CN103706305B - Split self-circulation chemical synthesizer - Google Patents
Split self-circulation chemical synthesizer Download PDFInfo
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- CN103706305B CN103706305B CN201310715536.7A CN201310715536A CN103706305B CN 103706305 B CN103706305 B CN 103706305B CN 201310715536 A CN201310715536 A CN 201310715536A CN 103706305 B CN103706305 B CN 103706305B
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- 239000000126 substance Substances 0.000 title abstract description 5
- 239000007788 liquid Substances 0.000 claims abstract description 79
- 238000000926 separation method Methods 0.000 claims abstract description 52
- 238000001816 cooling Methods 0.000 claims abstract description 45
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 45
- 239000002994 raw material Substances 0.000 claims abstract description 10
- 210000004027 cell Anatomy 0.000 claims description 60
- 230000015572 biosynthetic process Effects 0.000 claims description 22
- 239000003054 catalyst Substances 0.000 claims description 14
- 238000007789 sealing Methods 0.000 claims description 8
- 210000002421 cell wall Anatomy 0.000 claims description 7
- 238000009413 insulation Methods 0.000 claims description 7
- 238000005496 tempering Methods 0.000 claims description 7
- 239000000203 mixture Substances 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 abstract description 23
- 230000006835 compression Effects 0.000 abstract description 15
- 238000007906 compression Methods 0.000 abstract description 15
- 230000003197 catalytic effect Effects 0.000 abstract description 8
- 239000000047 product Substances 0.000 description 53
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 21
- 238000004519 manufacturing process Methods 0.000 description 16
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 14
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 14
- 239000008246 gaseous mixture Substances 0.000 description 13
- 229910021529 ammonia Inorganic materials 0.000 description 7
- 239000000498 cooling water Substances 0.000 description 7
- 238000002156 mixing Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 230000005484 gravity Effects 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 230000002194 synthesizing effect Effects 0.000 description 3
- 230000001174 ascending effect Effects 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 230000003292 diminished effect Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000000178 monomer Substances 0.000 description 2
- 239000008188 pellet Substances 0.000 description 2
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- 239000000443 aerosol Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000001308 synthesis method Methods 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
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Abstract
The invention discloses a split self-circulation chemical synthesizer and relates to a chemical synthesis reactor. A heat exchanger and a reactor form a self-circulation system, wherein the heat exchanger consists of a down pipe and a shell; a cooling chamber is formed by an inner space of the shell; the down pipe is arranged in the cooling chamber; the reactor consists of an upper end head, a wall body, a lower end head, a gas-liquid separator, a gas-collecting hood and a preheating chamber; the upper end head is arranged at an upper opening of the wall body; the lower end head is arranged at a lower opening of the wall body; the upper end head and an inner space defined by a middle section and an upper section of the wall body form a reaction chamber; the lower end head and an inner space defined by a lower section of the wall body form a gas-liquid separation chamber; a clapboard is arranged between the reaction chamber and the gas-liquid separation chamber for isolating; a circulating gas input opening is formed in the clapboard. The automatic circulation is realized by the chemical synthesizer under inner isobaric conditions, and a target product is timely separated, so that raw material gas can be totally synthesized into the target product through one-step compression only, the power consumption is greatly reduced, and the catalytic efficiency is improved.
Description
Technical field
The present invention relates to a kind of chemical industry equipment, be related specifically to a kind of chemosynthesis reaction device.
Background technology
Under catalyst existent condition, most of chemosynthesis reaction is all reversible reaction, after target product reaches finite concentration, will be in balance, reacts and will no longer carry out to the direction of synthesis target product.People are in the production process of carrying out combination reaction, can continue to make reaction to carry out to target product direction, mix products must be made to export from synthesis reactor and fill into new raw material gas in synthesis reactor, target product concentration in synthesis reactor is reduced, combination reaction is made to proceed after destruction of balance, after mix products exports from synthesis reactor, by separation equipment, unreacting gas is separated, again unreacting gas is returned in synthesis reactor and carry out circular response, because one way catalytic rate is only about 20%, unstripped gas must by being reacted into target product after the compression that repeatedly circulates in synthesis reactor, and the compression that circulates all needs to consume very large compression energy consumption at every turn.
