CN111765721A - Method and system for recovering ethane decarbonization tail gas in natural gas ethane recovery project - Google Patents
Method and system for recovering ethane decarbonization tail gas in natural gas ethane recovery project Download PDFInfo
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- 239000007789 gas Substances 0.000 title claims abstract description 156
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 title claims abstract description 90
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 74
- 239000003345 natural gas Substances 0.000 title claims abstract description 35
- 238000000034 method Methods 0.000 title claims abstract description 32
- 238000011084 recovery Methods 0.000 title claims abstract description 31
- 238000005262 decarbonization Methods 0.000 title claims abstract description 16
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 234
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 117
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 117
- 239000007788 liquid Substances 0.000 claims abstract description 87
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims abstract description 74
- 230000018044 dehydration Effects 0.000 claims abstract description 46
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 46
- 238000003860 storage Methods 0.000 claims abstract description 45
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 40
- 239000002808 molecular sieve Substances 0.000 claims abstract description 39
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 39
- 239000001294 propane Substances 0.000 claims abstract description 37
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 34
- 238000001179 sorption measurement Methods 0.000 claims abstract description 31
- 238000005057 refrigeration Methods 0.000 claims abstract description 29
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 24
- 230000023556 desulfurization Effects 0.000 claims abstract description 24
- 238000007670 refining Methods 0.000 claims abstract description 22
- 229910052742 iron Inorganic materials 0.000 claims abstract description 20
- 238000000746 purification Methods 0.000 claims abstract description 15
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 8
- 239000012071 phase Substances 0.000 claims description 43
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 38
- 239000007791 liquid phase Substances 0.000 claims description 25
- 238000005261 decarburization Methods 0.000 claims description 21
- 239000004215 Carbon black (E152) Substances 0.000 claims description 9
- 229930195733 hydrocarbon Natural products 0.000 claims description 9
- 150000002430 hydrocarbons Chemical class 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 8
- 230000001105 regulatory effect Effects 0.000 claims description 8
- 238000012546 transfer Methods 0.000 claims description 7
- 239000000126 substance Substances 0.000 claims description 6
- 238000005086 pumping Methods 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 3
- 238000013022 venting Methods 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 6
- 239000012535 impurity Substances 0.000 abstract description 3
- 238000000926 separation method Methods 0.000 abstract description 3
- 238000001704 evaporation Methods 0.000 abstract description 2
- 230000008020 evaporation Effects 0.000 abstract description 2
- 239000000047 product Substances 0.000 description 17
- 239000002994 raw material Substances 0.000 description 9
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 6
- 239000005977 Ethylene Substances 0.000 description 6
- 230000008901 benefit Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 238000007664 blowing Methods 0.000 description 2
- 239000009096 changqing Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000003507 refrigerant Substances 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 239000003915 liquefied petroleum gas Substances 0.000 description 1
- 230000001050 lubricating effect Effects 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
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- Organic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention provides a method and a system for recovering ethane decarbonization tail gas in natural gas ethane recovery engineering, wherein the system comprises an inlet separator, a three-section centrifugal compressor, a primary air cooler, a secondary air cooler, a tertiary air cooler, a secondary separator, a tertiary separator, an outlet separator, an iron-based wet-process fine desulfurization device, a molecular sieve dehydration device, an active carbon adsorption device, a propane refrigeration device, a flash evaporation separator and a food-grade carbon dioxide refining device; the method aims at the decarbonization tail gas which is high in carbon dioxide content and rich in H2S, low pressure, high yield and less impurities, and adopts multistage centrifugal pressurization and interstage fine H removal2S, medium and high pressure separation, molecular sieve dehydration, active carbon adsorption, propane shallow cold liquefaction, rectification purification, pressurized liquid storage and diversified product process technical route. The pressure meets the requirement that the tail gas returns to the output natural gas at any time, and can be according to the product marketThe need to adjust the production or to stop production, and also to produce carbon dioxide products of different quality.
Description
Technical Field
The invention belongs to the field of natural gas processing and treatment, and particularly relates to a system and a method for recovering ethane decarbonization tail gas in a natural gas ethane recovery project.
Background
Ethane is a high-quality raw material of ethylene, the production cost of ethylene prepared by cracking ethane is two thirds of the molecular weight of naphtha, and the ethylene raw material C is internationally2-C4The proportion is about 48 percent, and China is restricted by raw materials, and naphtha is mainly used. The ethane product is recovered from the natural gas and is used as the raw material for preparing the ethylene by the steam thermal cracking, so that the method has positive significance for improving the yield of the ethylene product, reducing the energy consumption of an ethylene device, improving the quality and increasing the efficiency.
Therefore, with the development of the natural gas industry, the ethane recovery of natural gas attracts attention of each large oil and gas field and becomes a new economic growth point of each large oil and gas field. In the natural gas ethane recovery project, the tail gas containing carbon dioxide is rectified and condensed at low temperature along with light hydrocarbon components such as ethane and the like, and is separated from the raw material ethane in an ethane decarburization device, so that the decarbonized tail gas containing high carbon dioxide is formed, and if the decarbonized tail gas cannot be effectively recovered, air pollution is caused, and the production cost is increased.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a system and a method for recovering ethane decarburization tail gas in a natural gas ethane recovery project.
