United states patent 1191 broz sept. 9, 1975 process for preparing 2, 409, 441 101946 metzger 260637 r monoethylene glycol and 2, 430, 443 111947 pecker. 260348.5 r 2, 756, 241 71956 c0urter., 260635 e ethylene oxide 3, 367, 847 21968 pierson 260637 r [75] inventor; stephen e. Broz, beaumont, tex, 3, 418, 338 121968 gilman et a1. 260348.5 r 3, 597, 452 81971 laemmle et a1. 260348.5 asslgneel ppg lndustl'les, pmsburgh, 3, 732, 320 51973 ford 260637 r [22] filed: feb. 13, 1973 [21] appl 332 056 primary examiner-joseph e. Evans attorney, agent, or firm-lrwin m. Stein [52] us. Cl. 260348.5 r; 260635 e; 260637 r [51] int. Gl c07c 3120; c07d 30132 [57] abstract [58] field of search 260635 e, 348.5 r, 637 r an improved process for p p g fiber grade mono [56] references cited ethylene glycol is provided which obviates the need for sewering large amounts of water. United states patents 2, 125, 333 81938 caner 260348.5 r 3 claims, 1 drawing figure e.o.reactor absorber stripper reabsorber e.o.refining e.o, purifyng columns (step a.) (step b) (srep c) (step d) (srep h) rec cle e1hyene 5.0. 1 5.0. 5.0. 00 5.0. H20 h20 r 5011 6 air 1 ethylene e.o.h20 p 5.0. Furge (inorganicsalts am u-v-absorbers)e.g.hg0 steam (condensed) g was h o meg 05 e 325r zxrllfi'e (optional 5014 0 h2o degasser activated teg carbon h20 meg deg teg deg teg teg ethylene glycol drying distillation train reactor evaporation column 1145s 05s teg (srep e) (srepf) -srep gl process for preparing monoethylene glycol and ethylene oxide description of the invention ethylene glycols (monoethylene glycol, diethylene glycol and triethylene glycol) are prepared commercially by several methods. One of these methods involves a two-stage reaction system, the first stage of which requires the direct o

The present invention relates to industrial organic synthesis, specifically to production of phenol and acetone by the cumene method.[0002]a well-known method for the production of phenol and acetone by oxidation of cumene with atmospheric oxygen, followed by the acid-catalytic decomposition of cumene hydroperoxide permits both end products to be produced with high yield (see, for example, kruzhalov b. D., golovanenko b. N., combined production of phenol and acetone, moscow, goskhimizdat, 1964, or kirk-othmer encyclopedia of industrial chemistry). This method is widely used to produce these products and is the principal technique used in world practice.[0003]methods are know for producing phenol and acetone in which, to reduce the yield of phenol tar, cumene oxidation products containing cumene hydroperoxide (chp), cumene, and dimethylphenylcarbinol (dmpc) cleavage in the presence of sulfuric acid to be separated in two stages. In the first stage, at a temperature of 55 to 80c, most of the chp (97 to 99%) is decomposed and dicumyl peroxide (dcp) is synthesized from dmpc and chp. In the second stage, acetone is added and the process fulfilled at a temperature of 80 to 146c to the obtained