Utilization liquefaction product

Midwest utilities are coal burners. They have the know-how and facilities to utilize solid fuels. Solvent refined coal, which has the potential of being the lowest cost coal liquefaction product because of its low hydrogen content, is of interest to this group. 

The total liquid product is a blend of streams from liquefaction and FLEXICOKING. Product utilization studies indicate that the 350 F-fraction should be used in gasoline/petrochemical manufacture and the 350°F+ fraction in fuel oil applications. 

In other fuel markets, coal liquids can be more competitive. Industrial boilers presently are not amenable to stack gas scrubbing. The same is true of smaller utility plants. In particular, peak load units require a clean, storable liquid fuel as an alternative to natural gas. However, the high viscosity of primary coal liquefaction products is undesirable for many of these applications. Also, their residual sulfur and nitrogen contents may be excessive as emission standards become more stringent. 

The feedstocks utilized in this program were derived from a midcontinent and mid-east crude mix, from H-Coal liquefaction of No. 6 Illinois coal, and from the shale liquefaction product from the TOSCO II conversion of Parachute Creek shale. Analyses of the full-range liquids is presented in Table I. Attention is directed to the high nitrogen and... 

Crynes, B. L., 1981. Processing Coal Liquefaction Products, in Chemistry of Coal Utilization, M. A. Elliott (Ed.), Second Supplementary Volume, pp. 1991-2070, John Wiley Sons, New York, 1981. 

The liquid products were distilled to determine the yield and properties of the residual (343°C+) and light liquid (343°C ) products. Table VI shows that Runs 2 and 3 in Table IV resulted in 27 and 34 wt.% conversion of the 343°C+ fraction, while the sulfur in this fraction was reduced to 0.25 and 0.18 wt.%, respectively. The distillate and light liquid product (343°C ) are also upgraded in this process. The additional light distillates produced could presumably be recycled to the liquefaction reactor or utilized as low sulfur light distillate fuel. 

A considerable effort has been emended in the past few years by many researchers in attempts to better understand the mechanism by which coal is liquefied. From this work has emerged the concept of short residence time coal liquefaction which promises potential process advantages, small reactor, minimum hydrogen flow, and the efficient utilization of hydrogen for a particular product slate. 

A cost efficient way to utilize wheat in ethanol production has been developed by researchers from Greece and the U.K. This process splits the grain into separate components, separating out the nonfermentable solids, and then uses a group of enzymes to ferment the proteins and starches using a single liquefaction and saccharification step. 

Dual Enzyme Processes. In some cases, especially in syrup production in Europe, a liquefaction process is used that incorporates both a thermostable enzyme and a high temperature heat treatment. This type of process provides better hydrolyzate filterability than that attained in an acid liquefaction process (9). Consequendy, dual-enzyme processes were developed that utilized multiple additions of either B. licheniformis or B. stearothermophilus a-amylase and a heat treatment step (see Fig. 1). 

We will examine three synthetic fuel scenarios and compare their implications regarding sulfur availability with the current and projected market for sulfur to the year 2000. The analysis will consider three production levels of synthetic fuels from coal and oil shale. A low sulfur Western coal will be utilized as a feedstock for indirect liquefaction producing both synthetic natural gas and refined liquid fuels. A high sulfur Eastern coal will be converted to naphtha and syncrude via the H-Coal direct liquefaction process. Standard retorting of a Colorado shale, followed by refining of the crude shale oil, will round out the analysis. Insights will be developed from the displacement of imported oil by synthetic liquid fuels from coal and shale. 

This two-reaction scheme, if truly operative, suggests a view of the potential utility of liquefaction more optimistic than that derived from the conventionally accepted scheme. The yield of TS is a function of the rates of the two reactions. Therefore an increase in the rate of the TS route, or a decrease in the rate of char formation, would bring about increased TS yields. In turn, an increase in the rate of TS formation could be brought about with an increase in the reducing capacity of the system, rather than through an increase in reaction temperature. And thus in principle, increases in TS yield to product quantities representing all of the convertible portion of the starting coal could be obtained, and at no cost to product quality. 

All liquefaction processes produce a wide spectrum of products. Ultimately each product from a coal conversion plant will be utilized in a manner that provides the highest economic return to the plant owner. Products boiling below about 350 F will be disposed of to the transportation and petrochemical sectors of the... 

ER E has studied these alternatives for the utilization of coal liquefaction bottoms in the production of hydrogen and fuel gas and in doing so has had discussions of partial oxidation with Texaco and Shell. These studies have identified a potentially attractive processing sequence utilizing FLEXICOKING to produce additional liquids and plant fuel, and partial oxidation to produce hydrogen. 

In this way, we know that the coal liquefaction system constitutes a structure of multi-target system. In addition to these subtargets, the coal liquefaction system attaches an accomodate system which includes oxygen prdduction, hydrogen production, power production, and utilities. 

In the past the liquefaction of natural gas used a classic cascade cycle. The process required 120,000 hp for liquefaction of over 150 million standard cubic feet (mmscf) per day. Provisions are made for some of these cycles to use seawater for cooling. Later, baseload LNG plants utilized mixed refrigerant cycles, such as Air Products and Chemicals, Inc. s propane precooled mixed refrigerant system. Baseload plant capacities range from about 70 mmscf/day to about 350 mmscf/day of LNG. Baseload plants move LNG from remote sites by ship to populated areas. For... 

The currently available processes for natural gas utilization are shown in Figure 12.1. While conversion of gas to methanol and ammonia has been commercially practiced for decades, the demand for these products is small compared with the overall supply of remote gas. The liquefaction of natural gas to LNG can allow the transport of gas over long distances, but the capital costs for both the on-shore liquefaction and re-vaporization facilities and the cryogenic... 

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