CN103113905A - Composite pulverized coal destructive distillation device and method - Google Patents
Composite pulverized coal destructive distillation device and method Download PDFInfo
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- CN103113905A CN103113905A CN2013100696009A CN201310069600A CN103113905A CN 103113905 A CN103113905 A CN 103113905A CN 2013100696009 A CN2013100696009 A CN 2013100696009A CN 201310069600 A CN201310069600 A CN 201310069600A CN 103113905 A CN103113905 A CN 103113905A
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Abstract
The invention discloses a composite pulverized coal destructive distillation device and method and relates to a pulverized coal destructive distillation device and method so as to solve the problem that a hot carrier and pulverized coal are not ideally mixed in a mixer in the conventional coal fluidization destructive distillation technology. According to the device, one end of a hot carrier vertical pipe is connected with a raising pipe reactor, and the other end of the hot carrier vertical pipe is connected with a charring device; and one end of the raising pipe reactor is introduced with dry gas, and the other end of the raising pipe reactor is communicated with a destructive distillation reactor. The method comprises the following steps: 1, mixing high-temperature semicoke and pulverized coal in the raising pipe reactor, and carrying out a destructive distillation reaction; 2, inputting one part of high-temperature semicoke in the charring device into the raising pipe reactor through the hot carrier vertical pipe, and allowing the other part of high-temperature semicoke to enter a semicoke cooler through a discharging vertical pipe so as to be discharged into a semicoke storage tank after cooling; 3, reacting oil gas and semicoke coke in the destructive distillation reactor; and 4, returning the semicoke fine powder back to the destructive distillation reactor, allowing the semicoke fine powder to enter the charring device to serve as partially combusted semicoke through a semicoke conveying pipe, and raising the temperature to become a hot carrier after combustion. The device and the method are used for destructive distillation of pulverized coalwith the particle size of less than or equal to 5mm.
Description
Technical field
The present invention relates to a kind of coal dust destructive distillation device and method, be specifically related to a kind of coal dust composite dry distillation unit and method, belong to coal chemical technology.
Background technology
Due to the day by day deficient oil price with growing to even greater heights of world's crude resources, countries in the world are all in positive search for oil alternate resources, and utilizing the coal that is rich in organic matter to produce coal liquefaction petroleum replacing resource by retorting technique has become the important supplement scheme.China is the energy structure of the few oil of rich coal, and coal accounts for approximately 70% proportion.The dominant position of energy expenditure determines to realize the coal high-efficiency clean utilization, is to solve China's coal burning pollution, oil shortage, the important channel of realizing resource, the energy, environment global optimization and Sustainable development.Most of coal is rich in organic matter, can get tar liquid, solid-state semicoke, gaseous state carbonization gas through being heated to 480 ℃～900 ℃ destructive distillation under isolated air conditions.The oil of producing by destructive distillation belongs to stock oil, can produce oil fuel through hydrogenation, but also fine chemical product is produced in deep processing.
Destructive distillation is the important mode of production of industrial chemicals, compares with the gasification mode, has improved the utilization ratio of hydrogen content of coal, compares with direct liquefaction, greatly reduces investment and technical difficulty.
Coal is after heating (500 ℃ of left and right) destructive distillation, and contained organic matter decomposition generates coalite tar, carbonization gas and coal semicoke; Coal tar is the automobile-used fuel such as processing vapour, diesel oil further, and deep processing is fine chemical material.China coal oleaginousness (Ge Jinfa) is mostly 5～20%.Therefore, rationally utilize China's coal resource can alleviate to a certain extent petroleum resources shortage present situation.
At present, this area coal fluidized retoring technology commonly used adopts be the Shandong strange～Rule gas process method (Lurgi Ruhrgas) and Dalian University of Technology's solid thermal carriers dry distillation (the new method of DG), these two kinds of methods are very similar, technical process is granularity less than the coal dust of 6mm with after the coke thermal barrier mixes, and carries out destructive distillation in gravity moving-bed vertical reactor.The coal gas and the tarry vapours that produce cause gas sweetening and coke tar recovery system, and the coke of circulation partly leaves upright furnace and promotes heating with pneumatic conveyor, and separate with waste gas and turn back to upright furnace as thermal barrier afterwards again.Carrying out pyrolysis under normal pressure, to obtain calorific value be 26～32MJ/m
3Coal gas, semicoke and coal-based crude oil.Although the oily yield of the method is high, the carbonization gas calorific value is high, and power consumption is little.But also have high-temperature spiral mechanical mixer complex structure, the metal cost is high; Thermal barrier mixes undesirable in mixing tank with coal dust, need long-time the heat transfer to guarantee the destructive distillation effect; Equipment attrition is serious simultaneously, easily stops up, and single device treatment capacity is limited.
