CN209872884U - Device for pressurized water absorption decarburization of biogas by using micro-channel mixing device - Google Patents
Device for pressurized water absorption decarburization of biogas by using micro-channel mixing device Download PDFInfo
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- CN209872884U CN209872884U CN201920424562.7U CN201920424562U CN209872884U CN 209872884 U CN209872884 U CN 209872884U CN 201920424562 U CN201920424562 U CN 201920424562U CN 209872884 U CN209872884 U CN 209872884U
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 105
- 238000005261 decarburization Methods 0.000 title claims abstract description 28
- 238000002156 mixing Methods 0.000 title claims abstract description 19
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 14
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 118
- 238000000926 separation method Methods 0.000 claims abstract description 38
- 239000000203 mixture Substances 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 42
- 238000007664 blowing Methods 0.000 claims description 33
- 230000008929 regeneration Effects 0.000 claims description 30
- 238000011069 regeneration method Methods 0.000 claims description 30
- 239000007788 liquid Substances 0.000 claims description 14
- 238000001179 sorption measurement Methods 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- 238000003860 storage Methods 0.000 claims description 3
- 239000002912 waste gas Substances 0.000 claims description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 2
- 239000003463 adsorbent Substances 0.000 claims description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 2
- 239000002808 molecular sieve Substances 0.000 claims description 2
- 239000000741 silica gel Substances 0.000 claims description 2
- 229910002027 silica gel Inorganic materials 0.000 claims description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 2
- 229910001220 stainless steel Inorganic materials 0.000 claims description 2
- 239000010935 stainless steel Substances 0.000 claims description 2
- 238000000746 purification Methods 0.000 abstract description 9
- 238000010438 heat treatment Methods 0.000 abstract description 3
- 230000002745 absorbent Effects 0.000 abstract 1
- 239000002250 absorbent Substances 0.000 abstract 1
- 230000018044 dehydration Effects 0.000 abstract 1
- 238000006297 dehydration reaction Methods 0.000 abstract 1
- 238000003912 environmental pollution Methods 0.000 abstract 1
- 238000004064 recycling Methods 0.000 abstract 1
- 238000000034 method Methods 0.000 description 35
- 238000005406 washing Methods 0.000 description 24
- 230000008569 process Effects 0.000 description 23
- 238000005262 decarbonization Methods 0.000 description 20
- 239000003345 natural gas Substances 0.000 description 8
- 238000005265 energy consumption Methods 0.000 description 4
- 239000012528 membrane Substances 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 238000003795 desorption Methods 0.000 description 3
- 238000011049 filling Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- -1 alcohol amine Chemical class 0.000 description 2
- 238000005034 decoration Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 239000004642 Polyimide Substances 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 229920001721 polyimide Polymers 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Gas Separation By Absorption (AREA)
Abstract
The utility model discloses a device for pressurizing water to absorb and decarbonize methane by utilizing a micro-channel mixing device, which takes water as only CO2The absorbent continuously pumps the methane and the water into the micro-channel mixing device for absorption at a certain flow rate under a certain pressure, the gas-water mixture in an emulsified state leaves the mixing device and then enters a gas-water separation tower, and the purified gas after decarburization overflows through gas-water separation to form high-purity biomethane gas after dehydration. Containing CO in high concentration2The absorbed water is subjected to pressure reduction and heating treatment to make CO in the absorbed water2Quickly overflows and is recovered, and the regenerated water returns to the microchannel mixing device for recycling after being subjected to pressurization heat exchange. The utility model has the advantages of high decarburization efficiency, compact equipment, no environmental pollution and the like, and can provide a low-cost solution for decarburization and purification of methane.
Description
Technical Field
The utility model belongs to the environmental protection field, concretely relates to utilize CO among microchannel mixing arrangement desorption marsh gas2The apparatus of (1).