In existing synthesis reactor, under the condition of applications catalyst synthesis, the operating pressure of synthetic ammonia is at 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, multi-stage compression must be taked to realize, compression energy consumption is very large, therefore, existing synthesis reactor repeatedly must circulate and unstripped gas could be synthesized the production process of target product with multi-stage compression, there is the shortcoming that power consumption is large.
Summary of the invention
The object of the invention is to overcome existing chemical synthesis equipment and unstripped gas need be carried out the large shortcoming of iterative cycles compression power consumption, design a kind of Split self-circulation chemical synthesis device, carry out automatic cycle by chemical synthesis device oneself and carry out chemosynthesis reaction, make unstripped gas only just all need can synthesize target product by first compression, significantly to reduce power consumption and to improve catalytic efficiency, in the production of synthetic ammonia, methyl alcohol, dimethyl ether and need carry out realizing energy-saving and emission-reduction in the production process of chemical synthesis at other.
Split self-circulation chemical synthesis device of the present invention, it is characterized in that forming self-circulation system by heat exchanger and reactor, wherein, heat exchanger is made up of down-comer and shell (30), the interior space of shell (30) forms cooling chamber (V), down-comer is arranged in cooling chamber (V), the upper end mouth of pipe of down-comer is connected to input interface a(32 after the top of cooling chamber (V) passes), the lower end mouth of pipe of down-comer is connected to output interface a(25 after the bottom of cooling chamber (V) passes), input interface b(26 is arranged at the bottom of cooling chamber (V)) access, output interface b(31 is arranged at the top of cooling chamber (V)) pick out, reactor is by upper end (1), wall body (4), lower end (18), gas-liquid separator (17), gas skirt (15) and preheating chamber (II) composition, upper end (1) is disc structure, wall body (4) is cylindrical structure, lower end (18) is circular arc bottom structure, upper end (1) is arranged on the upper port of wall body (4), lower end (18) is arranged on the lower port of wall body (4), the interior space that upper end (1) surrounds with stage casing and the epimere of wall body (4) forms reative cell (I), the interior space that lower end (18) surrounds with the hypomere of wall body (4) forms gas-liquid separation chamber (III), dividing plate (11) is had to isolate between reative cell (I) and gas-liquid separation chamber (III), dividing plate (11) forms the diapire of reative cell (I), dividing plate (11) there is circulating air input port (9), gas-liquid separator (17), gas skirt (15) and preheating chamber (II) are arranged in gas-liquid separation chamber (III), gas skirt (15) is in the top of gas-liquid separator (17), the top of gas skirt (15) is preheating chamber (II), heat(ing) coil (13) is had in preheating chamber (II), the interior space of gas skirt (15) forms collection chamber (IV), the top of gas skirt (15) is by communicating pipe b(16) be connected to the entrance of preheating chamber (II), the outlet of preheating chamber (II) is by communicating pipe a(12) be connected to circulating air input port (9), input interface c(23 is arranged at the top of gas-liquid separation chamber (III)) access, the formation liquid collecting zone, bottom of gas-liquid separation chamber (III), the bottom of liquid collecting zone has product exit (20) to pick out, the bottom of reative cell (I) has catalyst discharge outlets (10) to pick out, and output interface c(34 is arranged at the top of reative cell (I)) pick out, the output interface c(34 on reative cell (I) top) be connected to the input interface a(32 of heat exchanger), the output interface a(25 of heat exchanger) be connected to the input interface c(23 on gas-liquid separation chamber (III) top), the output interface a(25 at heat exchanger) and the input interface c(23 on gas-liquid separation chamber (III) top) between connecting pipe on have raw material tonifying Qi interface (22) to access, the top of reative cell (I) is by output interface c(34) and the input interface a(32 of heat exchanger) be communicated to heat exchanger down-comer in space, the interior space of down-comer is by output interface a(25) and the input interface c(23 on gas-liquid separation chamber (III) top) be communicated to gas-liquid separation chamber (III), gas-liquid separation chamber (III) by collection chamber (IV) by communicating pipe b(16) be communicated to preheating chamber (II), preheating chamber (II) is by communicating pipe a(12) and circulating air input port (9) be communicated to the bottom of reative cell (I).
