CN111871032B - Online filtration system of three-phase suspension bed - Google Patents
Online filtration system of three-phase suspension bed Download PDFInfo
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- CN111871032B CN111871032B CN202010629993.4A CN202010629993A CN111871032B CN 111871032 B CN111871032 B CN 111871032B CN 202010629993 A CN202010629993 A CN 202010629993A CN 111871032 B CN111871032 B CN 111871032B
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/11—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with bag, cage, hose, tube, sleeve or like filtering elements
- B01D29/114—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with bag, cage, hose, tube, sleeve or like filtering elements arranged for inward flow filtration
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/11—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with bag, cage, hose, tube, sleeve or like filtering elements
- B01D29/31—Self-supporting filtering elements
- B01D29/33—Self-supporting filtering elements arranged for inward flow filtration
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/50—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with multiple filtering elements, characterised by their mutual disposition
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/50—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with multiple filtering elements, characterised by their mutual disposition
- B01D29/56—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with multiple filtering elements, characterised by their mutual disposition in series connection
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/60—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor integrally combined with devices for controlling the filtration
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/60—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor integrally combined with devices for controlling the filtration
- B01D29/606—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor integrally combined with devices for controlling the filtration by pressure measuring
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/60—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor integrally combined with devices for controlling the filtration
- B01D29/608—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor integrally combined with devices for controlling the filtration by temperature measuring
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/62—Regenerating the filter material in the filter
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/62—Regenerating the filter material in the filter
- B01D29/66—Regenerating the filter material in the filter by flushing, e.g. counter-current air-bumps
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/006—Separating solid material from the gas/liquid stream by filtration
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1836—Heating and cooling the reactor
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Filtration Of Liquid (AREA)
Abstract
An on-line filtration system for a three-phase suspended bed, comprising: the filter unit comprises a suspended bed cylinder and a filter assembly arranged in the middle of the suspended bed cylinder; a filtrate collecting tank for receiving filtrate products is arranged at a liquid outlet of the filtering component, and a slurry tank for supplementing slurry to the suspended bed cylinder and a liquid supplementing tank for supplementing liquid to the suspended bed cylinder are arranged at the bottom of the suspended bed cylinder; the back-blowing unit comprises a back-blowing liquid collecting tank and a back-blowing gas collecting tank which are arranged at the liquid outlet of the filtering component; the gas circulation and heat exchange unit comprises a separator, a circulating gas heat exchanger, a cooling water heat exchanger, a circulating gas supercharger and a heating furnace; the control unit is configured to control the filtering unit, the back flushing unit, the gas circulation and heat exchange unit to work.
Description
Technical Field
The invention relates to an online filtering system of a three-phase suspension bed, belonging to the technical field of manufacturing of suspension bed filtering devices.
Background
The gas-liquid-solid three-phase suspension bed has the advantages of uniform temperature distribution, reduced pressure, low operation cost and the like, and is particularly widely applied to the synthesis of liquid fuels such as coal-to-liquid oil, coal-to-methanol, dimethyl ether and the like. In order to ensure the normal operation of the suspension bed, reduce the loss of the catalyst and ensure the quality of the liquid fuel synthesis product, solid-liquid separation is one of key technologies, and the most reliable and effective means for the gas-liquid-solid three-phase suspension bed is to adopt a filtering medium filtering method.
The gas-liquid-solid three-phase suspension bed is generally cross-flow filtration, the pressure difference at two sides of the filter is used as driving force, and the filter is regenerated and recovered to the initial flux by adopting purge gas or feed liquid and the like for back flushing. Different from the traditional filter, the suspension bed internal filtration is that the filtration operation is carried out under a gas-liquid-solid three-phase system, the outer surface of a porous filtration pipe is used for bearing a filter cake, and the three-phase fluid in a turbulent flow state can improve the shearing force and the turbulent flow diffusion effect on the surface of the filter element to a certain extent and inhibit the growth of a filter cake layer. A relatively large number of studies have been made in the academic world on the three-phase cross-flow filtration process and mathematical models (Hwang. K.J and Wu. Y.J, chem. Eng. J,139(2), 296. 303, 2008; Huizonga. P and Kuipers. J,44(6), 1277. 1288, 1998; Shimizu Y and Uryu. K,81(1),55-60, 1996).
Patent CN102553343A discloses a continuous separation method of catalyst and product for slurry bed synthesis of liquid fuel. After the slurry is separated by a high-speed centrifuge to obtain a light liquid component and a heavy liquid component, the concentrated oil slurry is pressurized by a centrifugal pump and returns to the slurry bed reactor to participate in the reaction again, and the light liquid component is subjected to secondary separation in a multi-layer metal sintering net filter. The main problem of the technical scheme is that the catalyst is very easy to inactivate after leaving the slurry bed reaction environment or severe blockage is caused by local temperature runaway.
Patent CN205948686U discloses a cross-flow filtration device and a cross-flow filtration system, including a buffer tank, a circulation pump and a filtration chamber. The cross-flow filtering membrane in the filtering cavity divides the filtering cavity into an inner cavity and an outer cavity, the filtering liquid is sent into the inner cavity, and the filtered liquid material is sent back to the buffer tank. The system can only be applied to ceramic membrane cross-flow filtration, the operable temperature and pressure range is limited, and the filtration pressure difference is realized by increasing the liquid pressure in the inner cavity by adjusting the power of the circulating pump, so that the system is very inconvenient.
