CN216538373U - Final stage water transfer heat bed layer ammonia synthesis reactor - Google Patents
Final stage water transfer heat bed layer ammonia synthesis reactor Download PDFInfo
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- CN216538373U CN216538373U CN202123199126.0U CN202123199126U CN216538373U CN 216538373 U CN216538373 U CN 216538373U CN 202123199126 U CN202123199126 U CN 202123199126U CN 216538373 U CN216538373 U CN 216538373U
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Abstract
The utility model discloses a final-stage water-transfer heat bed ammonia synthesis reactor, which comprises an ammonia reactor, a steam drum, a boiler water-supply heater and a hot water pump, wherein the ammonia reactor is provided with an ammonia reactor outer cylinder, ammonia reactor internals are arranged in the ammonia reactor outer cylinder, the ammonia reactor internals comprise a primary heat-insulation catalyst bed layer, a primary interlayer heat exchanger, a secondary heat-insulation catalyst bed layer, a secondary interlayer heat exchanger and a final-stage catalyst bed layer which are sequentially connected from top to bottom, a water-transfer heat exchanger is arranged in the final-stage catalyst bed layer, a boiler water-supply pipe is communicated with the boiler water-supply heater, and the boiler water-supply heater is communicated with the steam drum through a steam drum water-supply pipe; the reaction heat of the final catalyst bed layer is timely removed through the water in the water heat transfer tube bundle embedded in the catalyst bed layer, and the by-product of 12.0MPa saturated steam is generated, so that the reaction heat of the catalyst bed layer is ensured not to be accumulated, the temperature of the catalyst bed layer is always controlled to be 340 ℃, the temperature is far away from a balance curve, and the ammonia content at the outlet of the bed layer is 41.53 percent.
Description
Technical Field
The utility model relates to the technical field of chemical equipment, in particular to a final-stage water-transfer thermal bed ammonia synthesis reactor.
Background
At present, large-scale low-pressure (15.0MPa) ammonia synthesis reactors existing in domestic and foreign ammonia synthesis technology suppliers are all three-stage heat-insulating catalyst beds, interlayer gas-gas heat exchangers are adopted between the two-stage heat-insulating beds and between the two-stage heat-insulating beds to remove heat at an outlet of a heat-insulating section, the temperature of gas at the inlet of the next-stage heat-insulating catalyst bed is ensured to be less than or equal to 380 ℃, high-temperature synthesis gas at the outlet of the three-stage heat-insulating catalyst bed directly enters a direct-connected waste heat boiler, and 3.8MPa saturated steam is a byproduct.
Under the best operation parameters, the ammonia net value of the existing ammonia synthesis reactor is only 20.7 percent, the main task of completing the ammonia synthesis reaction is a first-stage adiabatic catalyst bed layer and a second-stage adiabatic catalyst bed layer, the net value of three-stage (final-stage) ammonia is only 3.53 percent, the catalyst loading accounts for more than 50 percent of the total loading, and only 3.53/20.07 of the synthetic ammonia yield is completed to 17.59 percent. The three-stage (final stage) has low synthetic ammonia yield mainly because the three-stage (final stage) is an adiabatic catalyst bed, the reaction 'equilibrium temperature span' at 426 ℃ of the outlet is 10 ℃, and the ammonia synthesis reaction equilibrium temperature span is too small, so that the synthesis rate of ammonia is inhibited.
The existing synthetic ammonia reactor adopts a direct connection mode of a waste heat boiler and gas at an outlet of a three-stage bed layer of the synthetic ammonia reactor, and the structure corresponding to an adiabatic catalyst bed layer can not ensure that a catalyst bed layer, particularly a final catalyst bed layer, carries out synthetic ammonia reaction under an isothermal condition.
In view of the drawbacks, the inventors have finally obtained the present invention through long-term research and practice.
