CN105018121A - Gas, tar and activated carton co-production system - Google Patents
Gas, tar and activated carton co-production system Download PDFInfo
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- CN105018121A CN105018121A CN201510477423.7A CN201510477423A CN105018121A CN 105018121 A CN105018121 A CN 105018121A CN 201510477423 A CN201510477423 A CN 201510477423A CN 105018121 A CN105018121 A CN 105018121A
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Abstract
The invention discloses a gas, tar and activated carton co-production system. The system comprises a pyrolysis furnace, an activation furnace and a cooling furnace which are sequentially communicated. The pyrolysis furnace comprises a preheat furnace body and a pyrolysis furnace body, a coal inlet and a pyrolyzing gas outlet are formed in one end of the preheat furnace body, a heat-isolation jacket is disposed on the outer side of the activation furnace, and a heating chamber is formed between the activation furnace and the heat-isolation jacket; one end of the cooling furnace is connected with a discharge box, an activated carbon outlet and a cooling gas inlet are formed in the discharge box, a cooling jacket is arranged on the outer side of the cooling furnace, and a cooling chamber is formed between the cooling furnace and the cooling jacket; a cooling water inlet and a steam outlet are formed in the cooling jacket, and the steam outlet is communicated with the cooling gas inlet. Semicoke activated associated gas is used in the system to supply heat for pyrolysis, pyrolysis efficiency is improved, and meanwhile the content of nitrogen in pyrolysis gas is reduced. Mixed gas of carbon dioxide and water vapor can preheat the cooling furnace when passing through the cooling furnace and can prepare for being introduced in the activation furnace and serving as a gas activation agent, and activated carbon can be effectively cooled.
Description
Technical field
The invention belongs to pyrolysis gas, tar and Activated Carbon Production technical field, specifically relate to the co-generation system of a kind of pyrolysis gas, tar and gac.
Background technology
Gac is a kind of loose porous class carbonaceous material, has adsorption, is widely used in the industries such as chemical industry, medicine, environmental protection.Blue charcoal, i.e. semicoke, be the solid matter of a kind of high fixed carbon content that in a kind of employing, low-temperature pyrolysis explained hereafter goes out, by-product tar and coke-oven gas while producing semicoke, semicoke can be widely used in the productive life fields such as calcium carbide, iron alloy, gac preparation and city resident's cleaning coal.Tar purposes is very extensive, and can produce clean fuel oil, be also the important source material of the organic chemical industries such as synthetic plastics, dyestuff, fiber, rubber, agricultural chemicals, medicine, high temperature material; Coke-oven gas can be used for generating, metallurgy, hydrogen making, synthetic ammonia, methyl alcohol, Chemicals and the industrial calcining thermal source etc. such as stupid.
At present, domestic and international coal retorting technique comprises: the external-heat horizontally-arranged revolution charring furnace pyrolytic process etc. of the Toscoal technique of external-heat vertical heater technique, internal heat type vertical heater technique, the U.S., the LR technique of Germany, USSR (Union of Soviet Socialist Republics) 3TX (ETCH)-175 technique, the fluid bed fast pyrolysis technique of Australia, Chinese multistage rotary kiln technique, Chinese solid thermal carriers new distillation process, Xi'an Sanrui Industrial Co., Ltd..It is use the most at present that internal thermal upright carbonization furnace thermo-cracking prepares blue charcoal technique, and the technique of blue charcoal prepared by largest, maximum a kind of cracking raw coal.Technical process is mainly: feed coal vertically adds coke oven continuously by coal bunker on body of heater top, retort section is fallen into after preheating, retort section pyrolysis temperature is 600 DEG C ~ 700 DEG C, after destructive distillation heat used mixes with air primarily of firing tunnel in coking furnace in quirk, be blown into retort section by gas blower through burner to burn, retort section bottom coke falls into water sealed tank cooling, then discharges.Raw gas is indoor along bed of material rising in destructive distillation, and by coal gas collecting hood, upcast, bridge tube successively through Venturi meter tower, rotating stream tray scrubber washing, coal gas melts down heating under the effect of blower fan, and remainder diffuses.Tar enters settling tank dehydration, and then concentrate on tar pool and carry out standing thermostatically heating and second dehydration, the tar after dehydration is processed oil.
