CN107641536B - System device and process suitable for natural gas dehydration treatment for offshore platform liquefaction - Google Patents
System device and process suitable for natural gas dehydration treatment for offshore platform liquefaction Download PDFInfo
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Abstract
The invention discloses a natural gas dehydration treatment system and a natural gas dehydration treatment process suitable for offshore platform liquefaction, and the system comprises a filtering separator, a first hypergravity machine, a triethylene glycol condenser, a lean/rich liquid heat exchanger, a booster pump, a buffer tank, a reboiler, a second hypergravity machine, a flash tank, a delivery pump, a first stop valve, a second stop valve, a third stop valve, a stripping agent condenser, a three-phase separator, a stripping agent dryer, a stripping agent storage tank, a stripping agent pump, a first flowmeter, a second flowmeter and a three-way valve. The natural gas dehydration and triethylene glycol regeneration parts of the device adopt the supergravity reactor, so that the height and the size of the device can be reduced; the device can improve the purity of the regenerated triethylene glycol barren solution to 99.999 wt%, and the triethylene glycol barren solution is used as an absorbent, so that the dew point of the water at the outlet of the natural gas subjected to water absorption treatment in an absorption system can be reduced to be below 100 ℃ below zero; can meet the processing requirements of natural gas for liquefaction on space-limited occasions such as offshore platforms and the like.
Description
Technical Field
The invention relates to the technical field of petroleum and natural gas treatment and processing, in particular to a system device and a process suitable for natural gas dehydration treatment for offshore platform liquefaction.
Background
Natural gas is a clean fuel, has small combustion pollution and high heat value, and occupies more and more important position in modern energy structures. In recent decades, land oil and gas exploration degree is higher, the scale of an oil and gas field is found to be smaller, and the contribution of newly added reserves to the increase of oil and gas reserves in the world is reduced. Compared with the world ocean oil and gas exploration and development, the exploration and development of the world ocean oil and gas are rapidly developed and continuously obtain important findings, the discovered oil and gas fields have large scale and high productivity, and the proportion of the oil and gas output to the total world output is continuously increased. The marine continental shelf of China contains abundant natural gas resources, and the accelerated development and utilization of the resources have very important practical and strategic significance for relieving the energy shortage condition of China and ensuring and promoting the economic development of China. At present, most of oil and gas fields in China are far away from the coast, and the natural gas is difficult to transport to land for use through a pipeline after being extracted, so that the natural gas needs to be liquefied on an ocean platform, and the transportation of ships is facilitated.
Natural gas produced from offshore fields typically contains a large amount of water vapor that, if untreated, forms solid hydrates with hydrocarbons in the natural gas during cryogenic liquefaction of the natural gas. On one hand, the solid hydrate can block pipelines and equipment of a liquefaction system, on the other hand, the solid hydrate can impact a high-pressure storage tank in the process of transporting liquefied natural gas by a ship to generate static electricity, and serious potential safety hazards are brought. Therefore, before natural gas liquefaction, the natural gas must be dehydrated to extremely low content, so that the water dew point of the natural gas reaches below-l 00 ℃, so as to ensure that no solid water or solid hydrate is condensed and separated out in a liquid phase component in the natural gas liquefaction process, and ensure the safe operation of production and transportation devices.
At present, the common methods for dehydrating natural gas include a solid adsorption method, a solvent absorption method, a freeze separation method, and the like. Because the dehydrated water dew point of the natural gas for liquefaction is required to be below-100 ℃, the dehydration treatment of the natural gas for liquefaction in industry generally adopts a solid adsorption method with higher dehydration depth, and the method has large basic investment and high adsorbent regeneration energy consumption, so that the actual industrial production of the natural gas for liquefaction generally adopts sectional dehydration, firstly triethylene glycol is adopted to carry out primary dehydration on the natural gas to remove most of water in the natural gas, and then the solid adsorption method is used to remove low-content water in the natural gas to ensure that the water dew point reaches the required-100 ℃. On the one hand, the triethylene glycol absorption method and the solid adsorption method are used simultaneously, prying is not easy to occur, and the cost of the device is increased.
The supergravity technology is a process-intensive emerging technology capable of enhancing mass transfer. The supergravity technology utilizes the centrifugal force generated by a rotor rotating at a high speed to crush liquid into liquid films and liquid drops with tiny polarity, the updating speed of a phase interface is accelerated, the mass transfer process is greatly enhanced, the advantages of short retention time, high vapor-liquid mass transfer efficiency and small equipment size are achieved, and the requirements of an offshore platform on the size and the height of the equipment can be met.
