CN205328897U - Device of synthetic ethylene glycol - Google Patents
Device of synthetic ethylene glycol Download PDFInfo
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- CN205328897U CN205328897U CN201521145220.XU CN201521145220U CN205328897U CN 205328897 U CN205328897 U CN 205328897U CN 201521145220 U CN201521145220 U CN 201521145220U CN 205328897 U CN205328897 U CN 205328897U
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Abstract
The utility model provides a device of synthetic ethylene glycol, including the air entrainment reactor, first condenser (4), second condenser (5), recycle hydrogen compressor (6), the air entrainment reactor includes the 1st hydrogenation ware (1) and the 2nd hydrogenation ware (3), above -mentioned equipment correspondingly links together through the structure of pipeline according to the design, be provided with the first cooler that can reduce the reaction temperature on the 1st hydrogenation ware (1), be provided with the second cooler that can reduce the reaction temperature on the 2nd hydrogenation ware (3). Compared with the prior art, the utility model discloses an advantage lie in, provide the apparatus for producing of a suitable industrialization large -scale production ethylene glycol, introduce reactor connection in series -parallel mode in the synthetic flow of ethylene glycol of this device, introduce around tubular heat exchanger simultaneously, reduced area, solved the difficult problem that the production scale maximized, reduced the energy consumption simultaneously, reduced the running cost to economic benefits has been improved effectively.
Description
Technical field
This utility model relates to the synthesis device of a kind of chemical combination product, especially the device of a kind of synthesizing glycol。
Background technology
Ethylene glycol (EthyleneGlycol, it is called for short EG) have another name called glycol, it it is the simplest and most important aliphatic dihydroxy alcohol, also it is a kind of important Organic Chemicals, can be used for producing multiple chemical products, such as polyester fiber, antifreezing agent, unsaturated polyester resin, lubricant, plasticizer, nonionic surfactant, explosive, coating and ink etc., application is widely。Chemical property is similar to ethanol, mainly can generate ester with inorganic or organic acid reaction, and general first only one of which hydroxyl reacts, and through raising temperature, increasing acid consumption etc., two hydroxyls can be made all to form ester。As with the nitric acid reaction being mixed with sulphuric acid, then form dinitrate。Acyl chlorides or anhydride easily make two hydroxyls form ester。Ethylene glycol is heating under catalyst (manganese dioxide, aluminium oxide, zinc oxide or sulphuric acid) acts on, and can occur in molecule or intermolecular dehydration。Ethylene glycol can form alkoxide with alkali metal or alkaline-earth metal effect。In process hides and pharmaceuticals industry, it is used separately as hydrating agents and solvent。The derivant dinitrate of ethylene glycol is explosive。Monomethyl ether or single ether of ethylene glycol are good solvents, such as first cellosolve HOCH2CH2OCH3 solubilized fiber, resin, paint and other many Organic substances。The solvability of ethylene glycol is very strong, but its easy metabolism oxidation, generate poisonous oxalic acid, thus solvent can not be widely used as。Ethylene glycol is an antifreeze, and the glycol water of 60%, freezing point can be reduced to-48.3 DEG C。The traditional industry production method of ethylene glycol is that epoxyethane water is legal。This route technological process length, energy consumption are high, glycol selectivity is low, and the method belongs to petrochemical industry route, and petroleum resources dependency is big, and ethylene glycol price is big with crude oil price fluctuating margin。Therefore, China of the few oil of many coals is extremely important by preparing ethylene glycol based on the Non oil-based route of natural gas or coal-based feedstocks。Synthesis gas indirect method synthesizing glycol, namely from carbon monoxide, coupling obtains oxalate diester, then through carbon one route of oxalate diester catalytic hydrogenation preparing ethylene glycol, is recently be acknowledged as technical and better economy a kind of process route。
Existing a kind of application number is that CN201310389599.8 name is called that the Chinese invention patent of " a kind of method and apparatus with coal for raw material production synthesizing glycol " discloses a kind of structure, its structure includes oxidative esterification operation, carbonylation operation and preparing ethylene glycol by using dimethyl oxalate plus hydrogen operation, also including dry decontamination equipment, described dry decontamination equipment is the saturation water in this process gas will to be dried before entering oxonation device from oxidative esterification tower process gas out。Said method, avoid methyl nitrite in process gas (MN) noxious emission of the enrichment in regenerative process and regeneration gas in adsorption tower, avoid oxonation product dimethyl oxalate. (DMO) to meet water and resolve into the oxalic acid corrosion to equipment, the long-term operation of equipment is provided guarantee, improves the high-grade-goods rate of final products ethylene glycol。But it is more complicated that shortcoming is technique, produce instability, so its structure needs to improve。
