CN203715567U - Rolling type biomass pyrolysis poly-generation device - Google Patents
Rolling type biomass pyrolysis poly-generation device Download PDFInfo
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- CN203715567U CN203715567U CN201420027279.8U CN201420027279U CN203715567U CN 203715567 U CN203715567 U CN 203715567U CN 201420027279 U CN201420027279 U CN 201420027279U CN 203715567 U CN203715567 U CN 203715567U
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- roller
- pyrolysis
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- roller press
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
Abstract
The utility model belongs to the technical field of utilization of biomass energy, and particularly relates to a rolling type biomass pyrolysis poly-generation device. The device comprises a hopper, a feeding system, a drying system, a rolling type pyrolysis reactor, a gas and solid separation system, a pyrolysis gas condensation system, a flammable gas combustion system, a solid coke collecting box, a liquid collecting box and a flammable gas storage tank, wherein the rolling type pyrolysis reactor consists of a bearing belt, a transmission roller, a driving system, a sealed reaction chamber, a high-temperature smoke heat exchanger coil tube and a multi-stage heat transmission compression roller. A biomass raw material is dried and then sent to the rolling type pyrolysis reactor, runs on the bearing belt and is subjected to forced rolling by the multi-stage heat transmission compression roller and rapidly pyrolyzed; a part of the flammable gas as one of pyrolysis products is combusted to obtain high-temperature flue gas for heating the surface of the roller and providing heat needed by biomass pyrolysis. By adopting the multi-stage heat transmission compression roller, the device can be used for implementing the forced rolling and heat transmission of the biomass raw material, so that rapid pyrolysis of the biomass raw material is realized and a self-heating pyrolysis process is realized.
Description
Technical field
The utility model belongs to biomass energy utilization technologies field, is specifically related to a kind of device of roller press type biomass pyrolytic Poly-generation.
Background technology
Pyrolysis is that a kind of important biomass are utilized technology.When biomass are carried out pyrolysis under oxygen free condition, formed solid-liquid-gas three phase pyrolysis product, there is higher grade and using value, so this research obtained the extensive concern of lot of domestic and foreign R&D institution, and core technology is wherein the development of reactor.
Biomass pyrolysis under oxygen free condition is an endothermic process, and need provides heat continually in reaction; Yet biomass are again a kind of poor conductors of heat, be difficult to the intensification of being heated rapidly.Therefore, be applicable to the reactor of biomass pyrolytic under oxygen free condition, its development key is: (1) can make the required heat of biomass pyrolytic enter inside reactor; (2) can make biomass absorb enough heats and complete pyrolytic reaction.Conventional biomass pyrolysis reactor, consider the thermal conductivity of biomass extreme difference, for making fully pyrolysis of biomass material, general one of following two kinds of method of design that adopt: (1) extends the residence time of biomass in pyrolysis reactor, make heat can fully be delivered to the inside of biological particles, thereby realize the abundant pyrolysis of biomass; (2) adopt superfine biological particles, make biological particles abundant decomposes just at short notice.Generally speaking, above-mentioned two principle of design, or can reduce the processing efficiency (extend pyrolytic reaction time) of reactor, or can increase the pre-treatment cost (adopting superfine biological particles) of raw material.If solve above-mentioned two technical problems simultaneously, must significantly improve the structure of reactor, be a revolutionary job.
Summary of the invention
The purpose of this utility model is to overcome the deficiencies in the prior art, and a kind of device of roller press type biomass pyrolytic Poly-generation is provided.
The utility model provides a kind of device of roller press type biomass pyrolytic Poly-generation, and this device comprises:
Hopper, feed system, dehumidification system, roller press type pyrolysis reactor, gas solid separation system, pyrolysis gas condenser system, combustible gas firing system, solid coke collection box, liquid collecting case, combustible gas storage tank; Described roller press type pyrolysis reactor comprises support band, live roll, drive system, enclosed reaction chamber, high-temperature flue gas heat exchange coil and Multi-stage transmission hot-pressing roller, described Multi-stage transmission hot-pressing roller is arranged in pairs along support band direction, pressure roller running horizontal tangential is identical with raw material transmission direction, foremost is one-level heat transfer pressure roller I, be followed successively by backward two-stage heat transmission pressure roller II,, final stage heat transfer pressure roller N, wherein, N is more than or equal to 1 integer; For example, heat transfer pressure roller N is even XX level of I level, II level, III level or X level.
