CN205347278U - Synthetic methyl nitrite's device - Google Patents
Synthetic methyl nitrite's device Download PDFInfo
- Publication number
- CN205347278U CN205347278U CN201521145219.7U CN201521145219U CN205347278U CN 205347278 U CN205347278 U CN 205347278U CN 201521145219 U CN201521145219 U CN 201521145219U CN 205347278 U CN205347278 U CN 205347278U
- Authority
- CN
- China
- Prior art keywords
- tower
- methanol
- import
- outlet
- pipeline
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model provides a synthetic methyl nitrite's device, including esterification column (3) and scrubbing tower (4), esterification column (3) lower part is provided with first import (31), second import (32), esterification column (3) top is provided with gas outlet (33), gas outlet (33) are connected with scrubbing tower (4) import (41) through the pipeline, esterification column (3) are provided with methyl alcohol import (34), esterification column (3) bottom is provided with liquid phase export (35), the top of scrubbing tower (4) is provided with methyl nitrite finished product gas outlet (42), be provided with methyl alcohol washing liquid import (43) on scrubbing tower (4), scrubbing tower (4) are provided with washing liquid export (44), washing liquid export (44) is connected with the washing liquid import (36) that sets up on esterification column (3) through the pipeline. Its advantage lies in: utilize the speed gassing body of the effectual recovery processing of less equipment and goods and materials, make and discharge the gaseous requirement of satisfying the environmental protection totally and discharging, and this device production technology is stable, and very ideal of efficiency is produced to methyl nitrite dirt, and does not need other restock NO in this device to it produces the cost further to have reduced dirt.
Description
Technical field
This utility model relates to the synthesis device of a kind of chemical combination product, especially a kind of device synthesizing methyl nitrite.
Background technology
Methyl nitrite, English name: methylnitrite, molecular formula: CH3O-NO, is a kind of colourless, odorless gas under normal temperature and pressure.Fusing point-17 DEG C, boiling point-12 DEG C.Facile hydrolysis discharges nitrous acid.Its steam can form explosive mixture with air.Irradiated by sunlight or be heated and all easily decompose, have the danger blasted.Preparation for the medicines such as organic synthesis medium vessels diastole agent and explosive.Current industrialized coal-ethylene glycol route all introduces methyl nitrite, namely first pass through nitric oxide, oxygen reacts generation methyl nitrite with methanol, then methyl nitrite and carbon monoxide coupling react generation dimethyl oxalate., and Hydrogenation of Dimethyl Oxalate reaction generates ethylene glycol.This route reaction mild condition, flow process are short, reduced investment, but the emphasis being rationally recycled as device economy of periodic off-gases and acid waste water in esterification, and practical it is intended to utilize less equipment and goods and materials, configured by rational flow process, play energy-saving and cost-reducing purpose.
Existing a kind of application number is that CN201210314836.X name is called that the Chinese invention patent application of " a kind of process unit producing methyl nitrite " discloses a kind of structure, its structure includes reactive distillation column, pre-reactor, preheater, reboiler, Methanol Recovery dashpot and acid tank, the built-in condenser of reactive distillation column, described pre-reactor, preheater, reactive distillation column, reboiler and Methanol Recovery dashpot are sequentially connected, the input of pre-reactor connects with the NO circulating air pipeline in carbonylation operation and oxygen pipeline respectively, oxygen pipeline is provided with air-separating plant, the two ends of recooler communicate with described condenser and reactive distillation column respectively, recooler one end is connected with carbonylation system, acid tank input port is connected with acid water pipe and technique hose respectively, it is respectively equipped with the first circulating pump and the second circulating pump between described Methanol Recovery dashpot and described acid tank and reactive distillation column.This invention simplifies process unit, has saved production equipment and has reduced production cost.But its shortcoming is technique or more complicated, production technology is not as stable, so its structure needs to improve.
Summary of the invention
Technical problem to be solved in the utility model is to provide a kind of device synthesizing methyl nitrite for above-mentioned prior art present situation, existing methyl nitrite synthesis flow introduces methanol wash column tower, utilize less equipment effectively reclaim and process periodic off-gases, make discharge gas fully meet environmental requirement.
