although pvc resin shows superior physical and chemical properties , the resin has an inherent physical property drawback - poor processability , in other words , its higher processing temperature approaches its decomposition temperature that results in a serious risk of decomposition , thus the application scope thereof is limited . to solve this deterioration problem , processing aids are developed to be incorporated in pvc resin , thus both of soft pvc or rigid pvc show a great innovation . so presently all pvc resin processors add processing aids to let pvc resin show better fusion . for this reason , an extra processing aid should be incorporated in pvc resin to get better fusion and overcome the deterioration problem during processing . after several years tests , research and development , the inventor of the present invention finds that alkyl acrylates monomers or alkyl acrylates polymers are added into a vinyl halide monomer or a vinyl halide monomer based polymerizable monomer mixture to conduct graft or copolymerization via a solution , bulk , or suspension process , the resulted polyvinyl halide resin without the addition of any processing aid shows superior fusion , lubrication and high transparency . the processed products thereof also show good processing properties , such as low flow - mark , low air - mark and high melt strength etc ., thus can be used in various polyvinyl halide applications : such as processing techniques including roll mill , extrusion , blown film , foaming etc ., and the resulted products contain soft , semi - rigid and rigid types with transparent , semi - transparent and non - transparent appearances , especially the transparent rigid product shows excellent transparency , high gloss and low haze . according to the invention , the functional polyvinyl halide resin is produced as follows : ( 1 ) 10 . 0 wt % ˜ 0 . 1 wt % based on the total composition of alkyl acrylate monomers or alkyl acrylate / acrylate based polymer latex or powder ; ( 2 ) 90 . 0 wt % · 99 . 9 wt % based on the total composition of a vinyl halide monomer or a vinyl halide monomer based polymerizable monomer mixture ; are used to conduct copolymerization or graft - reaction , wherein the vinyl halide monomer or the vinyl halide monomer based polymerizable monomer mixture can added stepwisely or all in one time , and the percentage of the vinyl halide monomer in the vinyl halide monomer based polymerizable monomer mixture should be not less than 55 %. alkyl acrylate monomers or alkyl acrylate / acrylate based polymer latex or powder is continuously fed during polymerization or added before polymerization ; the way of the polymer latex addition is to be fed into a polymerization reactor before polymerization reaction , or continuously fed into the reactor during reaction , while the polymer powder is incorporated into the polymerization reactor prior to the reaction . continuously batchwisely added in the polymerization of the invention , the alkyl acrylate monomers are selected from methyl methacrylate ( mma ), ethyl methacrylate , n - propyl methacrylate , isopropyl methacrylate , n - butyl methacrylate , isobutyl methacrylate , stearyl methacrylate , phenyl methacrylate , benzyl methacrylate , all of them can be substituted with the following groups ; halogen , hydroxyl , alkoxy , alkylthio , cyano etc . according to the present invention , the above mentioned alkyl acrylates / acrylates polymer latex / powder can be an optional grafting or core - shell structures including unicore - unishell , unicore - multishell , multicore - unishell or multicore - multishell . the composition of two core - shell structures in the latex can be adjusted in accordance with the desired physical properties . the acrylic copolymer latex / powder added during the polymerization is produced by an emulsion , solution or bulk polymerization in the mode of an optional grafting . it has different structures including unicore - unishell , unicore - multishell , multicore - unishell or multicore - multishell . in addition , the acrylic copolymer powder can be produced by spray dryer and salt out . latex is a polymer with the core - shell structure , and can be produced via a solution or emulsion polymerization , and the way of polymerization may be a batchwise , semi - batchwise or continuous mode . latex can be dried with salt - out or spray - drying to become a powder . latex can be added continuously into the polymerization reactor during polymerization or added prior to polymerization to conduct copolymerization or graft - reaction . the dose of latex or powder is 10 . 0 %˜ 0 . 01 % or 10 . 0 %˜ 0 . 1 % based on the weight of the vinyl halide monomer or the polymerization monomers mixture . in the present invention , the aforementioned resin powder obtained from a vinyl halide monomer or a vinyl halide monomer based polymerizable monomer mixture includes vinyl halide homo - polymer and copolymer , for example , polyvinyl chloride or copolymer of vinyl chloride and other monomers , wherein copolymer is made from the copolymerization of more than 50 wt % of vinyl halide and the balance of other monomers . the monomers to be copolymerized contain vinyl alkanoates , such as vinyl acetate ; vinylidene halides , such as vinylidene chloride ; alkyl esters of carboxylic acids , such as acrylic acid , ethyl acrylate , 2 - ethyl hexyl acrylate , etc . and unsaturated hydrocarbons , such as allyl acetate , etc . the initiator used in the polymerization of the functional polyvinyl halide composites is a water soluble or oil soluble organic peroxide which can generate a free radical under heating , e . g . hydroperoxides , dialkyl peroxide , peroxyketal , diacyl peroxide , peroxyester , peroxymonocarbonate , peroxydicarbonates etc ., or a photo - decomposable initiator . all of them are known from the arts and can be applied in the polymerization of the present invention . as for dispersants which are also known in the arts , partially hydrolyzed polyvinyl alcohols ( pva ) with different degrees of hydrolysis and hydroxyl propyl methyl celluloses ( hpmc ) with different viscosities may be also incorporated in the reaction . depending on the actual demand , other heat stabilizers , lubricants , colorants , plasticizers or fillers may be added together in compounding . now the invention is further explained with examples which are used to illustrate the features of the present invention , without restricting the invention in any way whatsoever . 70 kg of de - ionic pure water , 56 g of a dispersant - polyvinyl alcohol ( pva with a hydrolysis degree of 78 mol %) are added into a 200 liter polymerization tank . after firmly closing the cap of the tank and evacuated to − 740 mmhg of vacuum for 10 minutes , 70 kg of vinyl chloride monomer and 0 . 7 g of a peroxide initiator of tert - butyl peroxyneodecanote ( bnd ) are incorporated under a paddle stirrer agitation with a rotation speed of 390 rpm and raising the temperature to 64 ° c . to proceed polymerization for 5 hours , then an antioxidant is added to stop polymerization upon a pressure drop of − 1 . 5 kg / cm 2 , the un - reacted vinyl chloride monomer is recycled , and pvc product is discharged , dried to become a powder sample . 70 kg of de - ionic pure water , 56 g of a dispersant - polyvinyl alcohol ( pva with a hydrolysis degree of 78 mol %) are added into a 200 liter polymerization tank . after firmly closing the cap of the tank and vacuumized to − 740 mmhg for 10 minutes , 70 kg of vinyl chloride monomer and 0 . 56 g of a peroxide initiator - bnd ( tert - butyl peroxyneodecanote ) are incorporated with raising the temperature to 64 ° c . to proceed polymerization for 90 minutes , then a monomer mixture of methyl methacrylate ( mma ) and butyl acrylate ( ba ) is continuously added for 30 minutes . after the addition is completed , a polymerization reaction is proceeded for 3 hours , then a powder sample is collected , wherein the proportion of mma and ba in the continuous feed is 140 g vs 28 g . 70 kg of de - ionic pure water , 56 g of a dispersant - polyvinyl alcohol ( pva with a hydrolysis degree of 78 mol %), 140 g of mma and 28 g of ba are added into a 200 liter polymerization tank . after firmly closing the cap of the tank and evacuated to − 740 mmhg of vacuum for 10 minutes , 70 kg of vinyl chloride monomer and 0 . 