CN109971521A - A kind of method of methane concentration separation in low concentration coal-bed gas - Google Patents
A kind of method of methane concentration separation in low concentration coal-bed gas Download PDFInfo
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- CN109971521A CN109971521A CN201910270800.8A CN201910270800A CN109971521A CN 109971521 A CN109971521 A CN 109971521A CN 201910270800 A CN201910270800 A CN 201910270800A CN 109971521 A CN109971521 A CN 109971521A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/542—Adsorption of impurities during preparation or upgrading of a fuel
Abstract
The invention discloses the methods that methane concentration in a kind of low concentration coal-bed gas separates.It includes the following steps: to carry out low concentration coal-bed gas following processing at least once, realizes the concentration and separation to methane in the low concentration coal-bed gas；The processing is handled successively to carry out compression processing, purified treatment, pressure-swing adsorption concentration.The method of the present invention is simple, disengaging time is fast, the volumn concentration of methane in low concentration coal-bed gas can be concentrated into 92% or more by 10~30%.
Description
Technical field
The present invention relates to the methods that methane concentration in a kind of low concentration coal-bed gas separates, and belong to gas separation field.
Background technique
Low concentration coal-bed gas refers to the coal bed gas that methane concentration is lower than 30%.It is provided according to national " safety regulations in coal mine ",
When utilizing to coal bed gas, methane concentration must not be lower than 30%.For this part of coal bed gas, current way is in coal mine
Nearby do domestic fuel or direct emission.China has been developed that low concentration coal-bed gas generation technology for 2005, and obtains in the whole nation
Popularity application, but due to the generation technology conveying technology of coalbed methane containing oxygen is required it is high, and with the grid-connected difficulty of power grid, because
This resource utilization is not high.Continuous improvement with the country to environmental requirement, natural gas as a kind of clean energy resource demand by
Cumulative to add, low concentration coal-bed gas rapid pressure swing adsorption, which is concentrated and separated compressed natural gas (CNG) processed and liquefied natural gas (LNG), to be had
The raising low concentration coal-bed gas utilization rate of effect.The main method that pressure swing adsorption method is concentrated and separated as low concentration coal-bed gas, has
Simple process, the feature that low energy consumption, investment is small
Low concentration coal-bed gas pressure-swing adsorption concentration separates compressed natural gas (CNG) processed at present and liquefied natural gas (LNG) is big
All single column adsorption time is controlled in 120s or more, and by the way of stage variable pressure adsorbing separation, and single column adsorption time exists
120s low concentration coal-bed gas pressure-swing adsorption concentration separating technology below, which does not have, successfully to be reported.
Summary of the invention
The object of the present invention is to provide the method that methane concentration in a kind of low concentration coal-bed gas separates, the method for the present invention letters
List, disengaging time are fast, the volumn concentration of methane in low concentration coal-bed gas can be concentrated into 92% or more by 10~30%.
The method that methane concentration separates in a kind of low concentration coal-bed gas provided by the invention, including the following steps: will be low dense
It spends coal bed gas and carries out following processing at least once, realize the concentration and separation to methane in the low concentration coal-bed gas；
The processing is handled successively to carry out compression processing, purified treatment, pressure-swing adsorption concentration.
In above-mentioned method, the volumn concentration of methane can be 10~30% in the low concentration coal-bed gas, specifically may be used
It is 10~15%, 10~20%, 15~20%, 14.79% or 19.77%.
In above-mentioned method, the number of processing is 1~5 time, preferably 2 times.
In above-mentioned method, pressure of the low concentration coal-bed gas after compression processing can be 0.1~0.5MPa, specifically may be used
For 0.15MPa, 0.17MPa, 0.2MPa or 0.3MPa.
In above-mentioned method, the step of purified treatment, is as follows: by the low concentration after the compression processing
Coal bed gas is once dusted, removes water, oil removing.
In above-mentioned method, the dedusting, water removal, oil removing are de- by sequentially connected cyclone demister, dissolved salt formula respectively
Water installations and charcoal canister are handled.
In above-mentioned method, the bulk density of the active carbon loaded in the charcoal canister can be 400~500g/L, specifically may be used
For 500g/L.
In above-mentioned method, the adsorbent that the pressure-swing adsorption concentration processing uses is BM-3 type carbon molecular sieve；
The temperature of the pressure-swing adsorption concentration processing can be 5~35 DEG C, and concretely 25 DEG C, the time can be 60~120s,
Concretely 90s is that boost to pressure can be 0.1~0.5MPa to 0.001~0.1MPa/s with rate of pressure rise, concretely
0.01MPa/s boosts to 0.17MPa；
The pressure-swing adsorption concentration processing carries out in conventional six-tower vacuum adsorption tower.
