CN113108551A - Process and device for extracting high-purity helium in liquefied natural gas production process - Google Patents
Process and device for extracting high-purity helium in liquefied natural gas production process Download PDFInfo
- Publication number
- CN113108551A CN113108551A CN202110543949.6A CN202110543949A CN113108551A CN 113108551 A CN113108551 A CN 113108551A CN 202110543949 A CN202110543949 A CN 202110543949A CN 113108551 A CN113108551 A CN 113108551A
- Authority
- CN
- China
- Prior art keywords
- gas
- helium
- low
- temperature
- natural gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 title claims abstract description 145
- 239000001307 helium Substances 0.000 title claims abstract description 144
- 229910052734 helium Inorganic materials 0.000 title claims abstract description 144
- 239000003949 liquefied natural gas Substances 0.000 title claims abstract description 49
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 23
- 238000000034 method Methods 0.000 title claims abstract description 20
- 230000008569 process Effects 0.000 title claims abstract description 18
- 239000007789 gas Substances 0.000 claims abstract description 103
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 102
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 52
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 41
- 238000003860 storage Methods 0.000 claims abstract description 39
- 230000003197 catalytic effect Effects 0.000 claims abstract description 38
- 238000006356 dehydrogenation reaction Methods 0.000 claims abstract description 38
- 239000001257 hydrogen Substances 0.000 claims abstract description 38
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 38
- 239000003345 natural gas Substances 0.000 claims abstract description 31
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 26
- 239000002994 raw material Substances 0.000 claims abstract description 19
- 230000018044 dehydration Effects 0.000 claims abstract description 16
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 16
- 229910052754 neon Inorganic materials 0.000 claims abstract description 9
- GKAOGPIIYCISHV-UHFFFAOYSA-N neon atom Chemical compound [Ne] GKAOGPIIYCISHV-UHFFFAOYSA-N 0.000 claims abstract description 9
- 238000001179 sorption measurement Methods 0.000 claims abstract description 9
- 238000000605 extraction Methods 0.000 claims abstract description 7
- 230000009467 reduction Effects 0.000 claims abstract description 5
- 239000012071 phase Substances 0.000 claims description 27
- 239000000463 material Substances 0.000 claims description 26
- 238000001816 cooling Methods 0.000 claims description 23
- 238000000746 purification Methods 0.000 claims description 17
- 239000007791 liquid phase Substances 0.000 claims description 12
- 238000005261 decarburization Methods 0.000 claims description 11
- 239000007788 liquid Substances 0.000 claims description 10
- 239000011344 liquid material Substances 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 9
- 238000003303 reheating Methods 0.000 claims description 8
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 6
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 claims description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 5
- 239000012530 fluid Substances 0.000 claims description 5
- 239000001301 oxygen Substances 0.000 claims description 5
- 229910052760 oxygen Inorganic materials 0.000 claims description 5
- 239000002826 coolant Substances 0.000 claims description 4
- 230000001105 regulatory effect Effects 0.000 claims description 4
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 3
- 239000005977 Ethylene Substances 0.000 claims description 3
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 239000012535 impurity Substances 0.000 claims description 3
- 239000001294 propane Substances 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- JVFDADFMKQKAHW-UHFFFAOYSA-N C.[N] Chemical compound C.[N] JVFDADFMKQKAHW-UHFFFAOYSA-N 0.000 claims description 2
- 238000004880 explosion Methods 0.000 description 9
- 238000006243 chemical reaction Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 239000003507 refrigerant Substances 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000005262 decarbonization Methods 0.000 description 1
- 230000007123 defense Effects 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 230000009965 odorless effect Effects 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 239000004065 semiconductor Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
Images
Classifications
-
- 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
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention relates to a process for extracting high-purity helium in a liquefied natural gas production process, which comprises the following steps of: extracting BOG (boil off gas) before the raw material natural gas enters an LNG (liquefied natural gas) storage tank after being cooled and liquefied; carrying out secondary temperature reduction and liquefaction on the BOG to separate hydrogen-containing crude helium; carrying out catalytic dehydrogenation, dehydration, pressure swing adsorption and nitrogen and neon removal on the hydrogen-containing crude helium to obtain high-purity helium; doping part of high-purity helium gas into the crude helium gas containing hydrogen before the catalytic dehydrogenation reaction of the crude helium gas; the invention also relates to a device for extracting high-purity helium in the production process of liquefied natural gas, which comprises a first-stage low-temperature heat exchanger, a first throttle valve, a low-temperature separator, a first-stage compressor, a second-stage low-temperature separator, a third throttle valve, a denitrification tower, a catalytic dehydrogenation reactor, a dehydrator, a pressure swing adsorber and a helium storage tank which are sequentially arranged on a helium extraction path through pipelines; the process and the device have reasonable design and simple operation, the extraction efficiency of helium is high, and the concentration of finally extracted high-purity helium can reach 99.999%.
Description
Technical Field
The invention belongs to the technical field of gas separation, and particularly relates to a process and a device for extracting high-purity helium in a liquefied natural gas production process.