The technical scheme that the above-mentioned technical problem of this utility model solution adopts is: the device of this synthesis methyl nitrite, include esterification column and scrubbing tower, it is characterized in that, described esterification column bottom is provided with the first import that oxygen is connected with the mixture pipe of nitrogen, with come from the second import that carbonylation circulating air is connected, described esterification column top is provided with the gas outlet of methyl nitrite gas and unreacting gas, described gas outlet is connected by the import of pipeline with scrubbing tower bottom, described esterification column top is provided with methanol import, it is provided with liquid-phase outlet bottom described esterification column, the top of described scrubbing tower is provided with methyl nitrite finished product gas outlet, described scrubbing tower is provided with methanol cleaning mixture import, the bottom of described scrubbing tower is provided with cleaning mixture outlet, the outlet of described cleaning mixture is connected with the cleaning mixture import being arranged on esterification column by pipeline.
As improvement, described methanol import is connected by the vapour-liquid outlet of pipeline and the first methanol bathing tower bottom, the bottom of described first methanol bathing tower is provided with the air intlet communicated with air and comes from the circulating air import of carbonylation circulating air, the top of described first methanol bathing tower is provided with gaseous phase outlet, described gaseous phase outlet is connected by the lower inlet of pipeline and the second methanol bathing tower bottom, described second methanol bathing tower top is provided with and methanol solution import, the emptying gas outlet meeting discharge standard it is provided with at the top of the second methanol bathing tower, the bottom of the second methanol bathing tower is provided with mixture export, described mixture export is connected by pipeline and the first methanol bathing tower top inlet port.
As improvement, the outlet of described cleaning mixture is connected with the triple feed inlet of esterification column after esterification heat exchanger cooling by pipeline one tunnel and is back in esterification column and carries out esterification, another road is connected with the upper inlet of carbon monoxide stripping tower, the bottom of described carbon monoxide stripping tower is provided with carbon monoxide air inlet, the top of described carbon monoxide stripping tower is provided with the mixed gas outlet of the methyl nitrite gas after carbon monoxide air stripping and unreacting gas, described mixed gas outlet is connected by the lower inlet of pipeline with scrubbing tower bottom, the bottom of described carbon monoxide stripping tower is provided with the gas-liquid mixed of methyl nitrite gas and unreacting gas and exports.
As improvement, the outlet of described gas-liquid mixed is connected with nitrate reductase heater inlet by pipeline, the outlet of nitrate reductase heater is connected with the first import of nitrate reductase tower by pipeline, described nitrate reductase tower bottom is provided with the second import of nitrate reductase tower, described nitrate reductase tower the second import is connected with carbonylation circulating air by pipeline, the top of described nitrate reductase tower is provided with the mixed gas outlet that gas and unreacted after reduction are complete, described mixed gas outlet is connected with the 4th import of esterification column by pipeline, the bottom of described nitrate reductase tower is provided with the nitrate reductase tower liquid-phase outlet after reduction.
As improvement, described nitrate reductase tower liquid-phase outlet is connected with the first import of methanol distillation column by pipeline, the top of described methanol distillation column is provided with methanol gas outlet, the outlet of described methanol gas is connected with the methanol eddy tank import of methanol eddy tank through methanol condenser by pipeline, the bottom of described methanol eddy tank is provided with the outlet of methanol eddy tank, the outlet of described methanol eddy tank is connected with the second import of methanol distillation column by pipeline, the bottom of described methanol distillation column is provided with methanol distillation column liquid-phase outlet, described methanol distillation column liquid-phase outlet is connected with sewage disposal portion by pipeline.
