CN210683692U - Slurry bed reaction device for preventing catalyst from settling - Google Patents
Slurry bed reaction device for preventing catalyst from settling Download PDFInfo
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- CN210683692U CN210683692U CN201921863499.3U CN201921863499U CN210683692U CN 210683692 U CN210683692 U CN 210683692U CN 201921863499 U CN201921863499 U CN 201921863499U CN 210683692 U CN210683692 U CN 210683692U
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Abstract
The utility model provides a slurry bed reaction device for preventing catalyst from settling, which comprises a slurry bed reactor, wherein a gas distributor is arranged in the slurry bed reactor; the bottom inlet of the slurry bed reactor is sequentially communicated with a main circulating gas compressor and a synthetic gas air cooler through a synthetic gas pipeline; the synthesis gas air cooler is provided with an auxiliary outlet and is communicated with a synthesis gas inlet of the auxiliary circulating gas compressor inlet liquid separation tank through a pipeline; the top outlet of the auxiliary circulating gas compressor inlet liquid separation tank is communicated with the auxiliary circulating gas compressor, the bottom of the auxiliary circulating gas compressor inlet liquid separation tank is provided with a light sump oil outlet, the middle of the auxiliary circulating gas compressor inlet liquid separation tank is provided with a decarburization tail gas inlet, and the decarburization tail gas inlet is used for receiving decarburization tail gas from a decarburization unit; the auxiliary circulating gas compressor is provided with a decarbonization tail gas outlet and a synthesis gas outlet, and the synthesis gas outlet is communicated with the bottom inlet of the slurry bed reactor.
Description
Technical Field
The utility model belongs to the technical field of the ft synthesis, especially, relate to a prevent slurry bed reaction unit that catalyst subsides.
Background
The development and research of Fischer-Tropsch (F-T) synthesis reactors has progressed significantly over decades, typically with fixed bed reactors, fluidized bed reactors and slurry bed reactors. In recent years, considerable research has been devoted to slurry bed F-T synthesis, a process in which synthesis gas (H2+ CO) is reacted in a bubbling manner up through a liquid phase inert medium containing a finely divided catalyst. Compared with other reactors, the slurry bed reactor mainly has the following advantages: easy control of temperature and pressure, high operation flexibility, high product flexibility, good heat and mass transfer effects, uniform catalyst load, high conversion per pass, and high C content5 +The hydrocarbon selectivity is high, and in addition, the reactor also has the advantages of catalyst cracking resistance, simple structure, investment saving and the like.
As the slurry bed reactor utilizes the process gas-synthesis gas as the power for reaction mixing, once the power of a gas source disappears due to the loss of a main circulation compressor or other leakage reasons, the catalyst can be deposited, the catalyst entering a distributor is difficult to blow out by the gas to cause the blockage of the distributor, the resistance is increased after the blockage of the distributor, the production load cannot be increased, and the safety problems of overpressure operation of a front system and the like can be caused.
SUMMERY OF THE UTILITY MODEL
The utility model provides a prevent thick liquid attitude bed reaction unit that catalyst subsides, the utility model provides a device can in time provide air supply power for the distributor, makes the distributor be in the tympanic bulla state all the time, prevents that the thick liquid from subsiding and pouring to the inside jam distributor of distributor.
The utility model provides a slurry bed reaction device for preventing catalyst from settling, which comprises a slurry bed reactor, wherein a gas distributor is arranged in the slurry bed reactor;
the bottom inlet of the slurry bed reactor is sequentially communicated with a main circulating gas compressor and a synthetic gas air cooler through a synthetic gas pipeline;
the synthesis gas air cooler is provided with an auxiliary outlet and is communicated with a synthesis gas inlet of the auxiliary circulating gas compressor inlet liquid separation tank through a pipeline;
the top outlet of the auxiliary circulating gas compressor inlet liquid separation tank is communicated with the auxiliary circulating gas compressor, the bottom of the auxiliary circulating gas compressor inlet liquid separation tank is provided with a light sump oil outlet, the middle of the auxiliary circulating gas compressor inlet liquid separation tank is provided with a decarburization tail gas inlet, and the decarburization tail gas inlet is used for receiving decarburization tail gas from a decarburization unit;
the auxiliary circulating gas compressor is provided with a decarbonized tail gas outlet and a synthesis gas outlet, and a pipeline of the synthesis gas outlet is merged into an outlet pipeline of the main circulating gas compressor and communicated with a bottom inlet of the slurry bed reactor.
