CN108325476A - A kind of suspension type U-shaped vapour pipe isothermal reactor and reaction method - Google Patents
A kind of suspension type U-shaped vapour pipe isothermal reactor and reaction method Download PDFInfo
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- CN108325476A CN108325476A CN201810126070.XA CN201810126070A CN108325476A CN 108325476 A CN108325476 A CN 108325476A CN 201810126070 A CN201810126070 A CN 201810126070A CN 108325476 A CN108325476 A CN 108325476A
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- pipe
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 49
- 239000000725 suspension Substances 0.000 title claims abstract description 23
- 238000000034 method Methods 0.000 title claims abstract description 12
- 239000003054 catalyst Substances 0.000 claims abstract description 79
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 72
- 239000007789 gas Substances 0.000 claims abstract description 56
- 239000012495 reaction gas Substances 0.000 claims abstract description 15
- 239000002245 particle Substances 0.000 claims description 9
- 238000007789 sealing Methods 0.000 claims description 7
- 239000003795 chemical substances by application Substances 0.000 claims description 6
- 230000000694 effects Effects 0.000 claims description 5
- 238000011068 loading method Methods 0.000 claims description 5
- 229910052573 porcelain Inorganic materials 0.000 claims description 2
- 230000009466 transformation Effects 0.000 description 11
- 239000004744 fabric Substances 0.000 description 9
- 238000009834 vaporization Methods 0.000 description 6
- 230000008016 vaporization Effects 0.000 description 6
- 239000003034 coal gas Substances 0.000 description 5
- 239000000203 mixture Substances 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 229910002804 graphite Inorganic materials 0.000 description 3
- 239000010439 graphite Substances 0.000 description 3
- 230000002779 inactivation Effects 0.000 description 3
- 238000012423 maintenance Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000005997 Calcium carbide Substances 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000032683 aging Effects 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000010410 dusting Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000005457 optimization Methods 0.000 description 2
- 230000005855 radiation Effects 0.000 description 2
- 230000036632 reaction speed Effects 0.000 description 2
- 230000008439 repair process Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- AFTDTIZUABOECB-UHFFFAOYSA-N [Co].[Mo] Chemical class [Co].[Mo] AFTDTIZUABOECB-UHFFFAOYSA-N 0.000 description 1
- 238000007259 addition reaction Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000003250 coal slurry Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 230000011218 segmentation Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0285—Heating or cooling the reactor
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/40—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with water vapor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
- B01J2208/00132—Tubes
Abstract
The invention discloses a kind of suspension type U-shaped vapour pipe isothermal reactor and reaction methods.The isothermal reactor includes outer barrel, inner cylinder and catalyst cylinder；The inner cavity top of the inner cylinder is equipped with bobbin carriage, is equipped with steam isolating cylinder in the bobbin carriage, which is divided into two regions of hydroecium and steam chest by the inner cavity of bobbin carriage；The catalyst cylinder is equipped with more U-shaped vapour pipes, and wherein one end of U-shaped vapour pipe is connected to the water inlet on bobbin carriage hydroecium, and the other end of U-shaped vapour pipe is connected to the venthole on bobbin carriage steam chest；The outer barrel bottom is equipped with unreacting gas entrance and reaction gas exports, and the annular gap between the unreacting gas entrance and inner barrel and outer barrel is connected to, which is connected to the inner cavity of catalyst cylinder.The isothermal reactor resistance of the present invention is extremely low, and operation is easy, equipment is simple, light-weight and catalyst service life is long.
Description
Technical field
The present invention relates to a kind of suspension type U-shaped vapour pipe isothermal reactor and reaction method, be mainly used in inorganic chemical industry,
In organic chemical industry, environmental engineering, it is particluarly suitable for carrying out CO under constant temperature low temperature and steam reaction is transformed into CO2With H2's
Technique.
Background technology
Coal gas, natural gas conversion gas, oven gas conversion gas, calcium carbide stove exhaust, blast furnace gas, coal gas of converter etc., these gas
Body contains a large amount of CO, such as CO contents in calcium carbide tail gas are 80% or so, in coal gasification producer gas CO contents be~
65%, water-coal-slurry coal gas CO contents be~45%, CO it is convertible be H processed2Effective way, reaction equation is：
CO+H2O（Vapour）CO2+H2+Q
Transformationreation is reversible exothermic reaction, it is necessary to have catalyst and excessive H2O（Water vapour）It can just make reaction to generation H2
Direction carries out, wherein Q=9590cal/mol.
High CO transformation is mostly used cobalt-molybdenum series catalyst, and use temperature range is 200 DEG C~470 DEG C.
