CN204767539U - Application low temperature condensation method carries out device system that VOC got rid of - Google Patents
Application low temperature condensation method carries out device system that VOC got rid of Download PDFInfo
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- CN204767539U CN204767539U CN201520403126.3U CN201520403126U CN204767539U CN 204767539 U CN204767539 U CN 204767539U CN 201520403126 U CN201520403126 U CN 201520403126U CN 204767539 U CN204767539 U CN 204767539U
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Classifications
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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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- 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
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses an application low temperature condensation method carries out device system that VOC got rid of, including VOC desorption module, energy recuperation module and refrigerating module, the external gas of VOC desorption pair of module carries out the VOC desorption, and refrigerating module provides refrigerating medium and gives VOC desorption module, and the heat of refrigerating module release is retrieved to the energy recuperation module, and the external gas behind the energy recuperation pair of module VOC desorption module desorption VOC heats. The utility model discloses a VOC desorption module adopts the cooling method to realize VOC desorption gaseous to external world, has higher VOC desorption efficiency, refrigerating module can give the refrigerating medium that provides of VOC desorption module continuation to can realize utilizing refrigerating medium's circulation is high -efficient, can save the outer refrigerating medium owing to increase and the cost that increases.
Description
Technical Field
The utility model relates to a VOC desorption, in particular to utilize the low temperature condensation method to carry out the device system of VOC desorption to gases such as marsh gas, landfill gas shale gas, synthetic gas.
Background
Volatile Organic Compounds (VOC) generally refer to organic compounds having a vapor pressure of > 70.91Pa at room temperature and a boiling point in air of 260 ℃ or lower, and generally include alkanes, alkenes, alkynes, aromatics, ketones, alcohols, ethers, esters, and the like, and organic compounds partially containing N, O, s, halogen, and other substitute atoms. VOC is ubiquitous in biogas or landfill gas and the like, and detection methods such as gas chromatography, spectrum (GC-MS) and the like are operated, so that the number of VOC substances can reach hundreds, and common VOC comprises benzene, toluene, xylene, pinene and the like.
In the process of gas purification process such as biogas or landfill gas, including the main processes such as purification by using a gas separation membrane, the VOC is required to be pre-removed so as to meet the inlet conditions of the processes such as purification by using the gas separation membrane, and the like, and ensure the efficiency and the service life of the main purification process and the quality of the biogas (such as whether the hydrocarbon dew point is saturated or not) of the rear-end product.
However, because the VOC components in different gases such as biogas or landfill gas are complex and have different concentrations, it is difficult to perform qualitative or quantitative determination on the VOC components, which increases the difficulty in selecting the VOC removal process. At present, the main processes for removing VOC from biogas or landfill gas are as follows: active carbon adsorption, catalytic oxidation combustion, condensation and the like.
Activated carbon adsorption is generally of the disposable and regenerative type. The disposable activated carbon is simple in adsorption configuration, but is generally only suitable for low-concentration VOC removal, and the activated carbon with saturated adsorption is classified as dangerous waste, which causes secondary pollution if directly discarded in the environment.
The regenerative activated carbon is suitable for removing VOC with higher concentration, but needs to be provided with a heat source and an activated carbon regeneration facility, so that the equipment cost and the energy consumption cost in the VOC removing process are higher; the active carbon gradually loses activity after being regenerated for many times, so the active carbon needs to be replaced every three to five years; in addition, the activated carbon may discharge VOC to the surrounding environment during regeneration, which may cause secondary pollution.
The catalytic combustion method can convert most of VOC substances into water and carbon dioxide, but due to the fact that VOC components in methane or landfill gas are complex and the combustion temperatures are different, insufficient combustion is easily caused, VOC removal is insufficient, and further downstream process performance is affected. And the catalytic combustion method has higher equipment cost and energy consumption cost.
The common condensation method VOC removing device mainly comprises normal temperature cold drying equipment and deep cooling condensation equipment. The normal temperature cold drying equipment is mature, the equipment cost and the energy consumption cost are low, the normal temperature cold drying equipment is mainly used for controlling the moisture pressure dew point in the methane or the landfill gas to be reduced to about 5 ℃, and meanwhile, some high-boiling-point VOCs are removed by the normal temperature cold drying equipment. But overall the VOC removal rate is not high and cannot directly meet the purification process inlet conditions.