Patent CN107362756A discloses a petrochemical production device using a cross-flow filter, which comprises a reaction kettle, a filter cylinder, an air vibrator and other main devices. In the technical scheme, the filter element regeneration mode is that a liquid feed pipe reversely enters the cross-flow filter through a material outlet, and the residual solid attached to the filter element falls off by feed liquid under the action of an air vibration hammer. Frequent air vibration hammers cause great damage to equipment, and the adoption of the feed liquid back-blowing filter element only can reduce the overall filtering efficiency.
Patents CN206438079U and CN201020213529.9 disclose cross-flow filters and separation systems, but they all have the problems of too narrow operating temperature and pressure range, unreasonable filter element back-blowing regeneration process, unable continuous operation or difficult on-line slurry replacement.
Disclosure of Invention
The invention aims to solve the technical problem that the shortcomings of the prior art are overcome, and the three-phase suspension bed online filtering system is provided, wherein a plurality of functional modules are independently arranged, so that the maintenance and the replacement are convenient and quick, and the parameters such as air pressure in a suspension bed cylinder body can be maintained, and the stability of a filtering process can be ensured; the method of combining gas back flushing and liquid back flushing solves the problems of uneven back flushing and low efficiency of the traditional back flushing; the arrangement of the gas circulation and heat exchange unit can also avoid equipment damage caused by too high temperature of circulating gas while recovering part of system heat.
The technical problem to be solved by the invention is realized by the following technical scheme:
the invention provides an on-line filtering system of a three-phase suspension bed, which comprises:
the filter unit comprises a suspended bed cylinder and a filter assembly arranged in the middle of the suspended bed cylinder; a filtrate collecting tank for receiving filtrate products is arranged at a liquid outlet of the filtering component, and a slurry tank for supplementing slurry to the suspended bed cylinder and a liquid supplementing tank for supplementing liquid to the suspended bed cylinder are arranged at the bottom of the suspended bed cylinder;
the back-blowing unit comprises a back-blowing liquid collecting tank and a back-blowing gas collecting tank which are arranged at the liquid outlet of the filtering component;
a gas circulation and heat exchange unit which comprises a separator, a circulating gas heat exchanger, a cooling water heat exchanger, a circulating gas supercharger and a heating furnace, the separator comprises a cyclone separator arranged at the upper part in the suspension bed cylinder body and a filler type cyclone separation tank arranged outside the suspension bed cylinder body, the air outlet of the cyclone separator is communicated with the air inlet of the filler type cyclone separation tank, the air outlet of the filler type cyclone separation tank is communicated with the tube pass inlet of the circulating gas heat exchanger, the tube pass outlet of the circulating gas heat exchanger is communicated with the tube pass inlet of the cooling water heat exchanger, the tube pass outlet of the cooling water heat exchanger is communicated with the gas inlet of the circulating gas supercharger, the gas outlet of the circulating gas supercharger is communicated with the shell pass inlet of the circulating gas heat exchanger, and the shell pass outlet of the circulating gas heat exchanger is communicated with the circulating gas inlet positioned at the bottom of the suspended bed cylinder through a heating furnace;
and the control unit is configured to control the filter unit, the back flushing unit, the gas circulation and heat exchange unit to work.
In order to promote the uniform mixing of the gas-liquid-solid three phases in the cylinder body of the suspension bed and simultaneously crush the coalesced large bubbles possibly existing in the cylinder body of the suspension bed again, the upper part of the cylinder body of the suspension bed is provided with a stirring paddle; further, a stirring paddle is arranged in the slurry tank.
In order to prevent the slurry from being solidified, the filtrate collecting tank, the slurry tank, the liquid supplementing tank, the back-blowing liquid collecting tank and the back-blowing gas collecting tank are all provided with heat tracing devices.
Preferably, the filter assembly comprises at least one vertically disposed candle filter, and the general inlet of the filter assembly is fitted with a sparger.
Preferably, the tubular filters are arranged in a central symmetry manner, the tubular filters are sintered metal meshes, sintered metal powder filter cores, metal fiber membranes, sintered metal felts, laser perforated meshes, wedge-shaped metal meshes or composite metal filter cores, the diameter of each tubular filter is 10-200mm, and the length of each tubular filter is 10-2000 mm.
In order to obtain the degree of fouling of the filter assembly, the filtrate collection tank further comprises a weighing unit; and a release gas buffer tank comprising a wet flowmeter is arranged at the gas outlet of the filtrate collecting tank.
In order to facilitate the discharge of the slurry or the filtered residue, a sewage discharge pipeline is arranged between the suspended bed cylinder and the slurry tank.
In order to overcome the defects of the existing back blowing technology, the back blowing unit performs back blowing by adopting a mode of combining gas isobaric back blowing and liquid isovolumetric back blowing, wherein the liquid volume adopted by the liquid isovolumetric back blowing is 4-20 times of the volume of the tubular filter, the back blowing frequency of the gas isobaric back blowing is 2-15, and the duration of single back blowing is 5-60 s.
In order to further trap solid and liquid, a gas-liquid separation tank is arranged between the tube side outlet of the circulating gas heat exchanger and the tube side inlet of the cooling water heat exchanger.
