CN111981767A - Natural gas single-tower cryogenic helium extraction device and method - Google Patents
Natural gas single-tower cryogenic helium extraction device and method Download PDFInfo
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- CN111981767A CN111981767A CN202010841863.7A CN202010841863A CN111981767A CN 111981767 A CN111981767 A CN 111981767A CN 202010841863 A CN202010841863 A CN 202010841863A CN 111981767 A CN111981767 A CN 111981767A
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- 239000001307 helium Substances 0.000 title claims abstract description 169
- 229910052734 helium Inorganic materials 0.000 title claims abstract description 169
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 title claims abstract description 169
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 148
- 238000000605 extraction Methods 0.000 title claims abstract description 104
- 239000003345 natural gas Substances 0.000 title claims abstract description 74
- 238000000034 method Methods 0.000 title claims abstract description 49
- 239000007789 gas Substances 0.000 claims abstract description 54
- 238000010992 reflux Methods 0.000 claims abstract description 31
- 239000003507 refrigerant Substances 0.000 claims abstract description 31
- 238000005057 refrigeration Methods 0.000 claims abstract description 30
- 239000007788 liquid Substances 0.000 claims abstract description 21
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 10
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 5
- 229930195733 hydrocarbon Natural products 0.000 claims description 66
- 150000002430 hydrocarbons Chemical class 0.000 claims description 66
- 239000004215 Carbon black (E152) Substances 0.000 claims description 64
- 239000012071 phase Substances 0.000 claims description 40
- 239000007791 liquid phase Substances 0.000 claims description 31
- 238000001816 cooling Methods 0.000 claims description 21
- 238000003303 reheating Methods 0.000 claims description 18
- 238000000926 separation method Methods 0.000 claims description 7
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 239000000126 substance Substances 0.000 description 2
- 238000003795 desorption Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000009965 odorless effect Effects 0.000 description 1
- 239000013307 optical fiber Substances 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 238000011084 recovery 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
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
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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
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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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
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
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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
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/028—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of noble gases
- F25J3/029—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of noble gases of helium
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/12—External refrigeration with liquid vaporising loop
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle
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- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention discloses a natural gas single-tower cryogenic helium extraction device and a method, wherein the device comprises a cold box, a helium extraction tower and a cryogen refrigeration cycle unit, the cold box is connected with a natural gas inlet pipeline, precooled natural gas is divided into two paths, one path of the natural gas is connected with a helium extraction tower reboiler, the other path of the natural gas is condensed by the cold box and then is connected with the helium extraction tower through a pipeline, a gas phase outlet at the top of the helium extraction tower is connected with a helium extraction tower condenser through a pipeline, and the cryogen refrigeration cycle unit is connected with the cold box. According to the invention, the helium in the natural gas is rectified and concentrated at low temperature by adopting the helium extraction tower, and a part of low-temperature natural gas enters the upper part of the helium extraction tower after being further condensed, so that the severe change of the gas-liquid load of the helium extraction tower caused by low content of the helium in the natural gas is avoided, and the stable operation of the helium extraction tower is ensured; meanwhile, the nitrogen refrigerant refrigeration cycle is arranged to provide cold energy for the tower top condenser, so that the reflux temperature of the helium extraction tower is greatly reduced, and the helium content in the top gas of the helium extraction tower is increased.
Description
Technical Field
The invention belongs to the technical field of helium recovery from natural gas, and particularly relates to a single-tower cryogenic helium extraction device and method for natural gas, which are suitable for one or more kinds of hydrocarbon mixtures such as natural gas containing helium.
Background
Helium is a colorless and odorless inert gas, is inert in chemical properties, is difficult to react with other substances under a general state, and has a liquefaction temperature of-268.9 ℃ under normal pressure. Helium has important applications in medical, ultra-low temperature, optical fiber, and other fields due to its unique properties. Helium-containing natural gas is currently the only source of helium for commercial production. By utilizing the property that the liquefaction temperature of helium is far lower than that of natural gas, a rectifying tower is arranged, and the helium is extracted from the natural gas by adopting a rectifying mode at low temperature; the natural gas is separated from the bottom of the rectifying tower in a liquid phase.