The weak point of aforesaid method is:
1, adopt internal heat type destructive distillation, comprise large quantity of air in stove, the caloric power of gas therefore generated is lower, and wherein hydrogen, methane are lower, and a nitrogen content is too high, does not reach the top condition of chemical utilization, can only be used as fuel.
2, adopt wet method to discharge of the coke during its blue charcoal quenching process, consume the latent heat of a part of blue charcoal, and product water content is higher, affects the quality of blue charcoal, limit the use of blue charcoal, increase transportation cost, need to consume extra energy and drying is carried out to it; The exhaust steam that quenching process in addition produces contains a large amount of hazardous and noxious substances, worsens execute-in-place environment, atmosphere pollution; And a large amount of phenolic wastewater that quenching produces, aftertreatment cost intensive.
3, the tar rate of recovery is on the low side.
Summary of the invention
The object of the invention is to overcome above-mentioned deficiency of the prior art, the co-generation system of a kind of coal gas, tar and gac is provided.The accompanying gas that this co-generation system make use of semicoke activation is that pyrolysis heat supply improves pyrolysis efficiency and decreases the nitrogen content in pyrolysis gas simultaneously; The mixed gas of carbonic acid gas and water vapour can not only be carried out preheating to it by cool furnace and then prepare as gas activation agent use for passing into activation furnace, effectively can also cool gac.
For achieving the above object, the technical solution used in the present invention is: a kind of coal gas, the co-generation system of tar and gac, it is characterized in that: comprise the pyrolysis oven for carrying out preheating and pyrolysis to coal, the activation furnace activated for the semicoke produced pyrolysis and the gac for producing activation carry out the cool furnace of cooling process, described pyrolysis oven, activation furnace is communicated with successively with cool furnace, described pyrolysis oven, activation furnace and cool furnace are rotary kiln, the pyrolysis body of heater that described pyrolysis oven comprises preheating body of heater and is communicated with preheating body of heater, described preheating body of heater is provided with coal inlet and pyrolysis gas outlet away from one end of pyrolysis body of heater, the arranged outside of described activation furnace has insulating jacket, be configured between described activation furnace and insulating jacket holding the heated chamber activating heated air, described cool furnace is connected with feed box away from one end of activation furnace, described feed box is provided with gac outlet and the cooling gas inlet for passing into water vapour and carbon dioxide gas mixture in feed box, the arranged outside of described cool furnace has cooling jacket, cooling chamber is formed between described cool furnace and described cooling jacket, described cooling jacket offers entrance of cooling water and vapour outlet, described entrance of cooling water and vapour outlet all lead to described cooling chamber, described vapour outlet is connected with described cooling gas inlet.
The co-generation system of above-mentioned a kind of pyrolysis gas, tar and gac, is characterized in that: comprise the separation system for coal gas and tar being separated from pyrolysis gas, and described separation system is connected with described pyrolysis gas outlet.
Above-mentioned a kind of pyrolysis gas, the co-generation system of tar and gac, it is characterized in that: described separation system comprises the fly-ash separator for removing the dust in pyrolysis gas, for carrying out the indirect cooler of condensation process and the electrical tar precipitator for carrying out tar trapping to the oil-water mixture formed after pyrolysis gas condensation to pyrolysis gas, and the absorption tower adopting MEA solution to trap the carbonic acid gas in pyrolysis gas and desorption tower, described pyrolysis gas outlet is connected with bottom fly-ash separator, the top of described fly-ash separator is connected with the bottom of indirect cooler, the top of described indirect cooler is connected with the bottom of electrical tar precipitator, the top of described electrical tar precipitator is connected with the bottom on absorption tower, the bottom on described absorption tower is connected with the top of described desorption tower, the bottom of described desorption tower is communicated with the top on absorption tower, the top on described absorption tower is provided with gas exit, the top of described desorption tower is provided with carbon dioxide outlet, the bottom of described electrical tar precipitator is connected with tar tank.
