Method for regulation of the process conditions in a moulding tool

Abstract: Method for regulation of the process conditions in a moulding tool intended for production of products of natural or synthetic polymers, which moulding tool comprises one or more moulding parts made of sintered metal with communicating pores obtained by pressing at a high pressure and sintering at a high tempera­ ture of a powdered material, in which moulding part or parts a moulding cavity has then been made, whereby the pores are open towards the moulding cavity, while the outer envelope surface of the moulding tool is tightened against leakage, which comprises filling the communicating pores with a liquid with a high vapo­ rizing temperature and regulating the pressure on the liquid in the pores by means of a suitable pressure producer connected with the communicating pores in the moulding tool.

Description: The present invention relates to a method for regulation of the process conditions in a moulding tool intended for production of products of natural or synthetic polymers as laid out in claim 1, which moulding tool comprises one or more moulding parts made of sintered metal with communicating pores. The moulding parts are obtained by pressing a powdered material at a high pressure and sintering at a high temperature. A moulding cavity is then made in the moulding part or parts, whereby the pores are open towards the moulding cavity, while the outer envelope surface of the moulding tool is tightened against leakage. From the Swedish patent 8501589-9 it is known before to produce moulding parts of sintered metal, whereby the moulding parts get communicating pores. A moulding cavity is produced in the moulding parts, which together constitute a mould intended for production of products of natural or synthetic polymers by injection moulding. When the moulding cavity has been completed the envelope surfaces are tightened. The center of said known invention consists in the formation of a reservoir in the pore system of the mould for temporary reception of air or another gas formed at the injection moulding. When the mould is opened after each production cycle the gas is released again from the reservoir. The known process disclosed above works very well. At some applications there are, however, difficulties in regulating the process conditions in the moulding tool. Moreover, in certain cases the pores will be clogged by by-products formed at the moulding of the polymer products. For instance at injection moulding of thermoplasts in steel moulds, often about 80 % of the production cycle, consists of cooling time. The thermoplast is injected via a gate or another nozzle into the moulding cavity at a temperature of about 150-220°C. The plastic product is cooled in the moulding cavity by convection and the heat is removed by water cooling in channels situated outside the moulding chamber or drilled into the mould steel. When cooling channels are placed in the mould steel, you often get the problem that they make the mould construction weaker. Of course, this is especially true for small areas. A weak mould construction cannot be accepted. Therefore, certain areas of the mould are not provided with cooling channels, which of course results in an insufficient cooling. There is another considerable problem to be able to arrange cooling channels in connection with a complex moulding cavity. This results in an uneven cooling or tempering of the moulding cavity and also a deterioration of the quality of the plastic product. Another very frequent problem, especially at the production of big products, is that the flow paths i.e. the distance from the injection site to the middle of the product is so long that the plastic is cooled to much before it has filled the whole cavity. Then, often certain inner parts of the cavity will not be filled. Moreover, especially at the moulding of thermosetting resins and rubber there is a often big problem to release the product formed from the mould unless a lubricant has been manually applied to the moulding cavity before each moulding cycle. Said work is detrimental to the environment and very unpleasant. Sometimes it is also difficult to get all parts of a product made of thermosetting resin fully cured. Thus, there are big problems to regulate the process conditions at the moulding of synthetic and natural polymers such as thermoplasts, thermosets and rubber. JP-A-56-38213, from which the invention starts, discloses a moulding process which makes use of a release