• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    process for treating an aqueous solution, and installation for treating an aqueous solution. A process and installation for the treatment of an aqueous solution containing substantial concentrations of a variety of contaminants, including solids, semisolids, colloids, complexes, oligomers, polyvalent, organic and monovalent, and which tends to form scale gels and precipitates at their concentration levels. are increased during treatment of the aqueous solution, the process comprising the steps of: a) feeding the aqueous solution to an ultrafiltration (uf) facility and recovering from a reduced uf permeate in such suspended solids, semisolids and colloids; b) feeding the uf permeatode obtained from step (a) to a nanofiltration (nf) plant and recovering from a reduced nf permeate in such complexes, polyvalent and organic oligomers and alimetation of the nf permeates obtained from (b) a first reverse osmosis (ro) installation and recovery from a reduced ro permeate in such monovalents. The process and plant can be used to treat process water from wet process acid phosphate production.
    公开号:BR112013001313B1
    申请号:R112013001313-3
    申请日:2011-07-06
    公开日:2018-12-26
    发明作者:Yilong Chen；Hongming TANG；Yanfeng Zhang
    申请人:Sunshine Kaidi New Energy Group Co., Ltd.；
    IPC主号:
    专利说明:

    DESCRIPTIVE REPORT
    METHOD AND APPARATUS FOR BIOMASS PYROLYSIS AT LOW TEMPERATURE AND BIOMASS GASIFICATION AT HIGH TEMPERATURE FIELD OF THE INVENTION
    The invention relates to a technology for the transformation of combustible materials into a clean and highly efficient synthesis gas, and more particularly to a method and system for the production of synthesis gas from biomass by low temperature pyrolysis and by high temperature gasification.
    BACKGROUND OF THE INVENTION
    The technology of gasification of combustible materials reached a surprising development in the late twentieth century, especially the technology of gasification of combustible coal, which has been very mature. Researchers have successfully developed a process for coal gasification that is widely applicable, highly efficient in gasification and free from pollution. Biomass gasification technology, such as tree branches, straw, and other agricultural and forest waste, is a new technology for the widespread use of energy in the 21st century. Conventional biomass gasification technology includes: fixed bed gasification , fluidized bed gasification, and two gasification phases, all of which are direct gasification technologies. The processes of direct gasification technology 20 are characterized in that the heat produced by a part of the biomass provides energy resources for gasification, air, oxygenated air, or a combination of oxygenated air and water vapor works as a oxidant during the gasification reaction. However, studies have shown that direct biomass gasification technologies are disadvantageous in the following 25 aspects:
    Firstly, the components and the calorific value of biomass fuels are unstable, biomass has a low combustion point and fast fuel reaction, so the explosion occurs easily. When part of the regions is overheated and cooked, the gasifier's operating temperature is very difficult to control.
    Second, when air functions as an oxidizer in which the content of inactive N2 gas is prominent, this results in a higher content of N2, a lower content of effective gas (CO + H2), and a lower proportion of H2 / CO, in addition, the heat value of the synthesis gas is low and unstable, which only keeps 5000 KJ / Nm3 below and hardly satisfies the need for later industrial use.
    Third, when oxygenated air functions as an oxidizer, despite the relatively low N2 content, an additional air separation device is required. Because of a large capacity and high consumption of
    2/12 energy from the air separation device, such a process greatly increases the cost of production.
    Fourth, when oxygenated air and water vapor work as both oxidants, although the N2 index in the synthesis gas is lowered, and the H2 content is increased, water vapor functioning as a reaction medium still consumes a large amount of thermal energy, plus the energy consumption for air separation, the process iarly maximizes the production cost.
    Fifth, about 15-20% of biomass is needed to seauto ignite to provide energy source for gasification, but at the same time a large amount of CO2 is produced in combustion, correspondingly, the effective gas content ( CO + H2) is reduced. In addition, high temperature synthesis gas and mixed air carry a large amount of sensitive heat and, therefore, the conversion of thermal energy to chemical energy is largely minimized and the efficiency of the cooled gas is also reduced, which is generally 70% less and not more than 80% in exceptional conditions.
    Sixth, the operating temperature of the gasifier is generally controlled from 800-1200 ° C, at such a temperature, the biomass gasification produces a large amount of tar that is difficult to remove, and a lot of aggregate tar in the device and pipes it is able to cause blockage of the tubes and contamination of the device.