Due to the low helium content of natural gas, commercially helium feed natural gas has a minimum helium content of 0.05% and a maximum of 8%. In the chinese patent CN201210513423.4, two rectifying towers are adopted, in the first rectifying tower, most of the natural gas components are separated, and then helium gas is further concentrated by the second rectifying tower, so that stable operation is ensured, the process flow is complex, and the investment is large. However, the helium is separated and extracted by adopting one rectifying tower, and the load change of the upper part and the lower part of the rectifying tower is large due to the low content of the helium in the natural gas, so that the operation is unstable, and the helium yield and concentration are influenced.
Disclosure of Invention
The invention aims to: aiming at the existing problems, the device and the method for extracting helium by using natural gas single-tower deep cooling can ensure the stable operation of the helium extracting tower and effectively improve the helium content in the top gas of the helium extracting tower.
The technical scheme adopted by the invention is as follows: a helium device is carried out to natural gas single tower cryrogenic, its characterized in that: comprises a cold box, a helium extracting tower and a refrigerant refrigeration cycle unit;
the inlet end of a precooling section in the cold box is connected with a natural gas inlet pipeline, the outlet end of the natural gas after precooling is divided into two paths, wherein one path is connected with a helium extracting tower reboiler at the bottom of the helium extracting tower through a pipeline, the helium extracting tower reboiler is connected with the inlet end of a cooling section in the cold box through a pipeline, the outlet end of the cooling section in the cold box is connected with the helium extracting tower through a pipeline provided with a first throttle valve, the other path is connected with the inlet end of a condensing section in the cold box through a pipeline, and the outlet end of the condensing section in the cold box is connected with the helium extracting tower through a pipeline provided with a second throttle valve;
the gas phase outlet at the top of the helium extracting tower is connected with a helium extracting tower condenser through a pipeline, and the condensed gas phase and the condensed liquid phase respectively pass through pipelines to the subsequent working procedure;
and the refrigerant refrigeration cycle unit is connected with the cold box and is used for providing cold energy for the cold box and the helium extraction tower condenser.
The natural gas single-tower cryogenic helium extraction device comprises a cooler and a cryogen refrigeration compressor, wherein the cooler is connected with a corresponding cooling section in a cold box, the corresponding cooling section in the cold box is connected with a helium extraction tower condenser through a pipeline provided with a fourth throttling valve, the helium extraction tower condenser is connected with the inlet end of a cryogen reheating section in the cold box through a pipeline, the outlet end of the cryogen reheating section in the cold box is connected with the cryogen refrigeration compressor through a pipeline, and the cryogen refrigeration compressor is connected with the cooler to form a cryogen refrigeration circulation loop.
According to the natural gas single-tower cryogenic helium extraction device, a gas phase at the top of a helium extraction tower is condensed by a helium extraction tower condenser and then divided into two paths, one path of liquid phase is connected with the top of the helium extraction tower through a pipeline and used for liquid phase reflux in the tower, the other path of gas phase is connected with the inlet end of a gas phase reheating section in a cold box through a pipeline, and the outlet end of the gas phase reheating section in the cold box is connected to a post-process through a pipeline.
According to the natural gas single-tower cryogenic helium extraction device, a liquid phase outlet at the bottom of the helium extraction tower is connected with an inlet end of a liquid phase reheating section in a cold box through a pipeline provided with a third throttle valve, and an outlet end of the liquid phase reheating section in the cold box is connected to a post-process through a pipeline.
The outlet end of a precooling section in the cold box is connected with a heavy hydrocarbon removal tower through a pipeline, a gas phase outlet at the top of the heavy hydrocarbon removal tower is connected with an inlet end of a secondary precooling section in the cold box through a pipeline, an outlet end of the secondary precooling section in the cold box is connected with a heavy hydrocarbon removal tower reflux tank through a pipeline, gas phase of the heavy hydrocarbon removal tower reflux tank is divided into two paths, one path is connected with a helium extraction tower reboiler at the bottom of the helium extraction tower through a pipeline, and the other path is connected with a condensing section in the cold box through a pipeline.
According to the natural gas single-tower cryogenic helium extraction device, the bottom liquid phase outlet of the heavy hydrocarbon removal tower reflux tank is connected with the upper part of the heavy hydrocarbon removal tower through a pipeline provided with a heavy hydrocarbon removal tower reflux pump, and liquid hydrocarbons at the bottom of the heavy hydrocarbon removal tower flow to a post-process through a pipeline.