The invention patent CN201410490633 in China reports a triethylene glycol natural gas dehydration system by a supergravity method and a process thereof, and the process adopts a supergravity rotary packed bed as an absorption and regeneration device, so that the mass transfer efficiency of the triethylene glycol-natural gas dehydration system is improved, the natural gas dehydration system is simplified, and the size of dehydration equipment is reduced. The system and the process can regenerate the triethylene glycol barren solution to 99.0 percent of purity at minimum, and the triethylene glycol solution with the purity is adopted for natural gas dehydration, so that the water dew point temperature can be reduced to about-18 ℃ at minimum, and the requirement of gas natural gas pipeline transportation under the common ambient temperature can be met.
Chinese utility model patent CN201720055206 reports a portable skid-mounted natural gas dehydration device, the device includes triethylene glycol hypergravity absorbing device and hypergravity triethylene glycol regenerating unit two parts, wherein hypergravity triethylene glycol regenerating unit adopts the dry gas of natural gas as the stripping gas, improves the purity of triethylene glycol after regeneration to about 99.8%, uses the triethylene glycol solution of this purity to carry out the natural gas dehydration, is expected to further reduce the water dew point temperature of natural gas (can reduce the water dew point temperature to about-40 ℃ in theory). Even in this case, the dehydration treatment requirements for the natural gas for liquefaction at the dew point distance of the natural gas water obtained by the dehydration treatment using the apparatus of this patent are still quite different.
Therefore, it is necessary to develop a dehydration system and a dehydration process that have high dehydration efficiency, small device size and low height, and the dehydration depth can meet the dehydration treatment requirement of natural gas for liquefaction. .
Disclosure of Invention
The first technical problem to be solved by the invention is to provide a system device suitable for dehydration treatment of natural gas for liquefaction on an offshore platform; the device can improve the purity of the regenerated triethylene glycol to 99.999 wt%, and the triethylene glycol lean solution is used as an absorbent, so that the water dew point of the outlet water of the natural gas subjected to water absorption treatment in an absorption system can be reduced to be below-100 ℃, and the dehydration treatment requirement of the natural gas for liquefaction is met. Meanwhile, the hypergravity reactor is used in both the natural gas dehydration part and the triethylene glycol regeneration part, and the equipment size and the investment are reduced by strengthening gas-liquid mass transfer, so that the natural gas treatment requirements of space-limited occasions such as offshore platforms and the like can be met.
The second technical problem to be solved by the invention is to utilize the dehydration process of the system device suitable for the dehydration treatment of the natural gas for the liquefaction of the offshore platform.
In order to solve the first technical problem, the invention adopts the following technical scheme:
the invention relates to a system device suitable for dehydration treatment of natural gas for offshore platform liquefaction, which comprises a filtering separator, a first hypergravity machine, a triethylene glycol condenser, a lean/rich liquid heat exchanger, a booster pump, a buffer tank, a reboiler, a second hypergravity machine, a flash tank, a delivery pump, a first stop valve, a second stop valve, a third stop valve, a stripping agent condenser, a three-phase separator, a stripping agent dryer, a stripping agent storage tank, a stripping agent pump, a first flowmeter, a second flowmeter and a three-way valve, wherein the first hypergravity machine is connected with the first stop valve;
an outlet of the filtering separator is connected with a gas phase inlet of a first hypergravity machine, a gas phase outlet of the first hypergravity machine is connected with an inlet of a first stop valve, and an outlet of the first stop valve is communicated with a downstream working section;
a liquid phase outlet of the first hypergravity machine is connected with a rich liquid inlet of the lean/rich liquid heat exchanger, a rich liquid outlet of the lean/rich liquid heat exchanger is connected with an inlet of the flash tank, a liquid phase outlet of the flash tank is connected with an inlet of the delivery pump, and a gas phase outlet of the flash tank is communicated with the tail gas treatment;
an outlet of the conveying pump is connected with a liquid phase inlet of a second hypergravity machine, a liquid phase outlet of the second hypergravity machine is connected with a liquid phase inlet of a reboiler, a gas phase outlet of the second hypergravity machine is connected with an inlet of a stripping agent condenser, an outlet of the stripping agent condenser is connected with an inlet of a three-phase separator, and a water drainage port is formed in the lower end of the three-phase separator;
a non-condensable gas outlet of the three-phase separator is communicated with tail gas treatment, a stripping agent outlet of the three-phase separator is connected with an inlet of a stripping agent dryer, and an outlet of the stripping agent dryer is connected to a first inlet of a three-way valve; the stripping agent storage tank and the third stop valve are sequentially connected with the first flow meter, and finally, the outlet of the first flow meter is connected to the second inlet of the three-way valve; the outlet of the three-way valve is connected with the inlet of a stripping agent pump, the outlet of the stripping agent pump is connected with the inlet of a second flowmeter, and the outlet of the second flowmeter is connected with a reboiler to realize the circulation of the stripping agent;
the utility model discloses a high-efficiency boiler, including reboiler, lean/rich liquid heat exchanger, condenser, reboiler gas phase export, reboiler gas phase access connection with the second hypergravity machine, the liquid phase export of reboiler is through second stop valve and buffer tank access connection, buffer tank bottom liquid phase export and booster pump access connection, the export of booster pump and the lean solution access connection of lean/rich liquid heat exchanger, the lean solution export and the condenser access connection of lean/rich liquid heat exchanger, the export of condenser is connected with the liquid phase import of first hypergravity machine, realizes the circulation of triethylene glycol.
