CN108888982B - Polypropylene process gas recovery equipment and recovery process - Google Patents
Polypropylene process gas recovery equipment and recovery process Download PDFInfo
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- CN108888982B CN108888982B CN201810697875.XA CN201810697875A CN108888982B CN 108888982 B CN108888982 B CN 108888982B CN 201810697875 A CN201810697875 A CN 201810697875A CN 108888982 B CN108888982 B CN 108888982B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0003—Condensation of vapours; Recovering volatile solvents by condensation by using heat-exchange surfaces for indirect contact between gases or vapours and the cooling medium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0051—Regulation processes; Control systems, e.g. valves
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
- B01D5/0081—Feeding the steam or the vapours
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Abstract
The invention belongs to the technical field of polypropylene process gas recovery, and particularly relates to polypropylene process gas recovery equipment and a recovery process. The recovery device mainly comprises a condensing device connected with a polypropylene process gas inlet pipeline, wherein the condensing device comprises a cylindrical shell, a winding pipe type core is arranged in the cylindrical shell, the winding pipe type core is formed by spirally winding a plurality of parallel condensing pipes for conveying refrigerant materials, the plurality of condensing pipes are divided into at least three pipe groups, and each pipe group correspondingly conveys one refrigerant material; and a conveying pipe communicated with the polypropylene process gas inlet pipeline and used for conveying the polypropylene process gas is further arranged in the cylindrical shell, and the conveying pipe is spirally wound in the pipe group gaps of the condensing pipes. The equipment system has simple structure and convenient installation, can effectively simplify the recovery process flow of the polypropylene process gas, and has the characteristics of energy conservation, stability and reliability.
Description
Technical Field
The invention belongs to the technical field of polypropylene process gas recovery, and particularly relates to polypropylene process gas recovery equipment and a recovery process.
Background
Before the polypropylene resin is extruded and granulated into a product, nitrogen is needed to blow off hydrocarbon gas carried in resin powder, and after the hydrocarbon removing process, materials such as propylene in the polypropylene process gas need to be recovered through a cooling process.
In the process of recycling the polypropylene process gas in the prior art, the polypropylene process gas is usually condensed step by step sequentially through three interstage cooling heat exchangers connected in series, as shown in fig. 1, the polypropylene process gas is condensed step by step sequentially through the three interstage cooling heat exchangers connected in series, the condensed process gas is decompressed and throttled and then subjected to gas-liquid separation through a gas-liquid separator to obtain a gas-phase light component refrigerant and a liquid-phase C3 refrigerant, the C3 refrigerant is split into two streams, one stream of the C3 refrigerant is decompressed and throttled to obtain a gas-liquid two-phase low-pressure C3 refrigerant, the gas-phase light component refrigerant provides a first stream of cold for a first-stage heat exchanger, the liquid-phase C3 refrigerant provides a second stream of cold for a second-stage heat exchanger, the gas-liquid two-phase low-pressure C3 refrigerant provides a third stream of cold for a third-stage heat exchanger, and the gas-phase light component materials respectively produced, Gas-liquid two-phase C3 material and gas-phase low-pressure C3 material, and the processes of production, recovery and circulation are carried out.
In the prior art, the polypropylene process gas is condensed only after undergoing two intermediate states in the recovery process, so that the process gas is always in a complex and changeable gas-liquid two-phase flow state, and the process gas is easy to drift when entering a next-stage heat exchanger from a previous-stage heat exchanger to continue falling film condensation, thereby causing the performance reduction and unstable operation of equipment; in addition, the existing polypropylene process gas recovery equipment system has the problems of difficult installation condition, large energy consumption loss, complex system structure and the like.
Disclosure of Invention
In order to avoid and overcome the problems in the prior art, the invention provides a polypropylene process gas recovery device and a recovery process. The equipment system has simple structure and convenient installation, can effectively simplify the recovery process flow of the polypropylene process gas, and has the characteristics of energy conservation, stability and reliability.
