CN103074093B - Integral process and system for directly drying and pyrolyzing lignite - Google Patents
Integral process and system for directly drying and pyrolyzing lignite Download PDFInfo
- Publication number
- CN103074093B CN103074093B CN201310034572.7A CN201310034572A CN103074093B CN 103074093 B CN103074093 B CN 103074093B CN 201310034572 A CN201310034572 A CN 201310034572A CN 103074093 B CN103074093 B CN 103074093B
- Authority
- CN
- China
- Prior art keywords
- gas
- temperature
- brown coal
- pyrolysis
- pyrolysis oven
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- 239000003077 lignite Substances 0.000 title claims abstract description 62
- 238000000034 method Methods 0.000 title claims abstract description 43
- 230000008569 process Effects 0.000 title claims abstract description 33
- 238000001035 drying Methods 0.000 title claims abstract description 29
- 239000007789 gas Substances 0.000 claims abstract description 87
- 238000000197 pyrolysis Methods 0.000 claims abstract description 64
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 43
- 239000000446 fuel Substances 0.000 claims abstract description 21
- 238000005406 washing Methods 0.000 claims abstract description 17
- 238000001914 filtration Methods 0.000 claims abstract description 13
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000003546 flue gas Substances 0.000 claims abstract description 10
- 238000010438 heat treatment Methods 0.000 claims abstract description 9
- 238000006243 chemical reaction Methods 0.000 claims abstract description 8
- 239000002994 raw material Substances 0.000 claims abstract description 6
- 230000003197 catalytic effect Effects 0.000 claims description 44
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 23
- 238000005979 thermal decomposition reaction Methods 0.000 claims description 18
- 238000001465 metallisation Methods 0.000 claims description 12
- 239000000428 dust Substances 0.000 claims description 11
- 239000002028 Biomass Substances 0.000 claims description 10
- 238000007233 catalytic pyrolysis Methods 0.000 claims description 10
- 238000013459 approach Methods 0.000 claims description 9
- 239000003245 coal Substances 0.000 claims description 9
- 239000002737 fuel gas Substances 0.000 claims description 8
- 239000000463 material Substances 0.000 claims description 8
- 239000000567 combustion gas Substances 0.000 claims description 7
- 230000008676 import Effects 0.000 claims description 7
- 238000000629 steam reforming Methods 0.000 claims description 6
- 229910052799 carbon Inorganic materials 0.000 claims description 3
- 230000018044 dehydration Effects 0.000 claims description 3
- 238000006297 dehydration reaction Methods 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- RNFJDJUURJAICM-UHFFFAOYSA-N 2,2,4,4,6,6-hexaphenoxy-1,3,5-triaza-2$l^{5},4$l^{5},6$l^{5}-triphosphacyclohexa-1,3,5-triene Chemical compound N=1P(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP=1(OC=1C=CC=CC=1)OC1=CC=CC=C1 RNFJDJUURJAICM-UHFFFAOYSA-N 0.000 claims description 2
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 239000011248 coating agent Substances 0.000 claims description 2
- 238000000576 coating method Methods 0.000 claims description 2
- 239000003063 flame retardant Substances 0.000 claims description 2
- 229910001220 stainless steel Inorganic materials 0.000 claims description 2
- 239000010935 stainless steel Substances 0.000 claims description 2
- 238000003786 synthesis reaction Methods 0.000 claims description 2
- 238000002309 gasification Methods 0.000 abstract description 15
- 238000002360 preparation method Methods 0.000 abstract description 3
- 239000000571 coke Substances 0.000 abstract description 2
- 238000006057 reforming reaction Methods 0.000 abstract description 2
- 230000002269 spontaneous effect Effects 0.000 abstract description 2
- 238000004523 catalytic cracking Methods 0.000 abstract 6
- 238000002485 combustion reaction Methods 0.000 abstract 1
- 238000005336 cracking Methods 0.000 abstract 1
- 230000006872 improvement Effects 0.000 description 7
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- 239000001257 hydrogen Substances 0.000 description 4
