CN103113945A - 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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- CN103113945A CN103113945A CN2013100412986A CN201310041298A CN103113945A CN 103113945 A CN103113945 A CN 103113945A CN 2013100412986 A CN2013100412986 A CN 2013100412986A CN 201310041298 A CN201310041298 A CN 201310041298A CN 103113945 A CN103113945 A CN 103113945A
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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 the field, particularly relate to a kind of methane purifying system and biogas purification method.
Background technology
Biogas is the organic a kind of inflammable gas that under anaerobic produces through microbial fermentation, 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), the hydrogen (H less than 1%
2), the oxygen (O less than 0.4%
2) and 0.1% ~ 3% hydrogen sulfide (H
2The gas composition such as S).
The biogas calorific value is high, pollutes less, and be a kind of clean energy.China began to apply in nineteen twenties, had obtained at present encouraging success.But traditional biogas source, such as methane-generating pit, the content of the methane in sewage gas of generation is lower, has limited the use of biogas.
Summary of the invention
Based on this, be necessary to provide a kind of methane purifying system and biogas purification method that improves methane content of bilogas.
A kind of methane purifying system comprises:
The one-level entrance separator is for solids and moisture formation first purifying marsh gas of the biogas that removes biogas source generation;
One stage compressor is communicated with described one-level entrance separator, is used for compressing described the first purifying marsh gas and forms the first compressed biogas;
Two stage compressor is communicated with a described stage compressor, is used for compressing described the first compressed biogas and forms the second compressed biogas;
The secondary entrance separator is communicated with described two stage compressor, is used for removing solids and moisture formation second purifying marsh gas of described the second compressed biogas;
Washing tower is communicated with described secondary entrance separator, the biogas after foreign gas that be used for to use amine liquid to remove described the second purifying marsh gas is purified and adsorbed the amine liquid of foreign gas; And
Amine liquid recycle unit is communicated with described washing tower, is used for removing described foreign gas of having adsorbed the amine liquid of foreign gas and obtains amine liquid recovery liquid, and amine liquid recovery liquid is delivered to described washing tower.
In embodiment, described amine liquid recycle unit comprises flash tank and stripping tower therein; Described flash tank is communicated with described washing tower, is used for removing the rich solution that described at least part of foreign gas of having adsorbed 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 recovery liquid for the foreign gas of the rich solution that removes described purification, and described amine liquid recovery liquid is delivered to described washing tower.
Therein in embodiment, described amine liquid recycle unit also comprises the heat exchanger that is communicated with described flash tank and described stripping tower, described stripping tower is provided with reboiler, and the rich solution that reclaims the purification that liquid and described flash tank export from the amine liquid of described reboiler output carries out heat exchange by described heat exchanger.
In embodiment, described amine liquid recycle unit comprises that also amine liquid reclaims the liquid water cooler, is communicated with described heat exchanger and described washing tower therein, is used for the amine liquid recovery liquid through heat exchange is further lowered the temperature and outputed to described washing tower.
In embodiment, described amine liquid recycle unit also comprises therein:
Water cooler is communicated with described stripping tower, is used for gas with described stripping tower output and carries out coolingly making the amine liquid condensing that gas gasifies become amine liquid;
The amine separator is communicated with described water cooler and described washing tower, is used for the foreign gas of water cooler output and the amine liquid separation after again liquefying;
Amine liquid recovery liquid surge tank is communicated with described amine separator, described stripping tower and described washing tower, is used for accommodating the amine liquid of amine separator generation and the amine liquid recovery liquid of described stripping tower generation, and described amine liquid and amine liquid recovery liquid are delivered to described washing tower.
