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ter/hiboiler split by taking low boilers and the water/ester azeotrope overheadin a distillation column. Low boilers might be separated from the ester in a second distillation column as their water azeotropes with an ester cut as a base vapor takeoff. The required separations, including all known byproducts, have to be defined from some source. At this point one can produce a fairly detailed process flow diagram with a wealth of information on it.

At some point one needs to do a theoretical balance around the process assuming100% stochiometric yields and the process capacity. This could be done at the block diagram stage.

Once the unit operations have been defined, a detailed mass balance including recyles and waste streams is to be done to show reactor yields and losses across unit operations. This will establish mass flow rates through the process and raw material requirements. An energy balance has to be done next.I will stop for now and complete this later if it appears to be what you are looking for.

You seem to have some parts of the design process in mind since you mention a hazop study. A hazop study is done when you have the process defined well enoughfor the study to be meaningful and to contribute to the design process.

Let's pause a moment and cover something that you know before starting this proc

ess; the site where such a plant could or will be built. Is this a grassroots effort? or an extension of an existing plant? or a conversion of an existing plant? The answer will influence several things in the process design.

Let's consider that you have a process description, property data for chemicalsinvolved, process chemistry, block flow diagram, semi-detailed process flow diagram, theoretical mass balance, unit operations modeling, and a site. Now a detailed mass and energy balance based on the process flow diagram, the reaction yields, and the unit operations engineering yields has to be built. Process conditions (pressure, temperatures, flows, etc.) should be noted. The mass balance should be by component.

List what utilities will be required for the process. Electricity for pumps, in

struments, etc. What will be used to heat or cool process streams. Closed loop cooling water system, river water, steam, hot oil, etc. Instrument air and compressed air. Nitrogen for blanketing. Where will these utilities come from? tie-in to existing facilities? new facilities?

The process diagram needs to be broken into sections for P&ID's. Moderately detailed P&ID's should be developed for each section. Items from the following considerations will be added to the P&ID's.ENVIRONMENTAL: Will this plant require a permit? Will it be a new permit or amodification of an existing permit? What will be the disposition of vapors from process vents? process wastes?SAFETY: Where will relief valves or rupture disks be required? What will be the bases for sizing the devices? Platforms, ladders, and process flooring must b

e built to standards. Are there other safety issues?MATERIALS OF CONSTRUCTION: what materials are required for equipment, piping, utilities, etc. You will need to determine where corrosion can occur and what materials are appropriate for each service. If organic acids are to be used in an esterification plant, one should know that dilute amounts are very corrosive on 316 SS. Typically the service may require something like Sandvik 2205.INSULATION: Where will insulation be used? what type. One needs to be concerned about under insulation corrosion also particularly with mineral wool or Calsil.INSTRUMENTS: What type of control system will be used with this plant? DCS? S

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ingle loop controllers? PLC? What instruments will be required with each unitoperation for level, flow, temperature, pressure, etc.Pumps: what types and sizes of pumps will be needed for each application. Consider mechanical reliability here in the sealing and flush applications.Equipment Sizing: You should begin to estimate the size of reactors, distillation columns, heat exchangers and other equipment that will be needed in the process.Information from these items should be included on the P&ID's that you are compiling.When the P&ID's are as well defined as one can make them, a hazop study can be done. The question to be asked is, "what are the effects of deviations from design intent" If a heat exchanger loses coolant flow, what is the effect and are there any process alarms or actions needed for this possibility.You are also ready to begin the process of estimating the cost of the process.One can use the module/factor approach and arrive at a budget estimate. It hasbeen my experience that cost estimates, once given, are never forgotten. It has been my practice to try to produce a 10% estimate if possible. You have a wealth of detail at hand by now. Equipment estimates can be obtained from vendors.

Knowing the site and the equipment layout, you can begin to estimate lengths of pipe, conduit, etc. The Richardson system is a method that allows one to makea semi-detailed capital estimate of the components, labor, and indirect costs associated with a project.

I know there are many other details that I have not spoken of. You will need to

incorporate them as you come across them. Engineering standards and approved vendor lists for your employer have to be followed. Try to bring some improvement to as many of the unit operations as you can.

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If you are starting from scratch, and none of this information is available, then you need to sit down with the development chemist(s) and determine exactly what he/she does in the lab and why. It's important to understand what he/she finds easy to do and what is difficult. This isn't necessarily the same on the plant. Some things are easy in the lab, but very difficult on the plant (i.e. solids handling), whereas others are easier on plant than in the lab.

Then define a very basic flowscheme. What you are trying to do is copy what ishappening in the lab on a larger scale. Don't try to size individual items of equipment, yet, and don't try to add instrumentation - unless it will help you understand how it will work.

Once you have a basic outline you can start adding details.As epoisses says, the most important thing is to keep discussing it. Show youroutline to the chemist(s) and get feedback on it. They (or you) may have forgotten something. It's very important to work as a team. They will most likely be proud of what they have done, and seeing what looks like a plant based on whatthey have done will give them a buzz. Take advantage of their enthusiasm!Talk to others as well, people with experience of the chemicals or of the proces

s (of developing a chemical process from scratch). With their help, you can start adding equipment sizes and the detail you need as described by bchoate above.

Don't forget, that most companies have several decision gates in any project. Don't get into too much detail before you are certain that the project is going ahead to the next stage. Doing a basic outline first will enable you (or someone else in your company) to come up with a rough cost, and, equally important, how long you think it will take to build. Feeding this back to the decision makers will give you an early indication as to whether this project is really going to happen or not. This is very important - it can save you a lot of time. Keep t

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he dialogue going. Things change in the commercial world very, very quickly. It's no good designing the perfect plant if it's decided that the plant is no longer needed.

Doing a HAZOP is almost the last thing you do in the design, and is often only done once the money for the project has been approved. Don't worry about it until the very latter stages of the project. However, safety should be paramount in your design. In a perfect design, the HAZOP would be a rubber stamping exercise - your design should aim to make it so. Thinking about it, and designing around it at this very early stage makes it very much easier (and safer!) than trying to shoehorn changes in later on.