AU759842B2 - Process for the treatment of a waste water - Google Patents

Process for the treatment of a waste water Download PDF

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Publication number
AU759842B2
AU759842B2 AU55354/00A AU5535400A AU759842B2 AU 759842 B2 AU759842 B2 AU 759842B2 AU 55354/00 A AU55354/00 A AU 55354/00A AU 5535400 A AU5535400 A AU 5535400A AU 759842 B2 AU759842 B2 AU 759842B2
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Prior art keywords
reverse osmosis
water
waste water
treatment
stream
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AU5535400A (en
Inventor
Eliza Antonie Gerrit Van Der Meijden
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Shell Internationale Research Maatschappij BV
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Shell Internationale Research Maatschappij BV
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    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00Multistage treatment of water, waste water or sewage
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/22Treatment of water, waste water, or sewage by freezing
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/44Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00Nature of the contaminant
    • C02F2101/30Organic compounds
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/34Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
    • C02F2103/36Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
    • C02F2103/38Polymers

Description

WO 01/00534 PCT/EP00/06037 1 PROCESS FOR THE TREATMENT OF A WASTE WATER The present invention relates to a process for the treatment of a waste water, in particular waste water from industrial processes containing at least hydrocarbons and salts.
The treatment or purification of waste water originating from industrial processes and containing at least hydrocarbons and salts (organic and/or inorganic) normally is a relatively expensive procedure.
Environmental legislation nowadays puts stringent demands on the purification of waste water streams from industrial processes, particularly when the purified waste water is to be released into the environment.
Accordingly, the choice of a purification method for industrial waste water is bound by practical, environmental and economic considerations.
One industrial process, wherein a relatively large amount of waste water is produced is the styrene monomer/propylene oxide (SM/PO) production process. In general such SM/PO process involves the steps of: reacting ethylbenzene with oxygen or air to form ethylbenzene hydroperoxide, (ii) reacting the ethylbenzene hydroperoxide thus obtained with propene in the presence of an epoxidation catalyst to yield propylene oxide and 1-phenyl ethanol, and (iii) converting the 1-phenyl ethanol into styrene by dehydration using a suitable dehydration catalyst. In the last step water is produced. In addition to this reaction water organic by-products such as aliphatic and aromatic hydrocarbons, aldehydes, ketones, alcohols, phenols and organic acids are produced in the course of the entire process. The by-products are separated from the main WO 01/00534 PCT/EP00/06037 2 products with the aid of clean water and the organic acids are neutralized using a basic-aqueous solution, such as an aqueous sodium (bi)carbonate and/or sodium hydroxide solution. Furthermore, additional water is introduced with the air in the step and as steam in step (iii) of the above process.
The waste water from an SM/PO production plant typically contains a total of from 1.0 to 3.5 wt% of non-salt organic compounds and from 3.0 to 6.0 wt% of organic salts. It may further contain up to 2.0 wt% of sodium carbonate and sodium bicarbonate and/or traces of sodium hydroxide, depending on the basic solution used in the neutralization of organic acids.
The input of clean water to an SM/PO plant can be up to tens of thousands kg per hour, while the output of waste water is normally about 50% higher than the input of clean water. The waste water cannot be discharged without additional purification treatment. As has already been indicated above, however, the choice of a suitable purification treatment is limited due to all sorts of practical, environmental and economic considerations.
Another well known method for producing propylene oxide, which also produces substantial amounts of waste water, is the co-production of propylene oxide and methyl tert-butyl ether (MTBE) starting from isobutane and propene. This process is well known in the art and involves similar reaction steps as the SM/PO process described above. In the epoxidation step tert-butyl hydroperoxide is reacted with propene forming propylene oxide and tert-butanol. Tert-butanol is subsequently etherified with methanol into MTBE, which is used as an additive in motor fuels.
Other examples of industrial processes producing large waste water streams are the production of KA oil (a mixture of cyclohexanone and cyclohexylalcohol) by Printed:07-09-20o1 DESCPAMD i o00940413-EP0006037 -3-
'JO.
oxidation of cyclohexane and the production of phenol and acetone by oxidising cumene.