Background
Biogas fermentation is an effective means for producing biological energy by using poor waste biomass. But CO in the biogas2The content is high (30-50%), so that the natural gas cannot be completely replaced, and the application range of the natural gas is greatly limited. In order to improve the quality of the biogas, the CO in the biogas must be removed2The content is less than or equal to 3 percent (volume ratio), and the quality of the fuel gas is improved. The currently common biogas decarburization method mainly comprises the following steps: pressure swing adsorption separation, membrane separation, alcohol amine absorption, high pressure water washing, etc. The pressure swing adsorption separation method has the disadvantages of more complex device and higher investment cost, and the methane yield in the decarburization process needs to be improved. Membrane separation CO realization by using permeation rate difference of polyimide membrane2However, the method has high requirements on the quality of raw material gas, needs multi-stage pretreatment, has high equipment investment and short membrane life, and leads to high decarburization cost of the method. Amine alcohol absorption method (chemical absorption method) for absorbing CO by weak alkaline alcohol amine solvent2However, the heating desorption energy consumption is high, solvent loss and metal corrosion exist, and the heating desorption energy is rarely used for methane decarburization and purification at present. Compared with the methods, the high-pressure water washing method increases the pressure of the system to increase the water to CO2The method has simple process, and is an environment-friendly decarburization process. However, the gas-liquid mass transfer efficiency in the water washing tower is low, so that the gas-water ratio is only 3: 1-5: 1, the circulating water consumption is high, the operation energy consumption is increased, and the process efficiency is urgently required to be improved.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problem thatThe defects of the prior art are that the mass transfer efficiency of water in the process of decarbonizing the marsh gas is improved by utilizing a micro-channel mixing device, so that CO in the marsh gas is efficiently removed2。
In order to achieve the purpose of the utility model, the utility model adopts the following technical scheme:
a device for absorbing pressurized water and decarbonizing methane by utilizing a micro-channel mixing device comprises a micro-channel mixer, a gas-water separation tower, a gas dehydrator, a pressure reducing valve, a first heat exchanger, a regeneration tower, a second heat exchanger, an air blowing tower and a third heat exchanger;
the micro-channel mixer is provided with a methane feeding hole and a pressurized water feeding hole, a discharging hole of the micro-channel mixer is connected with the gas-water separation tower, and a gas-water mixture formed by mixing methane and pressurized water is introduced into the gas-water separation tower;
the top of the gas-water separation tower is connected with an external methane gas storage tank through a gas discharge pipeline, and a gas dehydrator is positioned on the gas discharge pipeline; the bottom of the gas-water separation tower is connected with a first heat exchanger through a drain pipe, and a pressure reducing valve is positioned on the drain pipe;
the discharge hole of the first heat exchanger is connected with the regeneration tower, and the absorbed water in the gas-water separation tower is heated and then is led into the regeneration tower;
the top of the regeneration tower is connected with external CO through a gas discharge pipeline2The bottom of the collecting tank is sequentially connected with the second heat exchanger and the air-blowing tower through a drain pipe, and the regenerated water in the regeneration tower is cooled and then is sent into the air-blowing tower;
an air inlet is formed in the side face of the bottom of the air blowing tower, a waste gas outlet is formed in the side face of the top of the air blowing tower, and air is blown into the air blowing tower to be contacted with the regenerated water;
the bottom of the air-blowing tower is connected with a third heat exchanger through a drain pipe, and the regenerated water discharged from the air-blowing tower is cooled to normal temperature and then recycled.
Specifically, the microchannel mixer is made of stainless steel, the microchannel structure is interdigital, T-shaped, Y-shaped, heart-shaped or column-shaped, the cross section width of the microchannel is 40-200 μm, and the height of the microchannel is 40-1000 μm; the microchannel mixer may be provided with cooling means on the outer wall for controlling the temperature within the apparatus.
The height-diameter ratio of the gas-water separation tower is 8: 1-10: 1, and a gas-water mixture is introduced into the tower from the tower wall on the side surface of the top of the tower.
The gas dehydrator is an adsorption dehydrator, and the adsorbent is one or more of silica gel, alumina and molecular sieve.
The height-diameter ratio of the regeneration tower is 8: 1-10: 1, and the absorption water is pumped into the tower from the side surface of the top of the tower and sprayed from top to bottom through a liquid distributor.