Summary of the invention
Technical problem to be solved in the utility model is to provide the device of a kind of synthesizing glycol for above-mentioned prior art present situation, the ethylene glycol synthesis flow of this device introduces reactor connection in series-parallel pattern, it is simultaneously introduced wound tube heat exchanger, reduce energy consumption, decrease floor space, solve the difficult problem that production scale maximizes。
The technical scheme that the above-mentioned technical problem of this utility model solution adopts is: the device of this synthesizing glycol, include aerating reactor, it is characterized in that: described aerating reactor includes the first hydrogenation reactor and the second hydrogenation reactor, described first hydrogenation reactor is provided with hydrogen and the air inlet of grass ester dimethyl ester gaseous mixture, described first hydrogenation reactor is provided with the ethylene glycol of synthesis and the gas liquid outlet of the complete gas of unreacted, described gas liquid outlet is connected by the import of pipeline and the first condenser, the first alcohol product flow export after the bottom of the first condenser is provided with synthesizing alcohol, not cooled and unreacted residual air mixed gas outlet it is provided with at the top of described first condenser, described mixed gas outlet is connected by pipeline and the second hydrogenation reactor import, pipeline is connected to hydrogen make pipe a between mixed gas outlet and the second hydrogenation reactor import, described first hydrogenation reactor is provided with the first cooler that can reduce reaction temperature, described second hydrogenation reactor import carries pipe to be connected by pipeline with dimethyl oxalate., the gas-liquid mixed of the ethylene glycol and the complete gas of unreacted that are provided with synthesis on described second hydrogenation reactor exports, the outlet of described gas-liquid mixed is connected by the cooling import of pipeline and the second condenser, the second alcohol product flow export after the bottom of the second condenser is provided with synthesizing alcohol, not cooled and unreacted residual air mixing gaseous phase outlet it is provided with at the top of described second condenser, described second hydrogenation reactor is provided with the second cooler that can reduce reaction temperature。
As improvement, described mixing gaseous phase outlet is connected with the import of circulating hydrogen compressor by pipeline, and the compressed gas outlet that circulating hydrogen compressor is after compression is connected with air inlet by pipeline。
As improvement, the connection pipeline of mixing gaseous phase outlet and circulating hydrogen compressor import is connected to periodic off-gases pipeline。
As improvement, the outlet of described hydrogen delivery tube and grass ester dimethyl ester letter shoot is connected in the import of same mixture pipe, and the outlet of described mixture pipe is connected with the air inlet of the first hydrogenation reaction。
As improvement, the outlet of described circulating hydrogen compressor is connected with mixture pipe by pipeline and is connected with the reaction chamber of the first hydrogenation reactor。
As improvement, described first alcohol product flow export and the second alcohol product flow export are received organ pipe road with ethylene glycol after pipeline converges and are connected。
As improvement, described first cooler includes the cooling drum for cooling down, described first hydrogenation reactor is provided with the first-class outlet of gas liquid reaction thing, described first-class outlet is connected with the cooling import in cooling drum by pipeline, the flow export of the gas liquid reaction thing after being provided with cooling on cooling drum, described flow export is connected by the second inlet port of pipeline and the first hydrogenation reactor, is provided with, on cooling drum, the vapor outlet port flashing to steam after absorbing gas liquid reaction thing temperature。
As improvement, described second cooler includes the cooling drum for cooling down, described second hydrogenation reactor is provided with the second outlet of gas liquid reaction thing, the outlet of described second is connected with the cooling entrance in cooling drum by pipeline, the outflow interface of the gas liquid reaction thing after being provided with cooling on cooling drum, described outflow interface is connected by the second entrance interface of pipeline and the second hydrogenation reactor, is provided with, on cooling drum, the vapor stream outlet flashing to steam after absorbing gas liquid reaction thing temperature。