The technical scheme adopted by the invention is as follows:
a method for recovering ethane decarbonization tail gas in natural gas ethane recovery engineering comprises the following steps:
s1, introducing ethane decarburization tail gas from a boundary region into an inlet separator, separating free water carried by the ethane decarburization tail gas, introducing the separated gas phase into a three-section centrifugal compressor, and pumping a liquid phase into a condensate collection tank;
s2, gas phase tail gas separated by an inlet separator is connected to a first section inlet of a three-section centrifugal compressor, the pressurized tail gas is cooled by a first-stage air cooler, enters a second-stage separator to separate out condensed free water and enters a second section inlet of the compressor, the secondarily pressurized tail gas is cooled by a second-stage air cooler, enters a third-stage separator to separate out condensed free water and enters a third section inlet of the three-section centrifugal compressor, and the thirdly pressurized tail gas is cooled by a third-stage air cooler and enters an outlet separator to separate out the condensed free water;
s3, dividing the middle and high pressure tail gas separated by the outlet separator in the step S2 into two paths, and conveying one path of the tail gas to an iron-based wet fine desulfurization device for deep H removal2S; the other path is conveyed to a high-pressure tail gas storage tank;
s4, transferring the fine desulfurization tail gas from the iron-based wet fine desulfurization device in the step S3 into a molecular sieve dehydration device for dehydration;
s5, dividing the tail gas dehydrated by the molecular sieve dehydration device from the step S4 into two paths, wherein one path is conveyed to an activated carbon adsorption device for adsorption and purification to remove heavy hydrocarbon substances and residual trace H contained in the tail gas2S, conveying to a propane refrigeration device for cooling and liquefying; the other path is directly conveyed to a propane refrigeration device for cooling and liquefaction without adsorption and purification;
s6, introducing the liquid cooled and liquefied by the propane refrigeration device from the step S5 into a flash separator, wherein the liquid after flash evaporation is industrial liquid carbon dioxide;
s7, outputting the industrial liquid carbon dioxide obtained in the step S6 in two paths, and conveying one path to a corresponding industrial liquid carbon dioxide spherical tank for low-temperature storage; and the other path is conveyed to a food-grade carbon dioxide refining device for rectification and purification, a small amount of non-condensable gas contained in the industrial-grade liquid carbon dioxide is removed to obtain food-grade carbon dioxide, and the obtained food-grade carbon dioxide is further conveyed to a food-grade carbon dioxide spherical tank for low-temperature storage.
Further, the method further includes step S8, and the flash gas from step S6 and step S7 is sent to a venting device.
Further, the condensed water separated by the second-stage separator, the third-stage separator and the outlet separator in the step S2 is sent to the inlet separator to form a circulation.
A system for recovering ethane decarbonization tail gas in natural gas ethane recovery engineering at least comprises an inlet separator, a three-section centrifugal compressor, a first-stage air cooler, a second-stage air cooler, a third-stage air cooler, a second-stage separator, a third-stage separator, an outlet separator, an iron-based wet-method fine desulfurization device, a molecular sieve dehydration device, an active carbon adsorption device, a propane refrigeration device, a flash separator and a food-grade carbon dioxide refining device;
the tail gas of ethane decarburization is connected with an inlet of an inlet separator through a pipeline, a liquid phase outlet of the inlet separator is connected with a condensate collecting tank through a pipeline, a gas phase outlet of the inlet separator is connected with a first section inlet of a three-section centrifugal compressor through a pipeline, the first section outlet of the three-section centrifugal compressor is sequentially connected with a first-stage air cooler and a second-stage separator through pipelines, the gas phase outlet of the second-stage separator is connected with a second section inlet of the three-section centrifugal compressor through a pipeline, the second section outlet of the three-section centrifugal compressor is sequentially connected with a second-stage air cooler and a third-stage separator through pipelines, the gas phase outlet of the third-stage separator is connected with a third section inlet of the three-section centrifugal compressor through a pipeline, and the third section outlet of the three-section centrifugal compressor is;
the outlet separator is provided with a first gas phase outlet and a second gas phase outlet, the first gas phase outlet of the outlet separator is used for conveying high-pressure tail gas to a high-pressure tail gas storage tank through a pipeline, the second gas phase outlet of the outlet separator is sequentially connected with the iron-based wet-method fine desulfurization device and the molecular sieve dehydration device through pipelines, the molecular sieve dehydration device is provided with a first outlet and a second outlet, the first outlet of the molecular sieve dehydration device is directly connected with an inlet of the propane refrigeration device through a pipeline, the second outlet of the molecular sieve dehydration device is connected with an inlet of the propane refrigeration device through an activated carbon adsorption device, an outlet of the propane refrigeration device is connected with an inlet of the flash separator, the flash separator is provided with a gas phase outlet and a liquid phase outlet, the gas phase outlet of the flash separator is connected with an emptying device, the liquid phase outlet of the flash separator is divided into two paths, and one path is connected with the, the other path is connected with an inlet of a food-grade carbon dioxide refining device through a pipeline, and an outlet of the food-grade carbon dioxide refining device is connected with a food-grade liquid carbon dioxide storage tank through a pipeline.
Further, liquid phase outlets of the second-stage separator, the third-stage separator and the outlet separator are respectively connected with an inlet of the inlet separator through pipelines.
Further, install industrial grade liquid carbon dioxide pipeline on the industrial grade liquid carbon dioxide storage tank, be connected with ninth block valve and first loading pump on the industrial grade liquid carbon dioxide pipeline.
Further, install food level liquid carbon dioxide conveying line on the food level liquid carbon dioxide storage tank, be connected with tenth shut-off valve and second loading pump on the food level liquid carbon dioxide conveying line.
Preferably, the liquid phase outlet of the inlet separator is connected with the condensate collecting tank through a water transfer pump; a liquid level regulating valve and a liquid level meter are arranged on a connecting pipeline between the water transfer pump and the condensed water collecting tank, and the liquid level meter is arranged between the inlet separator and the liquid level regulating valve.