In order to solve the second technical problem, the present invention utilizes the dehydration process of the system apparatus suitable for dehydration of natural gas for offshore platform liquefaction, which comprises the following steps:
1) the natural gas with the pressure of 5-20MPa enters a filtering separator to remove free liquid water and solid impurities, and then is discharged from an outlet of the filtering separator;
2) the natural gas discharged in the step 1) enters a first hypergravity machine, is in countercurrent contact with triethylene glycol barren solution in the first hypergravity machine for dehydration, and the dehydrated dry gas is discharged out of the system and enters a downstream working section;
3) discharging the triethylene glycol rich solution after water absorption in the step 2) out of the first hypergravity machine, and allowing the triethylene glycol rich solution to enter a flash tank after heat exchange with triethylene glycol lean solution;
4) the triethylene glycol in the step 3) is flashed by a flash tank and then pumped into a second hypergravity machine by a delivery pump, the triethylene glycol is in countercurrent contact with a stripping agent gasified by a reboiler in the second hypergravity machine, and water in the triethylene glycol is transferred to a gas phase; on one hand, the stripping agent and the water in the triethylene glycol form an azeotrope, so that the water is transferred to a gas phase in the form of the azeotrope, and on the other hand, the gasified stripping agent can enhance the turbulence of the liquid-phase triethylene glycol, reduce the partial pressure of the water in the gas phase and promote the water to be transferred to the gas phase; discharging the regenerated triethylene glycol from a liquid phase outlet of the second hypergravity machine, and discharging a stripping agent from a gas phase outlet of the second hypergravity machine;
5) the stripping agent discharged from the gas phase outlet of the second hypergravity machine in the step 4) enters a stripping agent condenser, and is discharged out of the stripping agent condenser after being condensed into a liquid state;
6) the stripping agent discharged from the stripping agent condenser in the step 5) enters a three-phase separator, water is separated from the stripping agent, the non-condensable gas is led to tail gas treatment, water is discharged out of the system, and the stripping agent enters a stripping agent dryer;
7) drying the stripping agent entering the stripping agent dryer in the step 6) to further remove trace moisture in the stripping agent, and meanwhile, supplementing the stripping agent lost in the recovery process of the stripping agent through a stripping agent storage tank; then, a stripping agent pump is used for conveying the stripping agent into a reboiler, the stripping agent forms an azeotrope with water in the triethylene glycol rich solution discharged from the second hypergravity machine in the step 4) in the reboiler, and the stripping agent is gasified, so that the recycling of the stripping agent is realized; the triethylene glycol is discharged from a liquid phase outlet of the reboiler after being further regenerated;
8) step 7), feeding the triethylene glycol barren solution discharged from the liquid phase outlet of the reboiler into a buffer tank to form a stable liquid level in the buffer tank;
9) and 8) conveying the triethylene glycol lean solution in the buffer tank in the step 8) to a lean/rich solution heat exchanger by a booster pump, exchanging heat with the triethylene glycol rich solution in the step 3) in the lean/rich solution heat exchanger, condensing by a triethylene glycol condenser, and then feeding into the first hypergravity machine again to realize circulation of triethylene glycol.
As a further improvement of the technical scheme, in the step 2), the volume ratio of the triethylene glycol lean solution to the natural gas feed gas is 1: 5000-1: 10000.
as a further improvement of the technical scheme, in the step 2), the concentration of the triethylene glycol barren solution can reach 99.999 percent, and the dew point of water at the outlet of natural gas can reach below 100 ℃ below zero.
As a further improvement of the technical scheme, in the step 4), the stripping agent is one or more of isooctane, n-heptane, toluene, ethylbenzene and the like which can form a low-boiling-point azeotrope with water.
As a further improvement of the technical scheme, in the step 7), the volume ratio of the using amount of the stripping agent to the using amount of the triethylene glycol rich solution in the step 4) is 0.15-0.5.
As a further improvement of the technical proposal, in the step 5), the temperature of the condenser of the stripping agent is between 20 and 50 DEG C
As a further improvement of the technical solution, the hypergravity level of the first hypergravity machine in the step 2) is 100-500, and the hypergravity level of the second hypergravity machine in the step 2) is 100-500.
As a further improvement of the technical scheme, in the step 7), the temperature of the reboiler is 190-204 ℃.
As a further improvement of the technical proposal, in the step 9), the temperature of the triethylene glycol condenser is 15-30 ℃.