The co-generation system of above-mentioned a kind of pyrolysis gas, tar and gac, it is characterized in that: described separation system also comprises the oil-water mixture for collecting in indirect cooler and isolates the tar ammonia settling pond of tar, described tar ammonia settling pond offers tar delivery port, coke tar refuse delivery port and ammoniacal liquor relief outlet.
The co-generation system of above-mentioned a kind of pyrolysis gas, tar and gac, is characterized in that: described tar ammonia settling pond is sealed ammonia vessel.
The co-generation system of above-mentioned a kind of pyrolysis gas, tar and gac, is characterized in that: described indirect cooler is shell and tube heat exchanger.
The co-generation system of above-mentioned a kind of pyrolysis gas, tar and gac, is characterized in that: described fly-ash separator is high-temperature cyclone dust extractor.
The present invention compared with prior art has the following advantages:
1, structure of the present invention is simple, rationally novel in design.
2, the present invention carries out indirect heating by arranging heated chamber to the semicoke in activation furnace, avoid adopting burning semicoke to provide activation thermal source, thus add Activated Carbon Production ability, turn improve the quality of gac, replace air combustion room of the prior art heat-supplying mode, decrease the nitrogen content in coal gas.
3, the present invention is when cooling gac, by the indirect type of cooling and direct cooling direction being combined, can realize fully, thoroughly cooling gac, and can guarantee that the water ratio of gac is lower, improve the quality of gac.
4, the present invention passes through separation system, burnt oil and gas effectively can be separated from pyrolysis gas, and by can caloric power of gas be improved to the trapping of carbonic acid gas, additionally reduce the quantity discharged of carbonic acid gas simultaneously, avoid the impact that the existence of carbonic acid gas produces caloric power of gas.
5, separation system of the present invention is by arranging tar ammonia settling pond, can be further processed the pyrolysis gas oil-water mixture that condensation is formed in indirect cooler, from described oil-water mixture, effectively isolate tar, improve productive rate and the rate of recovery of tar.
6, fly-ash separator of the present invention adopts high-temperature cyclone dust extractor.By adopting high-temperature cyclone dust extractor, can ensure that the temperature in fly-ash separator is in the condition of high temperature, effectively to reduce heavy oil condensation in fly-ash separator.
7, raw material particle size of the present invention is less than or equal to the fine coal of 6mm, can make full use of small particle size coal.
Below by drawings and Examples, technical scheme of the present invention is described in further detail.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention.
Fig. 2 is the A-A sectional drawing in Fig. 1.
Fig. 3 is the B-B sectional drawing in Fig. 1.
Description of reference numerals:
1-pyrolysis oven; 1-1-preheating body of heater; 1-2-pyrolysis body of heater;
1-3-coal inlet; 1-4-pyrolysis gas outlet; 1-5-power set;
1-6-master wheel; 1-7-the first support roller; 1-8-the first supporting roller base;
2-activation furnace; 2-1-the second support roller; 2-2-the second supporting roller base;
2-3-the first bearing; 3-insulating jacket; 3-1-activation heat air import;
3-2-activation heat air outlet; 4-heated chamber; 5-cooling jacket;
5-1-entrance of cooling water; 5-2-vapour outlet; 6-cooling chamber;
7-cool furnace; 7-1-the 3rd support roller; 7-2-the 3rd supporting roller base;
7-3-the second bearing; 8-feed box; 8-1-gac outlet;
8-2-cooling gas inlet; 9-fly-ash separator; 10-indirect cooler;
11-electrical tar precipitator; 12-absorption tower; 12-1-gas exit;
13-desorption tower; 13-1-carbon dioxide outlet; 14-carbon dioxide storage tank;
15-tar tank; 16-tar medial launder; 17-tar slag chute;
18-tar ammonia settling pond; 19-ammoniacal liquor accumulator tank.
