CN104437266B - Phase change heat absorption temperature control reactor - Google Patents
Phase change heat absorption temperature control reactor Download PDFInfo
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- CN104437266B CN104437266B CN201410662869.2A CN201410662869A CN104437266B CN 104437266 B CN104437266 B CN 104437266B CN 201410662869 A CN201410662869 A CN 201410662869A CN 104437266 B CN104437266 B CN 104437266B
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- 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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Abstract
The invention discloses a phase change heat absorption temperature control reactor. The phase change heat absorption temperature control reactor comprises a pressure bearing shell and a catalyst frame arranged in the pressure bearing shell and a heat removing tube bundle, wherein the heat removing tube bundle comprises a water intake tube, a water exhaust tube, a lower circular tube, a plurality of heat exchange water tubes, an upper circular tube, a water branch tube and an air collecting bag, wherein the water intake tube is communicated with the lower circular tube; the lower circular tube is arranged on the bottom of the pressure bearing shell; the upper circular tube is positioned above the lower circular tube; the plurality of heat exchange water tubes are sequentially connected between the upper circular tube and the lower circular tube in parallel; the water branch tube is communicated with the air collecting bag and the upper circular tube respectively; the water exhaust tube and the gas collecting bag are communicated; the plurality of heat exchange water tubes are positioned in the catalyst frame; the catalyst frame, the heat removing tube bundle and the pressure bearing shell are separated, so that overhauling, catalyst self-unloading and catalyst filling are convenient; a heat removing water tube is buried into a bed layer of the catalyst, so that the reaction heat in the bed layer of the catalyst can be removed timely, and the phenomena of original conversion, synthesis and sintering of a hydrogenation catalyst are prevented.
Description
Technical field
The present invention relates to a kind of fixed bed catalytic reactor, the temperature control reactor of more particularly, to a kind of decalescence.
Background technology
After co transformationreation, as a kind of extensive application response device of chemical industry, therebetween, people are to shift-converter for device
Carry out multiple improvement, from original holoaxial to being changed to overall diameter to obtaining very good effect in terms of catalyst bed layer resistance, but urge
Agent bed is still adiabatic reaction, and beds are divided into some beds, take indirect heat exchange or use Technology Quenched with Water between every bed.
It is low that this indirect heat exchange reclaims transformation system heat quality, reclaims sensible heat and latent heat efficiency is low, the easy overtemperature of catalyst, convert simultaneously
Also it is mixed with the defects such as the side reactions such as methanation.
The carbonylation synthesis reactor of coal-ethylene glycol, adopts loading catalyst in the pipe of ф 25x2, pipe exterior-applied liquid medicine at present
Move heat, a shell-and-tube reactor is made up of thousands of holoaxials to ф 21 cylinder shape catalyst bed, gas skewness, pair are anti-
Answer that thing is many, catalyst bed layer resistance is big, thermal stress is big, equipment leakage, the carbonyl compound of a set of 200,000 tons/year of glycol unit
Reactor is become to need 6 shell reactor parallel runnings, the defect such as construction investment is big.
The esterification hydrogenation reactor of coal-ethylene glycol, adopts loading catalyst in the pipe of ф 38x2 at present, and pipe exterior-applied liquid medicine moves
Heat, a shell-and-tube reactor is made up of thousands of holoaxials to ф 34 cylinder shape catalyst bed, gas skewness, side reaction
The defect such as thing is many, catalyst bed layer resistance is big, thermal stress is big, equipment leakage, construction investment are big.
The reaction of natural gas from coal adopts: the heat-removing way of n adiabatic bed and n useless superheat boiler, and needs to increase
Plus reactants water steam, to suppress first, second adiabatic bed reaction, configures circulating air, otherwise occurs first, second exhausted simultaneously
Hott bed layer temperature runaway phenomenon, the defect such as operation energy consumption is high, plant investment is big, SR is big.
Coal liquifaction, the Fischer-Tropsch synthesis of coal paraffin also do not have in the large-scale gasifying device running, partly little run
Type F- T synthesis device reaction device is also shell and tube reactor, and fe (or co) series catalysts are seated in ф 76x4 pipe, still deposit
In gas skewness, overtemperature, carbon distribution, Long carbon chain alkane yield are low, resistance is big, equipment leakage, the defect such as be difficult to maximize.