Preferably, a heat exchanger is further arranged on a synthesis gas pipeline between the main circulating gas compressor and the slurry bed reactor.
Preferably, an isolating blind plate is arranged at a synthesis gas outlet of the synthesis gas air cooler.
Preferably, the slurry bed reactor is a bubble column, and a gas-solid separation device is arranged in the slurry bed reactor and used for separating the fine particle catalyst and the liquid product.
The utility model provides a slurry bed reaction device for preventing catalyst from settling, which comprises a slurry bed reactor, wherein a gas distributor is arranged in the slurry bed reactor; the bottom inlet of the slurry bed reactor is sequentially communicated with a main circulating gas compressor and a synthetic gas air cooler through a synthetic gas pipeline; the synthesis gas air cooler is provided with an auxiliary outlet and is communicated with a synthesis gas inlet of the auxiliary circulating gas compressor inlet liquid separation tank through a pipeline; the top outlet of the auxiliary circulating gas compressor inlet liquid separation tank is communicated with the auxiliary circulating gas compressor, the bottom of the auxiliary circulating gas compressor inlet liquid separation tank is provided with a light sump oil outlet, the middle of the auxiliary circulating gas compressor inlet liquid separation tank is provided with a decarburization tail gas inlet, and the decarburization tail gas inlet is used for receiving decarburization tail gas from a decarburization unit; the auxiliary circulating gas compressor is provided with a decarbonization tail gas outlet and a synthesis gas outlet, and the synthesis gas outlet is communicated with the bottom inlet of the slurry bed reactor. The utility model discloses newly allocate the pipeline to auxiliary cycle gas compressor entry branch fluid reservoir in the export of synthetic gas air cooler, utilize auxiliary cycle gas compressor to replace main cycle gas compressor to provide air supply power, for the distributor of slurry bed reactor in time provides air supply power, make the distributor be in the tympanic bulla state all the time, prevent that the catalyst from subsiding and blockking up the distributor.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required to be used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a schematic structural diagram of a device for preventing catalyst settling in a slurry bed reactor according to the present invention;
wherein, 1 is a slurry bed reactor, 2 is a main circulating gas compressor, 3 is a synthesis gas air cooler, 4 is an auxiliary circulating gas compressor, 5 is an auxiliary circulating gas compressor inlet liquid separation tank, 6 is a heat exchanger, 7 is an isolation blind plate, and 8 is a gas distributor.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
The utility model provides a slurry bed reaction device for preventing catalyst from settling, which comprises a slurry bed reactor, wherein a gas distributor is arranged in the slurry bed reactor;
the bottom inlet of the slurry bed reactor is sequentially communicated with a main circulating gas compressor and a synthetic gas air cooler through a synthetic gas pipeline;
the synthesis gas air cooler is provided with an auxiliary outlet and is communicated with a synthesis gas inlet of the auxiliary circulating gas compressor inlet liquid separation tank through a pipeline;
the top outlet of the auxiliary circulating gas compressor inlet liquid separation tank is communicated with the auxiliary circulating gas compressor, the bottom of the auxiliary circulating gas compressor inlet liquid separation tank is provided with a light sump oil outlet, the middle of the auxiliary circulating gas compressor inlet liquid separation tank is provided with a decarburization tail gas inlet, and the decarburization tail gas inlet is used for receiving decarburization tail gas from a decarburization unit;
the auxiliary circulating gas compressor is provided with a decarbonized tail gas outlet and a synthesis gas outlet, and a pipeline of the synthesis gas outlet is merged into an outlet pipeline of the main circulating gas compressor and communicated with a bottom inlet of the slurry bed reactor.
In the present invention, the slurry bed reactor is a reactor in which gas is bubbled through a liquid (slurry) layer in which solid fine particles are suspended to realize a gas-liquid-solid phase reaction process. The liquid phase in the slurry reactor may be the reactants or the carrier liquid for the suspended solid catalyst. In the present invention, the slurry bed reactor is a bubble in the slurry bed reactor for Fischer-Tropsch synthesis, the catalyst of the present invention is a solid phase, and the reactant is a gas phase, which contains a liquid phase medium.
