CN114735644A - Hydrogen production system of solid organic matter - Google Patents
Hydrogen production system of solid organic matter Download PDFInfo
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- CN114735644A CN114735644A CN202210297266.1A CN202210297266A CN114735644A CN 114735644 A CN114735644 A CN 114735644A CN 202210297266 A CN202210297266 A CN 202210297266A CN 114735644 A CN114735644 A CN 114735644A
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Abstract
The invention relates to the technical field of solid organic waste treatment, in particular to a hydrogen production system of a solid organic matter, which comprises: the rotary kiln pyrolysis reactor receives solid organic matters input from the outside and inputs high-temperature flue gas to generate pyrolysis gas; the gasification furnace receives the pyrolysis gas and inputs preheated oxygen to generate synthesis gas; a shift reactor receiving the syngas and inputting steam to generate a reaction gas; and the gas separator receives the reaction gas and separates out hydrogen. The invention has the beneficial effects that: the solid organic waste is treated by the pyrolysis-gasification technology of the solid organic matter, the heat utilization efficiency is effectively improved in the process of carrying out innocent treatment on the solid organic waste, the generation of dioxin precursors is inhibited by a reductive reaction system, and the secondary pollution is avoided. The whole device has simple structure, small occupied area, stable hydrogen generation process and convenient large-scale production.
Description
Technical Field
The invention relates to the technical field of solid organic waste treatment, in particular to a hydrogen production system of a solid organic matter.
Background
Solid organic waste refers to organic materials and substances produced in production, life and other activities that are discarded or discarded without losing their original utility value and that are in a solid form. With the progress of human production and living activities, a large amount of solid organic waste is generated every day. Meanwhile, the solid organic waste often has the characteristics of complex components, poor biodegradability, toxicity and the like, and the conventional treatment method has the disadvantages of poor treatment effect, small capacity, high cost and easy secondary pollution, so that the problem of relatively serious waste treatment is caused. Meanwhile, with the development of new energy technology, hydrogen energy is considered to be a better new energy development direction by virtue of the advantages of high energy density, cleanness and sustainability. Therefore, it is considered that hydrogen production from solid organic waste as a raw material and the harmless treatment of the solid organic waste while generating hydrogen gas are in the direction of development with high economic value.
In the prior art, there are related technologies for hydrogen production based on solid organic waste. For example, prior art 1 (patent publication No. CN104194834B) discloses a device for producing hydrogen by biomass pyrolysis and chemical looping of biomass pyrolysis gas, which is provided with a biomass pyrolysis gasification device and a chemical looping hydrogen production reaction device, and produces hydrogen by using pyrolysis gas generated by the biomass pyrolysis gasification device and water vapor to alternately react with oxygen carriers by oxidation-reduction reaction in the chemical looping hydrogen production device; for another example, prior art 2 (patent publication No. CN102286537B) discloses an apparatus and method for producing hydrogen by biological method using organic wastes, which produces hydrogen and organic wastewater by treating organic solid wastes through anaerobic fermentation, and further produces hydrogen by treating organic wastewater through a microbial electrolysis cell.
However, in practical implementation, the inventors found that, as in the technical solution disclosed in prior art 1, the metal oxide carrier needs to be additionally added in the chemical looping hydrogen production process, which makes the apparatus and the reaction process more complicated. For another example, in the technical scheme adopted in the prior art 2, the solid organic waste is treated based on a biological method, which causes the problems that the whole reaction device occupies a large area, the reaction period is long, and the hydrogen yield is unstable.
Disclosure of Invention
Aiming at the problems in the prior art, the hydrogen production system using the solid organic matter is provided.