Content of the invention
It is an object of the invention to overcoming the deficiencies in the prior art, there is provided a kind of temperature control reactor of decalescence, lead to
Cross water in heat exchanger tube and be converted into steam generation decalescence and remove heat of reaction in beds in time.
The present invention is achieved by the following technical solutions, and the present invention includes pressure-bearing shell and is arranged in pressure-bearing shell
Catalyst frame and shifting heat pipe bundle；Described shifting heat pipe bundle include water inlet pipe, outlet pipe, lower endless tube, multiple heat exchanging water pipe, upper endless tube,
Water arm, plenum chamber；Endless tube under described water inlet pipe connection, lower endless tube is arranged at the bottom of pressure-bearing shell, and upper endless tube is located at lower ring
On pipe, multiple heat exchanging water pipes are connected in parallel between endless tube and lower endless tube successively, and water arm is respectively communicated with plenum chamber and upper endless tube,
Outlet pipe is connected with plenum chamber, and multiple heat exchanging water pipes are located at catalyst inframe.
Described heat exchanging water pipe is shaped form, the lower endless tube of one end connection of heat exchanging water pipe, the upper endless tube of other end connection.Shaped form
Being capable of more efficiently raising heat exchange efficiency.
Described pressure-bearing shell includes upper cover, low head and cylinder, and described upper cover is connected by flange with cylinder, lower envelope
Head and cylinder are integrally formed, and upper cover opens up the delivery port for the air inlet of air inlet with for connecting outlet pipe, low head
On open up self-unloading mouth for catalyst discharging, for the gas outlet given vent to anger and the water inlet for connecting water inlet pipe.
Described catalyst frame includes sealing plate, support base, gas distributor and gas collecting jar with ground-on cover plate, and described sealing plate is arranged at gas
Frame structure is formed on the top of distributor, and the bottom of gas distributor and support base are tightly connected, the lower endless tube of support base supporting, goes out
Water pipe is connected to corresponding delivery port, gas collecting jar with ground-on cover plate being radially arranged in gas distributor along gas distributor through sealing plate
Centre, the bottom connection gas outlet of gas collecting jar with ground-on cover plate, gas distributor and cylinder gap radially forms gas distributing chamber, heat exchanging water pipe
In gas distributor, loading catalyst in gas distributor.
The junction of described delivery port and outlet pipe is provided with the first black box, and the junction of sealing plate and outlet pipe is provided with
The junction of the second black box, gas outlet and gas collecting jar with ground-on cover plate is provided with the 3rd black box.
Described gas distributor and gas collecting jar with ground-on cover plate is radially even opens up multiple passages, can effectively be uniformly distributed gas
Body.
The present invention is applied to co transformationreation, carbonylation reaction, esterification hydrogenation reaction, methanation reaction, methanol-fueled CLC
The reactors such as reaction, Fischer-Tropsch synthesis.
The present invention is directed to co transformationreation reactor existing problems and deficiency, and high water/gas, high co water-gas become now
The demand changed, develops the radial direction constant temperature shift-converter of water shifting heat, is converted into steam generation phase transformation using water in heat exchanging water pipe
The principle of heat absorption, by co+h2o→h2+co2+qPutTransformationreation is released heat and is removed beds in time it is ensured that catalyst bed
Layer temperature≤380 DEG C, and the saturated vapor of by-product 0.8～9.0mpa, beneficial to catalyst self-unloading be easy to shifting hot water tube bundle sections
Maintenance.Efficiently solve existing shift-converter reclaim that heat quality is low, reclaim heat energy efficiency low, the easy overtemperature of catalyst, first
Alkanisation side reaction, catalyst hardly possible self-unloading and the big defect of construction investment.
