A method for co-production of 1-chloro-3,3,3-trifluoropropene, 2,3,3,3-tetrafluoropropene and 1,3,3,3-tetrafluoropropene, characterized by comprising the following steps: (a) preheating hydrogen fluoride and 1,1,1,3,3-pentachloropropane, then inputting the preheated hydrogen fluoride and 1,1,1,3,3-pentachloropropane into a first reactor in a molar ratio of 9-15:1, wherein the first reactor includes two sections, namely an upper section and a lower section, the upper section is filled with an aluminum oxide supported chromium metal catalyst, the lower section is filled with a chromic oxide supported indium metal catalyst; the hydrogen fluoride and the 1,1,1,3,3-pentachloropropane reacting in the upper section of the first reactor at a temperature of 200-400°C and at an air flow rate of 300-1,000h -1; a reaction product entering the lower section of the first reactor to continuously react with the 1,1,2,3-tetrachloropropane, wherein the molar ratio of the 1,1,2,3-tetrachloropropane to the hydrogen fluoride is 3-5:9, and then obtaining a reaction product of the first reactor; (b) directly inputting the reaction product of the first reactor obtained in step (a) into a second reactor, and the reaction product of the first reactor reacting by the effect of a catalyst in the second reactor at a temperature of 250-450°C and at an air flow rate of 500-1,500h -1, and then obtaining a reaction product of the second reactor; (c) inputting the reaction product of the second reactor obtained in step (b) into a hydrogen chloride tower to be separated to obtain a tower bottom fraction and an tower top fraction of the hydrogen chloride tower, wherein the tower top fraction is hydrogen chloride; separately refining the hydrogen chloride to obtain hydrochloric acid; (d) passing the tower bottom fraction of the hydrogen chloride tower through a water washing tower, an alkaline washing tower and a drying tower in turn to remove hydrogen fluoride and hydrogen chloride, and then the remaining substance entering a first rectifying tower to be rectified to obtain a tower bottom fraction and an tower top fraction of the first rectifying tower; (e) the tower bottom fraction of the first rectifying tower entering a second rectifying tower to be separated to obtain a 1-chloro-3,3,3-trifluoropropene product and an tower top fraction of the second rectifying tower; the tower top fraction of the first rectifying tower entering a third rectifying tower to be separated to obtain a 2,3,3,3-tetrafluoropropene product at the top of the third rectifying tower and a 1,3,3,3-tetrafluoropropene product in the tower reactor. (a) preheating hydrogen fluoride and 1,1,1,3,3-pentachloropropane, then inputting the preheated hydrogen fluoride and 1,1,1,3,3-pentachloropropane into a first reactor in a molar ratio of 9-15:1, wherein the first reactor includes two sections, namely an upper section and a lower section, the upper section is filled with an aluminum oxide supported chromium metal catalyst, the lower section is filled with a chromic oxide supported indium metal catalyst; the hydrogen fluoride and the 1,1,1,3,3-pentachloropropane reacting in the upper section of the first reactor at a temperature of 200-400°C and at an air flow rate of 300-1,000h -1; a reaction product entering the lower section of the first reactor to continuously react with the 1,1,2,3-tetrachloropropane, wherein the molar ratio of the 1,1,2,3-tetrachloropropane to the hydrogen fluoride is 3-5:9, and then obtaining a reaction product of the first reactor; (b) directly inputting the reaction product of the first reactor obtained in step (a) into a second reactor, and the reaction product of the first reactor reacting by the effect of a catalyst in the second reactor at a temperature of 250-450°C and at an air flow rate of 500-1,500h -1, and then obtaining a reaction product of the second reactor; (c) inputting the reaction product of the second reactor obtained in step (b) into a hydrogen chloride tower to be separated to obtain a tower bottom fraction and an tower top fraction of the hydrogen chloride tower, wherein the tower top fraction is hydrogen chloride; separately refining the hydrogen chloride to obtain hydrochloric acid; (d) passing the tower bottom fraction of the hydrogen chloride tower through a water washing tower, an alkaline washing tower and a drying tower in turn to remove hydrogen fluoride and hydrogen chloride, and then the remaining substance entering a first rectifying tower to be rectified to obtain a tower bottom fraction and an tower top fraction of the first rectifying tower; (e) the tower bottom fraction of the first rectifying tower entering a second rectifying tower to be separated to obtain a 1-chloro-3,3,3-trifluoropropene product and an tower top fraction of the second rectifying tower; the tower top fraction of the first rectifying tower entering a third rectifying tower to be separated to obtain a 2,3,3,3-tetrafluoropropene product at the top of the third rectifying tower and a 1,3,3,3-tetrafluoropropene product in the tower reactor.