56 g of a peroxide initiator - bnd are incorporated with raising the temperature to 64 ° c . to proceed polymerization for 5 hours , then stopping the reaction , and a powder sample is collected . after drying , the resulted pvc powder is conducted the following physical property tests : example formulation : pvc ( k = 60 ): 100 parts , organotin stabilizer : 1 . 1 parts , lubricant : 0 . 6parts , operation temperature : 190 ° c ., time : 3 minutes , sheet thickness : 0 . 3 mm . comparative example formulation : pvc ( k = 60 ): 100 parts , organotin stabilizer : 1 . 1 parts , processing aid : 1 . 2 parts , lubricant : 0 . 6 parts , operation temperature : 190 ° c ., time : 3 minutes , sheet thickness : 0 . 3 mm . example formulation : pvc ( k = 60 ): 100 parts , organotin stabilizer : 1 . 1 parts , lubricant : 0 . 6 parts , plasticorder : haake buchler system 40 , set temperature : 140 ° c ., rotation speed : 45 rpm . comparative example formulation : pvc ( k = 60 ): 100 parts , organotin stabilizer : 1 . 1 parts , processing aid : 1 . 2 parts , lubricant : 0 . 6 parts , plasticorder : haake buchler system 40 , set temperature : 140 ° c ., rotation speed : 45 rpm . example formulation : pvc ( k = 60 ): 100 parts , organotin stabilizer : 1 . 1 parts , lubricant : 0 . 6 parts , time : 3 minutes , sheet thickness : 0 . 3 mm . sheet air - mark and flow - mark are evaluated via observation . comparative example formulation : pvc ( k = 60 ): 100 parts , organotin stabilizer : 1 . 1 parts , processing aid : 1 . 2 parts , lubricant : 0 . 6 parts , operation temperature : 190 l , time : 3 minutes , sheet thickness : 0 . 3 mm . sheet air - mark and flow - mark are evaluated via observation . example formulation : pvc ( k = 60 ): 100 parts , organotin stabilizer : 1 . 1 parts , lubricant : 0 . 6 parts , operation temperature : 190 l , time : 3 minutes , sheet thickness : 0 . 3 mm . the thickness of the compressed sheet is 0 . 5 cm which is tested with a integration ball type spectrometer ( hunterlab color quest xe ). comparative example formulation : pvc ( k = 60 ): 100 parts , organotin stabilizer : 1 . 1 parts , processing aid : 1 . 2 parts , lubricant : 0 . 6 parts , operation temperature : 190 l , time : 3 minutes , sheet thickness : 0 . 3 mm . the thickness of the compressed sheet is 0 . 5 cm which is tested with a integration ball type spectrometer ( hunterlab color quest xe ). the test results of the above 4 performance tests are listed in table 1 . according to table 1 , the processing properties of example 1 are better than those of example 2 , and its fusion is obviously faster , thus the continuous injection of the alkyl acrylate monomer liquid mixture is the best process , but the reactor cleanness of examples 1 & amp ; 2 is worse than that of the comparative example . acrylate / alkyl acrylate polymers latex or powder and vinyl chloride monomer are copolymerized or graft - reacted to obtain a functional polyvinyl chloride , wherein the acrylate polymers are prepared as follows : preparation of alkyl acrylate / acrylate polymer latex / powder : 4 different polymers ( a b c d ) are prepared as follows : 720 parts of de - ionic pure water , 2 . 0 parts of potassium oleate , 0 . 005 parts of ethylene di - amine tetra acetic acid tertsodium salt ( edta ) and 0 . 005 parts of ferrous sulfate ( feso 4 . 7h 2 o ) are added in 1 liter of a polymerization tank , after tightly closing the cover of the tank , vacuumized to − 740 mmhg and keeping for 10 minutes , nitrogen is introduced to raise the pressure to 1 kg / cm 2 , the temperature is elevated to 40 l under stirring , then 0 . 25 parts of sodium formaldehyde sulfoxylate ( sfs ) is incorporated into the reaction tank , after 3 minutes , all of 80 parts of methyl methacrylate ( mma ), 10 parts of ethyl acrylate ( ea ), 10 parts of butyl methacrylate ( bma ) and 0 . 5 parts of cumyl hydroperoxide ( chp ) are added into the tank to conduct the reaction for 1 hour , thus a core - layer latex ( a ) with a average particle diameter of 128 nm is obtained . 720 parts of de - ionic pure water , 2 . 0 parts of potassium oleate , 0 . 005 parts of ethylene di - amine tetra acetic acid tertsodium salt ( edta ), 0 . 005 parts of ferrous sulfate , 0 . 