- 239000003034 coal gas Substances 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 238000001833 catalytic reforming Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000010881 fly ash Substances 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000010504 bond cleavage reaction Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003415 peat Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 230000007017 scission Effects 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000035924 thermogenesis Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 238000007601 warm air drying Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
Images
Landscapes
- Processing Of Solid Wastes (AREA)
- Solid Fuels And Fuel-Associated Substances (AREA)
Abstract
The invention relates to an integral process and a system for directly drying and pyrolyzing lignite. The process comprises the steps of feeding fuel to a high-temperature catalytic cracking furnace for combustion, taking generated heat as a heat source for raw gas cracking reaction in the high-temperature catalytic cracking furnace, allowing moderate-temperature flue gas exhausted from a flue gas outlet at the upper part of the high-temperature catalytic cracking furnace to enter a heating jacket outside a pyrolyzing furnace, indirectly heating, drying and pyrolyzing a lignite raw material to generate semi-coke, raw gas and water vapor, exhausting tail flue gas, exhausting the raw gas and the unreacted water vapor from the pyrolyzing furnace, allowing the raw gas and the unreacted water vapor to enter the high-temperature catalytic cracking furnace for catalytic cracking and water vapor reforming reaction in the high-temperature catalytic cracking furnace to generate high-temperature pyrolysis gas, allowing part of high-temperature pyrolysis gas to flow back to an internal furnace pipe of the pyrolyzing furnace, and dedusting, washing, filtering and purifying the rest of high-temperature pyrolysis gas. According to the integral process and the system, drying and steam preparation links in the traditional lignite steam gasification application are removed, and the utilization efficiency of the spontaneous steam is improved.
Description
Technical field
Patent of the present invention relates to brown coal convection drying and thermal decomposition integrated metallization processes and system, be particularly related to the technique and the system that the low pressure water vapor producing in brown coal drying process are applied to follow-up catalytic reforming reaction, belong to low-quality coal clean and effective and utilize technical field.
Technical background
Total reserves of coal in China reach 6,000 hundred million tons, occupy third place in the world, and wherein brown coal proportion is about 12.7%.Brown coal are the coal of a kind of state between hard coal and peat, because the coal-forming time is short, moisture content higher (generally can reach 30%60%), volatile matter is high and point of ignition is low, make its poor heat stability, chemically reactive high, thermal value is generally below 4000kcal/kg.High-moisture percentage has reduced the energy density of brown coal, has brought very large difficulty to the conveying of brown coal and efficient utilization, has greatly limited the exploitation scale of brown coal.
Utilize the feature that brown coal chemically reactive is high, reacted and prepared synthetic gas by steam gasification, being used further to afterwards synthetic a series of chemical is important channels for brown coal clean utilization.Traditional brown coal utilize in scheme, and the brown coal of high-moisture percentage are entering before vapourizing furnace and must, through super-dry pre-treatment, as warm air drying, make its humidity be reduced to certain scope.This scheme of utilizing afterwards that is first dried, not only increased facility investment, and drying process need to consume more energy.In addition, the required steam of steam gasification is that a large amount of low pressure water vapors that dry evaporation produces are also not used by auxiliary steam-generating installation preparation mostly, and brown coal drying gasification reaction process energy repeat consumption phenomenon is serious, capacity usage ratio is low, and processing cost is high.