The utility model provides a slurry bed reactor's bottom is provided with gas distributor for the evenly distributed feed gas makes the bubble little and even, strengthens the gas-liquid mass transfer, but can not cause big pressure drop yet. The utility model discloses do not have special restriction to the concrete structure of gas distributor, adopt the commonly used gas distributor of technical staff in the field can.
The slurry bed reactor of the utility model is internally provided with a gas-solid separation device for separating fine particle catalyst and liquid product, and the particle diameter of the catalyst is preferably 50-200 μm; the catalyst is preferably an iron-based catalyst. The utility model discloses do not have special restriction to gas-solid separator's concrete structure, adopt in the ft synthesis gas-solid separator commonly used can.
The utility model discloses in, the bottom exit linkage of slurry bed reactor has the synthetic gas pipeline, main circulating gas compressor and synthetic gas air cooler have set gradually on the synthetic gas pipeline, and the synthetic gas is followed synthetic gas air cooler's entry gets into, gets into slurry bed reactor's bottom after main circulating gas compressor compression heaies up, carries out ft synthesis.
Preferably, a heat exchanger is further arranged between the main circulating gas compressor and the slurry bed reactor, and in the heat exchanger, the circulating gas after being compressed and heated exchanges heat with the synthesis gas discharged from the reactor, so that the temperature of the synthesis gas is further increased.
The utility model discloses in, the synthesis gas air cooler still is provided with supplementary export, supplementary export is linked together with supplementary circulation gas compression system, supplementary circulation gas compression system includes supplementary circulation gas compressor and supplementary circulation gas compressor entry branch fluid reservoir.
The auxiliary circulating gas compressor inlet liquid separation tank is provided with a decarbonization tail gas inlet and a synthesis gas inlet, the bottom of the auxiliary circulating gas compressor inlet liquid separation tank is provided with a light sump oil outlet, and the top outlet of the auxiliary circulating gas compressor inlet liquid separation tank is communicated with the inlet of the auxiliary circulating gas compressor. And an auxiliary outlet of the synthesis gas air cooler is communicated with a synthesis gas inlet of the auxiliary circulating gas compressor inlet liquid separation tank.
And the outlet of the auxiliary circulating gas compressor is connected into the outlet pipeline of the main circulating gas compressor through a pipeline and is communicated with the bottom inlet of the slurry bed reactor.
The utility model discloses in, still be provided with decarbonization tail gas outlet on auxiliary cycle gas compressor's the outlet pipeline, work as the utility model provides a main cycle gas compressor normal operating, auxiliary cycle gas compressor is used for compressing decarbonization tail gas.
The utility model also provides a method for preventing catalyst subsides in the slurry bed reactor, adopt the device for preventing catalyst subsides in the slurry bed reactor of the aforesaid, when main circulating compressor power disappears, cut off the decarbonization tail gas of auxiliary circulating gas compressor entry branch fluid reservoir, make the synthetic gas enter auxiliary circulating gas compressor entry branch fluid reservoir through the supplementary export of synthetic gas air cooler, utilize auxiliary circulating gas compressor to provide air supply power;
the temperature of the synthesis gas at the inlet of the auxiliary circulation compressor is 35 ℃, the pressure of the synthesis gas at the inlet of the auxiliary circulation compressor is 2.88MPa, and the temperature of the synthesis gas at the outlet of the auxiliary circulation compressor is 68 ℃ and the pressure of the synthesis gas at the outlet of the auxiliary circulation compressor is 3.35 MPa.
In the utility model, when the main circulating gas compressor normally operates, the synthesis gas enters the main circulating gas compressor after being cooled by the synthesis gas air cooler, enters the heat exchanger for heat exchange after being compressed and heated, enters from the bottom inlet of the slurry bed reactor, and performs Fischer-Tropsch synthesis reaction through the gas distributor;
at the moment, the auxiliary circulating gas compressor is used for compressing decarbonized tail gas, and the decarbonized tail gas is synthetic tail gas generated by Fischer-Tropsch synthesis reaction, and CO in the synthetic tail gas is removed through a decarbonization unit2And returning gas, wherein the decarbonized tail gas enters an inlet liquid separating tank of the auxiliary circulating gas compressor, after gas-liquid separation, light oil stain is discharged from a bottom outlet and enters a light oil stain tank, the decarbonized tail gas enters the auxiliary circulating gas compressor from a tank top outlet to be compressed, the compressed decarbonized tail gas is divided into two paths, one path of the tail gas goes to the synthesis reactor, the other path of the tail gas goes to the reverse blowing and washing system, and finally the tail gas enters the synthesis reactor.
