CN219441613U - Reaction kettle device with forced circulation for producing 1, 1-difluoroethane - Google Patents

Abstract

The application discloses a reaction kettle device with forced circulation for producing 1, 1-difluoroethane, which comprises a reaction cylinder, wherein the vertical inner space is divided into a feeding area, a reaction area and a discharging area, a first feeding port for a first material to enter is arranged below the reaction cylinder, and a second feeding port for a second material to enter and a discharging port are arranged above the reaction cylinder; the guide cylinder is arranged in the reaction zone and divides the reaction zone into a guide cylinder internal reaction zone and a corresponding buffer zone, wherein the ratio of the volume of the guide cylinder internal reaction zone to the volume of the buffer zone is 1:2-1:1; the ratio of the volume of the reaction zone to the internal volume of the reaction cylinder ranges from 1:2 to 1:4; the valve plate is arranged at the bottom of the guide cylinder and is provided with a plurality of material distribution outlets, and each material distribution outlet is communicated with a third feeding port outside the reaction cylinder through a third feeding pipe. The reactant circulates in the guide cylinder, which is helpful for maintaining the stable reaction temperature, and does not increase the safety requirement and maintenance cost of the equipment.

Description

Reaction kettle device with forced circulation for producing 1, 1-difluoroethane

Technical Field

The application relates to a reaction kettle device, in particular to a reaction kettle device with forced circulation for producing 1, 1-difluoroethane.

Background

1, 1-difluoroethane is an important fluorine-containing chemical product, is widely used in the fields of refrigeration, foaming, daily chemical and new material synthesis, and has the capacity of over one hundred thousand tons in China at present.

The existing production technology adopts acetylene and anhydrous hydrofluoric acid as raw materials, and the gas-liquid phase fluorination reaction generates 1, 1-difluoroethane under the action of a fluorosulfonic acid catalyst.

Reaction principle:

in the above reaction, it is very important to control the reaction temperature, and it is generally controlled to 20 to 40 ℃. The reaction temperature is too high, so that the polymerization of substances such as acetylene, intermediate substances such as fluoroethylene and the like and coking speed are accelerated, and the loss of raw material acetylene is about 10%; and the fluorosulfonic acid catalyst is deactivated along with the generation of the polymer, the dosage of the fluorosulfonic acid catalyst needs to be increased, and the consumption of the fluorosulfonic acid catalyst per ton of 1, 1-difluoroethane product is 20-30 KG/ton. It is well known that the reaction of acetylene and hydrofluoric acid to produce 1, 1-difluoroethane is a strongly exothermic reaction, and the heat of reaction is as high as 180.7kj/mol, so how to transfer to the heat of reaction, maintaining the reaction temperature stable is a critical factor in the production of 1, 1-difluoroethane.

The existing production process is to transfer the reaction heat in a manner of arranging a jacket or a built-in cooling pipe on the reaction kettle to keep the temperature in the reaction kettle stable, but the heat transfer and transfer manner is limited by a heat transfer area, so that the reaction heat cannot be completely transferred out, and particularly the fluidity of materials in a reaction kettle system cannot be increased, so that the problems of local overheating and overhigh local concentration of acetylene in the reaction kettle cannot be prevented.

In addition, an electric stirrer is arranged in the reaction kettle to improve the fluidity of materials so as to solve the problem of heat exchange effect. But the use of electric agitators increases, on the one hand, the production and operating costs of the reaction vessel and, on the other hand, the safety requirements of the production plant and the maintenance costs of the equipment.

Disclosure of Invention

A reaction kettle device with forced circulation for producing 1, 1-difluoroethane can timely transfer reaction heat generated by chemical reaction out of a reaction kettle without increasing the safety requirement and maintenance cost of equipment.

The application discloses take forced circulation's production 1, 1-difluoroethane reation kettle device, including the reaction barrel, vertically place and inner space divide into pan feeding district, reaction district and the ejection of compact district of mutual intercommunication by low to high in proper order, the below of reaction barrel is equipped with the first pan feeding mouth that supplies first material to get into, the top of reaction barrel is equipped with the second pan feeding mouth and the discharge gate that supply the second material to get into.