Hu Guoxin etc. are at Hydrogen-Rich Gas Production from Pyrolysis of Biomass in an Auto-generated Steam Atmosphere(ENERGY & FUELS, 2009,23:1748-1753), proposed directed gasification of humidogene material and produced the technique of high concentration hydrogen, this technique is dried humidogene material and pyrolysis, steam gasification, high-temp in-situ CO
2separation concentrates in a reactor to be carried out, and what make wet part of dry generation carries out steam gasification from bleed steam, in obtaining the gasification gas that product hydrogen concentration is higher, simplifies the operation, and reduces energy consumption.Guo Liejin etc. (patent CN 102126704A) carry out the catalytic gasification of biomass in supercritical water, and the vaporization rate of biomass can reach 100%, H in gaseous product
2volumn concentration even can surpass 50%, in reaction, do not have the byproduct such as tar, charcoal produce, can not cause secondary pollution.Can direct gasification for the high humidogene material of water content, do not need the drying process of high energy consumption.But these transform modes, mainly for biomass hydrogen preparation process, can not be produced combustion gas, or prepare synthetic gas and carry out the synthetic of industrial chemicals.Therefore start with from improving steam supply pattern, adopt brown coal high-efficiency cleaning to utilize technique to produce combustion gas or synthetic gas, the low pressure water vapor that brown coal drying process is produced is applied to follow-up gasification reforming reaction process, with energy efficient, minimizing equipment consumption and investment, be of great practical significance and good economy.Before this, have no the report that brown coal convection drying thermal decomposition integratedization is utilized.
Summary of the invention
In order to overcome the deficiencies in the prior art, the object of this invention is to provide a kind of brown coal convection drying and thermal decomposition integrated metallization processes and system, make brown coal in spontaneous steam atmosphere, carry out pyrolytic gasification, dry and the steam having saved in traditional brown coal steam gasification application is prepared link, has improved the utilising efficiency from bleed steam.
To achieve these goals, a technical scheme of the present invention is:
A kind of brown coal convection drying and thermal decomposition integrated system, this system is made up of pyrolysis oven, high-temperature catalytic pyrolyzer, surge tank, fuel hopper, gas blower, tornado dust collector, water washing tank and activated carbon filtration tank, described pyrolysis oven is made up of inner furnace and external heat chuck, the inner furnace of pyrolysis oven is provided with top material inlet mouth, air outlet, top, bottom carbon outleting port and bottom inlet mouth, and the heating jacket of pyrolysis oven is provided with bottom gas approach and top exhanst gas outlet, high-temperature catalytic pyrolyzer is provided with top inlet mouth, top exhanst gas outlet, air outlet, bottom and bottom fuel inlet, in high-temperature catalytic pyrolyzer, catalyzer is housed, surge tank is provided with top fuel gas inlet, left side gas outlet and right side gas outlet, the air outlet, top of pyrolysis oven inner furnace connects high-temperature catalytic pyrolyzer top inlet mouth, the bottom air inlet of pyrolysis oven inner furnace connects air outlet, surge tank left side, the bottom gas approach of pyrolysis oven external heat chuck connects the top exhanst gas outlet of high-temperature catalytic pyrolyzer, the air outlet, bottom of high-temperature catalytic pyrolyzer connects the top fuel gas inlet of surge tank, the bottom fuel inlet of high-temperature catalytic pyrolyzer and the discharge port of fuel hopper connect, the right side gas outlet of surge tank connects the top inlet mouth of gas cyclone fly-ash separator, tornado dust collector outlet and water washing tank import connect, import is connected with activated carbon filtration tank in water washing tank outlet.
As a further improvement on the present invention, described pyrolysis oven and high-temperature catalytic pyrolyzer are made by high temperature resistant stainless steel, and surface is through heat-resisting processing or liner flame retardant coating.
As a further improvement on the present invention, described high-temperature catalytic pyrolyzer is tubular structure, and raw gas enters from its top, and heavily reacted by thermogenesis catalytic pyrolysis and water vapour; High-temperature flue gas is outer and raw gas counter-current flow at pipe, for scission reaction provides heat.
