CN105771560A - Refined filtration system for low-concentration coal-bed methane - Google Patents
Refined filtration system for low-concentration coal-bed methane Download PDFInfo
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- CN105771560A CN105771560A CN201610272476.XA CN201610272476A CN105771560A CN 105771560 A CN105771560 A CN 105771560A CN 201610272476 A CN201610272476 A CN 201610272476A CN 105771560 A CN105771560 A CN 105771560A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1406—Multiple stage absorption
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
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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
- 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
- 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
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
-
- 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
- C10L3/105—Removal of contaminants of nitrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- 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
- C10L2290/541—Absorption of impurities during preparation or upgrading of a fuel
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Gas Separation By Absorption (AREA)
Abstract
本发明公开了一种低浓度甲烷的煤层气精过滤系统，与现有技术相比，本发明将进料的低浓度煤层气(甲烷进料体积分数为5％)浓缩到34％，回收率73.4％；达到国家三级煤层气使用指标，可考虑用于工业及民用燃料，发电。最后提出了低成本，低能耗，工艺简单，容易操作的煤层气分离浓缩的方法。
The invention discloses a low-concentration methane coalbed gas fine filtration system. Compared with the prior art, the invention concentrates the low-concentration coalbed gas (the methane feed volume fraction is 5%) fed to 34%, and the recovery rate is 73.4%; meet the national third-level coalbed methane use indicators, can be considered for industrial and civil fuel, power generation. Finally, a low-cost, low-energy-consumption, simple-process and easy-to-operate coalbed methane separation and concentration method is proposed.
Description
Technical field
The present invention relates to a kind of air filtering system, particularly relate to the coal bed gas essence filtration system of a kind of low-concentration methane.
Background technology
The separation method of current coal bed gas is mainly cryogenic rectification method, pressure-variable adsorption partition method, membrane separation process, hydrate thing method.In recent years, having some researcheres to gasoline, the organic solvent such as diesel oil absorbs the liquid phase composition of methane and has measured and calculated, and have selected suitable thermodynamical model.But current prior art operation condition requires height, energy consumption is big, equipment investment is big, and portion of techniques adopts the technology of membrane separating gas, and this is low for the selectivity of film, film cost height, poor mechanical property etc. constrain the membrane separation technique application at coal bed gas separation field.And too high pressure can produce potential safety hazard, be not suitable for adopting in coalbed methane containing oxygen separates, accordingly, there exist room for improvement.
Summary of the invention
The purpose of the present invention is that the coal bed gas essence filtration system providing a kind of low-concentration methane in order to solve the problems referred to above.
The present invention is achieved through the following technical solutions above-mentioned purpose:
nullThe present invention includes the first absorption tower、First flash column、First Heat Exchanger、Second absorption tower、Second flash column、Booster pump、Material mixer、Second heat exchanger、3rd absorption tower and desorber，Described first absorption tower is provided with gas inlet and colvent inlet，The upper end outlet on described first absorption tower is connected with the first entrance of described second absorption tower，The lower end outlet on described first absorption tower is connected with the entrance of described first flash column，The outlet of described first flash column is connected with the second entrance of described second absorption tower by First Heat Exchanger，The lower end outlet of described second absorption tower is connected with the entrance of described second flash column，First outlet of described second flash column is connected by the first entrance of described second heat exchanger with described 3rd absorption tower，Second outlet of described second flash column is connected with second entrance on described 3rd absorption tower by described booster pump and described material mixer，The lower end outlet on described 3rd absorption tower is connected with the entrance of described desorber，The lower end outlet of described desorber is connected with the recovery entrance of described second absorption tower，The upper end outlet of described desorber is clean gas outlet.