    Seventhly, the gas produced in biomass gasification contains an important content of alkali metal oxides comprising K and Na, which is generally 20-40% in total mass in ashes. However, at a temperature above 800 ° C, alkali metal oxides are able to be gasified and mixed in the synthesis gas, which affects not only the property of the synthesis gas, but also adheres to tubes and devices together with tar, thus resulting in severe corrosion in devices and pipes.
    Taking into account the existing problems mentioned above, direct biomass gasification technologies are difficult to be applied in practical production. Thus, a method for gasifying biomass that can be applied in industrial production and converted into commercial advantages is desired.
    SUMMARY OF THE INVENTION
    In view of the problems described above, it is an objective of the present invention to provide a method and system for the production of synthesis gas from biomass by low temperature pyrolysis and high temperature gasification. The method features easy control, energy savings and low cost. The synthesis gas produced has a high efficiency and high calorific value, with no
    3/12 alkali metal or tar dioxides.
    To achieve the above objective, a method is provided for the production of synthesis gas from biomass by low temperature pyrolysis and high temperature gasification. The method employs a superheated water vapor as an oxidizer and an energy carrier, conducts pyrolysis and biomass gasification at different temperature ranges, and finally produces clean desynthesis gas. The method comprises the following steps:
    a) Grinding the biomass, feeding the biomass to a pyrolysis furnace, spraying a superheated low temperature water vapor into the pyrolysis furnace, controlling the pyrolysis furnace at an operating temperature of 500-800 ° C, contacting the biomass with superheated low temperature water vapor to carry out a pyrolysis reaction to produce crude synthesis gas and an ash comprising a coke. Because the operating temperature of the pyrolysis furnace is below the alkali metal oxide sublimation points that comprise K and Na, the alkali metal oxides exist in the ash that comprises coke and the raw synthesis gas comprises no tar or lower tar .
    b) Cooling the ash which comprises the coke generally to a temperature of 150 ° C below, and separating the coke from the ashes. The coke is used for the production of synthesis gas in the next step, and the ashes comprising the alkali metal oxides are transported to an ash deposit.
    c) Transport of crude synthesis gas and coke in a gasifier, spraying a superheated high temperature water vapor to the gasifier, controlling the gasifier at an operating temperature of 1200-1600 ° C, contact of the biomass with water vapor superheated high temperature for conducting a gasification reaction and acquisition of primary synthetic gas. Because the operating temperature of the gasifier is above a temperature for forming tar, the raw synthesis gas and coke are completely aerated, and the acquired primary synthesis gas comprises no tar.
    d) cooling, dust removal, deacidification and drying of the primary synthesis gas to produce clean synthesis gas. The cooling process is not only a necessity for the entire process for the production of synthesis gas, but also recovers a large amount of sensitive heat for wide use. The dust removal process separates the dust from the raw synthesis gases, and decreases the dust concentration of the gas by 50 mg / Nm3 below. Harmful ingredients, such as H 2 S, COS, HCL, NH 3 , HCN and are removed from the synthesis gas in the deacidification process. After desiccation, the primary synthesis gas is transformed into gas
    4/12 of clean synthesis, which is stored for later industrial application.
    The biomass ground in step a) has a particle size of 20 mm χ 20 mm below and a water content of 40% by mass below. The biomass of such a particle size and water content contacts completely with the superheated high temperature water vapor, so that the processes of desiccation, separation of volatile materials, pyrolysis and evaporation are stably conducted, and the The gasifier's operating temperature is easy to control, cokes do not form in the pyrolysis oven.
    In step a), in a nitrogen atmosphere, a feed input to the pyrolysis furnace is supplied, in the event of fire and explosion caused by the leakage of crude synthesis gas from the pyrolysis furnace.
    In step a), a preferred operating temperature of the pyrolysis oven is controlled at 500-650 ° C, an operating pressure of the pyrolysis oven is controlled at 105-109 kPa. An inlet speed of low temperature superheated water vapor into the pyrolysis furnace is 35-50 m / s; a retention time of crude synthesis gas in the pyrolysis oven is 15-20s, and an exit speed of crude synthesis gas from the pyrolysis oven is 15-20 m / s. Thus, the pyrolysis furnace operates at normal pressure, and no special pressure device is needed, thereby reducing the cost of production. The biomass in the pyrolysis oven is quickly desiccated, separated from volatile matter, and pyrolyzed during contact with the crude synthesis gas and the low temperature superheated water vapor. In addition, the operating temperature of the pyrolysis furnace is much lower than the alkali metal oxide sublimation points, which are about 800 ° C, so that the alkali metal oxides are removed from the crude synthesis gas . The relatively lower outlet speed of the pyrolysis oven prevents ash from aggregating at the outlet of the pyrolysis oven and gas tubes.