A kind of biogas purification method that uses above-mentioned methane purifying system comprises the following steps:
The solids and the moisture that use the one-level entrance separator to remove in biogas form the first purifying marsh gas; Use described the first purifying marsh gas of one-level compressor compresses to form the first compressed biogas;
Use described the first compressed biogas of two stage compressor compression to form the second compressed biogas;
The solids and the moisture that use the secondary entrance separator to remove in described the second compressed biogas form the second purifying marsh gas;
Biogas after using amine liquid to remove foreign gas in described the second purifying marsh gas in washing tower to be purified and adsorbed the amine liquid of foreign gas; And
Use amine liquid recycle unit to remove foreign gas in the described amine liquid that has adsorbed foreign gas and obtain amine liquid and reclaim liquid, and described amine liquid is reclaimed liquid be delivered to described washing tower.
Therein in embodiment, described use amine liquid recycle unit removes foreign gas in the described amine liquid that has adsorbed foreign gas and obtains the step that amine liquid reclaims liquid and be divided into following steps:
Use flash tank to remove the rich solution that at least part of foreign gas in the described amine liquid that has adsorbed foreign gas is purified;
Use other foreign gases in the rich solution that stripping tower is purified flash tank to remove, form amine liquid and reclaim liquid, and described amine liquid is reclaimed liquid be delivered to described washing tower.
Therein in embodiment, described amine liquid is reclaimed liquid be delivered to the rich solution that first described amine liquid is reclaimed liquid and described purification before described washing tower and carry out heat exchange.
Therein in embodiment, will reclaim through the amine liquid of heat exchange liquid and use amine liquid to reclaim the liquid water cooler further to be delivered to described washing tower after cooling.
In embodiment, also comprise step therein:
The gas of described stripping tower output is used water cooler is cooling makes the amine condensation in gas become amine liquid;
Use the amine separator that gas and the amine liquid of water cooler output are separated, and amine liquid is delivered to washing tower.
above-mentioned methane purifying system and biogas purification method, by the one-level entrance separator, the solids and the part moisture that remove in biogas form the first purifying marsh gas, the first purifying marsh gas can be compressed to 0.1Mpa ~ 0.8Mpa by a stage compressor and form the first compressed biogas, the first compressed biogas can be compressed to 2.5Mpa ~ 8Mpa by two stage compressor again and form the second compressed biogas, remove solids in the second compressed biogas by secondary entrance separator and washing tower, biogas after being purified after the impurity such as moisture and carbonic acid gas, thereby can effectively improve methane content of bilogas, this methane purifying system can be increased to methane content of bilogas the 95%(percent by volume) more than, can be used as the fuel of gasfueled vehicles, than traditional firedamp gas equipment, effectively widened the use range of biogas, simultaneously, amine liquid recycle unit can be recycled amine liquid, can reduce costs.
Description of drawings
Fig. 1 is the structural representation of the methane purifying system of an embodiment.
Embodiment
For above-mentioned purpose of the present invention, feature and advantage can be become apparent more, below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in detail.A lot of details have been set forth in the following description so that fully understand the present invention.But the present invention can implement much to be different from alternate manner described here, and those skilled in the art can be in the situation that do similar improvement without prejudice to intension of the present invention, so the present invention is not subjected to the restriction of following public concrete enforcement.
Need to prove, when element is called as " being fixedly arranged on " another element, can directly can there be 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 have simultaneously centering elements.Term as used herein " vertical ", " level ", " left side ", " right side " and similar statement are just for illustrative purposes.
Unless otherwise defined, all technology of using of this paper and scientific terminology are with to belong to the implication that those skilled in the art of the present invention understand usually identical.The term that uses in specification sheets of the present invention herein is not intended to be restriction the present invention just in order to describe the purpose of specific embodiment.Term as used herein " and/or " comprise one or more relevant Listed Items arbitrarily with all combinations.
See also Fig. 1, the methane purifying system 10 of one embodiment comprises one-level entrance separator 110, a stage compressor 120, first-level buffer tank 130, deoxidation-nitrogen tower 140, two stage compressor 150, secondary entrance 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, and the solids and the moisture that are used for removing the biogas that biogas source 90 produces 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 entered one-level entrance separator 110, obviously solid phase particles was settlement separate for part, and the solid phase particles of part greater particle size separates by the whirlwind runner with liquid-phase particle, and less solid-liquid particle separates by the silk screen bed.