In the present invention, down-comer in heat exchanger is by central straight pipe (27), internal layer coil pipe (29) and outer coil pipe (28) combine, internal layer coil pipe (29) is arranged on the periphery of central straight pipe (27), in the periphery of internal layer coil pipe (29), outer coil pipe (28) is set, the upper end mouth of pipe of internal layer coil pipe (29) and the upper end mouth of pipe of outer coil pipe (28) are connected on the epimere of central straight pipe (27), the lower end mouth of pipe of internal layer coil pipe (29) and the lower end mouth of pipe of outer coil pipe (28) are connected on the hypomere of central straight pipe (27), the upper end mouth of pipe of central straight pipe (27) is connected to input interface a(32 after the top of cooling chamber (V) passes), the lower end mouth of pipe of central straight pipe (27) is connected to output interface a(25 after the bottom of cooling chamber (V) passes), tempering coil (6) is had in reative cell (I), half partition-type structures that the circulating air input port (9) of reative cell (I) is multi-through hole, heat-insulation layer (5) is installed in the outside of the outside of reative cell wall body (4) and upper end (1), heat insulation layer is had in the side of gas-liquid separation chamber (III) in the outside of preheating chamber (II) and dividing plate (11), gas-liquid separator (17) in gas-liquid separation chamber (III) comprises louvre type separator, coil pipe cooling separator and surface cooler formula separator, sealing ring a(2 is had) between upper end (1) and the joint face of reative cell wall body (4) upper port, sealing ring b(21 is had) between lower end (18) and the joint face of wall body (4) lower port.
Foregoing invention in the specific implementation, input interface b(26 heat exchanger) be connected on the feed pipe of cooling system, output interface b(31 heat exchanger) be connected on the return pipe of cooling system, cooling water is circulated in the cooling chamber (V) of heat exchanger, raw material tonifying Qi interface (22) is connected on the exhaust port of feed gas compressor, catalyst is set in reative cell (I) simultaneously, the requirement of catalyst according to target product is selected and activates, then in reactor, unstripped gas is inputted, unstripped gas is made to enter into reative cell (I), just combination reaction is carried out in reative cell (I), generate target product, when unstripped gas carries out combination reaction, heat can be produced, the reaction heat generated can make to heat up in reative cell (I), thus the unreacting gas in reative cell (I) and gaseous state target product are heated up, the density of the gaseous mixture of unreacting gas and the mixing of gaseous state target product is diminished, according to gravity circulation principle, gaseous mixture after intensification can carry out ascending motion, enter into the top of reative cell (I), simultaneously, down-comer in heat exchanger is because being placed in cooling water, make the fractional cold in down-comer very high, unreacting gas in down-comer and gaseous mixture are cooled and fast cooling, the density of unreacting gas or gaseous mixture is increased, according to gravity circulation principle, unreacting gas after cooling or gaseous mixture can carry out descending motion, output interface a(25 by heat exchanger) export the gas-liquid separation chamber (III) entering into reactor, gaseous mixture in gas-liquid separation chamber (III) after gas-liquid separator (17) is separated, be separated into liquid target product and the unreacting gas of gaseous state, liquid target product is exported by product exit (20) and product efferent duct (19) and enters product storage tank, unreacting gas by collection chamber (IV) by communicating pipe b(16) enter into preheating chamber (II) and carry out preheating, through the unreacting gas of preheating by communicating pipe a(12) enter reative cell (I) by circulating air input port (9) and carry out circular response, the unstripped gas that synthesis target product consumes is supplemented by raw material tonifying Qi interface (22), so go round and begin again, by chemical synthesis device oneself, in inside, isobaric condition forms automatic cycle, and isolate target product in time, make target product concentration in combination reaction device all the time lower than equalization point, make combination reaction can continue to carry out.The present invention makes unstripped gas only just all need can synthesize target product by first compression, overcomes unstripped gas and need carry out the large shortcoming of iterative cycles compression power consumption, improve catalytic efficiency, realize energy-saving and emission-reduction.
