CN208389981U - The radial methanol reactor of combined type heat exchange - Google Patents
The radial methanol reactor of combined type heat exchange Download PDFInfo
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- CN208389981U CN208389981U CN201820503992.3U CN201820503992U CN208389981U CN 208389981 U CN208389981 U CN 208389981U CN 201820503992 U CN201820503992 U CN 201820503992U CN 208389981 U CN208389981 U CN 208389981U
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Abstract
The utility model discloses a kind of radial methanol reactors of combined type heat exchange, are provided with internals inside the shell, form cloth air cavity between internals and shell；It is provided with getter cylinder in internals, forms reaction zone between getter cylinder and internals, tubulation is provided in reaction zone, catalyst is filled with around tubulation；Shell-and-tube heat exchanger is installed in getter cylinder, which has shell and the intracorporal heat exchanger tube of mounting shell, and heat exchanger extends along the axis direction of shell, and getter chamber is formed between the shell and getter cylinder of heat exchanger；The shell side of connection heat exchanger and the air inlet of getter chamber are provided in the upper end of heat exchanger；The shell side of connection heat exchanger and the gas outlet of syngas outlet pipe are provided in the lower end of heat exchanger.The reactor can reduce total equipment amount of commercial plant in the case where guaranteeing that reaction is normally carried out, and thus reduce equipment investment, and reduce technology controlling and process point and management difficulty.
Description
Technical field
The utility model is more particularly to a kind of radial methanol reactor of combined type heat exchange.
Technical background
Methanol-fueled CLC is a kind of with strongly exothermic chemical reaction, in order to improve reaction efficiency, is needed while reaction
Extra reaction heat is removed in time, although present methanol reactor is generally provided with heat exchanger, for moving reaction heat
It out, is at present usually that tubulation is installed in reactor, the loading catalyst around tubulation, cooling water will be passed through in tubulation to react
The torrid zone is walked, and the gas discharge reactor for completing reaction enters next procedure, since methanol-fueled CLC needs at a certain temperature
The more stable progress of ability, therefore the temperature for the reaction mixture gas body being discharged from reactor is still higher, needs further to drop
Wen Houcai can enter later process.Cooling for the reaction mixture gas body being discharged from reactor is being usually to be arranged at present
Special heat exchanger cools down to it, and cold source therein is cooling water or unstripped gas, no matter which kind of cold source is used, is required to set
Setting individual heat exchanger, which increase the investments of entire commercial plant, simultaneously because increasing for equipment, also increases technology controlling and process
Point and management cost and difficulty.
Utility model content
The purpose of the utility model is to overcome drawbacks described above, in the case where guaranteeing that reaction is normally carried out, reduce industry
Thus total equipment amount of device reduces equipment investment, and reduces technology controlling and process point and management difficulty.
For this purpose, the application first proposed a kind of radial methanol reactor of combined type heat exchange comprising shell, in shell
Lower end is provided with synthesis gas inlet pipe, syngas outlet pipe and refrigerant inlet pipe, and the upper end of shell is provided with refrigerant exit pipe；
It is provided with internals inside the shell, forms cloth air cavity between internals and shell；The axis direction along shell is provided in internals
The getter cylinder of extension, forms reaction zone between getter cylinder and internals, tubulation is provided in reaction zone, fill around tubulation
It is filled with catalyst；
Shell-and-tube heat exchanger is installed in getter cylinder, which has shell and the intracorporal heat exchanger tube of mounting shell, changes
Hot device extends along the axis direction of shell, and getter chamber is formed between the shell and getter cylinder of heat exchanger；
The upper end of heat exchanger is provided with air inlet, which is connected to the shell side and getter chamber of heat exchanger；It is exchanging heat
The lower end of device is provided with gas outlet, which is connected to the shell side and syngas outlet pipe of heat exchanger；
The upper end of the heat exchanger tube of heat exchanger is connected to cloth air cavity, the lower end connection synthesis gas inlet pipe of the heat exchanger tube；
The upper end of the tubulation is connected to refrigerant exit pipe, and the lower end of tubulation is connected to refrigerant inlet pipe；
The first through hole being provided between connection cloth air cavity reaction zone in internals is provided with connection reaction on getter cylinder
The second through-hole between area and getter chamber；
When the methanol reactor in use, unstripped gas enters the tube side of heat exchanger through synthesizing gas inlet pipe, enter back into
Cloth air cavity forms gaseous mixture radially into reaction is carried out in reaction zone through cloth air cavity, and gaseous mixture enters getter through getter cylinder
Chamber, then enter through air inlet the shell side of heat exchanger, through syngas outlet pipe stream after the unstripped gas heat exchange in heat exchanger tube and tube side
Out.Preferably, the upper end of the shell of heat exchanger is arranged in the air inlet.