Embodiment
As Fig. 1, a kind of coal gas shown in Fig. 2 and Fig. 3, the co-generation system of tar and gac, comprise the pyrolysis oven 1 for carrying out preheating and pyrolysis to coal, the activation furnace 2 activated for the semicoke produced pyrolysis and the gac for producing activation carry out the cool furnace 7 of cooling process, described pyrolysis oven 1, activation furnace 2 is communicated with successively with cool furnace 7, described pyrolysis oven 1, activation furnace 2 and cool furnace 7 are rotary kiln, the pyrolysis body of heater 1-2 that described pyrolysis oven 1 comprises preheating body of heater 1-1 and is communicated with preheating body of heater 1-1, described preheating body of heater 1-1 is provided with coal inlet 1-3 and pyrolysis gas outlet 1-4 away from one end of pyrolysis body of heater 1-2, the arranged outside of described activation furnace 2 has insulating jacket 3, be configured for holding the heated chamber 4 activating heated air between described activation furnace 2 and insulating jacket 3, wherein, described insulating jacket 3 offers activation heat air import 3-1 and activation heat air outlet 3-2, described activation heat air import 3-1 and activation heat air outlet 3-2 all leads to described heated chamber 4, described cool furnace 7 is connected with feed box 8 away from one end of activation furnace 2, described feed box 8 is provided with gac outlet 8-1 and the cooling gas inlet 8-2 for passing into water vapour and carbon dioxide gas mixture in feed box 8, the arranged outside of described cool furnace 7 has cooling jacket 5, cooling chamber 6 is formed between described cool furnace 7 and described cooling jacket 5, described cooling jacket 5 offers entrance of cooling water 5-1 and vapour outlet 5-2, described entrance of cooling water 5-1 and vapour outlet 5-2 all leads to described cooling chamber 6, described vapour outlet 5-2 is connected with described cooling gas inlet 8-2.
In the present embodiment, this co-generation system in use, described pyrolysis oven 1, activation furnace 2 and cool furnace 7 synchronous revolving, fine coal adds in the preheating body of heater 1-1 of pyrolysis oven 1 from coal inlet 1-3, fine coal after preheating enters in the pyrolysis body of heater 1-2 of pyrolysis oven 1, in pyrolysis body of heater 1-2, pulverized coal pyrolysis produces pyrolysis gas and semicoke, wherein pyrolysis gas exports from described pyrolysis gas outlet 1-4 to isolate coal gas and tar further, wherein semicoke enters activation in activation furnace 2 and produces gac, and gac enters in cool furnace 7 and enters feed box 8 again after cooling.
In the present embodiment, this co-generation system carries out indirect heating by the semicoke arranged in heated chamber 4 pairs of activation furnaces 2, avoid adopting burning semicoke to provide activation thermal source, thus add Activated Carbon Production ability, turn improve the quality of gac, replace air combustion room of the prior art heat-supplying mode, decrease the nitrogen content in coal gas.In addition, enter pyrolysis body of heater 1-2 for pulverized coal pyrolysis by the accompanying gas produced in activation furnace 2 and heat is provided, then enter the preheating that preheating body of heater 1-1 is fine coal heat is provided.In the present embodiment, because the gas activation agent passed in activation furnace 2 is the mixed gas of water vapour and carbonic acid gas, in the process of semicoke activation, create associated gas and CO and H
2mixed gas, H contained in described associated gas
2and then realize hydropyrolysis, improve the productive rate of tar and the quality of coal gas greatly.Described water vapour and the mixed gas of carbonic acid gas pass into feed box 8 and then contact gac by cool furnace 7 directly to cool, and the mixed gas of water vapour and carbonic acid gas is also preheated to enter in activation furnace 2 again and uses as gas activation agent while cooling gac.And, this co-generation system is when cooling gac, by the cooling performance considerably increased gac that the indirect type of cooling and direct cooling direction are combined, wherein, the mixed gas that direct cooling mode is above-mentioned water vapour and carbonic acid gas in cool furnace 7 to the direct cooling of gac, the described indirect type of cooling for pass into water coolant by entrance of cooling water 5-1 in cooling chamber 6, water coolant cools indirectly to gac in cool furnace 7 in a non-contact manner, while cooling gac, water coolant is heated to form vapor form and is delivered to cooling gas inlet 8-2 to form cooling gas for directly cooling with carbon dioxide mix from vapour outlet 5-2.