The height-diameter ratio of the air blowing tower is 4: 1-5: 1, and the regenerated water is pumped into the tower from the top of the tower and sprayed from top to bottom through the liquid distributor.
The filling coefficient of liquid in the gas-water separation tower is 40-50 vt%.
The filling coefficient of the liquid in the regeneration tower is 40-50 vt%.
The filling coefficient of liquid in the air blowing tower is 30-40 vt%.
The microchannel mixer is a micro chemical device, the average size of the width of the internal unit structure is in micron order, a large number of fluid channels with the diameter of below 1000 mu m are contained in the extremely small device, the specific surface area is increased, and a fluid thin layer with extremely small thickness is formed. In the microchannel, the fluid is mainly laminar flow, the mass transfer process is mainly intermolecular diffusion, and the mass transfer resistance is far lower than that of a conventional tower. CO generation using extremely high interfacial area of microchannel apparatus2And the solvent and the micro bubbles or liquid drops are dispersed in the whole absorption liquid to form a gas-liquid mixed emulsified state, which is beneficial to full contact of gas and liquid phases and strengthens the gas-liquid mass transfer process. Meanwhile, each channel in the micro-channel mixer is an independent mixer, and the amplification process is the superposition of the number of the channels. It can be seen that the microchannel mixer can achieve miniaturization of the gas-liquid absorption apparatus by increasing the water-to-CO ratio2The absorption efficiency of the system greatly reduces the consumption of circulating water and related energy consumption, is beneficial to reducing the operation cost of biogas purification, and improves the operation safety. Therefore, the micro-channel mixer is applied to methane decarburization, which is beneficial to reducing the site requirement and operating cost of methane purificationThe method has important value for promoting the production of biological energy and protecting the environment.
Has the advantages that:
the device of the utility model obviously improves the mass transfer efficiency of water to the methane decarburization process under medium and low pressure through the micro-channel mixer, compared with the existing high-pressure washing decarburization technology, the gas-liquid ratio can be increased from 4: 1-6: 1 to 20: 1-30: 1, and the power consumption and the regeneration energy consumption are greatly reduced because the water consumption is reduced by 70-80%. The mixer has small volume which is only one hundredth of a tower with the same processing capacity, and is continuously operated, convenient to manage and improved in safety. After the decarbonization and purification treatment of the device, CO in the obtained biological methane gas2The content of the product meets the quality requirement (CO) of the second kind of gas in the Natural gas (GB17820-2012)2Less than or equal to 3 percent) can be used for producing vehicle fuel.
Drawings
These and/or other advantages of the present invention will become more apparent from the following detailed description of the present invention when taken in conjunction with the accompanying drawings and the following detailed description.
FIG. 1 is a schematic view of the entire structure of the decarburization apparatus.
Wherein, 1 micro-channel mixer, 2 gas-water separation tower, 3 gas dehydrator, 4 pressure reducing valve, 5 first heat exchanger, 6 regeneration tower, 7 second heat exchanger, 8 air-blowing tower, 9 third heat exchanger.
Detailed Description
The invention will be better understood from the following examples.
The drawings in the specification show the structure, ratio, size, etc. only for the purpose of matching with the content disclosed in the specification, so as to be known and read by those skilled in the art, and not for the purpose of limiting the present invention, so the present invention does not have the essential meaning in the art, and any structure modification, ratio relationship change or size adjustment should still fall within the scope covered by the technical content disclosed in the present invention without affecting the function and achievable purpose of the present invention. Meanwhile, the terms "upper", "lower", "front", "rear", "middle", and the like used in the present specification are for the sake of clarity only, and are not intended to limit the scope of the present invention, and changes or adjustments of the relative relationship thereof are also considered to be the scope of the present invention without substantial changes in the technical content.
The following examples use the apparatus shown in FIG. 1 to perform pressurized water absorption decarburization of biogas. The device comprises a micro-channel mixer 1, a gas-water separation tower 2, a gas dehydrator 3, a pressure reducing valve 4, a first heat exchanger 5, a regeneration tower 6, a second heat exchanger 7, an air blowing tower 8 and a third heat exchanger 9.
