STATE STANDARD OF THE USSR

Occupational safety standards system

The vessel, operating under pressure.

Safety Valve

SAFETY

GOST 12.2.085-82

(ST SEV 3085-81)

The USSR State Committee STANDARDS

Moscow

Developed by the Ministry of Chemical and Petroleum Engineering

ARTISTS

VV Dyukin (Leader), PF Serb candidate. Econ. Science; II Smith,

II Novikov, PhD. tech. Science, VP Isakov, PhD. tech. Science; TF Kondratyev, Dr.

Sc. sciences, LM Lapshin

INTRODUCED by the Ministry of Chemical and Petroleum Engineering

Member of the AM Vasiliev

Approved and put into effect by Decision of the USSR State Committee on Standards of

December 30, 1982 № 5310

STATE STANDARD OF THE USSR

Occupational safety standards system

The vessel, operating under pressure.

VALVES SAFETY

Requirements Security

Occupational safety standards system. Vessels working under

pressure.Safety valves. Safety requirements

GOST

12.2.085-82

(ST SEV 3085-81)

Resolution of the USSR State Committee for Standards on December 30, 1982 № 5310

duration extended

to 01.07.83

to 01.07.88

Non-compliance with the standard may be illegal

This standard applies to the safety valves that are installed on vessels operating under

pressure over 0.07 MPa (0.7 kgf / cm 2).

Calculation capacity of the relief valve is a mandatory appendix 1.

Explanation of terms used in this standard, see the Reference Appendix 8.

Fully complies with the standard ST SEV 3085-81.

1. GENERAL REQUIREMENTS

1.1. Capacity of the safety valves and their number should be chosen so as to avoid giving

the vessel, a pressure operating pressure of more than 0.05 MPa (0.5 kgf / cm 2) at operating

pressure in the vessel to 0.3 MPa ( 3 kgf / cm 2), inclusive, by 15% in the operating pressure in

the vessel to 6.0 MPa (60 kgf / cm 2),

inclusive, and 10% in the operating pressure in the

vessel above 6.0 MPa (60 kgf / cm 2).

1.2. Set pressure relief valve must be equal to the operating pressure in the vessel or greater

than, but not more than 25%.

1.3. Increase in excess of the working pressure on the PP. 1.1. and 1.2. be taken into

account when calculating the strength of GOST 14249-80.

1.4. The design and material elements of the safety valves and their accessories should be

chosen depending on the properties and operating medium.

1.5. Safety valves and accessories shall conform to the "Rules of construction and safe

operation of vessels under pressure," approved by the State Technical Supervision of the

USSR.

1.6. All safety valves and auxiliary devices shall be protected from arbitrary changes in

their adjustment.

1.7. Pressure relief valves should be located in areas accessible for inspection.

1.8. Permanently mounted on the vessels, which the operating conditions it is necessary to

turn off the safety valve should be installed using three-way diverter valve, or other switching

device between the relief valve and the vessel, provided that in any position of the closure

element switching device will be connected with the vessel, either or both of the safety

valves. In this case, each pressure relief valve must be designed so as to avoid giving the

vessel, a pressure of working on the meaning given in clause 1.1.

1.9. Work environment, coming out of the safety valve should be given to safety.

1.10. In the calculation of valve capacity should be considered counter of the valve.

1.11. In determining the capacity of the relief valve should be considered resistance

silencer. Installing it should not interfere with the operation of the safety valves.

1.12. In the area between the safety valve and silencer must be installed to install the fitting

instrument for measuring pressure.

2. REQUIREMENTS FOR SAFETY VALVES DIRECT ACTION

2.1. Lever-loading relief valves should be installed on stationary vessels.

2.2. The design of the truck and spring valve device shall be provided to check the health

of the valve is in working condition by forcing it open while the vessel. Enforceability of

opening shall be provided at a pressure of 80% opening. Not install safety valves without

tools to force open if it is not allowed on the properties of the medium (a poisonous,

explosive, etc.) or on the conditions of the process. In this case, check the safety valves

should be periodically in time is not fixed, but at least every 6 months, with the deletion of

the possibility of freezing, sticking polymerization or clogging the valve operating

environment.

