CN103819309A - Recycling device for exhaust gas in tower top of dehydrating tower system for production of methyl-2-buten-1-ol - Google Patents
Recycling device for exhaust gas in tower top of dehydrating tower system for production of methyl-2-buten-1-ol Download PDFInfo
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- CN103819309A CN103819309A CN201410047173.9A CN201410047173A CN103819309A CN 103819309 A CN103819309 A CN 103819309A CN 201410047173 A CN201410047173 A CN 201410047173A CN 103819309 A CN103819309 A CN 103819309A
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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
- C07C29/36—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring increasing the number of carbon atoms by reactions with formation of hydroxy groups, which may occur via intermediates being derivatives of hydroxy, e.g. O-metal
- C07C29/38—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring increasing the number of carbon atoms by reactions with formation of hydroxy groups, which may occur via intermediates being derivatives of hydroxy, e.g. O-metal by reaction with aldehydes or ketones
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
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Abstract
The invention relates to a production device, in particular to a recycling device for exhaust gas in a tower top of a dehydrating tower system for the production of methyl-2-buten-1-ol. The recycling device is characterized in that isobutene-rich gas which is discharged from the tower top of the dehydrating tower in the previous process in the production of methyl-2-buten-1-ol is fed to an overhead condenser, and is cooled with freeze saline water, and a condensate return tank is arranged at the lower part of the condenser to collect condensate from the condenser; non-condensable exhaust gas in the condenser enters a gas-liquid separator, and isobutene is further recovered; filler is packed in the middle section in the gas-liquid separator; liquid-phase washing liquid at the upper part of the gas-liquid separator is introduced from feedstock in a light-component separating column, wherein the feedstock is a process material; an exhaust gas condenser is arranged at the tower top of the dehydrating tower, and adopts saline water for cooling. The recycling device has the benefits that the exhaust discharge amount and the nitrogen supplementing amount of the tower top of the dehydrating tower system are optimally controlled; isobutene in the exhaust gas is recovered, the nitrogen consumption is reduced, pollution to the environment is reduced, and the purpose of recycling waste material is achieved.
Description
Technical field
The present invention relates to a kind of production equipment, more particularly, relate to a kind of organic chemicals prenol production equipment.
Background technology
Prenol is a kind of important organic fine chemical intermediates, has been widely used in the field such as agricultural chemicals and synthetic perfume.Along with the development of cement external additive industry, particularly carboxyl acid graft copolymer have become the study hotspot of research institution of each major company of the world, prenol product becomes the important source material of producing polycarboxylate water-reducer.In concrete production and construction, use this high-performance cement water reducer, can reduce more than 30% water consumption, strengthen concrete intensity more than 30%, simultaneously can corresponding minimizing cement consumption.
At the product of industrial synthetic prenol, main operational path has iso-butylene and formaldehyde reaction synthesis technique and Hydrolyzing Process of Chloroisopentene.Other preparation method also has the hydrolysis of isopentene ester, isoamyl
the methods such as alkene hydration, isoamyl olefine aldehydr hydrogenation.
At present, prenol product only has a certain manufacturer production of company and the China of Germany, Japan at present.Engineering construction is being done everywhere by China, and concrete requirement is huge, and high-performance cement water reducer requirement is also huge.Along with prenol industrial expansion, the progress of technology, cuts down the consumption of raw materials, carries out energy-conservation exploitation, will become the emphasis of prenol research and development.
Summary of the invention
The object of the invention is to overcome the deficiency of prior art, a kind of organic chemicals prenol production equipment is provided.