In above-mentioned invention, heat exchanger and reactor are carried out split manufacture, then links together, when obtaining said function, making monomer structure simpler, manufacturing more easily more convenient with maintenance.In the present invention, the unreacting gas that need cool or gaseous mixture are cooled by the cooling passage in helix tube, thus the physics stroke that flowing material is cooled in heat exchanger lengthens, and is thus more easily cooled; Adopt the measure of the nested setting of many group helix tubes, make the compact conformation of heat exchanger and floor space little, make full use of the interior space of cooling chamber (V), obtain larger heat transfer area, thus cooling effectiveness is improved; Helix tube has very high bearing capacity, can, in high pressure or super-pressure applications, therefore be adapted at applying in the system of chemical industry synthesis.
In above-mentioned invention, the effect arranging heat(ing) coil (13) in preheating chamber (II) carries out preheating to unstripped gas, equipment investment run initial, reative cell (I) is made to produce the room temperature being applicable to target product synthesis by ringing, the adjustment of operating temperature is carried out when equipment normally runs, meanwhile, the effect making unstripped gas accelerate circulation catalysis is played.During work, the heat medium in heat(ing) coil (13) is high-temperature water or the water vapour of 150-250 DEG C.
In above-mentioned invention, the effect arranging tempering coil (6) in reative cell (I) is the operating temperature controlling reative cell (I), during concrete enforcement, on top set temperature sensor (3) of reative cell (I), according to the temperature information that temperature sensor (3) detects, control the operating temperature of reative cell (I) by the flow of cooling water in operation tempering coil (6).
In above-mentioned invention, gas skirt (15) is set in gas-liquid separation chamber (III), its effect is that unreacting gas is assembled at gas skirt (15), the interior space of gas skirt (15) is made to form collection chamber (IV), make heavy target product not enter the top of gas skirt (15), thus prevent the gaseous target product in gas-liquid separation chamber (III) from being fed back to the catalytic efficiency had influence in reative cell (I) in reative cell (I) by closed circuit.
In above-mentioned invention, gas-liquid separator (17) is set in gas-liquid separation chamber (III), its objective is that a target product is separated in time, reduce the target product concentration in reactor, combination reaction is carried out to favourable direction, makes unstripped gas accelerate synthesis target product, improve catalytic efficiency.Described gas-liquid separator (17) comprises louvre type separator, coil pipe cooling separator and surface cooler formula separator, when using louvre type separator, gas-liquid separation is carried out to collide separate mode, when aerosol particle in mixture runs into louver plate washer in flow process, agglomerating and form liquid target product through colliding mutually condensation; When using coil pipe cooling separator and surface cooler formula separator, gas-liquid separation is carried out in condensation separation mode, when the surface temperature of coil pipe or surface cooler drops to below the evaporating temperature of target product, just the target product of gaseous state is made to condense in the surface of coil pipe or surface cooler and isolate liquid product, or when the room temperature of gas-liquid separation chamber (III) is reduced to below the evaporating temperature of target product, the target product of gaseous state is just condensed into liquid target product, reaches separation object.
In above-mentioned invention, circulating air input port (9) is designed to half partition-type structures of multi-through hole, catalyst in reative cell (I) can not be leaked by circulating air input port (9), and half partition-type structures of multi-through hole can not hinder unreacting gas to enter in reative cell (I).
