CN112968629B - Compressed gas purification system and process without external power supply - Google Patents
Compressed gas purification system and process without external power supply Download PDFInfo
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- CN112968629B CN112968629B CN202110182927.1A CN202110182927A CN112968629B CN 112968629 B CN112968629 B CN 112968629B CN 202110182927 A CN202110182927 A CN 202110182927A CN 112968629 B CN112968629 B CN 112968629B
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- H—ELECTRICITY
- H02—GENERATION; CONVERSION OR DISTRIBUTION OF ELECTRIC POWER
- H02N—ELECTRIC MACHINES NOT OTHERWISE PROVIDED FOR
- H02N11/00—Generators or motors not provided for elsewhere; Alleged perpetua mobilia obtained by electric or magnetic means
- H02N11/002—Generators
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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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
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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
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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- Separation Of Gases By Adsorption (AREA)
Abstract
The invention provides a compressed gas purification system and a compressed gas purification process without external power supply, and belongs to the technical field of gas purification. The system comprises a heat exchanger, a gas-liquid separator, an air inlet pipeline, an adsorber, a product pipeline, an expansion machine, a heater, a heat accumulator, a regeneration pipeline, an exhaust pipeline and a plurality of valves, wherein branch parts of the air inlet pipeline and the exhaust pipeline are connected to a feed end of the adsorber, branch parts of the product pipeline and the regeneration pipeline are connected to a discharge end of the adsorber, an air inlet of the gas-liquid separator is connected to a hot side exhaust port of the heat exchanger, and a hot side air inlet of the heat exchanger is connected to a feed gas inlet. The system is self-sufficient in electric power, external power supply is not needed, so that the energy consumption of the system is reduced, the purification performance of the system is improved, and the system has great energy-saving significance in industrial occasions such as compressed air drying and natural gas treatment.
Description
Technical Field
The invention relates to the technical field of gas purification, in particular to a compressed gas purification system and a compressed gas purification process without external power supply.
Background
Gas purification is a common raw material gas treatment process in the fields of metallurgy, energy, chemical industry, environmental protection and the like, such as gas pollutant removal, compressed air drying, raw material natural gas drying and the like. The main function of gas purification is to avoid the harm caused by impurities (such as environmental pollution, pipeline freezing and blocking, material corrosion and explosion), and ensure the smooth operation of subsequent use or subsequent processes.
The temperature swing adsorption method is a common gas purification process, and can remove impurities (such as water vapor, carbon dioxide, acetylene, nitrogen dioxide, carbon monoxide, hydrogen sulfide and volatile organic compounds) in raw gas to a constant level by introducing the raw gas into a purification device, so as to obtain product gas with the purity reaching the standard.
In practical application, the existing temperature swing adsorption gas purification process has the following problems:
the feed gas and product gas typically have a higher pressure for reasons including one or more of the following: the source gas of the feed gas has a relatively high pressure, the feed gas is pressurized due to the high pressure required by the product gas, and the feed gas is pressurized due to the purification process requirements. However, in the process of circulating the high-pressure gas, the high-pressure product gas is depressurized and used as purge gas for the purification apparatus, so that the pressure contained in the high-pressure gas is wasted.
The above problems can be solved if the following energy saving method can be adopted. Namely: the pressure energy of the high-pressure gas is utilized through the expansion machine, electric energy and cold energy are obtained simultaneously, the cold energy is further used for cooling the feed gas, and the electric energy is input into the heater to be used for heating the blowing gas. In order to continuously output electric energy, a heat accumulator is arranged, a heater and the heat accumulator are connected in a specific mode, and a valve is regulated and controlled in a specific method to carry out switching operation. And finally, the system is self-sufficient in power without external power supply.
Disclosure of Invention
The invention aims to provide a compressed gas purification system and a compressed gas purification process without external power supply.
