CN202725143U - Slurry bed reactor - Google Patents
Slurry bed reactor Download PDFInfo
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- CN202725143U CN202725143U CN 201220258572 CN201220258572U CN202725143U CN 202725143 U CN202725143 U CN 202725143U CN 201220258572 CN201220258572 CN 201220258572 CN 201220258572 U CN201220258572 U CN 201220258572U CN 202725143 U CN202725143 U CN 202725143U
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Abstract
The utility model provides a slurry bed reactor, comprising a reactor cylinder. A gas guiding into device is arranged on the lower portion of an inner cavity of the reactor cylinder. The inner cavity of the reactor cylinder is provided with Fischer Tropsch wax and a catalyst separation device. A Fischer Tropsch wax extraction and blowback system connected with the Fischer Tropsch wax and the catalyst separation device to extract Fischer Tropsch wax and to back wash the Fischer Tropsch wax and the catalyst separation device. The inner cavity of the reactor cylinder is provided with a gas-liquid separation device arranged above the Fischer Tropsch wax and the catalyst separation device. The slurry bed reactor decreases the gas volume entering the Fischer Tropsch wax and the catalyst separation device through the gas-liquid separation device, and therefore effectively prevents the gas from invading the surface of filtering medium and improves the active area of the filtering medium. At the same time, the slurry bed reactor also effectively prevents the gas from blowing dry channels of the filtering medium to cause catalyst granule to dry up on the filtering medium to reduce the permeability of the filtering medium.
Description
Technical field
The utility model relates to the synthetic field of Fischer-Tropsch, more specifically, relates to a kind of paste state bed reactor.
Background technology
In recent years, the global crude oil price is progressively soaring, and particularly in the country of some rich coal oil starvations, the energy technique of development Non oil-based route is subject to extensive concern.Synthetic synthesis gas (the H that refers to of Fischer-Tropsch
2+ CO) under the effect of catalyst, under suitable reaction temperature and reaction pressure, the course of reaction of synthetic hydrocarbon liquid fuel and high valuable chemicals.Coal or natural gas via Fischer-Tropsch synthesis are converted into high-quality liquid fuel and high valuable chemicals, not only reasonable, efficient, clean utilization coal resources, but also remedied the relative deficiency of petroleum resources, so that the Fischer-Tropsch synthetic technology becomes the effective way of substitute energy source for petroleum technology.
Follow the development of chemical industry, the fischer-tropsch synthesis process route has experienced fixed-bed process, Circulating Fluidized Bed Process, fixed fluidized bed technique and slurry attitude bed process.Compare fixed bed reactors, circulating fluid bed reactor and fixed fluidized-bed reactor, three phase slurry bed Fischer-Tropsch synthesis device is easy to realize the low temperature Fischer-Tropsch synthesis, have that reaction heat is easy to shift out, reaction temperature is even, the back-mixing degree is high, can load and unload online the advantages such as catalyst and production capacity are large, and three phase slurry bed fischer-tropsch synthesis process technology has obtained tremendous development.
For synthesis gas syrup state bed Fischer Tropsch synthetic reaction, carrying out along with reaction, constantly produce the hydrocarbon products of different chain length, the light hydrocarbons product enters the cold and hot high score in downstream and cold and hot low minute gas-liquid separation device with other Fischer-Tropsch synthetic and unreacted synthesis gas by reactor head, carry out gas-liquid separation, obtain light hydrocarbon products.And in the situation of the heavy hydrocarbon (Fischer-Tropsch wax) that fischer-tropsch reaction generates slurry catalyst concentration (reactor liquid level) certain limit within keeping reactor, must continuously from gas-liquid-solid three-phase slurry attitude bed, extract out, and then filter the qualified Fischer-Tropsch wax product of acquisition through essence.
But, the use of three phase slurry bed bioreactor has also brought new problem, in paste state bed reactor, the fischer-tropsch catalysts particle that 20 ~ 200 μ m are tiny and liquid hydrocarbon (Fischer-Tropsch wax) Product mix together, their effective separation is the technological difficulties of syrup state bed Fischer Tropsch synthesis technology development always.
Patent GB2403728A disclose a kind of outside the reactor of Fischer-Tropsch synthetic separating catalyst slurries filter method, but this process route is longer, and extract the conveying of suspension out and return paste state bed reactor and power that the catalyst slurry that is filtered is carried is all provided by pump from paste state bed reactor, very easily cause the breakage of catalyst granules in this process, difficulty and the gas solid separation load of liquid-solid separation have been increased, and need the regularly interior catalyst of post-reactor, thereby long operation brings inconvenience to reactor.
Patent CN1589957A discloses a kind of automatic fitration/backpurge system for the liquid-solid separation of three phase slurry bed bioreactor, its filter minute multilayer directly is placed in the reactor, under the effect of filtration pressure difference, gas-liquid is passed filter medium, enter liquid collection trough and carry out gas-liquid separation, obtain the Fischer-Tropsch wax product, the catalyst granules that is trapped within the filter medium outer surface is peeled off to the reactor slurry district through the timing backwash.As everyone knows, the syrup state bed Fischer Tropsch reactor is the gas-liquid-solid phase reaction device, and gas holdup is higher, and it is easy many that gas sees through filter medium than clear liquid, affected the clear liquid extraction, reduced effective utilization of filter filter area.Simultaneously, gas also can dry up the filter element duct, causes some catalyst granules to dry up in the filter element duct, has reduced the filter element permeability.In addition, synthesis gas is drawn reactor, and the synthesis gas effective rate of utilization reduces.Be trapped within the catalyst on filter medium surface, growth along with filtration time, the catalyst filter cake thickens, this system does not have effective way to slow down the degree that the catalyst filter cake thickens, can only could be with it from the filter medium sur-face peeling by compulsory backwash, can prolong backwashing time or increase the backwash frequency, cause clear liquid to find time shorten, reduce system effectiveness.