2.3. Spring safety valves must be protected against excessive heating (cooling) and the

direct effects of the working environment, if it has a detrimental effect on the material

springs. With the full opening of the valve should be possible for the mutual contact between

the spring coils.

2.4. Mass of the load and the length of the lever arm and cargo safety valve should be

selected so that the burden was on the end of the lever. The lever arm ratio should not exceed

1:10. In the application load from the suspension of his connection should be one-piece. Load

shall not exceed 60 pounds and must be specified (stamped or cast) on the surface of the

cargo.

2.5. In the body of the pressure relief valve in the inlet and outlet pipe must be able to

remove condensate from the places of his flock.

3. Requirements for the safety valves are controlled by ITEMS

3.1. Safety valves and accessories shall be designed so that failure of any control or

regulatory authority, or power failure protection function was preserved vessel overpressure

by duplicating, or other measures.Shall be so designed to meet the requirements of

paragraphs. 2.3 and 2.5.

3.2. The pressure relief valve must be able to control them manually or remotely.

3.3. Safety valves, operated by electricity, must be equipped with two mutually

independent power sources. In electrical circuits, where disconnection of power supply is a

pulse valve is opened, you can have one power supply.

3.4. The pressure relief valve shall be constructed of a harmful impact in opening and

closing.

3.5. If the governing body is the pulse valve, the diameter of the orifice of the valve must

be at least 15 mm. The inner diameter of the pulse lines (inlet and outlet) must be at least 20

mm in diameter and at least Outlets pulse valve. Control lines and control lines must provide

reliable condensate drainage. Install shut-off on these lines is prohibited. Can a switching

device, if at any position of the device control line will remain open.

3.6. Work environment, used to control the safety valves must not be subjected to freezing,

coking, polymerization and a corrosive effect on metal.

3.7. The design of valve shall be closing at a pressure of at least 95% of P n.

3.8. When used for auxiliary external power supply safety valve must be fitted with at least

two independently acting control circuit, which should be designed so that failure of one of

the other chain control circuit ensures reliable operation of the safety valve.

4. REQUIREMENTS Suction-and discharge SAFETY VALVES

4.1. Pressure relief valves should be installed on the connecting tubes or pipes. When

mounted on a pipe (line) of several safety valves cross-section tube (pipe) shall not be less

than 1.25 of the total area of the section valves mounted on it. In determining section widths

from 1,000 mm in length, you must also consider the value of their resistance.

4.2. In pipelines safety valves shall be provided with adequate compensation for thermal

expansion. Mounting and pipeline safety valves must be designed taking into account the

static loads and dynamic forces generated by the safety valve.

4.3. Supply lines must be performed with an emphasis on the length of the side of the

vessel. In the supply line should exclude fluctuations in temperature of the wall (heat stroke)

at the safety valve.

4.4. Inner diameter inlet pipe shall be at least the maximum internal diameter of the transfer

tube pressure relief valve, which determines the capacity of the valve.

4.5. Inner diameter inlet pipe should be calculated based on the maximum capacity of the

safety valve. Pressure drop in the supply line shall not exceed 3% of P and a safety valve.

4.6. Inner diameter blow-off line should be at least the maximum internal diameter of the

safety valve outlet.

4.7. Inner diameter blow-off line shall be designed so that at the rate equal to the maximum

relief capacity, back to its outlet connection does not exceed the maximum pressure.

ANNEX 1

Mandatory

Capacity calculation

Relief capacity in kg / h should be calculated as follows:

for steam -For the pressure in MPa,

-For the pressure in kg / cm 2;

for gas -For the pressure in MPa,

-For the pressure in kg / cm 2;

for liquids -For the pressure in MPa,

-For the pressure in kg / cm 2,

where Is the maximum pressure in front of the safety valve, MPa (kgf / cm 2);

Is the maximum pressure for the safety valve, MPa (kgf / cm 2);

The specific volume of steam at the valve at the parameters and M 3 / kg;

The density of the real gas at the valve settings and In kg / m 3, determined from

tables or diagrams of state of real gas or calculated by the formula

-For the pressure in MPa ( in J / kg, hail).