The present invention is directed to filling pd/ai2o3Series catalysts, the carbonylation shell and tube synthesis reactor existing problems of ethylene glycol
And deficiency, develop the radial direction constant temperature carbonyl compound reactor of water shifting heat, be converted into steam generation phase using water in heat exchanging water pipe
The principle of changeable heat-absorbing, by co+ch3ono→(cooch3)2+no+qPutReaction is released heat and is removed beds in time it is ensured that urging
Agent bed temperature≤140 DEG C, and the saturated vapor of by-product 0.2～0.3mpa, beds adopt full radial structure.Effectively
Solve the existing carbonylation synthesis easy overtemperature of reactor catalyst, side reaction is big, bed resistance is big, be difficult to maximize, catalyst
Difficult self-unloading and the big defect of construction investment.
The present invention be directed to filling cu series catalysts, ethylene glycol esterification hydrogenation shell and tube synthesis reactor existing problems and not
Foot, develops the radial direction constant temperature hydrogenation reactor of water shifting heat, is converted into steam generation decalescence using water in heat exchanging water pipe
Principle is by ch3Ono adds h2Reaction (4h2+(cooch3)2→(ohch2c h2oh)2+2ch3oh+qPut) removal is urged in time to release heat
Agent bed is it is ensured that reaction bed temperature≤250 DEG C, and the saturated vapor of by-product 1.8～3.2mpa, and beds adopt
Full radial structure.Efficiently solve the existing esterification easy overtemperature of hydrogenation reactor catalyst, side reaction is big, bed resistance is big, be difficult to
Maximization, catalyst hardly possible self-unloading and the big defect of construction investment.
The present invention is directed to the ni series catalysts using temperature at 320～420 DEG C, develops the radial direction constant temperature methane of water shifting heat
Synthesis reactor, is converted into the principle of steam generation decalescence using water in heat exchanging water pipe, by co and h2Methanation reaction
(co+h2→ch4+h2o+qPut) release heat and remove beds in time it is ensured that reaction bed temperature≤420 DEG C, and by-product
The saturated vapor of 3.8～12.0mpa, beds adopt full radial structure.Efficiently solve existing methane synthesis reactor
The defect such as the easy overtemperature of catalyst, bed resistance are big, operation energy consumption is high, plant investment is big, SR is big.
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, opens
Send the radial direction constant temperature Fischer-Tropsch synthesis device of water shifting heat, be converted into the former of steam generation decalescence using water in heat exchanging water pipe
Reason, by co and h2Fischer-Tropsch synthesis (nco+ (2n+1) h2→cnh2n+2+nh2o+qPut) release heat remove catalyst in time
Bed is it is ensured that co reaction bed temperature≤240 DEG C, and the saturated vapor of by-product 1.8～2.8mpa；Fe reaction bed temperature
≤ 260 DEG C, and the saturated vapor of by-product 1.6～3.8mpa, beds are using full radial structure.Efficiently solve existing expense
The defect that support synthesis reactor exists.
The operation principle of the present invention is as follows:
Gas enters inside upper cover from air inlet pipe, subsequently into gas distributing chamber, by the uniform radial direction of gas distributor
Enter catalyst frame, have co-mo (or pd/ai2o3, or cu or ni or cu-zn or fe (or co)) series catalysts urge in bar
The exothermic reactions such as conversion, synthesis, hydrogenation are completed, reacted gas passes through gas collecting jar with ground-on cover plate and discharges decalescence by gas outlet under part
Temperature control reactor.The exothermic reaction liberated heats such as conversion, synthesis or hydrogenation are by the heat exchanging water pipe being embedded in catalyst inframe portion
Water is converted into steam and removes the saturated vapor under heat of reaction in beds, and by-product different pressures in time.
Unsaturated water enters lower endless tube by water inlet pipe, is assigned to heat exchanging water pipe by lower endless tube, unsaturated water is in heat exchanging water pipe
Inside flow from bottom to top, and complete the absorption to catalyst bed heat inside heat exchanging water pipe, occur water to be converted into the phase of steam
Become, and become supersaturation water, subsequently into water arm, plenum chamber, outlet pipe, in the drum of the temperature control reactor periphery of phase transformation
Flash off saturated vapor.