Specifically, a first cut-off valve is arranged on a connecting pipeline between the ethane decarbonization tail gas and an inlet of the inlet separator;
an inlet pressure detector is connected on a connecting pipeline between the gas phase outlet of the inlet separator and the first section inlet of the three-section centrifugal compressor;
a second cut-off valve is arranged on a connecting pipeline between a first gas phase outlet of the outlet separator and the high-pressure tail gas storage tank; a third cut-off valve is arranged on a connecting pipeline between a second outlet of the outlet separator and an inlet of the iron-based wet fine desulfurization device;
a fourth block valve is arranged on a connecting pipeline between the first outlet of the molecular sieve dehydration device and the inlet of the propane refrigeration device; a fifth block valve is arranged on a connecting pipeline between a second gas phase outlet of the molecular sieve dehydration device and the activated carbon adsorption device;
a sixth block valve is arranged on a connecting pipeline between the liquid phase outlet of the flash separator and the industrial-grade liquid carbon dioxide storage tank; a seventh block valve is arranged on a connecting pipeline between the liquid phase outlet of the flash separator and the inlet of the food-grade carbon dioxide refining device; and an eighth block valve is arranged on a connecting pipeline between the outlet of the food-grade carbon dioxide refining device and the food-grade liquid carbon dioxide storage tank.
Further, a variable frequency motor is connected to the three-section centrifugal compressor, and the variable frequency motor and the inlet pressure detector form a control loop.
The invention has the following beneficial effects:
(1) the invention aims at the decarbonization tail gas which is high in carbon dioxide content and rich in H2S, low pressure, high yield and less impurities, and adopts multistage centrifugal pressurization and interstage fine H removal2S, medium and high pressure separation, molecular sieve dehydration, active carbon adsorption, propane shallow cold liquefaction, rectification purification, pressurized liquid storage and diversified product process technical route. The pressure meets the requirement that the tail gas returns to the exported natural gas at any time, the product yield can be adjusted or the production can be stopped according to the needs of the product market, and carbon dioxide products with different qualities can be produced, for example, industrial-grade carbon dioxide products can be produced, and food-grade products can also be produced.
(2) The method and the system for recovering the carbon dioxide from the ethane decarburization tail gas in the natural gas ethane recovery project can realize deep dehydration of the engineering raw material ethane and meet the requirement that the water dew point of an ethane gaseous product reaches 0.1ppm quality index; the method and the system can automatically complete the adsorption, heating and cold blowing sequence control and circulation of molecular sieve dehydration, and can adjust the set period or adjust the sequence control step at any time according to the adsorption effect, thereby achieving the purpose of deep dehydration of ethane without human intervention.
(3) The method and the system for recovering the carbon dioxide from the ethane decarburization tail gas in the natural gas ethane recovery project can realize the recovery and utilization of the carbon dioxide in the tail gas of the ethane decarburization device; the environmental pollution caused by the local emission of carbon dioxide is reduced, the influence of the application of carbon dioxide emission indexes on the construction progress of engineering is reduced, the carbon dioxide emission is prevented from occupying the indexes of local carbon emission, and the recovered carbon dioxide can be changed into valuable substances to improve the economic benefit.
The foregoing description is only an overview of the technical solutions of the present invention, and in order to clearly understand the technical solutions of the present invention and to implement the technical solutions according to the contents of the description, the following detailed description is given with reference to the preferred embodiments of the present invention and the accompanying drawings.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings needed in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings without creative efforts.
FIG. 1 is a schematic process flow diagram of the present invention.
Description of reference numerals:
1. ethane decarbonization tail gas; 2. a first shut-off valve; 3. an inlet separator; 4. an inlet pressure detector; 5. a three-stage centrifugal compressor; 6. a variable frequency motor; 7. a primary air cooler; 8. a secondary separator; 9. a secondary air cooler; 10. a third stage separator; 11. a third-stage air cooler; 12. an outlet separator; 13. a third block valve; 14. an iron-based wet fine desulfurization device; 15. a molecular sieve dehydration unit; 16. a fourth block valve; 17. a fifth block valve; 18. an activated carbon adsorption unit; 19. a propane refrigeration unit 20, a flash separator; 21. a seventh block valve; 22. a food-grade carbon dioxide refining unit; 23. an industrial-grade liquid carbon dioxide storage tank; 24. a food-grade liquid carbon dioxide storage tank; 25. a sixth block valve; 26. a ninth block valve; 27. a first loading pump; 28. an eighth block valve; 29. a tenth block valve; 30. a second loading pump; 31. an industrial grade liquid carbon dioxide transfer line; 32. a food grade liquid carbon dioxide delivery line; 33. an emptying device; 34. a second block valve; 35. a high-pressure tail gas storage tank; 36. transferring a water pump; 37. a liquid level regulating valve; 38. a liquid level meter; 39. and a condensed water collection tank.
Detailed Description
The following description of the embodiments of the present invention is provided for illustrative purposes, and other advantages and effects of the present invention will become apparent to those skilled in the art from the present disclosure.
The exemplary embodiments of the present invention will now be described with reference to the accompanying drawings, however, the present invention may be embodied in many different forms and is not limited to the embodiments described herein, which are provided for complete and complete disclosure of the present invention and to fully convey the scope of the present invention to those skilled in the art. The terminology used in the exemplary embodiments illustrated in the accompanying drawings is not intended to be limiting of the invention. In the drawings, the same units/elements are denoted by the same reference numerals.