Need to prove, biogas source 90 is used for providing biogas.Biogas source 90 can be the methane-generating pit of self-assembling formation, can be also the biogas generation apparatus such as the artificial mathane generating pool of building or industrialized tank for sewage gas, is not construed as limiting at this, as long as can produce biogas.
One stage compressor 120 is communicated with one-level entrance separator 110, is used for compression the first purifying marsh gas and forms the first compressed biogas.In present embodiment, a stage compressor 120 is compressed to 0.1Mpa ~ 0.8Mpa with the first purifying marsh gas.Certainly, in other embodiments, the air pressure of the first compressed biogas also can be adjusted as required.Need to prove, in other embodiments, can also between biogas source 90 and one-level entrance separator 110, the booster fan (not shown) be set, can improve the air pressure of the biogas that enters one-level entrance separator 110, the unstripped gas quality that enters a stage compressor is improved, thereby extend the work-ing life of a stage compressor 120.
First-level buffer tank 130 is communicated with a stage compressor 120, is used for cushioning the pressure of the first compressed biogas that obtains after processing through a stage compressor 120.First-level buffer tank 130 can play voltage stabilizing, current stabilization to the first compressed biogas, plays the effect of balance flow process material, and is safer when making the first compressed biogas be formed the second compressed biogas by two stage compressor 150 compressions.
Deoxidation-nitrogen tower 140 is communicated with first-level buffer tank 130, is used for removing a kind of from the oxygen of the firstth compressed biogas of first-level buffer tank 130 outputs and nitrogen.Deoxidation-nitrogen tower is a kind of a kind of tower equipment for removing the oxygen (perhaps nitrogen) that biogas contains.Its similar in: settle filler, gas bottom in and top out according to the order of grid-ceramic bead-stainless (steel) wire-sorbent material (being fixed on bed)-stainless (steel) wire-ceramic bead-grid in tower.If to remove oxygen as main, can adopt iron is that compound adsorbent, manganese are compound adsorbent or acticarbon, being preferably iron is compound adsorbent; If to remove nitrogen as main, can select fluosilicic stone sorbent material (or fluosilicic stone molecular sieve), perhaps active aluminum ball (Al
2O
3), if want oxygen nitrogen all to remove, should determine different sorbent materials according to each gaseous fraction, carry out proportioning and feed intake.
Two stage compressor 150 is communicated with deoxidation-nitrogen tower 140, is used for forming the second compressed biogas from the first at least a compressed biogas compression that has removed oxygen and nitrogen of deoxidation-nitrogen tower 140 outputs.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 be adjusted as required.
Level 2 buffering tank 170 is communicated with washing tower 166, is used for the pressure of the biogas after buffering is purified.Level 2 buffering tank 170 can play voltage stabilizing, current stabilization to the biogas after purifying, and is safer when making biogas after purification be formed High-pressure Marsh Gas by three-stage compressor 180 compressions.
Three-stage compressor 180 is communicated with level 2 buffering tank 170, is used for from the Marsh gas compression to 15 after the purification of level 2 buffering tank 170 outputs ~ 30Mpa, forming High-pressure Marsh Gas.
Biogas storage device 185 is communicated with three-stage compressor 180, is used for the High-pressure Marsh Gas that 180 compressions of can three-stage compressor form.Biogas storage device 185 is hold-up vessel or storage bottle.
Amine liquid recycle unit 190 comprises that throttling valve 182, flash tank 191, heat exchanger 192, stripping tower 193, amine liquid reclaim liquid water cooler 195, amine liquid reclaims liquid surge tank 196, water cooler 197, amine separator 198 and amine surge tank 199.
Flash tank 191 is communicated with throttling valve 182, is used for removing at least part of foreign gas of the amine liquid that has adsorbed foreign gas, the rich solution that is purified.Foreign gas is the impurity such as carbonic acid gas, moisture and hydrogen sulfide.In the rich solution that purifies, the decreasing ratio of foreign gas is about 30%.