Dehydration tower system tower top tail gas recycling device in a kind of prenol production, it is characterized in that, a upper operation dehydration column overhead in prenol is produced out be rich in isobutene gas, enter overhead condenser, cooling with chilled brine, the not solidifying tail gas of condenser consists of nitrogen, iso-butylene, 23 ℃ of service temperatures, working pressure 0.2MPaG;
Condenser is provided with phlegma return tank, collects the lime set that condenser gets off;
The not solidifying tail gas of condenser enters gas-liquid separator, further reclaims iso-butylene; Filler is loaded in the inner stage casing of gas-liquid separator;
The liquid phase washings on gas-liquid separator top, draws from light component knockout tower charging, and charging is process stream, and in dehydration column overhead, portion is provided with tail gas condenser, cooling with chilled brine in tail gas condenser, is cooled to-10 ℃;
Gas-liquid separator top is provided with liquid phase shower, and shower bottom is provided with two rounds;
Gas-liquid separator bottom is provided with return tank, and gas-liquid separator bottom is provided with fluid-tight between return tank;
Gas-liquid separator bottom liquid phase isobutene logistic, is recovered in dehydration column overhead return tank; The gas phase on gas-liquid separator top, removes low low pressure flare separating tank, is discharged into flare system;
Dehydration column overhead is provided with return tank, and return tank is provided with liquid collecting bag, with isobutylene separation and water; Return tank is provided with nitrogen access tube, to be filled with nitrogen;
A upper operation dehydration column overhead in prenol is produced has pressure to divide process control system, is connected with nitrogen valve in the present invention, vent valve, can optimize the magnitude of recruitment of nitrogen and the loss that discharge brings; Dehydration tower pressure on top surface superelevation, exhaust valve opening, is discharged into flare system; When pressure is low, exhaust valve closure;
Dehydration tower pressure on top surface is ultralow, and nitrogen valve is opened, and system fills into nitrogen; Pressure superelevation, exhaust valve closure.
Beneficial effect of the present invention is, dehydration tower system tower top exhaust emissions amount and supplementary nitrogen amount are optimized to control; And the iso-butylene in tail gas is reclaimed, reduce nitrogen consumption, reduce the pollution to environment.The iso-butylene reclaiming returns to process system, continues to purify and reclaims, and supplements prenol device iso-butylene raw material.Guarantee that prenol device dehydration tower system tower top is recycled containing iso-butylene tail gas, as the raw material of this device, turn waste into wealth, make it the energy and reclaimed.
Accompanying drawing explanation
Fig. 1 schematic flow sheet of the present invention.
In figure, there are condenser 1E-401, return tank 1V-401, phlegma return tank 1V-412, gas-liquid separator 1T-412, tail gas condenser 1E-413, nitrogen valve 1PV-4104A, vent valve 1PV-4104B.
Embodiment
Below in conjunction with accompanying drawing and specific examples, the present invention is made and being described in further detail.
Take the tower top tail gas recycling device of producing dehydration tower system in 5000 tons of prenols per year as example.
As shown in the figure, a upper operation dehydration tower 1T-401 top of tower in prenol is produced out be rich in isobutene gas, enter overhead condenser 1E-401, cooling with chilled brine, the not solidifying tail gas of condenser 1E-401 consists of nitrogen 50kg/h, iso-butylene 5kg/h, 23 ℃ of service temperatures, working pressure 0.2MPaG;
The not solidifying tail gas of condenser 1E-401 enters gas-liquid separator 1T-412, further reclaims iso-butylene; Gas-liquid separator 1T-412 loads filler in inner stage casing;
The liquid phase washings on gas-liquid separator 1T-412 top, draws from light component knockout tower charging, and charging is process stream, is provided with tail gas condenser 1E-413 at dehydration tower 1T-401 top of tower, cooling with chilled brine in tail gas condenser 1E-413, is cooled to-10 ℃;
Gas-liquid separator 1T-412 top is provided with liquid phase shower, and shower bottom is provided with two rounds;
Gas-liquid separator 1T-412 bottom is provided with return tank 1V-401, and gas-liquid separator 1T-412 bottom is provided with fluid-tight between return tank 1V-401;
Gas-liquid separator 1T-412 bottom liquid phase isobutene logistic, is recovered in dehydration tower 1T-401 return tank of top of the tower 1V-401; The gas phase on gas-liquid separator 1T-412 top, removes low low pressure flare separating tank, is discharged into flare system;
A upper operation dehydration column overhead in prenol is produced has pressure to divide process control system PIC-4104, is connected with in the present invention nitrogen valve 1PV-4104A, vent valve 1PV-4104B, can optimize the magnitude of recruitment of nitrogen and the loss that discharge brings; Dehydration tower 1T-401 tower top pressure exceedes 0.6MPaG, and vent valve 1PV-4104B opens, and flow 8kg/h, is discharged into flare system; Pressure is lower than 0.59MPaG, and vent valve 1PV-4104B closes;
By said process, can reduce the loss that dehydration tower 1T-401 tower top discharge brings as far as possible, also can reduce a nitrogen content in the magnitude of recruitment of nitrogen and system.