    In step c), a preferred gasifier operating temperature is controlled at 1200-1400 ° C, and a preferable gasifier operating pressure is controlled at 105-109 kPa. An inlet speed of the superheated high temperature water vapor to the gasifier is 35-50 m / s, and a retention time of the raw synthesis gas in the gasifier is 15-20s, and an outlet speed of the gas from primary synthesis from the gasifier is 15-20 m / s. Thus, the gasifier operates at normal pressure, and no special pressure device is needed, thereby reducing the cost of production. A high inlet speed of high temperature superheated water vapor to the gasifier greatly improves the contact and mixing of the crude synthesis gas and coke. The gasifier's operating temperature range is suitable, which guarantees full gasification of the gas
    5/12 crude and coke synthesis during contact with high temperature superheated water vapor, the acquired primary synthesis gas comprises no tar; at the same time energy consumption is reduced as much as possible, and the gasifier's performance is greatly improved.
    In step d), the primary synthesis gas is cooled to a temperature of 260-320 ° C, and then cleaned. While the outlet temperature of the primary synthesis gas from the gasifier is still high, around 120-1400 ° C, the cooling process is not only favorable for the subsequent collection of dust, edacidification and desiccation, but also useful for recovering the sensitive heat in the primary synthesis gas, so as to obtain a wide use of the exhaust heat.
    A system for the production of synthesis gas from biomass by low temperature pyrolysis and high temperature gasification according to the aforementioned method, comprises: the pyrolysis oven, the gasifier, a low temperature plasma torch heater , a high temperature plasma torch heater, a water storage tank, a water pump, and a heat exchanger.
    The water storage tank is connected to a water inlet of the heat exchanger through the water pump. A steam outlet from the heat exchanger is both connected to a steam inlet of the low temperature plasma torch heater 20 and to a steam inlet of the high temperature plasma torch heater. A steam outlet from the low temperature torch heater is connected to a steam nozzle in the pyrolysis oven. A steam outlet from the high temperature plasma torch heater is connected to a gasifier steam nozzle.
    A gas outlet of the pyrolysis oven is connected to a gas inlet of the aerator, an ash outlet of the pyrolysis oven is connected to an ash inlet of an ash cooler, and an ash outlet of the ash cooler is connected to a coke ash separator inlet. A gas outlet of the gasifier is connected to a gas inlet of the heat exchanger, and a gas outlet of the heat exchanger is connected to a dust collector, a de-acidifying tower and a series desiccator.
    The plasma torch heating apparatus is advantageous in ultra-high temperature heat, rapid heat and mass transfer, high efficiency, and adjustable calorific power, when it is used to heat water in the storage tank 35 water, superheated steam high temperature water can be effective, successively, and steadily produced. The high temperature of the superheated water vapor works not only as an oxidizer but also as an
    6/12 energy carrier, so the aerator is kept working steadily. The heat exchanger effectively recovers a large amount of the sensitive heat from the synthetic primary gas. The water in the water storage tank is preheated and transformed into saturated water vapor, due to the sensitive heat, and the saturated water vapor is then transported to the plasma torch heater, thus the energy consumption of the plasma torch heater is lowered, and overall use of heat energy is achieved.
    A nitrogen protection device is connected to a feed input of the pyrolysis oven. A nitrogen sealing layer prevents the crude synthesis gas 10 from leaking out of the gasifier, and keeps air outside the gasifier, fire and explosion are eliminated and the property of the crude synthesis gas is ensured. A coke outlet from the ash coke separator is connected to a coke inlet of the aerator by means of a coke conveyor. For example, a screw feeder is used to transport the coke directly to the aerator, so that the intermediate manual transport is stored, which improves the stability and succession of the aerator.
    The steam nozzles arranged in the pyrolysis oven and gasifier are grouped at 2-4 levels in height, respectively, and the steam nozzles at each level are uniformly and tangentially arranged along a circumferential direction.
    Thus, the superheated water vapor is sprayed into the pyrolysis oven and gasifier from different levels, and a uniform and stable temperature displayed is maintained at different height levels, which results in a complete contact between the water vapor overheated and reagents.
