CN102895922B - Industrial plate type reactor for preparing glycol by hydrogenating oxalate or preparing alcohol by hydrogenating ester - Google Patents
Industrial plate type reactor for preparing glycol by hydrogenating oxalate or preparing alcohol by hydrogenating ester Download PDFInfo
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- CN102895922B CN102895922B CN201210407137.XA CN201210407137A CN102895922B CN 102895922 B CN102895922 B CN 102895922B CN 201210407137 A CN201210407137 A CN 201210407137A CN 102895922 B CN102895922 B CN 102895922B
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Abstract
The invention relates to an industrial plate type reactor for preparing glycol by hydrogenating oxalate or preparing alcohol by hydrogenating ester. Heat exchange plates and a cooling pipe are arranged in a catalyst bed layer of a reactor, wherein the heat exchange plates are arrayed in the catalyst bed layer in following mode: placed along a direction parallel to a radial direction of the catalyst bed layer and arrayed along a concentric fan or arrayed in a form of approximate concentric circle along the direction vertical to the radial direction of the of the catalyst bed layer. The industrial plate type reactor overcomes the defect that the present reactor for preparing the alcohol by hydrogenating the ester, especially, for preparing the glycol by hydrogenating the oxalate, is a tube reactor, and also overcomes the defects that a single reactor is small in catalyst filling volume and high in pressure drop and multiple reactors are required by mass production. The industrial plate type reactor provided by the invention can increase the utilization factor of a hydrogenation catalyst and the volume use ratio of the reactor; the catalyst filling volume is increased; the reactor production capacity is increased; the investment in device and equipment is saved; the running cost is lowered; and the industrial plate type reactor has an excellent industrialized application effect in the technologies of preparing the glycol by hydrogenating the oxalate and preparing the alcohol by hydrogenating the ester.
Description
Technical field
The present invention relates to a kind of industrialization plate-type reactor being applicable to ester through hydrogenation alcohol, particularly relate to a kind of industrialization plate-type reactor being applicable to hydrogenation of oxalate for preparing ethylene glycol.
Background technology
Ethylene glycol (MEG) is a kind of important Organic Chemicals, mainly for the production of polyester fiber, antifreezing agent, unsaturated polyester resin, lubricant, plasticizer, non-ionic surface active agent and explosive etc., in addition for industries such as coating, soup, brake-fluid and ink, as solvent and the medium of ammonium pertorate, for the production of special solvent glycol ether etc., purposes is very extensive.
At present, the fixed bed reactors of hydrogenation of oxalate for preparing ethylene glycol adopt shell and tube reactor substantially.Shell and tube reactor makes simple, but has certain limitation in raising respond.Generally, improve respond and solve mainly through raising heat exchange area and loaded catalyst, namely will strengthen the diameter of tubulation or increase the quantity of tubulation.Bed radial temperature profile can be produced so uneven, cause reaction wayward, and increase the generation of side reaction.In addition, when power requirement height to a certain extent time, shell and tube reactor volume is comparatively large, axially and radial larger temperature difference system energy efficiency will be caused to reduce, even make the hydrogenation reaction in reactor normally to run.
The reaction of hydrogenation of oxalate for preparing ethylene glycol is the mutually reversible catalytic exothermic reaction of gas-solid, for ensureing carrying out continuously of heat-producing chemical reaction, constantly need shift out reaction heat, carrying out to make course of reaction along optimum temperature curve.And current industrial employing shell and tube reactor is for the shortcoming such as avoiding catalyst easily aging, service life is short, usually adopt in practice and load catalyst in a large number, to strengthen reserve factor, the mode of extending catalyst replacement cycle, but too large reserve factor, add catalyst bed layer height, thus considerably increase equipment running resistance and power consumption.
Hydrogenation of oxalate for preparing ethylene glycol reaction is calandria type fixed bed reactor due to what adopt, generally there is focus at inside reactor.For this reaction, the too high ethylene glycol excessive hydrogenation that not only can cause of hot(test)-spot temperature generates ethanol, and can cause the sintering of copper in catalyst, reduces the service life of catalyst.