Summary of the invention
The objective of the invention is that to exist thermal barrier to mix in mixing tank with coal dust undesirable in order to solve existing coal fluidized retoring technology, need the problem of long-time heat transfer assurance destructive distillation effect, and a kind of coal dust composite dry distillation unit and method are provided.
Of the present invention being achieved through the following technical solutions:
device: comprise the semicoke storage tank, the semicoke water cooler, drainage conduit, head tank, blanking machine, mother tube, main air blower, the first multistage cyclone separator, the device of making charcoal, the device dense bed of making charcoal, main air distributor, the thermal barrier standpipe, the semicoke transfer lime, the discharge standpipe, air main, auxiliary burner, the semicoke inclined tube, heat collector, riser reactor, the second multistage cyclone separator, the dry distillation reactor device, semicoke decline standpipe, supercharger, turbine machine, the heat-obtaining standpipe, dry gas inlet pipe and stripped vapor device, the first multistage cyclone separator are arranged on the top in the device of making charcoal, and the device dense bed of making charcoal is arranged on the middle part in the device of making charcoal, thermal barrier standpipe, the semicoke transfer lime, the output terminal of discharge standpipe and heat-obtaining standpipe all is arranged on the bottom in the device of making charcoal, the input terminus of heat-obtaining standpipe is connected with supercharger, one end of heat collector is connected with the heat-obtaining standpipe, the other end semicoke inclined tube of heat collector is connected with the device dense bed of making charcoal, the input terminus of discharge standpipe is connected with drainage conduit, the input terminus of drainage conduit is connected with turbine machine, the output terminal of drainage conduit is connected with the semicoke water cooler, the semicoke water cooler is connected with the semicoke storage tank, the input terminus of semicoke transfer lime is connected with supercharger, and the dry distillation reactor device is divided into the dilute phase section from top to bottom, close phase section and stripping stage, the second multistage cyclone separator is arranged in the dilute phase section, the stripped vapor device is arranged in stripping stage, the lower end of dry distillation reactor device is connected with the semicoke transfer lime by semicoke decline standpipe, the output terminal of thermal barrier standpipe is connected with riser reactor, the output terminal of riser reactor is arranged in close phase section, the input terminus of riser reactor is connected with the dry gas inlet pipe, head tank is connected with blanking machine, blanking machine is connected with the dry gas inlet pipe by mother tube, the output terminal of air main is arranged in the device dense bed of making charcoal and with main air distributor and is connected, the input terminus of air main is connected with auxiliary burner, air main is connected with main air blower with supercharger respectively.
Method: its step is as follows:
step 1, coal dust raw material after pulverizing by head tank through blanking machine, mother tube enters bottom riser reactor, sending the high temperature semicoke by the thermal barrier standpipe mixes with the coal dust raw material, when the high temperature semicoke enters, dry gas is input into riser reactor bottom by the dry gas inlet pipe, coal dust raw material and high temperature semicoke are 1: 3.0～12.0 by ratio of weight and the number of copies, the high temperature semicoke mixes in riser reactor with coal dust and carries out dry distillation reactor, the lifting reaction pressure is 0.10MPa～0.30MPa, generate oil gas and semicoke coke after reaction, the semicoke coke enters in the dry distillation reactor device with destructive distillation oil gas and continues dry distillation reactor, reaction times is 2min～8min,
step 2, semicoke in the dry distillation reactor device advances in the semicoke transfer lime through semicoke decline standpipe, the air that is come by supercharger again delivers in the device of making charcoal, supercharging wind enters to circulate in heat collector for semicoke in the device of making charcoal through the heat-obtaining standpipe provides pressure, its pressure is 0.10MPa～0.30MPa, air by main air blower through auxiliary burner, air main, main air distributor enters in the device of making charcoal and provides the air catalytic combustion for semicoke, become the high temperature semicoke after making the temperature of semicoke reach 600 ℃～800 ℃, part high temperature semicoke is inputed in riser reactor by the thermal barrier standpipe and provides heat source for reaction for the coal dust raw material, another part high temperature semicoke is through the discharge standpipe, drainage conduit enters and enters in the semicoke storage tank after cooling in the semicoke water cooler,
Step 3, oil gas and semicoke coke react 2min～8min in the dry distillation reactor device after, dry distillation reactor pressure is 0.10Mpa～0.30Mpa, reaction oil gas upwards moves with dry gas and send into oil recovery system by the Oil/Gas Pipe at top after the second multistage cyclone separator separates, the semicoke natural subsidence, be that the stripped vapor of 380 ℃～520 ℃ passes in stripping stage with temperature, stripped vapor carries out stripping to semicoke, make to be attached on semicoke oil gas and to separate, oil gas upwards operation is sent into oil recovery system by the Oil/Gas Pipe at top after the second multistage cyclone separator separates;
Step 4, semicoke fine powder return to close phase section in the dry distillation reactor device, enter in the device of making charcoal through semicoke decline standpipe, semicoke transfer lime and use as partially combusted semicoke, and heating up after burning becomes thermal barrier.
