CN114735644A - A hydrogen production system of solid organic matter - Google Patents

Abstract

The invention relates to the technical field of solid organic waste treatment, in particular to a hydrogen production system for solid organic matter, comprising: a rotary kiln pyrolysis reactor, receiving solid organic matter input from the outside, and inputting high-temperature flue gas to generate pyrolysis gas ; Gasifier, receiving pyrolysis gas and inputting preheated oxygen to generate synthesis gas; Shift reactor, receiving synthesis gas and inputting steam to generate reaction gas; Gas separator, receiving reaction gas and separating out hydrogen . The beneficial effect of the invention is that: the solid organic waste is treated by the solid organic matter pyrolysis-gasification technology, the heat utilization efficiency is effectively improved in the process of harmless treatment of the solid organic waste, and the reduction reaction is carried out. The system inhibits the generation of dioxin precursors and avoids secondary pollution. The overall device has a simple structure, a small footprint, and a stable hydrogen generation process, which is convenient for large-scale production.

Description

A hydrogen production system of solid organic matter

technical field

The invention relates to the technical field of solid organic waste treatment, in particular to a hydrogen production system for solid organic matter.

Background technique

Solid organic waste refers to organic objects and substances in solid form that have lost their original use value or have not lost their use value but have been discarded or abandoned during production, life and other activities. With the development of human production and living activities, a large amount of solid organic waste will be produced every day. At the same time, since solid organic waste often has the characteristics of complex composition, poor biodegradability, and toxicity, conventional treatment methods have poor treatment effect, low capacity, high cost, and easy to cause secondary pollution, which leads to serious waste treatment problems. At the same time, with the development of new energy technologies, hydrogen energy is considered to be a better new energy development direction due to its advantages of high energy density, cleanness and sustainability. Therefore, using solid organic wastes as raw materials for hydrogen production, and realizing the harmless treatment of solid organic wastes while generating hydrogen, is considered to be a development direction with high economic value.

In the prior art, there are related technologies for hydrogen production based on solid organic wastes. For example, prior art 1 (patent publication number: CN104194834B) discloses a device for biomass pyrolysis and biomass pyrolysis gas chemical chain hydrogen production, by setting biomass pyrolysis gasification device and chemical chain hydrogen production reaction device, using The pyrolysis gas produced by the biomass pyrolysis gasification device is used in the chemical chain hydrogen production device to alternately undergo oxidation-reduction reaction with water vapor and oxygen carrier to prepare hydrogen; A device and method for biologically producing hydrogen from organic wastes. The method uses anaerobic fermentation to process organic solid wastes to generate hydrogen and organic waste water, and further processes organic waste water to produce hydrogen through microbial electrolysis cells.

However, in the actual implementation process, the inventors found that, as in the technical solution disclosed in the prior art 1, since an additional metal oxide carrier needs to be added during the chemical chain hydrogen production process, the device and the reaction process are complicated. For another example, the technical solution adopted in the prior art 2 is based on the biological treatment of solid organic waste, which results in a larger area of the overall reaction device, a longer reaction period, and an unstable hydrogen output rate. The problem.

SUMMARY OF THE INVENTION

In view of the above problems existing in the prior art, a system for producing hydrogen from solid organic matter is now provided.

The specific technical solutions are as follows:

A hydrogen production system for solid organic matter, comprising:

Rotary kiln pyrolysis reactor, the rotary kiln pyrolysis reactor receives the solid organic matter input from the outside, and inputs high-temperature flue gas, so as to use the high-temperature flue gas to pyrolyze the solid organic matter to generate pyrolysis gas ;

a gasifier receiving the pyrolysis gas output from the rotary kiln pyrolysis reactor and inputting preheated oxygen to generate syngas using the preheated oxygen and the pyrolysis gas;

a shift reactor that receives the syngas output from the gasifier and inputs steam to generate a reaction gas from the steam and the syngas;

A gas separator, the gas separator receives the reaction gas output from the shift reactor, and the gas separator separates hydrogen from the reaction gas to complete the hydrogen production process.