The specific technical scheme is as follows:
a solid organic hydrogen production system comprising:
the rotary kiln pyrolysis reactor receives the solid organic matters input from the outside and inputs high-temperature flue gas so as to pyrolyze the solid organic matters by using the high-temperature flue gas to generate pyrolysis gas;
the gasification furnace receives the pyrolysis gas output from the rotary kiln pyrolysis reactor and inputs preheated oxygen so as to generate synthesis gas by adopting the preheated oxygen and the pyrolysis gas;
a shift reactor receiving the synthesis gas output from the gasification furnace and inputting steam to generate a reaction gas from the steam and the synthesis gas;
a gas separator that receives the reactant gas output from the shift reactor, the gas separator separating hydrogen from the reactant gas to complete a hydrogen production process.
Preferably, the output end of the rotary kiln pyrolysis reactor is further connected with a hot blast stove, and the hot blast stove and the gasification furnace simultaneously receive the pyrolysis gas output from the rotary kiln pyrolysis reactor;
preheating air is also input into the hot blast stove;
and the hot blast stove generates the high-temperature flue gas according to the preheated air and the pyrolysis gas.
Preferably, the flue gas output end of the hot blast stove is connected with the heat input end of a first heat exchanger;
the heat output end of the first heat exchanger is connected with the flue gas input end of the rotary kiln pyrolysis reactor and is used for inputting the high-temperature flue gas into the rotary kiln pyrolysis reactor;
inputting air from the outside at a cold input end of the first heat exchanger, wherein the first heat exchanger heats the air by adopting the heat of the high-temperature flue gas to generate the preheated air;
and the cold output end of the first heat exchanger is connected with the air input end of the hot blast stove and is used for inputting the preheated air into the hot blast stove.
Preferably, the hydrogen production system further comprises a steam generator, and the heat input end of the steam generator is connected with the output end of the gasification furnace;
the steam generator is internally provided with water input from the outside and generates the steam by adopting the heat of the synthesis gas output by the gasification furnace and the water;
and the steam output end of the steam generator is connected with the steam input end of the shift reactor and is used for inputting the steam into the shift reactor.
Preferably, the hydrogen production system further comprises a second heat exchanger, and the heat input end of the second heat exchanger is connected with the heat output end of the steam generator;
oxygen is input from the outside at the cold input end of the second heat exchanger, and the second heat exchanger heats the oxygen by adopting the heat of the synthesis gas to generate the preheated oxygen;
and the cold output end of the second heat exchanger is connected with the oxygen input end of the gasification furnace and is used for inputting the preheated oxygen into the gasification furnace.
Preferably, the hydrogen production system further comprises a filter, wherein the input end of the filter is connected with the heat output end of the heat exchanger, and the output end of the filter is connected with the synthesis gas input end of the shift reactor;
the filter receives the synthesis gas output by the second heat exchanger, and the synthesis gas is input into the shift reactor after impurities in the synthesis gas are removed by the filter.
Preferably, the synthesis gas comprises carbon monoxide;
a catalyst is disposed in the shift reactor for performing a water gas shift reaction of the syngas and the steam in the shift reactor to generate the hydrogen.
Preferably, the reaction gas comprises the hydrogen and carbon dioxide;
and a molecular sieve is arranged in the gas separator and used for adsorbing the carbon dioxide to separate the hydrogen.
Preferably, the rotary kiln pyrolysis reactor is provided with a rotary kiln jacket and a rotary kiln, the rotary kiln jacket is wrapped outside the rotary kiln, and the rotary kiln is used for containing the solid organic matters;
the rotary kiln is sleeved on one side of the output end of the rotary kiln pyrolysis reactor in a clamping manner, and the flue gas input end is arranged on one side of the output end of the rotary kiln pyrolysis reactor;
a flue gas output end is further arranged on one side of the rotary kiln which is sleeved on the feed end of the rotary kiln pyrolysis reactor;
the high-temperature flue gas passes through the rotary kiln jacket along the direction from the flue gas input end to the flue gas output end.
Preferably, the mass of the pyrolysis gas input into the hot blast stove is 10% -15% of the mass of the pyrolysis gas output by the rotary kiln pyrolysis reactor.