Because CO transformation is strong exothermal reaction, the heat of releasing makes catalyst bed heat up, once temperature makes more than catalyst
With temperature, catalyst dusting, sintering, inactivation are easily led to.1%CO is often reacted by equation calculating（Butt）, 5 DEG C~6 DEG C of temperature liter；
CO contents are higher in coal gas, i.e. transformation CO is more, Wen Shengyue high.
Such as：Coal gas 100（Mol, butt）, CO65%, water-gas ratio R=1.1, CO is 13% after transformation（Mol, butt）,
Release heat：52×9590=498680Kcal/h；
Specific heat capacity Cp：9.01kcal/kmol.℃；
Reacting rear material：208kmol/h；
498680=208×9.01×△t=266.1℃
If 245 DEG C of temperature before reaction, temperature is after reaction：266.1+245=511.1℃.
This temperature（511.1℃）Maximum temperature is used higher than catalyst, the activity of catalyst can be seriously affected, cause to convert
Efficiency reduces.
Therefore, the temperature for how controlling reaction process is allowed to be no more than the maximum operation (service) temperature that catalyst allows, while again
Water-gas ratio is controlled, is allowed to add water vapour reduction, also to inhibit methanation reaction after water vapour reduction.Rationally control
Reaction temperature is the key that transformationreation safety and stability Effec-tive Function.
Traditional control temperature methods are：Segmentation adiabatic reaction -- heating -- moves hot cooling mode, and this pattern is for height
CO% gas conversions have shortcomings, if equipment number of units is more, long flow path, and the easy overtemperature of first segment, catalyst dusting easy to aging.
Modern reaction heat cool-down method is：Phase transformation moves hot isothermal method.It buries and is permitted i.e. in reactor catalyst bed
More water pipes, water absorbing reaction hot vapour turn to water vapour, and the latent heat of vaporization is very big, and vapourizing temperature is constant, therefore catalysts bed
Keep Isothermal Condition.
Existing waterpipe type phase transformation moves thermal conversion reactor, there is double-jacket tube formula, single hose, wherein more outstanding is double sets
Tubular type（Or perverse blade）Reactor, such as the Chinese invention patent application CN201610652865.5 applied before applicant, water
Pipe is after heated, and the free reduction of energy, securely and reliably, the time between overhauls(TBO) is up to 6 to seven years.This reactor can react machine by CO
Reason, reaction beginning reaction speed is fast, needs catalytic amount few, and exothermic heat of reaction is more, needs heat exchange area big, and stringing is more and close.Instead
It answers end reaction speed slow, needs catalytic amount more, exothermic heat of reaction is few, needs heat exchange area small, stringing is rare and dilute.Maintenance week
Phase is up to 6 to seven years, in addition reaction temperature is up to 6 to seven years in constant temperature low temperature per furnace catalyst service life, but deficiency
Place is that inner tube only has guide functions, non-heat transfer area, therefore consumable material is more, and reactor is heavy, and large-scale plant transport is limited,
Investment is more.Single hose reactor, general upper and lower ends nozzle and gas collection divide compression ring pipe or cylinder mutually to weld, and cannot be wanted by reaction
Dilute, density stringing is sought, the fillet welding difficulty that connects is larger, and quality is difficult to control.
Invention content
The present invention is intended to provide a kind of suspension type U-shaped vapour pipe isothermal reactor and reaction method, which has existing
The advantages of for double-jacket tube formula water cooling pipe reactor, while low temperature isothermal at high CO transformationreations can be made to reach any transformation rate, it hinders
Power is extremely low, and operation is easy, equipment is simple, light-weight and catalyst service life is long.
To achieve the goals above, the technical solution adopted in the present invention is：
A kind of suspension type U-shaped vapour pipe isothermal reactor, including outer barrel, the inner cylinder being set in outer barrel, for filling out in inner cylinder
Fill the catalyst cylinder of catalyst；It is structurally characterized in that：The inner cavity top of the inner cylinder is equipped with bobbin carriage, be equipped in the bobbin carriage steam every
From cylinder, which is divided into two regions of hydroecium and steam chest by the inner cavity of bobbin carriage；
The catalyst cylinder is equipped with more U-shaped vapour pipes, wherein one end of U-shaped vapour pipe and the water inlet on bobbin carriage hydroecium
Connection, the other end of U-shaped vapour pipe are connected to the venthole on bobbin carriage steam chest；
The outer barrel bottom is equipped with unreacting gas entrance and reaction gas exports, between the unreacting gas entrance and inner barrel and outer barrel
Annular gap is connected to, which is connected to the inner cavity of catalyst cylinder, and reaction gas outlet is with setting at catalyst cylinder center
The center gas collecting tube connection being vertically arranged, the center gas collecting tube are used to collect the reaction gas after reacting in catalyst cylinder.