Background
Helium is an extremely light, colorless, odorless, non-toxic, and non-combustible, monatomic inert gas. Of all the gases known, helium has the lowest boiling point and liquefies at-268.934 ℃ (4.18K), approaching absolute zero-273.15 ℃, which is the one that humans find most difficult to liquefy. Helium is a rare strategic resource and is widely applied to various fields of national defense and military industry, aerospace, medical health, semiconductor industry, metal manufacturing and the like, and because the content of helium in air is extremely low (about 0.005 percent), the difficulty and energy consumption of separation from the air are very high, the helium extracted from natural gas is a main way for industrially producing the helium at home and abroad. Helium concentrations in natural gas from individual gas fields in the united states are as high as 8%, while those in china are only around 0.2%.
At present, the number of processes for producing helium designed in China is large, Chinese patent CN111692837A discloses a system for co-producing helium by using an LNG production device, the existing structure for recovering BOG gas and the system for co-producing helium adopted by the patent are disclosed in the patent, helium is extracted from boil-off gas (BOG) of a Liquefied Natural Gas (LNG) storage tank, but the defects that the LNG storage tank has large amount of evaporation gas when gas is taken from the LNG storage tank, the helium concentration is relatively low, the content of hydrogen in the BOG is high, explosion safety accidents are easy to occur in the rear-end catalytic dehydrogenation link and the like are overcome.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a process and a device for extracting high-purity helium in the production process of liquefied natural gas, so that the helium concentration and the hydrogen content reduction in BOG in the LNG production stage are realized, and the safety of the helium purification process is ensured.
The technical scheme of the invention is as follows:
the invention provides a process for extracting high-purity helium in a liquefied natural gas production process, which comprises the following steps of:
extracting BOG (boil off gas) before entering an LNG (liquefied natural gas) storage tank after the raw natural gas subjected to decarburization, dehydration, debenzolization and demercuration purification is cooled and liquefied;
reheating the BOG to normal temperature, pressurizing, performing secondary cooling liquefaction, and separating out a nitrogen and methane mixed liquid material and hydrogen-containing crude helium;
carrying out catalytic dehydrogenation and dehydration on the hydrogen-containing crude helium to obtain crude helium;
removing nitrogen and neon from the crude helium through pressure swing adsorption to obtain high-purity helium;
part of high-purity helium gas is doped into the hydrogen-containing crude helium gas before the catalytic dehydrogenation reaction of the crude helium gas.
Further, the raw material natural gas after decarburization, dehydration, debenzolization and demercuration purification is cooled and liquefied through a primary low-temperature heat exchanger, the temperature of the liquefied raw material natural gas is-157 ℃ to-162 ℃, and the pressure is 1840 kPa;
separating a gas-phase material BOG and a liquid-phase material LNG in the liquefied raw material natural gas through a low-temperature separator, recovering cold energy from the gas-phase material BOG discharged from the low-temperature separator, and reheating, wherein a liquid-phase outlet of the low-temperature separator is connected to an LNG storage tank;
before BOG pressurization and secondary cooling liquefaction, the cooling capacity is recovered by a primary low-temperature heat exchanger for reheating; pressurizing BOG to 4-5 Mpa, and cooling and liquefying with a two-stage low-temperature separator at-191-194 deg.C and 1.8 MPa.
Further, before the liquefied raw material natural gas enters the low-temperature separator, the pressure is adjusted to 150kPa through a first throttle valve.
Further, the high purity helium gas added before the crude helium gas catalytic dehydrogenation reaction reduces the hydrogen content in the catalytic dehydrogenation reaction to below 2%.
The invention also provides a device for extracting high-purity helium gas in the liquefied natural gas production process, which can apply the process, and comprises a first-stage low-temperature heat exchanger, a first throttle valve, a low-temperature separator, a first-stage compressor, a second-stage low-temperature separator, a third throttle valve, a denitrification tower, a catalytic dehydrogenation reactor, a dehydrator, a pressure swing adsorber and a helium gas storage tank which are sequentially arranged on a helium gas extraction path through pipelines;
the gas outlet of the pressure swing adsorber is also communicated with a pure gas pipe, the other end of the pure gas pipe is communicated with a pipeline between the denitrification tower and the catalytic dehydrogenation reactor, and a gas regulating valve and a gas flowmeter are arranged on the pure gas pipe;
the primary low-temperature heat exchanger is used for cooling and liquefying the raw material natural gas subjected to decarburization, dehydration, debenzolization and demercuration purification; the low-temperature separator is used for gas-liquid separation of the liquefied raw material natural gas, and a gas phase outlet of the low-temperature separator is connected to the primary compressor after cold energy and reheat are recovered by the primary low-temperature heat exchanger; the secondary low-temperature separator is used for cooling and liquefying gas-phase materials discharged from the low-temperature separator to obtain a mixed liquid material of nitrogen and methane and crude helium gas containing hydrogen; the denitrification tower is used for separating nitrogen and methane mixed liquid materials in the liquefied gas-phase materials, and a gas-phase outlet of the denitrification tower is connected to the catalytic dehydrogenation reactor; the catalytic dehydrogenation reactor is used for reacting hydrogen in the hydrogen-containing crude helium gas with the metered oxygen to generate water, and the dehydrator is used for dehydrating and discharging the crude helium gas; and adsorbing the impurity gas by the crude helium gas through a pressure swing adsorber to obtain high-purity helium gas, wherein the helium gas storage tank is used for storing the high-purity helium gas.
