CN109852429B - Hydrogen production system and method by coupling coal combustion and garbage steam gasification - Google Patents
Hydrogen production system and method by coupling coal combustion and garbage steam gasification Download PDFInfo
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- 238000002485 combustion reaction Methods 0.000 title claims abstract description 89
- 238000002309 gasification Methods 0.000 title claims abstract description 83
- 239000010813 municipal solid waste Substances 0.000 title claims abstract description 74
- 239000003245 coal Substances 0.000 title claims abstract description 52
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 41
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 38
- 239000001257 hydrogen Substances 0.000 title claims abstract description 38
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 17
- 230000008878 coupling Effects 0.000 title claims abstract description 10
- 238000010168 coupling process Methods 0.000 title claims abstract description 10
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 10
- 238000000034 method Methods 0.000 title claims description 13
- 239000007789 gas Substances 0.000 claims abstract description 65
- 239000000571 coke Substances 0.000 claims abstract description 44
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 35
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 35
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 15
- 239000003546 flue gas Substances 0.000 claims abstract description 15
- 239000002817 coal dust Substances 0.000 claims abstract description 6
- 238000000629 steam reforming Methods 0.000 claims abstract description 5
- 239000004576 sand Substances 0.000 claims abstract description 4
- 238000001816 cooling Methods 0.000 claims abstract description 3
- 239000012535 impurity Substances 0.000 claims abstract description 3
- 238000002156 mixing Methods 0.000 claims abstract description 3
- 239000000463 material Substances 0.000 claims description 22
- 239000002918 waste heat Substances 0.000 claims description 13
- 239000002893 slag Substances 0.000 claims description 12
- 239000003795 chemical substances by application Substances 0.000 claims description 10
- 230000018044 dehydration Effects 0.000 claims description 9
- 238000006297 dehydration reaction Methods 0.000 claims description 9
- 238000001179 sorption measurement Methods 0.000 claims description 9
- 239000002245 particle Substances 0.000 claims description 8
- 239000000843 powder Substances 0.000 claims description 8
- 230000009471 action Effects 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 6
- 230000005611 electricity Effects 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 229910052799 carbon Inorganic materials 0.000 claims description 5
- 238000006243 chemical reaction Methods 0.000 claims description 5
- 238000009826 distribution Methods 0.000 claims description 5
- 229920006395 saturated elastomer Polymers 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 5
- 239000007787 solid Substances 0.000 claims description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 4
- 230000003647 oxidation Effects 0.000 claims description 3
- 238000007254 oxidation reaction Methods 0.000 claims description 3
- 238000012545 processing Methods 0.000 claims description 3
- 238000006722 reduction reaction Methods 0.000 claims description 3
- 238000001035 drying Methods 0.000 claims description 2
- 238000000197 pyrolysis Methods 0.000 claims description 2
- 238000012546 transfer Methods 0.000 claims description 2
- 238000007781 pre-processing Methods 0.000 claims 1
- 238000010248 power generation Methods 0.000 abstract description 3
- 230000008569 process Effects 0.000 description 5
- 238000013461 design Methods 0.000 description 4
- 230000001276 controlling effect Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000011161 development Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000012216 screening Methods 0.000 description 2
- 239000000969 carrier Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000009970 fire resistant effect Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000007885 magnetic separation Methods 0.000 description 1
- 150000002927 oxygen compounds Chemical class 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Processing Of Solid Wastes (AREA)
- Gasification And Melting Of Waste (AREA)
Abstract
The invention discloses a hydrogen production system and a hydrogen production method by coupling coal combustion and garbage steam gasification, which are used for mixing garbage coke and coal dust to produce hot sand and hot flue gas and producing steam for a circulating fluidized bed coal burning system for heat supply or power generation; a fixed bed garbage gasification system for converting household garbage into coke and hydrogen-rich synthetic gas; and the synthesis gas treatment system is used for cooling and purifying the synthesis gas, separating tar impurities and obtaining high-quality hydrogen-rich synthesis gas. The invention gasifies the garbage under the reducing condition, and the steam reforming reaction of the steam, the tar and the coke is carried out, and simultaneously the gas yield and the gas quality are improved, so that the hydrogen-rich synthetic gas is obtained to realize the hydrogen production function of the garbage.