In order to realize the purpose of the invention, the invention adopts the following technical scheme:
a polypropylene process gas recovery device comprises a first throttling pressure reducing valve, a gas-liquid separator, a flow divider, a second throttling pressure reducing valve and a condensing device connected with a polypropylene process gas inlet pipeline; the condensing device comprises a cylindrical shell with openings at two ends, a winding tube type core body is arranged in the cylindrical shell, the winding tube type core body is formed by spirally winding a plurality of parallel condensing tubes for conveying refrigerant materials, the condensing tubes are divided into at least three tube groups, and each tube group correspondingly conveys one refrigerant material; an upper end enclosure and a lower end enclosure are fixedly arranged at two ends of the cylindrical shell respectively, the feed end and the discharge end of each condensing tube are connected with the lower end enclosure and the upper end enclosure respectively, and a plurality of tube holes butted with each condensing tube are formed in the upper end enclosure and the lower end enclosure respectively; the upper end enclosure is fixedly provided with a plurality of integrated discharge pipe boxes, each discharge pipe box is correspondingly communicated with one condensation pipe group, the lower end enclosure is fixedly provided with a plurality of integrated feed pipe boxes, and each feed pipe box is correspondingly communicated with one condensation pipe group; the cylindrical shell is internally provided with a conveying pipe which is communicated with a polypropylene process gas inlet pipeline and is used for conveying the polypropylene process gas, and the conveying pipe is spirally wound in the pipe group gaps of the condensing pipes; the feed end of gas-liquid separator is connected with the discharge end of conveyer pipe, first throttle relief pressure valve sets up in conveyer pipe and gas-liquid separator's connecting line, gas-liquid separator's gaseous phase material discharge end corresponds and connects a feed tube case, gas-liquid separator's liquid phase material discharge end with the feed end of shunt is connected, the shunt is equipped with two discharge ends at least, every discharge end of shunt corresponds respectively and connects a feed tube case, second throttle relief pressure valve sets up in the connecting line of one of them feed tube case and shunt.
Preferably, the tube bundle supporting mechanism is further arranged in the cylindrical shell and comprises a vertically arranged central tube, the condensation tube is wound on the outer annular surface of the central tube, a fixing sleeve is sleeved on the inner side of the upper end of the central tube and fixedly connected with the inner plate surface of the upper end enclosure, the central tube is connected with the fixing sleeve through a connecting pin, and the lower end of the central tube is fixedly connected with the inner plate surface of the lower end enclosure.
Further preferably, the condensation pipes are wound at least two layers in the radial direction of the central cylinder, distance limiting filler strips are arranged between the condensation pipes, the distance limiting filler strips are used for enabling the condensation pipes to be mutually spaced, and each distance limiting filler strip is provided with a pipe hoop used for limiting the condensation pipes in the radial direction of the central cylinder.
Further preferably, a jacket for tightly wrapping and fixing the condenser tube is sleeved outside the outermost condenser tube of the central cylinder.
Preferably, a plurality of bushings are fixedly arranged on the outer side of the jacket and are uniformly distributed along the axial direction of the jacket at intervals, a plurality of sliding blocks are arranged on the bushings and are uniformly distributed along the circumferential direction of the bushings at intervals, the sliding blocks are attached to the inner wall of the cylindrical shell, and the sliding blocks can slide on the inner wall surface of the cylindrical shell along the axial direction of the cylindrical shell.
Further preferably, the plurality of sliding blocks on each bushing are arranged in a one-to-one correspondence mode along the axial direction of the jacket, the plurality of sliding blocks arranged on one side of the jacket and positioned in the same vertical direction are integrated into an integral structure, and the sliding surface of each sliding block of the integral structure is completely attached to the inner wall of the cylindrical shell.