Further, the temperature of the fluid flowing out after being cooled by the primary low-temperature heat exchanger is-157 ℃ to-162 ℃, the outlet pressure of the primary compressor is 4Mpa to 5Mpa, the temperature of the mixed material flowing out after being cooled by the secondary low-temperature separator is-191 ℃ to-194 ℃, and the pressure of the mixed material is adjusted to 1.8MPa by a third throttle valve before entering the denitrification tower.
Further, the coolant in the secondary low-temperature separator consists of the following components in parts by weight: 20-25% of methane, 30-35% of ethylene, 0-1% of ethane, 4-10% of nitrogen, 10-20% of propane and 3-15% of isopentane.
Further, a liquid phase outlet of the cryogenic separator is connected to an LNG storage tank; the pressure swing adsorber is a double-tower pressure swing adsorption device, the helium storage tank is a high-pressure helium storage tank, a secondary compressor is connected between the pressure swing adsorber and the high-pressure helium storage tank, and high-purity helium obtained by adsorbing miscellaneous gases through the pressure swing adsorber is pressurized by the secondary compressor and then enters the helium storage tank.
Compared with the prior art, the invention has the beneficial effects that:
the process and the device have reasonable design and simple operation, the extraction efficiency of helium is high, and the concentration of finally extracted high-purity helium can reach 99.999 percent;
compared with the traditional method of taking gas from the LNG tank, the BOG is obtained before the raw material natural gas enters the LNG storage tank, so that the content of evaporated methane in the BOG is reduced, the helium concentration is improved, the helium concentration in the BOG is increased by more than two times compared with the original concentration, and the subsequent purification of helium is facilitated; before the catalytic dehydrogenation reaction is carried out, the high-purity helium is used for diluting the hydrogen to be below the explosion limit concentration, so that explosion in the catalytic dehydrogenation reaction is prevented, hydrogen damage of a pipeline caused by the high-concentration hydrogen is prevented, and the purification process is safer;
according to the device, the low-temperature separator for gas-liquid separation is additionally arranged before the raw material natural gas is cooled and liquefied and enters the LNG storage tank, and the BOG is taken from a gas phase outlet of the low-temperature separator, so that the content of methane in the BOG is reduced, and the concentration of helium is improved; the pure gas pipe is additionally arranged, the obtained high-purity helium part after pressure swing adsorption is led back to the front of the catalytic dehydrogenation reactor, and the hydrogen in the crude helium to be reacted is diluted to the position below the explosion limit concentration, so that explosion in the catalytic dehydrogenation reaction is avoided, and meanwhile, the hydrogen damage of the pipeline caused by the high-concentration hydrogen is prevented, so that the device is safe to operate, and the service lives of the pipeline and the device are prolonged.
Drawings
FIG. 1 is a schematic view of the structure of the apparatus of the present invention.
In the figure, a primary low-temperature heat exchanger (1), a first throttling valve (21), a second throttling valve (22), a third throttling valve (23), a low-temperature separator (3), a primary compressor (4), a secondary low-temperature separator (5), a denitrogenation tower (6), a catalytic dehydrogenation reactor (7), a dehydrator (8), a pressure swing adsorber (9), a helium storage tank (10), a gas flowmeter (11), a gas regulating valve (12), a secondary compressor (13), a pure gas pipe (14), an LNG storage tank (15) and an air cooler (16).
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The invention provides a process for extracting high-purity helium in a liquefied natural gas production process, which comprises the following steps of:
extracting BOG (boil off gas) before entering an LNG (liquefied natural gas) storage tank after the raw natural gas subjected to decarburization, dehydration, debenzolization and demercuration purification is cooled and liquefied; at the moment, the components in the BOG are methane, neon, nitrogen, hydrogen and helium, wherein the content of the nitrogen, the content of the hydrogen and the content of the helium are respectively 11.4%, 0.93% and 2.8%;
reheating the BOG to normal temperature, pressurizing, performing secondary cooling liquefaction, and separating out a nitrogen and methane mixed liquid material and hydrogen-containing crude helium; the methane and most of nitrogen in the BOG are liquefied and removed after the BOG is cooled and liquefied for the second time; the crude hydrogen-containing helium comprises about 65% of helium and the rest of nitrogen, hydrogen and neon;
carrying out catalytic dehydrogenation and dehydration on the hydrogen-containing crude helium to obtain crude helium; in order to remove the excessive oxygen in the reaction, the crude helium is also subjected to deoxidation treatment; crude helium comprises about 90% helium and the remainder nitrogen and neon;
removing nitrogen and neon from the crude helium through pressure swing adsorption to obtain high-purity helium; performing pressure swing adsorption by using activated carbon and a molecular sieve to finally obtain 99.999% of high-purity helium, and then storing the high-purity helium;
in order to ensure the reaction safety and avoid explosion, part of high-purity helium is doped into the crude helium containing hydrogen before the catalytic dehydrogenation reaction of the crude helium, so that the hydrogen content during the catalytic dehydrogenation reaction is reduced to the explosion limit concentration, namely below 4% volume concentration, and the process safety is ensured.
Furthermore, the high-purity helium gas added before the crude helium gas catalytic dehydrogenation reaction reduces the hydrogen content in the catalytic dehydrogenation reaction to below 2%.
