CN215667861U - Light oil recovery device of hot potash decarburization system - Google Patents
Light oil recovery device of hot potash decarburization system Download PDFInfo
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- CN215667861U CN215667861U CN202121724734.6U CN202121724734U CN215667861U CN 215667861 U CN215667861 U CN 215667861U CN 202121724734 U CN202121724734 U CN 202121724734U CN 215667861 U CN215667861 U CN 215667861U
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Abstract
The utility model belongs to a treatment device of a hot potash decarburization system, and relates to a light oil recovery device of the hot potash decarburization system. The device comprises a purification gas separator, wherein the purification gas separator is connected with a three-phase separator, the three-phase separator is provided with three outlets which are respectively connected with a fuel gas tank, an oil tank and a flash tank, and the flash tank is connected with a hot potash decarburization device. Through design three-phase separator before hot potash decarburization device, not only get rid of the hydrocarbon material in the synthetic tail gas, avoid influencing the decarbonization process, can also avoid the light oil component to the influence of burning furnace, can also manage simultaneously and give vent to anger, oil, water phase, are used for different purposes respectively, increase the utilization ratio. A flash evaporation tank is arranged between the three-phase separator and the hot potash decarburization system, so that impurities can be further removed.
Description
Technical Field
The utility model belongs to a treatment device of a hot potash decarburization system, and relates to a light oil recovery device of the hot potash decarburization system.
Background
The information in this background section is only for enhancement of understanding of the general background of the utility model and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art that is already known to a person of ordinary skill in the art.
The Fischer-Tropsch synthesis process mainly comprises coal gasification, gas purification, transformation and reforming, synthesis, product refining and modification and the like, and is one of the most important ways for high-efficiency conversion and utilization of non-petroleum carbon-containing resources (natural gas, coal, residual oil, biomass and the like). The Fischer-Tropsch synthesis product is mainly straight-chain paraffin of C1-C200, and the initial product is further treated to obtain oil fuel of gasoline, diesel oil and other fuels with certain specifications and chemicals of ethylene, propylene, lubricating oil, paraffin wax and other chemicals.
The decarbonization process is a matching technology of the Fischer-Tropsch synthesis process and has the function of separating part of CO in the Fischer-Tropsch synthesis tail gas2Removing the catalyst from the circulating gas to ensure that the Fischer-Tropsch reaction reaches the designed conversion efficiency, and the conversion per pass (CO + H) of the general industrial iron-based catalyst slurry bed Fischer-Tropsch reactor2) 30% -35% of CO in synthetic tail gas2The content is 10 to 15 percent, and CO2The selectivity is between 2 and 4 percent. In order to increase the total conversion rate of the synthesis gas, a large amount of synthesis tail gas needs to be circulated and is firstly sent to a decarbonization device to remove CO2To below 2 percent, and then circularly returning to the Fischer-Tropsch synthesis reactor for ensuringEvidence of Tower gas CO2The content is about 0.5 percent, and the total conversion rate can reach 90 to 95 percent.
However, the inventor researches that a large amount of hydrocarbon substances contained in Fischer-Tropsch synthesis tail gas enter a decarburization solution to cause solution foaming and rise of tower pressure difference, and the absorption tower is flooded in severe cases to influence the stable operation of the device, so that the oil content of a solution system is reduced, and the phenomenon that a large amount of hydrocarbon substances enter a heat accumulating type incinerator to be oxidized after an oil phase in the decarburization solution is subjected to flash evaporation is avoided, and a large amount of oil gas resources are wasted. In addition, the high oil content of the decarbonization solution can destroy the performance of the potassium carbonate solution, so that the decarbonization efficiency is reduced, the material consumption is high, and the conversion efficiency of the Fischer-Tropsch synthesis is influenced.
SUMMERY OF THE UTILITY MODEL
In order to solve the problem that in a hot potash decarburization system, a gas has more hydrocarbon components, which affects the hot potash decarburization process and avoids the influence of light oil components on an incinerator, the utility model provides a light oil recovery device of the hot potash decarburization system.
