CN204294104U - A kind of CO that is carrier with anaerobic fermentation natural pond liquid 2absorption and storage utilize system - Google Patents
A kind of CO that is carrier with anaerobic fermentation natural pond liquid 2absorption and storage utilize system Download PDFInfo
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- CN204294104U CN204294104U CN201420750028.2U CN201420750028U CN204294104U CN 204294104 U CN204294104 U CN 204294104U CN 201420750028 U CN201420750028 U CN 201420750028U CN 204294104 U CN204294104 U CN 204294104U
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Abstract
The CO being carrier with anaerobic fermentation natural pond liquid designed by the utility model
2absorption and storage utilize system, comprise triplate line valve, rich carbon natural pond liquid delivery pump, rich carbon natural pond liquid mixing storage facilities, regenerate rich carbon natural pond liquid delivery pump, rich or poor heat exchanger, rich carbon natural pond liquid CO
2reclaim equiment, the fresh natural pond liquid storage facilities, natural pond liquid filter plant, natural pond liquid concentrator, natural pond liquid mixing apparatus, heater, the CO that are communicated with successively by pipeline
2absorption equipment.The low cost that the utility model produces with organic anaerobic fermentation, alkalescent and the natural pond liquid being rich in plant growth nutritional labeling is medium, by rich CO
2cO in gas
2absorption integrated with storage application, by CO
2transfer to plant part or soil and water-bearing layer from gaseous state, significantly reduce CO
2absorption and storage utilize cost, can realize the CO of low cost
2absorb and store and utilize.
Description
Technical field
The utility model relates to CO
2absorption and storage utilize technical field, are specifically related to a kind of CO being carrier with anaerobic fermentation natural pond liquid
2absorption and storage utilize system.
Background technology
Based on the rich CO of the low pressure such as the biogas of gas-liquid chemical principle, rubbish landfill gas, pyrolysis gas of biomass and coal-fired flue-gas
2cO in gas
2chemical absorbing technology be the main flow CO in above-mentioned field
2one of isolation technics, its maturation that possesses skills, business are applied extensively, to gas wide adaptability, simple to operate and CO
2separative efficiency is high, target gas purity is high (as the CO at biogas and rubbish landfill gas
2in, CH
4for target product) etc. advantage, be in the recent period can the technology of large-scale promotion application.But also there is CO in traditional chemical absorption techniques
2it is urgently to be resolved hurrily that separation costs crosses high critical bottleneck.CO
2separation costs is high main high owing to chemical absorption process system cloud gray model energy consumption, especially the rich CO of absorbent
2regeneration of waste liquor hear rate is huge.
For chemical absorption method CO
2separation costs is high, the especially rich CO of absorbent
2the difficult problem that regeneration of waste liquor energy consumption is high, current reply pattern mainly contains two kinds: (1) is at traditional C O
2on chemical absorption method Process ba-sis, utilize new and effective low energy consumption CO
2absorbent or to CO
2absorb and be optimized or innovate to reduce CO with regenerative process
2hot recycling energy consumption in separation process.In New Absorbent, apply as adopted the New Absorbent such as ammoniacal liquor, N methyldiethanol amine and piperazine composite absorber to substitute traditional ethanol amine (MEA) absorbent, thus expect to obtain high CO
2the double dominant of absorption rate and low regeneration energy consumption.At CO
2optimization of the CCRs aspect, controls absorbent solution at CO as adopted cold (inter-cooling) technology in absorption tower
2temperature rise in absorption process, by improving the CO of absorbent
2absorbability reaches the object reducing absorbent flow and then reduce regeneration energy consumption.At CO
2regenerative process optimization aspect, as adopted novel film decompression regeneration technology to substitute conventional tower regenerative process, organically combining the membrane material technology of high-specific surface area and decompression regeneration techniques, thus reaching the object reducing regeneration temperature and utilize low grade heat energy.But this kind of pattern is still based on traditional C O
2chemical absorption process, remains the rich CO of highly energy-consuming
2the hot recycling process of absorbent solution, even if adopt new absorbent, its regenerative process is also still limited by the restriction of the aspect such as kinetics and thermodynamics, and the regeneration energy consumption range of decrease is limited, is difficult to reach the target significantly reducing regeneration energy consumption.Meanwhile, the optimization of absorption or regenerative process may increase the complexity of process system, thus increases the operation easier of system, but also can increase the overall investment of system.(2) CO that do not recycle of absorbent
2absorb, utilize and storage integrated pattern.This kind of pattern has abandoned the rich CO that in traditional chemical absorption process, energy consumption is the highest
2the regenerative process of solution, does not recycle absorbent, but directly by CO
2absorb and high value added product production integration, by CO
2convert the chemical products compared with high added value to.This kind of pattern has given up CO
2regenerative process, thus without the need to consuming high temperature regeneration steam, system energy consumption significantly reduces, and effectively can reduce CO
2separation costs, the sale of the high value added product simultaneously obtained also can subsidize CO
2separation costs.Under this kind of pattern, most typical is be that absorbent absorbs CO with ammoniacal liquor
2generate carbonic hydroammonium technique.But this technique relies on the chemical absorbent such as ammoniacal liquor, needs to utilize in a large number the commercialization chemical products such as ammoniacal liquor, large-scale application may cause chemical products seriously supply falls short of demand, the demand of the fertilizer such as carbonic hydroammonium is also limited simultaneously.Therefore, the application scale of this kind of pattern is limited, can only use among a small circle.