In order to ensure the safe and stable operation of the circulating gas supercharger, circulating gas buffer tanks are arranged at the front and the rear of the circulating gas supercharger; and a defoaming net is arranged in the circulating gas buffer tank.
In conclusion, the three-phase suspension bed online filtering system can complete the operation under complex working conditions such as a three-phase system, high-temperature and high-pressure continuous filtering and the like; a plurality of functional modules are independently arranged, so that the maintenance and the replacement are convenient and quick, and the parameters such as air pressure in the cylinder body of the suspension bed and the like can be maintained, thereby ensuring the stability of the filtering process; the method of combining gas back flushing and liquid back flushing solves the problems of uneven back flushing and low efficiency of the traditional back flushing; the arrangement of the gas circulation and heat exchange unit can recover part of system heat and avoid equipment damage caused by too high temperature of the circulating gas.
The technical solution of the present invention will be described in detail below with reference to the accompanying drawings and specific embodiments.
Drawings
FIG. 1 is a schematic structural diagram of an on-line filtration system of a three-phase suspension bed according to the present invention;
FIG. 2 is a schematic layout of a tubular filter of the three-phase suspension bed on-line filtration system of the present invention.
Detailed Description
The invention provides a three-phase suspension bed online filtering system, which can be used for solid-liquid separation in the fields of coal chemical industry, petrochemical industry and the like, in particular can be used for solid-liquid separation of various slurries such as water/solid particles, oil/solid particles, wax/solid particles and the like, and is preferably used for solid-liquid separation of wax/solid particle slurry by adopting a cross-flow filtering mode, wherein the concentration of the slurry is not higher than 50 wt%, and the particle size range of the solid particles is 5-500 mu m.
FIG. 1 is a schematic structural diagram of the three-phase suspension bed on-line filtration system of the present invention. As shown in figure 1, the three-phase suspension bed online filtering system comprises a filtering unit, a back flushing unit, a gas circulation and heat exchange unit and a control unit. The control unit is electrically connected with the filtering unit, the back flushing unit and the gas circulation and heat exchange unit.
The control unit is configured to receive signals of the filtering unit, the back flushing unit and the gas circulation and heat exchange unit and control the filtering unit, the back flushing unit and the gas circulation and heat exchange unit to work. For example, the control unit can adopt an upper computer and a lower computer for control, the lower computer mainly completes data acquisition and control, and the upper computer completes functions of configuration, data communication, storage, data processing and the like, so that automatic detection and automatic control functions of parameters such as temperature, pressure, flow, filtering pressure difference, liquid level and the like are realized, and sequential operation functions such as automatic valve switching and the like are realized.
The filtering unit comprises a suspended bed cylinder 10 and a filtering component 9 arranged in the middle of the suspended bed cylinder 10.
The material of the suspension bed cylinder 10 can be carbon steel, stainless steel, nickel-based alloy steel, chrome molybdenum alloy steel and the like, and preferably stainless steel. The diameter of the suspension bed cylinder 10 is 0.15-1m, and the height is 1.5-15 m. The suspension bed cylinder 10 is required to meet the requirements of high temperature and high pressure process, for example, the maximum operating pressure is 20MPa, and the maximum operating temperature is 500 ℃. The upper part of the suspension bed cylinder 10 is provided with the stirring paddle 11, the invention does not limit the type and the specific installation position of the stirring paddle 11, and a person skilled in the art can select the stirring paddle 11 according to the process requirements, and the stirring paddle 11 can promote the uniform mixing of the gas-liquid-solid three phases in the suspension bed cylinder 10 and can also crush the coalescent large bubbles possibly existing in the suspension bed cylinder 10 again.
The filter assembly 9 comprises at least one vertically disposed filter. In this embodiment, the filter is preferably a tube filter 19. In order to filter the slurry in the suspension bed cylinder 10 uniformly, the tubular filters 19 are arranged in a central symmetry. The number of the tubular filters is not limited by the invention, preferably one to ten, and the number of the tubular filters can be flexibly changed and adjusted by a person skilled in the art according to the suspension bed liquid level control and the performance of the adopted filter.
FIG. 2 is a schematic layout of a tubular filter of the three-phase suspension bed on-line filtration system of the present invention. When the number of the candle filters 19 is one, as shown in fig. 2, the candle filter 19 is disposed at the center axis of the suspension bed cylinder 10; when the number of the tube filters 19 is two, three or four, the tube filters 19 are symmetrically arranged; when the number of the tube filters 19 is five or six, one of the tube filters 19 is disposed at the central axis of the suspension bed cylinder 10, and the other tube filters 19 are symmetrically arranged. The invention is not limited to the location of the tubular filter, as long as it ensures that the slurry passes through the tubular filter uniformly as it is being filtered.
The tubular filter is, for example, a sintered metal mesh, a sintered metal powder filter element, a metal fiber membrane, a sintered metal felt, a laser perforated mesh, a wedge-shaped metal mesh, a composite metal filter element, etc., and preferably, the diameter of a single tubular filter may be 10 to 200mm and the length may be 10 to 2000 mm.
In order to be able to achieve a uniform flow rate per filter, a distributor (not shown) is installed at the general inlet of the filter assembly 9.