In GB-A-2,252,052 further information is given about prior art methods for treating waste water and about typical compositions of SM/PO waste water streams. The purification process disclosed in GB-A-2,252,052 involves freeze-concentration combined with salts-removal, whereby the waste water is separated into an at least two-fold concentrated waste product, salt crystals and a purified melt water product.
The method disclosed in GB-A-2,252,052, however, still leaves room for improvement. More specifically, it has been found that the melt water produced in the freeze-concentration process may still contain a too high an amount of organics, in particular in terms of chemical oxygen demand (COD) and in terms of specific species, especially phenol. Accordingly, the present invention aims to provide a method for further reducing the organics level in waste water streams produced in production processes for propylene oxide, but also applicable to waste water streams of a much wider range of industrial processes.
JP 09136079A discloses a process for recycling drainage. US-A-5,443,733 relates to a process for preparing drinking water from waste water as produced in air- and spacecraft. Neither of these cases contains information on how to purify waste water feed originating from industrial processes.
Accordingly, the present invention relates to a process comprising treatment of a waste water feed containing organic contaminants and originating from jSTR/ industrial processes, which process comprises the steps Sof i AMENDED SHEET 29-06-20011 iPrited:07-09-2001 ESCPAMD 00940413-EP0006037 3a subjecting the waste water feed to a freeze-concentration treatment thereby producing at least a brine stream a concentrated waste product) and a water stream having a reduced content of organic contaminants; and subjecting this water stream to a reverse osmosis treatment thereby producing a purified water stream as the permeate and a relatively contaminated water stream as retentate.
Reverse osmosis is well known in the prior art, e.g.
from the article by Rautenbach R et al: "Membranverfahren zur Fraktionierung von Gemischen mit Organischen Komponenten" Chemie. Ingenieur. Technik, De, Verlag Chemie GmbH. Weinheim, vol. 61, No. 7, 1 July 1989 (1989-07-01), pages 535-544, XP000095268 ISSN: 0009-286X, and Kastelan-Kunst L et al: "FT30 membranes of characterized porosities in the reverse osmosis organics removal from aqueous solutions" Water Research, NL, Elsevier Science Publishers, Amsterdam, vol. 31, No. 11, 1 November 1997 (1997-11-01), pages 2878-2884, XP004094234 ISSN: 0043-1354 and JP 63-A-130188.
N:\M\TS0895PCT 2 AMENDED SHEET 29-06-2001 -4 25 The waste water feed to be treated by the present process has a chemical oxygen demand of at least 500 mg/l, preferably of at least 1000 mg/l, and a phenol content of at least 10 mg/l. Chemical oxygen demand (COD) is a measure of the oxygen required to oxidise all of the oxidisable materials in the sample. It is a good measure of how polluted a water sample is., because many species can be present in a water sample, each at low levels but in total contributing a significant amount of pollution. COD is determined by automated analysers, which mix a certain amount of an oxidising agent, such as oxygen, and optionally a catalyst to oxidise the compounds present in the sample.
The carbon dioxide thus generated is measured, often by infra-red analysers, and reported in units of mg oxygen (02) consumed per litre water or in ppm 02. Typical waste water discharge specifications are 100 mg/l COD, as this is considered to be close to the level that is naturally present in water from decaying organic material.
Step of the process according to the present invention is the freeze concentration process as described in GB-A-2,252,052. This process typically produces at least a brine stream and a water stream having a reduced content of organic contaminants. Salt crystals may also be produced depending on the salt concentration of the waste water feed and on the ratio of puri;fied water and brine produced in the freeze concentration unit. Accordingly, step suitably comprises the steps of: (al) cooling the waste water feed to form a freeze concentrate comprising the brine stream, possibly salt crystals and water having a reduced content of organic ontaminants in the form of ice crystals; WO 01/00534 PCT/EP00/06037 5 (a2) separating the ice crystals from the freeze concentrate and converting the ice crystals into the water stream to be further treated in step and (a3) removing the salt crystals, if present, from the remaining freeze concentrate yielding the brine stream and a salts stream.
Step (al) will normally involve the formation of ice crystals by crystallisation upon cooling of the waste water. Such crystallisation is suitably performed in two separate units: a nucleation unit followed by a growth unit. In the nucleation unit the waste water is cooled until small ice crystals are formed. Typically, the temperature in the nucleation unit is from -5 to -20 *C.
