Method and heat exchange system utilizing variable partial bypass

Patent metadata

Field	Value
Publication number	US-9828275-B2
Application number	US-201313955923-A
Country	US
Kind code	B2
Filing date	Jul 31, 2013
Priority date	Jun 28, 2013
Publication date	Nov 28, 2017
Grant date	Nov 28, 2017

Abstract

Temperature overshoot of internal components of a counter-flow shell and tube heat heat exchange may be reduced or avoided by adjusting the degree to which a tube-side fluid partially bypasses the heat exchanger.

First claim

What is claimed is:

1. A method for reducing overheating of internal components of a counter-flow shell and tube heat exchanger utilizing variable partial bypass of a reactant flow, said method comprising the steps of:
dividing a first feed flow of a cool reactant with a first control valve between a first main flow of the cool reactant and a first bypass flow of the cool reactant, the first main flow flowing through a counter-flow shell and tube heat exchanger on a tube-side of the heat exchanger;
exchanging heat at the shell and tube heat exchanger between the first main flow and a flow of a hot shell-side fluid and combining the first main flow with the first bypass flow to produce a first combined flow of heated reactant and also a flow of cooled shell-side fluid, the first combined flow being heated inside the shell and tube heat exchanger through heat exchange with the hot shell-side fluid and exiting the heat exchanger at a first reactant outlet of the heat exchanger and being received into a first outlet conduit fluidly communicating with the first reactant outlet;
measuring a temperature of the first combined flow at or downstream of the first reactant outlet with a first temperature sensor that is disposed in the outlet conduit; and
controlling relative proportions of the first main flow and first bypass flow with a first programmable logic controller and the first control valve based upon the measured temperature of the first combined flow, wherein less heat is transferred from the shell-side fluid to the first bypass flow than is transferred from the shell-side fluid to the first main flow;
dividing a second feed flow of a cool reactant with a second control valve between a second main flow of the cool reactant and a second bypass flow of the cool reactant, the second main flow flowing through a shell and tube heat exchanger on the tube-side;
exchanging heat at the shell and tube heat exchanger between the second main flow and a flow of a hot shell-side fluid and combining the second main flow with the second bypass flow to produce a second combined flow of heated reactant and the flow of cooled shell-side fluid, the second combined flow being heated inside the shell and tube heat exchanger through heat exchange with the hot shell-side fluid and exiting the heat exchanger at a second reactant outlet of the heat exchanger;
measuring a temperature of the second combined flow at or downstream of the second reactant outlet;
controlling relative proportions of the second main flow and second bypass flow with the second control valve, the second control valve being controlled by either the second programmable logic controller or the first logic controller based upon the measured temperature of the second combined flow, wherein:
less heat is transferred from the shell-side fluid to the second bypass flow than is transferred from the shell-side fluid to the second main flow; and
control of the relative proportions of the first feed flow into the first main and bypass flows is independent of control of the relative proportions of the second feed flow into the second main and bypass flows; and

directing the first combined flow exiting the first and second reactant outlets to first and second burners operatively associated with a furnace, wherein:
the shell-side fluid is air that is heated through heat exchanger with hot combustion gases at a recuperator or regenerator;
the first and second reactants are the same and are selected from the group consisting of industrially pure oxygen, oxygen-enriched air, and natural gas;
if the first and second reactants are industrially pure oxygen or oxygen-enriched air, the first and second reactants of the first and second combined flows are combusted with fuel at the first and second burners;
if the first and second reactants are natural gas, the first and second reactants of the first and second combined flows are combusted with an oxidant at the first and second burners; and
the furnace is a glass melting furnace.

2. The method of claim 1 , wherein the reactant is an oxidant having an oxygen concentration higher than that of air.

3. The method of claim 2 , wherein the reactant is industrially pure oxygen.

4. The method of claim 2 , wherein the reactant is oxygen-enriched air.

5. The method of claim 1 , wherein the reactant is a gaseous fuel.

6. The method of claim 1 , wherein the shell-side fluid is air or an inert gas.

7. The method of claim 1 , wherein the heat exchanger includes:
first, second and third plenums, the third plenum receiving the first combined flow and fluidly communicating with the first reactant outlet;
at least one first upstream reactant tube receiving the first main flow and extending through an interior of the shell from the first plenum and fluidly communicating with the second plenum;
a first bypass tube receiving the first bypass flow and extending between the first control valve and the second plenum and extending at least partially outside the shell of the heat exchanger, wherein the first main flow and the first bypass flow are combined at the second plenum; and
at least one first downstream reactant tube receiving the first combined flow and extending between the second and third plenums.

8. The method of claim 1 , wherein the shell and tube heat exchanger includes:
first, second and third plenums, the third plenum receiving the first combined flow and fluidly communicating with the first reactant outlet;
at least one first upstream reactant tube receiving the first main flow and extending through an interior of the shell from the first plenum and fluidly communicating with the second plenum;
a first bypass tube receiving the first bypass flow and extending between the first control valve and the second plenum and extending at least partially outside the shell of the heat exchanger, wherein the first main flow and the first bypass flow are combined at the second plenum;
at least one first downstream reactant tube receiving the first combined flow and extending between the second and third plenums;
fourth, fifth and sixth plenums, the fourth plenum receiving the second combined flow and fluidly communicating with the second reactant outlet;
at least one second upstream reactant tube receiving the second main flow and extending inside the shell from the fourth plenum and fluidly communicating with the fifth plenum;
a second bypass tube receiving the second bypass flow and extending between the second control valve and the fifth plenum and extending at least partially outside the shell of the heat exchanger, wherein the second main flow and the second bypass flow are combined at the fifth plenum;
at least one second downstream reactant tube receiving the second combined flow and extending between the fifth and sixth plenums.

9. The method of claim 1 , wherein the hot shell-side fluid is obtained from a recuperator or regenerator.

10. The method of claim 9 , wherein the cooled shell-side fluid is directed to a recuperator or regenerator to heat the cooled shell-side fluid in order to produce the hot shell-side fluid.

Assignees

• Air Liquide American

Inventors

• Kang Taekyu

Classifications

• F28F27/00

  Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus (control arrangements in general G05) · CPC title

• C03B5/2353 Primary

  by combustion with pure oxygen or oxygen-enriched air, e.g. using oxy-fuel burners or oxygen lances · CPC title

• F28D21/001

  for thermal power plants or industrial processes · CPC title

• C03B5/237

  Regenerators or recuperators specially adapted for glass-melting furnaces · CPC title

• C03B2211/40

  using oxy-fuel burners · CPC title