In general, for traditional C O
2the key issue that chemical absorption method technique exists, the CO that absorbent does not recycle
2absorption, utilization and storage integrated pattern have low CO
2separation costs advantage, highly pays close attention to, but it needs the key issue solved to be the low cost of development of new and reproducible CO
2absorbent carrys out alternative traditional business chemical industry absorbent and applies, and also needs to expand rich CO simultaneously
2the range of application of absorbent, thus reach CO that is extensive, low cost
2utilize and store.And at CO
2storage aspect, except the storing mode such as geology and ocean, the solid carbon of soil and plant also should merit attention.Soil converges ground as maximum carbon source and carbon, if the CO that can be separated
2effectively be stored in soil, effectively will expand CO
2storage channel, realize CO
2large scale storage.Equally, if can by CO
2effectively be stored in plant part, also significantly will expand CO
2application approach, reduce CO
2store the risk utilized.
Therefore, needing exploitation a kind of is the CO of carrier with " low cost, hypotoxicity and renewable " absorbent
2absorption and storage utilize integral process system, reduce CO to reach
2separation costs and CO
2the object of regeneration energy consumption, and its by Regeneratable absorbent by CO
2after absorbing, by isolated CO
2transfer in soil and plant body, thus realize CO
2extensive utilization and storage.
Summary of the invention
The purpose of this utility model is exactly to provide a kind of CO being carrier with anaerobic fermentation natural pond liquid
2absorption and storage utilize system, and this system significantly can reduce CO
2separation costs and CO
2regeneration energy consumption, expand CO simultaneously
2storage utilization orientation.
For realizing this object, the CO that a kind of designed by the utility model is carrier with anaerobic fermentation natural pond liquid
2absorption and storage utilize system, comprise triplate line valve, rich carbon natural pond liquid delivery pump, rich carbon natural pond liquid mixing storage facilities, regenerate rich carbon natural pond liquid delivery pump, rich or poor heat exchanger, rich carbon natural pond liquid CO
2reclaim equiment, the fresh natural pond liquid storage facilities, natural pond liquid filter plant, natural pond liquid concentrator, natural pond liquid mixing apparatus, heater, the CO that are communicated with successively by pipeline
2absorption equipment; First port of described triplate line valve connects CO
2the mixed liquor delivery outlet of absorption equipment, second port of triplate line valve connects the rich carbon natural pond liquid inlet of rich carbon natural pond liquid mixing storage facilities, the dilute phase leakage fluid dram of connection natural pond, the dilute phase input port liquid concentrator of rich carbon natural pond liquid mixing storage facilities by rich carbon natural pond liquid delivery pump; 3rd port of described triplate line valve connects the cry-fluid inlet of rich or poor heat exchanger, the cryogenic fluid outlet of rich or poor heat exchanger and rich carbon natural pond liquid CO by regeneration rich carbon natural pond liquid delivery pump
2the regeneration rich carbon natural pond liquid inlet of reclaim equiment is connected by pipeline; Rich carbon natural pond liquid CO
2the poor carbon natural pond liquid leakage fluid dram of reclaim equiment is connected by pipeline with the high temperature fluid entrance of rich or poor heat exchanger, and the high temperature fluid outlet of rich or poor heat exchanger is communicated with the liquid input port, poor carbon natural pond of described natural pond liquid mixing apparatus by poor carbon natural pond liquid delivery pump; Pipeline between second port of described triplate line valve and rich carbon natural pond liquid delivery pump is provided with flowmeter; Pipeline between the liquid input port, poor carbon natural pond of described natural pond liquid mixing apparatus and poor carbon natural pond liquid delivery pump is provided with flowmeter and concentration sensor; Described natural pond liquid mixing apparatus has outer source additive inlet; Described CO
2absorption equipment has rich CO
2gas inlet and mixed solution inlet opening, described rich CO
2gas inlet is positioned at CO
2the bottom of absorption equipment, mixed solution inlet opening is positioned at CO
2the top of absorption equipment, described natural pond liquid mixing apparatus connects CO by heater
2the mixed solution inlet opening of absorption equipment; Described rich carbon natural pond liquid mixing storage facilities has rich carbon natural pond liquid leakage fluid dram; Described rich carbon natural pond liquid CO
2the bottom of reclaim equiment has air inlet, described rich carbon natural pond liquid CO
2the top of reclaim equiment has regeneration gas exhaust outlet.
In technique scheme, described rich carbon natural pond liquid CO
2reclaim equiment inner bottom part is provided with heating element heater, described rich carbon natural pond liquid CO
2the air inlet of reclaim equiment is connected with air pump by heater.Described rich carbon natural pond liquid CO
2the regeneration gas exhaust outlet of reclaim equiment is connected by pipeline with condensing unit.