-For the pressure in kg / cm 2 ( in kg · m / kg · ° C);

Is the gas constant, and choose by Reference Annex 5;

-Compressibility of a real gas purchased by Reference Annex 7 for an ideal gas = 1;

The temperature of the environment before the valve at the pressure , ° C;

-Sectional area of the valve, which is equal to the smallest cross-sectional area in the

flow tube, mm 2;

-Flow coefficient corresponding to the area For gases;

-Flow coefficient corresponding to the area For liquids;

The density of the fluid in the valve settings and In kg / m 3;

-Factor, which takes into account the physical and chemical properties of water vapor

in the operating parameters before the safety device chosen by Reference Annex 2 for

saturated steam and helper applications for 3-heated steam or calculated by the formula

-For the pressure in MPa,

-For the pressure in kg / cm 2;

-Adiabatic index;

-Factor, which takes into account the pressure ratio before and after the pressure relief

valve is selected by Reference to Annex 4, depending on the and The coefficient =

1 for ,

where

-For the pressure in MPa,

-For the pressure in kg / cm 2,

Is the critical pressure ratio is selected by Reference Appendix 5 or calculated by the

formula

;

-Factor, which takes into account the physical and chemical properties of the gas at

operating parameters are selected by reference to applications 5 and 6 or calculated by the

formula:

at ,

at

for the pressure in MPa or

for the pressure in kg / cm 2.

Flow coefficients of safety valves for gaseous media ( ) Or ( ) Fluids must be

specified in the data sheet safety valve.

APPENDIX 2

Reference

The values of the coefficient B 1 for saturated steam at k = 1,135

MPa (kgf /

cm 2)

0.2

(2,0)

0.6

(6,0)

1.0

(10,0)

1.5

(15,0)

2.0

(20,0)

3.0

(30,0)

B 1 0.530 0.515 0.510 0.505 0.500 0.500

MPa (kgf /

cm 2)

4.0

(40,0)

6.0

(60,0)

8.0

(80,0)

10.0

(100,0)

11.0

(110,0)

12.0

(120,0)

B 1 0.505 0.510 0.520 0.530 0.535 0.540

MPa (kgf /

cm 2)

13.0

(130,0)

14.0

(140,0)

15.0

(150,0)

16.0

(160,0)

17.0

(170,0)

18.0

(180,0)

B 1 0.550 0.560 0.570 0.580 0.590 0.605

MPa (kgf /

cm 2)

19.0

(190,0)

20.0

(200,0)

B 1 0.625 0.645

APPENDIX 3

Reference

The coefficient B 1 for superheated steam at k = 1,31

The value of B1 at a steam temperature T 1, ° C

MPa (kgf / cm 2)

250 300 350 400 450 500 550 600

0,2 (2,0) 0.480 0.455 0.440 0.420 0.405 0.390 0.380 0.365 1,0 (10,0) 0.490 0.460 0.440 0.420 0.405 0.390 0.380 0.365 2,0 (20,0) 0.495 0.465 0.445 0.425 0.410 0.390 0.380 0.365 3,0 (30,0) 0.505 0.475 0.450 0.425 0.410 0.395 0.380 0.365 4,0 (40,0) 5.520 0.485 0.455 0.430 0.410 0.400 0.380 0.365 6,0 (60,0) 0.500 0.460 0.435 0.415 0.400 0.385 0.370 8,0 (80,0) 0.570 0.475 0.445 0.420 0.400 0.385 0.370 16,0 (160,0) 0.490 0.450 0.425 0.405 0.390 0.375 18,0 (180,0) 0.480 0.440 0.415 0.400 0.380 20,0 (200,0) 0.525 0.460 0.430 0.405 0.385 25,0 (250,0) 0.490 0.445 0.415 0.390 30,0 (300,0) 0.520 0.460 0.425 0.400 35,0 (350,0) 0.560 0.475 0.435 0.405 40,0 (400,0) 0.610 0.495 0.445 0.415

