CN117186913A

CN117186913A - Biomass internal heating type airflow rotary carbonization method and carbon steam co-production equipment

Info

Publication number: CN117186913A
Application number: CN202311351683.0A
Authority: CN
Inventors: 吴峰源
Original assignee: Individual
Current assignee: Individual
Priority date: 2023-10-18
Filing date: 2023-10-18
Publication date: 2023-12-08

Abstract

The invention provides a biomass internal heating type airflow rotary carbonization method and carbon vapor co-production equipment, and provides a technology for biomass large-scale pyrolysis carbonization and carbon vapor co-production. The method comprises the processes of biomass raw material feeding, anaerobic separation, pyrolysis gas mixed combustion, fluidization carbonization, gas-solid distribution, rotary carbonization, carbon mixing, heat supply, pyrolysis gas circulation reciprocity and the like; the equipment comprises a stock bin/hopper, a feeder, an anaerobic sorter, a mixer, a pyrolysis gas fan, an internal heating type fluidization tube, a gas-solid distributor, a carbon discharging mechanism, an internal heating type rotary furnace, a gas burner, a waste heat boiler and the like. The carbonization method and the carbon-steam co-production equipment have strong adaptability to raw materials, high cracking carbonization efficiency and more balanced cracking carbonization process, particularly overcome the problem of pipe blockage of tar and powder, and radically eliminate the deflagration problem of the common internal heating type rotary carbonization furnace.

Description

Biomass internal heating type airflow rotary carbonization method and carbon steam co-production equipment

Technical Field

The invention belongs to the field of biomass waste recycling technology and biomass energy equipment, and particularly relates to a biomass internal heating type airflow rotary carbonization method and carbon steam co-production equipment.

Background

The biomass resources in China are very rich, the distribution is wide, and the biomass resources can be continuously supplied. Especially, with the continuous development and progress of society, the living standard of people, especially rural residents, is remarkably improved. With the increasing production scale of agriculture and forestry in China, simultaneously, a great deal of liquefied gas and coal are used as daily energy sources in rural areas. Therefore, wood and bamboo scraps, chaff, crop straw and other agricultural and forestry wastes are more and more increased. The agriculture and forestry waste is not easy to dispose, and a large amount of land is occupied by stacking; if the waste is directly burnt (such as straw is burnt), air pollution and ecological environment damage can be caused. How to effectively utilize biomass waste of agriculture and forestry to change waste into valuable is always a hot topic. Therefore, the method has important practical significance in researching biomass waste recycling and reasonably developing and utilizing technology.

The biomass carbonization technology is one of effective ways for comprehensively recycling agriculture and forestry biomass waste in a high-valued mode and improving the added value of commodities. The biomass charcoal has wide application, and is applied to various fields of industry, agriculture, environmental protection, families and the like, such as manufacturing gunpowder, explosive, mosquito-repellent incense combustion improver, charcoal base fertilizer and the like.

The traditional carbonization production adopts an intermittent smoldering carbonization process, and has the problems of uneven carbonization and low production efficiency. At present, a production mode of a rotary carbonization furnace is adopted in the market, and the rotary carbonization furnace basically adopts an external heating mode to ensure the anaerobic state in the furnace. However, this external heating method requires the outer wall of the rotary kiln as a heat conduction surface; not only has low heat conduction efficiency, but also the heating temperature is limited by the metal material of the rotary kiln. Therefore, the external heating type rotary carbonization furnace is difficult to realize the production of carbon products with large scale and low volatile matters. The internal heating type heating mode is to directly introduce high-temperature flue gas into the furnace so as to solve the problem of limited heat conducting surface and provide feasibility for large-scale carbonization production. However, the internal heat type rotary kiln has difficulty in solving the problem of oxygen content in the furnace atmosphere. Oxygen in the furnace is likely to cause deflagration to cause potential safety hazard; and oxygen may ablate a portion of the char, resulting in a decrease in the yield of char product. At present, the internal heating type rotary charcoal furnace is only used in the production process of coal-based or wood-based activated charcoal.

In addition, biomass waste sources in reality are various, and particularly, the biomass waste sources have various shapes and sizes, including long strips, square shapes, flakes and powder. The biomass wastes are often mixed, doped and piled together in the actual collection, storage and transportation processes. The carbonization time and carbonization degree required by these biomass wastes also differ significantly. Without differential treatment of these principles, it is also difficult to ensure the uniformity of the char product, making it more difficult to achieve a large scale carbonization process. Therefore, the blocky raw materials (such as long strip-shaped and blocky bamboo blocks and the like) and powdery raw materials (such as saw dust and bamboo powder and the like) in the biomass waste are subjected to differential carbonization, and the carbonization yield is improved. There is a need to find a new carbonization method and carbon vapor co-production equipment with much higher productivity and thermal efficiency than the traditional methods.

Disclosure of Invention

The invention provides a biomass internal heating type air flow rotary carbonization method and carbon vapor co-production equipment, which can effectively improve the productivity of the existing rotary carbonization furnace, improve the heating efficiency in the carbonization process, and simultaneously overcome the problem of the differentiation of the size and the shape in biomass raw materials,

the method and the equipment provided by the invention can directly mix the bulk raw material and the powdery raw material together for feeding without sorting the biomass raw material in advance. Moreover, the internal heating mode is utilized on the equipment, so that the heat conduction speed and carbonization efficiency of the raw materials are improved, and large-scale carbonization production is realized. Meanwhile, the carbonization time of the powdery raw materials can be automatically and effectively shortened, and the carbonization time of the blocky raw materials can be automatically prolonged, so that the carbonization equilibrium is achieved.

In order to achieve the technical aim of carbonizing the novel biomass waste, the invention provides a biomass internal heating type airflow rotary carbonization method and carbon vapor co-production equipment.

The technical scheme of the invention is realized as follows:

an internal heating type airflow rotary carbonization method for biomass, comprising the following steps:

(1) Feeding biomass raw materials: the biomass raw materials are put into the separation space by a feeder through a bin/hopper as a buffer; the biomass raw material is mixed with a bulk raw material and a powdery raw material;

(2) Anaerobic sorting process: in the separation space, performing anaerobic separation on the biomass raw material by utilizing low-temperature pyrolysis gas; the heavier blocky raw materials in the biomass raw materials after separation fall into the internal heating rotary furnace, and the lighter powdery raw materials in the biomass raw materials are led out along with low-temperature pyrolysis gas;

the anaerobic sorting is specifically a sorting mode utilizing an airflow sorting principle, and is characterized in that the internal atmosphere is in an anaerobic state; the oxygen-free state is that the oxygen molecular content of the gas is 0 or approximately 0, and the oxygen content is less than 1% can be set as a standard of approximately 0; the low-temperature pyrolysis gas is a gaseous product of the internal heating rotary furnace, contains combustible gas components and is in an anaerobic state;

(3) And (3) mixing and burning pyrolysis gas: mixing the low-temperature pyrolysis gas and the high-temperature flue gas in the step (2) to generate fluidized pyrolysis gas; the powdery raw material in the step (1) also enters the fluidized pyrolysis gas;

the mixed combustion is specifically under-oxygen combustion of pyrolysis gas, and aims to deplete the oxygen content in high-temperature flue gas and raise the temperature of the pyrolysis gas, and is characterized in that gaseous products are still combustible gas and are in an anaerobic state;

The fluidized pyrolysis gas is a gaseous product of mixed combustion of low-temperature pyrolysis gas and high-temperature flue gas, is combustible gas and is in an anaerobic state; the high-temperature flue gas is a gaseous product of a gas combustion furnace;

(4) And (3) fluidization and carbonization: the fluidized pyrolysis gas in the step (3) is used as a heat source to fluidize and carbonize the powdery raw material;

the fluidization carbonization is characterized in that the powdery raw material is driven by the fluidization cracking gas to be in a fluidization state, and the fluidization cracking gas and the powdery raw material in the fluidization state perform suspension heat exchange so as to quickly convert the powdery raw material into carbon powder; the fluidization carbonization is also characterized in that the fluidization pyrolysis gas and the powdery raw material move in the same direction, the solid output is carbon powder, and the gaseous output is medium-temperature pyrolysis gas; the medium-temperature cracking gas is in an anaerobic state;

(5) And (3) gas-solid distribution: dividing the medium-temperature pyrolysis gas in the step (4) into two parts: the first part does not carry carbon powder, and the second part carries carbon powder; feeding a first portion of the medium temperature cracked gas as a gaseous fuel to a gas burner;

and the distribution ratio of the first part medium-temperature pyrolysis gas and the second part medium-temperature pyrolysis gas takes the heat source flow required by the internal heating rotary furnace as a standard for optimizing and meeting the second part medium-temperature pyrolysis gas, and the redundant medium-temperature pyrolysis gas is redistributed to be used as the first part medium-temperature pyrolysis gas. Specifically, excessive distribution of pyrolysis gas in the second part can cause the partial pressure of the internal heat type rotary furnace to be large, and the pyrolysis gas leaks from the dynamic sealing part of the internal heat type rotary furnace; the second portion has too little distribution of pyrolysis gas and can result in insufficient heat source requirements for the inner heated rotary kiln.