In technique scheme, be communicated with by natural pond liquid delivery pump between described fresh natural pond liquid storage facilities and natural pond liquid filter plant, be communicated with by natural pond liquid delivery pump between natural pond liquid filter plant and natural pond liquid concentrator, be communicated with by natural pond liquid delivery pump between natural pond liquid concentrator and natural pond liquid mixing apparatus; Described natural pond liquid filter plant has sludge outlet; Described CO
2absorption equipment has purified gas exhaust outlet.
In technique scheme, the pipeline between described natural pond liquid filter plant and natural pond liquid concentrator is provided with liquid flow controller and flowmeter; Pipeline between the dilute phase leakage fluid dram of described natural pond liquid concentrator and the dilute phase input port of rich carbon natural pond liquid mixing storage facilities is provided with flowmeter.
In technique scheme, the pipeline between described fresh natural pond liquid storage facilities and natural pond liquid filter plant is provided with flowmeter and temperature sensor; Pipeline between described natural pond liquid filter plant and natural pond liquid concentrator is provided with temperature sensor; Pipeline between described natural pond liquid concentrator and natural pond liquid mixing apparatus is provided with flowmeter and temperature sensor; First port of described triplate line valve and CO
2pipeline between the mixed liquor delivery outlet of absorption equipment is provided with flowmeter and temperature sensor; Described rich or poor heat exchanger high temperature fluid entrance and rich carbon natural pond liquid CO
2pipeline between the poor carbon natural pond liquid leakage fluid dram of reclaim equiment is provided with flowmeter and temperature sensor; Described natural pond liquid mixing apparatus and CO
2pipeline between absorption equipment is provided with concentration sensor; Described rich or poor heat exchanger cryogenic fluid outlet and rich carbon natural pond liquid CO
2pipeline between the regeneration rich carbon natural pond liquid inlet of reclaim equiment is provided with flowmeter.
In technique scheme, in the liquid concentrator of described natural pond, be provided with rolling NF membrane.
Following beneficial effect can be brought after utilizing structure of the present utility model:
1, the low cost, the alkalescent and the natural pond liquid being rich in plant growth nutritional labeling is medium, by rich CO that produce with organic anaerobic fermentation of the utility model
2cO in gas
2absorption integrated with storage application, by CO
2transfer to plant part or soil and water-bearing layer from gaseous state, significantly reduce CO
2absorption and storage utilize cost, can realize the CO of low cost
2absorb and store and utilize.
2, in the utility model, the Agroforestry ecosystem of rich carbon natural pond liquid utilizes and can also improve soil quality, increases the yield of biomass of agriculture and forestry plant, reaches and from air, absorb CO further
2object.
3, in the utility model, when being handling object with biogas, rubbish landfill gas and pyrolysis gas of biomass etc., the utility model not only can improve the calorific value of gas, produces the recyclable organism methane or bio-natural gas that have a extensive future, also can by CO
2transfer in plant part or soil, realize CO
2clean negative emission, achieve many things at one stroke.
4, in the utility model, hypotoxicity, high reaction rate and based on the outer source additive generating bicarbonate radical, the CO of natural pond liquid can be improved in the liquid mixing apparatus of natural pond, is selected
2absorbability, to ensure in natural pond liquid that original plant growth promoting enters component content constant.Meanwhile, by the parameter such as additive concentration and reaction temperature, ensure that natural pond liquid has lower plant physiology toxicity, reach the high CO of natural pond liquid
2absorbability and low physiological-toxicity double goal.Simultaneously with the existing CO being absorbent with commercialization chemical products such as ammoniacal liquor
2absorb and compare with high value added product production integration technique, employing amount is large, cheap, toxicity is low and be rich in plant growth and promote that the natural pond liquid of the beneficiating ingredient such as hormone, amino acid and vitamin is as absorbent main body, has effectively evaded in traditional handicraft the difficult problem that chemical products consume in a large number.
5, in the utility model, a small amount of rich carbon natural pond liquid is used for regeneration, thus reduces the use amount of outer source additive.Meanwhile, CO can also be produced in regeneration
2the fertile byproduct of gas, can be used for the gas fertilising of warmhouse booth.
6, in the utility model, the natural pond slag after natural pond liquid filters can as Solid nutritional raw material, and adopting nanofiltration to concentrate can improve nutrient concentrations, reduces natural pond liquid reservoir volume, reduces conveying cost.
7, the utility model is due to temperature required lower in regenerative process, thus effectively can utilize waste heat or other low-grade energies.
Accompanying drawing explanation
Fig. 1 is a kind of CO that is carrier with anaerobic fermentation natural pond liquid of the utility model
2absorb and store the structure and the schematic flow sheet that utilize system.