The system comprises a heat exchanger, a gas-liquid separator, an air inlet pipeline, an absorber, a product pipeline, an expander, a heater, a heat accumulator, a regeneration pipeline, an exhaust pipeline and a valve, wherein an air inlet of the gas-liquid separator is connected with an air outlet at the hot side of the heat exchanger, an air inlet at the hot side of the heat exchanger is connected with a raw material gas inlet, and an air outlet of the gas-liquid separator is connected with a non-branch part of the air inlet pipeline; the gas inlet pipeline, the product pipeline, the regeneration pipeline and the gas exhaust pipeline are provided with a branch part and a non-branch part, and the two branch parts of the gas inlet pipeline are respectively connected with the feed ends of the first adsorber and the second adsorber through a first valve and a second valve; two branch parts of the exhaust pipeline are respectively connected with the feed ends of the first adsorber and the second adsorber through a third valve and a fourth valve; two branch parts of the product pipeline are respectively connected with the discharge ends of the first adsorber and the second adsorber through a fifth valve and a sixth valve; two branch parts of the regeneration pipeline are respectively connected with the discharge ends of the first adsorber and the second adsorber through a seventh valve and an eighth valve; the non-branch part of the product pipeline is connected with the air inlet of the expander and the product gas outlet, and the air outlet of the expander is connected with the cold side air inlet of the heat exchanger; the lower end of the heat accumulator is connected to the upper end of the heater, the upper end of the heat accumulator and the lower end of the heater are respectively connected to the non-branch part of the regeneration pipeline through a valve nine and a valve ten, and the upper end of the heat accumulator and the lower end of the heater are also respectively connected to a cold side exhaust port of the heat exchanger through a valve eleven and a valve twelve; and a cable is arranged between the expander and the heater, and the expander provides electric energy for the heater.
The method specifically comprises the following steps:
s1: the raw material gas is introduced into a hot side air inlet of the heat exchanger, the temperature is reduced after heat is released in the heat exchanger, and then the raw material gas is discharged through a hot side air outlet of the heat exchanger;
s2: gas from a hot side exhaust port of the heat exchanger passes through a gas-liquid separator and then is introduced into the adsorber in the adsorption step through a gas inlet pipeline, so that the gas passes through the adsorber to be changed into product gas and is discharged to a product pipeline;
s3: one part of the gas from the product pipeline is used as product gas, and the other part of the gas is introduced into a gas inlet of the expander to drive the expander to generate power, so that the pressure of the gas is reduced, and the gas is discharged through a gas outlet of the expander;
s4: the gas from the exhaust port of the expander is introduced into the cold side air inlet of the heat exchanger, the temperature is increased after the heat is absorbed in the heat exchanger, and then the gas is exhausted through the cold side exhaust port of the heat exchanger;
s5: gas from the cold side vent of the heat exchanger is passed through a regeneration line to the adsorber in the regeneration step, passing through the adsorber and venting to a vent line.
Wherein, the first adsorber and the second adsorber repeatedly execute a cycle including an adsorption step and a regeneration step.
S1, the raw material gas is one of air, natural gas or mixed gas containing volatile organic compounds; the pressure of the feed gas is in the range of 5-10 bar.
The mass flow of the gas entering the expansion machine in the S3 accounts for 5-15% of the mass flow of the raw material gas.
The regeneration step in the S5 comprises a heating step and a cooling step, when the adsorber is in the heating step, a valve ten and a valve eleven are opened, a valve nine and a valve twelve are closed, and gas flows through the heat accumulator and the heater in sequence; when the adsorber is in the cool down step, valves nine and twelve are open, valves ten and eleven are closed, and the gas flows through the heater and regenerator in sequence.
The duration of the heating step is greater than the duration of the cooling step; in the heating step, the exhaust temperature of the heater is in a descending trend along with the time, and the change range of the exhaust temperature is larger than 50 ℃ from the beginning of the heating step to the end of the heating step.
The mass flow rate of the gas flowing through the expander in the heating step is greater than the mass flow rate of the gas flowing through the expander in the cooling step.
