CN103752224A - Synthesis reactor with spiral preheating passage - Google Patents
Synthesis reactor with spiral preheating passage Download PDFInfo
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- CN103752224A CN103752224A CN201410000928.XA CN201410000928A CN103752224A CN 103752224 A CN103752224 A CN 103752224A CN 201410000928 A CN201410000928 A CN 201410000928A CN 103752224 A CN103752224 A CN 103752224A
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Abstract
The invention discloses a synthesis reactor with a spiral preheating passage, and relates to chemical synthesis reaction equipment. The synthesis reactor mainly comprises an upper end, a reaction chamber wall body, a spiral flow guide plate, an upper partition plate, a lower partition plate, a lower end and a reactor shell, wherein the reactor shell surrounds the periphery of the reaction chamber wall body; a space is formed between the reactor shell and the reaction chamber wall body; the spiral flow guide plate is spirally arranged in the space between the reactor shell and the reaction chamber wall body, so that the spiral preheating passage is formed in the space between the reactor shell and the reaction chamber wall body; the upper end of the spiral preheating passage is sealed by the upper partition plate; the lower partition plate is sealed at the lower ends of the spiral preheating passage and a reaction chamber; a through hole group is distributed at the lower part of the reaction chamber wall body in a surrounding way; the lower part of the spiral preheating passage is communicated to the lower part of the reaction chamber through the through hole group. According to the synthesis reactor with the spiral preheating passage, reaction heat in the reaction chamber can be fully used for heating raw gas or unreacted gas in the spiral preheating passage, and a target product can be easily catalytically synthesized.
Description
Technical field
The present invention relates to a kind of chemical industry equipment, specially refer to a kind of chemosynthesis reaction device.
Background technology
In the production of chemical synthesis, all need unstripped gas or unreacted device to carry out preheating, make it under suitable temperature conditions, catalyze and synthesize target product.Under the condition existing at catalyst, most of chemosynthesis reactions are all reversible reactions, when target product reaches after finite concentration, will be in balance, and reaction will no longer be carried out to the direction of synthetic target product.People are in carrying out the production process of combination reaction, in order to make reaction can continue to carry out to target product direction, must make mix products export from synthesis reactor and fill into new raw material gas in synthesis reactor, target product concentration in synthesis reactor is reduced, after destruction of balance, make combination reaction proceed, after mix products is exported from synthesis reactor, by separation equipment, unreacting gas is separated, again unreacting gas is returned and in synthesis reactor, carries out circular response, because one way catalytic rate is only in 20% left and right, unstripped gas must be by being repeatedly reacted into target product after circulation compression in synthesis reactor, and each circulation compression all needs to consume very large compression energy consumption.
In existing synthesis reactor, under the synthetic condition of applications catalyst, the operating pressure of synthetic ammonia is more than 8MPa, the operating pressure of synthesizing methanol is between 3～15MPa, the operating pressure of direct synthesis of dimethyl ether from synthesis gas is between 2～5MPa, obtain above-mentioned operating pressure, must take multi-stage compression to realize, compression energy consumption is very large, therefore, existing synthesis reactor must repeatedly circulate and multi-stage compression could synthesize unstripped gas the production process of target product, has the shortcoming that power consumption is large.
Summary of the invention
The object of the invention is to overcome the shortcoming of existing chemical synthesis equipment, design a kind of unstripped gas that makes and only need compress the synthesis reactor with spiral preheating channel that just can all synthesize target product by one way, making full use of reaction heat makes unstripped gas or unreacting gas carry out preheating, significantly to reduce power consumption and to improve catalytic efficiency, in the production of synthetic ammonia, methyl alcohol, dimethyl ether and in other need carry out the production process of chemical synthesis, realize energy-saving and emission-reduction.