Wherein, 1-natural pond liquid storage facilities, 2-natural pond liquid filter plant, 2.1-sludge outlet, 3-natural pond liquid concentrator, 3.1-dilute phase leakage fluid dram, 4-natural pond liquid mixing apparatus, 4.1-outer source additive inlet, liquid input port, 4.2-poor carbon natural pond, 5-heater, 6-CO
2absorption equipment, 6.1-rich CO
2gas inlet, 6.2-purified gas exhaust outlet, 6.3-mixed solution inlet opening, 6.4-mixed liquor delivery outlet, 7-rich carbon natural pond liquid delivery pump, 8-rich carbon natural pond liquid mixing storage facilities, 8.1-rich carbon natural pond liquid leakage fluid dram, 8.2-dilute phase input port, 8.3-rich carbon natural pond liquid inlet mouth, 9-regenerate rich carbon natural pond liquid delivery pump, 10-rich or poor heat exchanger, 10.1-cry-fluid inlet, 10.2-cryogenic fluid outlet, 10.3-high temperature fluid entrance, 10.4-high temperature fluid exports, 11-rich carbon natural pond liquid CO
2reclaim equiment, 11.1-regenerate rich carbon natural pond liquid inlet, 11.2-poor carbon natural pond liquid leakage fluid dram, 11.3-air inlet, 11.4-regeneration gas exhaust outlet, 12-air pump, 13-poor carbon natural pond liquid pump, 14-flowmeter, 15-temperature sensor, 16-concentration of absorbing sensor, 17-liquid flow controller, 18-heating element heater, 19-condensing unit, 20-natural pond liquid delivery pump, 21.1-triplate line valve, 21.2-the first port, 21.3-the second port, 21-the three port
Detailed description of the invention
Below in conjunction with the drawings and specific embodiments, the utility model is described in further detail:
The CO being carrier with anaerobic fermentation natural pond liquid as shown in Figure 1
2absorption and storage utilize system, comprise triplate line valve 21, rich carbon natural pond liquid delivery pump 7, rich carbon natural pond liquid mixing storage facilities 8, regenerate rich carbon natural pond liquid delivery pump 9, rich or poor heat exchanger 10, rich carbon natural pond liquid CO
2reclaim equiment 11, the fresh natural pond liquid storage facilities 1, natural pond liquid filter plant 2, natural pond liquid concentrator 3, natural pond liquid mixing apparatus 4, heater 5, the CO that are communicated with successively by pipeline
2absorption equipment 6; First port 21.1 of described triplate line valve 21 connects CO
2the mixed liquor delivery outlet 6.4 of absorption equipment 6, second port 21.2 of triplate line valve 21 connects the rich carbon natural pond liquid inlet 8.3 of rich carbon natural pond liquid mixing storage facilities 8 by rich carbon natural pond liquid delivery pump 7, the dilute phase input port 8.2 of rich carbon natural pond liquid mixing storage facilities 8 connects the dilute phase leakage fluid dram 3.1 of natural pond liquid concentrator 3; 3rd port 21.3 of described triplate line valve 21 connects the cry-fluid inlet 10.1 of rich or poor heat exchanger 10, cryogenic fluid outlet 10.2 and the rich carbon natural pond liquid CO of rich or poor heat exchanger 10 by regeneration rich carbon natural pond liquid delivery pump 9
2the regeneration rich carbon natural pond liquid inlet 11.1 of reclaim equiment 11 is connected by pipeline; Rich carbon natural pond liquid CO
2the poor carbon natural pond liquid leakage fluid dram 11.2 of reclaim equiment 11 is connected by pipeline with the high temperature fluid entrance 10.3 of rich or poor heat exchanger 10, and the high temperature fluid outlet 10.4 of rich or poor heat exchanger 10 is communicated with the liquid input port, poor carbon natural pond 4.2 of described natural pond liquid mixing apparatus 4 by poor carbon natural pond liquid delivery pump 13; Pipeline between second port 21.2 of described triplate line valve 21 and rich carbon natural pond liquid delivery pump 7 is provided with flowmeter 14; Pipeline between the liquid input port, poor carbon natural pond 4.2 of described natural pond liquid mixing apparatus 4 and poor carbon natural pond liquid delivery pump 13 is provided with flowmeter 14 and concentration sensor 16; Described natural pond liquid mixing apparatus 4 has outer source additive inlet 4.1; Described CO
2absorption equipment 6 has rich CO
2gas inlet 6.1 and mixed solution inlet opening 6.3, described rich CO
2gas inlet 6.1 is positioned at CO
2the bottom of absorption equipment 6, mixed solution inlet opening 6.3 is positioned at CO
2the top of absorption equipment 6, described natural pond liquid mixing apparatus 4 connects CO by heater 5
2the mixed solution inlet opening 6.3 of absorption equipment 6; Described rich carbon natural pond liquid mixing storage facilities 8 has rich carbon natural pond liquid leakage fluid dram 8.1; Described rich carbon natural pond liquid CO
2the bottom of reclaim equiment 11 has air inlet 11.3, described rich carbon natural pond liquid CO
2the top of reclaim equiment 11 has regeneration gas exhaust outlet 11.4.
In technique scheme, described rich carbon natural pond liquid CO
2heating element heater 18 is provided with, described rich carbon natural pond liquid CO in reclaim equiment 11
2the air inlet 11.3 of reclaim equiment 11 is connected with air pump 12 by heater 5, described rich carbon natural pond liquid CO
2the regeneration gas exhaust outlet 11.4 of reclaim equiment 11 is connected by pipeline with condensing unit 19; Pipeline between described natural pond liquid filter plant 2 and natural pond liquid concentrator 3 is provided with liquid flow controller 17 and flowmeter 14; Pipeline between the dilute phase leakage fluid dram 3.1 of described natural pond liquid concentrator 3 and the dilute phase input port 8.2 of rich carbon natural pond liquid mixing storage facilities 8 is provided with flowmeter 14; Rolling NF membrane is provided with in described natural pond liquid concentrator 3; Described natural pond liquid filter plant 2 has sludge outlet 2.1; Described CO
2absorption equipment 6 has purified gas exhaust outlet 6.2.