Concrete operation method of the present invention is:
(1) adopt the method for continuous cyclic absorption to coal bed gas absorption cleaning, coal bed gas absorbs from entrance at the bottom of the tower on the first absorption tower with the carbon tetrachloride solvent counter current contacting from tower top, by the solubility curve to coal bed gas of the carbon tetrachloride above it is known that carbon tetrachloride is best to the dissolving selectivity of carbon dioxide, so Main Function is to absorb whole CO in the first absorption tower2, and the methane of 5%,
The absorption liquid on (2) first absorption towers is through the first flash column, the methane of a small amount of 5% that flash separation the first absorption tower absorbs is discharged from tower top, the liquid of the flash distillation at the bottom of the first flash column tower enters second absorption tower, after second absorption tower, substantial amounts of nitrogen and oxygen are mainly discharged by tower top, second absorption tower is under the effect of the solvent carbon tetrachloride newly added, and methane is all absorbed；
(3) the absorption liquid at the bottom of second absorption tower is through the flash distillation of the second flash column, and the gas of the second flash column flash distillation is from tower top out at the bottom of the tower entering the 3rd absorption tower, and absorbent originates from a part for the carbon tetrachloride bottom the second flash column；
(4) through the absorption again on the 3rd absorption tower, owing to solute effect in carbon tetrachloride of nitrogen and oxygen is than the difference of methane, so what the top flash distillation on the 3rd absorption tower went out is substantial amounts of nitrogen and oxygen.Finally enter desorber from the low carbon tetrachloride solution rich in methane out of the 3rd absorbing tower and carry out desorbing methane gas therein, be then carbon tetrachloride lean solution at the bottom of tower, it is possible to continue cycling through and be back in second absorption tower and serve as absorbent.
The beneficial effects of the present invention is:
The present invention is the coal bed gas essence filtration system of a kind of low-concentration methane, and compared with prior art, the low concentration coal-bed gas (methane feed volume fraction is 5%) of charging is concentrated to 34% by the present invention, the response rate 73.4%；Reach three grades of coal bed gas service indexs of country, it is contemplated that for industry and domestic fuel, generating.Finally proposing low cost, low energy consumption, technique is simple, it is easy to the coal bed gas of operation separates the method for concentration.
Accompanying drawing explanation
Fig. 1 is the structural representation of the present invention.
In figure: B1-the first absorption tower, B2-the first flash column, B3-First Heat Exchanger, B4-second absorption tower, B5-the second flash column, B6-booster pump, B7-material mixer, B8-the second heat exchanger, B9-the 3rd absorption tower, B10-desorber.
Detailed description of the invention
Below in conjunction with accompanying drawing, the invention will be further described:
nullAs shown in Figure 1: the present invention includes the first absorption tower B1、First flash column B2、First Heat Exchanger B3、Second absorption tower B4、Second flash column B5、Booster pump B6、Material mixer B7、Second heat exchanger B8、3rd absorption tower B9 and desorber B10，First absorption tower B1 is provided with gas inlet and colvent inlet，The upper end outlet of the first absorption tower B1 is connected with first entrance of second absorption tower B4，The lower end outlet of the first absorption tower B1 is connected with the entrance of the first flash column B2，The outlet of the first flash column B2 is connected by second entrance of First Heat Exchanger B3 and second absorption tower B4，The lower end outlet of second absorption tower B4 is connected with the entrance of the second flash column B5，First outlet of the second flash column B5 is connected by first entrance of the second heat exchanger B8 and the three absorption tower B9，Second outlet of the second flash column B5 is connected by second entrance of booster pump B6 and material mixer B7 and the three absorption tower B9，The lower end outlet of the 3rd absorption tower B9 is connected with the entrance of desorber B10，The lower end outlet of desorber B10 is connected with the recovery entrance of second absorption tower B4，The upper end outlet of desorber B10 is clean gas outlet.