The utility model content
The utility model purpose is to provide a kind of filter blowback frequency few, and Fischer-Tropsch wax energy long period is stable effectively to be extracted out from reactor, realizes the paste state bed reactor of Fischer-Tropsch synthetic pulp state bed reactor stable and continuous operation.
The utility model provides a kind of paste state bed reactor, comprises reactor shell, and the bottom of the inner chamber of reactor shell is provided with gas leading-in device, is provided with Fischer-Tropsch wax and catalyst separation device in the inner chamber of reactor shell; The outer setting of reactor shell has and is communicated with to extract out Fischer-Tropsch wax with catalyst separation device with Fischer-Tropsch wax and the Fischer-Tropsch wax of Fischer-Tropsch wax and catalyst separation device backwash is extracted out and blowback system; Also be provided with the gas-liquid separation device of the top that is positioned at Fischer-Tropsch wax and catalyst separation device in the inner chamber of reactor shell.
Further, gas-liquid separation device comprises that gas-liquid revolves a minute separator, and gas-liquid is revolved a minute separator and comprised gas-liquid entrance, gaseous phase outlet and liquid outlet; The gas-liquid entrance is communicated with the inner chamber of reactor shell, and gaseous phase outlet is communicated with the gas outlet that is positioned at the reactor shell top, and liquid outlet extends to Fischer-Tropsch wax and catalyst separation device is inner.
Further, the top of reactor shell is provided with dividing plate, and gas-liquid is revolved the below that minute separator is arranged on dividing plate, and gaseous phase outlet extends to the top of dividing plate, and the gas-liquid entrance is positioned at the below of dividing plate.
Further, Fischer-Tropsch wax and catalyst separation device comprise slurries collector and the Fischer-Tropsch wax and the catalyst separator that are arranged on its lower end; Fischer-Tropsch wax and catalyst separator comprise the shell separator of tubulose and are arranged on a plurality of cross-flow filtration cores of shell separator inside.
Further, slurries collector bottom also is provided with the grout distribution device, and the grout distribution device comprises a plurality of taper grout distribution hole, each grout distribution hole and a corresponding setting of cross-flow filtration core.
Further, the cross-flow filtration core is interior cross-flow filtration core, and interior cross-flow filtration core inner is the slurries down going channel, forms the filtrate chamber between interior cross-flow filtration core outside and the shell separator; Each grout distribution hole and the coaxial setting of an interior cross-flow filtration core.
Further, the cross-flow filtration core is outer cross-flow filtration core, and outer cross-flow filtration core inner is the filtrate chamber, forms the slurries down going channel between outer cross-flow filtration core outside and the shell separator.
Further, three adjacent cross-flow filtration cores are triangularly arranged inner at shell separator in a plurality of cross-flow filtration cores.
Further, the slurries collector is tapered.
Further, the cross-flow filtration core is metal powder sintered filter element or woven wire sintered filter core or wedge shape filter core or multiple membrane type filter core, and its filter core precision is 0.5 ~ 100 micron.
Further, the gas-liquid liquid outlet that revolves minute separator is positioned at the slurries collector.
Further, also be provided with the air deflector that is positioned at Fischer-Tropsch wax and catalyst separation device bottom in the inner chamber of reactor shell; Air deflector comprises the section of being located thereon to the upper diversion division of the descending slurries water conservancy diversion of Fischer-Tropsch wax and catalyst separation device, and is positioned at its underpart to the lower diversion division of the slurries water conservancy diversion of air deflector bottom.
Further, the external diameter of air deflector is greater than the external diameter of Fischer-Tropsch wax and catalyst separation device.
Further, upper diversion division is " people " font along its axial cross section; Lower diversion division is " people " font of handstand along its axial cross section.
Further, Fischer-Tropsch wax and catalyst separation device and gas-liquid separation device are a plurality of, and the number of Fischer-Tropsch wax and catalyst separation device is greater than or equal to the number of gas-liquid separation device.
Further, the Fischer-Tropsch wax that each gas-liquid separation device is corresponding with it and the coaxial setting of catalyst separation device; A plurality of Fischer-Tropsch waxes and catalyst separation device are distributed on the reactor cross-section, perhaps uniform along a circumference in the reactor shell, perhaps uniform along the concentric circles contour of the two or more different radiis in the reactor shell, perhaps in the inner chamber of reactor shell along the vertical direction multilayer arrange.
Further, the top of Fischer-Tropsch wax and catalyst separation device is positioned at the following 1-15 rice of specified liquid level of the inner chamber of reactor shell.
Further, gas leading-in device comprises gas distributor, and gas distributor is positioned at the air deflector bottom; Gas distributor is the bottom of a pan disc type distributor or rung formula distributor or bubble cap distributor.
Further, paste state bed reactor also comprises single hop or the multistage heat production coil pipe that evenly is arranged on reactor shell inside, passes into deaerated water in the heat production coil pipe.
Further, Fischer-Tropsch wax is extracted out with blowback system and is comprised wax product surge tank and blowback medium surge tank; The pressure of wax product surge tank is lower than reactor shell internal pressure 0.1 ~ 0.5MPa; The pressure of blowback medium surge tank is higher than reactor shell internal pressure 0.3 ~ 0.8MPa; The blowback medium is the mixture of synthesis gas or nitrogen or the synthetic self-produced liquid wax of Fischer-Tropsch or above-mentioned substance.
