CN203890266U - Device system for simultaneously purifying methane and carbon dioxide from biogas - Google Patents
Device system for simultaneously purifying methane and carbon dioxide from biogas Download PDFInfo
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- CN203890266U CN203890266U CN201420264639.6U CN201420264639U CN203890266U CN 203890266 U CN203890266 U CN 203890266U CN 201420264639 U CN201420264639 U CN 201420264639U CN 203890266 U CN203890266 U CN 203890266U
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Abstract
The utility model relates to a device system for simultaneously purifying methane and carbon dioxide from biogas. The device system comprises a compressor I, a pretreatment device I, a first-stage hollow fiber membrane, a second-stage hollow fiber membrane and a CO2 recovery device, wherein an inlet of the compressor I is connected with a biogas feedstock pipeline, an outlet of the compressor I is connected with an inlet of the pretreatment device I; an outlet of the pretreatment device I is connected with an inlet of the first-stage hollow fiber membrane; a non-permeable gas outlet of the first-stage hollow fiber membrane is connected with an inlet of the second-stage hollow fiber membrane, a permeate gas outlet of the first-stage hollow fiber membrane is connected with an inlet of the CO2 recovery device; a purified gas outlet of the CO2 recovery device is a CO2 purified gas outlet; and a non-permeable gas outlet of the second-stage hollow fiber membrane is a CH4 purified gas outlet. The device system has the characteristics of simple process, compact device structure, small device size, high automation degree, and wide application range, is convenient to operate and is safe and reliable.
Description
Technical field
The utility model relates to a kind of apparatus system of the methane and carbon dioxide of simultaneously purifying from biogas, is specifically related to a kind of CH that purifies from biogas
4time reclaim high-purity CO
2apparatus system.
Background technology
In current methane purification process section, CO in tail gas
2purity have more than 90%, and tail gas is to be generally directly discharged into atmosphere, a large amount of CO in discharge gas
2with a small amount of CH
4, this part gas purging can affect environment, aggravation Greenhouse effect.
Methane gas is one of important factor affecting Greenhouse effect, and CH4 gas is higher more than 20 times than the actual influence of CO2, must progressively control minimizing.Methane gas only carries out separation and purifies being effectively used.And carbonic acid gas also can be produced the industrial chemicals such as dry ice after purifying.
Utility model content
The purpose of this utility model is for present embrane method methane purification technique, when CH4 in biogas is purified to CO in the discharge gas of system
2recycle, can realize " zero release " of methane purification system.
The utility model is achieved through the following technical solutions:
Simultaneously purify from the biogas apparatus system of methane and carbon dioxide, comprises marsh gas desulfuration dewaterer, compressor I, pretreatment unit I, first step hollow-fibre membrane, second stage hollow-fibre membrane and CO
2retrieving arrangement; Described marsh gas desulfuration dewaterer is provided with import and outlet; Described compressor I is provided with import and outlet, and described pretreatment unit I is provided with import and outlet; Described first step hollow-fibre membrane is provided with import, impermeable gas outlet and oozes vent outlet; Described second stage hollow-fibre membrane is provided with import, impermeable gas outlet and oozes vent outlet; Described CO
2retrieving arrangement is provided with import, the outlet of purification gas and tail gas outlet; Wherein, the import of described marsh gas desulfuration dewaterer is connected through pipeline with biogas source, and the outlet of described marsh gas desulfuration dewaterer is connected through pipeline with the import of described compressor I; The outlet of described compressor I is connected through pipeline with the import of described pretreatment unit I; The outlet of described pretreatment unit I is connected through pipeline with the import of described first step hollow-fibre membrane; The impermeable gas outlet of described first step hollow-fibre membrane is connected through pipeline with the import of described second stage hollow-fibre membrane, described first step hollow-fibre membrane ooze vent outlet and described CO
2the import of retrieving arrangement connects through pipeline; Described CO
2the tail gas outlet of retrieving arrangement is connected through pipeline with the import of described compressor I, described CO
2the purification gas outlet of retrieving arrangement is CO
2products export; The vent outlet that oozes of described second stage hollow-fibre membrane is connected through pipeline with the import of described compressor I, and the impermeable gas outlet of described second stage hollow-fibre membrane is CH
4products export.