The coefficient B 1 for superheated steam at k = 1,31

APPENDIX 4

Reference

The coefficient B 2

In value for k, equal

1.100 1.135 1.310 1.400

0.500 - -

0.528 1.100 at cr 0.990

0.545 - 0.990 0.990

0.577 0.990 0.990

0.586 0.980 0.975 0.990

0.600 0.990 0.957 0.945 0.930

0.700 0.965 0.955 0.830 0.820

0.800 0.855 0.850 0.628 0.620

0.900 0.655 0.650

APPENDIX 5

Reference

The values of the coefficient B 3 for gas

k B 3 at cr R

Gas at t = 0 ° C and P = 0,1 MPa

(1kgs/sm 2)

cr J / kg · Grade kg m / kg ·

Grade

Nitrogen

Ammonia

Argon

Acetylene

Butane

Hydrogen

Air

Helium

Difluorodichloromethane

Oxygen

Methane

Methyl chloride

Carbon monoxide

Propane

Hydrogen sulfide

Sulfur dioxide

Carbon dioxide

Chlorine

Ethane

Ethylene

1.40

1.32

1.67

1.23

1.10

1.41

1.40

1.66

1.14

1.40

1.30

1.20

1.40

1.14

1.30

1.40

1.31

1.34

1.22

1.24

0.770

0.757

0.825

0.745

0.710

0.772

0.770

0.820

0.720

0.770

0.755

0.730

0.770

0.720

0.755

0.770

0.756

0.762

0.744

0.750

0.528

0.543

0.488

0.559

0.586

0.527

0.528

0.488

0.576

0.528

0.547

0.564

0.528

0.576

0.547

0.528

0.545

0.540

0.560

0.557

298

490

207

320

143

4120

287

2080

68.6

260

515

165

298

189

244

130

189

118

277

296

30.25

49.80

21.20

32.50

14.60

420.00

29.27

212.00

7.00

26.50

52.60

16.80

30.25

19.25

24.90

13.23

19.25

11.95

28.20

30.23

The coefficient B 3 for gases

1-xenon, 2-diphenyl mixture, 3-yodovodorod, 4-krypton, 5-chloro, 6-sulfur oxide, 7-butane, argon, 8-level

ozone, methyl chloride, 9-carbon dioxide, 10-methyl, 11 propane, 12, hydrogen chloride, and 13-oxygen,

hydrogen sulfide, nitrogen-14, the air, and 15-carbon monoxide, ethane, 16 ethylene, diethylene 17, producer

gas, 18 neon, 19 ammonia, 20-methane; 21 cooking gas, 22 helium, 23-hydrogen

ANNEX 6

Reference

The values of the coefficient B 3

Value B 3 at k, equal

MPa (kgf / cm 2)

1.135 1.20 1.30 1.40 1.66 2.0 2.5 3.0

0.100

0.200 0.960

0.300 0.930

0.354 0.865

0.393 0.820 0.959

0.400 0.770 0.929 0.957

0.445 0.730 0.755 0.928 0.950

0.450 0.715 0.864 0.925 0.942

0.488 0.863 0.920 0.935

0.500 0.819 0.860 0.919 0.933

0.528 0.819 0.853 0.912 0.925

0.546 0.769 0.816 0.850 0.902 0.915

0.550 0.754 0.768 0.818 0.845 0.900 0.914

0.564 0.753 0.765 0.815 0.842 0.899 0.911

0.577 0.729 0.752 0.764 0.810 0.840 0.898 0.900

0.600 0.714 0.725 0.750 0.762 0.805 0.835 0.877 0.880

0.650 0.701 0.712 0.732 0.748 0.773 0.800 0.848 0.850

0.700 0.685 0.693 0.713 0.720 0.745 0.775 0.810 0.815

0.750 0.650 0.655 0.674 0.678 0.696 0.718 0.716 0.765

0.800 0.610 0.613 0.625 0.630 0.655 0.670 0.700 0.705

0.850 0.548 0.550 0.558 0.560 0.572 0.598 0.615 0.620

0.900 0.465 0.468 0.474 0.475 0.482 0.502 0.520 0.525

1.000 0 0 0 0 0 0 0 0

The values of the coefficient B 3

ANNEX 7

Reference

The coefficient B 4 for:

nitrogen, air

Temperature T 1, ° C

MPa (kgf / cm 2)