    Based on the inherent characteristics of water, ash, volatile matter, and melting point of biomass ash, and combined with the operating characteristics of the gasifier, the method of the invention employs superheated water vapor instead of conventional oxidizing air. or oxygenated air, to produce synthesis gas from biomass by pyrolysis at low temperature and gasification at high temperature. Advantages of the invention are summarized below:
    First, the superheated water vapor is used to gasify the biomass indirectly. Overheated water vapor is not only an oxidizer but also an energy carrier, so oxidizing air or oxygenated air is not needed, which means that a high energy consumed air separation device is not required, and energy consumption throughout the process and total production costs are largely minimized.
    Second, no auto ignition occurs in biomass during pyrolysis and gasification, thus solving problems in the gasification process
    Conventional 7/12, such as the explosion of fuel in the pyrolysis oven or gasifier, regional coke, and difficulties in controlling each process. Since air or oxygenated air is no longer needed in the reaction, the synthesis gas has a high proportion of H 2 / CO, and a high content of the effective gas (CO + H 2 ), which is 85% above thus, the heat value of the synthesis gas is greatly improved, and the use of the synthesis gas is much wider.
    Third, the main reaction devices are the pyrolysis oven and the gasifier. Biomass is first pyrolysed in crude synthesis gas and coke at a low temperature, and both productions are aerated at an elevated temperature. Once the temperature ranges are properly adjusted, the crude synthesis gas produced does not comprise alkali metal oxides, the tar and coke are all transformed into the primary synthesis gas, so that the carbon conversion is very high, the gas of acquired primary synthesis is absent of impurities that are dirty and corrosive to the equipment and tubes, and the subsequent cleaning process becomes much simpler.
    Fourthly, the plasma torch heater produces all the heat energy that is necessary for the gasification of biomass by the superheated water vapor outside the gasifier, the thermal energy of the biomass fuel is completely transformed into chemical energy, and the efficiency of refrigerated gas is 88% below, which is 8% higher than that of conventional gas.
    Fifth, the plasma torch heater has a high thermal efficiency and an adjustable input power, when the biomass fuel components change, the power of the plasma torch heater can be adjusted, so that it is very convenient for control the temperature of the superheated water vapor, and maintain the gasifier's work stable, and ensure a stable output of the primary synthesis gas and a stable property.
    Tests have shown that the method and system of the invention is applicable to different types of biomass fuels, and is especially applicable in the industries of the integrated combination of gasification biomass cycle and liquid biomass fuel.
    BRIEF DESCRIPTION OF THE DRAWINGS
    FIG. 1 is a diagram of the structure of a system for producing synthesis gas from biomass by low temperature pyrolysis and high temperature gasification of the invention.
    DETAILED DESCRIPTION OF CONFIGURATIONS
    A method and system for producing synthesis gas from biomass by low temperature pyrolysis and high temperature gasification is specifically
    8/12 described with the accompanying drawings:
    As shown in FIG. 1, a system for the production of synthesis gas from biomass by pyrolysis at low temperature and gasification at high temperature, consisting of: a conveyor belt 1, a pulley 2, a screw feeder 3, a pyrolysis oven 5 and a gasifier 9 for pyrolysis and biomass gasification, respectively; a low temperature plasma torch heater 8 and a high temperature plasma torch heater 10 for the supply of superheated water to the pyrolysis oven 5 and gasifier 9, respectively, a water storage tank 17 and a water pump 16 for supplying water to the low temperature plasma torch heater 8 and high temperature plasma torch heater 10, a heat exchanger 11 for wide use of heat energy; and a dust collector 12, a de-acidification tower 13, and a desiccator 14 for further cleaning of the synthesis gas.
    An outlet end of the conveyor belt 1 is arranged over an inlet of the hopper 2, an outlet of the hopper 2 is connected to a feed inlet of the screw feeder 3, and a feed outlet of the screw feeder 3 is connected to a feed input from the pyrolysis oven 5.
    As a key device for a first stage of biomass processing, the pyrolysis furnace 5 comprises an enclosure comprising a chilled air jacket or a chilled water jacket, and is thermally insulated at normal pressure. The feed inlet of the pyrolysis oven 5 is arranged on an upper part or an upper end; to ensure a uniform addition of biomass and a stable flow field inside the pyrolysis oven, the number of feed inlets is two or four. A nitrogen protection device4 is connected to the feed input of the pyrolysis oven 5, so that a nitrogen sealing layer is formed to effectively separate the crude synthesis gas from the air. A gas outlet from the pyrolysis furnace 5 is arranged over the top or bottom, and is connected to a gas inlet of the gasifier 9 via a tube, so that the raw synthesis gas is transported to the gasifier 9 The pyrolysis oven 5 comprises an ash outlet disposed at a bottom, the number of the ash outlet is one or two. An ash discharged from the ash outlet is in a liquid state. The ash outlet is connected to an ash inlet of an ash cooler 6 for cooling the ash comprising a coke. An ash outlet from the ash cooler is connected to a feed inlet of a coke ash separator 7 to separate the coke from the ash. Preferably, the coke outlet from the coke ash separator
    9/12 is connected to a coke inlet of the gasifier 9 via a coke conveyor 19, which is an energy saver compared to manual transport and ensures a stable and continuous operation of the gasifier 9.