Description
Technical Field
The invention belongs to the field of solid waste disposal, and particularly relates to a hydrogen production system and method by coupling coal combustion and garbage steam gasification.
Background
In order to reduce the damage of pollutants generated in the energy use process to the human environment, people pay more attention to the development and utilization of hydrogen energy. The hydrogen energy is used as an ideal secondary energy, is clean and pollution-free, has high combustion heat value and convenient storage and transportation, and is regarded as the energy with the most development potential in the future.
The organic component of the municipal solid waste contains a large amount of carbon and oxygen compounds, so that the municipal solid waste can be regarded as a renewable resource, and the municipal solid waste can be reduced by utilizing the steam gasification technology, and the hydrogen-rich synthetic gas can be produced to recover hydrogen energy. However, the steam gasification process needs to absorb a large amount of heat, and the stable and sustainable operation needs to be fully coupled with the combustion heating system.
On the other hand, under the large background of coal-to-electricity capacity removal, the utilization rate of power plant equipment is low, and outdated thermal power plants exceeding 20GW are eliminated, so that most existing steam turbines of the coal-fired power plants cannot operate at full load. The coal burning system of the active coal power plant is utilized to provide heat required by the steam gasification of the garbage, so that the stable operation of the steam gasification of the household garbage can be realized, meanwhile, the mechanical strength of the coke product of the gasification process of the garbage is smaller, and the physical property parameters of the coke product are close to those of coal after crushing, so that the coke product can be mixed with the coal to replace part of raw coal.
Therefore, it is necessary to design a system and a method for coupling coal with steam gasification of garbage, and supply heat generated by coal combustion to the garbage gasification system to realize a continuous and stable steam gasification hydrogen production process.
Disclosure of Invention
The invention aims to realize continuous and stable steam gasification of household garbage, and simultaneously send gasified garbage coke into a coal-fired boiler to be mixed with coal to replace part of coal-fired load, thereby realizing the function of indirectly converting a thermoelectric product into hydrogen-rich synthetic gas.
In order to solve the technical problems, a first technical scheme of the invention is as follows: a hydrogen production system by coal combustion coupling garbage vapor gasification is characterized in that: comprising
The circulating fluidized bed coal burning system is used for mixing and burning garbage coke and coal dust to generate hot sand and hot flue gas and steam for heating or generating electricity;
a fixed bed garbage gasification system for converting household garbage into coke and hydrogen-rich synthetic gas;
and the synthesis gas treatment system is used for cooling and purifying the synthesis gas, separating tar impurities and obtaining high-quality hydrogen-rich synthesis gas.
Preferably, the circulating fluidized bed coal burning system comprises: fluidized bed combustion furnace, cyclone separator at outlet of combustion furnace, feed back leg, spiral feeder of combustion furnace and waste heat boiler; the lower part of the left wall surface of the hearth of the fluidized bed combustion furnace is provided with a coal powder feeding port which is connected with a spiral feeder of the combustion furnace, and the lower part of the right wall surface of the hearth is connected with a feed back leg; the bottom of the fluidized bed combustion furnace is provided with a slag discharging port, and the fluidized gas is introduced into the hearth from the bottom through an air distribution plate right above the slag discharging port; the top of the fluidized bed combustion furnace is connected and communicated with a cyclone separator at the outlet of the combustion furnace, and the cyclone separator at the outlet of the combustion furnace is connected with a waste heat boiler.
Preferably, the fixed bed garbage gasification system comprises: a fixed bed gasifier, a gasifier outlet cyclone separator, a coke crusher and a gasifier screw feeder; a garbage feeding port is arranged at the upper part of the right wall surface of the hearth of the fixed bed gasifier and is connected with a spiral feeder of the gasifier; the upper part of the left wall surface is connected with a cyclone separator at the outlet of the combustion furnace, and a coke discharge hole at the lower part of the left wall surface is connected with a coke crusher; the bottom of the gasification furnace is provided with a gasifying agent inlet, and the top of the hearth is communicated with a cyclone separator at the outlet of the gasification furnace.