The technical scheme has the following advantages or beneficial effects: the solid organic waste is treated by the pyrolysis-gasification technology of the solid organic matter, the heat utilization efficiency is effectively improved in the process of carrying out innocent treatment on the solid organic waste, the generation of dioxin precursors is inhibited by a reductive reaction system, and the secondary pollution is avoided. The whole device has simple structure, small occupied area, stable hydrogen generation process and convenient large-scale production.
Drawings
Embodiments of the present invention will now be described more fully hereinafter with reference to the accompanying drawings. The drawings are, however, to be regarded as illustrative and explanatory only and are not restrictive of the scope of the invention.
FIG. 1 is a schematic block diagram of a hydrogen production system according to an embodiment of the present invention;
FIG. 2 is a schematic block diagram of a hydrogen production system according to another embodiment of the present invention;
FIG. 3 is a schematic block diagram of a hydrogen production system according to another embodiment of the present invention;
FIG. 4 is a schematic block diagram of a hot blast stove in one embodiment of the present invention;
FIG. 5 is a schematic block diagram of a hot blast stove according to another embodiment of the present invention;
FIG. 6 is a schematic view of a gasifier-shift reactor segment in an embodiment of the present invention;
FIG. 7 is a schematic view of a rotary kiln pyrolysis reactor in an embodiment of the invention;
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict.
The invention is further described with reference to the following drawings and specific examples, which are not intended to be limiting.
The invention comprises the following steps:
a solid organic hydrogen production system, as shown in fig. 1, comprising:
the rotary kiln pyrolysis reactor 2 receives solid organic matters input from the outside, and inputs high-temperature flue gas so as to pyrolyze the solid organic matters by the high-temperature flue gas to generate pyrolysis gas;
the gasification furnace 3 receives the pyrolysis gas output from the rotary kiln pyrolysis reactor 2, and inputs preheated oxygen to generate synthesis gas by adopting the preheated oxygen and the pyrolysis gas;
a shift reactor 9, the shift reactor 9 receiving the synthesis gas output from the gasification furnace and inputting steam to generate a reaction gas from the steam and the synthesis gas;
and the gas separator 10, the gas separator 10 receives the reaction gas output from the shift reactor 9, and the gas separator 10 separates hydrogen from the reaction gas to complete the hydrogen production process.
Specifically, to prior art, the chemical looping hydrogen production reaction process is loaded down with trivial details, biological hydrogen plant is great and the unstable problem of output, through carrying out pyrolysis-gasification to solid organic matter in this embodiment, generates the synthetic gas that contains hydrogen and carbon monoxide to through the water gas reaction realized including the reaction gas of carbon dioxide and hydrogen according to carbon monoxide and steam generation, and adsorb carbon dioxide in following the reaction gas through gas separator 10, and then obtain the higher hydrogen of purity. The technical means makes the whole reaction process simpler, thereby simplifying the device and reducing the occupied area of the device. Meanwhile, the invention has low requirements on raw materials, can be suitable for taking solid organic matters such as crop straws, livestock and poultry manure, domestic garbage, municipal sludge and other agricultural and forestry and municipal domestic wastes as raw materials, realizes a stable gas production process, is beneficial to industrial mass production, and is further widely applied to the harmless treatment process of organic wastes.
Further, as shown in fig. 2, in order to achieve a better utilization rate of energy in the reaction process, in another embodiment, a hot blast stove 4 is further disposed at an output end of the rotary kiln pyrolysis reactor 2, and is used for combusting pyrolysis gas to generate high-temperature flue gas required by the rotary kiln pyrolysis reactor 2; meanwhile, in order to improve the combustion efficiency of the hot blast stove 4, the air input into the hot blast stove 4 is preheated by the first heat exchanger 5, and the hot end of the first heat exchanger 5 is connected with the output end of the hot blast stove, so that the heat of high-temperature flue gas is fully utilized, and the energy consumption is reduced. In this embodiment, the gasification furnace 3 and the shift reactor 9 are sequentially provided with the steam generator 6, the second heat exchanger 7 and the filter 8, so that the waste heat resource of the synthesis gas is fully utilized, and further, the steam required by the shift reactor and the preheated oxygen for improving the gasification efficiency of the gasification furnace 3 are generated. And impurities in the synthesis gas are filtered out through the filter 8, so that the reaction yield is improved.
