CN111821785A - Method for removing catalyst particles carried by Fischer-Tropsch synthesis tail gas and system and application used by method - Google Patents
Method for removing catalyst particles carried by Fischer-Tropsch synthesis tail gas and system and application used by method Download PDFInfo
- Publication number
- CN111821785A CN111821785A CN201910310528.1A CN201910310528A CN111821785A CN 111821785 A CN111821785 A CN 111821785A CN 201910310528 A CN201910310528 A CN 201910310528A CN 111821785 A CN111821785 A CN 111821785A
- Authority
- CN
- China
- Prior art keywords
- liquid
- washing
- tail gas
- gas
- catalyst
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
- B01D47/06—Spray cleaning
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a method for removing a catalyst carried by Fischer-Tropsch synthesis tail gas, and a system and application thereof. The method comprises the following steps: contacting the synthesis gas with a catalyst to carry out Fischer-Tropsch synthesis reaction to generate tail gas carrying catalyst particles and heavy oil wax; contacting the tail gas with a washing solution for washing to obtain a washing waste liquid containing the catalyst particles carried in the tail gas and clean tail gas; wherein the kinematic viscosity of the wash liquor is greater than 6mm2And s. The method can effectively and efficiently remove the catalyst in the tail gas of the Fischer-Tropsch synthesis slurry bed reactor, obviously reduce the problem of blockage of a subsequent gas-liquid separation device of the Fischer-Tropsch synthesis reactor, and reduce the content of the catalyst in the tail gas treated by the washing tower to 1-10 ppm; the method has the advantages of simple process, no need of changing the original reaction equipment, no influence of the original production schedule and yield setting, good applicability and application in all Fischer-Tropsch synthesis slurry bed reaction processes.
Description
Technical Field
The invention relates to the field of Fischer-Tropsch synthesis, in particular to a method for removing catalyst particles carried in Fischer-Tropsch synthesis tail gas and a system used by the method.
Background
With the rising of the price of petroleum in recent years, people pay more and more attention to the development of a technology for producing alternative oil products, synthesis gas is produced by coal, natural gas or other substances, the synthesis gas is treated by water gas shift and synthesis gas purification processes according to the requirement of a Fischer-Tropsch synthesis catalyst on the synthesis gas, hydrocarbons are produced by Fischer-Tropsch synthesis by taking the treated synthesis gas as a raw material, meanwhile, oxygen-containing compounds are byproduct, and then the oil products are processed by adopting a mature petroleum processing technology to produce high-quality environment-friendly oil products. The development of the Fischer-Tropsch synthesis technology has very important significance for developing the production technology for replacing oil products.
The Fischer-Tropsch synthesis reactor is a core reactor of a Fischer-Tropsch synthesis technology, and a three-phase slurry bed reactor capable of producing more hydrocarbon products is widely adopted at home and abroad at present. The slurry bed reactor has the advantages of uniform and easily-controlled temperature, wide gas velocity operation range, high alpha value of the product, on-line replacement of the catalyst and the like.
In the Fischer-Tropsch synthesis reactor, the synthesis gas is converted into Fischer-Tropsch synthesis products such as wax and the like under the action of a catalyst. The wax remains in the reactor and mixes with the catalyst in a slurry state, and unreacted feed gas and gas phase products leave the reactor as tail gas. Due to the large amount of tail gas, a small amount of fine catalyst particles and fines can be entrained. Catalyst fine particles and powder can be deposited at the turning positions of the heat exchanger, the separator and the gas phase pipeline, the pressure drop of the heat exchanger is increased due to long-term accumulation, the separator is difficult to separate, the pipeline resistance is increased, the raw materials of the oil product hydrogenation device are unqualified, and the device can be stopped when the device is serious.
CN101723774A provides a method for removing an iron catalyst carried in slurry bed fischer-tropsch synthesis tail gas, that is, in a slurry bed fischer-tropsch synthesis reactor, unreacted raw gas and part of catalyst fine powder carried by a gas phase (fischer-tropsch synthesis tail gas) generated by a reaction enter a settling section of the fischer-tropsch synthesis reactor, and the catalyst fine powder carried by the fischer-tropsch synthesis tail gas is converged on a reactor wall and returns to a slurry phase through the reactor wall under the action of a horizontal magnetic field in the settling section, so as to further remove the catalyst carried by the tail gas.
The Fischer-Tropsch synthesis slurry bed reactor requires that the particle size of the catalyst is between 20 and 100 microns, otherwise the catalyst and a product cannot form a slurry phase, but the catalyst is more and more worn, the average diameter of the particles is smaller and smaller, the viscosity of the mixture of the catalyst and oil wax is larger and larger, and the separation effect of the catalyst particles is poorer and poorer. And the fine catalyst particles carried by the high-flow-rate tail gas can be deposited at the turning positions of the heat exchanger, the separator and the gas phase pipeline, the pressure drop of the heat exchanger is increased due to long-term accumulation, the separation of the separator is difficult, the pipeline resistance is increased, the raw materials of the oil product hydrogenation device are unqualified, and the device can be stopped when the device is serious.
Therefore, the tail gas of the fischer-tropsch synthesis reactor needs to be subjected to high-efficiency gas-solid separation, and further needs to be subjected to high-efficiency removal of fine particle catalysts carried in the tail gas.
Disclosure of Invention
The invention aims to solve the problem that the catalyst in the tail gas of a Fischer-Tropsch synthesis slurry bed reactor cannot be effectively removed in the prior art, and provides a method for removing catalyst particles in the Fischer-Tropsch synthesis tail gas.
In order to achieve the above object, the first aspect of the present invention provides a method for removing catalyst particles carried in fischer-tropsch synthesis tail gas, comprising: contacting the synthesis gas with a catalyst to carry out Fischer-Tropsch synthesis reaction to generate tail gas carrying catalyst particles and heavy oil wax; contacting the tail gas with a washing solution for washing to obtain a washing waste liquid containing the catalyst particles carried in the tail gas and clean tail gas; wherein the kinematic viscosity of the washing liquid is more than 6mm2/s。
Preferably, the scrubbing liquid is contacted with the off-gas in a countercurrent direction.
Preferably, the temperature of the tail gas is 150-350 ℃, and the gas flow rate is 1-10 m/s; more preferably, the temperature of the tail gas is 220-300 ℃, and the gas flow rate is 2-6 m/s.
Preferably, the kinematic viscosity of the washing liquid is 10-50mm2/s。
Preferably, the washing liquid is an oil or wax that is liquid at a temperature in the range of 150 ℃ to 250 ℃.
Preferably, the off-gas passes through the scrubbing liquid and is in countercurrent contact with the scrubbing liquid.
Preferably, the spraying speed of the washing liquid is 5-60 m/s; the washing temperature is 120-250 ℃, and the washing pressure is 2-3.8 MPa; more preferably, the spraying rate of the washing liquid is 10-50m/s, the washing temperature is 150-230 ℃, and the washing pressure is 2.5-3.5 MPa.
