CN101890324A - Reactor used in crude gas variable-temperature reaction process - Google Patents
Reactor used in crude gas variable-temperature reaction process Download PDFInfo
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- CN101890324A CN101890324A CN2010100040903A CN201010004090A CN101890324A CN 101890324 A CN101890324 A CN 101890324A CN 2010100040903 A CN2010100040903 A CN 2010100040903A CN 201010004090 A CN201010004090 A CN 201010004090A CN 101890324 A CN101890324 A CN 101890324A
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Abstract
The invention relates to a reactor used in a crude gas variable-temperature reaction process. A centripetal radial reactor structure is adopted and a discharging inner pipe constant-temperature material passage is used. When the reaction component content of the crude gas serving as a raw material fluctuates in a certain range, the temperature distribution on the wall of the reactor still has high uniformity and stability so that the safety of equipment can be enhanced remarkably; the distribution uniformity of reaction material flow in a catalyst bed layer can be enhanced, so that the reaction efficiency is improved; and the dirty accommodating capacity of a catalyst can be brought into full play and running period can be prolonged by using the characteristic that the filling amount of catalyst bed layers with equal thickness in a centripetal direction changes from large to small. The reactor is particularly suitable for oxygen removal and/or a crude gas processing process for preparing hydrogen from carbon monoxide.
Description
Technical field
The present invention relates to a kind of used in crude gas variable-temperature reaction process radial inflow radial reactor.
Background technology
Raw coke oven gas of the present invention, typically refer to the gas of forming by hydrogen, carbon monoxide and other component (such as oxygen) from pyrolysis of coal (destructive distillation) process or other process, typical raw coke oven gas composition sees Table 1, and its temperature is generally normal temperature, pressure is pressure-fired.Since the unstable characteristics of charging that pyrolysis of coal (destructive distillation) process is intrinsic, all fluctuations within the specific limits of oxygen content and carbon monoxide content in the raw coke oven gas.
The volume content of the typical raw coke oven gas of table 1, %v
| The component sequence number | Component | Raw coke oven gas A | Raw coke oven gas B |
| 1 | H 2 | 30.30 | 14.52 |
| 2 | CH 4 | 7.48 | 2.48 |
| 3 | C 2H 6 | 0.00 | 0.16 |
| 4 | C 2H 4 | 0.87 | 0.09 |
| 5 | C 3H 8 | 0.03 | |
| 6 | I-C 4H 10 | ||
| 7 | n-C 4H 10 | ||
| 8 | CO 2 | 7.63 | 11.12 |
| 9 | CO | 12.87 | 14.92 |
| 10 | N 2 | 32.68 | 49.13 |
| 11 | O 2 | 0.69 | 0.07 |
| 12 | H 2O | 7.48 | 7.48 |
| 13 | Tar, naphthalene | Trace | Trace |
| Add up to | 100.00 | 100.00 |
In many occasions, form according to raw coke oven gas, need to its handle with remove in the raw coke oven gas oxygen and or finish carbon monodixe conversion hydrogen manufacturing, usually the unstripped gas or chemical industry synthetic raw gas or the fuel gas etc. that after the condensation cooled dehydrated, can be used as transformation absorption purifying hydrogen of hydrogen through the reaction effluent that this process obtains, exothermic reaction takes place and causes remarkable temperature rise in this process usually, reactor of the present invention is this process reactor, can certainly be used for raw coke oven gas hypothermic response process.
