Patent Application
20130014645
The present invention relates to processes for production of (meth)acrylic acid and, more particularly, to a method for removal of organic compounds from waste water streams in such processes.
The production of (meth)acrylic acid monomers is generally accomplished by vapor phase oxidation of alkanes, alkenes, or mixtures thereof to produce a mixed product gas which contains (meth)acrylic acid as well as various other compounds including unreacted raw materials, by-products, impurities, etc. To separate the (meth)acrylic acid from the other compounds, the mixed product gas may be contacted with an aqueous stream in an absorption step to produce an aqueous (meth)acrylic acid product which comprises mostly (meth)acrylic acid, water and small amounts of the other compounds. An absorber off-gas is also produced by the absorption step and comprises at least some of the other compounds, which are mostly organic compounds, such as, without limitation, unreacted alkane, unreacted alkene, aldehydes and other undesirable volatile organic compounds (VOCs).
Originally, conventional absorption was commonly employed to convert the mixed product gas to the more concentrated aqueous (meth)acrylic acid product (see U.S. Pat. No. 6,399,817). More recently, fractional absorption has been utilized because it more efficiently separates the components of the mixed product gas and, therefore, produces more concentrated aqueous (meth)acrylic acid products which can facilitate downstream purification processes (see, for example, U.S. Pat. Nos. 6,482,981 and 7,183,428). In fractional absorption, mixed product gas containing (meth)acrylic acid and aqueous absorbing medium are fed to a fractional absorber wherein (meth)acrylic acid and higher boiling point components of the mixed product gas are absorbed into the aqueous liquid phase to produce an aqueous (meth)acrylic acid stream which exits from the bottom of the fractional absorber, while the lightest components, such as acetic acid, are retained in the gas phase and exit from the top as the absorber off-gas.
Regardless of the particular absorption method, the resulting aqueous (meth)acrylic acid product is often subjected to further purification processes, such as distillation, stripping, fractionation, rectification, etc., in one or more separation apparati, for removal of additional amounts of water, unreacted compounds and other impurities, to produce a (meth)acrylic acid product having the desired purity. Many of the purification steps result in production of waste streams comprising mostly water, which is why they are commonly referred to as waste water streams, although they also contain minor amounts of organic compounds derived from the above-described oxidation and absorption processes (see, for example, U.S. Pat. Nos. 6,399,817, 6,482,981 and 7,183,428).
Common practice was to simply discharge the waste water streams to streams, rivers, lakes or ponds, but environmental concerns led to regulations requiring pre-treatment of process waste water to first remove or render inert environmentally harmful compounds contained therein. Thus, discarding process waste water has added costs to the overall process operation. To reduce such disposal costs as well as the environmental hazards, it became more common to recycle waste water streams back to various steps in the manufacturing process, such as to the oxidation reactor or the absorber (see, U.S. Pat. Nos. 5,248,819 and 6,399,817). Additionally, waste water streams have been treated prior to recycle or discard, to recover and remove organic components which may be used elsewhere or directed to a more economical disposal method. It is also known to recycle the absorber off-gas to the oxidation reactor or back to the absorber itself (see, U.S. Pat. Nos. 5,248,819 and 6,677,482).
Efforts continue to identify and develop methods and techniques by which the waste streams of (meth)acrylic acid production processes can be more efficiently used, reused, treated and discarded. The method of the present invention increases the efficiency of such production processes by using the absorber off-gas from a fractional absorber in a (meth)acrylic acid production process as stripping gas to strip organic compounds from waste water streams prior to recycle or discharge.
The present invention provides a method for removing acetic acid from a waste water stream which is produced during purification of (meth)acrylic acid. The method involves first performing fractional absorption with a mixed gas comprising (meth)acrylic acid, acetic acid, propylene and acrolein to produce an aqueous product stream comprising (meth)acrylic acid, water and acetic acid, and an absorber off-gas stream comprising propylene and acrolein. Next, the aqueous product stream is distilled to produce a purified (meth)acrylic acid stream and a waste water stream comprising water and acetic acid. The method of the present invention further involves contacting the absorber off gas and the waste water stream whereby at least a portion of the acetic acid moves from the waste water stream to the absorber off gas to produce a stripped waste water stream having a decreased acetic acid content and an enriched absorber off gas having an increased acetic acid content. The enriched absorber off gas stream is provided to a thermal oxidizer.
The stripped waste water stream may be discarded or subjected to further processing to remove or render inert one or more components therein. All or a portion of the stripped waste water stream may fed to at least one other process step.
A more complete understanding of the present invention will be gained from the embodiments discussed hereinafter and with reference to the accompanying drawings, wherein:
All percentages stated herein are weight percentages, unless otherwise specified.
As used herein, the term “(meth)acrylic acid” means either acrylic acid or methacrylic acid, or both.
As used herein, the term “(meth)acrolein” means either acrolein or methacrolein.
The term “stripping,” as used herein, refers to the contacting of a stripping gas with a solution containing target substances so as to migrate one or more target substances from the solution to the gas phase.