In the methanol reactor, be provided with heat exchanger, the heat exchanger be used for will react after gaseous mixture and unstripped gas into
Row heat exchange, while reducing mixture temperature, can be improved the temperature of unstripped gas.It as needed, can be by the temperature of unstripped gas
Degree is promoted to slightly below its optimal reaction temperature, react the unstripped gas for entering reaction zone can at once, to greatest extent
When ground is shortened using low temperature feedstock gas, the lower problem of the reaction efficiency of the unstripped gas of reaction zone is initially entered, it can be effective
The combined coefficient of ground raising methanol.In addition relative to the currently used mode heated outside reactor to unstripped gas, subtract
A few heat exchange equipment, advantageously reduces the expenditure of construction of entire system for methanol synthesis, due to reducing heat exchange equipment, can subtract
Few corresponding administration fee and technology controlling and process point.
In addition, after setting heat exchanger, due to reducing the temperature of the gaseous mixture after reacting, gaseous mixture can be effectively reduced
Temperature improve the security performance of reactor to reduce the internal pressure of reactor.
Further, catalyst cover board is installed in the upper end of internals, supporter is installed in the lower end of internals；Catalyst cover board with
The first air cavity is formed between the top of shell, and the second air cavity is formed between supporter and the bottom of shell；The heat exchanger changes
Heat pipe is connected to the first air cavity after extending upward through catalyst cover board, and first air cavity is connected to cloth air cavity；The shell side of the heat exchanger connects
Logical second air cavity, syngas outlet pipe are connected to the second air cavity.
Above-mentioned design can make full use of the space of shell upper and lower ends, upper end and gas distribution without the heat exchanger tube in heat exchanger
Special connecting pipe is set between chamber, while special without being arranged between the shell side of heat exchanger and syngas outlet pipe
Connecting pipe can effectively simplify the structure of whole equipment, reduce the complexity of equipment.
Further, the lower end of the shell of heat exchanger is mounted on supporter, is equipped with bottom in the lower end of the shell of heat exchanger
Portion's tube sheet, is equipped with bottom bulkhead on the downside of the tube sheet of bottom, and the synthesis gas inlet pipe is connected to bottom bulkhead；In bottom tube sheet
The gas outlet is provided between shell；The lower end of the heat exchanger tube of heat exchanger is mounted on the tube sheet of bottom.Special bottom is set
After portion's tube sheet and bottom bulkhead, the size of component is advantageously reduced, improve machining accuracy and reduces difficulty of processing, to reduce equipment
Manufacturing cost.Special tube sheet, which is arranged, can make full use of existing standarized component, the use of nonstandard component be reduced, with advantageous
In the plant maintenance in later period.
Further, top tube sheet is installed on the top of the shell of heat exchanger, top tube sheet is mounted on catalyst cover board, changes
The upper end of the heat exchanger tube of hot device is mounted on the tube sheet of top.
Top tube sheet, which is arranged, can equally select the tube sheet of existing standard model, in favor of the plant maintenance in later period.
Further, the tubulation is at least divided into three groups, is provided with a upper perforated plate sub-assembly and one corresponding to every group of tubulation
Lower perforated plate sub-assembly；Each upper perforated plate sub-assembly includes a upper perforated plate and one is mounted on upper cover on upper perforated plate, and upper cover connects
Logical refrigerant exit pipe；Each lower perforated plate sub-assembly includes a lower perforated plate and one is mounted on lower head on lower perforated plate, and lower head connects
Logical refrigerant inlet pipe.