The recovery process of the polypropylene process gas recovery equipment comprises the following steps:
s1, introducing the gas-phase polypropylene process gas with the temperature controlled within 313.15-313.65K and the pressure controlled within 4.15-4.25 MPa into a conveying pipe in the condensing device, and condensing to obtain a gas-liquid two-phase process gas with the temperature controlled within 251.15-252.27K and the pressure controlled within 4.1-4.2 MPa;
s2, after the gas-liquid two-phase process gas passes through a first throttling and reducing valve, gas-liquid separation is carried out through the gas-liquid separator to obtain gas-phase light-component refrigerant and liquid-phase C3 refrigerant, the temperature of the gas-phase light-component refrigerant is 248.15-248.65K, and the pressure of the gas-phase light-component refrigerant is 2.7-2.79 MPa, and the gas-phase light-component refrigerant is introduced into a corresponding feeding pipe box on a condensing device;
s3, introducing the liquid-phase C3 refrigerant into the flow divider and dividing the liquid-phase C3 refrigerant into two streams, namely a first liquid-phase C3 refrigerant and a second liquid-phase C3 refrigerant, and introducing the second liquid-phase C3 refrigerant into one corresponding feeding pipe box on the condensing device;
s4, introducing the first liquid-phase C3 refrigerant into a second throttling and reducing valve to obtain a gas-liquid two-phase low-pressure C3 refrigerant with the temperature of 243.09-243.89K and the pressure of 0.45-0.55 MPa, and introducing the gas-liquid two-phase low-pressure C3 refrigerant into a corresponding feeding pipe box on a condensing device.
The invention has the beneficial effects that:
according to the process flow, cold energy is given to the process gas-heated material to be recovered by the three cold materials, and then the product obtained after heat exchange of the three cold materials is put into production recovery circulation, so that condensation of the process gas-heated material can be realized at one time without additionally inputting cold energy, each cold material does not need to cool the process gas-heated material step by step through a plurality of interstage heat exchangers, and the cooling flows of the multistage discrete heat exchangers are integrated into one device, so that the flow is more convenient, and the irreversible loss of temperature difference from the cold materials to the heat absorption process of the process gas-heated material in the recovery process is reduced (can reach 6%); through the condensing unit, not only can three cold materials be guaranteed to provide cold energy simultaneously to enable the gas-phase polypropylene process gas to finish the once continuous uniform falling film condensation, thereby avoiding the process gas from being in a complicated and changeable gas-liquid two-phase flow state, greatly simplifying the equipment installation conditions, saving the equipment installation space and simplifying the equipment system structure. The invention overcomes the defect of stepwise condensation of the polypropylene process gas in the traditional process, thoroughly solves the problems of the prior art, realizes the unification of process flow innovation and device innovation, and has the characteristics of energy conservation, high efficiency, integration, compactness, stability and reliability.
Drawings
FIG. 1 is a flow diagram of a conventional polypropylene process gas recovery plant system;
FIG. 2 is a flow diagram of a polypropylene process gas recovery plant system according to the present invention;
FIG. 3 is a schematic view of a condensing unit according to the present invention;
fig. 4 is an internal structure showing view of the condensing apparatus shown in fig. 3.
Fig. 5 is a partially enlarged view of fig. 4.
The reference numerals have the following meanings:
10-condensing unit 11-cylindrical shell 12-condenser pipe 121-distance limiting filler strip 122-pipe hoop
13-upper end enclosure 14-lower end enclosure 15-discharge pipe box 16-feed pipe box 171-central cylinder
172-fixed sleeve 173-connecting pin 18-jacket 191-bushing 192-slide block
20-first throttle reducing valve 30-gas-liquid separator 40-flow divider
50-second throttle reducing valve A-gas phase polypropylene process gas A3-gas-liquid two-phase process gas
AD-gas phase light component refrigerant ABC-liquid phase C3 refrigerant AB-first liquid phase C3 refrigerant
AC-second liquid phase C3 refrigerant ABB-gas-liquid two-phase low-pressure C3 refrigerant
B-gas phase low pressure C3 material C-gas liquid two phase C3 material D-gas phase light component material
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below with reference to the accompanying drawings and embodiments, and all other embodiments obtained by a person of ordinary skill in the art based on the embodiments of the present invention without creative efforts belong to the protection scope of the present invention.
