CN103265986A - Method for extracting coal-based natural gas from methanol blowdown gas and method for producing CNG (compressed natural gas) - Google Patents
Method for extracting coal-based natural gas from methanol blowdown gas and method for producing CNG (compressed natural gas) Download PDFInfo
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- CN103265986A CN103265986A CN2013102094028A CN201310209402A CN103265986A CN 103265986 A CN103265986 A CN 103265986A CN 2013102094028 A CN2013102094028 A CN 2013102094028A CN 201310209402 A CN201310209402 A CN 201310209402A CN 103265986 A CN103265986 A CN 103265986A
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Abstract
The invention discloses a method for extracting coal-based natural gas from methanol blowdown gas and method for producing CNG (compressed natural gas), and relates to a method for preparing coal-based natural gas and method for producing the CNG. For solving the problems that the existing treatment on the methanol blowdown gas is to produce the city gas, the heat value of the gas is low, and the economy benefit is bad, the method comprises the following steps: step one, carrying out washing treatment; step two, treating the membrane separation hydro-extraction; step three, converting the carbon oxide; step four, decarbonization treatment; step five, concentrating the methane by membrane separation; and step six, extracting the coal-based natural gas and producing CNG. The method disclosed by the invention not only satisfies the requirement of the modern city to the natural gas, but also the natural gas can be further pressurized to as the vehicle fuel (CNG), the heat value of the natural gas is capable of achieving 46,000KJ/cu.m, the economy benefit of the coal gasification deep-processing is improved, and the method is suitable for the industrial production. The method disclosed by the method is applied to the field for producing the methanol and field for extracting coal-based natural gas by using the methanol blowdown gas produced in the methanol production process and producing the CNG.
Description
Technical field
The present invention relates to produce the method for coal-based gas and the method for producing CNG.
Background technology
Utilize the by-product part of vapourizing furnace production city coal gas to be methyl alcohol, introducing along with Sweet natural gas, domestic gas day by day reduces until withdrawing from, the natural gas via processing treatment also can be used as CNG (compressed natural gas) onboard fuel, substituting gasoline uses as automobile fuel, therefore market for natural gas has a high potential, and supply falls short of demand, discharge (being the methyl alcohol blow-out gas) and will have a certain amount of tail gas in the methanol production process, main enrich methane in this part gas, hydrogen, carbon monoxide and carbonic acid gas, there is not the methyl alcohol blow-out gas to extract before the coal-based gas technology, processing to the methyl alcohol blow-out gas mainly is for the production of town gas, and the calorific value of coal gas is lower, is generally 13794KJ/m
3～16302KJ/m
3, deficiency in economic performance.
Summary of the invention
The present invention is for the production of town gas for solving existing processing to the methyl alcohol blow-out gas, and the calorific value of coal gas is lower, the problem of deficiency in economic performance, and a kind of method of methyl alcohol blow-out gas extraction coal-based gas and the method for producing CNG are provided.
The method that a kind of methyl alcohol blow-out gas of the present invention extracts coal-based gas may further comprise the steps:
One, washing is handled: adopt water washing device to wash to the methyl alcohol blow-out gas, obtain except the methyl alcohol blow-out gas behind the methyl alcohol;
Two, membrane sepn is carried hydrogen and is handled: feed membrane separation unit separating hydrogen gas, the methyl alcohol blow-out gas behind the hydrogen that is removed with what step 1 obtained except the methyl alcohol blow-out gas behind the methyl alcohol;
Three, carbon monodixe conversion is handled: the methyl alcohol blow-out gas behind the hydrogen removed that step 2 is obtained becomes in the conversion tower in feeding, be catalyzer with the Fe-Cr series catalysts, be to handle under 320～500 ℃ in temperature, the methyl alcohol blow-out gas that goes out to become the conversion tower feeds low the change in the conversion tower, and be catalyzer with the Cu-Zn series catalysts, be to handle under 190～280 ℃ in temperature, go out to hang down to become the concentration that obtains carbon monoxide behind the conversion tower less than 3% methyl alcohol blow-out gas;
Four, carbonization treatment: utilize decarbonization device with n-formyl sarcolysine base diethanolamine be sorbent material remove the carbon monoxide that step 3 obtains concentration less than the carbonic acid gas in 3% the methyl alcohol blow-out gas, obtain the methyl alcohol blow-out gas after the decarburization;
Five, membrane sepn concentrates methane: utilize membrane separation unit under ℃ condition of dew-point temperature≤-50 the methyl alcohol blow-out gas after the step 4 decarburization to be carried out the dehydrogenation gas disposal, the concentration that obtains hydrogen is coal-based gas less than 5% concentrated methane gas.