Preferably, the liquid-gas ratio of the washing liquid to the tail gas is at least 0.1L/m3(ii) a More preferably, the liquid-gas ratio of the washing liquid to the tail gas is 0.5-5L/m3。
Preferably, the method further comprises a process of returning the washing waste liquid to the washing, or a process of returning a part of the obtained stabilizing liquid to the washing after stabilizing the washing waste liquid.
Preferably, the temperature of the stabilizing liquid is greater than 100 ℃; more preferably, the temperature of the stabilizing solution is from 150 ℃ to 250 ℃.
Preferably, the process further comprises returning at least a portion of the heavy oil wax as wash liquid.
The second aspect of the present invention provides a system for removing catalyst particles carried in fischer-tropsch synthesis tail gas, wherein the system comprises: the reactor 1 and at least one washing tower 2, the tail gas outlet 12 at the top of the reactor 1 is communicated with the gas phase inlet 21 of the washing tower, the washing tower is also provided with a washing liquid inlet 23 and a liquid phase outlet 24 and a liquid level meter 25, and the washing liquid is used in the washing tower to remove the catalyst in the tail gas.
Preferably, a gas distributor 14 is arranged in the washing tower 2; preferably, the gas distributor 14 opens downwardly.
Preferably, the reactor 1 further comprises a heavy oil wax outlet 13, the heavy oil wax outlet 13 being in communication with the scrubbing liquid inlet 23 of the scrubbing tower.
Preferably, the system further comprises a stabilization tank 3, and the washing liquid inlet 23 and the liquid phase outlet 24 of the washing tower are respectively communicated with the stabilization tank 3; more preferably, heat preservation and/or heating means are provided in the stabilization tank 3.
Preferably, the heavy oil wax outlet 13 of the reactor 1 is in communication with the stabilizer tank 3.
In a third aspect, the invention provides the use of a method according to the first aspect of the invention and a system according to the second aspect of the invention in the field of fischer-tropsch synthesis.
The method can effectively and efficiently remove the catalyst in the tail gas of the Fischer-Tropsch synthesis slurry bed reactor, obviously reduce the problem of blockage of a subsequent gas-liquid separation device of the Fischer-Tropsch synthesis reactor, and reduce the content of the catalyst in the tail gas treated by the washing tower to 1-10 ppm; the method has the advantages of simple process, no need of changing the original reaction equipment, no influence of the original production schedule and yield setting, good applicability and application in all Fischer-Tropsch synthesis slurry bed reaction processes.
Drawings
FIG. 1 is a schematic view of a first embodiment of the present invention;
FIG. 2 is a schematic view of a second embodiment of the present invention;
FIG. 3 is a schematic view of a third embodiment of the present invention;
fig. 4 is a schematic view of a fourth embodiment of the present invention.
Description of the reference numerals
1. A slurry bed reactor; 2. a washing tower; 3. a stabilization tank; 4. a circulation pump; 5. a transfer pump; 6. a gas-liquid-solid separation device; 7. a liquid-solid separation filter; 8. a pipeline; 9. a heat exchanger; 10. a gas-liquid separation device; 11. a wax polishing filtration system; 12. a tail gas outlet of the slurry bed reactor; 13. a heavy oil outlet of the slurry bed reactor; 14. a gas distributor; 21. a gas phase inlet of the scrubber; 23. a wash liquid inlet; 24. a liquid phase outlet of the scrubber; 25. liquid level meter
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
The invention provides a method for removing catalyst particles carried by Fischer-Tropsch synthesis tail gas, which comprises the following steps: contacting the synthesis gas with a catalyst to carry out Fischer-Tropsch synthesis reaction to generate tail gas carrying catalyst particles and heavy oil wax; contacting the tail gas with a washing solution for washing to obtain a washing waste liquid containing the catalyst particles carried in the tail gas and clean tail gas; wherein the kinematic viscosity of the washing liquid is more than 6mm2/s。
In the invention, the reaction process of the Fischer-Tropsch synthesis carried out in the reactor is as follows: the synthesis gas (carbon monoxide and hydrogen) enters from the inlet end at the bottom of the reactor, passes through the gas distributor and then enters the reactor. The reactor was previously charged with liquid wax (solvent) and catalyst. And after the gas-liquid-solid three phases are subjected to Fischer-Tropsch synthesis reaction in the reactor, a hydrocarbon product is generated. Wherein, the heavy products (heavy oil wax) are discharged after being filtered by a liquid-solid separation filter distributed in the reactor, and the tail gas is discharged after being separated by a gas-liquid-solid separation device at the top of the reactor.
In the present invention, the reactor is preferably a slurry bed reactor.
In the present invention, the catalyst packed in the reactor may be selected according to the prior art, for example, the catalyst comprises a carrier and an active metal supported on the carrier, or a precipitated phase catalyst, and the active metal may be, for example, Fe, Cu, K, Mo, Si, Ni, etc.
The particle size of the catalyst can be selected according to the prior art as long as the reaction proceeds efficiently, for example, a particle size of 20 to 100 μm and an average particle size of 50 to 90 μm. Herein, the particle size is the diameter of a spherical particle, or the "equivalent particle size" of a non-spherical particle. "equivalent particle size" refers to the diameter of a particle as measured when the physical property or behavior of the particle is closest to that of a homogeneous sphere of a certain diameter.
According to the prior art, the catalyst provided in the reactor requires a particle size of the catalyst of 20 to 100 μm, otherwise the catalyst and the product cannot form a slurry phase. However, as the reaction proceeds, the catalyst is worn more and more, the average particle diameter is smaller and smaller, and the catalyst smaller than 20 μm is increased gradually, while the gas-solid separation device at the top of the slurry bed reactor has a poor separation effect on the catalyst smaller than 20 μm, so that the concentration of the catalyst carrying fine particles by the exhaust gas is larger and larger.
In the present invention, the Fischer-Tropsch synthesis conditions in the reactor can be selected according to the prior art, for example, the temperature is 220 ℃ and 300 ℃, and the pressure is 2.5-3.5 MPa.
According to the invention, the scrubbing liquid is brought into counter-current contact with the exhaust gas during the scrubbing process.
More preferably, the temperature of the tail gas is 150-350 ℃, and the gas flow rate is 1-10 m/s; further preferably, the temperature of the tail gas is 220-300 ℃, and the gas flow rate is 2-6 m/s.
In the invention, the tail gas is discharged from the reactor and enters the washing tower.
In the present invention, the heavy oil wax contains a hydrocarbon having 30 or more carbon atoms as a main component.
According to the invention, the kinematic viscosity of the washing liquid is between 10 and 50mm2/s。
According to the invention, the washing liquid is oil or wax which is liquid in the temperature range of 150-250 ℃. The wash liquor may be selected from one or more of, for example, heavy diesel, liquid wax and fischer-tropsch wax.
In the present invention, the kinematic viscosity is a ratio of kinetic viscosity to density measured at 40 ℃.
According to the invention, the exhaust gas passes through the scrubbing liquid and is in countercurrent contact with the scrubbing liquid.