Compared with prior art, the utility model has the advantage of: in existing methyl nitrite synthesis flow, introduce methanol wash column tower, utilize less equipment and goods and materials effectively to recycle periodic off-gases body, make discharge gas fully meet the requirement of environment protection emission；And this device stable processing technique, methyl nitrite production efficiency is very good, further, this utility model introduces carbon monoxide gas and mentions nitrate reductase equipment, makes by-product nitric acid obtain sufficient recycling, decrease consumption of raw materials, in the sewage of discharge, nitric acid content is less than 0.1%, complies fully with the requirement of GB, and does not need in this device to be additionally supplemented with NO, thus reduce further production cost, then improve 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 synthesis methyl nitrite of the present embodiment, include esterification column 3 and scrubbing tower 4, described esterification column 3 bottom is provided with the first import 31 that oxygen is connected with the mixture pipe d of nitrogen, with come from the second import 32 that carbonylation circulating air is connected, described esterification column 3 top is provided with the gas outlet 33 of methyl nitrite gas and unreacting gas, described gas outlet 33 is connected with the import 41 of scrubbing tower 4 bottom by pipeline, described esterification column 3 top is provided with methanol import 34, it is provided with liquid-phase outlet 35 bottom described esterification column 3, the top of described scrubbing tower 4 is provided with methyl nitrite finished product gas outlet 42, described scrubbing tower 4 is provided with methanol cleaning mixture import 43, the bottom of described scrubbing tower 4 is provided with cleaning mixture outlet 44, described cleaning mixture outlet 44 is connected with the cleaning mixture import 36 being arranged on esterification column 3 by pipeline.Described methanol import 34 is connected by the vapour-liquid outlet 11 bottom pipeline and the first methanol bathing tower 1, the bottom of described first methanol bathing tower 1 is provided with the air intlet 12 communicated with air and the circulating air import 13 coming from carbonylation circulating air, the top of described first methanol bathing tower 1 is provided with gaseous phase outlet 14, described gaseous phase outlet 14 is connected by the lower inlet 21 of pipeline and the second methanol bathing tower 2 bottom, described second methanol bathing tower 2 top is provided with and methanol solution import 22, the emptying gas outlet 23 meeting discharge standard it is provided with at the top of the second methanol bathing tower 2, the bottom of the second methanol bathing tower 2 is provided with mixture export 24, described mixture export 24 is connected by pipeline and the first methanol bathing tower 1 top inlet port 15.Described cleaning mixture outlet 44 is connected with the triple feed inlet 37 of esterification column 3 after esterification heat exchanger a cooling by pipeline one tunnel and is back in esterification column 3 and carries out esterification, another road is connected with the upper inlet 51 of carbon monoxide stripping tower 5, the bottom of described carbon monoxide stripping tower 5 is provided with carbon monoxide air inlet 52, the top of described carbon monoxide stripping tower 5 is provided with the mixed gas outlet 53 of the methyl nitrite gas after carbon monoxide air stripping and unreacting gas, described mixed gas outlet 53 is connected with the lower inlet 45 of scrubbing tower 4 bottom by pipeline, the bottom of described carbon monoxide stripping tower 5 is provided with the gas-liquid mixed outlet 54 of methyl nitrite gas and unreacting gas.Described gas-liquid mixed outlet 54 is connected with nitrate reductase heater b import by pipeline, the outlet of nitrate reductase heater b is connected with the first import 61 of nitrate reductase tower 6 by pipeline, described nitrate reductase tower 6 bottom is provided with nitrate reductase tower the second import 62, described nitrate reductase tower the second import 62 is connected with carbonylation circulating air by pipeline, the top of described nitrate reductase tower 6 is provided with the mixed gas outlet 63 that gas and unreacted after reduction are complete, described mixed gas outlet 63 is connected with the 4th import 38 of esterification column 3 by pipeline, the bottom of described nitrate reductase tower 6 is provided with the nitrate reductase tower liquid-phase outlet 64 after reduction.Described nitrate reductase tower liquid-phase outlet 64 is connected with the first import 71 of methanol distillation column 7 by pipeline, the top of described methanol distillation column 7 is provided with methanol gas outlet 72, described methanol gas outlet 72 is connected with the methanol eddy tank import 81 of methanol eddy tank 8 through methanol condenser e by pipeline, the bottom of described methanol eddy tank 8 is provided with methanol eddy tank outlet 82, described methanol eddy tank outlet 82 is connected with the second import 73 of methanol distillation column 7 by pipeline, the bottom of described methanol distillation column 7 is provided with methanol distillation column liquid-phase outlet 74, described methanol distillation column liquid-phase outlet 74 is connected with sewage disposal portion by pipeline.Esterification column 3 in this device is preferably reactive distillation column.Can certainly be the other kinds of reactor that can realize synthetic reaction, specifically can determine by designing requirement.
Following device is described further,
1, the production system of synthesis methyl nitrite as shown in Figure 1, (the first methanol wash column tower is namely referred to including esterification column, scrubbing tower, methanol wash column tower I, as follows), methanol wash column tower II (namely referring to the second methanol wash column tower, as follows), CO stripping tower, nitrate reductase tower, methanol distillation column, esterification heat exchanger, nitrate reductase heater, methanol condenser, methanol eddy tank.