To achieve these goals, another technical scheme of the present invention is:
A kind of brown coal convection drying and thermal decomposition integrated metallization processes, comprise the following steps:
S1. fuel is sent in high-temperature catalytic pyrolyzer and burnt, the heat of generation is as the thermal source of high-temperature catalytic pyrolyzer;
S2. the temperature that the top exhanst gas outlet of high-temperature catalytic pyrolyzer is discharged is the middle temperature flue gas of 500900 DEG C, enter pyrolysis oven external heat chuck by gas approach, dry and the pyrolysis to brown coal heating raw materials, produces semicoke, contains raw gas and water vapor, and flue tail gas is emptying after purifying;
S3. raw gas and unreacted water vapor are discharged from pyrolysis oven top gas outlet, enter high-temperature catalytic pyrolyzer through fuel gas inlet, at inner catalytic pyrolysis and the steam reforming reaction of occurring of high-temperature catalytic pyrolyzer, the Pintsch process gas that reaction produces;
S4. the part in Pintsch process gas passes back into pyrolysis oven inner furnace, and as thermal source, to brown coal direct heating, remainder is after dedusting, washing and filtration, purification are processed, as outer combustion gas or the synthesis material of supplying.
As a further improvement on the present invention, described fuel adopts the biomass that particle diameter is 0.025mm0.25mm, after this fuel and air mixed, in high-temperature catalytic pyrolyzer, burns, and can produce the high temperature of 1000-1200 DEG C, for catalytic pyrolysis furnace provides heat.
As a further improvement on the present invention, the dry and pyrolysis in described step 2 comprises first brown coal thermal dehydration, produces low pressure water vapor, then continues to heat up, and pyrolysis produces coal semicoke and raw gas.
As a further improvement on the present invention, the temperature when raw gas in described step 2 goes out pyrolysis oven is 300600 DEG C.
As a further improvement on the present invention, the temperature of the Pintsch process gas in described step 4 in the time entering pyrolysis oven is 7001000 DEG C;
As a further improvement on the present invention, the raw gas in described step 4 is after catalytic pyrolysis and steam reforming reaction, and the Pintsch process gas E temperature of generation is 800-1000 DEG C.
This technique is suitable for the multiple type of furnace, comprises three sections of stoves, vertical heater etc., not high to entering the granularity requirements of stove brown coal.
This technique is applicable to brown coal or other coal of water ratio 20%60%, is also applicable to the raw material of the high-moisture percentage such as domestic refuse, mud.
Beneficial effect:
(1) in this technique, pyrolysis coal gas is not diluted by extraneous gas, and the combustion gas of generation is finally all for outer confession; The low pressure water vapor (50500 Pa) that pyrolysis produces is used to the water vapor catalytic reforming reaction of brown coal and pyrolysis gas, and the utilization ratio of steam is higher; System does not have extra water vapor to pass into, Energy Intensity Reduction.
(2) this technique is integrated into a process system by the dry of brown coal with pyrolytic gasification, has saved independent drying process and equipment, and flow process is simple, easy and simple to handle, has reduced facility investment and operation cost.
(3) in this technique, in the pyrolytic gasification process of brown coal, required energy is supplied with by biomass, because biomass are renewable energy source, therefore the present invention has very large environmental benefit.
Brief description of the drawings
Fig. 1 is brown coal convection drying and thermal decomposition integrated metallization processes and the system flow schematic diagram of the embodiment of the present invention 1.
1 pyrolysis oven in figure, 2 high-temperature catalytic pyrolyzer, 3 surge tanks, 4 fuel hoppers, 5 gas blowers, 6 tornado dust collector, 7 water washing tanks, 8 activated carbon filtration tanks, 11 pyrolysis oven bottom gas approachs, 12 air outlet, pyrolysis oven tops, 13 high-temperature catalytic pyrolyzer top inlet mouths, 14 air outlets, high-temperature catalytic pyrolyzer bottom, 15 surge tank top fuel gas inlet, 16 pyrolysis oven bottom inlet mouths, 17 cyclonic separator imports, 18 cyclonic separator outlets, 19 water washing tank imports, 20 water washing tank outlets, 21 activated carbon filtration tank imports; A brown coal raw material, B lignite semi-coke, C raw gas, D water vapor, E Pintsch process gas, coal gas after F purifies, G biomass micron fuel, warm flue gas in H, J tail gas.