In technique scheme, be communicated with by natural pond liquid delivery pump 20 between described fresh natural pond liquid storage facilities 1 and natural pond liquid filter plant 2, be communicated with by natural pond liquid delivery pump 20 between natural pond liquid filter plant 2 and natural pond liquid concentrator 3, be communicated with by natural pond liquid delivery pump 20 between natural pond liquid concentrator 3 and natural pond liquid mixing apparatus 4; Pipeline between described fresh natural pond liquid storage facilities 1 and natural pond liquid filter plant 2 is provided with flowmeter 14 and temperature sensor 15; Pipeline between described natural pond liquid filter plant 2 and natural pond liquid concentrator 3 is provided with temperature sensor 15; Pipeline between described natural pond liquid concentrator 3 and natural pond liquid mixing apparatus 4 is provided with flowmeter 14 and temperature sensor 15; First port 21.1 and CO of described triplate line valve 21
2pipeline between the mixed liquor delivery outlet 6.4 of absorption equipment 6 is provided with flowmeter 14 and temperature sensor 15; Described rich or poor heat exchanger 10 high temperature fluid entrance 10.3 and rich carbon natural pond liquid CO
2pipeline between the poor carbon natural pond liquid leakage fluid dram 11.2 of reclaim equiment 11 is provided with flowmeter 14 and temperature sensor 15; Described natural pond liquid mixing apparatus 4 and CO
2pipeline between absorption equipment 6 is provided with concentration sensor 16; Described rich or poor heat exchanger 10 cryogenic fluid outlet 10.2 and rich carbon natural pond liquid CO
2pipeline between the regeneration rich carbon natural pond liquid inlet 11.1 of reclaim equiment 11 is provided with flowmeter 14.
A kind ofly utilize the above-mentioned CO being carrier with anaerobic fermentation natural pond liquid
2absorb and store the CO being carrier with anaerobic fermentation natural pond liquid utilizing system
2absorb and store the method utilized, in the method, fresh natural pond liquid is mixed to form with the poor carbon natural pond liquid of outer source additive and backflow and mixes natural pond liquid, the rich CO such as biogas, rubbish landfill gas, pyrolysis gas of biomass or flue gas after storing, filter and be concentrated
2cO in gas
2absorb at absorption stage mixed natural pond liquid and form rich carbon natural pond liquid.In the larger situation of natural pond liquid demand, major part rich carbon natural pond liquid directly enters the liquid mixing of rich carbon natural pond and storage facilities, then after dilution, be directly used in Agroforestry ecosystem application, for the pouring of farm-forestry crop or plant, promote the growth of crop or plant, thus the CO that will carry
2be stored in crop or plant part and soil and water-bearing layer.When natural pond liquid demand is less, most of rich carbon natural pond liquid enters CO after caning be passed through poor rich liquid heat exchanger heating
2in reclaim equiment, through heating up and air purging assisted Regeneration, by the CO carried in the liquid of rich carbon natural pond
2regeneration, thus form poor carbon natural pond liquid, poor carbon natural pond liquid is delivered in the liquid mixing apparatus of natural pond after being lowered the temperature by poor rich liquid heat exchanger and recycles.And the CO born again
2cO in/air gas mixture
2volume fraction is controlled in about 0.08% ~ 0.1%, directly can be used for the gas fertilising application of warmhouse booth.