The invention has the beneficial effects as follows: a kind of Split self-circulation chemical synthesis device of design, heat exchanger and reactor are carried out split manufacture, make monomer structure simpler, manufacture more easily and overhaul more convenient.During production, by chemical synthesis device oneself, in inside, isobaric condition forms automatic cycle, and isolate target product in time, make unstripped gas only just all need can synthesize target product by first compression, significantly to reduce power consumption and to improve catalytic efficiency, in the production process of chemical synthesis, realize energy-saving and emission-reduction.Compared with routine techniques, instant invention overcomes 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
Accompanying drawing is the structure chart of Split self-circulation chemical synthesis device of the present invention.
In figure: 1. upper end, 2. sealing ring a, 3. temperature sensor, 4. reative cell wall body, 5. heat-insulation layer, 6. tempering coil, 7. coolant outlet, 8. cooling water inlet, 9. circulating air input port, 10. catalyst discharge outlets, 11. dividing plates, 12. circulating air communicating pipe a, 13. heat(ing) coils, 14. preheating chamber fender bodies, 15. gas skirts, 16. circulating air communicating pipe b, 17. gas-liquid separators, 18. lower ends, 19. product efferent ducts, 20. product exit, 21. sealing ring b, 22. raw material tonifying Qi interfaces, 23. input interface c, 24. tube connector a, 25. output interface a, 26. input interface b, 27. central straight pipes, 28. outer coil pipes, 29. internal layer coil pipes, the shell of 30. cooling chambers, 31. output interface b, 32. input interface a, 33. tube connector b, 34. output interface c, I. reative cell, II. preheating chamber, III. gas-liquid separation chamber, IV. collection chamber, V. cooling chamber.
Detailed description of the invention
In embodiment shown in the drawings, Split self-circulation chemical synthesis device forms self-circulation system by heat exchanger and reactor, wherein, heat exchanger is made up of down-comer and shell (30), the interior space of shell (30) forms cooling chamber (V), down-comer is arranged in cooling chamber (V), the upper end mouth of pipe of down-comer is connected to input interface a(32 after the top of cooling chamber (V) passes), the lower end mouth of pipe of down-comer is connected to output interface a(25 after the bottom of cooling chamber (V) passes), input interface b(26 is arranged at the bottom of cooling chamber (V)) access, output interface b(31 is arranged at the top of cooling chamber (V)) pick out, reactor is by upper end (1), wall body (4), lower end (18), gas-liquid separator (17), gas skirt (15) and preheating chamber (II) composition, upper end (1) is disc structure, wall body (4) is cylindrical structure, lower end (18) is circular arc bottom structure, upper end (1) is arranged on the upper port of wall body (4), lower end (18) is arranged on the lower port of wall body (4), the interior space that upper end (1) surrounds with stage casing and the epimere of wall body (4) forms reative cell (I), the interior space that lower end (18) surrounds with the hypomere of wall body (4) forms gas-liquid separation chamber (III), dividing plate (11) is had to isolate between reative cell (I) and gas-liquid separation chamber (III), dividing plate (11) forms the diapire of reative cell (I), dividing plate (11) there is circulating air input port (9), gas-liquid separator (17), gas skirt (15) and preheating chamber (II) are arranged in gas-liquid separation chamber (III), gas skirt (15) is in the top of gas-liquid separator (17), the top of gas skirt (15) is preheating chamber (II), heat(ing) coil (13) is had in preheating chamber (II), the interior space of gas skirt (15) forms collection chamber (IV), the top of gas skirt (15) is by communicating pipe b(16) be connected to the entrance of preheating chamber (II), the outlet of preheating chamber (II) is by communicating pipe a(12) be connected to circulating air input port (9), input interface c(23 is arranged at the top of gas-liquid separation chamber (III)) access, the formation liquid collecting zone, bottom of gas-liquid separation chamber (III), the bottom of liquid collecting zone has product exit (20) to pick out, the bottom of reative cell (I) has catalyst discharge outlets (10) to pick out, and output interface c(34 is arranged at the top of reative cell (I)) pick out, the output interface c(34 on reative cell (I) top) be connected to the input interface a(32 of heat exchanger), the output interface a(25 of heat exchanger) be connected to the input interface c(23 on gas-liquid separation chamber (III) top), the output interface a(25 at heat exchanger) and the input interface c(23 on gas-liquid separation chamber (III) top) between connecting pipe on have raw material tonifying Qi interface (22) to access, the top of reative cell (I) is by output interface c(34) and the input interface a(32 of heat exchanger) be communicated to heat exchanger down-comer in space, the interior space of down-comer is by output interface a(25) and the input interface c(23 on gas-liquid separation chamber (III) top) be communicated to gas-liquid separation chamber (III), gas-liquid separation chamber (III) by collection chamber (IV) by communicating pipe