A method for extracting helium by using natural gas through single-tower cryogenic cooling is characterized by comprising the following steps: the method comprises the following steps:
the method comprises the following steps that firstly, natural gas from a natural gas inlet pipeline enters a cold box for precooling and then is divided into two paths, wherein: 50-95% of one path enters a reboiler of a helium extraction tower through a pipeline, then is sent into a cold box through the pipeline, is cooled to minus 90-minus 110 ℃, and then is throttled to 600 kPa.a-3000 kPa.a through a first throttle valve to enter the middle part of the helium extraction tower; the other strand of 5-50% enters a cold box for further condensation to-100 to-150 ℃, is throttled by a second throttle valve and enters the upper part of a helium extraction tower;
secondly, helium gas which is rectified and concentrated by the helium extracting tower enters a helium extracting tower condenser from the top of the helium extracting tower and is condensed to minus 180 ℃ to minus 182 ℃, and the condensed gas phase and the condensed liquid phase are respectively transmitted to the post-process through pipelines;
and thirdly, the nitrogen refrigerant from the cooler enters a cold box to be cooled to-170 to-182 ℃, is throttled to 200kPa.a to 500kPa.a by a fourth throttle valve, enters a helium extraction tower condenser to be reheated to-175 to-185 ℃, enters the cold box through a pipeline to be further reheated to 20 to 30 ℃, enters a refrigerant refrigeration compressor to be pressurized to 800kPa.a to 4000kPa.a, enters the cooler to be cooled to 30 to 40 ℃ and then enters the cold box, and a refrigerant refrigeration cycle is formed to provide the required cold energy for the helium extraction tower condenser and the cold box.
The invention relates to a method for extracting helium by cryogenic natural gas with single tower, which comprises the following steps that in the first step, natural gas from a natural gas inlet pipeline enters a cold box to be precooled to-25 to-45 ℃, then enters the lower part of a heavy hydrocarbon removal tower to be separated, liquid hydrocarbon at the bottom of the heavy hydrocarbon removal tower enters post-process treatment, gas phase at the top of the heavy hydrocarbon removal tower enters the cold box to be further precooled to-50 to-65 ℃, then enters a reflux tank of the heavy hydrocarbon removal tower to be subjected to gas-liquid separation, and the separated gas phase is divided into two paths, wherein the gas phase is in the same direction as the two paths precooled by the cold.
In the first step, a liquid phase obtained after gas-liquid separation in a heavy hydrocarbon removal tower reflux tank is pressurized by a heavy hydrocarbon removal tower reflux pump and then enters the top of a heavy hydrocarbon removal tower, and liquid hydrocarbon at the bottom of the heavy hydrocarbon removal tower passes through a pipeline to a post-process.
In the second step, after helium gas at the top of the helium extraction tower is condensed by a helium extraction tower condenser, a liquid phase of the helium gas enters the top of the helium extraction tower to be used as reflux, a gas phase enters a cooling box to be reheated to 20-30 ℃ and then is subjected to post-process treatment, natural gas serving as liquid hydrocarbon is throttled to 300-1000 kPa.a from the bottom of the helium extraction tower through a fourth throttling valve and then is sent to the cooling box to be reheated to 20-30 ℃ and then is sent to the post-process treatment.
Compared with the prior art, the invention has the following positive effects: the helium in the natural gas is rectified and concentrated at low temperature by adopting a helium extracting tower, and a part of low-temperature natural gas enters the upper part of the helium extracting tower after being further condensed, so that the severe change of the gas-liquid load of the helium extracting tower caused by low content of the helium in the natural gas is avoided, and the stable operation of the helium extracting tower is ensured; meanwhile, the nitrogen refrigerant refrigeration cycle is arranged to provide cold energy for the tower top condenser, so that the reflux temperature of the helium extraction tower is greatly reduced, and the helium content in the top gas of the helium extraction tower is increased.
Drawings
The invention will be described by way of specific embodiments and with reference to the accompanying drawings, in which
Fig. 1 is a schematic view of the principle of embodiment 1 of the present invention.
Fig. 2 is a schematic diagram of embodiment 2 of the present invention.