0 50 100 200

0 1.00 1.00 1.00 1.00

10,0 (100,0) 0.98 1.02 1.04 1.05

20,0 (200,0) 1.03 1.08 1.09 1.10

30,0 (300,0) 1.13 1.16 1.17 1.18

40,0 (400,0) 1.27 1.26 1.25 1.24

100,0 (1000,0) 2.05 1.94 1.80 1.65

Hydrogen

Temperature T 1, ° C

MPa (kgf / cm 2)

0 50 100 200

0 1.00 1.00 1.00 1.00

100,0 (1000,0) 1.71 1.60 1.52 1.43

Oxygen

Temperature T 1, ° C

MPa (kgf / cm 2)

0 50 100 200

0 1.00 1.00 1.00 1.00

10,0 (100,0) 0.92 0.97 1.00 -

20,0 (200,0) 0.91 - 1.02 1.06

30,0 (300,0) 0.97 - 1.07 1.10

40,0 (400,0) 1.07 - 1.12 1.14

50,0 (500,0) 1.17 - 1.20 1.19

80,0 (800,0) 1.53 - 1.44 1.37

100,0 (1000,0) 1.77 - 1.59 -

Methane

Temperature T 1, ° C

MPa (kgf / cm 2)

0 50 100 200

0 1.00 1.00 1.00 1.00

10,0 (100,0) 0.78 0.90 0.96 1.00

15,0 (150,0) 0.73 0.88 0.95 1.01

20,0 (200,0) 0.77 0.89 0.96 1.02

30,0 (300,0) 0.90 0.96 1.01 1.08

50,0 (500,0) 1.20 1.20 1.20 1.20

100,0 (1000,0) 2.03 1.87 1.74 1.62

carbon monoxide

Temperature T 1, ° C

MPa (kgf / cm 2)

0 50 100 200

0 1.00 1.00 1.00 1.00

10,0 (100,0) 0.97 1.01 1.03 1.05

20,0 (200,0) 1.02 1.06 1.08 1.11

30,0 (300,0) 1.12 1.16 1.17 1.18

40,0 (400,0) 1.26 1.25 1.24 1.23

100,0 (1000,0) 2.10 1.94 1.83 1.70

carbon dioxide

Temperature T 1, ° C

MPa (kgf / cm 2)

0 50 100 200

1 1.00 1.00 1.00 1.00

5,0 (50,0) 0.10 0.60 0.80 0.93

10,0 (100,0) 0.20 0.40 0.75 0.87

20,0 (200,0) 0.39 0.43 0.60 0.87

30,0 (300,0) 0.57 0.57 0.66 0.88

60,0 (600,0) 1.07 1.02 1.01 1.07

100,0 (1000,0) 1.70 1.54 1.48 1.41

ethylene

Temperature T 1, ° C

MPa (kgf / cm 2)

0 50 100 200

0 1.00 1.00 1.00 1.00

5,0 (50,0) 0.20 0.74 0.87 0.96

7,0 (70,0) 0.23 0.60 0.81 0.94

10,0 (100,0) 0.32 0.47 0.73 0.92

15,0 (150,0) 0.45 0.51 0.68 0.90

20,0 (200,0) 0.58 0.60 0.70 0.89

30,0 (300,0) 0.81 0.81 0.82 0.95

100,0 (1000,0) 2.35 2.18 1.96 1.77

ANNEX 8

Reference

Explanation of terms used in this standard

G-throughput mass flow of the working fluid through the relief valve.

Operating pressure P p-GOST 14249-80.

Setting pressure P n is the greatest pressure at the inlet to the valve at which the

predetermined leak in the gate.