CN105439904B - The absorption process of acrylonitrile - Google Patents
The absorption process of acrylonitrile Download PDFInfo
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- CN105439904B CN105439904B CN201410428907.8A CN201410428907A CN105439904B CN 105439904 B CN105439904 B CN 105439904B CN 201410428907 A CN201410428907 A CN 201410428907A CN 105439904 B CN105439904 B CN 105439904B
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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
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- Y02P20/50—Improvements relating to the production of bulk chemicals
Abstract
The present invention relates to the absorption process of acrylonitrile, mainly solve that the problems such as absorption water content consumption is big exists in the prior art.In the present invention by using containing acrylonitrile etc. phase feed logistics (1) and liquid phase feed logistics (2) respectively enter the bottom and middle part on the first absorption tower (1a), gaseous stream III (3) is isolated in tower top, in the first absorption tower (1a) tower reactor discharge absorbing liquid V (5)；Gaseous stream III (3) enters the bottom second absorption tower (3a), is absorbed through poor-water (7) in second absorption tower (3a) and tower top takes out outer exhaust phase light component VIII (8) after cold recovery and second absorption tower tower bottoms VI (6) is taken out in bottom of tower；Second absorption tower tower bottoms VI (6) is back to the first absorption tower tower top；The technical solution that the poor-water (7) inputs through second absorption tower tower top, preferably solves the problems, such as this, can be used in ammoxidation of propylene acrylonitrile production industrial production.
Description
Technical field
The present invention relates to the absorption process of the acrylonitrile in process for production of acrylonitrile.
Background technology
Acrylonitrile is a kind of important organic chemical industry's base stock, is mainly used to produce acrylic fibers, acrylonitrile-butadiene-benzene
The chemical products such as vinyl plastics (ABS), polyacrylonitrile, acrylamide, nitrile rubber, by-product acetonitrile are fine solvents and organic
Synthetic intermediate, Cymag can be made in by-product hydrogen cyanide nearby, or acetone cyanohydrin is made, and be used as the original of synthesizing methyl acrylic acid
Material.Process for production of acrylonitrile undergoes cyanoethanol method and acetylene method.Currently, the main propylene ammoxidation method of domestic and international production method.
In the technique, unstripped gas propylene, ammonia, air are passed through fluidized-bed reactor from bottom with certain proportion and are reacted, and reaction heat is used
High steam occurs for soft water circulation and stress, and high-purity propylene nitrile can be obtained through chilling, absorption, rectifying etc. in gas after reaction.
Acrylonitrile absorptive unit is the main processes in acrylonitrile process.Since ammoxidation of propylene reaction is an individual
Product iodine reduces the progress that reaction pressure is conducive to acrylonitrile main reaction, can improve the cured once through yield of propylene, thus
It is required that acrylonitrile absorbing tower tower has the characteristics that pressure drop is low.Meanwhile to prevent the cohesion for absorbing polymer in water from blocking up tower.Patent
CN1055917C disclose it is a kind of have that pressure drop is low, production capacity is big, while can be anti-blocking acrylonitrile absorbing tower.Document
US363607 describes the technique for reducing methacrylonitrile content in acrylonitrile product.In the technique, from acrylonitrile heavy constituent gas
Stripper tower reactor draws a part of logistics and returns to absorption tower medium position, and the methacrylonitrile that stripping tower tower reactor is enriched with is in absorption tower
Part vaporizes, and is vented from absorption tower tower top, to reduce the content of methacrylonitrile in acrylonitrile product.Document US363608 is situated between
The technique of methacrylonitrile content in another reduction acrylonitrile product that continued.Document CN1153760C discloses a kind of acrylonitrile
Production technology, improvements are that absorption tower provides the second absorption water using nozzle.
In existing literature or report, the absorption technique problem of shorter mention acrylonitrile, especially in ensureing absorption tail gas
Under the premise of content containing cyanogen compound is up to standard, how to improve absorbing liquid acrylonitrile concentration, reduces the problem of absorbing water.
