CN215822390U - Liquid nitrogen condensing system for oil gas recovery - Google Patents
Liquid nitrogen condensing system for oil gas recovery Download PDFInfo
- Publication number
- CN215822390U CN215822390U CN202122010666.3U CN202122010666U CN215822390U CN 215822390 U CN215822390 U CN 215822390U CN 202122010666 U CN202122010666 U CN 202122010666U CN 215822390 U CN215822390 U CN 215822390U
- Authority
- CN
- China
- Prior art keywords
- cooler
- organic
- pipeline
- liquid nitrogen
- tail gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
The utility model discloses a liquid nitrogen condensing system for oil gas recovery, which comprises a primary cooler, a secondary cooler and a tertiary cooler, wherein an organic tail gas inlet pipe is arranged on the primary cooler, a liquefaction pipeline on the primary cooler is communicated with a steam-water separator, organic waste gas of the steam-water separator is communicated to the secondary cooler through a pipeline, the secondary cooler is connected with a first air temperature reheater through a nitrogen pipeline, the secondary cooler is connected with a second air temperature reheater through an organic tail gas pipe, a first organic condensate discharge port on the secondary cooler is connected with a condensate collecting tank, organic tail gas cooled by the secondary cooler is communicated with the tertiary cooler through a pipeline, a second organic condensate discharge port on the tertiary cooler is connected to the condensate collecting tank, and a liquid nitrogen pipeline is arranged on the tertiary cooler. The utility model can recycle the cold energy contained in the treated tail gas and cold nitrogen through the multi-channel heat exchanger.
Description
Technical Field
The utility model belongs to the technical field of oil gas recovery, and particularly relates to a liquid nitrogen condensation system for oil gas recovery.
Background
Petrochemical industry, chemical industry enterprise are for production convenience, deposit temporarily through the storage tank with the form of liquid to raw and other materials chemicals for most. Some of the organic solvents which are liquid at normal temperature have high volatility, and organic tail gas with nitrogen as background is discharged under the condition that the storage tank breathes. For the high-concentration organic tail gas, most condensing and recycling devices are condensed by mechanical condensation or liquid nitrogen, and the petrochemical industry and the chemical industry almost use large amount of nitrogen due to safety considerations, so that the liquid nitrogen condensation is more favorable, the nitrogen vaporized by the liquid nitrogen can be continuously utilized and almost does not consume electric energy (relative to mechanical condensation), the traditional liquid nitrogen condensing system is three-level condensation, and the adjusting means only controls the temperature of the tail gas to be cooled according to a final-level liquid nitrogen condenser, so that the liquid nitrogen is wasted, the frosting of the condenser is seriously switched frequently, the tail gas treatment fluctuation is large, the finally embodied form is that the consumption of the liquid nitrogen is increased, and energy is not saved.
The process diagram of the traditional liquid nitrogen condensation recycling organic solvent in the attached figure 2 of the specification, wherein a is organic tail gas, b is a first-stage cooler A/B, c, a second-stage cooler A/B, d, a third-stage cooler A/B, e, low-temperature liquid nitrogen, f is a rewarming nitrogen return pipe network, g is a condensate collecting port, h is a condensate collecting port, i is a condensate collecting port, j is rewarming organic tail gas, k is a first air temperature rewater, and l is a second air temperature rewater; in the traditional technology for condensing and recycling the organic solvent by using the liquid nitrogen (wherein three heat exchangers of a first-stage cooler A/B, a second-stage cooler A/B and a third-stage cooler A/B are all used and prepared and are alternately used by switching valves), the amount of the liquid nitrogen can be adjusted to control the tail gas at the outlet of the third-stage cooler A/B to reach the target temperature (the required organic matter removal rate can be achieved at the design temperature, and the removed organic matter is discharged through condensate liquid), while the first second-stage cooler A/B only utilizes the supercooling cold quantity of the cold tail gas and the cold nitrogen gas without an adjusting means, so that the cooling temperature of the tail gas of the first two stages is changed, the organic tail gas such as water or some organic matter with high condensation point is solidified on the tube wall, and the condition that the three-stage coolers are all generated affects the heat exchange efficiency and increases the pressure drop at two ends of the heat exchangers, affecting normal operation. And for organic tail gas containing water vapor, the water content in the three condensate collecting ports is not beneficial to the recovery of some pure organic solvents miscible with water, and further separation treatment is needed.