Preferably, the synthesis gas processing system comprises: electronic oil remover, CO 2 An adsorption tower, a dehydration tower and a heat exchanger; after gas-solid separation of the synthesis gas in the gasifier through the cyclone separator at the outlet of the gasifier, the synthesis gas sequentially passes through the electronic oil remover, the heat exchanger and the CO 2 And the adsorption tower and the dehydration tower are used for obtaining the hydrogen-rich synthetic gas.
Preferably, in the circulating fluidized bed coal burning system, the pulverized coal is fed into the fluidized bed combustion furnace from a combustion furnace screw feeder.
Preferably, the circulating fluidized bed coal burning system adopts a double-pressure-stage waste heat boiler, part of heat is used for producing low-pressure saturated steam, the low-pressure saturated steam is used as a steam gasifying agent to be introduced into a gasification furnace, and the rest of heat is used for producing superheated steam to be introduced into a steam turbine to perform work and generate power.
Preferably, in the fixed bed garbage gasification system, the dried garbage is fed into the fixed bed gasifier from a gasifier screw feeder.
Preferably, in the fixed bed garbage gasification system, after garbage coke discharged from a gasification furnace passes through a coke crusher, the particle size is reduced, the mechanical strength is reduced, and the garbage coke is easy to mix with pulverized coal; the particle size of the garbage coke which is crushed and then sent into the fluidized bed combustion furnace is less than 30mm.
Preferably, in the synthesis gas treatment system, air obtains power from a fan, exchanges heat with synthesis gas discharged from an electronic oil remover at a heat exchanger, and is respectively introduced into a fluidized bed combustion furnace and a fixed bed gasification furnace as fluidizing gas and gasifying agent after heating, and meanwhile, the flow rate of the synthesis gas is controlled through a flow control valve.
The second technical scheme of the invention is as follows: the method for producing the hydrogen by coupling coal combustion and garbage steam gasification is characterized by comprising the following steps of:
step 1): coal powder is fed from a coal powder feeding port at the upper part of the left wall surface of the fluidized bed combustion furnace through a combustion furnace screw feeder, combustion reaction occurs under the oxidation action of fluidized gas, flue gas generated by combustion entrains heat-carrying bed materials to enter a cyclone separator at an outlet of the combustion furnace, gas-solid separation is carried out under the action of centrifugal force, heat-carrying bed material particles fall into a fixed bed gasification furnace through a material returning device, and the flue gas enters a double-pressure-stage waste heat boiler; the temperature of the flue gas at the outlet of the fluidized bed combustion furnace reaches 890 ℃;
step 2): the pretreated household garbage is fed from the upper part of the right wall surface of the fixed bed gasifier through a gasifier screw feeder, and then mixed with the heat-carrying bed material to transfer heat at the bottom of the fixed bed gasifier, so that devolatilization reaction and gasification reduction reaction are carried out, and steam reforming reaction is carried out in the steam atmosphere; discharging the garbage coke generated by gasification into a coke crusher, crushing, and feeding the crushed garbage coke into a fluidized bed combustion furnace through a feed back leg to mix with pulverized coal; generated by gasification as H 2 、CO 2 、CO、H 2 O and CH 4 The main crude synthesis gas enters a cyclone separator at the outlet of the gasifier, ash is separated and enters a synthesis gas treatment system, and the temperature of the crude synthesis gas at the outlet of the fixed bed gasifier is about 600-800 ℃;
step 3): the garbage coke entering the fluidized bed combustion furnace from the feed back leg is fully mixed with coal dust for combustion, fixed carbon is converted, and slag generated by the coke and the coal is discharged from a slag outlet of the fluidized bed combustion furnace; the heat generated by combustion is used for producing steam for supplying heat or generating electricity;
step 4): the crude synthetic gas from the cyclone separator at the outlet of the gasification furnace firstly passes through an electronic oil remover to remove tar, and then passes through a heat exchanger to exchange heat with air blown out from a fan; next through CO 2 Adsorption tower, most of CO contained in synthesis gas 2 Is adsorbed; and finally removing water in the dehydration tower to obtain the hydrogen-rich synthetic gas with higher quality.
Preferably, the temperature of the heat-carrying bed material falling into the fixed bed gasifier in the step 1) reaches 850 ℃.
Preferably, the water content of the household garbage in the step 2) is less than 20% after the household garbage is subjected to pretreatment such as crushing and drying.