    As a key device for a second stage of biomass processing, the gasifier 9 also comprises a box comprising a chilled coating or chilled water coating, and is thermally insulated at normal pressure. The coke inlet of the aerator 9 is arranged at the top or at an upper end. To ensure a uniform addition of coke and a stable flow field inside the gasifier 9, the number of the coke inlet is one or 10 two, depending on the capacity. An ash outlet from the aerator 9 is arranged at a bottom, from which an ash is discharged in a liquid state; the number of the ash outlet is one or two, depending on the capacity. The gas outlet of the aerator 9 is arranged at the top, or at a lower end, and is connected to a gas inlet of the heat exchanger 15 11, a gas outlet of the heat exchanger 11 is connected to the dust collector 12, the de-acidification tower 13, and the desiccator 14 in series, and an outlet of the desiccator 14 is connected to a gas storage tank 15.
    The superheated water vapor sprayed in the pyrolysis oven 5 and the gasifier 9 is transformed from soft or saline water in the water storage tank 17 by heating. An outlet of the water storage tank 17 is connected to a water inlet of the heat exchanger 11 through the water pump 16. The heat exchanger 11 is generally a dismantled boiler. A steam outlet from the heat exchanger 11 is simultaneously connected to a steam inlet of the low temperature plasma torch heater8 and a steam inlet of the high temperature plasma torch heater. A steam outlet from the low temperature plasma torch heater8 is connected to a steam nozzle of the pyrolysis oven 5 via a tube. The steam outlet of the high temperature plasma torch heater is connected to a gas nozzle of the aerator 9 via a tube. Preferably, the 30 steam nozzles arranged in the pyrolysis oven 5 and gasifier 9 are grouped in
    2-4 levels of height, respectively, and the steam nozzles of each level are uniformly and tangentially arranged along a circumferential direction. Thus, a uniform and stable deposited vapor is maintained, and complete contact between the superheated water vapor and the reagents is achieved.
    The system also includes an ash deposit 18, and the solid ash from the coke ash separator 7 and the ash liquid from the gasifier 9 are transported to the ash deposit 18 by manual or mechanical mode.
    12/10
    A method for producing synthesis gas from biomass by low temperature pyrolysis and high temperature gasification using the above system is specifically described below.
    A) Ground biomass is transported to the pyrolysis furnace 5 through the conveyor belt 5, the hopper 2, and the screw feeder 3, in turn, at the same time nitrogen is introduced from a nitrogen protection device 4 for a feed inlet of the pyrolysis oven 5. When the biomass is a gray straw, for example, branches and roots of trees, a particle size of the biomass is controlled at 20 mm χ 20 mm below, and a water content of the biomass is controlled at 40% mass below. When biomass is yellow straw, for example, stems of beaten cereal, stalk, callus stems, the size of the biomass particles can be relatively large.
    B) Desalinated water is emitted from a water storage tank 17 to a water inlet of the heat exchanger 11 through a water pump 16, and the desalinated water exchanges heat with a primary synthesis gas inlet. from a gas inlet of the heat exchanger 11, and a sensitive heat is extracted by the desalinated water, during which 0.4-0.6 Mpa of saturated steam is produced. Saturated steam is emitted from a steam outlet from the heat exchanger 11 to the low temperature plasma torch heater8 and the high temperature plasma torch heater O and transformed into superheated water vapor of different temperatures.
    C) The superheated low temperature water vapor produced from the low temperature plasma torch heater8 is at a temperature of 500-800 ° C, and is introduced into the pyrolysis oven 5 through the steam nozzles.
    Operating parameters of the pyrolysis oven 5 are: 500-650 ° C temperature, and 105-109 kPa pressure. An entry speed of the low temperature superheated water vapor into the pyrolysis oven 5 is controlled at 35-50 m / s, so that the biomass is fully in contact with the superheated low temperature water vapor and pyrolyzed in the gas. crude synthesis and ashes comprising coke. The crude synthesis gas is maintained in the pyrolysis oven 5 for 15-20s, and an output rate of the crude synthesis gas from the pyrolysis oven 5 is controlled at 15-20 m / s.