The present invention has the advantage that compared to existing technology
(1) the catalyst frame of the present invention, shifting heat pipe bundle are separated with pressure-bearing shell, easy access, catalyst self-unloading, catalyst
Filling；
(2) it is embedded in moving hot-water line inside beds and beds internal-response heat can be removed in time, keep away
Exempt from original conversion, synthesis and hydrogenation catalyst and be sintered phenomenon generation, efficiently solve the catalysis such as existing conversion, synthesis and hydrogenation
Agent service life is short, easy overtemperature, side reaction thing are many, bed temperature is wayward, time length of driving, be difficult to maximize, operation energy consumption
The defect such as high, construction investment is big；
(3) temperature of beds is adjusted by byproduct steam pressure it is ensured that to adjust aspect flexible, easy to control；With
When also ensuring that driving, take and add steam to water circulation system, rapidly controlled shifting thermal reactor temperature rise is got up, to shorten
The driving time；
(4) Natural Circulation is taken in water route, and when stopping suddenly, the reactant of controlled shifting thermal reactor internal residual part continues
Reaction, water route remain on holding circulation, and by beds internal heat removal it is ensured that the controlled shifting of unexpected dead ship condition heat
The bed temperature of reactor also will not surpass, effective protection catalyst service life；
(5) gas distributor of controlled shifting thermal reactor and gas collecting jar with ground-on cover plate are realized inside and outside double items and are compensated, and so that radial gas is divided
Cloth error≤5.0% is it is ensured that gas is evenly distributed；Controlled shifting thermal reactor bed overall resistance≤0.01mpa；
(6) adopt overall diameter to beds it is easy to larger-scale unit, not only solve a transport difficult problem, reduce engineering simultaneously
Investment.
Brief description
Fig. 1 is the structural representation of the present invention.
Specific embodiment
Below embodiments of the invention are elaborated, the present embodiment is carried out under premised on technical solution of the present invention
Implement, give detailed embodiment and specific operating process, but protection scope of the present invention is not limited to following enforcements
Example.
As shown in figure 1, the present embodiment includes pressure-bearing shell 1 and the catalyst frame 2 being arranged in pressure-bearing shell 1 and moves heat pipe
Bundle 3；Described shifting heat pipe bundle 3 includes water inlet pipe 31, outlet pipe 32, lower endless tube 33, multiple heat exchanging water pipe 34, upper endless tube 35, water prop up
Pipe 36, plenum chamber 37；Endless tube 33 under described water inlet pipe 31 connection, lower endless tube 33 is arranged at the bottom of pressure-bearing shell 1, upper endless tube 35
On lower endless tube 33, multiple heat exchanging water pipes 34 are connected in parallel between endless tube 35 and lower endless tube 33 successively, and water arm 36 is respectively
Connection plenum chamber 37 and upper endless tube 35, outlet pipe 32 is connected with plenum chamber 37, and multiple heat exchanging water pipes 34 are located at catalyst frame 2
Interior.
The heat exchanging water pipe 34 of the present embodiment is shaped form, the lower endless tube 33 of one end connection of heat exchanging water pipe 34, and the other end connects
Upper endless tube 35.Shaped form being capable of more efficiently raising heat exchange efficiency.
Pressure-bearing shell 1 includes upper cover 11, low head 12 and cylinder 13, and described upper cover 11 and cylinder 13 pass through flange 14
It is connected, low head 12 and cylinder 13 are integrally formed, upper cover 11 opens up for the air inlet 15 of air inlet and be used for connecting water outlet
The delivery port 16 of pipe 32, low head 12 opens up the self-unloading mouth 17 for catalyst discharging, for the gas outlet 18 given vent to anger with use
In the water inlet 19 connecting water inlet pipe 31.
Catalyst frame 2 includes sealing plate 21, support base 22, gas distributor 23 and gas collecting jar with ground-on cover plate 24, and described sealing plate 21 sets
Frame structure is formed on the top being placed in gas distributor 23, and the bottom of gas distributor 23 and support base 22 are tightly connected, and support
The lower endless tube 33 of seat 22 supporting, outlet pipe 32 is connected to corresponding delivery port 16 through sealing plate 21, and gas collecting jar with ground-on cover plate 24 is distributed along gas
The central authorities being radially arranged in gas distributor 23 of device 23, the bottom connection gas outlet 18 of gas collecting jar with ground-on cover plate 24, gas distributor 23 He
Cylinder 13 gap radially forms gas distributing chamber 25, and heat exchanging water pipe 34 is located in gas distributor 23, gas distributor 23
Interior loading catalyst.