The labels in the figure are: 1 is the natural gas admission line, 2 is the cold box, 4 is for taking off the heavy hydrocarbon tower, 7 is for taking off the heavy hydrocarbon tower reflux drum, 9 is for taking off the heavy hydrocarbon tower reflux pump, 13 is for carrying the helium tower, 14 is for carrying the helium tower reboiler, 17 is first choke valve, 21 is the second choke valve, 24 is for carrying the helium tower condenser, 29 is the third choke valve, 32 is cryogen compressor, 34 is the cooler, 37 is the fourth choke valve.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, 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 some, but not all, embodiments of the present invention. The components of embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations.
Thus, the following detailed description of the embodiments of the present invention, presented in the figures, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. 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.
It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict.
It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, it need not be further defined and explained in subsequent figures.
In the description of the embodiments of the present invention, it should be noted that the indication of the orientation or the positional relationship is based on the orientation or the positional relationship shown in the drawings, or the orientation or the positional relationship which is usually placed when the product of the present invention is used, or the orientation or the positional relationship which is usually understood by those skilled in the art, or the orientation or the positional relationship which is usually placed when the product of the present invention is used, and is only for the convenience of describing the present invention and simplifying the description, but does not indicate or imply that the indicated device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and therefore, cannot be understood as limiting the present invention. Furthermore, the terms "first" and "second" are used merely to distinguish one description from another, and are not to be construed as indicating or implying relative importance.
In the description of the embodiments of the present invention, it should be further noted that the terms "disposed" and "connected" are to be interpreted broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected, unless explicitly stated or limited otherwise; may be directly connected or indirectly connected through an intermediate. The specific meanings of the above terms in the present invention can be understood in specific cases by those skilled in the art; the drawings in the embodiments are used for clearly and completely describing the technical scheme in the embodiments of the invention, and obviously, the described embodiments are a part of the embodiments of the invention, but not all of the embodiments. The components of embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations.
Example 1:
as shown in figure 1, the natural gas single-tower cryogenic helium extraction device comprises a cold box 2, a helium extraction tower 13 and a refrigerant refrigeration cycle unit.
The inlet end of a pre-cooling section in the cold box 2 is connected with a natural gas inlet pipeline 1, the outlet end of the natural gas after pre-cooling is divided into two paths, one path is connected with a helium extraction tower reboiler 14 at the bottom of a helium extraction tower 13 through a pipeline, the helium extraction tower reboiler 14 is connected with the inlet end of a cooling section in the cold box 2 through a pipeline, the outlet end of the cooling section in the cold box 2 is connected with the helium extraction tower 13 through a pipeline provided with a first throttle valve 17, the other path is connected with the inlet end of a condensing section in the cold box 2 through a pipeline, and the outlet end of the condensing section in the cold box 2 is connected with the helium extraction tower 13 through a pipeline provided with a second throttle valve 21.
The top gas phase outlet of the helium extraction tower 13 is connected with a helium extraction tower condenser 24 through a pipeline, and the condensed gas phase and the condensed liquid phase respectively pass through pipelines to the subsequent working procedure; specifically, the gas phase at the top of the helium extraction tower 13 is condensed by a helium extraction tower condenser 24 and then divided into two paths, one path of liquid phase is connected with the top of the helium extraction tower 13 through a pipeline and is used for liquid phase reflux in the tower, the other path of gas phase is connected with the inlet end of a gas phase reheating section in the cold box 2 through a pipeline, and the outlet end of the gas phase reheating section in the cold box 2 is connected to the post-process through a pipeline; and a liquid phase outlet at the bottom of the helium extraction tower 13 is connected with an inlet end of a liquid phase reheating section in the cold box 2 through a pipeline provided with a third throttle valve 29, and an outlet end of the liquid phase reheating section in the cold box 2 is connected to a post-process through a pipeline.
The refrigerant refrigeration cycle unit is connected with the cold box 2 and is used for providing cold energy for the cold box 2 and the helium extraction tower condenser 24; in this embodiment, the refrigerant refrigeration cycle unit includes a cooler 34 and a refrigerant refrigeration compressor 32, the cooler 34 is connected to a corresponding cooling section in the cold box 2, the corresponding cooling section in the cold box 2 is connected to the helium extraction tower condenser 24 through a pipeline provided with a fourth throttle valve 37, the helium extraction tower condenser 24 is connected to an inlet end of a refrigerant reheating section in the cold box 2, an outlet end of the refrigerant reheating section in the cold box 2 is connected to the refrigerant refrigeration compressor 32 through a pipeline, and the refrigerant refrigeration compressor 32 is connected to the cooler 34 to form a refrigerant refrigeration cycle loop.