SUMMERY OF THE UTILITY MODEL
In order to solve the technical defects, the utility model adopts the technical scheme that a final-stage water-transfer heat bed ammonia synthesis reactor is provided, which comprises an ammonia reactor, a steam drum, a boiler water-supply heater and a hot water pump, wherein the ammonia reactor is provided with an ammonia reactor outer cylinder, ammonia reactor internals are arranged in the ammonia reactor outer cylinder, the ammonia reactor internals comprise a first-stage heat-insulation catalyst bed layer, a first-stage interlayer heat exchanger, a second-stage heat-insulation catalyst bed layer, a second-stage interlayer heat exchanger and a final-stage catalyst bed layer which are sequentially connected from top to bottom, a water-transfer heat exchanger is arranged in the final-stage catalyst bed layer, a boiler water-supply pipe is communicated with the boiler water-supply heater, the boiler water-supply heater is communicated with the steam drum through a steam drum water-supply pipe, the steam drum is communicated with the hot water pump through a steam drum descending pipe, and the hot water pump is communicated with the water-transfer heat exchanger through a heat exchanger water inlet pipe, the water heat transfer heat exchanger is communicated with the steam drum through a heat exchanger water outlet pipe.
Preferably, the steam drum is further provided with a steam pipe for controlling the internal pressure of the steam drum.
Preferably, the outer cylinder of the ammonia reactor comprises an outer cylinder flat cover, an outer cylinder barrel and an outer cylinder lower end socket, the ammonia reactor internal part is arranged in the outer cylinder barrel, the upper end of the outer cylinder barrel is provided with the detachable outer cylinder flat cover, and the lower end of the outer cylinder barrel is provided with the outer cylinder lower end socket.
Preferably, an internal part cylinder is arranged in the outer cylinder of the ammonia reactor, the primary heat insulation catalyst bed layer, the primary interlayer heat exchanger, the secondary heat insulation catalyst bed layer, the secondary interlayer heat exchanger and the final catalyst bed layer are all arranged in the internal part cylinder, a detachable internal part flat cover is arranged at the upper end of the internal part cylinder, and an internal part lower end socket is arranged at the lower end of the internal part cylinder.
Preferably, the first air inlet pipe is communicated with the upper end of the first-stage heat-insulating catalyst bed layer through the first-stage interlayer heat exchanger, and cold air in the first air inlet pipe exchanges heat with reaction gas after the reaction of the first-stage interlayer heat exchanger and the first-stage heat-insulating catalyst bed layer.
Preferably, the second air inlet pipe is communicated with the upper end of the first-stage heat-insulating catalyst bed layer through the second-stage interlayer heat exchanger, and cold air in the second air inlet pipe exchanges heat with reaction gas after the reaction of the second-stage interlayer heat exchanger and the second-stage heat-insulating catalyst bed layer.
Preferably, the secondary line pipe is communicated with the upper end of the first-stage heat insulation catalyst bed layer, and cold air is introduced into the secondary line pipe.
Preferably, the first air inlet pipe is provided with a preliminary heat exchange section, and the preliminary heat exchange section is arranged between the ammonia reactor outer barrel and the ammonia reactor internal part and extends from the internal part lower end socket to the internal part flat cover.
Preferably, the last catalyst bed layer is communicated with the boiler water supply heater through an air outlet pipe, and gas after reaction in the last catalyst bed layer exchanges heat with heat exchange liquid entering from the boiler water supply pipe through the boiler water supply heater.
Preferably, the first-stage adiabatic catalyst bed layer, the second-stage adiabatic catalyst bed layer and the last-stage catalyst bed layer are all filled with catalysts, and the catalysts are iron-based catalysts, ruthenium-based catalysts or cobalt-based catalysts for ammonia synthesis.
Preferably, the heat exchange medium circulating in the water heat transfer heat exchanger and the steam drum is a liquid cold medium which absorbs heat and then is converted from a liquid phase to a gas phase.