The present invention has following beneficial effect:
One, method of the present invention adopts the fine coal raw material of particle diameter 0～5mm, it is the fluidisation raw material of wide-size distribution, but little than the circulating fluidized bed particle size range, fluidisation is easy than circulating fluidized bed, gas consumption is little relatively, and raw material is when adding riser reactor, owing to being rapidly heated simultaneously, raw material heat collapses particle diameter and further diminishes, and the water vapor in raw material is conducive to reduce fluidization gas; Device of the present invention can be realized raw material and semicoke normal fluidisation, conveying and destructive distillation in device, and can obtain higher coal tar yield.Under processing condition of the present invention, the coal tar yield reaches 80～92%.
Two, the present invention utilizes riser reactor, make charcoal device and dry distillation reactor device carry out compound destructive distillation to coal dust; Solid thermal carriers are combined destructive distillation with gaseous heat-carrier; The coal tar reaction times is short, gas-oil separation is fast, and second pyrolysis is few, and in gas, hydrogen, hydrogen sulfide can promote the oil product lighting.
Three, the present invention is by the air feed of main air blower, control make charcoal gas volume that device makes charcoal, control the temperature of the device of making charcoal by the heat-obtaining amount of heat collector, the temperature of thermal barrier (semicoke) is easy to control, and makes the temperature of the device of making charcoal and pyrolysis temperature to the variation strong adaptability of coal and ature of coal.
Four, make charcoal the high temperature semicoke that produces as the destructive distillation thermal source of fine coal, the solid thermal carriers heat exchange is fast, and operating pressure is high, and equipment volume is little, the equipment heat insulating ability is good, and heat radiation is few, after high temperature semicoke destructive distillation heat supply, the heat producing steam provides power for device, and heat utilization efficiency is high, reaches more than 80%.
Five, processing method of the present invention is succinct, and the dynamic seal of distillation apparatus high-temperature component is few; Working pressure is high, and equipment volume is relatively little; The high-temperature machinery structure is few, stable equipment operation, and the cost of overhaul is low; The oil quality that generates is good, and oil-collecting ratio is high.The coal tar of gained can the production high added value gasoline, diesel oil, asphaltic products., Elementary Chemical Industry raw material and fuel gas.
Description of drawings
Fig. 1 is one-piece construction front view of the present invention, and Fig. 2 is the process flow sheet of example 1.
Embodiment
embodiment one: present embodiment is described in conjunction with Fig. 1 and Fig. 2, present embodiment comprises semicoke storage tank 1, semicoke water cooler 2, drainage conduit 3, head tank 4, blanking machine 5, mother tube 6, main air blower 8, the first multistage cyclone separator 10, the device 11 of making charcoal, the device dense bed 12 of making charcoal, main air distributor 13, thermal barrier standpipe 14, semicoke transfer lime 16, discharge standpipe 17, air main 19, auxiliary burner 20, semicoke inclined tube 21, heat collector 22, riser reactor 24, the second multistage cyclone separator 26, dry distillation reactor device 27, semicoke decline standpipe 31, supercharger 33, turbine machine 34, heat-obtaining standpipe 35, dry gas inlet pipe 36 and stripped vapor device 38, the first multistage cyclone separator 10 is arranged on the top in the device 11 of making charcoal, the device dense bed 12 of making charcoal is arranged on the middle part in the device 11 of making charcoal, the device 11 of the making charcoal main air of making charcoal adopts air or oxygen-rich air, main air is used for the fluidisation semicoke, charcoal in the burning semicoke, the control amount of making charcoal accounts for the 2-10% of semicoke carbon content, according to water-content in raw material with efflux semicoke quality product calculative determination, the device 11 of making charcoal is inner for partly making charcoal, the interior coal semicoke of the device 11 of making charcoal is the bubbling bed state, can reduce fluidisation main air consumption, the device 11 of making charcoal adopts the combustion with meagre oxygen technology, make charcoal and contain a large amount of CO in flue gas 9, by the waste heat boiler recovery heat that again burns, the volume of reduction equipment effectively, thereby