CN104645897B - The controlled water shifting heat reactor of a kind of double-seal head - Google Patents
The controlled water shifting heat reactor of a kind of double-seal head Download PDFInfo
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- CN104645897B CN104645897B CN201510072235.6A CN201510072235A CN104645897B CN 104645897 B CN104645897 B CN 104645897B CN 201510072235 A CN201510072235 A CN 201510072235A CN 104645897 B CN104645897 B CN 104645897B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—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
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
- C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
- C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
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- 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
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- 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
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0833—Heating by indirect heat exchange with hot fluids, other than combustion gases, product gases or non-combustive exothermic reaction product gases
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0872—Methods of cooling
- C01B2203/0888—Methods of cooling by evaporation of a fluid
- C01B2203/0894—Generation of steam
Abstract
The invention discloses the controlled water shifting heat reactor of a kind of double-seal head, the top of main cylinder connects lower flange, and the bottom of main cylinder connects lower outside head, and upper flange is connected with lower flange; One end of described Catalyst packing pipe is connected between interior end socket and gas distributing cylinder, the other end is successively through dividing plate and upper outside head, described aqueduct one end is communicated between dividing plate and upper outside head, the other end is set in heat exchanger tube, the body of described heat exchanger tube is positioned at gas distributing cylinder, the outlet of heat exchanger tube dividing plate and between end socket, the cylindrical shell of described gas collecting jar with ground-on cover plate is positioned at gas distributing cylinder, the outlet of gas collecting jar with ground-on cover plate connects gas outlet. Heat exchanger tube is embedded in to beds inside can be removed beds internal-response heat in time, the defect such as efficiently solve catalyst short, the easy overtemperatures in service life such as existing conversion, synthetic and hydrogenation, side reaction thing is many, bed temperature is wayward, the driving time long, be difficult to maximization, operation energy consumption is high, construction investment is large.
Description
Technical field
The present invention relates to a kind of fixed bde catalyst, the conversion under gas phase state, synthetic, hydrogenation reactor, in particularThe controlled water shifting heat reactor of a kind of double-seal head.
Background technology
After CO transformationreation, device is as a kind of extensive use reactor of chemical industry, and therebetween, people have carried out shift-converterImprovement repeatedly, by original holoaxial to change into overall diameter to, aspect catalyst bed layer resistance, obtaining very good effect, but catalyst bedLayer is still adiabatic reaction, and beds is divided into some beds, takes indirect heat exchange or use Technology Quenched with Water between every bed. ThisConnecing heat exchange, to reclaim transformation system heat energy grade low, reclaims sensible heat and latent heat efficiency is low, the easy overtemperature of catalyst, conversion simultaneously are also mixed withThe defects such as side reaction such as methanation.
The carbonylation of coal-ethylene glycol synthesizes reactor, adopts at present the interior loading catalyst of pipe of ф 25X2, pipe external application water shifting heat,A shell-and-tube reactor is made up of to ф 21 cylinder shape catalyst beds thousands of holoaxials, and distribution of gas is inhomogeneous, side reaction thingMany, catalyst bed layer resistance is large, thermal stress is large, equipment leakage, the carbonylation of glycol unit of a set of 200,000 tons/year are syntheticThe defects such as reactor needs the parallel running of 6 shell reactors, and construction investment is large.
The esterification hydrogenation reactor of coal-ethylene glycol, adopts loading catalyst in the pipe of ф 38X2, pipe external application water shifting heat, one at presentPlatform shell-and-tube reactor is made up of to ф 34 cylinder shape catalyst beds thousands of holoaxials, distribution of gas is inhomogeneous, side reaction thing is many,The defects such as catalyst bed layer resistance is large, thermal stress is large, equipment leakage, construction investment are large.
At present, the reaction of coal preparing natural gas adopts: the hot mode that moves of n adiabatic bed+n the overheated boiler that gives up, and need to increaseAdd reactants water steam and suppress first, second adiabatic bed reaction, configuration cycles gas simultaneously, otherwise occur that first, second is exhaustedHott bed layer temperature runaway phenomenon, the defect such as operation energy consumption is high, plant investment is large, SR is large.
At present, the Fischer-Tropsch synthesis of coal liquefaction, coal paraffin processed is not also at the maximization device of operation, and part is little operationType Fischer-Tropsch synthesizer reactor is also shell and tube reactor, and Fe (or Co) series catalysts is seated in ф 76X4 pipe, stillHave that distribution of gas is inhomogeneous, overtemperature, carbon distribution, long carbochain alkane yield is low, resistance large, equipment leakage, be difficult to maximize etc.Defect.