As shown in fig. 2 to 4, a polypropylene process gas recovery device comprises a first throttle reducing valve 20, a gas-liquid separator 30, a flow divider 40, a second throttle reducing valve 50 and a condensing unit 10 connected with a polypropylene process gas inlet pipeline; the condensing device 10 comprises a cylindrical shell 11 with openings at two ends, a winding pipe type core is arranged in the cylindrical shell 11, the winding pipe type core is formed by spirally winding a plurality of parallel condensing pipes 12 for conveying refrigerant materials, the plurality of condensing pipes 12 are divided into at least three pipe groups, and each pipe group correspondingly conveys one refrigerant material; an upper seal head 13 and a lower seal head 14 are fixedly arranged at two ends of the cylindrical shell 11 respectively in a welding mode, a feeding end and a discharging end of each condensing tube 12 are respectively connected with the lower seal head 14 and the upper seal head 13, and a plurality of tube holes butted with the condensing tubes 12 are formed in the upper seal head 13 and the lower seal head 14; a plurality of integrated discharge pipe boxes 15 are fixedly arranged on the upper end enclosure 13 in a welding manner, each discharge pipe box 15 is correspondingly communicated with one condensation pipe 12 pipe group, a plurality of integrated feed pipe boxes 16 are fixedly arranged on the lower end enclosure 14 in a welding manner, and each feed pipe box 16 is correspondingly communicated with one condensation pipe 12 pipe group; a conveying pipe communicated with a polypropylene process gas inlet pipeline and used for conveying the polypropylene process gas is further arranged in the cylindrical shell 11, and the conveying pipe is spirally wound in the pipe group gaps of the condensing pipes 12; the feed end of gas-liquid separator 30 is connected with the discharge end of conveyer pipe, first throttle relief pressure valve 20 sets up in the connecting line of conveyer pipe and gas-liquid separator 30, gas-phase material discharge end of gas-liquid separator 30 corresponds one feeding tube case 16 of connecting, the liquid phase material discharge end of gas-liquid separator 30 with the feed end of shunt 40 is connected, shunt 40 is equipped with two discharge ends at least, every discharge end of shunt 40 corresponds one feeding tube case 16 of connecting respectively, second throttle relief pressure valve 50 sets up in the connecting line of one of them feeding tube case 16 and shunt 40.
As shown in fig. 3 and 4, a tube bundle supporting mechanism is further disposed in the cylindrical shell 11, the tube bundle supporting mechanism includes a vertically disposed central tube 171, the condensing tube 12 is wound around an outer annular surface of the central tube 171, a fixing sleeve 172 is sleeved on an inner side of an upper end of the central tube 171, the fixing sleeve 172 is fixedly connected to an inner plate surface of the upper head 13, the central tube 171 is connected to the fixing sleeve 172 through a connecting pin 173, and a lower end of the central tube 171 is fixedly connected to an inner plate surface of the lower head 14. By such design, simultaneous expansion and contraction of the cylindrical housing 11 and the center cylinder 171 due to rapid temperature changes is accommodated.
As shown in fig. 3 and 4, the condensation pipes 12 are wound at least two layers in the radial direction of the central cylinder 171, distance-limited filler strips 121 are arranged between the condensation pipes 12, the distance-limited filler strips 121 are used for spacing the condensation pipes 12 from each other, and each distance-limited filler strip 121 is provided with a pipe hoop 122 for limiting each condensation pipe 12 in the radial direction of the central cylinder 171. Such design can provide directional buffering space for the expend with heat and contract with cold of each condenser pipe 12 on the one hand, and on the other hand can increase the area of contact of polypropylene technology gas heat material and each condenser pipe 12 to be favorable to guaranteeing the heating power action control between polypropylene technology gas heat material and each strand of cold material.
As shown in fig. 3, 4 and 5, a jacket 18 for tightly wrapping and fixing the condensation pipe 12 is sleeved outside the outermost condensation pipe 12 of the central cylinder 171; the outer side of the jacket 18 is fixedly provided with a plurality of bushings 191, the bushings 191 are uniformly distributed along the axial direction of the jacket 18 at intervals, the bushings 191 are provided with a plurality of sliding blocks 192, the sliding blocks 192 are uniformly distributed along the circumferential direction of the bushings 191 at intervals, the sliding blocks 192 are attached to the inner wall of the cylindrical shell 11, and the sliding blocks 192 can slide on the inner wall surface of the cylindrical shell 11 along the axial direction of the cylindrical shell 11 to adapt to expansion and contraction of the tube bundle caused by rapid temperature change, so that the thermal stress generated among the tube bundle, the cylindrical shell 11 and the tube bundle supporting mechanism is reduced to the minimum.