(6) And (3) process judgment: measuring the medium-temperature cracking gas temperature T of the second part in the step (5), and comparing the medium-temperature cracking gas temperature T with the carbonization temperature T; the carbonization temperature T is the temperature required by the block-shaped raw materials in the internal heating rotary furnace to reach the carbonization requirement;

if the medium-temperature pyrolysis gas temperature T is more than or equal to the carbonization temperature T, introducing the medium-temperature pyrolysis gas in the second part in the step (5) into an internal heating rotary furnace;

if the temperature T of the medium-temperature pyrolysis gas is less than the carbonization temperature T, performing secondary mixed combustion on the medium-temperature pyrolysis gas and the high-temperature flue gas in the second part in the step (5); introducing the high-temperature pyrolysis gas into an internal heating rotary furnace;

the secondary mixed combustion is secondary mixed combustion of medium-temperature pyrolysis gas and high-temperature flue gas; the high-temperature pyrolysis gas is a gaseous product of secondary mixed combustion and is characterized by being in an oxygen-free state, and the temperature of the high-temperature pyrolysis gas is higher than the carbonization temperature T;

(7) And (3) a rotary carbonization process: introducing the high-temperature pyrolysis gas or the medium-temperature pyrolysis gas of the second part in the step (6) into an internal heating rotary furnace as a heat source to carry out rotary carbonization;

the rotary carbonization is specifically characterized in that the blocky raw materials and the heat source are subjected to direct heat exchange in a rotary furnace, and the blocky raw materials are gradually heated to the carbonization temperature T and converted into carbon blocks; the rotary carbonization is characterized in that the heat source and the bulk raw materials move in countercurrent (reverse direction), the solid output is carbon blocks, and the gaseous output is low-temperature pyrolysis gas; the rotary carbonization is characterized in that the internal atmosphere of the internal heating rotary furnace is always in an anaerobic state;

(8) Mixing and discharging carbon: the carbon powder is settled in the internal heating rotary furnace, mixed with the carbon blocks and discharged through a carbon outlet of a carbon discharging mechanism, cooled and discharged

(9) And (3) heat supply: the medium-temperature pyrolysis gas of the first part in the step (5) is fully combusted in a gas burner, and gaseous products are high-temperature flue gas; the high-temperature flue gas and the low-temperature pyrolysis gas are mixed to burn, so that heat energy is provided for fluidization and carbonization; the redundant high-temperature flue gas or medium-temperature pyrolysis gas in the gas burner can be introduced into a waste heat boiler or a gas boiler for energy recovery and utilization, and steam is generated to supply heat for enterprises.

(10) Pyrolysis gas circulation mutually benefits: the circulation is to re-introduce the low-temperature pyrolysis gas generated in the step (7) back to the step (2) for the anaerobic separation, so as to realize the pyrolysis gas circulation; the reciprocity is that the gaseous output (low-temperature pyrolysis gas) in the rotary carbonization process provides a heat source for the fluidization carbonization, the gaseous output (medium-temperature pyrolysis gas) in the fluidization carbonization process also provides a heat source for the rotary carbonization, and the two carbonization processes are mutually utilized;

in some embodiments, the bulk feedstock in the biomass feedstock has a maximum diameter of no more than 50cm.

In some embodiments, the biomass feedstock is desirably dried to reduce the water content of the biomass feedstock to below 20%.

In some embodiments, the powdery feedstock in the biomass feedstock is small in diameter and in a fluidized state, so that fluidized carbonization can be completed or nearly completed in a short time (a few seconds).

In some embodiments, the thickness of the inner wall of the inner heating type rotary furnace is increased or a heat storage material is embedded to form a heat storage inner wall, the high-temperature pyrolysis gas or the medium-temperature pyrolysis gas and the heat storage inner wall perform gas-solid phase heat exchange, and the heat storage inner wall performs conduction heat exchange with the bulk raw materials, so that a heat exchange path is increased, and the heat exchange efficiency of the inner heating type rotary furnace is improved.

In order to further achieve the above object, the present invention further provides a biomass internal heating type air flow rotary carbon vapor co-production device, comprising: the device comprises a storage bin/hopper, a feeder, an anaerobic sorter, a mixing burner, a pyrolysis gas fan, an internal heating type fluidization tube, a gas-solid distributor, a carbon discharging mechanism, an internal heating type rotary furnace, a gas burner and a waste heat boiler.

The bottom of the bin/hopper is connected with the feeder; the feeder is connected to the anaerobic sorter so that biomass feedstock in the silo/hopper passes through the feeder into the space inside the anaerobic sorter.

The anaerobic sorter is a mechanism utilizing the airflow sorting principle and can separate blocky raw materials from powdery raw materials in biomass raw materials, and is characterized in that the internal atmosphere is in an anaerobic state; the anaerobic sorter is provided with an inlet and an outlet; the inlet of the anaerobic sorter is connected with the feeding end of the internal heating rotary furnace and the internal space is communicated; the gaseous product low temperature cracked gas of the internal heated rotary kiln is introduced into the gas stream as a gas stream sort; the block-shaped raw materials fall into the feeding end of the internal heating rotary furnace; the powdery raw material is led out from an outlet of the anaerobic sorter along with the low-temperature pyrolysis gas; the outlet of the anaerobic sorter is connected with the mixer;

the mixer is a mechanism for mixing and combusting low-temperature pyrolysis gas and high-temperature flue gas, and the gaseous output is fluidized pyrolysis gas; the mixer is provided with a first inlet, a second inlet and an outlet; the first inlet of the mixer is connected with an anaerobic separator, and the low-temperature pyrolysis gas is introduced; the second inlet of the mixer is connected with the gas burner, and the high-temperature flue gas is introduced; the outlet of the mixer is connected with an internal heating type fluidization pipe to lead out fluidization pyrolysis gas; the high-temperature flue gas is a gaseous output of the gas burner;

The internal heating type fluidization tube is a mechanism for implementing fluidization and carbonization, the solid output is carbon powder, and the gaseous output is medium-temperature pyrolysis gas; the internal heating type fluidization tube is characterized in that the internal powder raw material is in a fluidization state under the action of air flow, and the internal heating type fluidization tube is a long channel with a refractory material or high temperature resistant metal as an outer wall and is provided with an inlet and an outlet; the inlet of the internal heating type fluidization tube is connected with the mixer to introduce the fluidization and pyrolysis gas and the carried powdery raw materials; the outlet of the internal heating type fluidization tube is connected with a gas-solid distributor, and medium-temperature pyrolysis gas and carried carbon powder are led out into the gas-solid distributor;

the pyrolysis gas fan provides power for the flow of the low-temperature pyrolysis gas; the pyrolysis gas fan can be arranged between the anaerobic sorter and the mixer, between the mixer and the internal heating type fluidization pipe, and between the internal heating type fluidization pipe and the gas-solid distributor;

the gas-solid distributor is a mechanism for redistributing carbon powder carried by the medium-temperature pyrolysis gas; the gas-solid distributor is of an internal three-way structure and is provided with an inlet, a first outlet and a second outlet; the redistribution refers to dividing the medium-temperature cracked gas into two parts: the medium-temperature pyrolysis gas in the first part does not carry carbon powder, and the medium-temperature pyrolysis gas in the second part carries carbon powder; the first outlet of the gas-solid distributor is connected with the gas burner, and the medium-temperature pyrolysis gas of which the first part does not carry carbon powder is introduced into the gas burner; the second outlet of the gas-solid distributor has two connection modes:

The first mode is that the second part of pyrolysis gas and carried carbon powder are introduced into the inner space of the carbon outlet mechanism;

the second mode is that the second medium-temperature cracking gas and the carried carbon powder are introduced into the secondary mixer; the secondary mixer is a mechanism for mixing and combusting medium-temperature pyrolysis gas, and the gaseous output is high-temperature pyrolysis gas; the secondary mixer is provided with a first inlet, a second inlet and an outlet; the first inlet of the secondary mixer is connected with the gas-solid distributor; the second inlet of the secondary mixed burner is connected with a gas burner, and the high-temperature flue gas is introduced; the outlet of the secondary mixer is connected with the carbon outlet mechanism through a high-temperature fan, and the high-temperature pyrolysis gas and the carried carbon powder are introduced into the inner space of the carbon outlet mechanism;

the invention provides biomass internal heating type air flow rotary carbon vapor co-production equipment, wherein a second outlet of a gas-solid distributor provides two connection modes. In the first mode, the medium-temperature pyrolysis gas in the second part is directly used as an internal heat source of the internal heating rotary furnace; the connecting mode has simple structure, but the medium-temperature cracking gas temperature is lower, and the connecting mode is suitable for producing carbon products with higher volatile matters; in the second mode, the second part of medium-temperature pyrolysis gas is firstly subjected to secondary mixed combustion and is converted into high-temperature pyrolysis gas and then used as an internal heat source of the internal heating rotary furnace; the connection mode is suitable for producing carbon products with low volatile matters;

The carbon outlet mechanism is provided with an air inlet and a feed inlet, and the bottom of the carbon outlet mechanism is provided with a carbon outlet; an air inlet of the carbon outlet mechanism is connected with the gas-solid distributor or the high-temperature fan; the feeding port of the carbon discharging mechanism is connected with the discharging end of the internal heating rotary furnace, and the internal space is communicated; the medium-temperature pyrolysis gas or the high-temperature pyrolysis gas in the second part is taken as an internal heat source to enter the internal space of the internal heating rotary furnace from the feed inlet of the carbon outlet mechanism; the carbon outlet of the carbon outlet mechanism is also connected with cooling equipment for cooling the discharged carbon blocks and carbon powder;

the internal heating type rotary furnace is a rotary furnace mechanism for heating biomass raw materials through an internal heat source, and a rotary furnace wall is internally embedded with insulating bricks or externally wrapped with insulating materials; the internal heating rotary furnace is provided with a feeding end and a discharging end; biomass raw materials enter from a feeding end of the internal heating rotary furnace, are converted into carbon and then enter the carbon discharging mechanism from a discharging end of the internal heating rotary furnace; the low-temperature pyrolysis gas is introduced into the anaerobic separator from the feeding end of the internal heating rotary furnace;

the gas burner is a mechanism for fully burning combustible gas, and the gaseous output is high-temperature flue gas; the gas burner is provided with an inlet, a hollow distribution port and a first outlet; the inlet of the gas burner is connected with the gas-solid distributor; the air distribution port of the gas burner is connected with an air distribution fan; the first outlet of the gas burner is connected with the mixer to provide the high-temperature flue gas for the mixer. The gas burner is provided with a waste heat outlet; the waste heat outlet is connected with a waste heat boiler, waste heat recovery and utilization are carried out on redundant high-temperature flue gas, and carbon-steam co-production is realized;

In some embodiments, the feed end or discharge end of the inner heated rotary kiln is provided with a taper to reduce the port diameter of the feed end or discharge end; the cone arranged above can reduce the dynamic seal of the connection of the feeding end and the anaerobic sorter, and also can reduce the dynamic seal of the connection of the discharging end and the carbon outlet mechanism, thereby being beneficial to improving the reliability of the dynamic seal and reducing the cost.

In some embodiments, the gas burner is further provided with a second outlet, using a second connection of the gas-solid distributor; the second outlet is connected with the secondary mixed burner and provides high-temperature smoke for secondary mixed combustion;

in some embodiments, the two connection modes of the second outlet of the gas-solid distributor are realized by arranging two valves at the second outlet of the gas-solid distributor. Specifically, the second outlet of the gas-solid distributor is connected with the inlet of the carbon outlet mechanism through one valve, and meanwhile, the second outlet of the gas-solid distributor is connected with the inlet of the secondary mixer through the other valve. The switching of the connection of the first and second mode is achieved by the closing and opening of two valves.

In some embodiments, a barometer is provided in the char-forming mechanism, the internal heated rotary kiln, or the anaerobic sorter to measure the pressure in the internal space of the internal heated rotary kiln. The first outlet or the second outlet of the gas-solid distributor is also provided with a valve, and the flow of the pyrolysis gas in the second part is regulated by the opening of the valve, so that the pressure of the inner space of the internal heating rotary furnace is regulated. When the internal heating rotary furnace is in normal operation, the pressure of the internal space should be kept stable near zero pressure.

After the biomass internal heating type airflow rotary carbonization method and the biomass internal heating type airflow rotary carbonization equipment are adopted, the beneficial effects of the invention are as follows:

(1) The adaptability to raw materials is strong. The method and the equipment provided by the invention can be suitable for biomass raw materials mixed by bulk raw materials and powdery raw materials. The invention can directly use mixed biomass raw materials without sieving or sorting the biomass raw materials.

(2) High carbonization efficiency. The method and the equipment provided by the invention adopt an internal heating mode, overcome the limitation of the heat conducting surface in the existing equipment, and improve the heat conducting speed and the carbonization efficiency of biomass raw materials.

(3) The carbonization is more balanced. The method and the equipment provided by the invention can automatically adjust the carbonization process according to the granularity condition of the raw materials. For powdery raw materials, fluidization carbonization is used to effectively shorten carbonization time; and the carbonization time of the blocky raw materials is prolonged by adopting rotary carbonization, so that the carbonization uniformity of different raw materials is achieved.

(4) Overcomes the problem of pipe blockage caused by tar and powder. The pyrolysis gas in the conventional rotary carbonization furnace is led out through a pipeline, tar contained in the pyrolysis gas is separated out in the leading-out process, and the pyrolysis gas and powder are adhered to the pipe wall together to cause the problem of pipe blockage. The method and the equipment provided by the invention can improve the temperature of pyrolysis gas through mixed combustion, avoid tar condensation, overcome the problem of pipe blockage and ensure long-term stable operation of the equipment.

(5) And the problem of deflagration is completely eradicated. The method and the equipment provided by the invention adopt an internal heating mode, but the heat sources are in an anaerobic state through mixed combustion or secondary mixed combustion. The invention solves the problem of oxygen content of the internal atmosphere of the internal heating rotary carbonization furnace, thereby avoiding the potential safety hazard that the internal heating rotary carbonization furnace is easy to cause deflagration.

Drawings

FIG. 1 is a process flow diagram of the present invention.

Fig. 2 provides a schematic structural diagram of a first embodiment of the apparatus.

Wherein: (1) a hopper, (2) a feeder, (3) an anaerobic classifier, (3-1) an anaerobic classifier inlet, (3-2) an anaerobic classifier outlet, (4) a burner, (4-1) a burner first inlet, (4-2) a burner second inlet, (4-3) a burner outlet, (5) a pyrolysis gas fan, (6) an internal heating fluidization tube, (6-1) an internal heating fluidization tube inlet, (6-2) an internal heating fluidization tube outlet, (7) a gas-solid distributor, (7-1) a gas-solid distributor inlet, (7-2) a gas-solid distributor first outlet, (7-3) a gas-solid distributor second outlet, (8) a char-discharging mechanism, (8-1) a char-discharging mechanism inlet, (8-2) a char-discharging mechanism outlet, (9) an internal heating rotary furnace, (9-1) an internal heating rotary furnace feed end, (9-2) an internal heating rotary furnace discharge end, (10) a gas burner, (10-1) a gas burner inlet, (10-2) a gas burner first outlet, (7-3) a gas distributor first outlet, (10) a gas burner, a second gas burner (4-outlet) a gas burner (10-5), (11) The secondary mixer comprises a (11-1) secondary mixer first inlet, (11-2) secondary mixer second inlet, (11-3) secondary mixer outlet, (12) high temperature fan and (13) waste heat boiler.