Therefore, a liquid nitrogen condensing system for recovering oil gas, which is used for VOCs waste gas treatment, treating organic tail gas and simultaneously recovering an organic solvent, is proposed to solve the problems.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a liquid nitrogen condensing system for oil gas recovery, which aims to solve the problems in the background technology.
In order to achieve the purpose, the utility model provides the following technical scheme: a liquid nitrogen condensing system for oil gas recovery comprises a primary cooler, a secondary cooler and a tertiary cooler, wherein an organic tail gas inlet pipe is arranged on the primary cooler, a liquefaction pipeline on the primary cooler is communicated with a steam-water separator, organic waste gas after precooling is separated by the steam-water separator is communicated with the secondary cooler through a pipeline, the secondary cooler is connected with a first air temperature reheater through a nitrogen pipeline, the secondary cooler is connected with a second air temperature reheater through an organic tail gas pipe, the rewarming nitrogen pipe on the first air temperature reheater is communicated with a pipe network, the organic tail gas pipe is communicated with a discharge pipe after rewarming on the second air temperature reheater, a first organic condensate discharge port on the secondary cooler is connected with a condensate collecting tank through a pipeline, and the organic tail gas after cooling by the secondary cooler is communicated with the tertiary cooler through a pipeline, and a second organic condensate discharge port on the third-stage cooler is also connected to a condensate collecting tank through a pipeline, and a liquid nitrogen pipeline is arranged on the third-stage cooler.
Preferably, a chilled water inlet pipe and a chilled water return pipe are arranged on the primary cooler, and a second regulating valve is arranged on the chilled water inlet pipe.
Preferably, the liquid nitrogen pipeline is provided with a first regulating valve, so that the removal rate or the recovery rate of the organic tail gas can be ensured by effectively regulating the flow of liquid nitrogen.
Preferably, the second-stage cooler and the third-stage cooler are both double-channel heat exchangers, the double-channel heat exchangers are used for defrosting alternately by switching valves, and the use is convenient.
The utility model has the technical effects and advantages that: the liquid nitrogen condensation system for recovering oil gas is used for treating VOCs waste gas, organic solvent can be recovered while treating organic tail gas, the organic tail gas is precooled to 0-3 ℃ through a primary cooler, organic matters and water vapor with high condensation point at the temperature can be liquefied firstly, the part of liquid substances are separated through a steam-water separator, the cold energy of cold gas nitrogen and cold tail gas is recovered from the precooled organic waste gas through a secondary cooler, a double-channel secondary cooler is used for respectively cooling the organic tail gas through the cold gas nitrogen and the cold tail gas after tertiary cooling, the surplus cold energy of the two parts is fully utilized to further cool the organic tail gas, then the removal rate or the recovery rate of the organic tail gas is ensured through regulating the flow of liquid nitrogen through a tertiary cooler, the precooling temperature of the tail gas can be controlled by regulating the flow of freezing water, the tail gas is controlled to reach the target cooling temperature by regulating the flow of liquid nitrogen, the cold energy contained in the treated tail gas and cold nitrogen gas is recycled by a multi-channel heat exchanger, and the condensate of the cooler is recycled by a condensate tank or separated and recycled by post-treatment.
Drawings
FIG. 1 is a schematic structural view of the present invention;
FIG. 2 is a diagram of a conventional process for recovering an organic solvent by condensing liquid nitrogen.