A kind of method of utilizing coal-based gas to produce CNG of the present invention may further comprise the steps:
Utilize compressor under ℃ condition of dew-point temperature≤-50 to the processing of boosting of the described coal-based gas of claim 1, namely obtain CNG.
The methyl alcohol blow-out gas elder generation that the method for the methyl alcohol blow-out gas that produces in the processing methanol production process of the present invention will contain methane handles the methyl alcohol that goes in the methyl alcohol blow-out gas by washing, propose the hydrogen processing by membrane sepn then and separate most of hydrogen, after purifying, send methanol synthesizer back to, handle by carbon monodixe conversion again, with carbon monodixe conversion, CO is transformed into CO under the effect of catalyzer
2And hydrogen, again by carbonization treatment, adopt MDEA (n-formyl sarcolysine base diethanolamine solvent) as absorption agent, to remove the CO in the methyl alcohol blow-out gas
2, absorbed CO
2Amine aqueous solution analyse and discharge CO through pyrolysis again
2Back recycling capable of circulation, concentrate methane by membrane sepn at last, isolate remaining hydrogen, return methanol synthesizer after purification concentrates and produce methyl alcohol, the methane gas that contains high density that part is left is as the Sweet natural gas of civil natural gas or industrial high heating value, satisfy modern city to the demand of Sweet natural gas, the remaining methane gas that contains high density of another part can be by further pressurizeing as vehicle fuel (CNG compressed natural gas) simultaneously, and found on the basis of production methanol product, utilize blow-out gas to extract a kind of method of Sweet natural gas, the calorific value of Sweet natural gas can reach 36000KJ/m
3～46000KJ/m
3, improved the economic benefit of gasification of coal deep processing, be fit to suitability for industrialized production, be applied to produce the methyl alcohol field and extract coal-based gas and production CNG field with the methyl alcohol blow-out gas that produces in the methanol production process.
Description of drawings
Fig. 1 is process flow sheet of the present invention.
Embodiment
Embodiment one: the method that a kind of methyl alcohol blow-out gas of present embodiment extracts coal-based gas may further comprise the steps:
One, washing is handled: adopt water washing device to wash to the methyl alcohol blow-out gas, obtain except the methyl alcohol blow-out gas behind the methyl alcohol;
Two, membrane sepn is carried hydrogen and is handled: feed membrane separation unit separating hydrogen gas, the methyl alcohol blow-out gas behind the hydrogen that is removed with what step 1 obtained except the methyl alcohol blow-out gas behind the methyl alcohol;
Three, carbon monodixe conversion is handled: the methyl alcohol blow-out gas behind the hydrogen removed that step 2 is obtained becomes in the conversion tower in feeding, be catalyzer with the Fe-Cr series catalysts, be to handle under 320～500 ℃ in temperature, the methyl alcohol blow-out gas that goes out to become the conversion tower feeds low the change in the conversion tower, and be catalyzer with the Cu-Zn series catalysts, be to handle under 190～280 ℃ in temperature, go out to hang down to become the concentration that obtains carbon monoxide behind the conversion tower less than 3% methyl alcohol blow-out gas;
Four, carbonization treatment: utilize decarbonization device with n-formyl sarcolysine base diethanolamine be sorbent material remove the carbon monoxide that step 3 obtains concentration less than the carbonic acid gas in 3% the methyl alcohol blow-out gas, obtain the methyl alcohol blow-out gas after the decarburization;
Five, membrane sepn concentrates methane: utilize membrane separation unit under ℃ condition of dew-point temperature≤-50 the methyl alcohol blow-out gas after the step 4 decarburization to be carried out the dehydrogenation gas disposal, the concentration that obtains hydrogen is coal-based gas less than 5% concentrated methane gas;
Wherein the hydrogen that removes in the hydrogen that separates in the step 2 and the step 5 is sent methyl alcohol synthetic reactor back to as the unstripped gas utilization.
Water washing device described in the step 1 is made up of the water wash column that efficient regular wire packing is housed, high-pressure hydraulic pump, desalination tank, interchanger and gas-liquid separator; The water wash column that efficient regular wire packing wherein is housed provides the place of removing methyl alcohol, and desalination tank and interchanger play the effect of heat exchange, and gas-liquid separator is used for the phlegma that produces owing to temperature variation in the operating process of separating step one.