FIG. 3 is a schematic diagram of the structure of an anaerobic sorter.

Wherein, (2) a feeder, (3) an anaerobic sorter, (3-1) an anaerobic sorter inlet, (3-2) an anaerobic sorter outlet, (3-3) a mask, (3-4) a scraping ruler, (6) an internal heating rotary furnace, and (6-1) a feeding end of the internal heating rotary furnace.

Fig. 4 is a schematic structural view of the burner of the present invention.

Wherein, (4) the mixer, (4-1) the first inlet of the mixer, (4-2) the second inlet of the mixer, (4-3) the outlet of the mixer, (4-4) the distribution chamber, (4-5) the combustion chamber, (4-6) the combustion hole.

Fig. 5 is a schematic structural view of a gas-solid distributor according to the present invention.

Wherein, (7) the gas-solid distributor, (7-1) the gas-solid distributor inlet, (7-2) the gas-solid distributor first outlet, (7-3) the gas-solid distributor second outlet; (7-3) gas-solid distributor cone opening.

Fig. 6 is a schematic structural diagram of a second embodiment of the apparatus.

Detailed Description

The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.

In this embodiment, taking bamboo processing waste as biomass raw material as an example, a specific embodiment of a biomass internal heating type airflow rotary carbonization method in the invention is further described in detail with reference to fig. 1:

an internal heating type airflow rotary carbonization method for biomass comprises the following steps:

(1) And (3) drying: the bamboo processing waste comprises block raw materials obtained by crushing bamboo heads and bamboo tips, the maximum block diameter is below 50mm, and powdery raw materials such as bamboo scraps, bamboo powder and the like; the water content of the biomass raw material is about 40%. The biomass raw material is dried and dehydrated by utilizing a drying rotary kiln, and the water content of the biomass raw material is reduced to below 20%.

(2) Feeding: the dried biomass raw material is sent into a hopper by a conveyer belt, and the hopper is used as a buffer memory; and then using a spiral feeder as a feeder, and putting the biomass raw material in the hopper into a separation space of the anaerobic separator according to the feeding amount of 2 tons/hour.

(3) Anaerobic sorting process: in the separation space of the anaerobic separator, a separation gas flow of 5 m/s upwards is formed by using low-temperature pyrolysis gas, and the whole separation space is in an anaerobic state. Heavier blocky raw materials in the biomass raw materials can fall into the bottom of the anaerobic sorter or the internal heating rotary furnace under the action of gravity; and the powdery raw materials with the average particle size smaller than 2mm in the biomass raw materials move upwards under the action of the sorting airflow and are led out from an outlet at the upper end of the anaerobic sorter along with the low-temperature pyrolysis gas. In this embodiment, the low-temperature pyrolysis gas is a gaseous product of an internal heating rotary furnace, the temperature is 310 ℃, and the low-temperature pyrolysis gas contains combustible gas components and is in an anaerobic state.

(4) And (3) mixing and burning pyrolysis gas: and mixing the low-temperature pyrolysis gas and the high-temperature flue gas discharged from the anaerobic separator in a mixer. The mixed combustion in the step is specifically under-oxygen combustion taking low-temperature pyrolysis gas as fuel, and the high-temperature flue gas provides oxygen molecules so as to deplete the oxygen content in the high-temperature flue gas and increase the temperature of the low-temperature pyrolysis gas. In this example, the mixed combustion product was a fluidized pyrolysis gas at 700 ℃, a combustible gas, and in an oxygen-free state. The powdered feedstock also moves with the fluidized pyrolysis gas. The high temperature flue gas required for the mixed combustion is led out from the gas combustion furnace.

(5) And (3) fluidization and carbonization: introducing the fluidized pyrolysis gas generated by the mixed combustion in the step (4) into an internal heating type fluidization tube through a pyrolysis gas fan; simultaneously, the powdery raw materials carried by the fluidized pyrolysis gas also enter the internal heating type fluidization tube. In the internal heating type fluidization tube, the fluidization cracking gas and the powdery raw material move in the same direction. Under the action of the fluidization and pyrolysis gas, the powdery raw material is driven to be in a fluidization state; the fluidized cracking gas carries out suspension heat exchange with the powdery raw material in a fluidized state, and the powdery raw material is rapidly heated to 500 ℃, so that fluidization carbonization occurs. In the embodiment, the solid product of fluidization and carbonization is carbon powder, and the temperature is 500 ℃; the gaseous output is medium-temperature pyrolysis gas, the temperature is 520 ℃, and the gaseous output is in an anaerobic state; both solid and gaseous effluent are led out from the outlet of the internal heating type fluidization pipe.

In the embodiment, the grain size of the powdery raw material is smaller than 2mm and is in a fluidization state under the working condition of high temperature of 700 ℃, so that fluidization carbonization can be completed within 8 seconds.

(6) And (3) gas-solid distribution: splitting the 520 ℃ medium-temperature pyrolysis gas generated in the step (5) into two parts: the first part of medium-temperature pyrolysis gas does not carry carbon powder, and accounts for about 40% of the total gas amount of the medium-temperature pyrolysis gas; the second part of medium-temperature pyrolysis gas carries carbon powder, and the carbon powder accounts for about 60% of the total gas amount of the medium-temperature pyrolysis gas; the first portion of the medium temperature cracked gas is fed to a gas burner as a gaseous fuel.

(7) Determining the technological parameters: in this example, the volatile content of the produced bamboo charcoal is required to be about 10%. Then a few bamboo blocks are taken and put into a high-temperature ceramic crucible, and a Gao Wenma boiler is utilized for carbonization test. The carbonization temperature T required by 10% of the volatile matters of the bamboo charcoal is determined by adopting a method for measuring the volatile matters of the carbon materials in YB/T5189-2000 national standard. In this example, the bamboo blocks were carbonized at a carbonization temperature t=560 ℃ and the volatile content in the fixed carbon was determined to be 10% by a horse boiling furnace test.

(8) And (3) process judgment and implementation: and (3) measuring the temperature t of the pyrolysis gas in the second part in the step (6) by using a K-type thermocouple. In this example, the measured medium temperature cracked gas temperature t=520℃.

In the embodiment, the measured medium-temperature pyrolysis gas temperature t=520℃ < bamboo block carbonization temperature t=560 ℃, and then the second medium-temperature pyrolysis gas in the step (6) is introduced into a secondary mixer to be subjected to secondary mixed combustion with high-temperature flue gas;

(9) Secondary mixed combustion process: the secondary mixed combustion in the step is under-oxygen combustion taking medium-temperature pyrolysis gas as fuel, and the high-temperature flue gas provides oxygen molecules, so that the oxygen content in the high-temperature flue gas is exhausted, and the temperature of the medium-temperature pyrolysis gas is further improved. In the embodiment, the output of the secondary mixed combustion is high-temperature pyrolysis gas which is combustible gas and is in an anaerobic state, and the temperature is 600 ℃; and then the high-temperature pyrolysis gas and the carbon powder carried by the high-temperature pyrolysis gas are introduced into a carbon discharging mechanism by a high-temperature fan.

(10) And (3) a rotary carbonization process: the pyrolysis gas at 600 ℃ is used as a heat source to be introduced into the carbon outlet mechanism, and then enters the inner space of the internal heating rotary furnace through the carbon outlet mechanism. Carbon powder carried by the pyrolysis gas also enters the internal space of the internal heating rotary furnace.

