CN205170778U - Biological methanator of synthetic gas and system - Google Patents
Biological methanator of synthetic gas and system Download PDFInfo
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- CN205170778U CN205170778U CN201520752083.XU CN201520752083U CN205170778U CN 205170778 U CN205170778 U CN 205170778U CN 201520752083 U CN201520752083 U CN 201520752083U CN 205170778 U CN205170778 U CN 205170778U
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Abstract
The utility model provides a biological methanator of synthetic gas and system, this reactor of includes the main part, this main part includes: the microbiological synthesis reaction zone sets up at the middle part of this main part, and the anaerobic microorganisms that utilizes this reactor in this district CO and the H2 in to the synthetic gas carries out biotransformation, generates and uses the biological natural gas of CH4 as main component, and the gas -liquid mixture district, set up in this microbiological synthesis reaction zone below, let in in this gas -liquid mixture district and use CO and synthetic gas and the microbial nutrition liquid of H2 as main component to realize the mixture of gas -liquid, gas -liquid after mixing rises up into carries out this biotransformation in this microbiological synthesis reaction zone. The utility model discloses developed the synthetic gas anaerobic microorganisms conversion reaction ware of a new low cost, low energy consumption, be clean energy with gas high efficient conversion such as pyrolysis gas, industry by -product gas, can these gas calorific values of effectual solution low and have a problem of potential safety hazard.
Description
Technical field
The utility model relates to a kind of equipment of biosynthesizing high-quality biological Sweet natural gas, particularly a kind of synthetic gas biomethanation reactor, and it is with CO and H with pyrolysis gas and industrial by-product coal gas etc.
2synthetic gas for main component is raw material, in biosynthesizing reactor, by anaerobion, described synthetic gas is converted into high-quality biological Sweet natural gas, belongs to the energy regeneration technical field of environmental engineering.
Background technology
Although containing a small amount of CO in pyrolysis gas
2and CH
4, but its main component is CO and H
2, there is the problems such as calorific value is low, CO content is high, need further methanation.The technology of current pyrolysis gas methanation is still in be explored than selecting the stage.Clearly propose during country 12 and give special assistance to coal preparing natural gas (coal → pyrolysis gas → methane) technology, domestic multiple coal preparing natural gas project that started, wherein pyrolysis gas methanation is also the important middle-chain of coal preparing natural gas.Current pyrolysis gas methanation technology mainly utilizes heterogeneous catalyst methanation reaction principle, and the hydrocarbon shortening in pyrolysis gas is generated methane.But the subject matter of this technology needs to carry out under high temperature (200-700 DEG C) high pressure (1-7.5MPa) condition, CO and H
2need fixing ratio, methanation catalyst is expensive, and catalyzer is subject to the impact of sulfide etc. and inactivation.
Blast furnace gas is the byproduct produced in iron manufacturing process, and main component is: CO, CO
2, N
2, H
2, CH
4deng, wherein combustiblecomponents CO content accounts for about 25%.Although the calorific value of blast furnace gas is not high, the energy value that huge output produces is very considerable.Gas production rate due to blast furnace gas is greater than the gas consumption of user, and superfluous blast furnace gas needs diffused by diffusing tower or adopt torch burning.Not only waste a large amount of energy, and have in a large amount of obnoxious flavour and dust discharge to air and produce serious environmental pollution.Coke-oven gas is in process of coking, and the inflammable gas obtained while output coke and tar products, its main component of its main component is hydrogen (55% ~ 60%) and methane (23% ~ 27%), is the byproduct of process of coking.Along with the development of coking industry, a large amount of coke(oven)gas resources is had to produce.Coke(oven)gas is used as except heating fuel except part returns pit kiln, and remaining gas is mainly used as the fuel gas of city resident, because urban pipe network is sent in inconvenience, also has a great deal of by torch burning emptying.
Current industrial coke-oven gas utilization ways mainly contains: directly utilize as gas; Generating; Hydrogen can be extracted by techniques such as pressure swing adsorption processs; Methanol after deep purifying; Synthetic ammonia or ferment etc.There is the shortcomings such as economic benefit is not high, energy consumption is large, greenhouse gas emissions are large, environmental benefit is low in these techniques.Pyrolysis gas, blast furnace gas, coal gas of converter are rich in CO simultaneously, and toxicity is large, and direct combustion completion hidden danger is large.Therefore, domestic research and the engineering mimoir having carried out coke(oven)gas preparing natural gas.