Unless otherwise defined, terms (including technical and scientific terms) used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. Further, it will be understood that terms, such as those defined in commonly used dictionaries, should be interpreted as having a meaning that is consistent with their meaning in the context of the relevant art and will not be interpreted in an idealized or overly formal sense.
The first embodiment:
the first embodiment of the invention relates to a method for recovering ethane decarburization tail gas in a natural gas ethane recovery project, which comprises the following steps with reference to FIG. 1:
s1, introducing the ethane decarburization tail gas 1 from the outside of the boundary area into an inlet separator 3, separating the free water carried by the ethane decarburization tail gas, introducing the separated gas phase into a three-section type centrifugal compressor 5, and pumping the liquid phase into a condensate collection tank 39;
s2, gas phase tail gas separated by the inlet separator 3 is connected to a first section inlet of the three-section centrifugal compressor 5, the supercharged tail gas is cooled by the primary air cooler 7, enters the secondary separator 8 to separate out condensed free water and enters a second section inlet of the compressor, the secondarily supercharged tail gas is cooled by the secondary air cooler 9, enters the tertiary separator 10 to separate out condensed free water and enters a third section inlet of the three-section centrifugal compressor 5, and the thirdly supercharged tail gas is cooled by the tertiary air cooler 11 and enters the outlet separator 12 to separate out the condensed free water;
s3, dividing the middle and high pressure tail gas separated by the outlet separator 12 in the step S2 into two paths, and conveying one path of the tail gas to the iron-based wet fine desulfurization device 14 for deep H removal2S; the other path is conveyed to a high-pressure tail gas storage tank 35;
s4, transferring the fine desulfurization tail gas from the iron-based wet fine desulfurization device 14 in the step S3 into a molecular sieve dehydration device 15 for dehydration;
s5, dividing the tail gas dehydrated by the molecular sieve dehydration device 15 from the step S4 into two paths, wherein one path is conveyed to an activated carbon adsorption device 16 for adsorption and purification to remove heavy hydrocarbon substances and residual trace H contained in the tail gas2After S, the mixture is conveyed to a propane refrigeration device 17 for cooling and liquefaction; the other path is directly conveyed to a propane refrigerating device 17 for cooling and liquefaction without adsorption and purification;
s6, the liquid cooled and liquefied by the propane refrigeration device 17 from the step S5 is connected to a flash separator 20, and the flash liquid is industrial liquid carbon dioxide;
s7, outputting the industrial liquid carbon dioxide obtained in the step S6 in two paths, and conveying one path to the corresponding industrial liquid carbon dioxide spherical tank 23 for low-temperature storage; and the other path is conveyed to a food grade carbon dioxide refining device 22 for rectification and purification, a small amount of non-condensable gas contained in the industrial grade liquid carbon dioxide is removed to obtain food grade carbon dioxide, and the obtained food grade carbon dioxide is further conveyed to a food grade carbon dioxide spherical tank 24 for low-temperature storage.
The method can realize the recycling of the carbon dioxide in the tail gas of the ethane decarburization device; the environmental pollution caused by the local emission of carbon dioxide is reduced, the influence of the application of carbon dioxide emission indexes on the construction progress of engineering is reduced, the carbon dioxide emission is prevented from occupying the indexes of local carbon emission, and the recovered carbon dioxide can be changed into valuable substances to improve the economic benefit.
Second embodiment
The embodiment relates to a system for recovering ethane decarbonization tail gas in natural gas ethane recovery engineering, which at least comprises an inlet separator 3, a three-section centrifugal compressor 5, a first-stage air cooler 7, a second-stage air cooler 9, a third-stage air cooler 11, a second-stage separator 8, a third-stage separator 10, an outlet separator 12, an iron-based wet-process fine desulfurization device 14, a molecular sieve dehydration device 15, an activated carbon adsorption device 18, a propane refrigeration device 19, a flash separator 20 and a food-grade carbon dioxide refining device 22, wherein the three-stage air cooler 9 is connected with the outlet separator 22;
ethane decarbonization tail gas is connected with an inlet of an inlet separator 3 through a pipeline, a liquid phase outlet of the inlet separator 3 is connected with a condensed water collecting tank 39 through a pipeline, a gas phase outlet of the inlet separator 3 is connected with a first section inlet of a three-section centrifugal compressor 5 through a pipeline, the first section outlet of the three-section centrifugal compressor 5 is connected with a first-stage air cooler 7 and a second-stage separator 8 through pipelines in sequence, a gas phase outlet of the second-stage separator 8 is connected with a second section inlet of the three-section centrifugal compressor 5 through a pipeline, a second section outlet of the three-section centrifugal compressor 5 is connected with a second-stage air cooler 9 through a pipeline in sequence, the three-stage separator 10 is connected, a gas phase outlet of the three-stage separator 10 is connected with a third-stage inlet of the three-stage centrifugal compressor 5 through a pipeline, and a third-stage outlet of the three-stage centrifugal compressor 5 is connected with the three-stage air cooler 11 and the outlet separator 12 through pipelines in sequence;
the outlet separator 12 is provided with a first gas phase outlet and a second gas phase outlet, the first gas phase outlet of the outlet separator 12 conveys high-pressure tail gas to a high-pressure tail gas storage tank 35 through a pipeline, the second gas phase outlet of the outlet separator 12 is sequentially connected with the iron-based wet-method fine desulfurization device 14 and the molecular sieve dehydration device 15 through pipelines, the molecular sieve dehydration device 15 is provided with a first outlet and a second outlet, the first outlet of the molecular sieve dehydration device 15 is directly connected with an inlet of the propane refrigeration device 19 through a pipeline, the second outlet of the molecular sieve dehydration device 15 is connected with an inlet of the propane refrigeration device 19 through an activated carbon adsorption device 18 through a pipeline, the outlet of the propane refrigeration device 19 is connected with an inlet of the flash separator 20, the flash separator 20 is provided with a gas phase outlet and a liquid phase outlet, the gas phase outlet of the flash separator 20 is connected with an emptying device 33, and the liquid phase outlet of the flash separator, one path is connected with an industrial liquid carbon dioxide storage tank 23 through a pipeline, the other path is connected with an inlet of a food grade carbon dioxide refining device 22 through a pipeline, and an outlet of the food grade carbon dioxide refining device 22 is connected with a food grade liquid carbon dioxide storage tank 24 through a pipeline.