Amine liquid reclaims liquid water cooler 195 and is communicated with heat exchanger 192, is used for that the amine liquid through heat exchange is reclaimed liquid and further lowers the temperature.
Amine liquid reclaims liquid surge tank 196 and is communicated with amine liquid recovery liquid water cooler 195.Amine liquid reclaims liquid surge tank 196 and is communicated with washing tower 166 by amine liquid pump (not shown).Amine liquid reclaims liquid surge tank 196 and is used for cushioning the further amine liquid recovery liquid of cooling of process amine liquid recovery liquid water cooler 195, and by the amine liquid pump, it is delivered to washing tower 166.Amine liquid reclaims liquid surge tank 196 and is provided with amine liquid interpolation mouth, and this adds mouth and is used for interpolation and additional amine liquid.Amine liquid reclaims liquid surge tank 196 can play voltage stabilizing, current stabilization to reclaiming liquid through amine liquid recovery liquid water cooler 195 further amine liquid of lowering the temperature, safer when making it be delivered to washing tower 166.
Further, methane purifying system 10 also comprises sledge-borne type casing (not shown), and one-level entrance separator 110, a stage compressor 120, first-level buffer tank 130, deoxidation-nitrogen tower 140, two stage compressor 150, secondary entrance separator 164, washing tower 166, level 2 buffering tank 170, three-stage compressor 180 and biogas storage device 185 are arranged in the sledge-borne type casing.Methane purifying system 10 can move comparatively easily, transport like this.Certainly, in the situation that treatment capacity less (40000 cubic metres/day), each device of native system can be integrated in a sledge-borne type casing, but in the situation that high throughput, a unit of possible native system or several unit independently become sled, whole system can have by a plurality of sleds and is combined into, from not difference of function.
above-mentioned methane purifying system, solids and the part moisture that can remove in the first compressed biogas by one-level entrance separator 110 obtain the first purifying marsh gas, the first class purification Marsh gas compression can be formed the first compressed biogas to 0.1Mpa ~ 0.8Mpa by a stage compressor 120, the first purifying marsh gas can be compressed to 2.5Mpa ~ 8Mpa by two stage compressor 150 again and form the second compressed biogas, remove solids in the second compressed biogas by secondary entrance separator 164 and washing tower 166, biogas after being purified after the impurity such as moisture and carbonic acid gas, this methane purifying system can be increased to methane content of bilogas the 95%(percent by volume) more than, make the content of methane in sewage gas higher, with the can to the high-pressure cylinder of the Marsh gas compression after purifying, can be used as the fuel of gasfueled vehicles, effectively widened the use range of biogas.
This methane purifying system compressed biogas terminal pressure scope is at 15Mpa ~ 30Mpa, three grades of compressions have been adopted, use a stage compressor 120, two stage compressor 150 and three-stage compressor 180 threes to coordinate, be that gradation is promoted to the goal pressure scope with gaseous tension, every like this stage compressor is less, cost is lower, simultaneously, pressurized vessel after every stage compressor is made according to pressure range and is got final product, if avoid adopting first compression to put in place, the compressor that uses will be very huge, and price is very expensive, thereby can reduce costs; In addition, from the beginning pressure is risen to goal pressure, all equipment all must be made according to this pressure rank thereafter, and cost is very large, and has great potential safety hazard, uses the mode of three grades of compression compressions can improve security, reduces equipment cost.
The above-mentioned methane purifying system of washing tower is by arranging amine liquid recycle unit 190, can remove washing tower 166 output absorption the foreign gas in the amine liquid of foreign gas generate amine liquid and reclaim liquid, can recycle amine liquid, improve the utilising efficiency of amine liquid, reduce cost.