The utility model comprises the steps: specifically
Step 1: fresh natural pond liquid is stored in fresh natural pond liquid storage facilities 1, airtight standing storage forms natural pond liquid supernatant;
Step 2: the liquid supernatant of natural pond described in step 1 draw from fresh natural pond liquid storage facilities 1 and enter in natural pond liquid filter plant 2 carry out successively coarse filtration and essence filter, progressively remove the suspended particulate substance that in the liquid of natural pond, diameter is greater than 5 μm, suspended particulate substance is discharged by sludge outlet 2.1, filtrate after essence filter enters natural pond liquid concentrator 3 and carries out concentrated formation natural pond concentrated liquor, and the water then in natural pond liquid concentrator 3 in the concentrated liquor of rolling nanofiltration membrane natural pond and small-molecule substance form dilute phase and natural pond liquid concentrates phase;
Step 3: described natural pond liquid concentrator 3 is transported in natural pond liquid mixing apparatus 4 by concentrated for natural pond liquid mutually, and outer source additive is added in natural pond liquid mixing apparatus 4, outer source additive and natural pond liquid are concentrated mix mutually, form mixed liquor, the described external source additive concentration added controls within the scope of 0.5 ~ 1.25mol/L, and the mixed liquor that described natural pond liquid mixing apparatus 4 exports enters CO after heater 5 heat temperature raising
2in absorption equipment 6, meanwhile, by CO to be separated
2rich CO
2gas is by rich CO
2gas inlet 6.1 is input to CO
2form reverse flow with described mixed liquor in absorption equipment 6, described mixed liquor absorbs CO
2rear formation rich carbon natural pond liquid, rich CO
2gas is absorbed rear remaining gas from CO
2the purified gas exhaust outlet 6.2 of absorption equipment 6 is discharged;
Step 4: the liquid of rich carbon natural pond described in step 3 enters in rich carbon natural pond liquid mixing storage facilities 8 through the second port 21.2 shunting of triplate line valve 21, pass through the range of flow of the described rich carbon natural pond liquid of shunting between 70% ~ 90%, the flow of the described rich carbon natural pond liquid of this shunting is monitored by the flowmeter 14 between the second port 21.2 of triplate line valve 21 and rich carbon natural pond liquid delivery pump 7, and by triplate line valve 21 regulable control, dilute phase described in step 2 is exported by the dilute phase leakage fluid dram 3.1 of natural pond liquid concentrator 3 and enters rich carbon natural pond liquid mixing storage facilities 8 by dilute phase input port 8.2, described dilute phase and add in rich carbon natural pond liquid mixing storage facilities 8 moisture content jointly dilute from rich carbon natural pond liquid leakage fluid dram 8.1 discharge described rich carbon natural pond liquid, rich carbon natural pond liquid dilution is formed after diluting 5 ~ 10 times, described rich carbon natural pond liquid dilution directly or after storing utilizes for Agro-ecology, plant or plant growth and soil solidification is supplied to store,
Step 5: in step 3, remaining described rich carbon natural pond liquid exports through the 3rd port 21.3 of triplate line valve 21, entering from rich or poor heat exchanger 10 cry-fluid inlet 10.1 by regenerating rich carbon natural pond liquid pump 9, carrying out entering rich carbon natural pond liquid CO after heat exchange is warming up to 60 ~ 80 DEG C
2in reclaim equiment 11, air is transported to heater 5 by air pump 12, heater 5 pairs of air heat, and the air after heating is from rich carbon natural pond liquid CO
2the air inlet 11.3 of reclaim equiment 11 enters rich carbon natural pond liquid CO
2described rich carbon natural pond liquid is carried out purging regeneration by reclaim equiment 11, regenerates CO
2gas, and remaining poor carbon natural pond liquid;
Step 6: described rich carbon natural pond liquid CO
2poor carbon natural pond liquid exports by reclaim equiment 11, and enter rich or poor heat exchanger 10 by high temperature fluid entrance 10.3, enter after poor carbon natural pond liquid carries out heat exchange cooling in rich or poor heat exchanger 10 in natural pond liquid mixing apparatus 4 and be mixed to form absorbing liquid with the concentrated phase of described natural pond liquid and described outer source additive, this absorbing liquid recycles according to the processing mode of mixed liquor in step 3, by the flow of poor carbon natural pond liquid described in the flowmeter 14 between liquid input port, poor carbon natural pond 4.2 and poor carbon natural pond liquid delivery pump 13 and concentration sensor 16 monitoring step 5, described natural pond liquid mixing apparatus 4 and CO
2the flow of mixed liquor described in flowmeter 14 between absorption equipment 6 and concentration sensor 16 monitoring step 3, adjust according to mixed liquor flow described in the flow of described poor carbon natural pond liquid and step 3 concentration needing the outer source additive added, make external source additive concentration scope in the new mixed liquor of formation in 0.5 ~ 1.25mol/L.
Above-mentioned in steps in, outer source additive is mainly with higher CO
2reactivity, hypotoxicity and based on the CO generating bicarbonate ion
2absorbent is main, as single or composite absorbers such as potassium hydroxide, ammoniacal liquor, amino-acid salts.
In the step 1 of technique scheme, described fresh natural pond liquid is that the natural pond liquid produced by producing methane through anaerobic fermentation engineering at 35 ~ 37 DEG C is detained and is formed for 20 days.
In the step 1 of technique scheme, the airtight standing storage 15 ~ 17 days under 35 ~ 37 DEG C of conditions of fresh natural pond liquid.
In the step 2 of technique scheme, the cycles of concentration of natural pond liquid is obtained by the flow proportional of the liquid flow controller 17 at liquid concentrator 3 inlet place, natural pond and the dilute phase flowmeter 14 of concentrator delivery outlet, and natural pond liquid cycles of concentration is controlled at 1.25 ~ 5 times, namely according to described natural pond liquid supernatant flow before concentrated and concentrated after ratio between described dilute phase flow be that 5:1 ~ 5:4 carries out concentrated control.
In the step 3 of technique scheme, for CO
2the mixing natural pond liquid absorbed is by concentrating natural pond liquid, external source absorbent, backflow lean solution mixed preparing, control by the flowmeter 14 that is provided with between the inlet 4.3 of mixing apparatus 4 and lean pump 13 and concentration of absorbing sensor 16, detect fertile absorber content in lean solution, liquid China and foreign countries, natural pond source additive concentration is controlled by regulating absorbent addition, and natural pond liquid concentrating degree is larger, addition is higher, thus the external source additive concentration in the liquid of mixing natural pond is controlled within the scope of the liquid of 0.5 ~ 1.25mol/L natural pond.