(pressure is to carry out under 0.3～2.0MPa) to known crude gas exothermic reaction process usually at pressurized conditions, usually the oxygen component transforms (gas-phase reaction: oxygen and hydrogen reaction generate gas water) 0.1% (volume) and can produce 10～12 ℃ even bigger temperature rise, usually the carbon monoxide component transforms (gas-phase reaction: carbon monoxide and water reaction generate carbon dioxide and hydrogen) 1% (volume) and can produce 9～11 ℃ even bigger temperature rise, the oxygen component transforms (gas-phase reaction: oxygen and hydrogen reaction generate gas water) 0.8% (volume) can produce 80～96 ℃ even bigger temperature rise, the carbon monoxide component transforms (gas-phase reaction: carbon monoxide and water reaction generate carbon dioxide and hydrogen) 12% (volume) can produce 108～132 ℃ even bigger temperature rise, that is to say that the temperature rise that the fuel factor of raw coke oven gas course of reaction causes is significant, and temperature rise concentrates on the front portion (but because concentration of reactants is the highest in the fresh feed) in the beds relatively.Known crude gas exothermic reaction process reactor is the axial restraint bed bioreactor, reaction mass passes through beds vertically, the problem that this version exists is: the temperature rise that the fuel factor of raw coke oven gas course of reaction causes directly influences wall of reactor, front portion in beds forms violent Temperature Distribution, if adopt the dilute catalyst activity methods, then increase catalyst volume, increase equipment volume, increase bed layer pressure and fall.Again because the equal ripple within the specific limits of oxygen content and carbon monoxide content in the raw coke oven gas, the wall of reactor temperature is in fluctuation, usually the oxygen content fluctuation can reach 0.4% (volume), the carbon monoxide content fluctuation can reach 5% (volume), the temperature rise fluctuating range can reach 40～50 ℃ even bigger), total overall reaction process temperature rise fluctuating range can reach 80～100 ℃ even bigger, and the temperature alternating process has reduced reactor lifetime.Again since the ratio of height to diameter of this reactor catalyst bed (the beds diameter: the catalyst bed layer height) less usually, reaction mass is difficult to be guaranteed by the uniformity of beds.Therefore, require the suitable reactor of a kind of structure of design, solve wall of reactor temperature fluctuation problem.
Radial reactor is owing to its high flux, low pressure degradation characteristic are widely used in fields (such as being the gasoline catalyzing reforming process) such as petrochemical industry, chemical synthesis, the energy, environment, radial reactor is pursued the uniformity of reaction logistics along the reactor axial distribution, in the hope of the reaction effect of the best.
Fig. 1 is a kind of structural representation of the radial reactor of catalytic reforming reaction process that is used for fixing, and it comprises: charging aperture (101), charging inner tube head distributor (102), sector drum (103), catalyst bed (104), central tube (105), expansion loop (106), movable calotte (107), discharging opening (108), catalyst discharge port (109) and porcelain ball layer (110) etc.Catalyst is seated in the annular space between central tube (105) and the sector drum (103), filling porcelain ball or dead catalyst above the beds, filling porcelain ball below the bed, oil gas enters through feed distributor from upper entrance, by around behind the sector drum radial flow through beds, enter central tube after reacting with catalyst, flow out from the central tube bottom at last.Reactor center is provided with a central tube, at wall some sector drums (or large-scale outside screen cloth) and their connector is set, and realizes that oil gas radially evenly flows.
Fig. 2 is a kind of radial reactor central tube, and it is by perforate cylinder (201), outer net (203) (kalamein silk screen or welding wedge wire screen net) and connector supporting seat (202), cover plate (204), hanger (205) etc. are formed up and down.Internal openings cylinder (201) forms with the thick stainless steel coiled sheet weldering of 6mm usually, bears the hydrostatic head of the accumulation quality generation of beds pressure reduction and catalyst.Inner cylinder is offered the aperture of certain area according to technological requirement, produces certain pressure drop during the air communication small holes, and the size in hole, quantity and layout are that evenly whether the realization response logistics flow in beds, the fine or not key of reaction effect.To fixed bed reforming reactor radially, central tube perforate cylinder is outer can covered with gold leafly to belong to silk screen, also can wrap welding wedge wire screen net, and main purpose is to prevent that catalyst runs off from central tube.Early stage central tube all is the kalamein silk screen, and its makes simple, low price, but low, the easy obstruction of intensity, fragile, catalyst are easily run off.The central tube perforate cylinder silk screen that belongs to substantially no longer covered with gold leaf outward replaces but weld the wedge wire screen net with one deck at present.When adopting outsourcing welding wedge wire screen net, note that slit (or perforate) direction of welding wedge wire screen net must be consistent with the flow direction of catalyst, to reduce the obstruction and the wearing and tearing of catalyst.In addition, the support bar of welding wedge wire screen net must stagger mutually with the aperture on the internal openings cylinder, must not block the aperture on the inner core.
Use the radial reactor of sector drum (103), the periphery of radial reactor has the some sector drums of even layout or the outer two kinds of forms of screen cloth of a major diameter is installed.Sector drum can be put into or take out from the reactor head manhole, is convenient to maintenance and replacing, but between two adjacent sector drums a slight dead angle is arranged, and is unfavorable for flowing of oil gas and catalyst.The outer screen cloth of major diameter can not take out in reactor, welding reactor top end socket will be packed reactor at last before the weld seam into cylindrical shell in, make troubles to manufacturing, in a single day damage in the use and be difficult to repair, this is a more serious defective, but it helps evenly flowing of oil gas and catalyst in the bed.In fixed bed and CONTINUOUS REFORMER radial reactor, what generally adopt is sector drum, only adopts the outer screen cloth of major diameter, the existing sector drum of also using instead in certain company of France continuous reforming reactor in the past.Sector drum has two kinds of versions, and the one, form with the thick punching of the steel plate of 1.2m (or 1.5mm), the one, make with welding wedge wire screen net.The punched-plate manufacturing is easier to, and uses more generally, and the manufacturing of welding wedge wire screen net is difficult slightly, uses lessly, but good rigidly, percent opening are big, can reduce catalyst abrasion and flow resistance.With the sector drum that corrosion resistant plate is made, towards plurality of rows, every row is the strip hole (each round heart is apart from being 3.2mm) of 16 long 13mm, wide 1.0mmm in the aperture area domestic demand, and punching quantity is very big, and the punching tolerance is tighter.For preventing that catalyst from flowing into sector drum behind, requires will post between sector drum back and the wall.For this reason, linearity, torsion resistance and back shape to sector drum all have strict requirement, continuous reforming reactor sector drum particularly, the top also has riser and the sealing plate or the special-purpose hermetically-sealed construction of D font, the fit clearance of the former riser and sealing plate and tolerance strictness are special constructions that manufacture difficulty is big.
Use the radial reactor of the outer screen cloth of major diameter, the basic building block of the outer screen cloth of its major diameter is a welding wedge wire screen net, and outer screen cloth slit is even, bright and clean smooth with the catalyst contact-making surface, screen cloth slit direction is consistent with the mobile direction of catalyst, helps catalyst and flows, and can reduce catalyst abrasion.The outer screen cloth of major diameter is because diameter is big, and rigidity is less relatively, and the assembling that is shaped is difficult, the bad control of dimensional tolerance, and manufacture difficulty is big.Welding wedge wire screen net is to be formed by Contact welding weldering system on the screen cloth bonding machine of a special use by support bar and V-arrangement grating.It has that any surface finish is smooth, the slit is even, percent opening is big, joint is firm, mechanical strength is high, good rigidly, characteristics such as be difficult for stopping up, not yielding.
A kind of continuous reforming reactor is the eclipsed form reactor, each reactor internals is formed by a central tube, 8～15 catalyst transports, the cover plate that is arranged in some sector drums of wall and is connected central tube and sector drum, oil gas enters from reactor inlet, flow in the sector drum equably by the sector drum top D font riser that is arranged in wall, radial flow is crossed beds then, enter central tube, flow out from the outlet of reactor top.In addition, also be provided with a chuck in central tube upper expansion joint outside, peripheral direction is offered some passages on chuck top, chuck bottom (being positioned under the cover plate) is the cylinder of making of welding wedge wire screen net, sub-fraction oil gas enters the passage on the chuck, welding wedge wire screen net from the cover plate bottom enters beds again, prevents that catalyst from assembling to central tube, forms the dead band.On the central tube of the last reactor of eclipsed form continuous reforming reactor, also increased the thick punched-plate that dashes full strip hole of one deck 1.2mm between welding wedge wire screen net and the internal openings cylinder, in case, avoid catalyst to flow to compressor or the product through oil gas vent from the central tube of the last reactor to prevent welding wedge wire screen network loss bad time.At this moment, during perforated area on determining central tube internal openings cylinder, should consider owing to blocked by middle punched-plate and the bilayer that welds the wedge wire screen net and to want corresponding increasing.
A kind of used in crude gas variable-temperature reaction process radial reactor of the present invention, one of its purpose is to improve reactive component in the uniformity of wall of reactor Temperature Distribution, particularly the raw material raw coke oven gas (such as oxygen and or carbon monoxide), and the wall of reactor Temperature Distribution still had the high uniformity and stability when content fluctuateed within the specific limits, thus the stability and the security of the operating process of the equipment of assurance.
A kind of used in crude gas variable-temperature reaction process radial reactor of the present invention, two of its purpose are to improve the uniformity that the reaction logistics distributes along beds, thereby improve the course of reaction conversion ratio.
Micro-tar, naphthalene etc. can coking cause catalyst to hinder inactivation gradually in operating process in the raw coke oven gas raw material, and the present invention is along Flow of Goods and Materials direction (radial centripetal direction), the loadings of equal thickness beds is by greatly to little variation, a kind of used in crude gas variable-temperature reaction process radial reactor of the present invention, three of its purpose is to give full play to catalyst and holds dirty ability, prolongs the cycle of operation.
Do not appear in the newspapers with similar methods of the present invention.
Summary of the invention
A kind of reactor used in crude gas variable-temperature reaction process of the present invention, constitute by the cylindrical vessel that has catalyst bed, the wall of cylindrical vessel is provided with charging aperture and discharging opening, charging aperture is connected with flow manifold, discharging opening is connected with the afflux runner, it is characterized in that: be flow manifold between the centrifugal sidewall of the wall of cylindrical vessel and catalyst bed, catalyst bed is the afflux runner in the sidewall entad, the reaction logistics is done entad to flow along radial direction in beds, radially passes through catalyst bed.
Feature of the present invention further is: from reactor axially, the catalyst bed cross section is an annular; The wall of cylindrical vessel is provided with the catalyst discharge duct; Be furnished with feed distributor with the end of pipe in the charging that charging aperture links to each other.
Feature of the present invention further is: during the reactor operate as normal, with pipe racks in the discharging that discharging opening links to each other one section sleeve pipe is arranged, space in sleeve pipe and the discharging between the pipe is a pipe constant temperature logistics runner in the discharging, is furnished with pipe constant temperature logistics inlet in the discharging in the discharging on the pipe.
Feature of the present invention further is: charging aperture and discharging opening are all on reactor top.
Feature of the present invention further is: charging aperture and discharging opening are all at reactor lower part.
Feature of the present invention further is: charging aperture and discharging opening, and one on reactor top, and another is at reactor lower part.
Feature of the present invention further is: with respect to the beds short transverse, the charging aperture center is corresponding to the beds middle part.
Feature of the present invention further is: the reactor internals comprise central tube and sector drum, and catalyst is seated in the annular space between central tube and the sector drum.
Feature of the present invention further is: central tube by perforate cylinder, outer net and up and down connector (hanger, cover plate, supporting base etc.) form.
Feature of the present invention further is: the inner cylinder perforate.
Feature of the present invention further is: outer net means comprises woven wire.
Feature of the present invention further is: outer net means comprises welding wedge wire screen net.
Feature of the present invention further is: the support bar of welding wedge wire screen net and the aperture on the internal openings cylinder stagger mutually.
Feature of the present invention further is: have one deck to dash the punched-plate in full strip hole between welding wedge wire screen net and the internal openings cylinder.
Feature of the present invention further is: sector drum is made of the perforate steel plate.
Feature of the present invention further is: sector drum is made of welding wedge wire screen net.
Feature of the present invention further is: the reactor internals comprise central tube and outer screen cloth, and catalyst is seated in the annular space between central tube and the outer screen cloth.
Feature of the present invention further is: the member of outer screen cloth comprises welding wedge wire screen net.
Feature of the present invention further is: the reactor internals comprise central tube and porous urceolus, and catalyst is seated in the annular space between central tube and the perforate urceolus.
Feature of the present invention further is: the porous urceolus is the porous wall urceolus.
Feature of the present invention further is: the loose structure urceolus is arranged to form as adjacent circumferential along nearly wall place in the bulge by a plurality of fan-shaped, hollow components, the porous urceolus is offered the distribution hole by catalyst one side, and the porous urceolus is by cylindrical vessel one not perforate of side.
Feature of the present invention further is: reactor is provided with two beds.
Feature of the present invention further is: after the mist that flows out the first bed central tube leaves reactor shell, enter the second bed charging space through the passage of reactor enclosure external body.
Feature of the present invention further is: reactor is provided with two beds, the first bed central tube is communicated with blender, blender is communicated with second feeding-passage, and the wall of cylindrical vessel is provided with second charging aperture, and mixer outlet links to each other with the second bed charging space.
Feature of the present invention further is: reactor is provided with a plurality of beds.
Feature of the present invention further is: reactor is provided with a plurality of beds, after the mist that flows out higher level's beds central tube leaves reactor shell, enters adjacent subordinate beds charging space through the passage of reactor enclosure external body.
Feature of the present invention further is: reactor is provided with a plurality of beds, higher level's catalyst layer central tube is communicated with blender, blender is communicated with adjacent subordinate feeding-passage, the wall of cylindrical vessel is provided with adjacent subordinate charging aperture, and mixer outlet links to each other with adjacent subordinate beds charging space.
The specific embodiment
Raw coke oven gas of the present invention refers to the raw coke oven gas that is suitable for making hydrogen, typically refers to the gas stream of being made up of hydrogen, carbon monoxide and other component (such as oxygen) from pyrolysis of coal (destructive distillation) process or other process.
Change within the specific limits owing to produce the pyrolysis of coal process conditions such as (destructive distillation) of raw coke oven gas, the character of raw coke oven gas also changes within the specific limits.The gas composition of raw coke oven gas of the present invention contain usually oxygen and or carbon monoxide, oxygen content is generally 0～1.5% (volume), is generally 0.2～0.9% (volume), is 0.3～0.7% (volume) especially that carbon monoxide content is generally 7～25% (volumes), is generally 10～20% (volumes), is 10～17% (volumes) especially.
According to raw coke oven gas composition, temperature, pressure condition, raw coke oven gas becomes before the unstripped gas that pipeline 1 carries, may through removing impurity (tar that may exist, naphthalene, dirt), increase water vapor concentration (satisfying the water carbon molecular proportion of transformationreation needs), a certain step or the Overall Steps of steps such as compression is boosted, intensification.
Variable-temperature reaction process of the present invention, refer to take place heat release and or the course of reaction of heat absorption, comprise removing oxygen in the raw coke oven gas and or finishing the course of reaction of carbon monodixe conversion hydrogen manufacturing.Described course of reaction is used catalyst usually, may use dehydrogenation catalyst and or carbon monoxide transformation catalyst.
Raw coke oven gas according to the present invention remove in the raw coke oven gas oxygen and or finish carbon monodixe conversion, the end reaction effluent that obtains usually after the condensation cooled dehydrated as unstripped gas or the chemical industry synthetic raw gas or the fuel gas etc. of transformation absorption purifying hydrogen of hydrogen.
Radial reactor is owing to its high flux, low pressure degradation characteristic are widely used in fields (such as being the gasoline catalyzing reforming process) such as petrochemical industry, chemical synthesis, the energy, environment, radial reactor is pursued the uniformity of reaction logistics along the reactor axial distribution, in the hope of the reaction effect of the best.
Usually, radial reactor according to gas reactant flow vertically the mobility status of sprue can be divided into two kinds on Z type and ∏ type, and the reaction logistics entad has and centrifugal branch along flowing of radial direction in bed, so the total entad ∏ type of fluidal texture of radial reactor reaction logistics, entad Z type, centrifugal ∏ type and four kinds of forms of centrifugal Z type.According to the object of the invention, select entad liquid form.
As everyone knows, for this axial even gas distribution of reactor radially, entad the II type flow (shown in Figure 4 flowing) entad be better than that the Z type flows (shown in Figure 3 flowing), therefore when other condition is identical, preferentially select entad II type fluidal texture for use.Devices needed is simple in structure but the Z type flows, so still for being extensive use of
Radial inflow radial fixed-bed reactor of the present invention can adopt any suitable disclosed radial reactor technology (such as entad radial reactor technical scheme of the gasoline catalyzing reforming process that a large amount of industrial successful Application achievements are arranged).
Describe the present invention in detail below in conjunction with accompanying drawing.Accompanying drawing does not limit interest field of the present invention for explanation the present invention draws.
As shown in Figure 3 and Figure 4, a kind of crude gas exothermic reaction process reactor of the present invention, constitute by the cylindrical vessel that has catalyst bed (4) (1), the wall of cylindrical vessel (1) is provided with charging aperture (2) and discharging opening (6), charging aperture (2) is connected with flow manifold (3), discharging opening (6) is connected with afflux runner (5), it is characterized in that: be flow manifold (3) between the wall of cylindrical vessel (1) and the centrifugal sidewall of catalyst bed (41), catalyst bed is afflux runner (5) in the sidewall (42) entad, the reaction logistics is done entad to flow along radial direction in beds (4), radially passes through catalyst bed.
In order to improve and to guarantee the uniformity that reaction mass flows in beds, reduce the device fabrication difficulty, reactor of the present invention, from reactor axially, catalyst bed (4) cross section is preferably annular.
On the wall of the cylindrical vessel of reactor of the present invention (1), can be provided with catalyst discharge duct (43), draw off catalyst when can be used for reactor down-time.
The end of pipe is furnished with feed distributor in the reactor of the present invention, the charging that links to each other with charging aperture (2), to improve the uniformity that charging distributes, can use various suitable schemes to carve the type net such as multihole distributor, metal and seal post, many narrow slit distribution grids etc.
Reactor of the present invention, during the reactor operate as normal, pipe (66) has one section sleeve pipe (62) in the discharging that links to each other with discharging opening (6), space in sleeve pipe (62) and the discharging between the pipe (66) is a pipe constant temperature logistics runner (63) in the discharging, is furnished with constant temperature logistics inlet (61) in the discharging on the pipe (66).
Constitute the mode of pipe constant temperature logistics runner (63) in the discharging, can be that sleeve pipe (62) is an overall structure with the interior pipe of discharging (66), also can be to utilize the flange of discharging opening (6) and the sleeve pipe formation demountable structure that one on outside companion flange folder has the integral entity base, can also be external overall parts (contain sleeve pipe (62) and be furnished with pipe (66) in (61) the part discharging of constant temperature logistics inlet) certainly.
Described constant temperature logistics refers to the suitable logistics harmless to technological operation of the more stable pressure of a dataway operation temperature, can do the constant temperature logistics such as from charging main flow pipeline, telling one road low discharge logistics, check valve and or stop valve preferably are set on the constant temperature logistics pipeline.
Reactor of the present invention, the position of charging aperture (2) and discharging opening (6): can be all on reactor top, also can be all at reactor lower part, can also one on top, another is in the bottom.
Reactor of the present invention, the relative position of charging aperture (2) can be that with respect to the beds short transverse, charging aperture (2) center is corresponding to the beds middle part.
Reactor of the present invention can use central tube and sector drum, and catalyst bed is arranged in the annular space between central tube and the sector drum.Central tube by perforate cylinder, outer net and up and down connector (hanger, cover plate, supporting base etc.) form.The inner cylinder perforate, outer net means is formed with woven wire or with welding wedge wire screen net, the support bar of welding wedge wire screen net and the aperture on the internal openings cylinder stagger mutually, can arrange that one deck dashes the punched-plate in full strip hole between welding wedge wire screen net and the internal openings cylinder.Sector drum is made of the perforate steel plate or is made of welding wedge wire screen net.
Reactor of the present invention can use central tube and outer screen cloth, and catalyst bed is arranged in the annular space between central tube and the outer screen cloth.Outer screen cloth is made up of welding wedge wire screen net.
Reactor of the present invention can use central tube and porous urceolus, and catalyst bed is arranged in the annular space between central tube and the perforate urceolus.The porous urceolus is the porous wall urceolus.The loose structure urceolus is arranged to form as adjacent circumferential along nearly wall place in the bulge by a plurality of fan-shaped, hollow components, and the porous urceolus is offered the distribution hole by catalyst one side, and the porous urceolus is by cylindrical vessel one not perforate of side.
Reactor of the present invention, reactor can be provided with two beds.After the mist that flows out the first bed central tube leaves reactor shell, enter the second bed charging space through the passage of reactor enclosure external body.
Reactor of the present invention, reactor can be provided with two beds, and the first bed central tube is communicated with blender, and blender is communicated with second feeding-passage, the wall of cylindrical vessel (1) is provided with second charging aperture, and mixer outlet links to each other with the second bed charging space.
Reactor of the present invention, reactor can be provided with a plurality of beds.After the mist that flows out higher level's beds central tube leaves reactor shell, enter adjacent subordinate beds charging space through the passage of reactor enclosure external body.
Reactor of the present invention, reactor can be provided with a plurality of beds, higher level's catalyst layer central tube is communicated with blender, blender is communicated with adjacent subordinate feeding-passage, the wall of cylindrical vessel (1) is provided with adjacent subordinate charging aperture, and mixer outlet links to each other with adjacent subordinate beds charging space.
In order at utmost to bring into play effect of the present invention, can use or use for reference known robust techniques.