Be appreciated that, when the biogas throughput ratio of 90 outputs from the biogas source is more steady, first-level buffer tank 130 can omit, this moment, deoxidation-nitrogen tower 140 was communicated with a stage compressor 120, the first compressed biogas directly is passed into deoxidation-nitrogen tower, if when in the biogas that biogas source 90 produces, oxygen level was low, deoxidation-nitrogen tower 140 can omit, one stage compressor 120 directly was communicated with two stage compressor 150 and got final product this moment.Level 2 buffering tank 170 also can omit, and this moment, washing tower 166 and three-stage compressor 180 were communicated with, and the biogas after purifying through washing tower 166 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 purify this moment can directly be used as other purposes.When from the absorption of washing tower 166 output foreign gas the amine flow velocity steadily and flow when little, throttling valve 182 also can omit, this moment, washing tower 166 and flash tank 191 were communicated with.Heat exchanger 192 also can omit, and this moment, flash tank 191 and stripping tower 193 were communicated with, and the rich solution of the purification of flash tank 191 outputs directly is delivered to stripping tower 193 and removes wherein foreign gas.Stripping tower 193 reclaims liquid water cooler 195 with amine liquid and is communicated with.Amine liquid reclaims liquid water cooler 195 and also can omit, and this moment, stripping tower 193 and amine liquid reclaimed 196 connections of liquid surge tank, and stripping tower 193 is delivered to amine liquid with amine liquid recovery liquid and reclaims liquid surge tank 196.Amine liquid reclaims liquid surge tank 196 and also can omit, and this moment, stripping tower 193 and washing tower 166 were communicated with, and stripping tower 193 reclaims liquid with amine liquid and is delivered to washing tower 166.Water cooler 197, amine separator 198 and amine surge tank 199 also can omit, and can with additive method discharge from the gas of stripping tower 193 outputs this moment.
Please refer to Fig. 1, the biogas purification method of an embodiment comprises the following steps:
Step S110, the solids and the moisture that use one-level entrance separator 110 to remove in biogas form 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, can be also the biogas generation apparatus such as the artificial mathane generating pool of building or industrialized tank for sewage gas, is not construed as limiting at this, as long as can produce biogas.
Preferably, the dehydration rate of the first purifying marsh gas of process step S110 processing is more than 50%.
Need to prove, can also carry out pressurized treatment to biogas before step S110.In present embodiment, the air pressure of biogas is increased to be no more than 150kPa, thereby the unstripped gas quality is improved.
Step S120, use one stage compressor 120 compression the first purifying marsh gas 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 be adjusted as required.
Step S130,130 pairs of the first compressed biogas of use first-level buffer tank are carried out buffered.
The first compressed biogas is carried out buffered can play voltage stabilizing, current stabilization to the first compressed biogas.
Step S140, use deoxidation-nitrogen tower 140 to remove at least a in oxygen in the first compressed biogas and nitrogen.
Deoxidation-nitrogen tower is a kind of a kind of tower equipment for removing the oxygen (perhaps nitrogen) that biogas contains.Its similar in: settle filler, gas bottom in and top out according to the order of grid-ceramic bead-stainless (steel) wire-sorbent material (being fixed on bed)-stainless (steel) wire-ceramic bead-grid in tower.If to remove oxygen as main, can adopt iron is that compound adsorbent, manganese are compound adsorbent or acticarbon, being preferably iron is compound adsorbent; If to remove nitrogen as main, can select fluosilicic stone sorbent material (or fluosilicic stone molecular sieve), perhaps active aluminum ball (Al
2O
3), if want oxygen nitrogen all to remove, should determine different sorbent materials according to each gaseous fraction, carry out proportioning and feed intake.
Step S150, the first compressed biogas of using two stage compressor 150 compressions to remove 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 be adjusted as required.
Step S160, the solids and the moisture that use secondary entrance separator 164 to remove in the second compressed biogas form the second purifying marsh gas.
Preferably, in step S160, the dehydration rate of the second purifying marsh gas is more than 30%.
Step S170, the biogas after using amine liquid to remove foreign gas in the second purifying marsh gas in washing tower 166 to be purified and adsorbed the amine liquid of foreign gas.
In present embodiment, second purifying marsh gas that will purify through secondary entrance separator 164, the impurity such as the carbonic acid gas that uses washing tower 166 further to remove wherein to comprise and moisture, the biogas after being purified.
Biogas after step S180,170 pairs of purifications of use level 2 buffering tank carries out buffered.
Level 2 buffering tank 170 can play voltage stabilizing, current stabilization to the biogas after purifying, so that safer during the Marsh gas compression formation High-pressure Marsh Gas of three-stage compressor 180 after purifying.
After biogas input level 2 buffering tank 170 after purifying is carried out buffered, can also carry out following steps:
Step S190, the biogas that uses three-stage compressor 180 to compress after purifying form High-pressure Marsh Gas.
In present embodiment, the air pressure of High-pressure Marsh Gas is 15Mpa ~ 30Mpa.
Step S200, use biogas storage device 185 can High-pressure Marsh Gas.
Biogas after the purification of can be as the fuel of gasfueled vehicles.
Step S210, the foreign gas of using amine liquid recycle unit 190 to remove in the amine liquid that has adsorbed foreign gas obtain amine liquid recovery liquid, and amine liquid recovery liquid are 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 in the amine liquid that has adsorbed foreign gas is purified.
Specifically in the present embodiment, in the rich solution of purification, the decreasing ratio of foreign gas is about 30%.
Step S212, use other foreign gases in the rich solution of the purification that stripping tower 193 obtains flash tank to remove, form amine liquid and reclaim liquid.
Stripping tower 193 is communicated with flash tank 191 by heat exchanger 192.Stripping tower 193 is used for removing the foreign gas of rich solution that is delivered to the purification of stripping tower 193 by heat exchanger 192, makes to remove in the rich solution of the foreign gas self-purification in rich solution to form amine liquid and reclaim liquid.Not only contain the foreign gas in the rich solution that is adsorbed on purification in the gas of stripping tower 193 outputs, also have 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 194 pairs of purifications of reboiler heats.
Step S213, use heat exchanger 193 carry out heat exchange with the rich solution that amine liquid reclaims liquid and purification.
In this step, the temperature that the amine liquid of carrying from stripping tower 193 reclaims liquid is higher, carries out can improving after heat exchange the temperature of the rich solution of purification, save energy with the rich solution of the purification that is delivered to stripping tower 193.Step S214, use amine liquid reclaim liquid water cooler 195 and will further lower the temperature through the amine liquid recovery liquid of heat exchange.
Step S215, the amine liquid that uses amine liquid to reclaim the further cooling of 196 pairs of processes of liquid surge tank reclaim liquid to carry out buffered and it is delivered to washing tower 166.
The amine liquid recovery liquid buffered of using amine liquid to reclaim the further cooling of 196 pairs of processes of liquid surge tank can reclaim liquid to amine liquid and play voltage stabilizing, current stabilization, and is safer when making it be delivered to washing tower 166.
Concrete, the amine liquid recovery liquid that amine liquid reclaims in liquid surge tank 196 is delivered to washing tower 166 by amine liquid pump (not shown).
Further, in step S212, use stripping tower 193 to remove foreign gas in the rich solution of purification and form in the process that amine liquid reclaims liquid, also generate the gas of the amine liquid that contains foreign gas and gasification, the processing of this gas is comprised the following steps:
Step S310, the gas that stripping tower 193 is exported use the cooling amine liquid condensing of gas vaporization that makes of water cooler 197 to become amine liquid.
The amine liquid that step S320, the foreign gas of using amine separator 198 that water cooler 197 is exported reach after liquefaction again separates.
In present embodiment, foreign gas is emptying after using amine separator 198 that the gas of water cooler 197 outputs and amine liquid are separated.
Step S330,199 pairs of amine liquid of use amine surge tank carry out buffered and amine liquid are delivered to amine liquid reclaiming liquid surge tank 196.
Certainly, also can use 199 pairs of amine liquid of amine surge tank carry out buffered and amine liquid directly is delivered in washing tower 166.
above-mentioned biogas purification method is by one-level entrance separator 110, the solids and the part moisture that remove in biogas form the first purifying marsh gas, the first purifying marsh gas can be compressed to 0.1Mpa ~ 0.8Mpa by a stage compressor 120 and form the first compressed biogas, the first compressed biogas can be compressed to 2.5Mpa ~ 8Mpa by two stage compressor 150 again and form the second compressed biogas, remove solids in the second compressed biogas by secondary entrance separator 164 and washing tower 166, biogas after being purified after the impurity such as moisture and carbonic acid gas, thereby can effectively improve methane content of bilogas, this methane purifying system can be increased to methane content of bilogas the 95%(percent by volume) more than, can be used as the fuel of gasfueled vehicles, than traditional firedamp gas equipment, effectively widened the use range of biogas.
By three compressions, be that gradation is promoted to the goal pressure scope with gaseous tension, every like this stage compressor is less, cost is lower, and simultaneously, the pressurized vessel after every stage compressor is made according to pressure range and got final product, if avoid adopting first compression to put in place, the compressor that uses will be very huge, and price is very expensive, thereby can reduce costs; In addition, from the beginning pressure is risen to goal pressure, all equipment all must be made according to this pressure rank thereafter, and cost is very large, and has great potential safety hazard, uses the mode of three grades of compression compressions can improve security, reduces equipment cost.
The absorption of above-mentioned biogas purification method by removing washing tower 166 output the foreign gas in the amine liquid of foreign gas generate amine liquid and reclaim liquid, can recycle amine liquid, improved the utilising efficiency of amine liquid, reduced cost.
Be appreciated that step S130 can omit.Step S180 also can omit, and the biogas after the purification of process washing tower 166 purifications this moment directly outputs to three-stage compressor 180.Step S190 and step S200 also can omit, and the biogas after the purification of process washing tower 166 processing this moment can directly be used as other purposes.When oxygen level in biogas and nitrogen content were low, step S140 can omit.Step S213 also can omit, and the rich solution of the purification of flash tank 191 output this moment directly is delivered to stripping tower 193, and stripping tower 193 removes foreign gas in the rich solution of purification and forms amine liquid and reclaim liquid and it is delivered to amine liquid and reclaim liquid water cooler 195.Step S214 also can omit, and the amine liquid of stripping tower 193 outputs this moment reclaims liquid and directly is delivered to amine liquid recovery liquid surge tank 196.Step S215 also can omit, and the amine liquid of stripping tower 193 outputs this moment reclaims liquid and directly is delivered to washing tower 166.Step S310, step S320 and step S330 also can omit, and can with additive method discharge from the gas of stripping tower 193 outputs this moment.Simultaneously, above-mentioned biogas purification method is not limited to adopt the above-mentioned order of listing to carry out, such as step S210 is not limited to carry out after step S180, step S190 and step S200, also can synchronize with step S180, step S190 or step S200 and carry out, step S310 also can be synchronizeed with step S213, step S214 or step S215 and carried out.
Following table is methane purifying system at the parameter value of the gas of use procedure Raw and the output of each main device
Table 1 biogas source of the gas parameter
| The component title | 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 of table 2 one-level compressor outlet output
| The component title | 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 of first compressed biogas that has removed oxygen of table 3 deoxidation-nitrogen tower outlet output
| The component title | 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 of table 4 two stage compressor outlet output
| The component title | 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 of table 5 washing tower outlet output
| The component title | 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 of table 6 three-stage compressor output
| The component title | 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 | ? | ? |
Can find out 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 the volume content 65% of methane in sewage gas is enhanced in the table 1.