Invention content
The technical problem to be solved by the present invention is to that there are acrylonitrile concentrations in absorbing liquid in previous literature is low, absorbs water
Big topic provides a kind of absorption process of new acrylonitrile.The premise up to standard of content containing cyanogen compound in ensureing absorption tail gas
Under, this method has the advantages that acrylonitrile concentration is high in absorbing liquid, it is small to absorb water.
In order to solve the above technical problems, the technical solution adopted by the present invention is as follows：The absorption process of acrylonitrile, including it is as follows
Step：Phase feed logistics (1) and liquid phase feed logistics (2) containing acrylonitrile, acetonitrile, hydrogen cyanide and water respectively enter the first suction
The bottom and middle part for receiving tower (1a), the gaseous stream III (3) containing acrylonitrile, acetonitrile, hydrogen cyanide and water is isolated in tower top,
The absorbing liquid V (5) containing acrylonitrile, acetonitrile, hydrogen cyanide and water is discharged in first absorption tower (1a) tower reactor.
Gaseous stream III (3) enter the bottom second absorption tower (3a), second absorption tower (3a) through poor-water (7) absorb and
Tower top takes out outer exhaust phase light component VIII (8) after cold recovery and second absorption tower tower bottoms VI (6) is taken out in bottom of tower；Second
Absorbing tower kettle liquid VI (6) is back to the first absorption tower tower top；The poor-water (7) inputs through second absorption tower tower top.
In above-mentioned technical proposal, the operation temperature on the first absorption tower is preferably 3.0~40.0 DEG C.
In above-mentioned technical proposal, the operating pressure preferred scope on the first absorption tower is 0.02~0.08MPa.
In above-mentioned technical proposal, the theoretical cam curve on the first absorption tower is preferably 5~30.
In above-mentioned technical proposal, liquid phase feed logistics feed entrance point preferred scope is in 2~28 theoretical towers at the first absorption tower
At plate.
In above-mentioned technical proposal, the operation temperature preferred scope of second absorption tower is 2.0~30.0 DEG C.
In above-mentioned technical proposal, the operating pressure preferred scope of second absorption tower is 0.01~0.07MPa.
In above-mentioned technical proposal, the theoretical cam curve preferred scope of second absorption tower is 7~35.
In above-mentioned technical proposal, the first absorption tower and second absorption tower preferably independently are selected from packed tower, plate column or void tower, more
Preferred filler tower.
In above-mentioned technical proposal, the weight ratio of the poor-water and the phase feed logistics for entering the first absorption tower is preferably
1.5~3.0.
Pressure in the present patent application file refers both to gauge pressure.
Due to absorbing acrylonitrile, acetonitrile, hydrogen cyanide in acrylonitrile quenching gas using double tower absorption technique in the present invention,
Under the premise of content containing cyanogen compound is up to standard in ensureing absorption tail gas, poor-water (absorbing water) amount decreases, third in absorbing liquid
Alkene nitrile concentration is improved, to make the energy consumption of the subsequent separation and purification of absorbing liquid decrease.Tests prove that using this hair
Bright technical solution, liquid vapour weight ratio are reduced to 1.83, and absorbing liquid acrylonitrile concentration is improved to 6.41%wt, achieve preferable
Technique effect.
Description of the drawings
Fig. 1 is the first flow diagram of the absorption process of acrylonitrile of the present invention.
Fig. 2 is industrial acrylonitrile absorbing tower schematic diagram.
In Fig. 1,1 is the phase feed logistics from aftercooler, and 2 be the liquid phase feed logistics from aftercooler, and 3 are
The top gaseous phase stream I II on the first absorption tower, 4 feed for the tower top on the first absorption tower, and 5 be the first absorption tower absorbing liquid V, and 6 are
Second absorption tower tower bottoms VI, 7 be the absorption water (poor-water) for inputting second absorption tower, and 8 are for outer exhaust phase light component VIII, 1a
First absorption tower, 2a are second absorption tower tower reactor extraction pump, and 3a is second absorption tower.