The invention aims at the decarbonization tail gas which is high in carbon dioxide content and rich in H2S, low pressure, high yield and less impurities, and adopts multistage centrifugal pressurization and interstage fine H removal2S, medium and high pressure separation, molecular sieve dehydration, active carbon adsorption, propane shallow cold liquefaction, rectification purification, pressurized liquid storage and diversified product process technical route. The pressure meets the requirement that the tail gas returns to the exported natural gas at any time, the product yield can be adjusted or the production can be stopped according to the needs of the product market, and carbon dioxide products with different qualities can be produced, for example, industrial-grade carbon dioxide products can be produced, and food-grade products can also be produced.
Third embodiment
In addition to the above embodiments, the liquid phase outlets of the second separator 8, the third separator 10 and the outlet separator 12 are respectively connected to the inlet of the inlet separator 3 through a pipeline.
And an industrial-grade liquid carbon dioxide conveying pipeline 31 is installed on the industrial-grade liquid carbon dioxide storage tank 23, and a ninth cut-off valve 26 and a first loading pump 27 are connected to the industrial-grade liquid carbon dioxide conveying pipeline 31.
And a food-grade liquid carbon dioxide conveying pipeline 32 is installed on the food-grade liquid carbon dioxide storage tank 24, and a tenth cut-off valve 29 and a second loading pump 30 are connected to the food-grade liquid carbon dioxide conveying pipeline 32.
The liquid phase outlet of the inlet separator 3 is connected with a condensed water collecting tank 39 through a water transfer pump 36; a liquid level regulating valve 37 and a liquid level meter 38 are arranged on a connecting pipeline between the water transfer pump 36 and the condensed water collecting tank 39, the liquid level meter 38 is arranged between the inlet separator 3 and the liquid level regulating valve 37, and the liquid level meter 38 and the liquid level regulating valve 37 form a control liquid level loop
A first cut-off valve 2 is arranged on a connecting pipeline between the ethane decarbonization tail gas and an inlet of the inlet separator 3; an inlet pressure detector 4 is connected on a connecting pipeline between a gas phase outlet of the inlet separator 3 and a first section inlet of the three-section centrifugal compressor 5;
a second cut-off valve 34 is arranged on a connecting pipeline between the first gas phase outlet of the outlet separator 12 and the high-pressure tail gas storage tank 35; a third shut-off valve 13 is arranged on a connecting pipeline between the second outlet of the outlet separator 12 and the inlet of the iron-based wet fine desulfurization device 14; a fourth block valve 16 is arranged on a connecting pipeline between the first outlet of the molecular sieve dehydration device 15 and the inlet of the propane refrigeration device 19; a fifth block valve 17 is arranged on a connecting pipeline between a second gas phase outlet of the molecular sieve dehydration device 15 and the activated carbon adsorption device 18; a sixth block valve 25 is arranged on a connecting pipeline between the liquid phase outlet of the flash separator 20 and the industrial-grade liquid carbon dioxide storage tank 23; a seventh block valve 21 is arranged on a connecting pipeline between the liquid phase outlet of the flash separator 20 and the inlet of the food-grade carbon dioxide refining device 22; an eighth block valve 28 is disposed on a connection pipeline between the outlet of the food grade carbon dioxide refining device 22 and the food grade liquid carbon dioxide storage tank 24. Specifically, the iron-based wet fine desulfurization device 14, the molecular sieve dehydration device 15, the fifth block valve 17, the activated carbon adsorption device 18 and the propane refrigeration device 19 are sequentially connected through a pipeline; the molecular sieve dehydration device 15, the fourth block valve 16 and the propane refrigeration device 19 are connected in sequence through pipelines; the propane refrigeration device 19, the flash separator 20, the seventh cut-off valve 21, the food-grade carbon dioxide refining device 22 and the eighth cut-off valve 28 are connected with the food-grade liquid carbon dioxide storage tank 24 end to end through pipelines; the flash separator 20, the sixth cut-off valve 25, the industrial-grade liquid carbon dioxide storage tank 23, the ninth cut-off valve 26, the first loading pump 27 and the industrial-grade liquid carbon dioxide conveying pipeline 31 are sequentially connected end to end through pipelines. The food-grade liquid carbon dioxide storage tank 24, the tenth cut-off valve 29, the second loading pump 30 and the food-grade liquid carbon dioxide conveying pipeline 32 are sequentially connected end to end through pipelines.
