CN202924752U - Triple-heat exchanger ammonia synthesis reactor - Google Patents
Triple-heat exchanger ammonia synthesis reactor Download PDFInfo
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- CN202924752U CN202924752U CN201220314837XU CN201220314837U CN202924752U CN 202924752 U CN202924752 U CN 202924752U CN 201220314837X U CN201220314837X U CN 201220314837XU CN 201220314837 U CN201220314837 U CN 201220314837U CN 202924752 U CN202924752 U CN 202924752U
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Abstract
The utility model discloses a triple-heat exchanger ammonia synthesis reactor, divided into three radial adiabatic reaction beds, wherein heat exchangers are arranged in all of the three reaction beds; and the three layers of heat exchangers are called as an upper heat exchanger, a middle heat exchanger and a lower heat exchanger, respectively. Unreacted cool air is divided into three flows A, B and C and the three flows A, B and C enter the upper heat exchanger, the middle heat exchanger and the lower heat exchanger of the reactor, respectively; after being heated, the three air flows are collected in a zero-mark space at the top of the reactor and then pass through the first, second and third reaction beds for reaction orderly and radially; and in the mean time of reaction, the mixed gas is cooled by new entering three flows A, B and C of cool air, respectively, and then flows out of the reactor and finally enters a steam heater waste boiler. The reactor provided by the utility model is high in ammonia net value of the synthetic ammonia (13.1%-16.3%), low in resistance (0.2-0.4 MPa), high in tower outlet temperature which is close to 400 DEG C, and high in heat recovery rate; however, the tower outlet temperature is lower than 400 DEG C; and the steam heater waste boiler does not need a valuable material, and is easy to load and unload the catalyst and easy to regulate the temperature.
Description
Technical field
The utility model belongs to the Ammonia Production technical field, is specifically related to a kind of three heat and hands over ammonia synthesis reactor.
Background technology
H
2,N
2The gas ammonia synthesis reaction is to be the reversible exothermic reaction that solid catalyst carries out at iron, and its reaction formula is:
Iron is that the solid catalyst main component is FeO, Fe
2O
3, it needs and H
2Reaction is reduced to Fe just catalytic activity, and its active temperature scope is 360 ℃～520 ℃; Reaction is turned right and is carried out soon, and it is many to generate ammonia, reacts all right.
React relevant with many factors:
1. temperature: temperature is low, does not have activity, and temperature is high, can burn out catalyzer. and therefore reaction is controlled in this temperature range;
2. catalyst grain size: granularity is little, and surface-area is large, to reacting favourable. but granularity is too little, gas-flow resistance is large, and energy consumption is high;
3. pressure: pressure is higher, and is more favourable to reaction, but pressure is higher, and the compression energy consumption is high, and reaction vessel is thicker, and is heavier, the selective pressure scope;
4. unstripped gas indifferent gas CH
4/ Ar content: CH
4/ Ar is low, and to reacting favourable, synthesis system pressure decreases, compression Energy Intensity Reduction, CH
4/ Ar is too low, and the technology for refining raw-material gas investment is large; Because be reversible reaction, enter reactor hydrogen/nitrogen and can not 100% become ammonia, namely part synthesizes ammonia, after separation, after unreacted hydrogen/nitrogen fills into new raw material gas, enters reactor reaction, minute ammonia, tonifying Qi, so circulation again;
5. circulation gas CH
4/ Ar content: CH in tonifying Qi
4One timing of/Ar content, CH
4/ Ar content is low, and to reacting favourable, but too low, synthetic gas is dropped a hint greatly, and unstripped gas consumption is many.
6. circulation gas NH
3Content: the ammonia that reactor generates can not all separate, and always has a small amount of gas ammonia can not condensation, remains in the circulation gas circulation gas NH
3Content is lower, and is more favourable to reaction, but too low, and the condensation gas ammonia needs freezing power consumption many;
7. temperature control: carry out with reaction, ceaselessly emit heat, temperature rises continuously, for maintaining in the catalyst activity temperature range, need in time cooling, intensification, law of drop temperature have an optimal temperature curve, along this line traffic control temperature, speed of response is the fastest, in other words, and at a certain amount of hydrogen-catalyst reactor, generation ammonia is maximum, perhaps generate a certain amount of ammonia, catalytic amount is minimum, and reactor volume is minimum.