The method of the present invention will be described with reference to
With reference to
Depending on the reactants fed to the reactor, the mixed product gas 1 generally includes inert gas(es), including but not limited to, nitrogen, helium, argon, etc.; acrylic acid; unreacted hydrocarbon reactants, including but not limited to, propylene, acrolein, propane, etc.; steam, and molecular oxygen containing reactants, including but not limited to, air, oxygen, etc.; reaction by-products, including but not limited to, acetic acid, formaldehyde, maleic acid, and other organics; as well as CO2, CO and H2O.
Generally, the composition of the mixed product gas 1 includes from 5 to 30% by weight acrylic acid, from 0.1 to 3.0% by weight acetic acid, from 0.02 to 0.2% by weight acrolein, from 30 to 95% by weight inert gas, and from 1 to 30% by weight steam, based on the total weight of the mixed product gas 1.
As shown in
The aqueous stream 3 may include any suitable amount of recycled wastewater 4 up to 100 weight percent recycled wastewater. Typically, the aqueous stream 3 will be a mixture of a wastewater stream 4 from an acrylic acid manufacturing process and an essentially pure water stream 5, for example, deionized water. In one embodiment, for example, the aqueous stream 3 includes a major amount of wastewater. In another embodiment, the aqueous stream 3 includes from 0.1% to 100% by weight of wastewater. Preferably, the aqueous stream 3 contains 100% by weight wastewater. Regardless of how much recycled wastewater is utilized, the aqueous stream 3 will contain a major amount of water and minor amounts of at least one of acrylic acid, acetic acid, and distillation solvent(s). Generally, the aqueous stream contains less than 3.0%, preferably less than 2.0%, more preferably less than 1.5% by weight acetic acid. In another embodiment, the aqueous stream is substantially free of distillation solvent(s) and/or acrylic acid.
With reference still to
Generally, the mixed product gas 1 is fed to the fractional absorber 2 at a temperature from 165° C. to 400° C., preferably 200° C. to 350 ° C., more preferably 250° C. to 325° C. The aqueous stream 3 is fed to the fractional absorber 2 at a rate of 0.1 to 1.0 pounds of aqueous stream 3 per one pound of hydrocarbon material (in mixed gas product stream 1) fed to the reactor depending on the desired concentration of acrylic acid to be recovered from the bottoms of the fractional absorber 2. The fractional absorber 2 may be any suitable fractional absorber design known in the art in which (meth)acrylic acid and higher boiling point components of the mixed product gas are absorbed into the aqueous liquid phase to produce the aqueous (meth)acrylic acid stream 9, while the lightest components, such as acetic acid, are retained in the gas phase and exit from the top as the absorber off-gas 8.
To concentrate the (meth)acrylic acid, the aqueous (meth)acrylic acid stream 9 is fed to one or more distillation columns, such as the product column 10 and the subsequent acetic acid recovery column 12 shown schematically in
The aqueous (meth)acrylic acid stream 9 is distilled in the product column 10 to form a (meth)acrylic acid stream 11 and an intermediate waste stream 13 comprising water, acetic acid and other organic compounds. The distillation performed in one or both of columns 10, 12 may be simple, non-azeotropic distillation. Where azeotropic distillation is desired, one or more distillation solvents suitable for the azeotropic distillation of a (meth)acrylic acid stream may be used in either or both of the distillation columns 10, 12. In one embodiment, for example, the solvent is substantially water insoluble, generally having a solubility, in water at room temperature, of 0.5 weight percent or less, preferably 0.2 weight percent or less. Suitable examples of such a water insoluble solvent include, but are not limited to heptane; heptene; cycloheptane; cycloheptene; cycloheptatriene; methylcyclohexane; ethylcyclopentane; 1,2-dimethylcyclohexane; ethylcyclohexane; toluene; ethylbenzene; ortho-, meta-, or para-xylene; trichloroethylene; trichloropropene; 2,3-dichlorobutane; 1-chloropentane; 1-chlorohexane; and 1-chlorobenzene. In another embodiment, the solvent is selected from ethyl acetate, butyl acetate, dibutyl ether, hexane, heptane, ethyl methacrylate, diethyl ketone, methyl propyl ketone, methyl isobutyl ketone, and methyl tert-butyl ketone. In a further embodiment, the distillation solvent is a mixed solvent which includes at least two solvents. Suitable examples of solvents useful in such mixed solvent include, but is not limited to, diethyl ketone, methyl propyl ketone, methyl isobutyl ketone, methyl tert-butyl ketone, isopropyl acetate, n-propyl acetate, toluene, heptane and methylcyclohexane. The preferred distillation solvent is toluene.
Emanating from the bottom of the product column 10 is a (meth) acrylic acid stream 11 which is substantially free of water. Generally, the (meth)acrylic acid stream 11 has less than 1000, preferably less than 800, more preferably less than 500 ppm of water. The acrylic acid stream may also contain insubstantial amounts of at least one of the following: acetic acid, propionic acid, β-acryloxypropionic acid (AOPA), acrolein, furfural, benzaldehyde, maleic acid, maleic anhydride, protoanemonin, and acetaldehyde.
