CN103113945B - Marsh gas purification system and marsh gas purification method - Google Patents
Marsh gas purification system and marsh gas purification method Download PDFInfo
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- CN103113945B CN103113945B CN201310041298.6A CN201310041298A CN103113945B CN 103113945 B CN103113945 B CN 103113945B CN 201310041298 A CN201310041298 A CN 201310041298A CN 103113945 B CN103113945 B CN 103113945B
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Abstract
The invention provides a marsh gas purification system. The system is characterized by comprising a primary inlet separator which is used for removing granular solid substances and moisture in marsh gas generated by a marsh gas source so as to form first purified marsh gas, a primary compressor which is communicated with the primary inlet separator and used for compressing the first purified marsh gas to form first compressed marsh gas, a secondary compressor which is communicated with the primary compressor and used for compressing the first compressed marsh gas to form second compressed marsh gas, a secondary inlet separator which is communicated with the secondary compressor and used for removing granular solid substances and moisture in the second compressed marsh gas to form second purified marsh gas, a washing tower which is communicated with the secondary inlet separator and used for removing impure gases in the second purified marsh gas by using amine liquid to obtain purified marsh gas and amine liquid containing absorbed impure gases, and amine liquid circulating equipment which is communicated with the washing tower and used for removing impure gases in the amine liquid by which impure gases are adsorbed to obtain amine liquid recycling liquid. The marsh gas purification system can be used for improving the content of marsh gas in marsh gas.
Description
Technical field
The present invention relates to biogas energy and utilize field, particularly relate to a kind of methane purifying system and biogas purification method.
Background technology
Biogas is organic under anaerobic through a kind of inflammable gas that fermentable produces, and its main ingredient is methane.General, biogas is by 50% ~ 80% methane (CH
4), 20% ~ 40% carbonic acid gas (CO
2), 0% ~ 5% nitrogen (N
2), be less than 1% hydrogen (H
2), be less than 0.4% oxygen (O
2) and 0.1% ~ 3% hydrogen sulfide (H
2the gas composition such as S).
Biogas calorific value is high, and polluting few, is a kind of clean energy.China started to apply in nineteen twenties, obtained encouraging success at present.But traditional biogas source, such as methane-generating pit, the content of the methane in sewage gas of generation is lower, limits the use of biogas.
Summary of the invention
Based on this, be necessary to provide a kind of methane purifying system and the biogas purification method that improve methane content of bilogas.
A kind of methane purifying system, comprising:
One-level entrance separator, for remove biogas source produce biogas in solids and moisture form the first purifying marsh gas;
Stage compressor, is communicated with described one-level entrance separator, forms the first compressed biogas for compressing described first purifying marsh gas;
Two stage compressor, is communicated with described stage compressor, forms the second compressed biogas for compressing described first compressed biogas;
Secondary inlet separator, is communicated with described two stage compressor, for removing solids in described second compressed biogas and moisture forms the second purifying marsh gas;
Washing tower, is communicated with described secondary inlet separator, obtains the biogas after purifying and adsorbed the amine liquid of foreign gas for using the amine liquid foreign gas removed in described second purifying marsh gas; And
Amine liquid recycle unit, is communicated with described washing tower, obtains amine liquid Ethylene recov, and amine liquid Ethylene recov is delivered to described washing tower for removing described foreign gas of having adsorbed in the amine liquid of foreign gas.
Wherein in an embodiment, described amine liquid recycle unit comprises flash tank and stripping tower; Described flash tank is communicated with described washing tower, for removing the rich solution that described at least part of foreign gas of having adsorbed in the amine liquid of foreign gas is purified; Described stripping tower is communicated with described flash tank and described washing tower, and described stripping tower forms amine liquid Ethylene recov for the foreign gas removed in the rich solution of described purification, and described amine liquid Ethylene recov is delivered to described washing tower.
Wherein in an embodiment, described amine liquid recycle unit also comprises the heat exchanger be communicated with described flash tank and described stripping tower, described stripping tower is provided with reboiler, and the rich solution of the purification that the amine liquid Ethylene recov exported from described reboiler and described flash tank export carries out heat exchange by described heat exchanger.
Wherein in an embodiment, described amine liquid recycle unit also comprises amine liquid Ethylene recov water cooler, is communicated with described heat exchanger and described washing tower, for lowering the temperature further to the amine liquid Ethylene recov through heat exchange and output to described washing tower.
Wherein in an embodiment, described amine liquid recycle unit also comprises:
Water cooler, is communicated with described stripping tower, and the gas for being exported by described stripping tower carries out cooling the amine liquid condensing making to gasify in gas and becomes amine liquid;
Amine separator, is communicated with described water cooler and described washing tower, and the amine liquid for the foreign gas that exported by water cooler and post liquefaction is again separated;
Amine liquid Ethylene recov surge tank, is communicated with described amine separator, described stripping tower and described washing tower, the amine liquid Ethylene recov that amine liquid and described stripping tower for accommodating the generation of amine separator generate, and described amine liquid and amine liquid Ethylene recov are delivered to described washing tower.
Use a biogas purification method for above-mentioned methane purifying system, comprise the following steps:
One-level entrance separator is used to remove solids in biogas and moisture forms the first purifying marsh gas; Described first purifying marsh gas of stage compressor compression is used to form the first compressed biogas;
Described first compressed biogas of two stage compressor compression is used to form the second compressed biogas;
Secondary inlet separator is used to remove solids in described second compressed biogas and moisture forms the second purifying marsh gas;
In washing tower, use the amine liquid foreign gas removed in described second purifying marsh gas to obtain the biogas after purifying and adsorbed the amine liquid of foreign gas; And
Use amine liquid recycle unit to remove described foreign gas of having adsorbed in the amine liquid of foreign gas and obtain amine liquid Ethylene recov, and described amine liquid Ethylene recov is delivered to described washing tower.