Compared with the prior art, the utility model has the beneficial effects that: 1, the reaction heat of the final catalyst bed of the utility model is timely removed through the water in the water heat-transfer tube bundle embedded in the catalyst bed, and the byproduct of 12.0MPa saturated steam is generated, so that the reaction heat of the catalyst bed is ensured not to be aggregated and accumulated, the temperature of the catalyst bed is always controlled to be 340 ℃ below zero, the temperature is far away from a balance curve, the ammonia content at the outlet of the bed is 41.53 percent, and the circulating gas entering a tower is reduced to 4698.82Nm3/tNH3The power consumption of the compression and circulation machine (only the low-pressure section and the high-pressure section of the press plus the circulation section) is reduced to 165.02KWh/tNH3The cold consumption is reduced to 73262.6Kcal/tNH3The byproduct of 12MPa steam is 1689.2kg/tNH3(ii) a 2, the utility model selects two-stage heat insulation before the final stage water-shift heat catalyst bed layerThe catalyst bed layer can effectively protect the noble metal catalyst of the final-stage water-transfer thermal catalyst bed layer, and effectively prolong the long-period operation of the whole reactor; 3, the two-stage adiabatic catalyst bed layer is selected before the final stage water-shift thermal catalyst bed layer, so that the heat balance of the reactor and the ammonia synthesis system can be maintained, and the system fluctuation is effectively reduced; 4, the reaction heat of the final-stage catalyst bed is timely removed through water in a water heat-removing tube bundle embedded in the catalyst bed, the temperature of the outlet of the bed is always controlled to be 340 ℃, a gas pipeline at the outlet of the ammonia synthesis reactor is directly connected with a boiler feed water heater to recover the waste heat of the synthesis gas, a direct-connected waste heat boiler is avoided, equipment leakage is avoided, and the operation safety of the device is effectively improved.
Drawings
FIG. 1 is a structural view of the final stage water-shift thermal bed ammonia synthesis reactor.
The figures in the drawings represent:
1-outer cylinder flat cover; 2-inner piece flat cover; 3-outer cylinder body; 4-first-stage adiabatic catalyst bed layer; 5-a primary interlayer heat exchanger; 6-internal cartridge; 7-a secondary adiabatic catalyst bed; 8-a secondary interlayer heat exchanger; 9-final catalyst bed layer; 10-water heat transfer heat exchanger; 11-internal piece lower end enclosure; 12-lower end enclosure of the outer cylinder; 13-an ammonia reactor outer barrel; 14-ammonia reactor internals; 15-an ammonia reactor; 16-steam drum; 17-boiler feed water heater; 18-a hot water pump; 19-a first inlet line; 20-a second air inlet pipe; 21-secondary line pipe; 22-an air outlet pipe; 23-boiler feed pipe; 24-steam drum water replenishing pipe; 25-drum downcomer; 26-heat exchanger water inlet pipe; 27-a heat exchanger water outlet pipe; 28-steam tube.
Detailed Description
The described and additional features and advantages of the present invention are described in more detail below with reference to the accompanying drawings.
As shown in FIG. 1, FIG. 1 is a structural view of the final stage water-moving hot bed ammonia synthesis reactor. The final stage water-transfer heat bed ammonia synthesis reactor comprises an ammonia reactor 15, a steam drum 16, a boiler water-feeding heater 17 and a hot water pump 18, wherein the ammonia reactor 15 is provided with an ammonia reactor outer cylinder 13, ammonia reactor internal parts 14 are arranged in the ammonia reactor outer cylinder 13, the ammonia reactor internal parts 14 comprise a primary heat-insulating catalyst bed layer 4, a primary interlayer heat exchanger 5, a secondary heat-insulating catalyst bed layer 7, a secondary interlayer heat exchanger 8 and a final catalyst bed layer 9 which are sequentially connected from top to bottom, a water-transfer heat exchanger 10 is arranged in the final catalyst bed layer 9, a boiler water-feeding pipe 23 is communicated with the boiler water-feeding heater 17, the boiler water-feeding heater 17 is communicated with the steam drum 16 through a steam drum water-supplementing pipe 24, the steam drum 16 is communicated with the hot water pump 18 through a steam drum descending pipe 25, the pump 18 is communicated with the water-transfer heat exchanger 10 through a heat exchanger water inlet pipe 26, the water heat transfer heat exchanger 10 is communicated with the steam drum 16 through a heat exchanger water outlet pipe 27.
The closed cycle of the final-stage bed layer heat transfer water is that the water of a boiler water supply heater recovers the waste heat of the synthesis gas, the water is supplemented into a steam drum through a steam drum water supplementing pipe, the water enters a hot water pump through a steam drum descending pipe to be pressurized, the pressurized water enters a water heat transfer heat exchanger embedded in the final-stage catalyst bed layer, the reaction heat of the final-stage catalyst bed layer is removed through the heat exchange of the water heat transfer heat exchanger, the reaction heat enters the steam drum through a water outlet pipe of the heat exchanger, steam is flashed out of the steam drum, and the reaction heat of the final-stage catalyst bed layer is removed out of the catalyst bed layer in a byproduct steam mode.
