CN209890520U

CN209890520U - Methyl chloride production waste heat recovery device

Info

Publication number: CN209890520U
Application number: CN201920009113.6U
Authority: CN
Inventors: 赵炳泉; 王长明; 窦冰之; 丁福坤; 和德杰
Original assignee: Silication Work Point Co Of Western Shandong Chemical Group Limited-Liability Co
Current assignee: Silication Work Point Co Of Western Shandong Chemical Group Limited-Liability Co
Priority date: 2019-01-03
Filing date: 2019-01-03
Publication date: 2020-01-03
Anticipated expiration: 2029-01-03

Abstract

The utility model relates to a waste heat recovery device, concretely relates to chloromethane production waste heat recovery device. The device includes 1# reation kettle, 2# reation kettle, 3# reation kettle, double-effect heat exchanger, methyl alcohol pre-heater, methyl alcohol vaporizer, methyl alcohol delivery pump, 1# backward flow jar, 2# backward flow jar, 3# backward flow jar, liquid phase methyl alcohol thermometer, methyl chloride gaseous phase export thermometer, gaseous phase methyl alcohol export thermometer, liquid phase methyl alcohol level gauge, contain alcoholic liquor level gauge, gaseous phase methyl alcohol export pressure gauge, liquid phase methyl alcohol flowmeter and valve. The device realizes the full utilization of the waste heat of the reaction gas, realizes the gasification of the raw materials without using steam, saves the use of circulating water cooling medium and realizes the purpose of saving energy. Moreover, the device can effectively realize the reutilization of the device energy, reduce the investment of field equipment facilities and save the production cost.

Description

Methyl chloride production waste heat recovery device

Technical Field

The utility model relates to a waste heat recovery device, concretely relates to chloromethane production waste heat recovery device.

Background

The synthesis process of the organic silicon chloromethane adopts gas-liquid reaction, methanol is gasified and mixed with hydrogen chloride according to a certain proportion, and then the mixture reacts to generate the chloromethane under the action of a catalyst zinc chloride and at the temperature of 140 ℃ and 150 ℃. The process needs to use steam to gasify liquid phase methanol, consuming steam; the temperature of the reaction chloromethane mixture is about 140-145 ℃, and a refrigerant cooler is needed for condensation. Low-pressure steam of 155 ℃ is needed for vaporizing methanol for 2.5T/h, and circulating water of 300m is needed for condensing methyl chloride³In terms of hours.

Chinese utility model CN202546701U discloses a waste heat recovery device for chloromethane production, high temperature methane chloride enters the barrel 1 from the methane chloride inlet 13 of the barrel 1, heat is transferred to the high efficiency heat transfer element 2, the methane chloride exchanges heat with the high efficiency heat transfer element 2 in the barrel 1, and the methane chloride is cooled and then goes to the subsequent working section from the methane chloride outlet 14; feed water enters the steam pocket 6 from a feed water inlet pipeline 8, enters the water inlet connecting pipe box 9 from the water inlet pipeline 9, enters the extension section jacket 5 of the high-efficiency heat transfer element 2 through a pipeline 12 between the jacket and the water inlet connecting pipe box, the feed water exchanges heat with the high-efficiency heat transfer element in the jacket 5 to generate steam, the steam enters the steam connecting pipe box 4 through a pipeline 11 between the jacket 5 and the steam connecting pipe box 4, and the steam enters the steam pocket 6 from the steam connecting pipe box 4 through a steam connecting pipeline 10 and is sent to steam using equipment through a steam outlet 7 of the steam pocket 6. The device has long transmission distance from the high-efficiency heat transfer element to the steam using equipment, which causes heat loss. And the device also needs cold water as a cooling medium.

Therefore, it is an urgent need in the current methyl chloride manufacturing enterprises to provide a simple and energy-saving methyl chloride waste heat recovery device.

SUMMERY OF THE UTILITY MODEL

The utility model aims to overcome the defect that current waste heat recovery device exists, provide a chloromethane production waste heat recovery device. The waste heat utilization of the reaction gas is realized, the raw material gasification is realized without using steam, and meanwhile, the use of circulating water cooling medium is saved, and the purpose of saving energy is realized by the device.