Membrane separation unit described in the step 2 is Pu Lisen
The membrane separation apparatus combination.
Middle change conversion tower described in the step 3 and the low conversion tower that becomes provide the place into carbon monodixe conversion.
Decarbonization device described in the step 4 is by the absorption tower, regenerator column, water circulating pump, interchanger, gas-liquid separator, mechanical filter and charcoal filter are formed, described absorption tower provides the place for the MDEA absorbing carbon dioxide, described regenerator column provides the place for the carbonic acid gas that the MDEA that has adsorbed carbonic acid gas removes absorption, the MDEA recycle that has removed carbonic acid gas that obtains, described water circulating pump provides power for the recirculated water in the step 4 process, described gas-liquid separator is used for the phlegma that produces owing to temperature variation in the operating process of separating step four, and described mechanical filter and charcoal filter play the effect of removing the micro-MDEA that contains in the carbonic acid gas that has removed.
Membrane separation unit described in the step 5 is Pu Lisen
The membrane separation apparatus combination.
The methyl alcohol blow-out gas elder generation that the method for the methyl alcohol blow-out gas that produces in the processing methanol production process of present embodiment will contain methane handles the methyl alcohol that goes in the methyl alcohol blow-out gas by washing, propose the hydrogen processing by membrane sepn then and separate most of hydrogen, after purifying, send methanol synthesizer back to, handle by carbon monodixe conversion again, with carbon monodixe conversion, CO is transformed into CO under the effect of catalyzer
2And hydrogen, again by carbonization treatment, adopt MDEA (n-formyl sarcolysine base diethanolamine solvent) as absorption agent, to remove the CO in the methyl alcohol blow-out gas
2, absorbed CO
2Amine aqueous solution analyse and discharge CO through pyrolysis again
2Back recycling capable of circulation, concentrate methane by membrane sepn at last, isolate remaining hydrogen, return methanol synthesizer after purification concentrates and produce methyl alcohol, the methane gas that contains high density that part is left is as the Sweet natural gas of civil natural gas or industrial high heating value, satisfy modern city to the demand of Sweet natural gas, the method operating pressure of present embodiment only is 3MPa～25MPa, low to matching requirements, only needing to replenish the low-pressure water steam in the process in reaction system gets final product, it is low to consume energy, and found on the basis of production methanol product, utilized blow-out gas to extract a kind of method of Sweet natural gas, improved the economic benefit of gasification of coal deep processing, be fit to suitability for industrialized production, be applied to produce the methyl alcohol field and extract the coal-based gas field with the methyl alcohol blow-out gas that produces in the methanol production process.
Embodiment two: what present embodiment and embodiment one were different is: the temperature except the methyl alcohol blow-out gas behind the methyl alcohol that obtains in the step 1 is 50 ℃, and other step and parameter are identical with embodiment one.
Embodiment three: what present embodiment was different with embodiment one or two is: obtaining coal-based gas pressure in the step 5 is 3.8Mpa～4.5Mpa, and other step and parameter are identical with embodiment one or two.
Embodiment four: a kind of method of utilizing coal-based gas to produce CNG of present embodiment may further comprise the steps:
Utilize compressor under ℃ condition of dew-point temperature≤-50 to the processing of boosting of the described coal-based gas of claim 1, namely obtain CNG.
Embodiment five: what present embodiment and embodiment four were different is: describedly boost that to handle concrete operations as follows: utilize compressor under ℃ condition of dew-point temperature≤-50 with the pressure of the described coal-based gas of claim 1 from boosting to 25.0MPa for 3.8MPa～4.5MPa, other step and parameter are identical with embodiment four.
The operating pressure of present embodiment only is 3MPa～25MPa, low to matching requirements, only needing to replenish the low-pressure water steam in the process in reaction system gets final product, it is low to consume energy, and found on the basis of production methanol product, utilized blow-out gas to extract a kind of method of Sweet natural gas, improved the economic benefit of gasification of coal deep processing, be fit to suitability for industrialized production, be applied to produce the methyl alcohol field and extract coal-based gas production CNG field with the methyl alcohol blow-out gas that produces in the methanol production process.