At present, be converted in the process of Sweet natural gas carrying out coke(oven)gas, all adopt chemical process, a small amount of CO (5-7%) contained in coke(oven)gas and CO
2(1-3%) under the effect of chemical catalyst and H
2effect under be converted into methane (formula 1 and formula 2), but, still have the H of suitable surplus
2residue (accounting for about 30% of coke(oven)gas), thus cause coke(oven)gas itself can not be converted into Sweet natural gas completely, and need extra supplementary CO
2.Current chemical catalysis realizes coke-oven gas methanation needs high temperature (200-700 DEG C) and chemical catalyst, and therefore cost is higher, does not also have suitable CO in addition
2source is as extra carbon source.
CO+3H
2=CH
4+ H
2o Δ G=-206.16kJ/mol formula 1
CO
2+ 4H
2=CH
4+ 2H
2o Δ G=-165.08kJ/mol formula 2
In sum, current synthetic gas methanation technology mainly adopts chemical synthesising technology, but the subject matter of this technology needs to carry out under high temperature (200-700 DEG C) high pressure (1-7.5MPa) condition, CO and H
2need fixing ratio, methanation catalyst is expensive, and catalyzer is subject to the impact of sulfide etc. and inactivation.The industrial by-product such as pyrolysis gas, coke-oven gas coal gas gas component is complicated, CO and H
2ratio be difficult to meet the demands, utilize the synthetic gas of chemosynthesis principle industry methanation technology there is very large defect.
Summary of the invention
For overcoming the defect of prior art, the utility model provides a kind of synthetic gas biomethanation reactor, can by with CO and H
2for CO, H in the synthetic gas of main component
2cH is converted into by biosynthetic mode
4.
For realizing the purpose of this utility model, according to an embodiment of the present utility model, a kind of synthetic gas biomethanation reactor, comprise main body, this main body comprises: Microbe synthesis reaction zone, be arranged on the middle part of this main body, utilize in this district anaerobion in this reactor to CO and H in synthetic gas
2carry out bio-transformation, generate with CH
4for the bio-natural gas of main component; And gas-liquid mixed district, be arranged on below this Microbe synthesis reaction zone, pass into CO and H in this gas-liquid mixed district
2for synthetic gas and the microbial nutrient solution of main component, and realize the mixing of gas-liquid, mixed gas-liquid rises up in this Microbe synthesis reaction zone carries out this bio-transformation.
Wherein this synthetic gas biomethanation reactor also comprises: gas-solid-liquid disengaging zone, is arranged on above this Microbe synthesis reaction zone, the bio-natural gas after separation and respectively collection of biological synthesis; And sludge discharging area, be arranged on the bottommost of this reactor, regularly get rid of the mud of reactor bottom.
Wherein this microbial nutrient solution is C: N: P ratio is the nutritive medium of 100 ~ 300: 5: 1.
Wherein the aspect ratio of this main body is 2: 1 ~ 10: 1.
Wherein this gas-liquid mixed district comprises: nutritive medium import and water distribution uniformity system, in order to pass into this microbial nutrient solution required for the anaerobion growth in this Microbe synthesis reaction zone applicable equably, the upflow velocity of this microbial nutrient solution in this reactor controls in 1 ~ 2m/h, makes this microbial nutrient solution soak into this anaerobion; And fuel gas inlet and aerating apparatus, in order to pass into CO and H
2for this synthetic gas of main component, and gas is divided into micro-bubble and rises to this Microbe synthesis reaction zone and react.
Wherein the temperature of reaction of this Microbe synthesis reaction zone is 30-40 DEG C or 50-60 DEG C, and the pH value of this anaerobion suitable growth is 6.5 ~ 7.5.
Wherein with CO and H
2for the H in this synthetic gas of main component
2all can more than 80% be reached with the transformation efficiency of CO.
Wherein this gas-solid-liquid disengaging zone comprises gas-liquid-solid separation device, water port and venting port, reacted gas-solid-liquid mixture is separated by this gas-liquid-solid separation device in this district, from this gas-solid-liquid mixture, isolated bio-natural gas is discharged by this venting port, isolated supernatant liquor is discharged by this water port (9), and isolated sludge reflux is to this reactor bottom.
Wherein this isolated sludge reflux is to this sludge discharging area, discharges this reactor by the mud discharging mouth be arranged on below this sludge discharging area.
According to another embodiment of the present utility model, a kind of synthetic gas biomethanation reactive system, comprising: synthetic gas biomethanation reactor as above; Nutritive medium storage tank and intake pump, wherein microbial nutrient solution is delivered to the nutritive medium import of this synthetic gas biomethanation reactor by this intake pump from this nutritive medium storage tank; And air intake pump, will with CO and H
2synthetic gas for main component is delivered to the fuel gas inlet of this synthetic gas biomethanation reactor.