After packet layout, relative to the design using single tube plate, the size of upper perforated plate and lower perforated plate can be reduced, is reduced
The difficulty of processing of tube sheet, while can be reduced using the tube sheet of existing standard series simultaneously because reducing the size of tube sheet
The size of corresponding upper cover and lower head, advantageously reduces the occupied space of upper cover and lower head, it is possible thereby to reduce
The height of equipment reduces the weight of equipment, reduces device fabrication expense.
To solve the above problems, the application also provides a kind of methanol synthesizing process, the methanol synthesizing process is using above-mentioned
Methanol reactor is synthesized, and the process in the methanol synthesizing process includes
The tube side that unstripped gas is entered to heat exchanger through synthesizing gas inlet pipe, enters back into cloth air cavity, through cloth air cavity along diameter
Gaseous mixture is formed to entering in reaction zone react, gaseous mixture enters getter chamber through getter cylinder, then enters through air inlet and change
The shell side of hot device is flowed out through heat exchanger tube with after the unstripped gas heat exchange in tube side through syngas outlet pipe, into next procedure；
Hot water in drum enters in tubulation from refrigerant inlet pipe, absorbs the reaction heat of unstripped gas, becomes steam-water mixing
Then object is discharged from refrigerant exit pipe, enters in drum, flash to the steam water interface in drum, steam is deviate from,
In drum under the promotion of steam pressure, the hot water in drum is re-introduced into tubulation through refrigerant inlet pipe, is recycled；
The discharge temperature of unstripped gas from the tube side of heat exchanger is 200-220 DEG C, and unstripped gas is in the reaction temperature of reaction zone
220-240℃.Further, unstripped gas is high compared with the discharge temperature of unstripped gas from the tube side of heat exchanger in the reaction temperature of reaction zone
15-25℃.In above-mentioned technique, in reactor, unstripped gas is formed by gaseous mixture and exchanges heat with reacting first, to absorb
Thermal energy in gaseous mixture reduces gaseous mixture from the discharge temperature in reactor, and the gaseous mixture being discharged from reactor can be directly entered
To the distilation stage, no longer need to cool down.The temperature of the unstripped gas entered in reactor simultaneously is improved, unstripped gas
Temperature close to its optimal reaction temperature, and slightly below its optimal reaction temperature, after unstripped gas enters the stage of reaction, anti-
Under the action of answering heat, reaction temperature can quickly enter optimum state.And in the prior art, usually it is arranged outside reactor
Individual heater heats unstripped gas, compared with heater is separately provided, not only reduces number of devices, reduces first
The whole cost of alcohol synthesis system, and also reduce technology controlling and process point, and shorten process flow, be conducive to process integration and
Improve product quality.
Further, gaseous mixture from the discharge temperature of methanol reactor be 65-85 DEG C.At such a temperature, not only fully will
Thermal energy in gaseous mixture is recycled, and is reduced the subsequent cooling to gaseous mixture and operated.
Specifically, the temperature of the hot water is 40-50 DEG C, and the temperature of steam water interface is 230-240 DEG C；It is dodged out of drum
The pressure of the steam steamed is 3.5-4.5MPa.Under above-mentioned condition, in the case where guaranteeing the discharge temperature of gaseous mixture, it can obtain
A certain amount of middle pressure steam.
Detailed description of the invention:
Fig. 1 is the structure diagram of methanol reactor.
Fig. 2 is the schematic diagram of methanol synthesizing process.
Specific embodiment:
Refering to fig. 1, the radial methanol reactor of combined type heat exchange comprising shell 11, shell 11 have main cylinder 111, peace
Upper shell end socket 112 and the lower casing end socket 113 for the lower end for being mounted on main cylinder 111 mounted in 111 upper end of main cylinder, shell
Lower end is provided with synthesis gas inlet pipe 61, syngas outlet pipe 15 and refrigerant inlet pipe 44, and the upper end of shell is provided with refrigerant
Outlet 24；Specifically in the present embodiment, synthesis gas inlet pipe 61, syngas outlet pipe 15 and refrigerant inlet pipe 44 are arranged at
On lower casing end socket 113, refrigerant exit pipe 34 is arranged on upper shell end socket 112.Internals 12 are provided in shell 11, inside
Cloth air cavity 51 is formed between part 12 and shell 11, the first through hole being provided between connection cloth air cavity reaction zone in internals 12.