The technological process of Fig. 1 is as follows：
In ammoxidation of propylene acrylonitrile production production technology, except the gas after ammonia chilling is divided into gas phase after aftercooler cools down
Feed stream and liquid phase feed logistics remove in phase feed logistics and contain acrylonitrile, acetonitrile, hydrogen cyanide and a small amount of organic matter
Outside, also contain a large amount of carbon dioxide, the light components such as nitrogen, water vapour, temperature is generally 20~45 DEG C, into the of the present invention
The bottom on one absorption tower, liquid phase feed logistics are aqueous solutions, contain with phase feed logistics mutually synthermal, are cooled to 10 DEG C of left sides
The right middle part for entering the first absorption tower.Poor-water (most of is water, the contains a small amount of organic impurities) warp come from follow-up refined unit
Exchange heat temperature adjustment after (its temperature is generally 2~7 DEG C), as absorb water enter second absorption tower tower top, in second absorption tower with
The absorption tail gas counter current contacting of rising, the tail gas (main component is carbon dioxide, nitrogen, water vapour etc.) after absorption discharge into row outside
Subsequent processing, the organic aqueous solutions such as acrylonitrile, acetonitrile, hydrogen propylhomoserin that second absorption tower absorbs, which are pumped up to first, to be absorbed
The top of tower, with the gas phase counter current contacting of rising in the first absorption tower, the gaseous stream after absorption enters second absorption tower
Bottom, (rich water ＞ enters subsequent refined unit to the absorbing liquids such as acrylonitrile, acetonitrile, hydrogen propylhomoserin that the first absorption tower absorbs.
In Fig. 2,1 is the gaseous stream from aftercooler, and 2 be the liquid phase stream from aftercooler, and 7 inhale for absorption tower
Water (poor-water) is received, 8 be outer exhaust phase light component, and 1a is absorption tower.
Below by embodiment, the present invention is further elaborated.
Specific implementation mode
In order to make the purpose , technical scheme and advantage of the present invention be clearer, the present invention further uses in detail below
Embodiment illustrates, but the present invention is limited to absolutely not these examples.
【Embodiment 1】
By the flow diagram of Fig. 1, the gas phase from aftercooler and liquid phase two streams respectively enter the first absorption tower
Bottom and middle part, poor-water enter the top of second absorption tower.Gas phase each group shunt volume is：5986.5 kgs/hr of acrylonitrile, second
165.1 kgs/hr of nitrile, 594.7 kgs/hr of hydrogen cyanide, 1401.6 kgs/hr of water, 15.4 kgs/hr of methacrylaldehyde,
360.9 kgs/hr of carbon monoxide, 1214.5 kgs/hr of carbon dioxide, 705.1 kgs/hr of oxygen, nitrogen 32477.7
Kg/hr, 103.3 kgs/hr of propane, 248.9 kgs/hr of propylene.Liquid phase each group shunt volume is：Acrylonitrile 422.7
Kg/hr, 42.4 kgs/hr of acetonitrile, 46.4 kgs/hr of hydrogen cyanide, 12275.5 kgs/hr of water, methacrylaldehyde 1.6
Kg/hr.Poor-water is 79250.6 kgs/hr.First absorbing tower top gas phase flow rate is 35289.9 kgs/hr,
Middle acrylonitrile, acetonitrile, hydrogen cyanide flow are respectively 2.4 kgs/hr, 0.0002 kg/hr, 16.2 kgs/hr, into the
Two absorb the bottom of the tower.The tower top temperature on the first absorption tower is 4.8 DEG C, pressure 0.029MPa, and bottom temperature is 32.4 DEG C, charging
Position is at middle part.
The tower top temperature of second absorption tower is 4.6 DEG C, pressure 0.014MPa, and bottom temperature is 4.6 DEG C.After absorption,
Tower top absorbs to be arranged outside tail gas, and flow is 35284.9 kgs/hr, wherein adding up to containing acrylonitrile, acetonitrile, hydrogen cyanide a concentration of
0.5ppm.Second absorption tower tower reactor flow quantity is at the top of 79255.5 kgs/hr of first absorption towers of entrance.