Any range recited herein is intended to include the endpoints and any number between the endpoints and any subrange subsumed therein or defined therein.
The starting materials of the present invention are commercially available, unless otherwise specified, and the equipment used in the present invention may be any equipment conventionally used in the art or may be any equipment known in the art.
Compared with the prior art, the invention has the following beneficial effects:
1) the dehydration depth is high. The stripping agent is introduced, so that an azeotrope can be formed with water in the triethylene glycol rich solution, the turbulence of liquid-phase triethylene glycol can be enhanced under the action of stripping gas after the stripping agent is gasified, the water partial pressure is reduced, and the migration of water from a liquid phase to a gas phase is greatly promoted under the combined action of the factors.
2) The system and the process provided by the invention can improve the purity of the regenerated triethylene glycol to 99.999 wt%, and the triethylene glycol barren solution is used as an absorbent, so that the water dew point of the outlet water of the natural gas subjected to water absorption treatment in an absorption system can be reduced to be below-100 ℃, and the dehydration treatment requirement of the natural gas for liquefaction is met.
3) The device has small size and low height. In the system, a natural gas dehydration system and a triethylene glycol regeneration system both adopt a supergravity reactor. Therefore, the system has the advantages of the supergravity technology: the gas-liquid contact area is greatly increased, the gas-liquid mass transfer efficiency is improved, the height of the device is low, the size of the device is small, the start and stop are easy, and the device is suitable for occasions with limited space, such as offshore platforms and the like.
Drawings
The following detailed description of embodiments of the invention is provided in connection with the accompanying drawings
FIG. 1 is a schematic diagram of a natural gas dehydration treatment system suitable for offshore platform liquefaction
Numerical designations in fig. 1:
1-a filtration separator; 2-a first hypergravity machine; 3-triethylene glycol condenser; 4-lean/rich liquor heat exchanger;
5, a booster pump; 6-a buffer tank; 7-a reboiler; 8-a second hypergravity machine;
9-a flash tank; 10-a delivery pump; 11-a first stop valve; 12-a second stop valve;
17-a third stop valve; 13-stripper condenser; 14-a three-phase separator; 15-stripper drier;
16-stripping agent storage tank; 18-stripper pump; 19-a first flow meter; 20-a second flow meter; 21-three-way valve.
Detailed Description
In order to more clearly illustrate the invention, the invention is further described below in connection with preferred embodiments. It is to be understood by persons skilled in the art that the following detailed description is illustrative and not restrictive, and is not to be taken as limiting the scope of the invention.
Referring to fig. 1, the natural gas dehydration treatment system for offshore platform liquefaction comprises a filtering separator 1, a first hypergravity machine 2, a triethylene glycol condenser 3, a lean/rich liquid heat exchanger 4, a booster pump 5, a buffer tank 6, a reboiler 7, a second hypergravity machine 8, a flash tank 9, a transfer pump 10, a first stop valve 11, a second stop valve 12, a third stop valve 17, a stripping agent condenser 13, a three-phase separator 14, a stripping agent dryer 15, a stripping agent storage tank 16, a stripping agent pump 18, a first flowmeter 19, a second flowmeter 20 and a three-way valve 21;
an outlet of the filter separator 1 is connected with a gas phase inlet of a first hypergravity machine 2, a gas phase outlet of the first hypergravity machine 2 is connected with an inlet of a first stop valve 11, and an outlet of the first stop valve 11 is communicated with a downstream working section;
a liquid phase outlet of the first hypergravity machine 2 is connected with a rich liquid inlet of a lean/rich liquid heat exchanger 4, a rich liquid outlet of the lean/rich liquid heat exchanger 4 is connected with an inlet of a flash tank 9, a liquid phase outlet of the flash tank 9 is connected with an inlet of a delivery pump 10, and a gas phase outlet of the flash tank 9 is communicated with a tail gas treatment;
an outlet of the delivery pump 10 is connected with a liquid phase inlet of a second hypergravity machine 8, a liquid phase outlet of the second hypergravity machine 8 is connected with a liquid phase inlet of a reboiler 7, a gas phase outlet of the second hypergravity machine 8 is connected with an inlet of a stripping agent condenser 13, an outlet of the stripping agent condenser 13 is connected with an inlet of a three-phase separator 14, and a water drain port is arranged at the lower end of the three-phase separator 14;
a non-condensable gas outlet of the three-phase separator 14 is communicated with tail gas treatment, a stripping agent outlet of the three-phase separator 14 is connected with an inlet of a stripping agent dryer 15, and an outlet of the stripping agent dryer 15 is connected to a first inlet of a three-way valve 21; the stripping agent storage tank 16 and the third stop valve 17 are sequentially connected with the first flowmeter 19, and finally, the outlet of the first flowmeter 19 is connected to the second inlet of the three-way valve 21; the outlet of the three-way valve 21 is connected with the inlet of a stripping agent pump 18, the outlet of the stripping agent pump 18 is connected with the inlet of a second flowmeter 20, and the outlet of the second flowmeter 20 is connected with the reboiler 7, so that the circulation of the stripping agent is realized;
the gas phase outlet of the reboiler 7 is connected with the gas phase inlet of the second hypergravity machine 8, the liquid phase outlet of the reboiler 7 is connected with the inlet of the buffer tank 6 through the second stop valve 12, the liquid phase outlet of the bottom of the buffer tank 6 is connected with the inlet of the booster pump 5, the outlet of the booster pump 5 is connected with the lean solution inlet of the lean/rich solution heat exchanger 4, the lean solution outlet of the lean/rich solution heat exchanger 4 is connected with the inlet of the condenser 3, the outlet of the condenser 3 is connected with the liquid phase inlet of the first hypergravity machine 2, and the circulation of triethylene glycol is realized.