Wherein in an embodiment, described use amine liquid recycle unit removes the step that described foreign gas of having adsorbed in the amine liquid of foreign gas obtains amine liquid Ethylene recov and is divided into following steps:
Use flash tank removes the rich solution that described at least part of foreign gas of having adsorbed in the amine liquid of foreign gas is purified;
Other foreign gases in the rich solution using stripping tower to be purified by flash tank remove, and form amine liquid Ethylene recov, and described amine liquid Ethylene recov is delivered to described washing tower.
Wherein in an embodiment, before described amine liquid Ethylene recov is delivered to described washing tower, first the rich solution of described amine liquid Ethylene recov and described purification is carried out heat exchange.
Wherein in an embodiment, be delivered to described washing tower by after the amine liquid Ethylene recov of heat exchange uses amine liquid Ethylene recov water cooler to lower the temperature further.
Wherein in an embodiment, also comprise step:
The gas exported by described stripping tower uses water cooler cooling to make the amine condensation in gas become amine liquid;
The gas using amine separator to be exported by water cooler and amine liquid are separated, and amine liquid is delivered to washing tower.
Above-mentioned methane purifying system and biogas purification method, by one-level entrance separator, remove solids in biogas and portion of water forms the first purifying marsh gas, first purifying marsh gas can be compressed to 0.1Mpa ~ 0.8Mpa by stage compressor and form the first compressed biogas, first compressed biogas can be compressed to 2.5Mpa ~ 8Mpa by two stage compressor again and form the second compressed biogas, the solids in the second compressed biogas is removed by secondary inlet separator and washing tower, the biogas after purifying is obtained after the impurity such as moisture and carbonic acid gas, thus effectively can improve methane content of bilogas, methane content of bilogas can be increased to 95%(percent by volume by this methane purifying system) more than, can as the fuel of gasfueled vehicles, compared to traditional firedamp gas equipment, effectively widen the use range of biogas, meanwhile, amine liquid recycle unit can be recycled amine liquid, can reduce costs.
Accompanying drawing explanation
Fig. 1 is the structural representation of the methane purifying system of an embodiment.
Embodiment
For enabling above-mentioned purpose of the present invention, feature and advantage become apparent more, are described in detail the specific embodiment of the present invention below in conjunction with accompanying drawing.Set forth a lot of detail in the following description so that fully understand the present invention.But the present invention can be much different from alternate manner described here to implement, those skilled in the art can when without prejudice to doing similar improvement when intension of the present invention, therefore the present invention is by the restriction of following public concrete enforcement.
It should be noted that, when element is called as " being fixedly arranged on " another element, directly can there is element placed in the middle in it on another element or also.When an element is considered to " connection " another element, it can be directly connected to another element or may there is centering elements simultaneously.Term as used herein " vertical ", " level ", "left", "right" and similar statement are just for illustrative purposes.
Unless otherwise defined, all technology used herein and scientific terminology are identical with belonging to the implication that those skilled in the art of the present invention understand usually.The object of term used in the description of the invention herein just in order to describe specific embodiment, is not intended to be restriction the present invention.Term as used herein " and/or " comprise arbitrary and all combinations of one or more relevant Listed Items.
Refer to Fig. 1, the methane purifying system 10 of one embodiment, comprises one-level entrance separator 110, stage compressor 120, first-level buffer tank 130, deoxidation-nitrogen tower 140, two stage compressor 150, secondary inlet separator 164, washing tower 166, level 2 buffering tank 170, three-stage compressor 180, biogas storage device 185 and amine liquid recycle unit 190.
One-level entrance separator 110 is communicated with biogas source 90, for remove biogas source 90 produce biogas in solids and moisture form the first purifying marsh gas.The dehydration rate of one-level entrance separator 110 is more than 50%.The similar of one-level entrance separator 110 is in cyclonic separator.After biogas enters one-level entrance separator 110, obviously solid phase particles is settlement separate for part, and the solid phase particles of part greater particle size is separated by whirlwind runner with liquid-phase particle, and less solid-liquid particle is then separated by silk screen bed.
It should be noted that, biogas source 90 is for providing biogas.Biogas source 90 can be the methane-generating pit of self-assembling formation, also can be the biogas generation apparatus such as the artificial mathane generating pool built or industrialized tank for sewage gas, in this no limit, as long as can produce biogas.
Stage compressor 120 is communicated with one-level entrance separator 110, forms the first compressed biogas for compressing the first purifying marsh gas.In present embodiment, the first purifying marsh gas is compressed to 0.1Mpa ~ 0.8Mpa by stage compressor 120.Certainly, in other embodiments, the air pressure of the first compressed biogas also can adjust as required.It should be noted that, in other embodiments, booster fan (not shown) can also be set between biogas source 90 and one-level entrance separator 110, the air pressure of the biogas entering one-level entrance separator 110 can be improved, the unstripped gas Quality advance entering stage compressor can be made like this, thus extend the work-ing life of stage compressor 120.
First-level buffer tank 130 is communicated with stage compressor 120, for cushioning the pressure of the first compressed biogas obtained after stage compressor 120 processes.First-level buffer tank 130 can play voltage stabilizing, current stabilization to the first compressed biogas, plays the effect of balance flow process material, safer when making the first compressed biogas be compressed formation the second compressed biogas by two stage compressor 150.
Deoxidation-nitrogen tower 140 is communicated with first-level buffer tank 130, for removing from the oxygen the firstth compressed biogas of first-level buffer tank 130 output and the one in nitrogen.Deoxidation-nitrogen tower is a kind of tower equipment of one for removing the oxygen (or nitrogen) contained in biogas.Its similar in: according to the subsequent application filler of grid-ceramic bead-stainless (steel) wire-sorbent material (being fixed on bed)-stainless (steel) wire-ceramic bead-grid in tower, gas bottom in and top out.If to remove oxygen, then can adopt iron system compound adsorbent, manganese system compound adsorbent or acticarbon, be preferably iron system compound adsorbent; If to remove nitrogen, then can select fluosilicic stone sorbent material (or fluosilicic stone molecular sieve), or active aluminum ball (Al
2o
3), all remove to oxygen nitrogen, then should determine different sorbent material according to each gaseous fraction, carry out proportioning and feed intake.