Compare with the axial restraint bed bioreactor, the invention has the advantages that to be:
1. make the gas material that contacts with wall of reactor be controlled to be the feed stream of temperature stabilization, improved the uniformity of wall of reactor Temperature Distribution, particularly the wall of reactor Temperature Distribution still had the high uniformity and stability when content fluctuateed within the specific limits when reactive component in the raw material raw coke oven gas (such as oxygen and or carbon monoxide), thereby guaranteed stability and the security of equipment operating process;
2. improve the uniformity that the reaction logistics distributes along beds, thereby improved reaction efficiency;
3. micro-tar, naphthalene etc. can coking cause catalyst to hinder gradually inactivation in operating process in the raw material, and the present invention is along Flow of Goods and Materials direction (radial centripetal direction), the loadings of equal thickness beds is by greatly to little variation, be beneficial to the performance catalyst and hold dirty ability, can prolong the cycle of operation.
The purpose that discharging inner tube constant temperature logistics runner (63) is set is the Temperature Distribution of the upper part that links to each other with discharging inner tube (66) of control cylindrical vessel (1), therefore, sleeve pipe (62) must go deep into the inside certain depth of cylindrical vessel (1) wall outline line.
Claims (29)
1. reactor used in crude gas variable-temperature reaction process, constitute by the cylindrical vessel that has catalyst bed (4) (1), the wall of cylindrical vessel (1) is provided with charging aperture (2) and discharging opening (6), charging aperture (2) is connected with flow manifold (3), discharging opening (6) is connected with afflux runner (5), it is characterized in that: be flow manifold (3) between the wall of cylindrical vessel (1) and the centrifugal sidewall of catalyst bed (41), catalyst bed is afflux runner (5) in the sidewall (42) entad, the reaction logistics is done entad to flow along radial direction in beds (4), radially passes through catalyst bed.
2. according to the described reactor of claim 1, it is characterized in that: from reactor axially, catalyst bed (4) cross section is an annular.
3. according to the described reactor of claim 2, it is characterized in that: the wall of cylindrical vessel (1) is provided with catalyst discharge duct (43).
4. according to the described reactor of claim 1, it is characterized in that: the end of pipe is furnished with feed distributor in the charging that links to each other with charging aperture (2).
5. according to the described reactor of claim 1, it is characterized in that: during the reactor operate as normal, pipe (66) has one section sleeve pipe (62) in the discharging that links to each other with discharging opening (6), space in sleeve pipe (62) and the discharging between the pipe (66) is a pipe constant temperature logistics runner (63) in the discharging, is furnished with pipe constant temperature logistics inlet (61) in the discharging in the discharging on the pipe (66).
6. according to claim 1 or 2 or 3 or 4 or 5 described reactors, it is characterized in that: charging aperture (2) and discharging opening (6) are all on reactor top.
7. according to claim 1 or 2 or 3 or 4 or 5 described reactors, it is characterized in that: charging aperture (2) and discharging opening (6) are all at reactor lower part.
8. according to claim 1 or 2 or 3 or 4 or 5 described reactors, it is characterized in that: charging aperture (2) and discharging opening (6), one on top, and another is in the bottom.
9. according to claim 1 or 2 or 3 or 4 or 5 described reactors, it is characterized in that: with respect to the beds short transverse, charging aperture (2) center is corresponding to the beds middle part.
10. according to claim 1 or 2 or 3 or 4 or 5 described reactors, it is characterized in that: the reactor internals comprise central tube and sector drum, and catalyst is seated in the annular space between central tube and the sector drum.
11., it is characterized in that according to the described reactor of claim 10: central tube by perforate cylinder, outer net and up and down connector (hanger, cover plate, supporting base etc.) form.
12. according to the described reactor of claim 10, it is characterized in that: the inner cylinder perforate.
13. according to the described reactor of claim 10, it is characterized in that: outer net means comprises woven wire.
14. according to the described reactor of claim 10, it is characterized in that: outer net means comprises welding wedge wire screen net.
15. according to the described reactor of claim 14, it is characterized in that: the support bar of welding wedge wire screen net and the aperture on the internal openings cylinder stagger mutually.
16., it is characterized in that: have one deck to dash the punched-plate in full strip hole between welding wedge wire screen net and the internal openings cylinder according to the described reactor of claim 14.
17. according to the described reactor of claim 10, it is characterized in that: sector drum is made of the perforate steel plate.
18. according to the described reactor of claim 10, it is characterized in that: sector drum is made of welding wedge wire screen net.
19. according to claim 1 or 2 or 3 or 4 or 5 described reactors, it is characterized in that: the reactor internals comprise central tube and outer screen cloth, and catalyst is seated in the annular space between central tube and the outer screen cloth.