Summary of the invention
The object of the invention is to overcome the deficiencies in the prior art, provide a kind of double-seal head controlled water shifting heat reactor, utilization is changedIn heat pipe, water is converted into steam generation decalescence principle and removes in time heat of reaction in beds, and under by-product different pressuresSaturated vapor.
The present invention is achieved by the following technical solutions, the present invention includes the Catalyst packing pipe that is connected as a single entity, water inlet pipe, onOutside head, dividing plate, outlet pipe, at least one aqueduct, at least one heat exchanger tube, upper interior end socket, upper flange, distribution of gasCylinder, gas collecting jar with ground-on cover plate, lower interior end socket and catalyst self-unloading pipe, the lower flange being connected as a single entity, main cylinder, lower outside head, catalyst are certainlyUnload mouth, air inlet and gas outlet; Described water inlet pipe is opened in the top of outside head, and dividing plate is arranged at outside head and upper interior envelopeBetween head, described outlet pipe is arranged between dividing plate and upper interior end socket, the bottom of described upper outside head, the bottom of upper interior end socket andThe top of gas distributing cylinder is connected on upper flange, and the bottom of described gas distributing cylinder is connected on lower interior end socket, described gasBody distributing barrel is set in main cylinder, and the top of described main cylinder connects lower flange, and the bottom of main cylinder connects lower outside head, onFlange is connected with lower flange; One end of described Catalyst packing pipe is connected between interior end socket and gas distributing cylinder, and the other end is complied withInferior through dividing plate and upper outside head, described aqueduct one end is communicated between dividing plate and upper outside head, and the other end is set in heat exchanger tubeIn, the body of described heat exchanger tube is positioned at gas distributing cylinder, the outlet of heat exchanger tube dividing plate and between end socket, described collectionThe cylindrical shell of inflator is positioned at gas distributing cylinder, and the outlet of gas collecting jar with ground-on cover plate connects gas outlet, described catalyst self-unloading mouth, air inlet and go outGas port is arranged at respectively in lower outside head, and described catalyst self-unloading pipe one end is connected on lower interior end socket, and the other end is connected in catalysisOn agent self-unloading mouth.
As one of optimal way of the present invention, between described upper outside head and upper flange, short circuit extend neck is set, described outlet pipe is establishedBe placed on short circuit extend neck, one end of short circuit extend neck connects upper outside head, and the other end is fixed on upper flange, and dividing plate is positioned at short circuit and connectsBetween cylinder and upper outside head.
As one of optimal way of the present invention, described heat exchanger tube is the structure that an end opening is sealed in one end, the body of heat exchanger tube andBlind end is positioned at gas distributing cylinder, and the openend of heat exchanger tube is arranged between dividing plate and upper interior end socket, and described aqueduct is set inIn heat exchanger tube.
As one of optimal way of the present invention, described interior end socket is flexible tubesheet or standard sealing head, and described standard sealing head is selected fromOne in dome head, ellipse head, conical head, butterfly end socket, ball crown type end socket. As optimal way of the present inventionOne of, described interior end socket and short circuit extend neck are welded on respectively on upper flange.
As one of optimal way of the present invention, described upper flange is special-shaped flange, and described special-shaped flange is standard flange or nonstandardAccurate flange.
As one of optimal way of the present invention, described upper flange is connected by securing member with lower flange, upper flange and lower flange itBetween be provided with gasket seal.
As one of optimal way of the present invention, described gasket seal is Ω gasket seal.
As one of optimal way of the present invention, described gas distributing cylinder is provided with multiple air admission holes.
As one of optimal way of the present invention, the cylindrical shell of described gas collecting jar with ground-on cover plate is provided with multiple gas collection holes.
The present invention is directed to CO transformationreation reactor existing problems and not enough, and present high water/gas, high CO Water gas shift/WGSDemand, develops the controlled water shifting heat shift-converter of double-seal head, and employing heat exchanger tube is embedded in transformation catalyst bed, and utilization is changedIn heat pipe, water is converted into steam generation decalescence principle by CO+H2O→H2+CO2+QPutHeat is emitted in transformationreation, and shifts out in timeBeds, guarantees reaction bed temperature≤380 DEG C, and the saturated vapor of by-product 0.8～9.0MPa, is beneficial to catalyst certainlyUnload and be convenient to the maintenance of heat exchanger tube part. Efficiently solve existing shift-converter reclaim heat energy grade low, reclaim heat energy efficiency low,The easy overtemperature of catalyst, methanation side reaction, the difficult self-unloading of catalyst and the large defect of construction investment.
The present invention is directed to filling Pd/AI2O3The carbonylation shell and tube synthesis reactor existing problems of series catalysts, ethylene glycol and not enough,Develop the controlled water shifting heat carbonyl compound of double-seal head reactor, employing is embedded in employing heat exchanger tube in transformation catalyst bed to profitBe converted into steam generation decalescence principle by CO+CH with water in heat exchanger tube3ONO→(COOCH3)2+NO+QPutReaction emit heat andTime shift out beds, guarantee reaction bed temperature≤140 DEG C, and the saturated vapor of by-product 0.2～0.3MPa, catalystBed adopts full radial structure. Efficiently solve that the synthetic easy overtemperature of reactor catalyst of existing carbonylation, side reaction are large, bed resistancePower is large, be difficult to maximize, the difficult self-unloading of catalyst and the large defect of construction investment.
The present invention is directed to esterification hydrogenation shell and tube synthesis reactor existing problems and the deficiency of filling Cu series catalysts, ethylene glycol, openSend the controlled water shifting heat hydrogenation reactor of double-seal head, employing is embedded in employing heat exchanger tube in transformation catalyst bed, utilize heat exchangeIn pipe, water is converted into steam generation decalescence principle by CH3ONO adds H2Reaction (4H2+(COOCH3)2→(OHCH2CH2OH)2+2CH3OH+QPut) emit heat and shift out in time beds, guarantee reaction bed temperature≤250 DEG C, and by-product 1.8～3.2MPaSaturated vapor, beds adopts full radial structure. Efficiently solve the easy overtemperature of existing esterification hydrogenation reactor catalyst,Side reaction is large, bed resistance is large, be difficult to maximize, the difficult self-unloading of catalyst and the large defect of construction investment.
The present invention is directed to inner catalyst unit of state and developed the series catalysts at the Ni of 320～420 DEG C of serviceability temperatures, develop twoThe controlled water shifting heat methane synthesis reactor of end socket, is embedded in employing in transformation catalyst bed by employing heat exchanger tube, utilizes heat exchanger tubeInterior water is converted into steam generation decalescence principle by CO and H2Methanation reaction (CO+H2→CH4+H2O+QPut) emit heat andTime shift out beds, guarantee reaction bed temperature≤420 DEG C, and the saturated vapor of by-product 3.8～12.0MPa, catalysisAgent bed adopts full radial structure. Efficiently solve that the easy overtemperature of existing methane synthesis reactor catalyst, bed resistance are large, operationThe defects such as energy consumption is high, plant investment is large, SR is large.
The present invention is directed to Fischer-Tropsch shell and tube synthesis reactor existing problems and the deficiency of filling Fe (or Co) series catalysts, exploitationGo out the controlled water shifting heat Fischer-Tropsch synthesis of double-seal head device, employing is embedded in employing heat exchanger tube in transformation catalyst bed, utilization is changedIn heat pipe, water is converted into steam generation decalescence principle by CO and H2Fischer-Tropsch synthesis (nCO+ (2n+1) H2→CnH2n+2+nH2O+QPut) emit heat and shift out in time beds, guarantee Co reaction bed temperature≤240 DEG C, and by-product 1.8～The saturated vapor of 2.8MPa; Fe reaction bed temperature≤260 DEG C, and the saturated vapor of by-product 1.6～3.8MPa, catalystBed adopts full radial structure. Efficiently solve the defect that existing Fischer-Tropsch synthesis device exists.