The slurry containing the small ice crystals is then passed to the growth unit, wherein the temperature is higher than the melting temperature of small ice crystals but lower than the melting temperature of larger ice crystals. As a result, small ice crystals will melt and larger ice crystals will grow in the growth unit. Typical temperatures in the growth unit are from -3 to -18 *C.
The size of the ice crystals will normally range from 0.2 mm to 0.8 mm.
In step (a2) the ice crystals are separated from the freeze concentrate once their size and quantity is sufficiently large. Preferably, such separation is achieved by means of filtration followed by washing the crystals in a packed bed wash column, but other separation techniques like centrifuging of the slurry may be applied as well. In such packed bed wash column the ice crystals-containing slurry is introduced under pressure and the crystal-free concentrate is filtered off at the lower end of the vertical column. This concentrate is suitably recycled to the waste water feed. The washed ice crystals are removed at the upper end of the wash WO 01/00534 PCT/EP00/06037 6 column and melted to yield the purified water stream.
Further details are described in GB-A-2,252,052.
If a sufficiently large amount of salts (mainly organic salts) is present in the waste water, these salts tend to precipitate and crystallize when the waste water is cooled and concentrated in step The salt crystals thus formed are separated from the ice crystals as described in step (a3) yielding the brine stream and a salts stream. Since the ice crystals are larger and less dense than the salt crystals such separation can be effectively achieved by filtration or centrifugation. The brine and the salt crystals, if any, formed in step (a) are suitably incinerated.
In step of the process according to the present invention the melt water stream from step i.e. the water stream having a reduced content of organic contaminants, is subjected to a reverse osmosis treatment thereby producing a purified water stream as the permeate and a relatively contaminated water stream as retentate (also sometimes referred to as concentrate). Suitably, said melt water stream is passed through a reverse osmosis unit comprising at least one reverse osmosis element in which the actual membrane is arranged.
Reverse osmosis is well known in the art. In general, a reverse osmosis element will comprise a high pressure compartment and a low pressure compartment separated by a reverse osmosis membrane. The water to be purified is normally pumped at a certain feed rate and at a certain pressure into the high pressure compartment. The pressure of the contaminated water entering this compartment should be sufficiently above its osmotic pressure to cause a permeate fraction to flow through the membrane.
This permeate fraction is then collected in the low pressure chamber, where it is recovered at a lower pressure than the pressure at which it entered the high WO 01/00534 PCT/EP00/06037 7 pressure compartment. The permeate, which is the purified water, is continuously or periodically withdrawn from said low pressure compartment. The retentate is continuously or periodically withdrawn from the high pressure chamber for further treatment, which may include incineration. Preferably, however, the retentate is entirely or partly recycled to the waste water feed for the freeze concentration unit the feed for step At least part of the retentate can also be re-used as wash water in the process in which the waste water was originally produced.
The entire reverse osmosis treatment carried out in step may involve passing the water to be purified through one or more reverse osmosis elements as described above. Such elements may be arranged in parallel and/or in series. Depending on the size and capacity of the reverse osmosis element and on the amount of water to be treated it is, for instance, possible to use two to ten rows of elements arranged in parallel, whereby each row of elements consists of two to ten elements arranged in series. It will be understood that the number and arrangement of reverse osmosis elements is entirely dependent on the amount of waste water to be treated and the size and capacity of the elements used. The reverse osmosis elements may be preceded by one or more prefilters to remove larger particles greater than 10 m) from the contaminated water feed. A pressure increasing pump may also be installed before the reverse osmosis element(s) to bring the pressure of the water at the required level.
The reverse osmosis treatment is preferably carried out under such conditions that the COD of the permeate is 100 mg/l or less, preferably 50 mg/l or less and more preferably 10 mg/l or less. Operation to achieve levels WO 01/00534 PCT/EP00/06037 8 below 5 mg/l is also possible. Preferred conditions to be applied in the reverse osmosis treatment include a temperature in the range of from 2 to 60 more preferably 5 to 40 'C and most preferably 10 to 30 'C.
The pressure of the water feed entering the high pressure compartment should anyhow be sufficiently high to cause a permeate fraction to flow through the membrane into the low pressure compartment in sufficiently high amounts.