It is provided with the getter cylinder 14 along the extension of 100 direction of axis of shell 11 in internals 12, is provided on getter cylinder
The second through-hole being connected between reaction zone and getter chamber.
Reaction zone is formed between getter cylinder 14 and internals, tubulation 13 is provided in reaction zone, around tubulation 13
It is filled with catalyst.
Shell-and-tube heat exchanger 30 is installed in getter cylinder 14, which has in shell 32 and installation shell 32
Heat exchanger tube 31, heat exchanger 30 extend along 100 direction of axis of shell 11, are formed between the shell 32 and getter cylinder 14 of heat exchanger 30
Getter chamber 52.
The upper end of heat exchanger 30 is provided with air inlet 34, specifically in the present embodiment, the setting of air inlet 34 is exchanging heat
The upper end of the shell 32 of device.The air inlet 34 is connected to the shell side and getter chamber 52 of heat exchanger 30.It is set in the lower end of heat exchanger 30
It is equipped with gas outlet 35, which is connected to the shell side and syngas outlet pipe 15 of heat exchanger 30.
The upper end of the heat exchanger tube 31 of heat exchanger 30 is connected to cloth air cavity 51, the lower end connection synthesis gas inlet pipe of heat exchanger tube 31
61。
The upper end of the tubulation 13 is connected to refrigerant exit pipe 24, and the lower end of tubulation 13 is connected to refrigerant inlet pipe 44.
When the methanol reactor in use, unstripped gas, which is synthesized gas inlet pipe 61, enters the tube side of heat exchanger 30, then into
Enter to cloth air cavity 51, forms gaseous mixture radially into reaction is carried out in reaction zone through cloth air cavity 51, gaseous mixture is through getter cylinder 14
Getter chamber 52 is entered, then enters the shell side of heat exchanger 30 through air inlet 34, is exchanged heat through the unstripped gas in heat exchanger tube 31 and tube side
It is flowed out by syngas outlet pipe 15.
Catalyst cover board 33 is installed in the upper end of internals 12, supporter 18 is installed in the lower end of internals.
The first air cavity 16 is formed between catalyst cover board 33 and the top of shell 11, between supporter 18 and the bottom of shell 11
Form the second air cavity 17；The heat exchanger tube 31 of heat exchanger 30 is connected to the first air cavity 16, the first air cavity after extending upward through catalyst cover board 33
16 connection cloth air cavitys 51；The shell side of heat exchanger 30 is connected to the second air cavity 17, and syngas outlet pipe 15 is connected to the second air cavity 17.
The lower end of the shell 32 of heat exchanger 30 is mounted on supporter 18, is equipped with bottom in the lower end of the shell 32 of heat exchanger
Portion's tube sheet 64, in bottom, the downside of tube sheet 64 is equipped with bottom bulkhead 63, and synthesis gas inlet pipe 61 is connected to bottom bulkhead 63.The bottom of at
Above-mentioned gas outlet 35 is provided between portion's tube sheet 34 and shell 32；The lower end of the heat exchanger tube 31 of heat exchanger 30 is mounted on lower tube
On plate 64.
Top tube sheet 36 is installed on the top of the shell 32 of heat exchanger 30, top tube sheet 36 is mounted on catalyst cover board 33
On, the upper end of the heat exchanger tube 31 of heat exchanger is mounted on the tube sheet 36 of top.
For convenience of installation and maintenance, tubulation 31 is divided into three groups, is provided with a upper perforated plate sub-assembly corresponding to every group of tubulation
With a lower perforated plate sub-assembly；Each upper perforated plate sub-assembly includes a upper perforated plate 21 and one is mounted on upper cover 22 on upper perforated plate,
The refrigerant exit pipe 24 of a connection upper cover is provided with corresponding to each upper cover.
Each lower perforated plate sub-assembly includes a lower perforated plate 41 and one is mounted on lower head 42 on lower perforated plate, is corresponded to each
Lower head is provided with the refrigerant inlet pipe 44 of a connection lower head.