The technical scheme of the invention has the following beneficial effects:
in the scheme, the invention obtains cold energy and electric energy by utilizing the expansion of high-pressure gas, the cold energy is used for reducing the temperature of feed gas, and the electric energy is stored in the heat accumulator in the step of cooling the adsorber and used for providing energy consumption required by the regeneration of the adsorber in the step of heating the adsorber through specific pipeline connection and valve switching, thereby realizing the self-sufficiency of system electric power without external power supply, further reducing the system energy consumption and improving the purification performance of the system, and having great significance for energy conservation in industrial occasions such as compressed air drying, natural gas treatment and the like.
Drawings
FIG. 1 is a process flow diagram of the system of the present invention.
Wherein: 1-heat exchanger, 2-gas-liquid separator, 4-expander, 5-heater, 6-regenerator, 31-adsorber I, 32-adsorber II, 33-inlet line, 34-product line, 35-regeneration line, 36-vent line, 45-cable, 331-valve I, 332-valve II, 341-valve V, 342-valve VI, 351-valve VII, 352-valve VIII, 353-valve nine, 354-valve eleven, 355-valve eleven, 356-valve twelve, 361-valve III, 362-valve IV.
Detailed Description
In order to make the technical problems, technical solutions and advantages of the present invention more apparent, the following detailed description is given with reference to the accompanying drawings and specific embodiments.
The invention provides a compressed gas purification system and a process without external power supply.
As shown in fig. 1, the system comprises a heat exchanger 1, a gas-liquid separator 2, a gas inlet pipeline 33, an adsorber, a product pipeline 34, an expander 4, a heater 5, a heat accumulator 6, a regeneration pipeline 35, a gas outlet pipeline 36 and a valve, wherein a gas inlet of the gas-liquid separator 2 is connected to a gas outlet at the hot side of the heat exchanger 1, a gas inlet at the hot side of the heat exchanger 1 is connected to a raw gas inlet, and a gas outlet of the gas-liquid separator 2 is connected to a non-branch part of the gas inlet pipeline 33; the feed line 33, the product line 34, the regeneration line 35, the exhaust line 36 have a branched portion and a nonbranched portion, the two branched portions of the feed line 33 being connected to the feed ends of the adsorbers one 31 and two 32, respectively, by valves one 331 and two 332; the two branch portions of the vent line 36 are connected to the feed ends of adsorber one 31 and adsorber two 32, respectively, by valve three 361 and valve four 362; the two branch parts of the product pipeline 34 are respectively connected with the discharge ends of the first adsorber 31 and the second adsorber 32 through a fifth valve 341 and a sixth valve 342; the two branch portions of the regeneration line 35 are connected to the discharge ends of the first adsorber 31 and the second adsorber 32 through a seventh valve 351 and an eighth valve 352, respectively; the two non-branched parts of the product line 34 are connected to the inlet of the expander 4 and the product gas outlet, the exhaust of the expander 4 is connected to the cold side inlet of the heat exchanger 1; the lower end of the regenerator 6 is connected to the upper end of the heater 5, the upper end of the regenerator 6 and the lower end of the heater 5 are connected to the non-branch portion of the regeneration line 35 through a valve nine 353 and a valve ten 354, respectively, and the upper end of the regenerator 6 and the lower end of the heater 5 are also connected to the cold-side exhaust port of the heat exchanger 1 through a valve eleven 355 and a valve twelve 356, respectively; a cable 45 is provided between the expander 4 and the heater 5, and the expander 4 supplies electric power to the heater 5.
In the specific application process, the system mainly comprises the following operation steps:
in the following operations, each adsorber repeatedly performs a cycle comprising an adsorption step and a regeneration step;
s1: the raw gas is introduced into the hot side of the heat exchanger 1, cooled in the heat exchanger 1, and discharged, and the raw gas generally refers to air, natural gas, and the like.