The junction of delivery port 16 and outlet pipe 32 is provided with the first black box 4, the connection of sealing plate 21 and outlet pipe 32
Place is provided with the second black box 5, and the junction of gas outlet 18 and gas collecting jar with ground-on cover plate 24 is provided with the 3rd black box 6.
Gas distributor 23 and gas collecting jar with ground-on cover plate 24 is radially even opens up multiple passages, can effectively be uniformly distributed gas
Body.
In figure hollow arrow is water (flow) direction, and filled arrows are gas flow.
The reactor of the present embodiment is applied to the high water/gas of 220,000 tons/year of synthetic ammonia installations than device:
1st, design condition and requirement:
Water-gas gas componant:
2nd, transformation system major economic indicators list
| Sequence number | Major economic indicators title | Major economic indicators |
| 1 | Byproduct steam amount (2.5～3.8mpa) | 1063.5g/tnh3 |
| 2 | Byproduct steam amount (1.0～1.27mpa) | 247.8kg/tnh3 |
| 3 | The heating deoxygenation water yield (3.0mpa) | 1311.313kg/tnh3 |
| 4 | The heating desalination water yield (directly removing thermal de-aeration) | 6388.78kg/tnh3 |
| 5 | Deoxygenation water heater condensate liquid | 95.2kg/tnh3 |
| 6 | Desalination water heater condensate liquid | 440.64kg/tnh3 |
| 7 | Detoxification groove (pre- change) conversion ratio | ≤ 13% |
| One change conversion ratio | >=85% | |
| Two change conversion ratios | >=98.14% | |
| 8 | System outlet co content (butt) | ≤ 0.75% |
| 9 | Transformation system resistance mpa | ≤0.05 |
Embodiment 2
The present embodiment is applied to the low water/gas of 400,000 tons/year of synthetic ammonia installations than device, other embodiment and embodiment 1
Identical.
1st, design condition and requirement:
Conversion tolerance: 160273nm3/h
Operating pressure: 2.1mpa
Operating temperature: 35～40 DEG C
Gas componant is:
| Sequence number | Title | co2% | Co% | h2% | o2% | n2% | ch4% |
| 1 | Semiwater gas | 7.87 | 29.3 | 46.03 | 0.3 | 15.19 | 1.02 |
| 2 | Conversion gas | 24.00 | 4～8 | 55.40 | 0 | 12.60 | 0.85 |
2nd, the present invention is compared with traditional total-low process heat-insulating shift-converter, can bring following energy-conservation:
.
Claims (5)
1. a kind of temperature control reactor of decalescence is it is characterised in that including pressure-bearing shell (1) and being arranged at pressure-bearing shell (1)
Interior catalyst frame (2) and shifting heat pipe bundle (3)；Described shifting heat pipe bundle (3) includes water inlet pipe (31), outlet pipe (32), lower endless tube
(33), multiple heat exchanging water pipes (34), upper endless tube (35), water arm (36), plenum chamber (37)；Ring under described water inlet pipe (31) connection
Pipe (33), lower endless tube (33) is arranged at the bottom of pressure-bearing shell (1), and upper endless tube (35) is located on lower endless tube (33), Duo Gehuan
Hot-water line (34) is connected in parallel between endless tube (35) and lower endless tube (33) successively, water arm (36) be respectively communicated with plenum chamber (37) and
Upper endless tube (35), outlet pipe (32) is connected with plenum chamber (37), and multiple heat exchanging water pipes (34) are located in catalyst frame (2)；Institute
State catalyst frame (2) and include sealing plate (21), support base (22), gas distributor (23) and gas collecting jar with ground-on cover plate (24), described sealing plate
(21) frame structure is formed on the top being arranged at gas distributor (23), and the bottom of gas distributor (23) and support base (22) are close
Envelope connects, the lower endless tube (33) of support base (22) supporting, and outlet pipe (32) is connected to corresponding delivery port through sealing plate (21)
(16), gas collecting jar with ground-on cover plate (24) is along the central authorities being radially arranged in gas distributor (23) of gas distributor (23), gas collecting jar with ground-on cover plate (24)
Bottom connection gas outlet (18), gas distributor (23) and cylinder gap radially forms gas distributing chamber (25), heat-exchanging water
Pipe (34) is located in gas distributor (23), the interior loading catalyst of gas distributor (23).