The cryogenic condensation method mainly means that VOC is basically condensed and removed by utilizing contact heat exchange between low-temperature substances such as liquid nitrogen and gases such as methane or landfill gas. The disadvantages are that the system is complex, the investment is high, and consumables such as liquid nitrogen are needed, which causes over high cost.
SUMMERY OF THE UTILITY MODEL
The utility model provides a VOC removing device to solve at least one of above-mentioned problem.
According to one aspect of the utility model, a device system for VOC removal by using a low-temperature condensation method is provided, which comprises a refrigerant compressor, an energy recovery device, a refrigerant oil separator, an air-cooled oil cooler, a condensing device, a high-pressure liquid storage device, a low-pressure liquid storage device, a first evaporator, a first gas-liquid separator, a second evaporator, a second gas-liquid separator and a refrigerant gas-liquid separator; wherein,
the inlet of a refrigerant compressor is connected with the outlet of a refrigerant gas-liquid separator, the outlet of the refrigerant compressor is connected with the refrigerant side inlet of an energy recovery device, the refrigerant side outlet of the energy recovery device is connected with the inlet of a refrigerant oil separator, the refrigerant side outlet of the oil separator is connected with the inlet of a condensing device, the outlet of the condensing device is connected with the inlet of a high-pressure liquid storage device, the outlet of the high-pressure liquid storage device is connected with the inlet of a low-pressure liquid storage device, the gas side outlet of the low-pressure liquid storage device is connected with the inlet of the refrigerant gas-liquid separator, the outlet of the refrigerant gas-liquid separator is connected with the inlet of the refrigerant compressor, the oil outlet of the refrigerant oil separator is connected with the;
the refrigerant side inlets of the first evaporator and the second evaporator are connected in parallel to the liquid side outlet of the low-pressure liquid storage device, and the refrigerant side outlets of the first evaporator and the second evaporator are connected in parallel to the inlet of the low-pressure liquid storage device;
the first evaporator and the second evaporator are connected in parallel at cooling gas side inlets, a cooling gas side outlet of the first evaporator is connected with an inlet of the first gas-liquid separator, a cooling gas side outlet of the second evaporator is connected with an inlet of the second gas-liquid separator, gas outlets of the first gas-liquid separator and the second gas-liquid separator are respectively connected with an inlet of the energy recovery device, and the energy recovery device is also provided with a gas outlet.
The first evaporator and the second evaporator of the utility model realize the VOC removal of the outside air by adopting a low-temperature condensation mode, and have higher VOC removal efficiency; the low-pressure liquid accumulator can continuously provide a refrigerating medium for the VOC removing module, the refrigerating medium can be efficiently recycled through the interconnection and circulation of the refrigerant compressor, the energy recovery device, the refrigerant oil separator, the air-cooled oil cooler, the condensing device, the high-pressure liquid accumulator, the low-pressure liquid accumulator and the refrigerant gas-liquid separator, and the cost increased by adding extra refrigerating medium can be saved; the energy recovery device can recover the extra heat generated at the outlet side of the refrigerant compressor, and the heat is used for heating the low-temperature outside gas subjected to VOC removal so as to increase the temperature of the outside gas, thereby being beneficial to the normal operation of the subsequent process, realizing the recycling of energy and saving the resource cost; in addition, the system has the advantages of simple and compact equipment structure, wide application range, convenient operation, safety, reliability, high automation degree and better economy, and is suitable for industrial production and application.
In some embodiments, the evaporation temperature of the evaporation side of the first and second evaporators is as low as zero degrees. Therefore, most of VOC can be removed at the evaporation temperature, and the VOC effect is better.
In some embodiments, the moisture on the evaporation side of the first and second evaporators is precipitated from the evaporation side surfaces of the first and second evaporators at the evaporation temperature and freezes. Therefore, the first evaporator and the second evaporator can allow micro water to enter, and a dehydration device is not required to be additionally arranged on the first evaporator and the second evaporator, so that the VOC removing process configuration is simplified.
In some embodiments, the first evaporator and the second evaporator are provided with heating means. Therefore, the heating device can unfreeze and remove frost condensed on the evaporation sides of the first evaporator and the second evaporator, so that heat exchange on the evaporation sides of the first evaporator and the second evaporator is facilitated, the internal environment temperature of the first evaporator and the second evaporator is maintained, and the first evaporator and the second evaporator can work normally.
In some embodiments, the first evaporator and the second evaporator operate alternately. Therefore, when one of the evaporators (the first evaporator or the second evaporator) is in a state of removing the frost layer covering the cooling side to cause shutdown, the other evaporator (the first evaporator or the second evaporator) is in a state of normal operation, and therefore, the alternate operation state improves the efficiency of VOC removal.