Preferably, described pretreatment unit I comprises cooling driers I, filter set I and well heater I; Described cooling driers I is provided with import and outlet; Described filter set I is provided with import and outlet; Described well heater I is provided with import and outlet; The outlet of described compressor I is connected through pipeline with the import of described cooling driers I; The outlet of described cooling driers I is connected through pipeline with the import of described filter set I; The outlet of described filter set I is connected through pipeline with the import of described well heater I; The outlet of described well heater I is connected through pipeline with the import of described first step hollow-fibre membrane.
Preferably, described apparatus system also comprises compressor II, pretreatment unit II and third stage hollow-fibre membrane; Described compressor II is provided with import and outlet; Described pretreatment unit II is provided with import and outlet; Described third stage hollow-fibre membrane is provided with import, oozes vent outlet and impermeable gas outlet; The vent outlet that oozes of described first step hollow-fibre membrane is connected through pipeline with the import of described compressor II; The outlet of described compressor II is connected through pipeline with the import of described pretreatment unit II; The outlet of described pretreatment unit II is connected through pipeline with the import of described third stage hollow-fibre membrane; Described third stage hollow-fibre membrane ooze vent outlet and described CO
2the import of retrieving arrangement connects through pipeline; The impermeable gas outlet of described third stage hollow-fibre membrane is connected through pipeline with the import of described first step hollow-fibre membrane.
Preferably, described pretreatment unit II comprises cooling driers II, filter set II and well heater II; Described cooling driers II is provided with import and outlet; Described filter set II is provided with import and outlet; Described well heater II is provided with import and outlet; The outlet of described compressor II is connected through pipeline with the import of described cooling driers II; The outlet of described cooling driers II is connected through pipeline with the import of described filter set II; The outlet of described filter set II is connected through pipeline with the import of described well heater II; The outlet of described well heater I is connected through pipeline with the import of described third stage hollow-fibre membrane.
Preferably, described filter set I comprises 4 grades of strainers that are connected in series successively.
Preferably, described filter set II comprises 4 grades of strainers that are connected in series successively.
Preferably, described first step hollow-fibre membrane, second stage hollow-fibre membrane and third stage hollow-fibre membrane comprise respectively a plurality of hollow fiber film assemblies that are connected in parallel.
Technique effect of the present utility model and advantage are:
The utility model can obtain CO
2and CH
4two kinds of highly purified gas products, utilize the energy fully, prevent from causing in exhaust emissions atmosphere environmental pollution and Greenhouse effect; Owing to having used embrane method purifying technique, technique is simple, compact equipment, equipment volume are little, and level of automation is high, easy to operate, safe and reliable, applied range.In technique of the present invention and device, the tail gas reflux technique of design, realizes " zero release " of system.
Accompanying drawing explanation
The apparatus system (two-stage membrane sepn) of a kind of methane and carbon dioxide of simultaneously purifying from biogas of Fig. 1
The apparatus system (three grades of membrane sepn) of a kind of methane and carbon dioxide of simultaneously purifying from biogas of Fig. 2
Fig. 3 pretreatment unit I structural representation
Fig. 4 hollow fiber film structure schematic diagram
Reference numeral:
1, marsh gas desulfuration dewaterer; 2, compressor I; 3, pretreatment unit I; 4, first step hollow-fibre membrane; 5, second stage hollow-fibre membrane; 6, CH
4storage tank; 7, CO
2retrieving arrangement; 8, compressor II; 9, pretreatment unit II; 10, third stage hollow-fibre membrane; 11, cooling driers I; 12, filter set I; 13, well heater I; 14, hollow fiber film assembly.