With following verification experimental verification beneficial effect of the present invention:
Test one: the method that a kind of methyl alcohol blow-out gas extracts coal-based gas may further comprise the steps:
One, washing is handled: adopt water washing device to wash to the methyl alcohol blow-out gas, obtain except the methyl alcohol blow-out gas behind the methyl alcohol;
Wherein the methyl alcohol blow-out gas at first enters the water wash column that efficient regular wire packing is housed in the step 1, wash by contacting with the de-salted water of being got to the water wash column cat head by high-pressure hydraulic pump, remove the methyl alcohol in the methyl alcohol blow-out gas, the methyl alcohol blow-out gas that does not contain methyl alcohol enters down handling procedure one, and the de-salted water that contains methyl alcohol is sent the hydrogen recovery system at the bottom of the washing Tata;
Wherein water wash column is for buying the T-101 water wash column from company of Chengdu Sai Pu Rising, and its working temperature is 90 ℃, and its operating pressure is 8.8MPa, and efficient regular wire packing BX is equipped with in its inside;
Two, membrane sepn is carried hydrogen and is handled: feed membrane separation unit separating hydrogen gas, the methyl alcohol blow-out gas behind the hydrogen that is removed with what step 1 obtained except the methyl alcohol blow-out gas behind the methyl alcohol;
Wherein membrane separation unit is gloomy in the V103A-L of company of Chengdu Sai Pu Rising is general for buying in the step 2
The membrane separation apparatus combination, its working temperature is 80 ℃, and its operating pressure is 8.8MPa, and the film chipware is equipped with in its inside;
In the step 2 at Pu Lisen
The hydrogen that membrane separation apparatus combination low-pressure permeability vapour records is sent methyl alcohol synthetic reactor back to, and the methyl alcohol blow-out gas that the non-infiltration gas of high pressure records removes behind the hydrogen enters into down treatment unit one;
The mist that the downstream of water wash column arranges methyl alcohol blow-out gas after a gas-liquid separator is removed the process step 1 washing of coming out from the water wash column cat head, carries in the step 2 wherein;
A well heater wherein is set in the downstream of gas-liquid separator in the step 2, to be warming up to 50 ℃ through the methyl alcohol blow-out gas after the step 1 washing, avoid leaving the saturated vapor that the methyl alcohol blow-out gas of gas-liquid separator contains and after the membrane separation unit infiltrating gas side concentrates, condense, guarantee Pu Lisen simultaneously
Membrane separation apparatus is in optimized working order;
Wherein gas-liquid separator is for buying the gas-liquid separator from the V-101 of company of Chengdu Sai Pu Rising, and its working temperature is 80 ℃, and its operating pressure is 8.8MPa, and inner scum dredger is the 304SS scum dredger;
Wherein well heater is for buying the well heater from the E-101 of company of Chengdu Sai Pu Rising, and its working temperature is 184 ℃, and its operating pressure is 1.0/8.8Mpa TS/SS, and its heat interchanging area is 10m
2, wherein the heating medium of well heater is low-pressure steam;
Three, carbon monodixe conversion is handled: the methyl alcohol blow-out gas behind the hydrogen removed that step 2 is obtained becomes in the conversion tower in feeding, be catalyzer with the KLB-101/9Fe-Cr series catalysts, be to handle under 360 ℃ in temperature, the methyl alcohol blow-out gas that goes out to become the conversion tower feeds low the change in the conversion tower, and be catalyzer with the KLB-201Cu-Zn series catalysts, be to handle under 210 ℃ in temperature, go out to hang down to become the concentration that obtains carbon monoxide behind the conversion tower less than 3% methyl alcohol blow-out gas;
Main chemical compositions and quality percentage composition are as follows in the wherein said KLB-101/9Fe-Cr catalyzer: Fe
2O
3〉=74%, Cr
2O
3〉=7%, graphite≤3%, its active (in the CO interconversion rate) 〉=70.0% in heat-resisting back, main chemical compositions and quality percentage composition are as follows in the wherein said KLB-201Cu-Zn catalyzer: CuO 〉=39%, ZnO 〉=42%, Al
2O
3〉=8%, graphite: 2%～3%, S≤0.02%, Cl≤0.01%, active (in the CO interconversion rate) 〉=93.0% before it is heat-resisting, active (in the CO interconversion rate) 〉=88.0% in heat-resisting back;