In the present embodiment, described pyrolysis oven 1, activation furnace 2 are communicated with successively with cool furnace 7, synchronous when turning round, so, described pyrolysis oven 1, activation furnace 2 and cool furnace 7 needs power set 1-5, described power set 1-5 drives the master wheel 1-6 on pyrolysis oven 1, and described master wheel 1-6 drives the preheating body of heater 1-1 of pyrolysis oven 1 and pyrolysis body of heater 1-2 to rotate, the first supporting roller base 1-8 that the two ends of described pyrolysis oven 1 are provided with the first support roller 1-7 and match with described first support roller 1-7.The second supporting roller base 2-2 that described activation furnace 2 is provided with the second support roller 2-1 near the part of pyrolysis oven 1 and matches with described second support roller 2-1.The 3rd supporting roller base 7-2 that described cool furnace 7 is provided with the 3rd support roller 7-1 near the part of feed box 8 and matches with described 3rd support roller 7-1.The bottom of described activation furnace 2 is provided with the first bearing 2-3, and the bottom of described cool furnace 7 is provided with the second bearing 7-3.Wherein, the step-down gear that described power set 1-5 comprises motor and is connected with motor-driven, the output shaft of described step-down gear is provided with the pinion(gear) be meshed with described master wheel 1-6.
In the present embodiment, this co-generation system also comprises the separation system for coal gas and tar being separated from pyrolysis gas, and described separation system is connected with described pyrolysis gas outlet 1-4.
As shown in Figure 1, described separation system comprises the fly-ash separator 9 for removing the dust in pyrolysis gas, for carrying out the indirect cooler 10 of condensation process and the electrical tar precipitator 11 for carrying out tar trapping to the oil-water mixture formed after pyrolysis gas condensation to pyrolysis gas, and the absorption tower 12 adopting MEA solution to trap the carbonic acid gas in pyrolysis gas and desorption tower 13, described pyrolysis gas outlet 1-4 is connected with bottom fly-ash separator 9, the top of described fly-ash separator 9 is connected with the bottom of indirect cooler 10, the top of described indirect cooler 10 is connected with the bottom of electrical tar precipitator 11, the top of described electrical tar precipitator 11 is connected with the bottom on absorption tower 12, the bottom on described absorption tower 12 is connected with the top of described desorption tower 13, the bottom of described desorption tower 13 is communicated with the top on absorption tower 12, the top on described absorption tower 12 is provided with gas exit 12-1, the top of described desorption tower 13 is provided with carbon dioxide outlet 13-1, the bottom of described electrical tar precipitator 11 is connected with tar tank 15.
