Water-gas shift conversion process

Claim 2

partially reacting the preheated gaseous stream from (1) at a temperature in the range of about 250* to 1,500* F. over water-gas shift catalyst in an adiabaTic section of said water-gas shift conversion zone to produce hydrogen and carbon dioxide;

Claim 3

introducing the partially reacted gaseous stream from (2) at substantially the same exit temperature as from (2) into the water-gas shift catalyst in said isothermal section in (1), continuing the exothermic water-gas shift reaction of said gaseous stream as it is passed longitudinally through said isothermal section, and keeping the temperature of said reaction gaseous stream substantially constant by concurrent indirect heat exchange with said gaseous coolant in (1), thereby preheating said gaseous coolant stream as described previously in (1); 4. introducing the partially reacted gaseous stream from (3) at substantially the same exit temperature as from (3) into the water-gas shift catalyst in the equilibrium-limited section in (1), continuing the exothermic water-gas shift reaction of said gaseous stream as it is passed longitudinally through said equilibrium-limited section in (1), and gradually reducing the temperature of said gaseous stream by concurrent indirect heat exchange with said gaseous coolant stream in (1) as described previously; and 5. removing the reacted gaseous stream from (4) as shifted product gas containing an increased amount of hydrogen.

Claim 4

The process of claim 1 further provided with the step of admixing supplemental H2O with the preheated gaseous stream leaving the equilibrium-limited section in step (1).

Claim 5

The process of claim 1 further provided with the step of admixing supplemental H2O with the preheated gaseous stream leaving the isothermal section in step (1).

Claim 6

The process of claim 1 wherein said water-gas shift catalyst is selected from the group of catalysts consisting of iron oxide promoted by 1 to 15 percent by weight of an oxide of a metal such as chromium, thorium, uranium, beryllium and antimony; and a catalyst mixture of copper and zinc oxides in a weight ratio of about 3 parts zinc to 1 part copper.

Claim 7

A water-gas shift conversion process at a pressure in the range of 1 to 350 atmospheres comprising: 1. introducing a stream of feed gas mixture comprising a CO-rich gas and H2O as a coolant into the first section of a three sectional shift conversion zone containing water-gas shift catalyst and heating said feed gas mixture to a temperature in the range of about 400* to 780* F. by indirect heat exchange in said first section with a concurrent stream of partially shifted effluent gas which was introduced from the second section of said water gas shift conversion zone and which is simultaneously undergoing catalytic water-gas shift reaction in said first section, and discharging the shifted effluent gas from said first section as a product gas stream comprising hydrogen and carbon dioxide at a temperature in the range of about 400* to 780* F.; 2. passing the stream of feed gas mixture coolant preheated in the first section of said shift conversion zone in step (1) through the second section of said catalytic water-gas shift conversion zone in indirect heat exchange with a concurrent stream of partially shifted effluent reactant gas which was introduced from the third section of said water-gas shift conversion zone and which is simultaneously undergoing catalytic water-gas shift reaction in said second section; 3. introducing the stream of feed gas mixture coolant preheated in the second section of said shift conversion zone in step (2) to a temperature in the range of about 600* to 950* F. into the third section of said water-gas shift conversion zone to contact said water-gas shift catalyst, subjecting said feed gas mixture to catalytic water-gas shift reaction, and discharging the shifted effluent reactant gas from said third section into said second section of said shift conversion zone as said partially shifted effluent reactant gas in step (2).

Claim 8

The process of claim 6 further provided with the steps of admixing supplemental H2O with the preheated feed gas mixture leaving step (1).

Claim 9

The process of claim 6 wherein the pressure in all three sections of the catalytic water-gas shift conversion zone is substantially the same, less normal minor pressure drop.

Claim 10

The process of claim 6 where in step (1) said stream of feed gas mixture is introduced into said first section at a temperature in the range of 350* to 620* F. and with a mole ratio (H2O/CO) in the range of about 2 to 5.

Claim 11

The process of claim 6 with the additional step of adding a minor amount of H2O to the feed gas coolant mixture removed from said second section in step (2) before introducing said feed gas mixture into said third section of said water-gas shift conversion zone in step (3).