Based on the natural gas single-tower cryogenic helium extraction device, the invention also provides a natural gas single-tower cryogenic helium extraction method, which specifically comprises the following steps:
the method comprises the following steps that firstly, 4000 kPa.a-6000 kPa.a of natural gas from a natural gas inlet pipeline and natural gas at the temperature of 30-40 ℃ enter a cold box for precooling and then are divided into two paths, wherein: 50-95% of one path enters a reboiler of a helium extraction tower through a pipeline, then is sent into a cold box through the pipeline, is cooled to minus 90-minus 110 ℃, and then is throttled to 600 kPa.a-3000 kPa.a through a first throttle valve to enter the middle part of the helium extraction tower; and the other strand of the natural gas enters a cold box for further condensation to-100 to-150 ℃, is throttled by a second throttle valve and enters the upper part of the helium extraction tower, the natural gas is divided into two strands of natural gas which are condensed to different temperatures and respectively enter the helium extraction tower, the overlarge gas-liquid load change at the top and the bottom of the helium extraction tower is avoided, and the stable operation of the helium extraction tower is realized.
And secondly, the helium gas rectified and concentrated by the helium extracting tower enters a helium extracting tower condenser from the top of the helium extracting tower and is condensed to minus 180 ℃ to minus 182 ℃, and the condensed gas phase and the condensed liquid phase are respectively transmitted to the subsequent working procedures through pipelines.
Specifically, after helium gas at the top of the helium extraction tower is condensed by a helium extraction tower condenser, a liquid phase of the helium gas enters the top of the helium extraction tower to be used as reflux, a gas phase enters a cold box to be reheated to 20-30 ℃ and then is subjected to post-process treatment, natural gas serving as liquid hydrocarbon is throttled from the bottom of the helium extraction tower to 300-1000 kPa.a through a fourth throttling valve and then is sent to the cold box to be reheated to 20-30 ℃ and then is sent to the post-process treatment.
And thirdly, the nitrogen refrigerant from the cooler enters a cold box to be cooled to-170 to-182 ℃, is throttled to 200kPa.a to 500kPa.a by a fourth throttle valve, enters a helium extraction tower condenser to be reheated to-175 to-185 ℃, enters the cold box through a pipeline to be further reheated to 20 to 30 ℃, enters a refrigerant refrigeration compressor to be pressurized to 800kPa.a to 4000kPa.a, enters the cooler to be cooled to 30 to 40 ℃ and then enters the cold box, and a refrigerant refrigeration cycle is formed to provide the required cold energy for the helium extraction tower condenser and the cold box.
Example 2:
as shown in fig. 2, embodiment 2 is substantially the same as embodiment 1, and its main difference is: the outlet end of a precooling section in the cold box 2 is connected with a heavy hydrocarbon removal tower 4 through a pipeline, the gas phase outlet at the top of the heavy hydrocarbon removal tower 4 is connected with the inlet end of a secondary precooling section in the cold box 2 through a pipeline, the outlet end of the secondary precooling section in the cold box 2 is connected with a heavy hydrocarbon removal tower reflux tank 7 through a pipeline, the gas phase of the heavy hydrocarbon removal tower reflux tank 7 is divided into two paths, one path is connected with a helium extraction tower reboiler 14 at the bottom of a helium extraction tower 13 through a pipeline, and the other path is connected with a condensing section in the cold box 2 through a pipeline; take off the bottom liquid phase export of heavy hydrocarbon tower reflux tank 7 and take off 4 upper portions of heavy hydrocarbon tower and be connected through being provided with the pipeline that takes off heavy hydrocarbon tower reflux pump 9, take off 4 bottom liquid hydrocarbons in heavy hydrocarbon tower and pass through pipeline to back process.