The pressure of the feed entering the high pressure compartment will normally be less than 60 bar and suitably will be in the range of from 3 to 50 bar, more suitably 5 to 35 bar, most suitably 10 to 30 bar. The pressure at which the permeate leaves the low pressure compartment will normally be at least 1 bar lower than the pressure of the water feed entering the high pressure compartment. This pressure differential suitably ranges from 1 to 30 bar. A maximum pressure differential of bar is even more preferred, while in a very much preferred embodiment the pressure differential is from 2 to 10 bar. The absolute pressure of the permeate leaving the low pressure compartment will normally be between 0.1 and 50 bar, suitably between 0.5 and 35 bar, while pressures from 1 to 30 bar are preferred. Very good results have been achieved at pressures of 5 to 25 bar.
The actual reverse osmosis unit used in carrying out the method of the present invention may be of usual and known design and construction. The membrane used may be any reverse osmosis membrane known to be useful in treating contaminated water. One type of membranes that has been found to be particularly suitable are the high rejection membranes, which are for instance used for desalination of seawater.
As has been indicated above, the process of the present invention is particularly useful for treating a WO 01/00534 PCT/EP00/06037 9 waste water feed originating from a process for the production of propylene oxide via the co-oxidation of isobutane or ethylbenzene, i.e. a process for the co-production of respectively tert-butyl alcohol (usually etherified into methyl tert-butyl ether) or styrene on the one hand and propylene oxide on the other hand. The waste water treatment according to the present invention is also very useful for waste water streams produced in processes like the production of KA oil (a mixture of cyclohexanone and cyclohexylalcohol) by oxidation of cyclohexane and the production of phenol and acetone by oxidising cumene. These oxidation processes are well known in the art and both produce large water streams contaminated with organic acids.
The present invention is illustrated by the following examples without limiting the scope of the invention to these specific embodiments.
Example Waste water from a commercial SM/PO process was treated in a freeze concentration process as described in GB-A-2,252,052 and as outlined above in steps (al) through The purified water was recovered in the form of ice crystals. These ice crystals were melted and passed into a reverse osmosis unit at a temperature of 15 oC.
The reverse osmosis unit consisted of a prefilter for removing particles having a diameter above 10 im from the water feed, followed by a pump to increase the pressure of the water feed (to 23 bar) and after the pump three reverse osmosis elements arranged in parallel. The membrane used in the reverse osmosis units was the SWHR 30 membrane ex DOW FilmTec. Each membrane had a surface of 7.5 m 2 and was arranged in the reverse osmosis element in a spirally wound fashion.
WO 01/00534 PCT/EP00/06037 10 The water was fed to the reverse osmosis unit at a flow rate of 1.2 m 3 per hour. The flux through each membrane amounted 27 litre per m 2 of membrane per hour.
The pressure differential across the membrane in each reverse osmosis element was 3 bar. From each reverse osmosis element 200 litres/hour of permeate were recovered.
The experiment was run for five subsequent days in a once-through mode, i.e. without any recycle of retentate.
Table 1 indicates the COD of the original waste water, of the purified water after freeze concentration and of the further purified water after reverse osmosis.
Also indicated are the concentrations of sodium, ethylbenzene (EB) and phenol of the purified water from the freeze concentration unit the feed to the reverse osmosis unit) and of the permeate obtained after the reverse osmosis treatment. All values given are average values determined over five days of measurements.
Table 1 Waste water treatment Waste water after freeze after reverse concentration osmosis COD (mg/l) 137 15.8 Na+ (mg/l) 17 9.1 0.47 EB (glg/l) 6,000 81 9 phenol 10,000 8 From Table 1 it is clear that the reverse osmosis treatment significantly reduces COD and phenol content of the purified water from the freeze concentration unit and hence further increases the quality of the purified water.
P:'OPERJcc-S5354-OO sp.doc-08/01/03 lOa- Throughout this specification and the claims which follow, unless the context requires otherwise, the word "comprise", and variations such as "comprises" and "comprising", will be understood to imply the inclusion of a stated integer or step or group of integers or steps but not the exclusion of any other integer or step or group of integers or steps.
The reference to any prior art in this specification is not, and should not be taken as, an acknowledgment or any 0 form of suggestion that that prior art forms part of the common general knowledge in Australia.