Two stage compressor 150 is communicated with deoxidation-nitrogen tower 140, for the first compressed biogas compression formation second compressed biogas being stripped of at least one in oxygen and nitrogen will exported from deoxidation-nitrogen tower 140.In present embodiment, the air pressure of the second compressed biogas is 2.5Mpa ~ 8Mpa, and certainly, in other embodiments, the air pressure of the second compressed biogas also can adjust as required.
Secondary inlet separator 164 is communicated with the second compressor 150, for removing solids in the second compressed biogas and moisture forms the second purifying marsh gas.The dehydration rate of secondary inlet separator 164 is more than 30%.Secondary inlet separator 164 and one-level entrance separator 110 similar, more accurate, solids and moisture can be removed further.
Washing tower 166 is communicated with secondary inlet separator 164, obtains the biogas after purifying and adsorbed the amine liquid of foreign gas for using the amine liquid foreign gas removed in the second purifying marsh gas.The amine liquid having adsorbed foreign gas exported from washing tower 166 is rich solution.Foreign gas is the impurity such as carbonic acid gas, moisture and hydrogen sulfide.The method of amine liquid absorption is adopted to realize carbon dioxide removal, its principle is in a tower, gas inputs from bottom, gas circuit is up in tower, from tower top conveying amine liquid, contrary with gas circuit direction, multipipe structure can be designed in tower to increase the contact area of amine liquid and gas, thus increase amine liquid to the washing effect of carbon dioxide in methane.Moisture in removal biogas, other impurity mainly rely on one-level entrance separator 110 and secondary inlet separator 164, and when using the absorption of amine liquid, remaining moisture and other impurity can be retained by amine liquid.In present embodiment, the solute in amine liquid is thanomin, and the volumetric concentration of amine liquid is 20 ~ 50%.In other embodiments, amine liquid also can be the mixing solutions that diethanolamine (DEA) solution and N-methyl glycol amine (MDEA) solution are mixed to form, wherein, in DEA solution, DEA volumetric concentration is 15 ~ 60%, in MDEA solution, the volumetric concentration of MDEA is 20 ~ 60%, and the volume ratio of diethanolamine (DEA) solution and N-methyl glycol amine (MDEA) solution is 1:4 ~ 1:2; The solvent of diethanolamine (DEA) solution is the solvent that can dissolve diethanolamine (DEA) and not react with diethanolamine (DEA), such as: water; Solvent in N-methyl glycol amine (MDEA) solution is the solvent that can dissolve N-methyl glycol amine (MDEA) and not react with N-methyl glycol amine (MDEA), such as: water.
Level 2 buffering tank 170 is communicated with washing tower 166, for cushioning the pressure of the biogas after purification.Level 2 buffering tank 170 can to purify after biogas play voltage stabilizing, current stabilization, make the biogas after purification by three-stage compressor 180 compress formed High-pressure Marsh Gas time safer.
Three-stage compressor 180 is communicated with level 2 buffering tank 170, for Marsh gas compression to the 15 ~ 30Mpa after the purification that will export from level 2 buffering tank 170, forms High-pressure Marsh Gas.
Biogas storage device 185 is communicated with three-stage compressor 180, compresses the High-pressure Marsh Gas formed for filling three-stage compressor 180.Biogas storage device 185 is hold-up vessel or storage bottle.
Amine liquid recycle unit 190 comprises throttling valve 182, flash tank 191, heat exchanger 192, stripping tower 193, amine liquid Ethylene recov water cooler 195, amine liquid Ethylene recov surge tank 196, water cooler 197, amine separator 198 and amine surge tank 199.
Throttling valve 182 is arranged between washing tower 166 and flash tank 191, and throttling valve 182 can control the flow velocity having adsorbed the amine liquid of foreign gas that washing tower 166 exports.
Flash tank 191 is communicated with throttling valve 182, for remove adsorbed foreign gas amine liquid at least part of foreign gas, the rich solution be purified.Foreign gas is the impurity such as carbonic acid gas, moisture and hydrogen sulfide.In the rich solution of purification, the decreasing ratio of foreign gas is about 30%.
Stripping tower 193 is by being communicated with flash tank 191 with heat exchanger 192.Stripping tower 193, for removing the foreign gas be delivered to by heat exchanger 192 in the rich solution of the purification of stripping tower 193, is made to remove in the rich solution of the foreign gas self-purification in the rich solution of purification and forms amine liquid Ethylene recov.Amine liquid Ethylene recov is the amine liquid removing the foreign gas of more than 99% at stripping tower, also claims lean solution.Not only containing the foreign gas be adsorbed in the rich solution of purification in the gas that stripping tower 193 exports, also has the amine liquid of partial gasification.
Stripping tower 193 is provided with reboiler 194, and reboiler 194 is arranged on the bottom of stripping tower 193.Reboiler 194 is heated for carrying out heating to the rich solution of purification.The amine liquid Ethylene recov that stripping tower 193 generates is delivered to heat exchanger 192, and the rich solution of the purification exported with flash tank 191 carries out heat exchange by heat exchanger 192, and the rich solution of the purification after heat exchange enters stripping tower 193.
Amine liquid Ethylene recov water cooler 195 is communicated with heat exchanger 192, for lowering the temperature further to the amine liquid Ethylene recov through heat exchange.