In the present embodiment, described separation system in use, first by fly-ash separator 9, the dust in pyrolysis gas is effectively tackled, condensation is carried out again by indirect cooler 10 pairs of pyrolysis gas, oil-water mixture and low temperature coal gas is formed after pyrolysis gas condensation, wherein low temperature coal gas enters and sends into electrical tar precipitator 11 and carry out tar trapping and remove tar in low temperature coal gas, the tar trapped in electrical tar precipitator 11 is delivered in tar tank 15, remaining coal gas enters bottom absorption tower 12, coal gas flows from bottom to top, lean solution is from the tower top on absorption tower 12 from top to bottom Continuous Flow, contact with the coal gas upwards passed into, carbonic acid gas in coal gas and MEA solution generation chemical reaction, carbonic acid gas is absorbed by MEA solution, coal gas after purification exports from the gas exit 12-1 at top, absorption tower 12, carbonic acid gas is while absorption, liquid discharges reaction heat, rich solution is admitted to the tower top of desorption tower 13, desorption tower 13 provides heat by reboiler, produce a large amount of steam, steam in desorption tower 13 on flowing, contact with the rich solution flowed down, rich solution is after heating and steam stripped dual function, carbonic acid gas gradually from rich solution desorb discharge, rich solution becomes lean solution, the top that described lean solution is delivered to absorption tower 12 from the bottom of desorption tower 13 again utilizes again, the carbonic acid gas separating sucking-off is delivered to carbon dioxide storage tank 14 from the carbon dioxide outlet 13-1 at desorption tower 13 top, and then provide activator for the activation of semicoke in activation furnace 2.
In the present embodiment, this separation system, by improving caloric power of gas to the trapping of carbonic acid gas, additionally reduces the quantity discharged of carbonic acid gas simultaneously, avoids the impact that the existence of carbonic acid gas produces caloric power of gas.
As shown in Figure 1, described separation system also comprises for collecting oil-water mixture bottom indirect cooler 10 and isolating the tar ammonia settling pond 18 of tar, described tar ammonia settling pond 18 offers tar delivery port, coke tar refuse delivery port and ammoniacal liquor relief outlet.By arranging tar ammonia settling pond 18, can be further processed the pyrolysis gas oil-water mixture that condensation is formed in indirect cooler 10, from described oil-water mixture, effectively isolating tar, improve the productive rate of tar.Wherein, described tar delivery port is connected with tar medial launder 16, and described tar medial launder 16 is connected with tar tank 15, and described coke tar refuse delivery port is connected with tar slag chute 17, and described ammoniacal liquor relief outlet is connected with ammoniacal liquor accumulator tank 19.
In the present embodiment, described tar ammonia settling pond 18 is sealed ammonia vessel.Described indirect cooler 10 is shell and tube heat exchanger.
In the present embodiment, described fly-ash separator 9 is high-temperature cyclone dust extractor.By adopting high-temperature cyclone dust extractor, can ensure that the temperature in fly-ash separator 9 is in the condition of high temperature, effectively to reduce heavy oil condensation in fly-ash separator 9.
The above; it is only preferred embodiment of the present invention; not the present invention is imposed any restrictions, every above embodiment is done according to the technology of the present invention essence any simple modification, change and equivalent structure transformation, all still belong in the protection domain of technical solution of the present invention.
Claims (7)
1. a coal gas, the co-generation system of tar and gac, it is characterized in that: comprise the pyrolysis oven (1) for carrying out preheating and pyrolysis to coal, the activation furnace (2) activated for the semicoke produced pyrolysis and the gac for producing activation carry out the cool furnace (7) of cooling process, described pyrolysis oven (1), activation furnace (2) is communicated with successively with cool furnace (7), described pyrolysis oven (1), activation furnace (2) and cool furnace (7) are rotary kiln, the pyrolysis body of heater (1-2) that described pyrolysis oven (1) comprises preheating body of heater (1-1) and is communicated with preheating body of heater (1-1), described preheating body of heater (1-1) is provided with coal inlet (1-3) and pyrolysis gas outlet (1-4) away from one end of pyrolysis body of heater (1-2), the arranged outside of described activation furnace (2) has insulating jacket (3), be configured between described activation furnace (2) and insulating jacket (3) holding the heated chamber (4) activating heated air, described cool furnace (7) is connected with feed box (8) away from one end of activation furnace (2), described feed box (8) is provided with gac outlet (8-1) and the cooling gas inlet (8-2) for passing into water vapour and carbon dioxide gas mixture in feed box (8), the arranged outside of described cool furnace (7) has cooling jacket (5), cooling chamber (6) is formed between described cool furnace (7) and described cooling jacket (5), described cooling jacket (5) offers entrance of cooling water (5-1) and vapour outlet (5-2), described entrance of cooling water (5-1) and vapour outlet (5-2) all lead to described cooling chamber (6), described vapour outlet (5-2) is connected with described cooling gas inlet (8-2).