Preferably, the output end of the rotary kiln pyrolysis reactor is further connected to a hot blast stove, and the hot blast stove and the gasifier simultaneously receive the pyrolysis gas output from the rotary kiln pyrolysis reactor;

Also input preheated air in the hot blast stove;

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 to the heat input end of a first heat exchanger;

The heat output end of the first heat exchanger is connected to the flue gas input end of the rotary kiln pyrolysis reactor for inputting the high temperature flue gas into the rotary kiln pyrolysis reactor;

The cold input end of the first heat exchanger inputs air from the outside, and the first heat exchanger uses the heat of the high temperature flue gas to heat the air to generate the preheated air;

The cold output end of the first heat exchanger is connected to the air input end of the hot blast stove 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 to the output end of the gasifier;

Water input from the outside is also input into the steam generator, and the steam generator generates the steam by using the heat of the synthesis gas output by the gasifier and the water;

The steam output end of the steam generator is connected to the steam input end of the shift reactor for inputting the steam to the shift reactor.

Preferably, the hydrogen production system further comprises a second heat exchanger, the heat input end of the second heat exchanger is connected to the heat output end of the steam generator;

The cold input end of the second heat exchanger inputs oxygen from outside, and the second heat exchanger uses the heat of the syngas to heat the oxygen to generate the preheated oxygen;

The cold output end of the second heat exchanger is connected to the oxygen input end of the gasifier for inputting the preheated oxygen into the gasifier.

Preferably, the hydrogen production system further comprises a filter, the input end of the filter is connected to the heat output end of the heat exchanger, and the output end of the filter is connected to the synthesis gas input end of the shift reactor ;

The filter receives the syngas output from the second heat exchanger, and after the filter removes impurities in the syngas, the syngas is fed into the shift reactor.

Preferably, the syngas contains carbon monoxide;

A catalyst is provided in the shift reactor, and the catalyst is used for the synthesis gas and the steam to perform a water-gas shift reaction in the shift reactor, thereby generating the hydrogen.

Preferably, the reaction gas includes the hydrogen and carbon dioxide;

A molecular sieve is provided in the gas separator, and the molecular sieve is used for adsorbing the carbon dioxide to separate the hydrogen.

Preferably, the rotary kiln pyrolysis reactor has a rotary kiln jacket and a rotary kiln, the rotary kiln jacket is wrapped outside the rotary kiln, and the rotary kiln is used to accommodate the solid organic matter;

The rotary kiln jacket is provided with the flue gas input end on one side of the output end of the rotary kiln pyrolysis reactor;

The rotary kiln jacket is also provided with a flue gas output end on one side of 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 to the hot blast furnace is 10% to 15% of the mass of the pyrolysis gas output from the rotary kiln pyrolysis reactor.

The above technical solution has the following advantages or beneficial effects: the solid organic waste is treated by the solid organic matter pyrolysis-gasification technology, and the heat utilization efficiency is effectively improved in the process of harmless treatment of the solid organic waste, and through The reduction reaction system inhibits the formation of dioxin precursors and avoids secondary pollution. The overall device has a simple structure, a small footprint, and a stable hydrogen generation process, which is convenient for large-scale production.

Description of drawings

Embodiments of the present invention are described more fully with reference to the accompanying drawings. However, the accompanying drawings are for illustration and illustration only, and are not intended to limit the scope of the present invention.

1 is a schematic block diagram of a hydrogen production system according to an embodiment of the present invention;

2 is a schematic block diagram of a hydrogen production system according to another embodiment of the present invention;

3 is a schematic block diagram of a hydrogen production system according to another embodiment of the present invention;

4 is a schematic block diagram of a hot blast stove in an embodiment of the present invention;

5 is a schematic block diagram of a hot blast stove in another embodiment of the present invention;

6 is a schematic diagram of a gasifier-shift reactor section in an embodiment of the present invention;

7 is a schematic diagram of a rotary kiln pyrolysis reactor in an embodiment of the present invention;

Detailed ways

The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, rather than all the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative work fall within the protection scope of the present invention.

It should be noted that the embodiments of the present invention and the features of the embodiments may be combined with each other under the condition of no conflict.

The present invention will be further described below with reference to the accompanying drawings and specific embodiments, but it is not intended to limit the present invention.