Specifically, the utility model is realized by the following technical scheme:
the utility model provides a hot potash decarbonization system light oil recovery unit, includes and purifies gas separator, purify gas separator and three-phase separator and be connected, three-phase separator is equipped with three export, connects fuel gas pitcher, oil tank, flash drum respectively, fuel gas pitcher is connected with hot potash decarbonization device.
One or more of the technical schemes have the following beneficial effects:
1) the direct hot potash decarburization system that passes through of synthesis tail gas with traditional technology, especially, synthesis tail gas contains a large amount of hydrocarbon composition, take place easily in hot potash decarburization system and lead to the solution foaming, influence the device steady operation, consequently, add the three-phase separator between gas purification separator and hot potash decarburization system, divide into water, oil, gas three-phase with synthesis tail gas, can not only solve the influence of hydrocarbon composition to hot potash decarburization system, improve the decarbonization effect, but also can utilize composition aqueous phase and gaseous phase in branch processing, and the high-usage rate.
2) It has also been found in experimental studies that if the gas separated in the three-phase separator is fed directly to the Fischer-Tropsch reactor, CO is present2Thus connecting the fuel gas tank with a hot potash decarbonation system.
3) If direct aqueous phase with the three phase separator separation and obtain discharges, cause the energy waste easily, consequently in some schemes, let in the flash drum with the aqueous phase, produce secondary steam and liquid phase through cooling, depressurization, the secondary steam that the flash distillation came out sends into corresponding preheating device and preheats.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to provide a further understanding of the utility model, and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the utility model and together with the description serve to explain the utility model and not to limit the utility model.
FIG. 1 is a light oil recovery apparatus of a hot potash decarburization system according to example 1 of the present invention;
FIG. 2 is a light oil recovery apparatus of the hot potash decarburization system according to embodiment 2 of the present invention;
FIG. 3 is a light oil recovery apparatus of the hot potash decarburization system according to comparative example 1 of the present invention;
wherein: 1. the device comprises a first purification gas separator, a three-phase separator, a fuel gas tank, a flash gas outlet, a regeneration tower, a first valve, a second valve, a third valve, a fourth valve, a second purification gas separator, a third valve, a fourth valve, a second purification gas separator, a third valve, a fifth valve and a fourth valve, wherein the first purification gas separator is 2, the three-phase separator is 3, the fuel gas tank is 4, the oil tank is 5, the flash tank is 6, the flash gas outlet is 7, the regeneration tower is 8, the first valve is 9, the second valve is 10, the third valve is 11, the fourth valve is 12, and the second purification gas separator is 13.
Detailed Description
It is to be understood that the following detailed description is exemplary and is intended to provide further explanation of the utility model as claimed. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the utility model. As used herein, the singular is intended to include the plural unless the context clearly dictates otherwise, and it should be understood that when the term "comprising" is used in the present invention, it indicates the presence of the features, steps, operations, devices, components and/or combinations thereof.
It is to be understood that the terms "upper", "lower", "horizontal", "top", "bottom", and the like are used in an orientation or positional relationship indicated on the drawings for convenience in describing the present invention and for simplicity in description, and do not indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and are not to be construed as limiting the present invention.
The inventor researches and discovers that the content of organic hydrocarbons in Fischer-Tropsch synthesis tail gas is high, the hot potash chemical absorption method can be used for reducing the dissolution loss of the hydrocarbons, but the decarburization device is in the operation process, because the Fischer-Tropsch synthesis tail gas contains a large amount of hydrocarbon substances, the solution can be foamed when entering the decarburization solution, the tower pressure difference is caused to rise, the absorption tower can be caused to flood when the decarburization device is serious, the stable operation of the device is influenced, in addition, the content of light oil components in the solution system is overhigh, the heat value of regenerated gas of a heat accumulating type incinerator can be caused to be overhigh to a certain extent, and the incinerator is unstable in operation.
