CN104841339A - Novel hydrogenation reactor for synthesis gas-to-ethylene glycol process - Google Patents
Novel hydrogenation reactor for synthesis gas-to-ethylene glycol process Download PDFInfo
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- CN104841339A CN104841339A CN201510180542.6A CN201510180542A CN104841339A CN 104841339 A CN104841339 A CN 104841339A CN 201510180542 A CN201510180542 A CN 201510180542A CN 104841339 A CN104841339 A CN 104841339A
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Abstract
The present invention relates to a novel hydrogenation reactor for a synthesis gas-to-ethylene glycol process. The reactor comprises a reactor housing, a heat exchange plate pair beam, a cooling medium distribution total pipe, a cooling medium distribution branch pipe, a cooling medium collection total pipe, and a cooling medium collection branch pipe, wherein the bottom portion of the reactor housing is provided with a cooling medium inlet, the top portion is provided with a cooling medium outlet, one end of the heat exchange plate pair beam is connected with the cooling medium inlet of the reactor housing through the cooling medium distribution total pipe and the cooling medium distribution branch pipe, the other end is connected with the cooling medium outlet of the reactor housing through the cooling medium collection total pipe and the cooling medium collection branch pipe, the heat exchange plate pair beam comprises a plurality of heat exchange plate pairs, the plate space exists in the heat exchange plate, a catalyst is filled between the adjacent heat exchange plate pairs, the housing space exists between the adjacent heat exchange plate pairs, raw material gas comprising dimethyl oxalate and hydrogen enters the reactor, then passes through the housing space, and reacts through the catalyst catalysis to produce ethylene glycol, the cooling fluid passes through the plate space, and the heat released by the reaction is taken away. Compared with the reactor in the prior art, the reactor of the present invention has advantages of flexible structure adjustment, high heat exchange efficiency, good reaction selectivity, on site assembly, and the like.
Description
Technical field
The present invention relates to synthesis gas preparing ethylene glycol technique, especially relate to a kind of new and effective novel hydrogenation reactor for the synthesis of gas preparing ethylene glycol technique.
Background technology
At present, in production ethylene glycol technique, the technique that synthesis gas produces ethylene glycol (EG) through dimethyl oxalate (DMO) has very strong competitiveness.DMO hydrogenation is a cascade reaction, and first DMO hydrogenation generates intermediate product methyl glycollate (MG), and MG repeated hydrogenation generates EG, EG excessive hydrogenation and then generates coproduct ethanol and 1,2-butanediol etc., also has other side reactions more to occur simultaneously.Therefore, DMO hydrogenation reaction is extremely responsive to temperature, even if very little temperature deviation all can produce tremendous influence to feed stock conversion and product composition.DMO hydrogenation process is rapid, and heat release is large and fast.Because reaction is to responsive to temperature, production process generally uses saturation water close to reaction temperature as cooling medium, therefore cooling medium and reactant have a narrow range of temperature, and require that the temperature difference in same level cross section and the temperature difference between hot(test)-spot temperature and saturation water control in less scope simultaneously; The thermal conductivity of reaction medium is low, and the overall thermal conductivity factor of beds is little; The thermal capacitance of reaction medium is less, and temperature easily fluctuates.In sum, DMO hydrogenation reaction requires harsh to moving thermal process, needs the heat-obtaining element adopting heat exchange efficiency high in reactor.The conversion ratio of current DMO hydrogenation process dimethyl oxalate in preparation has reached about 99%, and glycol selectivity reaches 94-97%, if can precise control of temperature, make glycol selectivity improve 0.5% or more, benefit can be further enhanced.
Existing shell-and-tube DMO hydrogenation reactor has following problem: the heat transfer coefficient of tubulation is not high, and need more heat exchange area, reactor volume is larger; Catalyst packing is in tubulation, and in a usual reactor, tubulation quantity has thousands of or up to ten thousand, and catalyst loading and unloading workload is large, and leak detection maintenance waits comparatively complicated; When improving single device output, shell and tube reactor often faces that pressure drop is large, hot(test)-spot temperature is high and the problem such as volume is excessive.