Wherein, the outlet of hopper is connected with the entrance of feed system, and the outlet of feed system is connected with dehumidification system entrance, and the outlet of dehumidification system is connected with the top opening for feed of roller press type pyrolysis reactor; The outlet of roller press type pyrolysis reactor side top is connected with the import of gas solid separation system, and below discharge port is connected with solid coke collection box entrance; The air outlet of gas solid separation system is connected with the import of pyrolysis gas condenser system; The liquid-phase outlet of pyrolysis gas condenser system is connected with the entrance of liquid collecting case, and gaseous phase outlet is divided into two-way, and a road is connected with the entrance of combustible gas firing system, and another road is connected with combustible gas storage tank entrance.The entrance of the high-temperature flue gas heat exchange coil in the Multi-stage transmission hot-pressing roller of the outlet of combustible gas firing system and roller press type pyrolysis reactor is connected; The outlet of high-temperature flue gas heat exchange coil and the smoke inlet of dehumidification system of Multi-stage transmission hot-pressing roller are connected; Multi-stage transmission hot-pressing roller is connected with the drive system outside being placed in enclosed reaction chamber; Every grade of heat transfer roller structure is identical, is hollow devices, internal layout high-temperature flue gas heat exchange coil; Described support band arranges ringwise, and two ends arrange protective grating; Respectively there is a transmission shaft at the two ends of support band, and one of them is main drive shaft, and another is driven shaft; It is indoor that driven shaft is placed in sealed reaction completely, main drive shaft be placed in enclosed reaction chamber outside drive system be connected.
Preferably, feed system is feeding screw or endless belt conveyor.
Preferably, gas solid separation system is at least one in cyclonic separator or sack cleaner or gravity settling chamber.
Preferably, pyrolysis gas condenser system is spray congealing system, falling liquid film condenser system or spraying and falling liquid film composite condensation system.
Preferably, described dehumidification system is fluidized bed drying system or heat accumulating type dehumidification system.
Preferably, in Multi-stage transmission hot-pressing roller, the gap between every pair of pressure roller is adjustable between 0.1mm-5cm; For example the gap between every pair of pressure roller can be 0.5mm or 1cm.
The beneficial effects of the utility model are:
Roller press type biomass pyrolytic multi-joint-production apparatus described in the utility model, its core is roller press type pyrolysis reactor, biomass material is realized transmission by support band in this reactor, and by the heat transfer pressure roller of multistage high temperature, material is forced to roll-in and heat transfer, thereby realize the quick decomposes of biomass material, its advantage mainly comprises: (1) rate of heat transfer is high, pyrolysis rate is fast, pressure roll-in by high temperature pressure roller to biomass material, increased greatly the contact area between high temperature roll surface and biomass material, thereby realize between high temperature roll surface and biomass material contacting cmpletely, complete and force to conduct heat, make the rapid decomposes of biomass, (2) adaptability to raw material is wide, and owing to forcing roll-in can significantly improve pyrolytic reaction speed, so the wide adaptability to raw material geometrical property, the biomass material of no matter whether pulverizing, all can directly send into pyrolysis reactor and force roll compacted pyrogenically, (3) regulation and control of pyrolytic reaction condition are convenient, by controlling the conditions such as the transmission speed of support band, the temperature of combustion of high-temperature flue gas and flow, can adjust easily the parameters such as pyrolysis reaction temperature, reaction times, thereby according to different materials, regulate and control different pyrolytic reactions, realize high-efficiency thermal decomposition and transform, (4) without using carrier gas, biomass material carries out transmission by support band, and reactor is interior without using carrier gas, thereby can make structure of reactor more compact, the power loss of also having avoided carrier gas intensification and condensation process to cause simultaneously, (5) self-heated pyrolysis process, the combustible gas burning that the biomass pyrolytic of take generates is thermal source, provides biomass pyrolytic required heat, thereby realizes the pyrolysis Poly-generation process of autothermal.