Based on the difference of the structural design, the method for extracting helium by cryogenic cooling of the natural gas by using the single tower mainly has the following differences: the method comprises the following steps that natural gas from a natural gas inlet pipeline enters a cold box to be pre-cooled to-25 to-45 ℃ and then enters the lower part of a heavy hydrocarbon removal tower to be separated, liquid hydrocarbon at the bottom of the heavy hydrocarbon removal tower enters post-process treatment, gas phase at the top of the heavy hydrocarbon removal tower enters the cold box to be further pre-cooled to-50 to-65 ℃, then enters a heavy hydrocarbon removal tower reflux tank to be subjected to gas-liquid separation, and the separated gas phase is divided into two paths, wherein the trend of the separated gas phase is consistent with that of the two paths after the gas phase is pre-cooled; get into after taking off heavy hydrocarbon tower reflux pump pressure boost through taking off the liquid phase behind the heavy hydrocarbon tower reflux tank gas-liquid separation and take off the heavy hydrocarbon tower top, take off the liquid hydrocarbon of heavy hydrocarbon tower bottom and pass through pipeline to back process, take off the heavy hydrocarbon tower through the setting, with heavy hydrocarbon desorption in the natural gas, avoid the natural gas to freeze stifled equipment or pipeline in condensation process.
The invention is not limited to the foregoing embodiments. The invention extends to any novel feature or any novel combination of features disclosed in this specification and any novel method or process steps or any novel combination of features disclosed.
Claims (10)
1. A helium device is carried out to natural gas single tower cryrogenic, its characterized in that: comprises a cold box (2), a helium extracting tower (13) and a refrigerant refrigeration cycle unit;
the inlet end of a pre-cooling section in the cold box (2) is connected with a natural gas inlet pipeline (1), the natural gas of which the outlet end is pre-cooled is divided into two paths, wherein one path is connected with a helium extraction tower reboiler (14) at the bottom of a helium extraction tower (13) through a pipeline, the helium extraction tower reboiler (14) is connected with the inlet end of a cooling section in the cold box (2) through a pipeline, the outlet end of the cooling section in the cold box (2) is connected with the helium extraction tower (13) through a pipeline provided with a first throttle valve (17), the other path is connected with the inlet end of a condensing section in the cold box (2) through a pipeline, and the outlet end of the condensing section in the cold box (2) is connected with the helium extraction tower (13) through a pipeline provided with a second throttle valve (21);
a gas phase outlet at the top of the helium extraction tower (13) is connected with a helium extraction tower condenser (24) through a pipeline, and the condensed gas phase and the condensed liquid phase are respectively transmitted to the subsequent working procedures through pipelines;
and the refrigerant refrigeration cycle unit is connected with the cold box (2) and is used for providing cold for the cold box (2) and the helium extraction tower condenser (24).
2. The natural gas single-tower cryogenic helium extraction device according to claim 1, characterized in that: the refrigerant refrigeration cycle unit comprises a cooler (34) and a refrigerant refrigeration compressor (32), wherein the cooler (34) is connected with a corresponding cooling section in the cold box (2), the corresponding cooling section in the cold box (2) is connected with a helium extraction tower condenser (24) through a pipeline provided with a fourth throttle valve (37), the helium extraction tower condenser (24) is connected with the inlet end of a refrigerant reheating section in the cold box (2), the outlet end of the refrigerant reheating section in the cold box (2) is connected with the refrigerant refrigeration compressor (32) through a pipeline, and the refrigerant refrigeration compressor (32) is connected with the cooler (34) to form a refrigerant refrigeration cycle loop.
3. The natural gas single-tower cryogenic helium extraction device according to claim 1, characterized in that: and the gas phase at the top of the helium extraction tower (13) is condensed by a helium extraction tower condenser (24) and then divided into two paths, one path of liquid phase is connected with the top of the helium extraction tower (13) through a pipeline and is used for liquid phase reflux in the tower, the other path of gas phase is connected with the inlet end of a gas phase reheating section in the cold box (2) through a pipeline, and the outlet end of the gas phase reheating section in the cold box (2) is connected to the subsequent process through a pipeline.
4. The natural gas single-tower cryogenic helium extraction device according to claim 1, characterized in that: and a liquid phase outlet at the bottom of the helium extraction tower (13) is connected with an inlet end of a liquid phase reheating section in the cold box (2) through a pipeline provided with a third throttle valve (29), and an outlet end of the liquid phase reheating section in the cold box (2) is connected to a post-process through a pipeline.