Preferably, the tar obtained from the electronic oil remover in the step 4) is conveyed to a feed inlet of a fixed bed gasifier, and enters the fixed bed gasifier for secondary pyrolysis gasification.
Compared with the existing garbage disposal technology, the invention has the following advantages:
(1) The invention gasifies the garbage under the reducing condition, and the steam reforming reaction of the steam, the tar and the coke is carried out, and simultaneously the gas yield and the gas quality are improved, so that the hydrogen-rich synthetic gas is obtained to realize the hydrogen production function of the garbage.
(2) The invention develops a new power generation technology improvement point on the basis of the original coal-fired power plant, fully utilizes the active coal motor group equipment and the flue gas treatment system, only needs to be coupled with a common fixed bed gasifier on the basis, and reduces a great amount of investment.
(3) The invention adopts the double-bed design of fluidized bed combustion and fixed bed gasification processes, takes bed materials as heat carriers, circulates between two hearths, solves the heat source input problem of the fixed bed garbage steam gasification endothermic reaction and the recycling problem of single-bed gasification coke, simultaneously achieves the aim of accurately controlling the temperature in the gasification furnace by controlling the circulating quantity of the bed materials, and ensures the continuous and stable operation of the system.
(4) According to the invention, environmental treatment and energy revolution are combined, domestic garbage is treated in a large scale, stable and efficient gasification of the garbage is realized, and secondary environmental pollution caused by direct incineration of the garbage is greatly reduced; the pulverized coal is mixed with the garbage coke to carry the equipment at full load, so that the coal consumption of coal and electricity is reduced, the renewable energy is improved, and the poly-generation of heat and electricity is realized through two processes of coupled combustion and gasification.
Drawings
The following is a further detailed description of embodiments of the invention with reference to the drawings
Fig. 1 is a schematic diagram of a system structure according to the present invention.
Reference numerals illustrate:
1. fluidized bed combustion furnace, 2 fixed bed gasifier, 3 burner outlet cyclone separator, 4 return leg, 5 coke breaker, 6 gasifier outlet cyclone separator, 7 electronic oil remover, 8 CO 2 Adsorption tower, 9, dehydration tower, 10, heat exchanger, 11, flow control valve, 12, blower, 13, return, 14, burner screw feeder, 15, gasifier screw feeder, 16, waste heat boiler a, waste, b, coal dust, c, coke, d, hydrogen-rich synthetic gas, e, tar, f, steam, g, flue gas, h, gasifying agent, i, fluidized bed slag, j, ash, k, fluidizing gas, m, steam.
Description of the embodiments
See the drawings. The embodiment discloses a hydrogen production system by coupling coal combustion and garbage steam gasification, which comprises a circulating fluidized bed coal burning system, a fixed bed garbage gasification system and a synthesis gas treatment system. Wherein, the coal burning system design is based on HG-480/13.7L.MG31 type circulating fluidized bed boiler with power of 135MW, and the gasification system design is based on fixed bed experimental data.
The circulating fluidized bed coal burning system comprises: a fluidized bed combustion furnace 1, a combustion furnace outlet cyclone 3, a feed back leg 4, a combustion furnace screw feeder 14 and a waste heat boiler 16. The lower part of the left wall surface of the hearth of the fluidized bed combustion furnace 1 is provided with a coal powder feeding port which is connected with a spiral feeder 14 of the combustion furnace, and the lower part of the right wall surface of the hearth is connected with a feed back leg 4; the bottom of the fluidized bed combustion furnace 1 is provided with a slag outlet, and the fluidizing gas k is introduced into the hearth from the bottom through a wind distribution plate right above the slag outlet; the top of the fluidized bed combustion furnace 1 is connected and communicated with a cyclone separator 3 at the outlet of the combustion furnace, and the outlet of the cyclone separator 3 at the outlet of the combustion furnace is connected with a waste heat boiler 16.
The fixed bed garbage gasification system comprises: a fixed bed gasifier 2, a gasifier outlet cyclone separator 6, a coke crusher 5 and a gasifier screw feeder 15; a garbage feeding port is arranged at the upper part of the right wall surface of the hearth of the fixed bed gasification furnace 2 and is connected with a gasification furnace screw feeder 15; the upper part of the left wall surface is connected with a cyclone separator 3 at the outlet of the combustion furnace, and a coke discharge hole at the lower part of the left wall surface is connected with a coke crusher 5; the bottom of the gasification furnace is provided with a gasifying agent h inlet, and the top of the hearth is connected and communicated with a cyclone separator 6 at the outlet of the gasification furnace.