2. a kind of temperature control reactor of decalescence according to claim 1 is it is characterised in that described heat exchanging water pipe (34)
For shaped form, the lower endless tube (33) of one end connection of heat exchanging water pipe (34), the upper endless tube (35) of other end connection.
3. a kind of temperature control reactor of decalescence according to claim 1 is it is characterised in that described pressure-bearing shell (1)
Including upper cover (11), low head (12) and cylinder, described upper cover (11) is connected by flange (14) with cylinder, low head
(12) it is integrally formed with cylinder, upper cover (11) opens up the air inlet (15) for air inlet and is used for connecting outlet pipe (32)
Delivery port (16), low head (12) opens up the self-unloading mouth (17) for catalyst discharging, for the gas outlet (18) given vent to anger and
For connecting the water inlet (19) of water inlet pipe (31).
4. a kind of decalescence according to claim 1 temperature control reactor it is characterised in that described delivery port (16) and
The junction of outlet pipe (32) is provided with the first black box (4), and the junction of sealing plate (21) and outlet pipe (32) is provided with second
Black box (5), the junction of gas outlet (18) and gas collecting jar with ground-on cover plate (24) is provided with the 3rd black box (6).
5. a kind of temperature control reactor of decalescence according to claim 1 is it is characterised in that described gas distributor
And gas collecting jar with ground-on cover plate (24) is radially even opens up multiple passages (23).
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| CN201410662869.2A CN104437266B (en) | 2014-11-18 | 2014-11-18 | Phase change heat absorption temperature control reactor |
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| CN201410662869.2A CN104437266B (en) | 2014-11-18 | 2014-11-18 | Phase change heat absorption temperature control reactor |
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| CN106582455A (en) * | 2017-01-23 | 2017-04-26 | 南京敦先化工科技有限公司 | Straight pipe header coil pipe type reactor for waterway natural circulation |
| CN107970867A (en) * | 2017-12-08 | 2018-05-01 | 河南心连心化肥有限公司 | A kind of radial reactor and preparation method for preparing 2- methylfurans |
| KR102454095B1 (en) * | 2020-10-30 | 2022-10-14 | 한국과학기술연구원 | Continuous hydrogen storage apparatus using liquid organic hydrogen carrier |
| CN114950280A (en) * | 2022-04-18 | 2022-08-30 | 牛忠玲 | Shell and tube heat exchanger and ft synthesis slurry bed reactor |
| CN115364774B (en) * | 2022-10-21 | 2023-02-03 | 江苏永大化工机械股份有限公司 | Radial reactor |
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| CN2680348Y (en) * | 2003-12-06 | 2005-02-23 | 杭州林达化工科技有限公司 | Catalytic reactor with interior heat exchange |
| EP2213367A4 (en) * | 2007-10-19 | 2014-05-07 | Lou Ren | A composite reaction apparatus and the chemical production method using the same |
| CN102234213B (en) * | 2010-04-20 | 2013-05-01 | 中国科学院过程工程研究所 | Complete methanation reaction device for synthesis gas |
| CN204261650U (en) * | 2014-11-18 | 2015-04-15 | 安徽新月化工设备有限公司 | A kind of temperature control reactor of decalescence |
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Effective date of registration: 20211122 Address after: No. 625, geguan Road, Liuhe District, Nanjing City, Jiangsu Province, 210000 Patentee after: NANJING DUNXIAN CHEMICAL TECHNOLOGY CO.,LTD. Address before: 234000 Building 5, Suma modern industrial park, Suzhou City, Anhui Province Patentee before: ANHUI XINYUE CHEMICAL EQUIPMENT Co.,Ltd. |