As shown in fig. 3, 4 and 5, the plurality of sliding blocks 192 on each bushing 191 are arranged in a one-to-one correspondence along the axial direction of the jacket 18, the plurality of sliding blocks 192 arranged on one side of the jacket 18 in the same vertical direction are integrated into an integral structure, and the sliding surface of the sliding block 192 of the integral structure completely fits the inner wall of the cylindrical shell 11. In this way, during the manufacturing and assembling of the condensation device 10, the slider 192 with an integrated structure can well perform the supporting and guiding functions so as to assemble the structural components in the cylindrical shell 11 in place.
The recovery process of the polypropylene process gas recovery equipment comprises the following steps:
s1, introducing the gas-phase polypropylene process gas A with the temperature controlled within 313.15-313.65K and the pressure controlled within 4.15-4.25 MPa into a conveying pipe in the condensing device 10 to be condensed to obtain a gas-liquid two-phase process gas A3 with the temperature controlled within 251.15-252.27K and the pressure controlled within 4.1-4.2 MPa (during initial condensation, the condensing device 10 is pre-cooled);
s2, after the gas-liquid two-phase process gas A3 passes through the first throttling and reducing valve 20, gas-liquid separation is carried out through the gas-liquid separator 30 to obtain a gas-phase light-component refrigerant AD and a liquid-phase C3 refrigerant ABC, wherein the gas-phase light-component refrigerant AD has the temperature of 248.15-248.65K and the pressure of 2.7-2.79 MPa, and the gas-phase light-component refrigerant AD is introduced into a corresponding feeding pipe box 16 on the condensing device 10 to provide cold energy for the gas-phase polypropylene process gas A to be recovered;
s3, introducing the liquid-phase C3 refrigerant ABC into the flow divider 40 and dividing the liquid-phase C3 refrigerant ABC into two flows, namely a first flow of liquid-phase C3 refrigerant AB and a second flow of liquid-phase C3 refrigerant AC, and introducing the second flow of liquid-phase C3 refrigerant AC into a corresponding feeding pipe box 16 on the condensing device 10 to provide cold energy for the gas-phase polypropylene process gas A to be recovered;
s4, introducing the first liquid-phase C3 refrigerant AB into a second throttling and reducing valve 50 to obtain a gas-liquid two-phase low-pressure C3 refrigerant ABB with the temperature of 243.09-243.89K and the pressure of 0.45-0.55 MPa, and introducing the gas-liquid two-phase low-pressure C3 refrigerant ABB into a corresponding feeding pipe box 16 on the condensing device 10 to provide cold energy for the gas-phase polypropylene process gas A to be recovered.
According to the recovery process, the gas-phase polypropylene process gas-heated materials are condensed, throttled and separated to form three cold materials, the three cold materials give cold energy to the process gas-heated materials to be recovered, and then products obtained after heat exchange of the three cold materials are put into production recovery circulation. According to the process flow, cold energy does not need to be additionally input, condensation of process gas hot materials can be realized at one time, each strand of cold materials does not need to cool the process gas hot materials step by step through a plurality of interstage heat exchangers, and the cooling flows of the multistage discrete heat exchangers are integrated into one device, so that the flow is more convenient and faster; and the three strands of cold materials provide cold energy simultaneously, so that the gas-phase polypropylene process gas-heated material is subjected to once continuous uniform falling film condensation, thereby avoiding the process gas from being in a complex and changeable gas-liquid two-phase flow state, and having the characteristics of energy conservation, high efficiency, stability and reliability.
According to specific experimental data, the following tables 1 and 2 are obtained through arrangement.