As a result, after unreacting gas enters the annular gap between inner barrel and outer barrel from unreacting gas entrance, urged entering
The inner cavity of agent cylinder is reacted under the effect of the catalyst, and when reaction enters effect of the water in U-shaped vapour pipe in reaction heat
Lower gradually vaporization, the other end of the steam U-shaped vapour pipe after vaporization overflows, to make low temperature isothermal at high CO transformationreations reach
Any transformation rate, and reaction gas flow dynamic resistance is extremely low, avoids catalyst inactivation, improves the service life of catalyst.Reaction
Gas collection afterwards is in the gas collecting tube of center, then exports and be discharged from reaction gas.
According to an embodiment of the invention, further optimization can also be made to the present invention, below the skill to be formed after optimization
Art scheme：
For the situation that reaction early period is different with late phase reaction heat release is reacted, the inside region of the steam isolating cylinder is and water inlet
The hydroecium of mouth connection, lateral area is steam chest, and the water ring chuck being connected to water inlet is equipped in the steam chest；The U-shaped vapour pipe
In one end of first part be connected to water ring chuck, the other end of first part is connected to steam chest, in the U-shaped vapour pipe
One end of two parts is connected to hydroecium, and the other end of second part is connected to steam chest.Pass through water ring chuck and hydroecium two-way in this way
Water inlet, steam are overflowed from steam chest, so as to arrange U-shaped vapour pipe according to the size of reaction heat.
As a kind of specific arrangement form, the U-shaped vapour pipe is divided into two groups, and one of which is the first U-shaped vapour pipe,
Another group is the second U-shaped vapour pipe；Wherein the first U-shaped vapour pipe is arranged in the central area of catalyst cylinder, the second U-shaped vapour pipe
It is circumferentially provided on the outside of the first U-shaped vapour pipe；The water inlet end of the first U-shaped vapour pipe is connected to the water ring chuck, the
The water inlet end of two U-shaped vapour pipes is connected to the hydroecium, the steam output end of the first U-shaped vapour pipe and the second U-shaped vapour pipe
Steam output end is connected to the steam chest；It is preferred that the center gas collecting tube is located at the central area of the first U-shaped vapour pipe.As a result,
One U-shaped vapour pipe is mainly responsible for transmission of the reaction later stage to exothermic heat of reaction, and the second U-shaped vapour pipe, which is mainly responsible for, reacts early period to anti-
Exothermic transmission is answered, to ensure that reaction heat is quickly exported, avoids catalyst inactivation.
Steam isolating cylinder is overhauled for convenience, the steam isolating cylinder includes at least two pieces and concentric can relatively turn
Dynamic arc panel, wherein in adjacent two pieces of arc panels, the inside radius of one piece of arc panel is not less than the outer radius of another piece of arc panel,
And it is equipped with sealing element in the junction of two pieces of arc panels；The steam isolating cylinder includes working condition and inspecting state, wherein：
Working condition is that at least two pieces of arc panels rotate to form generally columnar structure,
Inspecting state is that the concentric rotation of at least two pieces of arc panels is superimposed together.
Thus, it is desirable to when overhauling, the concentric rotation of arc panel is allowed to be superimposed together, so as to examine inside
Repair, when needing work, then by arc panel it is concentric rotation and fixation form columnar structure.
In order to facilitate the realization concentric rotation of arc panel, in the top of the steam isolating cylinder and the top of inner cylinder or bobbin carriage
It is equipped with sealing ring between wall, annular slide track is equipped between the bottom end of the steam isolating cylinder and the bottom interior wall of bobbin carriage；It is preferred that described
It is provided with cancave cambered surface on the top end face of arc panel, there is the bottom face of the arc panel convex spherical, the annular slide track to be equipped with and institute
State the cancave cambered surface annular groove of convex spherical cooperation.
Preferably, according to an embodiment of the invention, the steam isolating cylinder includes two pieces of semicircular arc panels.As a result,
Two pieces of semicircular arc panels are oppositely arranged in working condition and form monoblock type tubular structure, are superimposed in inspecting state
Together.
In order to facilitate providing water inlet and collect steam, the top of the outer barrel is equipped with drum, the drum by water pipe with into
The mouth of a river is connected to, which is connected to by steam pipe with venthole.Drum is down to U-shaped vapour pipe on one side under water, the outer reaction heat of absorption tube,
Gradually vaporization rises from another side, continues heated vaporization, and gas-vapor mix rises to drum, and steam is sent outside, underwater to drop, and constitutes
Water, steam circulation.
Preferably, the top of the outer barrel is equipped with drum, which is connected to by the first water pipe with hydroecium, which passes through
Second water pipe is connected to water ring chuck, and drum is connected to by steam pipe with steam chest.
It is reacted to ensure that gas can enter in catalyst cylinder to slight drag, the bottom of the catalyst cylinder is equipped with
Even balloon, equipped with the U-shaped vapour pipe for wrapping up the catalyst above even balloon；It is preferred that the catalysis of catalyst cylinder middle and upper part
Agent particle size is more than the catalyst particle size of catalyst cylinder middle and lower part.The catalyst particle size on top is more than and urges as a result,
The design of the catalyst particle size of agent cylinder lower part, to different to the demand of catalyst in catalyst cylinder according to reaction gas
And it is equipped with different.
Based on the same inventive concept, it is anti-using the suspension type U-shaped vapour pipe isothermal that the present invention also provides a kind of
Device is answered to carry out CO H2The method of reaction comprising gas reaction step and water gas shift step, wherein：
Gas reaction step is：Unreacting gas enters the annular gap between inner barrel and outer barrel from unreacting gas entrance, enters back into
It is reacted under the effect of the catalyst in catalyst cylinder, the gas collection after reaction is in the gas collecting tube of center, then from reaction gas
Outlet discharge；
Water gas shift step is：Water is flowed into from the water inlet of the first branch pipe of U-shaped vapour pipe, from the first branch pipe from top to bottom to U
The bottom of shape vapour pipe gradually vaporizes, be then folded to from the bottom of U-shaped vapour pipe and along the second branch pipe of U-shaped vapour pipe by lower and
On continue to vaporize, vapor enters from the venthole of the second branch pipe in bobbin carriage.
Compared with prior art, the beneficial effects of the invention are as follows：
1, have the advantages that double set water cooling pipe reactors all.
2, bobbin carriage substitutes tube sheet or pipe ring, and stringing is more, and relative weight is light.
3, light-weight without casing in U-shaped vapour pipe.
4, suspension type U-shaped vapour pipe, it is stronger to bear hot shrinkage ability, more reliable.
5, the outer barrel top of suspension type U-shaped vapour pipe isothermal reactor is there are space, and inner cylinder integrally can be to freely up and down stretching
Contracting.
6, the steam isolating cylinder of bobbin carriage a/b two halves cylinder composition, service personnel can enter bobbin carriage, mobile a one side of something be allowed to
Another b one side of something re-posteds check and repair bottom tube sheet and its half of cylinder nozzle weld seam.Same manner can overhaul another half of cylinder pipe
Mouth weld seam.
7, can, gather hole dilute by reaction process requirement, two kinds of U-shaped vapour pipe different areas of a/b shapes ensure automatically by best
Temperature line is reacted.
8, aperture radial direction catalyst cylinder extends at the top of inner cylinder, and catalyst is also filled to the top envelope of aperture radial direction catalyst cylinder
Head, unreacting gas reach from below to up top, from this radial through catalyst reach center gas collecting tube, top without circulation dead angle,
Keep volumetric efficiency big, catalyst agent utilization rate is high.
9, drum position height is appropriate, it is ensured that unpowered Water, steam circulation is realized in driving and parking or when with underrun.
In short, present invention is mainly applied to the gas deep conversions of high CO contents into H2, and it is further used as synthesis ammonia, first
Alcohol, acetic acid, ethylene glycol and other synthesis technologies and reactor.
Description of the drawings
Fig. 1 is the structure principle chart of one embodiment of the invention；
Fig. 2 is the elevational schematic view of bobbin carriage in Fig. 1；
Fig. 3 is a certain cross-sectional view of Fig. 2；
Fig. 4 is the schematic diagram that rack is supported in an embodiment of the present invention；
Fig. 5 is the schematic diagram of stringing on bobbin carriage in an embodiment of the present invention；
Fig. 6 is the partial enlarged view of a quarter covering of the fan of Fig. 5；
Fig. 7 is the elevational schematic view of isolating cylinder in an embodiment of the present invention；
Fig. 8 is the vertical section schematic diagram of Fig. 7；
Fig. 9 is a certain cross-sectional view in Fig. 7.
Specific implementation mode
Come that the present invention will be described in detail below with reference to attached drawing and in conjunction with the embodiments.It should be noted that in the feelings not conflicted
Under condition, the feature in embodiment and embodiment in the present invention can be combined with each other.For sake of convenience, hereinafter as occurred
"upper", "lower", "left", "right" printed words only indicate consistent with the upper and lower, left and right direction of attached drawing itself, do not play limit to structure
It is set for using.
A kind of suspension type U-shaped vapour pipe isothermal reactor（Attached drawing 1）Including drum 1, cylinder 3 is overhauled, outer barrel 8, inner cylinder 13 is small
Hole radial direction catalyst cylinder 14, cloth bobbin carriage 18, two pieces of semicircular arc board group contract axle center separating tubes 19, water ring set 4, the first U-shaped water
Steam pipe 9, the second U-shaped vapour pipe 10, center gas collecting tube 11, charging aperture 20, dumping pit 16, bottom threeway 15 of ventilating.
As shown in Figures 2 and 3, bobbin carriage is generally cylindrical, is divided by one or two semicircular arc board group contract axle center separating tube 19
For inside and outside two circle, inner ring is water, and outer ring is vapour.As shown in FIG. 8 and 9, separating tube 19 includes first part 23 and second part
24, first part 23 and second part 24 are semicircular arc plate, and wherein the inside radius of first part 23 is equal to or slightly greater than the
The outer radius of two parts 24.Two pieces of semicircular arc board groups close the cylindrical tube to form a monoblock type, and overlap is long side
Triangle also folds sealing strip 26 between first part 23 and second part 24, in the company of first part 23 and second part 24
The place of connecing is removably secured connected by fastener 27.As shown in figure 9, separating tube 19 combines to separate for two semicylindrical bodies
Two kinds of vapour, water materials, reactor are an entire barrels when running, and there is sealing strip 26 in the two joint, when out-of-service inspection overhauls,
One in two semicircular arc plates can do concentric movement, and in addition be bonded on one side, it is mobile after half of pore open wide, be convenient for
Check that maintenance, the same concentric inner cylinder of water ring chuck also move.
As shown in figure 8, there is the top end face of first part 23 and second part 24 cancave cambered surface 30, bottom face to have convex spherical
31, O-ring seals 28, preferably flexible graphite sealing ring are housed on cancave cambered surface 30.First part 23 and second part 24
Bottom face is arranged on soft graphite circuit 29, and the upper surface of soft graphite circuit 29 has the cancave cambered surface coordinated with convex spherical 31
Annular groove, first part 23 or second part 24 relatively move when convenient to overhaul.
As shown in Figures 2 and 3, there is half-section chuck in bobbin carriage barrel middle and upper part, claims water ring set 4, lower part is dished (torispherical) head, cylindrical surface
And more U-shaped vapour pipes are laid on lower dished (torispherical) head, pipelaying method is：Cylindrical surface is divided into about dry lattice by axial, per lattice distance
12~15mm, axially at least can three layers of U-shaped vapour pipe of cloth per lattice.This set of dished (torispherical) head presses diametric(al) cloth the first U-shaped vapour pipe
9, radius minimum cloth three in one side encloses U-shaped vapour pipe, and symmetrical another side radius also at least can the first U-shaped vapour pipe 9 of circle of cloth three.
Suspension type U-shaped vapour pipe isothermal reactor, catalyst are loaded into internals, wherein embedded U-shaped vapour pipe, bobbin carriage are
Cylinder, U-shaped vapour pipe cloth are welded on dished (torispherical) head and cylindrical surface.
When unreacting gas is from periphery toward central flow, by radial radiation shape stringing, radial tube spacing outer ring is small, toward center
Tube spacing is big.
When unreacting gas is flowed to from periphery toward center, by radial radiation shape stringing, radial tube spacing outer ring is small, toward center
Tube spacing is big.The tube bank of U-shaped steam is about beam 8m~14m, includes multiple grids in uniformly distributed three to four of the length direction of tube bank
Grid ring made of support rack 25, so as in manufacture and transport, reactor is under horizontal state, and support rack 25 can
Support the tube bank of U-shaped vapour pipe.
Bent for ease of U-shaped vapour pipe, innermost circle arc radius is 1.8 times of pipe outside diameter, as pipe outside diameter specification is 25 ×
2, then minimum arc radius is 45mm, upper and lower two U-shapeds vapour pipe lower end distance 6mm~8mm.
Reaction gas, steam flow in the course of work of the present invention are:Unreacting gas enters inner/outer tube annular from bottom threeway 15
Then gap and from bottom to top by each aperture of aperture radial direction catalyst cylinder radial inswept catalyst and is embedded in catalyst
Vapour pipe, reaction release heat and are absorbed and vaporized by vapour pipe water, and catalyst temperature keeps relative stability without significantly increasing.Instead
Reaction gas after answering is in aperture radial direction catalyst cylinder, centralization gas collecting tube 11, then is from top to bottom gone out by bottom threeway 15
Mouth discharge.
Steam flow in the course of work of the present invention is：From 1 time water of drum up to hydroecium 5, water ring chuck 4, water in hydroecium
Water pipe through 10 inside of the second U-shaped vapour pipe is gradually vaporized to bottom from top to bottom, then from the bottom of the second U-shaped vapour pipe 10
It is folded to from bottom to top, the water pipe in 10 outside of the second U-shaped vapour pipe continues to vaporize, and vapor rises to steam chest 6, by connection drum 1
Steam Pipe leads to drum 1.Water pipe of the water through 9 outside of the first U-shaped vapour pipe is from top to bottom to the gradual vapour in bottom in water ring chuck 4
Change, be then folded to from bottom to top from the bottom of the first U-shaped vapour pipe 9, the water pipe of 9 inside of the first U-shaped vapour pipe continues to vaporize, water
Steam rises to steam chest 6, reaches drum 1 by the Steam Pipe of connection drum 1.
After drum supplements water, for water toward downstream to each U-shaped vapour pipe, steam is sent to pipe after steam-water separation in gas-vapor mix
Net.
The drum position height of the present invention is to ensure driving and parking or when with underrun, realize that unpowered Water, steam circulation is
Principle.
Symmetrical two charging apertures 20 of outer barrel top end socket and tube sheet centre charging mouth 7 of loading catalyst of the present invention are packed into,
After running the several years, catalyst aging is drawn off from symmetrical two discharge ports 16 of outer barrel bottom bulkhead.Inner/outer tube top end socket is equipped with one
Isodiametric maintenance cylinder 3.
The internals of the reactor of the present invention are supported on outer barrel bottom, and there are space, inner cylinder integrally can be to upper and lower on outer barrel top
Freely stretch.
The area ratio of two U-like shape vapour pipes of the reactor of the present invention is different in catalyst cylinder flow direction with gas,
If unreacting gas is from around, toward center stream, the first U-shaped vapour pipe area accounts for the gross area 60%~70%, manages outer catalyst and accounts for always
The 35%~45% of catalyst.
The cylinder height and barrel diameter of the bobbin carriage 20（h/d）, claim ratio of height to diameter, with the first U-shaped vapour pipe, the second U-shaped
The area of vapour pipe respectively accounts for depending on the ratio of the gross area, and when the first U-shaped vapour pipe area accounting is larger, ratio of height to diameter is larger, on the contrary
Ratio of height to diameter is smaller.
The built-in granular size of suspension type U-shaped vapour pipe isothermal reactor warp-wise cylinder body bottom end socket of the present invention is 6~8mm
Porcelain ball, then up all fill catalyst from this（Catalyst particle 22）, until end socket part dress larger particles are urged at the top of cylinder
Agent（Catalyst particle 21）.
In the transformation system of the present invention, air inlet 34827Nm3/h, CO60% after isothermal converts, be down to by CO contents in gas
7.5%。
Suspension type isothermal transformation using the present invention, the specification of change furnace is DN4600 × 14000, and the specification of bobbin carriage is
DN3200 × 1000, loading catalyst total amount 140m3,7280 ㎡ of the cloth U-shaped vapour pipe gross area, outer ring loading catalyst account for total face
Product total amount 44%, cloth U-shaped vapour pipe area account for the gross area 62%, and inner ring loading catalyst accounts for total amount 56%, cloth U-shaped vapour pipe area
Account for the gross area 38%.
Contain higher CO unreacting gas in the present invention from periphery by catalyst reaction, toward center flow direction, CO reactions are reduced to
It is required that after content, in the gas collecting tube of centralization, drum is down to U-shaped vapour pipe on one side under water, the outer reaction heat of absorption tube, gradual vapour
Change, rise from another side, continue heated vaporization, gas-vapor mix rises to drum, and steam is sent outside, underwater to drop, and constitutes steam and follows
Ring.Reactor advantage can make low temperature isothermal at high CO transformationreations reach any transformation rate, and resistance is extremely low, operate easy, equipment
Simply, light-weight, catalyst service life is long.
The content that above-described embodiment illustrates should be understood as that these embodiments are only used for being illustrated more clearly that the present invention, without
For limiting the scope of the invention, after having read the present invention, various equivalent forms of the those skilled in the art to the present invention
Modification each fall within the application range as defined in the appended claims.
Claims (10)
1. a kind of suspension type U-shaped vapour pipe isothermal reactor, including outer barrel（8）, it is set to outer barrel（8）Interior inner cylinder（13）, it is set to
Inner cylinder（13）The interior catalyst cylinder for loading catalyst（14）；It is characterized in that：The inner cylinder（13）Inner cavity top be equipped with
Bobbin carriage（18）, the bobbin carriage（18）It is interior to be equipped with steam isolating cylinder（19）, the steam isolating cylinder（19）By bobbin carriage（18）Inner cavity be divided into
Two regions of hydroecium and steam chest；
The catalyst cylinder（14）Equipped with more U-shaped vapour pipes, wherein one end of U-shaped vapour pipe be located at bobbin carriage（18）On hydroecium
Water inlet connection, the other end of U-shaped vapour pipe be located at bobbin carriage（18）Venthole connection on steam chest；
The outer barrel（8）Bottom is equipped with unreacting gas entrance and reaction gas exports, the unreacting gas entrance and inner cylinder（13）With it is outer
Cylinder（8）Between annular gap connection, the annular gap and catalyst cylinder（14）Inner cavity connection, the reaction gas outlet and setting
In catalyst cylinder（14）The center gas collecting tube that center is vertically arranged（11）Connection, the center gas collecting tube（11）It is being catalyzed for collecting
Agent cylinder（14）Reaction gas after interior reaction.
2. suspension type U-shaped vapour pipe isothermal reactor according to claim 1, which is characterized in that the steam isolating cylinder
（19）Inside region be the hydroecium being connected to water inlet（5）, lateral area is steam chest, is equipped in the steam chest and is connected to water inlet
Water ring chuck（4）；One end of first part in the U-shaped vapour pipe and water ring chuck（4）Connection, first part it is another
End is connected to steam chest, one end of the second part in the U-shaped vapour pipe and hydroecium（5）Connection, the other end and vapour of second part
Room is connected to.
3. suspension type U-shaped vapour pipe isothermal reactor according to claim 2, which is characterized in that the U-shaped vapour pipe point
It it is two groups, one of which is the first U-shaped vapour pipe（9）, another group is the second U-shaped vapour pipe（10）；Wherein the first U-shaped vapour pipe
（9）It is arranged in catalyst cylinder（14）Central area, the second U-shaped vapour pipe（10）It is circumferentially provided on the first U-shaped vapour pipe（9）'s
Outside；The first U-shaped vapour pipe（9）Water inlet end and the water ring chuck（4）Connection, the second U-shaped vapour pipe（10）Into
Water end (W.E.) and the hydroecium（5）Connection, the first U-shaped vapour pipe（9）Steam output end and the second U-shaped vapour pipe（10）Steam output end
It is connected to the steam chest；It is preferred that the center gas collecting tube（11）Positioned at the first U-shaped vapour pipe（9）Central area.
4. suspension type U-shaped vapour pipe isothermal reactor according to claim 2, which is characterized in that the steam isolating cylinder
（19）Including at least two pieces can concentric relative rotation arc panel, wherein in adjacent two pieces of arc panels, one piece of arc panel it is interior
Radius is not less than the outer radius of another piece of arc panel, and is equipped with sealing element in the junction of two pieces of arc panels；The steam every
From cylinder（19）Including working condition and inspecting state, wherein：
Working condition is that at least two pieces of arc panels rotate to form generally columnar structure,
Inspecting state is that the concentric rotation of at least two pieces of arc panels is superimposed together.
5. suspension type U-shaped vapour pipe isothermal reactor according to claim 4, which is characterized in that the steam isolating cylinder
（19）Top and inner cylinder（13）Or bobbin carriage（18）Top inner wall between be equipped with sealing ring（28）, the steam isolating cylinder（19）'s
Bottom end and bobbin carriage（18）Bottom interior wall between be equipped with annular slide track；It is preferred that being provided with cancave cambered surface on the top end face of the arc panel
（30）, the bottom face of the arc panel is with convex spherical（31）, the annular slide track be equipped with and the convex spherical（31）Cooperation
Cancave cambered surface annular groove.
6. suspension type U-shaped vapour pipe isothermal reactor according to claim 4, which is characterized in that the steam isolating cylinder
（19）Including two pieces of semicircular arc panels.
7. the suspension type U-shaped vapour pipe isothermal reactor according to any one of claim 1-6, which is characterized in that described
Outer barrel（8）Top be equipped with drum（1）, the drum（1）It is connected to water inlet by water pipe, the drum（1）By steam pipe with go out
Steam ports is connected to.
8. suspension type U-shaped vapour pipe isothermal reactor according to claim 2 or 3, which is characterized in that the outer barrel（8）
Top be equipped with drum（1）, the drum（1）Pass through the first water pipe and hydroecium（5）Connection, the drum（1）By the second water pipe with
Water ring chuck（4）Connection, drum（1）It is connected to steam chest by steam pipe.
9. the suspension type U-shaped vapour pipe isothermal reactor according to any one of claim 1-6, which is characterized in that described
Catalyst cylinder（14）Bottom porcelain ball is housed, equipped with the U-shaped vapour pipe for wrapping up the catalyst above even balloon；It is preferred that described
Catalyst cylinder（14）The catalyst particle size of middle and upper part is more than catalyst cylinder（14）The catalyst particle size of middle and lower part.
10. a kind of suspension type U-shaped vapour pipe isothermal reactor using described in any one of claim 1-9 carries out CO H2Instead
The method answered, which is characterized in that including gas reaction step and water gas shift step, wherein：
Gas reaction step is：Unreacting gas enters inner cylinder from unreacting gas entrance（13）And outer barrel（8）Between annular gap,
Enter back into catalyst cylinder（14）It is inside reacted under the effect of the catalyst, the gas collection after reaction is in center gas collecting tube（11）
It is interior, then export and be discharged from reaction gas；
Water gas shift step is：Water is flowed into from the water inlet of the first branch pipe of U-shaped vapour pipe, from the first branch pipe from top to bottom to U
The bottom of shape vapour pipe gradually vaporizes, be then folded to from the bottom of U-shaped vapour pipe and along the second branch pipe of U-shaped vapour pipe by lower and
On continue to vaporize, vapor enters bobbin carriage from the venthole of the second branch pipe（18）It is interior.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109054908A (en) * | 2018-09-30 | 2018-12-21 | 中石化宁波工程有限公司 | A kind of isothermal conversion process of mating coal gasification |
| CN109052318A (en) * | 2018-09-30 | 2018-12-21 | 中石化宁波工程有限公司 | Isothermal shift-converter |
| CN109603689A (en) * | 2018-12-26 | 2019-04-12 | 湖南安淳高新技术有限公司 | Axial-radial flow reactor |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH06218270A (en) * | 1993-01-26 | 1994-08-09 | Mitsubishi Gas Chem Co Inc | Vertical type fluidized bed catalyst reactor |
| JPH06263405A (en) * | 1993-03-16 | 1994-09-20 | Tokyo Gas Co Ltd | Hydrogen producing device |
| US6365114B1 (en) * | 1999-02-10 | 2002-04-02 | Eisenmann Maschinenbau Kg | Reactor for performing a catalytic reaction |
| CN101898103A (en) * | 2010-02-24 | 2010-12-01 | 南京钟腾化工有限公司 | Molten salt internal circulating reactor with annual output of maleic anhydride up to 20,000t and reaction process thereof |
| CN203484134U (en) * | 2013-09-10 | 2014-03-19 | 张立军 | Water pipe type reaction device with steam pockets |
| CN106111022A (en) * | 2016-08-10 | 2016-11-16 | 湖南安淳高新技术有限公司 | Reactor |
| CN206156745U (en) * | 2016-09-22 | 2017-05-10 | 湖北三宁化工股份有限公司 | Novel isothermal shift -converter |
| CN208003921U (en) * | 2018-02-08 | 2018-10-26 | 湖南安淳高新技术有限公司 | Suspension type U-tube isothermal reactor |
-
2018
- 2018-02-08 CN CN201810126070.XA patent/CN108325476A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH06218270A (en) * | 1993-01-26 | 1994-08-09 | Mitsubishi Gas Chem Co Inc | Vertical type fluidized bed catalyst reactor |
| JPH06263405A (en) * | 1993-03-16 | 1994-09-20 | Tokyo Gas Co Ltd | Hydrogen producing device |
| US6365114B1 (en) * | 1999-02-10 | 2002-04-02 | Eisenmann Maschinenbau Kg | Reactor for performing a catalytic reaction |
| CN101898103A (en) * | 2010-02-24 | 2010-12-01 | 南京钟腾化工有限公司 | Molten salt internal circulating reactor with annual output of maleic anhydride up to 20,000t and reaction process thereof |
| CN203484134U (en) * | 2013-09-10 | 2014-03-19 | 张立军 | Water pipe type reaction device with steam pockets |
| CN106111022A (en) * | 2016-08-10 | 2016-11-16 | 湖南安淳高新技术有限公司 | Reactor |
| CN206156745U (en) * | 2016-09-22 | 2017-05-10 | 湖北三宁化工股份有限公司 | Novel isothermal shift -converter |
| CN208003921U (en) * | 2018-02-08 | 2018-10-26 | 湖南安淳高新技术有限公司 | Suspension type U-tube isothermal reactor |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109054908A (en) * | 2018-09-30 | 2018-12-21 | 中石化宁波工程有限公司 | A kind of isothermal conversion process of mating coal gasification |
| CN109052318A (en) * | 2018-09-30 | 2018-12-21 | 中石化宁波工程有限公司 | Isothermal shift-converter |
| CN109052318B (en) * | 2018-09-30 | 2022-04-08 | 中石化宁波工程有限公司 | Isothermal shift reactor |
| CN109603689A (en) * | 2018-12-26 | 2019-04-12 | 湖南安淳高新技术有限公司 | Axial-radial flow reactor |
| CN109603689B (en) * | 2018-12-26 | 2021-08-31 | 湖南安淳高新技术有限公司 | Axial radial reactor |
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