25 parts of sodium formaldehyde sulfoxylate ( sfs ), 45 parts of butyl acrylate ( ba ), 55 parts of styrene ( sm ) and 0 . 5 parts of cumyl hydroperoxide ( chp ) are added in 1 liter of a polymerization tank , thus a core - layer latex ( b ) with a average particle diameter of 113 nm is obtained . 20 ˜ 90 parts of core - layer seed latex ( a ) or ( b ), 0 . 01 parts of edta and 0 . 01 part of ferrous sulfate are fed into a 1 liter polymerization tank , after tightly closing the cover of the tank , evacuated to − 740 mmhg of vacuum and keeping for 10 minutes , nitrogen is introduced to raise the pressure to 1 kg / cm 2 , the temperature is elevated to 40 l under stirring , then 0 . 35 parts of sodium formaldehyde sulfoxylate ( sfs ) is incorporated into the reaction tank ; 10 minutes later , 0 . 3 parts of chp is added , and a mixture of 80 parts of mma , 20 parts of ea and 4 parts of potassium oleate is continuously injected for 1 hour , subsequently reacting for another one hour , a seed latex ( c ) with an average particle size of 120 ˜ 140 nm is resulted . 20 ˜ 90 parts of a seed latex made from a proportion range of 0 ˜ 100 parts of core - layer latex ( a ) and 100 ˜ 0 parts of core - layer latex ( b ), 0 . 01 parts of edta and 0 . 01 parts of ferrous sulfate are put into an one liter polymerization tank , closing the cover of the tank evacuated to − 740 mmhg of vacuum and keeping for 10 minutes , then nitrogen is injected to recover the pressure to be 1 kg / cm 2 and 0 . 35 parts of sfs is added ; 10 minutes later , 0 . 3 parts of chp is added and a mixture of 80 parts of mma , 20 parts of ea and 4 parts of potassium oleate is continuously injected for 1 hour , subsequently reacting for another one hour , a seed latex ( d ) with an average particle size of 130 ˜ 150 nm is resulted . polymer ( a ) belongs to a single core latex ( hard core ), polymer ( b ) belongs to a single core latex ( soft core ), polymer ( c ) belongs to a single core double layers latex and polymer ( d ) belongs to a double core double layers latex , wherein polymer ( a ), polymer ( b ), polymer ( c ) and polymer ( d ) can be mixed in a various proportion according to the desired physical properties and then used in the polymerization of vinyl chloride monomer . 70 kg of de - ionic pure water and 36 g of a dispersant ( pva with a hydrolysis degree of 78 mol %) are added in a 200 liter polymerization tank , which is then tightly closed and evacuated to − 740 mmhg of vacuum and kept for 10 minutes , thereafter 70 kg of vinyl chloride monomer and 0 . 56 g of a peroxide initiator - bnd are incorporated , raising the temperature to 64 □ to conduct polymerization ; after 2 hours reaction , a latex mixture of polymer ( a ) and ( c ) is continuously injected for 30 minutes , wherein the mixing proportion is listed in table 2 ; the reaction is kept for further 2 . 5 hours , then stopping the reaction , the resulted sample powder is collected . from the data of table 3 , all of examples 3 - 1 to 3 - 5 show better processing properties than those of the comparative example , that means the copolymerization of acrylate polymers and vinyl chloride makes pvc become a functional resin , wherein example 3 - 4 exhibits the best performance due to the proper doses of polymer latex ( a ) and polymer latex ( c ). the comparison between example 3 - 4 and example 3 - 5 shows polymer latex ( c ) is obviously positive to eliminate air - marks . 70 kg of de - ionic pure water , 56 g of a dispersant ( pva with a hydrolysis degree of 78 mol %) and a latex mixture of polymers ( b ) and ( d ) wherein the proportion of these two polymers is listed in table 4 are added in a 200 liter polymerization tank , which is then tightly closed and evacuated to − 740 mmhg of vacuum and kept for 10 minutes , thereafter 70 kg of vinyl chloride monomer and 0 . 56 g of a peroxide initiator - bnd are incorporated , raising the temperature to 64 l to conduct polymerization ; after 5 hours continuous reaction , then stopping the reaction , the resulted sample powder is collected . from the data of table 5 , all of examples 4 - 1 to 4 - 5 show better processing properties than those of the comparative example , that means , just the same as example 3 , the copolymerization of acrylate polymers and vinyl chloride makes pvc become a functional resin , polymer latex ( b ) is obviously assist to eliminate the sheeting air - marks , and polymer latex ( d ) can alleviate remarkably the sheeting flow - marks . 