2, communicating from the circulating air of carbonylation with esterification column bottom, oxygen, nitrogen communicate with esterification column bottom, and the outlet of esterification column top gas phase communicates with scrubbing tower lower entrances.Scrubbing tower top gaseous phase outlet circulating air removes oxonation, and methanol communicates with scrubbing tower upper entrance, and wash tower bottoms liquid-phase outlet communicates with esterification column upper entrance.Periodic off-gases communicates with methanol wash column tower I lower entrances, air enters methanol wash column tower I bottom, communicate with esterification column upper entrance bottom methanol wash column tower I, the outlet of methanol wash column tower I top gas phase communicates with methanol wash column tower II bottom, methanol communicates with methanol wash column tower II top, communicating with methanol wash column tower I top bottom methanol wash column tower II, methanol wash column tower II top is towards air emptying.The outlet of esterification column bottom liquid phases communicates with esterification heat exchanger, and esterification heat exchanger communicates with esterification column top.The outlet of esterification column bottom liquid phases communicates with CO stripping tower top, CO and CO stripping tower bottom communicates, the outlet of CO stripper-overhead communicates with scrubbing tower bottom, and the outlet of CO stripping tower bottom liquid phases communicates with nitrate reductase heater, and nitrate reductase heater outlet communicates with nitrate reductase tower upper entrance.Communicating from carbonylation circulating air with nitrate reductase tower lower entrances, the outlet of nitrate reductase top of tower communicates with esterification column lower entrances, and nitrate reductase tower bottom liquid-phase outlet communicates with methanol distillation column lower entrances.Methanol distillation column top exit communicates with methanol condenser, methanol condenser communicates with methanol eddy tank, the outlet of methanol eddy pot bottom communicates with methanol distillation column top, the gaseous phase outlet emptying of methanol eddy tank top, and methanol distillation column bottom liquid phases outlet decontaminated water processes.
The method that 3, the production system of above-mentioned synthesis methyl nitrite is used for producing methyl nitrite is as follows.
Circulating air from carbonylation enters esterification column with oxygen, nitrogen, and the methanol entered with top reacts, and generates methyl nitrite, esterification reaction temperature scope 30～80 DEG C, reaction pressure scope 0.2～0.5MPa (G).The gaseous component generated and unreacted inert component enter scrubbing tower bottom from esterification column top exit.Oxonation, scrubbing tower temperature range 20～70 DEG C, pressure limit 0.2～0.5MPa (G) is removed after methanol washs.Wash tower bottoms liquid phase enters esterification column.Balancing each other for maintaining system gas, arrange periodic off-gases emission point before esterification column on circulating air pipeline, discharge gas enters methanol wash column tower I, and air blasts methanol wash column tower I simultaneously, and top gas phase outlet enters methanol wash column tower II, and methanol wash column tower I bottom liquid phases enters esterification column.Low-temp methanol enters methanol wash column tower II, the periodic off-gases emptying after methanol wash column tower II processes, and bottom liquid phases enters methanol wash column tower I, methanol wash column tower II temperature range-10～10.Esterification column bottom liquid phases exit portion returns to esterification column after heat exchange, and remainder enters CO stripping tower, and the gas phase after air stripping enters scrubbing tower, enters nitrate reductase tower after liquid phase is heated, and CO enters scrubbing tower bottom.Part circulating air enters nitrate reductase tower, under the effect of catalyst, there is nitrate reductase reaction, top gas phase enters esterification column, nitrate reductase tower bottom liquid phase enters methanol distillation column, nitrate reductase temperature range 50～120 DEG C, reaction pressure scope 0.2～0.5MPa (G), regulate reaction temperature by inlet heater.Being recycled from the methanol in nitrate reductase tower liquid phase by methanol distillation column, Methanol Recovery tower bottom waste water decontaminated water processes.Methanol distillation column temperature range 80～180 DEG C, reaction pressure scope 0.2～0.5MPa (G).
Claims (5)
1. the device synthesizing methyl nitrite, include esterification column (3) and scrubbing tower (4), it is characterized in that, described esterification column (3) bottom is provided with the first import (31) that oxygen is connected with the mixture pipe (d) of nitrogen, with come from the second import (32) that carbonylation circulating air is connected, described esterification column (3) top is provided with the gas outlet (33) of methyl nitrite gas and unreacting gas, described gas outlet (33) is connected with the import (41) of scrubbing tower (4) bottom by pipeline, described esterification column (3) top is provided with methanol import (34), described esterification column (3) bottom is provided with liquid-phase outlet (35), the top of described scrubbing tower (4) is provided with methyl nitrite finished product gas outlet (42), described scrubbing tower (4) is provided with methanol cleaning mixture import (43), the bottom of described scrubbing tower (4) is provided with cleaning mixture outlet (44), described cleaning mixture outlet (44) is connected with the cleaning mixture import (36) being arranged on esterification column (3) by pipeline.