In the internal heating rotary furnace, the high-temperature pyrolysis gas at 600 ℃ and the bulk raw materials move in countercurrent (reverse direction); in the countercurrent movement process, the high-temperature pyrolysis gas exchanges heat with the blocky raw materials, and the blocky raw materials gradually heat to more than 560 ℃ and are converted into carbon blocks and discharged from a discharge end; in this embodiment, the internal atmosphere of the internal heat type rotary kiln is always in an anaerobic state, and the temperature of the low-temperature pyrolysis gas of the gaseous output is 310 ℃.

In the embodiment, the inner wall of the internal heating rotary furnace is embedded with refractory bricks with the thickness of 230mm to form a heat storage inner wall, high-temperature pyrolysis gas and the heat storage inner wall perform gas-solid phase heat exchange, and the heat storage inner wall performs conduction heat exchange with bulk raw materials, so that a heat exchange path can be increased, and the heat exchange efficiency of the internal heating rotary furnace is improved.

(11) Mixing and discharging carbon: the carbon powder carried by the pyrolysis gas is settled in the inner space of the internal heating rotary furnace, mixed with the carbon blocks and enters the carbon discharging mechanism together; and then discharged from a carbon outlet of the carbon discharging mechanism, cooled to normal temperature and packaged.

(12) And (3) heat supply: introducing the first part of medium-temperature pyrolysis gas generated in the step (6) into a gas burner as a gaseous fuel, and fully burning the gaseous fuel, wherein the burnt gaseous product is high-temperature flue gas with the temperature of 1100 ℃. In this embodiment, the high temperature flue gas is divided into two parts: a part of the low-temperature cracking gas is introduced into a mixer for mixing combustion with the low-temperature cracking gas; the other part is introduced into a secondary mixer for secondary mixing combustion with the medium-temperature pyrolysis gas;

in the embodiment, redundant high-temperature flue gas in the gas burner is introduced into a waste heat boiler with the pressure of 4 tons/hour for energy recovery, and steam with the pressure of 0.8MPa is generated for enterprises to use.

(13) Pyrolysis gas circulation mutually benefits: introducing the low-temperature pyrolysis gas at 310 ℃ generated in the step (10) back to the anaerobic separator again to be used as a separation gas flow, so as to realize pyrolysis gas circulation;

in the embodiment, gaseous output (low-temperature cracking gas at 310 ℃) of the rotary carbonization furnace is mixed and combusted to generate fluidized cracking gas in an anaerobic state at 700 ℃, and a heat source is provided for fluidization carbonization; secondary mixed combustion is carried out on gaseous output (medium-temperature pyrolysis gas at 520 ℃) of the internal heating type fluidization tube, high-temperature pyrolysis gas in an anaerobic state at 600 ℃ is generated, and a heat source is provided for rotary carbonization; the two carbonization processes are mutually utilized;

The invention also provides biomass internal heating type airflow rotary carbon-steam co-production equipment. In the following, the embodiment of the biomass internal heating type air flow rotary carbon vapor co-production device in the present invention is further described in detail by taking bamboo processing waste as biomass raw material as an example.

Example 1

Referring to fig. 2, an embodiment of a biomass internal heating type airflow rotary carbon vapor co-production device in the invention is as follows:

a biomass internal heat type air flow rotary carbon vapor co-production device, comprising: the device comprises a hopper 1, a feeder 2, an anaerobic sorter 3, a mixer 4, a pyrolysis gas fan 5, an internal heat type fluidization tube 6, a gas-solid distributor 7, a carbon discharging mechanism 8, an internal heat type rotary furnace 9, a gas burner 10, a secondary mixer 11, a high temperature fan 12 and a waste heat boiler 13.

In the embodiment, the hopper 1 is an inverted cone-shaped raw hopper with the length of 1m, the width of 1m and the depth of 1.5m, and the bottom opening of the hopper is 300mm multiplied by 300mm. The bottom of the hopper 1 is provided with a shut-off fan with an opening of 300mm multiplied by 300mm and a blanking speed of 20 cubic/hour. The feeder 2 is a screw feeder, and the basic parameters are as follows: 2m long, 0.4m diameter, and 20 cubic/hour feed rate.

The dried biomass raw material is conveyed into a hopper 1 by a conveying belt with the length of 12m according to the feeding amount of 3 tons/hour, and falls into a feeder 2 through a shut-off fan arranged at the bottom of the hopper 1. The feeder 2 feeds the biomass feedstock into the space inside the anaerobic sorter 3.

In this embodiment, the structure and function of the oxygen-free classifier 3 of the present invention will be described with reference to fig. 3. The anaerobic sorter 3 is a mechanism utilizing the principle of air flow sorting, and can separate bulk raw materials from powdery raw materials in the biomass raw materials. The anaerobic sorter 3 in this embodiment has a horizontally and transversely arranged conical structure, the opening of the conical bottom is used as an inlet 3-1, the diameter of the inlet is 1.7m, and the inlet is connected with the feeding end 9-1 of the internal heating rotary furnace 9 through dynamic sealing and the internal space is communicated. The cone roof is provided with a mask 3-3, and the feeder 2 feeds biomass raw material into the space inside the anaerobic sorter 3 through the mask 3-3. The anaerobic sorter 3 is provided with a scraping ruler 3-4 along the conical wall, and one end of the scraping ruler 3-4 is fixed on the inner wall of the internal heating rotary furnace 9; the scraping ruler 3-4 can do circular motion on the conical wall along with the rotation of the internal heating type rotary furnace 9, and the raw materials falling into the bottom of the anaerobic sorter 3 are scraped into the internal heating type rotary furnace 9.

The upper end of the anaerobic sorter 3 is provided with an outlet 3-2 with the diameter of 0.3m; the low-temperature pyrolysis gas (the temperature is 310 ℃, the combustible gas components are contained, and the low-temperature pyrolysis gas is in an anaerobic state) of the gaseous products of the internal heating rotary furnace is introduced into an anaerobic separator 3 from a feeding end 6-1 to be used as a separation gas stream; after the low-temperature cracking gas passes through the conical structure, the gas flow speed is accelerated, and a separation gas flow of 5 m/s upwards is formed near the outlet 3-2 of the anaerobic sorter 3. Heavier blocky raw materials in the biomass raw materials can fall into the internal heating rotary furnace 9 under the action of gravity; the raw materials which partially fall into the bottom of the anaerobic sorter 3 are also returned to the internal heat type rotary furnace 9 under the action of the scraping rule. And the powdery raw materials with the average particle size smaller than 2mm in the biomass raw materials move upwards under the action of the sorting airflow and are led out from an outlet 3-2 at the upper end of the anaerobic sorter 3 along with the low-temperature pyrolysis gas. The outlet 3-2 of the anaerobic sorter 3 is connected with the mixer 4; the separation space of the whole anaerobic sorter 3 is always in an anaerobic state during normal operation.

The mixer 4 is a mechanism for mixing and combusting low-temperature pyrolysis gas and high-temperature flue gas, and the gaseous output is fluidized pyrolysis gas; in the mixer 4, the low-temperature pyrolysis gas is used as fuel to perform under-oxygen combustion, and the high-temperature flue gas provides oxygen molecules, so that the purpose of the mixed combustion is to deplete the oxygen content in the high-temperature flue gas and raise the temperature of the low-temperature pyrolysis gas. In this embodiment, the temperature of the low temperature pyrolysis gas is 310 ℃; the high-temperature flue gas temperature is 1100 ℃, and the oxygen content is 5%; after mixed combustion, fluidized pyrolysis gas is generated, the temperature is 700 ℃, and the fluidized pyrolysis gas is in an anaerobic state. The mixer 4 is provided with a first inlet 4-1, a second inlet 4-2 and an outlet 4-3; the first inlet 4-1 of the mixer 4 is connected with the anaerobic separator 3, and low-temperature pyrolysis gas and powdery raw materials carried by the low-temperature pyrolysis gas are introduced; the second inlet 4-2 of the mixer burner 4 is connected with the gas burner 10, and high-temperature flue gas is introduced; the outlet 4-3 of the mixer 4 is connected with an internal heating type fluidization pipe 6 to lead out the fluidization cracking gas; the high-temperature flue gas is a gaseous product of the gas burner;

in this embodiment, the structure and function of the burner 4 of the present invention will be described with reference to fig. 4. In fig. 4A is a preferred mixer embodiment. The high-temperature flue gas enters the interior of the mixer 4 through the second inlet 4-2. A distribution chamber 4-4 is arranged inside the mixer 4, and the distribution chamber 4-4 distributes the high-temperature flue gas evenly into the annular combustion chamber 4-5. The surface of the combustion cavity 4-5 is distributed with uniform combustion holes 4-6, so that the high-temperature flue gas and the pyrolysis gas can be fully mixed to exhaust the oxygen content in the high-temperature flue gas.