In order to solve the problem that in a hot potash decarburization system, a gas has more hydrocarbon components, which affects the hot potash decarburization process and avoids the influence of light oil components on an incinerator, the utility model provides a light oil recovery device of the hot potash decarburization system.
Specifically, the utility model is realized by the following technical scheme:
the utility model provides a hot potash decarbonization system light oil recovery unit, includes and purifies gas separator, purification gas separator is connected with the three-phase separator, and the three-phase separator is equipped with three export, connects fuel gas pitcher, oil tank, flash drum respectively, the flash drum is connected with hot potash decarbonization device.
The direct hot potash decarburization system that passes through of synthetic tail gas with traditional technology, especially synthetic tail gas contains a large amount of hydrocarbon composition, take place easily in hot potash decarburization system and lead to the solution foaming, influence the device steady operation, consequently, add the three-phase separator between gas purification separator and hot potash decarburization system, divide synthetic tail gas into water, oil, gas three-phase, can not only solve the influence of hydrocarbon composition to hot potash decarburization system, improve the decarbonization effect, can also divide the composition aqueous phase and the gaseous phase that can recycle, the high-usage.
It has also been found in experimental studies that if the gas separated in the three-phase separator is fed directly to the Fischer-Tropsch reactor, CO is present2Thus connecting the fuel gas line to a hot potash decarburization system.
Flashing is a process where the pressure reduction results in a vapor-liquid separation phenomenon that is a change from one thermodynamic equilibrium state to the next. The flash tank is that the water phase with higher pressure and temperature enters a low-pressure container, so that the moisture in the sodium aluminate solution is separated out in the form of steam due to the reduction of pressure, and in practice, the production is limited to the volume of the pressure container and the flash capability, so that secondary steam in the water phase is separated sufficiently to provide heat required by the production through multi-stage flash evaporation.
The conventional treatment all is the aqueous phase that directly obtains the triphase separator separation and discharges, causes the energy waste easily, consequently in some schemes, lets in the aqueous phase in the flash drum, produces secondary steam and liquid phase through cooling, depressurization, and the secondary steam that the flash evaporation came out sends into corresponding preheating device and preheats.
In order to ensure the transportation performance, the pressure of the separated gas phase is not less than 1.0 MPa.
In some embodiments, the flash drum is provided with a flash gas outlet at the top, and the flash drum is connected with the regeneration tower.
The flash evaporation gas outlet can collect high-temperature steam to recover heat, so that energy is saved, and the liquid phase separated by the flash evaporation tank can be used for other reactions.
In one or more embodiments, valves are arranged between the purification gas separator and the three-phase separator, between the three-phase separator and the fuel gas tank, between the three-phase separator and the oil tank, and between the three-phase separator and the flash tank. The valves are added to better control each device, or when a certain device is overhauled, the valves can be separated from the devices in the previous process and the next process.
In order to improve the safety of the use of the shut-off valve, in some embodiments, the inlet end and the outlet end of the valve are respectively provided with a shut-off valve.
In some hot potash decarburization systems or fischer-tropsch synthesis devices, the number of the gas purification and separation devices is only one, because when setting up the three-phase separator, when the gas stripping excessively enters the hot potash decarburization systems, the absorption tower is easily flooded, the stable operation of the device is affected, in addition, the content of light oil components in the solution system is too high, the heat accumulating type incinerator regeneration gas heat value is also caused to be too high to a certain extent, and the incinerator is unstable in operation. Even if a three-phase separator is used, the obtained water phase is not large in quantity, enough secondary steam cannot be generated after the treatment of the flash drum, and further the heat energy of the secondary steam cannot be utilized to boost other reactions. However, in some embodiments of the present invention, since the three-phase separator is provided to separate oil, water, and gas, and a plurality of purge gas separators are used and connected to the three-phase separator, the above-mentioned problems may not occur.
In some embodiments, two purge gas separators I, II are provided.