The guide cylinder is integrally cylindrical with an upper opening and a lower opening and is arranged in the reaction zone, the reaction zone is divided into a guide cylinder internal reaction zone and a corresponding buffer zone by the guide cylinder, and the ratio of the volume of the guide cylinder internal reaction zone to the volume of the buffer zone is in the range of 1:2 to 1:1; the ratio of the volume of the reaction zone to the internal volume of the reaction cylinder ranges from 1:2 to 1:4;

the valve plate is arranged at the bottom of the guide cylinder and is matched with the inner cavity of the guide cylinder in an integral mode, a plurality of material distribution outlets are arranged on the valve plate in an array mode, and each material distribution outlet is communicated with a third feeding port outside the reaction cylinder through a third feeding pipe.

The first material and the second material enter and fill the feeding area and at least a part of the reaction area through a first feeding opening and a second feeding opening respectively, the third material enters the guide cylinder through a third feeding opening and a valve plate, the third material reacts with the first material and the second material in the guide cylinder to obtain a target product, and the target product is converted into a gas phase or heated to be a gas phase and leaves the reaction cylinder through the discharge opening.

The following provides several alternatives, but not as additional limitations to the above-described overall scheme, and only further additions or preferences, each of which may be individually combined for the above-described overall scheme, or may be combined among multiple alternatives, without technical or logical contradictions.

Optionally, the periphery of the valve plate is disposed in a gap with the inner wall of the guide cylinder, and the bottom surface of the valve plate is retracted compared with the lower edge of the guide cylinder.

Optionally, the horizontal plane where 3/5 of the internal volume of the reaction cylinder is located is a first critical plane, and the upper edge of the guide cylinder is lower than or equal to the first critical plane.

Optionally, the horizontal plane where 1/5 of the internal volume of the reaction cylinder is located is a second critical plane, and the lower edge of the guide cylinder is higher than or equal to the second critical plane.

Optionally, the sum of the total volumes of the feeding zone and the reaction zone is less than or equal to 1/2 of the internal volume of the reaction cylinder.

Optionally, a feed back port communicated with the discharge area is also arranged above the reaction cylinder; the circulating device comprises a condenser, a first passage connected between the condenser and the discharge port, and a second passage arranged between the condenser and the feed back port.

The mixed gas of the target product and each material flows to the condenser through the discharge port and the first passage, the target product keeps the gas phase after flowing through the condenser and leaves the reaction kettle device, and other substances in the mixed gas flow back to the reaction cylinder through the second passage after flowing through the condenser.

Optionally, the discharge port is disposed towards the discharge area, the mixed gas returned to the reaction cylinder via the condenser passes through the discharge area and returns to the reaction area, and the substances in the discharge area and the reaction cylinder are mutually mixed and heat exchange is completed.

Optionally, the ratio of the inner diameter of the reaction cylinder at the position of the reaction zone to the inner diameter of the guide cylinder ranges from 4:3 to 2:1.

Optionally, the reactor further comprises a temperature control sleeve sleeved on the outer periphery of the reaction cylinder, the temperature control sleeve at least covers a part of the reaction zone and the outer periphery of the reaction cylinder of the discharging zone, and the temperature control Wen Taobao comprises a heat exchange medium inlet and a heat exchange medium outlet.

Optionally, the temperature control jacket covers at least 50% of the axial distance of the reaction cylinder, wherein the portion of the discharge zone of the reaction cylinder is at least 65% of the total axial length of the temperature control jacket.

According to the technical scheme, the guide cylinder is arranged in the reaction cylinder, under the action of the catalyst, acetylene and hydrofluoric acid react in the guide cylinder to produce 1, 1-difluoroethane, gas phase materials and products in the guide cylinder flow upwards to generate pressure difference, liquid phase materials in the reaction kettle flow into the guide cylinder rapidly, the volume of the guide cylinder, the buffer area and the volume ratio of the reaction area are controlled to adjust the flow speed and flow of the materials so as to realize circulation in the guide cylinder, timely transfer out of reaction heat, stabilize the reaction temperature, overcome the problems of overhigh local temperature and overhigh local acetylene concentration in a reaction system, reduce the generation amount of tar-like polymers, improve the yield, prolong the service life of the catalyst and not increase the safety requirement and maintenance cost of equipment.

Drawings

FIG. 1 is a schematic structural diagram of a reaction kettle device for producing 1, 1-difluoroethane with forced circulation in one embodiment;

FIG. 2 is a schematic view of a valve plate according to an embodiment;

FIG. 3 is a schematic view of a flow guide cylinder according to an embodiment;

FIG. 4 is a schematic diagram of a material flow in an embodiment.