b(16) be communicated to preheating chamber (II), preheating chamber (II) is by communicating pipe a(12) and circulating air input port (9) be communicated to the bottom of reative cell (I).In the present embodiment, down-comer in heat exchanger is by central straight pipe (27), internal layer coil pipe (29) and outer coil pipe (28) combine, internal layer coil pipe (29) is arranged on the periphery of central straight pipe (27), in the periphery of internal layer coil pipe (29), outer coil pipe (28) is set, the upper end mouth of pipe of internal layer coil pipe (29) and the upper end mouth of pipe of outer coil pipe (28) are connected on the epimere of central straight pipe (27), the lower end mouth of pipe of internal layer coil pipe (29) and the lower end mouth of pipe of outer coil pipe (28) are connected on the hypomere of central straight pipe (27), the upper end mouth of pipe of central straight pipe (27) is connected to input interface a(32 after the top of cooling chamber (V) passes), the lower end mouth of pipe of central straight pipe (27) is connected to output interface a(25 after the bottom of cooling chamber (V) passes), tempering coil (6) is had in reative cell (I), half partition-type structures that the circulating air input port (9) of reative cell (I) is multi-through hole, heat-insulation layer (5) is installed in the outside of the outside of reative cell wall body (4) and upper end (1), heat insulation layer is had in the side of gas-liquid separation chamber (III) in the outside of preheating chamber (II) and dividing plate (11), gas-liquid separator (17) in gas-liquid separation chamber (III) is surface cooler formula separator, sealing ring a(2 is had) between upper end (1) and the joint face of reative cell wall body (4) upper port, sealing ring b(21 is had) between lower end (18) and the joint face of wall body (4) lower port, temperature sensor (3) is had on the top of reative cell (I).
The above embodiments are when applying, input interface b(26 heat exchanger) be connected on the feed pipe of cooling system, output interface b(31 heat exchanger) be connected on the return pipe of cooling system, cooling water is circulated in the cooling chamber (V) of heat exchanger, raw material tonifying Qi interface (22) is connected on the exhaust port of feed gas compressor, catalyst is set in reative cell (I) simultaneously, the requirement of catalyst according to target product is selected and activates, then in reactor, unstripped gas is inputted, unstripped gas is made to enter into reative cell (I), just combination reaction is carried out in reative cell (I), generate target product, when unstripped gas carries out combination reaction, heat can be produced, the reaction heat generated can make to heat up in reative cell (I), thus the unreacting gas in reative cell (I) and gaseous state target product are heated up, the density of the gaseous mixture of unreacting gas and the mixing of gaseous state target product is diminished, according to gravity circulation principle, gaseous mixture after intensification can carry out ascending motion, enter into the top of reative cell (I), simultaneously, down-comer in heat exchanger is because being placed in cooling water, make the fractional cold in down-comer very high, unreacting gas in down-comer and gaseous mixture are cooled and fast cooling, the density of unreacting gas or gaseous mixture is increased, according to gravity circulation principle, unreacting gas after cooling or gaseous mixture can carry out descending motion, output interface a(25 by heat exchanger) export the gas-liquid separation chamber (III) entering into reactor, gaseous mixture in gas-liquid separation chamber (III) after gas-liquid separator (17) is separated, be separated into liquid target product and the unreacting gas of gaseous state, liquid target product is exported by product exit (20) and product efferent duct (19) and enters product storage tank, unreacting gas by collection chamber (IV) by communicating pipe b(16) enter into preheating chamber (II) and carry out preheating, through the unreacting gas of preheating by communicating pipe a(12) enter reative cell (I) by circulating air input port (9) and carry out circular response, the unstripped gas that synthesis target product consumes is supplemented by raw material tonifying Qi interface (22), so go round and begin again, by chemical synthesis device oneself, in inside, isobaric condition forms automatic cycle, and isolate target product in time, make target product concentration in combination reaction device all the time lower than equalization point, make combination reaction can continue to carry out.The present embodiment makes unstripped gas only just all need can synthesize target product by first compression, overcomes unstripped gas and need carry out the large shortcoming of iterative cycles compression power consumption, improve catalytic efficiency, realize energy-saving and emission-reduction.During production, the heat medium in heat(ing) coil (13) is high-temperature water or the water vapour of 150-250 DEG C; According to the temperature information that temperature sensor (3) detects, control the operating temperature of reative cell (I) by the flow of cooling water in operation tempering coil (6), make the room temperature in reative cell (I) meet the temperature requirement of chemical synthesis.