According to paste state bed reactor of the present utility model, by above Fischer-Tropsch wax and catalyst separation device, gas-liquid separation device being set, reduce to enter the gas flow of Fischer-Tropsch wax and catalyst separation device, thereby prevent that effectively gas from occupying the filter medium surface, the effective area of raising filter medium.Simultaneously gas flow reduces, and has prevented effectively also that gas from drying up the duct of filter medium and the catalyst granules that causes dries up reduces the problem of filter medium permeability at filter medium.Moreover gas is by the gas-liquid separation device effective separation, thereby can get back to as soon as possible in the reactor recyclingly, improves the effective rate of utilization of synthesis gas.
Description of drawings
The accompanying drawing that consists of the application's a part is used to provide further understanding of the present utility model, and illustrative examples of the present utility model and explanation thereof are used for explaining the utility model, do not consist of improper restriction of the present utility model.In the accompanying drawings:
Fig. 1 is the system schematic according to paste state bed reactor of the present utility model;
Fig. 2 is the structural representation that revolves minute separator according to the gas-liquid of paste state bed reactor of the present utility model;
Fig. 3 is the structural representation according to the first embodiment of the Fischer-Tropsch wax of paste state bed reactor of the present utility model and catalyst separation device;
Fig. 4 is the schematic top plan view of Fig. 2;
Fig. 5 is the structural representation according to the second embodiment of the Fischer-Tropsch wax of paste state bed reactor of the present utility model and catalyst separation device; And
Fig. 6 is the structural representation according to the air deflector of paste state bed reactor of the present utility model.
The specific embodiment
Describe below with reference to the accompanying drawings and in conjunction with the embodiments the utility model in detail.
As shown in Figure 1, according to paste state bed reactor of the present utility model, comprising: reactor shell 10, the bottom of the inner chamber of reactor shell 10 is provided with gas leading-in device, is provided with Fischer-Tropsch wax and catalyst separation device 30 in the inner chamber of reactor shell 10; The outer setting of reactor shell 10 has and is communicated with to extract out Fischer-Tropsch wax with catalyst separation device 30 with Fischer-Tropsch wax and the Fischer-Tropsch wax of Fischer-Tropsch wax and catalyst separation device 30 backwashes is extracted out and blowback system 60; Also be provided with the gas-liquid separation device of the top that is positioned at Fischer-Tropsch wax and catalyst separation device 30 in the inner chamber of reactor shell 10.By the top at Fischer-Tropsch wax and catalyst separation device 30 gas-liquid separation device is set, reduces to enter the gas flow of Fischer-Tropsch wax and catalyst separation device 30, thereby prevent that effectively gas from occupying the filter medium surface, the effective area of raising filter medium.Simultaneously gas flow reduces, and has prevented effectively also that gas from drying up the duct of filter medium and the catalyst granules that causes dries up reduces the problem of filter medium permeability at filter medium.Moreover gas is by the gas-liquid separation device effective separation, thereby can get back to as soon as possible in the reactor recyclingly, improves the effective rate of utilization of synthesis gas.
As shown in Figure 2, gas-liquid separation device comprises that gas-liquid revolves minute separator 20, and gas-liquid is revolved minute separator 20 and comprised gas-liquid entrance 21, gaseous phase outlet 22 and liquid outlet 23; Gas-liquid entrance 21 is communicated with the inner chamber of reactor shell 10, and gaseous phase outlet 22 is communicated with the gas outlet b that is positioned at reactor shell 10 tops, and liquid outlet 23 is positioned at Fischer-Tropsch wax and catalyst separation device 30 inside.
Preferably, in conjunction with Fig. 1 and Fig. 2, be provided with dividing plate 11 on the top of reactor shell 10, the gas-liquid entrance 21 that gas-liquid is revolved minute separator 20 is arranged on dividing plate 11 bottoms, gaseous phase outlet 22 is arranged on dividing plate 11 tops, thereby make the gas-phase product effective separation behind the Fischer-Tropsch synthesis that gaseous phase outlet 22 discharges, and discharge reactor from the gas outlet b of reactor shell 10, enter next step separable programming.
As shown in Figure 3, Fischer-Tropsch wax and catalyst separation device 30 comprise slurries collector 31 and are arranged on Fischer-Tropsch wax and the catalyst separator 32 of its lower end, preferably, gas-liquid is revolved dipleg and Fischer-Tropsch wax and catalyst separation device 30 coaxial arrangement of minute separator 20, dipleg stretches into slurries collector 31 inside, thereby makes the slurries of discharging from dipleg liquid outlet 23 bottom directly enter slurries collector 31 inside.Reduce again collection process of slurries collector 31, increased the slurries amount of down going channel in Fischer-Tropsch wax and the catalyst separator 32, can increase circulation fluid speed to a certain extent, increase is washed away dynamics to the catalyst that is trapped in the filter medium surface, thereby can reduce the thickness of the filter cake on filter medium surface, the time interval that delayed blowback is washed, thus the stability that filters improved.
It is to discharge the restructuring of paste state bed reactor gas phase to divide and the small catalyst particles effective way that gas-liquid is revolved minute separator 20, in order to guarantee that revolving the slurries that minute separator 20 collects through gas-liquid directly enters in the slurries collector 31 of Fischer-Tropsch wax and catalyst separation device 30 as far as possible, the number that gas-liquid is revolved minute separator 20 is less than or equal to Fischer-Tropsch wax and catalyst separation device 30 numbers, be preferably and equal, namely each Fischer-Tropsch wax revolves minute separator 20 devices with catalyst separation device 30 corresponding gas-liquids.
Gas-liquid is revolved minute separator 20 can be taper, also can be the shape of other similar tapers, as be toroidal etc., all can meet the demands as long as slurries are played collecting action.