A kind of synthesis reactor with spiral preheating channel of the present invention, it is characterized in that synthesis reactor is mainly comprised of upper end (1), reative cell wall body (10), spiral deflector (4), upper spacer (36), lower clapboard (11), lower end (17) and reactor shell (5), wherein, reative cell wall body (10) is cylindrical structure, and the interior space of reative cell wall body (10) cylindrical structure forms reative cell (II); Reactor shell (5) is cylindrical structure, reactor shell (5) is gone along with sb. to guard him the periphery in reative cell wall body (10), between reactor shell (5) and reative cell wall body (10), have living space, spiral deflector (4) is arranged in the space between reactor shell (5) and reative cell wall body (10) in the mode of spiraling, and makes the space between reactor shell (5) and reative cell wall body (10) form spiral preheating channel (I); The upper end of spiral preheating channel (I) is sealed by upper spacer (36), and upper spacer (36) is cirque structure, and upper spacer (36) is connected between reactor shell (5) and reative cell wall body (10); Lower clapboard (11) is disc-shaped structure, and lower clapboard (11) is enclosed in the lower end of spiral preheating channel (I) and is enclosed in the diapire of the lower end formation reative cell (II) of reative cell (II); The bottom of reative cell wall body (10) has around the via hole group (25) who distributes, the bottom of spiral preheating channel (I) is communicated to the bottom of reative cell (II) by via hole group (25), circulating air input port (35) access is arranged at the top of spiral preheating channel (I); Upper end (1) is arranged on the upper port of reactor shell (5), and upper end (1) forms upper chamber (VI) with the space that go along with sb. to guard him on the top of reactor shell (5), and upper chamber (VI) has gaseous mixture output interface (38) to pick out; Lower end (17) is arranged on the lower port of reactor shell (5), lower end (17) forms lower chamber (IV) with the space that go along with sb. to guard him the bottom of reactor shell (5), gaseous mixture input interface (21) access is arranged at the top of lower chamber (IV), the bottom of lower chamber (IV) is liquid collecting zone, and the bottom of liquid collecting zone has product outlet (19) to pick out.
In the present invention, on the diapire of reative cell (II), there is catalyst discharging outlet (12) to pick out; Circulating air input port (35) is linked into the top of spiral preheating channel (I) by the outside of synthesis reactor; Gaseous mixture output interface (38) picks out synthesis reactor from upper chamber (VI); Heat-insulation layer (6) is installed on the lateral wall of reactor shell (5); In reative cell (II), have temperature adjustment coil pipe (8), the upper end of temperature adjustment coil pipe (8) has temperature control medium outlet (7) to pick out, and there is temperature control medium import (9) access the lower end of temperature adjustment coil pipe (8); Gas-liquid separator (16) and gas skirt (15) are set in lower chamber (IV), and gas-liquid separator (16) comprises louvre type separator, coil pipe cooling separator and surface cooler formula separator; The interior space of gas skirt (15) forms collection chamber (III), and the top of collection chamber (III) has gas skirt outlet (14) to pick out, and gas skirt outlet (14) picks out the lower sides of reactor shell (5) by circulating air delivery outlet (24); In the outer setting communicating pipe (33) of synthesis reactor, circulating air delivery outlet (24) is by being connected to the circulating air input port (35) on spiral preheating channel (I) top communicating pipe (33); Upper end (1) is disc structure, between upper end (1) and the joint face of reactor shell (5) upper end, has sealing ring a(2); Lower end (17) is circular arc bottom structure, between lower end (17) and the joint face of reactor shell (5) lower end, has sealing ring b(20).