Accompanying drawing explanation
The device schematic diagram of Fig. 1---biomass pyrolytic Poly-generation of the present utility model.
Fig. 2---the structural representation of roller press type pyrolysis reactor of the present utility model.
Number in the figure:
1-hopper; 2-feed system; 3-dehumidification system; 4-roller press type pyrolysis reactor; 5-gas solid separation system; 6-pyrolysis gas condenser system; 7 combustible gas combustion heat supplying systems; 8-solid coke collection box; 9-liquid collecting case; 10-combustible gas storage tank.
41-support band; 42-live roll; 43-drive system; 44-enclosed reaction chamber; 45-high-temperature flue gas heat exchange coil; 46-Multi-stage transmission hot-pressing roller.
I-one-level heat transfer pressure roller; II-two-stage heat transmission pressure roller; N-final stage heat transfer pressure roller.
Embodiment
The utility model provides a kind of device of roller press type biomass pyrolytic Poly-generation, below in conjunction with embodiment, the utility model is described further.Apparatus structure in each embodiment is roughly the same, as illustrated in fig. 1 and 2.
Embodiment 1
In roller press type biomass pyrolytic multi-joint-production apparatus in embodiment 1, N is III.
The outlet of hopper 1 is connected with the entrance of spiral feed system 2, and the outlet of spiral feed system 2 is connected with fluidized bed drying system 3 entrances, and the outlet of fluidized bed drying system 3 is connected with the top opening for feed of roller press type pyrolysis reactor 4; The 4 side top outlets of roller press type pyrolysis reactor are connected with the import of cyclone separation system 5, and below discharge port is connected with solid coke collection box 8 entrances; The air outlet of cyclone separation system 5 is connected with the import of falling liquid film condenser system 6 with spraying; Spraying is connected with the entrance of liquid collecting case 9 with the liquid-phase outlet of falling liquid film condenser system 6, and gaseous phase outlet is divided into two-way, and a road is connected with the entrance of combustible gas firing system 7, and another road is connected with combustible gas storage tank 10 entrances.The entrance of the high-temperature flue gas heat exchange coil 45 in the Multi-stage transmission hot-pressing roller 46 of the outlet of combustible gas firing system 7 and roller press type pyrolysis reactor 4 is connected; The outlet of the high-temperature flue gas heat exchange coil 45 of Multi-stage transmission hot-pressing roller 46 is connected with the smoke inlet of fluidized bed drying system 3.
As shown in Figure 2, described roller press type pyrolysis reactor 4 comprises that support band 41, live roll 42, drive system 43, enclosed reaction chamber 44, high-temperature flue gas heat exchange coil 45 and Multi-stage transmission hot-pressing roller 46 comprise I, II, III level heat transfer pressure roller, described I, II, III level heat transfer pressure roller are arranged in pairs along support band 41 directions, pressure roller running horizontal tangential is identical with raw material transmission direction, is connected with the drive system 43 outside being placed in enclosed reaction chamber 44.Every grade of heat transfer roller structure is identical, is hollow devices, and internal layout high-temperature flue gas heat exchange coil 45 for warming mill surface, and then provides biomass pyrolytic required heat.
Described support band 41 arranges ringwise, and two ends are provided with protective grating, for preventing material landing, and are made by heat resisting corrosion-proof corrosion material; Respectively there is a transmission shaft at the two ends of support band 41, and one of them is main drive shaft, and another is driven shaft, to realize the transmission of support band 41; Driven shaft is placed in enclosed reaction chamber 44 completely, main drive shaft be placed in enclosed reaction chamber 44 outside drive system 43 be connected.