Amine liquid Ethylene recov surge tank 196 is communicated with amine liquid Ethylene recov water cooler 195.Amine liquid Ethylene recov surge tank 196 is communicated with washing tower 166 by amine liquid pump (not shown).Amine liquid Ethylene recov surge tank 196 for cushioning the amine liquid Ethylene recov of lowering the temperature further through amine liquid Ethylene recov water cooler 195, and is delivered to washing tower 166 by amine liquid pump.Amine liquid Ethylene recov surge tank 196 is provided with amine liquid and adds mouth, and this interpolation mouth is used for adding and supplementary amine liquid.Amine liquid Ethylene recov surge tank 196 can play voltage stabilizing, current stabilization to the amine liquid Ethylene recov through the further cooling of amine liquid Ethylene recov water cooler 195, safer when making it be delivered to washing tower 166.
Water cooler 197 is communicated with stripping tower 193, and the gas for being exported by stripping tower 193 carries out cooling the amine liquid condensing making to gasify in gas and becomes amine liquid.
Amine separator 198 is communicated with water cooler 197.Amine separator 198 is communicated with stripping tower 193 by amine recycle pump (not shown).Amine separator 198 is separated with the amine liquid of post liquefaction again for the foreign gas that exported by water cooler 197, and by amine recycle pump, amine liquid is delivered to amine surge tank 199, and foreign gas is emptying.
Amine surge tank 199 is communicated with amine liquid Ethylene recov surge tank 196 and amine separator 198, for collecting the liquefied ammonia that amine separator 198 produces, carrying out buffered, and the liquefied ammonia in amine surge tank 199 is delivered to amine liquid Ethylene recov surge tank 196 to amine liquid.
Further, methane purifying system 10 also comprises sledge-borne type casing (not shown), and one-level entrance separator 110, stage compressor 120, first-level buffer tank 130, deoxidation-nitrogen tower 140, two stage compressor 150, secondary inlet separator 164, washing tower 166, level 2 buffering tank 170, three-stage compressor 180 and biogas storage device 185 are arranged in sledge-borne type casing.Such methane purifying system 10 conveniently can move, transport.Certainly, when treatment capacity less (40000 cubic metres/day), the each device of native system can be integrated in a sledge-borne type casing, but when high throughput, a unit of possible native system or several unit independently become sled, whole system can have and is combined into by multiple sled, functionally not difference.
Above-mentioned methane purifying system, solids in the first compressed biogas can be removed and portion of water obtains the first purifying marsh gas by one-level entrance separator 110, first class purification Marsh gas compression can be formed the first compressed biogas to 0.1Mpa ~ 0.8Mpa by stage compressor 120, first purifying marsh gas can be compressed to 2.5Mpa ~ 8Mpa by two stage compressor 150 again and form the second compressed biogas, the solids in the second compressed biogas is removed by secondary inlet separator 164 and washing tower 166, the biogas after purifying is obtained after the impurity such as moisture and carbonic acid gas, methane content of bilogas can be increased to 95%(percent by volume by this methane purifying system) more than, make the content of methane in sewage gas higher, by filling to high-pressure cylinder for the Marsh gas compression after purifying, can as the fuel of gasfueled vehicles, effectively widen the use range of biogas.
This methane purifying system compressed biogas terminal pressure scope is at 15Mpa ~ 30Mpa, have employed three stage compression, stage compressor 120, two stage compressor 150 and three-stage compressor 180 three is used to coordinate, namely gaseous tension is promoted to target pressure range by gradation, so every stage compressor is less, cost is lower, simultaneously, pressurized vessel after every stage compressor makes according to pressure range, avoid putting in place according to first compression, the compressor used will be very huge, and price is very expensive, thus can reduce costs; In addition, from the beginning pressure is risen to goal pressure, equipment all thereafter all must make according to this pressure rank, and cost is very large, and has great potential safety hazard, uses the mode of three stage compression compression to improve security, reduces equipment cost.
The above-mentioned methane purifying system of washing tower is by arranging amine liquid recycle unit 190, the foreign gas generation amine liquid Ethylene recov adsorbed in the amine liquid of foreign gas that washing tower 166 exports can be removed, can recycle amine liquid, improve the utilising efficiency of amine liquid, reduce cost.
Be appreciated that, when the biogas throughput ratio exported from biogas source 90 is more steady, first-level buffer tank 130 can omit, now deoxidation-nitrogen tower 140 is communicated with stage compressor 120, first compressed biogas is directly passed into deoxidation-nitrogen tower, if when in the biogas that biogas source 90 produces, oxygen level is lower, deoxidation-nitrogen tower 140 can omit, and now stage compressor 120 is directly communicated with two stage compressor 150.Level 2 buffering tank 170 also can omit, and now washing tower 166 is communicated with three-stage compressor 180, and the biogas after washing tower 166 is purified directly is compressed to 15 ~ 30Mpa by three-stage compressor 180.Three-stage compressor 180 and biogas storage device 185 also can omit, and the biogas after now purifying directly can be used as other purposes.When the amine flow velocity having adsorbed foreign gas exported from washing tower 166 is comparatively steady and flow is little, throttling valve 182 also can omit, and now washing tower 166 is communicated with flash tank 191.Heat exchanger 192 also can omit, and now flash tank 191 is communicated with stripping tower 193, and the rich solution of purification that flash tank 191 exports directly is delivered to stripping tower 193 and removes foreign gas wherein.Stripping tower 193 is communicated with amine liquid Ethylene recov water cooler 195.Amine liquid Ethylene recov water cooler 195 also can omit, and now stripping tower 193 is communicated with amine liquid Ethylene recov surge tank 196, and amine liquid Ethylene recov is delivered to amine liquid Ethylene recov surge tank 196 by stripping tower 193.Amine liquid Ethylene recov surge tank 196 also can omit, and now stripping tower 193 is communicated with washing tower 166, and amine liquid Ethylene recov is delivered to washing tower 166 by stripping tower 193.Water cooler 197, amine separator 198 and amine surge tank 199 also can omit, and the gas now exported from stripping tower 193 can be discharged with additive method.
Please refer to Fig. 1, the biogas purification method of an embodiment, comprises the following steps:
Step S110, one-level entrance separator 110 is used to remove solids in biogas and moisture forms the first purifying marsh gas.