In foregoing invention, utilize spiral deflector (4) to be arranged in the space between reactor shell (5) and reative cell wall body (10) in the mode of spiraling, make the space between reactor shell (5) and reative cell wall body (10) form spiral preheating channel (I), the effective travel of preheating channel is extended, unstripped gas or unreacting gas are extended the residence time in preheating channel, thereby the reaction heat that can more make full use of in reative cell (II) comes heating raw gas or unreacting gas, after unstripped gas after heating or unreacting gas enter in reative cell (II), easier catalyzed synthetic target product.When carrying out chemical synthesis production, in reative cell (II) and in spiral preheating channel (I), be full of unstripped gas or unreacting gas, unstripped gas in reative cell (II) or unreacting gas are under catalyst action, carry out combination reaction, generate target product, when unstripped gas carries out chemosynthesis reaction, can produce heat, the reaction heat generating can make to heat up in reative cell (II), the temperature raising is conducted heat by wall body (10) and the spiral deflector (4) of reative cell (II), spiral preheating channel (I) is heated up, thereby make spiral preheating channel (I) unstripped gas or unreacting gas be heated up and carry out preheating, unstripped gas after preheating or unreacting gas enter in reative cell (II) by the via hole group (25) of reative cell wall body (10) bottom, touch after catalyst, generate target product, is the gaseous mixture of target product and unreacting gas in reative cell (II).When constantly generating target product, just constantly produce reaction heat, thereby constantly unstripped gas or unreacting gas in spiral preheating channel (I) are carried out to preheating.
Above-mentioned invention in the specific implementation, periphery in synthesis reactor arranges down-comer, the gaseous mixture output interface (38) that the input interface of down-comer is connected to upper chamber (VI) is upper, the output interface of down-comer is connected on the gaseous mixture input interface (21) of lower chamber (IV).During production, in down-comer, be full of the gaseous mixture of target product and unreacting gas, by carrying out cooling to down-comer, gaseous mixture in pipe is lowered the temperature and density increase, according to gravity circulation theory, gaseous mixture after cooling can carry out descending motion, enter into lower chamber (IV), target product in gaseous mixture reaches dew-point temperature when following after cooling, just become liquid target product, the liquid target product separated through gas-liquid separator (16) enters basin by product outlet (19) output, unreacting gas exports (14) through collection chamber (III) by gas skirt, circulating air delivery outlet (24), communicating pipe (33) and circulating air input port (35) enter into spiral preheating channel (I), after pre-heating temperature elevation, via hole group (25) on the wall body of reative cell bottom enters into reative cell (II) again, carry out chemosynthesis reaction, reaction heat heats up the gaseous mixture in reative cell (II), according to gravity circulation theory, gaseous mixture after intensification can carry out ascending motion, enter into upper chamber (VI), at this moment, because the gaseous mixture in down-comer carries out descending motion, thereby producing gravitation makes the gaseous mixture in upper chamber (VI) enter into down-comer.So go round and begin again, by synthesis reactor and be arranged on peripheral down-comer and form automatic cycle in isobaric condition, and isolate in time target product, the unstripped gas that synthetic target product consumes supplements by raw material tonifying Qi interface, make target product concentration in synthesis reactor all the time lower than equalization point, make combination reaction can continue to carry out.Synthesis reactor of the present invention be arranged on after peripheral down-comer applied in any combination, make unstripped gas only need just compress and can all synthesize target product by one way, overcome unstripped gas and need carry out the large shortcoming of iterative cycles compression power consumption, improved catalytic efficiency, realized energy-saving and emission-reduction.
In above-mentioned invention, temperature adjustment coil pipe (8) is set in reative cell (II), temperature control medium is flowed in temperature adjustment coil pipe (8), by the input temperature control medium of high temperature or the temperature control medium of low temperature, reative cell (II) is carried out to auxiliary heating or auxiliary cooling, in the applicable synthetic room temperature of target product of initial generation of equipment investment operation, when equipment normally moves, carry out the adjusting of operating temperature, meanwhile, play the effect that makes unstripped gas accelerate circulation catalysis.
In above-mentioned invention, gas skirt (15) is set in lower chamber (IV), its effect is that unreacting gas is assembled at gas skirt (15), make the interior space of gas skirt (15) form collection chamber (III), make heavy target product enter the top less than gas skirt (15), thereby prevent that the gaseous state target product in lower chamber (IV) from feeding back in reative cell (II) by communicating pipe (33) and spiral preheating channel (I), have influence on the catalytic efficiency in reative cell (II).