reduce investment, the aggrandizement apparatus treatment capacity, reduce simultaneously high pressure main air amount, reduce power consumption, thermal barrier standpipe 14, semicoke transfer lime 16, the output terminal of discharge standpipe 17 and heat-obtaining standpipe 35 all is arranged on the bottom in the device 11 of making charcoal, the input terminus of heat-obtaining standpipe 35 is connected with supercharger 33 by pipeline, one end of heat collector 22 is connected with heat-obtaining standpipe 35, the other end of heat collector 22 is connected with the device dense bed 12 of making charcoal by semicoke inclined tube 21, the input terminus of discharge standpipe 17 is connected with drainage conduit 3, the delivering gas input terminus of drainage conduit 3 is connected with turbine machine 34 by pipeline, the output terminal of drainage conduit 3 is connected with semicoke water cooler 2, semicoke water cooler 2 is connected with semicoke storage tank 1 by pipeline, the delivering gas input terminus of semicoke transfer lime 16 is connected with supercharger 33 by pipeline, dry distillation reactor device 27 is divided into dilute phase section 37 from top to bottom, close phase section 28 and stripping stage 29, the second multistage cyclone separator 26 is arranged in dilute phase section 37, cyclone separator semicoke discharge gate is arranged in close phase section 28, stripped vapor device 38 is arranged in stripping stage 29, the lower end of dry distillation reactor device 27 is connected with semicoke transfer lime 16 by semicoke decline standpipe 31, the output terminal of thermal barrier standpipe 14 is connected with riser reactor 24, the output terminal of riser reactor 24 is arranged in close phase section 28, the input terminus of riser reactor 24 is connected with dry gas inlet pipe 36, the lifting medium of riser reactor 24 is that self-produced carbonization gas is through receiving the dry gas 7 after oil takes off the lighter hydrocarbons processing, contain a large amount of hydrogen and a certain amount of hydrogen sulfide in dry gas 7, but coal tar part lighting, the interior thermal barrier of riser reactor 24 and raw material are gas-solid and carry bed, head tank 4 is connected with blanking machine 5, blanking machine 5 is connected with dry gas inlet pipe 36 by mother tube 6, the output terminal of air main 19 is arranged in the device dense bed 12 of making charcoal and with main air distributor 13 and is connected, the input terminus of air main 19 is connected with auxiliary burner 20, air main 19 is connected with main air blower with supercharger 33 by pipeline respectively and is connected, heat collector 22 is used for controlling device 11 temperature of making charcoal, auxiliary burner 20 is the semicoke warm-up heating in the device 11 of making charcoal, can reduce the amount of making charcoal of the device 11 of making charcoal, play the function of regulating the semicoke quality, make dry gas and semicoke flexible as required.Dry distillation reactor device 27 adopts with high block form or height with the device 11 of making charcoal and is set up in parallel, and dry distillation reactor device 27 and the device 11 of making charcoal can be adjusted respectively pressure, and to satisfy the needs of actually operating, the interior semicoke of dry distillation reactor device 27 is the bubbling bed state.
Embodiment two: in conjunction with Fig. 1, present embodiment is described, present embodiment is different from embodiment one is that it also increases thermal barrier guiding valve 15 is arranged, and thermal barrier guiding valve 15 is arranged on thermal barrier standpipe 14.Other composition and annexation are identical with embodiment one.
Embodiment three: in conjunction with Fig. 1, present embodiment is described, present embodiment is different from embodiment one is that it also increases discharge guiding valve 18 is arranged, and discharge guiding valve 18 is arranged on discharge standpipe 17.Other composition and annexation are identical with embodiment one or two.
Embodiment four: in conjunction with Fig. 1, present embodiment is described, present embodiment is different from embodiment one is that it also increases heat-obtaining guiding valve 23 is arranged, and heat-obtaining guiding valve 23 is arranged on heat collector 22.Other composition and annexation are identical with embodiment three.
Embodiment five: in conjunction with Fig. 1, present embodiment is described, present embodiment is different from embodiment one is that it also increases semicoke decline guiding valve 32 is arranged, and semicoke decline guiding valve 32 is arranged on semicoke decline standpipe 31.Other composition and annexation are identical with embodiment four.