The dehydration process of the system device suitable for the dehydration treatment of the natural gas for the offshore platform liquefaction comprises the following steps:
1) the natural gas with the pressure of 5-20MPa enters a filtering separator to remove free liquid water and solid impurities, and then is discharged from an outlet of the filtering separator;
2) the natural gas discharged in the step 1) enters a first hypergravity machine, is in countercurrent contact with triethylene glycol barren solution in the first hypergravity machine for dehydration, and a dehydrated dry gas is discharged from a system and enters a downstream working section;
3) discharging the triethylene glycol rich solution after water absorption in the step 2) out of the first hypergravity machine, and allowing the triethylene glycol rich solution to enter a flash tank after heat exchange with triethylene glycol lean solution;
4) the triethylene glycol in the step 3) is flashed by a flash tank and then pumped into a second hypergravity machine by a delivery pump, the triethylene glycol is in countercurrent contact with a stripping agent gasified by a reboiler in the second hypergravity machine, and water in the triethylene glycol is transferred to a gas phase; on one hand, the stripping agent and the water in the triethylene glycol form an azeotrope, so that the water is transferred to a gas phase in the form of the azeotrope, and on the other hand, the gasified stripping agent can enhance the turbulence of the liquid-phase triethylene glycol, reduce the partial pressure of the water in the gas phase and promote the water to be transferred to the gas phase; discharging the regenerated triethylene glycol from a liquid phase outlet of the second hypergravity machine, and discharging a stripping agent from a gas phase outlet of the second hypergravity machine;
5) the stripping agent discharged from the gas phase outlet of the second hypergravity machine in the step 4) enters a stripping agent condenser, and is discharged out of the stripping agent condenser after being condensed into a liquid state;
6) the stripping agent discharged from the stripping agent condenser in the step 5) enters a three-phase separator, water is separated from the stripping agent, the non-condensable gas is led to tail gas treatment, water is discharged out of the system, and the stripping agent enters a stripping agent dryer;
7) drying the stripping agent entering the stripping agent dryer in the step 6) to further remove trace moisture in the stripping agent, and meanwhile, supplementing the stripping agent lost in the recovery process of the stripping agent through a stripping agent storage tank; then, a stripping agent pump is used for conveying the stripping agent into a reboiler, the stripping agent forms an azeotrope with water in the triethylene glycol rich solution discharged from the second hypergravity machine in the step 4) in the reboiler, and the stripping agent is gasified, so that the recycling of the stripping agent is realized; the triethylene glycol is discharged from a liquid phase outlet of the reboiler after being further regenerated;
8) step 7), feeding the triethylene glycol barren solution discharged from the liquid phase outlet of the reboiler into a buffer tank to form a stable liquid level in the buffer tank;
9) and 8) conveying the triethylene glycol lean solution in the buffer tank in the step 8) to a lean/rich solution heat exchanger by a booster pump, exchanging heat with the triethylene glycol rich solution in the step 3) in the lean/rich solution heat exchanger, condensing by a triethylene glycol condenser, and then feeding into the first hypergravity machine again to realize circulation of triethylene glycol.
In certain embodiments of the invention, the volume ratio of triethylene glycol lean solution to natural gas feed gas in step 2) is 1: 5000-1: 10000, or 1: 5000-1: 6000, or 1: 5000-1: 7000, or 1: 5000-1: 8000, or 1: 5000-1: 9000.
in certain embodiments of the invention, the triethylene glycol lean solution concentration in step 2) can reach 99.999%, and the dew point of the water at the outlet of the natural gas can reach below-100 ℃.
In certain embodiments of the present invention, in step 4), the stripping agent is one or more of isooctane, n-heptane, toluene, ethylbenzene, and the like, which can form a low boiling azeotrope with water.
In certain embodiments of the present invention, the volume ratio of the amount of stripping agent used in step 7) to the amount of triethylene glycol rich liquid used in step 4) is 0.15 to 0.5.