In sum, there is following shortcoming in current hydrogenation of oxalate for preparing ethylene glycol reaction: one is adopt pipe type heat transfer structure, and heat transfer coefficient is low, is difficult to realization effectively heat conduction reinforced; Two is hot and cold streams is that effective heat transfer temperature difference is little with the heat exchange of non-fully countercurrent flow.Due to the shortcoming of above two aspects, cause existing hydrogenation of oxalate for preparing ethylene glycol inside reactor effective heat exchange area less, consumptive material is many, and equipment manufacturing cost is high, and bulky, and I&M is all inconvenient.In addition, due to the shortcoming of above device structure, make the average reaction temperature in course of reaction lower, cause oxalate hydrogenation speed low, required catalyst amount is many, and equipment investment is high.
Summary of the invention
The present invention is directed to the deficiencies in the prior art, the plate-type reactor that when providing a kind of gas to flow, resistance is little, power consumption is low, callable heat is many, output is high, production cost is low.Solve and overcome existing hydrogenation reactor internal heat structure exist pipe type heat transfer heat transfer coefficient low, be difficult to realize heat conduction reinforced, hot and cold stream non-fully countercurrent flow, namely effective heat transfer temperature difference is little, volume is large, installation and maintenance are inconvenient, consumptive material is many, cost is high and average reaction temperature is lower, causes that hydrogenation reaction speed is low, catalyst consumption is large, invest large etc. problem and shortcoming.Board-like gas-solid catalysis device provided by the invention, increase heat transfer coefficient in chamber, enhance heat transfer, therefore greatly reduce hot(test)-spot temperature, considerably increase catalyst usage factor simultaneously, significantly reduce equipment running resistance and improve the production capacity of device.
The present invention realizes by the following technical solutions:
For an industrialization plate-type reactor for hydrogenation of oxalate for preparing ethylene glycol, its internal structure comprises the Reactor inlet pipe, inlet gas distributor, Heat Room, upper end inert filler layer, intermediate radial reaction bed, lower end inert filler layer, exit gas distributor and the reactor outlet pipe that are positioned at entrance point from top to bottom successively; Described intermediate radial reaction bed, comprises annular space, outer distributing barrel, beds, inside distributor and the center set tracheae between reactor shell inwall and outer distributing barrel that are connected with upper end inert filler layer from outside to inside successively.
Establish heat exchanger in described beds, the heat exchange element of heat exchanger is plate type heat exchanging element; Described plate type heat exchanging element is prefabricated heat exchanger plates in groups, and described heat exchanger plates is quadrilateral structure, is welded by two pieces of metallic plates, and all heat exchanger plates in same reactor are identical; The plate package be made up of heat exchanger plates is loaded in tower by top manhole, is embedded in beds, and plate package is overall by being fixed on the annular gusset common support of reactor shell inwall and center set tracheae outer wall.
The arrangement mode of described plate package in beds is: be parallel to beds radial direction and place and fan-shapedly to arrange along concentric, or be similar to concentric arrays perpendicular to beds radial direction; The reaction medium of circulation between various heat exchange plate, has different cross-current flow according to the different in kind of catalyst, and object extends the circulation distance of reaction medium between plate, and ensure that the pressure drop of each reaction medium circulation path is close to identical as far as possible; Utilize the fan-shaped arrangement position of plate type heat exchanger in reaction bed, can Appropriate application inside reactor heat, achieve good thermal coupling between vaporization and reaction, thus reach and increase heat-transfer effect, improve conversion ratio and optionally object.
When plate package be parallel to beds radial direction place and along concentric fan-shaped arrange time, according to the size of reactor inner space and the size of heat exchanger plates itself, establish one piece of heat exchanger plates along same radial direction or establish polylith heat exchanger plates successively; Fixed by annular or circular fastening hoop between the heat exchanger plates of distance reactor axle center same distance.
When plate package is similar to concentric arrays perpendicular to beds radial direction, same radial heat exchanger plates is arranged in parallel, and the plate package entirety being positioned at beds is surrounded fixing by being positioned near outer distributing barrel inwall and the outer peripheral circular fastening hoop of plate package; Effective distance between plates between the adjacent heat exchanger plates of same radial parallel arrangement is equal.
The heat exchange area of heat exchanger plates is larger than heat exchanger tube, so can take away more reaction heat.And gas flow through that the Area comparison of institute's contact catalyst is large and evenly, Reactive Synthesis efficiency comparison is high.Entire infrastructure is all the standard component of modular, once damage, can be easy to replace.
The thickness of described heat exchanger plates is 0.1 ~ 1.0mm.
The material of the metallic plate of described heat exchanger plates is SS304 metallic plate (gas converting heat plate) or DUPLEX metallic plate (steam heat-exchanging plate), mechanically very firm, good rigidly; Preferably SS304.