The present invention includes:

A solid organic hydrogen production system, as shown in Figure 1, includes:

Rotary kiln pyrolysis reactor 2, the rotary kiln pyrolysis reactor 2 receives the solid organic matter input from the outside, and inputs high-temperature flue gas, so as to use the high-temperature flue gas to pyrolyze the solid organic matter to generate pyrolysis gas;

Gasifier 3, the gasifier 3 receives the pyrolysis gas output from the rotary kiln pyrolysis reactor 2, and inputs preheated oxygen to generate synthesis gas by using the preheated oxygen and the pyrolysis gas;

a shift reactor 9, the shift reactor 9 receives the syngas output from the gasifier and inputs steam to generate a reaction gas from the steam and the syngas;

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, in view of the problems in the prior art that the chemical chain hydrogen production reaction process is cumbersome, the biological hydrogen production device is large and the output is unstable, in this embodiment, the solid organic matter is pyrolyzed-gasified to generate hydrogen and carbon monoxide. The synthesis gas is obtained, and the reaction gas containing carbon dioxide and hydrogen is generated according to carbon monoxide and steam through the water-gas reaction, and the carbon dioxide is adsorbed from the reaction gas through the gas separator 10, thereby obtaining high-purity hydrogen. The above technical means make the overall reaction process simpler, thereby simplifying the device and reducing the footprint of the device. At the same time, the invention does not require high raw materials, and can adapt to solid organic matter such as crop straw, livestock and poultry manure, domestic waste, urban sludge and other agricultural and forestry and urban domestic wastes as raw materials, and realizes a stable gas production process, which is beneficial to industrial production. It is widely used in the process of harmless treatment of organic waste.

Further, as shown in FIG. 2 , in order to achieve better utilization of energy during the reaction process, in another embodiment, a hot blast furnace 4 is also provided at the output end of the rotary kiln pyrolysis reactor 2 for The pyrolysis gas is burned to generate the high temperature flue gas required by the rotary kiln pyrolysis reactor 2; at the same time, in order to improve the combustion efficiency of the hot blast stove 4, the air input into the hot blast stove 4 is also preheated by the first heat exchanger 5 , the hot end of the first heat exchanger 5 is connected to the output end of the hot blast stove, thereby making full use of the heat of the high temperature flue gas and reducing energy consumption. In this embodiment, the steam generator 6, the second heat exchanger 7 and the filter 8 are arranged in the gasifier 3 and the shift reactor 9 in sequence, so as to fully utilize the waste heat resources of the synthesis gas, and further The steam required for the shift reactor and the preheated oxygen used by the gasifier 3 to increase the gasification efficiency are generated. And the impurities in the synthesis gas are filtered out through the filter 8, and the yield of the reaction is improved.

In the implementation process, solid organic matter refers to organic matter in a solid state, which may be solid organic waste or other organic matter for achieving lower production costs. In order to achieve better feeding effect, as shown in Figure 3, a feeding pump 1 is provided before the input end of the rotary kiln pyrolysis reactor 2 for continuous feeding of solid organic matter to achieve the effect of stable production. The feed pump 1 itself can be realized by using existing technologies, such as hydraulic pump, screw feed pump, plunger pump and so on. Meanwhile, in this embodiment, in order to collect the finally generated hydrogen, a hydrogen storage tank 11 is also provided at the output end of the gas separator 10 for collecting and storing the hydrogen. It should be noted that, in other embodiments, the output end of the gas separator 10 is also connected with other devices, such as a hydrogen pipeline for transporting hydrogen to external chemical equipment, a canning device for filling hydrogen, etc. The hydrogen storage tank 11 shown in FIG. 3 is only a storage container in this embodiment, which does not constitute a limitation to the invention as a whole.

In an embodiment, the rotary kiln pyrolysis reactor 2 is provided with a slag outlet for discharging the pyrolysis residue generated by the pyrolysis reaction.

In another embodiment, when the fixed carbon content of the solid organic matter is relatively high, the rotary kiln pyrolysis reactor 2 inputs the pyrolysis carbon and pyrolysis gas generated by the pyrolysis reaction into the gasifier 3;

The gasification furnace 3 is provided with a slag outlet for discharging the residue generated by the gasification reaction.