The three-stage centrifugal compressor 5 is connected with a variable frequency motor 6, and specifically, the ethane decarburization tail gas 1, the first cutoff valve 2, the inlet separator 3, the three-stage centrifugal compressor 5, the primary air cooler 7, the secondary separator 8, the three-stage centrifugal compressor 5, the secondary air cooler 9, the tertiary separator 10, the three-stage centrifugal compressor 5, the tertiary air cooler 11 and the outlet separator 12 are sequentially connected through pipelines; the variable frequency motor 6 and the inlet pressure detector 4 form a control loop, the rotating speed of the variable frequency motor can be adjusted according to the requirements on the air supply quantity and the air supply pressure, the phenomenon that air is large in air quantity and needs to be emptied is avoided, and therefore power consumption is reduced to the maximum extent.
The three-section centrifugal compressor 5 does not need to be provided with a gear speed increasing box or a lubricating auxiliary device required by the gear speed increasing box, effectively simplifies the structure of the centrifugal refrigerant compressor, and can reduce the overall dimension of the whole centrifugal compressor; the number of bearings and oil paths is correspondingly reduced, so that the number of fault points is reduced, and a control system is simplified; meanwhile, mechanical loss and noise caused by a gear speed increasing structure in the transmission process are avoided, and a sound insulation device for reducing noise can be omitted, so that the cost is reduced.
Fourth embodiment
The embodiment relates to a method for refrigerating by using a mixed refrigerant in natural gas ethane recovery engineering, which comprises the following steps:
s1, introducing the ethane decarburization tail gas 1 from the outside of the boundary area into an inlet separator 3, separating the free water carried by the ethane decarburization tail gas, introducing the separated gas phase into a three-section type centrifugal compressor 5, and pumping the liquid phase into a condensate collection tank 39;
s2, gas phase tail gas separated by the inlet separator 3 is connected to a first section inlet of the three-section centrifugal compressor 5, the supercharged tail gas is cooled by the primary air cooler 7, enters the secondary separator 8 to separate out condensed free water and enters a second section inlet of the compressor, the secondarily supercharged tail gas is cooled by the secondary air cooler 9, enters the tertiary separator 10 to separate out condensed free water and enters a third section inlet of the three-section centrifugal compressor 5, and the thirdly supercharged tail gas is cooled by the tertiary air cooler 11 and enters the outlet separator 12 to separate out the condensed free water; further, the condensed water separated by the second-stage separator 8, the third-stage separator 10 and the outlet separator 12 is delivered to the inlet separator 3 to form a circulation;
s3, dividing the middle and high pressure tail gas separated by the outlet separator 12 in the step S2 into two paths, and conveying one path of the tail gas to the iron-based wet fine desulfurization device 14 for deep H removal2S; the other standby flow is used for returning the high-pressure tail gas to the high-pressure tail gas storage tank 35;
s4, transferring the fine desulfurization tail gas from the iron-based wet fine desulfurization device 14 in the step S3 into a molecular sieve dehydration device 15 for dehydration;
s5, dividing the tail gas dehydrated by the molecular sieve dehydration device 15 from the step S4 into two paths, wherein one path is conveyed to an activated carbon adsorption device 16 for adsorption and purification to remove heavy hydrocarbon substances and residual trace H contained in the tail gas2After S, the mixture is conveyed to a propane refrigeration device 17 for cooling and liquefaction; the other path is directly conveyed to a propane refrigerating device 17 for cooling and liquefaction without adsorption and purification;
s6, the liquid cooled and liquefied by the propane refrigeration device 17 from the step S5 is connected to a flash separator 20, and the flash liquid is industrial liquid carbon dioxide;
s7, outputting the industrial liquid carbon dioxide obtained in the step S6 in two paths, and conveying one path to the corresponding industrial liquid carbon dioxide spherical tank 23 for low-temperature storage; and the other path is conveyed to a food grade carbon dioxide refining device 22 for rectification and purification, a small amount of non-condensable gas contained in the industrial grade liquid carbon dioxide is removed to obtain food grade carbon dioxide, and the obtained food grade carbon dioxide is further conveyed to a food grade carbon dioxide spherical tank 24 for low-temperature storage.
S8, the flash gas from step S6 and step S7 is sent to the emptying device 33.
It should be noted that the ethane decarburization tail gas from the outside of the battery limits is mainly composed of carbon dioxide, water, and H2S, ethane, methane and the like, wherein the volume content of carbon dioxide is 89.84%, the volume content of water is 9.56%, the volume content of ethane is 0.49%, and H20.09 percent of S, 0.01 percent of methane and 0.01 percent of propane by volume.
The pressure of the high-pressure tail gas output to the high-pressure tail gas storage tank 35 is 4.4MPa.g, and the temperature is 50 ℃.
It is worth mentioning that the purity of the industrial-grade liquid carbon dioxide reaches 99 percent, and the quality of the industrial-grade liquid carbon dioxide meets the requirements of first-class products in the national standard GB 6052; the purity of the qualified food-grade liquid carbon dioxide reaches 99.9 percent, and the quality of the qualified food-grade liquid carbon dioxide meets the requirements of the national standard GB 10621.
The application case is as follows:
the natural gas of the gas reservoir of the ancient world produced in the Changqing oil field contains a certain amount of ethane light hydrocarbon components, the average content of the ethane light hydrocarbon components is 5.4 percent, and the yield of the natural gas reaches 300 × 108m3A, wherein 200 × 108m3The concentrated recovery can be carried out, 105.27 ten thousand tons of ethane, 35.63 ten thousand tons of liquefied petroleum gas and 9.3 ten thousand tons of stable light hydrocarbon can be recovered each year, and the economic recovery value is higher.