A filtrate collecting tank 15 for receiving filtrate products is arranged at the liquid outlet of the filtering component 9. The filtrate collection tank 15 is provided with a heat tracing to prevent the solidification of slurry such as heavy oil, wax, etc. The heat tracing mode of the heat tracing device can be heat conduction oil, steam or electric heating. In order to measure the accumulated amount of the filtrate in real time and quickly know the dirt blocking degree and the back flushing regeneration effect of the filtering component 9, the filtrate collecting tank 15 further comprises a weighing unit, such as a precision electronic scale and the like. Because the gas-liquid-solid three-phase violent turbulence exists in the suspension bed cylinder 10, the filtrate product and the entrained gas which are permeated from the micropores of the filtering component are called release gas, and the volume ratio of the release gas to the filtrate product can accurately reflect the pollution and blockage degree of the filtering component. The outlet of the filtrate collection tank 15 is provided with a release gas buffer tank 14 comprising a wet flow meter so that the release gas is precisely metered and vented or enters the incinerator.
By controlling the filtration pressure differential, the slurry within the suspension bed cylinder 10 can be filtered. The filtration pressure difference refers to the pressure difference between the gas phase at the top of the suspended bed cylinder 10 and the gas phase in the filtrate collection tank 15. The filtration pressure difference is realized by controlling a valve behind the filtrate collection tank and an air source unit (such as a combination of a regulating valve and a constant pressure valve) to regulate the gas phase pressure of the filtrate collection tank after the gas phase pressure at the top of the suspended bed cylinder 10 is interlocked by the control unit. The control of the filtering pressure difference comprises an automatic mode and a manual mode, and the manual control mode of the filtering pressure difference can enable the system to quickly reach a target value of the filtering pressure difference; the automatic control mode of the filtering pressure difference can ensure that the system can maintain the filtering pressure difference to fluctuate within a small range near a target value and maintain the stable operation of the whole filtering process.
And a slurry tank 16 for supplementing slurry to the suspension bed cylinder is arranged at the bottom of the suspension bed cylinder 10. The slurry tank 16 is provided with a heat tracing device to prevent the slurry such as heavy oil, wax, etc. from solidifying. The heat tracing mode of the heat tracing device can be heat conduction oil, steam or electric heating. The supplemental slurry motive force of the slurry tank 16 may come from a pressure differential between the slurry tank 16 and the suspended bed cylinder 10 or a slurry transfer pump (not shown). Further, in order to prevent the solid particles in the slurry from depositing, a stirring paddle is provided in the slurry tank 16.
In order to facilitate the discharge of the slurry or the filtered residue, a sewage discharge pipeline is arranged between the suspension bed cylinder 10 and the slurry tank 16, so that the slurry conveying/discharging function is realized through switching of a series of valves on the pipeline, and operations such as temperature reduction, pressure relief, parking and the like are not needed.
Specifically, when slurry needs to be replenished into the suspended bed cylinder, the valve of the sewage pipeline is closed, the pipeline between the suspended bed cylinder 10 and the slurry tank 16 is communicated, and then the slurry can be conveyed from the slurry tank 16 to the suspended bed cylinder 10 through a slurry conveying pump, or the pressure difference between the slurry tank 16 and the suspended bed cylinder 10 is controlled, so that the pressure in the slurry tank 16 is greater than the pressure in the suspended bed cylinder 10, and the slurry is conveyed; when the slurry is required to be discharged, the valve at the liquid outlet of the slurry tank 16 is closed, and the valve of the sewage pipeline is opened, so that the suspended bed cylinder 10 is communicated with the outside through the sewage pipeline, and the filtered residue can be discharged by utilizing gravity or pressure.
It is necessary to supplement that, in order to control the pressure in each tank and pipeline in the three-phase suspension bed on-line filtering system, the three-phase suspension bed on-line filtering system further includes an air source unit for adjusting the system pressure. The gas source unit may use various gas sources in the prior art, and the present invention is not limited thereto. In addition, in order to conveniently control the passages between the tanks and the pipelines in the three-phase suspension bed online filtering system, a person skilled in the art can set valves at appropriate positions according to actual conditions, so as to control the on-off of the tanks and the pipelines. And the control unit controls the states of the air source unit and the valve according to different filtering steps to realize filtering. The control can be automatically controlled according to a preset program or manually controlled manually. The valve can be a regulating valve, a constant pressure valve, a pneumatic valve or a self-recovery safety valve and the like.
As the filtration test proceeds, filtrate product flows out all the time, the liquid level in the suspension bed cylinder 10 will gradually decrease, and the solid content will be higher and higher. In order to maintain consistent solid content in the suspension bed cylinder 10, the filtration unit further comprises a liquid supplementing tank 5 which is used for supplementing liquid to the suspension bed cylinder 10 and is arranged at the bottom of the suspension bed cylinder 10, wherein the liquid supplementing tank 5 is internally provided with liquid without solid particles and is provided with a heat tracing device so as to prevent slurry such as heavy oil and wax from being solidified. The heat tracing mode of the heat tracing device can be heat conduction oil, steam or electric heating. The fluid infusion can be performed in various manners, for example, the fluid infusion tank 5 can interlock the fluid level in the suspension bed (for example, when the fluid level gauge in the suspension bed cylinder 10 detects that the fluid level in the suspension bed cylinder 10 is lower than a predetermined threshold, the fluid level gauge sends a signal to the control unit, and the control unit controls components such as the air source unit and a valve between the suspension bed cylinder 10 and the fluid infusion tank 5, so that the fluid without solid particles in the fluid infusion tank 5 is delivered into the suspension bed cylinder 10), thereby ensuring the fluid level and the solid content of the slurry in the suspension bed cylinder 10. The arrangement of the liquid supplementing tank 5 can enable the three-phase suspension bed online filtering system to test the performance of the filter in the slurry with unchanged solid content for a long period.
