CN109173937B - Temperature-variable methanol synthesis reaction system - Google Patents
Temperature-variable methanol synthesis reaction system Download PDFInfo
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- CN109173937B CN109173937B CN201811160837.7A CN201811160837A CN109173937B CN 109173937 B CN109173937 B CN 109173937B CN 201811160837 A CN201811160837 A CN 201811160837A CN 109173937 B CN109173937 B CN 109173937B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/152—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
Abstract
The invention relates to a temperature-variable methanol synthesis reaction system, which comprises an isothermal shift converter, a steam drum and a heat exchanger, wherein the isothermal shift converter comprises a furnace body, a catalyst frame and a synthesis gas collecting pipe, wherein the catalyst frame and the synthesis gas collecting pipe are arranged in the furnace body; a raw material gas inlet, a synthetic gas outlet and a raw material gas channel are arranged on the furnace body, and a plurality of air holes are arranged on the side wall of the catalyst frame; a plurality of heat exchange tubes connected with the steam pocket are arranged in the catalyst bed layer; the side wall of the synthesis gas collecting pipe is provided with an air inlet, and the outlet of the synthesis gas collecting pipe is connected with a synthesis gas outlet; the catalyst bed is characterized in that a plurality of raw material gas preheating pipes are also arranged in the catalyst bed, the inlet of each raw material gas preheating pipe is connected with a first raw material gas conveying pipeline, and the outlet of each raw material gas preheating pipe is communicated with a raw material gas channel; the second raw material gas conveying pipeline is connected with a raw material gas inlet through a heat exchanger; and the first feed gas conveying pipeline and the second feed gas conveying pipeline are respectively provided with a first valve and a second valve.
Description
Technical Field
The invention relates to chemical equipment, in particular to a temperature-variable methanol synthesis reaction system.
Background
Methanol synthesis is a reversible exothermic reaction process. For the copper-based methanol synthesis catalyst, the reaction temperature needs to be maintained between 220 ℃ and 280 ℃, the catalyst does not have activity when the temperature is too low, and the service life and the product quality of the catalyst are influenced when the temperature is too high. In order to make the methanol synthesis reaction proceed in a suitable temperature range, heat exchange tubes are usually embedded in the catalyst reaction bed, and the reaction heat released during methanol synthesis is removed by the steam generated by the gasification of boiler water in the heat exchange tubes, and this type of reactor is called an isothermal methanol synthesis reactor.
Based on the consideration of prolonging the service life of the methanol synthesis catalyst, the reaction temperature of the catalyst is generally controlled between 240 ℃ and 260 ℃ in the initial stage of use, and the reaction temperature of the catalyst is generally controlled between 260 ℃ and 280 ℃ in the later stage of use. When the device is stably operated, the reaction heat removed by the steam generated by boiler water in the heat exchange tube is constant, but the reaction temperature slowly rises from 240 ℃ to 280 ℃ along with the aging of the catalyst, the temperature of the steam in the corresponding heat exchange tube slowly rises from 225 ℃ to 265 ℃, and the steam pressure generated by the boiler water gradually rises from 2.7MPAG to 5.2 MPAG.
The fluctuation of the reaction temperature at the initial stage and the final stage of the methanol synthesis can be transmitted to a heat exchange pipe used for heat transfer in a reaction bed layer, so that the fluctuation of the temperature and the pressure of steam generated in the heat exchange pipe is further caused, particularly, the steam quantity rich in production is more and more along with the large-scale and multi-series of a methanol synthesis device, but the isothermal methanol synthesis reactor can not solve the problems of the fluctuation of the steam pressure and the increase of the investment of related equipment and pipeline engineering all the time, and the method is mainly embodied as follows:
(1) considering from the design pressure, because the pressure of steam generated in the heat exchange tube fluctuates between 2.7MPAG and 5.2MPAG, higher design pressure needs to be considered for the associated equipment and pipeline, otherwise, the steam pressure requirement of 5.2MPAG in the later stage of the catalyst cannot be met, and the increase of the wall thickness of the equipment and the pipeline increases the engineering investment;
(2) in view of rich steam, although the high-quality steam of 5.2MPAG can be rich in the later stage of the catalyst, the balance of the steam pipe network of the whole plant is determined by the 2.7MPAG steam in the initial stage of the catalyst, and only the high-quality steam of 5.2MPAG can be decompressed and degraded for use in engineering design, so that pipeline valves and automatic control instrument elements related to decompression are required to be added, and certain impact is also caused on the steam pipe network of the whole plant.