In the invention, the washing liquid which is defined by the invention and has specific kinematic viscosity and 5% of distillation temperature of more than 150 ℃ is used for removing the catalyst in the tail gas more advantageously.
In the present invention, the Fischer-Tropsch wax is a waxy product produced by Fischer-Tropsch synthesis reaction, such as heavy oil wax.
According to the invention, preferably, the washing liquid is a heavy oil wax obtained in the fischer-tropsch synthesis of the present application.
According to the invention, the spraying rate of the washing liquid is 5-60 m/s; the washing temperature is 120-250 ℃, and the washing pressure is 2-3.8 MPa; more preferably, the spraying rate of the washing liquid is 10-50m/s, the washing temperature is 150-230 ℃, and the washing pressure is 2.5-3.5 MPa.
In the invention, after the washing liquid enters the washing tower in a spraying mode, liquid drops with the particle size of 1-5mm are formed in the washing tower, and preferably, the washing liquid forms liquid drops with the particle size of 1.5-3mm in the washing tower. According to the invention, when the washing liquid has the particle size, the washing liquid can have the highest removal efficiency on the catalyst in the tail gas, and the content of the catalyst particles carried in the removed tail gas is lower.
When the diameter of the liquid drops of the washing agent is too large, the washing agent cannot be fully contacted with the tail gas, the utilization rate of the washing agent is low, and the removal treatment is incomplete, so that the catalyst content in the tail gas finally discharged from the washing tower is high; when the diameter of the detergent liquid drop is too small, the removal of the catalyst in the tail gas is facilitated, but the reduction of the diameter of the detergent liquid drop requires more energy consumption, and the control of the process cost is not facilitated.
According to the invention, the liquid-gas ratio of the scrubbing liquid to the offgas is at least 0.1L/m3(ii) a Preferably, the liquid-gas ratio of the washing liquid to the tail gas is 0.5-5L/m3。
In the invention, the liquid-gas ratio of the washing liquid to the tail gas influences the contact time of the washing liquid and the tail gas, thereby influencing the removal treatment of the catalyst. The inventor finds that when the washing liquid and the tail gas have the liquid-gas ratio, the washing liquid and the tail gas can be in sufficient contact time, and the catalyst removal efficiency is ensured. When the liquid-gas ratio of the scrubbing liquid to the tail gas is too low, the content of the scrubbing agent contacting the tail gas per unit volume is reduced, so that the removal treatment is incomplete, and the catalyst content in the tail gas finally discharged from the scrubbing tower is high.
According to the invention, the method also comprises a process of returning the washing waste liquid to the washing, or a process of returning part of the washing waste liquid to the washing after being stabilized.
According to the invention, the stable temperature is greater than 100 ℃; preferably from 150 ℃ to 250 ℃.
In the invention, when the stable temperature meets the range, the stable liquid can be kept in a flowable liquid state all the time, which is beneficial to the removal of the subsequent catalyst.
In the invention, in the stabilizing process, the catalyst carried in the liquid slowly settles under the action of gravity, so that the liquid is gradually layered, the upper layer is the liquid carrying no catalyst or less catalyst, and the lower layer is the settled catalyst.
According to the invention, preferably, at least part of the upper layer of liquid is introduced into a washing column for washing the off-gas.
In the present invention, it is preferable that the catalyst settled in the lower layer is discharged out of the stabilization tank.
In the present invention, in order to ensure the stable flow rate of the transfer pump 5 after the stabilization tank, it is preferable to make the liquid level height of the stabilization tank lower than 2/3 and higher than 1/4.
According to the present invention, preferably, the process further comprises returning at least a portion of the heavy oil wax as wash liquid.
More preferably, the above-mentioned heavy oil wax carrying catalyst particles is subjected to a stabilization treatment. In the stabilizing process, under the action of gravity, the heavy oil wax carrying the catalyst fine powder is gradually layered, the upper layer is the heavy oil wax carrying no catalyst or less catalyst, and the lower layer is the settled catalyst.
Preferably, the at least part of the upper layer of heavy oil wax carrying no or less catalyst is returned to the washing process, while the other part of the upper layer of heavy oil wax carrying no or less catalyst is subjected to wax polishing treatment.
In the invention, preferably, the clean tail gas is subjected to heat exchange and separation treatment.
The second aspect of the invention provides a system for removing catalyst particles carried in Fischer-Tropsch synthesis tail gas, which comprises a reactor 1 and at least one washing tower 2, wherein a tail gas outlet 12 at the top of the reactor 1 is communicated with a gas phase inlet 21 of the washing tower, the washing tower is also provided with a washing liquid inlet 23, a liquid phase outlet 24 and a liquid level meter 25, and the washing liquid is used for removing the catalyst in the tail gas in the washing tower.
In the invention, the system also comprises a circulating pump 4 which is connected with the liquid level meter 25 and is used for stabilizing the liquid level of the washing tower.
In the invention, the reactor 1 is provided with a reactor inlet section, a gas distributor component, a reaction section (comprising a catalyst), a liquid-solid separation filter 7 and a gas-liquid-solid separation device 6 at the top of the reactor.
According to the invention, a gas distributor 14 is arranged in the scrubber 2; preferably, the gas distributor 14 opens downwardly.
According to the invention, the reactor 1 further comprises a heavy oil wax outlet 13, the heavy oil wax outlet 13 being in communication with the scrubbing liquid inlet 23 of the scrubbing tower.
According to the invention, the system also comprises a stabilization tank 3, the washing liquid inlet 23 and the liquid phase outlet 24 of the washing tower being respectively in communication with the stabilization tank 3; preferably, the stabilization tank is provided with a heat preservation and/or heating device to ensure that the temperature in the stabilization tank is greater than 100 ℃; more preferably from 150 c to 250 c, so that the liquid in the stabilization tank remains in a flowable liquid state at all times.
According to the invention, the heavy oil wax outlet 13 of the reactor 1 communicates with the stabilizer tank 3 to introduce at least a portion of the heavy oil wax into the stabilizer tank 3.
In the invention, the system also comprises a wax fine filtering system 11, wherein the wax fine filtering system 11 is communicated with the stabilizing tank 3 and is used for introducing at least part of heavy oil wax on the upper layer of the stabilizing tank 3 into the wax fine filtering system 11 for refining treatment.
According to the invention, the system also comprises at least one transfer pump 5 for liquid transfer, which communicates with the stabilization tank 3 and/or the wax polishing filter 11 and the washing column 2.
In the present invention, the "communication" is achieved by means of a pipeline 8, which preferably requires insulation and heat tracing.
In the present invention, a liquid level meter 25 is provided in the stabilization tank 3, which can be interlocked with the control of the transfer pump 5, wherein the transfer pump 5 is automatically turned on when the liquid level is higher than 2/3, and the transfer pump 5 is automatically turned off when the liquid level is lower than 1/4, so as to keep the liquid level in the stabilization tank and the flow rate in the pipeline 8 stable.
In the present invention, the system further comprises at least one heat exchanger 9 and at least one gas-liquid separation device 10. Preferably, the clean tail gas enters the heat exchanger 9 and the gas-liquid separation device 10 for heat exchange and separation.
