CN106943958A - Low-pressure medium circulation moves the reactor assembly of thermal control temperature - Google Patents
Low-pressure medium circulation moves the reactor assembly of thermal control temperature Download PDFInfo
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- CN106943958A CN106943958A CN201710185384.2A CN201710185384A CN106943958A CN 106943958 A CN106943958 A CN 106943958A CN 201710185384 A CN201710185384 A CN 201710185384A CN 106943958 A CN106943958 A CN 106943958A
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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
- B01J8/0242—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
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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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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
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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
Abstract
The present invention provides a kind of low-pressure medium and circulates the reactor assembly for moving thermal control temperature, main to include vertical shifting hot jacket pipe reactor, move hot temperature-controlling system；Reactor head, which is set, moves thermal medium distributing chamber and return passage, vertical pipes are formed by inner and outer tubes nesting, sleeve pipe extends down into beds to bottom, distributing chamber moves thermal medium and flows downwardly into inner tube, again return passage, the also circulation of shifting thermal medium, control assembly and heat exchanger including being arranged in return passage and/or outside reactor are flowed upwardly into from outer tube.It is circulated as heat transferring medium by using the vertical shifting hot jacket pipe reactor and normal pressure or low-voltage heat conducting oil, fused salt, nitrogen, carbon dioxide or superheated vapour close to reaction bed temperature and moves thermal control temperature, can elimination reaction focus, reacting balance is easily-controllable, operational security, reaction effect is good, catalyst life is long, is easier to draw off from reactor bottom during catalyst change, and influence of a small number of leakage sleeve pipes of closure to bed temperature and reaction effect is smaller.
Description
Technical field
The invention belongs to chemical reactor field, and in particular to a kind of low-pressure medium circulation moves the reactor assembly of thermal control temperature.
Background technology
Water-cooled, the reactor of air cooling is industrially commonly used, for some exothermic reactions, to control beds temperature
Degree.
The main purpose of reactor not overtemperature is controlled, one is that some reactions are reversible reactions, and temperature is too high to reduce reaction
The conversion ratio of thing and the yield of target product, two be side reaction when reducing high temperature, improves the selectivity of target product, three be to prolong
The service life of long catalyst or regeneration period.
Some methods set the fixed bed reactors of coil pipe or tubulation in, and catalyst is controlled by cooling or heat transferring medium
Bed temperature is distributed and reaction condition, and heat transferring medium can use catalyst in reaction raw materials, water under high pressure or fused salt, shell and tube reactor
Can be in tubulation or between tubulation.The subject matter of existing this kind of reactor includes beds temperature rise, the temperature difference and part
The control of focus is still difficult and the problem of influence catalytic reaction effect, catalyst service life, and catalyst passes through one section
When the operating of time is using needing to change, limited by heat exchange temperature control Components Shape, position or the problem of obstruction is difficult to draw off.
CN201510698217.9 discloses a kind of water-cooled radial reactor, including the radial direction of outer barrel, loading catalyst is anti-
Basket, water-cooling system, central tube, hydroecium, steam chest and loading and unloading structure are answered, the radial direction reaction basket is located in the outer barrel, and institute
State and gap is radially formed between reaction basket and the outer barrel, the water-cooling system includes stretching into the water-cooled that the radial direction reacts basket
Pipe, the water cooling tube is connected with the hydroecium and the steam chest respectively, and the central tube is stretched into the radial direction reaction basket, and portion
Divide and react basket through the radial direction and stretch out outside the outer barrel；The water-cooled reactor also includes being arranged at intervals in the outer barrel
Lower perforated plate and upper perforated plate, one end of the upper perforated plate and the outer barrel is spaced apart, and in described outer barrel one end and institute
State and form one of the hydroecium and the steam chest between upper perforated plate, the hydroecium is formed between the lower perforated plate and the upper perforated plate
Another with the steam chest, the lower perforated plate is arc tube sheet.The water-cooled radial reactor is less high such as reaction temperature
At 250 DEG C or so or less, the temperature conditionss of beds can be preferably controlled, the temperature difference of equal temperature section bed is smaller, when urging
When loading porcelain ball under agent bed, it is easier to draw off during catalyst change；But limited by water vapor pressure, for reaction temperature
At more than 250 DEG C, water-cooling system and hydroecium, the steam pressure of steam chest are just too high, cause pressure rating, the manufacturing cost of reactor
Too high, security during some purposes limits its application there is also greater risk.
The saturated vapor pressure situation of water when table 1 below is 200-330 DEG C.
Table 1
。
The content of the invention
In order to solve the above technical problems, the present invention provides the reactor assembly that a kind of low-pressure medium circulation moves thermal control temperature, it is main
To include catalytic reactor main body and move hot temperature-controlling system；
The catalytic reactor main body moves hot jacket pipe reactor using vertical, wherein, the top of reactor, which is set, moves thermal medium point
Cloth room and return passage, the low temperature before heat absorption move thermal medium and enter shifting thermal medium distributing chamber through moving thermal medium inlet, and are distributed downward
Flow into move thermal medium return passage under the inner tube of sleeve pipe, distributing chamber, the shifting thermal medium after heat absorption is between the inner and outer pipes of sleeve pipe
Space flows upwardly into return passage；The vertical pipes are formed by inner and outer tubes nesting, and inner tube upper end open is in shifting thermal medium point
Cloth room base plate, outer tube upper end open extends down into beds in shifting thermal medium return passage base plate, sleeve pipe, until catalysis
End closure under the bottom of agent bed, outer tube, inner tube lower end extends under outer tube on end closure and is open, and moves the chi of thermal sleeve
Very little, quantity and heat exchange area are appropriately arranged with ensureing to move thermal control temperature ability；The flow direction of reaction material is along vertical in beds
The upper entering and lower leaving or bottom in and top out in casing axis direction, or footpath perpendicular to casing axis direction ecto-entad or from inside to outside
To reactor is set enters outlet interface accordingly；Reactor head or upper lateral part set one or more Catalyst packings mouthful, from
Reactor bottom sets one or more catalyst unloadings mouthful；
It is described to move hot temperature-controlling system, except the shifting thermal medium distributing chamber of catalytic reactor body top and return passage and extend downwardly
Into the sleeve pipe of beds, also moved including being arranged in thermal medium distributing chamber and/or return passage, and/or outside reactor
Thermal medium circulation, control assembly and heat exchanger are moved, and thermal medium is moved by normal pressure or low pressure and is circulated shifting thermal control temperature.
In the present invention, moving heat transferring medium used by hot temperature-controlling system includes conduction oil, fused salt, plays circulation with pump, pressure is normal
Pressure or low pressure, can preferably control the temperature strip of reactor catalyst bed as needed in 150-600 DEG C of temperature range
Part；Conduction oil is generally used for the temperature control of 150-400 DEG C of scope, the different cultivars of 250-350 DEG C of available work temperature；Fused salt
For the temperature control of 350-600 DEG C of scope, wherein 400-600 DEG C scope can use such as 53% potassium nitrate, 40% natrium nitrosum, 7%
The ternary eutectic fused salt mixt of sodium nitrate, 350-500 DEG C of scope can use such as lithium nitrate or the fused salt mixt containing lithium nitrate.Lead
In deep fat, fused salt cyclic process, it can slightly cool through high-temperature heat-exchanging and remove heat, for preheating reaction raw materials or by-product high pressure
Steam utilization.Conduction oil, fused salt can largely be circulated by high temperature circulation pump, can also pass through such as venturi type suction mixer etc
Component, do not cooled using low discharge conduction oil, fused salt or suppressed through pump after suitably cooling and be used as venturi type suction mixer
Power and by most of conduction oil, fused salt direct circulation, the advantage of rear method is to reach identical temperature control effect, it is only necessary to low discharge
Heat-transfer Oil Pump, pump for liquid salts, or can use the Heat-transfer Oil Pump of a low discharge, pump for liquid salts to realize conduction oil, fused salt distributing chamber, return
Larger conduction oil, fused salt internal circulating load needed for flow chamber, because Heat-transfer Oil Pump, pump for liquid salts are easily suppressed.
In the present invention, move hot temperature-controlling system and also can use normal pressure or low pressure and the relatively low indifferent gas of degree of danger such as nitrogen, two
Carbonoxide, superheated vapour or its gaseous mixture move thermal control temperature as heat transferring medium circulation, and now catalytic reactor main body is only needed to
Possesses relatively low pressure rating, cost and security risk are all relatively low.Wherein nitrogen, carbon dioxide, superheated vapour or its mixing
Gas can largely be circulated by high temperature circulation machine, and the component of blender etc can be also evacuated by such as venturi type, is followed with low discharge
Ring gas do not cool or be pressurized after suitably cooling as venturi type be evacuated blender power and most of High Temperature Gas direct circulation,
The advantage of method is to reach identical temperature control effect afterwards, it is only necessary to low discharge, the circulator of big pressure head, or can use a rill
Amount, the circulator of big pressure head gas circulation amount larger needed for realizing between gas distributing chamber, return passage；Circulating air can be changed through high temperature
Hot device, which slightly cools, removes heat, is utilized for preheating reaction raw materials or by-product high-pressure steam.