Wherein removing methyl alcohol blow-out gas behind the hydrogen through step 2, to be heated to temperature be to become the conversion tower in entering after 360 ℃, after being down to 210 ℃, the gas temperature that go out to become the conversion tower enters the low conversion tower that becomes, go out to hang down the gas temperature that becomes the conversion tower and be down to 160 ℃ of laggard promoting the circulation of qi liquid separation, isolate moisture, after being down to 40 ℃, the gas temperature of isolating moisture carries out a gas-liquid separation again, isolate moisture again, the gas that obtains enters down handling procedure one, and the lifting of wherein said gas temperature is by realizing with the heat exchange of circulation de-salted water in interchanger; Wherein said twice gas-liquid separation realizes that by separator wherein said circulation de-salted water plays the heat exchange effect in the carbon monodixe conversion treating processes, and the circulation de-salted water is sent the saturator recycle back to through after the heat exchange;
The gas temperature that wherein goes out to hang down to become the conversion tower in the step 3 is down to 160 ℃ of laggard promoting the circulation of qi liquid and is separated, and isolates moisture, and the gas of isolating moisture is drawn a part and entered down one handling procedure and provide thermal source for regenerator column;
Wherein said interchanger goes into the tower interchanger for purchase change in the E-301 of company of Chengdu Sai Pu Rising and low change of E-302 goes into the tower interchanger, become tower interchanger working temperature among the wherein said E-301 and be 430 ℃/380 ℃ TS/SS, operating pressure is 5.4MPaA/5.4MpaA TS/SS, the low change of wherein said E-302 is gone into its working temperature of tower interchanger and is 200 ℃/280 ℃ TS/SS, and operating pressure is 5.9MPaA/5.3MPaA TS/SS;
Wherein said separator is for buying the V-301 High Temperature Gas liquid/gas separator from company of Chengdu Sai Pu Rising, and its working temperature is 200 ℃, and its operating pressure is 5.0MPaA, and there is the 304SS scum dredger its inside;
Four, carbonization treatment: utilize decarbonization device with n-formyl sarcolysine base diethanolamine be sorbent material remove the carbon monoxide that step 3 obtains concentration less than the carbonic acid gas in 3% the methyl alcohol blow-out gas, obtain the methyl alcohol blow-out gas after the decarburization;
Wherein the carbonization treatment described in the step 4 realizes by MDEA solution absorbs carbonic acid gas, temperature after the process step 3 is handled is that 40 ℃ methyl alcohol blow-out gas enters from the bottom, absorption tower, MDEA solution enters from top, absorption tower, gas phase and liquid phase countercurrent flow, carbonic acid gas is absorbed and enters MDEA solution, the MDEA solution that has absorbed carbonic acid gas is discharged at the bottom of the absorption tower and is entered regenerator column regeneration back recycle, unabsorbed gas phase is drawn from the top, absorption tower, being cooled to temperature is to enter gas-liquid separator separates after 56 ℃ to go out liquid phase, being warming up to temperature after liquid phase is drawn from the gas-liquid separator bottom is 79 ℃, enter regenerator column regeneration from regenerator column top, gas phase is drawn from the gas-liquid separator top, enters next road program after gac removes MDEA solution;
The gas phase temperature that wherein enters down one program is 40 ℃;
The MDEA solution that has wherein absorbed carbonic acid gas is discharged at the bottom of the absorption tower and is entered regenerator column from regenerator column top, in regenerator column, heat, being heated to temperature is 114 ℃, gas phase is drawn from the regenerator column cat head, temperature enters gas-liquid separator after being down to 93 ℃, isolated carbon dioxide is drawn high-altitude emptying from the gas-liquid separator top, and isolated MDEA solution is drawn from the gas-liquid separator bottom and is back to the recycle of regenerator column top again;
The MDEA solution after the regeneration of drawing of regenerator column bottom wherein, it is to reflux after 47 ℃ to enter the absorption tower from top, absorption tower that MDEA solution after the regeneration is down to temperature, wherein the MDEA solution after the regeneration is back to before the absorption tower through the degradation material in the filtering and removing solution, and wherein said filtration makes realization by adopting the series connection of mechanical filter and charcoal filter;
