CN112044363A - Coupling reactor for producing ethylene glycol from coal - Google Patents
Coupling reactor for producing ethylene glycol from coal Download PDFInfo
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- CN112044363A CN112044363A CN202010892129.3A CN202010892129A CN112044363A CN 112044363 A CN112044363 A CN 112044363A CN 202010892129 A CN202010892129 A CN 202010892129A CN 112044363 A CN112044363 A CN 112044363A
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- distributor
- collector
- refrigerant
- pipe
- pipes
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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
- B01J8/0285—Heating or cooling the reactor
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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
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention discloses a coupling reactor for producing coal-made ethylene glycol, which relates to the technical field of coal-made ethylene glycol production.A reactor body is provided with a material gas inlet, a synthesis gas outlet, a refrigerant outlet and a refrigerant inlet, wherein the refrigerant inlet, a refrigerant distributor, a heat exchange spiral plate, a refrigerant steam collector and the refrigerant outlet are sequentially communicated, and the external space of a cavity of the heat exchange spiral plate is a catalytic reaction zone; the refrigerant distributor comprises a distributor main pipe, distributor branch pipes, a distributor ring pipe and a distributor outlet pipe, wherein the distributor main pipe is communicated with the refrigerant inlet, the distributor main pipe is respectively communicated with the distributor ring pipe through the five distributor branch pipes, and the distributor ring pipe is communicated with the heat exchange spiral plate through the distributor outlet pipe; the refrigerant vapor collector comprises a collector inlet pipe, a collector ring pipe, collector branch pipes and a collector main pipe, and the structure of the refrigerant vapor collector is similar to that of the refrigerant distributor. The invention has the advantages that: the heat exchange efficiency of the heat exchange spiral plate is improved; the temperature of the catalytic reaction zone is uniform, and the coupling reaction effect is better.
Description
Technical Field
The invention relates to the technical field of coal-to-ethylene glycol production, in particular to a coupling reactor for coal-to-ethylene glycol production.
Background
The first step of the process route for producing the coal-to-ethylene glycol is coupling reaction to generate dimethyl oxalate, and the second step is hydrogenation of the dimethyl oxalate to produce the ethylene glycol. The coupling reactor is a large-scale device for synthesizing dimethyl oxalate. The coupling reactors in the prior art are various, and the structural common point between the coupling reactors is that a steel pipe is used as a heat exchange element, but the heat exchange efficiency is low. It is needed to provide a coupling reactor for producing ethylene glycol from coal, so as to improve the heat exchange efficiency.
Disclosure of Invention
The invention aims to solve the technical problem of providing a coupling reactor for producing ethylene glycol from coal, which can solve the problem of low heat exchange efficiency caused by adopting a steel pipe as a heat exchange element in the prior art.
In order to solve the technical problems, the technical scheme of the invention is as follows: the reactor comprises a skirt and a reactor body, wherein the skirt is arranged at the bottom of the reactor body, the reactor body comprises a lower seal head, a cylinder body and an upper seal head, a material gas inlet is formed in the top of the upper seal head of the reactor body, a synthesis gas outlet is formed in the bottom of the lower seal head of the reactor body, a refrigerant outlet is formed in the side edge of the upper part of the cylinder body, a refrigerant inlet is formed in the side edge of the lower part of the cylinder body, the refrigerant inlet is communicated with a refrigerant distributor, the refrigerant outlet is communicated with a refrigerant steam collector, a heat exchange spiral plate is arranged between the cold coal distributor and the refrigerant steam collector, the refrigerant distributor, the refrigerant steam collector and the heat exchange spiral plate are all arranged in the cylinder body, a cavity is formed inside the heat exchange spiral plate, and the space;
the refrigerant distributor comprises a distributor main pipe, distributor branch pipes, distributor ring pipes and distributor outlet pipes, wherein the distributor main pipe is communicated with a refrigerant inlet, the distributor main pipe is arranged in an L shape, five distributor ring pipes which are arranged concentrically are transversely arranged above the distributor main pipe, the side edge of the distributor main pipe is communicated with the five distributor branch pipes, the distributor branch pipes are in an L shape, each distributor branch pipe is respectively communicated with one distributor ring pipe, the top of each distributor ring pipe is communicated with a plurality of distributor outlet pipes, and the plurality of distributor outlet pipes are respectively communicated with the bottoms of the inner cavities of the heat exchange spiral plates;
the refrigerant steam collector comprises collector inlet pipes, collector ring pipes, collector branch pipes and a collector main pipe, wherein the collector main pipe is communicated with a refrigerant outlet, the collector main pipe is arranged in an L shape, the five concentrically arranged collector ring pipes are arranged below the collector main pipe in parallel with the distributor ring pipe, the side edge of the collector main pipe is communicated with the five collector branch pipes, the collector branch pipes are in an L shape, each collector branch pipe is respectively communicated with one collector ring pipe, the bottom of each collector ring pipe is communicated with a plurality of collector inlet pipes, and the plurality of collector inlet pipes are respectively communicated with the top of an inner cavity of the heat exchange spiral plate.
Furthermore, a supporting grid is arranged in the cylinder body, is arranged above the refrigerant inlet and is positioned below the branch pipe of the distributor, and is supported by four supporting ribs at the bottom, a lower ceramic ball layer is arranged above the supporting grid and is arranged below the heat exchange spiral plate, and an upper ceramic ball layer is arranged above the heat exchange spiral plate.
Further, different spiral sections formed by the heat exchange spiral plates are separated by spiral plate spacing retainers.
After adopting the structure, the invention has the advantages that: the heat exchange spiral plate is used as a heat exchange element, so that the heat exchange area is increased, the heat exchange efficiency can be greatly improved, the volume of the reactor can be reduced, the manufacturing cost of equipment is reduced, and in addition, compared with a tubular reactor, two thick tube plates are omitted, and the manufacturing cost is greatly saved;
according to the structural characteristics of the heat exchange spiral plate, the refrigerant distributor is arranged at the refrigerant inlet, the refrigerant steam collector is arranged at the refrigerant outlet, the purpose of opening an inlet and an outlet on the plate with equal arc length of the heat exchange spiral plate is achieved by adopting the structure, the refrigerant is uniformly conveyed into different positions of the inner cavity of the heat exchange spiral plate, so that the refrigerant in the inner cavity of the heat exchange spiral plate flows uniformly, the temperature of a catalytic reaction area is uniform, and the coupling reaction effect is better.
Drawings
FIG. 1 is a schematic structural view of the present invention;
FIG. 2 is a cross-sectional view A-A of FIG. 1;
fig. 3 is a sectional view B-B of fig. 1.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings.
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be described in detail with reference to the accompanying drawings and the detailed description. The following examples are presented to enable one of ordinary skill in the art to more fully understand the present invention and are not intended to limit the scope of the embodiments described herein.
As shown in fig. 1 to fig. 3, the following technical solutions are adopted in the present embodiment: the device comprises a skirt 2 and a reactor body, wherein the skirt 2 is arranged at the bottom of the reactor body, the skirt 2 is a bearing component and is used for supporting the weight of the whole device, an inspection hole 1 is formed in the side surface of the skirt 2, the reactor body is composed of a lower seal head 3, a cylinder 7 and an upper seal head 9, a material gas inlet 10 is formed in the top of the upper seal head 9 of the reactor body, a manhole 19 is further formed in the upper seal head 9, a synthesis gas outlet 17 is formed in the bottom of the lower seal head 3 of the reactor body, a discharge opening 20 is further formed in the lower seal head 3, a refrigerant outlet 11 is formed in the side edge of the upper part of the cylinder 7, a refrigerant inlet 16 is formed in the side edge of the lower part of the cylinder 7, the refrigerant inlet 16 is communicated with a refrigerant distributor 15, the refrigerant outlet 11 is communicated with a refrigerant steam collector 12, a heat exchange spiral plate 14 is arranged between the refrigerant distributor 15 and, the inside cavity that is of heat transfer spiral plate 14, the catalytic reaction district 13 of cavity exterior space for filling catalyst of heat transfer spiral plate 14, through spiral plate interval retainer 18 interval between the different spiral sections that heat transfer spiral plate 14 formed, a distance for keeping 14 spiral layers of heat transfer spiral plate and spiral layer between is unanimous and stable, adopt heat transfer spiral plate 14 as heat transfer element, heat transfer area increases, can greatly improve heat exchange efficiency, heat transfer efficiency of heat transfer spiral plate 14 can be more than 50% than conventional heat exchange tube height, therefore can reduce the volume of reactor body, the cost of reduction equipment.
According to the structural characteristics of the heat exchange spiral plate 14, the refrigerant distributor 15 is arranged at the refrigerant inlet 16, the refrigerant steam collector 12 is arranged at the refrigerant outlet 11, and by adopting the structure, the purpose of opening the inlet and the outlet on the plate with equal arc length of the heat exchange spiral plate 15 is achieved, and the refrigerant is uniformly conveyed into different positions of the inner cavity of the heat exchange spiral plate, so that the refrigerant in the inner cavity of the heat exchange spiral plate 15 flows uniformly, the temperature of the catalytic reaction zone 13 is uniform, and the coupling reaction effect is better.
The refrigerant distributor 15 has the following specific structure: the heat exchanger comprises a distributor main pipe 15-1, distributor branch pipes 15-2, distributor ring pipes 15-3 and distributor outlet pipes 15-4, wherein the distributor main pipe 15-1 is communicated with a refrigerant inlet 16, the distributor main pipe 15-1 is arranged in an L shape, five distributor ring pipes 15-3 transversely arranged are arranged above the distributor main pipe 15-1, the side edge of the distributor main pipe 15-1 is communicated with the five distributor branch pipes 15-2, the distributor branch pipes 15-2 are in an L shape, each distributor branch pipe 15-2 is respectively communicated with one distributor ring pipe 15-3, the top of each distributor ring pipe 15-3 is communicated with a plurality of distributor outlet pipes 15-4, and the plurality of distributor outlet pipes 15-4 are respectively communicated with the bottoms of inner cavities of heat exchange spiral plates 14.
The refrigerant vapor collector 12 is similar to the refrigerant distributor 15 in structure, and includes the following details: comprises a collector inlet pipe 12-4, a collector loop pipe 12-3, the collector comprises collector branch pipes 12-2 and a collector main pipe 12-1, wherein the collector main pipe 12-1 is communicated with a refrigerant outlet 11, the collector main pipe 12-1 is arranged in an L shape, five collector ring pipes 12-3 arranged in parallel with a distributor ring pipe 15-3 are arranged below the collector main pipe 12-1, five collector branch pipes 12-2 are communicated with the side edge of the collector main pipe 12-1, the collector branch pipes 12-2 are in an L shape, each collector branch pipe 12-2 is respectively communicated with one collector ring pipe 12-3, the bottom of each collector ring pipe 12-3 is communicated with a plurality of collector inlet pipes 12-4, and a plurality of collector inlet pipes 12-4 are respectively communicated with the top of an inner cavity of a heat exchange spiral plate 14.
The cylinder 7 is internally provided with a supporting grid 5, the supporting grid 5 is arranged above a refrigerant inlet 16 and is positioned below a distributor branch pipe 15-2, the supporting grid 5 is supported by four supporting ribs 4 at the bottom, a lower ceramic ball layer 6 is arranged above the supporting grid 5, the lower ceramic ball layer 6 is arranged below a heat exchange spiral plate 14, an upper ceramic ball layer 8 is arranged above the heat exchange spiral plate 14, and the upper ceramic ball layer 8 and the lower ceramic ball layer 6 are arranged to prevent a catalyst 13 from losing.
The working principle is as follows: the material gas is added into the reactor body from the material gas inlet 10, passes through the upper ceramic ball layer 8 and enters the catalyst 13, the catalytic area operates under the set temperature and pressure, the material gas generates coupling reaction to generate dimethyl oxalate, namely the material gas is changed into synthetic gas containing dimethyl oxalate after catalytic reaction, and the synthetic gas passes through the lower ceramic ball layer 9 and continuously flows downwards from the synthetic gas outlet 17.