In fig. 4B is a simplified mixer embodiment. The first inlet 4-1 adopts an elbow structure, and is connected into the mixer 4 from one side; the second inlet 4-2 adopts an embedded elbow structure and is connected into the interior of the mixer 4 from the other side. One end of the embedded elbow is welded with a cylindrical combustion chamber 4-5, and the surface of the combustion chamber is distributed with uniform combustion holes 4-6. A nozzle is arranged at the end of the cylindrical combustion chamber 4-5, so that the high-temperature flue gas further forms turbulent flow to improve the mixed combustion effect.

In fig. 4C, another simplified mixer embodiment is shown, employing a process configuration in which high temperature flue gas is carried away from the outer layer and pyrolysis gas is carried away from the inner layer. The mixer 4 is formed by a strip-shaped combustion pipeline which is built and cast by refractory bricks; one end is a second inlet 4-2, and the other end is an outlet 4-3. The high-temperature flue gas enters from one end of the combustion pipeline, is exhausted by mixed combustion and is led out from the outlet 4-3 at the other end of the combustion pipeline. The first inlet 4-1 adopts an embedded elbow structure, and introduces pyrolysis gas into the inner layer of the mixer 4. In this case, the temperature of the outer casing of the burner 4 exceeds 1000 ℃, and it is necessary to embed refractory bricks. In the example shown in fig. 2, the burner embodiment shown in fig. 4C is used.

The pyrolysis gas fan 5 provides power for the flow of the low-temperature pyrolysis gas; in the embodiment, the pyrolysis gas fan 5 is a centrifugal fan which is made of 304 stainless steel, has a full pressure of 2000Pa, has a flow rate of 15000 standard cubes/hour and has a power of 15 KW. The pyrolysis gas fan 5 is arranged between the outlet 4-3 of the mixer 4 and the internal heating type fluidization tube 6, the inlet of the pyrolysis gas fan 5 is connected with the outlet 4-3 of the mixer 4, and the outlet of the pyrolysis gas fan 5 is connected with the inlet of the internal heating type fluidization tube 6.

The internal heating type fluidization tube 6 in the embodiment is a channel-shaped carbonization channel which is cast by refractory bricks or adopts high-temperature resistant metal 310S as an outer wall, and has the length of 12m and the equivalent inner diameter of 0.5m. The internal heating type fluidization tube 6 is provided with an inlet 6-1 and an outlet 6-2; an inlet 6-1 of the internal heating type fluidization tube 6 is connected with a pyrolysis gas fan 5, and the fluidized pyrolysis gas at 700 ℃ and the carried powdery raw materials are introduced. The average airflow velocity in the internal heating type fluidization tube 6 is 6m/s, and the powdery raw material is in a fluidization state under the action of the airflow; the fluidized cracking gas carries out suspension heat exchange with the powdery raw material in a fluidized state, and rapidly heats the powdery raw material to 500 ℃ to generate fluidization carbonization. In this example, the solid product of fluidization and carbonization is carbon powder at 500 ℃ and the gaseous product is medium-temperature pyrolysis gas at 520 ℃. The outlet 6-2 of the internal heating type fluidization tube 6 is connected with the gas-solid distributor 7, and the medium-temperature pyrolysis gas at 520 ℃ and the carried carbon powder are led out into the gas-solid distributor 7.

The gas-solid distributor 7 is of an internal three-way structure and is provided with an inlet 7-1, a first outlet 7-2 and a second outlet 7-3; the gas-solid distributor 7 has the function of redistributing medium-temperature pyrolysis gas and carried carbon powder, wherein the medium-temperature pyrolysis gas is divided into two parts: the first part of medium-temperature pyrolysis gas does not carry carbon powder and is introduced into the gas burner 10 through the first outlet 7-2 of the gas-solid distributor 7; the second part of medium-temperature pyrolysis gas carries carbon powder and is introduced into the secondary mixer 11 through a second outlet 7-3 of the gas-solid distributor 7. In this embodiment, the first outlet 7-2 of the gas-solid distributor 7 is also connected with a butterfly valve, and the flow ratio of the pyrolysis gas in the first part and the second part is adjusted. In this embodiment, the opening degree of the butterfly valve may be adjusted according to a barometer provided at the top end of the carbon discharging mechanism 8. The opening of the butterfly valve is adjusted so that the internal pressure of the carbon discharging mechanism 8 is constant, in this embodiment, 10Pa.

In this embodiment, the structure and function of the gas-solid distributor 7 of the present invention will be described with reference to fig. 5. In fig. 5A is a preferred gas-solid dispenser embodiment. The gas-solid distributor 7 adopts the structure of a cyclone separator, but a cone opening 7-4 is arranged on the central tube. The medium-temperature pyrolysis gas and the carried carbon powder are introduced into the cyclone separator through an inlet 7-1. Under the action of centrifugal force, the carbon powder is led out from a second outlet 7-3 arranged at the bottom of the cyclone separator; while a part of medium-temperature pyrolysis gas without carbon powder is led out from a first outlet 7-2 arranged at the top of the cyclone separator; the existence of the cone opening 7-4 makes the internal air pressure of the air-solid distributor 7 be positive pressure, and partial medium-temperature cracking air is forced to be led out from the second outlet 7-3. Thereby achieving the functional requirements of the gas-solid distributor 7.

In fig. 5B is a simplified gas-solid dispenser embodiment. The gas-solid distributor 7 adopts a gravity settling chamber structure, and medium-temperature pyrolysis gas and carried carbon powder are introduced into the gravity settling chamber through the inlet 7-1. Under the action of a baffle plate, carbon powder and a part of medium-temperature pyrolysis gas are led out from a second outlet 7-3 arranged at the bottom of the settling chamber; and the other part of medium-temperature pyrolysis gas without carbon powder is led out by a first outlet 7-2 which is wound behind the baffle plate. This embodiment fulfills the functional requirements of the gas-solid distributor 7.

In fig. 5C is another more simplified gas-solid distributor embodiment. The gas-solid distributor 7 adopts the structure of an inertial dust collector, and medium-temperature pyrolysis gas and carried carbon powder are introduced into the straight pipe section through the inlet 7-1. The carbon powder flies along a straight line under the action of inertia, is concentrated at the other end of the straight pipe section and is led out from the second outlet 7-3. And the other part of medium-temperature pyrolysis gas without carbon powder is led out from the first outlet 7-2 through a bypass. This embodiment fulfills the functional requirements of the gas-solid distributor 7.

The secondary mixer 11 employs a similar mechanism to the mixer 4, and is also provided with a first inlet 11-1, a second inlet 11-2, and an outlet 11-3. The first inlet 11-1 of the secondary mixer 11 is connected with the gas-solid distributor 7, and medium-temperature pyrolysis gas is introduced; the second inlet 11-2 of the secondary mixer 11 is connected with the gas burner 10, and high-temperature flue gas is introduced; in this embodiment, the secondary mixer 11 mixes the medium-temperature pyrolysis gas at 520 ℃ with the high-temperature flue gas at 1100 ℃ with 5% oxygen content, and the gaseous output is the high-temperature pyrolysis gas at 600 ℃.

The high temperature fan 12 provides power for the flow of the high temperature pyrolysis gas; in the embodiment, the high-temperature fan 12 is a centrifugal fan made of 310S high-temperature stainless steel, with the full pressure of 2000Pa, the flow rate of 20000 standard cubic meters per hour and the power of 18 KW. The high-temperature fan 12 is arranged between the outlet 11-3 of the secondary mixer 11 and the carbon discharging mechanism 8, and introduces high-temperature pyrolysis gas and carried carbon powder into the inner space of the carbon discharging mechanism 8.