embodiment
embodiment 1
As shown in Figure 1, brown coal convection drying and thermal decomposition integrated system, be made up of pyrolysis oven 1, high-temperature catalytic pyrolyzer 2, surge tank 3, fuel hopper 4, gas blower 5, tornado dust collector 6, water washing tank 7, activated carbon filtration tank 8 etc.Described pyrolysis oven 1 is made up of inner furnace and external heat chuck, the inner furnace of pyrolysis oven 1 is provided with top material inlet mouth, air outlet, top 12, bottom carbon outleting port and bottom inlet mouth 16, and the heating jacket of pyrolysis oven 1 is provided with bottom gas approach 11 and top exhanst gas outlet, high-temperature catalytic pyrolyzer 2 is provided with top inlet mouth 13, top exhanst gas outlet 10, and air outlet, bottom 14 and bottom fuel inlet 9, be equipped with catalyzer in high-temperature catalytic pyrolyzer 2, surge tank 3 is provided with top fuel gas inlet 15, left side gas outlet and right side gas outlet, fuel hopper 4 is provided with its top feed mouth and bottom discharge mouth, the air outlet, top 12 of pyrolysis oven 1 inner furnace connects high-temperature catalytic pyrolyzer 1 top inlet mouth 13, the bottom inlet mouth 16 of pyrolysis oven 1 inner furnace connects surge tank 3 air outlets, left side 15, the bottom gas approach 11 of pyrolysis oven 1 external heat chuck connects the top exhanst gas outlet 10 of high-temperature catalytic pyrolyzer 2, the air outlet, bottom of high-temperature catalytic pyrolyzer 2 connects the top fuel gas inlet 15 of surge tank 3, the right side gas outlet of surge tank 3 connects the top inlet mouth 17 of gas cyclone fly-ash separator 6, the lower inlet 19 of tornado dust collector outlet 18 and water washing tank 7 connects, water washing tank outlet 20 and activated carbon filtration tank import 21 connect.
As shown in Figure 1, brown coal convection drying and thermal decomposition integrated metallization processes, comprise the following steps:
S1. start gas blower 5, biomass micron fuel G is sprayed into the interior burning of high-temperature catalytic pyrolyzer 2, high-temperature catalytic pyrolyzer 2 is heated to 1100 DEG C.
S2. start feed mechanism, brown coal A is sent into brown coal pyrolysis oven 1 continuously from its top feed mouth, warm flue gas H in high-temperature catalytic pyrolyzer 2 is introduced to pyrolysis oven 1 external heat chuck simultaneously, brown coal raw material A is heated to pyrolysis.Brown coal are heated to 150300 DEG C, and the moisture content in brown coal is become water vapor D by evaporation gradually, then continue to be warming up to 500600 DEG C, and pyrolysis produces semicoke B and raw gas C.
S3. raw gas C and unreacted water vapor enter high-temperature catalytic pyrolyzer 2
,there is catalytic pyrolysis and steam reforming reaction therein, and generate 900 DEG C of Pintsch process gas E.
S4. Pintsch process gas E discharges from the outlet of high-temperature catalytic pyrolyzer 2, Pintsch process gas E is introduced to pyrolysis oven 1, the Pintsch process gas E that is equivalent to former tolerance is back to pyrolysis oven, with the heat exchange of brown coal A counter current contact, brown coal are heated to 800 DEG C, coal semicoke B discharges from pyrolysis oven 1 bottom, after cooling, exports as fuel.Residue splitting gas after tornado dust collector 6, water washing tank 7, activated carbon filtration tank 8 purifying treatment as outer for combustion gas.