The utility model equipment utilization biosynthesis technology will with CO and H
2for H in the synthetic gas of main component
2, CO is converted into CH
4, transformation efficiency can reach more than 80%.Compared with existing chemical catalysis process, this technology have reaction conditions gentleness (without the need to High Temperature High Pressure), by product few, without the need to CO and H in fixing synthetic gas
2ratio and have the advantages such as tolerance to the sulfide in coke-oven gas and the tar in pyrolysis gas.
Accompanying drawing explanation
Fig. 1 is the structural representation of the utility model biomethanation reactor;
Fig. 2 is the configuration schematic diagram of biomethanation reactor of the present utility model.
Description of reference numerals is wherein as follows:
1, Microbe synthesis reaction zone; 2, gas-liquid mixed district; 3, gas-solid-liquid disengaging zone; 4, sludge discharging area; 5, nutritive medium import; 6, water distribution uniformity system; 7, fuel gas inlet; 8, aerating apparatus; 9, water port; 10, venting port; 11, mud discharging mouth; 12, nutritive medium storage tank; 13, intake pump 14, air intake pump.
Embodiment
Below in conjunction with drawings and Examples, the utility model is described in detail.
As shown in Figure 1, be synthetic gas biomethanation structure of reactor schematic diagram of the present utility model.According to another embodiment of the present utility model, this synthetic gas biomethanation reactor comprises main body, and this main body comprises: Microbe synthesis reaction zone 1, is arranged on the middle part of this main body, utilizes anaerobion in this reactor to CO and H in synthetic gas
2carry out bio-transformation, generate with CH
4it is main bio-natural gas; Gas-liquid mixed district 2, is arranged on below Microbe synthesis reaction zone 1, passes into CO and H in this district
2for synthetic gas and the microbial nutrient solution of main component, and realize the high efficient mixed of gas-liquid; Gas-solid-liquid disengaging zone 3, is arranged on above Microbe synthesis reaction zone 1, the bio-natural gas after separated and collected biosynthesizing; And sludge discharging area 4, be arranged on the bottommost of this reactor, regularly get rid of the mud of reactor bottom.
Described with CO and H
2for the synthetic gas of main component can be pyrolysis gas, blast furnace gas and coke-oven gas etc., can be wherein one or more mixing.
Anaerobion in described Microbe synthesis reaction zone 1 is slowly cultivated out by inoculation granule sludge or anaerobic sludge when device start.
Specifically, when device start, the bottom of reactor passes into granule sludge, and nutritive medium flows into bottom Sludge Bed, mixes contact with granule sludge.Microorganism in mud utilizes the organism in nutritive medium and CO and H2 in synthetic gas, continuous growth variability, finally tame into CO and H2 that specific anaerobion is used in transformation of synthetic gas, form the suspended sludge layer (the gas-solid-liquid mixture namely suspended) that a sludge concentration is less, namely described reaction zone.
Therefore, anaerobion is that seed sludge brings, and only passes into granule sludge when device start, along with the operation of equipment, slowly can cultivate the good granule sludge of the settling property that makes new advances or floc sludge, containing a large amount of anaerobions in this mud.
Gas-liquid mixed district 2 comprises nutritive medium import 5 and water distribution uniformity system 6, in order to pass into the nutritive medium in applicable Microbe synthesis reaction zone 1 required for microorganism growth uniformly and effectively, the upflow velocity of nutritive medium in reactor controls in 1 ~ 2m/h, makes this microbial nutrient solution soak into anaerobion in reaction zone 1.This gas-liquid mixed district 2 also comprises fuel gas inlet 7 and aerating apparatus 8, in order to pass into CO and H
2for the synthetic gas of main component, and gas is divided into micro-bubble and rises to Microbe synthesis reaction zone 1 and react.
Gas-solid-liquid disengaging zone 3 comprises gas-liquid-solid separation device, water port 9 and venting port 10, reacted gas-solid-liquid mixture is separated by this gas-liquid-solid separation device in this district, from this gas-solid-liquid mixture, isolated bio-natural gas is discharged by this venting port 10, isolated supernatant liquor is discharged by this water port 9, and isolated sludge reflux is to the sludge discharging area 4 of this reactor bottom, discharge this reactor by the mud discharging mouth 11 be arranged on below this sludge discharging area 4.
In embodiment of the present utility model, this main body is cylindric, and the aspect ratio of main body reactor is 2: 1 ~ 10: 1.This reactor reaction temperature is 30-40 DEG C or 50-60 DEG C, and the pH value of anaerobion suitable growth is 6.5 ~ 7.5.