The above embodiment has only expressed several embodiment of the present invention, and it describes comparatively concrete and detailed, but can not therefore be interpreted as the restriction to the scope of the claims of the present invention.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:
The one-level entrance separator is for solids and moisture formation first purifying marsh gas of the biogas that removes biogas source generation;
One stage compressor is communicated with described one-level entrance separator, is used for compressing described the first purifying marsh gas and forms the first compressed biogas;
Two stage compressor is communicated with a described stage compressor, is used for compressing described the first compressed biogas and forms the second compressed biogas;
The secondary entrance separator is communicated with described two stage compressor, is used for removing solids and moisture formation second purifying marsh gas of described the second compressed biogas;
Washing tower is communicated with described secondary entrance separator, the biogas after foreign gas that be used for to use amine liquid to remove described the second purifying marsh gas is purified and adsorbed the amine liquid of foreign gas; And
Amine liquid recycle unit is communicated with described washing tower, is used for removing described foreign gas of having adsorbed the amine liquid of foreign gas and obtains amine liquid recovery liquid, and amine liquid recovery liquid is delivered to described washing tower.
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, is used for removing the rich solution that described at least part of foreign gas of having adsorbed 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 recovery liquid for the foreign gas of the rich solution that removes described purification, and described amine liquid recovery liquid 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 that is communicated with described flash tank and described stripping tower, described stripping tower is provided with reboiler, and the rich solution that reclaims the purification that liquid and described flash tank export from the amine liquid of described reboiler output 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 comprises that also amine liquid reclaims the liquid water cooler, is communicated with described heat exchanger and described washing tower, is used for that the amine liquid through heat exchange is reclaimed liquid and further lowers the temperature 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, is used for gas with described stripping tower output and carries out coolingly making the amine liquid condensing that gas gasifies become amine liquid;
The amine separator is communicated with described water cooler and described washing tower, is used for the foreign gas of water cooler output and the amine liquid separation after again liquefying;
Amine liquid recovery liquid surge tank is communicated with described amine separator, described stripping tower and described washing tower, is used for accommodating the amine liquid of amine separator generation and the amine liquid recovery liquid of described stripping tower generation, and described amine liquid and amine liquid recovery liquid are delivered to described washing tower.
6. the biogas purification method of right to use requirement 1 ~ 5 described methane purifying system of any one, is characterized in that, comprises the following steps:
The solids and the moisture that use the one-level entrance separator to remove in biogas form the first purifying marsh gas; Use described the first purifying marsh gas of one-level compressor compresses to form the first compressed biogas;
Use described the first compressed biogas of two stage compressor compression to form the second compressed biogas;
The solids and the moisture that use the secondary entrance separator to remove in described the second compressed biogas form the second purifying marsh gas;
Biogas after using amine liquid to remove foreign gas in described the second purifying marsh gas in washing tower to be purified and adsorbed the amine liquid of foreign gas; And
Use amine liquid recycle unit to remove foreign gas in the described amine liquid that has adsorbed foreign gas and obtain amine liquid and reclaim liquid, and described amine liquid is reclaimed liquid be delivered to described washing tower.
7. biogas purification method according to claim 6, is characterized in that, described use amine liquid recycle unit removes foreign gas in the described amine liquid that has adsorbed foreign gas and obtains the step that amine liquid reclaims liquid and be divided into following steps:
Use flash tank to remove the rich solution that at least part of foreign gas in the described amine liquid that has adsorbed foreign gas is purified;
Use other foreign gases in the rich solution of the purification that stripping tower obtains flash tank to remove, form amine liquid and reclaim liquid, and described amine liquid is reclaimed liquid be delivered to described washing tower.
8. biogas purification method according to claim 7, is characterized in that, described amine liquid recovery liquid is delivered to described washing tower first the rich solution of described amine liquid recovery liquid and described purification carried out heat exchange before.
9. biogas purification method according to claim 8, is characterized in that, will reclaim through the amine liquid of heat exchange to be delivered to described washing tower after liquid uses amine liquid to reclaim the further cooling of liquid water cooler.
10. biogas purification method according to claim 7, is characterized in that, also comprises step:
The gas of described stripping tower output is used water cooler is cooling makes the amine condensation in gas become amine liquid;
Use the amine separator that gas and the amine liquid of water cooler output are separated, and amine liquid is delivered to washing tower.
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