S2: the gas discharged from the hot side of the heat exchanger 1 passes through the gas-liquid separator 2 and is introduced into the adsorber in the adsorption step through the gas inlet line 33, passes through the adsorber, is changed into a product gas, and is discharged to the product line 34;
s3: a part of the gas from the product line 34 is used as a product gas, and the other part of the gas is introduced into the gas inlet of the expander 4, and the pressure of the gas is reduced after the expander 4 is driven to generate electricity, and then the gas is discharged through the gas outlet of the expander 4; the electric energy output by the expansion machine 4 is supplied to a heater 5;
s4: gas exhausted from the expansion machine 4 enters the cold side of the heat exchanger 1, is heated in the heat exchanger 1 and is exhausted after being heated;
s5: the gas discharged from the cold side of the heat exchanger 1 is passed via a regeneration line 35 into the adsorber in the regeneration step, through which it is discharged into a discharge line 36. The regeneration step comprises: a heating step and a cooling step. When the adsorber is in the heating step: valves ten 354 and eleven 355 open, valves nine 353 and twelve 356 close, and gas flows through the regenerator 6 and heater 5 in sequence. While the adsorber is in the cooling step: valves nine 353 and twelve 356 open and valves ten 354 and eleven 355 close, and gas flows through heater 5 and regenerator 6 in sequence.
Further, the duration of the heating step is greater than the duration of the cooling step.
Further, in the heating step, the exhaust gas temperature of the heater 5 is in a downward trend with time, and the variation range of the exhaust gas temperature of the heater 5 is more than 50 ℃ from the beginning of the heating step to the end of the heating step.
Further, the pressure of the feed gas is in the range of 5-10 bar.
Further, the ratio of the mass flow of the gas entering the expander 4 to the mass flow of the raw material gas is in the range of 5-15%.
Further, the mass flow rate of the gas flowing through the expander 4 in the heating step is larger than the mass flow rate of the gas flowing through the expander 4 in the cooling step.
While the foregoing is directed to the preferred embodiment of the present invention, it will be appreciated by those skilled in the art that various changes and modifications may be made therein without departing from the principles of the invention as set forth in the appended claims.
Claims (6)
1. A compressed gas purification system without external power supply is characterized in that: the system comprises a heat exchanger (1), a gas-liquid separator (2), a gas inlet pipeline (33), adsorbers, a product pipeline (34), an expansion machine (4), a heater (5), a heat accumulator (6), a regeneration pipeline (35), a gas outlet pipeline (36) and valves, wherein a gas inlet of the gas-liquid separator (2) is connected with a gas outlet at the hot side of the heat exchanger (1), a gas inlet at the hot side of the heat exchanger (1) is connected with a raw gas inlet, a gas outlet of the gas-liquid separator (2) is connected with a non-branch part of the gas inlet pipeline (33), and two branches of the gas inlet pipeline (33) are respectively connected with the feed ends of the adsorbers (31) and the adsorbers (32) through a valve I (331) and a valve II (332); the two branches of the exhaust line (36) are respectively connected with the feed ends of the first adsorber (31) and the second adsorber (32) through a third valve (361) and a fourth valve (362); two branches of the product pipeline (34) are respectively connected with the discharge ends of the first adsorber (31) and the second adsorber (32) through a fifth valve (341) and a sixth valve (342); two branches of the regeneration pipeline (35) are respectively connected with the discharge ends of the first adsorber (31) and the second adsorber (32) through a seventh valve (351) and an eighth valve (352); the non-branch part of the product pipeline (34) is connected with the air inlet of the expansion machine (4) and the product gas outlet, and the air outlet of the expansion machine (4) is connected with the cold side air inlet of the heat exchanger (1); the lower end of the heat accumulator (6) is connected to the upper end of the heater (5), the upper end of the heat accumulator (6) and the lower end of the heater (5) are respectively connected to the non-branch part of the regeneration pipeline (35) through a valve nine (353) and a valve ten (354), and the upper end of the heat accumulator (6) and the lower end of the heater (5) are also respectively connected to the cold side exhaust port of the heat exchanger (1) through a valve eleven (355) and a valve twelve (356); a cable (45) is arranged between the expansion machine (4) and the heater (5), and the expansion machine (4) provides electric energy for the heater (5);