8. go out reactor (tower) gas temperature: tower exit temperature is low, and reaction heat circulates at inside reactor, and heat interchanging area is large in the tower, circulating flow rate is large, could press the reaction of optimal temperature curve, but therefore structure of reactor is complicated, consumptive material is many, heavy, and the circulator power consumption is large; Tower exit temperature is high, and reaction heat is utilized the generation saturation steam outside reactor, even produces middle high-pressure saturation steam, superheated vapour, heat interchanging area is little in the tower, and structure of reactor is simple, and consumptive material is few, the circulator power consumption is large, but therefore at the bottom of the tower and the heat regenerator material require very highly, investment is high.
The ammonia synthesis reactor design needs amid all these factors.
Existing a kind of ammonia synthesis reactor such as Fig. 1, reactor have four bed adiabatic catalytic beds, namely, the first anticatalysis 38, the second catalytic bed 39, the three catalytic beds 40, the four catalytic beds 41, first is axial, second and third, four for radially, in first without interchanger, second and third, there is respectively the tall and thin tubular heat exchange 35 of the second layer four centres, 36, the four layers of tall and thin tubular heat exchange 37 of the 3rd layer of tall and thin tubular heat exchange.Gas flow process in tower is: after the preheating unreacting gas in the 4th Tube Sheet of Heat Exchanger in bottom by after the 4th reaction hot gas heating, advance in the 3rd Tube Sheet of Heat Exchanger by the heating of the 3rd reaction hot gas, then enter in second Tube Sheet of Heat Exchanger by the heating of second reaction hot gas, temperature reaches 370 ℃～400 ℃, again after first reaction, temperature rise to 480 ℃; Hot gas is directly added outside tower enters second reaction after unreacted cold air is cooled to 410 ℃～430 ℃, temperature rise to 470 ℃; Reaction hot gas enters the 3rd reaction again by unreacted cold air cooling in second Tube Sheet of Heat Exchanger, temperature rise to 460 ℃; Then react hot gas by unreacted cold air cooling in the 3rd Tube Sheet of Heat Exchanger, enter the 4th reaction, temperature rise to 440 ℃, ammonia content 12%～14%, reaction finishes; At last, reaction hot gas is by 290 ℃～300 ℃ of unreacted cold air coolings in the 4th Tube Sheet of Heat Exchanger, goes out tower and advances to give up in the pan pipe, and heating tube produces steam outward.
But there is following deficiency in existing ammonia synthesis reactor:
1. this three heat hands over reactor that four layers of reaction gas are arranged, and repeatedly tears to four times complex structure open;
2. after first reaction, ammonia content has risen to 8%～9%, is directly added the cold shock of unreacted cold air outside tower, and ammonia content descends 1%～2%, makes total ammonia content descend 1%～2%, and ammonia net value is low;
3. first is axially, and gas-flow resistance is increased;
4. 85% unreacting gas is ganged up three interchanger and is heated, and gas-flow resistance is increased;
5. the end, the 3rd interchanger top, be full of the 3rd axial space, and heat interchanging area is larger, and the exhaust gas temperature is lower, and it is low to produce steam grade through useless pot.
The utility model content
The utility model is intended to overcome the deficiencies in the prior art, provides a kind of three heat to hand over ammonia synthesis reactor.
In order to achieve the above object, the technical scheme that provides of the utility model is:
Described three heat hand over ammonia synthesis reactor to comprise reactor shell, and described reactor shell leaves annular space by reactor outer cylinder body 14 and reactor inner barrel 11 suits between reactor inner barrel 11 and the reactor outer cylinder body 14;
Described reactor inner barrel 11 inside are divided into the 3rd reaction bed 20 by shrouding 9 from the bottom to top, the second reaction bed 15 and the first reaction bed 3, the second reaction bed 15 and 20 of the 3rd reaction beds are provided with the communicating pipe 16 of three evenly distribute (120 ° of distributions), the bore of communicating pipe 16 is 80mm～100mm, and pipe range is about 1/4 of reactor shell internal diameter; Be respectively equipped with in first, second, and third reaction bed loading catalyst and and reactor inner barrel 11 barrels between leave annular space sidewall the first bed basket the 6, second bed basket the 28 and the 3rd bed basket 27 radially radially radially of being distributed with some ventilating pits, described three radially the basket upper end be equipped with radially basket lid 10 with a plurality of perforates; Described first gap of radially leaving between basket 6 and reactor inner barrel 11 tops as first zero meter space; Wherein, radially the number of aperture of basket lid 10 is by middle cumulative many toward periphery, and the aperture is about 10mm.
Described the first bed radially basket the 6, second bed radially basket the 28 and the 3rd bed radially be respectively equipped with the first bed interchanger 4, the second bed interchanger 13 and the 3rd bed interchanger 21 that two ends up and down are end socket in basket 27 inside, described three interchanger include interchanger inner barrel 17 and interchanger outer cylinder body 18, leave annular space between described interchanger inner barrel 17 and the interchanger outer cylinder body 18; The tall and thin tubular heat exchange 4 of described the first bed, the tall and thin tubular heat exchange 13 of the second bed and the short and stout tubular heat exchange 21 of the 3rd bed are called again the heat friendship, middle heat is handed over and lower heat is handed over.