Embodiment
Below by specific specific examples explanation the technical solution of the utility model.Should be understood that one or more method stepss that the utility model is mentioned do not repel between the step that also has additive method step or clearly mention at these before and after described combination step can also insert additive method step; Should also be understood that these embodiment are only not used in restriction scope of the present utility model for the utility model is described.And, except as otherwise noted, the numbering of various method steps is only for differentiating the convenient tool of various method steps, but not for limiting the ordering of various method steps or limiting the enforceable scope of the utility model, the change of its relativeness or adjustment, without essence change technology contents in the situation that, when being also considered as the enforceable category of the utility model.
Simultaneously purify from the biogas apparatus system of methane and carbon dioxide, as shown in Figure 1, comprises marsh gas desulfuration dewaterer 1, compressor I 2, pretreatment unit I 3, first step hollow-fibre membrane 4, second stage hollow-fibre membrane 5 and CO
2retrieving arrangement 7; Described marsh gas desulfuration dewaterer 1 is provided with import and outlet; Described compressor I 2 is provided with import and outlet, and described pretreatment unit I 3 is provided with import and outlet; Described first step hollow-fibre membrane 4 is provided with import, impermeable gas outlet and oozes vent outlet; Described second stage hollow-fibre membrane 5 is provided with import, impermeable gas outlet and oozes vent outlet; Described CO
2retrieving arrangement 7 is provided with import, the outlet of purification gas and tail gas outlet; Wherein, the import of described marsh gas desulfuration dewaterer 1 is connected through pipeline with biogas source, and the outlet of described marsh gas desulfuration dewaterer 1 is connected through pipeline with the import of described compressor I 2; The outlet of described compressor I 2 is connected through pipeline with the import of described pretreatment unit I 3; The outlet of described pretreatment unit I 3 is connected through pipeline with the import of described first step hollow-fibre membrane 4; The impermeable gas outlet of described first step hollow-fibre membrane 4 is connected through pipeline with the import of described second stage hollow-fibre membrane 5, described first step hollow-fibre membrane 4 ooze vent outlet and described CO
2the import of retrieving arrangement 7 connects through pipeline; Described CO
2the tail gas outlet of retrieving arrangement 7 is connected through pipeline with the import of described compressor I 2, described CO
2the purification gas outlet of retrieving arrangement 7 is CO
2products export; The vent outlet that oozes of described second stage hollow-fibre membrane 5 is connected through pipeline with described compressor I 2 imports, and the impermeable gas outlet of described second stage hollow-fibre membrane 5 is CH
4products export.
Under preferable case, as shown in Figure 3:
Described pretreatment unit I 3 comprises cooling driers I 11, filter set I 12 and well heater I 13; Described cooling driers I 11 is provided with import and outlet; Described filter set I 12 is provided with import and outlet; Described well heater I 13 is provided with import and outlet; The outlet of described compressor I 2 is connected through pipeline with the import of described cooling driers I 11; The outlet of described cooling driers I 11 is connected through pipeline with the import of described filter set I 12; The outlet of described filter set I 12 is connected through pipeline with the import of described well heater I 13; The outlet of described well heater I 13 is connected through pipeline with the import of described first step hollow-fibre membrane 4.
Described filter set I 12 comprises 4 grades of strainers that are connected in series successively.
Under another preferable case, as shown in Figure 2:
Described apparatus system also comprises compressor II8, pretreatment unit II9 and third stage hollow-fibre membrane 10; Described compressor II8 is provided with import and outlet; Described pretreatment unit II9 is provided with import and outlet; Described third stage hollow-fibre membrane 10 is provided with import, oozes vent outlet and impermeable gas outlet; The vent outlet that oozes of described first step hollow-fibre membrane 4 is connected through pipeline with the import of described compressor II8; The outlet of described compressor II8 is connected through pipeline with the import of described pretreatment unit II9; The outlet of described pretreatment unit II9 is connected through pipeline with the import of described third stage hollow-fibre membrane 10; Described third stage hollow-fibre membrane 10 ooze vent outlet and described CO
2the import of retrieving arrangement 7 connects through pipeline; The impermeable gas outlet of described third stage hollow-fibre membrane 10 is connected through pipeline with the import of described first step hollow-fibre membrane 4.