Taking Inner Mongol brown coal as example, its thermal value is 3500kcal/kg, and full moisture content is 34.5%, and volatile content is 35%, and ash content is 11%.Brown coal particle size range after screening is 3mm20mm, enters continuously pyrolysis oven with the speed of 50kg/h, in pyrolysis oven 1, is heated and removes moisture content, produces low pressure water vapor D; After dehydration, brown coal A is heated to 800 DEG C gradually, and pyrolysis produces coal semicoke B, and raw gas C(is containing tar) and water vapour D.The middle temperature flue gas H(800 DEG C discharging after micron fuel G burning) pass into pyrolysis oven 1, to brown coal, A heats;
Raw gas C and water vapor D enter high-temperature catalytic pyrolyzer 2, at 1100 DEG C, catalytic pyrolysis and steam reforming reaction occur.900 DEG C of high anneal crack gas E(temperature that produce) part passes back into pyrolysis oven 1 to brown coal A heating pyrolysis, and residue combustion gas is delivered to user
through cyclone dust removal 6, washing 7, activated carbon filtration 8 after processing.
Through sampling analysis, after condensation, the composition of coal gas E is: hydrogen 45.6%, methane 9.2%, carbon monoxide 25.6%, carbonic acid gas 19.6%.
All the other processing sequencees of this example are with real.
Claims (8)
1. a brown coal convection drying and thermal decomposition integrated system, it is characterized in that, this system is made up of pyrolysis oven (1), high-temperature catalytic pyrolyzer (2), surge tank (3), fuel hopper (4), gas blower (5), tornado dust collector (6), water washing tank (7) and activated carbon filtration tank (8), described pyrolysis oven (1) is made up of inner furnace and external heat chuck, the inner furnace of pyrolysis oven (1) is provided with top material inlet mouth, air outlet, top (12), bottom carbon outleting port and bottom inlet mouth (16), and the heating jacket of pyrolysis oven (1) is provided with bottom gas approach (11) and top exhanst gas outlet, high-temperature catalytic pyrolyzer (2) is provided with top inlet mouth (13), top exhanst gas outlet (10), air outlet, bottom (14) and bottom fuel inlet (9), and high-temperature catalytic pyrolyzer is equipped with catalyzer in (2), surge tank (3) is provided with top fuel gas inlet (15), left side gas outlet and right side gas outlet, the air outlet, top (12) of pyrolysis oven (1) inner furnace connects high-temperature catalytic pyrolyzer (2) top inlet mouth (13), the bottom inlet mouth (16) of pyrolysis oven (1) inner furnace connects surge tank (3) air outlet, left side (15), the bottom gas approach (11) of pyrolysis oven (1) external heat chuck connects the top exhanst gas outlet (10) of high-temperature catalytic pyrolyzer (2), the air outlet, bottom of high-temperature catalytic pyrolyzer (12) connects the top fuel gas inlet (15) of surge tank (3), the right side gas outlet of surge tank (3) connects the top inlet mouth (17) of tornado dust collector (6), the lower inlet (19) of tornado dust collector outlets (18) and water washing tank (7) is connected, water washing tank outlet (20) is connected with activated carbon filtration tank import (21).
2. brown coal convection drying according to claim 1 and thermal decomposition integrated system, is characterized in that, described pyrolysis oven (1) and high-temperature catalytic pyrolyzer (2) are made by high temperature resistant stainless steel, and surface is through heat-resisting processing or liner flame retardant coating.
3. brown coal convection drying according to claim 1 and thermal decomposition integrated system, it is characterized in that, described high-temperature catalytic pyrolyzer (2) is tubular structure, and raw gas (C) and water vapour (D) enter from its top, and in tube side, is heated and catalytic pyrolysis and water vapor occur heavily reacts; High-temperature flue gas is outer and raw gas counter-current flow at pipe, for whole reaction provides heat.
4. brown coal convection drying and a thermal decomposition integrated metallization processes, is characterized in that, this technique comprises the following steps:
S1. fuel is sent into burning in high-temperature catalytic pyrolyzer (2), the heat of generation is as the thermal source of catalytic pyrolysis in high-temperature catalytic pyrolyzer (2) stove;
S2. the temperature that the top exhanst gas outlet (10) of high-temperature catalytic pyrolyzer (2) is discharged is the middle temperature flue gas (H) of 500900 DEG C, enter pyrolysis oven (1) external heat chuck by gas approach (11), to brown coal raw material (A) heat drying and pyrolysis, produce semicoke (B), contain raw gas (C) and water vapor (D), flue tail gas J is emptying after purifying;
S3. raw gas (C) is discharged with unreacted water vapor (D) air outlet (12) from pyrolysis oven, enter high-temperature catalytic pyrolyzer (2) through top inlet mouth (13), at inner catalytic pyrolysis and the steam reforming reaction of occurring of high-temperature catalytic pyrolyzer (2), produce Pintsch process gas (E);
S4. the part in Pintsch process gas (E) passes back into pyrolysis oven (1) inner furnace, and as thermal source, to brown coal direct heating, remainder is after the purifying treatment such as cyclone dust removal, washing and filtration, as outer combustion gas or the synthesis material of supplying.