Interchanger inner barrel 17 upper ends and the interchanger outer cylinder body 18 of described the 3rd bed interchanger 21 are provided with a plurality of ventilating pits; The 3rd bed tube heat-exchanger 21 is provided with the pipe core 7 that passes successively the second bed interchanger 13 and the first bed interchanger 4 and be communicated with first zero rice space; Interchanger outer cylinder body 18 upper ends of the 3rd bed interchanger 21 are connected with the center effuser 19 that is sleeved on the pipe core 7, leave the annular space as channel of gas collection between pipe core 7 and the center effuser 19; Effuser 19 tube wall tops in center are blind end, in the center effuser 19, the bottom tube wall is provided with a plurality of ventilating pits;
In the interchanger outer cylinder body 18 of described the second bed interchanger 13, the bottom barrel is provided with a plurality of ventilating pits; The second bed interchanger 13 upper end end sockets are connected with the center sleeve 5 that is set with and passes the first bed interchanger 4 with pipe core 7, between center sleeve 5 and the pipe core 7 annular space are arranged;
In the outer cylinder body 18 of described the first bed interchanger 4, the bottom barrel is provided with a plurality of ventilating pits, the first bed interchanger 4 upper end end sockets are communicated with first zero rice space;
Described reactor shell is provided with the cold air that enters and pass the first reaction bed from the reactor shell top and be communicated with the first bed interchanger 4 lower end end sockets and enters pipe C 8, enters and pass first, second reaction bed from the reactor shell top and the cold air that is communicated with the second bed interchanger 13 lower end end sockets enters and manages B 12; Described reactor shell upper end is provided with high pressure blind plate 1 and charging tube 2;
Described reactor outer cylinder body 14 tops are provided with unreacting gas outlet B 31, unreacting gas outlet B 31 is communicated with the cold air outlet pipe 33 that is provided with valve first 32, pipeline location between valve first 32 and unreacting gas outlet B 31 is drawn the branch's bend pipe 24 that is provided with valve second 34, and branch's bend pipe 24 is connected with the inlet end that cold air enters pipe B 12;
The reactor lower end is provided with unreacting gas import B 29, discharge tube 22 and threeway 23; Described threeway 23 is provided with unreacting gas import A 30, the outlet 26 of thermal response gas and thermal response gas for subsequent use outlet 25; Described unreacting gas import B 29 is communicated with annular space between reactor inner barrel 11 and the reactor outer cylinder body 14; Described unreacting gas import A 30 is communicated with the interchanger inner barrel 17 of the 3rd bed interchanger 21 and the annular space between the interchanger outer cylinder body 18; The outlet 26 of described thermal response gas and thermal response gas for subsequent use outlet 25 are communicated with the 3rd bed interchanger 21 lower end end socket inner chambers.
In addition, the effuser 19 top tube walls zone of not establishing ventilating pit in described center is mounted with catalyst particle to increase resistance to flow; The zone that the interchanger outer cylinder body 18 top barrels of described the second bed interchanger 13 are not established ventilating pit is mounted with catalyst particle to increase resistance to flow; The zone that the outer cylinder body 18 top barrels of described the first bed interchanger 4 are not established ventilating pit is mounted with catalyst particle to increase resistance to flow.Three layers radially the ventilating pit of basket on the sidewall be tubaeform, ventilating pit closely radially basket catalyzer one end is osculum; Described thermal response gas outlet 26 is direct-connected outlet; Described thermal response gas outlet 25 for subsequent use is the non-direct-coupled type outlet.
Wherein, described the first bed interchanger 4 and the second bed interchanger 13 are tall and thin tubular heat exchange; Described the 3rd bed interchanger 21 is short and stout tubular heat exchange.
Below in conjunction with principle of work the utility model is described further.