Described pretreatment unit II9 comprises cooling driers II, filter set II and well heater II; Described cooling driers II is provided with import and outlet; Described filter set II is provided with import and outlet; Described well heater II is provided with import and outlet; The outlet of described compressor II8 is connected through pipeline with the import of described cooling driers II; The outlet of described cooling driers II is connected through pipeline with the import of described filter set II; The outlet of described filter set II is connected through pipeline with the import of described well heater II; The outlet of described well heater I 13 is connected through pipeline with the import of described third stage hollow-fibre membrane 10.
Described filter set II comprises 4 grades of strainers that are connected in series successively.
Under another preferable case: as shown in Figure 4, described first step hollow-fibre membrane 4, second stage hollow-fibre membrane 5 and third stage hollow-fibre membrane 10 comprise respectively a plurality of hollow fiber film assemblies that are connected in parallel 14.
Embodiment 1: two-stage membrane separation process
Simultaneously purify from the biogas technique of methane and carbon dioxide, comprises the following steps:
(1) marsh gas raw materials carries out after desulfurization dewatering through marsh gas desulfuration dewaterer 1, through 2 compressions of compressor I, be pressurized to after 1.35MPa, enter pretreatment unit I, through cooling driers I, filter set I (comprising 4 grades of strainers that are connected in series), process, filtering accuracy reaches dust 0.01 μ m/Nm3, Residual oil 0.01mg/Nm3, ammonia or amine are less than 100ppm, H
2s is less than 15ppm, then passes through well heater I, and temperature reaches 35 ℃, enters first step hollow-fibre membrane 4 and carries out CO
2and CH
4roughing out;
(2) vent outlet that oozes at first step hollow-fibre membrane 4 obtains CO
2crude product (94% CO
2, the CH of 4v%
4, other are O
2, N
2deng), the CH that impermeable gas outlet obtains
4crude product enters second stage hollow-fibre membrane 5 degree of depth and purifies;
(3) second stage hollow-fibre membrane 5 infiltration gas exit gass with enter compressor I 2 after raw material biogas after desulfurization dewatering mixes and continue processing, hollow-fibre membrane 5 impermeable gas in the second stage export and obtain CH
4product, purity reaches more than 97%, meets vehicle fuel GB18047-2000 standard;
(4) the isolated CO of first step hollow-fibre membrane 4
2crude product is again through CO
2retrieving arrangement 7 carries out low temperature purification, enters compressor I 2 and continues to process, isolated CO after isolated backflow gas mixes with marsh gas raw materials
2purity reaches 99.9%, meets the product requirement of industrial carbon dioxide standard GB/T6052-2011.
2: three grades of membrane separation processes of embodiment
(1) marsh gas raw materials carries out after desulfurization dewatering through marsh gas desulfuration dewaterer 1, through 2 compressions of compressor I, be pressurized to after 1.0MPa, then enter pretreatment unit I 3, after the pre-treatment of cooling driers I 11, filter set I 12 (comprising 4 grades of strainers that are connected in series) and well heater I 13, filtering accuracy reaches dust 0.01 μ m/Nm3, Residual oil 0.01mg/Nm3, ammonia or amine are less than 100ppm, H
2s is less than 15ppm, and temperature reaches 40 ℃, then enters first step hollow-fibre membrane 4 and carries out CO
2and CH
4roughing out;
(2) vent outlet that oozes at first step hollow-fibre membrane 4 obtains CO
2crude product (the CO of 90v%
2, the CH of 8v%
4, other are O
2, N
2deng), through compressor II8, be compressed to 1.1MPa, enter pretreatment unit II9, after the pre-treatment of cooling driers II, filter set II (comprising 4 grades of strainers that are connected in series) and well heater II, filtering accuracy reaches dust 0.01 μ m/Nm3, Residual oil 0.01mg/Nm3, ammonia or amine are less than 100ppm, H
2s is less than 15ppm, and temperature reaches 40 ℃, then enters third stage hollow-fibre membrane 10; The CH that the impermeable gas outlet of first step hollow-fibre membrane 4 obtains