Chinese patent ZL 201210407137.X discloses a kind of industrial tray reactor for hydrogenation of oxalate for preparing ethylene glycol, described reactor is radial reactor, the heat-exchanger rig of described reactor is prefabricated heat exchanger plates in groups and cold pipe, can overcome that tubular reactor loaded catalyst is little, pressure drop large, large-scale production needs the shortcomings such as number of units is many.But this reactor has the following disadvantages: reactor is for radial, inside arranges isocon and header, and heat-exchanging component is heat exchanger plates and cold pipe, when these structures all will cause loading same volume of catalyst, compared with common shell and tube reactor, this reactor volume is larger; Heat exchanger plates in this reactor and the side of catalyst exposure are parallel-plate fin structure, plate wing spacing is 0.1 ~ 0.5mm, and in the document, describe that catalyst particle size is 3.2 ~ 5.5 × 3.2 ~ 5.5mm, obvious catalyst can not be seated between plate wing, and reacting gas easily passes through between plate wing, cause reacting gas short circuit, the total thermal resistance of plate and plate wing improves, and heat-transfer effect declines, the thermal accumlation of beds, reaction conversion ratio declines, and catalyst life shortens; This reactor cold pipe shape of cross section is triangle, trapezoidal, square, rhombus or parallelogram, other components are not had in cold pipe, if will bear the design pressure of about 40 kilograms in oxalate hydrogenation under, the wall of this cold pipe can be very thick, device fabrication cost increase; Equipment structure is more, and leak detection maintenance work is complicated, and catalyst loading and unloading is inconvenient.
Summary of the invention
Object of the present invention be exactly provide that a kind of structural adjustment is flexible, heat exchange efficiency is high to overcome defect that above-mentioned prior art exists, selective height, Catalyst packing be easily for the synthesis of the novel hydrogenation reactor of gas preparing ethylene glycol technique.
Object of the present invention can be achieved through the following technical solutions: a kind of novel hydrogenation reactor for the synthesis of gas preparing ethylene glycol technique, it is characterized in that, this reactor comprises shell of reactor, heat exchanger plates halved tie, cooling medium distribution header and arm, cooling medium and collects house steward and arm; Cooling medium entrance is provided with bottom described shell of reactor, top is provided with cooling medium outlet, the cooling medium entrance of cooling medium distribution header and arm coupled reaction device shell is passed through in described heat exchanger plates halved tie one end, and the other end collects the cooling medium outlet of house steward and arm coupled reaction device shell by cooling medium.Described heat exchanger plates halved tie by multiple heat exchanger plates to forming, each heat exchanger plates is internally plate journey, adjacent heat exchanger plates between loading catalyst, for shell side, shell side is walked after dimethyl oxalate and hydrogen feed gas enter reactor, and through catalyst reaction generating glycol, cooling fluid limp journey, takes away reaction liberated heat.
Described heat exchanger plates halved tie by multiple heat exchanger plates to forming, adjacent heat exchanger plates between loading catalyst, the parameter adjustable plates such as the thermal capacitance according to exothermic heat of reaction amount, heat transfer coefficient, reaction mass and catalyst and the requirement to temperature fluctuation between spacing.
Described heat exchanger plates forms an airtight plate journey cavity to by two metal sheets by welding, only respectively stay a port at two ends, each heat exchanger plates is connected to cooling medium distribution header to bottom port by cooling medium dispensing branch, and top port is collected arm by cooling medium and is connected to cooling medium collection house steward; Adjacent heat exchanger plates between be shell side, reacting gas flows through shell side from top to down, and is reacted by catalyst, cooling medium bottom-up through plate journey cavity flowing, carry out heat exchange.
Two metal sheet centres that composition heat exchanger plates is right are evenly provided with multiple contact, and multiple contact is crisscross arranged, and contact density is 200 ~ 5000 Ge/㎡, and contact spacing is 20 ~ 100mm.Preferred contact density is 1700 ~ 2200 Ge/㎡, and contact spacing is 20 ~ 25mm
Multipair heat exchanger plates, to be arrangeding in parallel, arranges support member bottom it, and top is provided with the heat exchanger plates distance pieces controlling spacing between each heat exchanger plates pair, and plate is 10 ~ 200mm to spacing.Preferred plate is 20 ~ 80mm to spacing.