In the figure: 1. an organic tail gas inlet pipe; 2. a primary cooler; 3. a secondary cooler; 4. a tertiary cooler; 5. a steam-water separator; 6. a condensate collection tank; 7. a liquid nitrogen pipeline; 8. a rewarming nitrogen pipe; 9. organic tail gas pipe after rewarming; 10. a first organic condensate discharge port; 11. a second organic condensate discharge port; 12. a first regulating valve; 13. a second regulating valve; 14. a first air-temperature reheater; 15. a second air-temperature reheater; 16. a chilled water supply pipe; 17. and a chilled water return pipe.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The utility model provides a liquid nitrogen condensing system for oil gas recovery, which comprises a primary cooler 2, a secondary cooler 3 and a tertiary cooler 4, wherein the secondary cooler 3 and the tertiary cooler 4 are both double-channel heat exchangers, and the double-channel heat exchangers are used for defrosting alternately by switching valves;
an organic tail gas inlet pipe 1 is arranged on the primary cooler 2, a chilled water inlet pipe 16 and a chilled water return pipe 17 are arranged on the primary cooler 2, a second regulating valve 13 is arranged on the chilled water inlet pipe 16, a liquefaction pipeline on the primary cooler 2 is communicated with a steam-water separator 5, precooled organic waste gas separated by the steam-water separator 5 is communicated with a secondary cooler 3 through a pipeline, the secondary cooler 3 is connected with a first air-temperature reheater 14 through a nitrogen pipeline, the secondary cooler 3 is connected with a second air-temperature reheater 15 through an organic tail gas pipe, a rewarming nitrogen pipe 8 on the first air-temperature reheater 14 is communicated with a pipe network, a rewarming organic tail gas pipe 9 on the second air-temperature reheater 15 is communicated with a discharge pipe, a first organic condensate discharge port 10 on the secondary cooler 3 is connected with a condensate collecting tank 6 through a pipeline, organic tail gas after the cooling of second grade cooler 3 is put through with tertiary cooler 4 mutually through the pipeline, second organic lime set discharge port 11 on the tertiary cooler 4 is connected to condensate collection tank 6 through the pipeline equally, be equipped with liquid nitrogen pipeline 7 on the tertiary cooler 4, be equipped with first adjusting valve 12 on the liquid nitrogen pipeline 7.
The liquid nitrogen condensation system for oil gas recovery comprises a primary cooler 2, a secondary cooler 3, a two-channel heat exchanger 3, a three-level cooler 4 and a three-level cooler, wherein organic tail gas is pre-cooled to 0-3 ℃ firstly (according to the analysis and setting of organic components), organic substances and water vapor with high condensation points at the temperature can be liquefied firstly (the temperature is above the freezing point of the substances), the part of liquid substances are separated by a steam-water separator 5, the pre-cooled organic waste gas recovers cold nitrogen and cold tail gas cold energy through the secondary cooler 3, the secondary cooler 3 is a two-channel heat exchanger (used for one use and one standby by alternately defrosting through a switching valve), the two channels respectively use cold nitrogen and the cold organic tail gas after three-level cooling, the excess cold energy of the two parts is fully utilized, the organic tail gas is further cooled, and then the removal rate or recovery rate of the organic tail gas is ensured by adjusting the flow rate of the liquid nitrogen through the three-level cooler 4 (used for one use and one standby by alternately defrosting through the switching valve), the precooling temperature of the tail gas can be controlled by adjusting the flow rate of the chilled water; the tail gas can be controlled to reach the target cooling temperature by adjusting the flow of the liquid nitrogen; the cold energy contained in the treated tail gas and cold nitrogen can be recycled through the multi-channel heat exchanger; the condensate of the cooler is recycled through a condensate tank or separated and recycled as a main component through post-treatment.
Compared with the traditional process for recycling the organic solvent by condensing liquid nitrogen, the primary cooler 2 ensures the pre-removal effect by adjusting the flow of chilled water, does not allow high condensation point substances to enter subsequent condensation, effectively reduces the frosting probability and has stable organic tail gas treatment effect; the intermediate cold recovery condenser is combined with a double-channel cooler, so that the material of the heat exchanger is reduced, and the cooling effect is better; for the organic solvent with pure components, the condensate is recovered and collected without containing water vapor, can be directly recycled, and can effectively reduce the consumption of liquid nitrogen.