In a third aspect, the invention provides the use of a method according to the first aspect of the invention and a system according to the second aspect of the invention in the field of fischer-tropsch synthesis.
One embodiment of the method of the present invention is described in conjunction with FIG. 1. The process for removing catalyst particles from fischer-tropsch synthesis tail gas according to the invention is carried out in a system as shown in figure 1.
The synthesis gas comprising carbon monoxide and hydrogen enters the reactor 1 at the bottom inlet end thereof, passes through a gas distributor (not shown), and then enters the reactor. The reactor is also provided with a reaction section (not shown in the figure), a liquid-solid separation filter 7 and a gas-liquid-solid separation device 6 at the top of the reactor. The reactor was pre-charged with liquid wax and catalyst. The synthesis gas is subjected to Fischer-Tropsch synthesis reaction under the action of a catalyst to produce hydrocarbon products. Wherein, the reaction conditions of the Fischer-Tropsch synthesis comprise: the reaction temperature is 220 ℃ and 300 ℃, and the pressure is 2.5-3.5 MPa.
Heavy products (heavy oil wax) in the hydrocarbon products are filtered by the liquid-solid separation filter 7 and discharged from the reactor 1 through the heavy oil outlet 13, and tail gas generated by the synthesis reaction is separated by the gas-liquid-solid separation device 6 and discharged from the reactor 1 through the tail gas outlet 12.
The off-gas discharged from the off-gas outlet 12 of the reactor 1 enters the scrubber 2 through the gas phase inlet 21 of the scrubber 2 and enters below the liquid level of the scrubber through the gas distributor 14. Washing liquid enters the washing tower from a washing liquid inlet 23 of the washing tower 2, and tail gas is in reverse contact with the washing liquid to carry out catalyst removal treatment. The spent scrubber liquor carrying the catalyst particles after the stripping is discharged from the scrubber tower via the liquid phase outlet 24 of the scrubber tower 2. Wherein, a liquid level meter 25 is further arranged in the washing tower 2 for keeping the liquid level in the washing tower stable. The temperature of the tail gas entering the washing tower is 150-350 ℃, and the gas flow rate is 1-10 m/s; preferably, the temperature of the tail gas is 220-300 ℃, and the gas flow rate is 2-6 m/s.
Wherein the washing liquid is oil or wax which is liquid in the temperature range of 150-250 ℃; more preferably, the washing liquid has a kinematic viscosity of more than 6mm2Oil wax per second; further preferably, the washing liquid has a kinematic viscosity of 10-50mm2Oil wax per second. Preferably, the washing liquid enters the washing tower in a spraying mode; more preferably, the spraying rate of the washing liquid is 5 to 60 m/s; the washing temperature is 120-250 ℃, and the washing pressure is 2-3.8 MPa; even more preferably, the spraying rate of the washing liquid is 10 to 50 m/s; the washing temperature is 150 ℃ and 230 ℃, and the washing pressure is 2.5-3.5 MPa. Wherein the particle diameter of the liquid drop of the washing liquid is 1-5mm, preferably, the particle diameter of the liquid drop of the washing liquid is 1.5-3 mm; washing liquor and tailThe liquid-to-gas ratio of gas is at least 0.1L/m3(ii) a Preferably, the liquid-gas ratio of the washing liquid to the tail gas is 0.5-5L/m3。
A second embodiment of the present invention will be described with reference to fig. 2. The process for removing catalyst particles from the tail gas from Fischer-Tropsch synthesis of the invention is carried out in the apparatus shown in FIG. 2.
The synthesis gas comprising carbon monoxide and hydrogen enters the reactor 1 at the bottom inlet end thereof, passes through a gas distributor (not shown), and then enters the reactor. The reactor is also provided with a reaction section (not shown in the figure), a liquid-solid separation filter 7 and a gas-liquid-solid separation device 6 at the top of the reactor. The reactor was pre-charged with liquid wax and catalyst. The synthesis gas is subjected to Fischer-Tropsch synthesis reaction under the action of a catalyst to produce hydrocarbon products. Wherein, the reaction conditions of the Fischer-Tropsch synthesis comprise: the reaction temperature is 220 ℃ and 300 ℃, and the pressure is 2.5-3.5 MPa. Wherein the particle diameter of the liquid drop of the washing liquid is 1-5mm, preferably, the particle diameter of the liquid drop of the washing liquid is 1.5-3 mm; the liquid-gas ratio of the washing liquid to the tail gas is at least 0.1L/m3(ii) a Preferably, the liquid-gas ratio of the washing liquid to the tail gas is 0.5-5L/m3。
Heavy products (heavy oil wax) in the hydrocarbon products are filtered by the liquid-solid separation filter 7 and discharged from the reactor 1 through the heavy oil outlet 13, and tail gas generated by the synthesis reaction is separated by the gas-liquid-solid separation device 6 and discharged from the reactor 1 through the tail gas outlet 12.
The off-gas discharged from the off-gas outlet 12 of the reactor 1 enters the scrubber 2 through the gas phase inlet 21 of the scrubber 2 and enters below the liquid level of the scrubber through the gas distributor 14. Wherein, in the washing tower, the temperature of the tail gas is 150-350 ℃, and the gas flow rate is 1-10 m/s; preferably, the temperature of the tail gas is 220-300 ℃, and the gas flow rate is 2-6 m/s.
The heavy oil wax discharged from the heavy oil outlet 13 of the reactor 1 is introduced into the washing tower 2 through the pipeline 8, and enters the washing tower from the washing liquid inlet 23 of the washing tower 2 to be used as the washing liquid for the catalyst removal treatment, and the tail gas and the washing liquid reversely contact to carry out the catalyst removal treatment. The spent scrubber liquor carrying the catalyst particles after the stripping is discharged from the scrubber tower via the liquid phase outlet 24 of the scrubber tower 2. Wherein, a liquid level meter 25 is further arranged in the washing tower 2 for keeping the liquid level in the washing tower stable.
The cleaned tail gas is transferred to a heat exchanger 9 and a gas-liquid separation device 10 in sequence for heat exchange and separation treatment.
Wherein the washing liquid is oil or wax which is liquid in the temperature range of 150-250 ℃; more preferably, the washing liquid has a kinematic viscosity of more than 6mm2Oil wax per second; further preferably, the washing liquid has a kinematic viscosity of 10-50mm2Oil wax per second. Preferably, the washing liquid enters the washing tower in a spraying mode; more preferably, the spraying rate of the washing liquid is 5 to 60 m/s; the washing temperature is 120-250 ℃, and the washing pressure is 2-3.8 MPa; more preferably, the spraying rate of the washing liquid is 10-50m/s, the washing temperature is 150-230 ℃, and the washing pressure is 2.5-3.5 MPa. Wherein the particle diameter of the liquid drop of the washing liquid is 1-5mm, preferably, the particle diameter of the liquid drop of the washing liquid is 1.5-3 mm; the liquid-gas ratio of the washing liquid to the tail gas is at least 0.1L/m3(ii) a Preferably, the liquid-gas ratio of the washing liquid to the tail gas is 0.5-5L/m3。
A third embodiment of the present invention is described with reference to fig. 3. The process for removing catalyst particles from the tail gas from Fischer-Tropsch synthesis of the invention is carried out in the apparatus shown in FIG. 3.