Biogas is provided by biogas source 90.Biogas source 90 can be the methane-generating pit of self-assembling formation, also can be the biogas generation apparatus such as the artificial mathane generating pool built or industrialized tank for sewage gas, in this no limit, as long as can produce biogas.
Preferably, the dehydration rate through the first purifying marsh gas of step S110 process is more than 50%.
It should be noted that, pressurized treatment can also be carried out to biogas before step S110.In present embodiment, make the air pressure of biogas increase to during pressurized treatment and be no more than 150kPa, thus make unstripped gas Quality advance.
Step S120, use stage compressor 120 compress the first purifying marsh gas and form the first compressed biogas.
Preferably, the air pressure of the first compressed biogas is 0.1Mpa ~ 0.8Mpa, and certainly, in other embodiments, the air pressure of the first compressed biogas also can adjust as required.
Step S130, use first-level buffer tank 130 carry out buffered to the first compressed biogas.
First compressed biogas is carried out buffered and can play voltage stabilizing, current stabilization to the first compressed biogas.
Step S140, use deoxidation-nitrogen tower 140 remove the oxygen in the first compressed biogas and at least one in nitrogen.
Deoxidation-nitrogen tower is a kind of tower equipment of one for removing the oxygen (or nitrogen) contained in biogas.Its similar in: according to the subsequent application filler of grid-ceramic bead-stainless (steel) wire-sorbent material (being fixed on bed)-stainless (steel) wire-ceramic bead-grid in tower, gas bottom in and top out.If to remove oxygen, then can adopt iron system compound adsorbent, manganese system compound adsorbent or acticarbon, be preferably iron system compound adsorbent; If to remove nitrogen, then can select fluosilicic stone sorbent material (or fluosilicic stone molecular sieve), or active aluminum ball (Al
2o
3), all remove to oxygen nitrogen, then should determine different sorbent material according to each gaseous fraction, carry out proportioning and feed intake.
Step S150, the first compressed biogas using two stage compressor 150 compression to be stripped of oxygen form the second compressed biogas.
In present embodiment, the air pressure of the second compressed biogas is 2.5Mpa ~ 8Mpa, and certainly, in other embodiments, the air pressure of the second compressed biogas also can adjust as required.
Step S160, secondary inlet separator 164 is used to remove solids in the second compressed biogas and moisture forms the second purifying marsh gas.
Preferably, in step S160, the dehydration rate of the second purifying marsh gas is more than 30%.
Step S170, in washing tower 166, the amine liquid foreign gas removed in the second purifying marsh gas is used to obtain the biogas after purifying and adsorbed the amine liquid of foreign gas.
In present embodiment, by the second purifying marsh gas purified through secondary inlet separator 164, use washing tower 166 to remove the impurity such as the carbonic acid gas that wherein comprises and moisture further, obtain the biogas after purifying.
Step S180, use level 2 buffering tank 170 carry out buffered to the biogas after purification.
Level 2 buffering tank 170 can to purify after biogas play voltage stabilizing, current stabilization, with make three-stage compressor 180 by purify after Marsh gas compression formed High-pressure Marsh Gas time safer.
After biogas input level 2 buffering tank 170 after purification is carried out buffered, can also following steps be carried out:
Step S190, use three-stage compressor 180 compress the biogas after purifying and form High-pressure Marsh Gas.
In present embodiment, the air pressure of High-pressure Marsh Gas is 15Mpa ~ 30Mpa.
Step S200, the filling High-pressure Marsh Gas of use biogas storage device 185.
Biogas after filling purification can be used as the fuel of gasfueled vehicles.
Step S210, use amine liquid recycle unit 190 remove the foreign gas of having adsorbed in the amine liquid of foreign gas and obtain amine liquid Ethylene recov, and amine liquid Ethylene recov is delivered to washing tower 166.
In the present embodiment, step S210 is divided into following steps:
Step S211, use flash tank 191 remove the rich solution that at least part of foreign gas of having adsorbed in the amine liquid of foreign gas is purified.
Specifically in the present embodiment, in the rich solution of purification, the decreasing ratio of foreign gas is about 30%.
Other foreign gases in the rich solution of the purification that flash tank obtains by step S212, use stripping tower 193 remove, and form amine liquid Ethylene recov.
Stripping tower 193 is communicated with flash tank 191 by heat exchanger 192.Stripping tower 193, for removing the foreign gas be delivered to by heat exchanger 192 in the rich solution of the purification of stripping tower 193, is made to remove in the rich solution of the foreign gas self-purification in rich solution and forms amine liquid Ethylene recov.Not only containing the foreign gas be adsorbed in the rich solution of purification in the gas that stripping tower 193 exports, also has the amine liquid of partial gasification.
Stripping tower 193 is provided with reboiler 194, and reboiler 194 is arranged on the bottom of stripping tower 193.The rich solution of reboiler 194 to purification heats.
The rich solution of amine liquid Ethylene recov and purification is carried out heat exchange by step S213, use heat exchanger 193.
In this step, higher from the temperature of the amine liquid Ethylene recov of stripping tower 193 conveying, the temperature of the rich solution of purification can be improved after carrying out heat exchange with the rich solution of the purification being delivered to stripping tower 193, save energy.Amine liquid Ethylene recov through heat exchange is lowered the temperature by step S214, use amine liquid Ethylene recov water cooler 195 further.
Step S215, use amine liquid Ethylene recov surge tank 196 carry out buffered to the amine liquid Ethylene recov through cooling further and are delivered to washing tower 166.
Use amine liquid Ethylene recov surge tank 196 can play voltage stabilizing, current stabilization to amine liquid Ethylene recov to the amine liquid Ethylene recov buffered through cooling further, safer when making it be delivered to washing tower 166.
Concrete, the amine liquid Ethylene recov in amine liquid Ethylene recov surge tank 196 is delivered to washing tower 166 by amine liquid pump (not shown).