In the implementation process, the solid organic matter refers to organic matter in a solid state, which can be solid organic waste or other organic matter, and is used for realizing lower production cost. In order to achieve a better feeding effect, as shown in fig. 3, a feeding pump 1 is arranged in front of an input end of a rotary kiln pyrolysis reactor 2, and is used for continuously feeding solid organic matters to achieve a stable production effect. The feed pump 1 itself can be implemented by using the prior art, such as a hydraulic pump, a screw feed pump, a plunger pump, etc. Meanwhile, in this embodiment, in order to collect the finally generated hydrogen, a hydrogen storage tank 11 is further disposed at the output end of the gas separator 10 for collecting and storing the hydrogen. It should be noted that, in other embodiments, other devices are connected to the output end of the gas separator 10, such as a hydrogen pipeline for delivering hydrogen to external chemical equipment, a canning device for filling hydrogen, and the like, and the hydrogen storage tank 11 shown in fig. 3 is only a storage container in this embodiment and does not limit the invention as a whole.
In one embodiment, the rotary kiln pyrolysis reactor 2 is provided with a slag outlet for discharging pyrolysis residue generated by the pyrolysis reaction.
In another embodiment, when the fixed carbon content of the solid organic matter is high, the rotary kiln pyrolysis reactor 2 inputs the pyrolysis carbon and pyrolysis gas generated by the pyrolysis reaction into the gasification furnace 3;
the gasification furnace 3 is provided with a slag outlet for guiding out the residue generated by the gasification reaction.
In a preferred embodiment, as shown in fig. 4, the output end of the rotary kiln pyrolysis reactor 2 is further connected to a hot blast stove 4, and the hot blast stove 4 and the gasification furnace 3 simultaneously receive pyrolysis gas output from the rotary kiln pyrolysis reactor 2;
preheating air is also input into the hot blast stove 4;
the hot blast stove 4 generates high-temperature flue gas according to the preheated air and the pyrolysis gas.
Specifically, for realizing the lower energy consumption in reaction process, set up hot-blast furnace 4 through the output at rotary kiln pyrolytic reaction ware 2 in this embodiment to divide partial pyrolysis gas as the fuel of hot-blast furnace 4, and then generate rotary kiln pyrolytic reaction ware 2 nearby and heat required high temperature flue gas in pyrolytic reaction, avoided the problem that external input high temperature flue gas needs extra consumption fuel, reduced manufacturing cost.
Further, in order to improve the combustion efficiency of the hot blast stove 4 and reduce the consumption of the hot blast stove on pyrolysis gas, in the embodiment, preheated air is input into the hot blast stove 4 by selection, and then the combustion efficiency of the hot blast stove 4 is improved.
In a preferred embodiment, as shown in fig. 5, the flue gas output end 4B of the hot blast stove 4 is connected to the heat input end 5A of a first heat exchanger 5;
the heat output end 5B of the first heat exchanger 5 is connected with the flue gas input end 2C of the rotary kiln pyrolysis reactor 2 and is used for inputting high-temperature flue gas into the rotary kiln pyrolysis reactor 2;
the cold input end 5C of the first heat exchanger 5 inputs air from the outside, and the first heat exchanger 5 heats the air by adopting the heat of the high-temperature flue gas to generate preheated air;
the cold output end 5D of the first heat exchanger 5 is connected with the air input end 4C of the hot blast stove 4 and is used for inputting preheated air into the hot blast stove 4.
Specifically, for realizing better energy utilization efficiency, set up first heat exchanger 5 between hot-blast furnace 4 and rotary kiln pyrolytic reaction ware 2 in this embodiment to utilize the high temperature flue gas of hot-blast furnace 4 output to preheat the air in order to generate preheated air, when preheating the air of inputing in the hot-blast furnace 4 in order to promote combustion efficiency, reduced the energy consumption, effectively utilized the waste heat resource of high temperature flue gas.