5. brown coal convection drying according to claim 4 and thermal decomposition integrated metallization processes, is characterized in that, described fuel adopts the biomass that particle diameter is 0.025mm0.25mm.
6. brown coal convection drying according to claim 4 and thermal decomposition integrated metallization processes, it is characterized in that, the dry and pyrolysis in described step 2 comprises first brown coal thermal dehydration, produces low pressure water vapor, then continue to heat up, pyrolysis produces coal semicoke (B), raw gas (C) and water vapour (D).
7. brown coal convection drying according to claim 4 and thermal decomposition integrated metallization processes, is characterized in that, the temperature when raw gas (C) in described step 2 and water vapor (D) go out pyrolysis oven is 300600 DEG C.
8. brown coal convection drying according to claim 4 and thermal decomposition integrated metallization processes, is characterized in that, the temperature of the Pintsch process gas E in described step 4 in the time entering pyrolysis oven is 7001000 DEG C;
Brown coal convection drying according to claim 4 and thermal decomposition integrated metallization processes, is characterized in that, the raw gas (C) in described step 4 is after catalytic pyrolysis and steam reforming reaction, and Pintsch process gas (E) temperature of generation is 800-1000 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310034572.7A CN103074093B (en) | 2013-01-30 | 2013-01-30 | Integral process and system for directly drying and pyrolyzing lignite |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310034572.7A CN103074093B (en) | 2013-01-30 | 2013-01-30 | Integral process and system for directly drying and pyrolyzing lignite |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103074093A CN103074093A (en) | 2013-05-01 |
| CN103074093B true CN103074093B (en) | 2014-07-02 |
Family
ID=48150795
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310034572.7A Expired - Fee Related CN103074093B (en) | 2013-01-30 | 2013-01-30 | Integral process and system for directly drying and pyrolyzing lignite |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103074093B (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104046371B (en) * | 2013-12-26 | 2016-05-25 | 聂红军 | One is utilized fixed bed brown coal drying device destructive distillation brown coal technique and system |
| CN105778953A (en) * | 2016-05-19 | 2016-07-20 | 北京神雾环境能源科技集团股份有限公司 | Oil shale pyrolysis and cracking tube system |
| CN105802685B (en) * | 2016-05-19 | 2019-02-01 | 神雾科技集团股份有限公司 | A kind of pyrolysis of coal and cracking tube cracking produce gas and combine gas power generation system |
| CN107057724A (en) * | 2016-12-31 | 2017-08-18 | 北京万机汇机电工程技术有限公司 | A kind of heat scission reaction system and its application |
| CN107880944B (en) * | 2017-12-15 | 2024-03-19 | 浙江天禄环境科技有限公司 | Three-stage dedusting cooling and automatic air locking device for lignite gasification reduction |
| CN109140427A (en) * | 2018-09-30 | 2019-01-04 | 西安鑫顶天装备智能科技有限公司 | A kind of combustion gas fission device |
| CN110862835A (en) * | 2019-12-03 | 2020-03-06 | 嘉禾聚能（天津）科技有限公司 | System for producing fuel gas |
| CN111100711A (en) * | 2019-12-27 | 2020-05-05 | 长沙万利节能科技有限公司 | Biomass thermal cracking gasification method |
| CN111607407A (en) * | 2020-06-15 | 2020-09-01 | 云南中翼鼎东投资集团生物科技开发有限公司 | Lignite mineral source soil conditioner and preparation method thereof |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE19945771C1 (en) * | 1999-09-24 | 2001-02-22 | Muehlen Gmbh & Co Kg Dr | Process for gasifying organic materials comprises cracking the materials by contacting with a hot heat carrier medium which is removed from a solid carbonaceous residue after leaving the pyrolysis reactor and conveyed to a heating zone |