The cornstalk that is 15% by moisture content, being crushed to median size is 3mm, through hopper 1 and spiral feed system 2, sends into fluidized bed drying system 3, inlet amount is 400kg/h; Moisture content is down to 8% after drying, then enters roller press type pyrolysis reactor 4; The length of support band 41 in roller press type pyrolysis reactor 4 (transmission length) is that 5m, width are 1.2m, and travelling speed is to be 1.25min the 4m/min(solid phase residence time), the gap between every grade of pair roller is 5mm; The flue-gas temperature entering in roller press type pyrolysis reactor 4 is 700 ℃, and pyrolysis reaction temperature is 460 ℃; Pyrolysis product, after gas solid separation and pyrolysis gas condensation, obtains coke, liquid and combustible gas three-phase pyrolysis product, and productive rate is separately 105kg/h, 180kg/h and 85kg/h.
Embodiment 2
Utilize the device described in embodiment 1 to realize biomass pyrolytic Poly-generation.
The rice straw that is 16% by moisture content, being crushed to median size is 3mm, through hopper 1 and spiral feed system 2, sends into fluidized bed drying system 3, inlet amount is 300kg/h; Moisture content is down to 8% after drying, then enters roller press type pyrolysis reactor 4; The length of support band 41 in roller press type pyrolysis reactor 4 (transmission length) is that 5m, width are 1.2m, and travelling speed is to be 2min the 2.5m/min(solid phase residence time), the gap between every grade of pair roller is 4mm; The flue-gas temperature entering in roller press type pyrolysis reactor 4 is 600 ℃, and pyrolysis reaction temperature is 400 ℃; Pyrolysis product, after gas solid separation and pyrolysis gas condensation, obtains coke, liquid and combustible gas three-phase pyrolysis product, and productive rate is separately 88kg/h, 128kg/h and 58kg/h.
Embodiment 3
In utilization and embodiment 1, essentially identical device is realized biomass pyrolytic Poly-generation, only changes spiral feed system into endless belt conveyor, and fluidized bed drying system changes heat accumulating type dehumidification system into.
The natural cornstalk that is 15% by moisture content, cut to mean length be 20cm, through hopper 1 and endless belt conveyor 2, send into heat accumulating type dehumidification system 3, inlet amount is 300kg/h; Moisture content is down to 9% after drying, then enters roller press type pyrolysis reactor 4; The length of support band 41 in roller press type pyrolysis reactor 4 (transmission length) is that 5m, width are 1.2m, and travelling speed is to be 1.67min the 3m/min(solid phase residence time), the gap between every grade of pair roller is 5.5mm; The flue-gas temperature entering in roller press type pyrolysis reactor 4 is 650 ℃, and pyrolysis reaction temperature is 430 ℃; Pyrolysis product, after gas solid separation and pyrolysis gas condensation, obtains coke, liquid and combustible gas three-phase pyrolysis product, and productive rate is separately 84kg/h, 135kg/h and 61kg/h.
Embodiment 4
In utilization and embodiment 1, essentially identical device is realized biomass pyrolytic Poly-generation, only changes III level heat transfer pressure roller into II level heat transfer pressure roller.
The cornstalk that is 15% by moisture content, being crushed to median size is 3mm, through hopper 1 and spiral feed system 2, sends into fluidized bed drying system 3, inlet amount is 300kg/h; Moisture content is down to 7% after drying, then enters roller press type pyrolysis reactor 4; The length of support band 41 in roller press type pyrolysis reactor 4 (transmission length) is that 5m, width are 1.2m, and travelling speed is to be 1.67min the 3m/min(solid phase residence time), the gap between every grade of pair roller is 4.5mm; The flue-gas temperature entering in roller press type pyrolysis reactor 4 is 700 ℃, and pyrolysis reaction temperature is 480 ℃; Pyrolysis product, after gas solid separation and pyrolysis gas condensation, obtains coke, liquid and combustible gas three-phase pyrolysis product, and productive rate is separately 74kg/h, 134kg/h and 66kg/h.