In above-mentioned method, the separation a of the BM-3 type carbon molecular sieveCH4/N2Can be 4.0, bulk density can for 600~
650g/L is concretely purchased from Co., Ltd, coal science and technology research institute.
In above-mentioned method, when the processing is more than once, second and pressure-variable adsorption described in the processing later
The exhaust gas discharged after concentration returns in the low concentration coal-bed gas and supplements raw material, to improve product recovery rate.
The invention has the following advantages that
The present invention is first compressed and is purified using low concentration coal-bed gas as raw material, then using pressure swing absorption process to coal seam
Methane in gas carries out separation concentration, and the gas after first order pressure-swing adsorption concentration is then carried out second-compressed and purification, right
Coal bed gas carries out second level pressure-swing adsorption concentration after compression purification, to make the concentration of methane in coal bed gas by 10 in unstripped gas
~30% is increased to 92% or more.The present invention is concentrated and separated method and only selects a kind of carbon molecular sieve (BM-3 type carbon molecular sieve), i.e.,
It can reach concentration CH4Shortening with the time of the purpose of deoxidation, and transformation of the present invention concentration, concentration and separation efficiency significantly improves,
It is of great significance and value in terms of the industrialization promotion of coal bed gas.
Detailed description of the invention
Fig. 1 is in the process flow chart and Examples 1 and 2 of methane concentration separation method in low concentration coal-bed gas of the present invention
The process flow chart of separating methane by concentration from low concentration coal-bed gas.
Specific embodiment
Experimental method used in following embodiments is conventional method unless otherwise specified.
The materials, reagents and the like used in the following examples is commercially available unless otherwise specified.
Device described in following embodiments or equipment are conventional equipment or equipment unless otherwise instructed.
Content described in following embodiments is volumn concentration unless otherwise instructed.
Wherein, measurement methane content is measured using analytical IR method, and the rate of recovery of methane (is referred to by pressure-variable adsorption
The amount that pure methane in product is obtained after concentration and separation accounts for the amount of pure methane in enrichment materials gas) it is calculated according to following formula:
Methane recovery=(amount of methane in methane content/unstripped gas of recycling) × 100%
Carbon molecular sieve BM-3 used is purchased from Co., Ltd, coal science and technology research institute, BM-3 type carbon point in following embodiments
The physical and chemical parameter of son sieve is as follows: adsorbent diameter (mm) is 2.5~3.2, and adsorbent granularity (mesh) is 4~12, adsorbent resistance to compression
Intensity (N/ particle) >=100, adsorbent heaping weight (g/cc) are 0.6~0.65, separation >=4.
Embodiment 1, to CH4The low concentration coal-bed gas that content is 10~15% carries out rapid concentration separation
The process flow of the present embodiment rapid concentration separation is as shown in Figure 1, wherein and 1 is the low concentration coal-bed gas of unstripped gas,
2 be compression step, and 3 be purifying step, and 4 be first order pressure-swing adsorption concentration step, and 5 empty tail for first order pressure-swing adsorption concentration
Gas, 6 be compression step, and 7 be purifying step, and 8 be second level pressure-swing adsorption concentration, and 9 return to gas for second level pressure-swing adsorption concentration,
10 be final products gas.
Detailed process is as follows:
1) low concentration coal-bed gas as unstripped gas is compressed, obtains compressed coal bed gas, the compressed coal
The pressure of layer gas is 0.15MPa；
Wherein, the title of unstripped gas each component and volumn concentration difference are as follows: CH4: 14.79%, O2:
17.89%, N2: 67.32%, raw gas pressure is 3~5kPa；
2) by compressed coal bed gas obtained by step 1) through filter dedusting, cyclone demister water removal, most afterwards through active carbon
Tank oil removing, the coal bed gas after being purified；Wherein, the active carbon bulk density in charcoal canister is 500g/L；
3) separation of first order pressure-swing adsorption concentration is carried out to the purified coal bed gas that step 2) obtains, after being concentrated
Coal bed gas, while first order pressure-swing adsorption concentration tail gas emptying process；
4) coal bed gas is compressed after step 3) being concentrated, and the pressure of coal bed gas after being compressed, the coal bed gas is
0.17MPa；
Wherein coal bed gas each component title and volumn concentration difference are as follows after first order pressure-swing adsorption concentration:
CH4: 39.16%, O2: 12.77%, N2: 48.07%；
5) compressed coal bed gas obtained by step 4) is removed water through cyclone demister, is most obtained afterwards through charcoal canister oil removing
Purified coal bed gas；Wherein, the active carbon bulk density in charcoal canister is 500g/L；
6) pressure-swing adsorption concentration separation in the second level is carried out to the purified coal bed gas that step 5) obtains, obtains product gas,
Second level pressure-swing adsorption concentration tail gas is mixed as gas is returned with fresh feed gas simultaneously.