Claims (9)

  1. 2. Process as claimed in claim i, wherein the waste water feed has a chemical oxygen demand of at least 1000, mg/l.
  2. 3. Process as claimed in claim 1 or 2, wherein the freeze concentration treatment comprises the steps of: 20 (al) cooling the wast water feed to form a freeze concentrate comprising the brine stream, possibly salt crystals and water having a reduced content of organic contaminants in the form of ice crystals; (a2) separating the ice crystals from the freeze concentrate and converting the ice crystals into the water stream to be further treated in step and (a3) removing the salt crystals, if present, from the remaining freeze concentrate yielding the brine stream and a salts stream.
  3. 4. Process as claimed in any one of claims 1-3, wherein the brine stream formed in step is incinerated. Process as claimed in any one of claims 1-4, wherein in -o ,tep the water stream having a reduced content of organic P:OPERUcc55354-00 spcc.doc-08/01/03 -12- contaminants is passed through a reverse osmosis unit comprising at least one reverse osmosis membrane.
  4. 6. Process as claimed in claim 5, wherein the reverse osmosis treatment is carried out under such conditions that the chemical oxygen demand of the permeate is 100 mg/l or less.
  5. 7. Process as claimed in claim 6, wherein the reverse osmosis treatment is carried out under such conditions that the chemical oxygen demand of the permeate is 50 mg/l or less.
  6. 8. Process as claimed in claim 7, wherein the reverse osmosis 10 treatment is carried out under such conditions that the :I chemical oxygen demand of the permeate is 10 mg/l or less.
  7. 9. Process as claimed in any one of claims 6-8, wherein the reverse osmosis is carried out at a temperature in the range of from 5 to
  8. 10. Process as claimed in any one of claims 1-9, wherein the retentate produced in step is at least partly recycled to the waste water feed for the freeze concentration treatment.
  9. 11. Process as claimed in any one of claims 1-10, wherein the retentate produced in step is at least partly re-used as 20 wash water in the process in which the waste water was originally produced. S12. Process as claimed in any one of claims 1-11, wherein the Swaste water feed originates from a process for preparing propylene oxide via the co-oxidation of isobutane or ethylbenzene. Dated this 8 t h day of January 2003 Shell Internationale Research Maatschappij B.V. by DAVIES COLLISON CAVE ~s Patent Attorneys for the Applicant(s)
AU55354/00A 1999-06-29 2000-06-27 Process for the treatment of a waste water Ceased AU759842B2 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP99202118 1999-06-29
EP99202118 1999-06-29
PCT/EP2000/006037 WO2001000534A1 (en) 1999-06-29 2000-06-27 Process for the treatment of a waste water

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CN103796982B (en) * 2011-09-16 2015-10-14 赢创罗姆有限公司 The preparation method of methacrylic acid and methacrylic ester
SG10201710018VA (en) * 2013-06-04 2018-01-30 Basf Se Process for reducing the total organic carbon in wastewater
ES2843825T3 (en) 2016-05-25 2021-07-20 Shell Int Research Process of preparing a catalyst and using it
CN109153588B (en) 2016-05-25 2021-09-24 国际壳牌研究有限公司 Method for treating waste water
DE102016114947B4 (en) 2016-08-11 2018-02-22 Gea Niro Pt B.V. Process for the high concentration of aqueous solutions and plant for carrying out the process
JP2021504108A (en) 2017-11-23 2021-02-15 シエル・インターナシヨナル・リサーチ・マートスハツペイ・ベー・ヴエー Process for wastewater treatment
EP3838849A1 (en) * 2019-12-19 2021-06-23 Sulzer Management AG A process for controlling of the purification of waste fluid generated during a petrochemical process using an incinerator
CN112429873A (en) * 2020-11-06 2021-03-02 上海市政工程设计研究总院(集团)有限公司 Reverse osmosis concentrated water treatment device under natural cold energy condition

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GB2262052A (en) * 1991-12-03 1993-06-09 Shell Int Research Process for the treatment of a waste water stream
US5443733A (en) * 1992-05-21 1995-08-22 Daimler-Benz Aerospace Airbus Gmbh Method and apparatus for treating waste water
JPH09136079A (en) * 1995-11-13 1997-05-27 Hitachi Ltd Wastewater recycling method

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US4592768A (en) * 1983-10-20 1986-06-03 Chicago Bridge & Iron Company Apparatus and process for desalination combining freeze concentration, centrifugation, and reverse osmosis
JPS63130188A (en) * 1986-11-21 1988-06-02 Mitsui Toatsu Chem Inc Treatment of phenolic waste water

Patent Citations (3)

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GB2262052A (en) * 1991-12-03 1993-06-09 Shell Int Research Process for the treatment of a waste water stream
US5443733A (en) * 1992-05-21 1995-08-22 Daimler-Benz Aerospace Airbus Gmbh Method and apparatus for treating waste water
JPH09136079A (en) * 1995-11-13 1997-05-27 Hitachi Ltd Wastewater recycling method

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AU5535400A (en) 2001-01-31
WO2001000534A1 (en) 2001-01-04
JP2003503187A (en) 2003-01-28
EP1200356A1 (en) 2002-05-02

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