Preferably, a steam pipe 28 for controlling the pressure inside the steam drum 16 is further provided on the steam drum 16.
Preferably, the ammonia reactor outer cylinder 13 comprises an outer cylinder flat cover 1, an outer cylinder 3 and an outer cylinder lower end enclosure 12, the ammonia reactor internal part 14 is arranged in the outer cylinder 3, and the upper end of the outer cylinder 3 is provided with the detachable outer cylinder flat cover 1 for realizing the detection and maintenance of the inside of the outer cylinder 3. The lower end of the outer cylinder barrel 3 is provided with the outer cylinder lower end enclosure 12.
An internal part cylinder 6 is arranged in the outer cylinder 3, the primary heat-insulating catalyst bed layer 4, the primary interlayer heat exchanger 5, the secondary heat-insulating catalyst bed layer 7, the secondary interlayer heat exchanger 8, the final catalyst bed layer 9 and the water heat transfer heat exchanger 10 are all arranged in the internal part cylinder 6, and a detachable internal part flat cover 2 is arranged at the upper end of the internal part cylinder 6 and used for realizing detection and maintenance of the interior of the internal part cylinder 6. The lower end of the internal part cylinder 6 is provided with an internal part lower end socket 11.
Preferably, the first air inlet pipe 19 is communicated with the upper end of the first-stage heat-insulating catalyst bed layer 4 through the first-stage interlayer heat exchanger 5, the second air inlet pipe 20 is communicated with the upper end of the first-stage heat-insulating catalyst bed layer 4 through the second-stage interlayer heat exchanger 8, and the secondary pipe 21 is communicated with the upper end of the first-stage heat-insulating catalyst bed layer 4.
Preferably, the first air inlet pipe 19 is provided with a preliminary heat exchange section, and the preliminary heat exchange section is arranged between the ammonia reactor outer cylinder 13 and the ammonia reactor internal parts 14 and is extended from the internal part lower end socket 11 to the internal part flat cover 2, so as to facilitate auxiliary heat dissipation of the primary adiabatic catalyst bed layer 4, the secondary adiabatic catalyst bed layer 7, and the final catalyst bed layer 9.
Specifically, cold air in the first air inlet pipe 19 enters the primary interlayer heat exchanger 5, and the reaction heat of the primary heat insulation catalyst bed layer 4 is removed; cold air in the second air inlet pipe 20 enters the secondary interlayer heat exchanger 8, and the reaction heat of the secondary heat insulation catalyst bed layer 7 is removed; the first air inlet pipe 19, the second air inlet pipe 20 and the secondary pipe 21 collect three gas streams respectively at the top end of the first-stage heat insulation catalyst bed layer 4, so that heat dissipation of gas to be treated before entering the first-stage heat insulation catalyst bed layer 4 is achieved.
The last catalyst bed layer 9 is communicated with the boiler feed water heater 17 through an air outlet pipe 22, and gas after reaction in the last catalyst bed layer 9 exchanges heat with heat exchange liquid entering from the boiler feed water pipe 23 through the boiler feed water heater 17.
Specifically, the outer cylinder flat cover 1, the outer cylinder barrel 3 and the outer cylinder lower end enclosure 12 form a pressure-resistant outer cylinder which can be filled with ammonia reactor internals.
The ammonia synthesis reactor internal part with three-stage catalyst bed layers is composed of the internal part flat cover 2, the first-stage heat insulation catalyst bed layer 4, the first-stage interlayer heat exchanger 5, the internal part barrel 6, the second-stage heat insulation catalyst bed layer 7, the second-stage interlayer heat exchanger 8, the last-stage catalyst bed layer 9, the water heat transfer heat exchanger 10, the internal part lower end cover 11, the first air inlet pipe 19, the second air inlet pipe 20, the secondary pipe 21, the air outlet pipe 22, the boiler water supply pipe 23, the heat exchanger water inlet pipe 26 and the heat exchanger water outlet pipe 27.