2. device according to claim 1, it is characterized in that: described methanol import (34) is connected by vapour-liquid outlet (11) of pipeline and the first methanol bathing tower (1) bottom, the bottom of described first methanol bathing tower (1) is provided with the air intlet (12) communicated with air and the circulating air import (13) coming from carbonylation circulating air, the top of described first methanol bathing tower (1) is provided with gaseous phase outlet (14), described gaseous phase outlet (14) is connected by the lower inlet (21) of pipeline and the second methanol bathing tower (2) bottom, described second methanol bathing tower (2) top is provided with and methanol solution import (22), emptying gas outlet (23) meeting discharge standard it is provided with at the top of the second methanol bathing tower (2), the bottom of the second methanol bathing tower (2) is provided with mixture export (24), described mixture export (24) is connected by pipeline and the first methanol bathing tower (1) top inlet port (15).
3. device according to claim 2, it is characterized in that: described cleaning mixture outlet (44) is connected and is back in esterification column (3) and carries out esterification with the triple feed inlet (37) of esterification column (3) by pipeline one tunnel after esterification heat exchanger (a) cooling, another road is connected with the upper inlet (51) of carbon monoxide stripping tower (5), the bottom of described carbon monoxide stripping tower (5) is provided with carbon monoxide air inlet (52), the top of described carbon monoxide stripping tower (5) is provided with the mixed gas outlet (53) of the methyl nitrite gas after carbon monoxide air stripping and unreacting gas, described mixed gas outlet (53) is connected with the lower inlet (45) of scrubbing tower (4) bottom by pipeline, the bottom of described carbon monoxide stripping tower (5) is provided with the gas-liquid mixed of methyl nitrite gas and unreacting gas and exports (54).
4. device according to claim 3, it is characterized in that: described gas-liquid mixed outlet (54) is connected with nitrate reductase heater (b) import by pipeline, the outlet of nitrate reductase heater (b) is connected with first import (61) of nitrate reductase tower (6) by pipeline, described nitrate reductase tower (6) bottom is provided with nitrate reductase tower the second import (62), described nitrate reductase tower the second import (62) is connected with carbonylation circulating air by pipeline, the top of described nitrate reductase tower (6) is provided with the mixed gas outlet (63) that gas and unreacted after reduction are complete, described mixed gas outlet (63) is connected with the 4th import (38) of esterification column (3) by pipeline, the bottom of described nitrate reductase tower (6) is provided with nitrate reductase tower liquid-phase outlet (64) after reduction.
5. device according to claim 4, it is characterized in that: described nitrate reductase tower liquid-phase outlet (64) is connected with first import (71) of methanol distillation column (7) by pipeline, the top of described methanol distillation column (7) is provided with methanol gas outlet (72), described methanol gas outlet (72) is connected with methanol eddy tank import (81) of methanol eddy tank (8) through methanol condenser (e) by pipeline, the bottom of described methanol eddy tank (8) is provided with methanol eddy tank outlet (82), described methanol eddy tank outlet (82) is connected with second import (73) of methanol distillation column (7) by pipeline, the bottom of described methanol distillation column (7) is provided with methanol distillation column liquid-phase outlet (74), described methanol distillation column liquid-phase outlet (74) is connected with sewage disposal portion by pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201521145219.7U CN205347278U (en) | 2015-12-30 | 2015-12-30 | Synthetic methyl nitrite's device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201521145219.7U CN205347278U (en) | 2015-12-30 | 2015-12-30 | Synthetic methyl nitrite's device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205347278U true CN205347278U (en) | 2016-06-29 |
Family
ID=56172886