Further, the temperature of the raw material natural gas after decarburization, dehydration, debenzolization and demercuration purification is 20 ℃ to 110 ℃, the raw material natural gas is cooled and liquefied through a primary low-temperature heat exchanger 1, the temperature of the liquefied raw material natural gas is-157 ℃ to 162 ℃, preferably-158 ℃, and the pressure is 1840kPa or so;
the gas-phase material BOG and the liquid-phase material LNG in the liquefied raw natural gas are separated through the low-temperature separator 3, namely the liquefied raw natural gas enters the LNG storage tank and is subjected to gas-liquid separation to obtain the BOG, compared with the method of obtaining gas in the LNG storage tank, the gas is obtained from the low-temperature separator 3, the concentration of helium in the BOG is increased by more than two times compared with the original concentration, and the subsequent purification of the helium is facilitated; adjusting the pressure of the gas-phase material BOG to about 150kPa, maintaining the temperature to about-158.6 ℃, and introducing into a low-temperature separator 3 for gas-liquid separation; a liquid phase outlet of the low-temperature separator 3 is connected to the LNG storage tank, and the liquid phase material LNG separated from the low-temperature separator 3 is collected; the outlet temperature of the cryogenic separator 3 was about-158.2 ℃.
Before BOG pressurization and secondary cooling liquefaction, the BOG is recovered by the primary low-temperature heat exchanger 1 to recover cold energy and reheat the BOG to normal temperature, and the pressure is adjusted to about 140kPa by the second throttle valve 21; then pressurizing the BOG at the normal temperature to 4-5 Mpa, preferably 4.2Mpa, increasing the temperature from the normal temperature to about 162 ℃ due to the volume compression of the gas, then introducing the BOG into a secondary low-temperature separator 5 for secondary cooling liquefaction, reducing the outlet temperature of the secondary low-temperature separator 5 to about-192.3 ℃, reducing the pressure to about 1.8MPa, and additionally, adding cooling equipment to ensure that the material at the temperature of 162 ℃ is cooled for two or more times to reach about-158 ℃ to-163 ℃ and then enters the secondary low-temperature separator 5; the BOG after the secondary cooling liquefaction by the secondary low-temperature separator 5 enters a denitrification tower 6 to remove liquid nitrogen and liquefied methane; the mixture fed into the denitrification tower 6 contains approximately 13% of gas phase components and 87% of liquid phase components, wherein the gas phase components are helium, nitrogen, hydrogen and neon, and the liquid phase components are methane and liquid nitrogen.
Further, if the BOG pressure changes, the pressure of the BOG after the secondary cooling liquefaction is adjusted to about 1.8MPa, and then catalytic dehydrogenation is carried out.
Further, before the liquefied raw natural gas enters the cryogenic separator 3, the pressure is adjusted to 150kPa by the first throttle valve 21.
As shown in fig. 1, the present invention further provides an apparatus for extracting high purity helium gas in the lng production process, which can apply the above process, and comprises a first-stage cryogenic heat exchanger 1, a first throttle valve 21, a cryogenic separator 3, a second valve 22, a first-stage compressor 4, a second-stage cryogenic separator 5, a third throttle valve 23, a denitrifier 6, a catalytic dehydrogenation reactor 7, a dehydrator 8, a pressure swing adsorber 9 and a helium gas storage tank 10, which are sequentially arranged on a helium gas extraction path through pipelines;
the gas outlet of the pressure swing adsorber 9 is also communicated with a pure gas pipe 14, the other end of the pure gas pipe 14 is communicated with a pipeline between the denitrification tower 6 and the catalytic dehydrogenation reactor 7, and the pure gas pipe 14 is provided with a gas regulating valve 12 and a gas flowmeter 11; the high-purity helium gas prepared by the pure gas pipe 14 can dilute the hydrogen gas before the catalytic dehydrogenation reaction, so that the concentration of the hydrogen gas is lower than the explosion limit concentration, and the explosion condition of the hydrogen gas reaction is avoided;
the primary low-temperature heat exchanger 1 is used for cooling and liquefying natural gas which is subjected to decarburization, dehydration, debenzolization and demercuration purification;
the low-temperature separator 3 is used for separating gas and liquid of the liquefied raw natural gas, and a gas-phase outlet of the low-temperature separator 3 recovers cold energy through the primary low-temperature heat exchanger 1 and can also be connected to the primary compressor 4 after being reheated to normal temperature through other heat exchange devices; the primary compressor 4 is used for pressurizing gas-phase materials;
the secondary low-temperature separator is used for cooling and liquefying gas-phase materials discharged from the pressurized low-temperature separator 3 to obtain a nitrogen-methane mixed liquid material and crude helium gas containing hydrogen;
the denitrification tower 6 is used for separating nitrogen and methane mixed liquid materials in the liquefied gas-phase materials, and a gas-phase outlet of the denitrification tower 6 is connected to the catalytic dehydrogenation reactor 7;
the catalytic dehydrogenation reactor 7 is used for reacting hydrogen in hydrogen-containing crude helium with metered oxygen to generate water, the dehydrator 8 is used for dehydrating and discharging the crude helium, the dehydrator 8 can also adsorb redundant oxygen and carbon dioxide generated with methane, and the dehydrator 8 can be a molecular sieve dryer in the prior art;
the crude helium gas is adsorbed by a pressure swing adsorber 9 to obtain high-purity helium gas, wherein the impurity gas is a small amount of nitrogen and neon, the pressure swing adsorber 9 is a double-tower pressure swing adsorption device, and double towers are alternately used, so that the device can continuously work;
the helium storage tank 10 is used for storing high purity helium.