Embodiment six: in conjunction with Fig. 1, present embodiment is described, the method for present embodiment realizes by following steps:
step 1, coal dust raw material after pulverizing by head tank 4 through blanking machine 5, mother tube 6 enters riser reactor 24 bottoms, sending the high temperature semicoke by thermal barrier standpipe 14 mixes with the coal dust raw material, when the high temperature semicoke enters, dry gas 7 is input into riser reactor 24 bottoms by dry gas inlet pipe 36, coal dust raw material and high temperature semicoke are 1: 3.0～12.0 by ratio of weight and the number of copies, high temperature semicoke and coal dust mix and carry out dry distillation reactor riser reactor 24 is interior, the lifting reaction pressure is 0.10MPa～0.30MPa, generate oil gas and semicoke coke after reaction, the semicoke coke enters in dry distillation reactor device 27 with destructive distillation oil gas and continues dry distillation reactor, reaction times is 2min～8min, high temperature semicoke and coal dust raw material are fluidized state in dry distillation reactor device 27,
step 2, semicoke in dry distillation reactor device 27 advances in semicoke transfer lime 16 through semicoke decline standpipe 31, air by supercharger 33 delivers in the device 11 of making charcoal again, supercharging wind 33 enters to circulate in heat collector 22 for semicoke in the device 11 of making charcoal through heat-obtaining standpipe 35 provides pressure, its pressure is 0.10MPa～0.30MPa, air by main air blower 8 through auxiliary burner 20, air main 19, main air distributor 13 enters in the device 11 of making charcoal and provides the air catalytic combustion for semicoke, become the high temperature semicoke after making the temperature of semicoke reach 600 ℃～800 ℃, part high temperature semicoke is inputed in riser reactor 24 by thermal barrier standpipe 14 and provides heat source for reaction for the coal dust raw material, another part high temperature semicoke is through discharge standpipe 17, drainage conduit 3 enters and enters in semicoke storage tank 1 after cooling in semicoke water cooler 2, carry out part and make charcoal by main air blower 8 with by the heat collector 22 heat-obtaining co-controllings device 11 of making charcoal, guarantee the temperature of thermal barrier.Auxiliary burner 20 can reduce the amount of making charcoal of the device 11 of making charcoal, and plays the function of regulating the semicoke quality, makes dry gas and semicoke flexible as required; The saturated middle pressure steam that external warmer 22 produces is through the residual neat recovering system recovered energy.Under the condition that satisfies thermal barrier heat supply and device steam consumption, improve simultaneously the semicoke quality, the device 11 of making charcoal is taked combustion with meagre oxygen, and combustion with meagre oxygen can reduce the air quantity of main air blower 8, contain a certain amount of CO in flue gas 9, the flue gas 9 at device 11 tops of making charcoal enters the residual neat recovering system recovered energy;
Step 3, oil gas and semicoke coke react 2min～8min in dry distillation reactor device 27 after, dry distillation reactor pressure is 0.10Mpa～0.30Mpa, reaction oil gas upwards moves with dry gas 7 and send into oil recovery system 25 by the Oil/Gas Pipe at top after the second multistage cyclone separator 26 separates, the semicoke natural subsidence, be that the stripped vapor 30 of 380 ℃～520 ℃ passes in stripping stage 29 with temperature, 30 pairs of semicokes of stripped vapor carry out stripping, make to be attached on semicoke oil gas and to separate, oil gas upwards operation is sent into oil recovery system 25 by the Oil/Gas Pipe at top after the second multistage cyclone separator 26 separates;
Step 4, semicoke fine powder return to close phase section 28 in dry distillation reactor device 27, enter in the device 11 of making charcoal through semicoke decline standpipe 31, semicoke transfer lime 16 and use as partially combusted semicoke, and heating up after burning becomes thermal barrier.
Embodiment seven: present embodiment is described in conjunction with Fig. 1, present embodiment is that the semicoke temperature of making charcoal in step 2 in device 11 are 650 ℃, after semicoke in riser reactor 24 mixes with coal dust, temperature is 450 ℃～550 ℃, semicoke temperature in dry distillation reactor device 27 is 450 ℃～500 ℃, and the semicoke temperature in semicoke transfer lime 16 is 450 ℃～480 ℃.Other step is identical with embodiment six.
Embodiment eight: in conjunction with Fig. 1, present embodiment is described, present embodiment is the particle diameter≤5mm of coal dust raw material in step 1, and the lattice gold oil length of coal dust raw material is 5%～20%, lattice gold water content≤30%.Other step is identical with embodiment six.
Embodiment nine: in conjunction with Fig. 1, present embodiment is described, present embodiment is that in step 1, the high temperature semicoke is 1: 5 with coal dust raw materials by weight portion ratio.Other step is identical with embodiment six.