The synthesis gas processing system comprises: electronic oil remover 7, CO 2 An adsorption tower 8, a dehydration tower 9 and a heat exchanger 10.
The operation of the embodiment of the hydrogen production system based on the coal combustion coupling garbage steam gasification comprises the following steps:
step 1): the pulverized coal b qualified by primary screening is crushed to have the grain diameter below 7mm and is fed from a pulverized coal feeding port at the upper part of the left wall surface of the fluidized bed combustion furnace 1 through a combustion furnace screw feeder 14, and the hearth is covered with bed material sand with the grain diameter less than or equal to 1 mm.
Step 2): preheated air with the temperature of about 200 ℃ is introduced into the fluidized bed combustion furnace 1 through an air distribution plate at the bottom of the fluidized bed combustion furnace 1; the pulverized coal b is ignited by combustion-supporting oil and is subjected to combustion reaction under the oxidation action of the fluidized gas k, flue gas g generated by combustion is carried with heat-carrying bed materials to enter a cyclone separator 3 at an outlet of a combustion furnace, gas-solid separation is carried out under the action of centrifugal force, heat-carrying bed material particles fall into a fixed bed gasifier 2 through a material returning device 13, and the flue gas g enters a double-pressure-stage waste heat boiler 16;
step 3): the flue gas carries out convection heat exchange in the waste heat boiler, part of heat is used for producing low-pressure saturated steam, steam m is introduced into the fixed bed gasification furnace 2, and the rest of heat is used for producing superheated steam f and is introduced into the steam turbine for power generation.
Step 4): the designed bed temperature of the combustion furnace is 890 ℃, the actual running bed temperature is kept at about 800-920 ℃, and the designed temperature of the flue gas at the outlet of the hearth reaches 890 ℃. The cyclone separator adopts heat-preserving, fire-resistant and wear-resistant materials to reduce heat loss, so that the temperature of the heat-carrying bed material particles falling into the fixed bed gasification furnace 2 reaches about 850 ℃. The bed material quantity is increased, the circulation quantity of materials is increased, and the bed temperature can be reduced; increasing the slag discharge amount, reducing the bed pressure, reducing the material amount and increasing the bed temperature.
Step 5): the pretreated (crushed raw garbage after screening and magnetic separation) household garbage a enters the fixed bed gasifier 2 through a feeding port above the right wall surface of the fixed bed gasifier 2 by a gasifier screw feeder 15. Gasifying agent h (air) is introduced from the bottom of the fixed bed gasifier 2, garbage a and the heat-carrying bed material are mixed and transferred in the fixed bed gasifier 2 to perform devolatilization reaction and gasification reduction reaction, and steam reforming reaction is performed in the steam atmosphere. The water content of the garbage raw material fed into the gasification furnace is less than 20%.
Step 6): the garbage coke c generated by gasification is discharged into a crusher 5, crushed and enters a fluidized bed combustion furnace 1 through a feed back leg 4 to be mixed with coal powder b. The particle size of the garbage coke c sent into the fluidized bed after being crushed is less than 30mm. Generated by gasification as H 2 、CO 2 、CO、H 2 O and CH 4 The main crude synthesis gas enters a cyclone separator 6 at the outlet of the gasification furnace, and ash j is separated and then enters a synthesis gas treatment system.
Step 7): the crude synthetic gas from the cyclone separator 6 at the outlet of the gasification furnace firstly passes through the electronic oil remover 7 to remove tar e, and then passes through the heat exchanger 10 to exchange heat with air blown out from the fan 12; second through CO 2 Adsorption tower 8, most of CO contained in the synthesis gas 2 Is adsorbed; finally, removing water in the dehydration tower 9 to obtain the hydrogen-rich synthetic gas d with higher quality. After the air blown out of the fan 12 is preheated and heated to about 200 ℃ and regulated and distributed by the flow control valve 11, one part of the air is used as fluidizing gas k to enter the fluidized bed combustion furnace 1, and the other part of the air is used as gasifying agent h to enter the fixed bed gasification furnace 2.