When the hot temperature-controlling system of shifting uses normal pressure or the superheated vapour of low pressure as heat transferring medium, in reactor head
Move and water pump, water-carrying capacity control can be set in thermal medium distributing chamber and return passage and sleeve pipe outside the superheated vapour for circulation, reactor
Regulating valve processed, return passage is exported high-temperature steam and realized simultaneously cool and/or condensation and the vaporization and heating that pump out saliva
The low temperature that contra-flow heat exchanger, the condensed water that contra-flow heat exchanger is exported and a small amount of steam that may be present further condense cooling is changed
Hot device, and/or high-temperature heat-exchanging, cryogenic heat exchanger outlet low pressure or without pressure pure water through pump beat pressurize after by governor valve control
The flow of water, enters after contra-flow heat exchanger heat exchange is vaporizated into steam and further heat exchange heating and moves thermal medium as superheated steam, should
Method is easy to implement, and operating is reliable steady.
When the hot temperature-controlling system of shifting uses normal pressure or the superheated vapour of low pressure as heat transferring medium, if it is considered to overheat is steamed
Vapour is all beaten by condensation, pump and vaporization needs higher heat exchange area and the contra-flow heat exchanger of manufacturing cost again, can also adopt
Blender is evacuated with venturi type and realizes that a large amount of superheated steams move the circulation of thermal medium, small part superheated steam need to only be cooled cold
It is solidifying, beaten through pump and exchange heat again vaporization and form appropriate pressure head, be used as venturi type pumping blender to promote most of superheated steam circulation
Power, only with the superheated steam of low discharge through high-temperature reflux heat exchanger cooling condensation, drop again through cryogenic heat exchanger during this
Low beaten to appropriate stability, pump is pressurizeed and controls water-carrying capacity, is evacuated after returning the vaporization of high-temperature reflux heat exchanger, heating as venturi type
The power of blender, realizes that remaining superheated steam moves a large amount of circulations of thermal medium.Condensed water can not also be beaten and direct by pump
Using the pure water or deionized water of the pressurization of pipe network, using the heat of small part superheated steam by appropriate flow in heat exchanger
Pressure (hydraulic) water heat exchange vaporization forms the pressurized vapor of appropriate pressure head, is pushed away with a part of pressurized vapor as the venturi type blender that draws gas
Supplied outside the power of dynamic major part superheated steam circulation, unnecessary pressurized vapor or enter steam pipe system, outer confession or enter steam pipe
The unnecessary pressurized vapor institute heat content of net is a part for exothermic heat of reaction；Condensation formed without pressure water enter condensation water storage tank or
Pipe network.
When the hot temperature-controlling system of shifting uses normal pressure or the superheated vapour of low pressure as heat transferring medium, the high temperature largely circulated
Superheated steam shifting thermal medium also first can remove partial heat through cooling heat exchanger and slightly cool, while steaming of the by-product low pressure to high pressure
Vapour, enters contra-flow heat exchanger and/or cryogenic heat exchanger again afterwards.Contra-flow heat exchanger steam condensate (SC) further drops through cryogenic heat exchanger
The purpose of temperature is easy for pump and beats to form appropriate pressure head.
In the present invention, the vertical catalyst bed Rotating fields for moving thermal sleeve catalytic reactor main body are flowed to according to Process Gas
Can be axially or radially.When in the big course of reaction of, conversion zone concentration very fast for some reaction speeds, thermal discharge,
Preferably, now each sleeve pipe can play shifting heat simultaneously and limit warm make the axial arrangement of reacting material flow upper entering and lower leaving in bed
With；The advantage of radial structure is that bed resistance is smaller, but only some vertical pipes has played shifting heat effect, can will be mainly anti-
The sleeve pipe distribution density of section is answered to increase.When the axial arrangement using reaction material upper entering and lower leaving, upper shifting heat in sleeve pipe outer tube
Medium can move up the heat in the high temperature bed of middle and lower part, and energy heating response material is improved in its temperature, thus normal operation
Allow to use relatively low reaction material inlet temperature, the risk of the outer vigorous reaction of device, improves work when can avoid that high-temperature feeding can be used
The security of skill process.
In the present invention, the vertical shifting thermal sleeve gos deep into the height 0.5-20m, tube pitch 0.02- of beds
0.10m, heat exchange area 5-100m2/m3Catalyst.The bottom of beds, can be laminated support with orifice plate screen cloth, can also be from
Reactor bottom, which starts to load inert ceramic balls from large to small, to be supported, and wherein latter arrangement is easy to unloading during catalyst change
Go out.It is preferred that the upper plane of inert ceramic balls filling is higher than the lower end plane of sleeve pipe, to prevent beds bottom from occurring overtemperature, fly
Temperature, and avoided when being changed with temperature, the variation casing length of pressure its lower end crush catalyst or cause sleeve pipe by
Damage, because porcelain ball surface is smooth, intensity is high, still has when tightly packed and be much better than spherical, bar shaped and the shifting of special-shaped catalyst
Kinetic force, can provide space for the downward elongation of sleeve pipe；The end socket of its lower end is that spherical, spheroid shape or taper are preferable.
It the position distribution of Catalyst packing pipe, diameter dimension and should be appropriately arranged with, keep away with the relative position of heat exchange sleeve
Exempt to influence the spacing for closing on heat exchange sleeve, it is ensured that the reaction bed temperature below Catalyst packing pipe meets the requirements.Catalyst
Filling pipe upper end may extend on the base plate for moving thermal medium distributing chamber or on roof, or beds upper lateral part reaction
Device outer wall.
In the present invention, the vertical shifting thermal sleeve catalytic reactor main body, can after long-term operating finds casing leak
The sleeve pipe leaked injection heatproof sealing agent is blocked during parking maintenance or the amount of will leak out drops to very low degree.Due to
Sleeve pipe quantity is a lot, usual more than hundreds of, and is independent of each other, and the several influences to temperature control effect of closure are little.
In the present invention, the vertical shifting thermal sleeve catalytic reactor, when entrance material reactant concentration is higher, will can be exported
Expect to return to the reactant concentration for diluting entrance material with appropriate recycle ratio, so as to the response situation and temperature point of beds
Cloth carries out suitable control, to realize the operating of safety and steady and reach more preferable reaction effect.But urged due to preferably controlling
Agent bed temperature, recycle ratio used does not need precise control, it is not required that very big.It is dilute that liquid material can return circulation by pump
Release, being recycled back into and mixing for gas material can be evacuated blender progress by venturi, be used as power using the pressure head of unstripped gas.Also
The preheating cooling heat exchanger of raw material is set, the reaction product of the reaction raw materials preheating of reactor inlet, outlet is cooled down.
The low-pressure medium circulation of the present invention moves the reactor assembly of thermal control temperature, by using the vertical shifting thermal sleeve catalysis
Reactor and normal pressure or the low-voltage heat conducting oil close to reaction bed temperature, fused salt, nitrogen, carbon dioxide, superheated vapour
Thermal control temperature is moved as heat transferring medium circulation, temperature conditions and the warm area distribution of beds can be preferably controlled, can eliminate
React focus, it is to avoid occur the abnormal conditions such as overtemperature, temperature runaway, reacting balance is easily-controllable, operational security, can reach higher reaction effect
Really, catalyst life is longer, is easier to draw off from reactor bottom during catalyst change, one or during the leakage of several heat exchanger tubes
Can be by injecting sealing agent closure and influenceing little to bed temperature control；The reaction out of control for some heat release temperature rise very great Yi, by
The larger reversible reaction of temperature influence and the more process of high temperature side reaction, the deoxygenation of such as coalbed methane containing oxygen, low concentration
H2During the direct oxidation reaction of S sour gas Recovered sulphur, the conversion ratio of reactant and the yield of target product are all higher, high temperature
Side reaction product is reduced, and the selectivity of target product is higher, and catalyst amount and reactor volume can be reduced very during same production capacity
Many, catalyst service life can be obviously prolonged.
Brief description of the drawings
Fig. 1, moves the whole pumps of thermal medium and plays the reactor assembly schematic diagram for realizing that the low-pressure medium circulation circulated moves thermal control temperature.
Fig. 2, moves thermal medium small part pump and packs the low-pressure medium circulation shifting that circulation is realized by venturi suction mixer
The reactor assembly schematic diagram of thermal control temperature.
Fig. 3, is condensed using superheated vapour as heat transferring medium and all, pump is beaten, vaporize the low-pressure medium circulation for realizing circulation
Move the reactor assembly schematic diagram of thermal control temperature.
Fig. 4-6, by heat transferring medium of superheated vapour, small part pump pack by venturi suction mixer realize circulate
Low-pressure medium circulation move thermal control temperature reactor assembly schematic diagram.
Fig. 7, reacts outlet material return dilution, simultaneously small part pump is packed by venturi by heat transferring medium of superheated vapour
Suction mixer realizes that the low-pressure medium circulation of circulation moves the reactor assembly schematic diagram of thermal control temperature.
Fig. 8, with axial catalyst bed and the catalytic reactor agent structure schematic diagram for entering outlet.
Fig. 9, with radial direction beds and the catalytic reactor agent structure schematic diagram for entering outlet.
Legend：1 reactor shell, 2 catalyst reaction beds, 3 Catalyst packing pipes, 4 move thermal medium distributing chamber, 5 heat exchange
Sleeve pipe inner tube, 6 heat exchange sleeve outer tubes, 7 base plates, the 8 radial direction reaction bed sidewall containers with passage, 9 vertical water-cooleds move hot jacket
Pipe, the 10 radial direction reaction bed inner tubes with passage, 11 support porcelain balls, 12 return passages move thermal medium outlet, and 13 distributing chamber move heat
Medium inlet, 14 catalyst unloadings mouthful, 15 reaction material gateways, 21 move thermal medium return passage.
Embodiment
Below by taking a kind of oxygen-containing coal bed gas deoxidation reaction test device as an example, thermal control temperature is moved to low-pressure medium of the present invention circulation
The application of reactor assembly and effect situation, are specifically described.
Embodiment 1
The deoxygenation experimental rig of a set of coalbed methane containing oxygen as shown in Figure 2, mainly includes catalytic reactor main body and shifting
Hot temperature-controlling system；
Catalytic reactor main body as shown in Figure 6 include housing 1, the catalyst reaction bed 2 of axial arrangement and feed inlet and outlet 15,
Catalyst packing pipe 3, catalyst unloading mouth 14, beds bottom filling porcelain ball 11 are supported, reaction material in beds
Flow direction be upper entering and lower leaving；Top, which is set, moves thermal medium distributing chamber 4 and return passage 21, and the low temperature before heat absorption moves thermal medium through moving heat
Medium entrance, which enters, moves thermal medium distributing chamber 4, and is distributed under the inner tube 5 for flowing downwardly into sleeve pipe 10, distributing chamber to move thermal medium
Return passage 21, the shifting thermal medium after heat absorption flows upwardly into return passage 21 from the space between the inner and outer pipes of sleeve pipe；The vertical pipes
10 are formed by inner tube 5 is nested with outer tube 6, and the upper end open of inner tube 5 is in moving thermal medium distributing chamber base plate 7, and the upper end open of outer tube 6 is in shifting
Thermal medium return passage base plate 7, sleeve pipe extends down into beds, until end seal under the bottom of beds, outer tube
Mouthful, inner tube lower end extends under outer tube on end closure and is open；
The height 2.25m of catalyst reactor bed；Move the spacing 28.5mm, sleeve pipe inner tube Φ 22x1mm, outer tube of thermal sleeve
Φ 38x3mm, sleeve pipe radical 360, the m of heat exchange area 983, move thermal medium distributing chamber and return passage difference in height 350mm；Reactor is straight
Footpath Φ 1500mm, total high 4500mm；Adverse current heating coalbed methane containing oxygen raw material is set before and after coal bed gas turnover deoxidation reactor and cold
But the preheating cooling heat exchanger of deoxidation coal bed gas（Heat exchange area 100m2）；The catalysis of Φ 3mm sulfur-tolerant types combustion deoxidizing is loaded between sleeve pipe
Agent 2.7m3, main active component is copper-manganese oxide, bottom filling Φ 6mm inert ceramic balls 0.15m3Support；Reactor feed gas,
The O worked off one's feeling vent one's spleen2The H of coal bed gas before concentration and other compositions, timing sampling analysis, detection preheating cooling heat exchanger2S≤20ppm；
It is described to move hot temperature-controlling system, except the shifting thermal medium distributing chamber of catalytic reactor body top and return passage and extend downwardly
Into the sleeve pipe of beds, also shifting thermal medium circulator or pump, observing and controlling component and heat exchange including being arranged on outside reactor
Device and the venturi suction mixer that thermal medium carries out a large amount of, high temperature circulation will be moved；Thermal medium is moved to be flowed by return passage outlet 12
Go out, sub-fraction is promoted through the laggard circulator of heat exchanger cooling or pump, entering venturi suction mixer will be most of as power
End cooling shifting thermal medium largely aspirate, mix, then through 13 times distributing chamber of entrance and be distributed flow into sleeve pipe inner tube to flow down, to
Baffling imports return passage upwards on end closure under downstream to outer tube, realizes the circulation and cooling for moving thermal medium；Thermal medium is moved to follow
35m is set before ring machine or pump2Heat exchanger, by-product 1.0MPa steam.
Using the experimental rig, thermal medium is moved by circulation of nitrogen, is beaten with centrifugal high pressure fan and is circulated and taken out for venturi
Persorption clutch provides power, has carried out the field investigation of kinds of processes condition, every kind of process conditions respectively operate 48h.Each position allusion quotation
Main composition situation before and after the circulating nitrogen gas of type, coal bed gas temperature, pressure, flow condition, and coal bed gas deoxidation, such as following table
Listed by 2-4.In process of the test, nitrogen cylinder is connected by pressure maintaining valve and supplied, is suitably vented when pressure exceeds, by the nitrogen of distributing chamber
Atmospheric pressure control nitrogen flow after 22kPa or so, blower fan is adjusted by frequency converter, and pressure head is automatically formed.
Table 2
Table 3
Table 4
Successively continuously run 10 days afterwards according to the condition of table 3, continuously run according to the condition of table 4 10 days, control condition and anti-
Answer effect without significant change, smooth running controls to adjust conveniently, do not find overtemperature focus, safer reliability.
Comparative example
Nitrogen flow after the circulator gradually reduced in the process of the test of the process conditions of table 4, then distributing chamber, return passage and urge
Agent bed temperature is gradually increasing, and CO contents of working off one's feeling vent one's spleen are gradually increasing, and when bed maximum temperature rises to 550 DEG C, work off one's feeling vent one's spleen CO
Content reaches 0.35%, and reaction effect is deteriorated, and technological condition and reaction effect now are as listed in table 5.
Table 5
Stop afterwards into coal bed gas, nitrogen continues to beat cycle down low catalyst bed temperature, treats that beds maximum temperature is down to
Stop nitrogen circulation cooling at 460 DEG C, switch to coal bed gas and relatively low flow that table 2 is constituted, carry out adiabatic reaction experiment, knot
Fruit reaction bed temperature rises rapidly, and CO contents of working off one's feeling vent one's spleen are gradually increasing, when bed maximum temperature rises to 580 DEG C, outlet
Gas CO contents reach 0.30%, and reaction effect is deteriorated, and technological condition and reaction effect now is as listed by table 6.
Table 6
Embodiment 2
Complete after above-mentioned experiment, remove the venturi suction mixer moved in thermal medium circulation line and centrifugal high pressure fan, if
Molten salt circulating pump, is changed to the flow of accompanying drawing 1, uses 53% potassium nitrate, 40% natrium nitrosum, 7% sodium nitrate ternary eutectic fused salt mixt instead
As thermal medium is moved, circulation is beaten by pump for liquid salts, the heat circulated in fused salt is taken away and cooled by heat exchanger byproduct steam
30 DEG C or so, the field investigation of kinds of processes condition is carried out, every kind of process conditions are first each to operate 48h, the temperature of coal bed gas, pressure
Main composition situation before and after power, flow condition and deoxidation, as listed by following table 7-9.In process of the test, by controlling return passage
Fused salt liquid level is by return passage fused salt Stress control in 5kPa or so, and fused salt pump discharge is by valve regulated, and distributing chamber's pressure head is automatic
Formed.
Table 7
Table 8
Table 9
Successively continuously run 10 days afterwards according to the condition of table 8, continuously run according to the condition of table 9 10 days, control condition and anti-
Answer effect without significant change, smooth running controls to adjust conveniently, do not find overtemperature focus, safer reliability.
On the basis of the technique of table 9, a venturi suction mixer, return passage outlet are installed in fused salt circulation line
Sub-fractions in 12 outflow fused salts are promoted through cool laggard pump for liquid salts of heat exchanger, and the pressure head formed by the use of pump for liquid salts is as dynamic
Power, return passage is exported 12 and flowed out after most of suction in fused salts, mixing enter distributing chamber through entrance 13, technological condition and
Deoxidation effect situation is as listed by table 10.
Table 10
On the basis of the technique of table 10, coal seam throughput is increased, and accordingly improves the pressure head of fused salt, technological condition and deoxidation
Effect situation is as listed by table 11.
Table 11
On the basis of the technique of table 10, coal bed gas venturi pumping blender is set, is used as power using the pressure head of unstripped gas, by end
The part deoxidation coal bed gas of cooling is drawn back, and dilutes coalbed methane containing oxygen, technological condition and deoxidation effect situation are as listed by table 12.
Table 12
In above process of the test, the CH in coal bed gas4And O2Reaction is essentially converted to CO2, in beds maximum temperature
Less than 515 DEG C CO≤0.10%, and more than 550 DEG C CO >=0.30%, illustrate reaction bed temperature be influence CO growing amounts
Key factor, the temperature control ability and effect of reactor are to reduce a condition of CO by-products contents；Detection preheating cooling heat exchange
The H of coal bed gas before device2S≤20ppm, only contains SO after deoxidation2, concentration is basically identical before and after deoxidation in terms of S, illustrates the last quilt of sulfide
Catalyst Adsorption is retained, in terms of two embodiments operation process of each twenties days, under each table process conditions, beds
The Temperature Distribution of warming-up section is relatively stable, illustrates a small amount of sulphur and catalyst activity reduction is caused at end, catalyst has certain
Resistant to sulfur ability.There is the obvious horizontal high temperature section of a heat release centre of beds vertical direction, and the temperature of bed is all up and down
It is lower slightly.In above process of the test, also control is aided in by controlling coal bed gas to preheat the insulation outside cooling heat exchanger and heat dispersal situations
The preheating situation of coal bed gas processed, to reach required temperature of reactor.
After the completion of experiment, the catalyst unloading mouthful of reactor bottom is opened, porcelain ball and catalyst are easy to draw off, and survey catalysis
Agent phosphorus content≤0.10%, illustrates without the carbon distribution problem for causing catalyst activity reduction.
From test situation and knowable to drawing off catalyst, the outer tube of porcelain ball and color regime, do not have to cover in operation process
Pipe leakage problem, even if but it may be speculated that the corrosion leakage of generation solder joint or weld seam, because operating pressure is relatively low, moves thermal medium
Or coal bed gas leaked by moving thermal sleeve caused by it is dangerous also relatively light, can after long-term operating finds casing leak
The sleeve pipe leaked injection heatproof sealing agent is blocked during parking maintenance or the amount of will leak out drops to very low degree.Due to
Sleeve pipe quantity is many and is independent of each other, and spacing is smaller, and several of closure moves thermal effect, the entirety control to bed temperature to overall
The influence of system and reaction effect is little.
In testing above, used catalyst is the universal combustion catalyst of prior art, and coal seam qi exhaustion is not used exclusively for
The special-purpose catalyst of oxygen, if filling is further improved or the more preferable coal bed gas deoxidation catalyst of performance, in low-pressure medium of the present invention
Circulation is moved under the conditions of the reactor assembly of thermal control temperature, is expected to obtain more preferable reaction effect, such as DNA vaccine can further improve,
By-product CO amount can be reduced further.
Claims (10)
1. a kind of low-pressure medium circulation moves the reactor assembly of thermal control temperature, mainly including reactor, the hot temperature-controlling system of shifting；
The reactor moves hot jacket pipe reactor using vertical, wherein, the top of reactor, which is set, to be moved thermal medium distributing chamber and returns
Flow chamber, the low temperature before heat absorption moves thermal medium and enters shifting thermal medium distributing chamber through moving thermal medium inlet, and distribution flows downwardly into sleeve pipe
Inner tube, to move thermal medium return passage under distributing chamber, after heat absorption to move thermal medium upward from the space between the inner and outer pipes of sleeve pipe
Flow into return passage；The vertical pipes are formed by inner and outer tubes nesting, inner tube upper end open in moving thermal medium distributing chamber base plate,
Outer tube upper end open extends down into beds in shifting thermal medium return passage base plate, sleeve pipe, until beds
End closure under bottom, outer tube, inner tube lower end extends under outer tube on end closure and is open, move the size of thermal sleeve, quantity, point
Cloth and heat exchange area ensure that shifting thermal control temperature ability；The flow direction of reaction material is along vertical pipes axis direction in beds
Upper entering and lower leaving or bottom in and top out, or radial direction perpendicular to casing axis direction ecto-entad or from inside to outside, reactor sets
Enter outlet interface accordingly；Reactor head or upper lateral part set one or more Catalyst packings mouthful, are set from reactor bottom
Put one or more catalyst unloadings mouthful；
It is described to move hot temperature-controlling system, except the shifting thermal medium distributing chamber of reactor head and return passage and extend down into catalysis
The sleeve pipe of agent bed, is also moved in thermal medium distributing chamber and/or return passage including being arranged on, and/or the shifting thermal medium outside reactor
Circulation, control assembly and heat exchanger, and shifting thermal control temperature is circulated by normal pressure or low pressure shifting thermal medium.
2. low-pressure medium circulation as claimed in claim 1 moves the reactor assembly of thermal control temperature, wherein, move the shifting used of hot temperature-controlling system
Thermal medium includes conduction oil, fused salt, and nitrogen, carbon dioxide, superheated vapour or its gaseous mixture, by high temperature circulation machine or
Pump is largely circulated；Or by venturi type suction mixer, pressurization cycle is moved after thermal medium suitably cooling with low discharge and made
For the power of venturi type suction mixer, remaining big flow moves thermal medium without cooling directly by venturi type suction mixer
Play circulation.