The coupling reaction is an exothermic reaction, in order to keep heat balance, the heat released by the reaction needs to be taken away, and the coupling reaction is realized by a set of heat exchange device taking a heat exchange spiral plate 14 as a core, the working process is that a refrigerant enters a distributor main pipe 15-1 from a refrigerant inlet 16, then flows into a distributor branch pipe 15-2, and then enters a distributor circular pipe 15-3, each distributor circular pipe 15-3 is provided with a plurality of distributor outlet pipes 15-4 which are communicated with the inner cavity of the heat exchange spiral plate 14, the refrigerant flows into the heat exchange spiral plate 14 through the distributor outlet pipes 15-4, the refrigerant exchanges heat with a catalytic reaction zone 13 outside the heat exchange spiral plate 14, the heat generated in the reaction process is absorbed into the refrigerant, so that the temperature of the catalytic reaction zone 13 is always kept near the set temperature, and the refrigerant becomes steam after absorbing heat and flows into a collector inlet pipe 12, then enters the collector loop 12-3, enters the collector branch pipes 12-2, and finally is collected in the collector main pipe 12-1 and flows away from the refrigerant outlet 11.
The foregoing shows and describes the general principles and features of the present invention, together with the advantages thereof. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, which are described in the specification and illustrated only to illustrate the principle of the present invention, but that various changes and modifications may be made therein without departing from the spirit and scope of the present invention, which fall within the scope of the invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (3)
1. Coupling reactor is used in production of coal system ethylene glycol, including skirt and reactor body, reactor body bottom is located to the skirt, and the reactor body comprises low head, barrel and upper cover, its characterized in that: the reactor comprises a reactor body, a material gas inlet, a synthesis gas outlet, a cooling medium distributor, a cooling medium steam collector, a heat exchange spiral plate, a catalyst filling reaction zone and a catalyst filling reaction zone, wherein the top of an upper seal head of the reactor body is provided with the material gas inlet, the bottom of a lower seal head of the reactor body is provided with the synthesis gas outlet, the side edge of the upper part of a cylinder body is provided with the cooling medium inlet, the side edge of the lower part of the cylinder body is provided with the cooling medium inlet, the cooling medium inlet is communicated with the cooling;
the refrigerant distributor comprises a distributor main pipe, distributor branch pipes, distributor ring pipes and distributor outlet pipes, wherein the distributor main pipe is communicated with a refrigerant inlet, the distributor main pipe is arranged in an L shape, five distributor ring pipes which are arranged concentrically are transversely arranged above the distributor main pipe, the side edge of the distributor main pipe is communicated with the five distributor branch pipes, the distributor branch pipes are in an L shape, each distributor branch pipe is respectively communicated with one distributor ring pipe, the top of each distributor ring pipe is communicated with a plurality of distributor outlet pipes, and the plurality of distributor outlet pipes are respectively communicated with the bottoms of the inner cavities of the heat exchange spiral plates;
the refrigerant steam collector comprises collector inlet pipes, collector ring pipes, collector branch pipes and a collector main pipe, wherein the collector main pipe is communicated with a refrigerant outlet, the collector main pipe is arranged in an L shape, the five concentrically arranged collector ring pipes are arranged below the collector main pipe in parallel with the distributor ring pipe, the side edge of the collector main pipe is communicated with the five collector branch pipes, the collector branch pipes are in an L shape, each collector branch pipe is respectively communicated with one collector ring pipe, the bottom of each collector ring pipe is communicated with a plurality of collector inlet pipes, and the plurality of collector inlet pipes are respectively communicated with the top of an inner cavity of the heat exchange spiral plate.
2. The coupling reactor for producing ethylene glycol from coal as claimed in claim 1, wherein: the improved heat exchanger is characterized in that a supporting grid is arranged in the cylinder, is arranged above the refrigerant inlet and is located below the distributor branch pipe, the supporting grid is supported by four supporting ribs at the bottom, a lower ceramic ball layer is arranged above the supporting grid, the lower ceramic ball layer is arranged below the heat exchange spiral plate, and an upper ceramic ball layer is arranged above the heat exchange spiral plate.