In order to solve the technical problem, the utility model discloses a following technical scheme:

the utility model provides a chloromethane production waste heat recovery device, including 1# reation kettle, 2# reation kettle, 3# reation kettle, double-effect heat exchanger, methyl alcohol pre-heater, methyl alcohol vaporizer, methyl alcohol delivery pump, 1# backward flow jar, 2# backward flow jar, 3# backward flow jar, liquid phase methyl alcohol thermometer, chloromethane gaseous phase export thermometer, gaseous phase methyl alcohol export thermometer, liquid phase methyl alcohol level gauge, contain alcoholic acid liquid level gauge, gaseous phase methyl alcohol export pressure gauge, liquid phase methyl alcohol flowmeter and valve;

the No. 1 reaction kettle is sequentially communicated with the No. 2 reaction kettle and the No. 3 reaction kettle, the No. 1 reaction kettle is connected with a double-effect heat exchanger through a pipeline, the double-effect heat exchanger is respectively connected with a methanol waste heat device and a methanol vaporizer, and the methanol waste heat device is connected with the methanol vaporizer; the methanol delivery pump is connected with the methanol preheater; 1# reflux tank and 2# reflux tank, 3# reflux tank connect gradually, and double-effect heat exchanger passes through pipeline and 1# reflux tank, 2# reflux tank and 3# reflux tank intercommunication.

The device changes the original method of using steam to vaporize methanol, adds a double-effect heat exchanger to lead the methyl chloride at 145 ℃ at the outlet of the methyl chloride reaction kettle to exchange heat with liquid methanol, reduces the temperature of the methyl chloride to be below 89 ℃ while heating the methyl alcohol to 90 ℃ for vaporization, and does not use steam any more for the gasification of the methyl alcohol; meanwhile, one methanol vaporizer and three chloromethane reaction kettles are saved through flow modification.

Preferably, the double-effect heat exchanger is a two-section heat exchanger and comprises an upper half section heat exchanger and a lower half section heat exchanger, and the upper and lower half section heat exchangers are connected through an expansion joint.

The connecting part between the two-section heat exchanger is extremely easy to corrode, and the phenomenon of leakage occurs. In order to avoid leakage, the device is provided with an expansion joint between the upper heat exchanger and the lower heat exchanger. The expansion joint can relieve the temperature difference stress caused by expansion difference to the instrument, avoid the stress deformation of the instrument and effectively prevent the leakage of methyl chloride.

Preferably, a liquid-phase methanol thermometer and a liquid-phase methanol level meter are arranged between the upper section of heat exchanger and the lower section of heat exchanger; the top end of the upper half section of the heat exchanger is provided with a gas phase chloromethane mixture inlet, the right side of the upper half section of the heat exchanger is provided with a gas phase methanol outlet, the gas phase methanol outlet is connected with a second valve through a pipeline, and the gas phase methanol outlet pipeline is provided with a gas phase methanol outlet pressure gauge and a gas phase methanol outlet thermometer; a liquid phase methanol inlet is formed in the right side of the lower half-section heat exchanger, and a third valve, a fourth valve and a liquid phase methanol flowmeter are arranged on a liquid phase methanol inlet pipeline; a gas-phase methyl chloride outlet is formed in the left side of the lower half-section heat exchanger, and a gas-phase methyl chloride outlet pipeline connected with the gas-phase methyl chloride outlet is provided with a methyl chloride gas-phase outlet thermometer and a fifth valve; the bottom end of the lower half-section heat exchanger is provided with a condensed alcohol-containing acid outlet, and an outlet pipeline connected with the lower half-section heat exchanger is provided with a sixth valve.

Preferably, the outlet pipeline of the No. 1 reaction kettle is provided with a seventh valve and an eighth valve, and the outlet pipeline of the No. 2 reaction kettle is provided with a ninth valve and a tenth valve; an eleventh valve is arranged between the outlet pipelines of the No. 1 reaction kettle and the No. 2 reaction kettle.

Preferably, the top ends of the 1# reaction kettle and the double-effect heat exchanger are provided with a gas-phase chloromethane mixture inlet which is connected with the top end of the double-effect heat exchanger, and a first valve is arranged on the reaction kettle.

The device controls the valves and detects the instruments to ensure that the chloromethane and the methanol finish heat exchange, ensure that the methanol is heated to 90 ℃ to be vaporized, and simultaneously reduce the temperature of the chloromethane to be below 89 ℃.