It is same cooling drum as improvement, the cooling drum in described first cooler and the cooling drum in the second cooler。
Compared with prior art, the advantage that this utility model adopts is in that, the process units of a kind of applicable industrialization large-scale production ethylene glycol is provided, the ethylene glycol synthesis flow of this device introduces reactor connection in series-parallel pattern, it is simultaneously introduced wound tube heat exchanger, decreases floor space, solve the difficult problem that production scale maximizes, reduce energy consumption simultaneously, decrease operating cost, thus being effectively improved economic benefit。
Accompanying drawing explanation
Fig. 1 is the production equipment flowsheet of this utility model embodiment。
Detailed description of the invention
Below in conjunction with accompanying drawing embodiment, this utility model is described in further detail。
As shown in Figure 1, the device of the synthesizing glycol of the present embodiment, include aerating reactor, described aerating reactor includes the first hydrogenation reactor 1 and the second hydrogenation reactor 3, described first hydrogenation reactor 1 is provided with hydrogen and the air inlet 11 of grass ester dimethyl ester gaseous mixture, described first hydrogenation reactor 1 is provided with the ethylene glycol of synthesis and the gas liquid outlet 12 of the complete gas of unreacted, described gas liquid outlet 12 is connected by the import 41 of pipeline and the first condenser 4, the first alcohol product flow export 42 after the bottom of the first condenser 4 is provided with synthesizing alcohol, not cooled and unreacted residual air mixed gas outlet 43 it is provided with at the top of described first condenser 4, described mixed gas outlet 43 is connected by pipeline and the second hydrogenation reactor import 31, between mixed gas outlet 43 and the second hydrogenation reactor import 31, pipeline is connected to hydrogen make pipe a, described first hydrogenation reactor 1 is provided with the first cooler that can reduce reaction temperature, described second hydrogenation reactor import 31 carries pipe b to be connected by pipeline with dimethyl oxalate., described second hydrogenation reactor 3 is provided with the ethylene glycol of synthesis and the gas-liquid mixed outlet 32 of the complete gas of unreacted, described gas-liquid mixed outlet 32 is connected by the cooling import 51 of pipeline and the second condenser 5, the second alcohol product flow export 52 after the bottom of the second condenser 5 is provided with synthesizing alcohol, not cooled and unreacted residual air mixing gaseous phase outlet 53 it is provided with at the top of described second condenser 5, described second hydrogenation reactor 3 is provided with the second cooler that can reduce reaction temperature。Described mixing gaseous phase outlet 53 is connected by the import of pipeline with circulating hydrogen compressor 6, and the compressed gas outlet that circulating hydrogen compressor 6 is after compression is connected with air inlet 11 by pipeline。The connection pipeline of mixing gaseous phase outlet 53 and circulating hydrogen compressor 6 import is connected to periodic off-gases pipeline d。The outlet of described hydrogen delivery tube and grass ester dimethyl ester letter shoot is connected in the import of same mixture pipe e, and the outlet of described mixture pipe e is connected with the air inlet 11 of the first hydrogenation reaction 1。Described circulating hydrogen compressor 6 is exported and is connected with mixture pipe e by pipeline and is connected with the reaction chamber of the first hydrogenation reactor 1。Described first alcohol product flow export 12 is received organ pipe road g with ethylene glycol with the second alcohol product flow export 32 after pipeline converges and is connected。Described first cooler includes the cooling drum 2 for cooling down, described first hydrogenation reactor 1 is provided with the first-class outlet 13 of gas liquid reaction thing, described first-class outlet 13 is connected with the cooling import 21 in cooling drum 2 by pipeline, the flow export 22 of the gas liquid reaction thing after being provided with cooling on cooling drum 2, described flow export 22 is connected by the second inlet port 14 of pipeline and the first hydrogenation reactor 1, is provided with, on cooling drum 2, the vapor outlet port 23 flashing to steam after absorbing gas liquid reaction thing temperature。Described second cooler includes the cooling drum 2 for cooling down, described second hydrogenation reactor 3 is provided with the second outlet 33 of gas liquid reaction thing, described second outlet 33 is connected with the cooling entrance 24 in cooling drum 2 by pipeline, the outflow interface 25 of the gas liquid reaction thing after being provided with cooling on cooling drum 2, described outflow interface 25 is connected by the second entrance interface 34 of pipeline and the second hydrogenation reactor 3, is provided with, on cooling drum 2, the vapor stream outlet 23 flashing to steam after absorbing gas liquid reaction thing temperature。Cooling drum 2 in described first cooler and the cooling drum 2 in the second cooler are same cooling drum 2。