In the step 4 of technique scheme, whether described rich carbon natural pond liquid dilution stores and the storage time adjusts according to the demand of reality rich carbon natural pond liquid dilution, and the maximum storage time of described rich carbon natural pond liquid dilution is 7 days; Described rich carbon natural pond liquid can stored on-site and utilization, also can be transported to and to store after utilizing ground again and to dilute rear utilization.
In the step 3 of technique scheme, the mixed liquor that described natural pond liquid mixing apparatus 4 exports is heated to 35 ~ 50 DEG C through heater 5; In described step 5, regulate rich carbon natural pond liquid CO by heating element heater 18
2the regenerative environ-ment of reclaim equiment 11, makes regeneration temperature maintain 60 ~ 80 DEG C, and natural pond liquid cycles of concentration is higher, and regeneration temperature is higher; The CO that the flow of described air pump 12 is born by regeneration gas exhaust outlet 11.4 again
2cO in gas
2volume fraction and above-mentioned regeneration temperature are determined jointly, ensure the CO born again
2cO in gas
2volume fraction is 0.08% ~ 0.10%.
In the step 3 of technique scheme, CO to be separated
2gas can be biogas, rubbish landfill gas, pyrolysis gas of biomass or flue gas.
In the step 5 of technique scheme, describedly regenerate CO
2gas is by rich carbon natural pond liquid CO
2the regeneration gas exhaust outlet 11.4 of reclaim equiment 11 enters in condensing unit 19, through the CO of condensed gas as warmhouse booth
2gas fertilizer utilizes.
In technique scheme, all pipelines all wrap up insulation material, to reduce natural pond liquid and initial rich solution at the operating thermal loss of pipeline.
In technique scheme, the critical component of natural pond liquid concentrator 4 is rolling NF membrane, adopts cross-flow filtration mode.
Claims (6)
1. the CO that is carrier with anaerobic fermentation natural pond liquid
2absorption and storage utilize system, it is characterized in that: comprise triplate line valve (21), rich carbon natural pond liquid delivery pump (7), rich carbon natural pond liquid mixing storage facilities (8), regenerate rich carbon natural pond liquid delivery pump (9), rich or poor heat exchanger (10), rich carbon natural pond liquid CO
2reclaim equiment (11), fresh natural pond liquid storage facilities (1) be communicated with successively by pipeline, natural pond liquid filter plant (2), natural pond liquid concentrator (3), natural pond liquid mixing apparatus (4), heater (5), CO
2absorption equipment (6); First port (21.1) of described triplate line valve (21) connects CO
2the mixed liquor delivery outlet (6.4) of absorption equipment (6), second port (21.2) of triplate line valve (21) connects rich carbon natural pond liquid inlet (8.3) of rich carbon natural pond liquid mixing storage facilities (8) by rich carbon natural pond liquid delivery pump (7), the dilute phase input port (8.2) of rich carbon natural pond liquid mixing storage facilities (8) connects the dilute phase leakage fluid dram (3.1) in natural pond liquid concentrator (3); 3rd port (21.3) of described triplate line valve (21) connects the cry-fluid inlet (10.1) of rich or poor heat exchanger (10), cryogenic fluid outlet (10.2) and the rich carbon natural pond liquid CO of rich or poor heat exchanger (10) by rich carbon natural pond liquid delivery pump (9) of regeneration
2rich carbon natural pond liquid inlet (11.1) of regeneration of reclaim equiment (11) is connected by pipeline; Rich carbon natural pond liquid CO
2poor carbon natural pond liquid leakage fluid dram (11.2) of reclaim equiment (11) is connected by pipeline with the high temperature fluid entrance (10.3) of rich or poor heat exchanger (10), and high temperature fluid outlet (10.4) of rich or poor heat exchanger (10) is communicated with liquid input port, the poor carbon natural pond (4.2) of described natural pond liquid mixing apparatus (4) by poor carbon natural pond liquid delivery pump (13); Pipeline between second port (21.2) of described triplate line valve (21) and rich carbon natural pond liquid delivery pump (7) is provided with flowmeter (14); Pipeline between liquid input port, the poor carbon natural pond (4.2) of described natural pond liquid mixing apparatus (4) and poor carbon natural pond liquid delivery pump (13) is provided with flowmeter (14) and concentration sensor (16); Described natural pond liquid mixing apparatus (4) has outer source additive inlet (4.1); Described CO
2absorption equipment (6) has rich CO
2gas inlet (6.1) and mixed solution inlet opening (6.3), described rich CO
2gas inlet (6.1) is positioned at CO
2the bottom of absorption equipment (6), mixed solution inlet opening (6.3) is positioned at CO
2the top of absorption equipment (6), described natural pond liquid mixing apparatus (4) connects CO by heater (5)
2the mixed solution inlet opening (6.3) of absorption equipment (6); Described rich carbon natural pond liquid mixing storage facilities (8) has rich carbon natural pond liquid leakage fluid dram (8.1); Described rich carbon natural pond liquid CO
2the bottom of reclaim equiment (11) has air inlet (11.3), described rich carbon natural pond liquid CO
2the top of reclaim equiment (11) has regeneration gas exhaust outlet (11.4).