Further, a gas phase outlet of the cryogenic separator 3 is connected back to the primary cryogenic heat exchanger 1 through a pipeline, so that a gas phase part of the cryogenic separator 3 is reheated through the primary cryogenic heat exchanger 1, the device for extracting high-purity helium gas in the liquefied natural gas production process further comprises an air cooler 16 arranged between the compressor 4 and the secondary cryogenic separator 5, and a third throttle valve 23 is arranged on a pipeline between the secondary cryogenic separator 5 and the denitrification tower 6, so that the pressure can be increased or reduced; in the production process of natural gas, raw material gas is subjected to decarburization, dehydration, debenzolization and demercuration purification, the temperature of the raw material natural gas subjected to decarburization, dehydration, debenzolization and demercuration purification is 20-110 ℃, and the raw material natural gas enters the device for helium purification; the temperature of the fluid flowing out after the temperature reduction of the first-stage low-temperature heat exchanger 1 is about-158 ℃, the pressure is about 1840kPa, after gas-liquid separation, the gas phase part in the low-temperature separator 3 is reheated to normal temperature by the first-stage low-temperature heat exchanger 1 and then compressed by the first-stage compressor 4, the pressure is changed to 4MPa-5MPa, preferably 4.2MPa, the temperature of the fluid is increased to about 162 ℃ due to volume compression, and is reduced to about-163 ℃ through the air cooler 16 for cooling, then the fluid is introduced into the secondary low-temperature separator 5 for cooling, the temperature of the secondary low-temperature separator 5 is reduced to 50 ℃ to 60 ℃, the temperature of the mixed material flowing out after the temperature of the secondary low-temperature separator 5 is reduced to minus 191 ℃ to minus 194 ℃, preferably about minus 192.3 ℃, the pressure is simultaneously reduced, the pressure is adjusted to about 1.8MPa through a second throttling valve 23, and then the mixed material enters a denitrification tower 6.
Further, the coolant in the secondary low-temperature separator 5 consists of the following components in parts by weight: 20-25% of methane, 30-35% of ethylene, 0-1% of ethane, 4-10% of nitrogen, 10-20% of propane and 3-15% of isopentane; the coolant in the secondary low-temperature separator 5 reduces the temperature of the material at-155 ℃ to-165 ℃ entering the secondary low-temperature separator 5 to 50 ℃ to 60 ℃, reduces the temperature of the material to be below the boiling point of methane, so that the methane is completely liquefied, and simultaneously, as the pressure of the material is 1.8MPa, the gas is basically liquefied into liquid nitrogen and only a trace amount of gas-phase nitrogen is available, so that all methane and most nitrogen can be separated from the gas phase, and the content of the helium is greatly improved; in addition, the refrigerant in the secondary low-temperature separator 5 is pressurized by the circulating compressor, expanded and refrigerated, and absorbs heat, and the component content adopted in the invention reduces the power consumption of the circulating compressor when compressing the refrigerant.
Further, the liquid phase outlet of the cryogenic separator 3 is connected to the LNG storage tank 15; the helium storage tank 10 is a high-pressure helium storage tank, a secondary compressor 13 is connected between the pressure swing adsorber 9 and the high-pressure helium storage tank, high-purity helium obtained by adsorbing miscellaneous gases by the pressure swing adsorber 9 is pressurized by the secondary compressor 13 and then enters the helium storage tank 10, and then the high-purity helium in the helium storage tank 10 can be subpackaged in helium steel bottles.
The process and the device have reasonable flow design, simple operation, safe operation and high helium extraction efficiency, and the concentration of the finally extracted high-purity helium can reach 99.999%.
It should be noted that the first-stage low-temperature heat exchanger 1 and the second-stage low-temperature separator 5 mentioned in the present invention are both low-temperature heat exchangers in the prior art, only the type of the medium therein is adjusted, and the circulating compressor and the refrigeration cycle device matched with the heat exchanger are conventionally matched; the denitrogenation tower 6, the catalytic dehydrogenation reactor 7, the pure oxygen filling device used in cooperation with the catalytic dehydrogenation reactor 7, the dehydrator 8 for dehydration and deoxidation or decarbonization and the pressure swing adsorber 9 are common devices in the field of gas separation and purification, and are not described again.
Although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that various changes in the embodiments and/or modifications of the invention can be made, and equivalents and modifications of some features of the invention can be made without departing from the spirit and scope of the invention.