Embodiment ten: present embodiment is described in conjunction with Fig. 1, present embodiment is that in step 1, high temperature semicoke and coal dust mix and carry out dry distillation reactor riser reactor 24 is interior, the lifting reaction pressure is 0.20MPa, generate oil gas and semicoke coke after reaction, the semicoke coke enters the dry distillation reactor device with destructive distillation oil gas, and (continue dry distillation reactor in 27, the reaction times is 5min.Other step is identical with embodiment six.
Application example of the present invention:
Example 1, adopt the Yilan long-flame coal, implement raw material and product semicoke character and see Table 1; Coal dust and semicoke ultimate analysis see Table 2; The contrast of this process unit produce oil boiling range sees Table 3; Produce the analysis in table 4 of carbonization gas; The operational condition of coal dust destructive distillation device sees Table 5.
Service data proof pyrolysis temperature is between 481 ℃～519 ℃, it is the oily yield Optimal Temperature scope of Yilan long-flame coal, change according to the actual coal of coal, consider actual under the little condition of oily yield impact, the setting pyrolysis temperature is lower can reduce the amount of making charcoal of coal, improve coal semicoke calorific value, therefore the pyrolysis temperature span of control is set as 496 ± 15 ℃.
The powder fluidized distillation process comprises material screening as shown in Figure 2, drying, and feeding section, dry distiller, the device of making charcoal, oil recovery system, semicoke are cooling, store, and residual neat recovering system.Coal dust enters dry distillation reactor by feeding section, gained coal tar advances the oil recovery system fractionation and gets product after dry distillation reactor, the coal dust semicoke enters the device of making charcoal after stripping, make charcoal rear semicoke through semicoke cooling segment discharger, the combustion with meagre oxygen flue gas is through the residual neat recovering system recovered energy, and the low-temperature flue gas dried feed enters atmosphere by chimney.
Receive oily part: oil gas enters separation column, tower tray is set in separation column, oil gas is by the tower underfeed, separation column is established stage casing and two, top backflow heat-obtaining, reflux and control tower top temperature at 150～180 ℃ in the top, lightweight coal tar oil gas distillates from tower top, through air cooler and fractionation tower top oil gas water cooler condensing cooling to 50 ℃, enters fractionation return tank of top of the tower standing separation.Rich gas is compressed to 0.4MPa and is cooled to 40～60 ℃ through the rich gas water cooler through promoting air compressor, advances rich gas and divides the flow container separatory, and separatory tank top gas is as dry gas, a part for promote dry gas 7, residue dry gas product is delivered to residual neat recovering system and is made postcombustion.At the bottom of return tank of top of the tower lightweight oil by the light oil pump through the cooling tank field of delivering to of light oil aftercooler; Oily fraction during the separation column middle part is extracted send middle oil tank after the cooling heat-obtaining; First by interchanger, then be cooled to 230 ℃ through the Fractionator Bottom oil cooler after the heavy oil of Fractionator Bottom is extracted out, the part section of hitting circulates, and all the other are cooled to 90 ℃ and go out device by getting rid of the heavy oil water cooler outward, tank sending district heavy oil tank.
Residual neat recovering system: the flue-gas temperature at device 11 tops of making charcoal is higher, owing to adopting part to make charcoal, is incomplete combustion, contains a large amount of CO gases.Enter waste heat boiler burning recovered energy.The self-produced part dry gas of supplementary device simultaneously in waste heat boiler is in order to produce overheated middle pressure steam.Install interior heat collector 22, semicoke water cooler 2, reach the saturated middle pressure steam that oil cooler produces, the superheated vapour that send waste heat boiler to produce.The device 11 of making charcoal controls according to the power needs of device the amount of making charcoal, and self-produced superheated vapour is personal to device.Approximately 180～250 ℃ of the flue gases that waste heat boiler is discharged are used for providing coal dust dry institute heat requirement; Again through the sack cleaner dedusting by the chimney safety dumping.