It is appreciated that in other embodiments, refrigerant exit pipe can only be set as one, then using setting branch pipe
Mode is connected on each upper cover.Alternatively, refrigerant inlet pipe can only be set as one, then by the way of branch pipe is arranged
It is connected on each lower head.
The methanol synthesizing process that methanol-fueled CLC is carried out using above-mentioned methanol reactor, is had follow steps:
Referring to Fig. 2, unstripped gas 304 is entered to the tube side of heat exchanger 30 through synthesizing gas inlet pipe 61, then into
First air cavity 16 of cover top portion, then diffuses into cloth air cavity 51 around, the first through hole in internals 12 into
Enter into reaction zone, reacted under the effect of the catalyst, form gaseous mixture, gaseous mixture enters heat exchanger through air inlet 34
In 30 shell side, the shell side along heat exchanger 30 flows downward, and enters in the second air cavity 17 through gas outlet 35, finally through synthesis gas
Outlet 15 flows out, and enters next procedure.
Hot water in drum 200 enters in tubulation 31 from refrigerant inlet pipe 44, absorbs the reaction heat of unstripped gas, becomes vapour
Then aqueous mixtures are discharged from refrigerant exit pipe 24, return in drum 200, dodge to the steam water interface in drum 200
It steams, steam 202 is deviate from, in drum under the promotion of steam pressure, the hot water in drum is again introduced into through refrigerant inlet pipe 44
Into tubulation 31, it is recycled.For the reduction for making up hot water amount after steam is deviate from, supplement water 203 is added into drum 200.
In the present embodiment, unstripped gas is 210 DEG C from the discharge temperature of the tube side of heat exchanger 30, and unstripped gas is in reaction zone
Reaction temperature is 230 DEG C.It is appreciated that the discharge temperature of unstripped gas can also be 200 DEG C or 220 DEG C, and at 200-220 DEG C
Between other temperature.
Gaseous mixture from the discharge temperature of methanol reactor be 75 DEG C.In other embodiments, gaseous mixture is from methanol reactor
Discharge temperature can also be 65 DEG C or 85 DEG C, or the arbitrary value between 65-85 DEG C.
To avoid unstripped gas in reaction, is influenced that its reaction temperature is caused excessively to increase by reaction heat, cause temperature runaway existing
As in the present embodiment, unstripped gas is high compared with the discharge temperature of unstripped gas from the tube side of heat exchanger by 20 in the reaction temperature of reaction zone
℃.It is appreciated that be in embodiment other, unstripped gas reaction zone reaction temperature compared with unstripped gas from the tube side of heat exchanger
Discharge temperature is higher by range and can select between 15-25 DEG C.
In the present embodiment, at 45 DEG C, the temperature of steam water interface is controlled at 235 DEG C, from drum for the temperature control of hot water
The pressure of the steam inside flashed off is 4.0MPa.
In other embodiments, according to specific needs, the temperature of hot water be can control at 40-50 DEG C, steam water interface
Temperature can control at 230-240 DEG C；The pressure of the steam flashed off out of drum can be 3.5-4.5MPa.
Claims (6)
- The radial methanol reactor 1. combined type exchanges heat, which is characterized in that including shell, the lower end of shell be provided with synthesis gas into Mouth pipe, syngas outlet pipe and refrigerant inlet pipe, are provided with refrigerant exit pipe in the upper end of shell；In being provided with inside the shell Part forms cloth air cavity between internals and shell；It is provided with the getter cylinder of the axis direction extension along shell in internals, is receiving Reaction zone is formed between inflator and internals, tubulation is provided in reaction zone, and catalyst is filled with around tubulation；Shell-and-tube heat exchanger is installed in getter cylinder, which has shell and the intracorporal heat exchanger tube of mounting shell, heat exchanger Axis direction along shell extends, and getter chamber is formed between the shell and getter cylinder of heat exchanger；The upper end of heat exchanger is provided with air inlet, which is connected to the shell side and getter chamber of heat exchanger；In heat exchanger Lower end is provided with gas outlet, which is connected to the shell side and syngas outlet pipe of heat exchanger；The upper end of the heat exchanger tube of heat exchanger is connected to cloth air cavity, the lower end connection synthesis gas inlet pipe of the heat exchanger tube；The upper end of the tubulation is connected to refrigerant exit pipe, and the lower end of tubulation is connected to refrigerant inlet pipe；Be provided in internals connection cloth air cavity reaction zone between first through hole, be provided on getter cylinder connection reaction zone with The second through-hole between getter chamber；When the methanol reactor in use, unstripped gas enters the tube side of heat exchanger through synthesizing gas inlet pipe, gas distribution is entered back into Chamber forms gaseous mixture radially into reaction is carried out in reaction zone through cloth air cavity, and gaseous mixture enters getter chamber through getter cylinder, then The shell side for entering heat exchanger through air inlet is flowed out with after the unstripped gas heat exchange in tube side through syngas outlet pipe through heat exchanger tube.