During reactor work, unreacting gas cold air is divided into A, B, C three stocks do not enter heat friendship under the reactor, middle heat friendship and upper Re Jiaonei, come together in first zero rice space after being heated to 360 ℃～400 ℃ by reaction hot gas, then through upper heat hand over, middle heat is handed over and lower heat is handed over reaction and go out reactor.Detailed process is as follows:
Unreacted cold air is divided into three strands of three gangs of A, B, C: the about 50% unreacted cold air of C thigh is handed over through outer heat and is heated to 190 ℃～230 ℃ and then enters pipe C 8 from reactor head by cold air and enter into the first bed interchanger 4 lower ends, enters first zero rice space after from bottom to top baffling is heated to 360 ℃～400 ℃; About 30% unreacting gas of B thigh never reaction gas inlet B 29 enters annular space between reactor inner barrel 11 and the reactor outer cylinder body 14, in this annular space, be heated to from the bottom to top about 226 ℃, then enter pipe B 12 from reactor head by cold air and enter the second bed interchanger 13 lower ends, from bottom to top be heated to 360 ℃～400 ℃ and enter first zero rice space by center sleeve 5; A-share about 20% about 107 ℃ unreacted cold air enters the 3rd bed interchanger 21 lower ends by unreacting gas import A 30, from bottom to top is heated to 360 ℃～400 ℃ and also enters first zero rice space through pipe core 7; At this, three strands of unreacted cold air are mixed in first zero rice space.Then about 5%～7% mixing cold air is through the first bed radially basket cover plate 10 oblique the first reaction bed 3 upper strata catalyst reactions that pass through of basket 6 upper ends radially, and about 93%～95% mixing cold air through the first bed radially the annular space between basket 6 and reactor inner barrel 11 barrels evenly by the first bed basket 6 sidewall upper vent holes radially, reacted by outer catalyzer in interior first reaction bed 3 of radially flowing through, hot gas is evenly by the ventilating pit on the interchanger outer cylinder body 18 of the first bed interchanger 4 after the reaction, come together in the interchanger inner barrel 17 of the first bed interchanger 4 and the annular space between the interchanger outer cylinder body 18, then descend through baffling between the first bed interchanger 4 tubulations, after being cooled to about 420 ℃, the C thigh cold air that is risen from 3 outlets of the first reaction bed out, prepares to enter 15 reactions of the second reaction bed; Equally, about 5%～7% cooled mixed gas is through the second bed radially basket cover plate 10 oblique the second reaction bed 15 upper strata catalyst reactions that pass through of basket 28 upper ends radially, and about 93%～95% mixed gas through the second bed radially the annular space between basket 28 and reactor inner barrel 11 barrels evenly by the second bed basket 28 sidewall upper vent holes radially, reacted by outer catalyzer in interior second reaction bed 15 of radially flowing through, hot gas is evenly by the ventilating pit on the interchanger outer cylinder body 18 of the second bed interchanger 13 after the reaction, come together in the interchanger inner barrel 17 of the second bed interchanger 13 and the annular space between the interchanger outer cylinder body 18, then descend through baffling between the second bed interchanger 13 tubulations, after being cooled to about 410 ℃, the B thigh cold air that is risen from 15 outlets of the first reaction bed out, prepares to enter 20 reactions of the 3rd reaction bed; Equally, about 5%～7% cooled mixed gas is through the 3rd bed radially basket cover plate 10 oblique the 3rd reaction bed 20 upper strata catalyst reactions that pass through of basket 27 upper ends radially, and about 93%～95% mixed gas through the 3rd bed radially the annular space between basket 27 and reactor inner barrel 11 barrels evenly by the 3rd bed basket 27 sidewall upper vent holes radially, reacted by outer catalyzer in interior the 3rd reaction bed 20 of radially flowing through, then by in the center effuser 19, ventilating pit on the tube wall of bottom enters channel of gas collection between pipe core 7 and the center effuser 19, from top to bottom enter the 3rd bed interchanger 21, then descend through baffling between the 3rd bed interchanger 21 tubulations, flow out ammonia synthesis reactor from the outlet of reactor lower end reaction gas after the A-share cold air that is risen is cooled to below 390 ℃, produce 2.5MPa～3.9Mpa saturation steam or superheated vapour through the useless pot of vapor superheater.
When catalyst reduction, close valve valve second, open valve valve first, make the annular space between reactor inner barrel 11 and the reactor outer cylinder body 14 have cold air to pass through so that the high pressure cylindrical shell is not overheated, but cold air does not advance middle heat friendship, from and catalytic bed is not lowered the temperature.
Not only be provided with reaction heat outlet 26 in the reactor lower end threeway 23, also be provided with a reaction heat outlet 25 for subsequent use, if the useless pot of configuration be non-direct-coupled type, then from then on outlet for subsequent use is joined the anti-hydrogen pipe of a high temperature and side and is put to give up and pot be connected.
Experiment shows, the utlity model has good effect:
Utilize domestic a kind of catalyzer and the first operation condition: pressure 15MPa, advance indifferent gas (CH in the tower gas
4+ Ar) the 2%(liquid nitrogen washing is made with extra care unstripped gas),
Unreacting gas advances 370 ℃ of zero rice temperature, ammonia content 2.2%; After first reaction, temperature rises to 500 ℃, and ammonia content increases to 11.00%; Advance upper heat friendship and indirectly be cooled to 410 ℃, after second reaction, temperature rises to 466 ℃, and ammonia content increases to 14.80%; Advance middle heat friendship and indirectly be cooled to 385 ℃, after the 3rd reaction, temperature rises to 440 ℃, and ammonia content increases to 18.5%; Advance lower heat friendship and indirectly be chilled to 390 ℃, reaction hot gas enters direct-connected with it useless pot or vapor superheater through the thermal response gas outlet 26 of threeway 23.
Utilize domestic a kind of catalyzer and the second operation condition: pressure 15MPa, advance indifferent gas (CH in the tower gas
4+ Ar) the non-liquid nitrogen washing of 14%(is made with extra care unstripped gas),
Unreacting gas advances 370 ℃ of zero rice temperature, ammonia content 2.2%; After first reaction, temperature rises to 482 ℃, and ammonia content increases to 9.80%; Advance upper heat friendship and indirectly be cooled to 420 ℃, after second reaction, temperature rises to 464 ℃, and ammonia content increases to 12.80%; Advance middle heat friendship and indirectly be cooled to 410 ℃, after the 3rd reaction, temperature rises to 445 ℃, and ammonia content increases to 15.2%; Advance lower heat friendship and indirectly be chilled to 380 ℃, reaction hot gas is through the thermal response gas outlet of threeway 23
26 enter direct-connected with it useless pot or vapor superheater.
Compared with prior art, the beneficial effects of the utility model are:
1, ammonia synthesis reactor of the present utility model is provided with three reaction beds radially, and unreacting gas divides A, B, C three strands and enters three interchanger in the reaction bed, gas-flow resistance≤0.3mpa.
2, in the utility model, the unreacting gas that enters each layer pass through first inner core and basket annular space radially from top to bottom with the from bottom to top unreacted cold air heat exchange of inner/outer tube ring, utilize inner barrel to do heat interchanging area, reduce each layer heat interchanging area, improve volumetric efficiency.
3, ammonia synthesis reactor of the present utility model upper end covers greatly and is provided with charging tube.In the conventional art, when new oxide catalyst reduction rear catalyst volume-diminished, freeboard appears in beds top, unreacting gas has reduced the whole set ability without any from then on straight-through outlet of reaction, and this is a historical difficult problem, and the utility model utilizes charging tube, can add and give first reducing catalyst, make it to be full of the first reaction bed and do not open heavy large lid, solve a historical difficult problem.In addition, catalyzer lengthens duration of service.Gas brings objectionable impurities, pollute or the murder by poisoning catalyzer, wherein first is the victim who stands in the breach, very fast aging inactivation, but first and second bed catalyst activity under it is still fine, can utilize this moment charging tube to be poisoned the first bed catalyst and pump out, add and give first reducing catalyst, need not change whole tower catalyzer, improved whole tower catalyst efficiency, cost saving, and do not open heavy large lid, reduced the off-time.
4, in the utility model, volumetric shrinkage after the catalyst reduction, the freedom in minor affairs space is formed at the second reaction bed top, heat hands over outer cylinder body top not establish ventilating pit in the cause, be that the certain thickness catalyzer is arranged below the freedom in minor affairs space, stop three layers on the straight-through interchanger to the of gas short circuit unreacted, guarantee that total ammonia net value can not reduce.
5, there is certain-length second and third three communicating pipe of interbed of the present utility model, be full of the granule catalyzer in the pipe, the 3rd top can not form the freedom in minor affairs space, when catalyzer uses for many years, aging inactivation, open discharge tube, the 3rd layer of catalyzer at first unloads, second layer catalyzer unloaded subsequently by three communicating pipe, within a short period of time, (about 24h) finished, and need not any power, and catalyzer is all unloaded, and open heavy large lid, the inner core of hundred tons of weights and decaying catalyst are hung out from urceolus and catalyzer is toppled over removing.Three communicating pipe both made things convenient for the self-unloading catalyzer, made through directly descending the 3rd layer gas large three communicating pipe because of resistance, and tolerance few (about 1%) can directly be surrendered tower through lower heat through catalyst reaction again, has namely guaranteed the higher ammonia net value of reaction.
6, the threeway of the utility model reactor lower end is provided with two reaction heat outlets, is applicable to the different useless pots of pattern (direct-connected/non-direct-coupled type) that connect.
7, the utility model advantage radially the cylinder ventilating pit be mouthful, gas at full speed sprays into, the bed gas distribution is even.
8, the utility model is at the bottom of the pressure, under the unfavorable operating mode such as indifferent gas content height, and pilot wire is extremely near the optimum temperuture line, and outlet ammonia is up to 15.3%, if unstripped gas (CH
4+ Ar)＜0.5%, advance tower unreacting gas (CH
4+ Ar) 3%～5%, then export ammonia up to more than the 18.5%..The utility model advantage is controlled out the temperature of tower reaction gas＜400 ℃, enters useless pot and produces an elevated pressures superheated vapour, but do not require special high temperature resistant anti-hydrogen material.
Description of drawings
Fig. 1 is the structural representation of ammonia synthesis reactor in the prior art;
Fig. 2 is structural representation of the present utility model.
Among the figure: 1, high pressure blind plate; 2, charging tube; 3, the first reaction bed; 4, the first bed interchanger; 5, center sleeve; 6, the first bed radially the basket; 7, pipe core; 8, cold air enters pipe C; 9, bottom sealing plate; 10, radially basket covers; 11, reactor inner barrel; 12, cold air enters pipe B; 13, the second bed interchanger; 14, reactor outer cylinder body; 15, the second reaction bed; 16, communicating pipe; 17, interchanger inner barrel; 18, interchanger outer cylinder body; 19, center effuser; 20, the 3rd reaction bed; 21, the 3rd bed interchanger; 22, discharge tube; 23, threeway; 24, branch's bend pipe; 25, thermal response gas outlet for subsequent use; 26, thermal reactor outlet; 27, the 3rd bed radially the basket; 28, the second bed radially the basket; 29, unreacting gas import B; 30, unreacting gas import A; 31, unreacting gas outlet B; 32, valve first; 33, cold air outlet pipe; 34, valve second; 35, the tall and thin tubular heat exchange of the second layer; 36, the 3rd layer of tall and thin tubular heat exchange; 37, the 4th layer of tall and thin tubular heat exchange; 38, the first catalytic bed; 39, the second catalytic bed; 40, the 3rd catalytic bed; 41, the 4th catalytic bed.
Embodiment
As shown in Figure 2, described three heat hand over ammonia synthesis reactor to comprise reactor shell, and described reactor shell leaves annular space by reactor outer cylinder body 14 and reactor inner barrel 11 suits between reactor inner barrel 11 and the reactor outer cylinder body 14;
Described reactor inner barrel 11 inside are divided into the 3rd reaction bed 20 by shrouding 9 from the bottom to top, the second reaction bed 15 and the first reaction bed 3, the second reaction bed 15 and 20 of the 3rd reaction beds are provided with the communicating pipe 16 of three evenly distribute (120 ° of distributions), the bore of communicating pipe 16 is 80mm～100mm, and pipe range is about 1/4 of reactor shell internal diameter; Be respectively equipped with in first, second, and third reaction bed loading catalyst and and reactor inner barrel 11 barrels between leave annular space sidewall the first bed basket the 6, second bed basket the 28 and the 3rd bed basket 27 radially radially radially of being distributed with some ventilating pits, described three radially the basket upper end be equipped with radially basket lid 10 with a plurality of perforates; Described first gap of radially leaving between basket 6 and reactor inner barrel 11 tops as first zero meter space; Wherein, radially the number of aperture of basket lid 10 is by middle cumulative many toward periphery, and the aperture is about 10mm.
Described the first bed radially basket the 6, second bed radially basket the 28 and the 3rd bed radially be respectively equipped with the first bed interchanger 4, the second bed interchanger 13 and the 3rd bed interchanger 21 that two ends up and down are end socket in basket 27 inside, described three interchanger include interchanger inner barrel 17 and interchanger outer cylinder body 18, leave annular space between described interchanger inner barrel 17 and the interchanger outer cylinder body 18; The tall and thin tubular heat exchange 4 of described the first bed, the tall and thin tubular heat exchange 13 of the second bed and the short and stout tubular heat exchange 21 of the 3rd bed are called again the heat friendship, middle heat is handed over and lower heat is handed over.