    D) The crude synthesis gas at a temperature of 500-650 ° C is emitted from the pyrolysis oven 5 to the gas inlet of the gasifier 9 through the tube, and the ash comprising the coke at a temperature of 500- 650 ° C is transported from the ash outlet of the pyrolysis oven 5 into the ash cooler, after heat recovery, the temperature of the ash comprising the ash is cooled to
    12/11
    150 ° C below. The coke is separated from the ash by the coke ash separator 7. The coke is then transported to the gasifier coke inlet 9 via the coke conveyor 19, and the ash from the coke ash separator 7 is transported to the coke ash separator. ash deposit 18.
    E) The superheated high temperature water vapor produced from the high temperature plasma torch heater 10 is at a temperature of 1200-1600 ° C, and is emitted into the gasifier 9 through the steam nozzles. Operating parameters of the aerator 9 are: 1200-1400 ° C temperature, and 105-109 kPa pressure. An inlet speed of superheated high temperature water vapor 10 to the gasifier 9 is controlled at 35-50 m / s, so that the raw synthesis gas is fully in contact with the superheated, high temperature water vapor in the gas. primary synthesis gas. The primary synthesis gas is maintained in the aerator 9 for 15-20s, and an outflow rate of the primary synthesis gas from the aerator 9 is controlled at 15-20 m / s.
    F) Liquid ash at a temperature of 1200-1400 ° C is emitted from the ash outlet of the gasifier 9 and transported to the ash tank 18 for wide use. The primary synthesis gas at a temperature of 1200-1400 ° C is transported from the gasifier 6 to the gas inlet of the heat exchanger 11 through the tube. After being cooled to a temperature of 260-320 ° C by 20 desalinated water, the primary synthesis gas is emitted from the gas outlet of the heat exchanger 11 to the dust collector 12. The powder in the primary synthesis gas is trapped by the dust collector 12, and a powder concentration of the primary synthesis gas at the outlet of the dust collector 12 is less than 50 mg / Nm 3 .
    G) After the removal of dust, the primary synthesis gas is transported to the desaccification tower 25, in which the harmful ingredients, such as H 2 S, COS, HCL, NH 3 and
    HCN are removed.
    H) After de-acidification, the primary synthesis gas is transported to desiccator 14, in which water is removed, and clean synthesis gas is acquired. The clean synthesis gas is transported to a gas storage tank 15 and is stored for further industrial application.
    After several times of testing and data detection, the main components and characteristics of the clean synthesis gas are shown in Table 1. As shown in Table 1, the clean synthesis gas produced by the method comprises 90% of a total content of (CO + H 2 ), in an H 2 / CO ratio equal to or greater than 35 1, a heat value of the synthesis gas is 12.5-13.4 MJ / Nm 3 , and an efficiency of the refrigerated gas is about 88%. Thus, synthesis gas can bring great commercial advantages, and is especially applicable in the combination industries
    12/12 integrated gasification biomass cycle and liquid biomass fuel.
    Table 1
    Number Component unity Value 1 CO % (vol.) 30-40 2 h 2 % (vol.) 40-50 3 N 2 + Air % (vol.) <1.0 4 CO 2 % (vol.) 15-20 5 ch 2 % (vol.) 5-6 6 CnHm % (vol.) <2 7 Synthesis gas heat value (PCI) MJ / Nm 3 12.5-13.4 8 Efficiency of a cooled gas % -88.0
    1/4
    权利要求:
    Claims (9)
    [1]
    1. METHOD FOR LOW TEMPERATURE BIOMASS PYROLYSIS AND HIGH TEMPERATURE BIOMASS GASIFICATION, the method using superheated water vapor as an oxidizer and energy carrier, leading to biomass pyrolysis and gasification at different temperature ranges, and, finally, producing clean synthesis gas, characterized by the fact that the method comprises the following steps:
    a) generation of a first superheated water vapor at a temperature of 500-800 ° C; milling of biomass; feeding the biomass to a pyrolysis furnace while spraying a first superheated water vapor generated by a first plasma torch heater to the pyrolysis furnace. controlling the pyrolysis furnace at an operating temperature of 500-650 ° C, contacting the biomass with the first superheated water vapor so that a pyrolysis reaction produces crude and gray synthesis gas that comprises coke;
    b) cooling the ash, and separating the coke from the ash;
    c) generation of a second superheated water vapor at a temperature of 1200-1600 ° C, transport of the crude synthesis gas and coke to a gasifier, the spraying of a second superheated water vapor generated by a second torch heater. plasma for the gasifier, controlling the gasifier at an operating temperature of 12001600 ° C, contacting the biomass with the second water vapor
    Petition 870180138891, of 10/8/2018, p. 3/31
    [2]
    2/4 superheated to conduct a gasification reaction to produce primary synthesis gas: e
    d) cooling, dust removal, deacidification and drying of synthetic primary gas to obtain clean synthesis gas.