The utility model is described in further detail below:
1, the production system of synthesizing glycol as shown in Figure 1, (the first hydrogenation reactor is namely referred to including hydrogenation reactor I, as follows), hydrogenation reactor II (namely refer to that second adds institute's hydrogen reactor, as follows), product condenser I (namely refer to the first condenser, as follows), product condenser II (namely refer to the second condenser, as follows), circulating hydrogen compressor, drum (namely refer to cooling drum, as follows)。
2, dimethyl oxalate. is separately added into hydrogenation reactor I, hydrogenation reactor II；Recycle hydrogen enters hydrogenation reactor I, hydrogenation reactor I outlet and communicates with product condenser I entrance；Product condenser I gaseous phase outlet communicates with hydrogenation reactor II entrance；New hydrogen fills in hydrogenation reactor II, and hydrogenation reactor II outlet communicates with product condenser II entrance, and product condenser II gaseous phase outlet communicates with circulating hydrogen compressor, and circulating hydrogen compressor entrance arranges periodic off-gases emission point, and discharge capacity is 34Nm3/ t ethylene glycol, ethylene glycol drum communicates with hydrogenation reactor I/II, is used for removing steam generation by reaction heat。
The method that 3, the production system of above-mentioned synthesizing glycol is used for producing ethylene glycol is as follows:
Recycle hydrogen and dimethyl oxalate. enter from the top of hydrogenation reactor I and start reaction, generate ethylene glycol, and hydrogenation reaction temperature 160～260 DEG C, catalyst system is Cu/SiO2, react for gas phase fast reaction, response time 1～10S, product enters product condenser I, by controlling the temperature of product condenser I, is separated by the ethylene glycol of generation, the temperature range of product condenser I is 40～260 DEG C, and pressure limit is 2.0～3.3MPa (G)。Product condenser I gas phase, supplementary new hydrogen and dimethyl oxalate. enter hydrogenation reactor II, and it is 1～10: 1 that dimethyl oxalate. enters the ratio of hydrogenation reactor I/II, and hydrogenation reactor II reaction temperature 160～260 DEG C, catalyst system is Cu/SiO2, react for gas phase fast reaction, response time 1～10S, product enters product condenser II, by controlling the temperature of product condenser II, is separated by the ethylene glycol of generation, the temperature range of product condenser II is 40～260 DEG C, and pressure limit is 2.0～3.3MPa (G)。Product condenser II gaseous phase outlet enters circulating hydrogen compressor, and circulating hydrogen compressor outlet enters hydrogenation reactor I top, forms closed cycle。Circulating hydrogen compressor entrance arranges periodic off-gases emission point, and discharge capacity is 34Nm3/ t ethylene glycol, is used for hydrogen content and gas-liquid equilibrium needed for the system that maintains, and hydrogen content span of control is 90%～98%。Hydrogenation reactor I/II shares a drum, in order to remove reaction heat, and by-product 0.5MPa (G) steam。Above-mentioned hydrogen/ester ratio is: 40～100, reaction pressure 2.0～3.3MPa (G), reaction temperature 160～260 DEG C。The position that new hydrogen fills into is hydrogenation reactor II entrance, and the amount of filling into is 1600Nm3/ t ethylene glycol, new hydrogen/circulation oxygen is: 0.1245～00463。
Claims (9)
1. the device of a synthesizing glycol, include aerating reactor, it is characterized in that: described aerating reactor includes the first hydrogenation reactor (1) and the second hydrogenation reactor (3), described first hydrogenation reactor (1) is provided with hydrogen and the air inlet (11) of grass ester dimethyl ester gaseous mixture, described first hydrogenation reactor (1) is provided with the ethylene glycol of synthesis and the gas liquid outlet (12) of the complete gas of unreacted, described gas liquid outlet (12) is connected by the import (41) of pipeline and the first condenser (4), the first alcohol product flow export (42) after the bottom of the first condenser (4) is provided with synthesizing alcohol, not cooled and unreacted residual air mixed gas outlet (43) it is provided with at the top of described first condenser (4), described mixed gas outlet (43) is connected by pipeline and the second hydrogenation reactor import (31), between mixed gas outlet (43) and the second hydrogenation reactor import (31), pipeline is connected to hydrogen make pipe (a), described first hydrogenation reactor (1) is provided with the first