Described support member is be arranged on the strip draw-in groove a of multipair heat exchanger plates to bottom, and this draw-in groove is provided with multiple bayonet socket;
Described heat exchanger plates distance pieces is be arranged on the strip draw-in groove b of multipair heat exchanger plates to top, and this draw-in groove is provided with multiple bayonet socket;
Each heat exchanger plates inserts in support member bayonet socket to bottom, and top is inserted in corresponding distance pieces bayonet socket, by adjustment heat exchanger plates to the position at bayonet socket, regulates the spacing that heat exchanger plates is right.
Described catalyst is the catalyst that Hydrogenation of Dimethyl Oxalate reaction uses, and comprises CuO-SiO
2system, type of feed is even closely knit filling.Because the spacing between adjacent heat exchanger plates in reactor of the present invention pair is adjustable, therefore, the catalyst that DMO hydrogenation adopts, no matter the size of grain diameter is how many, can load equably.
Connecting pipe between described cooling medium collection house steward and the cooling medium of shell of reactor export is provided with expansion joint, in order to the thermal stress of absorption heat-exchange plate halved tie.
Described shell of reactor comprises cylindrical shell, upper cover, manhole, low head, reacting gas inlet, product gas outlet, cooling medium entrance, cooling medium outlet and catalyst discharge port.
Described heat exchanger plates halved tie lifts into reactor shell from upper cover, is fixed by supports support, and reactor can Assembling; Catalyst directly loads between reactor upper cover or manhole one by one heat exchanger plates pair, draws off from low head discharge port; Cooling medium is the saturation water close to reaction temperature, is steam water interface when going out reactor.
In novel hydrogenation reactor of the present invention, Catalyst packing heat exchanger plates pair and heat exchanger plates between, i.e. reactor shell side, unstripped gas enters reactor shell side from reacting gas inlet, laminar flow is by beds vertically, and product gas flows out from reactor other end product gas outlet; Cooling medium enters in plate from reactor bottom by distribution header and dispensing branch, discharges reactor, two kind fluid countercurrent current heat exchange after being gathered by collection arm and house steward.
Heat exchanger plates is staggered to upper some contacts, makes the violent turbulence of cooling medium internal fluid, accelerates the heat transmission of internal fluid, makes cooling medium internal temperature gradient almost nil; Due to the repeatedly disturbance continuously of contact, cooling medium fluid is in turbulence state always, and fluid does not have boundary layer, and the exchange heat of fluid and plate is in forced-convection heat transfer state always; Due to the rough surface that plate is right, when cooling medium undergoes phase transition, the small bubble of generation not easily pools air pocket, and more can not be polymerized to large air film on plate surface, heat transfer form can ensure boiling heat transfer, and heat transfer coefficient is high.
Due to the efficient heat transfer efficiency in cooling medium side, and the heat transfer coefficient of catalyst side is little many, the temperature of the temperature making wooden partition face closely cooling medium, can provide the maximum temperature difference of reaction side with cold side, and the heat of reaction medium that is farthest cooled is taken away.
Reaction side gas, near heat exchange element wall place, often forms air film, and the thermal resistance that this air film produces accounting in the entire thermal resistance of reaction side is heavy very large.And at this new type of plate effects on surface, because its shape is uneven, the positive perturbation action to gas film behavior, is made air film renewal speed accelerate, thus reduce its thermal resistance, improve the heat transfer coefficient of reaction side entirety.
Compared with prior art, the present invention has the following advantages:
One, heat exchange efficiency is high, and the conversion ratio of DMO hydrogenation is high and selective good.The contact that new type of plate is right and the rough surface peening disturbance of two side liquids, enhance heat exchange efficiency, reaction heat is removed in time, can reduce hot(test)-spot temperature, and simultaneous reactions temperature distributes gently, closer to isothermal reaction, thus reduce the generation of side reaction, improve selective, reduce the consumption of raw materials of unit product, increase the benefit, also make product property reliable and stable.Simultaneously plate between spacing adjustability strong, can according to the requirement of thermal discharge and variations in temperature, the spacing that adjustable plate is right, meets reaction requirement.
Two, same loaded catalyst, the volume of this novel hydrogenation reactor is relatively little.At same loaded catalyst, height for reactor is identical, plate is when to spacing and caliber, catalyst thickness is identical at once mutually, and ensure enough heat exchange areas, the diameter of this novel reactor is approximately about 70% of shell-and-tube reactor diameter, volume is about about 40% of shell-and-tube reactor, reactor volume reduces greatly, and reactor has expansion space, can load more multi-catalyst, be conducive to improving separate unit reactor output, be conducive to equipment enlarging.