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201521145219.7U Active CN205347278U (en) | 2015-12-30 | 2015-12-30 | Synthetic methyl nitrite's device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205347278U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106883127A (en) * | 2017-04-14 | 2017-06-23 | 高化学（江苏）化工新材料有限责任公司 | A kind of device for continuously generating methyl nitrite |
| CN106904714A (en) * | 2017-02-14 | 2017-06-30 | 新疆天智辰业化工有限公司 | Nitrate reductase purification technique in coal-ethylene glycol production |
| CN107033004A (en) * | 2017-05-31 | 2017-08-11 | 西安汉术化学工程股份有限公司 | Nitrate reductase method in methyl nitrite preparation process |
| CN107793316A (en) * | 2017-12-05 | 2018-03-13 | 中国科学院大连化学物理研究所 | A kind of method of microreactor synthesis methyl nitrite |
-
2015
- 2015-12-30 CN CN201521145219.7U patent/CN205347278U/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106904714A (en) * | 2017-02-14 | 2017-06-30 | 新疆天智辰业化工有限公司 | Nitrate reductase purification technique in coal-ethylene glycol production |
| CN106883127A (en) * | 2017-04-14 | 2017-06-23 | 高化学（江苏）化工新材料有限责任公司 | A kind of device for continuously generating methyl nitrite |
| CN106883127B (en) * | 2017-04-14 | 2019-03-05 | 高化学（江苏）化工新材料有限责任公司 | A kind of device continuously generating methyl nitrite |
| CN107033004A (en) * | 2017-05-31 | 2017-08-11 | 西安汉术化学工程股份有限公司 | Nitrate reductase method in methyl nitrite preparation process |
| CN107793316A (en) * | 2017-12-05 | 2018-03-13 | 中国科学院大连化学物理研究所 | A kind of method of microreactor synthesis methyl nitrite |
| CN107793316B (en) * | 2017-12-05 | 2020-04-07 | 中国科学院大连化学物理研究所 | Method for synthesizing methyl nitrite by microreactor |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN205347278U (en) | Synthetic methyl nitrite's device | |
| RU2659069C1 (en) | Method and system of devices for producing dimethyloxalate by carbonylation of industrial synthesis gas under medium-high and high pressure and production of ethylene glycol by hydration of dimethyloxalate | |
| CN106631759B (en) | A kind of system and method producing methacrylic acid coproducing methyl methacrylaldehyde | |
| WO2021078239A1 (en) | Gas-liquid bubbling bed reactor, reaction system and method for synthesizing carbonate | |
| US20110288343A1 (en) | Method for synthesizing polyoxymethylene dimethyl ethers catalyzed by an ionic liquid | |
| CN104761429B (en) | A kind of method for producing dimethyl carbonate and ethylene glycol | |
| JP2015067610A (en) | Reaction system and method for producing polymethoxy dimethyl ether | |
| CN101357890A (en) | Methyl carbonate synthesis and refining technique using heat pump technique and apparatus thereof | |
| CN205188178U (en) | Methyl nitrite's regenerating unit system in synthetic gas system ethylene glycol technology | |
| CN106588667A (en) | Regeneration process and regeneration device system of methyl nitrite in process for preparation of ethylene glycol from synthesis gas | |
| CN101925387B (en) | Reflux condenser | |
| CN106414422A (en) | Apparatus and method for producing cyclic carbonate | |
| CN106928021A (en) | A kind of method of preparing ethylene glycol by using dimethyl oxalate plus hydrogen | |
| CN102850216B (en) | Dimethyl oxalate production device | |
| CN103804142A (en) | System and method used for preparing glycol via hydrogenation of oxalic ester | |
| CN110218151A (en) | A kind of device and method that tower reactor Flash Type heat pump reactive distillation prepares propyl propionate | |
| CN105272859A (en) | Production method for alkyl nitrite | |
| CN107033004A (en) | Nitrate reductase method in methyl nitrite preparation process | |
| CN106608865B (en) | Power-economizing method for ethylene carbonate Lipase absobed | |
| CN206731083U (en) | A kind of synthesis gas preparing ethylene glycol technique nitrate reductase purifying column | |
| CN102964248B (en) | Method for producing nitric oxide and synthesizing dimethyl oxalate through carbonylation | |
| CN110483282B (en) | Device and method for producing high-concentration ethylene glycol diacetate | |
| CN112876371A (en) | Method for simultaneously producing bis (dimethylaminoethyl) ether and tetramethylethylenediamine | |
| CN101367733B (en) | Heat pump distillation apparatus and process for diethyl carbonate | |
| CN107353206B (en) | Production method and system of dimethyl carbonate with recyclable ester exchange catalyst |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP03 | Change of name, title or address |
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. |