In a preferred embodiment, as shown in fig. 6, the hydrogen production system further comprises a steam generator 6, wherein a heat input end 6A of the steam generator 6 is connected to an output end 3C of the gasification furnace;
water input from the outside is input into the steam generator 6, and the steam generator 6 generates steam by using the heat and the water of the synthesis gas output by the gasification furnace 3;
the steam output 6D of the steam generator 6 is connected to the steam input 9B of the shift reactor 9 for inputting steam to the shift reactor 9.
Specifically, for realizing the whole lower energy consumption and the higher energy utilization ratio of hydrogen manufacturing system, set up steam generator 6 through the output at gasifier 3 in this embodiment, utilize the high temperature synthetic gas that generates through gasification reaction in gasifier 3 to heat water, and then generate shift reactor 9 and carry out the required steam of water gas reaction, avoided the energy resource consumption that extra input steam brought, reduced the holistic energy consumption of hydrogen manufacturing system.
In a preferred embodiment, the hydrogen production system further comprises a second heat exchanger 7, wherein a heat input end 7A of the second heat exchanger 7 is connected with a heat output end 6B of the steam generator;
oxygen is input from the outside at a cold input end 7C of the second heat exchanger 7, and the second heat exchanger 7 heats the oxygen by adopting the heat of the synthesis gas to generate preheated oxygen;
the cold output end 7D of the second heat exchanger 7 is connected to the oxygen input end 3C of the gasification furnace 3 for inputting preheated oxygen into the gasification furnace.
Specifically, in order to reduce the energy consumption of the gasification furnace 3 during the further gasification reaction of the pyrolysis gas, in this embodiment, the second heat exchanger 7 is arranged to collect the heat of the syngas, so as to preheat the oxygen to be input into the gasification furnace 3, thereby generating preheated oxygen, thereby reducing the energy consumption of the gasification furnace 3 and improving the utilization efficiency of the waste heat resource of the syngas.
In a preferred embodiment, the hydrogen production system further comprises a filter 8, an input end 8A of the filter is connected to a heat output end 7B of the heat exchanger, and an output end 8B of the filter is connected to a synthesis gas input end 9A of a shift reactor 9;
the filter 8 receives the synthesis gas output from the second heat exchanger 7, and after impurities in the synthesis gas are removed by the filter 8, the synthesis gas is input to the shift reactor 9.
Specifically, in order to achieve a better reaction effect in the shift reactor 9, in this embodiment, the synthesis gas input into the shift reactor 9 is filtered by the addition of the filter 8, so as to filter out impurities in the synthesis gas, and prevent the impurities in the synthesis gas from entering the shift reactor 9 to affect the reaction process or cause the overall maintenance period of the shift reactor 9 to be shortened.
In practice, the filter 8 may be a bag filter, or other type of filter such as a ceramic dust collector or the like. In this embodiment, the impurities in the syngas are mainly dust and tar, so a better filtering effect can be achieved by providing a cloth bag filter. In other embodiments, the filter 8 can be adjusted by those skilled in the art according to the product of the gasification furnace 3, since the specific kind of solid organic matter varies, i.e. when other components of the raw material are used. For example, in an embodiment, the organic waste with high fixed carbon content is used as the raw material, and the dust content of the syngas generated in the gasification furnace 3 is high in this embodiment. In order to achieve a good purification effect on the synthesis gas, in the embodiment, a bag filter and a cyclone dust collector are combined to achieve a large amount of dust filtering effect.
In a preferred embodiment, the synthesis gas comprises carbon monoxide;
the shift reactor 9 is provided with a catalyst for water gas shift reaction of synthesis gas and steam in the shift reactor to generate hydrogen.