In certain embodiments of the invention, the temperature of the stripper condenser in step 5) is from 20 ℃ to 50 ℃.
In some embodiments of the invention, the supergravity level of the first supergravity machine in step 2) is 100-; the supergravity level of the second supergravity machine in the step 2) is 100-.
In certain embodiments of the invention, in step 7), the reboiler temperature is from 190 ℃ to 204 ℃.
In certain embodiments of the invention, the temperature of the triethylene glycol condenser in step 9) is from 15 ℃ to 30 ℃.
Example 1
The device and the process are used for deeply removing water in natural gas by using triethylene glycol:
the pressure of natural gas entering the system is 7MPa, and the volume ratio of triethylene glycol barren solution to natural gas raw material gas is 1: 10000, the ratio of the using amount of the stripping agent to the using amount of the triethylene glycol rich solution is 0.15: 1, a stripping agent is n-heptane, the temperature of a triethylene glycol condenser is 30 ℃, the hypergravity level of a first hypergravity machine is 200, the hypergravity level of a second hypergravity machine is 200, and the temperature of a reboiler is 200 ℃; under the process condition, the purity of the regenerated triethylene glycol barren solution reaches about 99.999 wt%, and the water dew point of the outlet natural gas reaches below minus 104 ℃.
Example 2
As described in example 1, the supergravity level of the first supergravity machine rotation speed is adjusted to 100 under the same other conditions, and after the treatment of the process, the purity of the regenerated triethylene glycol barren solution reaches about 99.999 wt%, and the water dew point of the natural gas reaches below-100 ℃.
Example 3
As described in example 1, the temperature of the triethylene glycol condenser is adjusted to 20 ℃ under the same other conditions, and after the treatment of the process, the purity of the regenerated triethylene glycol barren solution reaches about 99.999 wt%, and the dew point of natural gas water reaches below-107 ℃.
Example 4
As described in example 1, the stripping agent is changed into a mixture of 50% isooctane and 50% n-heptane under the same conditions, and after the treatment of the process, the purity of the regenerated triethylene glycol barren solution reaches about 99.999 wt%, and the water dew point of natural gas reaches below-102 ℃.
Example 5
As described in example 1, the supergravity level of the second supergravity machine is adjusted to 100 under the same other conditions, and after the treatment of the process, the purity of the regenerated triethylene glycol barren solution reaches about 99.998 wt%, and the dew point of natural gas water reaches below-100 ℃.
Comparative example 1
As described in example 1, the supergravity level of the first supergravity machine is adjusted to 20 under the same other conditions, and after the treatment of the process, the purity of the regenerated triethylene glycol barren solution reaches about 99.999 wt%, and the dew point of natural gas water reaches below-88 ℃.
Comparative example 2
As described in example 1, the reboiler temperature was adjusted to 170 ℃ without changing other conditions, and after the treatment by the present process, the purity of the regenerated triethylene glycol barren solution was about 99.991 wt%, and the dew point of natural gas water was below-62 ℃.
Comparative example 3
As described in example 1, the temperature of the triethylene glycol condenser is adjusted to 40 ℃ under the same other conditions, and after the treatment of the process, the purity of the regenerated triethylene glycol barren solution reaches about 99.999 wt%, and the dew point of natural gas water reaches below-96 ℃.
Comparative example 4
As described in example 1, the ratio of the stripping agent amount to the triethylene glycol rich solution amount was adjusted to 0.05: after the treatment by the process, the purity of the regenerated triethylene glycol barren solution reaches about 99.992 wt%, and the water dew point of natural gas reaches below-80 ℃.
Comparative example 5
As described in example 1, the volume ratio of the triethylene glycol lean solution to the natural gas feed gas is 1: 20000, after the treatment by the process, the purity of the regenerated triethylene glycol barren solution reaches about 99.999 wt%, and the dew point of natural gas water reaches below-82 ℃.
Comparative example 6
As described in example 1, other conditions are not changed, a stripping agent pump is closed, the system does not participate in the stripping agent any more, after the treatment of the process, the purity of the regenerated triethylene glycol lean solution reaches about 99.100 wt%, and the dew point of natural gas water reaches below-18 ℃.
It can be seen from the above examples and comparative examples that the system device and process provided by the present invention can significantly improve the purity of the regenerated triethylene glycol lean solution in the regeneration step during the implementation process, and the dehydration depth of the natural gas can be greatly improved by using the triethylene glycol with the purity as the absorption liquid for the dehydration treatment of the natural gas, and the dehydration treatment requirements of the natural gas for liquefaction can be directly met through the optimization of the system and the process.
It should be understood that the above-described embodiments of the present invention are merely examples for clearly illustrating the present invention, and are not intended to limit the embodiments of the present invention. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. Not all embodiments are exhaustive. All obvious changes and modifications which are obvious to the technical scheme of the invention are covered by the protection scope of the invention.