    wherein the pyrolysis furnace of step a) additionally has a controlled operating pressure between 105-109 kPa; a speed of entry of the first superheated water vapor into the pyrolysis furnace of 35-50 m / s; and a retention time of the crude synthesis gas in the pyrolysis furnace of 15-20s, and an exit speed of the crude synthesis gas from the pyrolysis furnace of 15-20 m / s.
    2. METHOD FOR BIOMASS PYROLYSIS AT LOW TEMPERATURE AND HIGH TEMPERATURE BIOMASS GASIFICATION, according to claim 1, characterized by the fact that the biomass ground in step a) has a particle size less than 20 mm x 20 mm and a water content less than 40% by mass.
    [3]
    3. METHOD FOR LOW-TEMPERATURE BIOMASS PYROLYSIS AND HIGH-TEMPERATURE BIOMASS GASIFICATION, according to claims 1 and 2, characterized in that in step a) a nitrogen atmosphere is supplied to a feed input of the pyrolysis oven .
    [4]
    4. METHOD FOR BIOMASS PYROLYSIS AT LOW TEMPERATURE AND HIGH TEMPERATURE BIOMASS GASIFICATION, according to claims 1 and 2, characterized by the fact that the gasifier's operating temperature in the
    Petition 870180138891, of 10/8/2018, p. 4/31
    3/4 step c) be controlled at 1200-1400 ° C, and a gasifier operating pressure is controlled at 105-109 kPa; an inlet speed of the second superheated water vapor in the gasifier is 35-50 m / s, and a retention time of the raw synthesis gas in the gasifier is 15-20s, and an exit speed of the primary synthesis gas at from the aerator is 15-20 m / s.
    [5]
    5. METHOD FOR LOW TEMPERATURE BIOMASS PYROLYSIS AND HIGH TEMPERATURE BIOMASS GASIFICATION, according to claims 1 and 2, characterized in that in step d), the primary synthesis gas is cooled to a temperature of 260-320 ° C.
    [6]
    6. EQUIPMENT FOR BIOMASS PYROLYSIS AT LOW TEMPERATURE AND HIGH TEMPERATURE BIOMASS GASIFICATION, according to the method of claim 1, the apparatus comprising: a pyrolysis oven (5); an aerator (9); a first plasma torch heater (8); a second plasma torch heater (10); a water storage tank (17); a water pump (16); and a heat exchanger (11); characterized by the fact that the water storage tank (17) is connected to a water inlet of the heat exchanger (11) through the water pump (16); a steam outlet from the heat exchanger (11) is connected to a steam inlet of the first plasma torch heater (8) and to a steam inlet of the second plasma torch heater (10); a steam outlet from the first plasma torch heater (8) is connected to a steam nozzle in the pyrolysis oven (5); a steam outlet from the heater of the second plasma torch (10) is connected to an aerator steam nozzle (9); a gas outlet of the pyrolysis oven (5) is connected to a gas inlet of the gasifier (9), an ash outlet of the pyrolysis oven (5) is connected to an ash inlet of an ash cooler (6) , an ash outlet from the ash cooler (6) is connected to a power inlet
    Petition 870180138891, of 10/8/2018, p. 5/31
    4/4 of a coke ash separator (7); a gas outlet of the aerator (9) is connected to a gas inlet of the heat exchanger (11); and a gas outlet from the heat exchanger (11) is connected to a dust collector (12), a de-acidification tower (13), and a desiccator (14) in series.
    [7]
    7. APPLIANCE FOR LOW TEMPERATURE BIOMASS PYROLYSIS AND HIGH TEMPERATURE BIOMASS GASIFICATION, according to claim 6, characterized by the fact that a nitrogen protection device (4) is connected to a pyrolysis furnace feed input (5 ).
    [8]
    8. EQUIPMENT FOR BIOMASS PYROLYSIS AT LOW TEMPERATURE AND HIGH TEMPERATURE BIOMASS GASIFICATION according to claims 6 and 7, characterized in that a coke outlet of the coke ash separator (7) is connected to a coke inlet of the gasifier ( 9) by means of a coke conveyor (19).