Specifically, for realizing comparatively simple reaction process, realized partly converting into hydrogen and carbon dioxide to the carbon monoxide in the synthetic gas through the water gas reaction in this embodiment, and then improved the hydrogen in the reaction gas of output and accounted for, realized comparatively simple reaction process when promoting the productivity, avoided chemical chain hydrogen manufacturing among the prior art to lead to the loaded down with trivial details problem of reaction process.
In the implementation process, the synthesis gas input into the shift reactor 9 mainly comprises carbon monoxide and hydrogen, wherein the hydrogen is the main product of the whole hydrogen production system, so that the synthesis gas is input into the shift reactor 9, the carbon monoxide is partially reacted by steam to generate hydrogen and carbon dioxide, the whole proportion of the hydrogen in the reaction gas can be improved, and higher yield is realized.
In a preferred embodiment, the reactant gases include hydrogen and carbon dioxide;
the gas separator 10 is provided with a molecular sieve for adsorbing carbon dioxide to separate hydrogen.
Specifically, in order to achieve a higher purity of hydrogen, in the present embodiment, with respect to the main products of the reaction gas generated in the shift reactor 9: hydrogen and carbon dioxide, set up specific molecular sieve, and then make molecular sieve adsorb carbon dioxide in the pressure swing adsorption process, and then output the higher hydrogen of purity.
In a preferred embodiment, as shown in fig. 7, the rotary kiln pyrolysis reactor 2 has a rotary kiln jacket 21 and a rotary kiln 22, the rotary kiln jacket 21 is wrapped outside the rotary kiln 22, and the rotary kiln 22 is used for containing solid organic matters;
a flue gas input end 2C is arranged on one side of the output end 2B of the rotary kiln pyrolysis reactor 2 of the rotary kiln jacket 21;
the rotary kiln jacket 21 is also provided with a flue gas output end 2D at one side of the feed end 2A of the rotary kiln pyrolysis reactor 2;
the high-temperature flue gas passes through the rotary kiln jacket along the direction from the flue gas input end 2C to the flue gas output end 2D.
Specifically, for realizing better solid organic matter pyrolysis effect to and better pyrolysis gas purity, the jacketed rotary kiln has been selected for use in this embodiment to carry out pyrolytic reaction, thereby make the high temperature flue gas that probably contains impurity not with pyrolysis gas direct contact, pass through rotary kiln jacket 21 with the opposite direction with feeding direction through setting up high temperature flue gas simultaneously, realized the even heating to rotary kiln 22, and then make the abundant pyrolysis of solid organic matter.
In a preferred embodiment, the mass of the pyrolysis gas input into the hot blast stove 4 is 10-15% of the mass of the pyrolysis gas output by the pyrolysis reactor of the rotary kiln.
The invention is further illustrated below with reference to a production example:
in this embodiment, the hydrogen production system shown in fig. 3 is selected as the hydrogen production system, the solid organic matter is selected from garbage oversize products such as rubber, textile fabrics and plastics, and the feeding pump 1 is set as a hydraulic plunger pump. The rotary kiln pyrolysis reactor 2 was set at a rotational speed of 6rad/min for stirring and transporting the solid organic matter pumped by the feed pump 1 to the rear end. Meanwhile, 700 ℃ high-temperature flue gas is input into a rotary kiln jacket 21 of the rotary kiln pyrolysis reactor 2 to heat the rotary kiln 22, so that the temperature of the tail end of the rotary kiln 22 reaches over 500 ℃, the solid organic matter is fully pyrolyzed to generate pyrolysis gas and a small amount of pyrolysis residues, and the pyrolysis residues are discharged from a discharge hole in the bottom of the tail end of the rotary kiln 22. According to different specific components in the solid organic matter, the mass of the pyrolysis residue is 5-20% of the mass of the solid organic matter input into the rotary kiln pyrolysis reactor 2. Then, the pyrolysis gas output by the rotary kiln pyrolysis reactor 2 is introduced into the gasification furnace 3, and part of the pyrolysis gas is shunted and enters the hot blast stove 4 to be used as fuel for generating high-temperature flue gas.