When the main circulation gas compressor fails and cannot supply power for the synthesis gas, the isolation baffle at the outlet of the synthesis gas air cooler is closed, the corresponding valve is closed, synthesis gas is output from the auxiliary outlet of the auxiliary synthesis gas air cooler and enters the inlet liquid separation tank from the synthesis gas inlet of the inlet liquid separation tank of the auxiliary circulation gas compressor, after gas-liquid separation is carried out in the liquid separation tank, the synthesis gas is output from the outlet at the top of the liquid separation tank and enters the auxiliary circulation gas compressor, the auxiliary circulation gas compressor supplies power for the synthesis gas, and after the synthesis gas is compressed and heated in the auxiliary circulation gas compressor, the synthesis gas enters the bottom inlet of the slurry bed reactor through heat exchange of the heat exchanger and then is subjected to Fischer-Tropsch synthesis reaction through the gas distributor.
In the utility model, when the main circulation air compressor operates normally and supplies power for the synthesis gas,
the pressure of the synthesis gas at the inlet of the main circulating gas compressor is 2.88MPa, and the temperature is 35 ℃; after being compressed by a main circulating gas compressor, the pressure is increased to 3.35MPa, the temperature is increased to 68 ℃, and after heat exchange by a heat exchanger, the pressure of the synthesis gas is 3.2MPa, and the temperature is 205 ℃;
at the moment, the pressure of the decarbonized tail gas at the inlet of the auxiliary circulating gas compressor is 2.75MPa, and the temperature is 40 ℃; after being compressed by an auxiliary circulating gas compressor, the pressure is increased to 3.35MPa and 68 ℃.
In the utility model, when the main circulation gas compressor fails and cannot provide power for the synthesis gas, the decarbonization tail gas is cut off, the auxiliary circulation gas compressor provides power for the synthesis gas,
the temperature of the synthesis gas at the inlet of the auxiliary circulation compressor is 35 ℃, the pressure of the synthesis gas at the outlet of the auxiliary circulation compressor is 2.88MPa, the temperature of the synthesis gas at the outlet of the auxiliary circulation compressor is 68 ℃, the pressure of the synthesis gas is 3.35MPa, and the pressure of the synthesis gas is 3.2MPa and the temperature of the synthesis gas is 205 ℃ after heat exchange is carried out by the heat exchanger.
In the utility model, the catalyst used in the Fischer-Tropsch synthesis is an iron catalyst; the reaction temperature of the Fischer-Tropsch synthesis is preferably 260-280 ℃; the time of the Fischer-Tropsch synthesis reaction is preferably adjusted at any time according to the activity of the catalyst.
The utility model discloses preferentially with the feed gas that comes from purification unit and the synthetic gas that heats up to 205 ℃ through the heat exchanger after mixing, get into the gas distributor of slurry bed reactor bottom, the total sulfur content of feed gas < 0.05ppm, pressure is 3.2MPa, and the temperature is 220 ℃.
In the method, a new pipeline is arranged at the outlet of the synthesis gas air cooler to the liquid separation tank at the inlet of the auxiliary circulating gas compressor, when the main circulating gas compressor has a problem and the power of the gas source disappears, the decarburization tail gas is cut off, the synthesis gas enters an inlet liquid separation tank of an auxiliary circulation gas compressor through an outlet pipeline newly arranged on a synthesis gas air cooler, the gas phase is pumped into a distributor at the bottom of the reactor after being compressed by the auxiliary circulation gas compressor, the auxiliary circulation gas compressor is used for replacing a main circulation gas compressor to provide air source power to prevent slurry from settling and pouring into the distributor to block the distributor, once the air source power disappears due to the main circulation gas compressor or other leakage reasons, the auxiliary circulating gas compressor timely provides a gas source with the same power pressure and temperature as the original gas source, the distributor is guaranteed to have sufficient gas source power bubbling, a circulating loop is formed, and liquid separated by the liquid separating tank is sent to a sump oil system.
Compared with the prior art, the utility model has the advantages of it is following:
(1) the utility model provides a method can in time provide air supply power for the distributor, makes the distributor be in the tympanic bulla state all the time, prevents that the thick liquid from subsiding and leads to the inside jam of distributor.