The production line of the above embodiments as methyl alcohol, dimethyl ether, synthetic ammonia or other chemical synthesis product is applied.When applying as synthesizing methanol equipment, arrange at reative cell (I) with the Al of the CuO of 48%, the ZnO of 46% and 5%
2o
3for the pellet type catalyst of component, then the H of the CO of a volume and two volumes
2be input in reactor as unstripped gas after mixing, 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 synthesis method dimethyl ether equipment, arrange at reative cell (I) with the Al of the CuO of 48%, the ZnO of 46% and 5%
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
2be input in reactor as unstripped gas after mixing, 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, arrange with catalyst component based on Fe, with Al at reative cell (I)
2o
3, K
2o, CaO, SiO
2, BaO is promoter, then the N of a volume
2with the H of three volumes
2be input in reactor as unstripped gas after mixing, carry out Ammonia Production, the reaction equation that unstripped gas synthesizes ammonia is N
2+ 3H
2→ 2NH
3+ 92.1kj.
Claims (8)
1. a Split self-circulation chemical synthesis device, it is characterized in that forming self-circulation system by heat exchanger and reactor, wherein, heat exchanger is made up of down-comer and shell (30), the interior space of shell (30) forms cooling chamber (V), down-comer is arranged in cooling chamber (V), the upper end mouth of pipe of down-comer is connected to input interface a(32 after the top of cooling chamber (V) passes), the lower end mouth of pipe of down-comer is connected to output interface a(25 after the bottom of cooling chamber (V) passes), input interface b(26 is arranged at the bottom of cooling chamber (V)) access, output interface b(31 is arranged at the top of cooling chamber (V)) pick out,
Reactor is by upper end (1), wall body (4), lower end (18), gas-liquid separator (17), gas skirt (15) and preheating chamber (II) composition, upper end (1) is disc structure, wall body (4) is cylindrical structure, lower end (18) is circular arc bottom structure, upper end (1) is arranged on the upper port of wall body (4), lower end (18) is arranged on the lower port of wall body (4), the interior space that upper end (1) surrounds with stage casing and the epimere of wall body (4) forms reative cell (I), the interior space that lower end (18) surrounds with the hypomere of wall body (4) forms gas-liquid separation chamber (III), dividing plate (11) is had to isolate between reative cell (I) and gas-liquid separation chamber (III), dividing plate (11) forms the diapire of reative cell (I), dividing plate (11) there is circulating air input port (9), gas-liquid separator (17), gas skirt (15) and preheating chamber (II) are arranged in gas-liquid separation chamber (III), gas skirt (15) is in the top of gas-liquid separator (17), the top of gas skirt (15) is preheating chamber (II), heat(ing) coil (13) is had in preheating chamber (II), the interior space of gas skirt (15) forms collection chamber (IV), the top of gas skirt (15) is by communicating pipe b(16) be connected to the entrance of preheating chamber (II), the outlet of preheating chamber (II) is by communicating pipe a(12) be connected to circulating air input port (9), input interface c(23 is arranged at the top of gas-liquid separation chamber (III)) access, the formation liquid collecting zone, bottom of gas-liquid separation chamber (III), the bottom of liquid collecting zone has product exit (20) to pick out, the bottom of reative cell (I) has catalyst discharge outlets (10) to pick out, and output interface c(34 is arranged at the top of reative cell (I)) pick out,