The working principle and the working process of the utility model comprise the following steps:
1. organic tail gas flow: the organic tail gas is precooled to 0-3 ℃ by a first-stage cooler 2, liquid is removed by a steam-water separator 5, the gas phase enters a second-stage cooler 3 to recover surplus cold energy, the organic tail gas enters a third-stage cooler 4 after being further cooled to the design temperature, then returns to one channel in a double-channel tube pass in the second-stage cooler to release the surplus cold energy, and the organic tail gas is heated to a certain temperature and then is discharged or subjected to subsequent advanced treatment at a temperature slightly lower than the normal temperature by a second air-temperature reheater 15.
The primary cooler 2 ensures that the temperature of the organic tail gas is at a set temperature (0-3 ℃) through the flow regulation of chilled water, the tertiary cooler 4 controls the organic tail gas to reach the design temperature (design recovery rate) through the flow of liquid nitrogen, the liquid nitrogen is converted into low-temperature gaseous nitrogen after cold energy released by the tertiary cooler 4 is vaporized, the nitrogen continuously releases a part of excessive cold energy through another channel in a double-channel tube pass of the secondary cooler 3, the nitrogen is heated to a certain temperature again, and then the nitrogen is sent to the first air temperature reheater 14 to be further heated to a temperature slightly lower than the normal temperature and enters a nitrogen pipe network.
2. Condensing: the condensate of the secondary cooler 3 and the tertiary cooler 4 is directly collected through an organic condensate pipe, the organic tail gas component is single organic matter and can be directly recycled, the bi-component or multi-component organic solvent can be further separated and recycled as required, and the oil-water condensate in the steam-water separator 5 is further separated and recycled according to the technical and economic comparison.
When the pressure difference between the two ends of the second-stage cooler and the pressure difference between the two ends of the third-stage cooler reach the set pressure difference (frosting is serious) in the operation process, the standby cooler is switched, the frosting cooler is heated by hot nitrogen to be defrosted and waits for standby application, and the design is convenient for keeping the equipment continuously operating without stopping in the operation process.
Finally, it should be noted that: although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments or portions thereof without departing from the spirit and scope of the utility model.
Claims (5)
1. The utility model provides a liquid nitrogen condensing system for vapor recovery system, includes one-level cooler (2), second grade cooler (3) and tertiary cooler (4), its characterized in that: the organic tail gas inlet pipe (1) is arranged on the primary cooler (2), a liquefaction pipeline on the primary cooler (2) is communicated with a steam-water separator (5), organic waste gas after precooling is separated by the steam-water separator (5) is communicated with the secondary cooler (3) through a pipeline, the secondary cooler (3) is connected with a first air-temperature reheater (14) through a nitrogen pipeline, the secondary cooler (3) is connected with a second air-temperature reheater (15) through an organic tail gas pipe, a rewarming nitrogen pipe (8) on the first air-temperature reheater (14) is communicated with a pipe network, an organic tail gas pipe (9) on the second air-temperature reheater (15) is communicated with a discharge pipe, a first organic condensate discharge port (10) on the secondary cooler (3) is connected with a condensate collecting tank (6) through a pipeline, and the organic tail gas after cooling of the secondary cooler (3) is communicated with a tertiary cooler (4) through a pipeline, and a second organic condensate discharge port (11) on the third-stage cooler (4) is also connected to a condensate collecting tank (6) through a pipeline, and a liquid nitrogen pipeline (7) is arranged on the third-stage cooler (4).
2. The liquid nitrogen condensing system for oil and gas recovery of claim 1, wherein: the primary cooler (2) is provided with a chilled water inlet pipe (16) and a chilled water return pipe (17).
3. The liquid nitrogen condensing system for oil and gas recovery of claim 1, wherein: and a first regulating valve (12) is arranged on the liquid nitrogen pipeline (7).
4. The liquid nitrogen condensing system for oil and gas recovery of claim 2, wherein: and a second regulating valve (13) is arranged on the chilled water inlet pipe (16).