In above-mentioned invention, gas-liquid separator (16) is set in lower chamber (IV), its objective is that a target product separates in time, reduce the target product concentration in synthesis reactor, combination reaction is carried out to favourable direction, make unstripped gas accelerate synthetic target product, improve catalytic efficiency.Described gas-liquid separator (16) comprises louvre type separator, coil pipe cooling separator and surface cooler formula separator, when using louvre type separator, with collision separate mode, carry out gas-liquid separation, when the aerosol particle in mixture runs into louver plate washer in flow process, through collision, mutually condense agglomerating and form liquid target product; When using coil pipe cooling separator and surface cooler formula separator, in condensation separation mode, carry out gas-liquid separation, in the surface temperature of coil pipe or surface cooler, drop to the dew-point temperature of target product when following, just make the target product of gaseous state condense in the surface of coil pipe or surface cooler and isolate liquid product, or be reduced to the dew-point temperature of target product when following in the room temperature of lower chamber (IV), the target product of gaseous state is just condensed into liquid target product, reaches separated object.
The invention has the beneficial effects as follows: a kind of synthesis reactor with spiral preheating channel of design, utilize spiral deflector (4) to make the space between reactor shell (5) and reative cell wall body (10) form spiral preheating channel (I), the stroke of preheating channel is extended, thereby the reaction heat that can more make full use of in reative cell (II) comes heating raw gas or unreacting gas, make more easily catalyzed synthetic target product of unstripped gas or unreacting gas.Synthesis reactor of the present invention be arranged on after peripheral down-comer applied in any combination, make unstripped gas only need just compress and can all synthesize target product by one way, significantly to reduce power consumption and to improve catalytic efficiency, in the production process of chemical synthesis, realize energy-saving and emission-reduction.Compare with routine techniques, the present invention has overcome conventional chemical synthesis equipment need carry out the large shortcoming of iterative cycles compression power consumption unstripped gas.The present invention can apply on the production line of the chemical synthesis products such as methyl alcohol, dimethyl ether, synthetic ammonia.
Accompanying drawing explanation
Fig. 1 is a kind of synthesis reactor structure chart with spiral preheating channel of the present invention.
Fig. 2 moves the structure chart of hot assembly at the outside increase of the synthesis reactor down-comer with spiral preheating channel.
In figure: 1. upper end, 2. sealing ring a, 3. temperature sensor, 4. spiral deflector, 5. reactor shell, 6. heat-insulation layer, 7. temperature control medium outlet, 8. temperature adjustment coil pipe, 9. temperature control medium import, 10. reative cell wall body, 11. lower clapboards, 12. catalyst discharging outlets, 13. catalyst discharge ducts, 14. gas skirt outlets, 15. gas skirts, 16. gas-liquid separators, 17. lower ends, 18. product efferent ducts, 19. product outlets, 20. sealing ring b, 21. gaseous mixture input interfaces, 22. raw material tonifying Qi interfaces, 23. tube connector b, 24. circulating air delivery outlets, 25. via hole groups, 26. down-comer outlets, 27. cooling water inlets, 28. decline straight tubes, 29. decline coil pipe a, 30. decline coil pipe b, 31. move hot device shell, 32. coolant outlets, 33. communicating pipes, 34. down-comer imports, 35. circulating air input ports, 36. upper spacers, 37. tube connector a, 38. gaseous mixture output interfaces, I. spiral preheating channel, II. reative cell, III. collection chamber, IV. lower chamber, V. move heat-exchanging chamber, VI. upper chamber.