The synthesis gas comprising carbon monoxide and hydrogen enters the reactor 1 at the bottom inlet end thereof, passes through a gas distributor (not shown), and then enters the reactor. The reactor is also provided with a reaction section (not shown in the figure), a liquid-solid separation filter 7 and a gas-liquid-solid separation device 6 at the top of the reactor. The slurry bed reactor is pre-loaded with liquid wax and catalyst. The synthesis gas is subjected to Fischer-Tropsch synthesis reaction under the action of a catalyst to produce hydrocarbon products. Wherein, the reaction conditions of the Fischer-Tropsch synthesis comprise: the reaction temperature is 220 ℃ and 300 ℃, and the pressure is 2.5-3.5 MPa.
Heavy products (heavy oil wax) in the hydrocarbon products are filtered by the liquid-solid separation filter 7 and discharged from the reactor 1 through the heavy oil outlet 13, and tail gas generated by the synthesis reaction is separated by the gas-liquid-solid separation device 6 and discharged from the reactor 1 through the tail gas outlet 12.
The off-gas discharged from the off-gas outlet 12 of the reactor 1 enters the scrubber 2 through the gas phase inlet 21 of the scrubber 2 and enters below the liquid level of the scrubber through the gas distributor 14. The washing liquid enters the washing tower from a washing liquid inlet 23 of the washing tower 2 in a spraying mode, and the tail gas and the washing liquid reversely contact to carry out catalyst removal treatment. The spent scrubber liquor carrying the catalyst particles after the stripping is discharged from the scrubber tower via the liquid phase outlet 24 of the scrubber tower 2. Wherein, a liquid level meter 25 is further arranged in the washing tower 2 for keeping the liquid level in the washing tower stable. In the washing tower, the temperature of the tail gas is 150-350 ℃, and the gas flow rate is 1-10 m/s; preferably, the temperature of the tail gas is 220-300 ℃, and the gas flow rate is 2-6 m/s.
The washing liquid is oil or wax which is in a liquid state within the temperature range of 150-250 ℃; more preferably, the washing liquid has a kinematic viscosity of more than 6mm2Oil wax per second; further preferably, the washing liquid has a kinematic viscosity of 10-50mm2Oil wax per second. Preferably, the washing liquid enters the washing tower in a spraying mode; more preferably, the spraying rate of the washing liquid is 5 to 60 m/s; the washing temperature is 120-250 ℃, and the washing pressure is 2-3.8 MPa; more preferably, the spraying rate of the washing liquid is 10-50m/s, the washing temperature is 150-230 ℃, and the washing pressure is 2.5-3.5 MPa. Wherein the particle diameter of the liquid drop of the washing liquid is 1-5mm, preferably, the particle diameter of the liquid drop of the washing liquid is 1.5-3 mm; the liquid-gas ratio of the washing liquid to the tail gas is at least 0.1L/m3(ii) a Preferably, the liquid-gas ratio of the washing liquid to the tail gas is 0.5-5L/m3。
The system further comprises a stabilization tank 3, and a washing liquid inlet 23 and a liquid phase outlet 24 of the washing tower are respectively communicated with the stabilization tank 3. The washing waste liquid discharged from the liquid phase outlet 24 of the washing tower 2 is transferred to the washing tower 2 for washing the tail gas through the circulating pump 4, or transferred to the stabilizing tank 3 through the circulating pump 4, and in the stabilizing tank 3, the washing waste liquid is settled and layered, the upper layer is liquid without catalyst or with less catalyst, and the lower layer is catalyst. Wherein, be provided with level gauge 25 in the stabilizer, it is mutually supported with transfer pump 5, and when the liquid level was higher than 2/3, transfer pump 5 was automatic to be opened, and when the liquid level was less than 1/4, transfer pump 5 self-closing kept the liquid level in the stabilization tank and the stability of the interior flow of pipeline 8.
The liquid which does not carry catalyst or carries less catalyst in the upper layer is transferred into the washing tower 2 through the transfer pump 5 and the pipeline 8 and enters the washing tower from the washing liquid inlet 23 of the washing tower 2 in a spraying mode for washing the tail gas. The catalyst in the lower layer is discharged from the stabilization tank.
The cleaned tail gas is transferred to a heat exchanger 9 and a gas-liquid separation device 10 in sequence for heat exchange and separation treatment.
A fourth embodiment of the present invention will be described with reference to fig. 4. The process for removing catalyst particles from the tail gas from Fischer-Tropsch synthesis of the invention is carried out in the apparatus shown in FIG. 4.
The synthesis gas comprising carbon monoxide and hydrogen enters the reactor 1 at the bottom inlet end thereof, passes through a gas distributor (not shown), and then enters the reactor. The reactor is also provided with a reaction section (not shown in the figure), a liquid-solid separation filter 7 and a gas-liquid-solid separation device 6 at the top of the reactor. The reactor was pre-charged with liquid wax and catalyst. The synthesis gas is subjected to Fischer-Tropsch synthesis reaction under the action of a catalyst to produce hydrocarbon products. Wherein, the reaction conditions of the Fischer-Tropsch synthesis comprise: the reaction temperature is 220 ℃ and 300 ℃, and the pressure is 2.5-3.5 MPa.
Heavy products (heavy oil wax) in the hydrocarbon products are filtered by the liquid-solid separation filter 7 and discharged from the reactor 1 through the heavy oil outlet 13, and tail gas generated by the synthesis reaction is separated by the gas-liquid-solid separation device 6 and discharged from the reactor 1 through the tail gas outlet 12.
The off-gas discharged from the off-gas outlet 12 of the reactor 1 enters the scrubber 2 through the gas phase inlet 21 of the scrubber 2 and enters below the liquid level of the scrubber through the gas distributor 14. In the washing tower, the temperature of the tail gas is 150-350 ℃, and the gas flow rate is 1-10 m/s; preferably, the temperature of the tail gas is 220-300 ℃, and the gas flow rate is 2-6 m/s.
The heavy oil wax discharged from the heavy oil outlet 13 of the reactor 1 is introduced into the washing tower 2 through the pipeline 8, and enters the washing tower from the washing liquid inlet 23 of the washing tower 2 to be used as the washing liquid for the catalyst removal treatment, and the tail gas and the washing liquid reversely contact to carry out the catalyst removal treatment. The spent scrubber liquor carrying the catalyst particles after the stripping is discharged from the scrubber tower via the liquid phase outlet 24 of the scrubber tower 2. Wherein, a liquid level meter 25 is further arranged in the washing tower 2 for keeping the liquid level in the washing tower stable.