Claims (9)
1. Be applicable to offshore platform natural gas dehydration processing system for liquefaction, its characterized in that: the device comprises a filtering separator (1), a first hypergravity machine (2), a triethylene glycol condenser (3), a lean/rich liquid heat exchanger (4), a booster pump (5), a buffer tank (6), a reboiler (7), a second hypergravity machine (8), a flash tank (9), a delivery pump (10), a first stop valve (11), a second stop valve (12), a third stop valve (17), a stripping agent condenser (13), a three-phase separator (14), a stripping agent dryer (15), a stripping agent storage tank (16), a stripping agent pump (18), a first flowmeter (19), a second flowmeter (20) and a three-way valve (21);
the outlet of the filter separator (1) is connected with the gas phase inlet of a first hypergravity machine (2), the gas phase outlet of the first hypergravity machine (2) is connected with the inlet of a first stop valve (11), and the outlet of the first stop valve (11) is communicated with a downstream working section;
a liquid phase outlet of the first hypergravity machine (2) is connected with a rich liquid inlet of a lean/rich liquid heat exchanger (4), a rich liquid outlet of the lean/rich liquid heat exchanger (4) is connected with an inlet of a flash tank (9), a liquid phase outlet of the flash tank (9) is connected with an inlet of a delivery pump (10), and a gas phase outlet of the flash tank (9) is communicated with tail gas treatment;
the outlet of the delivery pump (10) is connected with the liquid phase inlet of a second hypergravity machine (8), the liquid phase outlet of the second hypergravity machine (8) is connected with the liquid phase inlet of a reboiler (7), the gas phase outlet of the second hypergravity machine (8) is connected with the inlet of a stripping agent condenser (13), the outlet of the stripping agent condenser (13) is connected with the inlet of a three-phase separator (14), and the lower end of the three-phase separator (14) is provided with a water outlet;
a non-condensable gas outlet of the three-phase separator (14) is communicated with tail gas treatment, a stripping agent outlet of the three-phase separator (14) is connected with an inlet of a stripping agent dryer (15), and an outlet of the stripping agent dryer (15) is connected to a first inlet of a three-way valve (21); the stripping agent storage tank (16) and the third stop valve (17) are sequentially connected with a first flow meter (19), and an outlet of the first flow meter (19) is connected to a second inlet of a three-way valve (21); the outlet of the three-way valve (21) is connected with the inlet of a stripping agent pump (18), the outlet of the stripping agent pump (18) is connected with the inlet of a second flowmeter (20), and the outlet of the second flowmeter (20) is connected with a reboiler (7) to realize the circulation of the stripping agent;
reboiler (7) gas phase outlet and the gas phase access connection of second hypergravity machine (8), the liquid phase export of reboiler (7) is through second stop valve (12) and buffer tank (6) access connection, buffer tank (6) bottom liquid phase export and booster pump (5) access connection, the export of booster pump (5) and the barren liquor access connection of poor/rich liquid heat exchanger (4), the barren liquor export and condenser (3) access connection of poor/rich liquid heat exchanger (4), the export of condenser (3) is connected with the liquid phase import of first hypergravity machine (2), realizes the circulation of triethylene glycol.
2. The dehydration process using the system installation for the dehydration treatment of natural gas for offshore platform liquefaction according to claim 1, characterized by comprising the following steps:
1) the natural gas with the pressure of 5-20MPa enters a filtering separator to remove free liquid water and solid impurities, and then is discharged from an outlet of the filtering separator;
2) the natural gas discharged in the step 1) enters a first hypergravity machine, is in countercurrent contact with triethylene glycol barren solution in the first hypergravity machine for dehydration, and a dehydrated dry gas is discharged from a system and enters a downstream working section;
3) discharging the triethylene glycol rich solution after water absorption in the step 2) out of the first hypergravity machine, and allowing the triethylene glycol rich solution to enter a flash tank after heat exchange with triethylene glycol lean solution;
4) the triethylene glycol in the step 3) is flashed by a flash tank and then pumped into a second hypergravity machine by a delivery pump, the triethylene glycol is in countercurrent contact with a stripping agent gasified by a reboiler in the second hypergravity machine, and water in the triethylene glycol is transferred to a gas phase; on one hand, the stripping agent and the water in the triethylene glycol form an azeotrope, so that the water is transferred to a gas phase in the form of the azeotrope, and on the other hand, the gasified stripping agent can enhance the turbulence of the liquid-phase triethylene glycol, reduce the partial pressure of the water in the gas phase and promote the water to be transferred to the gas phase; discharging the regenerated triethylene glycol from a liquid phase outlet of the second hypergravity machine, and discharging a stripping agent from a gas phase outlet of the second hypergravity machine;