Fischer-Tropsch wax and catalyst separation device 30 are arranged on below the liquid level of reactor, evenly be arranged on the cross section of reactor shell 10 or the circumference of uniform one or two or a plurality of reactor shell 10 interior different radiis on.Fischer-Tropsch wax and catalyst separation device 30 are evenly arranged in reactor, avoid along with the fischer-tropsch reactor long-play as far as possible, and the phenomenon that product is more and more heavier in the reactor occurs.The top of Fischer-Tropsch wax and catalyst separation device 30 is positioned at the following 1-15 rice of specified liquid level of the inner chamber of reactor shell 10.
Shown in Fig. 3 to 5, the Fischer-Tropsch wax of Fischer-Tropsch wax and catalyst separation device 30 and catalyst separator 32 comprise the shell separator 32a of tubulose and are arranged on a plurality of cross-flow filtration core 32b of shell separator 32a inside, cross-flow filtration core 32b can be interior cross-flow filtration core, the cross-flow filtration core inner is slurries down going channel 32c namely, form filtrate chamber 32d between interior cross-flow filtration core outside and the shell separator 32a, Fischer-Tropsch wax enters filtrate chamber 32d by down going channel 32c by filter core.Filtrate chamber 32d extracts out with the Fischer-Tropsch wax that is positioned at the reactor cylinder external body and is communicated with blowback system 60, thereby extracts the Fischer-Tropsch wax among the filtrate chamber 32d out.
Shown in Fig. 3 and 4, when cross-flow filtration core 32b is interior cross-flow filtration core, also be provided with grout distribution device 33 between slurries collector 31 and Fischer-Tropsch wax and the catalyst separator 32, grout distribution device 33 comprises a plurality of taper grout distribution hole 33a, in each cross-flow filtration core 32b all with the coaxial setting of a grout distribution hole 33a, slurries descending from the 33a of grout distribution hole are directly entered among the down going channel 32c, can reduce pressure and slurry flow rate loss in the descending process, increase circulation fluid speed, increase and wash away dynamics to being trapped in the filter medium surface catalyst.
Preferably, three adjacent grout distribution hole 33a are triangularly arranged as much as possible, thereby the slurries that enter in each interior cross-flow filtration core are equated, and the less dead band of can trying one's best, and prevent that catalyst deposit is on taper grout distribution plate.
As shown in Figure 5, cross-flow filtration core 32b can be outer cross-flow filtration core, and outer cross-flow filtration core inner is filtrate chamber 32d, forms slurries down going channel 32c between outer cross-flow filtration core outside and the shell separator 32a.Three adjacent outer cross-flow filtration cores are triangular in shape as much as possible to be distributed in shell separator 32a inside, thereby makes the grout distribution in each outer cross-flow filtration core outside even, improves filter efficiency.
In conjunction with Fig. 1 and Fig. 6, also be provided with the air deflector 70 that is positioned at Fischer-Tropsch wax and catalyst separation device 30 bottoms in the inner chamber of reactor shell 10; Air deflector 70 comprises the section of being located thereon to the upper diversion division 71 of the descending slurries water conservancy diversion of Fischer-Tropsch wax and catalyst separation device 30, and is positioned at its underpart to the lower diversion division 72 of the slurries water conservancy diversion of air deflector 70 bottoms.The disk diameter of air deflector 70 is slightly larger than the external diameter of Fischer-Tropsch wax and catalyst separation device 30.
Upper diversion division 71 is " people " font along its axial cross section, slurries to Fischer-Tropsch wax and catalyst separation device 30 down going channel 32c outflow give suitable guide functions, lower diversion division 72 is " people " font of handstand along its axial cross section, one side can give in the reactor, the gas-liquid-solid three-phase slurries guide functions of air deflector bottom, most important is to prevent that gas from entering Fischer-Tropsch wax and catalyst separation device 30 down going channel 32c on the other hand, reduces gas to the negative effect of slurries speed among Fischer-Tropsch wax and the catalyst separation device 30 down going channel 32c.
As shown in Figure 1, the gas leading-in device that is positioned at reactor shell 10 bottoms comprises gas distributor 50, and gas distributor 50 is positioned at air deflector 70 bottoms, and gas distributor 50 is the bottom of a pan disc type distributor or rung formula distributor or bubble cap distributor.
Because Fischer-Tropsch synthesis is high exothermic reaction, the heat that needs in time inside to be produced shifts out, general single hop or multistage heat production coil pipe 40 by being arranged on reactor shell 10 inside, and the high temperature deaerated water is introduced by the e mouth, after equality of temperature absorbed fischer-tropsch reaction heat, steam water interface was drawn through the f mouth.
Fischer-Tropsch wax is extracted out with blowback system 60 and is comprised wax product surge tank 61 and blowback medium surge tank 62, the pressure setting of wax product surge tank 61 is lower than reactor pressure 0.1 ~ 0.5MPa, preferred 0.3 ~ 0.4MPa under the effect of pressure differential, is retracted in the wax product surge tank 61 Fischer-Tropsch wax automatically; Blowback medium surge tank 62 setting pressures are higher than reactor pressure 0.8 ~ 0.3MPa, and preferred 0.5MPa, blowback medium are the synthetic self-produced liquid wax of synthesis gas, nitrogen or Fischer-Tropsch.Finish each control valve action by the PLC/DCS filter, realize wax/catalyst effective separation.
Wax product surge tank 61 pressure are lower than reactor pressure 0.1 ~ 0.5MPa, i.e. the blowback of cross-flow filtration core 32b action pressure differential resetting 0.1 ~ 0.5MPa, preferred 0.3 ~ 0.5MPa.If blowback action pressure differential resetting is too high, when the formation filter cake is thicker, could closes clear liquid according to the PLC/DCS logic control program and extract sequencing valve 61a out, open backwash sequencing valve 62c, 32b carries out blowback to the cross-flow filtration core, because the thicker blowback effect of filter cake is relatively poor; Cross-flow filtration core 32b inside and outside differential pressure was set low, so that the blowback action is too frequent, the pulse cleaning that there is no need is crossed filter core, not only blowback air enters screen pipe, affect circulation liquid speed, also relatively shortened clear liquid and found time, reduced the effective rate of utilization of filter.
The pressure of blowback medium surge tank 62 must not be lower than reactor pressure 0.3MPa, but also must not be higher than reactor pressure 0.8MPa.The pressure setting of blowback medium surge tank 62 is too low, can not carry out effective backwash to cross-flow filtration core 32b, so that filter effect worsens, after wax is extracted out after a while, the cartridge surface filter cake is more and more thicker, during hyperfiltration in-core external differential setting value, according to PLC/DCS logic filter control program, close clear liquid and extract sequencing valve 61a out, open backwash sequencing valve 62c, 32b carries out frequent blowback to the cross-flow filtration core, and frequent blowback pressure is low, and power is little may not necessarily to reach backwash effect, a large amount of blowback airs enters screen pipe in addition, the inner serum density of screen pipe reduces, and can not form effective circulation with reactor, and filter effect can further worsen.Setting under the suitable blowback time, if blowback medium surge tank 62 pressure settings are higher, moment gives larger blowback pressure reduction of cross-flow filtration core 32b, may affect filter core service life, but under the limiting case also moment shrivel and damage cross-flow filtration core 32b, also can increase accuracy of manufacture difficulty and manufacturing cost even improve filer element strength.
Built-in filtration paste state bed reactor inner catalyst slurries running is as follows: synthesis gas enters paste state bed reactor from air inlet a through gas distributor 50 and moves upward, rely on its drag force drive paste state bed reactor inner catalyst slurries and walk around air deflector 70 upwards motion outside Fischer-Tropsch wax and catalyst separation device 30, when moving on the slurries collector 31 rim of a cup, the light components that unreacted synthesis gas and fischer-tropsch reaction generate is because of upwards operation of the little continuation of its density, revolves minute separator 20 and carries out gas-liquid separation until enter gas-liquid; And heavier catalyst slurry is introduced into more greatly the slurries collector 31 of taper because of its density, directly enter the down going channel 32c of Fischer-Tropsch wax and catalyst separation device 30 from liquid outlet 23 from slurries collector 31 through the slurries of gas-liquid separation, form density contrast at Fischer-Tropsch wax and catalyst separation device 30 inside and outside catalyst slurries thus, form paste state bed reactor and Fischer-Tropsch wax and catalyst separation device 30 interior circulation.Fischer-Tropsch wax and catalyst separation device 30 inside and outside catalyst slurry density contrasts are larger, circulation fluid speed is larger, just stronger to crossing the cartridge surface scouring force, it is just thinner to cross cartridge surface catalyst filter cake, it is just fewer to cross filter core backwash number of times, Fischer-Tropsch wax is found time more long, and unit filter core area output is just larger.Gas holdup is lower in the down going channel 32c of Fischer-Tropsch wax and catalyst separation device 30, is conducive to the normal performance of filter element filtering function.Paste state bed reactor and Fischer-Tropsch wax and catalyst separation device 30 interior circulation not only can reduce the filter number of units, increase paste state bed reactor and effectively utilize the space, also can strengthen slurries back-mixing degree in the paste state bed reactor, strengthen being considered to the mass-transfer progress of paste state bed reactor weakness always, and so that reactor slurry concentration is more even, temperature is homogeneous more.In addition paste state bed reactor inner catalyst concentration of slurry homogeneous, temperature homogeneous, heat production coil pipe can be established two sections, but single hop is uniformly distributed in some waxes/catalyst separator gap.
Preferably embodiment is as described below according to the utility model, synthesis gas is entered through gas distributor 50 by the introducing of a mouth and is marked with finite concentration, in the paste state bed reactor of certain liquid level catalyst slurry, under certain fischer-tropsch reaction temperature and pressure, react, the light petroleum gas that generates, unreacted synthesis gas and small part heavy hydrocarbon revolve a minute separator gas-liquid entrance 21 by gas-liquid and enter gas-liquid and revolve minute separator 20, after gas-liquid separation, the gas phase part is drawn by gaseous phase outlet 22, anti-device top gas outlet b discharges from slurry attitude bed, enter subsequent separation system, separate, obtain light oil, mink cell focus and Fischer-Tropsch synthetic water.
The Fischer-Tropsch wax that generates in the paste state bed reactor, under the effect of filtration pressure difference, pass cross-flow filtration core 32b by the down going channel 32c of Fischer-Tropsch wax and catalyst separation device 30 and enter filtrate chamber 32d, enter wax product surge tank 61 by filtrate chamber 32d through clear liquid extraction sequencing valve 61a and reactor fluid level control valve 61b again, wax product surge tank pressure is regulated by round trip control valve 61c, stablizes thus the clear liquid filtration pressure difference.
Introduce blowback medium surge tank 62 from compressor blowback synthesis gas through replenishing gas sequencing valve 62a, utilize the round trip control valve 62b of blowback medium surge tank 62 to stablize the pressure of blowback medium surge tank, provide one to stablize strong backwash power for Fischer-Tropsch wax and catalyst separation device 30 thus; When Fischer-Tropsch wax and catalyst separation device 30 needed backwash, blowback air sequencing valve 62c opened, and instantaneous Fischer-Tropsch wax and the catalyst separation device 30 of entering of the synthesis gas of uniform temperature, certain pressure carries out backwash regeneration to cross-flow filtration core 32b.