4crude product enters second stage hollow-fibre membrane 5 degree of depth and purifies;
(3) outlet of the impermeable gas of second stage hollow-fibre membrane 5 obtains CH
4product, purity reaches more than 97%, meets vehicle fuel GB18047-2000 standard;
(4) the infiltration gas of second stage hollow-fibre membrane 5 and the raw material biogas of desulfurization dewatering are mixed into the 2 continuation processing of compressor I;
(5) the infiltration gas (98v%CO of third stage hollow-fibre membrane 10
2, 0.7v%CH
4, other O
2, N
2deng), through CO
2retrieving arrangement 7 carries out low temperature purification, and isolated tail gas is recycled to compressor I 2 after raw material biogas through desulfurization dewatering mixes to be continued to process, isolated CO
2purity reaches 99.9%, meets industrial carbon dioxide GB/T6052-2011 standard;
(6) impermeable gas of third stage hollow-fibre membrane 10, is circulated to the import of first step hollow-fibre membrane 4, mixes with pretreated gas in step (1), then enters first step hollow-fibre membrane 4 and continues to purify.
Claims (7)
1. the apparatus system of methane and carbon dioxide of simultaneously purifying from biogas, it is characterized in that, comprise marsh gas desulfuration dewaterer (1), compressor I (2), pretreatment unit I (3), first step hollow-fibre membrane (4), second stage hollow-fibre membrane (5) and CO
2retrieving arrangement (7); Described marsh gas desulfuration dewaterer (1) is provided with import and outlet; Described compressor I (2) is provided with import and outlet, and described pretreatment unit I (3) is provided with import and outlet; Described first step hollow-fibre membrane (4) is provided with import, impermeable gas outlet and oozes vent outlet; Described second stage hollow-fibre membrane (5) is provided with import, impermeable gas outlet and oozes vent outlet; Described CO
2retrieving arrangement (7) is provided with import, the outlet of purification gas and tail gas outlet; Wherein, the import of described marsh gas desulfuration dewaterer (1) is connected through pipeline with biogas source, and the outlet of described marsh gas desulfuration dewaterer (1) is connected through pipeline with the import of described compressor I (2); The outlet of described compressor I (2) is connected through pipeline with the import of described pretreatment unit I (3); The outlet of described pretreatment unit I (3) is connected through pipeline with the import of described first step hollow-fibre membrane (4); The impermeable gas outlet of described first step hollow-fibre membrane (4) is connected through pipeline with the import of described second stage hollow-fibre membrane (5), described first step hollow-fibre membrane (4) ooze vent outlet and described CO
2the import of retrieving arrangement (7) connects through pipeline; Described CO
2the tail gas outlet of retrieving arrangement (7) is connected through pipeline with the import of described compressor I (2), described CO
2the purification gas outlet of retrieving arrangement (7) is CO
2products export; The vent outlet that oozes of described second stage hollow-fibre membrane (5) is connected through pipeline with described compressor I (2) import, and the impermeable gas outlet of described second stage hollow-fibre membrane (5) is CH
4products export.
2. the apparatus system of a kind of methane and carbon dioxide of simultaneously purifying from biogas as claimed in claim 1, it is characterized in that, described pretreatment unit I (3) comprises cooling driers I (11), filter set I (12) and well heater I (13); Described cooling driers I (11) is provided with import and outlet; Described filter set I (12) is provided with import and outlet; Described well heater I (13) is provided with import and outlet; The outlet of described compressor I (2) is connected through pipeline with the import of described cooling driers I (11); The outlet of described cooling driers I (11) is connected through pipeline with the import of described filter set I (12); The outlet of described filter set I (12) is connected through pipeline with the import of described well heater I (13); The outlet of described well heater I (13) is connected through pipeline with the import of described first step hollow-fibre membrane (4).