5. The liquid nitrogen condensing system for oil and gas recovery of claim 1, wherein: and the secondary cooler (3) and the tertiary cooler (4) are both double-channel heat exchangers.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122010666.3U CN215822390U (en) | 2021-08-25 | 2021-08-25 | Liquid nitrogen condensing system for oil gas recovery |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122010666.3U CN215822390U (en) | 2021-08-25 | 2021-08-25 | Liquid nitrogen condensing system for oil gas recovery |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN215822390U true CN215822390U (en) | 2022-02-15 |
Family
ID=80196861
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202122010666.3U Active CN215822390U (en) | 2021-08-25 | 2021-08-25 | Liquid nitrogen condensing system for oil gas recovery |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN215822390U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115646125A (en) * | 2022-11-08 | 2023-01-31 | 瑞燃(上海)环境工程技术有限公司 | System and method for purifying and recycling high-concentration hydrogen chloride tail gas |
| CN116099318A (en) * | 2022-12-22 | 2023-05-12 | 瑞燃(上海)环境工程技术有限公司 | Method and system for treating waste gas and multi-component chemical tail gas of chemical tank area |
-
2021
- 2021-08-25 CN CN202122010666.3U patent/CN215822390U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115646125A (en) * | 2022-11-08 | 2023-01-31 | 瑞燃(上海)环境工程技术有限公司 | System and method for purifying and recycling high-concentration hydrogen chloride tail gas |
| CN115646125B (en) * | 2022-11-08 | 2023-10-31 | 瑞燃(上海)环境工程技术有限公司 | System and method for purifying and recycling high-concentration hydrogen chloride tail gas |
| CN116099318A (en) * | 2022-12-22 | 2023-05-12 | 瑞燃(上海)环境工程技术有限公司 | Method and system for treating waste gas and multi-component chemical tail gas of chemical tank area |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN215822390U (en) | Liquid nitrogen condensing system for oil gas recovery | |
| CN107345737B (en) | Double-tower double-condensation reflux expansion nitrogen making machine and nitrogen making method thereof | |
| CN111575044B (en) | Indirect oil gas condensation recovery device and recovery process thereof | |
| CN111536726A (en) | Non-stop self-defrosting dual-channel oil gas recovery condensing unit | |
| CN107940801A (en) | A kind of space division system for recycling compressed air waste-heat | |
| CN106924988A (en) | A kind of rectification type Auto-cascade cycle low-temperature condensing vapour piece-rate system with cold recovery | |
| CN210952405U (en) | Cryogenic condenser | |
| CN1952569A (en) | Process and equipment for liquefying air-containing coal-bed gas | |
| CN214371298U (en) | Carbon dioxide gathering liquefaction recovery device | |
| CN114518016A (en) | Carbon dioxide capturing, liquefying and recycling device and method | |
| CN211025713U (en) | Waste heat recovery disappears white device that unites waste water concentration | |
| CN219231933U (en) | Carbon dioxide capturing and storing system based on compression enthalpy increase and interstage energy utilization | |
| CN115342597A (en) | LNG cold energy used for air separation and seawater desalination system and comprehensive utilization method thereof | |
| CN115671993A (en) | Carbon dioxide capturing and storing system based on compression enthalpy increase and interstage energy utilization | |
| CN114485051A (en) | Liquid ammonia dual-condition refrigerating system and liquid carbon dioxide production equipment | |
| CN208667598U (en) | A kind of novel natural gas light ends unit | |
| CN106823440A (en) | A kind of oil and gas separating system of rectification type Auto-cascade cycle cryogenic condensation | |
| CN210825447U (en) | System for primary liquid ammonia purification becomes high-purity liquid ammonia | |
| RU2285212C2 (en) | Method and device for liquefying natural gas | |
| US3466884A (en) | Process and installation for the removal of easily condensable components from gas mixtures | |
| CN110345707A (en) | A kind of multi-stage condensing system and multi-stage condensing method for petroleum vapor recovery | |
| CN220990224U (en) | Oil gas recovery system | |
| CN115193086B (en) | Methane chloride separation and recovery system and method | |
| CN204779484U (en) | Excellent integrated device is transferred to multi -purpose station oil gas water treatment energy | |
| CN216845330U (en) | Air separation nitrogen yield improving and optimizing device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |