carbon monoxide in order to dissociate inlubiting complex and/or prevent or lessen coordination of the organomono› phosphite ligand with $_{the }$metal-organopolyphosphite ligand complex catalyst and facilitate its hydrolysis, then the hydroforrnylation is operated in a reaction region where control of carbon monoxide partial pressure. hydrogen par› tial pressure. total reaction pressure. hydroformylation reac› tion rate and/or temperature is more difficult. may cycle during continu› 

Hydroforrnylation reaction rate ous operation in a continuous stirred tank reactor as may carbon monoxide partial pressure. hydrogen partial pressure. total reaction pressure, hydroformylation reaction rate and/ or temperature if one $_{is }$hydroformylating under conditions where the reaction is of negative or inverse order in carbon monoxide. Cycling conditions disrupt steady operation of the unit. U niforrn partial pressures and temperature are desired. As used herein. "cycling" refers to frequent periodic and extreme changes in process parameters, e.g .• reaction rate. reaction temperature. total reaction pressure. carbon monoxide partial pressure, hydrogen partial pressure and total reaction pressure. during $_{the }$hydroformylation process. operating under con› 

The cycling may be initiated when ditions were the rate $_{of }$hydroformylation is inverse order in carbon monoxide. These conditions are not normally encountered with conventional triphenylphosphine- modified metal catalysts since the region where carbon monoxide is of negative rate order is also a region which gives lower isomer ratios and increased catalyst deactiva› tion. $_{Conventional }$triphenylphosphine-modified metal cata› lysts typically operate under conditions where increasing carbon monoxide partial pressure increases reaction rate and conversely decreasing carbon monoxide partial pressure decreases rate. pressures provide desired 

Higher carbon monoxide partial benefits $_{in }$organopolyphosphite modified metal catalysts in that olefin efficiency losses due to hydrogenation may be reduced and the dissociation of an inhibiting organomono› phosphite from the catalyst is favored. The dissociated or uncoordinated inhibiting organomonophosphite is more readily hydrolyzed and the hydrolysis fragments can be scrubbed from the solution as disclosed herein. Higher carbon monoxide partial pressures give both a higher lined out activity and lower efficiency losses to alkanes since the higher carbon monoxide partial pressure makes it a more effective competitor for a metal, e.g., rhodium, alkyl. If carbon monoxide reacts with the metal. e.g., rhodium. alkyl, the acyl precursor of the aldehyde is obtained; if hydrogen reacts with the metal, e.g .• rhodium. alkyl. the corresponding alkane is obtained. However. as indicated above. operating at the higher carbon monoxide partial pressures where hydroformylation is of a negative order significantly com› plicates control of partial pressures. the temperature dif› 

It is normally desirable to increase ference between the reaction temperature and the reactor cooling means, e.g., coolant. so that the equipment size can be minimized. Some have disclosed running at reactor temperatures hot enough to generate useful steam from the exothermic heat of reaction. A typical non-aqueous triph› enylphosphine system will have a temperature difference of approximately 30° C. between the reaction and the coolant. equipment is an important 

Design of the heat removal aspect of controlling the reaction partial pressures in this invention where the process is operated in inverse or nega› tive order in carbon monoxide. The temperature difference between the reaction product fluid temperature and the inlet coolant temperature should be small to provide the neces› sary control. The lower the temperature difference the better 

the control will be. For hydroformylation in regions where the reaction is of a negative order in carbon monoxide. the difference should be below 25° C. and more preferably below 20° C. Temperature difference below 15 ° C. may be achieved using heat transfer means such as evaporative cooling. enhanced heat transfer or larger equipment. used for exothermic 

Continuous stirred tank reactors reactions must have some means of removing the heat of reaction from the reactor. The cooling can be accomplished in a number of ways. putting a cooling jacket around the reactor, installing cooling coils in the reactor. or pumping the reactor solution through an external heat exchanger. In all cases the driving force for the heat removal is the tempera› ture difference between the reaction product fluid and the reactor zone coolant. by temperature. and 

Most chemical reactions are affected by some or all of the reactant concentrations. If a catalyst is used. its concentration also will affect the reaction rate. In most circumstances it is desirable to control the conditions in the reactor at some steady state. Changes in conditions may cause undesirable changes in selectivity. catalyst per- formance or other operational difficulties. Temperature has an exponential effect on $_{the }$hydroformylation reaction rate. A change in reaction temperature of 10° C. typically doubles the rate of reaction. If the reaction rate increases, the heat generated increases, and the extra heat must be removed to keep the temperature from continuing to increase. a system is described by the 

Removal of heat from following equation: 

Heat Removed=UMT 

35 wherein U is a heat transfer coefficient dependent on the conditions on both the process and coolant sides of the equipment. A is the surface area available for heat transfer, and ~Tis the appropriate temperature difference between the reaction product fluid temperature and inlet coolant tem› perature. At steady state, 

Heat Removed=Heat Generated by the reaction. 

As an illustration, assume a reaction is only dependent on reaction temperature. If for some reason the reactor tem› perature increases by 1 ° C .• the reaction rate will increase by approximately 10% which will in turn generate 10% more heat. If nothing is changed with the reaction zone cooler. the heat removed will depend on the new AT of the system. If the original AT was 5° C., the new AT will be 6° C.. a 20% (i.e. $^{1}$/s) increase in heat removed which tends to drive the system back to the original set of steady conditions. product fluid and 

If instead of a 5° C. ~T between reaction reaction zone coolant. e.g., heat exchanger. the ~T was 20° C .. a 1 ° C. increase in reactor temperature will give a new temperature difference between reaction product fluid and reaction zone coolant. e.g.. heat exchanger. of 21 ° C’. Whereas the reaction rate increased by 10%, there was only a 5% (i.e. ‰o) increase in the heat removal capability. Since more heat is being generated than is being removed. the reactor would continue to wann until some action is taken to increase the heat transfer from the system or until the reactant(s) were exhausted. of negative order, in order to 

When carbon monoxide is have an intrinsically stable system, a disturbance in the temperature must produce a smaller percentage increase in reaction rate than the percentage increase in ~T of the system. As used herein. "inlet coolant temperature" refers to the temperature of the coolant prior to entering any heat transfer means. e.g .. internal coils, external jackets. shell and 