In a preferred embodiment, as shown in Figure 4, the output end of the rotary kiln pyrolysis reactor 2 is also connected to a hot blast stove 4, and the hot blast stove 4 and the gasifier 3 are simultaneously received from the rotary kiln pyrolysis reactor 2 output pyrolysis gas;

Preheated 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, in order to achieve lower energy consumption in the reaction process, in this embodiment, a hot blast stove 4 is set at the output end of the rotary kiln pyrolysis reactor 2, and a part of the pyrolysis gas is diverted to serve as the fuel of the hot blast stove 4, Furthermore, the high temperature flue gas required for heating in the pyrolysis reaction of the rotary kiln pyrolysis reactor 2 is generated nearby, which avoids the problem of externally inputting the high temperature flue gas and requires additional fuel consumption and reduces the production cost.

Further, in order to improve the combustion efficiency of the hot blast stove 4 and reduce the consumption of the pyrolysis gas by the hot blast stove 4, in the embodiment, the preheated air is selected to be input into the hot blast stove 4, thereby improving the combustion efficiency of the hot blast stove 4.

In a preferred embodiment, as shown in FIG. 5 , the flue gas output end 4B of the hot blast stove 4 is connected to a heat input end 5A of the first heat exchanger 5;

The heat output end 5B of the first heat exchanger 5 is connected to the flue gas input end 2C of the rotary kiln pyrolysis reactor 2 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 uses the heat of the high temperature flue gas to heat the air to generate preheated air;

The cold output end 5D of the first heat exchanger 5 is connected to the air input end 4C of the hot blast stove 4 for inputting preheated air into the hot blast stove 4 .

Specifically, in order to achieve better energy utilization efficiency, in this embodiment, a first heat exchanger 5 is arranged between the hot blast stove 4 and the rotary kiln pyrolysis reactor 2, and the high temperature flue gas output from the hot blast stove 4 is used to The air is preheated to generate preheated air, and the air input into the hot blast stove 4 is preheated to improve the combustion efficiency, and at the same time, the energy consumption is reduced, and the waste heat resources of the high temperature flue gas are effectively utilized.

In a preferred embodiment, as shown in FIG. 6 , the hydrogen production system further includes a steam generator 6, and the heat input end 6A of the steam generator 6 is connected to the output end 3C of the gasifier;

The water input from the outside is also input into the steam generator 6, and the steam generator 6 uses the heat and water of the synthesis gas output by the gasifier 3 to generate steam;

The steam output end 6D of the steam generator 6 is connected to the steam input end 9B of the shift reactor 9 for inputting steam to the shift reactor 9 .

Specifically, in order to achieve the overall lower energy consumption and higher energy utilization rate of the hydrogen production system, in this embodiment, a steam generator 6 is provided at the output end of the gasifier 3, and the The high-temperature synthesis gas generated by the reaction heats the water, thereby generating the steam required for the water-gas reaction in the shift reactor 9, avoiding the energy consumption caused by the additional input of steam, and reducing the overall energy consumption of the hydrogen production system.

In a preferred embodiment, the hydrogen production system further includes a second heat exchanger 7, and the heat input end 7A of the second heat exchanger 7 is connected to the heat output end 6B of the steam generator;

The cold input end 7C of the second heat exchanger 7 inputs oxygen from the outside, and the second heat exchanger 7 uses the heat of the syngas to heat the oxygen 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 gasifier 3 for inputting preheated oxygen into the gasifier.

Specifically, in order to reduce the energy consumption of the gasifier 3 when the pyrolysis gas is further gasified, in this embodiment, the heat of the synthesis gas is collected by setting the second heat exchanger 7, and then the input gas is to be input. The oxygen in the gasifier 3 is preheated to generate preheated oxygen, thereby reducing the energy consumption of the gasifier 3 and improving the utilization efficiency of the waste heat resources of the synthesis gas.

In a preferred embodiment, the hydrogen production system further includes a filter 8, the input end 8A of the filter is connected to the heat output end 7B of the heat exchanger, and the output end 8B of the filter is connected to the synthesis gas of the shift reactor 9 Input 9A;

The filter 8 receives the syngas output from the second heat exchanger 7 , and after the filter 8 removes impurities in the syngas, the syngas 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 syngas input to the shift reactor 9 is filtered by adding a filter 8, thereby filtering out impurities in the syngas, avoiding the The entry of impurities in the syngas into the shift reactor 9 affects the reaction process or causes the overall maintenance period of the shift reactor 9 to be shortened.