70 kg of de - ionic pure water , 36 g of a dispersant ( pva with a hydrolysis degree of 78 mol %) and 35 g of polymer latex ( a ) are added in a 200 liter polymerization tank , which is then tightly closed and evacuated to − 740 mmhg of vacuum and kept for 10 minutes , thereafter the first stage of vinyl chloride monomer and 0 . 56 g of a peroxide initiator - bnd are incorporated , raising the temperature to 64 □ to conduct polymerization ; after 30 minutes reaction , then the second stage of vinyl chloride monomer is fed to keep a further reaction for 4 . 5 hours , thereafter stopping the reaction , the resulted sample powder is collected . the proportion of the first stage vcm and the second stage vcm , and the polymer latex fraction by weight are shown in table 6 . as shown in table 7 , all of the processing properties of examples 5 - 1 to 5 - 5 with a stepwise vcm injection are superior to those of the comparative example , wherein the proportion of the first vcm and the second vcm of example 5 - 4 is optimal at 3 / 7 , and polymer latex ( a ) exhibits remarkably to suppress the sheeting flow - marks . 70 kg of de - ionic pure water and 36 g of a dispersant ( pva with a hydrolysis degree of 78 mol %) are added in a 200 liter polymerization tank , which is then tightly closed and evacuated to − 740 mmhg of vacuum and kept for 10 minutes , thereafter 70 kg of vinyl chloride monomer and 0 . 56 g of a peroxide initiator - bnd are incorporated , raising the temperature to 64 □ to conduct polymerization ; after 30 minutes reaction , 140 g of polymer ( b ) is continuously injected for 30 minutes and reacted for further 4 . 5 hours , then stopping the reaction , the resulted sample powder is collected . 70 kg of de - ionic pure water and 36 g of a dispersant ( pva with a hydrolysis degree of 78 mol %) are added in a 200 liter polymerization tank , which is then tightly closed and evacuated to − 740 mmhg of vacuum and kept for 10 minutes , thereafter 70 kg of vinyl chloride monomer and 0 . 56 g of a peroxide initiator - bnd are incorporated , raising the temperature to 64 □ to conduct polymerization ; after 60 minutes reaction , 140 g of polymer ( c ) is continuously injected for 30 minutes and reacted for further 4 hours , then stopping the reaction , the resulted sample powder is collected . 70 kg of de - ionic pure water and 36 g of a dispersant ( pva with a hydrolysis degree of 78 mol %) are added in a 200 liter polymerization tank , which is then tightly closed and evacuated to − 740 mmhg of vacuum and kept for 10 minutes , thereafter 70 kg of vinyl chloride monomer and 0 . 56 g of a peroxide initiator - bnd are incorporated , raising the temperature to 64 l to conduct polymerization ; after 90 minutes reaction , the mixture of 140 g of polymer ( d ) and 140 g of polymer ( a ) is continuously injected for 30 minutes and reacted for further 3 . 5 hours , then stopping the reaction , the resulted sample powder is collected . 70 kg of de - ionic water , 36 g of a dispersant ( pva with a hydrolysis degree of 78 mol %) and polymer ( a ) powder are added in a 200 liter polymerization tank , which is then tightly closed and evacuated to − 740 mmhg of vacuum and kept for 10 minutes , thereafter 70 kg of vinyl chloride monomer and 0 . 56 g of a peroxide initiator - bnd are incorporated , raising the temperature to 64 l to conduct polymerization ; after 5 hours reaction , then stopping the reaction , the resulted sample powder is collected . polymers b , c , d and a are added in examples 6 , 7 , 8 and 9 respectively , as shown in table 8 , all of the processing properties of examples 7 ˜ 9 are better , wherein the polymer is added into the polymerization tank prior to the beginning of reaction in example 9 and a number of polymers are used instead of a single polymer in example 8 , both of them result in better sheeting air - marks & amp ; flow - marks .