Claims (1)
1. dehydration tower system tower top tail gas recycling device in a prenol production, it is characterized in that, a upper operation dehydration tower (1T-401) tower top in prenol is produced out be rich in isobutene gas, enter overhead condenser (1E-401), cooling with chilled brine, the not solidifying tail gas of condenser (1E-401) consists of nitrogen, iso-butylene, 23 ℃ of service temperatures, working pressure 0.2MPaG;
Condenser (1E-401) bottom is provided with phlegma return tank (1V-412), collects the lime set that condenser (1E-401) gets off; The not solidifying tail gas of condenser (1E-401) enters gas-liquid separator (1T-412), further reclaims iso-butylene; Filler is loaded in the inner stage casing of gas-liquid separator (1T-412);
The liquid phase washings on gas-liquid separator (1T-412) top, draw from light component knockout tower charging, charging is process stream, be provided with tail gas condenser (1E-413) at dehydration tower (1T-401) top of tower, cooling with chilled brine in tail gas condenser (1E-413), be cooled to-10 ℃; Gas-liquid separator (1T-412) top is provided with liquid phase shower, and shower bottom is provided with two rounds; Gas-liquid separator (1T-412) bottom is provided with return tank (1V-401), and gas-liquid separator (1T-412) bottom is provided with fluid-tight between return tank (1V-401);
Gas-liquid separator (1T-412) bottom liquid phase isobutene logistic, is recovered in dehydration tower (1T-401) return tank of top of the tower (1V-401); The gas phase on gas-liquid separator (1T-412) top, removes low low pressure flare separating tank, is discharged into flare system;
Dehydration tower (1T-401) tower top is provided with return tank (1V-401), and return tank (1V-401) is provided with liquid collecting bag, with isobutylene separation and water; Return tank (1V-401) is provided with nitrogen access tube, to be filled with nitrogen;
A upper operation dehydration tower (1T-401) tower top in prenol is produced has pressure to divide process control system (PIC-4104), is connected with nitrogen valve (1PV-4104A), vent valve (1PV-4104B) in the present invention; Dehydration tower (1T-401) tower top pressure superelevation, vent valve (1PV-4104B) is opened, and is discharged into flare system; Pressure is ultralow, and vent valve (1PV-4104B) is closed;
Dehydration tower (1T-401) tower top pressure is ultralow, and nitrogen valve (1PV-4104A) is opened, and system fills into nitrogen; Pressure overflows, and vent valve (1PV-4104B) is closed.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410047173.9A CN103819309A (en) | 2014-01-29 | 2014-01-29 | Recycling device for exhaust gas in tower top of dehydrating tower system for production of methyl-2-buten-1-ol |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410047173.9A CN103819309A (en) | 2014-01-29 | 2014-01-29 | Recycling device for exhaust gas in tower top of dehydrating tower system for production of methyl-2-buten-1-ol |
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| CN103819309A true CN103819309A (en) | 2014-05-28 |
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| CN201410047173.9A Pending CN103819309A (en) | 2014-01-29 | 2014-01-29 | Recycling device for exhaust gas in tower top of dehydrating tower system for production of methyl-2-buten-1-ol |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008037693A1 (en) * | 2006-09-26 | 2008-04-03 | Basf Se | Continuous method for producing citral |
| CN201776080U (en) * | 2010-08-26 | 2011-03-30 | 深圳市诺为气流控制系统有限公司 | Spray tower group device for treating waste gases |
| CN102701923A (en) * | 2012-06-11 | 2012-10-03 | 北京科尔帝美工程技术有限公司 | System device and process for preparing polymethoxy dimethyl ether |
| CN103254036A (en) * | 2013-05-22 | 2013-08-21 | 吉林众鑫化工集团有限公司 | Method for gaseous-phase catalysis-free continuous synthesizing of 3-methyl-3-butenyl-1-alcohol |
-
2014
- 2014-01-29 CN CN201410047173.9A patent/CN103819309A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008037693A1 (en) * | 2006-09-26 | 2008-04-03 | Basf Se | Continuous method for producing citral |
| CN201776080U (en) * | 2010-08-26 | 2011-03-30 | 深圳市诺为气流控制系统有限公司 | Spray tower group device for treating waste gases |
| CN102701923A (en) * | 2012-06-11 | 2012-10-03 | 北京科尔帝美工程技术有限公司 | System device and process for preparing polymethoxy dimethyl ether |
| CN103254036A (en) * | 2013-05-22 | 2013-08-21 | 吉林众鑫化工集团有限公司 | Method for gaseous-phase catalysis-free continuous synthesizing of 3-methyl-3-butenyl-1-alcohol |
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Application publication date: 20140528 |