It should be noted that, in the present invention, it is preferable to use the double-isolation differential pressure level gauge 18 with purging function to detect the liquid level in the suspension bed cylinder 10, so as to measure the liquid level of the slurry with characteristics of high viscosity, high solid content, easy solidification at low temperature, etc.
The back-blowing unit comprises a back-blowing liquid collecting tank 13 and a back-blowing gas collecting tank 12 which are respectively arranged at the liquid outlet of the filtering component 9. In order to preheat the back-blowing liquid and the back-blowing gas, the back-blowing liquid collecting tank 13 and the back-blowing gas collecting tank 12 are both provided with heat tracing devices, and the heat tracing modes of the heat tracing devices can be heat conduction oil, steam or electric heating.
As the filtration proceeds, solid particles will gradually block the micropores of the filtration module 9 and bridge on the surface of the tubular filter to form a filter cake, resulting in a sharp drop in filtration flux; especially for filtration processes involving reactions, catalyst particles deposited on the tube filter are prone to locally violent reactions and exotherms, resulting in irreversible fouling of the tube filter. The filter cake on the tubular filter can be removed by regularly back-blowing the filter component 9 through the back-blowing unit, so that the effect of recovering the filtering performance of the filter component 9 is achieved. The back-flushing is the reverse of the filtration process operation, i.e., liquid and/or gas is blown from a back-flushing liquid collection tank or a back-flushing gas collection tank into the filter in the suspended bed.
Specifically, when the three-phase suspension bed online filter system performs filtering, the valve between the blowback unit and the filter assembly 9 is closed, the valve between the filtrate collection tank 15 and the filter assembly 9 is opened, and the filtrate product and the like flow into the filtrate collection tank 15 due to the filtering pressure difference. When the three-phase suspension bed online filtering system performs back flushing, the valve between the back flushing unit and the filtering component 9 is opened, the valve between the filtrate collecting tank 15 and the filtering component 9 is closed, and the control unit, such as an air source control unit, pressurizes the back flushing unit, so as to discharge filter cakes and the like on the tubular filter.
The back-blowing gas can be inert gas or the same gas as that in the three-phase suspended bed online filtering system. The back-flushing liquid can be a filtrate product or a solid-free liquid with similar properties to the three-phase suspension bed online filtering system. The back-blowing driving force is from the back-blowing liquid collecting tank and the back-blowing gas collecting tank to the gas phase pressure difference of the suspended bed. The back-blowing gas is blown into the filter from the gas back-blowing tank, the kinetic energy is gradually converted into static pressure energy, and filter cakes on the outer surface of the filter are instantaneously blasted; the liquid back flushing is to press the liquid into the filter by high pressure gas or slurry pump, so that the filter cake can be removed by back flushing the filter uniformly.
In the invention, the back-blowing unit performs back-blowing by adopting a mode of combining gas isobaric back-blowing and liquid isovolumetric back-blowing. Wherein, the gas isobaric back-blowing filtering component is taken as the main part, and the liquid isobaric back-blowing filtering component is taken as the auxiliary part.
During the filtering operation of the filter assembly 9, initially solid particles may "bridge" within the pores of the filter and on the surface of the filter to form a filter cake, and subsequently fine particles may continuously penetrate into the filter cake, i.e., "pack effect", resulting in an increased cake thickness and a denser cake. Since the liquid has a low compressibility and can be distributed more uniformly on the inner side of the filter, the back blowing is performed by first using liquid isochoric back blowing, so that the filter cake can be blown loose first. According to the actual process conditions, the liquid amount adopted during the liquid equal-volume back flushing is preferably 4-20 times of the volume of the tubular filter. However, the back-flushing filter of liquid can cause the liquid to re-enter the slurry, which is contrary to the original purpose of solid-liquid separation and is low in economy, so that the back-flushing of liquid and the like is only used as an auxiliary.
The back-blowing gas is easy to blow out from the 'short circuit' in the micropore with small resistance, so that the filter can not be subjected to uniform back-blowing integrally, and the aspect that the gas isobaric back-blowing is not as good as the liquid isochoric back-blowing filtration is realized. However, the back-flushing gas is easier to separate from the system and does not have any influence on the system, so the back-flushing gas filter assembly mainly comprises a gas isobaric back-flushing filter assembly. The gas has high compressibility, and the compressed back-blowing gas can blow the filter cake open instantly when penetrating through the micropores of the filter element, so as to achieve the aim of removing the filter cake. When carrying out gas isobaric back flushing, different parameters such as single filtration period (20-200min), back flushing medium pressure (10-1000 KPa higher than system pressure), back flushing medium temperature (40-200 ℃), back flushing times (2-15), single back flushing duration (5-60s), filter soaking waiting time (2-10min) and the like need to be set according to actual conditions. The control unit can execute the back flushing process according to the set parameters, or a user can manually operate the back flushing process. Through the combined mode of the back flushing process, the defects that gas back flushing is not uniform and liquid back flushing can reduce the overall filtering efficiency can be overcome, the back flushing effect is optimized, and the service life of the filter is prolonged.