The raw material natural gas treatment capacity of the ancient natural gas treatment main plant in the Changqing oil field is 6000 × 104m3(200 hundred million/year), 4 sets of liquid hydrocarbon recovery processing devices with the same scale are arranged, and the processing scale of a single set of device reaches 1500 × 104m3/d。
The raw material ethane is an intermediate product of natural gas ethane recovery engineering, the ethane and propane are separated through a deethanizer, almost all carbon dioxide in the ethane is removed through an ethane decarbonization tower, and the remaining wet ethane gas is dehydrated through a molecular sieve to meet the quality index requirements of commercial ethane and the quality requirements of ethane cracking or ethane liquefaction.
In conclusion, the recovery method and the recovery system provided by the invention can realize deep dehydration of the engineering raw material ethane and meet the requirement that the water dew point of an ethane gaseous product reaches the quality index of 0.1 ppm; the method and the system can automatically complete the adsorption, heating and cold blowing sequence control and circulation of molecular sieve dehydration, and can adjust the set period or adjust the sequence control step at any time according to the adsorption effect, thereby achieving the purpose of deep dehydration of ethane without human intervention.
Parts of the above embodiments that are not specifically described are well known components and conventional structures or conventional means in the art and will not be described in detail herein.
The foregoing is illustrative of the preferred embodiments of the present invention, and the present invention is not to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein. Any simple modification, equivalent change and modification of the above embodiments according to the technical spirit of the present invention still fall within the scope of the technical solution of the present invention.
Claims (10)
1. The method for recovering the ethane decarburization tail gas in the natural gas ethane recovery project is characterized by comprising the following steps of:
s1, introducing ethane decarburization tail gas (1) from the outside of the boundary area into an inlet separator (3), separating free water carried by the ethane decarburization tail gas, introducing the separated gas phase into a three-section type centrifugal compressor (5), and pumping a liquid phase into a condensate collection tank (39);
s2, gas phase tail gas separated by an inlet separator (3) is connected into a first section inlet of a three-section centrifugal compressor (5), pressurized tail gas is cooled by a first-stage air cooler (7), enters a second-stage separator (8) to separate out condensed free water and enters a second section inlet of the compressor, the secondarily pressurized tail gas is cooled by a second-stage air cooler (9), enters a third-stage separator (10) to separate out the condensed free water and enters a third section inlet of the three-section centrifugal compressor (5), and the thirdly pressurized tail gas is cooled by a third-stage air cooler (11) and enters an outlet separator (12) to separate out the condensed free water;
s3, dividing the middle and high pressure tail gas separated by the outlet separator (12) in the step S2 into two paths, and conveying one path of the tail gas to an iron-based wet fine desulfurization device (14) for deep H removal2S; the other path is conveyed to a high-pressure tail gas storage tank (35);
s4, transferring the fine desulfurization tail gas from the iron-based wet fine desulfurization device (14) in the step S3 into a molecular sieve dehydration device (15) for dehydration;
s5, dividing the tail gas dehydrated by the molecular sieve dehydration device (15) from the step S4 into two paths, wherein one path is conveyed to an activated carbon adsorption device (16) for adsorption and purification to remove heavy hydrocarbon substances and residual trace H contained in the tail gas2After S, the mixture is conveyed to a propane refrigeration device (17) for cooling and liquefaction; the other path is directly conveyed to a propane refrigerating device (17) for cooling and liquefaction without adsorption and purification;
s6, the liquid cooled and liquefied by the propane refrigeration device (17) from the step S5 is connected to a flash separator (20), and the flash liquid is industrial liquid carbon dioxide;
s7, outputting the industrial liquid carbon dioxide obtained in the step S6 in two paths, and conveying one path to a corresponding industrial liquid carbon dioxide spherical tank (23) for low-temperature storage; and the other path is conveyed to a food grade carbon dioxide refining device (22) for rectification and purification, food grade carbon dioxide is obtained after a small amount of non-condensable gas contained in the industrial grade liquid carbon dioxide is removed, and the obtained food grade carbon dioxide is further conveyed to a food grade carbon dioxide spherical tank (24) for low-temperature storage.
2. The method for recovering the ethane decarbonized tail gas in the natural gas ethane recovery project according to claim 1, which is characterized in that: the method also comprises S8, and the flash gas from the step S6 and the step S7 is conveyed to a venting device (33).
3. The method for recovering the ethane decarbonized tail gas in the natural gas ethane recovery project according to claim 1, which is characterized in that: the condensed water separated by the second-stage separator (8), the third-stage separator (10) and the outlet separator (12) in the step S2 is conveyed to the inlet separator (3) to form a circulation.