Wherein the thermal source in the regenerator column is provided by interchanger by the gas that comes out from low change conversion tower in external steam and the step 3 in the step 4, external steam after the heat exchange becomes water of condensation discharges, and turns back to the treatment system described in the step 3 from the low gas that comes out the conversion tower that becomes in the step 3 after the heat exchange;
Wherein the water balance in the step 4 is realized by replenishing de-salted water;
Wherein the absorption tower is for buying from the T-401 absorption tower of company of Chengdu Sai Pu Rising, and its working temperature is 60 ℃, and operating pressure is 4.8MPaA, and inner stuffing is
Stainless Steel Helices;
Wherein regenerator column is for buying the T-402 regenerator column from company of Chengdu Sai Pu Rising, and its working temperature is 120 ℃, and its operating pressure is 0.16MPaA, and inner stuffing is
Stainless Steel Helices;
Wherein gas-liquid separator is for buying the V-501 gas-liquid separator from company of Chengdu Sai Pu Rising, and its working temperature is 40 ℃, and its operating pressure is 4.85MPaA;
Wherein interchanger is for buying the E-406 conversion gas reboiler from company of Chengdu Sai Pu Rising, and its working temperature is 160 ℃ of shell sides, tube side 117, ℃, its operating pressure is shell side 4.82MPa, tube side 0.16MPa;
Wherein the purchase that operates in that removes MDEA solution through gac is carried out in the T-403 purified gas adsorber of company of Chengdu Sai Pu Rising, and its working temperature is 40 ℃, and its operating pressure is 4.9MPaA;
Five, membrane sepn concentrates methane: utilizing membrane separation unit is under-50 ℃ of conditions the methyl alcohol blow-out gas after the step 4 decarburization to be carried out the dehydrogenation gas disposal in dew-point temperature, and the concentration that obtains hydrogen is 3% concentrated methane gas, is the extraction coal-based gas.
Wherein said concentrated methane gas purity 95%, the pressure of methane gas is 4.1Mpa;
Wherein membrane separation unit is gloomy in the V501A-J of company of Chengdu Sai Pu Rising is general for buying in the step 5
Membrane separation apparatus, its working temperature are 80 ℃, and its operating pressure is 5.0MPa, and there is the film chipware its inside;
In the step 5 from Pu Lisen
It is to send methyl alcohol synthetic reactor back to after 95% hydrogen gas compressor boosts that membrane separation apparatus combination low-pressure permeability vapour records purity, and the methane that the non-infiltration gas of high pressure records removes behind the hydrogen enters into down handling procedure one;
Wherein be introduced into gas-liquid separator through the methyl alcohol blow-out gas after the step 4 decarburization in the step 5 and remove the mist that carries through in the methyl alcohol blow-out gas after the step 4 decarburization, a well heater is set in the downstream of gas-liquid separator then will be warming up to 50 ℃ through the methyl alcohol blow-out gas after the step 4 decarburization, avoiding leaving the saturated vapor that the methyl alcohol blow-out gas of gas-liquid separator contains condenses after the membrane separation unit infiltrating gas side concentrates, guarantee that simultaneously gas-liquid separator is in optimized working order, wherein the heating medium of well heater is low-pressure steam;
Wherein gas-liquid separator is for buying the V-201 gas-liquid separator from company of Chengdu Sai Pu Rising, and its working temperature is 80 ℃, and its operating pressure is 4.84MPa, and there is the 304SS scum dredger its inside;
Wherein well heater is for buying the E-501 well heater from company of Chengdu Sai Pu Rising, and 184 ℃ of its working temperatures, its operating pressure are shell side 1.0MPa, tube side 5.0MPa, and wherein the heating medium of well heater is low-pressure steam;
Wherein compressor is for buying the C-601A/B hydrogen gas compressor from company of Chengdu Sai Pu Rising;
The method that test two, a kind of methyl alcohol blow-out gas that utilizes test one to obtain extract coal-based gas production CNG may further comprise the steps:
Utilize compressor under ℃ condition of dew-point temperature≤-50 to testing a coal-based gas that the obtains processing of boosting, pressure namely obtains CNG from for 4.1MPa boosts to 25.0MPa.