| JP3973840B2 (en) * | 2001-01-18 | 2007-09-12 | 独立行政法人科学技術振興機構 | Solid fuel gasifier |
| CN1262624C (en) * | 2004-12-16 | 2006-07-05 | 太原理工大学 | Combined process for dry distillation of coal and production of carbon black by plasma cracking |
| US20080016769A1 (en) * | 2006-07-24 | 2008-01-24 | Clean Energy, L.L.C. | Conversion of carbonaceous materials to synthetic natural gas by pyrolysis, reforming, and methanation |
| CN101045524B (en) * | 2007-05-04 | 2010-05-19 | 大连理工大学 | Method for preparing hydrogen-riched gas by solid fuel catalytic gasification |
| CN100459267C (en) * | 2007-07-03 | 2009-02-04 | 山东省科学院能源研究所 | Biomass hydrogen energy electric generation method |
| CN102010759A (en) * | 2010-12-14 | 2011-04-13 | 大连理工大学 | Method and device for producing hydrogen-rich gases by catalyzing and gasifying solid fuels |
-
2013
- 2013-01-30 CN CN201310034572.7A patent/CN103074093B/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN103074093A (en) | 2013-05-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103074093B (en) | Integral process and system for directly drying and pyrolyzing lignite | |
| CN102977927A (en) | Apparatus for preparing synthesis gas based on dual fluidized bed biomass gasification and preparation method thereof | |
| CN105588127B (en) | Using the boiler combustion system of biomass gasification device | |
| CN108913175A (en) | A kind of combined cycle system and its application method based on abandoned biomass catalytic pyrolysis product processing organic wastewater | |
| CN105542806A (en) | Device and method for producing clean fuel gas and biomass charcoal through continuous biomass carbonization | |
| CN105387459A (en) | Low-order ash coal graded utilization system and technology | |
| CN101508902A (en) | Biomass fuel cycle gasifying device and method thereof | |
| CN204727845U (en) | A kind of Multifunction sectional type biomass pyrolysis device | |
| CN108675588A (en) | Sludge high-drying charing process system | |
| CN206127211U (en) | Continuous pyrolysis and carbonization device of living beings | |
| CN106947541B (en) | Combined method and system for hydrogen production based on low-rank coal pyrolysis water vapor coke quenching water gas | |
| CN204369820U (en) | Biomass gasifying furnace waste heat comprehensive utilization system | |
| CN104479742B (en) | Biomass gas preparation system | |
| CN216786049U (en) | Device for preparing charcoal by biomass pyrolysis | |
| CN207756595U (en) | A kind of electricity generation system of debirs clean utilization | |
| CN203683468U (en) | System of medium and low temperature pyrolysis of low-rank coal by use of heat of high-temperature coke oven gas | |
| CN110129077A (en) | Pyrolytic process | |
| CN212769855U (en) | System for preparing hydrogen by pyrolyzing waste plastics | |
| CN105950196B (en) | A kind of pyrolysis of coal and cracking production of synthetic gas system | |
| CN205313462U (en) | System for be arranged in low temperature dry distillation of coal | |
| CN204369821U (en) | There is the biomass gasifying furnace that secondary tar filters | |
| CN204369819U (en) | From preheating biomass gasifying furnace | |
| CN114196425A (en) | Process method and device for preparing charcoal by biomass pyrolysis | |
| CN107267217A (en) | Biomass carbonization Quick-gasifying system | |
| CN209536987U (en) | A kind of coal preparing active carbon system being pyrolyzed and activation is combined |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140702 Termination date: 20160130 |