Table 1: the analysis of feed coal and product semicoke:
Table 2 coal and semicoke ultimate analysis (as received basis):
| Ultimate analysis: | C | H | N | S | O | Ash content | Moisture |
| Coal raw material as received basis | 54.9 | 5.389 | 1.02 | 0.164 | 28.6 | 3.38 | 6.52 |
| Coal semicoke as received basis | 75.41 | 3.38 | 1.679 | 0.512 | 9.945 | 7.8 | 1.23 |
Table 3: product tar dative gold tar contrast:
| Boiling range | Unit | This technique destructive distillation produce oil | The destructive distillation of lattice gold |
| Initial boiling point | ℃ | 78 | 81 |
| 5% recovered temperature | ℃ | 135 | 143 |
| 10% recovered temperature | ℃ | 167 | 177 |
| 20% recovered temperature | ℃ | 204 | 218 |
| 30% recovered temperature | ℃ | 230 | 250 |
| 40% recovered temperature | ℃ | 258 | 282 |
| 50% recovered temperature | ℃ | 284 | 314 |
| 60% recovered temperature | ℃ | 307 | 335 |
| 70% recovered temperature | ℃ | 334 | 362 |
| 80% recovered temperature | ℃ | 345 | 382 |
| Final boiling point | ℃ | 350(92％) | 384(90.4％) |
| Density (20 ℃) | g/cm 3 | 0.9517 | 0.9729 |
The analysis of table 4 carbonization gas:
Data by the present embodiment show, this handicraft product oil quality is good, and high-quality is lighter, and the hydrogen utilization ratio in coal is improved; The basic moisture-free of product semicoke of this technique, although ash content increases, calorific value is higher, the semicoke quality is good, is to gasify preferably, the materials such as fuel; The calorific value of carbonization gas is higher, and methane and hydrogen content are high, is the desirable feedstock of carrying hydrogen and producing Sweet natural gas and burning.
Claims (10)
1. coal dust composite dry distillation unit, it is characterized in that: described device comprises semicoke storage tank (1), semicoke water cooler (2), drainage conduit (3), head tank (4), blanking machine (5), mother tube (6), main air blower (8), the first multistage cyclone separator (10), the device (11) of making charcoal, the device dense bed (12) of making charcoal, main air distributor (13), thermal barrier standpipe (14), semicoke transfer lime (16), discharge standpipe (17), air main (19), auxiliary burner (20), semicoke inclined tube (21), heat collector (22), riser reactor (24), the second multistage cyclone separator (26), dry distillation reactor device (27), semicoke decline standpipe (31), supercharger (33), turbine machine (34), heat-obtaining standpipe (35), dry gas inlet pipe (36) and stripped vapor device (38), the first multistage cyclone separator (10) is arranged on the top in the device of making charcoal (11), the device dense bed (12) of making charcoal is arranged on the middle part in the device of making charcoal (11), thermal barrier standpipe (14), semicoke transfer lime (16), the output terminal of discharge standpipe (17) and heat-obtaining standpipe (35) all is arranged on the bottom in the device of making charcoal (11), the input terminus of heat-obtaining standpipe (35) is connected with supercharger (33), one end of heat collector (22) is connected with heat-obtaining standpipe (35), the other end semicoke inclined tube (21) of heat collector (22) is connected with the device dense bed (12) of making charcoal, the input terminus of discharge standpipe (17) is connected with drainage conduit (3), the input terminus of drainage conduit (3) is connected with turbine machine (34), the output terminal of drainage conduit (3) is connected with semicoke water cooler (2), semicoke water cooler (2) is connected with semicoke storage tank (1), the input terminus of semicoke transfer lime (16) is connected with supercharger (33), dry distillation reactor device (27) is divided into dilute phase section (37) from top to bottom, close phase section (28) and stripping stage (29), the second multistage cyclone separator (26) is arranged in dilute phase section (37), stripped vapor device (38) is arranged in stripping stage (29), the lower end of dry distillation reactor device (27) is connected with semicoke transfer lime (16) by the semicoke standpipe (31) that descends, the output terminal of thermal barrier standpipe (14) is connected with riser reactor (24), the output terminal of riser reactor (24) is arranged in close phase section (28), the input terminus of riser reactor (24) is connected with dry gas inlet pipe (36), head tank (4) is connected with blanking machine (5), blanking machine (5) is connected with dry gas inlet pipe (36) by mother tube (6), the output terminal of air main (19) is arranged in the device dense bed (12) of making charcoal and with main air distributor (13) and is connected, the input terminus of air main (19) is connected with auxiliary burner (20), air main (19) is connected 8 with supercharger (33) with main air blower respectively) be connected.
2. a kind of coal dust composite dry distillation unit according to claim 1, it is characterized in that: described device also comprises thermal barrier guiding valve (15), thermal barrier guiding valve (15) is arranged on thermal barrier standpipe (14).
3. described a kind of coal dust composite dry distillation unit according to claim 1 and 2, it is characterized in that: described device also comprises discharge guiding valve (18), discharge guiding valve (18) is arranged on discharge standpipe (17).
4. a kind of coal dust composite dry distillation unit according to claim 3, it is characterized in that: described device also comprises heat-obtaining guiding valve (23), heat-obtaining guiding valve (23) is arranged on heat collector (22).