The gas circulation and heat exchange unit comprises a separator, a circulating gas heat exchanger 3, a cooling water heat exchanger 30, a circulating gas supercharger 2 and a heating furnace 6.
The separator comprises a cyclone separator 8 arranged at the upper part in the suspended bed cylinder 10 and a packing type cyclone separation tank 7 arranged outside the suspended bed cylinder 10, wherein the air outlet of the cyclone separator 8 is communicated with the air inlet of the packing type cyclone separation tank 7. The cyclone separator 8 is used for trapping solid particles/catalyst in the suspended bed cylinder 10 to maintain stable solid content; and the gas obtained by the separation of the cyclone separator 8 leaves the suspended bed cylinder 10 and enters an external packing type cyclone separation tank 7 for secondary separation. The separator can effectively intercept solids and liquids, avoid the pollution and blockage of subsequent pipeline equipment and ensure the safe and stable operation of the equipment.
The gas outlet of the packed cyclone separation tank 7 is communicated with the tube side inlet of the circulating gas heat exchanger 3, the tube side outlet of the circulating gas heat exchanger 3 is communicated with the tube side inlet of the cooling water heat exchanger 30, the tube side outlet of the cooling water heat exchanger 30 is communicated with the gas inlet of the circulating gas supercharger 2, the gas outlet of the circulating gas supercharger 2 is communicated with the shell side inlet of the circulating gas heat exchanger 3, and the shell side outlet of the circulating gas heat exchanger 3 is communicated with the circulating gas inlet positioned at the bottom of the suspended bed cylinder 10 through the heating furnace 6. Further, a gas distributor 17 is arranged at the circulating gas inlet so that the pressurized and preheated circulating gas can bubble into the suspension bed cylinder 10 uniformly to maintain the uniform mixing of the gas-liquid-solid three phases.
In order to further trap solid and liquid, a gas-liquid separation tank 4 is arranged between the tube side outlet of the circulating gas heat exchanger 3 and the tube side inlet of the cooling water heat exchanger 30.
In order to ensure the safe and stable operation of the circulating gas booster compressor 2, the circulating gas buffer tank 1 is arranged around the circulating gas booster compressor 2, and a defoaming net is installed in the circulating gas buffer tank 1. The circulating air supercharger 2 is used for supercharging circulating air and adjusting the circulating air flow rate so as to adjust the air speed of the air tower in the suspension bed cylinder 10, and the air speed operation range of the air tower in the suspension bed cylinder 10 can be 0.05-1.5 m/s.
According to the structure, the gas coming out of the top of the suspension bed cylinder 10 and the circulating gas pressurized by the circulating gas supercharger 2 exchange heat for the first time in the circulating gas heat exchanger 3 and then enter the cooling water heat exchanger 30 to exchange heat with the cooling water for the second time, so that part of system heat can be recycled, and meanwhile, the circulating gas entering the circulating gas supercharger 2 is prevented from damaging equipment due to too high temperature.
The heating furnace 6 is used for further preheating the circulating gas entering the suspension bed cylinder 10.
It should be added that, in order to ensure the safe and stable operation of the three-phase suspension bed online filtering system of the present invention, the three-phase suspension bed online filtering system includes a temperature sensor and a pressure sensor electrically connected to the control unit, so as to detect the temperature and the pressure at the tank and the pipeline of the three-phase suspension bed online filtering system. The temperature sensor and the pressure sensor transmit detection signals to the control unit, and when the temperature and the pressure exceed preset threshold values, the control unit can perform protection in the modes of alarming, loop power supply closing, automatic pressure relief and the like. The arrangement positions of the temperature sensor and the pressure sensor are not limited, and preferably, the pipeline, the tank body and the suspension bed cylinder in the three-phase suspension bed online filtering system are all provided with the temperature sensor and the pressure sensor.
The three-phase suspension bed in-line filtration system of the present invention is further described with reference to the following specific examples.
Example one
In this example, the three-phase suspension bed in-line filtration system was used for filtering and separating wax and catalyst mixed slurry, wherein the catalyst particle content was 10 wt%, and the results of the distillation range analysis of the fischer-tropsch wax are shown in table 1. This example was conducted under a nitrogen atmosphere for filtration separation.
TABLE 1 results of wax distillation range analysis
| Fraction Recovered mass (%) | Boiling point BP (. degree. C.) |
| Tapping point IBP | 207.8 |
| 50 | 376.8 |
| 80 | 701.8 |
In this embodiment, the suspension bed cylinder 10 has a diameter of 150mm, a height of 3000mm, an operating temperature of 260 ℃ and 270 ℃, and an operating pressure of 1.0-1.5 MPa. The filtering component 9 consists of three parallel tubular filters, the tubular filters are five layers of sintered metal wire meshes, and the control precision of the filters is 40-50 μm.