In short, boiler water system pipelines and equipment in the methanol synthesis reactor need to be designed according to the harsh temperature and pressure, and medium-pressure steam generated in the later stage of the catalyst is degraded for use, so that the investment and the balance of a whole plant steam pipe network are not reasonable.
Chinese patent publication No. CN102698659A discloses a methanol synthesis reactor structure, in which heat exchange tubes are buried in a reaction bed, methanol synthesis is performed in a catalyst bed, and the released reaction heat is removed by boiler water in the heat exchange tubes. However, the steam pressure of the rich product in the later period of the catalyst is increased, and the related equipment and pipelines have to be designed according to the steam pressure and the temperature in the later period, so that the engineering investment is increased; meanwhile, when the balance design of the steam pipe network of the whole plant is carried out by the process system, the process system can only be designed according to the lower steam pressure and steam quality at the initial stage of the catalyst, but certain impact is caused on the steam pipe network of the whole plant at the later stage of the catalyst.
Disclosure of Invention
The invention aims to solve the technical problem of providing a variable-temperature methanol synthesis reaction system aiming at the current situation of the prior art, which can better solve the problems of water gasification temperature and pressure fluctuation of a boiler while meeting the initial and final reaction temperature interval of a methanol synthesis reaction catalyst, further realize the goals of reducing the engineering investment and optimizing a steam pipe network system of a whole plant, and meet the requirements of large-scale and energy-saving development of a methanol synthesis device.
The technical scheme adopted by the invention for solving the technical problems is as follows: the temperature-variable methanol synthesis reaction system comprises an isothermal shift converter, a steam drum and a heat exchanger, wherein the isothermal shift converter comprises a furnace body and a catalyst frame arranged in the furnace body, and a synthesis gas collecting pipe is arranged in the middle of the catalyst frame; the top of the furnace body is provided with a raw material gas inlet, and the bottom of the furnace body is provided with a synthesis gas outlet; a gap is formed between the side wall of the catalyst frame and the side wall of the furnace body, the gap forms a feed gas channel, a space between the synthesis gas collecting pipe and the catalyst frame forms a catalyst bed layer, and a plurality of air holes communicated with the feed gas channel and the catalyst bed layer are arranged on the side wall of the catalyst frame; a plurality of heat exchange tubes are arranged in the catalyst bed layer, the inlet of each heat exchange tube is connected with the boiler water outlet of the steam drum, and the outlet of each heat exchange tube is connected with the steam recovery port of the steam drum; the side wall of the synthesis gas collecting pipe is provided with a plurality of air inlets for communicating the catalyst bed layer with the inner cavity of the synthesis gas collecting pipe, and the outlet of the synthesis gas collecting pipe is connected with the synthesis gas outlet;
the method is characterized in that:
a plurality of raw material gas preheating pipes are further arranged in the catalyst bed layer, an inlet of each raw material gas preheating pipe is connected with a first raw material gas conveying pipeline, and an outlet of each raw material gas preheating pipe is communicated with the raw material gas channel;
the second feed gas conveying pipeline is connected with the feed gas inlet through the heat exchanger;
and the first feed gas conveying pipeline and the second feed gas conveying pipeline are respectively provided with a first valve and a second valve.