During implementation, the filter 8 may be a bag filter, or other types of filters such as ceramic dust collectors. In this embodiment, the impurities in the syngas are mainly dust and tar, so better filtering effect can be achieved by setting a bag filter. In other embodiments, since the specific type of solid organic matter changes, that is, when raw materials of other components are used, those skilled in the art can adjust the filter 8 according to the product of the gasifier 3 . For example, in an embodiment, organic wastes with a relatively high fixed carbon content are selected as raw materials, and in this embodiment, the dust content of the synthesis gas generated in the gasifier 3 is relatively high. In order to achieve a better purification effect on the syngas, in this embodiment, the filter effect on a large amount of dust is achieved by combining a bag filter and a cyclone dust collector.

In a preferred embodiment, the syngas contains carbon monoxide;

The shift reactor 9 is provided with a catalyst, and the catalyst is used for syngas and steam to perform a water-gas shift reaction in the shift reactor, thereby generating hydrogen.

Specifically, in order to achieve a relatively simple reaction process, in this embodiment, the carbon monoxide in the synthesis gas is partially converted into hydrogen and carbon dioxide through the water-gas reaction, thereby increasing the proportion of hydrogen in the output reaction gas, and improving the yield. At the same time, a relatively simple reaction process is realized, and the problem of cumbersome reaction process caused by chemical chain hydrogen production in the prior art is avoided.

In the implementation process, the synthesis gas input into the shift reactor 9 mainly contains carbon monoxide and hydrogen, wherein hydrogen is the main product of the overall hydrogen production system, so by inputting the synthesis gas into the shift reactor 9, the carbon monoxide is partially reacted by steam The generation of hydrogen and carbon dioxide can increase the overall proportion of hydrogen in the reaction gas, thereby achieving higher yields.

In a preferred embodiment, the reaction gas includes hydrogen and carbon dioxide;

A molecular sieve is provided in the gas separator 10, and the molecular sieve is used for adsorbing carbon dioxide to separate hydrogen.

Specifically, in order to achieve higher purity of hydrogen, in this embodiment, for the main products of the reaction gas generated in the shift reactor 9: hydrogen and carbon dioxide, a specific molecular sieve is set, so that the molecular sieve can be adsorbed in the pressure swing adsorption process. carbon dioxide, and then output hydrogen with higher 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 around the rotary kiln 22, and the rotary kiln 22 is used to contain solid organic matter;

The rotary kiln jacket 21 is provided with a flue gas input end 2C on one side of the output end 2B of the rotary kiln pyrolysis reactor 2;

The rotary kiln jacket 21 is also provided with a flue gas output end 2D on one side of the feed end 2A of the rotary kiln pyrolysis reactor 2;

The high temperature flue gas passes through the jacket of the rotary kiln along the direction from the flue gas input end 2C to the flue gas output end 2D.

Specifically, in order to achieve better pyrolysis effect of solid organic matter and better purity of pyrolysis gas, a jacketed rotary kiln is selected for the pyrolysis reaction in this embodiment, so that the high temperature flue gas that may contain impurities does not It is in direct contact with the pyrolysis gas, and at the same time, by setting the high-temperature flue gas to pass through the rotary kiln jacket 21 in the opposite direction to the feeding direction, the rotary kiln 22 is uniformly heated, and the solid organic matter is fully pyrolyzed.

In a preferred embodiment, the quality of the pyrolysis gas input to the hot blast stove 4 is 10% to 15% of the quality of the pyrolysis gas output from the rotary kiln pyrolysis reactor.