Further, in step S212, use stripping tower 193 foreign gas removed in the rich solution of purification to be formed in the process of amine liquid Ethylene recov, also generate the gas of the amine liquid containing foreign gas and gasification, the process of this gas is comprised the following steps:
Step S310, the gas exported by stripping tower 193 use water cooler 197 cooling to make the amine liquid condensing of gas vaporization become amine liquid.
The amine liquid of the foreign gas that water cooler 197 exports by step S320, use amine separator 198 and again post liquefaction is separated.
In present embodiment, after the gas using amine separator 198 to be exported by water cooler 197 and amine liquid are separated, foreign gas is emptying.
Step S330, use amine surge tank 199 pairs of amine liquid carry out buffered and amine liquid are delivered to amine liquid Ethylene recov surge tank 196.
Certainly, amine surge tank 199 pairs of amine liquid also can be used to carry out buffered and be directly delivered in washing tower 166 by amine liquid.
Above-mentioned biogas purification method is by one-level entrance separator 110, remove solids in biogas and portion of water forms the first purifying marsh gas, first purifying marsh gas can be compressed to 0.1Mpa ~ 0.8Mpa by stage compressor 120 and form the first compressed biogas, first compressed biogas can be compressed to 2.5Mpa ~ 8Mpa by two stage compressor 150 again and form the second compressed biogas, the solids in the second compressed biogas is removed by secondary inlet separator 164 and washing tower 166, the biogas after purifying is obtained after the impurity such as moisture and carbonic acid gas, thus effectively can improve methane content of bilogas, methane content of bilogas can be increased to 95%(percent by volume by this methane purifying system) more than, can as the fuel of gasfueled vehicles, compared to traditional firedamp gas equipment, effectively widen the use range of biogas.
By three second compression, namely gaseous tension is promoted to target pressure range by gradation, so every stage compressor is less, cost is lower, and meanwhile, the pressurized vessel after every stage compressor makes according to pressure range, avoid putting in place according to first compression, the compressor used will be very huge, and price is very expensive, thus can reduce costs; In addition, from the beginning pressure is risen to goal pressure, equipment all thereafter all must make according to this pressure rank, and cost is very large, and has great potential safety hazard, uses the mode of three stage compression compression to improve security, reduces equipment cost.
The foreign gas generation amine liquid Ethylene recov adsorbed in the amine liquid of foreign gas that above-mentioned biogas purification method exports by removing washing tower 166, can recycle amine liquid, improve the utilising efficiency of amine liquid, reduce cost.
Be appreciated that step S130 can omit.Step S180 also can omit, and the biogas now after the purification that washing tower 166 purifies directly outputs to three-stage compressor 180.Step S190 and step S200 also can omit, and the biogas now after the purification that washing tower 166 processes directly can be used as other purposes.When oxygen level in biogas and nitrogen content lower time, step S140 can omit.Step S213 also can omit, and the rich solution of the purification of now flash tank 191 output is directly delivered to stripping tower 193, and the foreign gas that stripping tower 193 removes in the rich solution of purification forms amine liquid Ethylene recov and is delivered to amine liquid Ethylene recov water cooler 195.Step S214 also can omit, and the amine liquid Ethylene recov that now stripping tower 193 exports directly is delivered to amine liquid Ethylene recov surge tank 196.Step S215 also can omit, and the amine liquid Ethylene recov that now stripping tower 193 exports directly is delivered to washing tower 166.Step S310, step S320 and step S330 also can omit, and the gas now exported from stripping tower 193 can be discharged with additive method.Simultaneously, above-mentioned biogas purification method is not limited to adopt the above-mentioned order listed to perform, such as step S210 is not limited to perform after step S180, step S190 and step S200, also synchronously can perform with step S180, step S190 or step S200, step S310 also synchronously can perform with step S213, step S214 or step S215.
The parameter value of the following table gas that to be methane purifying system export at a use procedure Raw and each main device
Table 1 biogas source of the gas parameter
| Ingredient names | Volume content (%) | Other parameters | Parameter value |
| Methane | 65 | Temperature | 30℃ |
| Nitrogen | 2.3 | Pressure | 0.02Mpa |
| Carbonic acid gas | 29.7 | ||
| Hydrogen sulfide | 1.7 | ||
| Water vapour | 0.45 | ||
| Oxygen | 0.4 | ||
| Hydrogen | 0.45 |
The parameter of the first compressed biogas that table 2 stage compressor outlet exports
| Ingredient names | Volume content (%) | Other parameters | Parameter value |
| Methane | 65 | Temperature | 45℃ |
| Nitrogen | 2.3 | Pressure | 0.7Mpa |
| Carbonic acid gas | 29.7 | ||
| Hydrogen sulfide | 1.7 | ||
| Water vapour | 0.45 | ||
| Oxygen | 0.4 | ||
| Hydrogen | 0.45 |
The parameter being stripped of the first compressed biogas of oxygen that table 3 deoxidation-nitrogen tower outlet exports
| Ingredient names | Volume content (%) | Other parameters | Parameter value |
| Methane | 65.26 | Temperature | 60℃ |
| Nitrogen | 2.31 | Pressure | 0.65Mpa |
| Carbonic acid gas | 29.82 | ||
| Hydrogen sulfide | 1.71 | ||
| Water vapour | 0.45 | ||
| Oxygen | 0 | ||
| Hydrogen | 0.45 |
The parameter of the second compressed biogas that the outlet of table 4 two stage compressor exports
| Ingredient names | Volume content (%) | Other parameters | Parameter value |
| Methane | 65.26 | Temperature | 60℃ |
| Nitrogen | 2.31 | Pressure | 5Mpa |
| Carbonic acid gas | 29.82 | ||
| Hydrogen sulfide | 1.71 | ||
| Water vapour | 0.45 | ||
| Oxygen | 0 | ||
| Hydrogen | 0.45 |
The parameter of the biogas after the purification that the outlet of table 5 washing tower exports
| Ingredient names | Volume content (%) | Other parameters | Parameter value |
| Methane | 95.33 | Temperature | 41.62℃ |
| Nitrogen | 3.44 | Pressure | 4.45Mpa |
| Carbonic acid gas | 0.36 | ||
| Hydrogen sulfide | 0 | ||
| Water vapour | 0.21 | ||
| Oxygen | 0 | ||
| Hydrogen | 0.66 |
The parameter of the High-pressure Marsh Gas that table 6 three-stage compressor exports
| Ingredient names | Volume content (%) | Other parameters | Parameter value |
| Methane | 95.33 | Temperature | 65℃ |
| Nitrogen | 3.44 | Pressure | 25.6Mpa |
| Carbonic acid gas | 0.36 | ||
| Hydrogen sulfide | 0 | ||
| Water vapour | 0.21 | ||
| Oxygen | 0 | ||
| Hydrogen | 0.66 |
As can be seen from table 5 and table 6, in the biogas after purification and High-pressure Marsh Gas, the volume content of methane is 95.33%, and in table 1, the volume content 65% of methane in sewage gas is enhanced.