The mass of the pyrolysis gas which is shunted to enter the hot blast stove 4 is 10% -15% of the mass of the pyrolysis gas which is output by the rotary kiln pyrolysis reactor 2, and the mass of the pyrolysis gas which is shunted to the hot blast stove 4 can be properly adjusted according to the tail end temperature of the rotary kiln pyrolysis reactor 2, so that the temperature in the rotary kiln pyrolysis reactor 2 meets the pyrolysis requirement and the total yield of the hydrogen production system is improved. In the hot blast stove 4, the pyrolysis gas and the preheated air preheated to about 150 ℃ are mixed and combusted to generate high-temperature flue gas, and the temperature of the high-temperature flue gas at the flue gas output end 4B of the hot blast stove 4 is about 800 ℃. Subsequently, the high-temperature flue gas heats the air in the first heat exchanger 5, so that the air is preheated to about 150 ℃ to meet the requirement of the hot blast stove 4 on the preheated air. The temperature of the high-temperature flue gas is reduced to about 700 ℃ after heat exchange through the first heat exchanger 5, and the high-temperature flue gas is input into the rotary kiln pyrolysis reactor 2 and used for heating the rotary kiln 22 so that the temperature of the rotary kiln 22 can meet the pyrolysis requirement of the solid organic matters.
The maximum temperature of the gasification furnace 3 is set to 900 ℃ or higher, and preheated oxygen at a temperature of about 150 ℃ is continuously supplied. The pyrolysis gas introduced into the gasification furnace 3 stays for a period of time in an atmosphere of 900 ℃ and undergoes a gasification reaction with the preheated oxygen, so that most of tar components in the pyrolysis gas are cracked into small molecular components, thereby generating and outputting synthesis gas mainly comprising carbon monoxide and hydrogen.
The temperature of the synthesis gas output by the output end 3C of the gasification furnace 3 is 750 ℃, and in order to fully utilize the waste heat resource of the synthesis gas, the synthesis gas is sequentially led into the steam generator 6 and the second heat exchanger 7 to respectively generate steam required by the shift reactor 9 and preheated oxygen required by the gasification furnace 3. The dust and tar components of the synthesis gas are then filtered by a filter 8 before entering the shift reactor 9. Because the impurities of the syngas in this embodiment are mainly dust and tar, the filter 8 in this embodiment is configured as a cloth bag filter, thereby achieving a better filtering effect on the impurities.
The shift reactor 9 is provided with a catalyst in advance, and the catalyst can sufficiently react the carbon monoxide component in the synthesis gas with the steam to generate carbon dioxide and hydrogen, and further improve the ratio of the hydrogen component in the synthesis gas generated by the gasification furnace 3, thereby generating a reaction gas mainly containing carbon dioxide and hydrogen. Subsequently, the carbon dioxide component in the reaction gas is adsorbed by the gas separator 10 provided with a molecular sieve in advance under the pressure swing adsorption, and hydrogen gas with high purity is generated and introduced into the hydrogen gas storage tank 11 for storage.
The invention has the beneficial effects that: the solid organic waste is treated by the pyrolysis-gasification technology of the solid organic matter, the heat utilization efficiency is effectively improved in the process of carrying out innocent treatment on the solid organic waste, the generation of dioxin precursors is inhibited by a reductive reaction system, and the secondary pollution is avoided. The whole device has simple structure, small occupied area, stable hydrogen generation process and convenient large-scale production.
While the invention has been described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes in form and detail may be made therein without departing from the spirit and scope of the invention.
Claims (10)
1. A system for producing hydrogen by using solid organic matters is characterized by comprising:
the rotary kiln pyrolysis reactor receives the solid organic matters input from the outside and inputs high-temperature flue gas so as to pyrolyze the solid organic matters by using the high-temperature flue gas to generate pyrolysis gas;
the gasification furnace receives the pyrolysis gas output from the rotary kiln pyrolysis reactor and inputs preheated oxygen so as to generate synthesis gas by adopting the preheated oxygen and the pyrolysis gas;
a shift reactor receiving the synthesis gas output from the gasification furnace and inputting steam to generate a reaction gas from the steam and the synthesis gas;
a gas separator that receives the reactant gas output from the shift reactor, the gas separator separating hydrogen from the reactant gas to complete a hydrogen production process.