agent which enters the moulding cavity through a porous section of the mould part. The porous section is formed of a metal layer by flame spraying of fine metal powder. The permeation of the release agent can be accelerated through the porous part by using compressed air. US-A-3525783 discloses a process which makes use of a silicone fluid as a release agent in a moulding process. The mould is formed from a relatively thin silicone rubber material and includes a porous section through which the silicone fluid can permeate during moulding in order to act as a release agent. US-A-4177238 discloses a method for cooling an injection moulded plastic article by using a mould having at least some porous section which enables cooling liquid to flow into the moulding cavity. This cooling liquid is allowed to vaporize to absorb heat of vaporization from the mould dyes so leading to their cooling. The porous section of the mould material is formed of metallic material, and the pressure of the liquid can be varied during the moulding process by means of a pressure regulator in order to improve cooling. According to the present invention the above problems have been solved and a method for regulation of the process conditions in a moulding tool intended for production of products of natural or synthetic polymers has been brought about. The moulding tool comprises one or more moulding parts made of sintered metal with communicating pores obtained by pressing a powdered material at a high pressure and sintering at a high temperature. A cavity has then been made in the moulding part or parts. The pores are open towards the moulding cavity while the outer envelope surface of the moulding tool is tightened against leakage. The process according to the invention comprises filling the communicating pores with a liquid with a high vaporizing temperature. The pressure on the liquid in the pores is regulated by means of a suitable pressure produced connected with the communicating pores in the moulding tool. Usually the pressure is arranged to be automatically increased to counteract the inner pressure of the mould against the liquid in the pores when polymer is introduced into the closed moulding tool. The pressure is then automatically decreased when the moulding tool is opened again and the inner pressure of the mould is released. In this way the pores will preferably be filled with the above liquid during the whole production cycle. Since the pressure on the liquid in the pore system is regulated automatically in the disclosed manner, the liquid will preferably be stationary in the pore system. Thus, generally the liquid will not be pressed back into the pores from the moulding cavity when the inner pressure increases at the supply of polymer to the closed moulding tool. Accordingly, suitably the liquid will not pulse backwards and forwards in the pore system during the production cycle. However, in some cases the liquid may be allowed to be pressed back up to a few millimetres into the pores for a short time when the mould is closed. Then the liquid will be pressed forward again to reach the surface of the moulding cavity. A clogging of the pores will be awoided at said embodiment of the invention too. Advantageously, a pressure sensor is placed in connection with the moulding cavity to sense the pressure in the moulding cavity. Thereby, a precise pressure regulation can be achieved. The pressure sensor is then connected with the pressure producer and regulates the pressure on the liquid in the pores, applied by said pressure producer. The pressure producer can for instance be a pump or a gas container. If a gas container is used the gas will exert a pressure on the liquid. Of course the pressure in the gas container can be regulated to any desired value. Many different gases can be used. However, nitrogen, carbon dioxide or air can be mentioned as examples of suitable gases. At the use of carbon dioxide as a pressure medium the reaction conditions at the moulding of certain thermosetting resins can be influenced. Thus, at the curing of some thermosetting resins water is formed which together with the carbon dioxide form carbonic acid. In this way the pH of the resin in the mould will be decreased. Thereby, the curing reaction of the resin can be influenced. The gases also influence the wetting of the polymer material against the moulding cavity. At the moulding of a thermosetting resin a gaseous state curing agent or catalyst being inert to the liquid in the pores may be used as a pressure medium for said liquid. The curing agent or catalyst will pass through the liquid and reach the resin in the moulding cavity in a concentration being enough for curing of the resin. As examples of gaseous curing agents or catalysts, sulphur dioxide, a tertiary amine such as triethylamine or trimethylamine, methyl formate, ethyl formate or propyl formate can be mentioned. Usually said gaseous curing agents or catalysts are mixed with a carrier gas such as air or nitrogen. In this way the concentration of the curing agent or catalyst in the gas mixture can be varied in any desirable proportion. It is very important that the pressure is kept on such a level that the liquid will not spout out into the moulding cavity when the moulding tool is opened and the inner pressure of the mould is released. Instead the liquid should be forced out very slowly from the pores into the moulding cavity and form a thin layer on the surface of the moulding cavity. This layer can work as a lubricant or release agent in the moulding cavity. Therefore, a conventional lubricant or release agent which is sprayed in the moulding cavity or supplied in another way can often be avoided. Of course this is another advantage according to the invention. The liquid prevents the pores from being clogged by by-products formed at the moulding of the polymer products or by fillers etc in the polymer material used. Accordingly, such by-products will be included in the polymer product instead of clogging the pores in the porous moulding parts of the moulding tool. The liquid is intended for absorbing air, steam and other gases which are possibly formed at the moulding. These gases can then be released from the liquid when the moulding tool is opened after each production cycle. If necessary the liquid can also be removed from the pores at certain intervals to be degassed. Since the liquid is evenly distributed in the whole pore system an even tempering of the moulding tool is obtained. If necessary the moulding tool can be heated or cooled by outside aggregates and/or by circulating a temperature regulating medium via channels with tight walls arranged in the porous moulding parts or any other parts of the moulding tool. Usually, the temperature in the moulding tool is regulated to between about +50°C and about +240°C. However, of course it is possible to work outside said interval too. The limit upwards in temperature is the vaporizing temperature of the liquid used. Many different kinds of thermosets can be worked according to the invention. Polyester, polyurethane, urea-formaldehyde resin, phenol-formaldehyde resin and melamine-formaldehyde resin can be mentioned as examples on suitable plastics. The pore size of the sintered material can be varied within wide limits. However, suitably the average particle size is about 10-200 µm, preferably 10-100 µm. The moulding tool is mainly intended for injection moulding, compression moulding, blow moulding or extrusion. The liquid used can be a synthetic or a natural product such as an ester, silicon oil, wax or paraffin. The ester can consist of a reaction product of a polyhydric alcohol such as pentaerythritol, trimethylolpropane or neopentyl glycol and a monocarboxylic acid and/or a di-basic or tri-basic carboxylic acid. The liquid used, for example in the form of an ester has suitably hydrophilic properties, whereby the absorption of steam during the production cycle is facilitated. The hydrophilic properties can be obtained by an ammonium ion, a protonized amine or a protonized substituted amine in the ester. From a general point of view the following is valid for the liquid used according to the present invention: 1. It should not be charred at the use. 2. It should have a vaporizing temperature above the temperature existing in the moulding tool, i.e. usually above about 250°C. 3. It should be able to dissolve (absorb) gases released at the moulding. 4. It should be inert and not influence the properties of the polymer product produced. 5. It should not be oxidized at the use. The liquid used, for example in the form of an ester as disclosed above, can be used as such or as an aqueous solution or an aqueous emulsion. The water content can be varied within wide limits. However, normally it is between about 0.005 and about 15 per cent by weight, preferably about 0.1 and 12 per cent by weight or 0.5 and 8 per cent by weight. The liquid can also contain an emulsifier. The liquid used can suitably contain a component consisting of a mixture of compounds with the general formula: where R means R₁ means C₄H₉, C₅H₁₁, C₆H₁₃, C₇H₁₅, C₈H₁₇, C₉H₁₉, C₁₁H₂₃, C₁₃H₂₇, C₁₅H₃₁, C₁₇H₃₅, C₁₇H₃₃, C₁₇H₃₁, C₁₉H₃₉, C₂₁H₄₃, C₂₃H₄₇ or C₁₇H₃₄OH, where R₂ means CH₂, C₂H₄, C₃H₆, C₄H₈, C₇H₁₄, C₈H₁₆, C₂H₂, C₆H₄, C₆H₃COOH, C₆H₃COO⁻-NH₄⁺, or C₆H₁₀ and R₃ ⊕ consists of an ammonium ion, a protonized monoethanolamine, diethanolamine, triethanolamine, diisopropanolamine, triisopropanolamine, N,N-dimethylethanolamine, N,N-dimethylaminometylpropanol, aminomethylpropanol, triethylamine or morpholine, at the same time as the compounds in the mixture only differ from each other in respect of the values for m, n and p, so that also the mixture can be represented by the above formula I, whereby the mean value ( m ) for m is between 3 and 8, the mean value ( n ) for n is less than ( m ) and the mean value ( p ) for p is between 0.5 and 8, preferably between 0.5 and 3. One suitable component to be used according to the invention has the above formula where R means R₁ means C₇H₁₅ eller C₁₇H₃₃, n = 2.0 - 3.5 R₂ means C₂H₄, C₃H₆, C₄H₈, C₇H₁₄, C₈H₁₆, C₂H₂ or C₆H₄; R₃ ⊕ means a protonized triethanoamine, diethanolamine, N,N-dimethylaminomethylpropanol, N,N-dimethylethanolamine or triisopropanolamine p = 0.5 - 2.0 and m = 4. Other specific compounds suitable to be used according to the invention have the above formula, where R means R₁ means C₇H₁₅ or C₁₇H₃₃, n = 1.0 - 2.5 R₂ means C₂H₄, C₃H₆, C₄H₈, C₇H₁₄, C₈H₁₆, C₂H₂ or C₆H₄; R₃ ⊕ means a protonized triethanolamine, diethanolamine, N,N-dimethylaminomethylpropanol, N,N-dimethyletanolamine or triisopropanolamine; p = 0.5 - 1.5 and m = 3. The present invention will be explained further in connection with the embodiment examples below, of which examples 1-7 relate to the production of specific components intended to be used according to the invention. Examples 1-7 show the components before neutralization, while examples 8-14 show corresponding components after neutralization. Example 1 1 mole (136.2 g) trimethylol propane (TMP), 1 mole (273,3 g) oleic acid and 65 g xylene were charged into a glass bulb provided with a stirrer, a water separator, a thermometer and an inert-gas supply. The xylene was used for azeotropic removal by distillation of esterification water formed. The temperature was raised successively to 250°C, whereupon esterification water formed was separated. At an acid number less than 3 mg KOH/g the reaction was stopped. Remaining xylene was separated under vacuum. The product obtained, 391.5 g TMP-oleate with an OH-value of 285 mg KOH/g, was a bright pale oil at 20°C. 1 mole (391.5 g) TMP-oleate as produced above was reacted at a temperature of 150°C with 1 mole (148.2 g) phthalic anhydride in a glass bulb provided with a stirrer and a thermometer. Then 539 g TMP-oleate phthalate with an acid value of 99 mg KOH/g was obtained. The product was a viscous oil at 20°C. Example 2 1 mole (138.4 g) pentaerythritol (PENTA), 2.7 moles (427.1 g) pelargonic acid (an aliphatic C₉-acid) and 65 g xylene were charged into a glass bulb provided with a stirrer, a water separator, a thermometer and an inert-gas supply. The temperature was raised successively to 250°C, whereupon esterification water formed was separated. At an acid number less than 3 mg KOH/g the reaction was stopped. Remaining xylene was separated under vacuum. 517 g PENTA pelargonate in the form of a bright, pale oil at 20°C and with an OH-value of 135 mg KOH/g was obtained. 1 mole (517 g) PENTA pelargonate was reacted at a temperature of 150°C with 1 mole (98 g) maleic acid anhydride in a glass bulb provided with a stirrer and a thermometer. Thereby, 609 g PENTA pelargonate maleate with an acid number of 88 mg KOH/g was obtained after suction filtration. The product was a bright, pale oil at 20°C. Example 3 1 mole (138.4 g) pentaerythritol (PENTA), 3 moles (432 g) 2-ethyl-hexanoic acid and 65 g toluene were charged into a glass bulb provided with a stirrer, a water separator, a thermometer and an inert-gas supply. The toluene was used for azeotropic removal by distillation of esterification water formed. The temperature was raised successively to 250°C, whereupon esterification water formed was separated. At an acid number less than 3 mg KOH/g the reaction was stopped. Remaining toluene was separated. 517 g PENTA-2-ethylhexoate with an OH-value of 108 mg KOH/g was obtained. The product was a bright, pale oil at 20°C. 1 mole (517 g) PENTA-2-ethylhexoate was reacted with 1 mole (146.1 g) adipic acid under nitrogen gas atmosphere in a glass bulb provided with a stirrer and a thermometer in the presence of toluene and at a temperature of 250°C. The reaction was continued for 1.5 hours, whereupon esterification water formed was separated. Then the toluene was separated under vacuum. 641 g PENTA-2-ethylhexoate adipate with an acid number of 80 mg KOH/g was obtained. The product was a low viscous oil at 40°C. Example 4 1 mole (138.4 g) pentaerythritol (PENTA), 1 mole (273.3 g) oleic acid and 65 g xylene were charged into a glass bulb provided with a stirrer, a water separator, a thermometer and an inert-gas supply. The temperature was successively raised to 250°C, whereupon esterification water formed was separated. At an acid number less than 1 mg KOH/g the reaction was stopped. Remaining xylene was separated under vacuum. The product was pressure filtered to remove unreacted PENTA. 370 g PENTA-oleate with an OH-value of 226 mg KOH/g was obtained. The product was viscous light-brown oil at 20°C. 286 g PENTA-oleate was reacted at a temperature of 150°C with 108 g phthalic anhydride in a glass bulb provided with a stirrer and a thermometer. After a filtration 355 g PENTA-oleate phthalate with an acid number of 98 mg KOH/g was obtained. The product was a viscous oil at 20°C. Example 5 1 mole (136.2 g) trimethylol propane (TMP), 2.2 moles (317 g) 2-ethylhexanoic acid and 20 g xylene were charged into a glass bulb provided with a stirrer, a water separator, a thermometer and an inert-gas supply. The xylene was used for azeotropic removal by distillation of esterification water formed. The temperature was raised successively to 260°C, whereupon esterification water formed was separated. At an acid number less than 2 mg KOH/g the reaction was stopped. Remaining xylene was separated under vacuum. 411 g TMP-2-ethylhexoate with an OH-value of 99 mg KOH/g was obtained. The product was a pale low viscous oil at 20°C. 1 mole (411 g) TMP-2-ethylhexoate and 0.8 mole (117 g) adipic acid were charged into a glass bulb provided with a stirrer, a thermometer and an inert-gas supply. The temperature was raised successively to 250°C and kept there for 30 minutes at atmospheric pressure and then for another 30 minutes under vacuum (a pressure of 100 mm Hg). Then 514 g TMP-2-ethylhexoate adipate with an acid number of 91 mg KOH/g was obtained. The product was a low viscous oil at 40°C. Example 6 1 mole (517 g) PENTA-2-ethylhexoate produced according to Example 3 was reacted with 1 mole (188 g) azelaic acid at 250°C under nitrogen gas atmosphere in a glass bulb provided with a stirrer and a thermometer. The reaction was continued for 1.5 hours at atmospheric pressure and thereafter for another 30 minutes under vacuum (a pressure of 80 mm Hg). All the time the temperature was 250°C. Then 680 g PENTA-2-ethylhexoate azelate with an acid number of 72 mg KOH/g was obtained. The product was a low viscous oil at 40°C. Example 7 1 mole (250 g) di-trimethylol propane (Di-TMP), 2.8 moles (403 g) 2-ethylhexanoic acid and 30 g xylene were charged into a glass bulb provided with a stirrer, a water separator, a thermometer and an inert-gas supply. The xylene was used for azeotropic water separation. The temperature was raised slowly to 260°C, whereupon esterification water formed was separated. At an acid number less than 2 mg KOH/g the heating was interrupted and remaining xylene was separated under vacuum. 603 g Di-TMP-2-ethylhexoate with an OH-value of 109 mg KOH/g was obtained. The product was a pale low viscous oil at 20°C. 1 mole (603 g) Di-TMP-2-ethylhexoate and 1.2 moles (175 g) adipic acid were charged into a glass bulb provided with a stirrer, a thermometer and an inert-gas supply. The temperature was raised successively to 250°C and kept there for 30 minutes at atmospheric pressure and then for another 30 minutes under vacuum (a pressure of 100 mm Hg). Then 756 g Di-TMP-2-ethylhexoate adipate with an acid number of 87 mg KOH/g was obtained. The product was a low viscous oil at 40°C. Example 8 25 g TMP-oleate phthalate produced according to Example 1 was mixed with 4 g N,N-dimethyl ethanolamine. 1 g water was added at stirring to the mixture obtained whereby a mixture containing 3.3 per cent of water was obtained. The mixture is very suitable as a heat storing and temperature equalizing liquid in the pores of the moulding parts made of sintered metal of a moulding tool for example intended for injection moulding or compression moulding of plastic products. The mixture will also prevent the pores from being clogged by by-products formed at the moulding of the polymer products or by fillers etc. in the plastics material used. Example 9 25 g PENTA pelargonate maleate produced according to Example 2 was mixed with 10 g triethanolamine. 2 g water was added at stirring to the mixture obtained, whereby a mixture containing 5.4 per cent of water was obtained. This mixture can be used for the same field of use as mentioned in Example 8. Example 10 25 g PENTA-2-ethylhexoate adipate produced according to Example 3 was mixed with 10 g triethanolamine. 0.5 g water was added at stirring to the mixture obtained, whereby a mixture containing 1.4 per cent of water was obtained. This mixture can be used for the same field of use as mentioned in Example 8. Example 11 25 g PENTA-oleate phthalate produced according to Example 4 was mixed with 10 g triisopropanol amine. 3 g water was added at stirring to the mixture obtained, whereby a mixture containing 7.9 per cent of water was obtained. This mixture could be used for the same field of application as disclosed in Example 8. Example 12 25 g TMP-2-ethylhexoate adipate produced according to Example 5 was mixed with 3.6 g diethanolamine and 2.9 g diethyleneglycol monobutylether. 3 g water was added at stirring to the mixture obtained, whereby a mixture containing 8.7 per cent of water was obtained. The mixture was very suitable for the same field of application as disclosed in Example 8. Example 13 25 g PENTA-2-ethylhexoate azelate produced according to Example 6 was mixed with 12 g triethanolamine and 3.7 g diethyleneglycol monobutylether. 5 g water was added to the mixture obtained, whereby a mixture containing 12.3 per cent of water was obtained. The mixture was very suitable for the same field of application as disclosed in Example 8. Example 14 25 g Di-TMP-2-ethylhexoate adipate produced according to Example 7 was mixed with 5.2 g N,N-dimethylaminomethyl propanol and 3.0 g diethylenglycol monobutylether. 4 g water was added to the mixture obtained, whereby a mixture containing 10.8 per cent of water was obtained. The mixture is very suitable for the same field of application as mentioned in Example 8. The invention is not limited to the embodiments shown, since these can be modified in different ways within the scope of the present invention.

Claims: Method for regulation of the process conditions in a moulding tool intended for production of products of natural or synthetic polymers, which moulding tool comprises one or more moulding parts made of sintered metal with communicating pores obtained by pressing at a high pressure and sintering at a high temperature of a powdered material, in which moulding part or parts a moulding cavity has then been made, whereby the pores are open towards the moulding cavity, while the outer envelop surface of the moulding tool is tightened against leakage, which comprises filling the communicating pores during the entire production cycle with a liquid having a high vaporisation temperature, which is stationary during said cycle in the pores system, and regulating the pressure on the liquid in the pores by means of a suitable pressure producer connected with the communicating pores in the moulding tool in such a manner that the liquid will be forced out of the pores into the moulding cavity and from a thin layer on the surface of the cavity; wherein a thermosetting resin is moulded and a gaseous curing agent or catalyst, which is inert to the liquid in the pores, is used as a pressure medium for said liquid, which curing agent or catalyst will pass through the liquid and reach the resin in the closed moulding cavity in a concentration large enough to cure the thermosetting resin. Method according to claim 1, wherein the pressure is automatically increased to counteract the inner pressure of the mould against the liquid in the pores when polymer is introduced into the closed moulding tool and the pressure is automtically decreased when the moulding tool is opened again and the inner pressure of the mould is released. Method according to any one of claims 1-2, characterized in that the liquid prevents the pores from being clogged by by-products formed at the moulding of the polymer products or by fillers etc in the polymer material used. Method according to any one of claims 1-3, characterized in that the liquid is intended to absorb air, steam and other gases which are possibly formed at the moulding, whereby said gases can then be released from the liquid when the moulding tool is opened after each production cycle. Method according