The above embodiment only have expressed several embodiment of the present invention, and it describes comparatively concrete and detailed, but therefore can not be interpreted as the restriction to the scope of the claims of the present invention.It should be pointed out that for the person of ordinary skill of the art, without departing from the inventive concept of the premise, can also make some distortion and improvement, these all belong to protection scope of the present invention.Therefore, the protection domain of patent of the present invention should be as the criterion with claims.
Claims (10)
1. a methane purifying system, is characterized in that, comprising:
One-level entrance separator, for remove biogas source produce biogas in solids and moisture form the first purifying marsh gas;
Stage compressor, is communicated with described one-level entrance separator, forms the first compressed biogas for compressing described first purifying marsh gas;
Deoxidation-nitrogen tower, described deoxidation-nitrogen tower is communicated with described stage compressor, for removing from the oxygen described first compressed biogas that described stage compressor exports and at least one in nitrogen, described deoxidation-nitrogen tower is a kind of tower equipment of one for removing oxygen or the nitrogen contained in biogas, its structure is the subsequent application filler according to grid-ceramic bead-stainless (steel) wire-sorbent material-stainless (steel) wire-ceramic bead-grid in tower, described sorbent material is fixed on bed, gas bottom in and top out;
Two stage compressor, is communicated with described deoxidation-nitrogen tower, for described first compressed biogas compression formation second compressed biogas being stripped of at least one in oxygen and nitrogen will exported from described deoxidation-nitrogen tower;
Secondary inlet separator, is communicated with described two stage compressor, for removing solids in described second compressed biogas and moisture forms the second purifying marsh gas;
Washing tower, is communicated with described secondary inlet separator, obtains the biogas after purifying and adsorbed the amine liquid of foreign gas for using the amine liquid foreign gas removed in described second purifying marsh gas;
Level 2 buffering tank, described level 2 buffering tank is communicated with described washing tower, for cushioning the pressure of the biogas after purification;
Three-stage compressor, described three-stage compressor is communicated with described level 2 buffering tank, for from Marsh gas compression to the 15 ~ 30Mpa after the described purification of described level 2 buffering tank output, forming High-pressure Marsh Gas;
Biogas storage device, described biogas storage device is communicated with described three-stage compressor, for the described High-pressure Marsh Gas that filling described three-stage compressor compression is formed; And
Amine liquid recycle unit, is communicated with described washing tower, obtains amine liquid Ethylene recov, and amine liquid Ethylene recov is delivered to described washing tower for removing described foreign gas of having adsorbed in the amine liquid of foreign gas;
Also comprise the booster fan be arranged on before one-level entrance separator.
2. methane purifying system according to claim 1, is characterized in that, described amine liquid recycle unit comprises flash tank and stripping tower; Described flash tank is communicated with described washing tower, for removing the rich solution that described at least part of foreign gas of having adsorbed in the amine liquid of foreign gas is purified; Described stripping tower is communicated with described flash tank and described washing tower, and described stripping tower forms amine liquid Ethylene recov for the foreign gas removed in the rich solution of described purification, and described amine liquid Ethylene recov is delivered to described washing tower.
3. methane purifying system according to claim 2, it is characterized in that, described amine liquid recycle unit also comprises the heat exchanger be communicated with described flash tank and described stripping tower, described stripping tower is provided with reboiler, and the rich solution of the purification that the amine liquid Ethylene recov exported from described reboiler and described flash tank export carries out heat exchange by described heat exchanger.
4. methane purifying system according to claim 3, it is characterized in that, described amine liquid recycle unit also comprises amine liquid Ethylene recov water cooler, is communicated with described heat exchanger and described washing tower, for lowering the temperature further to the amine liquid Ethylene recov through heat exchange and output to described washing tower.
5. methane purifying system according to claim 2, is characterized in that, described amine liquid recycle unit also comprises:
Water cooler, is communicated with described stripping tower, and the gas for being exported by described stripping tower carries out cooling the amine liquid condensing making to gasify in gas and becomes amine liquid;
Amine separator, is communicated with described water cooler and described washing tower, and the amine liquid for the foreign gas that exported by water cooler and post liquefaction is again separated;
Amine liquid Ethylene recov surge tank, is communicated with described amine separator, described stripping tower and described washing tower, the amine liquid Ethylene recov that amine liquid and described stripping tower for accommodating the generation of amine separator generate, and described amine liquid and amine liquid Ethylene recov are delivered to described washing tower.