Table 1: material and energy balance meter under the invention
| A | A3 | ABC | AB | AD | D | AC | C | ABB | B | |
| Propylene content | 0.453 | 0.453 | 0.821 | 0.821 | 0.113 | 0.113 | 0.821 | 0.821 | 0.821 | 0.821 |
| Pressure MPa | 4.2 | 4.1 | 2.7 | 2.6 | 2.7 | 2.6 | 2.6 | 2.6 | 0.53 | 0.53 |
| Temperature K | 313.15 | 251.64 | 248.15 | 249.02 | 248.15 | 301.29 | 249.02 | 298.29 | 243.89 | 299.58 |
| Specific enthalpy J/kg | 25986 | -247606 | -390640 | -390640 | -56111 | 11600 | -390640 | -260773 | -390640 | 78651 |
| Specific entropy J/kgK | -3072 | -4022 | -5647 | -5652 | -1747 | -1493 | -5652 | -5179 | -5626 | -3856 |
| Flow rate kg/s | 0.903 | 0.903 | 0.511 | 0.454 | 0.392 | 0.392 | 0.057 | 0.057 | 0.454 | 0.454 |
Table 2: comparison table for irreversible loss of temperature difference between the invention and original equipment and process under same reference
In the recovery process, after the gas-phase light-component refrigerant AD, the second liquid-phase C3 refrigerant AC and the gas-liquid two-phase low-pressure C3 refrigerant ABB respectively provide cold energy for the process gas hot materials, products after heat exchange are respectively a gas-phase light-component material D, a gas-liquid two-phase C3 material C and a gas-phase low-pressure C3 material B. As can be seen from Table 1, the propylene content in the gas-phase polypropylene process gas A was about 45%, whereas the propylene content in the C3 feed (B, C) could reach about 82% after the present recovery process. As can be seen from table 2, compared with the conventional multi-stage cooling process, the recovery process of the present invention has the advantage that the irreversible loss of the temperature difference of the refrigerant to the process gas heat absorption material during the recovery process is reduced by 6% under the same reference.
Claims (6)
1. A polypropylene process gas recovery equipment is characterized in that: comprises a first throttle reducing valve (20), a gas-liquid separator (30), a flow divider (40), a second throttle reducing valve (50) and a condensing device (10) connected with a polypropylene process gas inlet pipeline; the condensing device (10) comprises a cylindrical shell (11) with openings at two ends, a winding tubular core body is arranged in the cylindrical shell (11), the winding tubular core body is formed by spirally winding a plurality of parallel condensing pipes (12) for conveying refrigerant materials, the condensing pipes (12) are divided into at least three pipe groups, and each pipe group correspondingly conveys one refrigerant material; an upper end enclosure (13) and a lower end enclosure (14) are fixedly arranged at two ends of the cylindrical shell (11), a feeding end and a discharging end of each condensing tube (12) are respectively connected with the lower end enclosure (14) and the upper end enclosure (13), and a plurality of tube holes butted with the condensing tubes (12) are formed in the upper end enclosure (13) and the lower end enclosure (14); the upper end enclosure (13) is fixedly provided with a plurality of integrated discharge pipe boxes (15), each discharge pipe box (15) is correspondingly communicated with one pipe group of the condensation pipe (12), the lower end enclosure (14) is fixedly provided with a plurality of integrated feed pipe boxes (16), and each feed pipe box (16) is correspondingly communicated with one pipe group of the condensation pipe (12); a conveying pipe communicated with a polypropylene process gas inlet pipeline and used for conveying the polypropylene process gas is further arranged in the cylindrical shell (11), and the conveying pipe is spirally wound in the pipe group gaps of the condensing pipes (12); the feeding end of the gas-liquid separator (30) is connected with the discharging end of the conveying pipe, the first throttling and reducing valve (20) is arranged in a connecting pipeline of the conveying pipe and the gas-liquid separator (30), the discharging end of a gas-phase material of the gas-liquid separator (30) is correspondingly connected with one feeding pipe box (16), the discharging end of a liquid-phase material of the gas-liquid separator (30) is connected with the feeding end of the flow divider (40), the flow divider (40) is at least provided with two discharging ends, each discharging end of the flow divider (40) is respectively and correspondingly connected with one feeding pipe box (16), and the second throttling and reducing valve (50) is arranged in a connecting pipeline of one feeding pipe box (16) and the flow divider (40);