Interchanger inner barrel 17 upper ends and the interchanger outer cylinder body 18 of described the 3rd bed interchanger 21 are provided with a plurality of ventilating pits; The 3rd bed tube heat-exchanger 21 is provided with the pipe core 7 that passes successively the second bed interchanger 13 and the first bed interchanger 4 and be communicated with first zero rice space; Interchanger outer cylinder body 18 upper ends of the 3rd bed interchanger 21 are connected with the center effuser 19 that is sleeved on the pipe core 7, leave the annular space as channel of gas collection between pipe core 7 and the center effuser 19; Effuser 19 tube wall tops in center are blind end, in the center effuser 19, the bottom tube wall is provided with a plurality of ventilating pits;
In the interchanger outer cylinder body 18 of described the second bed interchanger 13, the bottom barrel is provided with a plurality of ventilating pits; The second bed interchanger 13 upper end end sockets are connected with the center sleeve 5 that is set with and passes the first bed interchanger 4 with pipe core 7, between center sleeve 5 and the pipe core 7 annular space are arranged;
In the outer cylinder body 18 of described the first bed interchanger 4, the bottom barrel is provided with a plurality of ventilating pits, the first bed interchanger 4 upper end end sockets are communicated with first zero rice space;
Described reactor shell is provided with the cold air that enters and pass the first reaction bed from the reactor shell top and be communicated with the first bed interchanger 4 lower end end sockets and enters pipe C 8, enters and pass first, second reaction bed from the reactor shell top and the cold air that is communicated with the second bed interchanger 13 lower end end sockets enters and manages B 12; Described reactor shell upper end is provided with high pressure blind plate 1 and charging tube 2;
Described reactor outer cylinder body 14 tops are provided with unreacting gas outlet B 31, unreacting gas outlet B 31 is communicated with the cold air outlet pipe 33 that is provided with valve first 32, pipeline location between valve first 32 and unreacting gas outlet B 31 is drawn the branch's bend pipe 24 that is provided with valve second 34, and branch's bend pipe 24 is connected with the inlet end that cold air enters pipe B 12;
The reactor lower end is provided with unreacting gas import B 29, discharge tube 22 and threeway 23; Described threeway 23 is provided with unreacting gas import A 30, the outlet 26 of thermal response gas and thermal response gas for subsequent use outlet 25; Described unreacting gas import B 29 is communicated with annular space between reactor inner barrel 11 and the reactor outer cylinder body 14; Described unreacting gas import A 30 is communicated with the interchanger inner barrel 17 of the 3rd bed interchanger 21 and the annular space between the interchanger outer cylinder body 18; The outlet 26 of described thermal response gas and thermal response gas for subsequent use outlet 25 are communicated with the 3rd bed interchanger 21 lower end end socket inner chambers.
In addition, the effuser 19 top tube walls zone of not establishing ventilating pit in described center is mounted with catalyst particle to increase resistance to flow; The zone that the interchanger outer cylinder body 18 top barrels of described the second bed interchanger 13 are not established ventilating pit is mounted with catalyst particle to increase resistance to flow; The zone that the outer cylinder body 18 top barrels of described the first bed interchanger 4 are not established ventilating pit is mounted with catalyst particle to increase resistance to flow.Three layers radially the ventilating pit of basket on the sidewall be tubaeform, closely radially basket catalyzer one end is osculum; Described thermal response gas outlet 26 is direct-connected outlet; Described thermal response gas outlet 25 for subsequent use is the non-direct-coupled type outlet.
Wherein, described the first bed interchanger 4 and the second bed interchanger 13 are tall and thin tubular heat exchange; Described the 3rd bed interchanger 21 is short and stout tubular heat exchange.
Claims (5)
1. a heat is handed over ammonia synthesis reactor, comprise reactor shell, it is characterized in that described reactor shell leaves annular space by reactor outer cylinder body (14) and reactor inner barrel (11) suit between reactor inner barrel (11) and the reactor outer cylinder body (14);
Described reactor inner barrel (11) inside is divided into the 3rd reaction bed (20) from the bottom to top, the second reaction bed (15) and the first reaction bed (3); Be provided with three equally distributed communicating pipe (16) between described the second reaction bed (15) and the 3rd reaction bed (20); Be respectively equipped with in described first, second, and third reaction bed loading catalyst and and reactor inner barrel (11) barrel between leave annular space sidewall the first bed basket (6), the second bed basket (28) and the 3rd bed basket (27) radially radially radially of being distributed with some ventilating pits, described three radially the radially basket that is equipped with a plurality of perforates of basket upper end cover (10); First gap of radially leaving between basket (6) and reactor inner barrel (11) top as first zero meter space;
Described the first bed radially basket (6), the second bed radially basket (28) and the 3rd bed are the first bed interchanger (4), the second bed interchanger (13) and the 3rd bed interchanger (21) of end socket in two ends about radially basket (27) inside is respectively equipped with, described three interchanger include interchanger inner barrel (17) and interchanger outer cylinder body (18), leave annular space between described interchanger inner barrel (17) and the interchanger outer cylinder body (18);