6. use a biogas purification method for the methane purifying system described in any one of claim 1 ~ 5, it is characterized in that, comprise the following steps:
One-level entrance separator is used to remove solids in biogas and moisture forms the first purifying marsh gas; Described first purifying marsh gas of stage compressor compression is used to form the first compressed biogas;
Deoxidation-nitrogen tower is used to remove the oxygen in the first compressed biogas and at least one in nitrogen, described deoxidation-nitrogen tower is a kind of tower equipment of one for removing oxygen or the nitrogen contained in biogas, its structure is the subsequent application filler according to grid-ceramic bead-stainless (steel) wire-sorbent material-stainless (steel) wire-ceramic bead-grid in tower, described sorbent material is fixed on bed, gas bottom in and top out;
Described first compressed biogas using two stage compressor compression to be stripped of oxygen forms the second compressed biogas;
Secondary inlet separator is used to remove solids in described second compressed biogas and moisture forms the second purifying marsh gas;
In washing tower, use the amine liquid foreign gas removed in described second purifying marsh gas to obtain the biogas after purifying and adsorbed the amine liquid of foreign gas;
Level 2 buffering tank is used to carry out buffered to the biogas after purification;
Biogas after using three-stage compressor compression to purify forms High-pressure Marsh Gas;
Use the filling High-pressure Marsh Gas of biogas storage device; And
Use amine liquid recycle unit to remove described foreign gas of having adsorbed in the amine liquid of foreign gas and obtain amine liquid Ethylene recov, and described amine liquid Ethylene recov is delivered to described washing tower;
Use one-level entrance separator to remove also to comprise before solids in biogas and moisture form the first purifying marsh gas and pressurized treatment is carried out to biogas.
7. biogas purification method according to claim 6, is characterized in that, described use amine liquid recycle unit removes the step that described foreign gas of having adsorbed in the amine liquid of foreign gas obtains amine liquid Ethylene recov and is divided into following steps:
Use flash tank removes the rich solution that described at least part of foreign gas of having adsorbed in the amine liquid of foreign gas is purified;
Other foreign gases in the rich solution of the purification using stripping tower to be obtained by flash tank remove, and form amine liquid Ethylene recov, and described amine liquid Ethylene recov is delivered to described washing tower.
8. biogas purification method according to claim 7, is characterized in that, first the rich solution of described amine liquid Ethylene recov and described purification is carried out heat exchange before described amine liquid Ethylene recov is delivered to described washing tower.
9. biogas purification method according to claim 8, is characterized in that, is delivered to described washing tower by after the amine liquid Ethylene recov of heat exchange uses amine liquid Ethylene recov water cooler to lower the temperature further.
10. biogas purification method according to claim 7, is characterized in that, also comprises step:
The gas exported by described stripping tower uses water cooler cooling to make the amine condensation in gas become amine liquid;
The gas using amine separator to be exported by water cooler and amine liquid are separated, and amine liquid is delivered to washing tower.
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Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5642630A (en) * | 1996-01-16 | 1997-07-01 | Abdelmalek; Fawzy T. | Process for solids waste landfill gas treatment and separation of methane and carbon dioxide |
| US5681360A (en) * | 1995-01-11 | 1997-10-28 | Acrion Technologies, Inc. | Landfill gas recovery |
| CN1300635A (en) * | 2000-12-19 | 2001-06-27 | 中国冶金建设集团鞍山焦化耐火材料设计研究总院 | Process for removing CO2 and H2S from biological gas |
| CN1371893A (en) * | 2001-02-19 | 2002-10-02 | 张文慧 | Technological process and apparatus for preparing enriched methane gas by utilizing refuse marsh gas |
| CN101475859A (en) * | 2009-01-21 | 2009-07-08 | 东莞市康达机电工程有限公司 | Method and apparatus for preparing sulfur-free natural gas from methane |
| CN101544920A (en) * | 2009-05-07 | 2009-09-30 | 赵昱 | Process for preparing compressed natural gas by deodorizing and purifying landfill gas |
| CN102086417A (en) * | 2009-12-02 | 2011-06-08 | 青岛天人环境股份有限公司 | Method for purifying marsh gas and recovering elemental sulfur and carbon dioxide |
| CN202131295U (en) * | 2011-07-15 | 2012-02-01 | 王仕华 | System for preparing compressed natural gas by methane |
| CN102559316A (en) * | 2011-12-31 | 2012-07-11 | 浙江工业大学 | Methane purifying method and equipment thereof |
| JP5112665B2 (en) * | 2006-09-05 | 2013-01-09 | 神戸市 | Digestion gas purification method and purification apparatus in digestion gas utilization system |
-
2013
- 2013-02-01 CN CN201310041298.6A patent/CN103113945B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5681360A (en) * | 1995-01-11 | 1997-10-28 | Acrion Technologies, Inc. | Landfill gas recovery |
| US5642630A (en) * | 1996-01-16 | 1997-07-01 | Abdelmalek; Fawzy T. | Process for solids waste landfill gas treatment and separation of methane and carbon dioxide |
| CN1300635A (en) * | 2000-12-19 | 2001-06-27 | 中国冶金建设集团鞍山焦化耐火材料设计研究总院 | Process for removing CO2 and H2S from biological gas |
| CN1371893A (en) * | 2001-02-19 | 2002-10-02 | 张文慧 | Technological process and apparatus for preparing enriched methane gas by utilizing refuse marsh gas |
| JP5112665B2 (en) * | 2006-09-05 | 2013-01-09 | 神戸市 | Digestion gas purification method and purification apparatus in digestion gas utilization system |
| CN101475859A (en) * | 2009-01-21 | 2009-07-08 | 东莞市康达机电工程有限公司 | Method and apparatus for preparing sulfur-free natural gas from methane |
| CN101544920A (en) * | 2009-05-07 | 2009-09-30 | 赵昱 | Process for preparing compressed natural gas by deodorizing and purifying landfill gas |
| CN102086417A (en) * | 2009-12-02 | 2011-06-08 | 青岛天人环境股份有限公司 | Method for purifying marsh gas and recovering elemental sulfur and carbon dioxide |
| CN202131295U (en) * | 2011-07-15 | 2012-02-01 | 王仕华 | System for preparing compressed natural gas by methane |
| CN102559316A (en) * | 2011-12-31 | 2012-07-11 | 浙江工业大学 | Methane purifying method and equipment thereof |
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