The present invention has the following advantages compared to existing technology: inlet distribution of the present invention, catchment, the catalytic reaction Trinity can be singleSolely the assembly of lifting separates with outer cylinder body, easy access, catalyst self-unloading, Catalyst packing;
Heat exchanger tube is embedded in to beds inside can be removed beds internal-response heat in time, avoid original conversion,Synthetic and hydrogenation catalyst is sintered phenomenon and occurs, efficiently solve the catalyst such as existing conversion, synthetic and hydrogenation service life short,Easily overtemperature, side reaction thing is many, bed temperature is wayward, the driving time long, be difficult to maximization, operation energy consumption is high, construction investmentThe defect such as large;
The temperature of beds regulates by byproduct steam pressure, guarantees that adjusting aspect is flexible, easy to control; Also guarantee simultaneouslyWhen driving, take to add steam to water circulation system, rapidly the temperature rise of controlled a kind of double-seal head water shifting heat reactor is got up, to contractThe short driving time;
Natural Circulation is taked in water route, and while parking suddenly, the reactant of inside reactor nubbin of the present invention continues reaction, waterRoad also still keeps circulation, and beds internal heat is shifted out, and guarantees at the controlled water of a kind of double-seal head of unexpected dead ship conditionThe bed temperature that moves thermal reactor also can not surpass, effectively guard catalyst service life;
Gas distributing cylinder of the present invention and gas collecting jar with ground-on cover plate adopt bidirectional compensating between reactor inside and outside, make the radial gas mistake that distributesDifference≤5.0%, guarantees that distribution of gas is even; Reactor bed overall resistance≤0.01MPa;
Adopt overall diameter to beds, be easy to device and maximize, not only solve a transport difficult problem, reduce construction investment simultaneously.
Brief description of the drawings
Fig. 1 is structural representation of the present invention.
Detailed description of the invention
Below embodiments of the invention are elaborated, the present embodiment is implemented under taking technical solution of the present invention as prerequisite,Provided detailed embodiment and concrete operating process, but protection scope of the present invention is not limited to following embodiment.
As shown in Figure 1, the present embodiment comprise the Catalyst packing pipe 2 that is connected as a single entity, water inlet pipe 3, upper outside head 4, dividing plate 6,Outlet pipe 7, multiple aqueduct 18, multiple heat exchanger tube 19, upper interior end socket 10, upper flange 11, gas distributing cylinder 16, gas collectionCylinder 20, lower interior end socket 23 and catalyst self-unloading pipe 27, the lower flange 13 being connected as a single entity, main cylinder 15, lower outside head 24,Catalyst self-unloading mouth 29, air inlet 25 and gas outlet 28;
Water inlet pipe 3 is opened in the top of outside head 4, and dividing plate 6 is arranged between outside head 4 and upper interior end socket 10, water outletPipe 7 is arranged between dividing plate 6 and upper interior end socket 10, between upper outside head 4 and upper flange 11, short circuit extend neck 9 is set, water outletPipe 7 is arranged on short circuit extend neck 9, and one end of short circuit extend neck 9 connects upper outside head 4, and the other end is fixed on upper flange 11,Dividing plate 6 is between short circuit extend neck 9 and upper outside head 4, and short circuit extend neck 9 is convenient to device and is distributed; In upper, end socket 10 and short circuit connectCylinder 9 is welded on respectively on upper flange 11, and the top of gas distributing cylinder 16 is connected on upper flange 11, gas distributing cylinder 16Bottom is connected on lower interior end socket 23, and gas distributing cylinder 16 is set in main cylinder 15, and the top of main cylinder 15 connects laxative remedyOrchid 13, the bottom of main cylinder 15 connects lower outside head 24, and upper flange 11 is connected with lower flange 13; Catalyst packing pipe 2One end is connected between interior end socket 10 and gas distributing cylinder 16, and the other end passes dividing plate 6 and upper outside head 4, catalysis successivelyAgent filling pipe 2 tops that are positioned at outside outside head 4 are provided with Catalyst packing mouth 1, and aqueduct 18 one end are communicated in dividing plate 6 HesBetween upper outside head 4, the other end is set in heat exchanger tube 19, and the body of heat exchanger tube 19 is positioned at gas distributing cylinder 16, heat exchangePipe 19 outlet dividing plate 6 and between end socket 10, the cylindrical shell of gas collecting jar with ground-on cover plate 20 is positioned at gas distributing cylinder 16, gas collectionThe outlet of cylinder 20 connects gas outlet 28 by escape pipe 26, and establish respectively catalyst self-unloading mouth 29, air inlet 25 and gas outlet 28Be placed in lower outside head 24, catalyst self-unloading pipe 27 one end are connected on lower interior end socket 23, and the other end is connected in catalyst self-unloadingOn mouth 29.
In the present embodiment, Catalyst packing pipe 2, upper outside head 4, dividing plate 6 and aqueduct 18 have formed inlet distribution chamber 5,Dividing plate 6, upper interior end socket 10, upper flange 11, outlet pipe 7 and heat exchanger tube 19 have formed collecting chamber 8, upper interior end socket 10, onFlange 11, gas distributing cylinder 16, heat exchanger, lower interior end socket 23 have formed catalyst frame 22, upper flange 11, lower flange 13,Outer cylinder body, lower outside head 24, lower interior end socket 23, air inlet 25 and gas outlet 28 have formed distribution of gas chamber 17, gas collecting jar with ground-on cover plateSpace in 20 forms collection chamber 21.