Interchanger inner barrel (17) upper end and the interchanger outer cylinder body (18) of described the 3rd bed interchanger (21) are provided with a plurality of ventilating pits; The 3rd bed interchanger (21) is provided with the pipe core (7) that passes successively the second bed interchanger (13) and the first bed interchanger (4) and be communicated with first zero rice space; Interchanger outer cylinder body (18) upper end of the 3rd bed interchanger (21) is connected with the center effuser (19) that is sleeved on the pipe core (7), leaves the annular space as channel of gas collection between pipe core (7) and the center effuser (19); Center effuser (19) tube wall top is blind end, in the center effuser (19), the bottom tube wall is provided with a plurality of ventilating pits;
In the interchanger outer cylinder body (18) of described the second bed interchanger (13), the bottom barrel is provided with a plurality of ventilating pits; The second bed interchanger (13) upper end end socket is connected with the center sleeve (5) that is set with and passes the first bed interchanger (4) with pipe core (7), between center sleeve (5) and the pipe core (7) annular space is arranged;
In the outer cylinder body (18) of described the first bed interchanger (4), the bottom barrel is provided with a plurality of ventilating pits, the first bed interchanger (4) upper end end socket is communicated with first zero meter space;
Described reactor shell is provided with the cold air that enters and pass the first reaction bed from the reactor shell top and be communicated with the first bed interchanger (4) lower end end socket and enters pipe C(8), enter and pass first, second reaction bed from the reactor shell top and the cold air that is communicated with the second bed interchanger (13) lower end end socket enter manage B(12); Described reactor shell upper end is provided with high pressure blind plate (1) and charging tube (2);
Described reactor outer cylinder body (14) top is provided with unreacting gas outlet B(31), described unreacting gas outlet B(31) is communicated with the cold air outlet pipe (33) that is provided with valve first (32), at valve first (32) and unreacting gas outlet B(31) between pipeline location draw the branch's bend pipe (24) that is provided with valve second (34), branch's bend pipe (24) enters with cold air and manages B(12) inlet end be communicated with;
The reactor lower end is provided with unreacting gas import B(29), discharge tube (22) and threeway (23); Described threeway (23) is provided with unreacting gas import A(30), thermal response gas outlet (26) and thermal response gas for subsequent use outlet (25); Described unreacting gas import B(29) with reactor inner barrel (11) and reactor outer cylinder body (14) between annular space be communicated with; Described unreacting gas import A(30) is communicated with the interchanger inner barrel (17) of the 3rd bed interchanger (21) and the annular space between the interchanger outer cylinder body (18); Described thermal response gas outlet (26) and thermal response gas for subsequent use outlet (25) are communicated with the 3rd bed interchanger (21) lower end end socket inner chambers.
2. three heat as claimed in claim 1 are handed over ammonia synthesis reactor, it is characterized in that the zone that described center effuser (19) top tube wall is not established ventilating pit is mounted with catalyst particle; The zone that interchanger outer cylinder body (18) the top barrel of described the second bed interchanger (13) is not established ventilating pit is mounted with catalyst particle; The zone that outer cylinder body (18) the top barrel of described the first bed interchanger (4) is not established ventilating pit is mounted with catalyst particle.
3. three heat as claimed in claim 1 are handed over ammonia synthesis reactor, it is characterized in that, described the first bed radially basket (6), the second bed radially basket (28) and the 3rd bed radially the ventilating pit on basket (27) sidewall be tubaeform, on one side ventilating pit closely radially a basket catalyzer be osculum.
4. three heat as claimed in claim 1 are handed over ammonia synthesis reactor, it is characterized in that described thermal response gas outlet (26) is direct-connected outlet; Described thermal response gas outlet for subsequent use (25) is the non-direct-coupled type outlet.
5. hand over ammonia synthesis reactor such as each described three heat of claim 1 to 4, it is characterized in that described the first bed interchanger (4) and the second bed interchanger (13) are tall and thin tubular heat exchange; Described the 3rd bed interchanger (21) is short and stout tubular heat exchange.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201220314837XU CN202924752U (en) | 2012-07-02 | 2012-07-02 | Triple-heat exchanger ammonia synthesis reactor |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201220314837XU CN202924752U (en) | 2012-07-02 | 2012-07-02 | Triple-heat exchanger ammonia synthesis reactor |
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| CN202924752U true CN202924752U (en) | 2013-05-08 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102701235A (en) * | 2012-07-02 | 2012-10-03 | 湖南安淳高新技术有限公司 | Ammonia synthesis reactor with three heat exchangers |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102701235A (en) * | 2012-07-02 | 2012-10-03 | 湖南安淳高新技术有限公司 | Ammonia synthesis reactor with three heat exchangers |
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