20. according to the described reactor of claim 19, it is characterized in that: the member of outer screen cloth comprises welding wedge wire screen net.
21. according to claim 1 or 2 or 3 or 4 or 5 described reactors, it is characterized in that: the reactor internals comprise central tube and porous urceolus, catalyst is seated in the annular space between central tube and the perforate urceolus.
22. according to the described reactor of claim 21, it is characterized in that: the porous urceolus is the porous wall urceolus.
23. according to the described reactor of claim 21, it is characterized in that: the loose structure urceolus is arranged to form as adjacent circumferential along nearly wall place in the bulge by a plurality of fan-shaped, hollow components, the porous urceolus is offered the distribution hole by catalyst one side, and the porous urceolus is by cylindrical vessel one not perforate of side.
24. according to claim 1 or 2 or 3 or 4 or 5 described methods, it is characterized in that: reactor is provided with two beds.
25., it is characterized in that: after the mist that flows out the first bed central tube leaves reactor shell, enter the second bed charging space through the passage of reactor enclosure external body according to the described method of claim 24.
26. according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: reactor is provided with two beds, the first bed central tube is communicated with blender, blender is communicated with second feeding-passage, the wall of cylindrical vessel (1) is provided with second charging aperture, and mixer outlet links to each other with the second bed charging space.
27. according to claim 1 or 2 or 3 or 4 or 5 described methods, it is characterized in that: reactor is provided with a plurality of beds.
28. according to the described method of claim 27, it is characterized in that: reactor is provided with a plurality of beds, after the mist that flows out higher level's beds central tube leaves reactor shell, enter adjacent subordinate beds charging space through the passage of reactor enclosure external body.
29. according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that: reactor is provided with a plurality of beds, higher level's catalyst layer central tube is communicated with blender, blender is communicated with adjacent subordinate feeding-passage, the wall of cylindrical vessel (1) is provided with adjacent subordinate charging aperture, and mixer outlet links to each other with adjacent subordinate beds charging space.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010100040903A CN101890324A (en) | 2010-01-19 | 2010-01-19 | Reactor used in crude gas variable-temperature reaction process |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010100040903A CN101890324A (en) | 2010-01-19 | 2010-01-19 | Reactor used in crude gas variable-temperature reaction process |
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| CN101890324A true CN101890324A (en) | 2010-11-24 |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103071429A (en) * | 2013-01-30 | 2013-05-01 | 中国石油化工股份有限公司 | Radial fixed bed reactor for oxy-dehydrogenation of butylene |
| CN106606997A (en) * | 2015-10-23 | 2017-05-03 | 中国石油化工股份有限公司 | Upflow distributor and upflow reactor |
| CN109294627A (en) * | 2018-09-29 | 2019-02-01 | 国家能源投资集团有限责任公司 | Isothermal converting means and the complete conversion reaction system of synthesis gas comprising it |
| CN112275225A (en) * | 2019-07-25 | 2021-01-29 | 中国石化工程建设有限公司 | Radial moving bed reaction system and flow-solid reaction method |
| CN112275224A (en) * | 2019-07-25 | 2021-01-29 | 中国石化工程建设有限公司 | Moving bed reaction system and catalytic reaction method |
-
2010
- 2010-01-19 CN CN2010100040903A patent/CN101890324A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103071429A (en) * | 2013-01-30 | 2013-05-01 | 中国石油化工股份有限公司 | Radial fixed bed reactor for oxy-dehydrogenation of butylene |
| CN106606997A (en) * | 2015-10-23 | 2017-05-03 | 中国石油化工股份有限公司 | Upflow distributor and upflow reactor |
| CN109294627A (en) * | 2018-09-29 | 2019-02-01 | 国家能源投资集团有限责任公司 | Isothermal converting means and the complete conversion reaction system of synthesis gas comprising it |
| CN112275225A (en) * | 2019-07-25 | 2021-01-29 | 中国石化工程建设有限公司 | Radial moving bed reaction system and flow-solid reaction method |
| CN112275224A (en) * | 2019-07-25 | 2021-01-29 | 中国石化工程建设有限公司 | Moving bed reaction system and catalytic reaction method |
| CN112275225B (en) * | 2019-07-25 | 2022-09-27 | 中国石化工程建设有限公司 | Radial moving bed reaction system and flow-solid reaction method |
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Application publication date: 20101124 |