Wherein the micro-channel mixer 1 is provided with a methane feeding hole and a pressurized water feeding hole, a discharging hole of the micro-channel mixer 1 is connected with the gas-water separation tower 2, and a gas-water mixture obtained by mixing methane and pressurized water is introduced into the gas-water separation tower 2; the top of the gas-water separation tower 2 is connected with an external methane gas storage tank through a gas discharge pipeline, and a gas dehydrator 3 is positioned on the gas discharge pipeline; the bottom of the gas-water separation tower 2 is connected with a first heat exchanger 5 through a drain pipe, and a pressure reducing valve 4 is positioned on the drain pipe; the discharge hole of the first heat exchanger 5 is connected with the regeneration tower 6, and the absorbed water in the gas-water separation tower 2 is heated and then is led into the regeneration tower 6; the top of the regeneration tower 6 is connected with external CO through a gas discharge pipeline2The bottom of the collecting tank is sequentially connected with the second heat exchanger 7 and the air-blowing tower 8 through a drain pipe, and the regenerated water in the regeneration tower 6 is cooled and then is sent into the air-blowing tower 8; an air inlet is formed in the side face of the bottom of the air blowing tower 8, a waste gas exhaust port is formed in the side face of the top of the air blowing tower 8, and air is blown into the air blowing tower 8 to be contacted with the regenerated water; the bottom of the air-blowing tower 8 is connected with a third heat exchanger 9 through a drain pipe, and the regenerated water discharged from the air-blowing tower 8 is cooled to normal temperature and then recycled.
Example 1
In this example, CO is used2The biogas (methane content 51%) with content up to 45% is the purification object, and the comparison of biogas decarburization performance is carried out by respectively using a water washing tower and a micro-channel mixing device, and the specific decarburization treatment is carried out according to the following process conditions.
(1) The biogas is decarbonized by adopting a washing tower, and the height-diameter ratio of the washing tower is 8:1, the volume is 500mL, the operating pressure of decarburization is 1.2Mpa, the inflow velocity is 150mL/min, the inflow velocity is 30mL/min, and the gas-water ratio is 5:1, continuously treating 40L of methane at the decarbonization temperature of 20 ℃.
(2) The biogas adopts an interdigital micro-channel mixer (the width (W) of the characteristic dimension of the cross section of the micro-channel is 50 μm, the height (H) is 150 μm, and the volume of the device is 4.5cm3Decarbonizing with inlet flow rate of 150mL/min, inlet flow rate of 5mL/min, gas-water ratio of 30:1, the other conditions are the same as in (1).
In this example, the same gas-water separation column (height to diameter ratio of 8:1, volume of 500mL, separation temperature of 20 ℃ C.), regeneration column (height to diameter ratio of 8:1, volume of 500mL, regeneration temperature of 40 ℃ C.) and blowing column (height to diameter ratio of 4:1, volume of 200mL) were used for both decarburization processes, and the operation processes were the same. The results are shown in Table 1.
TABLE 1
| Decarbonization device | Water washing tower | Microchannel mixer |
| Average CO in biomethane gas2Content (%) | 4.3 | 1.1 |
| Methane loss rate (%) | 0.7 | 0.5 |
| CO2Removal Rate (%) | 95.16 | 98.76 |
It can be seen that the micro-channel mixer is adopted, and CO in the marsh gas2The removal rate is improved from 95.16 percent to 98.76 percent, and the average CO in the biogas2The content is less than or equal to 1.5 percent, the quality requirement of the second-class gas in natural gas (GB17820-2012) is met, and the loss rate of methane is less than or equal to 1 percent. And the water consumption required for treating the same volume of methane is reduced by 83.3 percent.
Example 2
In this example, CO is used2The biogas (methane content 55%) with the content of 40% is a purification object, and the decarbonization performance of the biogas is compared by a water washing tower and a micro-channel mixing device respectively, and the specific decarbonization treatment is carried out according to the following process conditions.