Concrete operation method of the present invention is:
(1) adopt the method for continuous cyclic absorption to coal bed gas absorption cleaning, coal bed gas absorbs from entrance at the bottom of the tower on the first absorption tower with the carbon tetrachloride solvent counter current contacting from tower top, by the solubility curve to coal bed gas of the carbon tetrachloride above it is known that carbon tetrachloride is best to the dissolving selectivity of carbon dioxide, so Main Function is to absorb whole CO in the first absorption tower2, and the methane of 5%,
The absorption liquid on (2) first absorption towers is through the first flash column, the methane of a small amount of 5% that flash separation the first absorption tower absorbs is discharged from tower top, the liquid of the flash distillation at the bottom of the first flash column tower enters second absorption tower, after second absorption tower, substantial amounts of nitrogen and oxygen are mainly discharged by tower top, second absorption tower is under the effect of the solvent carbon tetrachloride newly added, and methane is all absorbed；
(3) the absorption liquid at the bottom of second absorption tower is through the flash distillation of the second flash column, and the gas of the second flash column flash distillation is from tower top out at the bottom of the tower entering the 3rd absorption tower, and absorbent originates from a part for the carbon tetrachloride bottom the second flash column；
(4) through the absorption again on the 3rd absorption tower, owing to solute effect in carbon tetrachloride of nitrogen and oxygen is than the difference of methane, so what the top flash distillation on the 3rd absorption tower went out is substantial amounts of nitrogen and oxygen.Finally enter desorber from the low carbon tetrachloride solution rich in methane out of the 3rd absorbing tower and carry out desorbing methane gas therein, be then carbon tetrachloride lean solution at the bottom of tower, it is possible to continue cycling through and be back in second absorption tower and serve as absorbent.
Device parameter
The flow stream parameters of equipment
The flow stream parameters of the first absorption tower B1
The flow stream parameters of second absorption tower B4
The flow stream parameters of desorber B10
The ultimate principle of the present invention and principal character and advantages of the present invention have more than been shown and described.Skilled person will appreciate that of the industry; the present invention is not restricted to the described embodiments; described in above-described embodiment and description is that principles of the invention is described; without departing from the spirit and scope of the present invention; the present invention also has various changes and modifications, and these changes and improvements both fall within the claimed scope of the invention.Claimed scope is defined by appending claims and equivalent thereof.
Claims (2)
- null1. the coal bed gas essence filtration system of a low-concentration methane，It is characterized in that: include the first absorption tower、First flash column、First Heat Exchanger、Second absorption tower、Second flash column、Booster pump、Material mixer、Second heat exchanger、3rd absorption tower and desorber，Described first absorption tower is provided with gas inlet and colvent inlet，The upper end outlet on described first absorption tower is connected with the first entrance of described second absorption tower，The lower end outlet on described first absorption tower is connected with the entrance of described first flash column，The outlet of described first flash column is connected with the second entrance of described second absorption tower by First Heat Exchanger，The lower end outlet of described second absorption tower is connected with the entrance of described second flash column，First outlet of described second flash column is connected by the first entrance of described second heat exchanger with described 3rd absorption tower，Second outlet of described second flash column is connected with second entrance on described 3rd absorption tower by described booster pump and described material mixer，The lower end outlet on described 3rd absorption tower is connected with the entrance of described desorber，The lower end outlet of described desorber is connected with the recovery entrance of described second absorption tower，The upper end outlet of described desorber is clean gas outlet.