The washing liquid is oil or wax which is in a liquid state within the temperature range of 150-250 ℃; more preferably, the washing liquid has a kinematic viscosity of more than 6mm2Oil wax per second; further preferably, the washing liquid has a kinematic viscosity of 10-50mm2Oil wax per second. Preferably, the washing liquid enters the washing tower in a spraying mode; more preferably, the spraying rate of the washing liquid is 5 to 60 m/s; the washing temperature is 120-250 ℃, and the washing pressure is 2-3.8 MPa; more preferably, the spraying rate of the washing liquid is 10-50m/s, the washing temperature is 150-230 ℃, and the washing pressure is 2.5-3.5 MPa. Wherein the particle diameter of the liquid drop of the washing liquid is 1-5mm, preferably, the particle diameter of the liquid drop of the washing liquid is 1.5-3 mm; the liquid-gas ratio of the washing liquid to the tail gas is at least 0.1L/m3(ii) a Preferably, the liquid-gas ratio of the washing liquid to the tail gas is 0.5-5L/m3。
The system further comprises a stabilization tank 3, and a washing liquid inlet 23 and a liquid phase outlet 24 of the washing tower are respectively communicated with the stabilization tank 3. The heavy oil wax carrying catalyst particles discharged from the liquid phase outlet 24 of the washing tower 2 is returned to the washing tower 2 through the circulating pump 4 for washing the tail gas, or is transferred to the stabilization tank 3 through the circulating pump 4, in the stabilization tank 3, the heavy oil wax carrying catalyst particles is settled and layered, the upper layer is the heavy oil wax carrying no catalyst or less catalyst, and the lower layer is the catalyst. Wherein, be provided with level gauge 25 in the stabilizer 3, it is mutually supported with transmission pump 5, and when the liquid level was higher than 2/3, the pump was automatic to be opened, and when the liquid level was less than 1/4, the pump self-closing kept the stability of the interior liquid level of stability jar and flow in the pipeline 8.
One part of the heavy oil wax which does not carry catalyst or carries less catalyst at the upper layer is transferred into the washing tower 2 through the transfer pump 5 and the pipeline 8, and enters the washing tower from a washing liquid inlet 23 of the washing tower 2 in a spraying mode for washing tail gas, and the other part of the heavy oil wax enters the wax fine filtering system 11 for further treatment. The catalyst in the lower layer is discharged from the stabilization tank.
The cleaned tail gas is transferred to a heat exchanger 9 and a gas-liquid separation device 10 in sequence for heat exchange and separation treatment.
The present invention will be described in detail below by way of examples. In the following examples, the content parameter of the catalyst was measured by a roasting method, and the specific test method was: weighing a certain amount of slurry sample, and roasting in a muffle furnace at 600 ℃ for 4 h. Weighing the rest solid catalyst sample again after roasting, and calculating the mass percentage of the solid catalyst;
the kinematic viscosity of the washing liquid is measured by a full-automatic kinematic viscosity measuring instrument according to GB/T265.
Example 1
As shown in fig. 1, the synthesis gas reacts in the fischer-tropsch synthesis reactor 1, the produced heavy oil wax (heavy product) is filtered by the liquid-solid separation filter 7 and then discharged from the heavy oil outlet 13, and the reaction tail gas is separated in the gas-liquid-solid separation device 6 at the top of the reactor, and then leaves the reactor through the tail gas outlet 12 and enters the scrubber 2. The catalyst content in the tail gas is 50 ppm.
The off-gas enters the scrubber 2 via the gas phase inlet 21 of the scrubber 2 and enters below the liquid level of the scrubber through the gas distributor 14 opening downwards, the temperature of the off-gas being 270 ℃ and the gas phase flow rate being 2 m/s. Kinematic viscosity of 10mm2The scrubbing liquid heavy diesel oil/s enters the scrubbing tower from a scrubbing liquid inlet 23 of the scrubbing tower 2 in a spraying mode and reversely contacts with the tail gas, the spraying speed of the scrubbing liquid is 15m/s, and the temperature in the scrubbing tower is 250 ℃. The particle diameter of the liquid drop of the washing liquid is 1.5mm, and the liquid-gas ratio of the washing liquid to the tail gas is 0.1L/m3。
According to detection, when the Fischer-Tropsch synthesis reaction is carried out for 300 hours, the content of the catalyst in the clean tail gas washed by the washing tower is detected to be 4 ppm; when the Fischer-Tropsch synthesis reaction is carried out for 600 hours, the content of the catalyst in the clean tail gas washed by the washing tower is detected to be 6ppm, and the requirements (10ppm) of the heat exchanger and a subsequent gas-liquid separation device on the raw material gas are completely met.
Example 2
As shown in fig. 3, the synthesis gas reacts in the fischer-tropsch synthesis reactor 1, and the produced heavy oil wax (heavy product) is filtered by the liquid-solid separation filter 7, discharged from the heavy oil outlet 13, and enters the stabilization tank 3; reaction tail gas is separated by a gas-liquid-solid separation device 6 at the top of the reactor, leaves the reactor through a tail gas outlet 12 and enters a washing tower 2. The catalyst content in the tail gas is 60 ppm.
The off-gas enters the scrubber 2 via the gas phase inlet 21 of the scrubber 2 and enters the scrubber through the gas distributor 14 which is open downwards, the temperature of the off-gas being 250 ℃ and the gas phase flow rate being 10 m/s. The heavy oil wax in the stabilization tank 3 is led to a washing tower 2 as washing liquid for washing tail gas, wherein the kinematic viscosity of the heavy oil wax is 20mm2And s. The heavy oil wax enters the washing tower in a spraying mode through a washing liquid inlet 23 of the washing tower 2 and is in reverse contact with the tail gas. The spraying rate of the washing liquid was 18m/s, and the temperature in the washing column was 230 ℃. The cleaned tail gas enters a heat exchanger 9 and a subsequent gas-liquid separation device 10 for further treatment. The particle diameter of the liquid drop of the washing liquid is 3mm, and the liquid-gas ratio of the washing liquid to the tail gas is 0.5L/m3。
The washing waste liquid carrying the catalyst fine powder generated in the washing is discharged from the liquid phase outlet 24 of the washing tower 2 and transferred to the stabilization tank 3 via the circulation pump 4. In the stabilization tank 3, the washing waste liquid carrying the catalyst fine powder is layered, the heavy oil wax with less catalyst in the upper layer is introduced to the washing tower 2 for washing the tail gas, and the slurry with higher catalyst concentration in the lower layer is pumped out to a wax fine filtering system 11 for further treatment.
The detection shows that the Fischer-Tropsch synthesis reaction is carried out for 300 hours, and the content of the catalyst in the clean tail gas washed by the washing tower is detected to be 2 ppm; when the Fischer-Tropsch synthesis reaction is carried out for 600 hours, the content of the catalyst in the clean tail gas washed by the washing tower is detected to be 4ppm, and the requirements (10ppm) of the heat exchanger and a subsequent gas-liquid separation device on the raw material gas are completely met.
Example 3
Catalyst fines in the exhaust gas were removed as described in reference to example 2, except that: in the scrubber, the off-gas enters below the liquid level of the scrubber through a gas distributor 14 which opens upwards.