According to some embodiments of the utility model, through analyzing and researching components in the condensate of the purification gas separator I, II of the hot potash decarburization device, the condensate is enriched with a large amount of oil substances (the components of the condensate are similar to those of a low-carbon hydrocarbon liquid product), a hydrocarbon separation and recovery system is additionally arranged, an oil-water separator is additionally arranged, the condensate of the enriched large amount of oil substances is subjected to three-phase separation, the operation condition of the oil-water separation system is improved, oil-water separation of the condensate of the purification gas separator I, II of the decarburization device is realized, hydrocarbons are recovered as crude products, and the condensate is returned to the system for reuse, so that the cyclic utilization rate of the condensate is further improved, the desalted water consumption of the system is reduced, and the yield of oil is improved.
According to some embodiments of the utility model, by arranging the three-phase separator or the oil-water separator, the material consumption of the decarburization device is further reduced, the operation flexibility of the decarburization device is increased, the operation conditions of the oil-water separation system are improved, the system problems of high energy consumption, poor water balance, high potassium carbonate consumption and the like of the decarburization device are solved, the purposes of energy conservation and emission reduction, support saving and consumption reduction are achieved, and the operation quality of the decarburization device is greatly improved.
Some embodiments of the utility model have at least the following advantages: (1) the consumption of the desalted water of the system is obviously reduced, and the desalted water is consumed by 1254m per day from the prior average3The desalted water is reduced to 350m consumed per day3Desalted water, namely the consumption of desalted water of a system is reduced by about 37.64m3The desalted water is saved by about 301.1km per year if the desalted water is produced according to 8000h per year3(ii) a (2) The average recovered light oil yield is about 33.71 tons after the decarbonization oil-water separation process flow is optimized, and if the production is calculated according to 8000 hours per year, the yield can be improved by about 1.12 ten thousand tons per year.
According to some embodiments of the utility model, technical experience is provided for the optimized operation of the original design process of the large-scale coal-to-liquids Fischer-Tropsch synthesis tail gas decarbonization device, the operation conditions of the hot potash decarbonization system are improved, and valuable experience which can be used for borrowing is provided for production improvement, energy conservation and consumption reduction of enterprises.
In order to realize energy source reuse, in one or more embodiments, a flash gas outlet on the flash drum is connected with an endothermic reaction device.
In some embodiments, the fuel gas tank is provided with a pressure gauge, so that the gas pressure can be monitored in real time conveniently, the phenomenon that the gas enters a hot potash decarburization system when the pressure is too high, large impact is caused on a solution, violent reaction is caused, and the safety is improved.
In one or more embodiments, the oil tank is connected to a lower hydrocarbon recovery oil line for recovery and reuse.
The hydrocarbon or oil separated in the three-phase separator is flammable and hazardous, and therefore in one or more embodiments the tank is provided with a level control valve at a location that is 80% of the overall height.
In some embodiments, the flash tank is provided with a liquid level regulating valve at a position with a height of 30% of the overall height, and the liquid level is controlled to be lower than 30% of the overall height, so that more steam can be flashed off to provide heat energy for other reactions.
The condensate containing a large amount of oil substances and obtained by separating the purification gas separator of the hot potash decarburization device is subjected to three-phase separation, so that oil-water separation and recycling of the condensate of the purification gas separator of the decarburization device are realized, the cyclic utilization rate of the condensate is further improved, the desalted water consumption of a system is reduced, the oil product yield is improved, and the production cost is reduced.
The present invention is described in further detail below with reference to specific examples, which are intended to be illustrative of the utility model and not limiting.
Example 1
As shown in fig. 1, the light oil recovery device for a hot potash decarburization system provided by this embodiment includes a gas-purifying separator 1, the gas-purifying separator 1 is connected with a three-phase separator 2, the three-phase separator 2 is provided with three outlets, which are respectively connected with a fuel gas tank 3, an oil tank 4 and a flash evaporation tank 5, the fuel gas tank 3 is connected with the hot potash decarburization device, the top of the flash evaporation tank 5 is provided with a flash evaporation gas outlet 6, and the flash evaporation tank 5 is connected with a regeneration tower 7.