Wherein, microbial nutrient solution is C: N: P ratio is the nutritive medium of 100 ~ 300: 5: 1, is preferably 200: 5: 1.Reacted liquid at the isolated liquid in gas-solid-liquid disengaging zone 3.Nutritive medium is for anaerobion provides nutrition, anaerobion and gas in 1st district after the microbial reaction be responsible for, produce the mixture of solid-liquid-gas, be separated by special gas-liquid-solid separation device in gas-solid-liquid disengaging zone 3, described gas-liquid-solid separation device is matured product, can directly utilize prior art or prior art is transformed a little, not describing in detail.The main component of the liquid after separation such as has full carbon, full nitrogen, full phosphorus, full potassium, ammonium nitrogen, rapid available phosphorus and available potassium etc., in addition also containing various vitamin B group, protein, cellulase and growth hormone etc., and containing various trace element and each seed amino acid etc., liquid after described separation can be used as organic fertilizer, for using outside root or plant leaf surface sprinkling.
Fig. 2 is the configuration schematic diagram of the complete outfit of biomethanation reactor of the present utility model.
Refer to Fig. 2, according to another embodiment of the present utility model, a kind of synthetic gas biomethanation reactive system, comprising: synthetic gas biomethanation reactor as above; Nutritive medium storage tank 12 and intake pump 13, wherein microbial nutrient solution is delivered to the nutritive medium import 5 of this synthetic gas biomethanation reactor by this intake pump 13 from this nutritive medium storage tank 12; And air intake pump 14, the synthetic gas that is main component with CO and H2 is delivered to the fuel gas inlet 7 of this synthetic gas biomethanation reactor.
Be described below in conjunction with the workflow of accompanying drawing to biomethanation reactive system of the present utility model.
As shown in Figure 2, nutritive medium is delivered to nutritive medium import 5 by intake pump 13 by nutritive medium storage tank 12, then enters reactor bottom equably by water distribution uniformity system 6.With CO and H
2for the synthetic gas of main component is delivered to fuel gas inlet 7 by air intake pump 14, then be micro-bubble by aerating apparatus 8 by gas reforming, micro-bubble and nutritive medium are after gas-liquid mixed district 2 mixes, and micro-bubble carries the Microbe synthesis reaction zone 1 that nutritive medium rises in the middle part of reactor and reacts.Wherein, nutritive medium provides nutrition for the anaerobion in Microbe synthesis reaction zone 1, and anaerobion is to CO and H in synthetic gas
2carry out bio-transformation, generate with CH
4it is main bio-natural gas.The bio-natural gas generated carries reacted liquid and solid (i.e. mud) and enters gas-solid-liquid disengaging zone 3 and carry out gas-solid-liquid and be separated, bio-natural gas is discharged reactor by venting port 10 and is carried out Collection utilization, supernatant liquor discharges tank body by water port 9, sludge reflux, to sludge discharging area 4, discharges reactor by mud discharging mouth 11.
The utility model equipment utilization biosynthesis technology will with CO and H
2for H in the synthetic gas of main component
2and CO is converted into CH
4, transformation efficiency all can reach more than 80%.Compared with existing chemical catalysis process, this technology have reaction conditions gentleness (without the need to High Temperature High Pressure), by product few, without the need to CO and H in fixing synthetic gas
2ratio and to the sulfide in coke-oven gas and the tar in pyrolysis gas have tolerance etc. advantage.
The utility model develops the synthetic gas anaerobic microbial conversion reactor of a kind of new low cost, less energy-consumption, will with CO and H
2synthetic gas Efficient Conversion for main component is clean energy, effectively can solve these fuel gases calorific values low and there is the problem of potential safety hazard.
Claims (9)
1. a synthetic gas biomethanation reactor, comprises main body, it is characterized in that, this main body comprises:
Microbe synthesis reaction zone (1), is arranged on the middle part of this main body, utilizes anaerobion in this reactor to CO and H in synthetic gas in this district
2carry out bio-transformation, generate with CH
4for the bio-natural gas of main component; And
Gas-liquid mixed district (2), is arranged on this below, Microbe synthesis reaction zone (1), passes into CO and H in this gas-liquid mixed district (2)
2for synthetic gas and the microbial nutrient solution of main component, and realize the mixing of gas-liquid, mixed gas-liquid rises up in this Microbe synthesis reaction zone (1) carries out this bio-transformation.
2. synthetic gas biomethanation reactor according to claim 1, is characterized in that, also comprise:
Gas-solid-liquid disengaging zone (3), is arranged on this top, Microbe synthesis reaction zone (1), the bio-natural gas after separation and respectively collection of biological synthesis; And
Sludge discharging area (4), is arranged on the bottommost of this reactor, regularly gets rid of the mud of reactor bottom.