Claims (8)
1. The process for extracting high-purity helium gas in the liquefied natural gas production process is characterized by comprising the following steps of:
extracting BOG (boil off gas) before entering an LNG (liquefied natural gas) storage tank after the raw natural gas subjected to decarburization, dehydration, debenzolization and demercuration purification is cooled and liquefied;
reheating the BOG to normal temperature, pressurizing, performing secondary cooling liquefaction, and separating out a nitrogen and methane mixed liquid material and hydrogen-containing crude helium;
carrying out catalytic dehydrogenation and dehydration on the hydrogen-containing crude helium to obtain crude helium;
removing nitrogen and neon from the crude helium through pressure swing adsorption to obtain high-purity helium;
part of high-purity helium gas is doped into the hydrogen-containing crude helium gas before the catalytic dehydrogenation reaction of the crude helium gas.
2. The process for extracting high purity helium gas in a liquefied natural gas production process as claimed in claim 1, wherein:
cooling and liquefying the raw natural gas subjected to decarburization, dehydration, debenzolization and demercuration purification by a primary low-temperature heat exchanger, wherein the temperature of the liquefied raw natural gas is-157 ℃ to-162 ℃;
separating a gas-phase material BOG and a liquid-phase material LNG in the liquefied raw material natural gas through a low-temperature separator, recovering cold energy from the gas-phase material BOG discharged from the low-temperature separator, and reheating, wherein a liquid-phase outlet of the low-temperature separator is connected to an LNG storage tank;
before BOG pressurization and secondary cooling liquefaction, the cooling capacity is recovered by a primary low-temperature heat exchanger for reheating; pressurizing BOG to 4-5 Mpa, and cooling and liquefying twice in a secondary low-temperature separator at-191 deg.C to-194 deg.C.
3. The process for extracting high purity helium gas in a liquefied natural gas production process as claimed in claim 2, wherein: before the liquefied raw material natural gas enters the low-temperature separator, the pressure is adjusted to 150kPa through a first throttle valve.
4. The process for extracting high purity helium gas in a liquefied natural gas production process as claimed in claim 1, wherein:
the high purity helium gas incorporated prior to the crude helium catalytic dehydrogenation reaction reduces the hydrogen content to below 2% when the catalytic dehydrogenation reaction is carried out.
5. Device of extracting high-purity helium in liquefied natural gas production process which characterized in that: the system comprises a first-stage low-temperature heat exchanger, a first throttle valve, a low-temperature separator, a first-stage compressor, a second-stage low-temperature separator, a third throttle valve, a denitrification tower, a catalytic dehydrogenation reactor, a dehydrator, a pressure swing adsorber and a helium storage tank which are sequentially arranged on a helium extraction path through pipelines;
the gas outlet of the pressure swing adsorber is also communicated with a pure gas pipe, the other end of the pure gas pipe is communicated with a pipeline between the denitrification tower and the catalytic dehydrogenation reactor, and a gas regulating valve and a gas flowmeter are arranged on the pure gas pipe;
the primary low-temperature heat exchanger is used for cooling and liquefying the raw material natural gas subjected to decarburization, dehydration, debenzolization and demercuration purification; the low-temperature separator is used for gas-liquid separation of the liquefied raw material natural gas, and a gas phase outlet of the low-temperature separator is connected to the primary compressor after cold energy is recovered by the primary low-temperature heat exchanger for reheating; the secondary low-temperature separator is used for cooling and liquefying gas-phase materials discharged by the pressurized low-temperature separator to obtain a nitrogen-methane mixed liquid material and crude helium gas containing hydrogen; the denitrification tower is used for separating nitrogen and methane mixed liquid materials in the liquefied gas-phase materials, and a gas-phase outlet of the denitrification tower is connected to the catalytic dehydrogenation reactor; the catalytic dehydrogenation reactor is used for reacting hydrogen in the hydrogen-containing crude helium gas with the metered oxygen to generate water, and the dehydrator is used for dehydrating and discharging the crude helium gas; and adsorbing the impurity gas by the crude helium gas through a pressure swing adsorber to obtain high-purity helium gas, wherein the helium gas storage tank is used for storing the high-purity helium gas.
6. The apparatus for extracting high purity helium gas in a liquefied natural gas production process according to claim 5, wherein: the temperature of the fluid flowing out after the temperature reduction of the primary low-temperature heat exchanger is-157 ℃ to-162 ℃, the outlet pressure of the primary compressor is 4MPa to 5MPa, the temperature of the mixed material flowing out after the temperature reduction of the secondary low-temperature separator is-191 ℃ to-194 ℃, and the pressure is 1.8 MPa.
7. The apparatus for extracting high purity helium gas in a liquefied natural gas production process according to claim 6, wherein: the coolant in the secondary low-temperature separator consists of the following components in parts by weight: 20-25% of methane, 30-35% of ethylene, 0-1% of ethane, 4-10% of nitrogen, 10-20% of propane and 3-15% of isopentane.