5) the stripping agent discharged from the gas phase outlet of the second hypergravity machine in the step 4) enters a stripping agent condenser, and is discharged out of the stripping agent condenser after being condensed into a liquid state;
6) the stripping agent discharged from the stripping agent condenser in the step 5) enters a three-phase separator, water is separated from the stripping agent, the non-condensable gas is led to tail gas treatment, water is discharged out of the system, and the stripping agent enters a stripping agent dryer;
7) drying the stripping agent entering the stripping agent dryer in the step 6) to further remove trace moisture in the stripping agent, and meanwhile, supplementing the stripping agent lost in the recovery process of the stripping agent through a stripping agent storage tank; then, a stripping agent pump is used for conveying the stripping agent into a reboiler, the stripping agent forms an azeotrope with water in the triethylene glycol rich solution discharged from the second hypergravity machine in the step 4) in the reboiler, and the stripping agent is gasified, so that the recycling of the stripping agent is realized; the triethylene glycol is discharged from a liquid phase outlet of the reboiler after being further regenerated;
8) step 7), feeding the triethylene glycol barren solution discharged from the liquid phase outlet of the reboiler into a buffer tank to form a stable liquid level in the buffer tank;
9) and 8) conveying the triethylene glycol lean solution in the buffer tank in the step 8) to a lean/rich solution heat exchanger by a booster pump, exchanging heat with the triethylene glycol rich solution in the step 3) in the lean/rich solution heat exchanger, condensing by a triethylene glycol condenser, and then feeding into the first hypergravity machine again to realize circulation of triethylene glycol.
3. The dehydration process of claim 2, wherein said dehydration process is applied to a system device for dehydration of natural gas for liquefaction on an offshore platform, and comprises the following steps: in the step 2), the volume ratio of the triethylene glycol barren solution to the natural gas feed gas is 1: 5000-1: 10000.
4. the dehydration process of claim 2, wherein said dehydration process is applied to a system device for dehydration of natural gas for liquefaction on an offshore platform, and comprises the following steps: in the step 4), the stripping agent is one or more of isooctane, n-heptane, toluene, ethylbenzene and other substances capable of forming a low-boiling-point azeotrope with water.
5. The dehydration process of claim 2, wherein said dehydration process is applied to a system device for dehydration of natural gas for liquefaction on an offshore platform, and comprises the following steps: in the step 7), the volume ratio of the using amount of the stripping agent to the using amount of the triethylene glycol rich solution in the step 4) is 0.15-0.5.
6. The dehydration process of claim 2, wherein said dehydration process is applied to a system device for dehydration of natural gas for liquefaction on an offshore platform, and comprises the following steps: in step 5), the temperature of the stripping agent condenser is 20 ℃ to 50 ℃.
7. The dehydration process of claim 2, wherein said dehydration process is applied to a system device for dehydration of natural gas for liquefaction on an offshore platform, and comprises the following steps: the supergravity level of the first supergravity machine in the step 2) is 100-500; the supergravity level of the second supergravity machine in the step 2) is 100-500.
8. The dehydration process of claim 2, wherein said dehydration process is applied to a system device for dehydration of natural gas for liquefaction on an offshore platform, and comprises the following steps: in the step 7), the temperature of the reboiler is 190-204 ℃.
9. The dehydration process of claim 2, wherein said dehydration process is applied to a system device for dehydration of natural gas for liquefaction on an offshore platform, and comprises the following steps: in step 9), the temperature of the triethylene glycol condenser is 15 ℃ to 30 ℃.
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| CN111454758B (en) * | 2020-04-10 | 2022-02-11 | 北京石油化工学院 | Efficient compact natural gas glycol dehydration system and method |
| CN112226257A (en) * | 2020-09-03 | 2021-01-15 | 海洋石油工程股份有限公司 | Factory debugging test method for offshore platform triethylene glycol natural gas dehydration and regeneration system |
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| CA2736223A1 (en) * | 2010-04-08 | 2011-10-08 | Joseph A. Witherspoon | Ultra-low emission natural gas dehydration unit with continuously fired reboiler |
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| CN105861089B (en) * | 2016-06-17 | 2019-01-25 | 中石化节能环保工程科技有限公司 | A kind of gas phase concentrate formula triethylene glycol dehydrating regeneration system |
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| CN1326433A (en) * | 1998-09-25 | 2001-12-12 | 通用电气公司 | Process for isolation and removal of unwanted water from chemical reaction |
| CN205035299U (en) * | 2014-06-26 | 2016-02-17 | 乔治·克劳德方法的研究开发空气股份有限公司 | A equipment for being directed at acrylic acid is purifyd |
| CN104194854A (en) * | 2014-09-23 | 2014-12-10 | 北京化工大学 | Hypergravity-process triglycol natural gas dehydration system and process using system |
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