Paste state bed reactor three-phase slurries district, the down going channel 32c of Fischer-Tropsch wax and catalyst separation device 30 and air deflector 70 form circulation by the mode of cross-flow filtration, the motive force of the drag force that the synthesis gas that utilization enters paste state bed reactor upwards makes progress to catalyst slurry and the down going channel 32c inner and outer ring logistics density contrast formation of Fischer-Tropsch wax and catalyst separation device 30 realizes the circulation process, continuously the catalyst that is trapped in cross-flow filtration core 32b surface is washed away, filter filter cake and keep thinner state, reduce the backwash frequency, prolong clear liquid and find time, this also is that waxy stone can be continually from the prerequisite of Fischer-Tropsch wax with catalyst separation device 30 extractions.
Fischer-Tropsch wax extraction automatic backflushing washing procedure goes round and begins again through PLC/DCS and repeatedly moves, and each filter is carried out the reasonable arrangement clear liquid extract out and the blowback time.Reaction heat is shifted out by the deaerated water that has certain saturated vapor pressure in the heat production coil pipe, utilize the utility model paste state bed reactor to finish Fischer-Tropsch wax extraction in the device, control reactor liquid level is stablized temperature of reactor, is fischer-tropsch reaction device long period steady running effective ways.
5.8 meters of the internal diameters of the reactor shell 10 of the built-in filtration paste state bed reactor of the utility model, 42 meters of the tangent line height of reactor shell 10, normal paste state bed reactor liquid level (specified liquid level) is controlled in 30 ± 2 meters scopes, 5 meters arrange 12 of built-in Fischer-Tropsch wax and catalyst separation devices under the paste state bed reactor liquid level, uniform on 1.2 meters circumferences of reactor shell, every Fischer-Tropsch wax and 50 millimeters 12 18 meters long cross-flow filtration core 32b of catalyst separation device 30 interior installation Φ, on the paste state bed reactor dividing plate, revolve minute separator 20 with wax/12 gas-liquids of catalyst filter coaxial arrangement, the dipleg that gas-liquid is revolved minute separator 20 stretches in the slurries collector 31 of taper, 0.5 ~ 1 meter of down going channel 32c outlet apart from Fischer-Tropsch wax and catalyst separation device 30 arranges air deflector 70, at air deflector 70 lower gas distributors 50.Paste state bed reactor heat production coil pipe 40 is distributed in the annular space reactor slurry district of Fischer-Tropsch wax and catalyst separation device 30.
Hydrogen and carbon monoxide mix by certain hydrogen-carbon ratio, as fischer-tropsch reaction raw material---synthesis gas, a certain amount of synthesis gas is through being heated to 235 ~ 250 ℃, adjust pressure to 2.8 ~ 3.5MPa and spray into paste state bed reactor slurries district by paste state bed reactor entrance a through gas distributor 50, under the effect of gas-liquid-solid three-phase slurries district fischer-tropsch synthetic catalyst, Fischer-Tropsch synthesis occurs, the light components that generates and unreacted synthesis gas revolve through gas-liquid discharges from paste state bed reactor gaseous phase outlet b after minute separator 20 purifies, entering follow-up cold and hot high-low pressure piece-rate system separates, obtain light oil, mink cell focus, Fischer-Tropsch synthetic water and uncondensable exhaust gas, the sub-fraction of exhaust gas is as the tail gas discharger, most ofly is back to reactor inlet through recycle compressor and again participates in Fischer-Tropsch synthesis and carry out recycling.Fischer-Tropsch wax utilizes the mode of cross-flow filtration in the down going channel 32c of Fischer-Tropsch wax and catalyst separation device 30, keep less catalyst filter cake thickness, under filtration pressure difference (reactor slurry district pressure and wax product surge tank pressure differential) 0.3 ~ 0.4MPa promotes, pass cross-flow filtration core 32b and enter filtrate chamber 32d, enter wax product surge tank 61 by filtrate chamber 32d through clear liquid extraction sequencing valve 61a and reactor fluid level control valve 61b again, wax product surge tank pressure is regulated by round trip control valve 61c, stablizes thus the clear liquid filtration pressure difference.
When filtering pressure reduction and reach the upper limit or program and need carry out the filter core backwash, blowback air sequencing valve 62c opens, and instantaneous Fischer-Tropsch wax and the catalyst separation device 30 of entering of the synthesis gas of uniform temperature, certain pressure carries out backwash to cross-flow filtration core 32b and regenerate.After backwash finishes, be used to introduce blowback medium surge tank 62 from compressor blowback synthesis gas through replenishing gas sequencing valve 62a, it is carried out supplementary pressure, be kept above reactor pressure 0.8 ~ 0.3MPa, preferred 0.5MPa, utilize blowback medium surge tank round trip control valve 62b to stablize blowback medium surge tank pressure, provide one to stablize strong backwash power for Fischer-Tropsch wax and catalyst separation device 30 thus.Extract the automatic backflushing washing procedure out through the PLC/DCS repeatedly operation that goes round and begins again by wax, each filter reasonable arrangement clear liquid is extracted out and the blowback time, Fischer-Tropsch wax is extracted out in reactor endlessly, the reactor liquid level is effectively controlled, and built-in filtration paste state bed reactor obtains the long period steady running.
Fischer-tropsch reaction heat shifts out in the paste state bed reactor, it also is the most important important the key link of design paste state bed reactor, heat production coil pipe entrance e is by the deaerated water of introducing with paste state bed reactor reaction temperature uniform temp, take full advantage of the gasification latent heat of water, gas-vapor mix drains into drum by heat production coil pipe outlet f, by the drum exhaust steam, shift out reaction heat, the thermal source that institute's producing steam can be used as other facilities is used.The large calorimetric that the fischer-tropsch reaction of strong heat release produces is effectively shifted out by equality of temperature saturated vapor setting-out.