(2) The utility model provides a method can prolong the maintenance cycle is changed to the slurry bed reactor distributor, increases distributor life, reduces enterprise economic consumption.
Examples
Under normal conditions, the main circulation compressor and the auxiliary circulation compressor both run normally, synthesis gas (2.88MPa and 35 ℃) at the inlet of the main circulation compressor is compressed and pressurized to 3.35MPa and 68 ℃ by the main circulation gas compressor, decarbonization gas at the inlet of the auxiliary circulation compressor is 2.75MPa and 40 ℃, and the pressure is pressurized to 3.35MPa and 68 ℃ after the compression by the auxiliary circulation compressor. The synthesis gas compressed by the main circulating gas compressor is heated to 205 ℃ through a heat exchanger, and the pressure is 3.2 MPa. Raw gas with 3.2MPa, 220 ℃ and total sulfur content less than 0.05ppm from the purification unit is mixed with circulating synthesis gas with 3.2MPa and 205 ℃ and then enters a distributor at the bottom of the reactor. The synthesis gas entering a slurry bed reactor (R-6101) passes through a slurry bed layer containing a catalyst in a bubbling mode to carry out F-T synthesis reaction;
when the main circulating gas compressor fails, an isolation blind plate and related valves at the outlet of the air cooler are closed, so that the synthesis gas is output from an auxiliary outlet of the synthesis gas air cooler, the synthesis gas (2.88MPa and 45 ℃) at the inlet of the auxiliary circulating gas compressor is compressed and boosted to 3.3MPa and 65 ℃ by the auxiliary circulating gas compressor, the temperature is raised to 205 ℃ by a heat exchanger, and the pressure is 3.2 MPa. Raw gas with 3.2MPa, 220 ℃ and total sulfur content less than 0.05ppm from the purification unit is mixed with circulating synthesis gas with 3.2MPa and 205 ℃ and then enters a distributor at the bottom of the reactor. The synthesis gas entering the slurry bed reactor (R-6101) is bubbled through the slurry bed layer containing the catalyst to carry out the F-T synthesis reaction.
It can be seen from the above embodiment that, having used the utility model provides a behind the method, can guarantee that gas distributor has sufficient air supply power all the time, be in the tympanic bulla state, effectively prevented the inside jam of distributor that the catalyst subsides and lead to.
Claims (4)
1. A slurry bed reaction device for preventing catalyst from settling comprises a slurry bed reactor, wherein a gas distributor is arranged in the slurry bed reactor;
the bottom inlet of the slurry bed reactor is sequentially communicated with a main circulating gas compressor and a synthetic gas air cooler through a synthetic gas pipeline;
the synthesis gas air cooler is provided with an auxiliary outlet and is communicated with a synthesis gas inlet of the auxiliary circulating gas compressor inlet liquid separation tank through a pipeline;
the top outlet of the auxiliary circulating gas compressor inlet liquid separation tank is communicated with the auxiliary circulating gas compressor, the bottom of the auxiliary circulating gas compressor inlet liquid separation tank is provided with a light sump oil outlet, the middle of the auxiliary circulating gas compressor inlet liquid separation tank is provided with a decarburization tail gas inlet, and the decarburization tail gas inlet is used for receiving decarburization tail gas from a decarburization unit;
the auxiliary circulating gas compressor is provided with a decarbonized tail gas outlet and a synthesis gas outlet, and a pipeline of the synthesis gas outlet is merged into an outlet pipeline of the main circulating gas compressor and communicated with a bottom inlet of the slurry bed reactor.
2. The slurry bed reactor according to claim 1, wherein a heat exchanger is further provided on the synthesis gas line between the main circulation gas compressor and the slurry bed reactor.
3. The slurry bed reactor according to claim 1, wherein an isolation blind plate is provided at a syngas outlet of the syngas air cooler.
4. The slurry bed reactor according to claim 1, wherein the slurry bed reactor is a bubble column, and a gas-solid separation device is arranged in the slurry bed reactor and used for separating the fine particle catalyst and the liquid product.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112745880A (en) * | 2019-10-31 | 2021-05-04 | 内蒙古伊泰煤制油有限责任公司 | Method for preventing catalyst in slurry bed reactor from settling and slurry bed reactor |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112745880A (en) * | 2019-10-31 | 2021-05-04 | 内蒙古伊泰煤制油有限责任公司 | Method for preventing catalyst in slurry bed reactor from settling and slurry bed reactor |
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