to any one of claims 1-4 characterized in that an even tempering in the moulding tool is obtained by the distribution of the liquid in the whole pore system. Method according to any one of claims 1-5, characterized in that the moulding tool is heated or cooled by outside aggregates and/or by circulating a temperature regulating medium via channels with tight walls arranged in the porous moulding parts or any other parts of the moulding tool. Method according to claim 6, characterized in that the temperature in the moulding tool is regulated to between about +50°C and about +240°C. Method according to any one of claims 1-7, characterized in that the moulding tool is intended for injection moulding, compression moulding, blow moulding or extrusion. Method according to claim 8., characterized in that the resins can consist of polyester, polyurethane, urea-formaldehyde, phenol-formaldehyde or melamine-formaldehyde. Method according to any one of claims 1-9, characterized in that the liquid works as a lubricant or a release agent in the moulding cavity. Method according to any one of claims 1-10, characterized in that the liquid used is a synthetic product or a natural product, such as an ester, silicon oil, wax or paraffin. Method according to claim 11, characterized in that the ester consists of a reaction product of a polyalcohol such as pentaerythritol, trimethylol propane or neopentyl glycol and a monocarboxylic acid and/or a di-basic or tri-basic carboxylic acid. Method according to claim 12, characterized in that the synthetic product has hydrophilic properties. Method according to claim 13, characterized in that the hydrophilic properties are obtained by an ammonium ion, a protonized amine or a protonized substituted amine in the ester. Method according to any one of claims 1-14, characterized in that a pressure sensor is placed in connection to the moulding cavity to sense the pressure in the moulding cavity, whereby the pressure sensor is connected with the pressure producer and regulates the pressure on the liquid in the pores, applied by said pressure producer. Method according to any one of claims 1-15, characterized in that the pressure producer is a gas container, whereby the gas exerts a pressure on the liquid. Method according to claim 16, wherein the gas consists of nitrogen, carbon dioxide or air. Method according to claim 1, wherein the gaseous curing agent or catalyst is sulphur dioxide, a tertiary amine, such as triethylamine or trimethylamine, methyl formate, ethyl formate or propyl formate. Method according to any one of claims 1-18, characterized in that the liquid used contains a component consisting of a mixture of compounds with the general formula where R means R₁ means C₄H₉, C₅H₁₁, C₆H₁₃, C₇H₁₅, C₈H₁₇, C₉H₁₉, C₁₁H₂₃, C₁₃H₂₇, C₁₅H₃₁, C₁₇H₃₅, C₁₇H₃₃, C₁₇H₃₁, C₁₉H₃₉, C₂₁H₄₃, C₂₃H₄₇ eller C₁₇H₃₄OH, where R₂ means CH₂, C₂H₄, C₃H₆, C₄H₈, C₇H₁₄, C₈H₁₆, C₂H₂, C₆H₄, C₆H₃COOH, C₆H₃COO⁻-NH₄⁺, or C₆H₁₀ and R₃ ⊕ consists of an ammonium ion, a protonized monoethanolamine, diethanolamine, triethanolamine, diisopropanolamine, triisopropanolamine, N,N-dimethylethanolamine, N,N-dimethylaminometylpropanol, aminomethylpropanol, triethylamine or morpholine, at the same time as the compounds in the mixture only differ from each other in respect of-the values for m, n and p, so that also the mixture can be represented by the above formula I, whereby the mean value ( m ) for m is between 3 and 8, the mean value ( n ) for n is less than ( m ) and the mean value ( p ) for p is between 0.5 and 8, preferably between 0.5 and 3. Method according to claims 19, characterized in that R means R₁ means C₇H₁₅ eller C₁₇H₃₃, n = 2,0 - 3,5 R₂ means C₂H₄, C₃H₆, C₄H₈, C₇H₁₄, C₈H₁₆, C₂H₂ or C₆H₄; R₃ ⊕ means a protonized triethanolamine, diethanolamine, N,N-dimethylaminomethylpropanol, N,N-dimethylethanolamine or triisopropanolamine p = 0.5 - 2.0 and m = 4. Method according to claim 20, characterized in that R means R₁ means C₇H₁₅ or C₁₇H₃₃, n = 1,0 - 2,5 R₂ means C₂H₄, C₃H₆, C₄H₈, C₇H₁₄, C₈H₁₆, C₂H₂ or C₆H₄; R₃ ⊕ means a protonized triethanolamine, diethanolamine, N,N-dimethylaminomethylpropanol; N,N-dimethyletanolamine or triisopropanolamine; p = 0.5 - 1.5 and m = 3. Method according to any one of claims 1-21, characterized in that the liquid used contains an emulsifier.

Inventors: ABERG ANDERS B H, LARSSON OWE G T, ABERG, ANDERS B. H., LARSSON, OWE G. T.
Applicants: AGA AB, AGA AKTIEBOLAG
Application year: 1989
Main classification: B29C33
IPC codes: B29C45, B22F5, B29C35, B29C33