CN1073533C - Process for recovering by-product gaseous hydrocyanic acid from acrylonitrile production - Google Patents
Process for recovering by-product gaseous hydrocyanic acid from acrylonitrile production Download PDFInfo
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- CN1073533C CN1073533C CN95112140A CN95112140A CN1073533C CN 1073533 C CN1073533 C CN 1073533C CN 95112140 A CN95112140 A CN 95112140A CN 95112140 A CN95112140 A CN 95112140A CN 1073533 C CN1073533 C CN 1073533C
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- gas phase
- acid
- hydrocyanic acid
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Abstract
The present invention relates to a technology for recovering byproduct gas phase hydrocyanic acid in the production of acrylonitrile. Finished products are prepared through direct reaction with absorbates in a gas phase state under negative pressure. The technology has the advantages of short technological process, reduced investment for equipment, few leakage point of equipment, obviously reduced polymerization of gas phase HCN in transport, extended production period, and whole absorption of gas phase HCN by alkali liquid, etc. Compared with existing technologies, the present invention has higher economic benefits.
Description
The invention belongs to the recovery method of chemical industry prussic acid, the recovery method of the by product gaseous hydrocyanic acid in particularly a kind of acrylonitrile process.
In the acrylonitrile process process, by product prussic acid is steamed by dehydrogenation cyanic acid column overhead, its treatment process is in the following way always: overhead fraction enters dehydrogenation cyanic acid tower reflux exchanger, the part that needs to reflux is condensed into liquid phase, pass back in the tower, the output part enters prussic acid finished product condenser with gas phase, after condensation, deliver to reactor and liquid caustic soda etc. and absorb the material reaction finished product by liquid phase prussic acid transferpump, non-condensable gas is carried part prussic acid secretly through gas-liquid separation, carry out safe handling by the vacuum pumping torch, there is following deficiency in this treatment process:
(1) liquid phase prussic acid is in being transported to reactor process, need the equipment such as pump, condenser of some amount, facility investment is big, long flow path, leakage point are many, because prussic acid is violent in toxicity, so carry leakage easily in the prussic acid process in malleation, dangerous big.
(2) prussic acid is under liquid phase state, polymerization easily takes place and blocking pipe, equipment, and shorten the production cycle and also increased the difficulty of maintenance, thus the normal safety in production of influence.
(3) rate of recovery of prussic acid is low, and after gas-liquid separation, non-condensable gas is carried the part prussic acid torch that reduces internal heat secretly and handled, and causes environmental pollution.
The objective of the invention is to overcome the deficiency that above-mentioned prior art exists, and the recovery technology to the gaseous hydrocyanic acid of by-product in the acrylonitrile process process that provides that a kind of facility investment is few, safe, the rate of recovery is high.
Realize above-mentioned purpose, technical essential of the present invention be by-product gaseous hydrocyanic acid directly with gas phase state with absorb material reaction, make finished product.
Prussic acid directly is recovered utilization with gas phase state, do not need to be condensed into liquid phase, not only can omit equipment such as condenser, transferpump, gas-liquid separator in the technology, and have prussic acid and can access whole recovery, the corresponding raising of production security has prolonged many advantages such as production cycle.
When prussic acid moves with gas phase state, be preferably under the condition of negative pressure, be more conducive to improve production security, extend manufacture cycle.
Illustrate below in conjunction with process flow diagram:
Fig. 1 is a process flow diagram of the present invention.
Fig. 2 is the prior art processes schematic flow sheet.
Such as Fig. 1, dehydrogenation cyanic acid column overhead cut is in the partial condensation reflux column that dehydrogenation cyanic acid tower reflux condenser will reflux, gas phase partly is gaseous hydrocyanic acid, extracted out by the injector negative pressure, whole tower system and hydrogen cyanide conveyance conduit are moved under negative pressure, and the tower top pressure of control dehydrogenation cyanic acid tower is 0.7～0.8kg/cm2(absolutely). Injector adopts conventional chemical industry equipment, Absorb material and be introduced into surge tank, by the gas phase HCN haptoreaction in circulating pump and the injector, Injector doubles as reactor. Product is back in the surge tank, along with the carrying out of reaction, The concentration of the absorption material in the surge tank reduces gradually, and the concentration of product increases gradually, Be reduced to finite concentration (when the absorption material was alkali lye, concentration was 1.6%) when absorbing material concentration When following, be the gained finished product, change in addition then a surge tank, repeat said process. Inhale Receiving material such as alkali lye, acetone etc. makes HCN be converted into useful chemical products.
Below for adopting an embodiment of technology of the present invention.
Control dehydrogenation cyanic acid Tata still temperature is 75～78 ℃ (former technology is 85 ℃), and the cat head temperature is 18～22 ℃ (former technology is 27～29 ℃), and tower top pressure is 0.7～0.8kg/cm
2(cutting off), (former technology is 0.07kg/cm
2(table)), whole dehydrogenation cyanic acid tower lies under this negative pressure and moves, the production cycle of dehydrogenation cyanic acid tower reboiler is increased to more than 4 months by 1 month of former technology, the production cycle of dehydrogenation cyanic acid tower was increased to more than 1 year by original 4 months, and the gaseous hydrocyanic acid that comes out from dehydrogenation cyanic acid tower reflux exchanger is all absorbed generation sodium cyanide (described former technology is prior art of the present invention) by liquid caustic soda.