The second feed gas conveying pipeline is connected with the first channel of the heat exchanger; the synthesis gas conveying pipeline is connected with the first branch and the second branch, the first branch is connected with the second channel of the heat exchanger, the second branch is provided with a third valve, and the synthesis gas conveying pipeline is connected with the synthesis gas outlet.
Further, the first raw material gas conveying pipeline is connected with a gas distributor, and an inlet of each raw material gas preheating pipe is connected with the gas distributor; the gas distributor is positioned at the lower part of the furnace body. The design of the gas distributor can ensure that the raw material gas uniformly enters each raw material gas preheating pipe, thereby further ensuring the uniformity of heat removal of the catalyst bed layer.
Preferably, each feed gas preheating pipe is uniformly distributed in the catalyst bed layer, and the heat exchange pipes are divided into a plurality of groups and are respectively distributed around each feed gas preheating pipe to uniformly remove heat.
In order to facilitate the temperature control of the catalyst bed layer in the later operation stage of the device, preferably, each feed gas preheating pipe and each heat exchange pipe arranged around the feed gas preheating pipe form a pipe group;
the sum of the cross sectional areas of the feed gas preheating pipes is 15-40% of the sum of the cross sectional areas of the heat exchange pipes. The scheme can further ensure the uniformity of heat removal of the catalyst bed layer in the whole operation process of the device.
Preferably, connecting lines between the center of each feed gas preheating pipe and the centers of the three adjacent heat exchange pipes form a rhombus; the feed gas preheating pipes and the three heat exchange pipes which are positioned at the four top points of the same rhombus form a group of heat exchange pipe pairs.
Further, a part of the heat exchange tubes can be shared between adjacent heat exchange tube pairs. So that the arrangement of each heat exchange tube at the position of the catalyst bed layer is more reasonable, and the heat removal of the catalyst bed layer is more uniform after the feed gas preheating tube is closed.
The outlet of each heat exchange tube is connected with a steam connecting tube through a steam collecting tube, and the steam connecting tube is connected with a steam recovery port of the steam drum; the steam connecting pipe is provided with an expansion joint so as to conveniently and smoothly collect steam and absorb the thermal expansion of the steam connecting pipe.
Preferably, a boiler water outlet of each steam drum is connected with a pipe box through a water inlet connecting pipe, and an inlet of each heat exchange pipe is connected with the pipe box.
For convenient maintenance, the synthesis gas collecting pipe can be formed by connecting the multistage barrel in a detachable mode in sequence, and a plurality of foot ladders are arranged on the inner side wall of the barrel at intervals in sequence along the axial direction.
Compared with the prior art, the variable-temperature methanol synthesis reaction system provided by the invention overcomes the defects of the prior art, the isothermal water-cooling methanol synthesis reactor is designed into the variable-temperature methanol synthesis reaction system, the heat exchange tube and the feed gas preheating tube are arranged at the catalyst bed position, and the heat removal quantity can be changed according to the activity requirement of the catalyst at each stage of the operation of the device, so that the requirement of the catalyst activity temperature at different reaction stages is met, the constant yield is maintained, and meanwhile, the problems of increased wall thickness of the heat exchange tube, increased wall thickness of a steam pocket, changed matching pipelines and equipment and the like caused by the method that the pressure in the steam pocket and the heat exchange tube is increased to improve the reaction temperature at the later stage of the reaction in the prior art are avoided, the equipment investment is reduced.
Drawings
FIG. 1 is a schematic diagram of an embodiment of the present invention;
FIG. 2 is a longitudinal sectional view of a reactor section in an embodiment of the invention;
FIG. 3 is a cross-sectional view taken along line A-A of FIG. 2;
FIG. 4 is an enlarged view of a portion C of FIG. 3;
Detailed Description
The invention is described in further detail below with reference to the accompanying examples.
As shown in fig. 1 to 4, the variable temperature methanol synthesis reaction system includes:
the furnace body 1 is of a conventional structure and comprises an upper seal head 11, a lower seal head 12 and a cylinder body 13 connected between the upper seal head 11 and the lower seal head 12. The upper seal head 11 is provided with a manhole 15 and a raw material gas inlet 14, and the raw material gas inlet 14 is connected with a second raw material gas conveying pipeline 62. The second raw material gas conveying pipeline 62 is provided with a heat exchanger 65 and a first medium channel communicated with the heat exchanger 65; the second raw material gas delivery pipe 62 is also provided with a first valve 64. The inlet of the second raw material gas delivery pipe 62 is communicated with a raw material gas pipe 66.
The catalyst frame 2 is used for filling a catalyst and is arranged in the cylinder 13. The catalyst frame 2 may be any one of the prior art as required, and may be an axial reactor, a radial reactor, or an axial-radial reactor, for example, which may be set as required. In this embodiment, the reactor is a radial reactor, the raw material gas enters the catalyst frame from through holes (not shown) on the sidewall of the catalyst frame 2, and the through holes on the sidewall of the catalyst frame function as gas distributors.
The synthesis gas collecting pipe 3 is used for collecting synthesis gas and sending the synthesis gas out of the furnace body 1 through a synthesis gas conveying pipeline 33, is arranged in the middle of the inner cavity of the catalyst frame, and is formed by sequentially and detachably connecting a plurality of sections of cylinders 31, and in the embodiment, the cylinders 31 are connected through flanges 34; the side wall of each cylinder 31 is provided with a plurality of air inlets (not shown in the figure) for the synthesis gas to enter the synthesis gas collecting pipe 3 from the catalyst bed layer; a plurality of footsteps 32 are sequentially arranged on the inner side wall of the cylinder 31 at intervals along the axial direction. The end cover is detachably connected to the upper end port of the synthesis gas collecting pipe 3, and is communicated with the manhole 15 after being disassembled, so that an overhaul worker can enter the synthesis gas collecting pipe 3; the lower port of the synthesis gas collecting tube 3 is connected with a synthesis gas conveying pipe 33. The synthesis gas conveying pipeline 33 is connected with the first branch 35 and the second branch 36, and the first branch 35 is connected with a second medium channel of the heat exchanger 65; the second branch 36 is provided with a third valve 37, and the second branch 36 is used as a bypass line of the second medium channel of the heat exchanger 65 and is connected with an inlet and outlet line of the second medium channel of the heat exchanger 65.
The feed gas preheating pipes 6 are vertically arranged in a cavity between the catalyst frame 2 and the synthesis gas collecting pipe 3 in parallel with the axis of the furnace body 1 and are uniformly arranged. The inlet of each raw material gas preheating pipe 6 is communicated with a gas distributor 56, the inlet of the gas distributor 56 is connected with a first raw material gas conveying pipeline 61, a second valve 63 is arranged on the first raw material gas conveying pipeline 61, and the first raw material gas conveying pipeline 61 is connected with a raw material gas pipeline 66.
The gas distributor 56 is arranged at the lower part of the furnace body; the outlet of each raw material gas preheating pipeline 6 is limited on the upper end plate 21 of the catalyst frame 2 and exposed out of the upper end plate 21, so that the preheated second raw material gas enters the cavity between the catalyst frame and the upper end enclosure, is further mixed with the first raw material gas and then enters the catalyst frame from the gap between the catalyst frame and the side wall of the cylinder body through each through hole.
And a plurality of heat exchange tubes 4 are arranged in the space between the catalyst frame 2 and the synthesis gas collecting tube 3 and are parallel to the feed gas preheating tubes 6. Each heat exchange tube can be a straight tube, a corrugated tube or a U-shaped tube, and any one of the prior art can be selected according to the requirement. This embodiment is a straight tube.
For the sake of distinction, each feed gas preheating tube 6 is shown by a filled circle and each heat exchange tube 4 is shown by a hollow circle in fig. 4.
In the present embodiment, the heat exchange tubes 4 are uniformly arranged in the cavity between the catalyst frame 2 and the synthesis gas collecting tube 3; each heat exchange tube 4 and each raw material gas preheating tube 6 are arranged in a rhombus shape, each heat exchange tube 4 and each raw material gas preheating tube 6 respectively occupy four vertexes of the rhombus shape to form a group of heat exchange tube pairs 5 (a dashed box in fig. 4), and each group of heat exchange tube pairs 5 is respectively provided with three heat exchange tubes 4 and one raw material gas preheating tube 6. Each group of heat exchange tube pairs are adjacently arranged in the same direction.
The relative size of each heat exchange tube 4 and each raw material gas preheating tube 6 can be adjusted according to the scale of the device and the specification design of the reactor, so as to adjust the relative heat exchange area. The heat exchange tubes 4 and the feed gas preheating tubes 6 in the embodiment have the same relative sizes. The sum of the heat exchange areas of the feed gas preheating pipes 6 is 15-40%, in this embodiment 25%, of the sum of the total heat exchange areas.
A water inlet pipeline for communicating the steam drum 60 with each heat exchange pipe, comprising a water inlet connecting pipe 51 and a pipe box 52 communicated with the outlet of the water inlet connecting pipe 51; the tube box 52 may be a loop structure, as shown in fig. 1 of the present embodiment, or a box structure, and any one of the prior arts may be used according to the needs.
The inlet of each heat exchange tube 4 is communicated with the tube box 52.
A steam pipe including a steam connection pipe 53 and a steam collection pipe 54 connecting the steam drum; the outlet of the steam collecting pipe 54 is connected with the steam connecting pipe 53, and the inlets of the steam collecting pipe 54 are respectively connected with the outlets of the heat exchanging pipes 4.
The steam collection pipe 54 may be of a loop configuration, a box configuration, or other configuration.
And expansion joints 55 provided on the two steam connection pipes 53 for absorbing thermal stress.
The catalyst activity is high at the initial stage of the device operation. The raw material gas is divided into two paths, namely a first raw material gas and a second raw material gas, and the second raw material gas passes through a second raw material gas conveying pipeline 62, is preheated by a heat exchanger 65, and then enters the cavity of the upper end enclosure of the reactor through a raw material gas inlet 14. The first raw material gas enters the raw material gas preheating pipe 6 through the first raw material gas conveying pipeline 61 through the gas distributor 56, enters the cavity of the upper end enclosure after being preheated, and is mixed with the first raw material gas to form mixed gas. Cooling water enters each heat exchange tube from the water inlet pipeline and exchanges heat with the reaction heat of the catalyst bed layer. The mixed gas reaches the feeding temperature, descends along the gap between the catalyst frame and the cylinder body, enters the catalyst bed layer through the through holes on the side wall of the catalyst frame and carries out methanol synthesis reaction; the cooling water in each heat exchange tube is heated to be changed into steam, and the steam is returned to the steam pocket through the steam pipeline. The synthesis gas obtained from the methanol synthesis reaction enters the downstream after the raw material gas is preheated by the heat exchanger 65.
In the initial stage of the operation of the device, the catalyst is low in activity temperature and needs to remove more heat, the raw material gas and the cooling water are used for simultaneously removing heat, the catalyst bed layer is maintained at a set temperature for methanol synthesis reaction, and the yield is constant at a set value.
In the later stage of the operation of the device, the activity temperature of the catalyst is increased due to the reduction of the activity of the catalyst; at this time, parameters such as steam drum and boiler water and steam pressure in the steam drum are kept unchanged, the opening degree of the second valve 63 is gradually reduced, and the opening degree of the first valve 64 is gradually increased. The heat extraction of the feed gas preheating pipe 6 is gradually reduced, and the activity temperature of the catalyst is maintained. And in the final stage of the operation of the device, the second valve is closed, the first valve is fully opened, all the raw material gas enters the heat exchanger from the second raw material gas conveying pipeline, exchanges heat with the high-temperature synthesis gas from the synthesis gas conveying pipeline 33, and enters the cavity of the upper end enclosure through the raw material gas inlet. Cooling water is still introduced into each heat exchange tube to take away the reaction heat generated by the catalyst bed layer. The feed gas preheating pipe 6 does not participate in the heat exchange of the catalyst bed layer, and only cooling water in the heat exchange pipe is used for heat extraction, so that the heat exchange amount is reduced, the heat removal amount of the catalyst bed layer is reduced, the temperature of the catalyst bed layer is increased, the requirement on the activity temperature of a catalyst at the later stage is met, the methanol synthesis reaction is normally carried out, and the yield is still maintained at a design value; and the steam pressure of the steam outlet drum is unchanged, and parameters of matched pipelines and equipment do not need to be changed.
Due to the special arrangement of the feed gas preheating tubes and the heat exchange tubes, the heat exchange tubes can still uniformly remove heat from the catalyst bed even if the feed gas preheating tubes are closed.
Claims (7)
1. A temperature-variable methanol synthesis reaction system comprises an isothermal shift converter, a steam drum (60) and a heat exchanger (65), wherein the isothermal shift converter comprises a furnace body (1) and a catalyst frame (2) arranged in the furnace body (1), and a synthesis gas collecting pipe (3) is arranged in the middle of the catalyst frame; the top of the furnace body (1) is provided with a raw material gas inlet (14), and the bottom of the furnace body (1) is provided with a synthesis gas outlet; a gap is formed between the side wall of the catalyst frame and the side wall of the furnace body, the gap forms a feed gas channel, a space between the synthesis gas collecting pipe (3) and the catalyst frame forms a catalyst bed layer, and a plurality of air holes communicated with the feed gas channel and the catalyst bed layer are arranged on the side wall of the catalyst frame; a plurality of heat exchange tubes (4) are arranged in the catalyst bed layer, the inlet of each heat exchange tube is connected with the boiler water outlet of the steam drum (60), and the outlet of each heat exchange tube is connected with the steam recovery port of the steam drum; the side wall of the synthesis gas collecting pipe (3) is provided with a plurality of air inlets for communicating the catalyst bed layer with the inner cavity of the synthesis gas collecting pipe, and the outlet of the synthesis gas collecting pipe is connected with the synthesis gas outlet;
the method is characterized in that:
a plurality of raw material gas preheating pipes (6) are further arranged in the catalyst bed layer, an inlet of each raw material gas preheating pipe is connected with a first raw material gas conveying pipeline (61), and an outlet of each raw material gas preheating pipe is communicated with the raw material gas channel;
a second feed gas delivery conduit (62) is connected to the feed gas inlet (14) through the heat exchanger (65);
a first valve (63) and a second valve (64) are respectively arranged on the first raw material gas conveying pipeline (61) and the second raw material gas conveying pipeline (62);
the raw material gas preheating pipes (6) are uniformly distributed in the catalyst bed layer, and the heat exchange pipes (4) are divided into a plurality of groups and are respectively arranged around the raw material gas preheating pipes;
each feed gas preheating pipe and each heat exchange pipe arranged around the feed gas preheating pipe form a pipe group;
the sum of the cross sectional areas of the feed gas preheating pipes is 15-40% of the sum of the cross sectional areas of the heat exchange pipes;
connecting lines between the center of each raw material gas preheating pipe (6) and the centers of the three adjacent heat exchange pipes form a rhombus; the feed gas preheating pipes and the three heat exchange pipes which are positioned at the four top points of the same rhombus form a group of heat exchange pipe pairs.