- 2. the coal bed gas essence filtration system of low-concentration methane according to claim 1, it is characterised in that: concrete operation method is:(1) adopt the method for continuous cyclic absorption to coal bed gas absorption cleaning, coal bed gas absorbs from entrance at the bottom of the tower on the first absorption tower with the carbon tetrachloride solvent counter current contacting from tower top, by the solubility curve to coal bed gas of the carbon tetrachloride above it is known that carbon tetrachloride is best to the dissolving selectivity of carbon dioxide, so Main Function is to absorb whole CO in the first absorption tower2, and the methane of 5%,The absorption liquid on (2) first absorption towers is through the first flash column, the methane of a small amount of 5% that flash separation the first absorption tower absorbs is discharged from tower top, the liquid of the flash distillation at the bottom of the first flash column tower enters second absorption tower, after second absorption tower, substantial amounts of nitrogen and oxygen are mainly discharged by tower top, second absorption tower is under the effect of the solvent carbon tetrachloride newly added, and methane is all absorbed；(3) the absorption liquid at the bottom of second absorption tower is through the flash distillation of the second flash column, and the gas of the second flash column flash distillation is from tower top out at the bottom of the tower entering the 3rd absorption tower, and absorbent originates from a part for the carbon tetrachloride bottom the second flash column；(4) through the absorption again on the 3rd absorption tower, owing to solute effect in carbon tetrachloride of nitrogen and oxygen is than the difference of methane, so what the top flash distillation on the 3rd absorption tower went out is substantial amounts of nitrogen and oxygen.Finally enter desorber from the low carbon tetrachloride solution rich in methane out of the 3rd absorbing tower and carry out desorbing methane gas therein, be then carbon tetrachloride lean solution at the bottom of tower, it is possible to continue cycling through and be back in second absorption tower and serve as absorbent.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610272476.XA CN105771560A (en) | 2016-04-27 | 2016-04-27 | Refined filtration system for low-concentration coal-bed methane |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610272476.XA CN105771560A (en) | 2016-04-27 | 2016-04-27 | Refined filtration system for low-concentration coal-bed methane |
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| CN105771560A true CN105771560A (en) | 2016-07-20 |
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| CN201610272476.XA Pending CN105771560A (en) | 2016-04-27 | 2016-04-27 | Refined filtration system for low-concentration coal-bed methane |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4623371A (en) * | 1984-08-03 | 1986-11-18 | El Paso Hydrocarbons Company | Utilizing the Mehra process for processing and BTU upgrading of nitrogen-rich natural gas streams |
| CN1035440A (en) * | 1987-09-23 | 1989-09-13 | 先进提取技术有限公司 | Handle the technology of rich nitrogen, Fu Qing and rich olefins gas with physical solvent |
| US20050120878A1 (en) * | 2003-12-04 | 2005-06-09 | Dennis Leppin | Process for separating carbon dioxide and methane |
| CN102329672A (en) * | 2011-09-06 | 2012-01-25 | 北京昊业怡生科技有限公司 | Method for separating and producing methane and carbon dioxide from marsh gas |
| CN203319966U (en) * | 2013-07-10 | 2013-12-04 | 安徽理工大学 | Separation and purification system for coal bed gas hydrate |
| CN203764088U (en) * | 2014-02-14 | 2014-08-13 | 西安科技大学 | System for enriching coal bed gas |
| CN205796895U (en) * | 2016-04-27 | 2016-12-14 | 西安科技大学 | A kind of coal bed gas essence filtration system of low-concentration methane |
-
2016
- 2016-04-27 CN CN201610272476.XA patent/CN105771560A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4623371A (en) * | 1984-08-03 | 1986-11-18 | El Paso Hydrocarbons Company | Utilizing the Mehra process for processing and BTU upgrading of nitrogen-rich natural gas streams |
| CN1035440A (en) * | 1987-09-23 | 1989-09-13 | 先进提取技术有限公司 | Handle the technology of rich nitrogen, Fu Qing and rich olefins gas with physical solvent |
| US20050120878A1 (en) * | 2003-12-04 | 2005-06-09 | Dennis Leppin | Process for separating carbon dioxide and methane |
| CN102329672A (en) * | 2011-09-06 | 2012-01-25 | 北京昊业怡生科技有限公司 | Method for separating and producing methane and carbon dioxide from marsh gas |
| CN203319966U (en) * | 2013-07-10 | 2013-12-04 | 安徽理工大学 | Separation and purification system for coal bed gas hydrate |
| CN203764088U (en) * | 2014-02-14 | 2014-08-13 | 西安科技大学 | System for enriching coal bed gas |
| CN205796895U (en) * | 2016-04-27 | 2016-12-14 | 西安科技大学 | A kind of coal bed gas essence filtration system of low-concentration methane |
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Application publication date: 20160720 |