The output interface c(34 on reative cell (I) top) be connected to the input interface a(32 of heat exchanger), the output interface a(25 of heat exchanger) be connected to the input interface c(23 on gas-liquid separation chamber (III) top), the output interface a(25 at heat exchanger) and the input interface c(23 on gas-liquid separation chamber (III) top) between connecting pipe on have raw material tonifying Qi interface (22) to access; The top of reative cell (I) is by output interface c(34) and the input interface a(32 of heat exchanger) be communicated to heat exchanger down-comer in space, the interior space of down-comer is by output interface a(25) and the input interface c(23 on gas-liquid separation chamber (III) top) be communicated to gas-liquid separation chamber (III), gas-liquid separation chamber (III) by collection chamber (IV) by communicating pipe b(16) be communicated to preheating chamber (II), preheating chamber (II) is by communicating pipe a(12) and circulating air input port (9) be communicated to the bottom of reative cell (I).
2. a kind of Split self-circulation chemical synthesis device according to claim 1, it is characterized in that down-comer in heat exchanger is by central straight pipe (27), internal layer coil pipe (29) and outer coil pipe (28) combine, internal layer coil pipe (29) is arranged on the periphery of central straight pipe (27), in the periphery of internal layer coil pipe (29), outer coil pipe (28) is set, the upper end mouth of pipe of internal layer coil pipe (29) and the upper end mouth of pipe of outer coil pipe (28) are connected on the epimere of central straight pipe (27), the lower end mouth of pipe of internal layer coil pipe (29) and the lower end mouth of pipe of outer coil pipe (28) are connected on the hypomere of central straight pipe (27), the upper end mouth of pipe of central straight pipe (27) is connected to input interface a(32 after the top of cooling chamber (V) passes), the lower end mouth of pipe of central straight pipe (27) is connected to output interface a(25 after the bottom of cooling chamber (V) passes).
3. a kind of Split self-circulation chemical synthesis device according to claim 1, is characterized in that there is tempering coil (6) in reative cell (I).
4. a kind of Split self-circulation chemical synthesis device according to claim 1, is characterized in that half partition-type structures that the circulating air input port (9) of reative cell (I) is multi-through hole.
5. a kind of Split self-circulation chemical synthesis device according to claim 1, is characterized in that installing heat-insulation layer (5) on the outside of the outside of reative cell wall body (4) and upper end (1); Heat insulation layer is had in the side of gas-liquid separation chamber (III) in the outside of preheating chamber (II) and dividing plate (11).
6. a kind of Split self-circulation chemical synthesis device according to claim 1, is characterized in that the gas-liquid separator (17) in gas-liquid separation chamber (III) comprises louvre type separator, coil pipe cooling separator and surface cooler formula separator.
7. a kind of Split self-circulation chemical synthesis device according to claim 1, is characterized in that there is sealing ring a(2 between upper end (1) and the joint face of reative cell wall body (4) upper port).
8. a kind of Split self-circulation chemical synthesis device according to claim 1, is characterized in that there is sealing ring b(21 between lower end (18) and the joint face of wall body (4) lower port).
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Effective date of registration: 20170808 Address after: 063500 Luannan Tangshan City County, Hebei Province Anping West alley Ben towns District 102 Building No. 5 Patentee after: Li Jianmei Address before: Zhejiang province Quzhou City Kecheng District 324000 Kaixuan Road No. 6 (WITHUB industrial design Industrial Park Building 2, room B-302) Patentee before: Quzhou Yunrui Industry Design Co., Ltd. |
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