Before the filtration operation is started, preparation works are carried out, such as slurry preheating, back-blowing gas preheating, circulating gas preheating, pressurization and the like. As shown in FIG. 1, the slurry tank 16 is started to stir and accompany heat, and after the catalyst particles and the wax slurry are uniformly mixed and preheated to 200 ℃, pressurized nitrogen gas is introduced into the suspension bed cylinder 10. The whole system is adjusted to 1.0-1.5MPa by adjusting a valve, and the circulating gas supercharger 2 is started to push gas to circularly flow in the devices such as the suspension bed cylinder 10, the filler type cyclone separation tank 7, the circulating gas heat exchanger 3, the cooling water heat exchanger 30, the heating furnace 6 and the like. The circulating gas heat exchanger 3 and the cooling water heat exchanger 30 recover part of heat in the circulating gas and ensure that the temperature of the circulating gas entering the circulating gas supercharger 2 is lower than 80 ℃. Circulating gas is preheated to about 200-250 ℃ by the heating furnace 6 and then is bubbled into the suspension bed cylinder 10 from the gas distributor 17 to drive wax/catalyst slurry in the suspension bed cylinder 10 to be mixed vigorously. The paddles 11 in the suspension bed cylinder 10 stir the slurry at a frequency of 36 HZ. The blowback gas tank is preheated to about 200 ℃ and 250 ℃, and the pressure is maintained to be 50-150KPa higher than the gas phase pressure at the top of the suspension bed cylinder 10.
In this embodiment, the filtration process includes three processes of filtration, soaking and standing, and blowback regeneration.
After the filtering pressure difference is manually adjusted to be 30-200KPa, the filtering mode can be switched to an automatic programmed filtering mode controlled by a control unit. The automatic programmed filtration mode can open the valve between the filter assembly 9 and the filtrate collecting tank 15 automatically after starting, so that the filtrate product flows into the filtrate collecting tank 15, and meanwhile, the automatic programmed filtration mode can interlock the gas phase pressure at the top of the suspension bed cylinder 10, finely adjust the regulating valve and the constant pressure valve behind the filtrate collecting tank 15, ensure that the filtration pressure difference fluctuates in a minimum range, and maintain the stable operation of the whole filtration process. The single filtration run time was 40-120 minutes. When it is desired to stop filtration, the valve between the filter assembly 9 and the filtrate collection tank 15 can be closed.
The soaking standing can make the filter cake become loose by soaking in the slurry and be sheared and washed off. The soaking time is maintained at 1-5 minutes.
The back flushing regeneration can instantly explode the filter cake on the outer surface of the filtering component 9 and recover the filtering performance of the filtering component 9. The parameters of the back flushing procedure in this embodiment are: the pressure of the back blowing gas is higher than the gas phase pressure at the top of the cylinder 10 of the suspension bed by 10-1000 KPa; the back flushing time is 5-60 seconds; the temperature of a back-blowing medium is 40-200 ℃; the back flushing times are 2-15. According to the actual working condition, each process parameter can be properly adjusted.
Through tests, the three-phase suspension bed online filtering system in the embodiment stably operates for half a year without stopping due to blockage faults.
Example two
In this example, the three-phase suspension bed in-line filtration system was used for oil slurry filtration separation, wherein the catalyst particle content was 35 wt%, and the results of distillation range analysis of heavy oil are shown in table 2. This example was conducted under a nitrogen atmosphere for filtration separation.
TABLE 2 analysis of distillation range of heavy oil
| Fraction Recovered mass (%) | Boiling point BP (. degree. C.) |
| Tapping point IBP | 210 |
| 50 | 358.8 |
| 80 | 412 |
In this embodiment, the suspension bed cylinder 10 has a diameter of 150mm, a height of 3000mm, an operating temperature of 240 ℃ and 250 ℃, and an operating pressure of 1.0-1.5 MPa. The filter assembly 9 consists of two parallel tubular filters made of sintered metal powder, the filter control precision being 30-40 μm.
In this embodiment, the filtration process includes three processes of filtration, soaking and standing, and blowback regeneration.
The filtration and soaking quiet climate in this embodiment are similar to those in the embodiment, except that in the back-blowing regeneration step, the embodiment is performed by combining the back-blowing of gas and the back-blowing of liquid. Specifically, in this embodiment, the liquid medium is first used for back flushing to regenerate the filter assembly 9, and then the gas back flushing filter assembly 9 is used for regeneration: the clean heavy oil with the temperature of 180-200 ℃ is quickly pressed into the filter assembly 9 by high-pressure nitrogen, the back flushing time is 10-30 seconds, the filter cake on the outer surface of the filter is removed completely, and the back flushing operation of the liquid medium can also be controlled by the control unit.
Through tests, the three-phase suspension bed online filtering system in the embodiment filters and separates oil slurry, and after stable operation for 3 months, the vehicle is not stopped due to blockage faults. The filter disassembled after parking is detected to have no obvious blockage.
In conclusion, the three-phase suspension bed online filtering system can complete the operation under complex working conditions such as a three-phase system, high-temperature and high-pressure continuous filtering and the like; a plurality of functional modules are independently arranged, so that the maintenance and the replacement are convenient and quick, and the parameters such as air pressure in the cylinder body of the suspension bed and the like can be maintained, thereby ensuring the stability of the filtering process; the method of combining gas back flushing and liquid back flushing solves the problems of uneven back flushing and low efficiency of the traditional back flushing; the arrangement of the gas circulation and heat exchange unit can recover part of system heat and avoid equipment damage caused by too high temperature of the circulating gas.