Reference numerals in the drawings are described as follows:

11. a reaction cylinder; 110. a feed back port; 111. a feeding area; 112. a reaction zone; 113. a discharge zone; 114. a first feed inlet; 115. a second feed inlet; 116. a discharge port; 117. a feeding pipe; 118. a third feed inlet; 119. a first critical surface; 120. a second critical plane; 12. a guide cylinder; 121 a reaction zone inside the guide cylinder; 122. a buffer area; 13. a port plate; 131. a material dispensing outlet; 14. a circulation device; 141. a condenser; 142. a first passage; 143. a second passage; 15. a temperature control sleeve; 151. a heat exchange medium inlet; 152. a heat exchange medium outlet; 153. a waste liquid port; a. a first material; b. a second material; c. a third material; d. 1, 1-difluoroethane.

Detailed Description

The following description of the technical solutions in the embodiments of the present application will be made clearly and completely with reference to the drawings in the embodiments of the present application, and it is apparent that the described embodiments are only some embodiments of the present application, not all embodiments. All other embodiments, which can be made by one of ordinary skill in the art without undue burden from the present disclosure, are within the scope of the present disclosure.

It will be understood that when an element is referred to as being "connected" to another element, it can be directly connected to the other element or intervening elements may also be present. When an element is referred to as being "disposed on" another element, it can be directly on the other element or intervening elements may also be present.

Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs. The terminology used herein in the description of the present application is for the purpose of describing particular embodiments only and is not intended to be limiting of the application. The term "and/or" as used herein includes any and all combinations of one or more of the associated listed items.

As shown in fig. 1-2, the present application discloses a reaction kettle device for producing 1, 1-difluoroethane with forced circulation, comprising a reaction cylinder 11, a guide cylinder 12 and a valve plate 13.

The reaction cylinder 11 is vertically placed, the inner space is sequentially divided into a feeding area 111, a reaction area 112 and a discharging area 113 which are communicated with each other from low to high, a first feeding port 114 for a first material a to enter is arranged below the reaction cylinder 11, and a second feeding port 115 and a discharging port 116 for a second material b to enter are arranged above the reaction cylinder 11.

The guide cylinder 12 is integrally in a cylindrical shape with upper and lower openings and is arranged in the reaction zone 112, the guide cylinder 12 divides the reaction zone 112 into a guide cylinder internal reaction zone 121 and a corresponding buffer zone 122, and the ratio of the volume of the guide cylinder internal reaction zone 121 to the volume of the buffer zone 122 ranges from 1:2 to 1:1; the ratio of the volume of the reaction zone 112 to the internal volume of the reaction cylinder 11 ranges from 1:2 to 1:4.

The valve plate 13 is arranged at the bottom of the guide cylinder 12 and is matched with the inner cavity of the guide cylinder 12 in the whole shape, a plurality of material distribution outlets 131 are arranged on the valve plate 13 in an array mode, each material distribution outlet 131 is communicated with a third feeding port 118 outside the reaction cylinder 11 through a third feeding pipe 117, and acetylene is uniformly distributed in the guide cylinder through the valve plate 13.

The first material a and the second material b respectively enter and fill the feeding area 111 and at least a part of the reaction area 112 through the first feeding opening 114 and the second feeding opening 115, the third material c enters the guide cylinder 12 through the third feeding opening 118 and the valve plate 13, the third material c reacts with the first material a and the second material b in the guide cylinder 12 to obtain a target product d, and the target product d is converted into a gas phase or heated to be a gas phase and leaves the reaction cylinder 11 through the discharging opening 116.

In this embodiment, when the axial length of the guide shell 12 is consistent with that of the reaction zone 112, the volume of the buffer zone 122 is the volume of the annular region between the guide shell 12 and the reaction barrel 12, and the reaction zone 112 includes the buffer zone 122 and the internal volume of the guide shell 12. The ratio of the volume of the reaction zone 121 to the volume of the buffer zone 122 within the guide cylinder ranges from 1:2 to 1:1, and the ratio of the volume of the reaction zone 112 to the internal volume of the reaction cylinder 11 ranges from 1:2 to 1:4. The ratio can be controlled to adjust the flow rate and flow rate of the material in a range so as to form circulation in the guide cylinder, and specific values can be selected according to the characteristics of the material.

In one embodiment, the first material a and the second material b are liquid phase materials, and the third material c is gas phase material. The material of the guide cylinder 12 can be common manganese steel or stainless steel, and the valve plate 13 can be common carbon steel.

In one embodiment, as shown in fig. 4, the first material a is anhydrous hydrofluoric acid, the second material b is fluorosulfonic acid, and the third material c is acetylene. The reaction cylinder 11 is internally provided with a guide cylinder 12, reaction raw materials of acetylene and hydrofluoric acid enter the guide cylinder 12 from the bottom, under the action of catalyst fluorosulfonic acid, acetylene and anhydrous hydrofluoric acid react in the guide cylinder 12 to generate a product of 1, 1-difluoroethane, under the action of reaction heat, the anhydrous hydrofluoric acid, the fluorosulfuric acid and the product of 1, 1-difluoroethane rapidly flow upwards in the guide cylinder 12, so that a large pressure difference is generated between the upper and lower sides of the guide cylinder 12, the anhydrous hydrofluoric acid and the fluorosulfuric acid in the buffer zone 122 enter the guide cylinder 12 from the bottom, rapid circulation is formed inside and outside the guide cylinder 12, acetylene, anhydrous hydrofluoric acid and fluorosulfuric acid are promoted to be fully mixed and react in the reaction cylinder 11, excessive anhydrous hydrofluoric acid is vaporized by reverse heat, and most of reaction heat is taken away by vaporization latent heat, and the effect of maintaining the stable reaction temperature is achieved.

In one embodiment, as shown in fig. 3, the outer periphery of the valve plate 13 is disposed in a gap with the inner wall of the guide cylinder 12, and the reactant in the buffer zone 122 enters the guide cylinder 12 from the gap under the action of the pressure difference. Compared with the lower edge of the guide cylinder 12, the bottom surface of the valve plate 13 is retracted, acetylene is completely introduced into the guide cylinder 12, chemical reaction mainly occurs in the guide cylinder 12, and driving force is generated for circulation. The ratio between the retracted distance D and the axial length of the guide cylinder 12 is in the range of 0.05 to 0.2, and the proper ratio can be selected according to the flow rate of the materials in practical use.

In one embodiment, the reaction cylinder 11 is a straight cylinder, as shown in fig. 4, a horizontal plane where 3/5 of the internal volume of the reaction cylinder 11 is located is a first critical plane 119, and an upper edge of the guide cylinder 12 is lower than or equal to the first critical plane 119. The upper position of the guide cylinder 12 is too high, and under the condition of insufficient material liquid level, the guide cylinder 12 can isolate the materials in the guide cylinder 12 from the materials outside the guide cylinder, so that the circulation is hindered.

In one embodiment, the level at 1/5 of the internal volume of the reaction cylinder 11 is the second critical surface 120, and the lower edge of the guide cylinder 12 is higher than or equal to the second critical surface 120. Too low a lower edge of the guide shell 12 can affect the amount of material circulated therethrough, resulting in insufficient circulation and affecting the circulation effect.

In some embodiments, the sum of the total volumes of the feed zone 111 and the reaction zone 112 is less than 1/2 of the internal volume of the reaction cylinder 11. This arrangement allows for a larger discharge zone 113, more convenient transfer of heat of reaction out of the reaction zone 112, and easier control of reaction temperature.

In this embodiment, as shown in fig. 4, a feed back port 110 communicating with a discharge area 113 is further provided above the reaction cylinder 11. There is also provided a circulation device 14 comprising a condenser 141, a first passage 142 connected between the condenser 141 and the discharge opening 116, a second passage 143 provided between the condenser 141 and the return opening 110.

The mixed gas of the 1, 1-difluoroethane and the materials is kept in gas phase after passing through a discharge hole 116 and a first passage 142 to a condenser 141,1,1-difluoroethane and leaves the reaction kettle device to enter the next working procedure after passing through a condenser 141, other substances in the mixed gas are cooled into liquid phase after passing through the condenser 141, and the liquid phase returns to the reaction cylinder 11 through a second passage 143 to continue the reaction. Further, the discharge port 116 is provided toward the discharge zone 113, and the mixture gas returned to the reaction cylinder 11 via the condenser 141 is returned to the reaction zone 112 through the discharge zone 113 and mixed with the substances in the reaction cylinder 11 in the discharge zone 113 and completes the heat exchange. The returned anhydrous hydrofluoric acid is lower than the temperature in the reaction cylinder 11, and is mixed with other high-temperature materials under the forced circulation generated by the guide cylinder 12, so that partial reaction heat is balanced, and the effect of maintaining the stable reaction temperature is achieved.