3. The coupling reactor for producing ethylene glycol from coal as claimed in claim 1, wherein: different spiral sections formed by the heat exchange spiral plates are spaced by spiral plate spacing retainers.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010892129.3A CN112044363B (en) | 2020-08-31 | 2020-08-31 | Coupling reactor for producing ethylene glycol from coal |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010892129.3A CN112044363B (en) | 2020-08-31 | 2020-08-31 | Coupling reactor for producing ethylene glycol from coal |
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| Publication Number | Publication Date |
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| CN112044363A true CN112044363A (en) | 2020-12-08 |
| CN112044363B CN112044363B (en) | 2022-09-13 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202010892129.3A Active CN112044363B (en) | 2020-08-31 | 2020-08-31 | Coupling reactor for producing ethylene glycol from coal |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114682171A (en) * | 2022-04-15 | 2022-07-01 | 北京海望氢能科技有限公司 | High-efficiency dehydrogenation or hydrogenation reactor and dehydrogenation or hydrogenation process system for organic liquid |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1031373A2 (en) * | 1999-02-27 | 2000-08-30 | Metallgesellschaft Aktiengesellschaft | Reactor and process for catalytic conversion of gaseous mixtures |
| CN2424435Y (en) * | 2000-06-01 | 2001-03-21 | 李大刚 | Alternating spiral sheet heat exchanger |
| DE10000584A1 (en) * | 2000-01-10 | 2001-07-12 | Basf Ag | Process for the catalytic gas phase oxidation to maleic anhydride |
| CN204220126U (en) * | 2014-11-24 | 2015-03-25 | 苏州市锦翔压力容器制造有限公司 | Spiral plate type chloroethylene synthesizing converter |
| CN104606913A (en) * | 2015-01-09 | 2015-05-13 | 西安近代化学研究所 | Device for recovering solvents of explosive modeling powder water suspension granulation process |
| CN104841339A (en) * | 2015-04-16 | 2015-08-19 | 中国五环工程有限公司 | Novel hydrogenation reactor for synthesis gas-to-ethylene glycol process |
| CN105080433A (en) * | 2015-09-02 | 2015-11-25 | 德艾柯工程技术（上海）有限公司 | Novel plate-type axial reactor |
| CN206739957U (en) * | 2017-04-05 | 2017-12-12 | 新乡市双诚环保设备有限公司 | Strake heat exchanger |
| CN110170281A (en) * | 2019-05-06 | 2019-08-27 | 新奥科技发展有限公司 | A kind of reactor |
-
2020
- 2020-08-31 CN CN202010892129.3A patent/CN112044363B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1031373A2 (en) * | 1999-02-27 | 2000-08-30 | Metallgesellschaft Aktiengesellschaft | Reactor and process for catalytic conversion of gaseous mixtures |
| DE10000584A1 (en) * | 2000-01-10 | 2001-07-12 | Basf Ag | Process for the catalytic gas phase oxidation to maleic anhydride |
| CN2424435Y (en) * | 2000-06-01 | 2001-03-21 | 李大刚 | Alternating spiral sheet heat exchanger |
| CN204220126U (en) * | 2014-11-24 | 2015-03-25 | 苏州市锦翔压力容器制造有限公司 | Spiral plate type chloroethylene synthesizing converter |
| CN104606913A (en) * | 2015-01-09 | 2015-05-13 | 西安近代化学研究所 | Device for recovering solvents of explosive modeling powder water suspension granulation process |
| CN104841339A (en) * | 2015-04-16 | 2015-08-19 | 中国五环工程有限公司 | Novel hydrogenation reactor for synthesis gas-to-ethylene glycol process |
| CN105080433A (en) * | 2015-09-02 | 2015-11-25 | 德艾柯工程技术（上海）有限公司 | Novel plate-type axial reactor |
| CN206739957U (en) * | 2017-04-05 | 2017-12-12 | 新乡市双诚环保设备有限公司 | Strake heat exchanger |
| CN110170281A (en) * | 2019-05-06 | 2019-08-27 | 新奥科技发展有限公司 | A kind of reactor |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114682171A (en) * | 2022-04-15 | 2022-07-01 | 北京海望氢能科技有限公司 | High-efficiency dehydrogenation or hydrogenation reactor and dehydrogenation or hydrogenation process system for organic liquid |
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| CN112044363B (en) | 2022-09-13 |
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Address after: 9 Huaxing Road, Jiuhua Town, Rugao City, Nantong City, Jiangsu Province, 226500 Applicant after: Jiangsu Yongda Chemical Machinery Co., Ltd. Address before: 9 Huaxing Road, Jiuhua Town, Rugao City, Nantong City, Jiangsu Province, 226500 Applicant before: JIANGSU YONGDA CHEMICAL MACHINERY CO.,LTD. |
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