2. the co-generation system of a kind of pyrolysis gas according to claim 1, tar and gac, it is characterized in that: comprise the separation system for coal gas and tar being separated from pyrolysis gas, described separation system is connected with described pyrolysis gas outlet (1-4).
3. a kind of pyrolysis gas according to claim 2, the co-generation system of tar and gac, it is characterized in that: described separation system comprises the fly-ash separator (9) for removing the dust in pyrolysis gas, for carrying out the indirect cooler (10) of condensation process and the electrical tar precipitator (11) for carrying out tar trapping to the oil-water mixture formed after pyrolysis gas condensation to pyrolysis gas, and the absorption tower (12) adopting MEA solution to trap the carbonic acid gas in pyrolysis gas and desorption tower (13), described pyrolysis gas outlet (1-4) is connected with fly-ash separator (9) bottom, the top of described fly-ash separator (9) is connected with the bottom of indirect cooler (10), the top of described indirect cooler (10) is connected with the bottom of electrical tar precipitator (11), the top of described electrical tar precipitator (11) is connected with the bottom of absorption tower (12), the bottom on described absorption tower (12) is connected with the top of described desorption tower (13), the bottom of described desorption tower (13) is communicated with the top of absorption tower (12), the top on described absorption tower (12) is provided with gas exit (12-1), the top of described desorption tower (13) is provided with carbon dioxide outlet (13-1), the bottom of described electrical tar precipitator (11) is connected with tar tank (15).
4. the co-generation system of a kind of pyrolysis gas according to claim 3, tar and gac, it is characterized in that: described separation system also comprises the oil-water mixture for collecting in indirect cooler (10) and isolates the tar ammonia settling pond (18) of tar, and described tar ammonia settling pond (18) offers tar delivery port, coke tar refuse delivery port and ammoniacal liquor relief outlet.
5. the co-generation system of a kind of pyrolysis gas according to claim 4, tar and gac, is characterized in that: described tar ammonia settling pond (18) is sealed ammonia vessel.
6. the co-generation system of a kind of pyrolysis gas according to claim 3, tar and gac, is characterized in that: described indirect cooler (10) is shell and tube heat exchanger.
7. the co-generation system of a kind of pyrolysis gas according to claim 3, tar and gac, is characterized in that: described fly-ash separator (9) is high-temperature cyclone dust extractor.
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| CN105694935A (en) * | 2016-04-06 | 2016-06-22 | 府谷县三联煤电化工有限责任公司 | Dry distillation and activation integrated furnace for pulverized coal |
| CN106336876A (en) * | 2016-10-25 | 2017-01-18 | 江汉大学 | Small Chinese medicine residue carbonization furnace |
| CN106336876B (en) * | 2016-10-25 | 2022-05-31 | 江汉大学 | Miniaturized traditional Chinese medicine residue carbonization furnace |
| CN112094660A (en) * | 2020-07-22 | 2020-12-18 | 宁夏杰润生物科技有限公司 | Full-automatic feeding and discharging ultralong biomass pyrolysis furnace |
| CN112094655A (en) * | 2020-07-22 | 2020-12-18 | 宁夏杰润生物科技有限公司 | Ultralong biomass pyrolysis furnace |
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