Three, Catalyst packing is easy.Catalyst packing at this novel reactor shell side, plate pair and plate between, plate between contactless, plate is to quantity usually tens or hundreds of, and far fewer than tubulation quantity, filling workload is little.
Four, be easy to install, transport and maintenance.As a whole, can directly lift into reactor, plate have tube sheet to both sides to plate-type heat-exchange assembly, and reactor can Assembling, and reduce cost of transportation, plate is few to quantity, and inspection and maintenance work is simple.
Accompanying drawing explanation
Fig. 1 is the structural representation of a kind of novel hydrogenation reactor for the synthesis of gas preparing ethylene glycol technique of the present invention;
Fig. 2 is heat exchanger plates halved tie structure top view of the present invention.
In Fig. 1 shown in label:
1, reacting gas inlet, 2, cooling medium outlet, 3, cooling medium collects house steward, and 4, cooling medium collects arm, 5, shell of reactor, 6, heat exchanger plates halved tie, 7, catalyst discharge port, 8, product gas outlet, 9, cooling medium entrance, 10, cooling medium distribution header, 11, cooling medium dispensing branch.
In Fig. 2 shown in label:
12, distance pieces draw-in groove, 13, support member draw-in groove.
Detailed description of the invention
Below in conjunction with the drawings and specific embodiments, the present invention is described in detail.
Embodiment 1
As shown in Figure 1, for the synthesis of a novel hydrogenation reactor for gas preparing ethylene glycol technique, this reactor comprises shell of reactor 5, heat exchanger plates halved tie 6, cooling medium distribution header 10, cooling medium dispensing branch 11, cooling medium collects house steward 3 and cooling medium collects arm 4; Described shell of reactor 5 comprises cylindrical shell, upper cover, manhole, low head, reacting gas inlet 1, product gas outlet 8, cooling medium entrance 9, cooling medium outlet 2 and catalyst discharge port 7.
As shown in Figure 2, cooling medium entrance 9 is provided with bottom described shell of reactor 5, top is provided with cooling medium outlet 2, described heat exchanger plates halved tie 6 by multiple heat exchanger plates to parallel and equidistantly rearrange, adjacent heat exchanger plates between loading catalyst, the parameter adjustable plates such as the thermal capacitance according to exothermic heat of reaction amount, heat transfer coefficient, reaction mass and catalyst and the requirement to temperature fluctuation between spacing.
Described heat exchanger plates forms an airtight plate journey cavity to by two metal sheets by welding, only respectively stay a port at two ends, each heat exchanger plates is connected to cooling medium distribution header 10 to bottom port by cooling medium dispensing branch 11, and top port is collected arm 4 by cooling medium and is connected to cooling medium collection house steward 3; Adjacent heat exchanger plates between be shell side, reacting gas flows through shell side from top to down, and is reacted by catalyst, cooling medium bottom-up through plate journey cavity flowing, cool.Two metal sheet centres that composition heat exchanger plates is right are evenly provided with multiple contact, and multiple contact is crisscross arranged, and contact density is 200 ~ 5000 Ge/㎡, and contact spacing is 20 ~ 100mm.Contact density is 1700 ~ 2200 Ge/㎡ in the present embodiment, and contact spacing is 20 ~ 25mm
Multipair heat exchanger plates, to be arrangeding in parallel, arranges support member bottom it, and top is provided with the heat exchanger plates distance pieces controlling spacing between each heat exchanger plates pair, and plate is 10 ~ 200mm to spacing.Plate is 20 ~ 80mm to spacing in the present embodiment.
Multipair heat exchanger plates, to be arrangeding in parallel, is arranged on bottom it on support member, and top is provided with the heat exchanger plates distance pieces controlling spacing between each heat exchanger plates pair.Described support member is be arranged on the strip draw-in groove b13 of multipair heat exchanger plates to bottom, and this draw-in groove is provided with multiple bayonet socket; Described heat exchanger plates distance pieces is be arranged on the strip draw-in groove a12 of multipair heat exchanger plates to top, and this draw-in groove a12 is provided with individual bayonet socket; Each heat exchanger plates inserts in support member bayonet socket to bottom, and top is inserted in corresponding distance pieces bayonet socket, by adjustment heat exchanger plates to the position at bayonet socket, regulates the spacing that heat exchanger plates is right.