In example, two-stage pressure-swing absorber used is six-tower vacuum adsorption tower, and the internal diameter of adsorption tower is 542mm, the first order
Sorbent used carbon molecular sieve is BM-3 in pressure-swing adsorption concentration, and adsorption temp is 25 DEG C, adsorption time 90s, adsorptive pressure
For 0.15MPa.Sorbent used carbon molecular sieve is BM-3 in the processing of second level pressure-swing adsorption concentration, and adsorption temp is 25 DEG C, is inhaled
The attached time is 90s, adsorptive pressure 0.17MPa.
The tail gas emptying that first order pressure-swing adsorption concentration generates in the step, the tail gas that second level pressure-swing adsorption concentration generates
Returning in unstripped gas according to abovementioned steps 2)-step 6) continues to be concentrated and separated.
The methane content in product gas is measured using analytical IR method, wherein each component title and volume basis
Content is respectively as follows: CH4: 93.06%, O2: 0.82%, N2: 3.12%, methane recovery 91.23%.
Embodiment 2, to CH4The low concentration coal-bed gas that content is 15~20% carries out rapid concentration separation
The process flow of the present embodiment rapid concentration separation is as shown in Figure 1, wherein and 1 is the low concentration coal-bed gas of unstripped gas,
2 be compression step, and 3 be purifying step, and 4 be first order pressure-swing adsorption concentration step, and 5 is useless for the emptying of first order pressure-swing adsorption concentration
Gas, 6 be compression step, and 7 be purifying step, and 8 be second level pressure-swing adsorption concentration, and 9 return to gas for second level pressure-swing adsorption concentration,
10 be final products gas.
Detailed process is as follows:
1) low concentration coal-bed gas 1 as unstripped gas is compressed, obtains compressed coal bed gas, the compressed coal
The pressure of layer gas is 0.15MPa；
Wherein, the title of unstripped gas each component and volumn concentration difference are as follows: CH4: 19.77%, O2:
16.84%, N2: 63.39%, raw gas pressure is 3~5kPa；
2) by compressed coal bed gas obtained by step 1) through filter dedusting, cyclone demister water removal, most afterwards through active carbon
Tank oil removing, the coal bed gas after being purified；Wherein, the active carbon bulk density in charcoal canister is 500g/L；
3) separation of first order pressure-swing adsorption concentration is carried out to the purified coal bed gas that step 2) obtains, after being concentrated
Coal bed gas, while first order pressure-swing adsorption concentration tail gas emptying process.
4) coal bed gas is compressed after step 3) being concentrated, and the pressure of coal bed gas after being compressed, the coal bed gas is
0.17MPa；
Wherein coal bed gas each component title and volumn concentration difference are as follows after first order pressure-swing adsorption concentration:
CH4: 54.70%, O2: 9.51%, N2: 35.79%；
5) compressed coal bed gas obtained by step 4) is removed water through cyclone demister, is most obtained afterwards through charcoal canister oil removing
Purified coal bed gas；Wherein, the active carbon bulk density in charcoal canister is 500g/L；
6) pressure-swing adsorption concentration separation in the second level is carried out to the purified coal bed gas that step 5) obtains, obtains product gas,
Second level pressure-swing adsorption concentration tail gas is mixed as gas is returned with fresh feed gas simultaneously.
In example, two-stage pressure-swing absorber used is six-tower vacuum adsorption tower, and the internal diameter of adsorption tower is 542mm, the first order
Sorbent used carbon molecular sieve is BM-3 in pressure-swing adsorption concentration, and adsorption temp is 25 DEG C, adsorption time 90s, adsorptive pressure
For 0.15MPa.Sorbent used carbon molecular sieve is BM-3 in the processing of second level pressure-swing adsorption concentration, and adsorption temp is 25 DEG C, is inhaled
The attached time is 90s, adsorptive pressure 0.17MPa.
The tail gas emptying that first order pressure-swing adsorption concentration generates in the step, the tail gas that second level pressure-swing adsorption concentration generates
Returning in unstripped gas according to abovementioned steps 2)-step 6) continues to be concentrated and separated.
The methane content in product gas is measured using analytical IR method, wherein each component title and volume basis
Content is respectively as follows: CH4: 96.02%, O2: 0.8%, N2: 3.2%, methane recovery 90.83%.