Claims (10)
1. The utility model provides an online filtration system of three-phase suspension bed which characterized in that, online filtration system of three-phase suspension bed includes:
the filter unit comprises a suspended bed cylinder and a filter assembly arranged in the middle of the suspended bed cylinder; a filtrate collecting tank for receiving filtrate products is arranged at a liquid outlet of the filtering component, and a slurry tank for supplementing slurry to the suspended bed cylinder and a liquid supplementing tank for supplementing liquid to the suspended bed cylinder are arranged at the bottom of the suspended bed cylinder;
the back-blowing unit comprises a back-blowing liquid collecting tank and a back-blowing gas collecting tank which are arranged at the liquid outlet of the filtering component;
a gas circulation and heat exchange unit which comprises a separator, a circulating gas heat exchanger, a cooling water heat exchanger, a circulating gas supercharger and a heating furnace, the separator comprises a cyclone separator arranged at the upper part in the suspension bed cylinder body and a filler type cyclone separation tank arranged outside the suspension bed cylinder body, the air outlet of the cyclone separator is communicated with the air inlet of the filler type cyclone separation tank, the air outlet of the filler type cyclone separation tank is communicated with the tube pass inlet of the circulating gas heat exchanger, the tube pass outlet of the circulating gas heat exchanger is communicated with the tube pass inlet of the cooling water heat exchanger, the tube pass outlet of the cooling water heat exchanger is communicated with the gas inlet of the circulating gas supercharger, the gas outlet of the circulating gas supercharger is communicated with the shell pass inlet of the circulating gas heat exchanger, and the shell pass outlet of the circulating gas heat exchanger is communicated with the circulating gas inlet positioned at the bottom of the suspended bed cylinder through a heating furnace;
the control unit is configured to control the filtering unit, the back flushing unit and the gas circulation and heat exchange unit to work.
2. The three-phase suspended bed online filtering system of claim 1, wherein the upper part of the suspended bed cylinder is provided with a stirring paddle; and a stirring paddle is arranged in the slurry tank.
3. The three-phase suspended bed in-line filtration system of claim 1, wherein the filtrate collection tank, the slurry tank, the makeup tank, the blowback liquid collection tank, and the blowback gas collection tank are each equipped with a heat tracing apparatus.
4. The three-phase suspended bed in-line filtration system of claim 1, wherein the filter assembly comprises at least one vertically disposed tube filter, and a distributor is mounted at the general inlet of the filter assembly.
5. The in-line three-phase suspended bed filtration system of claim 4, wherein the candle filter is arranged in a central symmetry, the candle filter is a sintered metal mesh, a sintered metal powder filter element, a metal fiber membrane, a sintered metal felt, a laser perforated mesh, a wedge-shaped metal mesh, or a composite metal filter element, the candle filter has a diameter of 10-200mm and a length of 10-2000 mm.
6. The three-phase suspended bed in-line filtration system of claim 1, wherein the filtrate collection tank further comprises a weighing unit; and a release gas buffer tank comprising a wet flowmeter is arranged at the gas outlet of the filtrate collecting tank.
7. The three-phase suspended bed in-line filtration system of claim 1, wherein a blowdown line is provided between the suspended bed cylinder and the slurry tank.
8. The three-phase suspended bed online filtering system of claim 4, wherein the back-blowing unit performs back-blowing by a combination of gas isobaric back-blowing and liquid isobaric back-blowing, wherein the liquid volume used for the liquid isobaric back-blowing is 4-20 times of the volume of the tubular filter, the back-blowing frequency of the gas isobaric back-blowing is 2-15, and the duration of single back-blowing is 5-60 s.
9. The three-phase suspended bed online filter system of claim 1, wherein a gas-liquid separation tank is arranged between the tube side outlet of the circulating gas heat exchanger and the tube side inlet of the cooling water heat exchanger.
10. The in-line filtration system of claim 1, wherein a recycle gas buffer tank is provided before and after the recycle gas booster; and a defoaming net is arranged in the circulating gas buffer tank.
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| US5352610A (en) * | 1990-03-22 | 1994-10-04 | Braeutigam Hans Juergen | Tubular membrane assembly |
| CN1233453C (en) * | 2003-09-03 | 2005-12-28 | 上海兖矿能源科技研发有限公司 | Automatic filtering/back purging system liquid and solid separation for in three phase paste state bed reactor |
| CN101396647B (en) * | 2007-09-29 | 2011-03-16 | 中科合成油技术有限公司 | Gas-liquid-solid three-phase suspended bed reactor for f-t synthesis and use thereof |
| CN102626568A (en) * | 2012-04-13 | 2012-08-08 | 上海蓝科石化工程技术有限公司 | Product filtering system for three-phase slurry bed reactor |
| CN102698662B (en) * | 2012-06-01 | 2015-02-04 | 神华集团有限责任公司 | Slurry bed reactor |
| CN205570941U (en) * | 2016-04-18 | 2016-09-14 | 中国石油大学(华东) | Be applied to online cleaning equipment among mink cell focus suspension bed hydrocracking unit |
| CN107344035A (en) * | 2017-08-11 | 2017-11-14 | 中石化宁波工程有限公司 | A kind of continuous filtration system and filter method |
| CN108939661A (en) * | 2018-09-30 | 2018-12-07 | 陕西燎原净化设备有限公司 | A kind of cleaning of automatic on-line exempts to tear filter device open |
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