Described catalyst is CuO-SiO
2system, type of feed is: even closely knit filling.
Connecting pipe between described cooling medium collection house steward and the cooling medium of shell of reactor export is provided with expansion joint, in order to the thermal stress of absorption heat-exchange plate halved tie.
Described heat exchanger plates halved tie lifts into reactor shell from upper cover, is fixed by supports support; Catalyst directly loads between reactor upper cover or manhole one by one heat exchanger plates pair, draws off from low head discharge port; Cooling medium is the saturation water close to reaction temperature, is steam water interface when going out reactor.
In novel hydrogenation reactor of the present invention, Catalyst packing heat exchanger plates pair and heat exchanger plates between, i.e. reactor shell side, unstripped gas enters reactor shell side from reacting gas inlet, laminar flow is by beds vertically, and product gas flows out from reactor other end product gas outlet; Cooling medium enters in plate from reactor bottom by distribution header and dispensing branch, discharges reactor, two kind fluid countercurrent current heat exchange after being gathered by collection arm and house steward.
By above-mentioned reactor for the synthesis of gas preparing ethylene glycol technique, separate unit reactor diameter 3.8m, filling CuO-SiO
2series catalysts 60m
3, its treating capacity can reach annual output 100000 tons of ethylene glycol production capacity, in the operating condition: reaction pressure 2.8Mpa, reaction temperature 195 DEG C, even in the filling of the catalyst in reactor of the present embodiment, pressure field distribution is even, pressure drop is less than 50KPa, and under the effect that the heat exchanger plates of the present embodiment is right, can by Axial response temperature stabilization at about 195 DEG C, and radial temperature difference is little, substantially, this DMO hydrogenation reactor can be considered isothermal reactor, dimethyl oxalate conversion ratio>=99.99%, glycol selectivity 98.5%, meet technological requirement, and remarkable benefit.
Claims (10)
1. for the synthesis of a novel hydrogenation reactor for gas preparing ethylene glycol technique, it is characterized in that, this reactor comprises shell of reactor, heat exchanger plates halved tie, cooling medium distribution header and arm, cooling medium and collects house steward and arm; Cooling medium entrance is provided with bottom described shell of reactor, top is provided with cooling medium outlet, the cooling medium entrance of cooling medium distribution header and arm coupled reaction device shell is passed through in described heat exchanger plates halved tie one end, and the other end collects the cooling medium outlet of house steward and arm coupled reaction device shell by cooling medium; Described heat exchanger plates halved tie by multiple heat exchanger plates to forming, each heat exchanger plates is internally plate journey, adjacent heat exchanger plates between loading catalyst, for shell side, shell side is walked after the unstripped gas that dimethyl oxalate and hydrogen form enters reactor, and through catalyst reaction generating glycol, cooling fluid limp journey, takes away reaction liberated heat.
2. a kind of novel hydrogenation reactor for the synthesis of gas preparing ethylene glycol technique according to claim 1, it is characterized in that, described heat exchanger plates forms an airtight plate journey cavity to by two metal sheets by welding, only respectively stay a port at two ends, each heat exchanger plates is connected to cooling medium distribution header to bottom port by cooling medium dispensing branch, and top port is collected arm by cooling medium and is connected to cooling medium collection house steward; Adjacent heat exchanger plates between be shell side, reacting gas flows through shell side from top to down, and is reacted by catalyst, cooling medium from bottom to top through plate journey cavity flowing, cool.
3. a kind of novel hydrogenation reactor for the synthesis of gas preparing ethylene glycol technique according to claim 2, it is characterized in that, two metal sheet centres that composition heat exchanger plates is right are evenly provided with multiple contact, multiple contact is crisscross arranged, contact density is 200 ~ 5000 Ge/㎡, and contact spacing is 20 ~ 100mm.
4. a kind of novel hydrogenation reactor for the synthesis of gas preparing ethylene glycol technique according to claim 1, it is characterized in that, multipair heat exchanger plates is to be arrangeding in parallel, be arranged on bottom it on support member, top is provided with and controls each heat exchanger plates to the heat exchanger plates distance pieces of spacing, and heat exchanger plates is 10 ~ 200mm to spacing.