The present invention is further described below in conjunction with a production example:

In this embodiment, the hydrogen production system as shown in FIG. 3 is selected as the hydrogen production system, the solid organic matter is selected from the waste sieve such as rubber, textile, plastic, etc., and the feed pump 1 is set as a hydraulic plunger pump. The rotational speed of the rotary kiln pyrolysis reactor 2 is set to 6 rad/min, which is used to agitate the solid organic matter pumped by the feed pump 1 and transport it to the rear end. At the same time, a high temperature flue gas of 700°C is input into the rotary kiln jacket 21 of the rotary kiln pyrolysis reactor 2 to heat the rotary kiln 22, so that the end temperature of the rotary kiln 22 reaches above 500°C, thereby making the solid organic matter fully pyrolyze to generate pyrolysis. gas, and a small amount of pyrolysis residue, which is discharged from the discharge port at the bottom of the end of the rotary kiln 22. Depending on the specific components in the solid organic matter, the mass of the pyrolysis residue is 5% to 20% of the mass of the solid organic matter input to the rotary kiln pyrolysis reactor 2 . Subsequently, the pyrolysis gas output from the rotary kiln pyrolysis reactor 2 is introduced into the gasifier 3, and part of the pyrolysis gas is split into the hot blast furnace 4 as fuel for generating high-temperature flue gas.

The quality of the pyrolysis gas shunted into the hot blast stove 4 is 10% to 15% of the quality of the pyrolysis gas output from the rotary kiln pyrolysis reactor 2, and the split flow to the hot blast stove 4 can be appropriately adjusted according to the end temperature of the rotary kiln pyrolysis reactor 2 Therefore, the temperature in the rotary kiln pyrolysis reactor 2 meets the pyrolysis demand and improves the overall yield of the hydrogen production system. In the hot blast stove 4, the pyrolysis gas and the preheated air preheated to about 150°C are mixed for combustion to generate high temperature flue gas. The temperature of the high temperature flue gas at the flue gas output end 4B of the hot blast stove 4 is about 800°C. Subsequently, the high temperature flue gas heats the air in the first heat exchanger 5 , so that the air is preheated to about 150° C. to meet the demand of the hot blast stove 4 for preheated air. The temperature of the high-temperature flue gas is reduced to about 700°C after heat exchange by the first heat exchanger 5 and is input into the rotary kiln pyrolysis reactor 2 for heating the rotary kiln 22 so that the temperature of the rotary kiln 22 meets the level of solid organic matter. Pyrolysis needs.

The maximum temperature of the gasifier 3 is set to 900°C or higher, and preheated oxygen with a temperature of about 150°C is continuously input. The pyrolysis gas introduced into the gasifier 3 stays in an atmosphere of 900°C for a period of time, and undergoes a gasification reaction with preheated oxygen, so that most of the tar components in the pyrolysis gas are cracked into small molecular components, thereby generating and outputting Syngas whose main components are carbon monoxide and hydrogen.

The temperature of the syngas output from the output end 3C of the gasifier 3 is 750°C. In order to make full use of the waste heat resources of the syngas, the syngas is introduced into the steam generator 6 and the second heat exchanger 7 in turn to generate shift reactions respectively. The steam required by the gasifier 9, and the preheated oxygen required by the gasifier 3. The dust and tar components in the syngas are then filtered through filter 8 before entering shift reactor 9 . Since the impurities in the syngas in this embodiment are mainly dust and tar, the filter 8 in this embodiment is configured as a bag filter, thereby achieving better filtering effect on impurities.

A catalyst is pre-installed in the shift reactor 9, which can make the carbon monoxide component in the syngas and the steam react sufficiently to generate carbon dioxide and hydrogen, and further increase the proportion of the hydrogen component in the syngas generated by the gasifier 3. , thereby generating a reaction gas whose main components are carbon dioxide and hydrogen. Subsequently, through the gas separator 10 pre-installed with molecular sieves, the carbon dioxide component in the reaction gas can be adsorbed under the action of pressure swing adsorption, thereby generating hydrogen with higher purity, and introducing it into the hydrogen storage tank 11 for storage.

The beneficial effect of the invention is that: the solid organic waste is treated by the solid organic matter pyrolysis-gasification technology, the heat utilization efficiency is effectively improved in the process of harmless treatment of the solid organic waste, and the reduction reaction is carried out. The system inhibits the generation of dioxin precursors and avoids secondary pollution. The overall device has a simple structure, a small footprint, and a stable hydrogen generation process, which is convenient for large-scale production.

