Process for the production of biodiesel in continuous mode without catalysts

• US 7,524,982 B2
• Filed: 06/30/2006
• Issued: 04/28/2009
• Est. Priority Date: 07/06/2005
• Status: Expired due to Fees

• Current Assignee: Fundacao Regional Integrada, Intecnial S/A
• Original Assignee: Fundacao Regional Integrada, Intecnial S/A
• Inventors: Nascimento Sobrinho, Elói Ricardo, Osvaldo Baldus, Ari, Vladimir De Oliveira, José, Dariva, Cláudio, Dall'Agnol, Alcir
• Primary Examiner(s): Carr; Deborah D
• Application Number:
  US11/477,451
• Publication Number:
  US 20070010681A1
• Time in Patent Office: 1,033 Days
• Field of Search: 554/174
• US Class Current: 554/174
• CPC Class Codes: C10G 2300/1011 Biomass
• CPC Class Codes: C10L 1/026 for compression ignition
• CPC Class Codes: C11C 1/005 Splitting up mixtures of fatty acids into their constituents processes intended for both fats and fatty acids C11B7/00
• CPC Class Codes: Y02E 50/10 Biofuels, e.g. bio-diesel
• CPC Class Codes: Y02P 30/20 using bio-feedstock

Abstract

A continuous, non catalytic process for producing biodiesel from vegetable oils and ethanol or methanol includes pumping a mixture of vegetable alcohol through a pump towards a tube shaped reactor, wherein the mixture is submitted to high pressure and temperature, where the resulting product is non reacted alcohol, glycerin and a mixture of esters (biodiesel) which is directed to the reservoir at the reactor outlet where an upper phase of alcohol is redirected through an alcohol return pipe to the pump inlet, and the intermediate phase, biodiesel, and the lower phase (mostly of glycerin) are led to the separation reservoir or decantation tank, where the alcohol is removed through the alcohol return pipe, being biodiesel and glycerin the final products, which are then collected for the end to which they were aimed.

Claims

1. A continuous non-catalytic process of producing biodiesel, comprising:

dispensing alcohol and vegetable oil;

pumping the alcohol and vegetable oil into a reactor;

applying a pressure between about 20 Bar and 400 Bar and a temperature between about 150°

C. and 450°

C. to the alcohol and vegetable oil in the reactor, thereby forming a mixture of non-reacted alcohol, glycerin, and esters;

releasing the mixture of non-reacted alcohol, glycerin, and esters from the reactor via a flow and pressure control valve;

cooling the mixture of non-reacted alcohol, glycerin, and esters in a cooler;

of the mixture of non-reacted alcohol, glycerin, and esters, separating an upper phase of non-reacted alcohol from an intermediate phase of esters and a lower phase of glycerin and directing the intermediate phase of esters and the lower phase of glycerin to a separation reservoir;

separating the esters from the glycerin.

2. The process of claim 1, wherein the alcohol comprises ethanol or methanol.

3. The process of claim 1 further comprising, prior to separating the esters from the glycerin, purifying the intermediate phase of esters and the lower phase of glycerin through evaporation.

4. The process of claim 1 further comprising:

pumping the evaporated non-reacted alcohol back to the cooler;

cooling the cooler with the non-reacted alcohol; and

returning the non-reacted alcohol to be dispensed with the vegetable oil.

5. The process of claim 1 further comprising:

pumping the evaporated non-reacted alcohol back to the reactor;

heating the non-reacted alcohol at the reactor; and

returning the non-reacted alcohol to be dispensed with the vegetable oil.

6. The process of claim 1, wherein separating the upper phase of non-reacted alcohol from the intermediate phase of esters and the lower phase of glycerin comprises passing the non-reacted alcohol, the esters, and the glycerin through a hot water washing unit and separating the upper phase of non-reacted alcohol through distillation.

7. The process of claim 6, further comprising

pumping the evaporated non-reacted alcohol back to the reactor;

heating the non-reacted alcohol at the reactor; and

returning the non-reacted alcohol to be dispensed with the vegetable oil.

8. The process of claim 6 further comprising

pumping the evaporated non-reacted alcohol back to the cooler;

cooling the cooler with the non-reacted alcohol; and

returning the non-reacted alcohol to be dispensed with the vegetable oil.

9. The process of claim 1, wherein separating the upper phase of non-reacted alcohol from the intermediate phase of esters and the lower phase of glycerin and separating the esters from the glycerin comprises

separating the non-reacted alcohol, the esters, and the glycerin in one or more centrifugation units.

10. The process of claim 1 wherein the alcohol is methanol and the vegetable oil is canola oil and the molar ratio of the dispensed alcohol/vegetable oil is between about 3.5:

1 and 42;

1.

11. A non-catalytic process of producing biodiesel, comprising:

mixing alcohol and vegetable oil;

applying a pressure between about 20 Bar and 400 Bar and a temperature between about 150°

C. and 450°

C. to the alcohol and vegetable oil, thereby forming non-reacted alcohol, glycerin, and esters;

cooling the non-reacted alcohol, glycerin, and esters; and

separating the non-reacted alcohol, glycerin, and esters.

12. The process of claim 11, wherein the non-reacted alcohol is returned and utilized in the step of mixing alcohol and vegetable oil.