In some embodiments, the energy recovery device recovers heat at the outlet of the refrigeration compressor and heats the gas flowing into the energy recovery device from the first gas-liquid separator and the second gas-liquid separator with the recovered heat. From this, energy recuperation device can realize the cyclic utilization of energy, has saved the resource cost, and energy recuperation device can heat the gas (the gas after VOC deviates from) that gets into self, can promote the temperature of gas (the gas after VOC deviates from) that the gas (the temperature of the gas after VOC deviates from under general condition all is lower, when carrying out subsequent technology, need heat the intensification to gas to reach the technological requirement, can do benefit to the normal clear of other technologies after the VOC desorption.
In some embodiments, the gas flowing from the first evaporator and the second evaporator cooled gas side inlet is biogas or landfill gas or shale gas or syngas.
Drawings
Fig. 1 is a schematic structural diagram of a device system for VOC removal using a low-temperature condensation method according to an embodiment of the present invention.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.
Fig. 1 schematically shows a schematic structural diagram of a device system for VOC removal using cryocondensation according to a practical embodiment of the present invention.
As shown in fig. 1, an embodiment of the present invention includes a VOC removal module a, a refrigeration module B, and an energy recovery module C. The method for removing VOC by adopting condensation precipitation has high removal efficiency, and when the method is adopted, stable and reliable refrigerating media need to be provided for the VOC removal module A, so as to avoid the problems that a whole set of VOC removal system is too complex and the cost of the refrigerating media is too high due to the fact that low-temperature substances such as liquid nitrogen are adopted as the refrigerating media, the refrigerating module B of the utility model provides the refrigerating media for the VOC removal module A in a way of recycling the refrigerating media, namely, the refrigerating media are recycled to the refrigerating module B after being utilized by the VOC removal module A, and the refrigerating module B carries out condensation treatment on the recycled refrigerating media, and then the obtained product is supplied to the VOC removing module A again so as to be recycled.
As shown in fig. 1, can produce extra heat at the in-process that refrigeration module a was handled the refrigerant, in order to avoid these extra heat losses and cause the waste, the utility model discloses an energy recuperation module C gets up these extra heat recoveries, and the outside gas temperature after the VOC desorption is all lower, often need through promoting the temperature just can carry out subsequent technology, consequently, can be used for heating the lower outside gas of VOC desorption back temperature with the heat of retrieving in the energy recuperation module C, realize the recycle of resource to reach the purpose of practicing thrift the cost.
The following are specific examples:
as shown in fig. 1, in this embodiment, the VOC removing module a includes a first evaporator 8, a second evaporator 10, a first gas-liquid separator 9, and a second gas-liquid separator 11, the refrigerating module B includes a refrigerant compressor 1, a refrigerant-oil separator 3, an air-cooled oil cooler 4, a condensing device 5, a high-pressure reservoir 6, a low-pressure reservoir 7, and a refrigerant-gas-liquid separator 12, and the energy recovery module C includes an energy recovery device 2.
As shown in fig. 1, an inlet of the refrigerant compressor 1 is connected to an outlet of the refrigerant gas-liquid separator 12, an outlet of the refrigerant compressor 1 is connected to an inlet of a refrigerant side c of the energy recovery device 2, an outlet of the refrigerant side c of the energy recovery device 2 is connected to an inlet of the refrigerant oil separator 3, an outlet of a refrigerant side e of the oil separator 3 is connected to an inlet of the condensing device 5, an outlet of the condensing device 5 is connected to an inlet of the high-pressure accumulator 6, an outlet of the high-pressure accumulator 6 is connected to an inlet of the low-pressure accumulator 7, a gas side outlet of the low-pressure accumulator 7 is connected to an inlet of the refrigerant gas-liquid separator 12, an outlet of the refrigerant gas-liquid separator 12 is connected to an inlet of the refrigerant compressor 1, an oil outlet of the refrigerant oil separator 3 is connected to an inlet of the air-cooled oil cooler 4.
As shown in fig. 1, the inlets a1 of the evaporation sides a of the first evaporator 8 and the second evaporator 10 are connected in parallel to the liquid side outlet of the low pressure accumulator 7, and the outlets a2 of the evaporation sides a of the first evaporator 8 and the second evaporator 10 are connected in parallel to the inlet of the low pressure accumulator 7.