In the embodiment, the carbon outlet mechanism 8 is a cabin body with the length of 1m, the width of 2m and the height of 2 m; the carbon outlet mechanism 8 is provided with an air inlet 8-1 and a feed inlet 8-2, and the bottom is provided with a carbon outlet 8-3. The diameter of the feed inlet 8-2 is 1.7m, and the feed inlet is connected with the discharge end 9-2 of the internal heating rotary furnace 9 through dynamic sealing and the internal space is communicated. The air inlet 8-1 of the carbon outlet mechanism 8 is connected with a high-temperature fan, and high-temperature pyrolysis gas and carried carbon powder are introduced into the inner space of the internal heating rotary furnace 9. The carbon outlet 8-3 of the carbon outlet 8 is connected with a water cooling screw, and the carbon blocks and the carbon powder discharged from the carbon outlet 8-3 are cooled to normal temperature.

The internal heat type rotary kiln 9 is a rotary kiln mechanism for heating a biomass raw material by an internal heat source. In the embodiment, the internal heating rotary kiln 9 is selected to have a length of 15m, a diameter of 2m and an inclination of 5Is supported by two tugs and is driven to rotate by a gear. Two layers of refractory bricks or insulating bricks are embedded in the furnace wall of the internal heating rotary furnace 9, and insulating cotton with the thickness of 100mm is wrapped outside. The internal heating rotary furnace 9 is provided with a feeding end 9-1 and a discharging end 9-2; biomass raw materials enter from a feeding end 9-1 of an internal heating rotary furnace 9, are converted into carbon and then enter a carbon discharging mechanism 8 from a discharging end 9-2; the carbonized gaseous product low-temperature pyrolysis gas is introduced into the anaerobic sorter 3 from the feed end 9-1 of the internal heating rotary kiln 9.

The gas burner 10 is a mechanism for sufficiently burning a combustible gas. In this embodiment, the gas burner 10 employs a combination of a combustion gun and a combustion chamber. The gas burner 10 is provided with an inlet 10-1, a distribution port 10-2, a first outlet 10-3 and a second outlet 10-4. An inlet 10-1 of the gas burner 10 is connected with a gas-solid distributor, and medium-temperature pyrolysis gas is introduced; the air distribution port 10-2 is connected with an air distribution fan; the medium-temperature pyrolysis gas and air are burnt in a burning gun, and the flame enters a burning chamber to generate high-temperature flue gas with the temperature of 1100 ℃ and the oxygen content of 5%. The first outlet 10-3 of the gas burner 10 is connected to the burner 4 for providing the burner 4 with high temperature flue gases. The second outlet 10-4 of the gas burner 10 is connected to the secondary mixer 11 to provide high temperature flue gas to the secondary mixer 11.

In this embodiment, the gas burner 10 is further provided with a waste heat outlet 10-5 connected to a waste heat boiler 13, and generates steam with a pressure of 4 tons/hour and 0.8MPa for enterprises. The tail gas of the waste heat boiler 13 passes through environmental protection equipment and is discharged through a chimney after reaching the discharge standard.

Example two

Referring to fig. 6, another embodiment of a biomass internal heating type air flow rotary carbon vapor co-production device in the present invention is shown:

A biomass internal heat type air flow rotary carbon vapor co-production device, comprising: the device comprises a hopper 1, a feeder 2, an anaerobic sorter 3, a mixer 4, a pyrolysis gas fan 5, an internal heat type fluidization tube 6, a gas-solid distributor 7, a carbon discharging mechanism 8, an internal heat type rotary furnace 9, a gas burner 10, a secondary mixer 11 and a high temperature fan 12.

In contrast to the first embodiment, the mixer 4 in the present embodiment adopts a preferable scheme as shown in fig. 4A. In the technical scheme, the annular combustion chamber 4-5 and the uniform combustion holes 4-6 are adopted, so that the high-temperature flue gas and the pyrolysis gas are fully mixed, and the mixed combustion efficiency is improved. In this embodiment, the temperature of the low temperature pyrolysis gas is 310 ℃; the high-temperature flue gas temperature is 1100 ℃, and the oxygen content is 5%; after mixed combustion, the fluidized pyrolysis gas with higher temperature is generated, the temperature can reach 800 ℃, and the fluidized pyrolysis gas is in an anaerobic state.

Compared with the first embodiment, the temperature of the fluidized pyrolysis gas reaches 800 ℃, and the internal heating type fluidization pipe 6 adopts a channel-shaped carbonization channel formed by casting refractory bricks in a building way, so that the high-temperature fluidization carbonization is realized. In this example, the fluidized pyrolysis gas at 800 ℃ is subjected to suspension heat exchange with the powdery raw material in a fluidized state, and fluidization carbonization occurs. The solid product of fluidization carbonization is carbon powder at 600 ℃, and the gaseous product is medium-temperature pyrolysis gas at 620 ℃.

The gas-solid distributor 7 of this example employs a simplified gas-solid distributor embodiment as shown in fig. 5B, relative to the first example. The scheme has simple structure and relatively low manufacturing cost. The first outlet 7-2 is provided with a butterfly valve 1 for adjusting the flow ratio of the pyrolysis gas in the two parts.

In this embodiment, a three-way pipe is connected to the second outlet 7-3 of the gas-solid distributor 7, as compared with the first embodiment. One end is connected with an air inlet 8-1 of the carbon outlet mechanism 8 through a butterfly valve 2, and the other end is connected with a first inlet 11-1 of the secondary mixer 11 through a butterfly valve 3.

In contrast to the first embodiment, in this embodiment, a thermocouple is provided at the outlet 6-2 of the internally heated fluidization tube 6 to measure the medium-temperature cracking gas temperature t. If the medium-temperature pyrolysis gas temperature T is more than or equal to the carbonization temperature T, opening a butterfly valve 2, closing a butterfly valve 3, and directly introducing the medium-temperature pyrolysis gas of the second part into the inner space of the carbon outlet mechanism 8; if the temperature T of the medium-temperature pyrolysis gas is less than the carbonization temperature T, the butterfly valve 2 is closed, the butterfly valve 3 is opened, and the medium-temperature pyrolysis gas of the second part is introduced into a secondary mixer to be subjected to secondary mixed combustion with high-temperature flue gas. In the embodiment, when the medium-temperature pyrolysis gas temperature T (620 ℃) measured by the thermocouple is greater than the carbonization temperature T (560 ℃) of the bamboo blocks, the butterfly valve 2 is opened, and the butterfly valve 3 is closed.

Compared with the first embodiment, in the present embodiment, the feeding end 9-1 or the discharging end 9-2 of the internal heating rotary kiln 9 is provided with a cone, so that the diameters of two ports are effectively reduced; the cone can reduce the dynamic seal of the connection of the feeding end 9-1 and the anaerobic sorter 3, and also can reduce the dynamic seal of the connection of the discharging end 9-2 and the carbon outlet mechanism 8, thereby being beneficial to improving the reliability of dynamic seal and reducing the cost.

In contrast to the first embodiment, in this embodiment, the gas burner 10 eliminates the burning gun and adopts a large-space combustion chamber scheme. The combustible gas and air are subjected to diffusion combustion in the space of the combustion chamber, so that the combustion efficiency is reduced, but local high-temperature points are avoided, and the generation of nitrogen oxides in the combustion process is inhibited.

All examples are given solely for the purpose of illustrating the invention and are not to be construed as a specific limitation thereof.