5. a kind of coal dust composite dry distillation unit according to claim 4, it is characterized in that: described device also comprises semicoke decline guiding valve (32), semicoke decline guiding valve (32) is arranged on semicoke decline standpipe (31).
6. one kind is utilized claim 1 coal dust composite dry distillation unit to realize the compound method for destructive distillation of coal dust, and it is characterized in that: described method realizes by following steps:
step 1, coal dust raw material after pulverizing by head tank (4) through blanking machine (5), mother tube (6) enters bottom riser reactor (24), sending the high temperature semicoke by thermal barrier standpipe (14) mixes with the coal dust raw material, when the high temperature semicoke enters, dry gas (7) is input into riser reactor (24) bottom by dry gas inlet pipe (36), coal dust raw material and high temperature semicoke are 1: 3.0～12.0 by ratio of weight and the number of copies, the high temperature semicoke mixes in riser reactor (24) with coal dust and carries out dry distillation reactor, the lifting reaction pressure is 0.10MPa～0.30MPa, generate oil gas and semicoke coke after reaction, the semicoke coke enters with destructive distillation oil gas and continues dry distillation reactor in dry distillation reactor device (27), reaction times is 2min～8min,
step 2, semicoke in dry distillation reactor device (27) advances in semicoke transfer lime (16) through the semicoke standpipe (31) that descends, the air that is come by supercharger (33) again delivers in the device of making charcoal (11), supercharging wind (33) enters in the device of making charcoal (11) through heat-obtaining standpipe (35) and provide pressure for semicoke circulates in heat collector (22), its pressure is 0.10MPa～0.30MPa, air by main air blower (8) through auxiliary burner (20), air main (19), main air distributor (13) enters in the device of making charcoal (11) and provides the air catalytic combustion for semicoke, become the high temperature semicoke after making the temperature of semicoke reach 600 ℃～800 ℃, part high temperature semicoke is inputed in riser reactor (24) by thermal barrier standpipe (14) and provides heat source for reaction for the coal dust raw material, another part high temperature semicoke is through discharge standpipe (17), drainage conduit (3) enters and enters in semicoke storage tank (1) after cooling in semicoke water cooler (2),
step 3, oil gas and semicoke coke react 2min～8min in dry distillation reactor device (27) after, dry distillation reactor pressure is 0.10Mpa～0.30Mpa, reaction oil gas upwards moves with dry gas (7) and send into oil recovery system (25) by the Oil/Gas Pipe at top after the second multistage cyclone separator (26) separates, the semicoke natural subsidence, be that the stripped vapor (30) of 380 ℃～520 ℃ passes in stripping stage (29) with temperature, stripped vapor (30) carries out stripping to semicoke, make and be attached on semicoke oil gas and separate, oil gas upwards operation is sent into oil recovery system (25) by the Oil/Gas Pipe at top after the second multistage cyclone separator (26) separates,
Step 4, semicoke fine powder return to close phase section (28) in dry distillation reactor device (27), enter in the device of making charcoal (11) through semicoke decline standpipe (31), semicoke transfer lime (16) and use as partially combusted semicoke, heating up after burning becomes thermal barrier.
7. the compound method for destructive distillation of a kind of coal dust according to claim 6, it is characterized in that: the semicoke temperature in the device of making charcoal in step 2 (11) is 650 ℃, after semicoke in riser reactor (24) mixes with coal dust, temperature is 450 ℃～550 ℃, semicoke temperature in dry distillation reactor device (27) is 450 ℃～500 ℃, and the semicoke temperature in semicoke transfer lime (16) is 450 ℃～480 ℃.
8. the compound method for destructive distillation of a kind of coal dust according to claim 6, it is characterized in that: the particle diameter≤5mm of coal dust raw material in step 1, the lattice gold oil length of coal dust raw material is 5%～20%, lattice gold water content≤30%.
9. the compound method for destructive distillation of a kind of coal dust according to claim 6, it is characterized in that: in step 1, the high temperature semicoke is 1: 5 with coal dust raw materials by weight portion ratio.
10. the compound method for destructive distillation of a kind of coal dust according to claim 6, it is characterized in that: in step 1, the high temperature semicoke mixes in riser reactor (24) with coal dust and carries out dry distillation reactor, the lifting reaction pressure is 0.20MPa, generate oil gas and semicoke coke after reaction, the semicoke coke enters with destructive distillation oil gas and continues dry distillation reactor in dry distillation reactor device (27), and the reaction times is 5min.
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Application publication date: 20130522 |