A first valve 8 is arranged between the purification gas separator 1 and the three-phase separator 2, a second valve 9 is arranged between the three-phase separator 2 and the fuel gas tank 3, a third valve 10 is arranged between the three-phase separator 2 and the oil tank 4, and a fourth valve 11 is arranged between the three-phase separator 2 and the flash tank 5.
Example 2
As shown in fig. 2, the light oil recovery apparatus for a hot potash decarburization system provided in this embodiment is different from embodiment 1 in that the number of the purge gas separators is 2, and the purge gas separators are respectively connected to the three-phase separator 2, a fifth valve 13 is provided between the purge gas separator 12 and the three-phase separator 2, the first valve 8 controls the purge gas separator 1, and the fifth valve 13 controls the purge gas separator 2, so that the mixed exhaust gas of the purge gas separator 1 and the purge gas separator 2 can be separately introduced into the three-phase separator 2. The inlet ends and the outlet ends of the first valve 8, the second valve 9, the third valve 10, the fourth valve 11 and the fifth valve 13 are respectively provided with a stop valve.
Comparative example 1
As shown in fig. 3, the light oil recovery device of the hot potash decarburization system provided in this embodiment is different from that of embodiment 1 in that a three-phase separator is not designed, the clean gas separator 1 is directly connected to the flash tank 5, the fuel gas tank 3 is connected to the hot potash decarburization device, a flash gas outlet 6 is provided at the top of the flash tank 5, the flash tank 5 is connected to the regeneration tower 7, and the flash gas outlet 6 is connected to the hot potash decarburization device. A first valve 8 is arranged between the connection of the purification gas separator 1 and the flash tank 5, and cut-off valves are arranged in front of and behind the first valve 8.
In terms of production process, the tail gas is directly led into the flash tank in the comparative example 1, which is not beneficial to the separation of the gas stripping of the hydrocarbon and influences the subsequent decarburization effect. Moreover, the pressure drop is very dangerous for the gas mixture (water, oil, gas phase).
The above disclosure is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the scope of the present invention, therefore, the present invention is not limited by the appended claims.
Claims (10)
1. The light oil recovery device of the hot potash decarburization system is characterized by comprising a purification gas separator, wherein the purification gas separator is connected with a three-phase separator, the three-phase separator is provided with three outlets which are respectively connected with a fuel gas tank, an oil tank and a flash tank, and the flash tank is connected with the hot potash decarburization device.
2. The light oil recovery device of the hot potash decarburization system as recited in claim 1, wherein a flash evaporation gas outlet is provided at the top of the flash evaporation tank, and the flash evaporation tank is connected with the regeneration tower.
3. The light oil recovery apparatus for a hot potash decarburization system as claimed in claim 1, wherein valves are provided between the clean gas separator and the three-phase separator, between the three-phase separator and the fuel gas tank, between the three-phase separator and the oil tank, and between the three-phase separator and the flash drum.
4. The light oil recovery apparatus for a hot potash decarburization system as recited in claim 3, wherein cut-off valves are provided at the inlet and outlet ends of the valve, respectively.
5. The light oil recovery device of the hot potash decarburization system as recited in claim 1, wherein the number of the purge gas separators is plural, and the plural purge gas separators are connected to the three-phase separator.
6. The light oil recovery device of the hot potash decarburization system as recited in claim 2, wherein the flash gas outlet of the flash drum is connected to the hot potash decarburization device.
7. The light oil recovery device of the hot potash decarburization system as recited in claim 1, wherein the fuel gas tank is connected to a fuel gas pipe network.
8. The light oil recovery apparatus of a hot potash decarburization system as recited in claim 1, wherein the oil tank is connected to a lower hydrocarbon recovery oil line.
9. The light oil recovery apparatus for a hot potash decarburization system as recited in claim 1, wherein the oil tank is provided with a level control valve at a position at 80% of the overall height.
10. The light oil recovery apparatus for a hot potash decarburization system as recited in claim 1, wherein the flash drum is provided with a liquid level regulating valve at a position 30% of the height of the overall height.
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