8. The apparatus for extracting high purity helium gas in a liquefied natural gas production process according to claim 5, wherein: the liquid phase outlet of the low-temperature separator is connected to an LNG storage tank; the pressure swing adsorber is a double-tower pressure swing adsorption device, the helium storage tank is a high-pressure helium storage tank, a secondary compressor is connected between the pressure swing adsorber and the high-pressure helium storage tank, and high-purity helium obtained by adsorbing miscellaneous gases through the pressure swing adsorber is pressurized by the secondary compressor and then enters the helium storage tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110543949.6A CN113108551A (en) | 2021-05-17 | 2021-05-17 | Process and device for extracting high-purity helium in liquefied natural gas production process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110543949.6A CN113108551A (en) | 2021-05-17 | 2021-05-17 | Process and device for extracting high-purity helium in liquefied natural gas production process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN113108551A true CN113108551A (en) | 2021-07-13 |
Family
ID=76723268
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110543949.6A Pending CN113108551A (en) | 2021-05-17 | 2021-05-17 | Process and device for extracting high-purity helium in liquefied natural gas production process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113108551A (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113548649A (en) * | 2021-08-18 | 2021-10-26 | 广州市粤佳气体有限公司 | Helium purification low-temperature adsorption process |
| CN113686098A (en) * | 2021-09-27 | 2021-11-23 | 西南石油大学 | Natural gas liquefaction and helium recovery method |
| CN113694705A (en) * | 2021-08-11 | 2021-11-26 | 宁夏天利丰能源利用有限公司 | Process method and equipment for extracting pure helium gas from BOG gas |
| CN114562852A (en) * | 2022-03-22 | 2022-05-31 | 北京中科富海低温科技有限公司 | Helium de-neon system and method thereof |
| CN114674115A (en) * | 2022-04-02 | 2022-06-28 | 珠海森铂低温能源装备有限公司 | System and method for extracting high-purity helium from BOG flash gas of liquefied natural gas |
| CN114669164A (en) * | 2022-03-24 | 2022-06-28 | 浙江大学 | System and method for preparing high-purity helium from natural gas BOG |
| CN116281896A (en) * | 2022-12-01 | 2023-06-23 | 煤炭科学技术研究院有限公司 | Helium extraction method for helium-containing coal bed gas concentration at low temperature |
| CN116951900A (en) * | 2023-08-30 | 2023-10-27 | 宁夏天利丰能源利用有限公司 | Natural gas liquefaction and high-purity helium extraction integrated process |
| CN117308513A (en) * | 2023-10-10 | 2023-12-29 | 宁夏天利丰能源利用有限公司 | Process for extracting crude helium gas by low-temperature rectification |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101445755A (en) * | 2008-12-22 | 2009-06-03 | 中国石油集团长城钻探工程有限公司 | Coal bed gas purifying and liquefying method |
| CN106315527A (en) * | 2016-08-11 | 2017-01-11 | 四川空分设备(集团)有限责任公司 | Refining technique for extracting high purity helium from highly hydrogenous raw helium |
| CN107514872A (en) * | 2017-09-27 | 2017-12-26 | 中科瑞奥能源科技股份有限公司 | The technique and system of helium are reclaimed from LNG storage tank flash steam |
| CN108458549A (en) * | 2018-03-23 | 2018-08-28 | 中科瑞奥能源科技股份有限公司 | Helium and liquefied System and method for are carried from natural gas |
| CN208332859U (en) * | 2018-03-23 | 2019-01-04 | 中科瑞奥能源科技股份有限公司 | Helium and liquefied system are proposed from natural gas |
| CN110686464A (en) * | 2019-10-15 | 2020-01-14 | 北京石油化工工程有限公司 | Method and device for recovering helium in flash steam of liquefied natural gas |
| US20200088466A1 (en) * | 2018-09-13 | 2020-03-19 | Air Products And Chemicals, Inc. | Helium Extraction from Natural Gas |
| CN111533095A (en) * | 2020-04-28 | 2020-08-14 | 大连海奥膜技术有限公司 | Equipment and process for purifying helium from BOG gas |
| CN112023618A (en) * | 2020-07-22 | 2020-12-04 | 中国石油天然气股份有限公司西南油气田分公司成都天然气化工总厂 | Crude helium refining system and method |
-
2021
- 2021-05-17 CN CN202110543949.6A patent/CN113108551A/en active Pending
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101445755A (en) * | 2008-12-22 | 2009-06-03 | 中国石油集团长城钻探工程有限公司 | Coal bed gas purifying and liquefying method |
| CN106315527A (en) * | 2016-08-11 | 2017-01-11 | 四川空分设备(集团)有限责任公司 | Refining technique for extracting high purity helium from highly hydrogenous raw helium |
| CN107514872A (en) * | 2017-09-27 | 2017-12-26 | 中科瑞奥能源科技股份有限公司 | The technique and system of helium are reclaimed from LNG storage tank flash steam |
| CN108458549A (en) * | 2018-03-23 | 2018-08-28 | 中科瑞奥能源科技股份有限公司 | Helium and liquefied System and method for are carried from natural gas |
| CN208332859U (en) * | 2018-03-23 | 2019-01-04 | 中科瑞奥能源科技股份有限公司 | Helium and liquefied system are proposed from natural gas |
| US20200088466A1 (en) * | 2018-09-13 | 2020-03-19 | Air Products And Chemicals, Inc. | Helium Extraction from Natural Gas |
| CN110686464A (en) * | 2019-10-15 | 2020-01-14 | 北京石油化工工程有限公司 | Method and device for recovering helium in flash steam of liquefied natural gas |
| CN111533095A (en) * | 2020-04-28 | 2020-08-14 | 大连海奥膜技术有限公司 | Equipment and process for purifying helium from BOG gas |
