Systems and processes for polyacrylic acid production

Patent metadata

Field	Value
Publication number	US-10428165-B2
Application number	US-201615550111-A
Country	US
Kind code	B2
Filing date	Feb 12, 2016
Priority date	Feb 13, 2015
Publication date	Oct 1, 2019
Grant date	Oct 1, 2019

Abstract

Disclosed are systems and methods for the production of polyacrylic acid and superabsorbent polymers from ethylene oxidation to form ethylene oxide. Reacting the ethylene oxide with carbon monoxide to form to beta propiolactone (BPL) or polypropiolactone (PPL), or a combination thereof. An outlet configured to provide a carbonylation stream comprising the BPL or PPL, or a combination thereof and using one or more reactors to convert BPL to acrylic acid or to convert at least some of the BPL to PPL, and then to convert PPL to acrylic acid. An outlet configured to provide a PPL stream to a second reactor tm to convert at least some of the PPL to AA or a third reactor to convert at least some of the PPL to AA. The outlet configured to provide an AA stream to a fourth reactor to convert the AA to polyacrylic acid.

First claim

What is claimed is:

1. An integrated system for producing polyacrylic acid (PAA) and superabsorbent polymer (SAP) from ethylene, comprising:
an oxidative reactor, comprising:
an inlet configured to receive ethylene,
an oxidative reaction zone configured to convert ethylene to ethylene oxide (EO), and
an outlet configured to provide an EO stream comprising the EO;

a central reactor, comprising:
an inlet configured to receive EO from the EO stream of the oxidative reactor, and carbon monoxide (CO) from a CO source,
a central reaction zone configured to convert EO to beta propiolactone (BPL) or polypropiolactone (PPL), or a combination thereof, and
an outlet configured to provide a carbonylation stream comprising the BPL, or a carbonylation stream comprising the PPL, or a combination thereof;

one or more of (i), (ii) and (iii):
(i) a first reactor, comprising:
an inlet configured to receive BPL from the carbonylation stream of the central reactor,
a first reaction zone configured to convert BPL to acrylic acid (AA), and
an outlet configured to provide an AA stream comprising the AA,

(ii) a second (a) reactor, comprising:
an inlet configured to receive BPL from the carbonylation stream of the central reactor,
a second (a) reaction zone configured to convert BPL to PPL, and
an outlet configured to provide a PPL stream comprising the PPL, and

a second (b) reactor, comprising:
an inlet configured to receive the PPL stream of the second (a) reactor,
a second (b) reaction zone configured to convert at least some of the PPL to AA, and
an outlet configured to provide an AA stream comprising the AA, and

(iii) a third reactor, comprising:
an inlet configured to receive PPL from the carbonylation stream of the central reactor,
a third reaction zone configured to convert PPL to AA, and
an outlet configured to provide an AA stream comprising the AA;

a fourth reactor, comprising:
an inlet configured to receive the AA stream of one or more of the first, second (b) and third reactor,
a fourth reaction zone configured to convert AA to polyacrylic acid (PAA), or a salt thereof, and
an outlet configured to provide a PAA stream comprising the PAA, or a salt thereof;

a fifth reactor, comprising:
an inlet configured to receive PAA, or a salt thereof, from the PAA stream of the fourth reactor,
a fifth reaction zone configured to directly convert the PAA, or a salt thereof, to superabsorbent polymer (SAP), and
an outlet configured to provide a SAP stream comprising the SAP; and

a controller to independently modulate production of the EO, BPL, PPL, AA, PAA and SAP.

2. The system of claim 1 , comprising two of (i), (ii) and (iii).

3. The system of claim 1 , comprising (i), (ii) and (iii).

4. The system of claim 1 , wherein the system produces AA at 200 kilotons to 800 kilotons per annum (kta).

5. The system of claim 1 , wherein the AA has less than 5% by weight of an aldehyde impurity or a compound that derives from the oxidation of propylene.

6. The system of claim 1 , wherein the inlet to the fourth reactor is configured to receive one or more reactant streams comprising sodium hydroxide, and the fourth reaction zone is configured to form a PAA sodium salt from the one or more reactant streams in the presence of a radical initiator.

7. The system of claim 1 , wherein the fourth reaction zone is configured to convert AA to polyacrylic acid (PAA), or a salt thereof, by gel polymerization, suspension polymerization, or solution polymerization.

8. The system of claim 1 , wherein the PAA, or a salt thereof, has less than 5% by weight of an aldehyde impurity or a compound that derives from the oxidation of propylene.

9. The system of claim 1 , wherein the inlet to the fourth reactor is configured to further receive one or more reactant streams each comprising a co-reactant to co-polymerize with AA, and the fourth reaction zone is configured to form one or more co-polymers of PAA selected from the group consisting of a polyacrylamide co-polymer, ethylene maleic anhydride co-polymer, cross-linked carboxymethylcellulose co-polymer, polyvinyl alcohol co-polymer, cross-linked polyethylene oxide co-polymer, and starch grafted polyacrylonitrile co-polymer of PAA.

10. The system of claim 1 , wherein the inlet to the fifth reactor is configured to further receive one or more reactant streams each comprising a cross-linking agent.

11. The system of claim 1 , wherein the SAP has less than 1000 parts per million residual monoethylenically unsaturated monomer, and has less than 5% by weight of an aldehyde impurity or a compound that derives from the oxidation of propylene.

12. The system of claim 1 , wherein the controller independently modulates production of the BPL by the central reactor.

13. The system of claim 1 , wherein the AA stream has:
less than 1000 parts per million residual monoethylenically unsaturated monomer,
(ii) less than 5% by weight or less than 10,000 ppm of an aldehyde impurity,
(iii) less than 5% by weight or less than 10,000 ppm of a compound that derives from the oxidation of propylene,
(iv) less than 5% by weight or less than 10,000 ppm of furfural,
(v) less than 5% by weight or less than 10,000 ppm of acetic acid,
(vi) less than 5% by weight or less than 10,000 ppm of stabilizers,
(vii) less than 5% by weight or less than 10,000 ppm of radical polymerization inhibitors,
(viii) less than 5% by weight or less than 10,000 ppm of anti-foam agents,
or any combination of (i)-(viii).

Assignees

• Novomer Inc

Inventors

• Sookraj Sadesh H

Classifications

• C07C51/14

  on a carbon-to-carbon unsaturated bond in organic compounds · CPC title

• C07C51/377

  by splitting-off hydrogen or functional groups; by hydrogenolysis of functional groups {(C07C51/36 - C07C51/373 take precedence)} · CPC title

• C07C51/145

  with simultaneous oxidation · CPC title

• C08F2/01 Primary

  characterised by special features of the polymerisation apparatus used · CPC title

• C07C51/12 Primary

  on an oxygen-containing group in organic compounds, e.g. alcohols · CPC title