3. synthetic gas biomethanation reactor according to claim 1 and 2, is characterized in that, the aspect ratio of this main body is 2: 1 ~ 10: 1.
4. synthetic gas biomethanation reactor according to claim 1 and 2, is characterized in that, this gas-liquid mixed district (2) comprising:
Nutritive medium import (5) and water distribution uniformity system (6), in order to pass into this microbial nutrient solution required for the anaerobion growth in this Microbe synthesis reaction zone (1) applicable equably, the upflow velocity of this microbial nutrient solution in this reactor controls in 1 ~ 2m/h, makes this microbial nutrient solution soak into this anaerobion; And
Fuel gas inlet (7) and aerating apparatus (8), in order to pass into CO and H
2for this synthetic gas of main component, and gas is divided into micro-bubble and rises to this Microbe synthesis reaction zone (1) and react.
5. synthetic gas biomethanation reactor according to claim 1 and 2, is characterized in that, the temperature of reaction of this Microbe synthesis reaction zone (1) is 30-40 DEG C or 50-60 DEG C, and the pH value of this anaerobion suitable growth is 6.5 ~ 7.5.
6. synthetic gas biomethanation reactor according to claim 1 and 2, is characterized in that, with CO and H
2for the H in this synthetic gas of main component
2all can more than 80% be reached with the transformation efficiency of CO.
7. synthetic gas biomethanation reactor according to claim 2, it is characterized in that, this gas-solid-liquid disengaging zone (3) comprises gas-liquid-solid separation device, water port (9) and venting port (10), reacted gas-solid-liquid mixture is separated by this gas-liquid-solid separation device in this district, from this gas-solid-liquid mixture, isolated bio-natural gas is discharged by this venting port (10), isolated supernatant liquor is discharged by this water port (9), and isolated sludge reflux is to this reactor bottom.
8. synthetic gas biomethanation reactor according to claim 7, it is characterized in that, this isolated sludge reflux, to this sludge discharging area (4), discharges this reactor by the mud discharging mouth (11) being arranged on below, this sludge discharging area (4).
9. a synthetic gas biomethanation reactive system, is characterized in that, comprising:
As claim 1 to 8 any one as described in synthetic gas biomethanation reactor;
Nutritive medium storage tank (12) and intake pump (13), wherein microbial nutrient solution is delivered to the nutritive medium import (5) of this synthetic gas biomethanation reactor by this intake pump (13) from this nutritive medium storage tank (12); And
Air intake pump (14), will with CO and H
2synthetic gas for main component is delivered to the fuel gas inlet (7) of this synthetic gas biomethanation reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520752083.XU CN205170778U (en) | 2015-09-24 | 2015-09-24 | Biological methanator of synthetic gas and system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520752083.XU CN205170778U (en) | 2015-09-24 | 2015-09-24 | Biological methanator of synthetic gas and system |
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| Publication Number | Publication Date |
|---|---|
| CN205170778U true CN205170778U (en) | 2016-04-20 |
Family
ID=55734792
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|---|---|---|---|
| CN201520752083.XU Withdrawn - After Issue CN205170778U (en) | 2015-09-24 | 2015-09-24 | Biological methanator of synthetic gas and system |
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| Country | Link |
|---|---|
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106554829A (en) * | 2015-09-24 | 2017-04-05 | 北京联合创业环保工程股份有限公司 | Synthesis gas biomethanation reactor and system |
-
2015
- 2015-09-24 CN CN201520752083.XU patent/CN205170778U/en not_active Withdrawn - After Issue
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106554829A (en) * | 2015-09-24 | 2017-04-05 | 北京联合创业环保工程股份有限公司 | Synthesis gas biomethanation reactor and system |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP02 | Change in the address of a patent holder | ||
| CP02 | Change in the address of a patent holder |
Address after: 100160 Beijing Fengtai District South Fourth Ring Road 188 18 District 25 building 305 Patentee after: BEIJING UNITED PIONEER ENVIRONMENTAL ENGINEERING CO.,LTD. Address before: 100161 room 1, unit 1, Ma Guan Ying home, Fengtai District, Beijing 1502 room. Patentee before: BEIJING UNITED PIONEER ENVIRONMENTAL ENGINEERING CO.,LTD. |
|
| AV01 | Patent right actively abandoned | ||
| AV01 | Patent right actively abandoned | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20160420 Effective date of abandoning: 20230112 |
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| AV01 | Patent right actively abandoned |
Granted publication date: 20160420 Effective date of abandoning: 20230112 |