The utility model discloses the beneficial effect who gains:

the device realizes the full utilization of the waste heat of the reaction gas, realizes the gasification of the raw materials without using steam, saves the use of circulating water cooling medium and realizes the purpose of saving energy. Moreover, the device can effectively realize the reutilization of the device energy, reduce the investment of field equipment facilities and save the production cost.

Drawings

FIG. 1 is a schematic structural view of the waste heat recovery device for chloromethane production of the present invention;

FIG. 2 is a schematic structural diagram of a double-effect heat exchanger

Wherein, the reaction kettle No. 1.1, the reaction kettle No. 2.2, the reaction kettle No. 3.3, the double-effect heat exchanger No. 4, the methanol preheater No. 5, the methanol vaporizer No. 6, the reflux tank No. 7.1, the reflux tank No. 8.2, the reflux tank No. 9.3, the seventh valve No. 10, the seventh valve No. 11, the eighth valve No. 12, the eleventh valve No. 13, the ninth valve No. 14, the tenth valve No. 15, the twelfth valve No. 16, the thirteenth valve No. 17, the fourteenth valve No. 18, the first valve No. 19, the second valve No. 20, the fifteenth valve No. 21, the third valve No. 22, the fourth valve No. 23, the sixteenth valve No. 24, the seventeenth valve No. 25, the eighteenth valve No. 26, the sixth valve No. 27, the nineteenth valve No. 28, the twentieth valve No. 29, the twenty-first valve No. 30, the twelfth valve No. 31, the twenty-thirteenth valve No. 32, the twenty-fourth valve No. 33, the twenty-fifth valve No, 35. the system comprises a twenty-seventh valve, 36, a fifth valve, 37, a twenty-eighth valve, 38, an expansion joint, 39, a methanol delivery pump, 40, a methyl chloride outlet thermometer, 41, a liquid phase methane liquid level meter, 42, a liquid phase methane thermometer, 43, a gas phase methane outlet pressure gauge, 44, a gas phase methane outlet thermometer, 45, an alcohol acid-containing liquid level meter, 46, a liquid phase methanol flow meter, 47, an upper half section heat exchanger, 48, a lower half section heat exchanger, 49, a gas phase methyl chloride mixture inlet, 50, a gas phase methanol outlet, 51, a liquid phase methanol inlet, 52, a gas phase methyl chloride outlet and 53, a condensation alcohol acid-containing outlet.

Detailed Description

The technical solutions in the embodiments of the present invention are described below clearly and completely, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiment of the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.

Example 1

Shown by figure 1, the utility model discloses the device includes 1

# reation kettle

1, 2

# reation kettle

2, 3# reation kettle 3, double effect heat exchanger 4, methyl alcohol pre-heater 5, methyl alcohol vaporizer 6, methyl

alcohol delivery pump

39, 1# backward flow jar 7, 2#

backward flow jar

8, 3# backward flow jar 9, liquid phase methyl alcohol thermometer 42, methyl chloride gaseous phase export thermometer 40, gaseous phase methyl alcohol export thermometer 44, liquid phase methyl alcohol level gauge 41, contain alcoholic liquor level gauge 45, gaseous phase methyl alcohol export pressure gauge 43, liquid phase methyl alcohol flowmeter 46 and valve;

the # 1 reaction kettle 1 is sequentially communicated with the # 2 reaction kettle 2 and the # 3 reaction kettle 3, the # 1 reaction kettle 1 is connected with a double-effect heat exchanger 4 through a pipeline, the double-effect heat exchanger 4 is respectively connected with a methanol waste heat device 5 and a methanol vaporizer 6, and the methanol waste heat device 5 is connected with the methanol vaporizer 6; the methanol delivery pump 39 is connected with the methanol preheater 5; 1# reflux tank 7 is connected gradually with 2

# reflux tank

8, 3# reflux tank 9, and double effect heat exchanger 4 passes through the pipeline and communicates with 1# reflux tank 7, 2

# reflux tank

9 and 3# reflux tank 9.

The double-effect heat exchanger is a two-section heat exchanger and comprises an upper half section heat exchanger 47 and a lower half section heat exchanger 48 which are connected through an expansion joint 38.