Poor-water and the phase feed logistics weight ratio for entering the first absorption tower are 1.83, and absorbing liquid acrylonitrile concentration is
6.41%wt.
【Embodiment 2】
With embodiment 1, only change absorption pressure, second absorption tower pressure is 0.044MPa, the other the same as in Example 1.First
Absorbing tower top gas phase flow rate be 35245.6 kgs/hr, wherein acrylonitrile, acetonitrile, hydrogen cyanide flow respectively be 0.6 kilogram/it is small
When, it is micro, 2.5 kgs/hr, into second absorption tower bottom.The tower top temperature on the first absorption tower is 4.8 DEG C, and pressure is
0.059MPa, bottom temperature are 32.6 DEG C, and feed entrance point is at middle part.
The tower top temperature of second absorption tower is 4.6 DEG C, pressure 0.044MPa, and bottom temperature is 4.6 DEG C.After absorption,
Tower top absorbs to be arranged outside tail gas, and flow is 35246.4 kgs/hr, wherein adding up to containing acrylonitrile, acetonitrile, hydrogen cyanide a concentration of
0.3ppm.Second absorption tower tower reactor flow quantity is at the top of 79249.8 kgs/hr of first absorption towers of entrance.
Poor-water and the phase feed logistics weight ratio for entering the first absorption tower are 1.83, and absorbing liquid acrylonitrile concentration is
6.41%wt.
【Embodiment 3】
With embodiment 1, only change liquid-gas ratio, poor-water is 89250.6 kgs/hr.The other the same as in Example 1.First absorbs
Column overhead gas phase flow rate be 35276.4 kgs/hr, wherein acrylonitrile, acetonitrile, hydrogen cyanide flow respectively be 1.0 kgs/hr,
It is micro, 4.8 kgs/hr, into second absorption tower bottom.The tower top temperature on the first absorption tower is 4.8 DEG C, and pressure is
0.029MPa, bottom temperature are 29.7 DEG C, and feed entrance point is at middle part.
The tower top temperature of second absorption tower is 4.6 DEG C, pressure 0.014MPa, and bottom temperature is 4.6 DEG C.After absorption,
Tower top absorbs to be arranged outside tail gas, and flow is 35284.3 kgs/hr, wherein adding up to containing acrylonitrile, acetonitrile, hydrogen cyanide a concentration of
0.4ppm.Second absorption tower tower reactor flow quantity is at the top of 89242.9 kgs/hr of first absorption towers of entrance.
Poor-water and the phase feed logistics weight ratio for entering the first absorption tower are 2.06, and absorbing liquid acrylonitrile concentration is
5.82%wt.
【Comparative example】
By the flow diagram of Fig. 2, the gas phase from aftercooler and liquid phase two streams respectively enter the bottom on absorption tower
And middle and lower part, poor-water enter the top on absorption tower.Gas phase each group shunt volume is：5986.5 kgs/hr of acrylonitrile, acetonitrile
165.1 kgs/hr, 594.7 kgs/hr of hydrogen cyanide, 1401.6 kgs/hr of water, 15.4 kgs/hr of methacrylaldehyde, one
360.9 kgs/hr of carbonoxide, 1214.5 kgs/hr of carbon dioxide, 705.1 kgs/hr of oxygen, nitrogen 32477.7 thousand
Grams Per Hour, 103.3 kgs/hr of propane, 248.9 kgs/hr of propylene.Liquid phase each group shunt volume is：Acrylonitrile 422.7 thousand
Grams Per Hour, 42.4 kgs/hr of acetonitrile, 46.4 kgs/hr of hydrogen cyanide, 12275.5 kgs/hr of water, methacrylaldehyde 1.6 thousand
Grams Per Hour.Poor-water is 79250.6 kgs/hr.