Two pieces of metallic plates of described heat exchanger plates have identical impression, heat exchanger plates hollow, and two pieces of metallic plates peripherally weld, surperficial spot welding simultaneously, and then punching press is made, the fluidly passage of the slit-shaped between two metallic plates; When fluid flows through the plate of above-mentioned impression in crankle mode, on the one hand accelerate rate of flow of fluid, greatly improve overall heat-transfer coefficient, and extend the time that fluid passes through, the reaction not only making beds assemble is taken away by the fluid of this heat exchanger in time, makes plate inner fluid obtain preheating simultaneously.
Described impression is corrugated, linear, polyline shaped or bubbling shape.
The metallic plate of described heat exchanger plates and the side of catalyst exposure are parallel-plate fin structure, and plate wing spacing is 0.1 ~ 0.5mm; Parallel-plate fin structure described in employing, fluid can be made fully to mix in reaction zone and to improve heat transfer efficiency, overcome shell and tube reactor limitation in this respect, make structure of reactor compacter simultaneously, bed volume is less, therefore avoids reactor radial temperature difference and axial temperature difference.
The fluid channel design of described plate type heat exchanging element, the flow direction along cooling medium comprises successively: cooling medium inlet, main distributing pipe, plate package distributing pipe, plate package, heat exchanger plates steam outlet pipe, plate package steam collecting pipe, main collecting pipe and steam outlet pipe mouth.
The process of circulation of cooling medium in described heat exchange element is: enter reactor from cooling medium inlet, enter in the heat exchanger plates of each plate package through main distributing pipe and plate package distributing pipe, after heat exchanger plates and beds heat exchange, produce after mesolow saturated steam collects in heat exchanger plates steam outlet pipe and enter plate package steam collecting pipe, finally, mesolow steam from plate package is discharged reactor through main collecting pipe from steam outlet pipe mouth and is delivered to the external world, carries out follow-up low pressure steam recycling recycling.
Described cooling medium is boiler feedwater or other cooling fluid, and reaction heat is shifted out beds in time, produces mesolow saturated vapor simultaneously; Also can gas-gas heat exchange.
In described heat exchanger plates, the type of flow of cooling medium and the outer reactant of plate is cross-flow.
Cold pipe is established in described beds.
When plate package be parallel to beds radial direction place and along concentric fan-shaped array time, described cold pipe, between adjacent two heat exchanger plates of distance reactor axle center same distance, embeds in wedge shape in beds; To keep effective distance between plates of described adjacent two heat exchanger plates equal, effective distance between plates of described adjacent two heat exchanger plates is remaining distances after the distance between described adjacent two heat exchanger plates deducts shared by cold pipe space.
When plate package is similar to concentric arrays perpendicular to beds radial direction, described cold pipe is between the adjacent heat exchanger plates group of distance reactor axle center same distance, embed in wedge shape in beds, to keep effective distance between plates of described adjacent two plate package equal, the effective distance between plates between described adjacent plate package then for the distance between adjacent two plate package deduct shared by cold pipe space after remaining distance.
Described cold pipe shape of cross section is triangle, trapezoidal, square, rhombus or parallelogram; Preferably trapezoidal.
In described beds, effective distance between plates of adjacent heat exchanger plates or adjacent heat exchanger plates group is 20 ~ 200mm, is preferably 40 ~ 80mm.
Medium in described cold pipe is air, unstripped gas, fused salt, water or without medium, is preferably water.
The fluid channel design of described cold pipe, the direction along cooling fluid flowing comprises successively: cold pipe import, cold pipe import distributing pipe, and cold pipe, cold pipe exit collector and cold pipe export.
The process of circulation of cooling fluid in cold pipe is: cooling medium enters from cold pipe import, after cold pipe import distributing pipe distributes, enter each cold pipe, collects after cold pipe flows out cold pipe exit collector, then from cold pipe outlet outflow reactor.
The inlet gas distributor of described reactor and exit gas distributor, arranged along the perpendicular flow direction importing and exporting fluid, and on distributor, perforate arrangement is in inverted triangle or parallelogram; Preferably inverted triangle.
The outer distributing barrel of described radial reaction bed and inside distributor are a cylindrical metal shell, it establishes perforate, by the flow direction of fluid, the perforate distribution density be in the unit length of fluid flowing upstream is larger, the perforate distribution density be in fluid flow downstream unit length is less, thus ensure that being uniformly distributed of air-flow, dead angle is reduced, and improves the utilization rate of catalyst.
Perforate on described outer distributing barrel and inside distributor is circular, square, triangle, grid or fillet shape; Be preferably fillet shape; On cylinder, perforate is arranged as circumferential or spirality.
The catalyst being used for hydrogenation of oxalate for preparing ethylene glycol is loaded in space between the heat exchanger plates of described beds and heat exchanger plates and between heat exchanger plates and cold pipe.
The grain shape of described catalyst is cylindric, Raschig ring, clover, bunge bedstraw herb, the five fingers ball or spherical; Preferably cylindric.
Described catalyst particle size is 3.2 ~ 5.5 × 3.2 ~ 5.5mm, is preferably 3.2 × 3.2mm.
The housing upper end of described plate-type reactor is provided with manhole, lower end establishes ring-shaped distributed catalyst to draw off the mouth of pipe, under normal service condition, catalyst is supported by lower end inert filler bed, when drawing off catalyst, to draw off nozzle flange to lay down, the filler in the catalyst of catalytic bed and bottom inert filler layer draws off mouth of pipe outflow reactor from catalyst.
The process of circulation of reacting gas in described plate-type reactor is: the reacting gas after preheating enters reactor by Reactor inlet pipe, first through inlet gas distributor, then further preheating in Heat Room, again through the further uniform distribution of upper end inert filler layer, gas after distribution flows down along annular space between reactor shell inwall and outer distributing barrel, enters beds react by the outer distributing barrel of radial reaction bed; Most product enters center set tracheae by the inside distributor of radial reaction bed, small part is also had directly to enter lower end inert filler layer from the inside distributor of radial reaction bed, then two strands of products are simultaneously through exit gas distributor, flow out from reactor outlet pipe.
Described plate-type reactor, for in hydrogenation of oxalate for preparing ethylene glycol industrialized unit, but be not limited to " oxidative coupling reaction synthesizing dimethyl oxalate and dimethyl carbonate " reactor that this device also can be used for indication in patent " a kind of technological process of producing ethylene glycol with coproduction product dimethyl carbonate " ZL2008 10043079.0 claim, and as the patent No. 201220194360.6, " a kind of acetate produces ethanol and the technique of selective coproduction 2-butanols "; The acetate hydrogenation reactor of indication in patent No. 201210134269.X " a kind of acetate produces ethanol and the technique of selective coproduction 2-butanols and process matched therewith system thereof ".
The main feature of described plate-type reactor is that heat exchanger plates is inserted in beds, and leak water in plate or other heat transferring medium, the heat exchange area of heat exchanger plates is larger than heat exchanger tube, so can take away more reaction heat.And gas flow through that the Area comparison of institute's contact catalyst is large and evenly, Reactive Synthesis efficiency comparison is high.Entire infrastructure is all the standard component of modular, once damage, can be easy to replace.Adopt parallel fins plank frame, fluid fully mixes in fan-shaped reaction zone, overcomes shell and tube reactor limitation in this respect, the raising of heat transfer efficiency simultaneously, make structure of reactor compacter, less bed volume, avoid reactor radial temperature difference and axial temperature difference; Utilize the fan-shaped arrangement position of plate type heat exchanger in reaction bed, Appropriate application inside reactor heat, between vaporization and reaction, achieve good thermal coupling, thus reach and increase heat-transfer effect, improve conversion ratio and optionally object.
Described plate-type reactor fully excavates the potentiality of catalyst, considerably increase catalyst usage factor, equipment running resistance is only 1/6 of shell-and-tube reactor, heat exchange element simultaneously, its overall heat-transfer coefficient is more much larger than general heat exchanger, the reaction heat that catalyst can be made to assemble is taken away by the fluid of this plate in time, under the characteristic with lower resistance, use plate-type reactor can significantly increase yield, easy to make feasible, not only greatly can reduce investment and production cost, but also because having automatic dress, unload the function of carried catalyst, new way has been started for current hydrogenation of oxalate for preparing ethylene glycol or ester through hydrogenation alcohol maximize, there is good promotion prospect and economic benefit.
Described plate-type reactor, is applied in hydrogenation of oxalate for preparing ethylene glycol industrialized unit, is convenient in addition expand large-scale feature.
Accompanying drawing explanation
A kind of industrialization plate-type reactor internal structure schematic diagram for hydrogenation of oxalate for preparing ethylene glycol of Fig. 1
Fig. 2 is a kind of is fan pattern structural representation for plate type heat exchanging element in the industrialization plate-type reactor of hydrogenation of oxalate for preparing ethylene glycol in beds
The parallel-plate wing structure of Fig. 3 heat exchanger plates and cold pipe partial structurtes elevation
Fig. 4 plate package be parallel to beds radial direction place and along concentric fan-shaped array local structural graph
Fig. 5 plate package be parallel to beds radial direction place and along concentric fan-shaped array schematic diagram
Fig. 6 is a kind of is similar to concentric arrays structural representation for plate type heat exchanging element in the industrialization plate-type reactor of hydrogenation of oxalate for preparing ethylene glycol perpendicular to beds radial direction
Fig. 7 plate package is similar to concentric arrays local structural graph perpendicular to beds radial direction
Fig. 8 plate package is similar to concentric arrays schematic diagram perpendicular to beds radial direction
Reference numeral:
1 Reactor inlet pipe
2 inlet gas distributors
3 upper end inert filler layers
4 intermediate radial reaction beds
5 center set tracheaes
6 lower end inert filler layers
7 cooling medium inlets
8 catalyst draw off the mouth of pipe
9 steam outlet pipe mouths
10 main collecting pipes
Annular space between 11 reactor shell inwalls and outer distributing barrel
12 beds
13 exit gas distributors
14 reactor outlet pipes
15 Heat Rooms
16 inside distributors
17 cold pipe imports
18 cold pipe outlets
19 cold pipe exit collectors
20 outer distributing barrels
21 cold pipe inlet distributor
22 main distributing pipes
23 plate package distributing pipes
24 plate package
25 plate wings
26 cold pipe outlet pipes
27 cold pipe cross sections
28 heat exchanger plates steam outlet pipes
29 cold pipes
30 heat exchanger plates
31 fastening hoops
32 reactor shell
33 plate package steam collecting pipes
34 annular gussets
Detailed description of the invention
Below in conjunction with specific embodiment, set forth the present invention further.Should be understood that these embodiments are only not used in for illustration of the present invention to limit the scope of the invention.In addition should be understood that those skilled in the art can do any change or amendment to the present invention, and these equivalent form of values fall within the application's appended claims limited range equally after having read the content that the present invention tells about.
The experimental technique of unreceipted actual conditions in embodiment below, usually conveniently condition, as: chemical industry operation handbook, or according to the condition that manufacturer advises.
The board-like hydrogenation reactor of annual output 300000 tons of hydrogenation of oxalate for preparing ethylene glycol as shown in Figure 1 and Figure 2, internal diameter 4.0m, highly (T.L) 12.0m, synthesis pressure 2.0 ~ 5.0MPa; Its internal structure comprises the Reactor inlet pipe 1, inlet gas distributor 2, Heat Room 15, upper end inert filler layer 3, intermediate radial reaction bed 4, lower end inert filler layer 6, exit gas distributor 13 and the reactor outlet pipe 14 that are positioned at entrance point from top to bottom successively; Described intermediate radial reaction bed 4, comprises annular space 11, outer distributing barrel 20, beds 12, inside distributor 16 and the center set tracheae 5 between reactor shell 32 inwall and outer distributing barrel that are connected with upper end inert filler layer 3 from outside to inside successively;
Establish prefabricated heat exchanger plates 30 in groups in described beds 12, it is long that monolithic heat exchanger plates 30 is of a size of 7m() × 0.4m(is wide) quadrilateral structure, be welded by two pieces of SS304 metallic plates, in same reactor, all heat exchanger plates 30 are identical; Two pieces of metallic plates have identical bubbling shape impression, heat exchanger plates 30 hollow, and two pieces of metallic plates peripherally weld, surperficial spot welding simultaneously, and then punching press is made, the fluidly passage of the slit-shaped between two metallic plates; The side of described metallic plate and catalyst exposure is parallel-plate fin structure, and plate wing 25 spacing is 0.1 ~ 0.5mm; 3 pieces of heat exchanger plates 30 are established along same radial direction; The plate package 24 be made up of heat exchanger plates 30 be parallel to beds 12 radial direction place and along concentric fan-shaped array, as shown in Figure 5; Plate package 24 entirety is by being fixed on annular gusset 34 common support of reactor shell 32 inwall and center set tracheae 5 outer wall; Fixed by circular fastening hoop (31) between the heat exchanger plates 30 of distance reactor axle center same distance; Cold pipe 29 is established away between adjacent two heat exchanger plates 30 of distance reactor axle center, center set tracheae 5 place same distance in described beds 12, described cold pipe 29 embeds beds 12 in wedge shape, cold pipe cross section 27 shape is inverted trapezoidal along axle center, and the effective distance between plates between adjacent two heat exchanger plates 30 of distance reactor axle center same distance is 60mm.
In the heat exchanger plates 30 of beds 12 and the space of cold pipe 29, filling is used for the catalyst of the board-like hydrogenation of hydrogenation of oxalate for preparing ethylene glycol.
The fluid channel design of described plate package 24, the flow direction along cooling medium comprises successively: the import 7 of cooling medium, main distributing pipe 22, plate package distributing pipe 23, plate package 24, heat exchanger plates steam outlet pipe 28, plate package steam collecting pipe 33, main collecting pipe 10 and steam outlet pipe mouth 9.
The fluid channel design of described cold pipe 29, the direction along cooling fluid flowing comprises successively, cold pipe import 17, cold pipe import distributing pipe 21, cold pipe 29, cold pipe exit collector 19 and cold pipe outlet 26.
Described inlet gas distributor 2 and exit gas distributor 13, the perpendicular flow direction along reacting gas is arranged, and on distributor, perforate is arranged as del.
Outer distributing barrel 20 and the inside distributor 16 of described radial reaction bed 4 are cylindrical metal shell, and inside distributor 16 diameter is 0.85m, and outer distributing barrel 20 diameter is 3.8m, and it all establishes perforate, and hole shape is fillet shape, and perforate circumferentially arranges; By the flow direction of fluid, the perforate distribution density be in the unit length of fluid flowing upstream is comparatively large, and the perforate distribution density be in fluid flow downstream unit length is less, thus ensure that being uniformly distributed of air-flow, dead angle is reduced, and improves the utilization rate of catalyst.
The lower end of described plate-type reactor establishes the catalyst of apportion in the form of a ring to draw off the mouth of pipe 8, under normal service condition, catalyst is supported by reactor lower end inert filler layer 6, when drawing off catalyst, catalyst is drawn off the mouth of pipe 8 flange to lay down, the catalyst of beds 12 and the filler of lower end inert filler layer 6 draw off the mouth of pipe 8 outflow reactor from catalyst.
Boiler feedwater (CL is walked in heat exchanger plates 30
-be less than 4PPM), reactor is entered from cooling medium inlet 7, enter in each plate package 24 through main distributing pipe 22, then enter after plate package distributing pipe 23 in the heat exchanger plates 30 of each plate package 24, after heat exchanger plates 30 and catalyst heat exchange, produce after mesolow saturated steam collects in heat exchanger plates steam outlet pipe 28 and enter plate package steam collecting pipe 33, finally, mesolow steam from plate package is discharged reactor through main collecting pipe 10 from steam outlet pipe mouth 9 and is delivered to extraneous recycling, and sending water vapour pressure outside is 0.9 ~ 1.6MPa.
Also boiler feedwater is walked in cold pipe 29, supercooling tube import 17 is led in boiler feedwater and cold pipe inlet distributor 21 enters the cold pipe 29 being positioned at beds 12, the unnecessary heat of reaction of beds 12 is taken away by indirect heat exchange, then reactor is discharged through cold pipe exit collector 19 from cold pipe outlet 18, logical like this supercooling tube 29 auxiliary heat-exchanging is to guarantee that outer reaction zone beds 12 Temperature Distribution distributes for optimal temperature, thus ensure the high conversion of catalyst and selective, improve catalyst usage factor.
When carrying out hydrogenation reaction, mist (temperature 185 DEG C, pressure 3MPa) first enter upper end inert filler layer 3 from tower top Reactor inlet pipe 1 by inlet gas distributor 2, to strengthen distribution of gas, in Heat Room 15 through further with steam indirect heat exchange after and gas phase redistribution after, mixing temperature reaches 200 DEG C, flow down along annular space 11 between reactor shell 32 inwall and outer distributing barrel 20, the fan-shaped conversion zone of beds 12 is entered by the outer distributing barrel 20 of radial reaction bed 4, catalyst granules (3.2mm × 3.2mm) shape is cylindric, beds 12 hot(test)-spot temperature is 203 DEG C, reaction conversion ratio 100%, glycol selectivity 99%.Qualified thick ethylene glycol is produced in now reaction, and it is 185 DEG C that material goes out temperature of reactor.Finally, major part product enters center set tracheae 5 from the inside distributor 16 of intermediate radial reaction bed (4), small part is also had directly to enter lower floor's inert filler layer 6 from inside distributor 16, then two strands of products are simultaneously through exit gas distributor 13, flow out from reactor outlet pipe 14, reaction bed pressure reduces to 0.06MPa.