A liquid phase methanol thermometer 42 and a liquid phase methanol liquid level meter 41 are arranged between the upper section of heat exchanger and the lower section of heat exchanger; the top end of the upper half-section heat exchanger 47 is provided with a gas phase methyl chloride mixture inlet 49, the right side of the upper half-section heat exchanger is provided with a gas phase methanol outlet 50 which is connected with the second valve 19 through a pipeline, and the gas phase methanol outlet pipeline is provided with a gas phase methanol outlet pressure gauge 43 and a gas phase methanol outlet thermometer 44; a liquid phase methanol inlet 51 is formed in the right side of the lower half-section heat exchanger 48, and a third valve 21, a fourth valve 22 and a liquid phase methanol flowmeter 46 are arranged on a liquid phase methanol inlet pipeline; a gas-phase methyl chloride outlet 52 is arranged at the left side of the lower half-section heat exchanger 48, and a gas-phase methyl chloride outlet pipeline connected with the gas-phase methyl chloride outlet is provided with a methyl chloride gas-phase outlet thermometer 40 and a fifth valve 36; the bottom end of the lower half-section heat exchanger 48 is provided with a condensed alcohol-containing acid outlet 53, and an outlet pipeline connected with the condensed alcohol-containing acid outlet is provided with a sixth valve 26.

The outlet pipeline of the No. 1 reaction kettle 1 is provided with a seventh valve 10 and an eighth valve 11, and the outlet pipeline of the No. 2 reaction kettle 2 is provided with a ninth valve 13 and a tenth valve 14; an eleventh valve 12 is arranged between outlet pipelines of the No. 1 reaction kettle 1 and the No. 2 reaction kettle 2.

The top ends of the 1# reaction kettle 1 and the double-effect heat exchanger 4 are provided with a gas phase chloromethane mixture inlet 54 which is connected with each other, and a first valve 18 is arranged on the reaction kettle.

The device specifically comprises the following operation steps:

1) and after the pipeline of the double-effect heat exchanger 4 is installed, the tube side and shell side hydraulic tests are both 0.26MPa, the system performs nitrogen replacement after the tests have no leakage, and the oxygen content of the tube side and shell side sampling analysis system is not more than 0.5 percent and is qualified.

2) And putting the double-effect heat exchanger 4 into operation on the premise of stable production of the methyl chloride synthesis system. And slightly opening the gas-phase methanol outlet valve 19 of the double-effect heat exchanger, paying attention to the change of the liquid-phase methanol thermometer 42 of the double-effect heat exchanger 4 after gas noise exists on site, not opening the valve 19 any more if the temperature rises or the gas noise can be heard, and slightly opening one fifth of the valve 19 until the valve 19 is fully opened if the temperature does not rise any more and the gas noise cannot be heard.

3) And after the gas-phase methanol valve 19 is fully opened, opening a methanol delivery pump 39 to the self-regulating valve 22 of the double-effect heat exchanger 4, supplementing the liquid level to 60-80% according to a methanol liquid level meter 41 in the double-effect heat exchanger 4, slightly opening a chloromethane gas-phase outlet valve 36, and fully opening the valves after the system pressure is balanced. And opening a condensation alcohol acid-containing outlet regulating valve 26 to control the liquid level of the gas-liquid separator to be 20-40%.

4) And slightly opening the outlet gas of the reaction kettle to enter the double-effect heat exchanger inlet valve 18, further preheating the equipment, observing the number change of a gas-phase methane outlet pressure gauge 43 and a gas-phase methane outlet thermometer 44 of the double-effect heat exchanger, and slightly opening the methyl chloride gas inlet valve 18 if the temperature and the pressure stop rising. In order to maintain the pressure of the methanol system stable, the methanol vaporizer vapor self-regulating valve 37 must be guaranteed to have an opening of 5-10%.

5) After the pressure of the methanol system is stable, the first valve 18 of the double-effect heat exchanger is slowly opened to enlarge the gas in the reaction kettle, if the first valve 18 is completely opened, the twenty-eighth valve 37 of the vapor in the methanol vaporizer can be controlled within 10%, adjustment is not carried out, and if the twenty-eighth valve 37 cannot be controlled within 10%, the gas in the reaction kettle is gradually reduced to enter the original first-cold seventh valve 10 of the reaction kettle, so that the gas feeding amount of the double-effect heat exchanger is increased. And (3) observing the change condition of a cold pressure difference during the process of closing the seventh valve 10 of the original first cold gas phase inlet, keeping the opening of the original first cold seventh valve 10 if the pressure difference rises, and also paying attention to the change condition of the temperature of the second cold outlet of the reaction kettle during the process of closing the first cold inlet, and stopping closing the seventh valve 10 of the original first cold inlet if the temperature of the second cold outlet of the reaction kettle rises to 50 ℃ or the opening of the original methanol vaporizer steam self-regulating valve is less than 10%. And in the adjusting process, the change condition of the methanol liquid level in the double-effect heat exchanger is observed, and the methanol liquid level in the double-effect heat exchanger is maintained at 60-80% by using the fourth valve 22 at the methanol inlet of the double-effect heat exchanger. Meanwhile, the seventeenth valve 24 and the sixteenth valve 23 at the outlet of the methanol delivery pump 39 are adjusted to control the methanol liquid level of the original methanol vaporizer and the preheater within a normal range.