The above are only preferred embodiments of the present invention, and are not intended to limit the embodiments and protection scope of the present invention. For those skilled in the art, they should be aware of the equivalent replacement and Solutions obtained by obvious changes shall all be included in the protection scope of the present invention.

Claims (10)

1. a hydrogen production system of solid organic matter, is characterized in that, comprises: Rotary kiln pyrolysis reactor, the rotary kiln pyrolysis reactor receives the solid organic matter input from the outside, and inputs high-temperature flue gas, so as to use the high-temperature flue gas to pyrolyze the solid organic matter to generate pyrolysis gas ; a gasifier receiving the pyrolysis gas output from the rotary kiln pyrolysis reactor and inputting preheated oxygen to generate syngas using the preheated oxygen and the pyrolysis gas; a shift reactor that receives the syngas output from the gasifier and inputs steam to generate a reaction gas from the steam and the syngas; A gas separator, the gas separator receives the reaction gas output from the shift reactor, and the gas separator separates hydrogen from the reaction gas to complete the hydrogen production process. 2 . The hydrogen production system according to claim 1 , wherein the output end of the rotary kiln pyrolysis reactor is also connected to a hot blast stove, and the hot blast stove and the gasifier are simultaneously received from the rotary kiln. 3 . the pyrolysis gas output from the kiln pyrolysis reactor; Also input preheated air in the hot blast stove; 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 to the heat input end of a first heat exchanger; The heat output end of the first heat exchanger is connected to the flue gas input end of the rotary kiln pyrolysis reactor for inputting the high temperature flue gas into the rotary kiln pyrolysis reactor; The cold input end of the first heat exchanger inputs air from the outside, and the first heat exchanger uses the heat of the high temperature flue gas to heat the air to generate the preheated air; The cold output end of the first heat exchanger is connected to the air input end of the hot blast stove for inputting the preheated air into the hot blast stove. 4. The hydrogen production system according to claim 1, wherein the hydrogen production system further comprises a steam generator, and the heat input end of the steam generator is connected to the output end of the gasifier; Water input from the outside is also input into the steam generator, and the steam generator generates the steam by using the heat of the synthesis gas output by the gasifier and the water; The steam output end of the steam generator is connected to the steam input end of the shift reactor for inputting the steam to the shift reactor. 5 . The hydrogen production system according to claim 4 , wherein the hydrogen production system further comprises a second heat exchanger, and the heat input end of the second heat exchanger is connected to the heat of the steam generator. 6 . output; The cold input end of the second heat exchanger inputs oxygen from outside, and the second heat exchanger uses the heat of the syngas to heat the oxygen to generate the preheated oxygen; The cold output end of the second heat exchanger is connected to the oxygen input end of the gasifier for inputting the preheated oxygen into the gasifier. 6 . The hydrogen production system according to claim 5 , wherein the hydrogen production system further comprises a filter, the input end of the filter is connected to the heat output end of the heat exchanger, and the filter The output end is connected to the syngas input end of the shift reactor; The filter receives the syngas output from the second heat exchanger, and after the filter removes impurities in the syngas, the syngas is fed into the shift reactor. 7. The hydrogen production system according to claim 1, wherein the synthesis gas comprises carbon monoxide; A catalyst is provided in the shift reactor, and the catalyst is used for the synthesis gas and the steam to perform a water-gas shift reaction in the shift reactor, thereby generating the hydrogen. 8. The hydrogen production system according to claim 7, wherein the reaction gas comprises the hydrogen and carbon dioxide; A molecular sieve is provided in the gas separator, and the molecular sieve is used for adsorbing the carbon dioxide to separate the hydrogen. 9. The hydrogen production system according to claim 3, wherein the rotary kiln pyrolysis reactor has a rotary kiln jacket and a rotary kiln, and the rotary kiln jacket is wrapped outside the rotary kiln, so The rotary kiln is used for containing the solid organic matter; The rotary kiln jacket is provided with the flue gas input end on one side of the output end of the rotary kiln pyrolysis reactor; The rotary kiln jacket is also provided with a flue gas output end on one side of 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 production system according to claim 2 , wherein the mass of the pyrolysis gas input to the hot blast stove is 10 times the mass of the pyrolysis gas output from the rotary kiln pyrolysis reactor. 11 . %～15%.

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