As shown in fig. 1, inlets b1 of the first evaporator 8 and the second evaporator 10 on the cooling gas side b are connected in parallel to a gas inlet 13, an outlet b2 of the first evaporator 8 on the cooling gas side b is connected to an inlet of the first gas-liquid separator 9, an outlet b2 of the second evaporator 10 on the cooling gas side b is connected to an inlet of the second gas-liquid separator 11, gas outlets of the first gas-liquid separator 9 and the second gas-liquid separator 11 are connected to an inlet of the energy recovery device 2, and the energy recovery device 2 is further provided with a gas outlet 14.
As shown in fig. 1, the evaporation temperature of the evaporation side a of the first evaporator 8 and the second evaporator 10 is lower than zero, preferably lower than 45 degrees below zero, at which almost all the VOC will be condensed out, and furthermore, the outside air (biogas or landfill gas) entering the first evaporator 8 and the second evaporator 10 generally contains gaseous water, which will be condensed out due to the lower evaporation temperature of the evaporation side b of the first evaporator 8 and the second evaporator 10, so that it is possible to eliminate the need to additionally add dehydration devices to the first evaporator 8 and the second evaporator 10, thereby simplifying the VOC removing process configuration, and the condensed out gaseous water will frost on the surface of the evaporation side a of the first evaporator 8 and the second evaporator 10, resulting in the temperature increase in the first evaporator 8 and the second evaporator 10, affecting the VOC removing efficiency of the first evaporator 8 and the second evaporator 10, therefore, a heating device (not shown) is further provided on the evaporation side a of the first evaporator 8 and the second evaporator 10 for melting and removing the frost covering the evaporation side a of the first evaporator 8 and the second evaporator 10; in order to better determine the timing of removing the frost, a temperature detector (not shown) may be disposed at the air outlet a2 of the first evaporator 8 and the second evaporator 10, when the temperature detected is higher than a set value, the evaporator (the first evaporator 8 or the second evaporator 10) may be stopped to remove the frost, and the other evaporator (the first evaporator 8 or the second evaporator 10) may be put into an operating state, so that the 2 evaporators operate alternately, thereby improving the VOC removing efficiency of the evaporators.
The process of the refrigeration module B for refrigerating the recovered refrigeration medium again is as follows: the refrigerant gas-liquid separator 12 firstly performs gas-liquid separation on the refrigeration medium recovered from the low-pressure liquid reservoir 7, the separated gaseous refrigeration medium forms a high-temperature and high-pressure refrigeration medium after being compressed by the refrigerant compressor 1, a large amount of heat is generated in the process, in order to avoid loss of the heat, an energy recovery module (heat exchanger) is arranged on a pipeline between the refrigerant compressor 1 and the refrigerant oil separator 3 to recover redundant heat, and the recovered heat is used for heating external gas with lower temperature after VOC is removed, so that the resource recycling is realized, and the purpose of saving the cost is achieved; the high-temperature high-pressure airflow coming out of the refrigerant compressor 1 is accompanied with suspended particles of oil, the oil needs to be separated out through the refrigerant oil separator 3, the separated oil is cooled by the air-cooled oil cooler 4 and then is recycled to the refrigerant compressor 1 for cyclic utilization, the high-temperature high-pressure airflow after oil separation enters the condensing device for further cooling to form liquid refrigeration medium and then is stored in the high-pressure liquid storage device 6, the refrigeration medium stored in the high-temperature liquid storage device 6 is new refrigeration medium, and the high-temperature high-pressure airflow can be supplied to the low-pressure liquid storage device 7 for use by two evaporators.
The external gas in this embodiment is biogas, and in other embodiments, the external gas may also be landfill gas, shale gas, or syngas.
The above are only some of the real-time aspects of the present invention. For those skilled in the art, without departing from the inventive concept, several modifications and improvements can be made, which are within the scope of the invention.