5. The natural gas single-tower cryogenic helium extraction plant according to any one of claims 1 to 4, characterized in that: the precooling section outlet end in the cold box (2) is connected with a heavy hydrocarbon removal tower (4) through a pipeline, the top gas phase outlet of the heavy hydrocarbon removal tower (4) is connected with the secondary precooling section inlet end in the cold box (2) through a pipeline, the secondary precooling section outlet end in the cold box (2) is connected with a heavy hydrocarbon removal tower reflux tank (7) through a pipeline, the gas phase of the heavy hydrocarbon removal tower reflux tank (7) is divided into two paths, one path is connected with a helium extraction tower reboiler (14) at the bottom of a helium extraction tower (13) through a pipeline, and the other path is connected with the condensing section in the cold box (2) through a pipeline.
6. The natural gas single-tower cryogenic helium extraction device according to claim 5, wherein: the bottom liquid phase outlet of the heavy hydrocarbon tower reflux tank (7) is connected with the upper part of the heavy hydrocarbon tower (4) through a pipeline provided with a heavy hydrocarbon tower reflux pump (9), and the bottom liquid hydrocarbon of the heavy hydrocarbon tower (4) passes through a pipeline to a post-process.
7. A method for extracting helium by using natural gas through single-tower cryogenic cooling is characterized by comprising the following steps: the method comprises the following steps:
the method comprises the following steps that firstly, natural gas from a natural gas inlet pipeline enters a cold box for precooling and then is divided into two paths, wherein: 50-95% of one path enters a reboiler of a helium extraction tower through a pipeline, then is sent into a cold box through the pipeline, is cooled to minus 90-minus 110 ℃, and then is throttled to 600 kPa.a-3000 kPa.a through a first throttle valve to enter the middle part of the helium extraction tower; the other strand of 5-50% enters a cold box for further condensation to-100 to-150 ℃, is throttled by a second throttle valve and enters the upper part of a helium extraction tower;
secondly, helium gas which is rectified and concentrated by the helium extracting tower enters a helium extracting tower condenser from the top of the helium extracting tower and is condensed to minus 180 ℃ to minus 182 ℃, and the condensed gas phase and the condensed liquid phase are respectively transmitted to the post-process through pipelines;
and thirdly, the nitrogen refrigerant from the cooler enters a cold box to be cooled to-170 to-182 ℃, is throttled to 200kPa.a to 500kPa.a by a fourth throttle valve, enters a helium extraction tower condenser to be reheated to-175 to-185 ℃, enters the cold box through a pipeline to be further reheated to 20 to 30 ℃, enters a refrigerant refrigeration compressor to be pressurized to 800kPa.a to 4000kPa.a, enters the cooler to be cooled to 30 to 40 ℃ and then enters the cold box, and a refrigerant refrigeration cycle is formed to provide the required cold energy for the helium extraction tower condenser and the cold box.
8. The method for cryogenic helium extraction from natural gas by using a single tower as claimed in claim 7, wherein: in the first step, natural gas from a natural gas inlet pipeline enters a cold box for precooling to-25-45 ℃ and then enters the lower part of a heavy hydrocarbon removal tower for separation, liquid hydrocarbon at the bottom of the heavy hydrocarbon removal tower enters post-process treatment, gas phase at the top of the heavy hydrocarbon removal tower enters the cold box for further precooling to-50-65 ℃, and then enters a heavy hydrocarbon removal tower reflux tank for gas-liquid separation, the separated gas phase is divided into two paths, and the gas phase is specifically consistent with the two paths after precooling by the cold box in the first step.
9. The method for cryogenic helium extraction from natural gas by using a single tower as claimed in claim 8, wherein: in the first step, the liquid phase after taking off heavy hydrocarbon tower reflux drum gas-liquid separation gets into after taking off heavy hydrocarbon tower reflux pump pressure boost and takes off heavy hydrocarbon tower top, takes off the liquid hydrocarbon of heavy hydrocarbon tower bottom and passes through pipeline to back process.
10. The method for cryogenic helium extraction from natural gas by using a single tower as claimed in claim 7, wherein: in the second step, after helium gas at the top of the helium extraction tower is condensed by a helium extraction tower condenser, a liquid phase of the helium gas enters the top of the helium extraction tower to be used as reflux, a gas phase enters a cold box to be reheated to 20-30 ℃ and then is subjected to post-process treatment, natural gas is used as liquid hydrocarbon and is throttled from the bottom of the helium extraction tower to 300-1000 kPa.a through a fourth throttling valve, and then is sent to the cold box to be reheated to 20-30 ℃ and then is sent to the post-process treatment.
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