| CN112023618A (en) * | 2020-07-22 | 2020-12-04 | 中国石油天然气股份有限公司西南油气田分公司成都天然气化工总厂 | Crude helium refining system and method |
Non-Patent Citations (1)
| Title |
|---|
| 张祉祐: "《制冷与低温技术下册》", 30 September 1981 * |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113694705A (en) * | 2021-08-11 | 2021-11-26 | 宁夏天利丰能源利用有限公司 | Process method and equipment for extracting pure helium gas from BOG gas |
| CN113548649A (en) * | 2021-08-18 | 2021-10-26 | 广州市粤佳气体有限公司 | Helium purification low-temperature adsorption process |
| CN113686098A (en) * | 2021-09-27 | 2021-11-23 | 西南石油大学 | Natural gas liquefaction and helium recovery method |
| CN114562852A (en) * | 2022-03-22 | 2022-05-31 | 北京中科富海低温科技有限公司 | Helium de-neon system and method thereof |
| CN114562852B (en) * | 2022-03-22 | 2022-09-06 | 北京中科富海低温科技有限公司 | Helium de-neon system and method thereof |
| CN114669164A (en) * | 2022-03-24 | 2022-06-28 | 浙江大学 | System and method for preparing high-purity helium from natural gas BOG |
| CN114674115A (en) * | 2022-04-02 | 2022-06-28 | 珠海森铂低温能源装备有限公司 | System and method for extracting high-purity helium from BOG flash gas of liquefied natural gas |
| CN116281896A (en) * | 2022-12-01 | 2023-06-23 | 煤炭科学技术研究院有限公司 | Helium extraction method for helium-containing coal bed gas concentration at low temperature |
| CN116281896B (en) * | 2022-12-01 | 2024-04-16 | 煤炭科学技术研究院有限公司 | Helium extraction method for helium-containing coal bed gas concentration at low temperature |
| CN116951900A (en) * | 2023-08-30 | 2023-10-27 | 宁夏天利丰能源利用有限公司 | Natural gas liquefaction and high-purity helium extraction integrated process |
| CN116951900B (en) * | 2023-08-30 | 2024-08-09 | 宁夏天利丰能源利用有限公司 | Natural gas liquefaction and high-purity helium extraction integrated process |
| CN117308513A (en) * | 2023-10-10 | 2023-12-29 | 宁夏天利丰能源利用有限公司 | Process for extracting crude helium gas by low-temperature rectification |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN113108551A (en) | Process and device for extracting high-purity helium in liquefied natural gas production process | |
| CN210237128U (en) | System for purifying helium from natural gas liquefied helium-containing tail gas | |
| CN112361712B (en) | Hydrogen liquefying equipment adopting helium refrigerating circulation system | |
| CN111964354B (en) | Method for separating and purifying helium gas by removing methane and nitrogen | |
| CN113959176B (en) | System and method for separating helium from liquefied natural gas flash gas | |
| CN110455038B (en) | Helium extraction unit, helium extraction device and system for co-producing helium | |
| CN114111215A (en) | Device for preparing liquid hydrogen by using low-temperature hydrogen-containing mixed gas and using method | |
| CN110217794B (en) | Production method and production device of high-purity carbon dioxide | |
| CN112393527A (en) | LNG flash steam recovery method and system | |
| CN111692837A (en) | System for utilize LNG apparatus for producing coproduction helium | |
| CN113144821A (en) | Multi-technology integrated separation process for producing high-purity helium gas from helium-rich natural gas liquefaction tail gas | |
| CN115888386A (en) | Process for extracting helium from high-nitrogen BOG gas | |
| CN109631494A (en) | A kind of helium production system and production method | |
| CN114314534B (en) | Natural gas helium extraction process | |
| US20240263873A1 (en) | Device and method for recovering carbon dioxide and nitrogen from flue gas | |
| CN217148577U (en) | System for extracting high-purity helium from low-helium BOG | |
| CN115155257B (en) | Method for extracting high-purity helium from low-helium-content BOG | |
| CN114777418B (en) | System for extracting helium from natural gas BOG by condensation method | |
| CN114165987B (en) | Liquid carbon dioxide production device and production method thereof | |
| CN114459203A (en) | Method for extracting high-purity helium gas in LNG production process based on flash evaporation technology | |
| CN117146527A (en) | Helium extracting device and method for low-temperature rectification of flash gas of liquefied natural gas | |
| CN113566493A (en) | Cryogenic separation system for helium recovery | |
| CN106731497B (en) | Decarbonizing and extracting N from nitric acid industrial tail gas 2 O purification device and process method | |
| CN111947394A (en) | Device and process for extracting helium from liquefied natural gas BOG | |
| CN114669164B (en) | System and method for preparing high-purity helium from natural gas BOG |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20230220 Address after: 100000 Beijing Chaoyang District Huixin East Street No. 16, 12th Floor Applicant after: SINOPEC OILFIELD SERVICE Corp. Applicant after: SINOPEC ZHONGYUAN PETROLEUM ENGINEERING DESIGN Co.,Ltd. Address before: 450000 unit 3, building 2, Greenland Yuansheng international, No. 49, Jinshui East Road, Zhengzhou area (Zhengdong), Zhengzhou pilot Free Trade Zone, Henan Province Applicant before: SINOPEC ZHONGYUAN PETROLEUM ENGINEERING DESIGN Co.,Ltd. |
|
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20210713 |