps
It is a kind of vertical external-heating pyrolysis oven, by pyrolytic reaction chamber 75, regenerator 76,83 4 parts in cooling room 77 and combustion chamber are formed, described pyrolysis chamber 75 is pyrolytic reaction chambers of low degree of coalification fine coal, described regenerator 76 is regenerator of air and fuel gas, described cooling room 77 is cooling rooms that pyrolysis generates hot semicoke, the equal combuster 83 in the front and back of described pyrolysis chamber 75 provides heat indirectly to described pyrolysis chamber 75, dry coal 80 enters described pyrolysis chamber 75 by entering the mouth, the gaseous product that pyrolysis produces is discharged by a plurality of outlets 79, the solid product semicoke is pushed focusing mechanism and sends in the cooling room 77, by the rare gas element from inlet 78 semicoke is cooled to discharge by outlet 82 after temperature is lower than 200 degrees centigrade, cooling exhaust is discharged by outlet 81.
According to another kind of preferred implementation of the present invention, described fuel comprises raw gas that pyrolysis is self-produced and from other fuel of pipeline 40, other fuel is selected from the liquid fuel of Sweet natural gas, liquefied petroleum gas (LPG), town gas, industrial synthetic gas, industrial tail gas and heavy oil, residual oil and other waste oil.
According to another kind of preferred implementation of the present invention, described condenser system 4 is composed in series by a plurality of telescoping indirect condensers 5, the interior pipe 6 of described condenser 5 is pyrolysis gaseous product passage, outer tube 7 is a cooling medium pass, the pyrolysis gaseous product enters from the interior pipe 6 of described indirect condenser 5, heat-eliminating medium enters from the outer tube 7 of described indirect condenser 5, pyrolysis gaseous product and heat-eliminating medium carry out indirect heat exchange by the wall of pipe 6 in described, flow out described condenser system 4 by pipeline 27 when making the temperature of pyrolysis gaseous product be reduced to below 180 ℃, the tar that cools down is discharged by pipeline 28 and is collected.
According to another kind of preferred implementation of the present invention, described cool furnace 3 is telescopic external-heat structure, by inner core 64, urceolus 65 and hinge dragon 63 3 parts are formed, described inner core 64 is a pyrolysis product semicoke passage, described urceolus 65 is the passage of heat-eliminating medium, there are cooling water system 71 and 73 in the two ends of described cool furnace 3, on the described hinge dragon 63 cooling water inlet 72 and outlet 74 are arranged, described hinge dragon 63 is by driven by motor 64 slowly rotations in inner core, semicoke in the described inner core 64 exports 70 directions to semicoke and moves under the drive of described hinge dragon 63, semicoke and heat-eliminating medium carry out indirect heat exchange by the wall between described inner core 64 and the urceolus 65 in the process that moves.
According to another kind of preferred implementation of the present invention, described heat-eliminating medium is selected from recirculated water, de-salted water, fresh water, air or rare gas element.
According to another kind of preferred implementation of the present invention, the product that adopts the method for the invention to obtain, caloric power of gas is greater than 20MJ/m
3, methane content is greater than 30 volume % in the coal gas; In the product tar less than 350 ℃ cut content greater than 50 weight %.
Below in conjunction with Figure of description the inventive method is described in more detail.
Accompanying drawing 1 is a technical route synoptic diagram of the present invention.
A, low degree of coalification fine coal predrying:
Described low degree of coalification fine coal is delivered to drying oven 1 by pipeline 12, carried out indirect heat exchange 20-70 minute with the drying medium that is transported to described drying oven 1 by pipeline 22 down at drying temperature 120-200 ℃, thereby the moisture content of described fine coal reaches below the 5.0 weight %, dried fine coal is discharged from described drying oven 1 by pipeline 15, the water vapor that drying process obtains and the heat exchange drying medium respectively by pipeline 13 and pipeline 14 from described drying oven 1 discharge;
At first be the low degree of coalification fine coal of 15mm with maximum particle size, as brown coal, long-flame coal, non-caking coal or weakly caking coal are delivered to the drying oven 1 of preheating by pipeline 12, provide the drying medium of heat to enter described drying oven 1 from different positions by pipeline 22 to described drying oven 1, carry out indirect heat exchange with the low degree of coalification fine coal in the described drying oven 1, the flow of drying medium can be determined according to the temperature of water vapor in the temperature of dried low degree of coalification fine coal in the pipeline 15 and the pipeline 13, make the temperature of low degree of coalification fine coal reach 120-200 ℃ through super-dry, and water-content is reduced to 5.0 weight % when following, discharge from the outlet 51 of described drying oven 1 by pipeline 15, the outlet 49 of the water vapor that obtains in the drying process along pipeline 13 from described drying oven 1 discharged, recycling after condensation, the outlet 50 of the drying medium of heat exchange along pipeline 14 from described drying oven 1 discharged.
In the present invention, described low degree of coalification fine coal should be appreciated that it is the low rank coal of maximum particle diameter less than 15mm, median size 1-10mm, and described low rank coal is meant brown coal, long-flame coal, non-caking coal and weakly caking coal.
Described drying medium is combustion exhaust that comes out from pyrolysis oven 2 or the useless flue gas of other burning or the steam that replenishes by pipeline (21), and preferably combustion exhaust or the steam that comes out from pyrolysis oven 2 more preferably is the combustion product gases from pyrolysis oven 2.