The ratio of the inner diameter of the reaction cylinder 11 at the location of the reaction zone 112 to the inner diameter of the guide cylinder 12 ranges from 4:3 to 2:1. The ratio is too small or too large, which causes the problem of insufficient circulation flow speed and circulation quantity, and the ratio is controlled within the range of 4:3 to 2:1, so that three substances of gas-phase substance acetylene and liquid-phase hydrofluoric acid and fluorosulfonic acid in the reaction cylinder 11 can be fully mixed and reacted in the reaction kettle.

In this embodiment, as shown in fig. 4, the reaction kettle device further includes a temperature control sleeve 15 sleeved on the outer periphery of the reaction cylinder 11, where the temperature control sleeve 15 covers at least a part of the outer periphery of the reaction cylinder 11 in the reaction zone 112 and the discharge zone 113, and the temperature control sleeve 15 includes a heat exchange medium inlet 151 and a heat exchange medium outlet 152. The lower edge of the temperature control sleeve 15 is lower than the upper edge of the guide cylinder 12, and the lower edge of the temperature control sleeve 15 is higher than the lower edge of the guide cylinder 12. A temperature control sleeve 15 is arranged at the upper half part of the reaction zone 112 and the discharge zone 113, so that the reaction heat can be transferred out of the reaction cylinder 11, and the reaction temperature is maintained stable; while the temperature jacket is disposed in the upper half of the reaction zone 112 without lowering the reaction temperature.

In some embodiments, the temperature control jacket 15 covers at least 50% of the distance over the axial distance of the reaction cylinder 11, wherein the portion of the discharge zone 113 of the reaction cylinder 11 is at least 65% of the total axial length of the temperature control jacket 15.

The embodiment of the application discloses a reaction kettle device operation method for producing 1, 1-difluoroethane with forced circulation, which comprises the following steps: firstly, adding 1/5 of the volume of the fluorosulfonic acid into the reaction cylinder 11; adding 2/5 volume of anhydrous hydrofluoric acid, adding the anhydrous hydrofluoric acid into the reaction cylinder 11, and calculating and determining the reaction heat generated by one mole of 1, 1-difluoroethane to be equal to the vaporization heat of the anhydrous hydrofluoric acid of 24 moles; then according to the mole ratio of HF to C ₂ H ₂ =2:1 ratio, while two materials are continuously dosed. The stable liquid level is controlled, so that the liquid level is ensured to meet the requirement that the inside and outside of the guide cylinder of the reaction kettle can generate liquid material circulation. Hydrofluoric acid and acetylene react under the action of a catalyst to generate 1, 1-difluoroethane, and simultaneously emit a large amount of heat, the temperature of the reaction kettle is controlled, and the reaction kettle is stabilized within the range of 35-40 ℃. The parameters of the temperature control are as follows: and (3) adjusting the flow of the liquid exchange medium in the condenser, the proportion of the reacted acetylene to the hydrofluoric acid and the flow. And after the fluorosulfonic acid catalyst is invalid, the catalyst is discharged from a waste liquid port 153 at the bottom of the reaction cylinder and enters a three-waste station for treatment.

The reactor device can reduce the consumption of the catalyst from 20-30 kg/t to about 18kg/t, reduce the acetylene loss caused by polymer coking factors from 10% to about 6%, greatly improve the raw material income, and does not increase the safety requirement and maintenance cost of equipment.

The technical features of the above-described embodiments may be arbitrarily combined, and all possible combinations of the technical features in the above-described embodiments are not described for brevity of description, however, as long as there is no contradiction between the combinations of the technical features, they should be considered as the scope of the description. When technical features of different embodiments are embodied in the same drawing, the drawing can be regarded as a combination of the embodiments concerned also being disclosed at the same time.

The above examples merely represent a few embodiments of the present application, which are described in more detail and are not to be construed as limiting the scope of the utility model. It should be noted that it would be apparent to those skilled in the art that various modifications and improvements could be made without departing from the spirit of the present application, which would be within the scope of the present application. Accordingly, the scope of protection of the present application shall be subject to the appended claims.