Advantage of the present invention:
1, equipment investment and maintenance cost have been reduced. This technology does not need gas phase HCN is changed For absorbing again after the liquid phase, directly be recovered by gas phase state, shortened flow process, than existing Technology has been omitted condenser, liquid phase delivery pump, vavuum pump and gas-liquid separator, thereby reduces The investment and corresponding equipment maintenance cost. From Fig. 1,2 flow chart, can find out.
The security of 2, producing improves. Because equipment reduces, its leakage point also reduces, gas Phase HCN greatly reduced its polymerism in course of conveying, thereby improved production Security.
3, rate of recovery height has been avoided atmosphere pollution. Gas phase HCN can access whole recovery, Become useful chemical products. Avoided combustion parts HCN in the prior art and cause big Gas pollutes.
4, prolong the technological operation cycle, increased economic benefit. Whole dehydrogenation cyanic acid tower Be to move under the condition of negative pressure, the HCN polymer obviously reduces, and the equipment operating cycle prolongs at double (production cycle of dehydrogenation cyanic acid tower reboiler is by increase in 1 month of former technology in above-described embodiment To more than 4 months, the production cycle of dehydrogenation cyanic acid tower was increased to more than 1 year by 4 months), big Reduced greatly maintenance, recondition expense, made the corresponding increase of economic benefit of enterprise.
Claims (2)
1, the recovery technology of the by product gaseous hydrocyanic acid in the acrylonitrile process, it is characterized in that described gaseous hydrocyanic acid is directly with gas phase state and absorption material reaction, make finished product, gaseous hydrocyanic acid negative pressure from dehydrogenation cyanic acid tower is extracted out, control dehydrogenation cyanic acid Tata still temperature is 75～78 ℃, tower top temperature is 18～22 ℃, and tower top pressure is 0.7～0.8kg/cm
2(cutting off).
2, technology according to claim 1 is characterized in that described gaseous hydrocyanic acid extracted out by the injector negative pressure from dehydrogenation cyanic acid tower, and in injector with absorb material reaction.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN95112140A CN1073533C (en) | 1995-08-10 | 1995-09-18 | Process for recovering by-product gaseous hydrocyanic acid from acrylonitrile production |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN95110570.1 | 1995-08-10 | ||
| CN95110570 | 1995-08-10 | ||
| CN95112140A CN1073533C (en) | 1995-08-10 | 1995-09-18 | Process for recovering by-product gaseous hydrocyanic acid from acrylonitrile production |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1143607A CN1143607A (en) | 1997-02-26 |
| CN1073533C true CN1073533C (en) | 2001-10-24 |
Family
ID=25743743
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN95112140A Expired - Fee Related CN1073533C (en) | 1995-08-10 | 1995-09-18 | Process for recovering by-product gaseous hydrocyanic acid from acrylonitrile production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1073533C (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1079093C (en) * | 1998-12-31 | 2002-02-13 | 中国石化集团齐鲁石油化工公司 | Tail gas recovering process from the second decyanation tower of acertonitrile equipment |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS57129822A (en) * | 1981-02-05 | 1982-08-12 | Asahi Chem Ind Co Ltd | Recovering and purifying method for hydrocyanic acid |
| DE3334321A1 (en) * | 1983-09-22 | 1985-04-11 | Lentia GmbH Chem. u. pharm. Erzeugnisse - Industriebedarf, 8000 München | Process for the purification of crude acetonitrile with the recovery of pure prussic acid |
| EP0360555A1 (en) * | 1988-09-21 | 1990-03-28 | E.I. Du Pont De Nemours And Company | Process for preparing sodium cyanide |
| EP0637584A1 (en) * | 1991-12-11 | 1995-02-08 | The Standard Oil Company | Method for stabilization of crude acetonitrile as oxidation or ammoxidation feed |
-
1995
- 1995-09-18 CN CN95112140A patent/CN1073533C/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS57129822A (en) * | 1981-02-05 | 1982-08-12 | Asahi Chem Ind Co Ltd | Recovering and purifying method for hydrocyanic acid |
| DE3334321A1 (en) * | 1983-09-22 | 1985-04-11 | Lentia GmbH Chem. u. pharm. Erzeugnisse - Industriebedarf, 8000 München | Process for the purification of crude acetonitrile with the recovery of pure prussic acid |
| EP0360555A1 (en) * | 1988-09-21 | 1990-03-28 | E.I. Du Pont De Nemours And Company | Process for preparing sodium cyanide |
| EP0637584A1 (en) * | 1991-12-11 | 1995-02-08 | The Standard Oil Company | Method for stabilization of crude acetonitrile as oxidation or ammoxidation feed |
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| Publication number | Publication date |
|---|---|
| CN1143607A (en) | 1997-02-26 |
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