    [9]
    9. EQUIPMENT FOR BIOMASS PYROLYSIS AT LOW TEMPERATURE AND HIGH TEMPERATURE BIOMASS GASIFICATION according to claims 6 or 7, characterized by the fact that the steam nozzles arranged in the pyrolysis oven (5) and the gasifier (9) are grouped in 2-4 levels of height, respectively, and the steam nozzles of each level will be uniformly and tangentially arranged along a circumferential direction.
    类似技术:
    公开号 | 公开日 | 专利标题
    BR112013001313B1|2018-12-26|method and apparatus for low temperature biomass pyrolysis and high temperature biomass gasification
    BR112013001318B1|2018-12-04|Process and apparatus for indirect gasification of biomass using water vapor
    BR112013001315B1|2019-03-26|METHOD AND APPARATUS FOR PYROLYSIS AND GASIFICATION OF BIOMASS THROUGH TWO INTERLIGED OVEN
    US8888872B2|2014-11-18|Gasifier cooling system
    BR112014016167B1|2020-01-21|island biomass gasification process under high temperature and atmospheric pressure
    RU2580740C2|2016-04-10|Method for cleaning synthesis gas from biomass at negative pressure to obtain oil products and configuration system thereof
    CN201770674U|2011-03-23|Biomass steam indirect gasification equipment
    MX2014007755A|2015-05-15|Biomass syngas purification process under positive pressure for producing oil and system configuration thereof.
    CN201737906U|2011-02-09|Biomass low-temperature cracking and high-temperature gasification equipment
    CN201770675U|2011-03-23|Biomass twin-joined cracking gasification device
    CN204918494U|2015-12-30|Coal gasification apparatus for producing of fixed bed and fluidized bed
    RU2588213C2|2016-06-27|Method of purifying synthetic gas from biomass at positive pressure to obtain oil products
    同族专利:
    公开号 | 公开日
    CA2805912A1|2012-01-26|
    ZA201300483B|2013-09-25|
    KR20130054356A|2013-05-24|
    CN101906325B|2013-09-04|
    RU2013107365A|2014-08-27|
    SG187570A1|2013-03-28|
    MX2013000835A|2013-05-20|
    US20130125464A1|2013-05-23|
    AU2011282076B2|2014-11-06|
    WO2012010059A1|2012-01-26|
    CA2805912C|2019-04-09|
    AP3671A|2016-04-15|
    JP2013531122A|2013-08-01|
    US8999022B2|2015-04-07|
    EP2597138B1|2018-10-24|
    AP2013006725A0|2013-02-28|
    EP2597138A4|2014-01-29|
    RU2526387C1|2014-08-20|
    EP2597138A1|2013-05-29|
    AU2011282076A1|2013-02-28|
    MY160733A|2017-03-15|
    JP5606624B2|2014-10-15|
    KR101472859B1|2014-12-15|
    CN101906325A|2010-12-08|
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    法律状态:
    2018-07-10| B07A| Application suspended after technical examination (opinion) [chapter 7.1 patent gazette]|
    2018-12-04| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|
    2018-12-26| B16A| Patent or certificate of addition of invention granted [chapter 16.1 patent gazette]|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 06/07/2011, OBSERVADAS AS CONDICOES LEGAIS. |
    2021-05-11| B21F| Lapse acc. art. 78, item iv - on non-payment of the annual fees in time|Free format text: REFERENTE A 10A ANUIDADE. |
    2021-08-31| B24J| Lapse because of non-payment of annual fees (definitively: art 78 iv lpi, resolution 113/2013 art. 12)|Free format text: EM VIRTUDE DA EXTINCAO PUBLICADA NA RPI 2627 DE 11-05-2021 E CONSIDERANDO AUSENCIA DE MANIFESTACAO DENTRO DOS PRAZOS LEGAIS, INFORMO QUE CABE SER MANTIDA A EXTINCAO DA PATENTE E SEUS CERTIFICADOS, CONFORME O DISPOSTO NO ARTIGO 12, DA RESOLUCAO 113/2013. |
    优先权:
    申请号 | 申请日 | 专利标题
    CN2010102340902A|CN101906325B|2010-07-20|2010-07-20|Process and apparatus thereof for low-temperature cracking and high-temperature gasification of biomass|
    CN201010234090.2|2010-07-20|
    PCT/CN2011/076921|WO2012010059A1|2010-07-20|2011-07-06|Method and apparatus for low-temperature biomass pyrolysis and high-temperature biomass gasification|
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