As can be seen from the above description, the utility model the above embodiments have realized following technique effect:
According to paste state bed reactor of the present utility model, by the top at Fischer-Tropsch wax and catalyst separation device gas-liquid separation device is set, reduce to enter the gas flow of Fischer-Tropsch wax and catalyst separation device, thereby prevent that effectively gas from occupying the filter medium surface, the effective area of raising filter medium.Simultaneously gas flow reduces, and has prevented effectively also that gas from drying up the duct of filter medium and the catalyst granules that causes dries up reduces the problem of filter medium permeability at filter medium.Moreover gas is by the gas-liquid separation device effective separation, thereby can get back to as soon as possible in the reactor recyclingly, improves the effective rate of utilization of synthesis gas.Bottom at Fischer-Tropsch wax and catalyst separation device arranges air deflector, has prevented that effectively synthesis gas from entering down going channel from the bottom, disturbs filtering to form.
The above is preferred embodiment of the present utility model only, is not limited to the utility model, and for a person skilled in the art, the utility model can have various modifications and variations.All within spirit of the present utility model and principle, any modification of doing, be equal to replacement, improvement etc., all should be included within the protection domain of the present utility model.
Claims (20)
1. paste state bed reactor comprises:
Reactor shell (10), the bottom of the inner chamber of described reactor shell (10) is provided with gas leading-in device, is provided with Fischer-Tropsch wax and catalyst separation device (30) in the inner chamber of described reactor shell (10);
The outer setting of described reactor shell (10) has and is communicated with to extract Fischer-Tropsch wax out with catalyst separation device (30) with described Fischer-Tropsch wax and the Fischer-Tropsch wax of described Fischer-Tropsch wax and catalyst separation device (30) backwash is extracted out and blowback system (60);
It is characterized in that, also be provided with the gas-liquid separation device of the top that is positioned at described Fischer-Tropsch wax and catalyst separation device (30) in the inner chamber of described reactor shell (10).
2. paste state bed reactor according to claim 1 is characterized in that,
Described gas-liquid separation device comprises that gas-liquid revolves a minute separator (20), and described gas-liquid is revolved a minute separator (20) and comprised gas-liquid entrance (21), gaseous phase outlet (22) and liquid outlet (23);
Described gas-liquid entrance (21) is communicated with the inner chamber of reactor shell (10), described gaseous phase outlet (22) is communicated with the gas outlet (b) that is positioned at described reactor shell (10) top, and described liquid outlet (23) extends to described Fischer-Tropsch wax and catalyst separation device (30) inside.
3. paste state bed reactor according to claim 2 is characterized in that,
The top of described reactor shell (10) is provided with dividing plate (11), described gas-liquid is revolved the below that a minute separator (20) is arranged on described dividing plate, and described gaseous phase outlet (22) extends to the top of described dividing plate (11), and described gas-liquid entrance (21) is positioned at the below of described dividing plate (11).
4. paste state bed reactor according to claim 2 is characterized in that,
Described Fischer-Tropsch wax and catalyst separation device (30) comprise slurries collector (31) and are arranged on Fischer-Tropsch wax and the catalyst separator (32) of its lower end;
Described Fischer-Tropsch wax and catalyst separator (32) comprise the shell separator (32a) of tubulose and are arranged on the inner a plurality of cross-flow filtration cores (32b) of described shell separator (32a).
5. paste state bed reactor according to claim 4 is characterized in that,
Described slurries collector (31) bottom also is provided with grout distribution device (33), described grout distribution device (33) comprises a plurality of taper grout distribution holes (33a), each described grout distribution hole (33a) and the corresponding setting of a described cross-flow filtration core (32b).
6. paste state bed reactor according to claim 5 is characterized in that,
Described cross-flow filtration core (32b) is interior cross-flow filtration core, and described interior cross-flow filtration core inner is slurries down going channel (32c), forms filtrate chamber (32d) between described interior cross-flow filtration core outside and the described shell separator (32a);
Each described grout distribution hole (33a) and the coaxial setting of a described interior cross-flow filtration core.
7. paste state bed reactor according to claim 4 is characterized in that,
Described cross-flow filtration core (32b) is outer cross-flow filtration core, and described outer cross-flow filtration core inner is filtrate chamber (32d), forms slurries down going channels (32c) between described outer cross-flow filtration core outside and the described shell separator (32a).
8. paste state bed reactor according to claim 4 is characterized in that,
Adjacent three described cross-flow filtration cores (32b) are triangularly arranged in described shell separator (32a) inside in a plurality of described cross-flow filtration cores (32b).
9. paste state bed reactor according to claim 4 is characterized in that, described slurries collector (31) is tapered.
10. paste state bed reactor according to claim 4 is characterized in that,
Described cross-flow filtration core (32b) is metal powder sintered filter element or woven wire sintered filter core or wedge shape filter core or multiple membrane type filter core, and its filter core precision is 0.5～100 micron.
11. paste state bed reactor according to claim 4 is characterized in that,
The liquid outlet (23) that described gas-liquid is revolved a minute separator (20) is positioned at described slurries collector (31).
12. paste state bed reactor according to claim 1 is characterized in that,
Also be provided with the air deflector (70) that is positioned at described Fischer-Tropsch wax and catalyst separation device (30) bottom in the inner chamber of described reactor shell (10);
Described air deflector (70) comprises the section of being located thereon to the upper diversion division (71) of the descending slurries water conservancy diversion of described Fischer-Tropsch wax and catalyst separation device (30), and is positioned at its underpart to the lower diversion division (72) of the slurries water conservancy diversion of described air deflector (70) bottom.