The detection shows that the Fischer-Tropsch synthesis reaction is carried out for 300 hours, and the content of the catalyst in the clean tail gas washed by the washing tower is detected to be 5 ppm; when the Fischer-Tropsch synthesis reaction is carried out for 600 hours, the content of the catalyst in the clean tail gas washed by the washing tower is detected to be 7ppm, and the requirements (10ppm) of the heat exchanger and a subsequent gas-liquid separation device on the raw material gas are completely met.
Example 4
Catalyst fines in the exhaust gas were removed as described in reference to example 2, except that: the spraying speed of the washing liquid in the washing tower 2 is 25m/s, and the liquid-gas ratio of the washing liquid to the tail gas is 5L/m3。
The detection shows that the Fischer-Tropsch synthesis reaction is carried out for 300 hours, and the content of the catalyst in the clean tail gas washed by the washing tower is 1 ppm; when the Fischer-Tropsch synthesis reaction is carried out for 600 hours, the content of the catalyst in the clean tail gas washed by the washing tower is detected to be 3ppm, and the requirements (10ppm) of the heat exchanger and a subsequent gas-liquid separation device on the raw material gas are completely met.
Example 5
Catalyst fines in the exhaust gas were removed as described in reference to example 1, except that: the particle size of the washing liquid droplets was 7 mm.
The detection shows that the Fischer-Tropsch synthesis reaction is carried out for 300 hours, and the content of the catalyst in the clean tail gas washed by the washing tower is detected to be 8 ppm; when the Fischer-Tropsch synthesis reaction is carried out for 600 hours, the content of the catalyst in the clean tail gas washed by the washing tower is detected to be 9ppm, and the requirements (10ppm) of the heat exchanger and a subsequent gas-liquid separation device on the raw material gas are completely met.
Example 6
Catalyst fines in the exhaust gas were removed as described in reference to example 1, except that: the liquid-gas ratio of the washing liquid to the tail gas is 0.05L/m3。
The detection shows that the Fischer-Tropsch synthesis reaction is carried out for 300 hours, and the content of the catalyst in the clean tail gas washed by the washing tower is detected to be 7 ppm; when the Fischer-Tropsch synthesis reaction is carried out for 600 hours, the content of the catalyst in the clean tail gas washed by the washing tower is detected to be 9ppm, and the requirements (10ppm) of the heat exchanger and a subsequent gas-liquid separation device on the raw material gas are completely met.
Comparative example 1
The synthesis gas reacts in a Fischer-Tropsch synthesis reactor 1, the produced heavy oil wax (heavy product) is filtered by a liquid-solid separation filter 7 and then discharged, and the reaction tail gas is separated by a gas-liquid-solid separation device 6 at the top of the reactor and then leaves the reactor, enters a heat exchanger 9 and a subsequent gas-liquid separation device 10 and is treated. The catalyst content in the tail gas is 50ppm, and the temperature is 270 ℃.
The detection shows that when the process is carried out for 600 hours, the heat exchanger 9 and the subsequent gas-liquid separation device 10 are blocked respectively.
Comparative example 2
Catalyst fines in the exhaust gas were removed as described in reference to example 2, except that: with a commercial kinematic viscosity of 6mm2The oil or wax as a wash liquid replaces the heavy oil wax, and the off-gas is washed in a wash column 2.
The detection shows that the Fischer-Tropsch synthesis reaction is carried out for 300 hours, and the content of the catalyst in the clean tail gas washed by the washing tower is 20 ppm; when the Fischer-Tropsch synthesis reaction is carried out for 600 hours, the content of the catalyst in the clean tail gas washed by the washing tower is detected to be 45ppm, and the requirement (10ppm) of a heat exchanger and a subsequent gas-liquid separation device on the raw material gas is not met.
Comparative example 3
The catalyst particles in the slurry bed Fischer-Tropsch synthesis tail gas are removed according to the method disclosed in CN 101723774A.
The detection shows that the Fischer-Tropsch synthesis reaction is carried out for 300 hours, and the content of the catalyst in the clean tail gas washed by the washing tower is 80 ppm; when the Fischer-Tropsch synthesis reaction is carried out for 600 hours, the content of the catalyst in the clean tail gas washed by the washing tower is detected to be 120ppm, and the requirement (10ppm) of a heat exchanger and a subsequent gas-liquid separation device on the raw material gas is not met.
Therefore, the method can effectively and efficiently remove the catalyst in the tail gas of the Fischer-Tropsch synthesis slurry bed reactor, obviously reduce the problem of blockage of a subsequent gas-liquid separation device of the Fischer-Tropsch synthesis reactor, reduce the content of the catalyst in the tail gas treated by the washing tower to 1-10ppm, and completely meet the requirements of subsequent processes, such as a heat exchanger and the gas-liquid separation device, on the raw material gas.
In addition, the method provided by the invention has a simple process, does not need to change the original reaction equipment, is not influenced by the original production schedule and yield setting, has good applicability, and can be applied to all Fischer-Tropsch synthesis slurry bed reaction processes.
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.
Claims (10)
1. A method for removing catalyst particles carried by Fischer-Tropsch synthesis tail gas comprises the following steps: contacting the synthesis gas with a catalyst to carry out Fischer-Tropsch synthesis reaction to generate tail gas carrying catalyst particles and heavy oil wax; contacting the tail gas with a washing solution for washing to obtain a washing waste liquid containing catalyst particles carried in the tail gas and clean tail gas; wherein the kinematic viscosity of the washing liquid is more than 6mm2/s。
2. The method of claim 1, wherein during the scrubbing, the scrubbing liquid is contacted with the tail gas in a counter-current direction;
preferably, the temperature of the tail gas is 150-350 ℃, and the gas flow rate is 1-10 m/s; more preferably, the temperature of the tail gas is 220-300 ℃, and the gas flow rate is 2-6 m/s;
preferably, the spraying speed of the washing liquid is 5-60 m/s; the washing temperature is 120-250 ℃, and the washing pressure is 2-3.8 MPa; more preferably, the spraying rate of the washing liquid is 10-50m/s, the washing temperature is 150-230 ℃, and the washing pressure is 2.5-3.5 MPa.
3. A method according to claim 1 or 2, wherein the kinematic viscosity of the wash liquor is from 10 to 50mm2/s；
Preferably, the washing liquid is oil or wax which is liquid in the temperature range of 150-250 ℃;
preferably, the tail gas passes through the washing liquid and is in reverse contact with the washing liquid;
preferably, the liquid-gas ratio of the washing liquid to the tail gas is at least 0.1L/m3(ii) a Preferably, the liquid-gas ratio of the washing liquid to the tail gas is 0.5-5L/m3；
Preferably, the particle size of the liquid drops of the washing liquid is 1-5 mm; more preferably, the washing liquid has a droplet size of 1.5 to 3 mm.
4. The method according to any one of claims 1 to 3, further comprising returning the washing waste liquid to the washing process, or returning a part of the obtained stabilizing liquid to the washing process after stabilizing the washing waste liquid;
preferably, the temperature of the stabilizing liquid is greater than 100 ℃; more preferably, the temperature of the stabilizing solution is from 150 ℃ to 250 ℃.