The specific embodiment
In embodiment shown in embodiment 1 Fig. 1, the synthesis reactor with spiral preheating channel is mainly comprised of upper end (1), reative cell wall body (10), spiral deflector (4), upper spacer (36), lower clapboard (11), lower end (17) and reactor shell (5), wherein, reative cell wall body (10) is cylindrical structure, and the interior space of reative cell wall body (10) cylindrical structure forms reative cell (II), reactor shell (5) is cylindrical structure, reactor shell (5) is gone along with sb. to guard him the periphery in reative cell wall body (10), heat-insulation layer (6) is installed on the lateral wall of reactor shell (5), between reactor shell (5) and reative cell wall body (10), have living space, spiral deflector (4) is arranged in the space between reactor shell (5) and reative cell wall body (10) in the mode of spiraling, and makes the space between reactor shell (5) and reative cell wall body (10) form spiral preheating channel (I), the upper end of spiral preheating channel (I) is sealed by upper spacer (36), and upper spacer (36) is cirque structure, and upper spacer (36) is connected between reactor shell (5) and reative cell wall body (10), lower clapboard (11) is disc-shaped structure, lower clapboard (11) is enclosed in the lower end of spiral preheating channel (I) and is enclosed in the diapire of the lower end formation reative cell (II) of reative cell (II), on the diapire of reative cell (II), there is catalyst discharging outlet (12) to pick out, in reative cell (II), there is temperature adjustment coil pipe (8), the upper end of temperature adjustment coil pipe (8) has temperature control medium outlet (7) to pick out, and there is temperature control medium import (9) access the lower end of temperature adjustment coil pipe (8), the bottom of reative cell wall body (10) has around the via hole group (25) who distributes, the bottom of spiral preheating channel (I) is communicated to the bottom of reative cell (II) by via hole group (25), circulating air input port (35) are linked into the top of spiral preheating channel (I) by the outside of synthesis reactor, upper end (1) is disc structure, upper end (1) is arranged on the upper port of reactor shell (5), between upper end (1) and the joint face of reactor shell (5) upper end, there is sealing ring a(2), upper end (1) forms upper chamber (VI) with the space that go along with sb. to guard him on the top of reactor shell (5), in upper chamber (VI), have temperature sensor (3), gaseous mixture output interface (38) picks out synthesis reactor from upper chamber (VI), lower end (17) is circular arc bottom structure, lower end (17) is arranged on the lower port of reactor shell (5), between the joint face of lower end (17) and reactor shell (5) lower end, there is sealing ring b(20), lower end (17) forms lower chamber (IV) with the space that go along with sb. to guard him the bottom of reactor shell (5), gaseous mixture input interface (21) access is arranged at the top of lower chamber (IV), the bottom of lower chamber (IV) is liquid collecting zone, the bottom of liquid collecting zone has product outlet (19) to pick out, gas-liquid separator (16) and gas skirt (15) are set in lower chamber (IV), gas-liquid separator (16) is louvre type separator, the interior space of gas skirt (15) forms collection chamber (III), and the top of collection chamber (III) has gas skirt outlet (14) to pick out, and gas skirt outlet (14) picks out the lower sides of reactor shell (5) by circulating air delivery outlet (24).In the present embodiment, in the outer setting communicating pipe (33) of synthesis reactor, circulating air delivery outlet (24) is by being connected to the circulating air input port (35) on spiral preheating channel (I) top communicating pipe (33).The present embodiment utilizes spiral deflector (4) to be arranged in the space between reactor shell (5) and reative cell wall body (10) in the mode of spiraling, make the space between reactor shell (5) and reative cell wall body (10) form spiral preheating channel (I), the stroke of preheating channel is extended, unstripped gas or unreacting gas are extended the residence time in preheating channel, thereby the reaction heat that can more make full use of in reative cell (II) comes heating raw gas or unreacting gas, after unstripped gas after heating or unreacting gas enter in reative cell (II), easier catalyzed synthetic target product.