(1) The biogas is decarbonized by adopting a washing tower, and the height-diameter ratio of the washing tower is 10:1, the volume is 500mL, the operating pressure of decarburization is 1.5Mpa, the inflow velocity is 180mL/min, the inflow velocity is 30mL/min, and the gas-water ratio is 6:1, continuously treating 20L of methane at the decarbonization temperature of 15 ℃.
(2) The biogas adopts a Y-shaped microchannel mixer (the width (W) of the characteristic dimension of the cross section of the microchannel is 200 μm, the height (H) is 100 μm, and the volume of the device is 6cm3) Decarbonizing with inlet flow rate of 180mL/min, inlet flow rate of 9mL/min, gas-water ratio of 20:1, the other conditions are the same as in (1).
In this example, the same gas-water separation column (height to diameter ratio 10:1, volume 500mL, separation temperature 15 ℃ C.), regeneration column (height to diameter ratio 10:1, volume 500mL, regeneration temperature 37 ℃ C.) and blowing column (height to diameter ratio 5:1, volume 200mL) were used for both decarburization processes, and the operation processes were the same. The results are shown in Table 2.
TABLE 2
| Decarbonization device | Water washing tower | Microchannel mixer |
| Average CO in biomethane gas2Content (%) | 5.1 | 1.8 |
| Methane loss rate (%) | 0.75 | 0.33 |
| CO2Removal Rate (%) | 93.04 | 97.53 |
It can be seen that the micro-channel mixer is adopted, and CO in the marsh gas2The removal rate is improved from 93.04 percent to 97.53 percent, and the average CO in the biogas2The content is less than or equal to 2 percent, the quality requirement of the second type of gas in natural gas (GB17820-2012) is met, the loss rate of methane is less than or equal to 0.5 percent, and the water consumption required for treating the methane with the same volume is reduced by 70 percent.
Example 3
In this example, CO is used2The biogas (methane content 60%) with the content of 38% is a purification object, and the decarbonization performance of the biogas is compared by a water washing tower and a micro-channel mixing device respectively, and the specific decarbonization treatment is carried out according to the following process conditions.
(1) The biogas is decarbonized by adopting a washing tower, and the height-diameter ratio of the washing tower is 9: 1, the volume is 300mL, the operating pressure of decarburization is 1.1Mpa, the inflow velocity is 160mL/min, the inflow velocity is 40mL/min, and the gas-water ratio is 4:1, continuously treating 30L of methane at the decarbonization temperature of 10 ℃.
(2) The biogas adopts a heart-shaped micro-channel mixer (the width (W) of the characteristic dimension of the cross section of a micro-channel is 60 μm, the height (H) is 60 μm, and the volume of the device is 5cm3) Decarbonizing with inlet gas flow rate of 160mL/min and inlet water flowThe speed is 6.4mL/min, the gas-water ratio is 25: 1, the other conditions are the same as in (1).
In this example, the same gas-water separation column (height to diameter ratio 10:1, volume 300mL, separation temperature 10 ℃ C.), regeneration column (height to diameter ratio 10:1, volume 300mL, regeneration temperature 40 ℃ C.) and blowing column (height to diameter ratio 4:1, volume 200mL) were used for both decarburization methods, and the operation processes were the same. The results are shown in Table 3.
TABLE 3
| Decarbonization device | Water washing tower | Microchannel mixer |
| Average CO in biomethane gas2Content (%) | 2.2 | 0.7 |
| Methane loss rate (%) | 1.33 | 0.26 |
| CO2Removal Rate (%) | 96.57 | 98.9 |
It can be seen that the micro-channel mixer is adopted, and CO in the marsh gas2The removal rate is improved from 96.57 percent to 98.9 percent, and the average CO in the biogas2The content is less than or equal to 1 percent, the quality requirement of the second class gas in natural gas (GB17820-2012) is met, the loss rate of methane is less than or equal to 1 percent, and the water consumption required for treating the methane with the same volume is reduced84％。
Example 4
In this example, CO is used2Biogas (methane content 55%) with content of 43% is a purification object, and the decarbonization performance of the biogas is compared by a water washing tower and a micro-channel mixing device respectively, and the specific decarbonization treatment is carried out according to the following process conditions.