The structure that heat exchanger tube 19 seals an end opening for one end, the body of heat exchanger tube 19 and blind end are positioned at gas distributing cylinder 16,The openend of heat exchanger tube 19 is arranged between dividing plate 6 and upper interior end socket 10, and aqueduct 18 is set in heat exchanger tube 19.
Upper flange 11 is connected by securing member 14 with lower flange 13, between upper flange 11 and lower flange 13, is provided with Ω gasket seal12. Gas distributing cylinder 16 is provided with multiple air admission holes. The cylindrical shell of gas collecting jar with ground-on cover plate 20 is provided with multiple gas collection holes.
The upper interior end socket 10 of the present embodiment is made for flexible tubesheet, and the upper interior end socket 10 in other embodiment can be also standard envelopeHead, standard sealing head is selected from the one in dome head, ellipse head, conical head, butterfly end socket, ball crown type end socket.
The special-shaped flange that the upper flange 11 of the present embodiment is nonstandard of flanges.
Gas enters distribution of gas chamber 17 by air inlet 25, in distribution of gas chamber 17, enters catalysis by gas distributing cylinder 16Agent frame 22 reacts, and reaction is emitted water in the hollow cylinder that heat forms by aqueduct 18 and heat exchanger tube 19 and absorbed. Go out catalystAfter frame 22 reactions, gas enters collection chamber 21, escape pipe 26 by gas collecting jar with ground-on cover plate 20, then by escape pipe 26 outflow reactors; NoSaturation water enters inlet distribution chamber 5 by water inlet pipe 3, is then evenly distributed to aqueduct 18, in aqueduct 18 inside from top to bottomFlow, flow out in aqueduct 18 bottoms in 180 ° of hollow cylinders that form at aqueduct 18 and heat exchanger tube 19 of upset from lower andUpper flowing, and absorption heat-exchange pipe 19 external catalyst bed heats, form supersaturation water and enter collecting chamber 8, then by outlet pipe7 outflow reactors enter extraneous drum, and in drum, flash off saturated vapor. Fig. 1 hollow core arrow is water (flow) direction, realHeart arrow is airflow direction.
The foregoing is only preferred embodiment of the present invention, not in order to limit the present invention, all in spirit of the present invention and formerAny amendment of doing, be equal to and replace and improvement etc., within all should being included in protection scope of the present invention.
Claims (10)
1. the controlled water shifting heat reactor of double-seal head, is characterized in that, comprises the Catalyst packing pipe (2) that is connected as a single entity, entersWater pipe (3), upper outside head (4), dividing plate (6), outlet pipe (7), at least one aqueduct (18), at least one heat exchanger tube(19), upper interior end socket (10), upper flange, gas distributing cylinder (16), gas collecting jar with ground-on cover plate (20), lower interior end socket (23) and catalysisAgent self-unloading pipe (27), the lower flange being connected as a single entity (13), main cylinder (15), lower outside head (24), catalyst self-unloading mouth (29),Air inlet (25) and gas outlet (28); Described water inlet pipe (3) is opened in the top of outside head (4), and dividing plate (6) is establishedBe placed between outside head (4) and upper interior end socket (10), described outlet pipe (7) is arranged at dividing plate (6) and upper interior end socket (10)Between, the top of the bottom of described upper outside head (4), the bottom of upper interior end socket (10) and gas distributing cylinder (16) connects respectivelyBe connected on upper flange (11) upper, it is upper that the bottom of described gas distributing cylinder (16) is connected to lower interior end socket (23), and described gas dividesCloth cylinder (16) is set in main cylinder (15), and the top of described main cylinder (15) connects lower flange (13), main cylinder (15)Bottom connect lower outside head (24), upper flange (11) is connected with lower flange (13); Described Catalyst packing pipe (2)One end is connected between interior end socket (10) and gas distributing cylinder (16), and the other end is successively through dividing plate (6) and upper outside head(4), described aqueduct (18) one end is communicated between dividing plate (6) and upper outside head (4), and the other end is set in heat exchanger tube(19), in, the body of described heat exchanger tube (19) is positioned at gas distributing cylinder (16), the outlet of heat exchanger tube (19) be positioned at everyBetween plate (6) and upper interior end socket (10), the cylindrical shell of described gas collecting jar with ground-on cover plate (20) is positioned at gas distributing cylinder (16), gas collecting jar with ground-on cover plate(20) outlet connects gas outlet (28), and described catalyst self-unloading mouth (29), air inlet (25) and gas outlet (28) are dividedBe not arranged at lower outside head (24) upper, it is upper that described catalyst self-unloading pipe (27) one end is connected in lower interior end socket (23), anotherEnd is connected on catalyst self-unloading mouth (29).