The structural representation of the drying oven 1 that the inventive method is used as shown in Figure 2.Overall structure types is the external-heat horizontal kiln, form by inner core 46, urceolus 44 and the dragon of the hinge in described inner core 46 45 3 parts, described inner core 46 is passages of low degree of coalification fine coal, urceolus 44 is passages of drying medium, described hinge dragon 45 rotates by driven by motor, 47 imports for low degree of coalification fine coal, the inlet 48 of drying medium is set to a plurality of on described drying oven 1,49 and 50 is respectively the water vapor that produces in the drying process and the outlet of heat exchange after drying medium, and 51 is the outlet of the low degree of coalification fine coal in dry back.
Drying medium enters described urceolus 44 by a plurality of drying medium inlets 48 on the described drying oven 1, and by the wall between described inner core 46 and the urceolus 44 to described inner core 46 heat supplies, and described hinge dragon 45 is slowly rotated under the drive of motor, low subsequently degree of coalification fine coal enters in the described inner core 46 by fine coal inlet 47, and under the drive of described hinge dragon 45, export 51 directions and move to described low degree of coalification fine coal, in moving process with described urceolus 44 in drying medium carry out indirect heat exchange, and dehydrate, the water vapor that is produced is discharged by outlet 49, the heat exchange drying medium is discharged by outlet 50, the low degree of coalification fine coal of exsiccant is discharged by outlet 51, the low residence time of degree of coalification fine coal in described drying oven 1 inner core 46 is 20-90 minute, specifically be to regulate by the rotating speed of regulating described hinge dragon 45, the rotating speed of described hinge dragon 45 is 0.1-10 rev/min, preferably 0.2-6 rev/min, more preferably 0.2-2.5 rev/min.
The pyrolysis of B, low degree of coalification fine coal:
The dry fine coal that allows above-mentioned steps A obtain is delivered to pyrolysis oven 2 by pipeline 15 and was carried out pyrolytic reaction 30-400 minute for 300 ℃-650 ℃ in temperature, obtain containing the pyrolysis gaseous product and the semicoke of coal gas, water and tar, described pyrolysis gaseous product is discharged from described pyrolysis oven 2 by pipeline 16, and described semicoke is discharged from described pyrolysis oven by pipeline 17; It is the air supplied with by pipeline 39 with the heat indirect supply that is produced in described pyrolysis reactor furnace 2 internal combustion by the fuel of the supply of pipeline 38 that described fine coal carries out the required heat of pyrolytic reaction;
The low degree of coalification fine coal of discharging along pipeline 15 through super-dry relies on self gravitation to enter pyrolysis oven 2, carries out pyrolytic reaction in this pyrolysis oven 2.The low temperature of reaction of degree of coalification fine coal in described pyrolysis oven 2 can be determined by the add-on of fuel and air, the gaseous product of pyrolytic reaction is the mixture that contains coal gas, tar and water, solid product is a semicoke, delivering to subsequent handling after described gaseous product is discharged by pipeline 16 handles, described solid product is discharged from described pyrolysis oven 2 by pipeline 17, after the waste gas that burning produces is discharged by pipeline 18, perhaps turn back to described drying oven 1 dry low degree of coalification fine coal, perhaps deliver to and produce the vapor recovery heat by pipeline 20 along pipeline 19.
The needed heat of the pyrolytic reaction of fine coal generation in the present invention be by the air of sending here by pipeline 39 and the fuel that provides by pipeline 38 at described pyrolysis oven 2 internal combustion indirect supplies, described fuel comprises from the pyrolysis raw gas of pipeline 37 with from other fuel of pipeline 40.Described other fuel should be appreciated that it is inflammable gas and flammable liquid fuel, and described inflammable gas for example is liquefied petroleum gas (LPG), Sweet natural gas, town gas or industrial synthetic gas, and flammable liquid fuel for example is heavy oil, residual oil or waste oil.
Described fuel is pyrolysis coal gas and inflammable gas preferably, more preferably is pyrolysis coal gas and day hot gas.
The pyrolysis oven 2 that the inventive method is used has two kinds of structure formations.First kind of pyrolysis oven 2 synoptic diagram as shown in Figure 3.Overall structure is horizontal external-heat pyrolysis stove, it is by inner core 53, urceolus 54 and the dragon of the hinge in described inner core 53 52 3 parts are formed, described inner core 53 is the low degree of coalification fine coal passage in dry back, and described urceolus 54 is the combustion channels of fuel and air, the 55th, and the inlet of the low degree of coalification fine coal in dry back, the 56th, fuel and gas inlet, the 57th, the outlet of pyrolysis gaseous product, the 58th, the useless exhanst gas outlet of burning, the 59th, the outlet of pyrolysis solid product semicoke.For the sealing member of described pyrolysis oven 2 is lowered the temperature, be provided with cooling system 60 at the two ends of described pyrolysis oven 2; For prolonging the work-ing life of described hinge dragon 52, be provided with circulating cooling medium import 61 and outlet 62 in the termination of described hinge dragon 52.
Fuel and air enter the urceolus 54 of described pyrolysis oven 2 by a plurality of inlets 56 of described first kind of pyrolysis oven 2, fuel and air burn in urceolus 54, the heat that is produced passes to inner core 53 by the wall between described inner core 53 and the urceolus 54, described hinge dragon 52 is slowly rotated in described inner core 53 under driven by motor, the low degree of coalification fine coal of drying is entered in the inner core 53 that is preheating to certain temperature by inlet 55, and under the drive of the hinge dragon 52 of constantly rotating, export 59 directions and move to semicoke, low degree of coalification fine coal absorbs the fuel combustion liberated heat by described wall in moving process, pyrolytic reaction takes place when reaching pyrolysis temperature, the gaseous product that pyrolysis produces is discharged from a plurality of pneumatic outlets 57, and the solid product semicoke is discharged from described inner core 53 by outlet 59, the useless flue gas that produces after fuel burns in described urceolus 54 is discharged by outlet 58, the recovery heat.The low degree of coalification fine coal of drying is 30-150 minute in the residence time of described pyrolysis oven 2, can regulate by the rotating speed of described hinge dragon 52 particularly, the rotating speed of described hinge dragon 52 is 0.1-8 rev/min, and preferably 0.1-5 rev/min more preferably is 0.1-2.5 rev/min.