Step 8): the temperature of the fixed bed gasification furnace 2 is regulated and controlled by controlling the proportion of the bed material quantity falling into the fixed bed gasification furnace 2 and the feeding quantity of the garbage a, so that the bed temperature of the fixed bed gasification furnace 2 and the temperature of the outlet synthetic gas are controlled at 600-800 ℃. Table 1 is a laboratory-based fixed bed tube furnace apparatus, and the characteristics of the products of the steam gasification of the garbage at different temperatures are analyzed under the condition of keeping the gasification atmosphere with the air equivalent ratio er=0.3 and the steam-carbon ratio (S/C) =1.5, so that a reference can be provided for designing the temperature control of the gasification hearth.
Table 1: distribution and characteristics of gasification products at different gasification temperatures.
| Gasification temperature (. Degree. C.) | 600 | 650 | 700 | 750 | 800 |
| Synthesis gas yield (Nm) 3 /kg MSW) | 0.27 | 0.38 | 0.47 | 0.54 | 0.65 |
| H 2 Volume ratio (Vol%) | 16.26 | 19.73 | 24.87 | 27.82 | 33.43 |
| LHV (MJ/Nm) of synthesis gas 3 ) | 19.83 | 19.15 | 18.67 | 17.02 | 16.53 |
| Carbon conversion (%) | 30.49 | 40.10 | 47.76 | 50.69 | 56.79 |
Claims (7)
1. A hydrogen production system by coal combustion coupling garbage vapor gasification is characterized in that: the circulating fluidized bed coal burning system is used for mixing and burning garbage coke and coal dust to generate hot sand and hot flue gas and steam for heating or generating electricity; a fixed bed garbage gasification system for converting household garbage into coke and raw synthesis gas; the synthesis gas treatment system is used for cooling and purifying the synthesis gas, separating tar impurities and obtaining high-quality hydrogen-rich synthesis gas;
the circulating fluidized bed coal burning system comprises: fluidized bed combustion furnace, cyclone separator at outlet of combustion furnace, feed back leg, spiral feeder of combustion furnace and waste heat boiler; the lower part of the left wall surface of the hearth of the fluidized bed combustion furnace is provided with a coal powder feeding port which is connected with a spiral feeder of the combustion furnace, and the lower part of the right wall surface of the hearth is connected with a feed back leg; the bottom of the fluidized bed combustion furnace is provided with a slag discharging port, and the fluidized gas is introduced into the hearth from the bottom through an air distribution plate right above the slag discharging port; the top of the fluidized bed combustion furnace is connected and communicated with a cyclone separator at the outlet of the combustion furnace, and the cyclone separator at the outlet of the combustion furnace is connected with a waste heat boiler;
the fixed bed garbage gasification system comprises: a fixed bed gasifier, a gasifier outlet cyclone separator, a coke crusher and a gasifier screw feeder; a garbage feeding port is arranged at the upper part of the right wall surface of the hearth of the fixed bed gasifier and is connected with a spiral feeder of the gasifier; the upper part of the left wall surface is connected with a cyclone separator at the outlet of the combustion furnace, and a coke discharge hole at the lower part of the left wall surface is connected with a coke crusher; the bottom of the gasification furnace is provided with a gasifying agent inlet, and the top of the hearth is communicated with a cyclone separator at the outlet of the gasification furnace;
feeding garbage from a gasification furnace screw feeder into a fixed bed gasification furnace; the garbage coke discharged from the fixed bed gasification furnace is crushed by a coke crusher and then is sent into a fluidized bed combustion furnace, and the particle size of the garbage coke sent into the fluidized bed combustion furnace is smaller than 30mm.
2. The coal combustion coupled refuse steam gasification hydrogen production system as defined in claim 1, further characterized by: the synthesis gas processing system comprises: electronic oil remover, CO 2 An adsorption tower, a dehydration tower and a heat exchanger; after gas-solid separation of the synthesis gas in the gasifier through the cyclone separator at the outlet of the gasifier, the synthesis gas sequentially passes through the electronic oil remover, the heat exchanger and the CO 2 And the adsorption tower and the dehydration tower are used for obtaining the hydrogen-rich synthetic gas.