cooler that can reduce reaction temperature, described second hydrogenation reactor import (31) is connected with dimethyl oxalate. conveying pipe (b) by pipeline, described second hydrogenation reactor (3) is provided with the ethylene glycol of synthesis and gas-liquid mixed outlet (32) of the complete gas of unreacted, described gas-liquid mixed outlet (32) is connected by the cooling import (51) of pipeline and the second condenser (5), the second alcohol product flow export (52) after the bottom of the second condenser (5) is provided with synthesizing alcohol, not cooled and unreacted residual air mixing gaseous phase outlet (53) it is provided with at the top of described second condenser (5), described second hydrogenation reactor (3) is provided with the second cooler that can reduce reaction temperature。
2. device according to claim 1, it is characterized in that: described mixing gaseous phase outlet (53) is connected by the import of pipeline with circulating hydrogen compressor (6), and the compressed gas outlet that circulating hydrogen compressor (6) is after compression is connected with air inlet (11) by pipeline。
3. device according to claim 2, it is characterised in that: on the connection pipeline of mixing gaseous phase outlet (53) and circulating hydrogen compressor (6) import, it is connected to periodic off-gases pipeline (d)。
4. device according to claim 3, it is characterized in that: the outlet of described hydrogen delivery tube and grass ester dimethyl ester letter shoot is connected in the import of same mixture pipe (e), and the outlet of described mixture pipe (e) is connected with the air inlet (11) of the first hydrogenation reactor (1)。
5. device according to claim 4, it is characterised in that: described circulating hydrogen compressor (6) outlet is connected with mixture pipe (e) by pipeline and is connected with the reaction chamber of the first hydrogenation reactor (1)。
6. device according to claim 5, it is characterised in that: described first alcohol product flow export (12) is received organ pipe road (g) with ethylene glycol with the second alcohol product flow export (32) after pipeline converges and is connected。
7. according to described device arbitrary in claim 1 to 6, it is characterized in that: described first cooler includes the cooling drum (2) for cooling down, described first hydrogenation reactor (1) is provided with the first-class outlet (13) of gas liquid reaction thing, described first-class outlet (13) is connected with the cooling import (21) in cooling drum (2) by pipeline, the flow export (22) of the gas liquid reaction thing after being provided with cooling in cooling drum (2), described flow export (22) is connected by second inlet port (14) of pipeline and the first hydrogenation reactor (1), cooling drum (2) is provided with the vapor outlet port (23) flashing to steam after absorbing gas liquid reaction thing temperature。
8. device according to claim 7, it is characterized in that: described second cooler includes the cooling drum (2) for cooling down, described second hydrogenation reactor (3) is provided with second outlet (33) of gas liquid reaction thing, described second outlet (33) is connected with the cooling entrance (24) in cooling drum (2) by pipeline, the outflow interface (25) of the gas liquid reaction thing after being provided with cooling in cooling drum (2), described outflow interface (25) is connected by the second entrance interface (34) of pipeline and the second hydrogenation reactor (3), cooling drum (2) is provided with the vapor stream outlet (23) flashing to steam after absorbing gas liquid reaction thing temperature。
9. device according to claim 8, it is characterised in that: the cooling drum (2) in described first cooler is same cooling drum (2) with the cooling drum (2) in the second cooler。
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201521145220.XU CN205328897U (en) | 2015-12-30 | 2015-12-30 | Device of synthetic ethylene glycol |
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| CN201521145220.XU CN205328897U (en) | 2015-12-30 | 2015-12-30 | Device of synthetic ethylene glycol |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105936834A (en) * | 2016-07-01 | 2016-09-14 | 北京神雾环境能源科技集团股份有限公司 | Combined system and method for processing oil gas generated by pyrolysis of low rank coal |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105936834A (en) * | 2016-07-01 | 2016-09-14 | 北京神雾环境能源科技集团股份有限公司 | Combined system and method for processing oil gas generated by pyrolysis of low rank coal |
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Address after: 315040, Zhejiang, Ningbo province Jiangdong North Road, No. 004, 435 (8-1) and creative Plaza creative court building 801 units Patentee after: Ningbo Zhongke Far East catalytic Engineering Technology Co Ltd Address before: 315040 Zhejiang Province, Ningbo City Jiangdong Road No. 435 Ningbo Hefeng creative square building 8 floor E Patentee before: Ningbo Jinyuandong Petrochemical Engineering Technology Co., Ltd. |