the process applying the compressed gas purification system comprises the following steps:
s1: the raw material gas is introduced into a hot side air inlet of the heat exchanger (1), the temperature is reduced after heat is released in the heat exchanger (1), and then the raw material gas is discharged through a hot side air outlet of the heat exchanger (1);
s2: gas from a hot side exhaust port of the heat exchanger (1) passes through the gas-liquid separator (2) and then is introduced into the adsorber in the adsorption step through the gas inlet pipeline (33), so that the gas passes through the adsorber to be changed into product gas and is discharged to the product pipeline (34);
s3: one part of the gas from the product pipeline (34) is used as product gas, and the other part of the gas is introduced into the gas inlet of the expander (4), the pressure of the gas is reduced after the expander (4) is driven to generate electricity, and then the gas is discharged through the gas outlet of the expander (4);
s4: the gas from the exhaust port of the expander (4) is introduced into the cold side inlet of the heat exchanger (1), the temperature is increased after the heat is absorbed in the heat exchanger (1), and then the gas is exhausted through the cold side exhaust port of the heat exchanger (1);
s5: gas from the cold side vent of the heat exchanger (1) is passed via a regeneration line (35) to the adsorber in the regeneration step, through which it is discharged to a vent line (36);
the regeneration step in the S5 comprises a heating step and a cooling step, when the adsorber is in the heating step, a valve ten (354) and a valve eleven (355) are opened, a valve nine (353) and a valve twelve (356) are closed, and gas flows through the heat accumulator (6) and the heater (5) in sequence; when the adsorber is in the cool down step, valves nine (353) and twelve (356) are open, valves ten (354) and eleven (355) are closed, and gas flows through heater (5) and regenerator (6) in sequence.
2. The compressed gas purification system without external power supply of claim 1, wherein: both adsorber one (31) and adsorber two (32) repeat a cycle that includes an adsorption step and a regeneration step.
3. The compressed gas purification system without external power supply of claim 1, wherein: the raw material gas in the S1 is one of air, natural gas or mixed gas containing volatile organic compounds; the pressure of the feed gas is in the range of 5-10 bar.
4. The compressed gas purification system without external power supply of claim 1, wherein: and the mass flow rate of the gas entering the expansion machine (4) in the S3 is 5-15% of the mass flow rate of the raw material gas.
5. The compressed gas purification system without external power supply of claim 1, wherein: the duration of the heating step is longer than the duration of the cooling step; in the heating step, the exhaust temperature of the heater (5) is in a descending trend along with the time, and the change range of the exhaust temperature is more than 50 ℃ from the beginning of the heating step to the end of the heating step.
6. The compressed gas purification system without external power supply of claim 1, wherein: the mass flow rate of the gas flowing through the expander (4) in the heating step is greater than the mass flow rate of the gas flowing through the expander (4) in the cooling step.
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| JPH0868318A (en) * | 1994-08-26 | 1996-03-12 | Komatsu Ltd | Exhaust gas heat recovery device for internal combustion engine having exhaust emission control device and its controlling method |
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| CN103410574B (en) * | 2013-07-31 | 2016-01-06 | 北京硕人海泰能源环境技术有限公司 | Natural gas pressure difference generating and cold recovery system and Application way |
| CN110578559B (en) * | 2018-06-08 | 2021-03-19 | 清华大学 | Compressed air energy storage and heat regeneration system and method |
| CN111238167B (en) * | 2020-03-17 | 2024-04-16 | 北京科技大学 | Energy-saving heating device and method for air separation device |
| CN112201824A (en) * | 2020-10-15 | 2021-01-08 | 西南化工研究设计院有限公司 | Method and system device for preparing hydrogen for purifying fuel cell |
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| JPH0868318A (en) * | 1994-08-26 | 1996-03-12 | Komatsu Ltd | Exhaust gas heat recovery device for internal combustion engine having exhaust emission control device and its controlling method |
| CN203394597U (en) * | 2013-07-31 | 2014-01-15 | 北京硕人海泰能源环境技术有限公司 | Natural gas differential pressure power generation and cold recovery system |
| CN204153781U (en) * | 2014-06-30 | 2015-02-11 | 北京科技大学 | Emission coal gas utilizes system |
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