It is as follows wherein to produce the process of CNG with test one coal-based gas that obtains: the concentration of test one hydrogen that obtains is that 3% concentrated methane gas is filtered by strainer earlier, then by the relief valve pressure regulation, be pressurized to 25Mpa by compressor unit again, enter dewatering unit then and carry out drying treatment, the purity that obtains CNG is 94%, and dew-point temperature is-50 ℃;
Its middle filtrator is for buying the mechanical filter from company of Chengdu Sai Pu Rising, and its working temperature is 50 ℃, and its operating pressure is 25MPaA;
Wherein compressor is for buying the compressor unit from company of Chengdu Sai Pu Rising, and its main technical details is as follows: discharge capacity is 3300Nm
3/ h, inlet air temperature≤30 ℃, exhaust temperature is not higher than 15 ℃ of envrionment temperatures, and intake pressure is 3.0MPa～4.2MPa, and exhaust pressure is 25MPa, and cooling water inflow is 43t/h;
Wherein said dewatering unit is for buying the moisture eliminator from company of Chengdu Sai Pu Rising, and its main technical details is as follows: operating pressure is 3.0MPa～4.2MPa, and the absorption working temperature is room temperature, and the reproduction operation temperature is 220 ℃, dew points at normal pressure≤-40 ℃.
The operating pressure that requires in test one and the test two only is 3MPa～25MPa, low to matching requirements, only needing to replenish the low-pressure water steam in the process in reaction system gets final product, it is low to consume energy, and found on the basis of production methanol product, utilized blow-out gas to extract a kind of method of Sweet natural gas, improved the economic benefit of gasification of coal deep processing, be fit to suitability for industrialized production, be applied to produce the methyl alcohol field and extract coal-based gas and production CNG field with the methyl alcohol blow-out gas that produces in the methanol production process.
Claims (5)
1. a methyl alcohol blow-out gas extracts the method for coal-based gas, it is characterized in that the method that a kind of methyl alcohol blow-out gas extracts coal-based gas may further comprise the steps:
One, washing is handled: adopt water washing device to wash to the methyl alcohol blow-out gas, obtain except the methyl alcohol blow-out gas behind the methyl alcohol;
Two, membrane sepn is carried hydrogen and is handled: feed membrane separation unit separating hydrogen gas, the methyl alcohol blow-out gas behind the hydrogen that is removed with what step 1 obtained except the methyl alcohol blow-out gas behind the methyl alcohol;
Three, carbon monodixe conversion is handled: the methyl alcohol blow-out gas behind the hydrogen removed that step 2 is obtained becomes in the conversion tower in feeding, be catalyzer with the Fe-Cr series catalysts, be to handle under 320～500 ℃ in temperature, the methyl alcohol blow-out gas that goes out to become the conversion tower feeds low the change in the conversion tower, and be catalyzer with the Cu-Zn series catalysts, be to handle under 190～280 ℃ in temperature, go out to hang down to become the concentration that obtains carbon monoxide behind the conversion tower less than 3% methyl alcohol blow-out gas;
Four, carbonization treatment: utilize decarbonization device with n-formyl sarcolysine base diethanolamine be sorbent material remove the carbon monoxide that step 3 obtains concentration less than the carbonic acid gas in 3% the methyl alcohol blow-out gas, obtain the methyl alcohol blow-out gas after the decarburization;
Five, membrane sepn concentrates methane: utilize membrane separation unit under ℃ condition of dew-point temperature≤-50 the methyl alcohol blow-out gas after the step 4 decarburization to be carried out the dehydrogenation gas disposal, the concentration that obtains hydrogen is coal-based gas less than 5% concentrated methane gas.
2. a kind of methyl alcohol blow-out gas according to claim 1 extracts the method for coal-based gas, it is characterized in that the temperature except the methyl alcohol blow-out gas behind the methyl alcohol that obtains in the step 1 is 50 ℃.
3. a kind of methyl alcohol blow-out gas according to claim 1 and 2 extracts the method for coal-based gas, and it is characterized in that obtaining in the step 5 coal-based gas pressure is 3.8Mpa～4.5Mpa.
4. method of utilizing the described coal-based gas of claim 1 to produce CNG is characterized in that a kind of method of utilizing coal-based gas to produce CNG may further comprise the steps:
Utilize compressor under ℃ condition of dew-point temperature≤-50 to the processing of boosting of the described coal-based gas of claim 1, namely obtain CNG.
5. a kind of method of utilizing coal-based gas to produce CNG according to claim 4 is characterized in that describedly boosting that to handle concrete operations as follows: utilize compressor under ℃ condition of dew-point temperature≤-50 with the pressure of the described coal-based gas of claim 1 from boosting to 25.0MPa for 3.8MPa～4.5MPa.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
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| CN115055028A (en) * | 2022-08-08 | 2022-09-16 | 中国华能集团清洁能源技术研究院有限公司 | Carbon capture system and method |
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