Claims (7)
1. The device system for removing VOC (volatile organic compounds) by using a low-temperature condensation method is characterized by comprising a refrigerant compressor (1), an energy recovery device (2), a refrigerant oil separator (3), an air-cooled oil cooler (4), a condensing device (5), a high-pressure liquid storage device (6), a low-pressure liquid storage device (7), a first evaporator (8), a first gas-liquid separator (9), a second evaporator (10), a second gas-liquid separator (11) and a refrigerant gas-liquid separator (12); wherein,
the inlet of the refrigerant compressor (1) is connected with the outlet of a refrigerant gas-liquid separator (12), the outlet of the refrigerant compressor (1) is connected with the refrigerant side inlet of the energy recovery device (2), the refrigerant side outlet of the energy recovery device (2) is connected with the inlet of a refrigerant oil separator (3), the refrigerant side outlet of the oil separator (3) is connected with the inlet of the condensing device (5), the outlet of the condensing device (5) is connected with the inlet of the high-pressure liquid accumulator (6), the outlet of the high-pressure liquid accumulator (6) is connected with the inlet of the low-pressure liquid accumulator (7), the gas side outlet of the low-pressure liquid accumulator (7) is connected with the inlet of the refrigerant gas-liquid separator (12), and the outlet of the refrigerant gas-liquid separator (12) is connected with the inlet of the refrigerant compressor (1), an oil liquid outlet of the refrigerant oil separator (3) is connected with an inlet of the air-cooled oil cooler (4), and an outlet of the air-cooled oil cooler (4) is connected with an inlet of the refrigerant compressor (1);
inlets of evaporation sides of the first evaporator (8) and the second evaporator (10) are connected into a liquid side outlet of the low-pressure liquid accumulator (7) in parallel, and outlets of refrigerant sides of the first evaporator (8) and the second evaporator (10) are connected into an inlet of the low-pressure liquid accumulator (7) in parallel;
the first evaporator (8) and the second evaporator (10) are connected in parallel at the cooling gas side inlet, the cooling gas side outlet of the first evaporator (8) is connected with the inlet of the first gas-liquid separator (9), the cooling gas side outlet of the second evaporator (10) is connected with the inlet of the second gas-liquid separator (11), the gas outlets of the first gas-liquid separator (9) and the second gas-liquid separator (11) are respectively connected with the inlet of the energy recovery device (2), and the energy recovery device (2) is further provided with a gas outlet.
2. The system of claim 1, wherein the evaporation temperature of the evaporation side of the first evaporator (8) and the second evaporator (10) is below zero.
3. The system of claim 2, wherein the moisture on the evaporating side of the first evaporator (8) and the second evaporator (10) is separated from the evaporating side surfaces of the first evaporator (8) and the second evaporator (10) at the evaporating temperature and is frozen.
4. The system of claim 3, wherein the first evaporator (8) and the second evaporator (10) are provided with heating means.
5. The system of claim 4, wherein the first evaporator (8) and the second evaporator (10) are operated alternately.
6. The system of claim 5, wherein the energy recovery device (2) recovers heat at the outlet of the refrigeration compressor (1), and the recovered heat heats the gas flowing into the energy recovery device (2) from the first gas-liquid separator (9) and the second gas-liquid separator (11).
7. The system of any of claims 1 to 6, wherein the gas flowing from the cooling gas side inlets of the first evaporator (8) and the second evaporator (10) is biogas or landfill gas or shale gas or synthesis gas.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201520403126.3U CN204767539U (en) | 2015-06-12 | 2015-06-12 | Application low temperature condensation method carries out device system that VOC got rid of |
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| CN201520403126.3U CN204767539U (en) | 2015-06-12 | 2015-06-12 | Application low temperature condensation method carries out device system that VOC got rid of |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104874199A (en) * | 2015-06-12 | 2015-09-02 | 苏州臻微工程技术有限公司 | Device system for using low temperature condensation method to remove VOC (volatile organic compound) |
| WO2019165782A1 (en) * | 2018-03-02 | 2019-09-06 | 南京工业大学 | Voc recovery system using cryogenic air |
| CN116078098A (en) * | 2023-04-06 | 2023-05-09 | 山东赛斯特冷冻系统有限公司 | VOCs waste gas treatment method |
-
2015
- 2015-06-12 CN CN201520403126.3U patent/CN204767539U/en not_active Withdrawn - After Issue
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104874199A (en) * | 2015-06-12 | 2015-09-02 | 苏州臻微工程技术有限公司 | Device system for using low temperature condensation method to remove VOC (volatile organic compound) |
| WO2019165782A1 (en) * | 2018-03-02 | 2019-09-06 | 南京工业大学 | Voc recovery system using cryogenic air |
| US11918950B2 (en) | 2018-03-02 | 2024-03-05 | Nanjing Tech University | Deep-condensation VOCs recovery system using air as refrigerant |
| CN116078098A (en) * | 2023-04-06 | 2023-05-09 | 山东赛斯特冷冻系统有限公司 | VOCs waste gas treatment method |
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