2. a kind of CO that is carrier with anaerobic fermentation natural pond liquid according to claim 1
2absorption and storage utilize system, it is characterized in that: described rich carbon natural pond liquid CO
2reclaim equiment (11) inner bottom part is provided with heating element heater (18), described rich carbon natural pond liquid CO
2the air inlet (11.3) of reclaim equiment (11) is connected with air pump (12) by heater (5), described rich carbon natural pond liquid CO
2the regeneration gas exhaust outlet (11.4) of reclaim equiment (11) is connected by pipeline with condensing unit (19).
3. a kind of CO that is carrier with anaerobic fermentation natural pond liquid according to claim 1
2absorption and storage utilize system, it is characterized in that: be communicated with by natural pond liquid delivery pump (20) between described fresh natural pond liquid storage facilities (1) and natural pond liquid filter plant (2), be communicated with by natural pond liquid delivery pump (20) between natural pond liquid filter plant (2) and natural pond liquid concentrator (3), be communicated with by natural pond liquid delivery pump (20) between natural pond liquid concentrator (3) and natural pond liquid mixing apparatus (4); Described natural pond liquid filter plant (2) has sludge outlet (2.1); Described CO
2absorption equipment (6) has purified gas exhaust outlet (6.2).
4. a kind of CO that is carrier with anaerobic fermentation natural pond liquid according to claim 1
2absorption and storage utilize system, it is characterized in that: the pipeline between described natural pond liquid filter plant (2) and natural pond liquid concentrator (3) is provided with liquid flow controller (17) and flowmeter (14); Pipeline between the dilute phase leakage fluid dram (3.1) of described natural pond liquid concentrator (3) and the dilute phase input port (8.2) of rich carbon natural pond liquid mixing storage facilities (8) is provided with flowmeter (14).
5. a kind of CO that is carrier with anaerobic fermentation natural pond liquid according to claim 1
2absorption and storage utilize system, it is characterized in that: the pipeline between described fresh natural pond liquid storage facilities (1) and natural pond liquid filter plant (2) is provided with flowmeter (14) and temperature sensor (15); Pipeline between described natural pond liquid filter plant (2) and natural pond liquid concentrator (3) is provided with temperature sensor (15); Pipeline between described natural pond liquid concentrator (3) and natural pond liquid mixing apparatus (4) is provided with flowmeter (14) and temperature sensor (15); First port (21.1) of described triplate line valve (21) and CO
2pipeline between the mixed liquor delivery outlet (6.4) of absorption equipment (6) is provided with flowmeter (14) and temperature sensor (15); Described rich or poor heat exchanger (10) high temperature fluid entrance (10.3) and rich carbon natural pond liquid CO
2pipeline between poor carbon natural pond liquid leakage fluid dram (11.2) of reclaim equiment (11) is provided with flowmeter (14) and temperature sensor (15); Described natural pond liquid mixing apparatus (4) and CO
2pipeline between absorption equipment (6) is provided with concentration sensor (16); Described rich or poor heat exchanger (10) cryogenic fluid outlet (10.2) and rich carbon natural pond liquid CO
2pipeline between rich carbon natural pond liquid inlet (11.1) of regeneration of reclaim equiment (11) is provided with flowmeter (14).
6. a kind of CO that is carrier with anaerobic fermentation natural pond liquid according to claim 1
2absorption and storage utilize system, it is characterized in that: be provided with rolling NF membrane in described natural pond liquid concentrator (3).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420750028.2U CN204294104U (en) | 2014-12-02 | 2014-12-02 | A kind of CO that is carrier with anaerobic fermentation natural pond liquid 2absorption and storage utilize system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420750028.2U CN204294104U (en) | 2014-12-02 | 2014-12-02 | A kind of CO that is carrier with anaerobic fermentation natural pond liquid 2absorption and storage utilize system |
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| CN204294104U true CN204294104U (en) | 2015-04-29 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104383804A (en) * | 2014-12-02 | 2015-03-04 | 华中农业大学 | CO2 absorption and storage utilization system and method adopting anaerobic fermentation biogas slurry as carrier |
| CN106497620A (en) * | 2016-09-09 | 2017-03-15 | 华中农业大学 | With biogas slurry as CO2The methane purification of absorbent and biogas slurry treatment System and method for |
-
2014
- 2014-12-02 CN CN201420750028.2U patent/CN204294104U/en not_active Withdrawn - After Issue
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104383804A (en) * | 2014-12-02 | 2015-03-04 | 华中农业大学 | CO2 absorption and storage utilization system and method adopting anaerobic fermentation biogas slurry as carrier |
| CN104383804B (en) * | 2014-12-02 | 2016-07-06 | 华中农业大学 | A kind of be carrier with anaerobic fermentation biogas slurry CO2Absorb and storage utilizes system and method |
| CN106497620A (en) * | 2016-09-09 | 2017-03-15 | 华中农业大学 | With biogas slurry as CO2The methane purification of absorbent and biogas slurry treatment System and method for |
| CN106497620B (en) * | 2016-09-09 | 2021-12-28 | 华中农业大学 | Biogas purification and biogas slurry treatment system and method with biogas slurry as CO2 absorbent |
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