The tower top temperature on absorption tower is 4.6 DEG C, pressure 0.014MPa, and bottom temperature is 27.5 DEG C.After absorption, tower top
It absorbs and is arranged outside tail gas, flow is 35283.6 kgs/hr, wherein adding up to a concentration of 0.9ppm containing acrylonitrile, acetonitrile, hydrogen cyanide.
Poor-water and the phase feed logistics weight ratio for entering the first absorption tower are 2.29, and absorbing liquid acrylonitrile concentration is
5.34%wt.
Claims (2)
1. the absorption process of acrylonitrile, includes the following steps：
Phase feed logistics (1) and liquid phase feed logistics (2) containing acrylonitrile, acetonitrile, hydrogen cyanide and water respectively enter the first suction
The bottom and middle part for receiving tower (1a), the gaseous stream III (3) containing acrylonitrile, acetonitrile, hydrogen cyanide and water is isolated in tower top,
The absorbing liquid V (5) containing acrylonitrile, acetonitrile, hydrogen cyanide and water is discharged in first absorption tower (1a) tower reactor；
Gaseous stream III (3) enters the bottom second absorption tower (3a), is absorbed through poor-water (7) in second absorption tower (3a) and through cold
Tower top takes out outer exhaust phase light component VIII (8) after amount recycling and second absorption tower tower bottoms VI (6) is taken out in bottom of tower；Second absorbs
Tower tower bottoms VI (6) is back to the first absorption tower tower top；The poor-water (7) inputs through second absorption tower tower top；The poor-water with
Weight ratio into the phase feed logistics on the first absorption tower is 1.5~3.0；The theoretical cam curve on the first absorption tower is 5~30,
The theoretical cam curve of second absorption tower is 7~35；The operation temperature on the first absorption tower is 3.0~40.0 DEG C, and operating pressure is
0.02~0.08MPa；The operation temperature of second absorption tower is 2.0~30.0 DEG C, and operating pressure is 0.01~0.07MPa；Wherein,
Liquid phase feed feed entrance point is at 2~28 theoretical trays at first absorption tower.
2. the absorption process of acrylonitrile according to claim 1, it is characterised in that the first absorption tower and second absorption tower are independent
Selected from packed tower, plate column or void tower.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410428907.8A CN105439904B (en) | 2014-08-27 | 2014-08-27 | The absorption process of acrylonitrile |
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| CN201410428907.8A CN105439904B (en) | 2014-08-27 | 2014-08-27 | The absorption process of acrylonitrile |
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| CN105439904B true CN105439904B (en) | 2018-07-17 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112441943A (en) * | 2019-09-05 | 2021-03-05 | 中石油吉林化工工程有限公司 | Method for controlling PH in water circulation system in operation process of acrylonitrile device |
| CN111905527A (en) * | 2020-07-07 | 2020-11-10 | 山西钢科碳材料有限公司 | Exhaust gas treatment system and treatment method thereof |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3885928A (en) * | 1973-06-18 | 1975-05-27 | Standard Oil Co Ohio | Acrylonitrile and methacrylonitrile recovery and purification system |
| CN1201784A (en) * | 1997-06-06 | 1998-12-16 | 中国石油化工总公司 | Acrylonitrile absorbing tower |
| CN1305392A (en) * | 1998-06-15 | 2001-07-25 | 索罗蒂亚公司 | Process for recovery of olefinically unsaturated nitriles |
-
2014
- 2014-08-27 CN CN201410428907.8A patent/CN105439904B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3885928A (en) * | 1973-06-18 | 1975-05-27 | Standard Oil Co Ohio | Acrylonitrile and methacrylonitrile recovery and purification system |
| CN1201784A (en) * | 1997-06-06 | 1998-12-16 | 中国石油化工总公司 | Acrylonitrile absorbing tower |
| CN1305392A (en) * | 1998-06-15 | 2001-07-25 | 索罗蒂亚公司 | Process for recovery of olefinically unsaturated nitriles |
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