Claims

1. The biomass internal heating type airflow rotary carbonization method is characterized by comprising the following steps of:

(1) Feeding biomass raw materials: the biomass raw materials are put into the separation space by a feeder through a bin/hopper as a buffer;

the biomass raw material is mixed with a bulk raw material and a powdery raw material;

(2) Anaerobic sorting process: in the separation space, carrying out anaerobic separation on the biomass raw materials by utilizing low-temperature pyrolysis gas, wherein the heavier blocky raw materials in the biomass raw materials fall into the internal heating rotary furnace after separation, and the lighter powdery raw materials in the biomass raw materials are led out along with the low-temperature pyrolysis gas;

The anaerobic sorting is specifically a sorting mode utilizing an airflow sorting principle, and the internal atmosphere is in an anaerobic state; the anaerobic condition is that the oxygen molecular content of the gas is 0 or approximately 0 (less than 1%); the low-temperature pyrolysis gas is a gaseous product of the internal heating rotary furnace, contains combustible gas components and is in an anaerobic state;

(3) And (3) mixing and burning pyrolysis gas: mixing the low-temperature pyrolysis gas and the high-temperature flue gas in the step (2) to generate fluidized pyrolysis gas;

the mixed combustion is specifically under-oxygen combustion of pyrolysis gas, and aims to deplete the oxygen content in high-temperature flue gas and raise the temperature of the pyrolysis gas, and is characterized in that gaseous products are still combustible gas and are in an anaerobic state; the fluidized pyrolysis gas is a gaseous product of mixed combustion of low-temperature pyrolysis gas and high-temperature flue gas; the high-temperature flue gas is a gaseous product of a gas combustion furnace;

the fluidization carbonization is specifically that the powdery raw material is driven by the fluidization cracking gas to be in a fluidization state, and the fluidization cracking gas and the powdery raw material in the fluidization state perform suspension heat exchange to convert the powdery raw material into carbon powder; the fluidization carbonization is also characterized in that the fluidization pyrolysis gas and the powdery raw material move in the same direction, the solid output is carbon powder, and the gaseous output is medium-temperature pyrolysis gas; the medium-temperature cracking gas is in an anaerobic state;

the secondary mixed combustion is secondary mixed combustion of medium-temperature pyrolysis gas and high-temperature flue gas; the high-temperature cracking gas is a gaseous product of secondary mixed combustion and is characterized in that the high-temperature cracking gas is combustible gas and is in an anaerobic state, and the temperature of the high-temperature cracking gas is higher than the carbonization temperature T;

(8) Mixing and discharging carbon: the carbon powder is settled in the internal heating rotary furnace, mixed with the carbon blocks and discharged through a carbon outlet of a carbon discharging mechanism after cooling;

(9) And (3) heat supply: the medium-temperature pyrolysis gas of the first part in the step (5) is fully combusted in a gas burner, and gaseous products are high-temperature flue gas; the high-temperature flue gas and the low-temperature pyrolysis gas are mixed to burn, so that heat energy is provided for fluidization and carbonization; the redundant high-temperature flue gas or medium-temperature pyrolysis gas in the gas burner can be introduced into a waste heat boiler or a gas boiler for energy recovery and utilization, and steam is generated to supply heat for enterprises;

(10) Pyrolysis gas circulation mutually benefits: the circulation is to re-introduce the low-temperature pyrolysis gas generated in the step (7) back to the step (2) for the anaerobic separation, so as to realize the pyrolysis gas circulation; the reciprocity is that the gaseous output (low-temperature pyrolysis gas) of the rotary carbonization process provides a heat source for the fluidization carbonization, the gaseous output (medium-temperature pyrolysis gas) of the fluidization carbonization process also provides a heat source for the rotary carbonization, and the two carbonization processes are mutually utilized.

2. A biomass internal heating type air flow rotary carbon vapor co-production device, which is characterized by comprising:

the device comprises a storage bin/hopper, a feeder, an anaerobic sorter, a mixing burner, a pyrolysis gas fan, an internal heating type fluidization tube, a gas-solid distributor, a carbon discharging mechanism, an internal heating type rotary furnace, a gas burner and a waste heat boiler;

the bottom of the bin/hopper is connected with the feeder; the feeder is connected with the anaerobic sorter so that biomass raw materials in the bin/hopper enter the internal space of the anaerobic sorter;

the anaerobic sorter is a mechanism utilizing the air flow sorting principle and is characterized in that low-temperature pyrolysis gas is used as sorting air flow, and the internal atmosphere is in an anaerobic state; the anaerobic sorter is provided with an inlet and an outlet; the inlet is connected with the feeding end of the internal heating rotary furnace and the internal space is communicated; the outlet is connected with the mixer;

the mixer is a mechanism for mixing and combusting low-temperature pyrolysis gas and high-temperature flue gas, and the gaseous output is fluidized pyrolysis gas; the mixer is provided with a first inlet, a second inlet and an outlet; the first inlet is connected with an anaerobic separator and introduces the low-temperature pyrolysis gas; the second inlet is connected with the gas burner and introduces the high-temperature flue gas; the outlet is connected with the internal heating type fluidization pipe and is used for leading out fluidized pyrolysis gas; the low-temperature pyrolysis gas is a gaseous product of the internal heating rotary furnace; the high-temperature flue gas is a gaseous output of the gas burner;

The internal heating type fluidization tube is a mechanism for implementing fluidization carbonization, the solid output is carbon powder, and the gaseous output is medium-temperature pyrolysis gas; the internal heating type fluidization pipe is a long-channel carbonization pipeline with a fireproof material or high-temperature resistant metal as an outer wall, and is provided with an inlet and an outlet; the inlet is connected with the mixer to introduce the fluidized pyrolysis gas and the carried powdery raw materials; the outlet is connected with the gas-solid distributor and used for leading out the medium-temperature pyrolysis gas and the carbon powder;

the pyrolysis gas fan can be arranged between the anaerobic sorter and the mixer, between the mixer and the internal heating type fluidization pipe, and between the internal heating type fluidization pipe and the gas-solid distributor to provide power for the flow of gas in the internal heating type fluidization pipe;

the gas-solid distributor is of an internal three-way structure and is provided with an inlet, a first outlet and a second outlet; the gas-solid distributor redistributes the medium-temperature pyrolysis gas and the carried carbon powder: the medium-temperature pyrolysis gas in the first part does not carry carbon powder and is led out from the first outlet; the medium-temperature pyrolysis gas in the second part carries carbon powder and is led out from the second outlet; the inlet is connected with the internal heating type fluidization tube; the first outlet is connected with a gas burner; the second outlet has two connection modes:

The first connecting mode is connected with the carbon outlet mechanism, and the pyrolysis gas and the carried carbon powder in the second part are introduced into the inner space of the carbon outlet mechanism;

the second connecting mode is connected with the secondary mixer; the secondary mixer is a mechanism for mixing and combusting the medium-temperature pyrolysis gas in the second part, and the gaseous output is high-temperature pyrolysis gas; the secondary mixer is provided with a first inlet, a second inlet and an outlet; the first inlet is connected with the gas-solid distributor; the second inlet is connected with the gas burner and introduces the high-temperature flue gas; the outlet is connected with the carbon outlet mechanism through a high-temperature fan, and the high-temperature pyrolysis gas and the carried carbon powder are introduced into the inner space of the carbon outlet mechanism;

the carbon outlet mechanism is provided with an air inlet and a feed inlet, and the bottom of the carbon outlet mechanism is provided with a carbon outlet; the air inlet is connected with the gas-solid distributor or the high-temperature fan; the feeding port is connected with the discharging end of the internal heating rotary furnace and the internal space is communicated; the carbon outlet is connected with cooling equipment for cooling the discharged carbon;

the internal heating type rotary furnace is a rotary furnace mechanism for heating biomass raw materials through an internal heat source; the internal heating rotary furnace is provided with a feeding end and a discharging end; biomass raw materials enter from the feeding end, are converted into carbon and then enter the carbon discharging mechanism from the discharging end; the low-temperature pyrolysis gas is introduced into the anaerobic sorter from the feeding end;

The gas burner is a mechanism for fully burning combustible gas, and the gaseous output is high-temperature flue gas; the gas burner is provided with an inlet, a hollow distribution port and a first outlet; the inlet is connected with the gas-solid distributor; the air distribution port is connected with an air distribution fan; the first outlet of the gas burner is connected with the mixer; the gas burner is also provided with a second outlet corresponding to the second connection mode of the gas-solid distributor; the second outlet is connected with the secondary mixed burner to provide high-temperature smoke for secondary mixed combustion. The gas burner is provided with a waste heat outlet; the waste heat outlet is connected with a waste heat boiler, waste heat recovery and utilization are carried out on redundant high-temperature flue gas, and carbon-steam co-production is realized.