the recovery process using the recovery equipment comprises the following steps:
s1, introducing the gas-phase polypropylene process gas (A) with the temperature controlled within 313.15-313.65K and the pressure controlled within 4.15-4.25 MPa into a conveying pipe in the condensing device (10) to be condensed to obtain a gas-liquid two-phase process gas (A3) with the temperature within 251.15-252.27K and the pressure within 4.1-4.2 MPa;
s2, after the gas-liquid two-phase process gas (A3) passes through a first throttling and reducing valve (20), gas-liquid separation is carried out through a gas-liquid separator (30) to obtain a gas-phase light component refrigerant (AD) and a liquid-phase C3 refrigerant (ABC) which have the temperature of 248.15-248.65K and the pressure of 2.7-2.79 MPa, and the gas-phase light component refrigerant (AD) is introduced into a corresponding feeding pipe box (16) on a condensing device (10);
s3, introducing the liquid-phase C3 refrigerant (ABC) into the flow divider (40) and dividing the liquid-phase C3 refrigerant (ABC) into two flows, namely a first flow of liquid-phase C3 refrigerant (AB) and a second flow of liquid-phase C3 refrigerant (AC), and introducing the second flow of liquid-phase C3 refrigerant (AC) into a corresponding feeding pipe box (16) on the condensing device (10);
s4, introducing the first liquid-phase C3 refrigerant (AB) into a second throttling and reducing valve (50) to obtain a gas-liquid two-phase low-pressure C3 refrigerant (ABB) with the temperature of 243.09-243.89K and the pressure of 0.45-0.55 MPa, and introducing the gas-liquid two-phase low-pressure C3 refrigerant (ABB) into a corresponding feeding pipe box (16) on the condensing device (10).
2. The polypropylene process gas recovery plant of claim 1, wherein: the tube bundle cooling device is characterized in that a tube bundle supporting mechanism is further arranged in the cylindrical shell (11), the tube bundle supporting mechanism comprises a vertically-arranged central tube (171), the condensation tube (12) is wound on the outer annular surface of the central tube (171), a fixing sleeve (172) is sleeved on the inner side of the upper end of the central tube (171), the fixing sleeve (172) is fixedly connected with the inner plate surface of the upper end enclosure (13), the central tube (171) is connected with the fixing sleeve (172) through a connecting pin (173), and the lower end of the central tube (171) is fixedly connected with the inner plate surface of the lower end enclosure (14).
3. The polypropylene process gas recovery plant of claim 2, wherein: the condenser tubes (12) are wound by at least two layers in the radial direction of the central cylinder (171), distance limiting filler strips (121) are arranged among the condenser tubes (12), the distance limiting filler strips (121) are used for enabling the condenser tubes (12) to be mutually spaced, and each distance limiting filler strip (121) is provided with a tube hoop (122) used for limiting each condenser tube (12) in the radial direction of the central cylinder (171).
4. The polypropylene process gas recovery plant of claim 3, wherein: the outer side of the outermost condensation pipe (12) of the central cylinder (171) is sleeved with a jacket (18) used for tightly wrapping and fixing the condensation pipe (12).
5. The polypropylene process gas recovery plant of claim 4, wherein: the outer side of the jacket (18) is fixedly provided with a plurality of bushings (191), the bushings (191) are uniformly distributed along the axial direction of the jacket (18) at intervals, the bushings (191) are provided with a plurality of sliding blocks (192), the sliding blocks (192) are uniformly distributed along the circumferential direction of the bushings (191) at intervals, the sliding blocks (192) are attached to the inner wall of the cylindrical shell (11), and the sliding blocks (192) can slide on the inner wall surface of the cylindrical shell (11) along the axial direction of the cylindrical shell (11).
6. The polypropylene process gas recovery plant of claim 5, wherein: the sliding blocks (192) on the lining barrels (191) are arranged in a one-to-one correspondence mode along the axial direction of the jacket (18), the sliding blocks (192) arranged on one side of the jacket (18) and located on the same vertical direction are integrated into an integrated structure, and the sliding surface of the sliding block (192) of the integrated structure is completely attached to the inner wall of the cylindrical shell (11).
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