The final catalyst bed layer 9, the water heat transfer heat exchanger 10, the steam drum 16, the boiler water supply heater 17, the hot water pump 18, the boiler water supply pipe 23, the steam drum water supply pipe 24, the steam drum descending pipe 25, the heat exchanger water inlet pipe 26, the heat exchanger water outlet pipe 27, the steam pipe 28 and the like jointly form an ammonia synthesis reaction catalyst bed layer with the water heat transfer at the final stage.
The heat-insulating bed layer of the ammonia synthesis reactor can be a zero section or a plurality of sections, and the heat-insulating bed layer of the ammonia synthesis reactor and the final-stage water-transfer thermal catalyst bed layer can be of axial, radial and axial-radial structures.
The catalyst can be iron catalyst, ruthenium catalyst, cobalt catalyst and other catalysts for ammonia synthesis;
the catalyst is respectively filled in the first-stage heat-insulating catalyst bed layer, the second-stage heat-insulating catalyst bed layer and the final-stage water heat-transfer catalyst bed layer.
The catalyst filled in the final catalyst bed layer can be selected from a catalyst with good low-temperature activity, and can also be selected from a wide-temperature-zone catalyst which can resist high temperature with the first-stage heat-insulating catalyst bed layer and the second-stage heat-insulating catalyst bed layer.
The heat exchange medium in the water heat transfer heat exchanger 10 may be one or a mixture of several liquid cold media that absorb heat and then convert from liquid phase to gas phase.
The ammonia synthesis reactor contains all organic and inorganic synthesis reactions.
Cold air in the first air inlet pipe enters a primary interlayer heat exchanger to remove reaction heat of a primary heat insulation catalyst bed layer; cold air in the second air inlet pipe enters a secondary interlayer heat exchanger, and the reaction heat of a secondary heat insulation catalyst bed layer is removed; the first air inlet pipe, the second air inlet pipe and the secondary line pipe are respectively collected to the top end of the first-stage heat-insulating catalyst bed layer; the inlet and outlet temperature of the first-stage adiabatic catalyst bed is controlled at 360 ℃/490 ℃, the inlet and outlet temperature of the second-stage adiabatic catalyst bed is controlled at 380 ℃/465 ℃, and the ammonia content of the outlet is 12.10 percent and 18.64 percent respectively.
The reaction heat of the final catalyst bed is timely removed through water in a water heat transfer tube bundle embedded in the catalyst bed, and 12.0MPa saturated steam is byproduct, so that the reaction heat of the catalyst bed is not accumulated, the temperature of the catalyst bed is always controlled at 340 ℃, the temperature is far away from a balance curve, the ammonia content at the outlet of the bed is 41.53 percent, and the steam byproduct amount is up to 1689.2kg/tNH3。
The heat of the last-stage bed layer can timely remove the reaction heat of the last-stage catalyst bed layer through a waterway closed-loop circulating system which is formed by a water heat transfer heat exchanger, a steam pocket, a boiler water supply heater, a hot water pump, a boiler water supply pipe, a steam pocket descending pipe, a heat exchanger water inlet pipe, a heat exchanger water outlet pipe, a steam pipe and the like.
In one embodiment:
the first-stage adiabatic catalyst bed layer is filled with Fe-Co catalyst with the filling diameter of 15.3m3；
The second-stage heat insulation catalyst bed layer is filled with iron-cobalt catalyst with the filling length of 24.0m3；
Ruthenium catalyst filling 37.5m is filled in the last stage water-transfer thermal catalyst bed layer3；
The specification of the ammonia synthesis reactor is
Primary interlayer heat exchanger
Two-stage interlayer heat exchanger
Water heat transfer heat exchanger
Steam pocket
Boiler water supply heater
Three hot water pumps with two opening and one standby specification of 1600m3/h
Yield of synthetic ammonia: 42.25t/h
Main operating parameter schedule
List of the most important economic indicators
| Parameter name | Electricity consumption | Cold energy consumption | By-product steam | Gas flow into the tower |
| Unit of | KWh/tNH3 | KCal/tNH3 | kg/tNH3 | Nm3/tNH3 |
| Economic index | 165.02 | 73262.60 | 1689.20 | 4698.82 |
The foregoing is merely a preferred embodiment of the utility model, which is intended to be illustrative and not limiting. It will be understood by those skilled in the art that various changes, modifications and equivalents may be made therein without departing from the spirit and scope of the utility model as defined in the appended claims.