3. low-pressure medium circulation as claimed in claim 2 moves the reactor assembly of thermal control temperature, wherein, the fused salt is containing 53% nitre
Sour potassium, 40% natrium nitrosum, the ternary eutectic fused salt mixt of 7% sodium nitrate, or be lithium nitrate and the fused salt mixt containing lithium nitrate.
4. low-pressure medium circulation as claimed in claim 2 moves the reactor assembly of thermal control temperature, wherein, move hot temperature-controlling system and used
When hot water and steam is as heat transferring medium, water pump, water-carrying capacity is set to control to adjust valve, high-temperature reflux heat exchanger, low temperature outside reactor
Heat exchanger, the pure water of cryogenic heat exchanger outlet play pressurization through pump after by the flow of governor valve control water, enter high-temperature reflux and exchange heat
Device heat exchange moves thermal medium after being vaporizated into steam and further heat exchange heating as the superheated steam of high temperature.
5. low-pressure medium circulation as claimed in claim 2 moves the reactor assembly of thermal control temperature, wherein, move hot temperature-controlling system and used
Venturi type is set to draw gas blender, high-temperature reflux heat exchanger, low-temperature heat exchange when hot water and steam is as heat transferring medium, outside reactor
Device, water pump, water-carrying capacity control to adjust valve, are condensed by the way that small part superheated steam is cooled, and condensed water is suppressed through water pump, re-vaporize
Appropriate pressure head is formed, the power for the most of superheated steam circulation of promotion of blender of being drawn gas as venturi type;Or directly use
The pressurized pure water or deionized water of pipe network, using the heat of small part superheated steam by the pressure (hydraulic) water of appropriate flow in heat exchanger
Heat exchange vaporization forms the pressurized vapor of appropriate pressure head, and big portion is promoted as the venturi type blender that draws gas with a part of pressurized vapor
Divide the power of superheated steam circulation.
6. low-pressure medium circulation as claimed in claim 1 moves the reactor assembly of thermal control temperature, wherein, the hot temperature-controlling system of shifting, which is used, to be connect
The shifting heat medium temperature of catalyst bed reaction temperature is bordering on, less distributing chamber, the return passage temperature difference is controlled, big flow is carried out and follows
Ring.
7. low-pressure medium circulation as claimed in claim 1 moves the reactor assembly of thermal control temperature, wherein, beds have parallel
The depressed structure of upper entering and lower leaving and the relatively low reaction material inlet temperature of use in casing axis direction；Or beds have vertically
Radial structure in casing axis direction enters air outlet structure and increases the sleeve pipe distribution density of key reaction section.
8. low-pressure medium circulation as claimed in claim 1 moves the reactor assembly of thermal control temperature, wherein, heat exchange sleeve gos deep into catalyst
The 0.5-20m of bed, tube pitch 0.02-0.10m, heat exchange area 5-100m2/m3Catalyst；And/or the bottom of beds
Filling inert ceramic balls are supported;And/or the end socket of its lower end is spherical, spheroid shape or taper；And/or Catalyst packing
Pipe upper end is extended on the base plate for moving thermal medium distributing chamber or on roof, or outside the reactor of beds upper lateral part
Wall.
9. low-pressure medium circulation as claimed in claim 1 moves the reactor assembly of thermal control temperature, wherein, also set up the preheating of reaction material
Cooling heat exchanger, the reaction material of the reaction material raw material preheating of reactor inlet, outlet is cooled down.
10. low-pressure medium circulation as claimed in claim 1 moves the reactor assembly of thermal control temperature, wherein, when entrance material reactant is dense
When degree is higher, material will be exported and returned with appropriate recycle ratio, the reactant concentration of entrance material is diluted.
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| CN107670592A (en) * | 2017-10-10 | 2018-02-09 | 湖南安淳高新技术有限公司 | A kind of shell-and-tube reactor and methanol synthesizing process |
| CN108455528A (en) * | 2018-01-15 | 2018-08-28 | 清华大学 | A kind of methane is low-temperature catalyzed to reform the device and method for producing solar energy fuel |
| CN111167382A (en) * | 2020-01-13 | 2020-05-19 | 清华大学 | Gas heat exchange type reactor and sulfuric acid catalytic decomposition method |
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| CN108455528A (en) * | 2018-01-15 | 2018-08-28 | 清华大学 | A kind of methane is low-temperature catalyzed to reform the device and method for producing solar energy fuel |
| CN111167382A (en) * | 2020-01-13 | 2020-05-19 | 清华大学 | Gas heat exchange type reactor and sulfuric acid catalytic decomposition method |
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