The (meth)acrylic acid stream 11 is suitable for use as a raw material in (meth)acrylic ester or (meth)acrylate polymer production. The (meth)acrylic acid may be used as is or be further processed, including but not limited, additional distillation to remove specific impurities and further processing to form various grades of (meth)acrylic acid.
As shown in
The second wastewater stream 14 may then be recycled and used elsewhere in the process, or discarded and sent to a water treatment facility. However, it would be advantageous to strip at least some of the organic compounds, such as acetic acid, out of the second wastewater stream 14 prior to recycling to prevent accumulation of the organic compounds in the process. Where the second wastewater stream 14 is sent for treatment and ultimate disposal, removing some of the organic compounds first will lessen the cost of treatment, and thereby, decrease the cost of disposing of this process waste stream.
Thus, in accordance with the method of the present invention, as shown in
The stripping column 16 may be any column suitable for stripping undesirable organic components from wastewater. Such columns are known in the art and include packed columns and tray-containing columns.
Generally, the gas used as the stripping gas 7 in the stripping column 16 should have a water content of from 0 to 100%, preferably 5 to 30%, more preferably 8 to 20% by weight, and a temperature from 20° C. to 250° C., preferably 45° C. to 125° C., more preferably from 50° C. to 90° C. The use of at least a portion of the absorber off-gas stream 8 as a stripping gas 7 is advantageous because the absorber off gas emerges from the absorber with a sufficient heat and water content for adequately stripping undesirable components from the wastewater. Accordingly, treatment of a potential waste gas stripping stream, i.e., heating and adding or removing water, is avoided.
However, at times it may be desirable to either use other stripping gas streams such as fresh air, combustion air, other waste gas streams, etc., either alone or in combination with all or a portion of an absorber off-gas stream 8. This may require additional heating of the stripping gas 7 to obtain a proper operating temperature range. Also, additional heat may be required to increase the removal of organics from the wastewater stream 14. Consequently, a live steam sparge, external or internal reboilers, stripping gas feed pre-heater, or other methods known in the art of supplying additional heat to a stripping column may be utilized. In addition, there may be instances wherein additional momentum transfer within the stripping column is required. For example, where there is an increased pressure drop within the column and absorber pressure is insufficient to provide adequate momentum transfer. Consequently, devices such as a blower may be utilized to increase such momentum transfer.
One or more polymerization inhibitors may be introduced into the production process at various points such as polymerization inhibitor feeds 20, 21 and 22 shown in
With reference back to
Efficacy of the method of the present invention is demonstrated by the following examples.
Gas stripping experiments were performed in the laboratory using a water saturated N2 stream to mimic the absorber off-gas (AOG) stream. This water-gas stream was preheated prior to introducing it into a stripping column at temperatures typical of a commercial-scale AOG stream. The experiments showed that organic compounds in the feed stream which simulated a wastewater process stream, were removed and absorbed into the water-gas (AOG) stream, and that the stripped bottoms stream from the stripper had a lower concentration of organic compounds. Details of the laboratory experiments are as follows.
A simulated wastewater feed containing acrylic acid (4.875 wt. %), acetic acid (4.657 wt. %) and water (91 wt. %) was prepared in a large container. The container was placed on a balance and a pump system was attached to it. N2 was metered in and preheated in a bath set at 70° C. and fed to the bottom of a shell and tube heat exchanger packed with stainless steel Raschig rings. Water (25 mol % based on N2 flow) was pumped into the exchanger system and the resulting flow was fed to the column system.
The column system was a 10-tray 1″ Oldershaw system with a 100 mL bottoms flask. The feed was added at the top tray at a rate of 600 grams per hour (g/h). The system was operated at constant liquid level in the bottoms. Hydroquinone (HQ) is used to inhibit polymerization in the simulated wastewater feed.
The N2 flow rates were metered in at 8 liters per minute (L/min), 13 L/min, 20 L/min, 28 L/min. The overheads and bottoms were collected hourly and analyzed for organic and water content.
In a typical experiment, the exchangers are preheated under N2 and once the exit temperature reaches 60° C., water is added to the exchanger and the heater is controlled by the sump target temperature (65° C.). The column is allowed to gain heat and once the top section (Tray 8) reaches 45° C. the feed is then introduced. The bottoms are removed to maintain a constant level and target flow. The cuts from the first hour are typically discarded and the bottoms and overheads are then collected hourly. An example of the data from one experimental run as described above are provided in the following Tables
Under the conditions of 8 and 13 L/min N2 flow, the resulting stripping efficiency was 4.6% (combined AA and AcOH) and at 13 L/min the stripping efficiency was 10.4% (combined). As the flow was increased, the stripping efficiency showed a near linear increase (see chart below) with a 30% value at 28 L/min flow, as shown in
Tables
Main Feed: 10.895% AA, 9.977% AcOH, 79% H2O at tray 10 (Top tray) @ 600 g/hr
| Number | Date | Country | |
|---|---|---|---|
| 61507674 | Jul 2011 | US |