5. The process of any of claims 1-4, further comprising returning at least a portion of the heavy oil wax as a wash liquid.
6. A system for removing catalyst particles carried by Fischer-Tropsch synthesis tail gas in accordance with any one of claims 1 to 5, which comprises a reactor (1) and at least one scrubber (2), wherein a tail gas outlet (12) at the top of the reactor (1) is communicated with a gas phase inlet (21) of the scrubber, the scrubber is provided with a scrubbing liquid inlet (23), a liquid phase outlet (24) and a liquid level meter (25), and scrubbing liquid is used in the scrubber to remove the catalyst in the tail gas.
7. A system according to claim 6, wherein a gas distributor (14) is provided in the scrubber tower (2); preferably, the gas distributor (14) opens downwards.
8. A system according to claim 6 or 7, wherein the reactor (1) further comprises a heavy oil wax outlet (13), the heavy oil wax outlet (13) being in communication with a scrubbing liquid inlet (23) of the scrubbing tower.
9. A system according to any one of claims 6-8, wherein the system further comprises a stabilization tank (3), the wash liquid inlet (23) and the liquid phase outlet (24) of the wash column being in communication with the stabilization tank (3), respectively; preferably, a heat preservation and/or heating device is arranged in the stabilization tank (3); more preferably, the heavy oil wax outlet (13) of the reactor (1) is in communication with the stabilizer tank (3).
10. Use of a method according to any one of claims 1 to 5 or a system according to any one of claims 6 to 9 in fischer-tropsch synthesis.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910310528.1A CN111821785A (en) | 2019-04-17 | 2019-04-17 | Method for removing catalyst particles carried by Fischer-Tropsch synthesis tail gas and system and application used by method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910310528.1A CN111821785A (en) | 2019-04-17 | 2019-04-17 | Method for removing catalyst particles carried by Fischer-Tropsch synthesis tail gas and system and application used by method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111821785A true CN111821785A (en) | 2020-10-27 |
Family
ID=72915524
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910310528.1A Pending CN111821785A (en) | 2019-04-17 | 2019-04-17 | Method for removing catalyst particles carried by Fischer-Tropsch synthesis tail gas and system and application used by method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111821785A (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101391198A (en) * | 2008-10-31 | 2009-03-25 | 神华集团有限责任公司 | Slurry bed ft synthetic reactor and technique |
| CN102000473A (en) * | 2010-11-26 | 2011-04-06 | 岳阳怡天化工有限公司 | Roast tail gas treatment method in production of catalytic cracking catalyst |
| CN201978749U (en) * | 2011-02-13 | 2011-09-21 | 青岛惠城石化科技有限公司 | Production device for reactivation of catalytic cracking dead catalyst |
| CN104548818A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Device and method for increasing washing efficiency of catalyst in reactant gas |
| CN110878216A (en) * | 2018-09-05 | 2020-03-13 | 国家能源投资集团有限责任公司 | Fischer-Tropsch synthesis process, Fischer-Tropsch synthesis system and application of Fischer-Tropsch synthesis system |
-
2019
- 2019-04-17 CN CN201910310528.1A patent/CN111821785A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101391198A (en) * | 2008-10-31 | 2009-03-25 | 神华集团有限责任公司 | Slurry bed ft synthetic reactor and technique |
| CN102000473A (en) * | 2010-11-26 | 2011-04-06 | 岳阳怡天化工有限公司 | Roast tail gas treatment method in production of catalytic cracking catalyst |
| CN201978749U (en) * | 2011-02-13 | 2011-09-21 | 青岛惠城石化科技有限公司 | Production device for reactivation of catalytic cracking dead catalyst |
| CN104548818A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Device and method for increasing washing efficiency of catalyst in reactant gas |
| CN110878216A (en) * | 2018-09-05 | 2020-03-13 | 国家能源投资集团有限责任公司 | Fischer-Tropsch synthesis process, Fischer-Tropsch synthesis system and application of Fischer-Tropsch synthesis system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US2987465A (en) | Gas-liquid contacting process | |
| CN102703712B (en) | Combined filtration process for recovering noble metal catalyst from fischer-tropsch synthesis products | |
| CN106190278A (en) | Cracking intermediate liquid product returns the hydrocarbon heat from hydrogenation cracking method inferior of pre-hydrogenation | |
| US3151060A (en) | Process and apparatus for liquid-gas reactions | |
| WO2009113620A1 (en) | Method for selectively removing catalysts from fischer-tropsch synthetic crude oil and method for recycling removed catalysts | |
| CN111286356A (en) | System for producing hydrocarbons by high-temperature Fischer-Tropsch synthesis | |
| CN111821785A (en) | Method for removing catalyst particles carried by Fischer-Tropsch synthesis tail gas and system and application used by method | |
| CN105051158B (en) | hydrocarbon synthesis reaction device | |
| CN110878216A (en) | Fischer-Tropsch synthesis process, Fischer-Tropsch synthesis system and application of Fischer-Tropsch synthesis system | |
| CN103228765B (en) | Method for producing hydrocarbon oil and system for producing hydrocarbon oil | |
| CN105944627A (en) | Device for preparing ethylene from acetylene through selective hydrogenation | |
| EA029799B1 (en) | Method for startup of bubble tower-type slurry bed reactor | |
| US2468521A (en) | Heat control in an exothermic reaction | |
| US20140286834A1 (en) | Integrated multi-step solid/liquid separation system for fischer-tropsch processes | |
| CN110819383A (en) | Process for the upflow hydrogenation of poor quality hydrocarbons using reactors with internal parallel reaction zones | |
| AU2010214107B2 (en) | Slurry reactor fines segregation and removal | |
| CN209636172U (en) | A kind of distillation equipment and processing system of catalytic slurry | |
| CN101210196B (en) | Conversion method for hydrocarbon oil | |
| CN204724145U (en) | A kind of F-T synthesis and separator | |
| CN204564102U (en) | A kind of F-T synthesis system | |
| US2472501A (en) | Process of regenerating synthesis catalyst with oxygen and return of oxidized catalyst to the synthesis reactor | |
| CN102498191A (en) | Method for producing hydrocarbon oil and synthetic reaction system | |
| CN104711006A (en) | Fischer-Tropsch synthesis system and method | |
| CN106701160B (en) | The setting method of circulating pump in boiling bed hydrogenation device | |
| CN106554806A (en) | Bulk bed reactor and method for converting heavy oil to light oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information | ||
| CB02 | Change of applicant information |
Address after: 100011 Beijing Dongcheng District, West Binhe Road, No. 22 Applicant after: CHINA ENERGY INVESTMENT Corp.,Ltd. Applicant after: Beijing low carbon clean energy Research Institute Address before: 100011 Beijing Dongcheng District, West Binhe Road, No. 22 Applicant before: CHINA ENERGY INVESTMENT Corp.,Ltd. Applicant before: NATIONAL INSTITUTE OF CLEAN-AND-LOW-CARBON ENERGY |
|
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20201027 |