6) The alcohol acid containing liquid level at the bottom of the double-effect heat exchanger is controlled by a twentieth valve 28 from the 1# reflux tank to the acid water tank, a twentieth valve 30, a twentieth valve 31 and a twenty-fourth valve 32 between a nineteenth valve 27 for discharging the liquid from the 1# reflux tank and a liquid discharging pipeline of the 2# reflux tank are required to be closed before adjustment, the nineteenth valve 27 for discharging the liquid from the bottom of the 1# reflux tank is closed, and a twenty-first valve 29 is opened. And controlling the liquid level at the bottom of the double-effect heat exchanger to be 20-40% by using a twentieth self-regulating valve 28 from the No. 1 reflux tank to the sour water tank.

Although the present invention has been described with reference to the accompanying drawings, it is not intended to limit the scope of the present invention, and it should be understood by those skilled in the art that various modifications and changes may be made without inventive changes in the technical solutions of the present invention.

Claims

1. The utility model provides a chloromethane production waste heat recovery device which characterized in that: the system comprises a 1# reaction kettle, a 2# reaction kettle, a 3# reaction kettle, a double-effect heat exchanger, a methanol preheater, a methanol vaporizer, a methanol delivery pump, a 1# reflux tank, a 2# reflux tank, a 3# reflux tank, a liquid-phase methanol thermometer, a chloromethane gas-phase outlet thermometer, a gas-phase methanol outlet thermometer, a liquid-phase methanol liquid level meter, an alcohol-containing acid liquid level meter, a gas-phase methanol outlet pressure meter, a liquid-phase methanol flow meter and a valve;

2. The methyl chloride production waste heat recovery device of claim 1, wherein the double-effect heat exchanger is a two-section heat exchanger, and comprises an upper half section heat exchanger and a lower half section heat exchanger, and the upper half section heat exchanger and the lower half section heat exchanger are connected through an expansion joint.

3. The methyl chloride production waste heat recovery device of claim 2, wherein a liquid phase methanol thermometer and a liquid phase methanol level meter are arranged between the upper section of heat exchanger and the lower section of heat exchanger; the top end of the upper half section of the heat exchanger is provided with a gas phase chloromethane mixture inlet, the right side of the upper half section of the heat exchanger is provided with a gas phase methanol outlet, the gas phase methanol outlet is connected with a second valve through a pipeline, and the gas phase methanol outlet pipeline is provided with a gas phase methanol outlet pressure gauge and a gas phase methanol outlet thermometer; a liquid phase methanol inlet is formed in the right side of the lower half-section heat exchanger, and a third valve, a fourth valve and a liquid phase methanol flowmeter are arranged on a liquid phase methanol inlet pipeline; a gas-phase methyl chloride outlet is formed in the left side of the lower half-section heat exchanger, and a gas-phase methyl chloride outlet pipeline connected with the gas-phase methyl chloride outlet is provided with a methyl chloride gas-phase outlet thermometer and a fifth valve; the bottom end of the lower half-section heat exchanger is provided with a condensed alcohol-containing acid outlet, and an outlet pipeline connected with the lower half-section heat exchanger is provided with a sixth valve.

4. The methyl chloride production waste heat recovery device according to any one of claims 1 to 3, wherein the outlet pipeline of the 1# reaction kettle is provided with a seventh valve and an eighth valve, and the outlet pipeline of the 2# reaction kettle is provided with a ninth valve and a tenth valve; an eleventh valve is arranged between the outlet pipelines of the No. 1 reaction kettle and the No. 2 reaction kettle.

5. The methyl chloride production waste heat recovery device of any one of claims 1 to 3, wherein the top ends of the 1# reaction kettle and the double-effect heat exchanger are provided with a gas-phase methyl chloride mixture inlet which is connected with each other and a first valve.