Claims (10)

1. A reaction kettle device for producing 1, 1-difluoroethane with forced circulation, comprising:

the reaction cylinder is vertically arranged, the internal space is sequentially divided into a feeding area, a reaction area and a discharging area which are mutually communicated from low to high, a first feeding port for a first material to enter is arranged below the reaction cylinder, and a second feeding port for a second material to enter and a discharging port are arranged above the reaction cylinder;

the guide cylinder is integrally cylindrical with an upper opening and a lower opening and is arranged in the reaction zone, the reaction zone is divided into a guide cylinder internal reaction zone and a corresponding buffer zone by the guide cylinder, and the ratio of the volume of the guide cylinder internal reaction zone to the volume of the buffer zone is in the range of 1:2 to 1:1; the ratio of the volume of the reaction zone to the internal volume of the reaction cylinder ranges from 1:2 to 1:4;

a valve plate which is arranged at the bottom of the guide cylinder and is matched with the inner cavity of the guide cylinder in an integral mode, a plurality of material distribution outlets are arranged on the valve plate in an array mode, and each material distribution outlet is communicated with a third feeding port outside the reaction cylinder through a third feeding pipe;

the first material and the second material enter and fill the feeding area and at least a part of the reaction area through a first feeding opening and a second feeding opening respectively, the third material enters the guide cylinder through a third feeding opening and a valve plate, the third material reacts with the first material and the second material in the guide cylinder to obtain a target product, and the target product is converted into a gas phase or heated to be a gas phase and leaves the reaction cylinder through the discharge opening.

2. The reaction kettle device for producing 1, 1-difluoroethane with forced circulation according to claim 1, wherein the periphery of the valve plate is arranged in a clearance with the inner wall of the guide cylinder and the bottom surface of the valve plate is retracted compared with the lower edge of the guide cylinder.

3. The reaction kettle device for producing 1, 1-difluoroethane with forced circulation according to claim 1, wherein a horizontal plane where 3/5 of the internal volume of the reaction cylinder is located is a first critical plane, and the upper edge of the guide cylinder is lower than or equal to the first critical plane.

4. The reaction kettle device for producing 1, 1-difluoroethane with forced circulation according to claim 3, wherein a horizontal plane where 1/5 of the internal volume of the reaction cylinder is located is a second critical plane, and the lower edge of the guide cylinder is higher than or equal to the second critical plane.

5. The reaction kettle device for producing 1, 1-difluoroethane with forced circulation according to claim 4, wherein the sum of the total volumes of the feed zone and the reaction zone is less than or equal to 1/2 of the internal volume of the reaction cylinder.

6. The reaction kettle device for producing 1, 1-difluoroethane with forced circulation according to claim 1, wherein a feed back port communicated with the discharge area is further arranged above the reaction cylinder;

the circulating device comprises a condenser, a first passage connected between the condenser and the discharge port, and a second passage arranged between the condenser and the feed back port;

the mixed gas of the target product and each material flows to the condenser through the discharge hole and the first passage, the target product keeps gas phase after flowing through the condenser and leaves the reaction kettle device, and other substances in the mixed gas flow back to the reaction cylinder through the second passage after flowing through the condenser.

7. The reaction kettle device for producing 1, 1-difluoroethane with forced circulation according to claim 6, wherein the discharge port is arranged towards the discharge area, the mixed gas returned to the reaction cylinder through the condenser passes through the discharge area to return to the reaction area, and substances in the discharge area and the reaction cylinder are mutually mixed and heat exchange is completed.

8. The reaction kettle device for producing 1, 1-difluoroethane with forced circulation according to claim 7, wherein the ratio of the inner diameter of the reaction cylinder at the position of the reaction zone to the inner diameter of the guide cylinder ranges from 4:3 to 2:1.

9. The reaction kettle device for producing 1, 1-difluoroethane with forced circulation according to claim 1, further comprising a temperature control sleeve sleeved on the outer periphery of the reaction cylinder, wherein the temperature control sleeve at least covers a part of the reaction zone and the outer periphery of the reaction cylinder of the discharge zone, and the control Wen Taobao comprises a heat exchange medium inlet and a heat exchange medium outlet.

10. The reactor apparatus for producing 1, 1-difluoroethane with forced circulation according to claim 9, wherein the temperature control jacket covers at least 50% of the distance in the axial direction of the reaction cylinder, and wherein the discharge area portion of the reaction cylinder occupies at least 65% of the total axial length of the temperature control jacket.