On the production line of the above embodiments as methyl alcohol, dimethyl ether, synthetic ammonia or other chemical synthesis product, apply.When applying as synthesizing methanol equipment, at reative cell (II), CuO with 48%, 46% ZnO and 5% Al are set
2o
3for the pellet type catalyst of component, then the H of the CO of a volume and two volumes
2after mixing, as unstripped gas, be input in synthesis reactor, carry out synthesizing methanol production, the reaction equation that unstripped gas synthesizes methyl alcohol is CO+2H
2→ CH
3oH+102.5kj; When applying as one-step method dimethyl ether synthesis equipment, at reative cell (II), CuO with 48%, 46% ZnO and 5% Al are set
2o
3for the pellet type catalyst of component, then add and fill out ZSM-5 molecular sieve, then the H of the CO of a volume and two volumes
2after mixing, as unstripped gas, be input in synthesis reactor, carry out dimethyl ether synthesis production, the reaction equation that unstripped gas synthesizes dimethyl ether is 2CO+4H
2→ (CH
3)
2o+H
2o+200.2kj; When applying as ammonia synthesis unit, reative cell (II) setting, with catalyst component, take Fe as main, with Al
2o
3, K
2o, CaO, SiO
2, BaO is promoter, then the N of a volume
2h with three volumes
2after mixing, as unstripped gas, be input in synthesis reactor, carry out Ammonia Production, the reaction equation that unstripped gas synthesizes ammonia is N
2+ 3H
2→ 2NH
3+ 92.1kj.
Claims (9)
1. a synthesis reactor with spiral preheating channel, it is characterized in that synthesis reactor is mainly comprised of upper end (1), reative cell wall body (10), spiral deflector (4), upper spacer (36), lower clapboard (11), lower end (17) and reactor shell (5), wherein, reative cell wall body (10) is cylindrical structure, and the interior space of reative cell wall body (10) cylindrical structure forms reative cell (II); Reactor shell (5) is cylindrical structure, reactor shell (5) is gone along with sb. to guard him the periphery in reative cell wall body (10), between reactor shell (5) and reative cell wall body (10), have living space, spiral deflector (4) is arranged in the space between reactor shell (5) and reative cell wall body (10) in the mode of spiraling, and makes the space between reactor shell (5) and reative cell wall body (10) form spiral preheating channel (I); The upper end of spiral preheating channel (I) is sealed by upper spacer (36), and upper spacer (36) is cirque structure, and upper spacer (36) is connected between reactor shell (5) and reative cell wall body (10); Lower clapboard (11) is disc-shaped structure, and lower clapboard (11) is enclosed in the lower end of spiral preheating channel (I) and is enclosed in the diapire of the lower end formation reative cell (II) of reative cell (II); The bottom of reative cell wall body (10) has around the via hole group (25) who distributes, the bottom of spiral preheating channel (I) is communicated to the bottom of reative cell (II) by via hole group (25), circulating air input port (35) access is arranged at the top of spiral preheating channel (I); Upper end (1) is arranged on the upper port of reactor shell (5), and upper end (1) forms upper chamber (VI) with the space that go along with sb. to guard him on the top of reactor shell (5), and upper chamber (VI) has gaseous mixture output interface (38) to pick out; Lower end (17) is arranged on the lower port of reactor shell (5), lower end (17) forms lower chamber (IV) with the space that go along with sb. to guard him the bottom of reactor shell (5), gaseous mixture input interface (21) access is arranged at the top of lower chamber (IV), the bottom of lower chamber (IV) is liquid collecting zone, and the bottom of liquid collecting zone has product outlet (19) to pick out.
2. a kind of synthesis reactor with spiral preheating channel according to claim 1, is characterized in that having catalyst discharging outlet (12) to pick out on the diapire of reative cell (II).
3. a kind of synthesis reactor with spiral preheating channel according to claim 1, is characterized in that circulating air input port (35) is linked into the top of spiral preheating channel (I) by the outside of synthesis reactor.
4. a kind of synthesis reactor with spiral preheating channel according to claim 1, is characterized in that gaseous mixture output interface (38) picks out synthesis reactor from upper chamber (VI).
5. a kind of synthesis reactor with spiral preheating channel according to claim 1, is characterized in that installing heat-insulation layer (6) on the lateral wall of reactor shell (5).