- 2. methanol reactor according to claim 1, which is characterized in that catalyst cover board is installed in the upper end of internals, The lower end of internals is equipped with supporter；The first air cavity, the bottom of supporter and shell are formed between catalyst cover board and the top of shell The second air cavity is formed between portion；The heat exchanger tube of the heat exchanger, which extends upward through, is connected to the first air cavity after catalyst cover board, and described first Air cavity is connected to cloth air cavity；The shell side of the heat exchanger is connected to the second air cavity, and syngas outlet pipe is connected to the second air cavity.
- 3. methanol reactor according to claim 2, which is characterized in that the lower end of the shell of heat exchanger is mounted on supporter On, bottom tube sheet is installed in the lower end of the shell of heat exchanger, bottom bulkhead, the synthesis are installed on the downside of the tube sheet of bottom Gas inlet pipe is connected to bottom bulkhead；The gas outlet is provided between bottom tube sheet and shell；Under the heat exchanger tube of heat exchanger End is mounted on the tube sheet of bottom.
- 4. methanol reactor according to claim 2, which is characterized in that be equipped with top on the top of the shell of heat exchanger Tube sheet, top tube sheet are mounted on catalyst cover board, and the upper end of the heat exchanger tube of heat exchanger is mounted on the tube sheet of top.
- 5. methanol reactor according to any one of claims 1-4, which is characterized in thatThe upper end of the shell of heat exchanger is arranged in the air inlet.
- 6. methanol reactor according to claim 1, which is characterized in that the tubulation is at least divided into three groups, corresponds to every Group tubulation is provided with a upper perforated plate sub-assembly and a lower perforated plate sub-assembly；Each upper perforated plate sub-assembly includes a upper perforated plate and one is mounted on upper cover on upper perforated plate, and upper cover is connected to refrigerant exit Pipe；Each lower perforated plate sub-assembly includes a lower perforated plate and one is mounted on lower head on lower perforated plate, and lower head is connected to refrigerant inlet Pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820503992.3U CN208389981U (en) | 2018-04-09 | 2018-04-09 | The radial methanol reactor of combined type heat exchange |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820503992.3U CN208389981U (en) | 2018-04-09 | 2018-04-09 | The radial methanol reactor of combined type heat exchange |
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| CN208389981U true CN208389981U (en) | 2019-01-18 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108393044A (en) * | 2018-04-09 | 2018-08-14 | 南京聚拓化工科技有限公司 | The radial methanol reactor of combined type heat exchange and methanol synthesizing process |
| CN112624044A (en) * | 2021-01-04 | 2021-04-09 | 南京聚拓化工科技有限公司 | Heat-insulation serial isothermal CO conversion reactor capable of producing superheated steam and coal gas conversion process |
-
2018
- 2018-04-09 CN CN201820503992.3U patent/CN208389981U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108393044A (en) * | 2018-04-09 | 2018-08-14 | 南京聚拓化工科技有限公司 | The radial methanol reactor of combined type heat exchange and methanol synthesizing process |
| CN108393044B (en) * | 2018-04-09 | 2023-10-27 | 南京聚拓化工科技有限公司 | Combined heat exchange radial methanol reactor and methanol synthesis process |
| CN112624044A (en) * | 2021-01-04 | 2021-04-09 | 南京聚拓化工科技有限公司 | Heat-insulation serial isothermal CO conversion reactor capable of producing superheated steam and coal gas conversion process |
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