Embodiment 5
In utilization and embodiment 3, essentially identical device is realized biomass pyrolytic Poly-generation, only changes III level heat transfer pressure roller into II level heat transfer pressure roller.
The natural cornstalk that is 15% by moisture content, cut to mean length be 20cm, through hopper 1 and endless belt conveyor 2, send into heat accumulating type dehumidification system 3, inlet amount is 300kg/h; Moisture content is down to 9% after drying, then enters roller press type pyrolysis reactor 4; The length of support band 41 in roller press type pyrolysis reactor 4 (transmission length) is that 5m, width are 1.2m, and travelling speed is to be 2.50min the 2m/min(solid phase residence time), the gap between every grade of pair roller is 5mm; The flue-gas temperature entering in roller press type pyrolysis reactor 4 is 680 ℃, and pyrolysis reaction temperature is 460 ℃; Pyrolysis product, after gas solid separation and pyrolysis gas condensation, obtains coke, liquid and combustible gas three-phase pyrolysis product, and productive rate is separately 81kg/h, 136kg/h and 63kg/h.
The foregoing is only preferred embodiment of the present utility model, not in order to limit the utility model, all within spirit of the present utility model and principle, any modification of making, be equal to replacement, improvement etc., within all should being included in scope of the present utility model.
Claims (6)
1. a roller press type biomass pyrolytic multi-joint-production apparatus, comprises hopper (1), feed system (2), dehumidification system (3), roller press type pyrolysis reactor (4), gas solid separation system (5), pyrolysis gas condenser system (6), combustible gas firing system (7), solid coke collection box (8), liquid collecting case (9), combustible gas storage tank (10); Described roller press type pyrolysis reactor (4) comprises support band (41), live roll (42), drive system (43), enclosed reaction chamber (44), high-temperature flue gas heat exchange coil (45) and Multi-stage transmission hot-pressing roller (46), described Multi-stage transmission hot-pressing roller (46) is arranged in pairs along support band (41) direction, pressure roller running horizontal tangential is identical with raw material transmission direction, foremost is one-level heat transfer pressure roller (I), be followed successively by backward two-stage heat transmission pressure roller (II), final stage heat transfer pressure roller (N), wherein, N is more than or equal to 1 integer;
Wherein the outlet of hopper (1) is connected with the entrance of feed system (2), and the outlet of feed system (2) is connected with dehumidification system (3) entrance, and the outlet of dehumidification system (3) is connected with the top opening for feed of roller press type pyrolysis reactor (4); The outlet of roller press type pyrolysis reactor (4) side top is connected with the import of gas solid separation system (5), and below discharge port is connected with solid coke collection box (8) entrance; The air outlet of gas solid separation system (5) is connected with the import of pyrolysis gas condenser system (6); The liquid-phase outlet of pyrolysis gas condenser system (6) is connected with the entrance of liquid collecting case (9), and gaseous phase outlet is divided into two-way, and a road is connected with the entrance of combustible gas firing system (7), and another road is connected with combustible gas storage tank (10) entrance.The entrance of the high-temperature flue gas heat exchange coil (45) in the Multi-stage transmission hot-pressing roller (46) of the outlet of combustible gas firing system (7) and roller press type pyrolysis reactor (4) is connected; The outlet of the high-temperature flue gas heat exchange coil (45) of Multi-stage transmission hot-pressing roller is connected with the smoke inlet of dehumidification system (3); Multi-stage transmission hot-pressing roller (46) is connected with the drive system (43) outside being placed in enclosed reaction chamber (44); Every grade of heat transfer roller structure is identical, is hollow devices, internal layout high-temperature flue gas heat exchange coil (45); Described support band (41) arranges ringwise, and two ends arrange protective grating; Respectively there is a transmission shaft at the two ends of support band (41), and one of them is main drive shaft, and another is driven shaft; Driven shaft is placed in enclosed reaction chamber (44) completely, main drive shaft be placed in enclosed reaction chamber (44) outside drive system (43) be connected.