3. The coal combustion coupled refuse steam gasification hydrogen production system as defined in claim 1, further characterized by: feeding pulverized coal from a spiral feeder of a combustion furnace into a fluidized bed combustion furnace; a double-pressure-stage waste heat boiler is adopted, part of heat is used for producing low-pressure saturated steam, the low-pressure saturated steam is used as a steam gasifying agent and is introduced into a fixed bed gasifying furnace, and the rest of heat is used for producing superheated steam and is introduced into a steam turbine to perform work and generate power.
4. The coal combustion coupled refuse steam gasification hydrogen production system as defined in claim 2, further comprising: the air obtains power from the fan, exchanges heat with the synthesis gas discharged from the electronic oil remover at the heat exchanger, and is used as fluidizing gas and gasifying agent to be respectively introduced into the fluidized bed combustion furnace and the fixed bed gasification furnace after being heated, and meanwhile, the flow of the air is controlled through a flow control valve.
5. A method of producing hydrogen in a hydrogen production system as claimed in claim 1, wherein: the method comprises the following steps:
step 1): coal powder is fed from a coal powder feeding port at the upper part of the left wall surface of the fluidized bed combustion furnace through a combustion furnace screw feeder, combustion reaction occurs under the oxidation action of fluidized gas, flue gas generated by combustion entrains heat-carrying bed materials to enter a cyclone separator at an outlet of the combustion furnace, gas-solid separation is carried out under the action of centrifugal force, heat-carrying bed material particles fall into a fixed bed gasification furnace through a material returning device, and the flue gas enters a double-pressure-stage waste heat boiler; the temperature of the flue gas at the outlet of the fluidized bed combustion furnace reaches 890 ℃;
step 2): the pretreated household garbage is fed from the upper part of the right wall surface of the fixed bed gasifier through a gasifier screw feeder, and then mixed with the heat-carrying bed material at the bottom of the fixed bed gasifier to carry out heat transfer, so as to carry out devolatilization reaction and gasification reduction reaction, and steam reforming reaction is carried out in the steam atmosphere; discharging the garbage coke generated by gasification into a coke crusher, crushing, and feeding the crushed garbage coke into a fluidized bed combustion furnace through a feed back leg to mix with pulverized coal; generated by gasification as H 2 、CO 2 、CO、H 2 O and CH 4 The main crude synthesis gas enters a cyclone separator at the outlet of the gasifier, ash is separated and enters a synthesis gas treatment system, and the temperature of the crude synthesis gas at the outlet of the fixed bed gasifier is 600-800 ℃;
step 3): the garbage coke entering the fluidized bed combustion furnace from the feed back leg is fully mixed with coal dust for combustion, fixed carbon is converted, and slag generated by the coke and the coal is discharged from a slag outlet of the fluidized bed combustion furnace; the heat generated by combustion is used for producing steam for supplying heat or generating electricity;
step 4): the crude synthetic gas from the cyclone separator at the outlet of the gasification furnace firstly passes through an electronic oil remover to remove tar, and then passes through a heat exchanger to exchange heat with air blown out from a fan; second through CO 2 Adsorption tower, most of CO contained in synthesis gas 2 Is adsorbed; and finally removing water in the dehydration tower to obtain the hydrogen-rich synthetic gas with higher quality.
6. The method of producing hydrogen as claimed in claim 5, wherein: and (2) crushing, drying and preprocessing the household garbage in the step (2), wherein the water content of the garbage fed into the fixed bed gasification furnace is less than 20%.
7. The method of producing hydrogen as claimed in claim 5, wherein: in the step 4): and (3) conveying tar obtained from the electronic oil remover to a feed inlet of the fixed bed gasifier, and entering the fixed bed gasifier to carry out secondary pyrolysis gasification.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910065523.7A CN109852429B (en) | 2019-01-24 | 2019-01-24 | Hydrogen production system and method by coupling coal combustion and garbage steam gasification |
Applications Claiming Priority (1)
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| CN108753326A (en) * | 2018-06-15 | 2018-11-06 | 北京三聚绿能科技有限公司 | A kind of straw thermal cracking technique |
| CN109385308A (en) * | 2018-11-28 | 2019-02-26 | 浙江工业大学 | A kind of the double bed electricity generation system and method for coal-fired coupling domestic garbage pyrolysis |
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