2. the controlled water shifting heat reactor of a kind of double-seal head according to claim 1, is characterized in that, described upper outside head (4)And short circuit extend neck (9) is set between upper flange (11), and it is upper that described outlet pipe (7) is arranged at short circuit extend neck (9), and short circuit connectsOne end of cylinder (9) connects upper outside head (4), and it is upper that the other end is fixed on upper flange (11), and dividing plate (6) is positioned at short circuit extend neck(9) and between upper outside head (4).
3. the controlled water shifting heat reactor of a kind of double-seal head according to claim 1, is characterized in that, described heat exchanger tube (19)For the structure that an end opening is sealed in one end, the body of heat exchanger tube (19) and blind end are positioned at gas distributing cylinder (16), heat exchangeThe openend of pipe (19) is arranged between dividing plate (6) and upper interior end socket (10), and described aqueduct (18) is set in heat exchanger tube(19) in.
4. the controlled water shifting heat reactor of a kind of double-seal head according to claim 1, is characterized in that, described interior end socket (10)For flexible tubesheet or standard sealing head, described standard sealing head is selected from dome head, ellipse head, conical head, butterfly end socket, ballOne in crown type end socket.
5. the controlled water shifting heat reactor of a kind of double-seal head according to claim 1, is characterized in that, described interior end socket (10)Be welded on respectively on upper flange (11) with short circuit extend neck (9).
6. the controlled water shifting heat reactor of a kind of double-seal head according to claim 1, is characterized in that, described upper flange (11)For special-shaped flange, described special-shaped flange is standard flange or nonstandard of flanges.
7. the controlled water shifting heat reactor of a kind of double-seal head according to claim 1, is characterized in that, described upper flange (11)Be connected by securing member (14) with lower flange (13), between upper flange (11) and lower flange (13), be provided with gasket seal.
8. the controlled water shifting heat reactor of a kind of double-seal head according to claim 7, is characterized in that, described gasket seal isΩ gasket seal (12).
9. the controlled water shifting heat reactor of a kind of double-seal head according to claim 1, is characterized in that described gas distributing cylinder(16) be provided with multiple air admission holes.
10. the controlled water shifting heat reactor of a kind of double-seal head according to claim 1, is characterized in that, described gas collecting jar with ground-on cover plate (20)Cylindrical shell be provided with multiple gas collection holes.
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| CN201510072235.6A CN104645897B (en) | 2015-02-11 | 2015-02-11 | The controlled water shifting heat reactor of a kind of double-seal head |
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| CN201510072235.6A CN104645897B (en) | 2015-02-11 | 2015-02-11 | The controlled water shifting heat reactor of a kind of double-seal head |
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| CN104645897A CN104645897A (en) | 2015-05-27 |
| CN104645897B true CN104645897B (en) | 2016-05-04 |
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| CN106040153B (en) * | 2016-06-30 | 2019-02-26 | 广州森弘电气机械有限公司 | Automatic mixing apparatus |
| CN107570088B (en) * | 2017-10-10 | 2023-11-17 | 湖南安淳高新技术有限公司 | Catalyst unloading system and method for shell-and-tube reactor |
| CN109052318B (en) * | 2018-09-30 | 2022-04-08 | 中石化宁波工程有限公司 | Isothermal shift reactor |
| CN109173936B (en) * | 2018-09-30 | 2021-10-08 | 中石化宁波工程有限公司 | Methanol synthesis water-cooling reactor |
| CN109821355B (en) * | 2019-03-15 | 2021-11-05 | 东北大学 | Radial flow pressure swing adsorption bed and use method thereof |
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| CN102886229B (en) * | 2012-10-08 | 2014-10-08 | 中国石油化工集团公司 | CO (carbon monoxide) full-radial isothermal converting furnace |
| CN204583141U (en) * | 2015-02-11 | 2015-08-26 | 南京敦先化工科技有限公司 | The controlled water shifting heat reactor of a kind of double-seal head |
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