3. the apparatus system of a kind of methane and carbon dioxide of simultaneously purifying from biogas as claimed in claim 2, is characterized in that, described filter set I (12) comprises 4 grades of strainers that are connected in series successively.
4. the apparatus system of a kind of methane and carbon dioxide of simultaneously purifying from biogas as claimed in claim 2, it is characterized in that, described apparatus system also comprises compressor II (8), pretreatment unit II (9) and third stage hollow-fibre membrane (10); Described compressor II (8) is provided with import and outlet; Described pretreatment unit II (9) is provided with import and outlet; Described third stage hollow-fibre membrane (10) is provided with import, oozes vent outlet and impermeable gas outlet; The vent outlet that oozes of described first step hollow-fibre membrane (4) is connected through pipeline with the import of described compressor II (8); The outlet of described compressor II (8) is connected through pipeline with the import of described pretreatment unit II (9); The outlet of described pretreatment unit II (9) is connected through pipeline with the import of described third stage hollow-fibre membrane (10); Described third stage hollow-fibre membrane (10) ooze vent outlet and described CO
2the import of retrieving arrangement (7) connects through pipeline; The impermeable gas outlet of described third stage hollow-fibre membrane (10) is connected through pipeline with the import of described first step hollow-fibre membrane (4).
5. the apparatus system of a kind of methane and carbon dioxide of simultaneously purifying from biogas as claimed in claim 4, is characterized in that, described pretreatment unit II (9) comprises cooling driers II, filter set II and well heater II; Described cooling driers II is provided with import and outlet; Described filter set II is provided with import and outlet; Described well heater II is provided with import and outlet; The outlet of described compressor II (8) is connected through pipeline with the import of described cooling driers II; The outlet of described cooling driers II is connected through pipeline with the import of described filter set II; The outlet of described filter set II is connected through pipeline with the import of described well heater II; The outlet of described well heater I (13) is connected through pipeline with the import of described third stage hollow-fibre membrane (10).
6. the apparatus system of a kind of methane and carbon dioxide of simultaneously purifying from biogas as claimed in claim 5, is characterized in that, described filter set II comprises 4 grades of strainers that are connected in series successively.
7. the apparatus system of a kind of methane and carbon dioxide of simultaneously purifying from biogas as claimed in claim 4, it is characterized in that, described first step hollow-fibre membrane (4), second stage hollow-fibre membrane (5) and third stage hollow-fibre membrane (10) comprise respectively a plurality of hollow fiber film assemblies that are connected in parallel (14).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420264639.6U CN203890266U (en) | 2014-05-22 | 2014-05-22 | Device system for simultaneously purifying methane and carbon dioxide from biogas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420264639.6U CN203890266U (en) | 2014-05-22 | 2014-05-22 | Device system for simultaneously purifying methane and carbon dioxide from biogas |
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| Publication Number | Publication Date |
|---|---|
| CN203890266U true CN203890266U (en) | 2014-10-22 |
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ID=51716694
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420264639.6U Expired - Fee Related CN203890266U (en) | 2014-05-22 | 2014-05-22 | Device system for simultaneously purifying methane and carbon dioxide from biogas |
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|---|---|
| CN (1) | CN203890266U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104003832A (en) * | 2014-05-22 | 2014-08-27 | 上海精腾新能源科技有限公司 | System and technique for simultaneously purifying methane and carbon dioxide from marsh gas |
-
2014
- 2014-05-22 CN CN201420264639.6U patent/CN203890266U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104003832A (en) * | 2014-05-22 | 2014-08-27 | 上海精腾新能源科技有限公司 | System and technique for simultaneously purifying methane and carbon dioxide from marsh gas |
| CN104003832B (en) * | 2014-05-22 | 2015-11-04 | 上海精腾新能源科技有限公司 | A kind ofly to purify the apparatus system of methane and carbon dioxide and technique from biogas simultaneously |
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|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20141022 Termination date: 20210522 |