13. paste state bed reactor according to claim 12 is characterized in that, the external diameter of described air deflector (70) is greater than the external diameter of described Fischer-Tropsch wax and catalyst separation device (30).
14. paste state bed reactor according to claim 12 is characterized in that,
Described upper diversion division (71) is " people " font along its axial cross section;
Described lower diversion division (72) is " people " font of handstand along its axial cross section.
15. each described paste state bed reactor in 14 is characterized in that according to claim 1,
Described Fischer-Tropsch wax and catalyst separation device (30) and described gas-liquid separation device are a plurality of, and the number of described Fischer-Tropsch wax and catalyst separation device (30) is greater than or equal to the number of described gas-liquid separation device.
16. paste state bed reactor according to claim 15 is characterized in that,
Described Fischer-Tropsch wax and the coaxial setting of catalyst separation device (30) that each described gas-liquid separation device is corresponding with it; A plurality of described Fischer-Tropsch waxes and catalyst separation device (30) are distributed on the reactor cross-section, perhaps uniform along a circumference in the reactor shell (10), perhaps the concentric circles contour of the two or more different radiis in the reactor shell (10) is uniform, perhaps in the inner chamber of reactor shell (10) along the vertical direction multilayer arrange.
17. paste state bed reactor according to claim 16 is characterized in that,
The top of described Fischer-Tropsch wax and catalyst separation device (30) is positioned at the following 1-15 rice of specified liquid level of the inner chamber of reactor shell (10).
18. paste state bed reactor according to claim 12 is characterized in that,
Described gas leading-in device comprises gas distributor (50), and described gas distributor (50) is positioned at described air deflector (70) bottom;
Described gas distributor (50) is the bottom of a pan disc type distributor or rung formula distributor or bubble cap distributor.
19. paste state bed reactor according to claim 1 is characterized in that,
Described paste state bed reactor also comprises single hop or the multistage heat production coil pipe (40) that evenly is arranged on described reactor shell (10) inside, and described heat production coil pipe passes into deaerated water in (40).
20. paste state bed reactor according to claim 1 is characterized in that,
Described Fischer-Tropsch wax is extracted out with blowback system (60) and is comprised wax product surge tank (61) and blowback medium surge tank (62);
The pressure of described wax product surge tank (61) is lower than reactor shell (10) internal pressure 0.1～0.5MPa;
The pressure of described blowback medium surge tank (62) is higher than reactor shell (10) internal pressure 0.3～0.8MPa;
The blowback medium is synthesis gas or nitrogen or the synthetic self-produced liquid wax of Fischer-Tropsch.
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| CN 201220258572 CN202725143U (en) | 2012-06-01 | 2012-06-01 | Slurry bed reactor |
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| CN 201220258572 CN202725143U (en) | 2012-06-01 | 2012-06-01 | Slurry bed reactor |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102698662A (en) * | 2012-06-01 | 2012-10-03 | 神华集团有限责任公司 | Slurry bed reactor |
| CN103769008A (en) * | 2014-02-12 | 2014-05-07 | 中国科学院上海高等研究院 | Inner circulation flow reactor of slurry reactor |
| CN104043291A (en) * | 2013-03-11 | 2014-09-17 | 神华集团有限责任公司 | Diversion-type gas-liquid separation unit, gas-liquid separation device and multi-phase flow reactor |
| CN104789253A (en) * | 2015-04-20 | 2015-07-22 | 神华集团有限责任公司 | Coal liquefaction reactor and coal liquefaction production system |
| US10035120B2 (en) | 2014-10-31 | 2018-07-31 | Sabic Global Technologies B.V. | Reactors for separating wax products from lightweight gaseous products of a reaction |
| CN110591763A (en) * | 2019-09-10 | 2019-12-20 | 南京延长反应技术研究院有限公司 | Intelligent enhanced control system and process for coal indirect liquefaction |
| US10525427B2 (en) | 2014-10-30 | 2020-01-07 | Sabic Global Technologies B.V. | Reactor comprising radially placed cooling plates and methods of using same |
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2012
- 2012-06-01 CN CN 201220258572 patent/CN202725143U/en not_active Expired - Lifetime
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102698662A (en) * | 2012-06-01 | 2012-10-03 | 神华集团有限责任公司 | Slurry bed reactor |
| CN102698662B (en) * | 2012-06-01 | 2015-02-04 | 神华集团有限责任公司 | Slurry bed reactor |
| CN104043291A (en) * | 2013-03-11 | 2014-09-17 | 神华集团有限责任公司 | Diversion-type gas-liquid separation unit, gas-liquid separation device and multi-phase flow reactor |
| CN103769008A (en) * | 2014-02-12 | 2014-05-07 | 中国科学院上海高等研究院 | Inner circulation flow reactor of slurry reactor |
| CN103769008B (en) * | 2014-02-12 | 2016-01-20 | 中国科学院上海高等研究院 | Slurry bed system common loop reactor |
| US10525427B2 (en) | 2014-10-30 | 2020-01-07 | Sabic Global Technologies B.V. | Reactor comprising radially placed cooling plates and methods of using same |
| US10035120B2 (en) | 2014-10-31 | 2018-07-31 | Sabic Global Technologies B.V. | Reactors for separating wax products from lightweight gaseous products of a reaction |
| CN104789253A (en) * | 2015-04-20 | 2015-07-22 | 神华集团有限责任公司 | Coal liquefaction reactor and coal liquefaction production system |
| CN110591763A (en) * | 2019-09-10 | 2019-12-20 | 南京延长反应技术研究院有限公司 | Intelligent enhanced control system and process for coal indirect liquefaction |
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