Comparative example,
Detailed process is as follows:
1) low concentration coal-bed gas that the methane concentration as unstripped gas is 20.10% is compressed, is obtained compressed
Coal bed gas, the pressure of the compressed coal bed gas are 0.6MPa；
Wherein, the title of unstripped gas each component and volumn concentration difference are as follows: CH4: 20.10%, O2:
16.84%, N2: 63.06%, raw gas pressure is 3~5kPa；
2) compressed coal bed gas obtained by step 1) is removed water through filter dedusting, is most obtained afterwards through charcoal canister oil removing
Purified coal bed gas；Wherein, the active carbon bulk density in charcoal canister is 500g/L；
3) separation of first order pressure-swing adsorption concentration is carried out to the purified coal bed gas that step 2) obtains, after being concentrated
Coal bed gas, while first order pressure-swing adsorption concentration tail gas emptying process；
4) coal bed gas is compressed after step 3) being concentrated, and the pressure of coal bed gas after being compressed, the coal bed gas is
0.5MPa；
Wherein coal bed gas each component title and volumn concentration difference are as follows after first order pressure-swing adsorption concentration:
CH4: 55.70%, O2: 8.51%, N2: 35.79%；
5) compressed coal bed gas obtained by step 4) is removed water through filter, is most purified afterwards through charcoal canister oil removing
Coal bed gas afterwards；Wherein, the active carbon bulk density in charcoal canister is 500g/L；
6) pressure-swing adsorption concentration separation in the second level is carried out to the purified coal bed gas that step 5) obtains, obtains product gas,
Second level pressure-swing adsorption concentration tail gas emptying process simultaneously.
In comparative example, two-stage pressure-swing absorber used is six-tower vacuum adsorption tower, and the internal diameter of adsorption tower is 542mm, first
Sorbent used carbon molecular sieve is BM-3 in grade pressure-swing adsorption concentration, and adsorption temp is 25 DEG C, adsorption time 210s, adsorption pressure
Power is 0.6MPa.Sorbent used carbon molecular sieve is BM-3 in the processing of second level pressure-swing adsorption concentration, and adsorption temp is 25 DEG C, is inhaled
The attached time is 270s, adsorptive pressure 0.5MPa.
The tail gas emptying that first order pressure-swing adsorption concentration generates in the step, the tail gas that second level pressure-swing adsorption concentration generates
Emptying.
The methane content in product gas is measured using analytical IR method, wherein each component title and volume basis
Content is respectively as follows: CH4: 96.32%, O2: 0.5%, N2: 3.2%, methane recovery 64.31%.
Claims (10)
1. a kind of method that methane concentration separates in low concentration coal-bed gas, include the following steps: to carry out low concentration coal-bed gas to
Few primary following processing, realizes the concentration and separation to methane in the low concentration coal-bed gas；
The processing is handled successively to carry out compression processing, purified treatment, pressure-swing adsorption concentration.
2. according to the method described in claim 1, it is characterized by: in the low concentration coal-bed gas methane volumn concentration
It is 10~30%.
3. method according to claim 1 or 2, it is characterised in that: the number of processing is 1~5 time.
4. method according to any one of claim 1-3, it is characterised in that: the low concentration coal-bed gas is through compression processing
Pressure afterwards is 0.1~0.5MPa.
5. method according to any of claims 1-4, it is characterised in that: the step of purified treatment is as follows: will
The low concentration coal-bed gas after the compression processing is once dusted, removes water, oil removing.
6. according to the method described in claim 5, it is characterized by: the dedusting, water removal, oil removing pass through respectively it is sequentially connected
Cyclone demister, dissolved salt formula dehydration device and charcoal canister are handled.
7. according to the method described in claim 6, it is characterized by: the bulk density of the active carbon loaded in the charcoal canister is
400~500g/L.
8. method according to any one of claims 1-7, it is characterised in that: what the pressure-swing adsorption concentration processing used
Adsorbent is BM-3 type carbon molecular sieve；
The temperature of pressure-swing adsorption concentration processing is 5~35 DEG C, and the time is 60~120s, with rate of pressure rise be 0.001~
It is 0.1~0.5MPa that 0.01MPa/s, which boosts to pressure,；
The pressure-swing adsorption concentration processing carries out in conventional six-tower vacuum adsorption tower.
9. according to the method described in claim 8, it is characterized by: the separation of the BM-3 type carbon molecular sieveFor
4.0, bulk density is 600~650g/L.
10. method according to claim 1 to 9, it is characterised in that: when the processing is more than once second
The exhaust gas discharged after the secondary and processing of pressure-swing adsorption concentration described in the processing later returns to be supplemented in the low concentration coal-bed gas
Raw material.
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