Board-like hydrogenation reactor can obtain more massive reaction unit by the quantity of the size or increase unit process body that increase unit process body.This is just different from the too huge shortcoming of volume after shell and tube reactor expansion scale.
Claims (13)
1. the industrialization plate-type reactor for hydrogenation of oxalate for preparing ethylene glycol or ester through hydrogenation alcohol, it is characterized in that, comprise successively be from top to bottom positioned at entrance point Reactor inlet pipe (1), inlet gas distributor (2), Heat Room (15), upper end inert filler layer (3), intermediate radial reaction bed (4), lower end inert filler layer (6), exit gas distributor (13) and reactor outlet pipe (14); Described intermediate radial reaction bed (4), comprises annular space (11), outer distributing barrel (20), beds (12), inside distributor (16) and the center set tracheae (5) between reactor shell (32) inwall and outer distributing barrel (20) that are connected with upper end inert filler layer (3) from outside to inside successively;
Described beds establishes heat exchanger in (12), and the heat exchange element of heat exchanger is plate type heat exchanging element; Described plate type heat exchanging element is prefabricated heat exchanger plates (30) in groups, and described heat exchanger plates (30) is quadrilateral structure, is welded by two pieces of metallic plates, and all heat exchanger plates (30) in same reactor are identical; The plate package (24) be made up of heat exchanger plates (30) loads in tower by top manhole, be embedded in beds (12), plate package (24) is overall by being fixed on annular gusset (34) common support of reactor shell (32) inwall and center set tracheae (5) outer wall;
The arrangement mode of described plate package (24) in beds (12) is: be parallel to beds (12) radial direction and place and fan-shapedly to arrange along concentric, or be similar to concentric arrays perpendicular to beds (12) radial direction;
The side of described metallic plate and catalyst exposure is parallel-plate fin structure, and plate wing (25) spacing is 0.1 ~ 0.5mm;
Cold pipe (29) is established in described beds (12);
When plate package (24) be parallel to beds (12) radial direction place and along concentric fan-shaped array time, described cold pipe (29) is positioned between adjacent two heat exchanger plates (30) of distance reactor axle center same distance; When plate package (24) is similar to concentric arrays perpendicular to beds (12) radial direction, described cold pipe (29) is positioned between the adjacent heat exchanger plates group (24) of distance reactor axle center same distance;
Described outer distributing barrel (20) and inside distributor (16) establish perforate, by the flow direction of fluid, the perforate distribution density be in the unit length of fluid flowing upstream is comparatively large, and the perforate distribution density be in fluid flow downstream unit length is less.
2. plate-type reactor as claimed in claim 1, it is characterized in that, when plate package (24) be parallel to beds (12) radial direction place and along concentric fan-shaped arrange time, according to the size of reactor inner space and the size of heat exchanger plates itself, establish one piece of heat exchanger plates (30) along same radial direction or establish polylith heat exchanger plates (30) successively; Fixed by annular or circular fastening hoop (31) between the heat exchanger plates (30) of distance reactor axle center same distance.
3. plate-type reactor as claimed in claim 1, it is characterized in that, when plate package (24) is similar to concentric arrays perpendicular to beds (12) radial direction, same radial heat exchanger plates (30) is arranged in parallel, and plate package (24) entirety being positioned at beds (12) is surrounded fixing by being positioned near outer distributing barrel (20) inwall and the outer peripheral circular fastening hoop (31) of plate package (24).
4. plate-type reactor as claimed in claim 1, it is characterized in that, the thickness of described heat exchanger plates (30) is 0.1 ~ 1.0mm.
5. plate-type reactor as claimed in claim 1, it is characterized in that, two pieces of metallic plates of described heat exchanger plates (30) have identical impression, heat exchanger plates (30) hollow, two pieces of metallic plates peripherally weld, surperficial spot welding simultaneously, then punching press is made, the fluidly passage of the slit-shaped between two metallic plates.
6. plate-type reactor as claimed in claim 5, it is characterized in that, described impression is corrugated, linear, polyline shaped or bubbling shape.