2. A variable temperature methanol synthesis reaction system according to claim 1, characterized in that the second feed gas delivery conduit (62) is connected to the first channel of the heat exchanger (65); the synthesis gas conveying pipeline (33) is connected with a first branch (35) and a second branch (36), the first branch is connected with a second channel of the heat exchanger, a third valve (37) is arranged on the second branch (36), and the synthesis gas conveying pipeline (33) is connected with the synthesis gas outlet.
3. The variable temperature methanol synthesis reaction system according to claim 2, wherein the first raw material gas delivery pipe (61) is connected with a gas distributor (56), and the inlet of each raw material gas preheating pipe (6) is connected with the gas distributor (56); the gas distributor (56) is positioned at the lower part of the furnace body (1).
4. The variable temperature methanol synthesis reaction system as claimed in claim 1, wherein a portion of the heat exchange tubes are shared between adjacent pairs of heat exchange tubes.
5. The temperature-variable methanol synthesis reaction system according to claim 4, wherein the outlet of each heat exchange tube (4) is connected with a steam connecting tube (53) through a steam collecting tube (54), and the steam connecting tube (53) is connected with a steam recovery port of the steam drum; and an expansion joint (55) is arranged on the steam connecting pipe.
6. The variable temperature methanol synthesis reaction system according to claim 5, wherein the boiler water outlet of each steam drum is connected with a pipe box (52) through a water inlet connecting pipe (51), and the inlet of each heat exchange pipe (4) is connected with the pipe box (52).
7. The temperature-variable methanol synthesis reaction system according to claim 6, wherein the synthesis gas collecting pipe (3) is formed by sequentially and detachably connecting a plurality of sections of cylinders, and a plurality of foot ladders are sequentially arranged on the inner side wall of each cylinder at intervals along the axial direction.
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| US4714592A (en) * | 1984-01-18 | 1987-12-22 | Toyo Engineering Corporation | Radial flow catalytic reactor including heat exchange apparatus within the bed |
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| CN102836676A (en) * | 2012-09-28 | 2012-12-26 | 神华集团有限责任公司 | Gas-solid phase catalytic reactor |
| CN205235934U (en) * | 2015-12-16 | 2016-05-18 | 河南顺达化工科技有限公司 | Adiabatic ethanol synthesis reactor |
| CN106232222A (en) * | 2014-04-18 | 2016-12-14 | 卡萨尔公司 | Isothermal tubulose catalytic reactor |
| CN206986062U (en) * | 2017-07-13 | 2018-02-09 | 南京国昌化工科技有限公司 | A kind of device of methanol-fueled CLC |
| CN108404821A (en) * | 2018-05-22 | 2018-08-17 | 中石化宁波工程有限公司 | A kind of energy-saving and high efficient radial direction methanol reactor |
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2018
- 2018-09-30 CN CN201811160837.7A patent/CN109173937B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4714592A (en) * | 1984-01-18 | 1987-12-22 | Toyo Engineering Corporation | Radial flow catalytic reactor including heat exchange apparatus within the bed |
| CN1623644A (en) * | 2003-12-06 | 2005-06-08 | 杭州林达化工科技有限公司 | Process and equipment for internal heat exchanging catalytic reaction |
| CN102836676A (en) * | 2012-09-28 | 2012-12-26 | 神华集团有限责任公司 | Gas-solid phase catalytic reactor |
| CN106232222A (en) * | 2014-04-18 | 2016-12-14 | 卡萨尔公司 | Isothermal tubulose catalytic reactor |
| CN205235934U (en) * | 2015-12-16 | 2016-05-18 | 河南顺达化工科技有限公司 | Adiabatic ethanol synthesis reactor |
| CN206986062U (en) * | 2017-07-13 | 2018-02-09 | 南京国昌化工科技有限公司 | A kind of device of methanol-fueled CLC |
| CN108404821A (en) * | 2018-05-22 | 2018-08-17 | 中石化宁波工程有限公司 | A kind of energy-saving and high efficient radial direction methanol reactor |
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