2. The hydrogen production system according to claim 1, wherein the output end of the rotary kiln pyrolysis reactor is further connected with a hot blast stove, and the hot blast stove and the gasification furnace simultaneously receive the pyrolysis gas output from the rotary kiln pyrolysis reactor;
preheating air is also input into the hot blast stove;
and the hot blast stove generates the high-temperature flue gas according to the preheated air and the pyrolysis gas.
3. The hydrogen production system according to claim 2, wherein the flue gas output end of the hot blast stove is connected with the heat input end of a first heat exchanger;
the heat output end of the first heat exchanger is connected with the flue gas input end of the rotary kiln pyrolysis reactor and is used for inputting the high-temperature flue gas into the rotary kiln pyrolysis reactor;
inputting air from the outside at a cold input end of the first heat exchanger, wherein the first heat exchanger heats the air by adopting the heat of the high-temperature flue gas to generate the preheated air;
and the cold output end of the first heat exchanger is connected with the air input end of the hot blast stove and is used for inputting the preheated air into the hot blast stove.
4. The hydrogen production system as claimed in claim 1, further comprising a steam generator, wherein a heat input end of the steam generator is connected with an output end of the gasification furnace;
the steam generator is internally provided with water input from the outside and generates the steam by adopting the heat of the synthesis gas output by the gasification furnace and the water;
and the steam output end of the steam generator is connected with the steam input end of the shift reactor and is used for inputting the steam into the shift reactor.
5. The hydrogen production system as claimed in claim 4, further comprising a second heat exchanger having a heat input connected to the heat output of the steam generator;
oxygen is input from the outside at the cold input end of the second heat exchanger, and the second heat exchanger heats the oxygen by adopting the heat of the synthesis gas to generate the preheated oxygen;
and the cold output end of the second heat exchanger is connected with the oxygen input end of the gasification furnace and is used for inputting the preheated oxygen into the gasification furnace.
6. The hydrogen generation system of claim 5, further comprising a filter having an input connected to the heat output of the heat exchanger and an output connected to the syngas input of the shift reactor;
the filter receives the synthesis gas output by the second heat exchanger, and the synthesis gas is input into the shift reactor after impurities in the synthesis gas are removed by the filter.
7. The hydrogen production system of claim 1, wherein the syngas comprises carbon monoxide;
a catalyst is disposed in the shift reactor for performing a water gas shift reaction of the syngas and the steam in the shift reactor to generate the hydrogen.
8. The hydrogen generation system of claim 7, wherein the reactant gas comprises the hydrogen gas and carbon dioxide;
and a molecular sieve is arranged in the gas separator and used for adsorbing the carbon dioxide to separate the hydrogen.
9. The hydrogen production system as claimed in claim 3, wherein the rotary kiln pyrolysis reactor is provided with a rotary kiln jacket and a rotary kiln, the rotary kiln jacket is wrapped outside the rotary kiln, and the rotary kiln is used for containing the solid organic matters;
the rotary kiln is sleeved on one side of the output end of the rotary kiln pyrolysis reactor in a clamping manner, and the flue gas input end is arranged on one side of the output end of the rotary kiln pyrolysis reactor;
a flue gas output end is further arranged on one side of the rotary kiln which is sleeved on the feed end of the rotary kiln pyrolysis reactor;
the high-temperature flue gas passes through the rotary kiln jacket along the direction from the flue gas input end to the flue gas output end.
10. The hydrogen generation system according to claim 2, wherein the mass of the pyrolysis gas input to the hot blast stove is 10% to 15% of the mass of the pyrolysis gas output from the rotary kiln pyrolysis reactor.
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