(1) The biogas is decarbonized by adopting a washing tower, and the height-diameter ratio of the washing tower is 8:1, the volume is 200mL, the operating pressure of decarburization is 0.8Mpa, the inflow velocity is 150mL/min, the inflow velocity is 30mL/min, and the gas-water ratio is 5:1, continuously treating 15L of methane at the decarbonization temperature of 10 ℃.
(2) The biogas adopts a T-shaped micro-channel mixer (the width (W) of the characteristic dimension of the cross section of a micro-channel is 200 μm, the height (H) is 800 μm, and the volume of the device is 10cm3) Decarbonizing with inlet flow rate of 150mL/min, inlet flow rate of 5mL/min, gas-water ratio of 30:1, the other conditions are the same as in (1).
In this example, the same gas-water separation column (height to diameter ratio of 8:1, volume of 200mL, separation temperature of 10 ℃ C.), regeneration column (height to diameter ratio of 9: 1, volume of 200mL, regeneration temperature of 37 ℃ C.) and blowing column (height to diameter ratio of 4:1, volume of 200mL) were used in both decarburization processes, and the operation processes were the same. The results are shown in Table 4.
TABLE 4
| Decarbonization device | Water washing tower | Microchannel mixer |
| Average CO in biomethane gas2Content (%) | 2.0 | 1.5 |
| Methane loss rate (%) | 0.31 | 0.32 |
| CO2Removal Rate (%) | 97.45 | 98.09 |
It can be seen that the micro-channel mixer is adopted, and CO in the marsh gas2The removal rate is improved from 97.45 percent to 98.09 percent, and the average CO in the biogas2The content is less than or equal to 2 percent, the quality requirement of the second type of gas in natural gas (GB17820-2012) is met, the loss rate of methane is less than or equal to 0.5 percent, and the water consumption required for treating the methane with the same volume is reduced by 83.3 percent.
Example 5
In this example, CO is used2The biogas (methane content 65%) with the content of 30% is a purification object, and the decarbonization performance of the biogas is compared by a water washing tower and a micro-channel mixing device respectively, and the specific decarbonization treatment is carried out according to the following process conditions.
(1) The biogas is decarbonized by adopting a washing tower, and the height-diameter ratio of the washing tower is 10:1, the volume is 200mL, the operating pressure of decarburization is 1.0Mpa, the inflow velocity is 200mL/min, the inflow velocity is 50mL/min, and the gas-water ratio is 4:1, continuously treating 25L of methane at the decarbonization temperature of 15 ℃.
(2) The marsh gas adopts a column-type micro-channel mixer (the width (W) of the characteristic dimension of the cross section of a micro-channel is 100 mu m, the height (H) is 1000 mu m, and the volume of the device is 10cm3) Decarbonizing with inlet flow rate of 200mL/min, inlet flow rate of 10mL/min, gas-water ratio of 20:1, the other conditions are the same as in (1).
In this example, the same gas-water separation column (height to diameter ratio of 8:1, volume of 200mL, separation temperature of 15 ℃ C.), regeneration column (height to diameter ratio of 8:1, volume of 200mL, regeneration temperature of 40 ℃ C.) and blowing column (height to diameter ratio of 4:1, volume of 200mL) were used for both decarburization processes, and the operation processes were the same. The results are shown in Table 5.
TABLE 5
| Decarbonization device | Water washing tower | Microchannel mixer |
| Average CO in biomethane gas2Content (%) | 2.3 | 0.9 |
| Methane loss rate (%) | 0.65 | 0.22 |
| CO2Removal Rate (%) | 95.05 | 98.05 |
It can be seen that the micro-channel mixer is adopted, and CO in the marsh gas2The removal rate is improved from 97.45 percent to 98.09 percent, and the average CO in the biogas2The content is less than or equal to 2 percent, the quality requirement of the second type of gas in natural gas (GB17820-2012) is met, the loss rate of methane is less than or equal to 0.5 percent, and the water consumption required for treating the methane with the same volume is reduced by 83.3 percent.