Claims (10)
1. A final-stage water-shift thermal bed ammonia synthesis reactor is characterized by comprising an ammonia reactor, a steam drum, a boiler feed water heater and a hot water pump, the ammonia reactor is provided with an ammonia reactor outer cylinder, the ammonia reactor outer cylinder is internally provided with ammonia reactor internal parts, the ammonia reactor internal part comprises a primary heat insulation catalyst bed layer, a primary interlayer heat exchanger, a secondary heat insulation catalyst bed layer, a secondary interlayer heat exchanger and a final catalyst bed layer which are sequentially connected from top to bottom, a water heat transfer heat exchanger is arranged in the final catalyst bed layer, a boiler water supply pipe is communicated with the boiler water supply heater, the boiler water supply heater is communicated with the steam drum through a steam drum water supply pipe, the steam drum is communicated with the hot water pump through a steam drum descending pipe, the hot water pump is communicated with the water heat transfer heat exchanger through a heat exchanger water inlet pipe, and the water heat transfer heat exchanger is communicated with the steam drum through a heat exchanger water outlet pipe.
2. The final water-moving hot bed ammonia synthesis reactor according to claim 1, wherein the steam drum is further provided with steam pipes for controlling the pressure inside the steam drum.
3. The final water-shift thermal bed ammonia synthesis reactor according to claim 1, wherein the outer cylinder of the ammonia reactor comprises an outer cylinder flat cover, an outer cylinder barrel and an outer cylinder lower end socket, the ammonia reactor internal parts are arranged in the outer cylinder barrel, the outer cylinder flat cover is detachably arranged at the upper end of the outer cylinder barrel, and the outer cylinder lower end socket is arranged at the lower end of the outer cylinder barrel.
4. The final water-shift thermal bed ammonia synthesis reactor according to claim 3, wherein an internal barrel is arranged in the outer barrel of the ammonia reactor, the primary adiabatic catalyst bed, the primary interlayer heat exchanger, the secondary adiabatic catalyst bed, the secondary interlayer heat exchanger and the final catalyst bed are all arranged in the internal barrel, a detachable internal flat cover is arranged at the upper end of the internal barrel, and an internal lower end socket is arranged at the lower end of the internal barrel.
5. The final water-shift hot-bed ammonia synthesis reactor according to claim 4, wherein a first inlet pipe communicates with the upper end of the first adiabatic catalyst bed through the first interlayer heat exchanger, and the cold gas in the first inlet pipe exchanges heat with the reaction gas after the reaction between the first interlayer heat exchanger and the first adiabatic catalyst bed.
6. The final stage water-shift hot bed ammonia synthesis reactor according to claim 5, wherein a second inlet pipe communicates with the upper end of the first adiabatic catalyst bed through the second stage interlayer heat exchanger, and the cold gas in the second inlet pipe exchanges heat with the reaction gas after the reaction of the second stage interlayer heat exchanger with the second adiabatic catalyst bed.
7. The final water-shifted hot bed ammonia synthesis reactor according to claim 6, wherein a secondary conduit is in communication with the upper end of the primary adiabatic catalyst bed, the secondary conduit having a cold gas introduced therein.
8. The final water-moving hot-bed ammonia synthesis reactor according to claim 1, wherein the final catalyst bed is in communication with the boiler feed water heater through an outlet pipe, and reacted gas in the final catalyst bed exchanges heat with a heat exchange liquid entering from the boiler feed water heater through the boiler feed water heater.
9. The final water-moving hot-bed ammonia synthesis reactor according to claim 1, wherein the first adiabatic catalyst bed, the second adiabatic catalyst bed, and the final catalyst bed are filled with catalysts, and the catalysts are iron-based catalysts, ruthenium-based catalysts, or cobalt-based catalysts for ammonia synthesis.
10. The final water-moving hot-bed ammonia synthesis reactor according to claim 1, wherein the heat exchange medium circulating within the water-moving heat exchanger and the steam drum is a liquid cold medium that absorbs heat and converts from a liquid phase to a vapor phase.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114307869A (en) * | 2021-12-17 | 2022-04-12 | 南京敦先化工科技有限公司 | Ammonia synthesis reactor |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114307869A (en) * | 2021-12-17 | 2022-04-12 | 南京敦先化工科技有限公司 | Ammonia synthesis reactor |
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