2. roller press type biomass pyrolytic multi-joint-production apparatus according to claim 1, is characterized in that: described feed system (2) is feeding screw or endless belt conveyor.
3. roller press type biomass pyrolytic multi-joint-production apparatus according to claim 1, is characterized in that: described gas solid separation system (5) is at least one in cyclonic separator or sack cleaner or gravity settling chamber.
4. roller press type biomass pyrolytic multi-joint-production apparatus according to claim 1, is characterized in that: described pyrolysis gas condenser system (6) is spray congealing system, falling liquid film condenser system or spraying and falling liquid film composite condensation system.
5. roller press type biomass pyrolytic multi-joint-production apparatus according to claim 1, is characterized in that: described dehumidification system (3) is fluidized bed drying system or heat accumulating type dehumidification system.
6. roller press type biomass pyrolytic multi-joint-production apparatus according to claim 1, is characterized in that: the gap in described Multi-stage transmission hot-pressing roller (46) between every pair of pressure roller is adjustable between 0.1mm-5cm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420027279.8U CN203715567U (en) | 2014-01-16 | 2014-01-16 | Rolling type biomass pyrolysis poly-generation device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201420027279.8U CN203715567U (en) | 2014-01-16 | 2014-01-16 | Rolling type biomass pyrolysis poly-generation device |
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| CN201420027279.8U Withdrawn - After Issue CN203715567U (en) | 2014-01-16 | 2014-01-16 | Rolling type biomass pyrolysis poly-generation device |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103788971A (en) * | 2014-01-16 | 2014-05-14 | 华北电力大学 | Rolling type biomass pyrolysis poly-generation device and rolling type biomass pyrolysis poly-generation method |
| CN104449793A (en) * | 2014-12-11 | 2015-03-25 | 广州迪森热能技术股份有限公司 | Biomass liquefaction system |
| CN104449791A (en) * | 2014-11-13 | 2015-03-25 | 常熟市高压容器制造有限公司 | Peristaltic solid-phase reactor and combined module |
| CN105062523A (en) * | 2015-07-30 | 2015-11-18 | 北京国电富通科技发展有限责任公司 | Pulverized coal upgrading pyrolysis device and upgrading pyrolysis process |
| CN110527534A (en) * | 2019-08-27 | 2019-12-03 | 浙江工业大学 | A method of class coal coke is prepared using domestic garbage pyrolysis |
-
2014
- 2014-01-16 CN CN201420027279.8U patent/CN203715567U/en not_active Withdrawn - After Issue
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103788971A (en) * | 2014-01-16 | 2014-05-14 | 华北电力大学 | Rolling type biomass pyrolysis poly-generation device and rolling type biomass pyrolysis poly-generation method |
| CN103788971B (en) * | 2014-01-16 | 2015-12-23 | 华北电力大学 | A kind of apparatus and method of roller press type biomass pyrolytic Poly-generation |
| CN104449791A (en) * | 2014-11-13 | 2015-03-25 | 常熟市高压容器制造有限公司 | Peristaltic solid-phase reactor and combined module |
| CN104449791B (en) * | 2014-11-13 | 2016-07-06 | 常熟市高压容器制造有限公司 | A kind of creeping motion type solid phase reactor and combined type module |
| CN104449793A (en) * | 2014-12-11 | 2015-03-25 | 广州迪森热能技术股份有限公司 | Biomass liquefaction system |
| CN105062523A (en) * | 2015-07-30 | 2015-11-18 | 北京国电富通科技发展有限责任公司 | Pulverized coal upgrading pyrolysis device and upgrading pyrolysis process |
| CN110527534A (en) * | 2019-08-27 | 2019-12-03 | 浙江工业大学 | A method of class coal coke is prepared using domestic garbage pyrolysis |
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Granted publication date: 20140716 Effective date of abandoning: 20151223 |
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