The utility model provides an utilize microchannel mixing arrangement to carry out the thinking and the method of the device that pressurizes water absorption decarbonization to marsh gas, the method and the way that specifically realize this technical scheme are many, above only the preferred embodiment of the utility model should point out, to the ordinary skilled person in this technical field, do not deviate from the utility model discloses under the prerequisite of principle, can also make a plurality of improvements and moist decorations, these improvements should also be regarded as with moist decorations the utility model discloses a protection scope. All the components not specified in the present embodiment can be realized by the prior art.
Claims (6)
1. A device for pressurized water absorption decarburization of biogas by using a microchannel mixing device is characterized by comprising a microchannel mixer (1), a gas-water separation tower (2), a gas dehydrator (3), a pressure reducing valve (4), a first heat exchanger (5), a regeneration tower (6), a second heat exchanger (7), an air blowing tower (8) and a third heat exchanger (9);
wherein the micro-channel mixer (1) is provided with a methane feeding hole and a pressurized water feeding hole, a discharging hole of the micro-channel mixer (1) is connected with the gas-water separation tower (2), and a gas-water mixture obtained by mixing methane and pressurized water is introduced into the gas-water separation tower (2);
the top of the gas-water separation tower (2) is connected with an external methane gas storage tank through a gas discharge pipeline, and the gas dehydrator (3) is positioned on the gas discharge pipeline; the bottom of the gas-water separation tower (2) is connected with a first heat exchanger (5) through a drain pipe, and a pressure reducing valve (4) is positioned on the drain pipe;
the discharge hole of the first heat exchanger (5) is connected with the regeneration tower (6), and the absorbed water in the gas-water separation tower (2) is heated and then is led into the regeneration tower (6);
the top of the regeneration tower (6) is connected with external CO through a gas discharge pipeline2The bottom of the collecting tank is sequentially connected with the second heat exchanger (7) and the air-blowing tower (8) through a drain pipe, and the regenerated water in the regeneration tower (6) is cooled and then is sent into the air-blowing tower (8);
an air inlet is formed in the side face of the bottom of the air blowing tower (8), a waste gas exhaust port is formed in the side face of the top of the air blowing tower (8), and air is blown into the air blowing tower (8) to be contacted with regenerated water;
the bottom of the air-blowing tower (8) is connected with a third heat exchanger (9) through a drain pipe, and the regenerated water discharged from the air-blowing tower (8) is cooled to normal temperature and then recycled.
2. The apparatus of claim 1, wherein the microchannel mixer (1) is made of stainless steel, and has a microchannel structure of interdigital, T, Y, heart or column type, a cross-sectional width of the microchannel is 40-200 μm, and a height of 40-1000 μm.
3. The device according to claim 1, wherein the height-diameter ratio of the gas-water separation tower (2) is 8: 1-10: 1, and the gas-water mixture is introduced into the tower from the tower wall on the side surface of the top of the tower.
4. The device according to claim 1, wherein the gas dehydrator (3) is an adsorption dehydrator, and the adsorbent is any one of silica gel, alumina or molecular sieve.
5. The device according to claim 1, wherein the height-diameter ratio of the regeneration tower (6) is 8: 1-10: 1, and the absorption water is pumped into the tower from the side surface of the top of the tower and sprayed from top to bottom through the liquid distributor.
6. The device according to claim 1, wherein the height-diameter ratio of the air-blowing tower (8) is 4: 1-5: 1, and the regenerated water is pumped into the tower from the top of the tower and sprayed from top to bottom through the liquid distributor.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109852448A (en) * | 2019-04-01 | 2019-06-07 | 南京工业大学 | It is a kind of that the device and method that pressure (hydraulic) water absorbs decarburization being carried out to biogas using microchannel mixing arrangement |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109852448A (en) * | 2019-04-01 | 2019-06-07 | 南京工业大学 | It is a kind of that the device and method that pressure (hydraulic) water absorbs decarburization being carried out to biogas using microchannel mixing arrangement |
| CN109852448B (en) * | 2019-04-01 | 2024-03-26 | 南京工业大学 | Device and method for absorbing and decarbonizing biogas by pressurized water by utilizing micro-channel mixing device |
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