7. plate-type reactor as claimed in claim 1, it is characterized in that, the fluid channel design of described plate type heat exchanging element, the flow direction along cooling medium comprises successively: cooling medium inlet (7), main distributing pipe (22), plate package distributing pipe (23), plate package (24), heat exchanger plates steam outlet pipe (28), plate package steam collecting pipe (33), main collecting pipe (10) and steam outlet pipe mouth (9).
8. plate-type reactor as claimed in claim 1, is characterized in that, described inlet gas distributor (2) and the upper perforate of exit gas distributor (13) are arranged as del or parallelogram.
9. plate-type reactor as claimed in claim 1, is characterized in that, the shape of described cold pipe cross section (27) is triangle, trapezoidal, square, rhombus or parallelogram.
10. plate-type reactor as claimed in claim 1, it is characterized in that, effective distance between plates of described beds (12) interior adjacent heat exchanger plates (30) or adjacent heat exchanger plates group (24) is 20 ~ 200mm.
11. plate-type reactors as claimed in claim 1, is characterized in that, described perforate is circular, square, triangle, grid or fillet shape; Described perforate be arranged as circumferential or spirality.
12. as arbitrary in claim 1-11 as described in plate-type reactor ester through hydrogenation alcohol technique or oxidation coupled reaction synthesizing dimethyl oxalate and dimethyl carbonate technique in application.
13. apply as claimed in claim 12, it is characterized in that, described ester through hydrogenation alcohol technique comprises hydrogenation of oxalate for preparing ethylene glycol technique and acetate hydrogenation produces ethanol and selective coproduction 2-butanols technique.
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| CN201210407137.XA CN102895922B (en) | 2012-10-23 | 2012-10-23 | Industrial plate type reactor for preparing glycol by hydrogenating oxalate or preparing alcohol by hydrogenating ester |
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| CN103216437B (en) * | 2013-03-29 | 2016-05-18 | 合肥通用机械研究院 | For the gas cushion of compressor test unit |
| EP3212319A1 (en) * | 2014-10-30 | 2017-09-06 | SABIC Global Technologies B.V. | Reactor comprising radially placed cooling plates and methods of using same |
| CN104841339A (en) * | 2015-04-16 | 2015-08-19 | 中国五环工程有限公司 | Novel hydrogenation reactor for synthesis gas-to-ethylene glycol process |
| CN104841340A (en) * | 2015-05-19 | 2015-08-19 | 中国五环工程有限公司 | Novel carbonylation reactor for process of producing glycol through synthesis gas |
| CN109395669A (en) * | 2017-08-18 | 2019-03-01 | 上海浦景化工技术股份有限公司 | A kind of axial-radial flow reactor for oxalic acid Arrcostab hydrogenation synthesizing of ethylene glycol |
| CN109395668A (en) * | 2017-08-18 | 2019-03-01 | 上海浦景化工技术股份有限公司 | A kind of coupled reactor for oxalic acid Arrcostab hydrogenation synthesizing of ethylene glycol |
| CN110357765B (en) * | 2018-04-09 | 2022-05-13 | 中国石化扬子石油化工有限公司 | Dimethyl succinate hydrogenation method |
| WO2020082202A1 (en) * | 2018-10-22 | 2020-04-30 | Pujing Chemical Industry Co., Ltd | Large-scale ethylene glycol reactor |
| CN109908841A (en) * | 2018-11-19 | 2019-06-21 | 易高环保能源研究院有限公司 | Reaction unit |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN2845904Y (en) * | 2004-12-14 | 2006-12-13 | 杭州林达化工技术工程有限公司 | Lateral tubular heat exchanging reaction device |
| EP2070590A1 (en) * | 2007-12-11 | 2009-06-17 | Methanol Casale S.A. | Supporting system of heat-exchange plates in isothermal chemical reactors |
| CN201161185Y (en) * | 2008-03-07 | 2008-12-10 | 钱进华 | Double-layer heat exchange plate-type reactor in parallel |
| CN102040474B (en) * | 2009-10-13 | 2013-07-31 | 中国石油化工股份有限公司 | Method for producing ethanediol from oxalic ester and hydrogen |
| CN202876771U (en) * | 2012-10-23 | 2013-04-17 | 上海戊正工程技术有限公司 | Industrialized plate type reactor for preparing glycol by oxalate hydrogenation or alcohol by ester hydrogenation |
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