6. a kind of synthesis reactor with spiral preheating channel according to claim 1, it is characterized in that in reative cell (II), there is temperature adjustment coil pipe (8), the upper end of temperature adjustment coil pipe (8) has temperature control medium outlet (7) to pick out, and there is temperature control medium import (9) access the lower end of temperature adjustment coil pipe (8).
7. a kind of synthesis reactor with spiral preheating channel according to claim 1, it is characterized in that arranging gas-liquid separator (16) and gas skirt (15) in lower chamber (IV), gas-liquid separator (16) comprises louvre type separator, coil pipe cooling separator and surface cooler formula separator; The interior space of gas skirt (15) forms collection chamber (III), and the top of collection chamber (III) has gas skirt outlet (14) to pick out, and gas skirt outlet (14) picks out the lower sides of reactor shell (5) by circulating air delivery outlet (24); In the outer setting communicating pipe (33) of synthesis reactor, circulating air delivery outlet (24) is by being connected to the circulating air input port (35) on spiral preheating channel (I) top communicating pipe (33).
8. a kind of synthesis reactor with spiral preheating channel according to claim 1, is characterized in that upper end (1), for disc structure, has sealing ring a(2 between upper end (1) and the joint face of reactor shell (5) upper end).
9. a kind of synthesis reactor with spiral preheating channel according to claim 1, is characterized in that lower end (17), for circular arc bottom structure, has sealing ring b(20 between lower end (17) and the joint face of reactor shell (5) lower end).
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| Application Number | Priority Date | Filing Date | Title |
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| CN201410000928.XA CN103752224B (en) | 2014-01-02 | 2014-01-02 | Synthesis reactor with spiral preheating passage |
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|---|---|---|---|
| CN201410000928.XA CN103752224B (en) | 2014-01-02 | 2014-01-02 | Synthesis reactor with spiral preheating passage |
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| CN103752224B CN103752224B (en) | 2015-05-20 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112097466A (en) * | 2020-10-16 | 2020-12-18 | 宋灵君 | Take chemical industry reation kettle of drying function to preheat feed arrangement |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85109055A (en) * | 1985-10-26 | 1987-07-01 | 李培基 | Coil pipe type reactor |
| US6926873B1 (en) * | 1999-06-15 | 2005-08-09 | Methanol Casale S.A. | Reactor in particular for exothermic reactions |
| CN202415424U (en) * | 2012-01-18 | 2012-09-05 | 江苏澳墅新保温材料有限公司 | Chemical reaction kettle |
| CN202803218U (en) * | 2012-08-09 | 2013-03-20 | 成都进界科技有限公司 | Novel low-pressure methanol synthesis tower |
| CN203635171U (en) * | 2014-01-02 | 2014-06-11 | 衢州昀睿工业设计有限公司 | Synthesis reactor with spiral preheating channel |
-
2014
- 2014-01-02 CN CN201410000928.XA patent/CN103752224B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85109055A (en) * | 1985-10-26 | 1987-07-01 | 李培基 | Coil pipe type reactor |
| US6926873B1 (en) * | 1999-06-15 | 2005-08-09 | Methanol Casale S.A. | Reactor in particular for exothermic reactions |
| CN202415424U (en) * | 2012-01-18 | 2012-09-05 | 江苏澳墅新保温材料有限公司 | Chemical reaction kettle |
| CN202803218U (en) * | 2012-08-09 | 2013-03-20 | 成都进界科技有限公司 | Novel low-pressure methanol synthesis tower |
| CN203635171U (en) * | 2014-01-02 | 2014-06-11 | 衢州昀睿工业设计有限公司 | Synthesis reactor with spiral preheating channel |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112097466A (en) * | 2020-10-16 | 2020-12-18 | 宋灵君 | Take chemical industry reation kettle of drying function to preheat feed arrangement |
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| CN103752224B (en) | 2015-05-20 |
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