4. The utility model provides a system for natural gas ethane recovery engineering ethane decarbonization tail gas is retrieved which characterized in that: the system at least comprises an inlet separator (3), a three-section centrifugal compressor (5), a first-stage air cooler (7), a second-stage air cooler (9), a third-stage air cooler (11), a second-stage separator (8), a third-stage separator (10), an outlet separator (12), an iron-based wet-method fine desulfurization device (14), a molecular sieve dehydration device (15), an active carbon adsorption device (18), a propane refrigeration device (19), a flash separator (20) and a food-grade carbon dioxide refining device (22);
the ethane decarburization tail gas (1) is connected with an inlet of an inlet separator (3) through a pipeline, a liquid phase outlet of the inlet separator (3) is connected with a condensed water collecting tank (39) through a pipeline, a gas phase outlet of the inlet separator (3) is connected with a first section inlet of a three-section centrifugal compressor (5) through a pipeline, the first section outlet of the three-section centrifugal compressor (5) is sequentially connected with a first-stage air cooler (7) through a pipeline, a second-stage separator (8) is connected with a gas phase outlet of the second-stage separator (8) through a pipeline, the second section outlet of the three-section centrifugal compressor (5) is sequentially connected with a second-stage air cooler (9) through a pipeline, a third-stage separator (10) is connected with a third section inlet of the three-stage centrifugal compressor (5) through a pipeline, the third section outlet of the three-stage centrifugal compressor (5) is sequentially connected with a third-stage air cooler (11) through a pipeline, An outlet separator (12);
the outlet separator (12) is provided with a first gas phase outlet and a second gas phase outlet, the first gas phase outlet of the outlet separator (12) conveys high-pressure tail gas to a high-pressure tail gas storage tank (35) through a pipeline, the second gas phase outlet of the outlet separator (12) is sequentially connected with the iron-based wet-method fine desulfurization device (14) and the molecular sieve dehydration device (15) through pipelines, the molecular sieve dehydration device (15) is provided with a first outlet and a second outlet, the first outlet of the molecular sieve dehydration device (15) is directly connected with an inlet of the propane refrigeration device (19) through a pipeline, the second outlet of the molecular sieve dehydration device (15) is connected with an inlet of the propane refrigeration device (19) through an activated carbon adsorption device (18) through a pipeline, the outlet of the propane refrigeration device (19) is connected with an inlet of the flash separator (20), the flash separator (20) is provided with a gas phase outlet and a liquid phase outlet, the gas phase outlet of the flash separator (20) is connected with the emptying device (33), the liquid phase outlet of the flash separator (20) is divided into two paths, one path is connected with the industrial liquid carbon dioxide storage tank (23) through a pipeline, the other path is connected with the inlet of the food grade carbon dioxide refining device (22) through a pipeline, and the outlet of the food grade carbon dioxide refining device (22) is connected with the food grade liquid carbon dioxide storage tank (24) through a pipeline.
5. The system for recovering the ethane decarbonized tail gas of the natural gas ethane recovery project according to claim 4, is characterized in that: and liquid phase outlets of the second-stage separator (8), the third-stage separator (10) and the outlet separator (12) are respectively connected with an inlet of the inlet separator (3) through pipelines.
6. The system for recovering the ethane decarbonized tail gas of the natural gas ethane recovery project according to claim 4, is characterized in that: and an industrial liquid carbon dioxide conveying pipeline (31) is installed on the industrial liquid carbon dioxide storage tank (23), and a ninth cut-off valve (26) and a first loading pump (27) are connected to the industrial liquid carbon dioxide conveying pipeline (31).
7. The system for recovering the ethane decarbonized tail gas of the natural gas ethane recovery project according to claim 4, is characterized in that: food-grade liquid carbon dioxide conveying pipeline (32) is installed on food-grade liquid carbon dioxide storage tank (24), and tenth block valve (29) and second loading pump (30) are connected to food-grade liquid carbon dioxide conveying pipeline (32).
8. The system for recovering the ethane decarbonized tail gas of the natural gas ethane recovery project according to claim 4, is characterized in that: the liquid phase outlet of the inlet separator (3) is connected with a condensed water collecting tank (39) through a water transfer pump (36); a liquid level regulating valve (37) and a liquid level meter (38) are arranged on a connecting pipeline between the water transfer pump (36) and the condensed water collecting tank (39), and the liquid level meter (38) is arranged between the inlet separator (3) and the liquid level regulating valve (37).
9. The system for recovering the ethane decarbonized tail gas of the natural gas ethane recovery project according to claim 4, is characterized in that: a first cut-off valve (2) is arranged on a connecting pipeline between the ethane decarburization tail gas (1) and an inlet of the inlet separator (3);
an inlet pressure detector (4) is connected to a connecting pipeline between a gas phase outlet of the inlet separator (3) and a first section inlet of the three-section centrifugal compressor (5);
a second cut-off valve (34) is arranged on a connecting pipeline between a first gas phase outlet of the outlet separator (12) and the high-pressure tail gas storage tank (35); a third shut-off valve (13) is arranged on a connecting pipeline between a second outlet of the outlet separator (12) and an inlet of the iron-based wet fine desulfurization device (14);
a fourth block valve (16) is arranged on a connecting pipeline between the first outlet of the molecular sieve dehydration device (15) and the inlet of the propane refrigeration device (19); a fifth block valve (17) is arranged on a connecting pipeline between a second gas phase outlet of the molecular sieve dehydration device (15) and the activated carbon adsorption device (18);
a sixth cut-off valve (25) is arranged on a connecting pipeline between a liquid phase outlet of the flash separator (20) and the industrial-grade liquid carbon dioxide storage tank (23); a seventh cut-off valve (21) is arranged on a connecting pipeline between the liquid phase outlet of the flash separator (20) and the inlet of the food-grade carbon dioxide refining device (22); and an eighth cut-off valve (28) is arranged on a connecting pipeline between the outlet of the food-grade carbon dioxide refining device (22) and the food-grade liquid carbon dioxide storage tank (24).
10. The system for recovering the ethane decarbonized tail gas of the natural gas ethane recovery project according to claim 8, characterized in that: the three-section centrifugal compressor (5) is connected with a variable frequency motor (6), and the variable frequency motor (6) and the inlet pressure detector (4) form a control loop.
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| JPS54115691A (en) * | 1978-02-07 | 1979-09-08 | Osaka Gas Co Ltd | Liquefied carbon dioxide producing equipment |
| US6301927B1 (en) * | 1998-01-08 | 2001-10-16 | Satish Reddy | Autorefrigeration separation of carbon dioxide |
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