For total energy approach efficient that improves first kind of pyrolysis oven 2 and the pyrolysis rate that improves low degree of coalification fine coal, its inner core 53 walls adopt thermal conductivity and the good material of wear resistance, make as silicon carbide, 321 stainless steels etc.; Urceolus 54 walls adopt the good material of heat-insulating property, and for example (clay brick etc.) are made; Described hinge dragon 52 is adopted the material that has than high-tensile in the time of 700 ℃, for example 430,431, ferritic steel such as 436L makes; For avoiding pyrogenous origin tar generation secondary reaction, a plurality of gaseous product outlets 57 can be set, for example 2-6 on described pyrolysis oven 2.
Second kind of pyrolysis oven 2 synoptic diagram that the inventive method is used as shown in Figure 4.It totally is vertical pyrolysis oven, mainly comprise pyrolysis chamber 75, regenerator 76, cooling room 77 and combustion chamber 83 4 parts, described pyrolysis chamber 75 is a dry coal generation pyrolytic reaction, described regenerator 76 is to fuel gas and preheating of air, described cooling room 77 is to the cooling of lowering the temperature of hot semicoke, described combustion chamber 83 is that fuel and air combustion heat release are to pyrolysis chamber's 75 indirect heatings, the 78th, the inert gas entrance that the cooling semicoke is used, the 80th, dry coal enters the inlet of described pyrolysis chamber 75, the 79th, a plurality of outlets of pyrolysis gaseous product, the 81st, discharge the waste gas outlet of described cooling room 77, the 82nd, the semicoke outlet of cooling back, heat passed to coal charge by the two side walls of described pyrolysis chamber 75 after the equal combuster 83 in the both sides of described pyrolysis chamber 75, fuel burnt in the combustion chamber.
Fuel and air enter the heat release of burning in the combustion chamber 83 of 75 both sides, pyrolysis chamber of described pyrolysis oven 2 after through regenerator 76 preheatings, the heat that produces passes to described pyrolysis chamber 75 by the wall between pyrolysis chamber and two side combusion chambers, 80 enter pyrolytic reactions take place in the pyrolysis chamber 75 by entering the mouth through exsiccant dry coal material subsequently, employing in the both sides, combustion chamber longitudinally the different positions method that sprays into air improve the heat-transfer effect of coal charge, the gaseous product that produces in the pyrolytic process is discharged by a plurality of outlets 79 on 75 tops, described pyrolysis chamber, the semicoke that pyrolysis produces is sent in the semicoke cooling room 77 by the lateral coke pushing in described pyrolysis chamber 75 mechanism, in described cooling room 77, hot semicoke is by the direct contact cooling of rare gas element from inlet 78, discharge by outlet 82 when making the temperature of hot semicoke be reduced to below 200 ℃, the cooling exhaust after the heat exchange is handled the back reusable edible through cooling after discharging by outlet 81.
For total energy approach efficient that improves second kind of pyrolysis oven 2 and the pyrolysis rate that improves low degree of coalification fine coal, pyrolysis chamber's 75 walls of described second kind of pyrolysis oven 2 adopt the good material of thermal conductivity, and for example (silicon carbide) is made; Combustion chamber 83 outside wall surface adopt the good material of heat-insulating property, and for example (clay brick, heat-insulation brick) made; Regenerator 76 adopt heat conductivilitys good material, for example (silica brick) is made; For avoiding pyrogenous origin tar generation secondary reaction, a plurality of gaseous product outlets 79 can be set, for example 2-6 on described pyrolysis oven (2).
The gaseous product that pyrolytic reaction generated contains incoagulability coal gas, condensability tar and pyrolysis water.In order to reclaim the high added value tar products and to obtain fine coal gas, the condensability material in the pyrolysis gaseous product need be carried out condensation separation.Described pyrolysis gaseous product enters condenser system 4 cooling of lowering the temperature by pipeline 16.Allow heat-eliminating medium and described gaseous product carry out indirect countercurrent flow, when the temperature of described gaseous product is reduced to below 180 ℃, discharge described cooling system 4 by pipeline 27, and enter gas scrubber 8, the liquid condensate of discharging from described condenser system 4 is a tar.
The pyrolysis gaseous product temperature of discharging from described condenser system 4 contains a large amount of tar light oil component and sour gas in time below 180 ℃, need recycle.Described pyrolysis gaseous product enters gas scrubber 8 by pipeline 27, directly contact with 0.2-5 weight % ammoniacal liquor and to carry out mass-and heat-transfer from pipeline 34, reduce the temperature of this pyrolysis gaseous product on the one hand, it is discharged by the pipeline 35 of gas scrubber 8 again, the water that contains tar light oil is on the other hand discharged from described gas scrubber 8 bottoms, removes most tar in this pyrolysis gaseous product.The water that contains tar light oil enters in the tar clarifying tank 9 by pipeline 29 clarifies separation.After the clarification, moisture tar light oil is discharged by pipeline 30 from the top of described tar clarifying tank 9, so that carry out further separating of tar and water, from the water that discharge described tar clarifying tank 9 bottoms, contain tar hardly, wherein most of water is sent in the ammonia vessel 10 with additional fresh ammoniacal liquor from pipeline 33 by pipeline 32 and is mixed, deliver to described gas scrubber 8 by pipeline 34 again, remainder water effluxes by pipeline 31.
From the pyrolysis gaseous product that the pipeline 35 of described gas scrubber 8 is discharged, also contain a spot of tar and pyrolysis water, for further reclaiming the high added value tar products, it is delivered in the micro-tar trap 11, in described micro-tar trap 11, tar content wherein can be reduced to 60mg/Nm
3Below, from described micro-tar trap 11, discharge by pipeline 37 as raw gas, wherein a part is delivered to described pyrolysis oven 2 through piping 38, remaining raw gas is as the outer confession of product, and micro-tar of catching in micro-tar trap 11 and pyrolysis water are sent to by pipeline 36 and carried out the further settlement separate of tar and water.
Described condenser system 4 is the indirect condensing system, and it is made up of a plurality of placed in-line indirect condensers 5, and preferably 1-5 indirect condenser 5 more preferably is 1-3 indirect condenser 5.Described indirect condenser 5 is the telescoping indirect condenser, is made of interior pipe 6 and outer tube 7, and described interior pipe 6 is passages of pyrolysis gaseous product, and described outer tube 7 is passages of heat-eliminating medium.
Heat-eliminating medium enters described outer tube 7 by pipeline 23 from the lower end of described condenser 5, the pyrolysis gaseous product enters described interior pipe 6 from the upper end of described condenser 5, pyrolysis gaseous product and heat-eliminating medium carry out the adverse current indirect heat exchange by the wall of pipe 6 in described, through overcooled pyrolysis gaseous product in described, manage 6 be discharged to by pipeline 25 after condenser, discharge after cooling by pipeline 24 from described outer tube 7 through the heat-eliminating medium of heat exchange and to recycle.
Described micro-tar trap 11 is present technique field micro-tar traps commonly used, and for example Xiangfan Jiuding Haotian Environmental Protection Equipment Co., Ltd. removes the micro-tar trap that tar (dirt) device, east, Anshan brightness environmental protection equipment company limited are sold with trade(brand)name honeycomb electrical tar precipitator with trade(brand)name electrical tar precipitator, Mount Everest Asia-Pacific, Hubei treating plant company limited with the trade(brand)name electricity.
The cooling of D, pyrolysis product semicoke:
The semicoke that above-mentioned steps B obtains is by pipeline 17 or deliver to cool furnace 3 cooling of lowering the temperature, perhaps directly efflux, lower the temperature when cooling when delivering to described cool furnace, hot semicoke cooled off 30-90 minute indirectly with the heat-eliminating medium that enters described cool furnace 3 by pipeline 41, the temperature of semicoke is reduced to below 200 ℃, discharges from described cool furnace 3 by pipeline 43 again; Heat-eliminating medium after the heat exchange is discharged from described cool furnace 3 by pipeline 42.
Fig. 5 is the structural representation of described cool furnace 3, described cool furnace 3 is horizontal external-heat cool furnace, by inner core 64, urceolus 65 and hinge dragon 63 are formed, described inner core 64 is passages of semicoke, described urceolus 65 is passages of heat-eliminating medium, described hinge dragon 63 is slowly being rotated in described inner core 64 under the drive of motor, the 66th, hot semicoke inlet, the 67th, gas-entrained relief outlet in semicoke, the 68th, described urceolus 65 heat-eliminating mediums outlet, the 69th, heat-eliminating medium inlet, the 70th, cooling semicoke relief outlet, 71 and 73 is the cooling water systems at described cool furnace 3 two ends, is used for sealing element is lowered the temperature; On described hinge dragon 63, be provided with cooling water inlet 72 and cooling water outlet 74,, play the effect of hot semicoke in the described inner core 64 of cooling simultaneously in order to prolong the work-ing life of described hinge dragon 63.
Heat-eliminating medium enters in the described urceolus 65 by the heat-eliminating medium inlet 69 of described cool furnace 3, hinge dragon 63 in the described inner core 64 takes place slowly to rotate under driven by motor, hot semicoke from described pyrolysis oven 2 enters in the described inner core 64 by semicoke inlet 66 subsequently, semicoke exports 70 Way outs to the cooling semicoke and moves under the drive of affiliated hinge dragon 63, hot semicoke in moving process with described urceolus 65 in the wall of heat-eliminating medium by described inner core 64 carry out the adverse current indirect heat exchange, the refrigerative semicoke is discharged as the product semicoke from described semicoke outlet 70, the heat-eliminating medium of process heat exchange is by exporting 68 discharges after recycle after the cooling in the described urceolus 65, and the cooling medium consumption in the described urceolus 65 is to determine according to the outlet semicoke temperature of the cooling semicoke outlet 70 of described cool furnace 3.The residence time of semicoke in described cool furnace 3 is to regulate by the rotating speed of the hinge dragon 63 in the described inner core 64, and the rotating speed of described hinge dragon is 0.1-12 rev/min, and preferably, this rotating speed is 0.1-10 rev/min, and more preferably, this rotating speed is 0.2-7 rev/min.
On meaning of the present invention, described heat-eliminating medium is construed as recirculated water, de-salted water, fresh water, air or rare gas element, and preferably recirculated water and de-salted water more preferably are recirculated water.
The invention still further relates to the product that adopts the inventive method to produce, for example adopt product raw gas calorific value that the present invention produces greater than 20MJ/m
3, methane content is greater than 30 volume % in the raw gas; In the product tar less than 350 ℃ cut content greater than 50 weight %.
Caloric power of gas is measured according to GB/T 12206-2006.
Methane content is measured according to GB/T 8984.1-1997.
[beneficial effect]
The present invention has following positively effect.
1. method proposed by the invention is to be raw material with low degree of coalification fine coal, efficiently utilizes the big problem of difficulty to have vital role to alleviating the fine coal that present coal mining process especially produces in the low rank coal recovery process.
2. the present invention has adopted the pyrolysis oven of two kinds of different structure forms, compares traditional internal heat type pyrolytic technique, effectively reduces inert component content and tar dustiness in the coal gas; Compare traditional external-heat pyrolysis technology, effectively improved heat transfer efficiency and pyrolytic reaction speed, alleviated high added value tar owing to can not in time discharge reactor and caused taking place secondary pyrolytic problem.
3. the present invention has adopted the predrying operation of low degree of coalification fine coal, adopted the external-heat horizontal kiln, compare directly pyrolytic technique of tradition, significantly reduced the water content of going into pyrolysis oven fine coal, alleviated and gone into pyrolysis oven fine coal and carry the erosion action of large quantity of moisture, alleviated the treatment capacity of subsequent condensation system simultaneously greatly the pyrolysis oven inner-wall material; Compare existing predrying technology, improved the comprehensive utilization ratio of energy and the drying rate of low degree of coalification fine coal.
4. the present invention proposes unique gas purification and tar and reclaim technology, on the basis that guarantees the high efficiente callback of high added value tar products, significantly reduce the quantity of wastewater effluent of conventional coke tar recovery technology, compare the directly tar recovery method of Quench of tradition, quantity of wastewater effluent can reduce more than 50%.
5. the present invention proposes pyrolysis char is carried out indirect refrigerative method, adopt horizontal external-heat cool furnace 3, compared with prior art, heat-eliminating medium can be realized complete recycle, can not produce a large amount of dust-laden waste water.
In a word, method of the present invention is the comprehensive high-efficiency utilization to low degree of coalification fine coal resource, promptly utilize the big low degree of coalification fine coal of a large amount of cheap intractabilities to produce high value-added product for raw material, to improving the coal resources utilization ratio of China, it is big to alleviate the traditional treatment method energy consumption, and the serious problem of environmental pollution is significant.
[description of drawings]
Fig. 1 is the process flow diagram of low degree of coalification pulverized coal pyrolysis technology
Fig. 2 is low degree of coalification fine coal drying oven structural representation
Fig. 3 is first a kind low degree of coalification pulverized coal pyrolysis stove synoptic diagram
Fig. 4 is second a kind low degree of coalification pulverized coal pyrolysis stove synoptic diagram
Fig. 5 is the cool furnace structural representation of pyrolysis char
Wherein, 1, drying oven; 2, pyrolysis oven; 3, cool furnace; 4, condenser system; 5, condenser; 6, interior pipe; 7, outer tube; 8, gas scrubber; 8 scrubbers; 9, tar clarifying tank; 10, ammonia vessel; 11, micro-tar trap; 12, pipeline; 13, pipeline; 14, pipeline; 15 pipelines; 16, pipeline; 17, pipeline; 18, pipeline; 19, pipeline; 20, pipeline; 21, pipeline; 22, pipeline; 23, pipeline; 24, pipeline; 25, pipeline; 27, pipeline; 28, pipeline; 29, pipeline; 30, pipeline; 31, pipeline; 32, pipeline; 33, pipeline; 34, pipeline; 35, pipeline; 36, pipeline; 37, pipeline; 38, pipeline; 39, pipeline; 40, pipeline; 41, pipeline; 42, pipeline; 43, pipeline; 44, urceolus; 45, hinge dragon; 46, inner core; 47, import; 48, inlet; 49, outlet; 50, outlet; 51, outlet; 52, hinge dragon; 53, inner core; 54, urceolus; 55, inlet; 56, inlet; 57, outlet; 58, outlet; 59, outlet; 60, cooling system; 61, import; 62, outlet; 63, hinge dragon; 64, inner core; 65, urceolus; 66, inlet; 67, outlet; 68, outlet; 69, inlet; 70, outlet; 71, cooling water system; 72, inlet; 73, cooling water system; 74, outlet; 75, pyrolysis chamber; 76, regenerator; 77, cooling room; 78, inlet; 79, outlet; 80, inlet; 81, outlet; 82, outlet; 83, combustion chamber.
[embodiment]
Embodiment 1:
Use the low degree of coalification fine coal in northern Shensi to implement the inventive method.
The maximum particle diameter of raw material fine coal is 12mm, and mean particle size is 8mm.Main coal analysis result is as described in the following table:
Table 1: coal analysis result
The concrete operations condition is as follows: pyrolysis oven 2 adopts structure formation one, join the low degree of coalification fine coal in northern Shensi in the inner core 46 of drying oven 1 by pipeline 12, make the fine coal in the inner core 46 be heated to 190 ℃ by the flow of regulating the combustion exhaust that pyrolysis oven 2 comes out described in the urceolus 44, make the low residence time of degree of coalification fine coal in drying oven reach 30 minutes by the rotating speed of regulating hinge dragon 45 in the inner core.
Dried fine coal flows out drying oven 1 by pipeline 15 with the flow of 1000kg/h and enters the inner core 53 of pyrolysis oven 2, from the pyrolysis raw gas of pipeline 38 with send into from the air of pipeline 39 in the urceolus 54 of pyrolysis oven 2 and burn, control pyrolysis rough coal tolerance flow makes the temperature of low degree of coalification fine coal in the inner core 53 reach 600 ℃ of temperature of reaction, the rotating speed of control hinge dragon 52 makes the low residence time of degree of coalification fine coal in inner core 53 reach 80 minutes, the raw gas that produces in the pyrolytic process, tar light oil, pyrolysis water and part are carried thin ash secretly and are pooled to pipeline 16 by a plurality of outlets 57, deliver to gaseous product cooling and tar recovery process with flow 352.71kg/h, concrete logistics composition sees Table 2, and the solid product semicoke that obtains relies on gravity to discharge from the outlet 59 of pyrolysis oven with the flow of 649.19kg/h.
Table 2: discharge pyrolysis oven 2 products behind the described pulverized coal pyrolysis and form
The gaseous product of discharging from pyrolysis oven 2 and carry thin ash secretly and enter condenser system 4 by pipeline 16, condenser system 4 is composed in series by three jacketed type indirect condensers 5, control flows into the cooling water inflow of indirect condensers at different levels respectively, make by gaseous product temperature after the pipeline 27 effusive condensations and be reduced to 150 ℃, flow is 274.80kg/h.The effluent of discharging condenser system 4 by pipeline 28 is tar, water and a small amount of coke powder, and total flux is 75.20kg/h.The gaseous product of discharging from condenser system 4 enters the gas scrubber 8, the weak ammonia that be 8% with concentration from pipeline 34, flow is 3050kg/h directly contacts Quench, most tar are discharged from gas scrubber 8 bottoms with the form of liquid state in the gaseous product in the process of Quench, temperature from gas scrubber 8 tops by pipeline 35 expellant gas products is 70 ℃, gas flow is 252.79kg/h, and its gaseous product is delivered in the micro-tar trap 11 of Xiangfan Jiuding Haotian Environmental Protection Equipment Co., Ltd. with the sale of trade(brand)name electrical tar precipitator.In this trace tar trap,, make the coal-tar middle oil content of raw gas of discharging micro-tar trap 11 be reduced to 60mg/Nm by pipeline 37 by regulating the voltage of micro-tar trap 11
3Below, wherein a part is burnt by the urceolus 54 that pipeline 38 returns pyrolysis oven 2, and all the other are sent outside.
The flow of the liquid condensate of discharging from gas scrubber 8 bottoms is 3072.00kg/h, wherein contain tar light oil, this condensate flow is fed in the tar clarifying tank 9 by pipeline 29, tar light oil and water flow out by pipeline 30 overflows from the top of tar clarifying tank 9 through the gravity separation of certain hour in tar clarifying tank 9.The bottom ejecta of tar clarifying tank 9 is washing water and a small amount of coke powder, wherein major part turns back to ammonia vessel 10 by pipeline 32, the amount of returning is 2500kg/h, and with deliver to gas scrubber 8 after fresh ammoniacal liquor from pipeline 33 mixes, be the ionic equilibrium of maintenance system, another small part effluxes by pipeline 31 as waste water.
The pyrolysis product semicoke temperature of discharging from pyrolysis oven 2 outlet at bottoms 59 is 600 ℃, enter in the inner core 64 of cool furnace 3 according to gravity by pipeline 17, the normal temperature recirculated cooling water enters in the urceolus 65 of cool furnace by pipeline 41, to make the residence time of hot semicoke in cool furnace be 80 minutes to the rotating speed of hinge dragon 63 in the control inner core 64, and the temperature that semicoke is discharged from the outlet 70 of cool furnace 3 is 180 ℃.
The product that adopts aforesaid method to obtain has raw gas and tar.Adopt the method for this specification sheets explanation to measure this raw gas calorific value 24MJ/m
3, methane content 36 volume % in the raw gas; Cut content less than 350 ℃ in the product tar is 51 weight %.
Embodiment 2: with Inner Mongol brown coal powder is that raw material is implemented the inventive method, and the maximum particle diameter of raw material is 10mm, and median size is 3mm, and main coal analysis data are as described in Table 3.
Table 3: Inner Mongol brown coal coal analysis data
The concrete operations condition is as follows: the method for this embodiment is identical with the process of embodiment 1, and just pyrolysis oven 2 adopts structure formation two, and the operating procedure condition of drying oven 1 and pyrolysis oven 2 is different, removes semicoke cool furnace 3, the raw material coal difference of use.Inner Mongol brown coal powder enters in the inner core 46 of drying oven 1 by pipeline 12, make the fine coal in the inner core 46 be heated to 140 ℃ by the flow of regulating drying medium in the urceolus 44, making the low residence time of degree of coalification fine coal in drying oven by the rotating speed of regulating hinge dragon 45 in the inner core is 85 minutes.
Dried fine coal flows out drying oven 1 by pipeline 15 with the flow of 500kg/h and enters in the pyrolysis chamber 75 based on the pyrolysis oven 2 of structure formation two, from the air of pipeline 39 with from the Sweet natural gas combustion chamber 83 internal combustion heat releases through entering 75 both sides, pyrolysis chamber after regenerator 76 preheatings respectively of pipeline 40, pyrolytic reaction when being heated to 400 ℃, the fine coal in the pyrolysis chamber 75 takes place, making the residence time of Inner Mongol brown coal powder in pyrolysis oven 2 is 320 minutes, the coal gas that pyrolysis produces, with the flow of 120.42kg/h degas cooling of attitude product and tar recovery process, concrete logistics is formed and is seen Table 5 by pipeline 16 for tar and water and micro-dust.The hot semicoke of solid product that produces pushes in the semicoke cooling room 77 rare gas element CO with coke pushing mechanism
278 enter in the described cooling room 77 hot semicoke is carried out direct contact cooling by entering the mouth, make the temperature of semicoke be reduced to 120 ℃ and discharge by outlet 82 as product, the rare gas element that absorbs heat is discharged pyrolysis ovens and is gone to reclaim the heat recycle by exporting 82.
Table 4: discharge the pyrolysis oven product behind the described pulverized coal pyrolysis and form
The gaseous product of discharging from second kind of pyrolysis oven 2 and carry the thin ash of trace secretly and enter condenser system 4 by pipeline 16, condenser system 4 is made up of a jacketed type indirect condenser 5, make the gaseous product temperature be reduced to 120 ℃ and flow out described condenser system with the flow of 99.92kg/h by pipeline 27, the effluent of discharging condenser system 4 by pipeline 28 is tar, water and a small amount of coke powder, and flow is 20.23kg/h.The gaseous product of discharging condenser system 4 enter in the gas scrubber 8 with concentration from pipeline 34 be 0.4%, weak ammonia that flow is 800kg/h directly contacts Quench, 35 expellant gas temperature are 70 ℃ from gas scrubber 8 tops along pipeline, gas flow is 71kg/h, and wherein tar content is 9.42g/Nm
3, by 11 pairs of gases of micro-tar trap further remove tar, the coal-tar middle oil content of gas of using micro-tar trap 11 is reduced to 60mg/Nm
3The Shi Zuowei raw gas is all sent outside.
The flow of the liquid condensate of discharging from gas scrubber 8 bottoms is 828.71kg/h, wherein contains tar light oil, and through gravity settling separation, tar light oil is from discharging from the upper end of tar clarifying tank by pipeline 30; Clarifying tank bottom ejecta is washing water, and is wherein most of by returning ammonia vessel 10 by pipeline 32, and all the other efflux as waste water by pipeline 31.
The product that adopts aforesaid method to obtain has raw gas and tar.Adopt the method for this specification sheets explanation to measure this raw gas calorific value 20MJ/m
3, methane content 30 volume % in the raw gas; In the product tar less than 350 ℃ cut content 58 weight %.
Claims (10)
1. one kind low degree of coalification pulverized coal pyrolysis method is characterized in that this method comprises the steps:
A, low degree of coalification fine coal predrying:
Described low degree of coalification fine coal is delivered to drying oven (1) by pipeline (12), carried out indirect heat exchange 20-70 minute with the drying medium that is transported to described drying oven (1) by pipeline (22) down at drying temperature 120-200 ℃, thereby the moisture content of described fine coal reaches below the 5.0 weight %, dry fine coal is discharged from described drying oven (1) by pipeline (15), the water vapor that drying process obtains and the heat exchange drying medium pass through pipeline (13) and pipeline (14) respectively and discharge from described drying oven (1);
The pyrolysis of B, low degree of coalification fine coal:
The dry fine coal that allows above-mentioned steps A obtain is delivered to pyrolysis oven (2) by pipeline (15) and was carried out pyrolytic reaction 30-400 minute for 300 ℃-650 ℃ in temperature, obtain containing the pyrolysis gaseous product and the semicoke of coal gas, water and tar, described pyrolysis gaseous product is discharged from described pyrolysis oven (2) by pipeline (16), and described semicoke is discharged from described pyrolysis oven by pipeline (17); It is the air supplied with by pipeline (39) with the heat indirect supply that is produced in described pyrolysis reactor furnace (2) internal combustion by the fuel of the supply of pipeline (38) that described fine coal carries out the required heat of pyrolytic reaction;
C, the condensation of pyrolysis gaseous product and tar reclaim:
The pyrolysis gaseous product that contains coal gas, water and tar that above-mentioned steps B obtains delivers to condenser system (4) by pipeline (16) and heat-eliminating medium wherein carries out the adverse current indirect heat exchange, the temperature of this pyrolysis gaseous product is reduced to is lower than 180 ℃, discharge described condenser system (4) by pipeline (27) again; What discharge from described condenser system (4) bottom is the tar liquid product, is discharged by pipeline (28);
Directly contact with 0.2-5 weight % ammoniacal liquor in gas scrubber (8) from the pyrolysis gaseous product of described pipeline (27), reduce the temperature of pyrolysis gaseous product, remove the tar of in above-mentioned pyrolysis gaseous product, carrying secretly simultaneously from ammonia vessel (10); Deliver to the tar clarifying tank (9) by pipeline (29) again from the water that contains tar that discharge described gas scrubber (8) bottom, the tar that contains water is discharged from described tar clarifying tank (9) top by pipeline (30) in the clarification back, the water of discharging from described tar clarifying tank (9) bottom does not contain tar, this water is delivered to gas scrubber (8) after sending into ammonia vessel (10) and fresh ammoniacal liquor from pipeline (33) mixes by pipeline (32), and remainder water effluxes by pipeline (31);
Deliver to micro-tar trap (11) from the pyrolysis gaseous product that described scrubber (8) is discharged by pipeline (35), make the tar content in the pyrolysis gaseous product be reduced to 60mg/m
3Below obtain a kind of raw gas, it is discharged from described micro-tar trap (11) top, wherein a part of raw gas is discharged by pipeline (37) and is sent outside, another part raw gas again by pipeline (37), (38) with the urceolus (54) of delivering to described pyrolysis oven (2) by the air of pipeline (39); The mixture that contains micro-tar and water of condensation of discharging from described micro-tar trap (11) bottom is discharged by pipeline (36) and is collected;
The cooling of D, pyrolysis product semicoke:
The semicoke that above-mentioned steps B obtains is by pipeline (17) or deliver to cool furnace (3) cooling of lowering the temperature, perhaps directly efflux, lower the temperature when cooling when delivering to described cool furnace (3), cooled off indirectly 30-90 minute with the heat-eliminating medium that enters described cool furnace (3) by pipeline (41) therein, the temperature of semicoke is reduced to below 200 ℃, discharges from described cool furnace (3) by pipeline (43) again; Heat-eliminating medium after the heat exchange is discharged from described cool furnace (3) by pipeline (42).
2. method according to claim 1 is characterized in that described low rank coal is selected from brown coal, long-flame coal, non-caking coal or weakly caking coal; Described fine coal is the powdery coal of largest particle diameter less than 15mm and median size 1-10mm.
3. method according to claim 1, it is characterized in that described drying oven (1) is a kind of horizontal sleeve formula structure, by inner core (46), urceolus (44) and hinge dragon (45) three parts are formed, described coal dust enters in the inner core (46) of described drying oven (1), the inlet (48) of drying medium from described drying oven (1) enters the described urceolus (44), the heat of drying medium passes to low degree of coalification fine coal in described inner core (46) by the wall between described inner core (46) and the urceolus (44), low degree of coalification fine coal in the described inner core (46) moves to Way out under the drive of described hinge dragon (45), fine coal is heated in moving process and carries out drying and dehydrating, the water vapor that in drying process, produces and the heat exchange drying medium discharge from outlet (49) and (50) respectively, the low degree of coalification fine coal of exsiccant is from outlet (51) discharge.
4. according to claim 1 or 3 described methods, it is characterized in that described drying medium is combustion exhaust that comes out from described pyrolysis oven (2) or waste heat flue gas or the steam that produces by other fuel combustion that pipeline (21) replenishes.
5. method according to claim 1, it is characterized in that described pyrolysis oven (2) is the external-heat reactor, it is the horizontal sleeve formula pyrolysis oven that there is driving member in a kind of portion within it, by inner core (53), urceolus (54), hinge dragon (52) three parts are formed, described inner core (53) is the passage of low degree of coalification fine coal, described urceolus (54) is a fuel channel, fuel and air enter described urceolus (54) heat release of burning by inlet (56), its heat passes to fine coal in the described inner core (53) by the wall between described inner core (53) and the urceolus (54), the hinge dragon (52) that slow rotation is arranged in the described inner core (53), fine coal moves under the drive of described hinge dragon (52), fine coal generation pyrolytic reaction in moving process; Perhaps
It is a kind of vertical external-heating pyrolysis oven, by pyrolysis chamber (75), regenerator (76), cooling room (77) and combustion chamber (83) four parts are formed, described pyrolysis chamber (75) is the pyrolytic reaction chamber of low degree of coalification fine coal, described regenerator (76) is the regenerator of air and fuel gas, described cooling room (77) is the cooling room that pyrolysis generates hot semicoke, the equal combusters in front and back (83) of described pyrolysis chamber (75) provide heat indirectly to described pyrolysis chamber (75), dry coal enters described pyrolysis chamber (75) by inlet (80), the gaseous product that pyrolysis produces is discharged by a plurality of outlets (79), the solid product semicoke is pushed focusing mechanism and sends in the cooling room (77), by the rare gas element from inlet (78) semicoke is cooled to discharge by outlet (82) after temperature is lower than 200 degrees centigrade, cooling exhaust is discharged by outlet (81).
6. method according to claim 1 or 5, it is characterized in that described fuel comprises that other fuel is selected from the liquid fuel of Sweet natural gas, liquefied petroleum gas (LPG), town gas, industrial synthetic gas, industrial tail gas and heavy oil, residual oil and other waste oil from the pyrolysis raw gas of pipeline (37) with from other fuel of pipeline (40).
7. method according to claim 1, it is characterized in that described condenser system (4) is composed in series by a plurality of indirect condensers (5), the interior pipe (6) of described condenser (5) is a pyrolysis gaseous product passage, outer tube (7) is a cooling medium pass, the pyrolysis gaseous product enters from the interior pipe (6) of described indirect condenser (5), heat-eliminating medium enters from the outer tube (7) of described indirect condenser (5), pyrolysis gaseous product and heat-eliminating medium carry out indirect heat exchange by the wall of pipe (6) in described, flow out described condenser system (4) by pipeline (27) when making the temperature of pyrolysis gaseous product be reduced to below 180 ℃, the tar that cools down is discharged by pipeline (28) and is collected.
8. method according to claim 1, it is characterized in that described cool furnace (3) is telescoping structure, by inner core (64), urceolus (65) and hinge dragon (63) three parts are formed, described inner core (64) is a pyrolysis product semicoke passage, described urceolus (65) is the passage of heat-eliminating medium, there are cooling water system (71) and (73) in the two ends of described cool furnace (3), cooling water inlet (72) and outlet (74) are arranged on the described hinge dragon (63), described hinge dragon (63) is slowly rotated in inner core by driven by motor, semicoke in the described inner core (64) moves to the semicoke Way out under the drive of described hinge dragon (63), and semicoke and heat-eliminating medium carry out indirect heat exchange by the wall between described inner core (64) and the urceolus (65) in the process that moves.
9. according to claim 1,6,7 or 8 described methods, it is characterized in that described heat-eliminating medium is selected from recirculated water, de-salted water, fresh water, air or rare gas element.
10. the product that obtains according to the described method of each claim among the claim 1-9 is characterized in that described product is raw gas and tar, and the raw gas calorific value is greater than 20MJ/m
3, methane content is greater than 30 volume % in the raw gas; In the product tar less than 350 ℃ cut content greater than 50 weight %.
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