5. a kind of novel hydrogenation reactor for the synthesis of gas preparing ethylene glycol technique according to claim 4, is characterized in that, described support member is be arranged on the strip draw-in groove a of multipair heat exchanger plates to bottom, and this draw-in groove is provided with multiple bayonet socket;
Described heat exchanger plates distance pieces is be arranged on the strip draw-in groove b of multipair heat exchanger plates to top, and this draw-in groove is provided with individual bayonet socket;
Each heat exchanger plates inserts in support member bayonet socket to bottom, and top is inserted in corresponding distance pieces bayonet socket, by adjustment heat exchanger plates to the position at bayonet socket, regulates the spacing that heat exchanger plates is right.
6. a kind of novel hydrogenation reactor for the synthesis of gas preparing ethylene glycol technique according to claim 1, is characterized in that, described catalyst is the catalyst that DMO hydrogenation reaction uses, and comprises CuO-SiO
2system, type of feed is even closely knit filling.
7. a kind of novel hydrogenation reactor for the synthesis of gas preparing ethylene glycol technique according to claim 1, it is characterized in that, connecting pipe between described cooling medium collection house steward and the cooling medium of shell of reactor export is provided with expansion joint, in order to the thermal stress of absorption heat-exchange plate halved tie.
8. a kind of novel hydrogenation reactor for the synthesis of gas preparing ethylene glycol technique according to claim 1, it is characterized in that, described shell of reactor comprises cylindrical shell, upper cover, manhole, low head, reacting gas inlet, product gas outlet, cooling medium entrance, cooling medium outlet and catalyst discharge port.
9. a kind of novel hydrogenation reactor for the synthesis of gas preparing ethylene glycol technique according to claim 8, it is characterized in that, described heat exchanger plates halved tie lifts into reactor shell from upper cover, is fixed by supports support, and reactor can Assembling; Catalyst directly loads between reactor upper cover or manhole one by one heat exchanger plates pair, draws off from low head discharge port; Cooling medium is the saturation water close to reaction temperature, is steam water interface when going out reactor.
10. the application of novel reactor in Hydrogenation of Dimethyl Oxalate technique as described in as arbitrary in claim 1-9.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105032305A (en) * | 2015-08-27 | 2015-11-11 | 德艾柯工程技术（上海）有限公司 | Novel radial plate type reactor |
| CN105258536A (en) * | 2015-10-13 | 2016-01-20 | 德艾柯工程技术（上海）有限公司 | Novel all-welding plate shell type heat exchanger |
| CN105879790A (en) * | 2016-06-06 | 2016-08-24 | 江苏怡达化学股份有限公司 | Novel HPPO reactor |
| CN112044363A (en) * | 2020-08-31 | 2020-12-08 | 江苏永大化工机械有限公司 | Coupling reactor for producing ethylene glycol from coal |
| CN112479822A (en) * | 2020-11-30 | 2021-03-12 | 南京延长反应技术研究院有限公司 | Enhanced micro-interface reaction system and method for preparing ethylene glycol by oxalate method |
| CN114247386A (en) * | 2021-11-24 | 2022-03-29 | 中国五环工程有限公司 | Evaporative isothermal hydrogenation reaction method and evaporative isothermal reaction system |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105032305A (en) * | 2015-08-27 | 2015-11-11 | 德艾柯工程技术（上海）有限公司 | Novel radial plate type reactor |
| CN105258536A (en) * | 2015-10-13 | 2016-01-20 | 德艾柯工程技术（上海）有限公司 | Novel all-welding plate shell type heat exchanger |
| CN105879790A (en) * | 2016-06-06 | 2016-08-24 | 江苏怡达化学股份有限公司 | Novel HPPO reactor |
| CN112044363A (en) * | 2020-08-31 | 2020-12-08 | 江苏永大化工机械有限公司 | Coupling reactor for producing ethylene glycol from coal |
| CN112479822A (en) * | 2020-11-30 | 2021-03-12 | 南京延长反应技术研究院有限公司 | Enhanced micro-interface reaction system and method for preparing ethylene glycol by oxalate method |
| CN114247386A (en) * | 2021-11-24 | 2022-03-29 | 中国五环工程有限公司 | Evaporative isothermal hydrogenation reaction method and evaporative isothermal reaction system |
| CN114247386B (en) * | 2021-11-24 | 2023-10-13 | 中国五环工程有限公司 | Evaporation type isothermal hydrogenation reaction method and evaporation type isothermal reaction system |
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